Agenda 07/10/2018 Item #16C 407/10/2018
EXECUTIVE SUMMARY
Recommendation to award Contract No. 16-6639, “Variable TDS Reverse Osmosis Conceptual Design”,
to CH2M, for professional engineering services to allow well water treatment of varying total dissolved
solids (TDS) in the amount of $367,403, and authorize the Chairman to execute the attached contract
and authorize the necessary budget amendment (Project 70104).
OBJECTIVE: To procure professional engineering design services for the Variable TDS Solids Reverse
Osmosis (RO) Conceptual Design Project. The resulting 30% design will be used as a basis for a future
design-build project that will reconfigure the North County Regional Water Treatment Plant (NCRWTP) so
that it can treat well water of varying TDS conditions.
CONSIDERATIONS: The proposed scope of work under Project 70104, “Water Plant Compliance
Assurance” is consistent with the Capital Improvement Program (CIP) contained in the 2014 Water,
Wastewater, Irrigation Quality Water, and Bulk Potable Water Master Plan/CIP Plan approve d by the Board
of County Commissioners (Board) on November 10, 2015, Agenda Item 9C, as Appendix III of the 2015
AUIR/CIE. Funding for project 70104 is available in, and is consistent with, the FY2018 CIP Budget.
Since 2000, the raw water conditions on wells 1-4 of the North RO (NRO) Wellfield have increased in
salinity. The NCRWTP’s RO membrane treatment process is limited to treating raw water with 6,000 TDS,
or less, while maintaining a target recovery of 75%. Out of 28 wells in the NRO Wellfield, we lls No. 1
through 4 have exceeded these limits, ranging from 15,000 TDS to 23,000 TDS. Each well represents an
investment of approximately $1,250,000.
While staff continues to monitor these conditions, it is initiating a design that is capable of process ing higher
TDS water if more wells increase in salinity. Should this occur, full design and construction would be
pursued.
On May 12, 2016, the Procurement Services Division issued Request for Proposal (RFP) #16-6639 and sent
out 1,666 notices. Fifty-two firms downloaded the RFP package and staff received three proposals by June
30, 2016.
On A u gu s t 2 5 , 2016, a selection committee ranked the t hr e e firms based on an evaluation of
their proposals. By consensus, the selection committee ranked the firms as follows:
1. CH2M
2. Tetra Tech
3. CDM Smith
On January 10, 2017, the Board of County Commissioners (Board) accepted the selection committee’s
ranking and authorized staff to negotiate a contract with the top -ranked firm, CH2M, for the conceptual
design (30% design) of the Variable TDS RO system at NCRWTP.
Under the Competitive Consultant’s Negotiation Act (CCNA), Florida Statute Section 287.055, staff
negotiated a recommended agreement with CH2M for a contract in the amount of $367,403 (attachment 1)
for the conceptual design (30% design) of the Variable TDS RO system at NCRWTP.
FISCAL IMPACT: A budget amendment is needed to transfer funds in the amount of $325,000 from
NCRWTP Op Tech Support, project 71066, and Water Treatment Plant Structural Rehab, project 70034, to
the “Variable TDS Reverse Osmosis Conceptual Design”, Project 70104, to cover design costs. The source of
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funding is the Water User Fees Fund (412).
GROWTH MANAGEMENT IMPACT: This project meets current Growth Management Plan standards to
ensure the adequacy and availability of viable public facilities.
LEGAL CONSIDERATIONS: This item is approved as to form and legality, and requires majority vote for
Board approval. -SRT
RECOMMENDATION: That the Board of County Commissioners, Ex-officio the Governing Board of the
Collier County Water-Sewer District, awards Contract No. 16-6639, “Variable TDS Reverse Osmosis
Conceptual Design” (Project 70104), to CH2M, for professional engineering services in the amount of
$367,403, and authorizes the Chairman to execute the attached contract and authorizes the necessary budget
amendment.
Prepared by: Oscar P. Martinez, P.E., PMP, Principal Project Manager, Engineering & Project
Management Division, Public Utilities Department
ATTACHMENT(S)
1. Attachment 1 - 16-6639 CH2M_Contract_CAO and Vendor Approved (PDF)
2. [Linked] 16-6639 CH2M_Proposal (PDF)
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COLLIER COUNTY
Board of County Commissioners
Item Number: 16.C.4
Doc ID: 5852
Item Summary: Recommendation to award Contract No. 16-6639, “Variable TDS Reverse
Osmosis Conceptual Design”, to CH2M, for professional engineering services to allow well water
treatment of varying total dissolved solids (TDS) in the amount of $367,403, and authorize the Chairman
to execute the attached contract and authorize the necessary budget amendment (Project 70104).
Meeting Date: 07/10/2018
Prepared by:
Title: Project Manager, Principal – Public Utilities Planning and Project Management
Name: Oscar Martinez
06/26/2018 12:38 PM
Submitted by:
Title: Division Director - Public Utilities Eng – Public Utilities Planning and Project Management
Name: Tom Chmelik
06/26/2018 12:38 PM
Approved By:
Review:
Water Steve Messner Additional Reviewer Completed 06/26/2018 3:27 PM
Public Utilities Operations Support Joseph Bellone Additional Reviewer Completed 06/27/2018 8:10 AM
Public Utilities Planning and Project Management Tom Chmelik Additional Reviewer Completed 06/27/2018 9:38 AM
Procurement Services Opal Vann Level 1 Purchasing Gatekeeper Completed 06/27/2018 1:18 PM
Procurement Services Ted Coyman Additional Reviewer Completed 06/27/2018 5:11 PM
Procurement Services Sandra Herrera Additional Reviewer Completed 06/27/2018 6:45 PM
Procurement Services Swainson Hall Additional Reviewer Completed 06/28/2018 8:52 AM
Public Utilities Department Sarah Hamilton Level 1 Division Reviewer Completed 06/28/2018 9:29 AM
Public Utilities Department George Yilmaz Level 2 Division Administrator Review Completed 06/28/2018 2:02 PM
County Attorney's Office Scott Teach Level 2 Attorney Review Completed 07/03/2018 9:30 AM
Office of Management and Budget Valerie Fleming Level 3 OMB Gatekeeper Review Completed 06/29/2018 10:33 AM
County Attorney's Office Jeffrey A. Klatzkow Level 3 County Attorney's Office Review Completed 06/29/2018 10:36 AM
Office of Management and Budget Susan Usher Additional Reviewer Completed 06/29/2018 12:17 PM
County Manager's Office Nick Casalanguida Level 4 County Manager Review Completed 07/02/2018 10:42 AM
Board of County Commissioners MaryJo Brock Meeting Pending 07/10/2018 9:00 AM
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WT0605161133SWF
June 30, 2016
Variable TDS Reverse Osmosis Conceptual Design
CCNA Solicitation 16-6639
Statement of Qualifications
Submitted to:
Master
TAB I Cover Letter/ Management Summary TAB ICover Letter/Management Summary
I-1
June 30, 2016
Collier County Government
Purchasing Department
3327 Tamiami Trail East
Naples, FL 34112
Attn: Swainson Hall, Procurement Strategist
RE: CCNA Solicitation - #16-6639 Variable TDS Reverse Osmosis Conceptual Design
Dear Mr. Hall and Members of the Selection Committee:
Collier County Public Utilities Department – Planning & Project Management Division (County) requires an
experienced and technically savvy engineering firm to provide options to manage increased total dissolved solids
(TDS) concentrations at the North County Regional Water Treatment Plant (NCRWTP). The chosen consultant
firm will provide a conceptual design of modifications to the reverse osmosis (RO) treatment process at the
WTP, including an opinion of probable construction cost and a schedule for implementation.
CH2M is that firm! With our extensive RO experience throughout Florida, the US, and worldwide, combined
with our institutional knowledge of Collier County, our staff has the skills and expertise required to successfully
and cost-effectively deliver the Variable TDS Reverse Osmosis Conceptual Design Project. The CH2M team has
the resources to deliver all services that will be required as part of this project.
CH2M has extensive RO/Membrane experience in Florida and worldwide. Within Tab III: Experience and
Capacity of Firm, CH2M has provided an overview of our firm’s experience in this area, followed by detailed
descriptions showcasing our relevant project work with variable TDS source water, desalination evaluation, and
desalination design. We have successfully completed more than 200 desalination studies and pilots and has
been instrumental in the delivery of more than 30 operating brackish water RO and 10 operating seawater RO
facilities worldwide.
Our team includes a multi-disciplined local Naples staff supported by the extensive, specialized resources of the
CH2M network, assuring both rapid responsiveness and unparalleled technical expertise. CH2M maintains an
integrated network of more than 170 offices worldwide, with more than 22,000 professional and support
personnel, including more than 800 staff in Florida. We have provided a variety of professional engineering
services for local clients, including Collier County, Lee County, Bonita Springs, and Marco Island, bringing to this
project established working relationships with area consultants, agencies, utilities, and stakeholders, as well as
an in-depth knowledge of the local sites, conditions, and challenges inherent to our region. CH2M team
members routinely work together and offer an “integrated” team approach to providing successful project
solutions.
CH2M will be responsible for project management,
capacity analysis, and preparation of design criteria package
plans and specifications for this project. To add specialized expertise and augment our capabilities, CH2M has teamed
with Water Science Associates (WSA) for hydrogeological services. WSA Firm Principals leverage over 50 years of
&
CH2M
5801 Pelican Bay Blvd
Suite 505
Naples, FL 34108
Tel 239.596.1715
Fax 239.596.2579
I-2
combined experience in water resource evaluation, permitting, and facility design and construction throughout
Florida and the Caribbean. Principal Kirk Martin, PG was the former lead hydrologist with a nationally recognized
engineering and infrastructure firm and Brian Barnes was the former director of South Florida operations for an
international infrastructure and environmental consulting firm. Kirk’s experience includes serving as the Technical
Director for the Collier County Wellfield Reliability Improvements and Expansion Program from 2004-2014.
The CH2M Team offers the County the right combination of local knowledge and experience with
direct access to industry recognized technical experts
CH2M brings to this project a history of working in Collier County since 1977. We know Collier
County’s systems and operations and bring an acute understanding of local conditions, as well as the
County’s staff, local subcontractors, contractors, and consultants. CH2M has worked at the NCRWTP
facility upgrading water treatment systems along with the local facility staff, giving us recent in-depth water
treatment process familiarity. Team member, WSA, is the designer for the NCRWTP wellfield and thoroughly
understands the issues contributing to the increasing source water TDS. This unparalleled recent source and
treatment experience at the NCRWTP gives CH2M an incomparable understanding of the issues faced during
analysis and design of the treatment facility.
Our proposed Project Manager, Joe Elarde, P.E., is known to County staff and is well qualified to
serve as the Project Manager and Task Leader. Based in our Naples office, he is a nationally
recognized specialist in membrane technologies—more than 19 years of water treatment planning
and design experience, and 21 years of membrane process experience working on projects that include study,
design, permitting, construction, startup, and operation of membrane filtration, nanofiltration, brackish water
reverse osmosis, and seawater desalination facilities all over the U.S., including many in Florida.
CH2M has established an international reputation in developing and applying desalination
technology for municipal facilities. A leader in the study and design of desalination facilities, we
have an extensive knowledge of alternative desalination treatment processes and what will be
critical for additional support and optimization. As detailed in Tab III, Experience and Capacity, we are confident
that no other firm in the nation has the pilot-, demonstration-, and full-scale operational experience with
desalination treatment that CH2M has to offer the County. This experience gives us a unique insight into the
strengths and weaknesses of the process, and it will allow us to evaluate and identify the most appropriate and
cost-effective process for local requirements. We encourage Collier County to contact the references we have
included in Tab V References to verify our performance on similar projects.
To increase familiarity with local conditions that may affect the performance of the work included in this RFP,
CH2M’s Joe Elarde and G.J. Schers conducted a site visit at the NCRWTP on June 6, 2016 at 9:30am. During the
site visit, CH2M carefully reviewed existing RO system and overall water treatment process components to
understand how the existing treatment components will impact modifications for variable TDS desalination. We
inspected facility treatment equipment, observed operations, and took photos of the existing conditions,
including pretreatment components, RO system process and mechanical components, post treatment
History of working with Collier County and institutional knowledge of your systems,operations,
and staff allows us to start work immediately upon NTP
Project organization that provides all required resources under the direction of a
proven, experienced Project Manager streamlines project delivery and minimizes schedule
Proven methodologies and lessons learned on the successful delivery of similar projects
ensures the County that you will receive the best option for a viable and cost effective process
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2
3
2
1
3
I-3
components, and the control system. All of these local conditions may have an impact on the evaluation of
options and the RO system modifications design.
After reviewing our response to the Request for Proposals, we trust that you will feel as we do; that the
experience, depth, and flexibility of the CH2M team offers Collier County the greatest advantage in completing a
quality project on time and within budget. We look forward to working on the variable TDS Reverse Osmosis
Conceptual Design project and continuing our successful partnership on the County.
Sincerely,
CH2M HILL Engineers, Inc.
William D. Beddow, P.E. Joe Elarde, P.E.
Vice President and Principal-in-Charge Project Manager
239-596-8989 x59207 239-404-7034
bill.beddow@ch2m.com joe.elarde@ch2m.com
TAB II Business PlanTAB IIBusiness Plan
II-1
Detailed Plan of Approach
Project Understanding
The existing North County Regional Water Treatment Plant (NCRWTP) has been operational since 1993 utilizing
membrane technology to treat groundwater. The nanofiltration (NF) system softens water from the shallow
Tamiami Aquifer and has a rated capacity of 12 mgd. The brackish water reverse osmosis (BWRO) system was
added in the late 1990’s and desalinates water from the deeper Lower Hawthorn Aquifer, which is part of the
Floridan Aquifer System. The BWRO system has a rated capacity of 8 mgd. It contains typical treatment
processes for a brackish groundwater system, including sand separation, cartridge filtration, sulfuric acid and
scale inhibitor addition for pre-treatment, two-stage single-pass reverse osmosis with inter-stage boost energy
recovery for main treatment, and degasification, chlorine disinfection and chemical additions for post
treatment. The NF and RO permeates are combined prior to degasification. Also, the NF and RO concentrates
are combined, re-pumped and discharged into an on-site deep injection well system. Exhibit II-a depicts a
simplistic process schematic.
Soon after startup of the BWRO system in 1999, five wells (e.g. RO-001 through RO-004 and RP-006)
experienced rapid increases in salinity. Within two years (2000-2001), total dissolved solids (TDS) levels in the
EXHIBIT II-a
NCRWTP Process Schematic
II-2
wells went up from 5,000 to 20,000 mg/L, and that water could not
be treated with the existing BWRO system. The source of saline
water was studies and was believed to be underlying more saline
aquifers, with conduits to the production zone, and not related to
upward migration from the deep injection well system. The wells
are completed at a depth between 700 and 900 feet below land
surface, have short open-hole interval in a high transmissive
formation, resulting in well productivities of around 2,000 to 2,500
gpm. Efforts were made to rehabilitate well RO-006 by back
plugging part of the open hole to stop salt groundwater inflow, at
the sacrifice of production, however these efforts were not
successful. Therefore, the wells have been largely unused.
Since 2002, additional, less saline wells were added further east to
maintain the production capacity of the WTP. The wellfield
information from Collier County was showcased in a recent paper
presented at the 2015 FSAWWA conference in Orlando by one of
CH2M team members (Exhibit II-b on following page). The paper
also presented other Floridan wellfields with similar water quality
issues and best practices described to overcome the issue.
Between 2005 and 2010, several consultants studied the TDS
increases in the wellfield as well as different aspects of the plant,
however additional membrane treatment technology to treat
saline water was not yet implemented by Collier County. In the late
2000’s the BWRO trains were fitted with inter-stage turbine energy
recovery devices (ERDs) to preserve energy and increase the
source water TDS level that the RO trains could treat.
This project envisions the development of a preliminary design for the most cost-effective solution to handle
variable TDS water, ranging from 3,000 to 20,000 mg/L from the current Hawthorn aquifer and potential Avon
Park aquifer while maintaining the plant rated capacity at 8.0 mgd. At this stage it is uncertain how the raw
water quality will develop in the wells under more continued production. Therefore, Collier County is looking for
a solution which is affordable, flexible, adjustable and implementable in phases.
It is envisioned that the preferred solution will be implemented via a future design-build phase of the project.
The preliminary design will be used as part of the design criteria procurement package. Collier County’s aim is to
continue using the existing infrastructure, modified to suit the high TDS water in their productive wells, while
also capable of treating existing TDS water efficiently, and either limit further migration of bad quality water to
other production wells or clean up the area of bad water quality altogether.
Since 2008, CH2M has been working successfully for Collier County on several upgrades projects at the NCRWTP.
These projects started with the evaluation and conceptual design for the addition of inter-stage turbine ERDs on
the existing RO trains in conjunction with Florida Power & Light. More recent improvement projects at the
CRWTP include design and services during construction (SDC) of higher capacity finished water transfer pumps,
design and SDC of new degasifier drop pipes, evaluation of WTP post-treatment degasification efficiency, design
of a liquid fluoride storage and feed system, and the refurbishment of existing NF trains (ongoing). Through
these projects, CH2M has become very familiar with the process equipment and infrastructure at the NCRWTP,
the existing operations and maintenance and specific pitfalls at the existing site. Also, following the instructions
on page 9 in the Request for Proposal, CH2M visited the NCRWTP site on June 6, 2016 to become even more
familiar with local conditions.
Implement the most cost-effective and
flexible treatment solution to handle
variable TDS raw water while maintaining
existing production capacity at NCRWTP.
This enables to use of the highly productive
– though saline – on-site wells with the
intent to limit the migration of bad water
quality to other wells in the wellfield.
Project Objective
II-3
EXHIBIT II-b CH2M Understands Water Quality Degradation in the Floridan Aquifer
Collier County North and South RO systems were showcased in a 2015 FSAWWA paper “Salinity increase in the Upper
Floridan Aquifer Wellfields in South Florida: What have we learned and how do we plan new systems?” by one of CH2M
team members. As part of this paper, Collier County’s well water quality was collected and analyzed for trends and
abnormalities. One section in the paper regarding the Northern wellfield is summarized below:
“Wells RO-001 through RO-004 and RO-006 at the western end of the wellfield which are producing from the Lower
Hawthorn Aquifer experienced rapid increases in salinity shortly after they were placed into operation. Chloride
concentration of water samples obtained from these wells during 2000 and 2001 ranged from approximately 2,000 to
3,000 mg/L. Chloride concentrations in these wells increased to between 6,000 to 10,000 mg/L within two year of
operation. A total of 19 additional production wells have been added to date to increase raw water supply capacity to
the RO WTP. Individual well yields in the wellfield generally range from 500 to 700 gpm with chlorides concentrations
ranging from 850 mg/L to 3,000 mg/L. In the Northern wellfield, 21% of the wells have seen a chloride increase of 5% or
higher during each 12 months of operation. The ‘bad’ wells are 001, 002, 003, and 004 and to a lesser extend 009…”
The graphics depicting combined raw water chloride trends of both Collier County’s wellfields (left) and individual
chloride increase in each northern well (right). Wells 002, 003 and 004 saw a significant chloride increase with current
levels around or just above 10,000 mg/L.
This salt increase is however not consistent across all constituents. Whereas chloride, TDS, magnesium, sulfate and
sodium almost quadrupled within that period, other constituents (not shown in graphics) like calcium and bicarbonate
only less than doubled and again others like fluoride, strontium and barium hardly increased at all. This in-depth
understanding of water quality degradation and trending is important for the solution developed for Collier County to
treat groundwater with variable TDS levels.
Work Plan
Interactive Workshop Decision Making Approach
CH2M uses an interactive decision and design workshop approach in its preliminary decision-making and
subsequent design processes. This interactive workshop approach is used to:
Solicit client direction
Rapidly sort through options
Evaluate technical, economical, operational benefits
Gain input from national experts and relevant project experience
Solidify optimal treatment approach for the variable TDS treatment system
Develops and documents a sound and defensible decision approach
II-4
Workshops will be conducted with the County throughout the
process selection and preliminary design process to review
treatment options, consider non-cost criteria, and review
projected costs including construction, operations and
maintenance (O&M) and overall lifecycle costs of different
options.
Process Selection Tools
The CH2M team has extensive experience with treatment
process analysis, and multi-variable benefit–cost analysis to
select treatment process schemes, including process evaluation
and testing, cost-benefit analysis of selected process, process
selection, and design and construction. We often use a pair-
wise comparison to help develop and rank criteria that are most
important to the County at the planning level before
implementing design. The analysis will incorporate a life cycle
analysis to ensure that O&M cost is included in the design
selection. Non-cost criteria should consider reliability, O&M considerations, and possibly environmental
considerations that may drive selection of an option that is not necessarily the lowest cost.
Design, Costing, and Optimization Tools
CH2M HILL’s proprietary technology and costing models
effectively capture our best practices and will help Collier County
quickly and cost-effectively find a true optimum solution. We
have developed and successfully applied a variety of simulation
and optimization modeling tools that quickly and accurately
estimate capital, O&M, and life-cycle costs, treatment
performance, and system control.
These one-of-a-kind models include CPES™ (our CH2M
Parametric Cost Estimating System tool), Replica™ (our dynamic
treatment simulation model), Source™ (our water treatment
mass balance tool), Preview™ (our facility visualization tool),
Voyage™ (our complex decision support model), and SI Port™
(our sustainability tool). We have linked major membrane
treatment manufacturer projection software into our process
models to ensure that we use the most-up-to-date
membrane performance information.
Specifically, this project will heavily use CPES which is a
proprietary conceptual design and cost estimating tool
that generates quick, accurate, and detailed cost
estimates at the conceptual stage of the project. CPES
costs are based on general arrangement drawings
derived from real projects and project specific process
design criteria. Using algorithms built into the model,
the system generates project-specific facility designs
and construction and lifecycle cost estimates. Compared
with traditional conceptual estimating techniques, CPES
yields a much clearer picture of the project’s unique
scope in a fraction of the time. We will use CPES to
quickly develop detailed comparative construction,
O&M and life cycle costs for candidate alternative
Component ranking with cost-benefit
analysis will highlight optimum treatment
solutions.
Preview™ will help Collier County visualize
different treatment options early during
conceptual design. These models are
refined during subsequent conceptual
design.
Replica™ will allow an analysis of all combinations
of water quality and treatment options in a virtual
water treatment environment without the need to
use constraint that may only help find apparent
optimum solutions.
Process
•Track components
(Water Quality)
–Treatment processes
–Separation
–Reactions
HYDRAULICS
PROCESS I
&
c
COMPLETE
DYNAMIC SYSTEM
MODEL
OPTIMIZATION
Hydraulics
•Move fluids through
system
–Pipes
–Pumps
–Valves
–Storage
Instrumentation &
Controls
•Drives system operation
–Measuring devices
–Transmitters
–Control Algorithms
II-5
treatment options to give Collier County real comparative costs. Preview™ will be used to help Collier County
visualize the different options developed in CPES before final selection. Replica™ will be used to model different
combinations of source water quality and treatment process options to determine the true optimum lifecycle
cost options without the need to make estimations to simplify the analysis that can find apparent optimum
solutions instead of true optimum solutions. Integrated process selection and design development with
advanced design tools such as these will be used to find the best
solution.
Task 1 - Project Kick Off and Information Review
This task provides the foundation for the project. It will confirm
Collier County’s project objectives, define the analytical framework
for developing and evaluating alternatives and guide the collection,
review and summary of information. Gaps in information will be
identified and actioned in coordination with Collier County. An
example of information, that is not yet available but would need to
be collected, is the current (extensive) water quality data of the
affected wells beyond conductivity and TDS, in particular the
constituents causing membrane scaling/fouling.
Key sub-tasks for this task include the following:
Hold kick off meeting to:
o Confirm project objectives, scope, schedule, project
team and communication lines
o Develop evaluation criteria for alternatives evaluation
o Receive and review requested information from wells
and treatment plant
Review information received and analyze, in coordination with
the membrane vendor, normalized membrane performance
data to determine trends or correlations between performance,
production and water quality
Summarize findings in an existing information review technical
memorandum, provide gap analysis and recommend on
gathering additional data
Conduct review meeting and provide meeting summary
Task 2 - Facilities Visit and Condition Assessment
This task will build on CH2M’s existing knowledge of the RO system
to create a better understanding of the background of the TDS issue
and facilitate an initial dialogue between parties on potential
strategies to mitigate variable TDS water. Also, it will provide
additional hands-on information of existing facilities to verify
suitability for continued use with the variable TDS water. An
example is the verification of appropriate pressure rating and
material compatibility of the pipework, pumps, and pressure vessels
to treat water with a significant higher TDS of the affected
production wells.
It is anticipated that an initial walkthrough will be held by CH2M’s
project leadership team with Collier County staff followed by
Information Needs of
NCRWTP Facilities
INFRASTRUCTURE INFORMATION
As built drawings
Information on ongoing projects
Equipment data sheets
Operations and Maintenance
(O&M) manuals
Consumptive Use Permit and
other relevant permits
OPERATIONAL DATA
Water quality data
Equipment performance and
rehabilitation data from SCADA,
normalization sheets, and other
tracking programs
Chemical and other consumables
data sheets and costs
Standard Operating Procedures
(SOP)
Set-points on SCADA
PREVIOUS REPORTS ON WATER
QUALITY VARIABILITY /
DEGRADATION
High pressure RO feasibility study,
CDM (2005)
Pilot testing high TDS well water,
Carollo (2006)
Performance evaluation of
degasifiers, odor control facilities,
Hazen & Sawyer (2007)
Inter-stage turbine energy
recovery device evaluation, Boyle
(2007)
High TDS RO expansion
preliminary design report, HDR
(2009)
II-6
detailed site visits of discipline engineers to verify specifications and conditions of particular components of the
RO system. This assessment will be limited to review of existing design documentation and visual inspection
covering assets that are readily and safely accessible. CH2M desalination process engineers will analyze system
operating data trends to estimate remaining existing membrane element life. Additional testing to verify
conditions, performance, and/or specifications will be identified and shared with Collier County.
Key sub-tasks of this task include the following:
Initial visit by CH2M’s project leadership team to existing WTP focusing on overall condition and reliability of
facilities, and determine vulnerability and single points of failure
Interview WTP staff
Detailed visits by discipline engineers to confirm specifications and assess condition of existing facilities:
o Production wells
o Well surface facilities and transmission
o RO treatment facilities and concentrate surface
facilities
o Blending and post treatment facilities
o Concentrate injection well
o Associated electrical infrastructure
o SCADA system and control loops
Summarize findings in a condition assessment technical
memorandum and provide recommendations for additional
testing
Conduct review meeting and provide meeting summary
Task 3 - Best Industry Practices for Treating Variable
TDS water
The purpose of this task is to establish best industry practices of
treating variable TDS water by collecting information from the
wide range of CH2M project experience, strategic partner
experience and other utility experience with similar water quality
issues and treatment as Collier County. This includes collecting
information on treatment which has not worked effectively or has
been previously discarded by the County. Contact will be made
with equipment manufacturers which are active in this market
segment including new and emerging technologies that are
anticipated to mature within the project timeframe.
Since the previous studies were executed for NCRWTP variable
TDS project, between 2004 and 2008, membrane treatment
technology has further improved with the following major global
developments:
1. More energy efficient, higher rejection membrane elements
2. Different type and more efficient energy recovery devices
3. Operational methods different from the typical continuous
reverse osmosis to provide low energy, high recovery, and
flexible treatment solutions, including forward osmosis and
closed circuit osmosis
Several global clients have trusted
CH2M team members to provide them
with cost-effective, innovative solutions
for variable water quality systems. A
brief summary is provided below:
Singapore Public Utility Board:
Marina East RO WTP utilizing
variable TDS waters,
feasibility/design
Cape Coral North BWRO WTP design
based on Floridan Aquifer System
water degradation
New York brackish and groundwater
desalination WTP siting study
Texas Water Development Board
Forward Osmosis/Reverse Osmosis
hybrid feasibility study
WRF evaluation and optimization of
emerging and existing Energy
Recovery devices for desalination
treatment plants
Chesapeake VI Northwest River WTP
design treating groundwater and
seawater blends
Fort Myers WTP conversion from NF
to RO technology while maintaining
existing infrastructure
CH2M is a Globally Recognized
Leader in Innovative
Membrane Design
II-7
4. Higher system recoveries by implementing concentrate reduction or zero liquid discharge systems including
Vibratory Shear Enhanced Processing (VSEP) flatbed membranes, electrical dialysis reversal (ERD) and
adding third stage RO following softening
5. More science based and therefore better performing scale inhibitors to facilitate higher system recoveries,
to reduce or eliminate sulfuric acid and to protect membranes better from scaling and fouling
Key activities of this task include the following:
Review literature/CH2M project experience and contact and potential visit other utilities with similar water
quality concerns and solutions (examples provided in Exhibit II-c)
Contact equipment manufacturers on treatment solutions for variable TDS feed water (examples:
Desalitech, Energy Recovery, membrane manufacturers and RO Original Equipment Manufacturers)
Conduct review meeting and provide meeting summary
Summarize findings in a best practices technical memorandum
EXHIBIT II-c Learning from Past CH2M Member Projects to Shortlist Promising Ways to Manage Variable TDS
Sources with variable or with steadily degrading water quality is not new in the industry and several utilities had or are
dealing with this same issue. The table below provides examples of utility issues and solutions.
Utility, Location Main Issue Solutions
Bonita Springs, Florida Gradual increase in TDS in wellfield,
with anticipated high future salinity
RO system designed for high pressure and
flexible recovery. Installed higher
rejection/lower energy membrane
elements and energy recovery as TDS
increased. Replica wellfield/RO process
modeling and optimization.
Public Utilities Board,
Singapore
Make beneficial use of fresh storm
water, when available, in a RO system
able to treat seawater
Skid design to allow both treatment of
brackish and sea water
Chesapeake, Virginia Multiple sources available including
groundwater and river water affected
by salt water intrusions
RO skid design to allow treatment of both
fresh and brackish water, or combination
thereof, with or without conventional pre-
treatment
Lee County, Florida Gradual increase in TDS in brackish
wellfields; some wells with rapid TDS
increase since startup
Additional/replacement wells, flow control
through VFDs for well pumps and, and
design of flexible RO system
City of Cape Coral, Florida Gradual increase in TDS in both
wellfields, however some wells with
rapid TDS increase since startup
Pro-active wellfield management, design of
slightly flexible RO treatment system, and
decreased RO recovery at South WTP
Palm Beach County, Florida Rapid and sharp TDS increase at
multiple wells since startup
Additional/replacement wells, flow control
through new VFDs for well pumps and
post-treatment mods to eliminate bypass
blend
City of Jupiter, Florida Gradual increase in TDS in wellfield,
however several wells rapid increase
since startup
Additional/replacement wells and addition
of inter-stage boost on RO trains after
startup
Long Beach, California None, just an innovative method to
treat seawater
Two pass NF system with second pass
concentrate recycled back to feed
Kittansett Golf Club in Marion,
Massachusetts
The high variability of the well TDS
from 1,000 to 10,000 ppm cannot be
handled by conventional RO.
Desalitech RO batch process to
automatically adjust to variable feed TDS
while producing low TDS permeate
II-8
Task 4 - Definition of Variable TDS Future Water Quality
The purpose of this task is to develop the most important design
criteria for the variable TDS treatment system, the variability of
the future water quality. This requires extensive water quality
data from individual wells, a thorough understanding of the
system operations and water degradation projections guided
preferably by a soluble transport three dimensional (3-D)
groundwater model.
Key activities include the following:
Establish existing operations of the wellfield and treatment
system and discuss future options for operations. One key
discussion will be the main purpose of the affected wells; e.g.
permanent operation, semi-permanent with main operation in
peak season or just standby.
Develop projections of relevant water quality parameters for
each well or each group of wells (TDS, chloride, sodium,
chloride, sodium, strontium, barium, sulfate, carbonate, gross
alpha)
Develop raw water well blending scenarios
Develop future water quality technical memorandum
Hold review meeting and provide meeting summary
Task 5 - Treatment Alternatives Evaluation for Handling
Variable TDS
This task covers the development of different options to deal with
variable TDS, including operational and capital solutions. From
experience, it is expected that a combination of several operational
measures can provide treatment of raw water up to a certain TDS
level without requiring capital expenditure. For instance, by
changing to more energy efficient, high rejection membranes,
reducing BWRO recovery and making chemical addition changes, it
can be expected that raw water up to around 10,000 mg/L TDS may
be treated with the existing system without making holistic
infrastructural changes at the NCRWTP. An insight into the
feasibility and effect of each candidate solution is important to
develop a strategic plan to overcome variable TDS water. The
options may include phasing based on actual needs to minimize
high capital and operating cost expenditure initially and may
include trade-offs between various performance criteria such as
treatment capacity, treated water quality, system recovery,
chemical and electricity use.
Key sub-tasks include the following:
Develop operational solutions:
1. Limit variable water quality:
a) Back plug or acidify production well(s)
b) Abandon well(s)
Based on previous work, CH2M knows that
water quality variation in the Upper
Floridan Aquifer can be caused by vertical
or radial migration conduits induced by
aquifer stresses caused by well water
withdrawal. The conduits include
abandoned wells, fissures, cracks and
fractures with a direct or non-direct
connection from more saline aquifers or
seawater to the well borehole, as illustrated
below.
The trends of various water quality
constituents may vary and depend upon the
nature of the recharge water:
Ion strength, conductivity, chloride,
sulfate, magnesium and sodium follow
the same general trend as TDS and can
be predicted by a groundwater model
Calcium, potassium and alkalinity may
have a less steep trend than TDS
Strontium, barium, gross alpha, and
silica may not have a trend at all
Trends in the last two categories may
be obtained by reviewing historical
data from Collier and other Upper
Floridan wellfields
We understand the Water
quality trends in the Upper
Floridan Aquifer
II-9
c) Add redundant wells
d) Provide hydraulic flow control of wells (flow, drawdown, conductivity)
e) Create raw water quality blending between wells
f) Establish pro-active wellfield management system using on-line data to establish well
prioritization and production
Based on our work with Collier County, we know that several of these best wellfield practices have
been implemented. Therefore, this task may be limited to sharing CH2M team’s experiences and
successes with these measures.
2. Modify treatment operations to handle variable water quality:
a) Change the recovery of reverse osmosis process
b) Replace with low energy, high rejection membrane elements to improve the salt rejection
c) Change chemical type and adjust chemical doses
3. Minimize the impacts of variable water quality:
a) Create raw or finished water blending between the NF and RO treatment systems
b) Establish additional post-treatment water treatment conditioning for pH, hardness, and
alkalinity
EXHIBIT II-d Operational Impacts of Increasing TDS in the Source Water
As part of a previous study, operational impacts to a 3.0 mgd BWRO system were evaluated to address an increase of
feed water TDS from 3,000 to 9,500 mg/L:
RO recovery reduces from 80% to 70%
Ability to RO bypass reduces from 10% to 2%, with permeate flow making up difference requiring train array to
increase from 54-27 vessels to 60-30 vessels
Feed pressure increases from 188 to 282 (with ERD)
Post-treatment chemicals to adjust alkalinity and hardness are increasing with higher TDS
Electricity and chemical costs for RO increase from $0.32 to $0.72 per 1000 gallons treated water
Along the same lines, a quick evaluation was done to verify how operations can be changed to allow continued use of
the existing RO pressure vessels, which are rated at 600 psi. Please refer below graphic for the results. The pressure
rating on the second stage will be exceeded at around 15,000 mg/L TDS. If the RO recovery is dropped from 60 to 50%,
the pressure rating of the first and second stage pressure vessels will not be exceeded until feed water TDS reaches
values of around 17,500 mg/L
II-10
Develop candidate solutions:
1. Treatment process concepts for extreme events with equipment inefficiencies most of time
c) Dedicated salt water reverse osmosis (SWRO) system for high TDS water;
d) Modify existing system to SWRO
The previous variable TDS studies were based on the concept of having to treat well water with the
worst quality. This lead to the design of two additional, dedicated high TDS SWRO skids. The
consequence of this addition was an increase in the overall WTP capacity from 20 to 22 mgd
requiring upgrades to the electrical equipment, power distribution, chemical dosing systems,
degasification and odor control, transfer pumping and process building. These upgrades made this
solution not competitive in terms of capital and operating costs and therefore were not
implemented.
2. Short-term treatment process modifications for elevated TDS feed with phased additional treatment
equipment for future extreme events
e) Maintain existing BWRO system with minor modifications and add a new treatment
technology, like softening, EDR or VSEP membrane technology, if and when needed
f) Maintain the existing BWRO system with minor modifications and integrate with existing NF
treatment system
• Recycle RO permeate back to NF feed for second pass; this may allow a continued
use of existing BWRO membrane elements at reduced system recovery avoiding
expensive upgrades
• Recycle NF concentrate to BWRO feed for TDS reduction; this concept has been
pioneered in Florida and at least one system operates successfully with this
• Reconfigure to in-series BWRO trains
for second pass
3. Implementation of a flexible system
g) Modify to new technology, like recirculation
desalination by Desalitech, which is operated
with concentrate recirculation in batch-mode
allowing treatment of high TDS water at
relatively high recovery rates and lower energy.
For Collier County, this can be an interesting
technology to handle the variable TDS water, which
can be integrated with existing RO train equipment
through the end of its useful life to cost-effectively
achieve higher feed TDS treatment over the short-
term. As existing RO system components reach the
end of their useful life, new components can be
installed designed to limits needed for 20,000 mg/L
TDS operation.
Provide description and process schematic for each option
List advantages/disadvantages for each option
Utilize our CPES™ cost model to quickly develop accurate
comparative capital, operating and lifecycle costs for several
alternatives for comparison purposes
Develop a Replica model to optimize operational and capital
solution combinations
Flexible RO Treats Variable TDS
at Increased Recovery Rates
A new promising technology by Desalitech
utilizes conventional BWRO equipment
configured in a different manner,
enhanced with recirculation pumps,
additional instrumentation and controls.
In addition to controlling RO flow and
recovery, operators can adjust flux and
cross-flow to reduce fouling and scaling
while increasing system recovery. Benefits
of a flexible RO system are the ability to
treat variable TDS feed water
instantaneously, increased resistance
against scaling, improved recoveries and
reduced energy use.
II-11
Conduct a benefit cost analysis using CH2M’s decision tools using optimized results
Prepare alternatives comparison technical memorandum
Conduct review meeting and provide meeting summary
Task 6 - Conceptual Design
After a preferred solution is identified, and agreed upon, under the previous task, further details will be
provided in a conceptual design. Previous CH2M models developed in the alternatives evaluation will be
updated with the conceptual design criteria to provide project-specific information. An early constructability
and operability review with Collier County will identify phasing options at this operational WTP site, needs for
temporary facilities or utilities and operational constraints during the implementation. Having identified those
aspects early will provide further confidence in the accuracy of the cost estimates and timing of construction.
Key sub-tasks include the following:
Develop conceptual design criteria
Assess changes to finished water quality and corrosion control
strategy and make recommendations regarding transition period
Constructability and operability review
Update Replica process model and construction and operating
costs in CPES using the developed conceptual design criteria
Update costs for budgeting purposes, including developing a
financial maintenance model
Develop conceptual design report:
o Description of system
o Process schematic
o Mass balance (using our Source™ mass balance tool)
o Hydraulics (refined in Replica)
o Design criteria tables
o Conceptual layout (refined in Preview)
o Controls and electrical systems
o Implementation schedule and phasing plan
o Capacity analysis over projected timing of the project
o Reliability analysis of treatment process components
o Cost estimate
Conduct review meeting and provide meeting summary
Task 7 - Preliminary Design
Following the Collier County’s approval of the conceptual design report, further details will be provided in a 30
percent design particulates. The content of these particulates will be driven by the multiple purposes of the
preliminary design report, including:
Allow buy-in and final approval from Collier County
Provide basis of design report requirements of the FDEP for the PWS permit application for the plant
changes
Create design criteria document for inclusion in procurement documentation for selection of the design-
build contractor
C lli C P j Obj i
Post-Membrane Water
Conditioning for Corrosion
Control
Treatment of variable TDS feed water
will result in variable RO permeate
water quality. While the NF permeate
will remain the dominant portion in the
blend water, variations of individual
salts constituents will exist in the
finished water. Also, operation of
NCRWTP may shift from dominant NF
to RO due to O&M activities and this
will also have an impact on finished
water quality. As part of the work,
particular constituents (hardness,
alkalinity and chloride-to-sulfate mass
ratio) will be modelled using our Source
model to assess to need and type of
post membrane water stabilization and
conditioning for corrosion control.
II-12
Key sub-tasks include the following:
Develop preliminary design particulates
Constructability and Operability review
Update operating cost, and Class IV opinion of probable construction cost
Develop draft preliminary design report:
o Description of system, design criteria
o PFD, hydraulic profile
o PIDs
o Single line diagrams
o Block diagrams, control system architecture, communications
o Equipment list, and data sheets
o Preliminary layout
o Preliminary equipment specifications
o Updated equipment replacement/addition/implementation schedule
o Projected construction schedules
o Updated construction and operating cost estimates
Conduct review meeting and provide meeting summary
Finalize preliminary design report
Detailed Time Line of Project
An initial project implementation schedule was developed based on the tasks and subtasks described above and
an anticipated contract term of 12 months included in the request for proposals. The current schedule shows
the submission of the final preliminary design report in week 45 after the notice to proceed. There are factors
outside of CH2M’s control affecting the schedule which will be finalized in coordination with the County.
Task Activities Deliverable From NTP
(in weeks)
1. Kick off project and Information Review
Kick-off Meeting
Existing info. review TM
Review meeting
2
4
5
2. Facilities Visit and Condition
Assessment
Visits, interviews
Detailed visits
Assessment TM
Review meeting
7
9
10
11
3. Best Industry Practices for Treating
Variable TDS Water
Best Practices TM
Review meeting
10
11
4. Projections Future Water Quality Water quality TM
Review meeting
14
15
5. Treatment Alternatives Evaluation for
Handling TDS Variability
Alternatives report
Review meeting
22
24
6. Conceptual design Conceptual design report
Review meeting
31
33
7. Preliminary design
Preliminary design report
Review meeting
Preliminary design report (final)
41
43
45
II-13
Variable TDS RO Conceptual Design
Weeks following Notice to Proceed
Tasks/Subtasks 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46
Task 1 Project Kick Off and Information Review
Review existing information
Develop existing information review TM
Collect additional data (by Collier)
Task 2 Facilities Visit and Condition Assessment
Initial visit, interviews staff
Detailed visits disipline engineers
Develop condition assessment TM
Task 3 Best Industruy Practices for Treating Variable TDS Water
Review literature, contact/visit utilities
Contact equipment manufacturers
Develop best practices TM
Task 4 Projections Future Water Quality
Establish existing, future operations of wellfield
Project future water quality
Develop water blending scenarios
Develop future water quality TM
Task 5 Treatment Alternatives Evaluation for Handling Variable TDS
Develop Operational solutions
Develop Capital solutions
List advantages/disadvantages
Collect vendor quotes, cost estimates
Develop alternative comparison TM
Task 6 Conceptual Design
Describe system, table design criteria
Develop drawings
Finished water quality and corrosion control
Constructability and O&M reviews
Cost estimating
Develop conceptual design report
Task 7 Preliminary Design
Develop drawings
Constructability and O&M reviews
Update cost estimating
Develop preliminary design report
Finalize preliminary design report
Milestones (meetings, deliverables)
Task 1 Project Kick Off and Information Review
Notice to Proceed/PO
Kick off meeting, collect information
Issue TM
Review meeting
Task 2 Facilities Visit and Condition Assessment
Issue TM
Review meeting
Task 3 Best Industruy Practices for Treating Variable TDS Water
Issue TM
Review meeting (combined Task 2 meeting)
Task 4 Projections Future Water Quality
Issue TM
Review meeting
Task 5 Treatment Alternatives Evaluation for Handling Variable TDS
Issue TM
Review meeting
Task 6 Conceptual Design
Issue report
Review meeting
Task 7 Preliminary Design
Issue draft report
Review meeting
Issue final report
Example Work Product
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 1
TECHNICAL MEMORANDUM
Marco Island Water Treatment Expansion Options
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: January 11, 2010
Summary and Recommendations
The capacity analysis reports for the past several years have indicated that Marco Island
Utilities will need 4 mgd of additional capacity by 2014 to meet build-out potable water
demands. In anticipation of this need for expansion, the City asked CH2M HILL to conduct
a study in 2007 of viable and cost effective expansion treatment options that would improve
finished water quality, better protect public health, meet anticipated regulations, and reduce
facility operating cost. The 2007 water expansion study identified membrane filtration, ion
exchange, low pressure RO, lime softening, in-line coagulation, and UV as potential
treatment processes. However treating a variable surface water like the Marco Lakes source
water can pose treatment risks. CH2M HILL therefore conducted an 8-month pilot study
that evaluated the treatment feasibility of potential treatment trains.
The pilot study confirmed the viability of four potential treatment trains and provided
estimated full-scale process design criteria. These criteria were used to rank each of the
process options, develop construction and operating cost estimates, and compare overall life
cycle costs of each process train. Exhibit 1 shows the projected operating, capital, present
worth and life cycle costs for each of the evaluated process trains.
EXHIBIT 1
Projected Life Cycle Cost of Process Train Options
Marco Island North Water Treatment Plant Expansion Options
Process Train Operating Cost
($/year)
Capital Cost
(2009$)
Present Worth
(2009 $)
Life Cycle Water Cost
(2009 $)
Option 1 – Coag/MF/UV $1,493,500 $7,992,000 $216,500,000 $1.06
Option 2 - MF/IX/UV $783,700 $10,663,000 $120,100,000 $0.59
Option 3 - LS/MF/UV $1,626,400 $11,904,000 $238,900,000 $1.17
Option 4 - MF/LPRO/UV $764,400 $7,029,000 $113,700,000 $0.56
- Present worth and life cycle amortization based on 20-year life cycle and 6 percent interest rate
Exhibit 2 shows the proposed process flow diagram for process option 4 which includes
membrane filtration of the Marco Lakes water followed by transfer of the water to the
SWTP, split treatment by one of the existing BWRO trains, UV disinfection, and blending
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 2
with BWRO permeate before distribution. Process train option 4 has the following benefits
that make it the most desired process option:
Reduced stress on brackish aquifer – The dependence on brackish groundwater will be
minimized because the new treatment process doesn’t require the BWRO permeate for
blending to meet finished water quality goals.
Operability: The MF and LPRO units can be shut off and started anytime and are
completely automated. The units can treat varying flows thus facilitates part time
operation. There are minimal continuous treatment chemicals.
Effective treatment for all finished water goals – The MF and LPRO process would
remove all target constituents including hardness, sulfate and chloride without the need
for blending.
Expandability: The treatment capacity at the NWTP can be increased to meet future
demands due to the relative small footprint of MF.
EXHIBIT 2
Option 4 – Proposed Process Flow Diagram
Marco Island North Water Treatment Plant Expansion Options
MARCO LAKES
RAW WATER
MEMBRANE
FILTRATION
WELLS
CARTRIDGE
FILTERS
FEED
PUMPS BWRO TRAINS DEGASIFIERS
STORAGE
TANKS
HIGH SERVICE
PUMPS
TO
DISTRIBUTION
SYSTEM
NWTP
SWTP
PROPOSED
EXISTING
UV
TRANSFER PUMP
STATION
Coagulant
FEED
PUMPS
CONVERTED
LPRO TRAINS
UV
CH2M HILL recommends implementing process train option 4. The new membrane
filtration system would be located at the NWTP, while an existing RO train and new UV
system would treat the water at the SWTP.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 3
Introduction
The City of Marco Island owns and operates two water treatment facilities, the North Water
Treatment Plant (NWTP) and the South Water Treatment Plant (SWTP). The NWTP is a
conventional lime softening plant that treats the Marco Lakes surface water and has a
capacity of 6.7 MGD. The lime softening facility primarily removes hardness, organics,
turbidity, and potential pathogens from the surface water supply. The SWTP is a Reverse
Osmosis (RO) treatment facility that treats brackish well water and has a capacity of 6.0
MGD. The RO process removes salt from the brackish feed water that exceeds drinking
water standards for TDS, sodium, chloride, and sulfate. A portion of the treated water from
the NWTP is blended with the RO permeate to add hardness to the SWTP finished water
and stabilize it before distribution. The NWTP is operated continuously above 6.0 mgd and
the SWTP is used to meet the remaining demand.
The City plans on expanding potable water production capacity at the NWTP to meet
increasing water demands and reduce the stress on the brackish aquifer at the SWTP. The
new treatment process train must treat Marco Lakes water at the NWTP, meet current and
proposed future regulations, blend with RO permeate at the SWTP, and produce water that
is similar to or better than existing water quality. The City has contracted CH2M HILL to
explore potential process options for treating additional Marco Lakes water. This technical
memorandum (TM) describes the Marco Lakes source water quality, the desired finished
water quality, the treatment processes that can meet these goals, and potential process trains
for the expansion.
Source Water and Finished Water Quality
The Marco Lakes raw water source is located approximately 10 miles north of the island and
is fed by the Henderson Creek and influenced by surficial groundwater. The City also uses
Aquifer Storage and Recovery (ASR) wells that are recharged during the wet season and
then used for additional capacity during the dry. The ASR recovered water is blended with
the surface water or used alone to feed the NWTP in the dry season. Both the Marco Lakes
surface water and recovered ASR well water are influenced by groundwater with elevated
levels of chloride and sulfate. Exhibit 3 presents the range of feed water quality entering the
NWTP.
The treated water must be similar to or improve upon existing finished water quality, as
well as meet current and proposed future regulatory requirements including Florida
Department of Environmental Protection (FDEP) primary and secondary drinking water
standards, the Stage 2 Disinfection / Disinfection Byproducts Rule (S2DBPR) and the Long-
Term 2 Enhanced Surface Water Treatment Rule (LT2SWTR). Exhibit 3 presents the City’s
anticipated finished water quality goals.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 4
EXHIBIT 3
Marco Lakes Raw Surface Water Quality and Desired Finished Water Quality
Marco Island North Water Treatment Plant Expansion Options
Parameter Marco Lakes Surface Water
Quality Range (Average)
Finished Water Quality Goal
pH 7.2 – 8.2 (7.8) 8.8
Temperature (Celsius) 20 – 32 (26) -
Chloride (mg/L) 66 – 154 (120) < 100
Sulfate (mg/L) 40 – 150 (100) < 80
TDS (mg/L) 190 – 600 (410) < 400
Total alkalinity (mg/L as CaCO3) 120 – 340 (235) > 35
Total hardness (mg/L as CaCO3) 170 – 380 (330) 100-120
Turbidity (NTU) 0.5 – 21 (1.5) < 0.3
TTHM (µg/L) - 80
HAA5 (µg/L) - 40
Total organic carbon (mg/L) 9.3 – 17 (14) 10*
Color (PCU) 20 – 70 (35) < 5
* Based on EPA D/DBPR requirement of 30% TOC removal; actual removal may be greater depending on
selected treatment process.
The raw Marco Lakes water is high in color, hardness, and total organic carbon (TOC)
including disinfection byproduct (DBP) precursors. The surface water may also include
pathogens that require removal or inactivation. The high concentrations of sulfate and
chloride may be contributing to copper corrosion problems on the north end of the island.
The selected process must effectively address these target constituents to meet the desired
water quality goals.
The finished water quality must be stable (non-corrosive) with a pH near 8.8, total alkalinity
above 35 mg/L as CaCO3, and total hardness between 100 to 120 mg/L as CaCO3. The
treatment process should minimize increases in sulfate and chloride, or even reduce them in
order to control copper corrosion. The new treatment process should meet all of these goals
before blending with the existing BWRO permeate that may be limited in the future.
The finished water must meet the S2DBPR by achieving 30 percent TOC removal and
maintaining a TTHM concentration below 80 g/L and a HAA5 concentration below 40
g/L at all points within the distribution system. The water must also meet the S2SWTR by
achieving 3-log Giardia, 2-log cryptosporidium and 4-log virus removal using a multiple
barrier disinfection approach and maintaining filtered water turbidity below 0.3 NTU.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 5
Treatment Processes to Address Target Constituents
Potential treatment processes that can remove organics, hardness, pathogens, turbidity,
chloride and sulfate were identified for consideration. These processes include:
Membrane filtration
In-line coagulation
Ion exchange
UV disinfection
Lime softening
Low pressure reverse osmosis
A general process description, target constituents, and process features for each of these
treatment processes are included in the sections below.
Membrane Filtration
The proposed membrane filtration (MF) system is a beneficial process component when
treating surface water and is therefore common to all process options. Membrane filtration
receives the most credit for pathogen removal by the LT2SWTR and produces consistently
low turbidity finished water independent of feed water turbidity.
The Pall pilot study demonstrated that their membrane filtration system can successfully
treat raw water, lime softened water, and in-line coagulated raw water. The differing feed
water types do not impact membrane system configuration, but do impact the design flux
rate, EFM interval, EFM chemicals, and CIP interval.
Lake water treatment by lime softening and coagulation increase the need for citric acid
EFMs. The clarified lime softened water improves the sustainable flux rate while in-line
coagulation without clarification increases the solids loading on the membranes and
therefore reduces sustainable flux rate.
The MF system trains are divided into banks containing several pressure vessels or
cartridges. The individual train flow remains relatively constant while individual banks are
backwashed. The MF systems typically operate in a “dead-end” configuration and
backwash at high trans-membrane pressure (TMP) or on a set time interval depending on
the feed solids loading (typically 10 to 60 minutes).
Occasionally, the system automatically performs an enhanced flux maintenance (EFM) that
includes recirculating a citric acid or sodium hypochlorite solution around or through the
membrane fibers for approximately 30 minutes. On a monthly basis or greater, depending
on the level of fouling, individual trains of the membrane system are scheduled for a clean-
in-place (CIP) cycle where a citric acid or sodium hypochlorite and/or sodium hydroxide
solution is recirculated through the membranes for an extended period of time to restore
productivity that could not be restored through backwash or EFM.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 6
Target Constituents
Pathogens (Giardia, Crypto and some virus)
Turbidity
Design Criteria
Flux – 60 to 80 gfd
Recovery – 90 to 95%
Backwash interval – 30 minutes
EMF interval – 3 days (alternating citric / hypochlorite)
CIP interval – > 30 days (citric / hypochlorite + caustic)
Process Features
Superior pathogen and turbidity removal – membrane filters are an absolute barrier to
pathogens larger than the design pore size including Giardia and Cryptosporidium.
Membrane filtration can be credited with up to 5-log Giardia and Crypto removal,
however a practical upper limit is 4-log for full-scale systems as demonstrated by direct
integrity testing. Finished water turbidity is always less than 0.1 NTU independent of
upstream water quality.
Excellent pretreatment for downstream RO processes – Membrane filtrate virtually
eliminates particulate fouling in downstream RO systems.
Small footprint – Membrane filters operate at high loading rate or flux and the hollow
fiber construction allows a high surface area in a small footprint.
Operability: Individual units can be started or stopped anytime and flow can be
adjusted up to the maximum design flux. The system is completely automated during
normal operation, backwash and EFM.
Expandability – MF systems are modular and can be easily expanded with additional
equipment installation and minimal infrastructure.
Backwash and cleaning chemicals – The membrane filtration system typically uses citric
acid, sodium hydroxide, and sodium hypochlorite for daily maintenance cleans and
monthly clean-in-place (CIP) events.
Low operating cost – MF systems operate at a TMP between 4 and 30 psi with minimal
chemical usage.
Backwash disposal – MF require disposal of backwash waste that is typically 3 to 10
percent of the feed flow.
In-Line Coagulation
In-line coagulation would be used to inject coagulant (ferric chloride or aluminum sulfate)
into the raw water pipeline to help coagulate dissolved organics in the raw water to
promote their removal by the MF system. An in-line rapid mixer would provide effective
mixing of the coagulant and help bind the dissolved organics to suspended pin floc that
would be subsequently removed by downstream filtration. An in-line coagulation and
mechanical mixer design drawing is shown in Exhibit 4.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 7
EXHIBIT 4
In-line mechanical mixer design drawing
Marco Island North Water Treatment Plant Expansion Options
Target Constituents
Color
TOC
DBP precursors
Design Criteria
Coagulant – Aluminum sulfate (~80 mg/L) or ferric chloride (~25 mg/L)
Mixer type – in-line powered mixer with variable speed motor
Process Features
Excellent pretreatment for downstream MF – The coagulation of dissolved organics
reduces fouling in downstream MF treatment.
Low capital cost – The in-line coagulation system is simple including only a chemical
tank, metering pump, injectors, and a mixer
Small footprint – The in-line coagulation system has minimal equipment and would be
installed into the feed water piping.
Additional sludge management: The addition of solids could reduce the efficiency of the
filtration process. Recycling the sludge to the lime plant would add operational costs.
Potentially high chemical usage – The coagulant dose required to achieve the desired
TOC and color removal can be up to 100 mg/L. The raw water pH may also have to be
reduced for optimum coagulation thus requiring a strong acid like sulfuric acid or
hydrochloric acid.
Increased salts – Coagulant and acid feed increases chloride and/or sulfate in the treated
water.
Ion Exchange
The proposed ion exchange (IX) system would use an anion exchange resin in pressure
vessels that selectively exchanges organics including TOC, color, and DBP precursors in the
feed water with chloride. A two-step regeneration process would then backwash and
regenerate the resin using a high concentration sodium chloride solution. The adsorption
and regeneration steps are conceptually shown in Exhibit 5.
ACID
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 8
IRON
EXHIBIT 5
Regeneration and Adsorption using IX resin
Marco Island North Water Treatment Plant Expansion Options
Target Constituents
Color
TOC
DBP precursors
Design Criteria
Number of units – 4
Vessel diameter – 11 ft
Regeneration interval – 3 days
IRON
IRON
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 9
Resin replacement interval – 7 years
Process Features
Operability – The unit can be shut off and started anytime and is completely automated.
The unit facilitates part-time operation because it can treat varying flows.
Excellent color and organics removal - Almost complete color removal and up to 70%
organics removal. The improved organics removal leads to reduced DBP formation.
Increased salts in treated water – Exchange between chloride and organics increases the
chloride concentration in finished water.
Minimal chemicals – Only salt is needed to regenerate the resin.
Brine disposal – Regeneration of the resin creates a brine waste with a high sodium
chloride concentration that requires proper disposal
No Repumping – The ion exchange is housed in pressure vessels that allow installation
in-line without breaking head.
Ultraviolet Disinfection
UV disinfection is a physical process that uses photochemical energy to prevent cellular
proteins and nucleic acids (i.e., DNA and RNA) from further replication. A cell that cannot
replicate also cannot infect. The germicidal UV light wavelengths range from 200 to 300 nm
with the optimum germicidal effect occurring at 253.7 nm. UV is a reliable component of a
multi disinfectant treatment strategy often used in conjunction with chlorine to provide a
dual barrier. The concept is further illustrated in Exhibit 6.
EXHIBIT 6
Multi Barrier UV Protection
Marco Island North Water Treatment Plant Expansion Options
Courtesy: Trojan UV
Exhibit 7 further illustrates the resistance of waterborne pathogens to UV.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 10
EXHIBIT 7
Pathogen Resistance to UV
City of Marco Island UV Disinfection Evaluation
Two of the most common UV systems available in the market are the Low Pressure systems
and the Medium Pressure systems. A brief description of each type is given below.
Low Pressure UV Systems
The low pressure (LP) UV systems include low intensity, high intensity and amalgam
lamps. The low pressure lamps emit monochromatic UV light and the majority of the
emissions are produced at the germicidal wavelength of 254 nm. The LP UV systems are
relatively efficient because approximately 40% of the input energy is converted to
germicidal UV and the lamps operate at temperatures between 40-95°C. However, the LP
UV lamps are lower intensity than medium pressure lamps and therefore require a
significantly larger footprint. Some of the advantages of LP lamps include greater lamp life
than medium pressure lamps, low energy consumption, and lower fouling than medium
pressure lamps because of lower operating lamp temperature and lower UV density.
Medium Pressure UV systems
Medium-pressure (MP) UV lamps produce significantly more UV light than low pressure
lamps. The total UV Type C output (i.e., wavelengths from 200 to 280 nm, the most
germicidal range) from a MP lamp is roughly 30 to 150 times higher than the output from a
LP lamp. However, the MP lamps produce output with a broad spectral energy distribution,
so the lamps are much less efficient at converting energy to germicidal energy. The
polychromatic output covers wavelengths that have different levels of germicidal
effectiveness. Combining the effects of the polychromatic light spectrum and the shorter
lamp lengths, the UV output from an MP lamp is typically about 10 to 20 times higher than
output from an LP lamp. The MP lamps need frequent cleaning as they operate at high
temperatures, have a shorter lamp life, and demand higher power compared to LP lamps.
Exhibit 8 summarizes the key features of low pressure and medium pressure UV systems.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 11
EXHIBIT 8
Comparison of Low Pressure and Medium Pressure UV Systems
City of Marco Island UV Disinfection Evaluation
Feature Low Pressure UV system Medium Pressure UV system
Power consumption (KWh/kgal) 0.02 (Giardia/crypto)
0.10 to 0.11 (virus)
0.04 to 0.09 (Giardia/crypto
0.20 to 0.24 (virus)
Reactor Footprint Length: 70” to 187”
Width: 39” to 87”
Length: 27” to 34”
Width: 41” to 54”
Equipment cost ~$247k (Giardia/crypto)
~$1.37M (virus)
~$220k (Giardia/crypto)
~$660k (virus)
Number of Lamps 30 to 84 lamps for 4,600 gpm 4 to 8 lamps for 4,600 gpm
Lamp life 12,000 hr 6,000 – 9,000 hr
Fouling Rate Lower due to lower temperature Higher due to higher temperature
Lamp Cleaning Manually initiated mechanical and
chemical cleaning systems
Fully automated mechanical and
chemical cleaning systems
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 12
UV Disinfection Benefits to Marco NWTP
The benefits of installing a UV system at the NWTP are
1. EPA regulations require a plant to achieve 4-log virus inactivation after the water is
exposed to air during a treatment process. UV disinfection could provide the additional
2-log virus inactivation post filtration without the need for extensive contact time. The
0.5 MG storage tanks can be reallocated to the water reclamation facility.
2. The plant currently falls under Bin 1 under the Long-Term 2 Enhanced Surface Water
Treatment Rule (LT2) and hence does not require inactivation of cryptosporidium.
However, changing watersheds for the NWTP source water could quickly change this
bin classification without warning and require more disinfection.
3. UV’s cost-effectiveness and ability at low doses to inactivate the pathogenic protozoa
(resistant to chlorine disinfection methods) will provide added benefits to meet future
disinfection requirements.
4. A UV system would provide virus, Giardia and cryptosporidium inactivation with the
virus inactivation as the limiting criteria for determining UV dose.
5. The City would improve public health protection with multiple disinfection barriers.
6. High organics in the raw surface water is a concern for the City because of disinfection
by products formation. Use of UV reduces use of free chlorine for disinfection, thus
reducing DBP formation. The free chlorine injection point could be moved closer to the
ammonia injection point because of lower CT requirements, leading to lower DBP
formation.
The proposed UV system would be an in-line reactor as shown in Exhibit 9 that would be
installed on the membrane filtered water line before blending with finished water from the
existing SWTP or NWTP. The UV system would be used for primary disinfection including
meeting the multiple barrier inactivation requirements of Giardia and Cryptosporidium, as
well as the required residual virus inactivation.
EXHIBIT 9
UV Disinfection unit
Marco Island North Water Treatment Plant Expansion Options
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 13
Target Constituents
Pathogens
Design Criteria
UV dose – 50 mJ/cm2
UV Transmission - > 90%
Target Giardia inactivation – 0.5-log
Target Cryptosporidium inactivation – 2.0-log
Target virus inactivation – 3.0-log
Process Features
Operability - UV is simple to install and requires minimal space, supervision and
maintenance.
DBP and free chlorine reduction - Eliminates the use of free chlorine as a primary
disinfectant and reduces DBP formation.
Low construction cost – The UV process has minimal equipment and may be installed in
filtered water piping thus reducing construction cost.
High operating cost: Operating cost is high relative to using free chlorine as primary
disinfectant.
No Disinfection residual – There is no disinfection residual in the water, thus requiring a
secondary disinfectant like the chloramines currently used by Marco Island.
Restricted water quality – Not suitable for water with high color, turbidity and dissolved
organics.
Low Pressure Reverse Osmosis
Low pressure reverse osmosis (LPRO) is the same process as the brackish water RO
(BWRO) system used at the SWTP. The LPRO system operates at a lower pressure (< 150 psi
versus > 300 psi) with some reduction in salt rejection (> 95% versus > 99%). The LPRO
membranes will effectively remove the target constituents from the pretreated Marco Lakes
water.
The existing BWRO trains at the SWTP can be used for a LPRO application by exchanging
the existing BWRO membrane elements for LPRO membrane elements and de-staging the
membrane feed pumps. The existing BWRO trains membrane can be used with limited
modification with the existing membrane elements and feed pumps as well at a higher
operating cost. Operating with the existing feed pumps and BWRO membrane elements
would allow the use of the trains for either surface water or brackish well water treatment.
Target Constituents
Salts (TDS, chloride, sulfate)
Hardness
Color
TOC
DBP precursors
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 14
Design Criteria
Flux – 12-15 gfd
Recovery – 85 to 90%
Feed pressure – 100 to 150 psi
Salt rejection > 95%
Treated hardness – < 10 mg/L as CaCO3
TOC reduction – > 95%
Treated color – < 2 PCU
Treated chloride and sulfate – 5 to 10 mg/L
Process Features
Removes most feed water constituents – The LPRO system will highly reject TOC, color,
DBP precursors, TDS, chloride, sulfate, and hardness.
Operability – LPRO is automated and is easy to start and stop with changing demands.
Maintenance is minimal.
Small footprint – The LPRO system is contained in compact trains that can fit into a
small footprint.
Post-treatment stabilization – RO permeate is aggressive and will corrode distribution
system piping unless post-treated or blended with feed water bypass flow.
Requires pretreatment – Upstream membrane filtration and potentially minimal
coagulation and biocide addition would be needed to reduce the fouling potential of the
raw surface water. RO membranes are not suitable for treating water with high
turbidity or organic/biological fouling potential.
Concentrate disposal – A portion of the feed water (10 to 20 percent) is lost to the
concentrate stream and requires proper disposal. The concentrate can be injected into a
concentrate injection well, or possibly sent to the WWTP for eventual use as irrigation
water.
Enhanced Lime Softening
Conventional softening uses lime to increase pH of the feed water to reduce the solubility of
calcium carbonate (above pH 9.0) and magnesium carbonate (above pH 11.0) thus
precipitating calcium and magnesium hardness that subsequently settles out in a
reactor/clarifier. The precipitate created by this softening process also removes feed water
turbidity. Enhanced lime softening uses the precipitation of magnesium Mg(OH)2 at high
pH, or coagulant added with the lime in the reaction zone to remove color, TOC and DBP
precursors that are otherwise not removed in the lime softening process.
A lime softening reactor/clarifier has been illustrated in Exhibit 10.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 15
EXHIBIT 10
Conventional Lime Softening Solids Contact Reactor Schematic
Marco Island North Water Treatment Plant Expansion Options
FROM INFILCO ACCELATOR LITERATRE
Target Constituents
Harness
Turbidity
Color
TOC
DBP precursors
Design Criteria
Reaction zone hydraulic retention time – 10 to 15 minutes
Reaction zone pH – 10 to 10.5
Settling zone overflow rate – < 2.0 gpm/ft2
Chemical feeds – Lime (150–200 mg/L) /Alum (10–20 mg/L) / CO2 (20–40 mg/L)
Dry solids production – 4,000 to 5,000 lbs/MG
Treated hardness – 80 to 120 mg/L as CaCO3
TOC reduction – 25% to 35
Treated color – 5 to 15 PCU
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 16
Process Features
Hardness removal – The lime softening process precipitates calcium carbonate and
potentially magnesium hydroxide to reduce the total hardness of the feed water.
Non-fouling process – The lime system is not susceptible to fouling by feed water
turbidity, organics, or biological activity.
Chemical intensive – Large doses of lime for softening, alum for organics removal,
carbon dioxide for recarbonation (post softening pH adjustment), and potentially soda
ash for non-carbonate hardness removal are required to make the lime softening process
work.
Solids disposal – The lime softening process generates a large amount of solids that
require dewatering and disposal.
Large footprint – The lime softening process requires a large footprint for the settling of
lime solids.
Increased operations and maintenance – The lime slaking process and solids generation
requires more operator attention and maintenance than other process options.
High operating cost – Operating cost can be high due to chemical consumption and
solids handling and disposal.
Process Train Options
Each of the unit processes above were used to develop the process train options listed below
for the treatment of 4 mgd of Marco Lakes raw water at the NWTP site. Each of these
process train options is designed to meet current and proposed future regulatory
requirements as well as the Marco Island finished water quality goals.
1. In-line coagulation/membrane filtration/UV/blending with BWRO permeate
2. Membrane filtration/Ion Exchange/UV/blending with BWRO permeate
3. In-line coagulation/enhanced lime softening/membrane filtration/UV
4. Membrane filtration/converted LPRO train/UV/blending with BWRO permeate
For each of these options, the flow through the existing NWTP conventional lime softening
train would be decreased during normal operation to 5 mgd to improve operability and
ensure the existing system can handle raw water quality excursions. This reduction in flow
would coincide with the decommissioning of the existing Zenon membrane system.
The sections below describe each of the process train options in more detail including target
treatment constituents, process flow diagrams, site layouts, process advantages, and
potential process limitations.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 17
Process Train Option 1 – In-line coagulation/membrane filtration/UV/blending with
BWRO permeate
Process Train Option 1 includes in-line coagulation, membrane filtration, UV, and blending
with BWRO permeate at the SWTP. Each of the processes were selected for their ability to
remove the target constituents listed in Exhibit 11.
EXHIBIT 11
Process Train Option 1 Process Constituent Removal
Marco Island North Water Treatment Plant Expansion Options
Treatment Process Target Constituents
In-line coagulation TOC, color, DBP precursors
Membrane filtration Pathogens, turbidity, floc
UV Multiple barrier Giardia inactivation, virus inactivation
Blending with RO permeate Hardness, residual color, residual TOC, chloride, sulfate
The In-line coagulation process would be installed on the existing raw water line as it enters
the NWTP site. The MF process, located on the NWTP site, would then remove the floc,
turbidity and pathogens from the coagulated water. A new filtrate pump station would
transfer the filtered water through an in-line UV system and ultimately to the SWTP for
blending with RO permeate. Exhibit 12 shows the proposed process flow diagram for this
process option. Exhibit 13 shows a conceptual layout at the NWTP site.
EXHIBIT 12
Option 1 - Process Flow Diagram
Marco Island North Water Treatment Plant Expansion Options
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 18
EXHIBIT 13
Option 1 - Preliminary Site Layout
Marco Island North Water Treatment Plant Expansion Options
Process Advantages
Simple process – The in-line coagulation, membrane filtration and UV system are
automated treatment processes.
Small footprint – the proposed layout fits within the limited space available on the
NWTP site, including space for future expansion of the membrane filtration system.
Process Limitations
High coagulant and sulfuric acid dosing – Pilot study data shows that high doses of
ferric chloride or aluminum sulfate are required to meet color and TOC goals. The high
chemical dosing has the following impacts:
High operating cost ($50k/year in chemical cost alone)
Reduced downstream MF flux due to the additional solids loading. A small amount
of coagulant (5-10 mg/L) improves membrane system performance, however the
target doses up to 80 mg/L reduce MF flux from 80 gfd to 60 gfd. This increase in
flux increases MF system cost.
Increased finished water chloride and sulfate from the sulfuric acid (H2SO4) and
alum (AL2(SO4)3) or ferric chloride (FeCl3). The increase in chloride and/or sulfate
may be as high as 50 to 150 mg/L.
Additional sludge production due to the increased solids created by coagulation
Operator safety when handling sulfuric acid and coagulants
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 19
Incomplete TOC and color removal – Pilot test results show that in-line coagulation will
only reduce TOC by 10 percent and reduce color to 15 - 20 PCU. Higher coagulant doses
needed to meet TOC and color removal goals increase the solids loading on the MF
system to above sustainable levels.
Requires blending with RO permeate – The proposed treatment processes do not
remove hardness and nor the required TOC and color. Blending with RO permeate is
needed to reduce these target constituents as well as chloride and sulfate that may
impact copper corrosion. The production capacity of the new process train would be
limited to operating only when the RO system at the SWTP is operational. A minimum
blend ratio of 1:2 (MF filtrate: BWRO permeate) would be needed to reduce finished
water color to 5 PCU and total hardness to approximately 100 mg/L as CaCO3.
Process Train Option 2 – Membrane filtration/Ion Exchange/UV/blending with
BWRO permeate
Process Option 2 includes membrane filtration of the raw Marco Lakes water followed by
ion exchange, UV, and blending with BWRO permeate at the SWTP. Each of the processes
were selected for their ability to remove the target constituents listed in Exhibit 14.
EXHIBIT 14
Process Train Option 2 Process Constituent Removal
Marco Island North Water Treatment Plant Expansion Options
Treatment Process Target Constituents
Membrane filtration Pathogens, turbidity
Ion Exchange TOC, color, DBP precursors
UV Multiple barrier Giardia inactivation, virus inactivation
Blending with RO permeate Hardness, residual TOC, chloride, sulfate
This treatment process option uses MF to remove turbidity, microorganisms and as a
pretreatment for IX. The IX system would reduce TOC and eliminate color from the
membrane filtrate. A new filtrate pump station would transfer the filtered water through an
in-line UV system and ultimately to the SWTP for blending with RO permeate. The
downstream UV treatment would provide the required additional ½ log Giardia and 3-log
virus inactivation. The treated water would have high hardness, alkalinity, sulfate and
chloride that would be blended with RO permeate to help meet finished water quality goals.
Exhibit 15 shows the proposed process flow diagram for this process option. Exhibit 16
shows a conceptual layout at the NWTP site.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 20
EXHIBIT 15
Option 2 - Process Flow Diagram
Marco Island North Water Treatment Plant Expansion Options
WELLS
CARTRIDGE
FILTERS FEED PUMPS BWRO TRAINS
STORAGE TANKS HIGH SERVICE
PUMPS
MARCO LAKES
RAW WATER ION-EXCHANGE
TO
DISTRIBUTION
SYSTEM
NWTP
SWTP
PROPOSED
EXISTING
DEGASIFIERS
UV
MEMBRANE
FILTRATION
EXHIBIT 16
Option 2 - Preliminary Site Layout
Marco Island North Water Treatment Plant Expansion Options
Process Advantages
Simple process – The membrane filtration, ion exchange and UV system are automated
treatment processes.
Small footprint – the proposed layout fits within the limited space available on the
NWTP site, including space for future expansion of the membrane filtration system
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 21
Organics removal – The IX process easily removes all color and 35 to 40 percent of the
TOC.
Safety – The proposed process train does not require the use of strong acids or
coagulants that can be a handling risk.
Improved MF system performance – The MF pilot was fed directly with the Marco Lakes
surface water without in-line coagulation and ran without operational issues at an
increased flux rate (65 up to 80 gfd)
Process Limitations
Potential increased MF fouling – Elimination of a small dose of coagulant upstream of
the membrane filtration system could increase the organic fouling potential during WQ
excursions.
Increased finished water chloride – The IX system replaces TOC with chloride during
the exchange process. While the increase in chloride would only be 10 to 20 mg/L, these
modest increases may further increase issues with copper corrosion.
Requires blending with RO permeate – The proposed treatment processes do not
remove hardness. Blending with RO permeate is needed to reduce total hardenss as
well as chloride and sulfate that may impact copper corrosion. The production capacity
of the new process train would be limited to operating only when the RO system at the
SWTP is operational. A minimum blend ratio of 1:2 (MF filtrate: BWRO permeate)
would be needed to reduce finished water total hardness to approximately 100 mg/L as
CaCO3.
Brine disposal – The IX system produces a bring waste that would require some capacity
in the existing injection wells.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 22
Process Train Option 3 – In-line coagulation/lime softening/membrane
filtration/UV
This treatment process option includes in-line coagulation followed by a new enhanced lime
softening reactor/clarifier to remove hardness, turbidity, color, and organics followed by
MF for pathogen and residual suspended solids removal. Each of the processes were
selected for their ability to remove the target constituents listed in Exhibit 17.
EXHIBIT 17
Process Train Option 3 Process Constituent Removal
Marco Island North Water Treatment Plant Expansion Options
Treatment Process Target Constituents
In-line coagulation TOC, color, DBP precursors
Enhanced lime softening Hardness, turbidity, additional TOC DBP precursors, and color
Membrane filtration Pathogens, turbidity, lime solids
UV Multiple barrier Giardia inactivation, virus inactivation
Blending with RO permeate Residual color, residual TOC, chloride, sulfate
The lime softening new process train would operate in parallel to the existing similar
process train at the NWTP. Additional improvements would include a new in-line
coagulation system that would feed both the existing and new lime softening reactor for
improved organics removal and a UV system that would disinfect all of the water treated by
the NWTP ensuring that both process trains meet the required 3-log Giardia and 4-log virus
inactivation without the need for a chlorine contact basin. Exhibit 18 shows the proposed
process flow diagram for this process option. Exhibit 19 shows a conceptual layout at the
NWTP site.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 23
EXHIBIT 18
Option 3 - Process Flow Diagram
Marco Island North Water Treatment Plant Expansion Options
EXHIBIT 19
Option 3 - Preliminary Site Layout
Marco Island North Water Treatment Plant Expansion Options
Process Advantages
High flux rate – MF can run at a higher flux rate because it would be treating low-
turbidity settled lime softened water.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 24
Harness and organics removal – The enhanced lime softening process can effectively
reduce hardness, organics and color to meet drinking water standard without the need
for blending with RO permeate.
Low fouling – The lime softening treatment process is not impacted by the fouling
potential of organic material in the feed water.
Finished water distribution flexibility – The treated water would be distributed at the
NWTP or at the SWTP because the treated water doesn’t require blending to meet
finished water quality goals.
Process Limitations
Operability – Part-time operation is difficult due to the long start-up time required to
stabilize the lime softening process. The lime softening process requires continuous
monitoring and adjustment with changing feed water quality
Large footprint – The lime softening process has a large footprint and may not fit well on
the NWTP site without variances on setbacks and layouts that result in limited access to
treatment components.
High operating cost – If operated for optimum TOC and color removal, the enhanced
lime softening process will use more lime and generate significantly more solids that
will require disposal. Both the added lime and sludge will increase operating cost.
Membrane scaling – The downstream MF units will be susceptible to CaCO3 scaling,
especially during softener upsets. Operation of the membrane system downstream of
lime softening may require more frequent acid cleaning or a lower operating flux rate.
Finished water chloride and sulfate – The lime softening process doesn’t remove
chloride or sulfate and the use of coagulant will increase concentration somewhat.
Process Train Option 4 – Membrane filtration/UV/converted LPRO train/blending
with BWRO permeate
This process option uses MF for removing turbidity and pathogens, as well as pretreatment
for downstream LPRO. A new pump station would transfer the filtrate to the SWTP for
further treatment by LPRO and UV disinfection. Each of the unit processes have been
selected to remove the target constituents shown in Exhibit 20
EXHIBIT 20
Process Train Option 4 Process Constituent Removal
Marco Island North Water Treatment Plant Expansion Options
Treatment Process Target Constituents
Membrane filtration Pathogens, turbidity
LPRO Hardness, color, TOC, DBP precursors, TDS, chloride, sulfate
UV Multiple barrier Giardia inactivation, virus inactivation
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 25
One or two of the existing BWRO trains at the RO WTP would be converted to LPRO by
replacing the existing brackish water membranes with low energy membrane elements.
These low energy elements would remove hardness, TOC, color, chloride, and sulfate from
the feed water at a much lower pressure (< 150 psi) compared to BWRO. The membrane
permeate would be blended with a feed water bypass stream, sent through UV for the
required additional ½ log Giardia and 3-log virus inactivation, and then blended with
BWRO permeate in the ground storage tanks. Exhibit 21 shows a process flow diagram for
this process train option Exhibit 22 shows a conceptual layout of the membrane filtration
system at the NWTP. The LPRO and UV systems would be located inside the existing SWTP
membrane building.
The existing BWRO trains membrane may also be used with limited modification while
using the existing membrane elements and feed pumps. This option would increase
operating cost, however it would decrease initial cost and would allow the use of the trains
for either surface water or brackish well water treatment.
EXHIBIT 21
Option 4 - Process Flow Diagram
Marco Island North Water Treatment Plant Expansion Options
MARCO LAKES
RAW WATER
MEMBRANE
FILTRATION
WELLS
CARTRIDGE
FILTERS
FEED
PUMPS BWRO TRAINS DEGASIFIERS
STORAGE
TANKS
HIGH SERVICE
PUMPS
TO
DISTRIBUTION
SYSTEM
NWTP
SWTP
PROPOSED
EXISTING
UV
TRANSFER PUMP
STATION
Coagulant
FEED
PUMPS
CONVERTED
LPRO TRAINS
UV
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 26
EXHIBIT 22
Option 4 - Preliminary Site Layout
Marco Island North Water Treatment Plant Expansion Options
4 MGD MF Building
Connection to
Raw Water
Pipeline
MF Building
Expansion to 6 MGD
Filtrate Pump Station
& UV System
Connection to
Existing 16-inch
Concentrate Line
Process Advantages
Reduced stress on brackish aquifer – The dependence on brackish groundwater will be
minimized because the new treatment process doesn’t require the BWRO permeate for
blending to meet finished water quality goals.
Operability: The MF and LPRO units can be shut off and started anytime and are
completely automated. The units can treat varying flows thus facilitates part time
operation. There are minimal continuous treatment chemicals.
Effective treatment for all finished water goals – The MF and LPRO process would
remove all target constituents including sulfate and chloride without the need for
blending.
Expandability: The treatment capacity at the NWTP can be increased to meet future
demands due to the relative small footprint of MF.
Process Limitations
Additional pilot testing – Additional pilot testing should be performed with RO to verify
fouling rate and determine operating protocol including additional pretreatment.
Potential need for in-line coagulation – Additional pilot testing may show that a low
dose of coagulant would be needed to reduce organic fouling of the LPRO membranes.
Expansion at SWTP site – Modifications would be required at the SWTP that may
effectively increase the capacity of the SWTP above 6 mgd. The higher capacity may
require additional staffing.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 27
Concentrate disposal – LPRO concentrate disposal could be an issue. The deep well
injection at the NWTP would be used to dispose the concentrate.
Projected Capital, Operating and Life Cycle Costs
Budgetary capital cost opinions were developed for each of the process train options based
on the design criteria developed during the pilot study. The capital cost opinions include
construction cost opinions in 2009 dollars, typical engineering fees, and a 30 percent
contingency. Exhibit 23 summarizes the capital cost opinion components for each process
train option.
EXHIBIT 23
Capital Cost Opinions of Proposed Process Train Options
Marco Island North Water Treatment Plant Expansion Options
Component Option 1 Option 2 Option 3 Option 4
Total BWRO Modifications - - - $227,000
Total Membrane Filtration $4,575,000 $3,379,000 $3,399,000 $3,379,000
Total Ion Exchange System - $3,013,000 - -
Total Lime Softening - - $3,839,000 -
Total UV System $866,000 $866,000 $866,000 $958,000
Subtotal Construction Cost $5,441,000 $7,258,000 $8,104,000 $4,564,000
Design (8%) $435,000 $581,000 $648,000 $365,000
SDC (5%) $272,000 $363,000 $405,000 $228,000
Verification Pilot Testing - - - $250,000
Subtotal Capital Cost $6,148,000 $8,202,000 $9,157,000 $5,407,000
Contingency (30%) $1,844,000 $2,461,000 $2,747,000 $1,622,000
Total Capital Cost w/ Cont $7,992,000 $10,663,000 $11,904,000 $7,029,000
- Costs are order of magnitude opinions based on typical design values with a +50/-30 level of accuracy
Exhibit 24 summarizes the projected operating costs for the current NWTP facility with UV,
as well as each of the process options. The operating costs do not include labor or
maintenance costs, are based on current Marco Island NWTP unit prices for chemicals and
power, and assume a 100 percent operating factor.
MARCO ISLAND WATER TREATMENT EXPANSION OPTIONS
MARCO NWTP EXPANSION OPTIONS TM - 1-11-10 28
EXHIBIT 24
Projected Operation Cost of Current NWTP and Proposed Process Train Options
Marco Island North Water Treatment Plant Expansion Options
Process Train Chemical
Cost
($/year)
Power
Cost
($/year)
Replacements
& Solids Cost
($/year)
Total
Operating Cost
($/year)
Treated
Water Cost
($/kgal)
Current - LS/GMF/UV $731,300 $840,500 $182,500 $1,754,300 $0.80
Option 1 - Coag/MF/UV $797,600 $513,400 $182,500 $1,493,500 $1.02
Option 2 - MF/IX/UV $165,400 $513,900 $104,400 $783,700 $0.54
Option 3 - LS/MF/UV $930,500 $513,400 $182,500 $1,626,400 $1.11
Option 4 - MF/LPRO/UV $142,400 $583,500 $38,500 $764,400 $0.52
- Operating costs do not include labor or maintenance costs
- Annual operating cost projections based on 100 percent operating factor
- Chemical and power costs are based on current Marco Island NWTP unit prices and may vary over time
Exhibit 25 shows the projected life cycle costs for the different process options assuming a
20-year life cycle and 6 percent interest rate.
EXHIBIT 25
Projected Life Cycle Cost of Process Train Options
Marco Island North Water Treatment Plant Expansion Options
Process Train Operating Cost
($/year)
Capital Cost
(2009$)
Present Worth
(2009 $)
Life Cycle Water Cost
(2009 $)
Option 1 – Coag/MF/UV $1,493,500 $7,992,000 $216,500,000 $1.06
Option 2 - MF/IX/UV $783,700 $10,663,000 $120,100,000 $0.59
Option 3 - LS/MF/UV $1,626,400 $11,904,000 $238,900,000 $1.17
Option 4 - MF/LPRO/UV $764,400 $7,029,000 $113,700,000 $0.56
- Present worth and life cycle amortization based on 20-year life cycle and 6 percent interest rate
- Operating costs do not include labor or maintenance costs
- Annual operating cost projections based on 100 percent operating factor
- Chemical and power costs are based on current Marco Island NWTP unit prices and may vary over time
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 1
TECHNICAL MEMORANDUM
Marco Island Filtration and UV Options Analysis
PREPARED FOR: City of Marco Island
PREPARED BY: CH2M HILL
DATE: April 5, 2010
Executive Summary
The source water quality for the Marco Island North Water Treatment Plant (NWTP) is
degrading because of increased groundwater influence, and because the South Florida
Water Management District (SFMWD) is redirecting additional stormwater into Henderson
Creek. The degrading quality is creating operating challenges and increasing treatment
cost. Changing water quality has also increased the estimated construction cost of the
proposed ultraviolet (UV) disinfection system that was identified as a cost effective
treatment for meeting the upcoming Long-Term 2 Enhanced Surface Water Treatment Rule
(LT2 ESWTR).
The NWTP maintenance cost is increasing because of aging water treatment infrastructure.
Recent inspections have identified major rehabilitation needs of the existing granular media
filters (GMF), Zenon membrane filtration (MF) system, and lime reactor. These
rehabilitation projects will require significant downtime of the NWTP and result in $1.5M in
additional maintenance cost. The maintenance staff anticipates a higher frequency of these
types of rehabilitation projects as the infrastructure continues to age.
CH2M HILL conducted an evaluation of potential treatment rehabilitation/upgrade options
to determine solutions that will improve treatment facility reliability and operability given
the changes in source water quality, as well reduce capital and operating cost over both now
and in the future. Options included combinations of rehabilitation versus replacement of
the existing media filters with a new MF system, rehabilitation versus replacement of the
existing Zenon system, and alternative UV disinfection options. CH2M HILL identified
three primary options including:
1. Rehabilitating the existing filters, lime reactor, and Zenon system, replacing the existing
transfer pumps, and installing UV for full virus, Giardia, and Crypto inactivation
required by the upcoming regulations.
2. Rehabilitating the lime reactor and filters, replacing the Zenon system with a new MF
system, and installing UV for only Giardia and Crypto inactivation, while modifying the
hypochlorite feed system to achieve the required virus inactivation.
3. Rehabilitating the lime reactor, while replacing the existing filters and Zenon system
with a new MF system that also can potentially meet the upcoming Giardia and Crypto
removal requirements.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 2
Recommendation
CH2M HILL recommends that the City replace the existing filters and Zenon system with a
new membrane filtration system as outlined in Option 3. This new membrane filtration
system will provide several benefits including:
Provide the most cost-effective long-term capital and operating cost solution for the
City.
Reduce the money wasted on short-term improvements that have limited or no-long
term benefit.
Improve the finished water quality, operability and reliability of the NWTP process.
Use the best available technology to manage degrading source water quality while
ensuring compliance with upcoming regulations.
The exhibit below shows a summary of the capital and operating costs for the three primary
options.
Additional cost assumption detail is provided in the attached spreadsheets.
EXHIBIT 1
Marco Expansion Options Cost Summary
Item Option 1 Option 2 Option 3 Option 3 (no UV)
Capital Cost with Contingency $4,953,900 $4,118,300 $4,727,500 $4,132,800
Approximate Future Exp Cost $3,400,000 $1,000,000 $1,000,000 $1,000,000
Operating Cost ($/kgal) $0.868 $0.653 $0.641 $0.635
Operating Cost ($/year at 6 mgd) $1,902,000 $1,430,000 $1,403,000 $1,391,000
Background
UV System Cost Impact from Source Water Quality Change
CH2M HILL conducted an initial investigation of ultraviolet light disinfection (UV) for virus
inactivation of lime softened and filtered Marco Lakes water in August 2009 using the
results of the membrane filtration pilot testing conducted in 2008. Pilot testing showed that
a filtered water UV transmittance (UVT) between 92 and 96 percent during July/August,
historically the time of year with the highest source water TOC and therefore anticipated to
have the lowest UVT. Based on this high UVT range, which would result in high UV
efficiency and low UV power consumption, CH2M HILL recommended that the City of
Marco implement UV disinfection in order to comply with both the requirements of the
EPA LT2ESWTR and FDEP “bird rule”, while eliminating the need for the existing 0.5-MG
storage tanks.
Recent changes in water quality in Marco Lakes water quality, stemming from changes in
the natural organic matter content of Henderson Creek water, have reduced North Water
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 3
Treatment Plant (NWTP) filtered water UVT to approximately 70 percent, despite a decrease
in color levels from 35 PCU to 23 PCU.
In response to this water quality change, CH2M HILL conducted jar testing during March
2010 to identify changes to alum and/or lime dosing that could improve the filtered water
UVT. The jar testing results indicate that UVT has some dependence on lime dose (higher
dose improves UVT) and on pH during alum addition (lower pH improves UVT), however
alum dose has minimal impact. In all cases, the best UVT that could be achieved was 76
percent. This compares to the 92-95 percent UVT measured in August 2009. The
significantly lower filtered water UVT has a major impact on UV system design: UV system
footprint, equipment and O&M cost are all estimated to double. UV system construction
cost is expected to increase by at least $600,000.
Filter Rehabilitation
The City is in the initial stages of rehabilitating the existing NWTP lime reactor and media
filters. The Florida Department of Environmental Protection (FDEP) has mandated that the
City make improvements to the structural components of these systems as well as replace
the filter media. These improvements are anticipated to cost $1.2M and are expected to take
up to 2 months to complete.
The existing Zenon membrane filtration system, installed in 1998 and which representing 20
percent of the total filtration capacity at the NWTP, is aging and is showing signs of
imminent failure. To restore structural and performance integrity, a minimum of 50 percent
of the membrane cassettes must be replaced, and the steel tank requires significant
refurbishment or replacement. Estimated cost for repair and/or replacement is a minimum
of $560,000 and must be completed in the near future to maintain the current NWTP
capacity of 6.7 mgd.
The City has explored options for temporary treatment during the anticipated 2-month
shutdown of the lime reactor and filters. A treatment system that can meet current SWTR
regulations without the use of the existing lime softening process is needed. Installing a
membrane filtration system with integrity testing capability that can provide a minimum 3-
log Giardia removal is a cost-effective option that can be implemented for a short period of
time. FDEP acceptance of this kind of direct filtration system is expected when used with a
free chlorine residual in the distribution system to achieve secondary Giardia disinfection
(part of normal annual distribution system maintenance) and blending with RO permeate at
the SWTP to reduce color and hardness. The cost of a temporary membrane filtration
system is estimated at $275,000 including equipment rental, installation, startup and
decommissioning.
Future Membrane Filtration Expansion
The City is planning to expand the NWTP by 4 mgd in 2013 to meet increasing finished
water demand on the island. An expansion evaluation conducted by CH2M HILL in 2007
identified direct filtration of the NWTP Marco Lakes source water using a microfiltration
(MF) or ultrafiltration (UF) as a cost effective expansion option if the filtered water was
transferred to the SWTP and then further treated with reverse osmosis (RO) or blended with
RO permeate from the existing treatment system.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 4
The City and CH2M HILL conducted a membrane filtration pilot study between January
and August of 2008 to identify the feasibility and cost of treating the Marco Island NWTP
source water with membrane filtration. A microfiltration (MF) pilot unit supplied by Pall
Corporation was used for the testing and displayed excellent performance when treating
raw water, in-line coagulated raw water, and lime softened water from the existing full-
scale reactor. Based on the results of the pilot study, the membrane filtration equipment
cost was estimated at $1.4M. After installing a building and other related process
components, the anticipated cost for the expansion was estimated at $7M.
Alternative Approaches
CH2M HILL began to evaluate alternatives for the temporary filtration system needed
during the rehabilitation, as well as the cost feasibility of installing a replacement to the
existing Zenon membrane filtration system. During the evaluation, Pall Corporation
introduced a new 2-mgd pre-packaged MF system with an approximate cost of $600,000.
This new package system, the Aria AP8, represents a significant cost savings over
previously quoted custom systems, and allows for significantly lower cost design and
installation than a custom system.
The City therefore has decided to revisit the current rehabilitation, UV and membrane
filtration expansion plan given the following factors:
Introduction of the lower cost 2-mgd MF pre-packaged skid
The unexpected $1.5M cost for rehabilitation of the media filters and lime softening
reactor.
The recent degradation of the Zenon system and anticipated $600k rehabilitation cost
The unexpected $600k increase in cost of the UV system.
The upcoming planned expansion using membrane filtration
Given these factors, two alternative options have been developed that seek to minimize the
investment in short-term fixes and old equipment and take advantage of recent cost
reduction in membrane filtration to improve the finished water quality, operability and
reliability of the NWTP. The sections below summarize three different approaches to the
current and future expansion of the filtration and UV systems.
Option 1 – Rehabilitate Lime Reactor, Zenon and Media Filters
and Install UV for 4-log Virus Inactivation
Description
This option includes rehabilitating the existing filters, lime reactor and Zenon system. UV
will be installed to achieve the virus, Crypto, and Giardia inactivation required by the
upcoming LT2ESWTR and FDEP bird rule after eliminating the 0.5MG tanks currently used
for virus and Giardia inactivation CT. Rehabilitating the existing media filters and Zenon
system would be adequate given that the new UV system would be installed to meet the
LT2ESWTR.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 5
Improvements / Action Items
1. Rehabilitate existing lime softener and media filters August-September 2010.
2. Meet with FDEP to discuss rehabilitation and ensure approval and permitting of short-
term direct filtration treatment using rental units.
3. Lease LT2 compliant membrane filtration units to allow 2 mgd of production during the
rehabilitation period.
Operate these units in direct filtration mode with upstream alum feed to reduce
color.
Obtain FDEP approval and permit to distribute MF-filtered water in conjunction
with maintaining a free chlorine residual during distribution and blending with RO
permeate at the SWTP.
Obtain FDEP approval and permit to distribute MF-filtered water to achieve 3-log
Giardia removal credit without the need for free chlorine residual or permeate
blending.
Pending FDEP approval, distribute un-softened MF-filtered water from the NWTP
during the rehabilitation.
4. Rehabilitate existing Zenon system to maintain current 6.7 mgd NWTP capacity beyond
the rental period of the MF units.
5. Install UV system for 2-log Virus and 3+ log Giardia and Crypto inactivation to meet
bird rule and LT2 without CT in storage tanks.
6. Install new transfer pumps to allow direct pumping to SWTP and 4MG tank thus
reducing operating cost and allow reallocation of existing 0.5MG tanks to RWPF.
7. Install future MF skids and building when expansion is required.
Potential Issues and Disadvantages
Short-term permitting during rehabilitation
Increased construction and operating cost of UV system to meet 2-log virus inactivation
at lower UVT (minimum 70%).
Money is spent on systems that may only last another 3-5 years. This options would
require ~$3.4M expansion cost in the future for membrane filtration, building, UV,
piping, & SWTP modifications.
Risk of UV non-compliance due to the change in the nature of the Marco Lakes Source
water.
While the 50% measured UV transmittance is similar to the values measured during
the pilot, the existing lime softener is having difficulty achieving UVT values that are
consistently above 70%.
Jar testing shows that achieving UVT above 75% would be difficult with the current
treatment system and modifications to the alum addition (including mixing and pH
adjustment) may be needed.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 6
Validation of UV equipment at UVT below 70% may be required to ensure
continued compliance (units are not currently validated below 70%)
Advantages
Makes full use of existing treatment equipment.
Requires the least amount of engineering design
Defers most of the NWTP expansion cost.
Option 2 – Rehabilitate Media Filters, Replace Zenon, Modify
Chlorination Addition, and Install Smaller UV
Description
This option includes rehabilitating the existing media filters and lime reactor, but replaces
the existing Zenon system with a new LT2-compliant membrane filtration system. The
option also includes relocating the existing chlorination point to allow virus inactivation
with free chlorine post-filters and adding chlorine to the filter backwash to control algae
growth.
Improvements / Action Items
1. Rehabilitate existing lime softener and media filters August-September 2010.
2. Meet with FDEP to discuss rehabilitation and ensure approval of short-term direct
filtration treatment using rental units.
3. Purchase LT2 compliant membrane filtration unit to allow 2 mgd of production during
the rehabilitation period.
Install in a temporary structure until a permanent structure is constructed.
Operate this unit in direct filtration mode with upstream alum feed to reduce color.
Obtain FDEP approval and permit to distribute MF-filtered water in conjunction
with maintaining a free chlorine residual during distribution and blending with RO
permeate at the SWTP.
Obtain FDEP approval and permit to distribute MF-filtered water to achieve 3-log
Giardia removal credit without the need for free chlorine residual or permeate
blending.
Pending FDEP approval, distribute un-softened MF-filtered water from the NWTP
during the rehabilitation.
4. Construct a new membrane filtration building and re-locate rented membrane filtration
package system to a permanent location inside the building.
5. Install UV that is sized for 2.5-log Giardia and Crypto inactivation to meet Long-Term 2
ESWTR requirements.
6. Relocate current hypochlorite injection point to the clearwell, or in the pipeline
downstream of the UV system after exposure of process water to open atmosphere to
meet the requirements of the FDEP bird rule.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 7
7. Relocate the ammonia feed point to a minimum of 30 seconds HRT downstream of the
hypochlorite injection point after achieving the required 2-log virus inactivation.
8. Add hypochlorite to the filter backwash for algae control.
Potential Issues
Need to assess ability to control algae when adding hypochlorite to the surface scrub
system or to the clearwell. If not feasible, addition of backwash pumps may be required.
Relocation of the MF system can increase cost and cause potential logistical issues.
Increases near-term cost needed for new membrane filtration building.
Schedule to install a new MF skid is tight to meet rehabilitation timeframe.
Risk of UV non-compliance due to the change in the nature of the Marco Lakes Source
water.
While the 50% measured UV transmittance is similar to the values measured during
the pilot, the existing lime softener is having difficulty achieving UVT values that are
consistently above 70 percent.
Jar testing shows that UVT above 75% would be difficult to achieve with the current
treatment system and modifications to the alum addition (including mixing and pH
adjustment) may be needed.
Validation of UV equipment at UVT below 70% may be required to ensure
continued compliance (units are not currently validated below 70%).
Advantages
Eliminates operational issues with existing Zenon system by upgrading to newer and
more robust membrane filtration technology.
Eliminates lease cost of equipment that does not provide long-term benefit.
Easier and lower-cost future membrane filtration expansion because new building
would already be installed (~$1M).
Would allow 2 mgd of production without lime softening reactor during future
maintenance by using direct filtration through LT2 compliant membrane system.
Allows consideration of low-pressure UV systems with lower operating cost.
Eliminate 100,000 gpd of blowdown (potable water to waste) by eliminating the Zenon
system with and annual treatment cost of about $60,000.
Operating cost will be lower than Option 1
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 8
Option 3 – Replace Media Filters with Membrane Filtration
Description
This option includes rehabilitating only the lime softening system and then replacing both
the existing media filters and Zenon system with a new LT2-compliant membrane filtration
system. The option also includes installing a new membrane building that is sized for future
expansion. The new MF system has been proven to provide more than the current required
3-log Giardia removal which could potentially eliminate the need for Giardia disinfection
including chlorine contact time and UV (pending FDEP acceptance).
Improvements / Action Items
1. Rehabilitate existing lime softener August-September 2010.
2. Meet with FDEP to discuss rehabilitation and ensure approval of short-term direct
filtration treatment using existing filters and long-term approval of MF for minimum 3-
log Giardia inactivation without secondary disinfection.
3. Operate existing media filters at low loading rate with direct upstream alum feed to
meet summer production requirements.
4. Purchase LT2 compliant 2-mgd membrane filtration skid to replace existing Zenon
system and install in a new membrane building.
Pending FDEP approval, this and future MF units could meet full Giardia removal
credit without the need for chlorine contact time and UV.
5. Provide space for, or if required install UV that is sized for 0.5-log Giardia inactivation to
meet secondary disinfection requirements.
6. Relocate current hypochlorite injection point to MF system feed pipe after exposure of
process water to open atmosphere to meet the requirements of the FDEP bird rule.
7. Relocate the ammonia feed point to a minimum of 30 seconds HRT downstream of the
hypochlorite injection point after achieving the required 2-log virus inactivation.
Potential Issues
Need to verify that FDEP will allow continued operation of media filters without
rehabilitation until after 6.7 mgd of membrane filtration is installed next year
Added engineering needed to work out phasing and expansion to eliminate potential
increased construction cost or future redesign.
Consistent and permitable near-term 6.7 mgd may require 4 MF trains, thus increasing
near-term installed equipment cost.
Increases near-term cost based on design, construction and installation of new
membrane filtration system and building.
Will require a larger MF building for future expansion that will be more challenging to
fit on the NWTP site. Building size can vary from 50’x60’ to 120’x60’ depending on
types of skids, configuration, and layout.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 9
May require common MF feed tank (or feed clearwell) to equalize flow between the
discharge of the lime softening reactor and the feed of the membrane filters. The AP8
skids each have a feed tank that can significantly increase building footprint. Using a
common feed tank may be more cost effective.
Need to verify that the existing lime softener can adequately treat recycled MF
backwash water. Solids that not removed after multiple recycles can accumulate in the
system and eventually impact MF performance. Additional low-cost treatment in the
backwash equalization basins may be needed.
Advantages
Eliminates the urgent need to provide temporary MF system this summer and reduces
total system downtime for rehabilitation.
Would allow NWTP to operate without lime softening reactor during periodic
maintenance.
Would allow ready conversion at NWTP from lime softening to membrane softening by
providing appropriate pretreated water.
Eliminates lease cost of equipment that does not provide long-term benefit.
May eliminate the need for UV provided FDEP approves MF for full Giardia and Crypto
removal credit.
System would be ready for future MF expansion with lowest construction cost and
minimal or no engineering (~$1M).
Gain land of filters, clearwell, transfer pumps, and existing control building.
Lower operating cost than current option.
Reduces operational issues associated with lime reactor upset and high turbidity
carryover into filters. Filtered water turbidity compliance will not be an issue.
Will produce consistently better finished water quality than existing system.
One filtration system that is easier to operate and automate.
Allocate portion of UV design costs to MF design costs.
Eliminates low UV transmittance issue.
Eliminates issues associated with open filters and need to meet FDEP ‘bird rule’.
Eliminates 100,000 gpd of UF reject flow by eliminating the Zenon system with and
annual treatment cost of about $60,000.
Summary of Capital and Operating Costs
The exhibit below summarizes the capital and operating costs for each of the options above.
Additional cost assumption detail is provided in the attached spreadsheets.
MARCO ISLAND FILTRATION AND UV OPTIONS ANALYSIS
MARCO FILTRATION AND UV OPTIONS ANALYSIS 4-5-10 10
EXHIBIT 2
Marco Expansion Options Cost Summary
Item Option 1 Option 2 Option 3 Option 3 (no UV)
Transfer Pumping System $401,600 $401,600 $257,700 $257,700
UV System $1,714,700 $715,300 $495,600 -
Membrane Filtration System $576,500 $1,081,100 $2,746,300 $2,746,300
Total Construction Cost $2,692,800 $2,198,000 $3,499,600 $3,004,000
Design $161,600 $219,800 $350,000 $350,000
SDC $107,700 $87,900 $140,000 $140,000
Lime & Filter Rehab $1,200,000 $1,200,000 $300,000 $300,000
Pall Rental / Installation $275,000 $50,000 - -
Subtotal Capital Cost $4,437,100 $3,755,700 $4,289,600 $3,794,000
Contingency $516,800 $362,600 $437,900 $338,800
Total Capital Cost with
Contingency
$4,953,900 $4,118,300 $4,727,500 $4,132,800
Approximate Future Exp Cost $3,400,000 $1,000,000 $1,000,000 $1,000,000
Operating Cost ($/kgal) $0.868 $0.653 $0.641 $0.635
Operating Cost ($/year at 6 mgd) $1,902,000 $1,430,000 $1,403,000 $1,391,000
Marco Island North Water Treatment
Plant Membrane Filtration
Improvements Project
Prepared for:
Marco Island Utilities
Prepared by:
Naples, FL
December 2010
TECHNICAL MEMORANDUM
Marco Island North Water Treatment Plant Membrane
Filtration Improvements Project Engineering Report
December 2010
TECHNICAL MEMORANDUM
Contents
1. Certifications
2. Marco Island NWTP Membrane Filtration Improvements
Project Overview
3. Marco Island NWTP Membrane Filtration Improvements
Project Water Quality
4. Marco Island NWTP Membrane Filtration System
5. Marco Island NWTP MF Improvements Project Disinfection
Design
6. Marco Island NWTP MF Improvements Project Chemical
Storage and Feed Systems
7. Marco Island NWTP MF Improvements Transfer Pumping
Design
8. Marco Island MF Project Backwash Recovery Basin
Modifications
9. Marco Island MF Improvements Project Electrical and I&C
Design
10. Marco Island MF Improvements Project Engineering Report
Drawings
Certifications
Professional Engineer
The engineering features of the Marco Island North Water Treatment Plant Membrane
Filtration Improvements Engineering Report, dated December 22, 2010, were prepared by,
or reviewed by, a Licensed Professional Engineer in the State of Florida. The information
contained herein the report is true and correct to the best of my knowledge, the report was
prepared in accordance with sound engineering principles.
_______________________
Joseph R. Elarde, P.E.
P.E. License Number: 59309
Process-Mechanical Design
_______________________
Norman E. Anderson, P.E.
P.E. License Number: 71642
Electrical/I&C Design
TECHNICAL MEMORANDUM
2. Marco Island NWTP Membrane Filtration
Improvements Project Overview
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island NWTP Membrane Filtration
Improvements Project Overview
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Introduction
Marco Island Utilities (MIU) owns and operates two water treatment facilities, the North
Water Treatment Plant (NWTP) and the South Water Treatment Plant (SWTP). The NWTP is
an aging 6.7 million gallons per day (mgd) conventional lime softening and filtration facility
that treats surface water from Marco Lakes. The SWTP is a 6.0-mgd reverse osmosis (RO)
facility that desalts brackish water from Mid-Hawthorn Aquifer Wells. Approximately 3
mgd of filtered blend water is transferred from the NWTP to the SWTP to help stabilize the
RO permeate and meet the higher demands on the south side of the island. Exhibit 1 shows
a process flow diagram of the Marco Island water treatment system including both the
NWTP and SWTP.
EXHIBIT 1
Proposed NWTP Site Layout
Marco Island Membrane Filtration Improvements Project Engineering Report
The Marco Island NWTP Membrane Filtration (MF) Improvements Project will improve the
operability, reliability and efficiency of the NWTP while working to meet both current and
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT OVERVIEW
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 2
future anticipated regulations. The project will also prepare the NWTP for future expansion
up to 10 mgd. Exhibit 2 shows an aerial of the NWTP with a summary of the project
components which include:
Install a 6.7 mgd microfiltration system including feed pumps, strainers, backwash
pumps, air system, instrumentation/control, and cleaning system in a newly
constructed building located on the existing NWTP site
Construct a new consolidated chemical storage and feed area for currently used
chemicals (alum, hypochlorite, phosphoric acid, citric acid), as well as a new sodium
hydroxide that will be used for MF cleaning
Relocate existing carbon dioxide and ammonia storage and feed systems to new
chemical storage area
Install new transfer pumps that will send filtered water to the SWTP for blending
Replace existing lime softening basin internal mechanism with a new mechanism of the
same type
Install new yard piping for temporary fill of the existing 4MG tank during construction
that will ultimately be used for permanent blend and 4MG tank fill
Modify existing backwash basin to provide solids settling before new backwash recycle
pumps transfer the recovered water to lime reactor inlet
Add instrumentation and control systems to automate new and existing chemical feed
systems, MF system, and transfer pumps.
Modify disinfection approach to achieve the full required Giardia, cryptosporidium, and
virus inactivation after exposure to air without chloramine contact time.
Remove from service and demolish existing sulfuric acid feed system, granular media
filters, clearwell, transfer pumps, old high service pump station, old control room,
electrical shed, and finished water pipe
Reallocate existing 0.5-MG tanks for use at the Reclaimed Water Production Facility
(RWPF)
Repower existing lime reactor, backwash basin pumps, and solids handling equipment
from new MF building electrical room
The MF Improvements project will simplify the overall process as demonstrated by the
process flow diagrams presented in Exhibit 3. As the diagrams show, the only new
components of the NWTP will be the MF system, transfer pumps, and sodium hydroxide
system used for MF cleaning. Modifications will include a change in disinfection approach
that takes advantage of the enhanced filtration and integrity monitoring of the MF system
and the refurbishing the lime reactor by installing new equipment that is the same as the
existing equipment.
The primary challenge of this project will be obtaining appropriate disinfection credit for the
microfiltration system which has integrity monitoring that is compliant Long-Term 2
Enhanced Surface Water Treatment Rule (LT2ESWTR) requirements. Current Florida
Department of Environmental Protection (FDEP) rules do not address the advanced
removal capabilities of the microfiltration system that have been demonstrated in third-
party validation testing and have been accepted by the United States Environmental
Protection Agency (USEPA) and other state agencies.
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT OVERVIEW
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 3
Section 62-550.817 (2)(b) FAC discusses the Giardia and virus removal and inactivation
requirements for subpart H systems treating surface water. The current language indicates
that “Systems providing reverse osmosis, ultrafiltration, or nanofiltration shall provide
sufficient disinfection to achieve a minimum of 0.5-log Giardia lamblia cyst and 2-log virus
inactivation to supplement membrane filtration treatment.” This language, written before
the LT2ESWTR and the USEPA membrane filtration guidance manual (MFGM), does not
address the use of microfiltration, nor the implementation and adoption of direct integrity
testing to directly and reliably demonstrate that MF systems greater than 4.5-log
Cryptosporidium and Giardia removal by both microfiltration and ultrafiltration membrane
systems. Information on several operating facilities in North America have demonstrated
that these membrane filtration systems can reliably exceed the 3-log Giardia and Crypto
removal requirements of the SWTR and LT2ESWTR. Therefore, MIU is proposing that FDEP
permit the selected microfiltration system for full 3-log Giardia and 3-log Crypto removal in
accordance with the MFGM. This will require a change or an exemption to the current rule
as described in 62-550.817 (2)(b) FAC.
MF has been classified by the USEPA as a ‘best available technology’ (BAT) for meeting the
Cryptosporidium removal requirements of the LT2ESWTR. As such it is also a BAT for
removal of the larger-sized Giardia. Using the proposed design criteria of this project,
following the guidelines of the MFGM and having selected a MF product whose
performance (for Crypto and Giardia removal) has been validated through third-party
testing (e.g., California Department of Public Health certification testing) should provide a
reliable and permitable system. To provide a safety factor with respect to compliance with
LT2ESWTR and SWTR, CH2M HILL proposes to design MF system such that during
operation, it will to achieve >4-log Giardia/Crypto removal 95 percent of the time and >3.5-
log Giardia/Crypto removal 100 percent of the time. The integrity of the MF system with
respect to removal of these pathogens will be demonstrated through continuous indirect
integrity testing and daily direct integrity testing in accordance with chapters 3 and 4 of the
MFGM.
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 4 EXHIBIT 2 NWTP MF Improvements Project Summary Aerial Marco Island Membrane Filtration Improvements Project Engineering Report
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT OVERVIEW MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 5 EXHIBIT 3 NWTP MF Improvements Before/After Improvements Process Flow Diagram Marco Island Membrane Filtration Improvements Project Engineering Report REFURBISHED LIME SOFTENING REACTORMARCO LAKES RAW WATERBLEND TRANSFER PUMPSSodium HypochloriteAmmoniaAlumLime4MG STORAGE TANKHIGH SERVICE PUMPSTO DISTRIBUTION SYSTEMBLEND TO SWTPMEMBRANE FILTRATIONPhosphoric AcidCIP TanksSodium HypochloriteSodium HydroxideCitric AcidLIME SOFTENING REACTORMARCO LAKES RAW WATERGRANULAR MEDIA FILTERSTRANSFER PUMPSSodium HypochloriteAmmoniaAlumLime0.5-MG STORAGE TANKSTRANSFER PUMPS4MG STORAGE TANKHIGH SERVICE PUMPSTO DISTRIBUTION SYSTEMBLEND TO SWTPZENON MEMBRANE FILTRATIONSulfuric AcidCLEARWELLPhosphoric AcidCIP SYSTEMSodium HypochloriteCitric AcidNew Process/PipeModified Process/PipeLEGEND
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT OVERVIEW MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 6 EXHIBIT 4 Upgraded NWTP Detailed Process Flow Diagram Marco Island Membrane Filtration Improvements Project Engineering Report LIME SOFTENING REACTORMARCO LAKES RAW WATERBLEND TRANSFER PUMPSNaOClNH3AlumLime4MG STORAGE TANKHIGH SERVICE PUMPSTO DISTRIBUTION SYSTEMTO SWTPTHICKENERFEED EQUALIZATION TANKFEED PUMPSSTRAINERSMEMBRANE FILTERSLIME SOLIDS BASINBACKWASH RECOVERY BASIN (MODIFIED)BACKWASH RECYCLE PUMPSBACKWASH PUMPSSLUDGE PRESSTRUCKSOLIDS DISPOSALCO2PO4RecycleSupernatentBackwashLimits of ImprovementsCitricNaOHCIP SYSTEMBlowdownRetentateBlowdownTO WWTPCIP WasteNaOClRAW WATER BYPASSNaOClBACKWASH WASTE PUMPS
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 7
MF Project Drivers
New Regulations
The NWTP is a surface water treatment facility whose design and operation must comply
with the requirements of the LT2ESWTR starting in October 2013. MIU wishes to remain
proactive in meeting the potential Cryptosporidium inactivation requirements of this rule,
as well as current Giardia and virus removal/inactivation requirements of the SWTR and
those further mandated by FDEP (i.e., ‘bird rule’). At present, the NWTP achieves the 2-log
virus and 0.5-log Giardia inactivation requirements of the bird rule by using chloramines to
provide sufficient CT in the existing finished water storage tanks. However, MIU desires to
use these tanks to provide more storage at the NWTP and for equalization at the adjacent
Reclaimed Water Production Facility.
FDEP Requirement for Filter Rehabilitation
The FDEP conducted routine inspections of the NWTP in 2009 and identified several old
components that were corroded or deteriorated. Several 40+ year-old structural components
of the existing filters pose a safety risk to operations staff, and other corroded filter
components have begun to impact treated water quality.
FDEP therefore mandated that MIU make improvements to the filters and lime softening
reactor. These improvements are anticipated to cost $1.6M ($1.2M for the filters) and are
expected to take up to 2 months to complete. The NWTP will not be able to produce the
water needed to meet finished water demands during this rehabilitation without a
temporary filtration system that is expected to cost approximately $275,000.
Zenon System Failure
The existing Zenon membrane filtration system, installed in 1998 and which representing 20
percent of the total filtration capacity at the NWTP, is aging and is showing signs of
imminent failure. Currently the system is operating at significantly reduced capacity. To
restore structural and performance integrity, a minimum of 50 percent of the membrane
cassettes must be replaced, and the steel tank requires significant refurbishment or
replacement. Estimated cost for repair and/or replacement is a minimum of $560,000 and
must be completed in the near future to maintain the current NWTP capacity of 6.7 mgd.
Repairing the Zenon system will extend the life of the system by approximately 3 years, but
will not ensure compliance with the upcoming LT2ESWTR.
UV System Cost Impact from Source Water Quality Change
CH2M HILL conducted an initial investigation of UV for disinfection at the NWTP in
August 2009 using the results of the membrane filtration pilot testing conducted in 2008.
Pilot testing showed that UV could meet the new regulations efficiently. CH2M HILL
recommended that MIU implement UV disinfection in order to comply with both the
requirements of the LT2ESWTR and FDEP bird rule.
Recent changes in Marco Lakes water quality prompted CH2M HILL to conduct additional
testing during March 2010 to identify the impact to the proposed UV system and if changes
to existing NWTP treatment could improve UV efficiency. The testing results indicated that
the water quality changes would significantly reduce the UV efficiency and that changes to
NWTP operation would result in little improvement. The lower UV system efficiency would
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT OVERVIEW
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 8
double the UV system footprint and O&M cost and would not meet the FDEP bird rule
without continued use of the 0.5-MG storage tanks. UV system construction cost was
expected to increase by at least $600,000 up to a total of $2.0M.
Backup for the Lime Softening Reactor and Filters During Annual Maintenance
MIU needs a treatment system that can meet current regulations, as well as the LT2ESWTR
during annual maintenance of the lime softening reactor and filters. A new membrane
filtrations system is a cost-effective option that can meet regulations when the lime softening
reactor is down for maintenance and be maintained without reducing system capacity.
Future Membrane Filtration Expansion
MIU is planning to expand the NWTP by 4 mgd in 2013 to meet increasing finished water
demand on the island. An expansion evaluation conducted by CH2M HILL in 2007
identified direct filtration of the NWTP Marco Lakes source water using a membrane
filtration as a cost effective expansion option.
MIU and CH2M HILL conducted a membrane filtration pilot study between January and
August of 2008 to identify the feasibility and cost of treating the Marco Island NWTP source
water with membrane filtration. A MF pilot unit supplied by Pall Corporation was used for
the testing and displayed excellent performance. Based on the results of the pilot study, the
membrane filtration equipment cost was estimated at $1.4M. After installing a building and
other related process components, the anticipated cost for the expansion was estimated at
$7M.
Based on all of these considerations, MIU and CH2M HILL have identified various
processes for meeting finished water treatment goals and the more stringent state and
federal regulations. After a detailed evaluation, membrane filtration followed by the
existing lime softening process has been selected as the preferred treatment that would
provide the best value while meeting all the goals and regulations.
Summary of MF System Design Criteria
Use of MF product whose membrane fiber and module characteristics comply with the
requirements of the LT2ESWTR
Meet the intent of the MFGM with respect to MF system product quality control/quality
assurance testing, direct and indirect integrity testing and MF system design
6.7-mgd minimum filtered water flow rate with one fully redundant MF train
Automated direct integrity testing of each membrane train on a 24-hour basis to verify a
minimum 3.5-log cryptosporidium and 3.5-log Giardia removal that exceeds current
and future requirements
Disinfection of the MF filtrate using free chlorine to meet the FDEP requirement for 2-log
virus inactivation when MF is used following lime softening or 3-log virus inactivation
when MF directly treats Marco Lakes water
Minimum design recovery rate of 95 percent with backwash equalization, treatment and
recycle to the inlet of the lime reactor
Design flux of 65 gfd as established through pilot testing based on direct treatment of
Marco Lakes water (most challenging MF feed water quality)
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT OVERVIEW
MARCO MF PROJECT OVERVIEW REPORT 12-22-10.DOCX 9
Automatic (PLC-controlled) operation of all MF system functions (filtration, backwash,
chemically-enhanced backwash, direct integrity testing and clean-in-place)
On-line laser turbidimeter for continuous, indirect integrity monitoring of filtrate from
each MF train
TECHNICAL MEMORANDUM
3. Marco Island NWTP Membrane Filtration
Improvements Project Water Quality
MARCO MF PROJECT WQ REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island NWTP Membrane Filtration
Improvements Project Water Quality
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Source Water
The NWTP source water comes from the Marco Lakes located approximately 10 miles north
of Marco Island. The source for the Marco Lakes is storm water runoff from adjacent
Henderson Creek with some influence from local groundwater. The majority of the year,
water from Henderson Creek flows into the Marco Lakes through an embankment which
significantly reduces turbidity. However MIU occasionally must open a weir gate between
Henderson Creek and Marco Lakes when lake levels drop and more flow is needed.
MIU also uses Aquifer Storage and Recovery (ASR) wells to store excess Marco Lakes water
during the wet season for use during the dry season. MIU injects filtered Marco Lakes water
into seven Floridan Aquifer wells during the wet season, and then recovers this water
during the dry season. The recovered water is blended with the surface water or used alone
to feed the NWTP in the dry season. The recovered ASR well water is influenced by the
brackish Floridan aquifer groundwater having elevated levels of chloride and sulfate.
Exhibit 1 presents the range of feed water quality. The feed water quality can vary due to
seasonal changes in Marco Lakes as well as the use of recovered water.
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT WATER QUALITY
MARCO MF PROJECT WQ REPORT 12-22-10.DOCX 2
EXHIBIT 1
Marco Lakes Source Water Quality
Marco Island Membrane Filtration Improvements Project Engineering Report
Parameter Marco Lakes Water
Quality Range
Marco Lakes Water
Quality Average
Finished Water
Quality Goal
pH 7.2 – 8.2 7.8 8.8
Temperature (Celsius) 20 – 32 26 -
Chloride (mg/L) 66 – 154 120 < 100
Sulfate (mg/L) 40 – 150 100 < 80
TDS (mg/L) 190 – 600 410 < 400
Total alkalinity (mg/L as CaCO3) 120 – 340 235 > 35
Total hardness (mg/L as CaCO3) 170 – 380 330 100-120
Turbidity (NTU) 0.5 – 21 1.5 < 0.1
TTHM (µg/L) - - <80
HAA5 (µg/L) - - <60
Total organic carbon (mg/L) 9.3 – 17 (14) 14 <10*
Color (PCU) 20 – 70 (35) 35 < 5
* Based on D/DBPR requirement of 30% TOC removal for surface waters with alkalinity greater than 120 mg/L
as CaCO3 and TOC greater than 8 mg/L. Actual TOC removal may be greater depending on selected process.
Finished Water Quality Goals
The treated water after the improvements project must improve upon existing finished
water quality. The finished water quality shall meet current and proposed future regulatory
requirements including FDEP primary and secondary drinking water standards, USEPA
S2DBPR and the LT2ESWTR.
Exhibit 2 presents MIU’s anticipated finished water quality goals based on these regulatory
requirements as well as MIU specific goals for aesthetic-based parameters.
The raw Marco Lakes water is high in color, hardness, and total organic carbon (TOC)
including disinfection byproduct (DBP) precursors. The surface water may also contain
pathogens that require removal or inactivation. The high concentrations of sulfate and
chloride may be contributing to copper corrosion problems in the distribution system on the
north end of the island. The improved treatment process must effectively address these
target constituents to meet the desired water quality goals.
The finished water quality must be stable (non-corrosive) with a pH near 8.8, total alkalinity
above 35 mg/L as CaCO3, and total hardness between 100 to 120 mg/L as CaCO3. The
treatment process should minimize increases in sulfate and chloride, or even reduce them in
order to control copper corrosion.
MARCO ISLAND NWTP MEMBRANE FILTRATION IMPROVEMENTS PROJECT WATER QUALITY
MARCO MF PROJECT WQ REPORT 12-22-10.DOCX 3
The finished water must meet the S2DBPR by achieving 30 percent TOC removal and
maintain a TTHM concentration below 80 g/L and a HAA5 concentration below 60 g/L
at all points within the distribution system.
The finished water must also meet the SWTR and LT2ESWTR by achieving 3-log Giardia, 2-
log Cryptosporidium and 4-log virus removal.
EXHIBIT 2
Finished Water Quality Goals
Marco Island Membrane Filtration Improvements Project Engineering Report
Parameter Point of Compliance Finished Water Quality
Standard
Acceptance Standard Description
Value Units
Plant Flow Rate
(Finished Water)
Total flow from meters
on Individual
membrane trains
6.7 MGD 24-hr average production that meets
Finished Water Quality Standards
Turbidity Membrane filtrate <0.3 NTU 95 percent of samples measured
continuous (recorded every 15 min)
with no measurements at or above
1.0 NTU
Cryptosporidium Membrane filtrate >3.5 log Total inactivation / removal credits
based upon membrane treatment
Giardia >3.5 log Total inactivation / removal credits
based upon membrane treatment
Virus Inactivation Membrane filtrate >4 log Total inactivation credits from
treatment process and primary
disinfectant
TTHM Distribution samples <80 ug/L
HAA5 Distribution samples <60 ug/L
Combined
Chlorine Dose
In Finished Water
Pipeline leaving
NWTP
3.0 to 4.0 mg/L
pH Finished Water
storage outlet to
distribution
8.5 – 8.8 pH units
TECHNICAL MEMORANDUM
4. Marco Island NWTP Membrane Filtration
System
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 1
TECHNICAL MEMORANDUM
Marco Island NWTP Membrane Filtration System
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Background
During the treatment alternatives evaluation phase of this project, Marco Island Utilities
(MIU) identified low-pressure membrane filtration as one of the processes to meet the
current and upcoming federal and state regulations for the NWTP. The membrane filtration
process will meet the requirements of the Florida Department of Environmental Protection
(FDEP) “bird rule” and the US Environmental Protection Agency (USEPA) Long-Term 2
Enhanced Surface Water Treatment Rule (LT2ESWTR). Membranes offer several advantages
over other filtration technologies, with the superior and absolute particle removal barrier a
key consideration in its selection.
A low-pressure membrane filtration process provided by Pall Water Processing Inc. (Pall) of
Cortland, NY was among one of the processes that were piloted at the NWTP. The 8-month
pilot study was conducted in 2008 and the results of the study were summarized in The
Marco Island Pilot Report dated January 6, 2010. During this study, the feasibility of the low-
pressure membrane process in meeting treatment goals was demonstrated. As part of this
study, the operating parameters such as flux, backwash intervals, and chemical cleaning
regimes were also established.
The NWTP source water quality has been degrading because of increased groundwater
influence, and because the South Florida Water Management District is redirecting
additional stormwater into the Henderson Creek. Therefore, low-pressure membrane
filtration process has been selected as the most cost-efficient way to upgrade the plant to
meet treatment and production objectives.
MIU selected a membrane system provided by Pall. Pall will be providing a low-pressure
membrane system with all the necessary ancillary components for the system in addition to
the microfiltration treatment trains. The details of the system will be outlined in this
technical memorandum.
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 2
Membrane Filtration System
The membrane filtration system generally consists of the following major systems:
Membrane Feed Tank
Membrane Feed Pumps
Pre-Filter Strainers
Membrane Filter Racks
Reverse Filtration (RF) System (i.e. backwash)
o RF pumps
o Compressed Air Scour System
Membrane Integirty Testing Air System
Chemical Cleaning System for Clean-in-Place/Enhanced Flux Maintenance (EFM)
A process flow diagram for the NWTP is presented in Exhibit 1that includes the systems
listed above.
EXHIBIT 1
NWTP Process Flow Diagram
Marco Island Membrane Filtration Improvements Project Engineering Report
The raw water feed for the plant will be Marco Lakes which will be pre-treated with the
refurbished lime softening reactor before it is introduced to the Membrane Filtration trains.
Lime softening followed by membrane filtration was selected as the ultimate treatment train
that would provide the best value to MIU while meeting all the finished water treatment
goals of complying with the current federal and state regulations.
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 3
Membrane System Components
The system components are presented in Exhibit 2 below:
EXHIBIT 2
Membrane System Components Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Description Value
Number of membrane trains 4(1) (3 Duty, 1 Standby)
(+ space for 2 additional trains in the
future)
Number of membrane modules populated
per train
72
Number of membrane spaces per train 80
Total number of populated membrane
modules
288 (216 Duty, 72 Standby)
Number of membrane feed pumps 3 (2 Duty, 1 Standby)
Number of pre-filter strainers 3 (2 Duty, 1 Standby)
Pre-filter strainer mesh size 300 µm
Number of RF pumps 2 (1 Duty, 1 Standby)
Air Compressors/Receivers 2 (1 Duty, 1 Standby)
Membrane Cleaning Chemicals Sodium hypochlorite
Sodium hydroxide
Citric acid
CIP/EFM Circulation Pumps 2 (1 Installed, 1 shelf spare)
CIP/EFM Batch Tanks 2 (1 acid, 1 base)
(1) Under normal operation mode all trains will be operational. Maximum flux has been set for
operation with 3 trains to accommodate down time for integrity testing, backwashing, EFMs,
and chemical cleans.
The new membrane system will be located in a new building at the NWTP site next to the
existing Lime Softening sytem. Exhibit 3 presents the new Membrane Treatment Building
where all the main membrane and ancillary systems are located.
Space has been allocated for future equipment including two membrane treatment trains,
one membrane feed pump and one pre-filter strainer.
Finished water will be sent to the 4 million gallon tank for distribution. A portion of the
membrane filtered water will be transferred with one of two centrifugal pumps to the SWTP
for blending with RO permeate before distribution.
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 4 BLEND TRANSFER PUMPS TO SWTP MEMBRANE FEED PUMPS PREFILTER STRAINERS CHEMICAL CLEANING SYSTEM MEMBRANE TREATMENT TRAINS RF PUMPS EXHIBIT 3 Membrane System Layout Plan – New Membrane Treatment Building Marco Island Membrane Filtration Improvements Project Engineering Report
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 5
Basis of Design/Equipment
Membrane Filter Trains
Four membrane trains initially rated for 6.7 million gallons per day net filtration capacity
will be installed. Each train will have space to install 10% more membranes in case filtrate
production can’t be met due to changes in operational conditions such as the raw water
source. The membrane system is sized to account for filtrate usage for backwashes,
chemical cleans, and chemical cleans and down time for integrity testing.
Piping and all ancillary equipment is sized to enable future expansion. The system has been
designed to be able to install two additional trains for an ultimate net filtration capacity of
approximately 10 million gallons per day.
The system is designed based on the parameters set during the 2008 membrane pilot study.
Characteristics of the membrane product and detailed productivity design criteria of the
membrane treatment trains are provided under separate headings in this technical
memorandum.
Membrane Feed Tank
A membrane feed tank will be installed between the membrane filter trains and the existing
Lime Softening Reactor. The tank has a capacity of 15,000 gallons and is provided to
equalize flow from the lime softening process to maintain uniform water quality into the
membrane filters. The membrane feed tank is sized for 3 minutes detention at maximum
flow.
Pre-Filter Straining System
The 300 micron pre-filter strainers are provided with two duty and a spare unit, each
dedicated to a feed pumps. Strainers will automatically backwash based on a timer or
differential pressure. Space for a future unit is provided that will be dedicated to the future
feed pump.
Feed System
Three horizontal split-case pumps (two duty and one spare) are provided. The pumps are
rated for 3,000 gpm each at 120 feet total dynamic head. The membrane feed system is
designed with space for a future pump. The pumps will be installed with variable speed
drives.
Backwash System
Filtrate will be used to flush the membranes during backwashes. Filtrate will be drawn
from the main filtrate header after the membrane treatment trains and pumped by two (one
duty and one spare) centrifugal pumps. The pumps are rated for 640 gpm at 70 feet total
dynamic head. The pumps will be installed with variable speed drives.
Compressed Air System
A compressed air system is also provided for backwashes and integrity testing. One duty
and one spare compressor with a compressed air tank are provided.
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 6
Chemical Cleaning System
A chemical cleaning system is provided for clean-in-places and enhanced flux
maintanances. Two separate tank systemswith chemical feed pumps for acid and
caustic/chlorine are provided. Solutions with chemicals will be made up in separate 7.5-
feet diameter tanks. Each tank is equipment is equipped with 45 kW heaters to increase
cleaning solution temperature for more efficient chemical cleans.
A recirculation pump rated for 240 gpm at 70 feet total dynamic head will be installed to
transfer and recirculate chemical solution. A pump will be kept on shelf as a spare. A drain
pump with a same rated capacity will be provided. Spent chemicals will be drained to a
new lift station that will pump the solution to the sanitary sewer.
Membrane Characteristics
The membrane characteristics are presented in Exhibit 4 below:
EXHIBIT 4
Membrane Characteristics
Marco Island Membrane Filtration Improvements Project Engineering Report
Characteristic Value
Outside membrane area 538 ft2
Fiber Outside Diameter 1.3 mm
Fiber Inside Diameter 0.7 mm
Module length 79 inches
Module diameter 6 inches
Nominal pore size ≤ 0.1 µm
Membrane material Hollow-fiber, monolithic PVDF
Flow direction Outside-in
Filtration Configuration Dead-end, deposition
Maximum allowable chlorine concentration 5,000 mg/L
Maximum allowable caustic concentration 1 N
Maximum allowable acid concentration 1 N
pH operating range 1-10
Temperature operating range 32°F - 104°F
Product Specific Challenge Test: The membrane specified for this project has undergone
Environmental Technology Verification (ETV) testing conducted by the USEPA and NSF
International (NSF). Refer to the Appendix for a copy of the certificate supplied by the
manufacturer.
NSF Certification: Membrane system components are NSF 61 certified. Refer to the
Appendix for a copy of the certificate supplied by the manufacturer.
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 7
Example LRV Calculation: Refer to the Appendix at the end of this technical memorandum
for an example of the LRV calculation method to be used at NWTP.
Considerations of Selecting Parameters in Pressure Decay Test: Refer to Appendix.
Productivity Design Criteria
The productivity design criteria are presented in Exhibit 5 below:
EXHIBIT 5
Productivity Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Criteria Value
Instantaneous flux at minimum design temperature
(all four trains in operation)
45.5 gfd (20°C)
Maximum instantaneous flux (one train out for EFM,
CIP, or Backwash)
60.7 gfd (20°C)
Minimum design recovery 95 %
CIP interval 30 days (minimum)
EFM interval Based on user defined
totalized filter flow interval -
3 days (minimum)
EFM duration 45 minutes
Reverse filtration/air scrub interval Based on user defined
totalized filter flow interval -
30 minutes (expected)
Reverse filtration/air scrub duration 2.5 minutes
Reverse filtration/air scrub water flow 8 gpm/module
Reverse filtration/air scrub air flow 3 scfm/module
Flush water flow rate 8 gpm / module
Flush duration 50 seconds
Average TMP at minimum design temperature 17.2 psi (20°C)
TMP Range (min – max) 4 psi – 40 psi
Maximum inlet pressure 50 psi
On-line service factor 59.7 %
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 8
Membrane System Modes of Operation
There are five basic modes of operation for the membrane system. The following is a
description of the system operation provided by Pall:
1. Forward Filtration (FF): The feed pump draws water from the membrane feed tank and
pumps it through the membrane filters through the feed port at the bottom of the
modules. The filtrate exits the filtrate port at top end of the modules.
2. Reverse Filtration and Air Scrub (RF & AS): As water is filtered, rejected particulate
accumulates on the membrane fiber’s surface. The effect is flow restriction in the
module increasing the transmembrane pressure (TMP.) After a user defined total
filtered flow volume, he module racks will go through a combined reverse filtration (RF)
and air scrub (AS) cycle that backwash the filters. Filtrate is pumped from the reverse
side of the membrane fibers (lumens) at a fixed filtration rate and while air is injected
into the modules on the feed side of the fibers. All discharge during the RF & AS is sent
out the upper drain. The combined water-air flow creates strong turbulent and shearing
force to dislodge dirt deposits on the membrane surface. The filtrate for the RF cycle
will be pumped from the main filtrate header after the membrane trains.The RF ans AS
cycle is anticipated to be automatically initiated every 30 minutes.
3. Reverse Flush (FL): This process follows an AS to flush waste out of the module.
During a FL, the RF pump is used to pump additional filtered water without air through
the fibers and out the upper drain to waste.
4. Enhanced Flux Maintenance (EFM): At a user defined flow volume which is anticipated
to be at least 3 days depending on feed water characteristics, the system will stop while
in forward filtration mode. During the EFM process, the feed side of the system is
drained and filtrate is then pumped from the permeate header to the CIP/EFM tank and
heated via a submerged water heater. Chemical (typically chlorine) is injected into the
heated water and the warm solution is then recirculated for 30 minutes through the
system on the feed side of the filter and back to the CIP/EFM tank. The solution is then
drained and the system is flushed using a standard AS and FL. The EFM procedure
functions to extend the interval between the full chemical clean-in-place.
5. Clean-In-Place (CIP): Approximately once a month, a more thorough chemical cleaning
is required. The CIP is a 2 step process. The first step consists of circulating a 1%
sodium hydroxide and 0.1% sodium hypochlorite solution on the feed side of the
modules for 3 hours. The second step consists of circulating a 2% citric acid solution on
the feed side of the module for 2 hours.
An on-board computer and PLC control the operation of the system. Critical operational
parameters are logged continuously and are recorded automatically on the system
computer’s hard drive. The real-time data is used for operation optimization and
troubleshooting.
Operational Control Parameters
The system includes both direct and continuous indirect membrane integrity testing
methods in accordance with the USEPA Membrane Filtration Guidance Manual. Key
operational control parameters are presented in Exhibit 6 below.
MARCO ISLAND NWTP MEMBRANE FILTRATION SYSTEM
MARCO MF PROJECT MEMBRANE REPORT 12-22-10.DOC 9
EXHIBIT 6
Optional Control Parameters
Marco Island Membrane Filtration Improvements Project Engineering Report
Criteria Value
Direct integrity test method Air pressure-hold, automatic
Minimum direct integrity test duration 5 minutes
Direct integrity test frequency 24 hours
Direct integrity test sensitivity/resolution 4-log/ 3 micron
Direct integrity test pressure > 14.5 psi + static pressure
Direct integrity warning setpoint LRV ≤ 4.0
Direct integrity shutdown setpoint LRV ≤ 3.5
Indirect integrity test method Individual filter permeate turbidity, continuous
(via Hach “FilterTrak 660” laser turbidimeter)
Indirect integrity warning setpoint Filtrate turbidity > 0.1 NTU
Automatically initiate direct integrity test When 2 consecutive, 15 minute filtrate turbidity readings
are > 0.15 NTU
Indirect integrity shutdown setpoint Filtrate turbidity ≥ 0.3 NTU
Operational Performance Criteria
Reverse Filtration – Reverse Filtration/Air Scrub is automatically triggered by a user
configured filtered time interval (or filtration volume) primary setpoint, with a TMP
secondary setpoint. This is anticipated the RL/AS will be initiated approximately every 30-
40 minutes. RF waste (i.e. backwash) and flush (i.e. filter-to-waste) contains no membrane
cleaning chemicals and shall be discharged to the NWTP backwash recovery basins.
Chemical Cleaning –EFMs are automatically triggered by a user-configured TMP setpoint.
Chemical solutions can be heated to increase the effiencies of the cleans. EFMs are
anticipated approximately every 3 days depending on source water characteristics.
CIPs are manually initiated by operations staff and are anticipated approximately once a
month. CIP will target restoring membrane permeability. All CIP spent waste will be sent
directly to sanitary sewer. Water softening is not required for process water.
TECHNICAL MEMORANDUM
5. Marco Island NWTP MF Improvements Project
Disinfection Design
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island NWTP MF Improvements Project
Disinfection Design
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Background
During the treatment alternatives evaluation phase of this project, Marco Island Utilities
(MIU) identified lime softening, low-pressure membrane filtration, and chlorination as the
preferred treatment train to meet the current and upcoming federal and state regulations for
the NWTP. This train will meet the requirements of the Florida Department of
Environmental Protection (FDEP) “bird rule” and the US Environmental Protection Agency
(USEPA) Long-Term 2 Enhanced Surface Water Treatment Rule (LT2ESWTR). Membrane
filtration offers several advantages over other filtration technologies, with the superior and
absolute particle removal barrier a key consideration in its selection. In conjunction with
lime softening and low pressure membranes, chlorine disinfection will be used to meet
disinfection requirements.
Disinfection System
The disinfection system has been dictated by current drinking water regulations. The
regulatory requirements that impact disinfection requirements for the NWTP include:
FDEP rules require 4-log virus inactivation after exposure to air
SWTR requires 3-log Giardia inactivation
ESWTR required 2-log cryptosporidium removal
Virus and Giardia Removal/Inactivation
The Surface Water Treatment Rule (SWTR), promulgated in 1989, seeks to prevent
waterborne diseases caused by viruses, such as Legionella and Giardia lamblia. To reduce
occurrence of these microbes in drinking water, the SWTR requires that water systems filter
and disinfect water from surface water sources, and from groundwater sources under the
direct influence of surface water.
The SWTR includes criteria requiring filtration and procedures for determining whether
filtration and disinfection systems are required. Water treatment plants must achieve at least
a 3 log (99.9 percent) removal or inactivation of Giardia and a 4 log (99.99 percent) removal
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT DISINFECTION DESIGN
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 2
or inactivation of viruses. Removal credit is given to systems that provide adequate
filtration. The remainder of the credit must be achieved through chemical disinfection (that
is, chlorine treatment) that inactivates the microorganism. Florida Department of
Environmental Protection (FDEP) rules have the additional restriction that the 4-log virus
removal/inactivation must occur downstream of any exposure to air.
The SWTR allows a 2.5 log Giardia credit and a 2.0 log virus credit for a well-operated
conventional treatment plant. Exhibit 1 provides a summary of filtration processes, along
with the associated Giardia and virus removal credits granted in the FDEP rules. Additional
disinfection credits must be achieved through chemical disinfection for microorganism
inactivation. To help utilities determine if inactivation requirements are being met, the
SWTR establishes and references “CT Tables” to determine associated chemical disinfection
credits. The CT tables are a function of the water pH, temperature, chlorine dose, and the
type of baffling or short circuit factor.
EXHIBIT 1
Typical Removal Credits for Various Treatment Technologies
Marco Island Membrane Filtration Improvements Project Engineering Report
Process Giardia Removal Virus Removal
Conventional treatment 2.5-log 2.0-log
Direct filtration 2.0-log 1.0-log
Slow sand filtration 2.0-log 2.0-log
Diatomaceous earth filtration 2.0-log 1.0-log
Alternative (membranes, bag filters,
cartridge filters)
Systems must demonstrate the log removal of the alternative filtration
method by pilot study or other means
Cryptosporidium Removal/Inactivation
The Long Term 2 Enhanced SWTR (LT2SWTR) was promulgated in 2006, and builds on
previous surface water treatment regulations. As with previous rules, LT2ESWTR goals
were to improve public health protection through the control of microbial contaminates by
focusing on systems with elevated Cryptosporidium risks, and to prevent significant
increase of microbial risk that might otherwise occur when systems implement the Stage 2
Disinfectant and Disinfection Byproducts (DDBP) Rule.
LT2ESWTR recognizes that systems may require additional protection against
Cryptosporidium, and that such decisions should be made on a system-specific basis.
System source water Cryptosporidium monitoring is required. Monitoring results are used
to classify systems in different categories, or bins, based on Cryptosporidium levels found in
source water. All systems are required to achieve 2-log removal and additional removal
may be required based on the results of source water monitoring. Exhibit 2 provides a
summary of bin classifications and total removal or inactivation requirements based on the
number of cysts found in source water.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT DISINFECTION DESIGN
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 3
EXHIBIT 2
Typical Removal Credits for Various Treatment Technologies
Marco Island Membrane Filtration Improvements Project Engineering Report
Cysts in Source Water (#/L)
Bin Classification
Total Cryptosporidium Treatment
Required
<0.075 Bin 1 2-log
>0.075 and <1.0 Bin 2 3-log
>1.0 and <3.0 Bin 3 4-log
Removal credits for Cryptosporidium are based on the “microbial toolbox” developed by the EPA. The Marco
Island NWTP has performed the necessary Cryptosporidium testing and is currently in Bin 1.
NWTP Disinfection Approach
A general process flow diagram for the NWTP is presented in Exhibit 3.
EXHIBIT 3
NWTP Process Flow Diagram
Marco Island Membrane Filtration Improvements Project Engineering Report
Giardia/Cryptosporidium Removal Design
Microfiltration membranes sieve particles from water based on pore size. Microfiltration
systems have been shown to have log-removal levels for Giardia and cryptosporidium cysts
above 4-log, because the cysts are larger than the membrane pore size. The Appendix
provides validation testing results for the Pall MF system demonstrating greater than 4-log
removal of the smaller Cryptosporidium cyst, as well as regulatory acceptance documents.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT DISINFECTION DESIGN
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 4
Section 62-550.817 (2)(b) FAC discusses the Giardia and virus removal and inactivation
requirements for subpart H systems treating surface water. The current language indicates
that “Systems providing reverse osmosis, ultrafiltration, or nanofiltration shall provide
sufficient disinfection to achieve a minimum of 0.5-log Giardia lamblia cyst and 2-log virus
inactivation to supplement membrane filtration treatment.” This language, written before
the LT2ESWTR and the USEPA membrane filtration guidance manual (MFGM), does not
address the use of microfiltration, nor the implementation and adoption of direct integrity
testing to directly and reliably demonstrate that MF systems greater than 4.5-log
Cryptosporidium and Giardia removal by microfiltration membrane systems. Information
on several operating facilities in North America have demonstrated that membrane
filtration systems can reliably exceed the 3-log Giardia and Crypto removal requirements of
the SWTR and LT2ESWTR. Therefore, MIU is proposing that FDEP permit the selected
microfiltration system for full 3-log Giardia and 3-log Crypto removal in accordance with
the MFGM. This will require a change or an exemption to the current rule as described in
62-550.817 (2)(b) FAC that provides no credit beyond conventional filtration for
microfiltration.
MF has been classified by the USEPA as a ‘best available technology’ (BAT) for meeting the
Cryptosporidium removal requirements of the LT2ESWTR. As such it is also a BAT for
removal of the larger-sized Giardia. Using the proposed design criteria of this project,
following the guidelines of the MFGM and having selected a MF product whose
performance (for Crypto and Giardia removal) has been validated through third-party
testing (e.g., California Department of Public Health certification testing) should provide a
reliable and permitable system. To provide a safety factor with respect to compliance with
LT2ESWTR and SWTR, CH2M HILL proposes to design MF system such that during
operation, it will to achieve >4-log Giardia/Crypto removal 95 percent of the time and >3.5-
log Giardia/Crypto removal 100 percent of the time. The integrity of the MF system with
respect to removal of these pathogens will be demonstrated through continuous indirect
integrity testing and daily direct integrity testing in accordance with chapters 3 and 4 of the
MFGM.
Log reduction value (LRV) is the metric for evaluating membrane performance. LRV is a
theoretical number calculated based on the plant flow, the hydraulic configuration of the
membranes, and the amount of flow that is by-passing the membrane. Feed water may by-
pass the membrane due to breaks in the membrane fibers. LRV is calculated for the
membrane system and reported in the SCADA System. A direct integrity warning point will
be set at a LRV less than or equal to 4.0. A direct integrity shutdown set point will be set at a
LRV less than or equal to 3.5. The proposed NWTP disinfection design is claiming 3.0-log
removal for the membrane system, which lower than the shut down set point.
Virus Removal/Inactivation Design
The membrane system will provide adequate Giardia and Cryptosporidium removal, but
virus inactivation will need to be achieved through multiple barriers. NWTP will receive 2-
log virus removal credit from lime softening plus filtration; the remaining 2-log required for
a total of 4-log removal/inactivation will be through free chlorine chlorination. If bypassing
the lime reactor during normal maintenance, the NWTP can continue to add alum coagulant
to achieve direct filtration which would provide 1-log virus removal per FDEP rules. The
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT DISINFECTION DESIGN
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 5
remaining 3-log inactivation when membrane filtering in-line coagulated would be achieved
by free chlorine contact time.
Virus inactivation is required after lime softening filtration, the last point of the process that
is open to the air, due to the FDEP ‘bird rule.’ The level of inactivation is presented in tables
published by the EPA and is based on CT (the required contact time x concentration of free
chlorine), water temperature, and pH. The required contact time for disinfection has been
evaluated as the time between the chlorine addition and the ammonia addition. Exhibit 4
shows the piping located in the Membrane Facility that was used for disinfection
calculations.
Exhibit 5 summarizes the chlorine disinfection design parameters. The hydraulic retention
time in the pipe between the feed tank and the ammonia injection point is 1.05 minutes
using the shortest flow path displayed in Exhibit 4 and the maximum flow shown in Exhibit
5. This represents the minimum contact time available in the line and given the 1.0 baffling
factor, the minimum T10. The resulting 3.15 CT is adequate to provide the needed 3 mg/L-
min CT for 3-log virus inactivation at the minimum 15C temperature and 3.0 mg/L chlorine
residual at the normal operating pH that is less than 9.0. To ensure continued compliance,
flow through the membrane system will be continuously monitored and a new total
chlorine residual analyzer will be located downstream of the ammonia injection point.
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 6 EXHIBIT 4 NWTP Chlorine Contact Pipe – Shortest Flow Path Inside Membrane Facility Marco Island Membrane Filtration Improvements Project Engineering Report
MARCO MF PROJECT DISINFECTION REPORT 12-22-10.DOCX 7
EXHIBIT 5
Disinfection Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Criteria Value
Maximum Flow 7.2 MGD (6.7 mgd at 95% recovery)
Baffling Factor 1.0 (pipe flow assumed to be plug flow)
Pipe diameter Feed/filtrate headers: 20 inches
Pump suction/discharge: 16 inches
Membrane skid piping: 8 inches
Pipe Length As shown in Exhibit 4
Minimum T10 (from discharge of feed tank to ammonia
addition point at maximum flow)
1.05 minutes
Temperature 15C to 32C
pH 8.5 to 8.8
Targeted Residual >3.0 mg/L of free chlorine
CT 3.15 mg-min/L
Virus Inactivation at 20C and pH 6-9 3- log
Exhibit 6 presents a summary of the proposed disinfection credits received through each
process:
EXHIBIT 6
Disinfection Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Treatment Process Virus Inactivation Giardia Inactivation Cryptosporidium
Inactivation
Lime Softening Reactor 2-log1 - -
Membrane Filtration 3-log 3-log
Free Chlorine Disinfection 3-log2 - -
Total Inactivation 5-log 3-log 3-log
Required Inactivation 4-log 3-log 2-log
(1) 2-log removal provided for Lime Softening in conjunction with Filtration process.
(2) Based on free chlorine residual of 3 mg/L, 15C, 6-9 pH
As Exhibit 6 demonstrates, the current design meets the disinfection requirements of 4-log
virus removal/inactivation, 3-log Giardia removal, and 2-log Cryptosporidium removal.
Chlorine will be dosed as sodium hypochlorite. The bulk storage tanks and the feed pumps
will be relocated as part of this upgrade. For more information on the chemical system, see
Marco Island NWTP MF Improvements Project Chemical Storage and Feed Systems Technical
Memorandum, December 2010.
TECHNICAL MEMORANDUM
6. Marco Island NWTP MF Improvements Project
Chemical Storage and Feed Systems
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island NWTP MF Improvements Project
Chemical Storage and Feed Systems
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Introduction
The existing chemical storage and feed systems at the Marco Island North Water Treatment
Plant (NWTP) are located in various locations around the WTP site and are manually
controlled. Many of these chemical systems must be relocated to make room for the new
membrane filtration (MF) building, as well as to move them from future demolition
locations. The NWTP MF improvements project includes constructing a new bulk chemical
and storage area that will serve to consolidate all of the new and existing chemicals on the
NWTP site. The benefits of centralizing the chemical bulk storage and feed systems include
the following:
Simplify chemical delivery by creating one fill station in an easily accessed location
Improve operations by automating chemical feed, adding SCADA monitoring of tank
levels, and centralizing chemicals near the treatment facilities for easy inspection
Promote safety by eliminating tote/drum handling, providing more accessible
eyewash/safety shower stations, improving lighting, and improved bulk tank
protection/containment
The chemical system improvements associated with this project fall into the following
categories:
Relocation of bulk storage and feed systems (carbon dioxide, alum, sodium
hypochlorite, phosphoric acid, citric acid)
Relocation of application point (ammonia, sodium hypochlorite, citric acid, phosphoric
acid)
New chemical associated with MF cleaning processes (sodium hydroxide)
The new and relocated chemical systems at the NWTP and their primary uses are listed in
Exhibit 1.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 2
EXHIBIT 1
New and Existing NWTP Treatment Chemicals
Marco Island Membrane Filtration Improvements Project Engineering Report
Aluminum sulfate (Alum) (47%) Raw water coagulation for organics removal (relocated storage and feed)
Ammonia – anhydrous (100%) Chloramine residual (relocated application point)
Carbon dioxide (100%) Recarbonation and post-lime pH adjustment (relocated storage and feed)
Citric acid (50%) MF cleaning (relocated storage and feed)
Lime (100%) Softening
Phosphoric acid (75%) Finished water corrosion control (relocated storage and feed)
Sodium hydroxide (50%) MF cleaning (new)
Sodium hypochlorite (12%) Finished water disinfection and MF cleaning (relocated storage and feed)
The following sections describe the design criteria of the new storage and feed systems, as
well as the relocation of existing storage, feed, and chemical application points. The
following sections also describe the new chemical feed control system and process
monitoring.
Chemical Descriptions
EXHIBIT 2
New and Existing NWTP Treatment Chemicals
Marco Island Membrane Filtration Improvements Project Engineering Report
Chemical Chemical Formula Specific Gravity Bulk Concentration
Alum Al2(SO4)3 1.335 47.0%
Ammonia NH3 1.0 100%
Carbon Dioxide CO2 (H2CO3) 1.0 100%
Citric Acid C6H8O7 1.24 50.0%
Lime CaO 2.3 100%
Sodium Hydroxide NaOH 1.53 50.0%
Phosphoric Acid H3PO4 (PO4) 1.70 75.0%
Sodium Hypochlorite NaOCl 1.18 12.0%
The sections below describe each of the chemicals used at the NWTP.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 3
Citric Acid
Citric acid is a weak organic acid. It is the most frequently used acid in membrane cleaning,
since it is less hazardous than mineral acids such as hydrochloric or sulfuric acid. The acid
works well on inorganic fouling contaminates and acts as a chelating agent.
Sodium Hydroxide
Sodium hydroxide is a reactive chemical used to increase the pH of the MF CIP cleaning
solution to higher than pH 12.
The reactivity of sodium hydroxide requires special materials for storage tanks (fiberglass
reinforced plastic resin such as Derakane 411), piping, feed pumps and instrumentation. In
the 50 percent concentration form, sodium hydroxide tanks and feed lines should be
equipped with heat tracing and insulation to maintain acceptable temperature ranges for the
chemical. Sodium hydroxide also requires special building construction and safety
equipment including chemical containment, fire sprinklers, chemical suits, and safety
showers.
Phosphoric Acid (Orthophosphate)
Treated water is typically aggressive (tendency to dissolve calcium carbonate) and must be
conditioned prior to being introduced into the distribution system to prevent corrosion of
piping. Orthophosphate is one method of corrosion control that promotes the formation of
calcium phosphate protective scale on distribution system piping. Orthophosphate has also
been proven to reduce lead, copper and some iron corrosion in distribution systems
The conversion of the orthophosphate species in the water between H3PO4 to H2PO4- and
HPO4-2 provides some additional buffering capacity to the finished water to stabilize pH.
Orthophosphate is typically added in the form of phosphoric acid, which is a low-cost
alternative to proprietary forms.
The reactivity of phosphoric acid requires special materials for storage tanks, piping, feed
pumps and instrumentation. Phosphoric acid also requires special building construction
and safety equipment including chemical containment, fire sprinklers, chemical suits, and
safety showers.
Sodium Hypochlorite
Sodium hypochlorite is a reactive chemical used to provide residual disinfection inside the
distribution system and is typically available with an active concentration between 5 and 15
percent, 12 percent solution being the most common. In finished water treatment, when
sodium hypochlorite is added to the water, two substances form, hypochlorous acid and the
less active hypochlorite ions. Water pH determines which form is more predominant.
Sodium hypochlorite is highly unstable and decomposes slowly over time into chlorine gas,
oxygen gas and sodium chlorate. The reaction speeds up at temperatures above 40 degrees
Fahrenheit. Sodium hypochlorite should not be stored for more than 30 days and it should
be kept in a cool, dark and dry area.
The reactivity of sodium hypochlorite requires special materials for storage tanks, piping,
feed pumps and instrumentation. Sodium hypochlorite also requires special building
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 4
construction and safety equipment including chemical containment, fire sprinklers,
chemical suits, and safety showers.
Treatment Process Description
Exhibit 3 shows the existing process flow diagram with current chemical application points,
as well as the process flow diagram after the installation of the new MF system. The
chemical application points will remain the same or will be slightly modified as described
below.
Alum, lime and carbon dioxide application points will remain unchanged.
Sodium hypochlorite will continue to be added downstream of the lime softening
reactor, but the application point will be moved to just upstream of the membrane feed
tanks. This will allow credit for virus inactivation and comply with the FEDP ‘bird rule’,
while reducing contact time that can increase DBP formation.
The Ammonia application point will be moved downstream of the new membrane
filters to provide free chlorine contact time for virus disinfection. The residence time in
the membrane filters is much shorter than the existing granular media filers, which
allows the ammonia to be added downstream of the filters without increasing DBP
formation.
Phosphoric acid will be added downstream of the new membrane filters, which is
similar to its current application point.
The new membrane system will continue to use hypochlorite and citric acid during
cleaning cycles.
Sodium hydroxide will be added to the new MF system cleaning process.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 5
EXHIBIT 3
NWTP Process Flow Diagram – Chemical Applications Points
Marco Island Membrane Filtration Improvements Project Engineering Report
LIME SOFTENING
REACTOR
MARCO
LAKES RAW
WATER
SAND FILTERS TRANSFER
PUMPS
Sodium
Hypochlorite
Ammonia
Alum Lime
0.5-MG
STORAGE
TANKS
TRANSFER
PUMPS
4MG STORAGE
TANK
HIGH
SERVICE
PUMPS
TO
DISTRIBUTION
SYSTEM
TO
SWTP
MEMBRANE
FILTRATION
Phosphoric
Acid
LIME SOFTENING
REACTOR
MARCO
LAKES RAW
WATER
BLEND
TRANSFER
PUMPS
Sodium
Hypochlorite
Ammonia
Alum Lime
4MG STORAGE
TANK
HIGH
SERVICE
PUMPS
TO
DISTRIBUTION
SYSTEM
TO
SWTP
MEMBRANE
FILTRATION
Phosphoric
Acid
CIP Tanks
Sodium Hypochlorite
Sodium Hydroxide
Citric Acid
Sodium Hypochlorite
Citric Acid
CIP PROCESS
Carbon
Dioxide
Carbon
Dioxide
EXISTING FACILITY
IMPROVED FACILITY
FEED
TANK
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 6
Chemical Systems Locations
Exhibit 4 shows the improved NWTP site plan including the locations of the new MF
building, chemical bulk storage and feed area, as well as the new and existing chemical
application points.
EXHIBIT 4
NWTP Site Layout – Bulk Chemical Storage Area, Piping and Outside Chemical Application Points
Marco Island Membrane Filtration Improvements Project Engineering Report
A new bulk chemical area will be constructed. This area will house, the existing CO2 and
Ammonia gas storage tanks as well as the sodium hypochlorite, the sodium hydroxide, the
citric acid, the phosporic acid and the alum tanks. The new bulk chemical storage area will
house bulk tanks and metering pump skids. The area will be covered to protect UV
degredation of tanks. The bulk tanks will be double-walled HDPE tanks. Secondary
containment will be provided by concrete curbs/walls which will be partitioned to separate
acidic and alkali chemicals. A new centralized chemical fill station will be provided with
curb containment for the occurrence of spills during filling. Chemical delivery tank trucks
will be able to pull up to the fill station and use ‘quick connect’ couplings to fill the bulk
tanks from one location.
Exhibit 5 shows the MF building layout including the new chemical piping runs and
chemical application points.
LIME REACTORMEMBRANE FILTRATION BUILDING
EXISTING FILTERS
EXISTING
4MG TANK
LIME
SILO
Relocated CO2
System
New Chemical
Fill Station
Existing Ammonia
Tank and Feed
Relocated Alum
SystemRelocated
Hypochlorite System Relocated
Phosphoric Acid
SystemNew Caustic
System Relocated Citric
Acid System
New Chemical
Lines
Carbon Dioxide Feed
Point (existing)
Alum Feed Point
(existing)
Hypochlorite Feed
Point (new – raw)
Hypochlorite Feed Point
(new – softened water))
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 7
EXHIBIT 5
MF Building Layout – Chemical Piping and Application Points
Marco Island Membrane Filtration Improvements Project Engineering Report
Inside the MF building, chemical lines will be transitioned from the conduit bank in a sump
and routed up the wall and overhead using trapeze-type hangers/supports supported off
the roof trusses. The CO2 line will be routed over to the relocated CO2 feed panel. There
are two application points (ammonia and phosphoric acid) at the top of the piping gallery
for the MF equipment. There are three application points (sodium hypochlorite, caustic,
and citric acid) at the CIP area. Three additional chemical lines (two sodium hypochlorite
and one alum) will be routed over to another transition sump located in the compressor
room. These three lines will then be routed underground to their respective application
points as shown in Exhibit 4.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 8
Chemical System Design Criteria
Exhibit 6 shows the design criteria for the new chemical storage, feed, chemical piping and
injection points for the chemicals used in the treatment process. General criteria for storage,
feed, transfer lines, and injection points are described in the sections below.
Bulk Chemical Storage
The bulk chemical storage was designed to meet the following general criteria.
Minimum 30-days of storage at average flow and dose
Minimum capacity to allow a full truckload of chemical with 20 percent excess capacity
Double-walled tanks provide primary containment
Secondary containment is provided by concrete curbs that divide the storage area into
two sections each with compatible alkali, or acidic chemicals
Day tanks are provided for primary treatment process chemicals that do not have on-
line residual feedback to indicate overfeed
Day tanks are sized for 26 hours of capacity at maximum flow and dose
Canopy cover provided to minimize UV exposure to chemical storage tanks.
Chemical Feed Pumps
The chemical feed pumps are designed to meet the following general criteria:
All chemical feed pumps are skid-mounted with isolation valves, pressure regulator
valves, pressure relief valves, gauges, and calibration columns.
Primary process chemical metering pumps are positive displacement type solenoid
diaphragm metering pumps with remote adjustable speed control and manual
adjustable stroke length.
Transfer pumps used for chemical cleaning makeup (sodium hydroxide, sodium
hypochlorite, & citric acid) are high-capacity air-driven positive displacement
diaphragm pumps.
Chemical Feed Lines
The chemical feed lines were designed to meet the following general criteria:
Liquid chemicals used HDPE tubing in a rigid PVC carrier pipe.
Gas lines (CO2 and ammonia) will be stainless steel tubing.
All liquid chemical tubing is contained in 2-inch PVC carrier pipes with minimal bends
and fittings.
All chemical feed lines are routed together from the bulk storage area to the new MF
building in a concrete-encased conduit bank buried approximately 18-inches below
grade.
Chemical lines will be routed overhead inside the MF Building using trapeze-type
hangers/supports from the roof trusses.
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 9
EXHIBIT 6
Treatment Process Chemical Storage and Feed Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Parameter Sodium Hypochlorite
Criteria
Phosphoric Acid
Criteria
Aluminum Sulfate
Criteria
Process Criteria
Dose (min/ avg/ max) (mg/L) 4.0/ 7.0/ 10.0 0.2 /0.5 /1.0 5.0 /7.0 /20.0
Process Flow (min/ avg/ max)
(mgd)
2.8/ 6.0/ 6.7 2.8/ 6.0/ 6.7 3.0 /6.3 /7.2
Application Points Lime Softened Water /
Raw Water
Filtered Water Raw Water
Chemical Feed
Number (duty + standby) 2+1 1+1 1+1
Metering Pump Type Solenoid Diaphragm Solenoid Diaphragm Solenoid Diaphragm
Metering Pump Capacity (gph) 21.2 0.24 9.6
Meeting Pump Turndown 6.3 to 1 12.6 to 1 10.1 to 1
Wetted Materials of Construction PVC PVC PVC
Metering Pump Control Remote speed /
manual stroke
Remote speed /
manual stroke
Remote speed /
manual stroke
Bulk Storage Tanks
Type Vertical Double-Wall Vertical Double-Wall Vertical Double-Wall
Materials of Construction HDPE HDPE HDPE
30 Days at Average Dose (gallons) 8,750 71 2,100
Truckload + 20% 5,800 4,100 5,200
Bulk Storage Volume (gallons) 8,700 4,500 4,500
Capacity at Avg. Flow/Dose (days) 30 1,913 64
Day Tanks
Type - Vertical Double-Wall Vertical Double-Wall
Materials of Construction - HDPE HDPE
Volume (gallons) - 10 300
Chemical Containment
Primary Double-walled tanks
and tubing carrier
pipes
Double-walled tanks
and tubing carrier
pipes
Double-walled tanks
and tubing carrier
pipes
Secondary Concrete curbs Concrete curbs Concrete curbs
Sizing Shared alkali
secondary
containment area
Shared acidic
secondary
containment area
Shared acidic
secondary
containment area
MARCO ISLAND NWTP MF IMPROVEMENTS PROJECT CHEMICAL STORAGE AND FEED SYSTEMS
MARCO MF PROJECT CHEMICAL REPORT 12-22-10.DOCX 10
EXHIBIT 6
Treatment Process Chemical Storage and Feed Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Parameter Sodium Hypochlorite
Criteria
Phosphoric Acid
Criteria
Aluminum Sulfate
Criteria
7,100 gallons 7,800 gallons 7,800 gallons
Chemical Lines
Type Tubing Tubing Tubing
Diameter (inches) 1/2 1/2 1/2
Material of Construction PVC PVC PVC
Velocity (average) 0.6 fps < 0.1 fps 0.3 fps
Containment 2-inch PVC Carrier
Pipe
2-inch PVC Carrier
Pipe
2-inch PVC Carrier
Pipe
TECHNICAL MEMORANDUM
7. Marco Island NWTP MF Improvements Transfer
Pumping Design
MARCO MF PROJECT TRANSFER PUMP REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island NWTP MF Improvements Transfer
Pumping Design
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Background
Increasing well salinity is reducing the reliability of the RO process at the South Water
Treatment Plant (SWTP) and if not carefully managed may ultimately reduce the current 6
mgd capacity. In order to preserve the existing brackish resource for peak day demands,
Marco Island Utilities has incorporated expanded surface water treatment into its 10-year
water resources and treatment plan. Part of this plan includes increasing the capacity of the
treated surface water that can be transferred from the NWTP to the SWTP.
The ongoing Marco Island South Water Treatment Plant Tank project includes switching the
use of the existing 12-inch blend line and the 16-inch concentrate line that run between the
NWTP and SWTP. Once converted, the larger 16-inch blend line will have the expanded
capacity to transfer more than 5 mgd of treated surface water from the NWTP to the SWTP
for blending with RO permeate. It should be noted that the 16-inch and 12-inch pipelines
have no existing connections to the existing distribution system.
The existing transfer pumps are aging converted higher service pumps that are maintenance
intensive and inefficient for the blend transfer operation. Therefore this project includes
adding new transfer pumps to the MF building that are sized for the 2-5 mgd of design
blend flow. The new transfer pumps will be constructed within the new membrane filtration
building and will be sized based on the flow capacity of the new 16-inch blend water main
and the new system hydraulic head between the NWTP and SWTP. Variable frequency
drives (VFDs) will be provided with new transfer pumps for flow control flexibility to the
SWTP.
Transfer Pump Design
The new transfer pump design is to install two transfer pumps (1 duty & 1 standby) within
the new membrane filtration building in-line downstream of the new membrane filtration
trains. The transfer pumps will discharge into a new 16-inch blend water main that will
convey water from the membrane filtration facility to an existing connection point with the
16-inch blend water main to the SWTP. The connection point is near the intersection of E.
Elkcam Cir. and Windward Dr. The initial membrane filtration facility configuration will
vary slightly from the proposed future configuration. In the initial configuration, the suction
will be from the filtrate header which will be hydraulically linked to the existing 4-MG
ground storage tank fill stand pipe. In the future configuration, the membrane filtration
MARCO ISLAND NWTP MF IMPROVEMENTS TRANSFER PUMPING DESIGN
MARCO MF PROJECT TRANSFER PUMP REPORT 12-22-10.DOCX 2
trains will be operated from two separate feed water supplies – Lime Softened Water & Raw
Water. The membrane filtration trains will then be valved to separate the feed and filtrate
headers based water supply source. The transfer pumps will be downstream of the raw
water membrane filtration trains which will no longer be hydraulically linked to the existing
4-MG ground storage tank. The pump suction will be from the raw water filtrate header
which will have a residual pressure of approximately 20 feet (8.7 psi). This filtrate residual
pressure will be controlled by the membrane filtration feed pumps.
Currently, the existing NWTP high service pumps discharge to the 12-inch blend water
main to the SWTP and to two water mains (one 12-inch and one 16-inch) that leave the
NWTP along Windward Drive, connecting to the distribution system near the intersection
of Windward Drive and Elkcam Circle. These existing pumps will remain in service
throughout the construction of the new membrane filtration facility.
New Transfer Pump Selection
The basis of design of the new SWTP transfer pumps is as follows:
The maximum pump size shall be based on the available capacity in the existing 16-inch
blend water main. The maximum practical pumping velocity in the 16-inch pipeline is 6
feet per second, therefore the maximum recommended pumping rate is 5.5 MGD (3,800
gpm)
The pumps will be sized for both initial and future membrane filtration configurations.
A high head and low head scenario will also be considered for each configuration. The
high head scenario is based on the SWTP RO train in operation and blending with the
NWTP blend water. The low head scenario assumes the RO trains are off. The selected
pump will be evaluated under initial/low-head, initial/high-head, future/low head,
and future/high-head conditions as described below.
The pump’s best efficiency point (BEP) shall be between of the low-head and high head
operating points.
The selected pump will be evaluated under initial/low-head, initial/high-head, future/low
head, and future/high-head conditions as described below.
The piping system from the new transfer pumps to the SWTP was modeled using a
hydraulic modeling program (AFT Fathom) to determine system head conditions at
initial/low-head, initial/high-head, future/low-head, and future/high-head conditions.
The system curves for each of the four scenarios are presented in the chart below. A
Peerless horizontal split case model 8AE15 with a 12.32” impeller diameter is
recommended. This pump’s 100% and 50% speed curves are also shown in Exhibit 1.
The fundamental control strategy for SWTP blend water transfer service is to operate the
pumps to maintain consistent RO blending at the SWTP. Flow signals from the SWTP RO
system will be used to modulate the speed of the operating pumps using the motor VFDs.
MARCO ISLAND NWTP MF IMPROVEMENTS TRANSFER PUMPING DESIGN
MARCO MF PROJECT TRANSFER PUMP REPORT 12-22-10.DOCX 3
EXHIBIT 1
Transfer Pump Curves and Blend Line System Curve
Marco Island Membrane Filtration Improvements Project Engineering Report
EXHIBIT 2
Transfer Pumping Scenarios
Marco Island Membrane Filtration Improvements Project Engineering Report
Scenario # Peerless Pump Conditions Model Flow (gpm) Model TDH
(ft)
1 8AE15 – 100% speed Initial/low head 3,500 110
2 8AE15 – 100% speed Initial/high head 3,360 114
3 8AE15 – 100% speed Future/low head 3,360 114
4 8AE15 – 100% speed Future/high head 3,230 118
5 8AE15 – 50% speed Initial/low head 1,830 27
6 8AE15 – 50% speed Initial/high head 1,650 24
7 8AE15 – 50% speed Future/low head 1,590 30
8 8AE15 – 50% speed Future/high head 1,380 33
MARCO ISLAND NWTP MF IMPROVEMENTS TRANSFER PUMPING DESIGN
MARCO MF PROJECT TRANSFER PUMP REPORT 12-22-10.DOCX 4
EXHIBIT 3
Transfer Pumping Design Criteria
Marco Island Membrane Filtration Improvements Project Engineering Report
Criteria Value
Type Horizontal Split-Case Centrifugak
Size 8
Number of pumps 2 (1 Duty & 1 Standby)
Capacity MAX - 3,500 gpm at 110 feet
MIN - 1,380 gpm at 33 feet
HP 125
Motor 1800 RPM, TEFC enclosure
Drive Variable speed
TECHNICAL MEMORANDUM
8. Marco Island MF Project Backwash Recovery
Basin Modifications
MARCO MF PROJECT BACKWASH REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island MF Project Backwash Recovery Basin
Modifications
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Introduction
The Marco Island North Water Treatment Plant (NWTP) currently uses granular media and
Zenon filters that intermittently backwash to remove solids from the filters. Approximately
3-5 percent of the total feed flow to the NWTP is used for backwash. To minimize waste, this
water is collected in a backwash recovery basin that equalizes the flow before it is pumped
back to the inlet of the lime softening reactor.
The new membrane filtration (MF) process operates similarly to the existing filters.
Approximately 3-5 percent of backwash will be generated that needs to be equalized and
recycled to the inlet of the lime reactor. However, the membrane filters are more efficient
than the existing filters at removing solids. To avoid concentrating ultra-fine solids in the
NWTP previously not removed by the filters and that may not be removed by the lime
reactor, the exiting backwash recovery basin must not only equalize flow, but also provide
additional solids removal and the ability to occasionally blow down accumulated solids.
This section describes the existing backwash recovery basins, testing conducted to
determine the needed treatment of the MF backwash waste, and the proposed modifications
to the existing basins.
Existing Backwash Recovery Basins
The Marco NWTP currently has a backwash recovery basin that equalizes backwash flow
before pumping to the head of the lime reactor. Exhibit 1 shows a schematic of the existing
concrete backwash recovery basin. The basin currently has a single backwash equalization
cell, an existing lime sludge holding cell, a thickener overflow cell, and an emergency
overflow cell. All backwash enters and exits the backwash equalization cell on a normal
basis. In the event of a high level in the equalization cell, water will overflow into the
emergency overflow cell where another pump will recycle water to the inlet of the lime
reactor. The thickener overflow and lime sludge holding cells operate independently of the
backwash system.
MARCO ISLAND MF PROJECT BACKWASH RECOVERY BASIN MODIFICATIONS
MARCO MF PROJECT BACKWASH REPORT 12-22-10.DOCX 2
EXHIBIT 1
Existing Backwash Recovery Basin
Marco Island NWTP Membrane Filtration Improvements Project Engineering Report
MF Backwash Treatment Requirements
The solids suspended in the MF backwash water require adequate time in an undisturbed
settling zone to reduce turbidity before recycle to the head of the lime reactor. The single
open cell currently used for backwash equalization and pumping will not work for this
purpose because the inlet flow mixes the solids in the basin and the backwash recycle pump
from the lowest point of the basin.
To help evaluate the design criteria for solids settling and propose modifications to the
existing backwash pond, a settling rate test was performed at the plant site using a 2” Pall
MF module. The Pall MF module helped mimic the actual full scale performance of MF
filtration and generation of backwash waste. Sufficient backwash volume was collected by
running the Pall module with lime softened feed water. The backwash was allowed to settle
in a jar for three hours. The turbidity of the top portion of the jar was recorded every 30
minutes. The settling test results shown in Exhibit 2 demonstrate that most of the solids
settling occur within the first 60-120 minutes as the turbidity drops from 8.3 NTU down to
between 1.2 and 1.6 NTU. After this time, there is little improvement in the turbidity.
Therefore the backwash basin must provide at least 60 minutes of undistributed settling
time and ideally more than 120 minutes.
MARCO ISLAND MF PROJECT BACKWASH RECOVERY BASIN MODIFICATIONS
MARCO MF PROJECT BACKWASH REPORT 12-22-10.DOCX 3
EXHIBIT 2
Backwash Settling Characteristics
Marco Island NWTP Membrane Filtration Improvements Project Engineering Report
Time (minutes) Backwash Water Turbidity (NTU)
0 8.33
30 2.07
60 1.60
90 1.47
120 1.19
150 1.13
180 1.16
Backwash Basin Modifications
The existing backwash recovery basin must be modified to meet the following goals:
Equalize backwash flows in a cell that is separate from a settling cell
Provide at least 60 minutes of undisturbed settling time at maximum flow
Maintain a relatively constant level in the settling zone
Pump from a separate basin that has clarified overflow water
Provide a way to occasionally purge solids from the equalization/settling cells
Exhibit 3 shows the proposed modifications to the existing backwash basin that will meet
the goals outlined above. The existing equalization cell will be converted into separate surge
and settling zones, while the emergency overflow cell will be converted into a pumping
zone.
MARCO ISLAND MF PROJECT BACKWASH RECOVERY BASIN MODIFICATIONS
MARCO MF PROJECT BACKWASH REPORT 12-22-10.DOCX 4
EXHIBIT 3
Backwash Basin Modifications
Marco Island NWTP Membrane Filtration Improvements Project Engineering Report
Key modifications to the backwash pond
Reinforced concrete wall
The reinforced concrete wall will divide the existing equalization cell into a surge zone and
a slow settling zone. A 4-ft gap between the zones will allow the backwash water to flow
from the surge zone into the settling zone. The wall is positioned to provide adequate
volume in the surge zone to equalize backwash flows while separating surge mixing from
the settling zone. The wall is also positioned to provide linear plug flow and adequate
settling time in the settling zone without the need for settling plates.
Existing vertical turbine pumps
The existing backwash recycle vertical turbine pumps, which are sized for the higher
current media filter backwash flows, will be used to purge solids from the surge and settling
zones as needed. The discharge piping of these pumps will be connected to the existing
RWPF off-spec water pond to provide a necessary air gap to avoid cross-connection. From
the off-spec ponds, the waste backwash water will be pumped to the head of the RWPF for
treatment.
Rectangular settling zone overflow weir
The rectangular weir will be cut into the existing wall and separate the settling zone from
the pumping zone. The weir will help maintain a consistent depth and uniform plug flow in
the settling zone to minimize short-circuiting and improve settling.
Cut in Weir into
Existing Wall
Existing Vertical Turbine
Blowdown Pumps
New Backwash Recycle
Submersible Pumps
New
Reinforced
Concrete Wall
30" Backwash line
from the filters
SLOW
SETTLING ZONE
SURGE ZONE
Existing Lime
Sludge Zone
Existing
Thickener
Overflow Zone
PUMPING
ZONE
To Lime
Reactor InletTo RWPF
Off-Spec Pond
MARCO ISLAND MF PROJECT BACKWASH RECOVERY BASIN MODIFICATIONS
MARCO MF PROJECT BACKWASH REPORT 12-22-10.DOCX 5
Pumping zone and new submersible pumps
New submersible pumps located in the pumping zone will return the treated backwash
water to the head of the lime reactor at a relatively constant rate. VFDs on the new
backwash recycle pumps will be controlled by the level in the pumping zone.
Exhibit 4 shows the design criteria for the modified backwash recovery basin.
EXHIBIT 4
Proposed Backwash Basin Design Criteria
Marco Island NWTP Membrane Filtration Improvements Project Engineering Report
Parameter Criteria
Backwash Characteristics
Instantaneous Backwash flow rate (min/max) 580/640 gpm
Backwash duration 2 minutes
Backwash interval 1-40 minutes
Backwash volume (min/max) 1,160/1,280 gallons
Daily average backwash flow (min/max) 143/245 gpm
Surge Zone
Dimensions (L x W x D) 50/28/4 feet
Volume 42,000 gallons
Capacity (number of backwashes) 33
Backwash Blowdown Pumps
Type Vertical Turbine
Number 2 (1 duty + 1 standby)
Capacity 1,500 gpm
Motor size 15 HP
Time required to drain basin 28 minutes
Settling Zone
Dimensions (L x W x D) 50/28/4 feet
Volume 42,000 gallons
HRT – minutes (min/average/max) 65/170/300 minutes
Weir length 24 feet
Weir overflow rate (min/max) <11.8 gpm/ft
Weir head height at max. flow of 640 gpm < 1 inch
Pumping Zone
Dimensions (L x W x D) 58/30/3 feet
Volume 39,000 gallons
HRT – minutes (min/average/max) 61/160/275 minutes
MARCO ISLAND MF PROJECT BACKWASH RECOVERY BASIN MODIFICATIONS
MARCO MF PROJECT BACKWASH REPORT 12-22-10.DOCX 6
EXHIBIT 4
Proposed Backwash Basin Design Criteria
Marco Island NWTP Membrane Filtration Improvements Project Engineering Report
Parameter Criteria
Backwash Recycle Pumps
Type Submersible
Number 2 (1 duty + 1 standby)
Capacity 400 gpm
Motor size 3 HP
Control VFD
TECHNICAL MEMORANDUM
9. Marco Island MF Improvements Project
Electrical and I&C Design
MARCO MF PROJECT ELECTRICAL-I&C REPORT 12-22-10.DOCX 1
TECHNICAL MEMORANDUM
Marco Island MF Improvements Project Electrical and
I&C Design
PREPARED FOR: Marco Island Utilities
PREPARED BY: CH2M HILL
DATE: December 2010
Instrumentation & Control
Overall Operations and Control Philosophy
The control system will be PLC based with communications via Ethernet. All necessary
instrumentation will be provided to allow effective monitoring and control of the treatment
process.
Refer to the provided P&IDs and Block Diagrams for additional details.
Process Instrumentation and Control System (PICS)
The process instrumentation and control system (PICS) will expand on the existing control
system at the Marco Island North Water Treatment Plant (NWTP) and include a new plant
PLC, new Membrane Filtration Package system PLC and new Remote I/O (RIO) located at
the new Chemical Storage area. The existing Wonderware SCADA system will be expanded
to add screens for new processes added as a part of this project including screens for the
Membrane Filtration system. Local manual controls at motor controllers and valve operators
will provide a means of locally controlling and overriding PLC control. In general,
instruments will locally indicate process measurements.
The main portion of the NWTP upgrades and control system will be a packaged Membrane
Filtration System. The Membrane Filtration package system will be controlled by an Allen-
Bradley ControlLogix PLC and will communicate with the NWTP SCADA system via
Ethernet/IP communications. Any required communications between the Membrane
Filtration PLC and the Plant PLC system will be via hardwired I/O interfaces to minimize
communications errors.
Additionally, existing fiber optic Ethernet connections currently terminated in the Sand
Filter Electrical/Control Room and to the North and South Construction trailers will be re-
routed and terminated to the existing WTP Operations Building. Additional telephone and
CATV interfaces will also be re-routed and terminated in the WTP Operations Building as
required.
The PICS design will not include any type of network security. It is assumed the Owner
will work with their IT consultant and secure their network according to their standards.
Any additional network security appliances will be provided by the Owner. It is noted that
MARCO ISLAND MF IMPROVEMENTS PROJECT ELECTRICAL AND I&C DESIGN
MARCO MF PROJECT ELECTRICAL-I&C REPORT 12-22-10.DOCX 2
the Membrane Filtration system requires remote network access for troubleshooting and
maintenance requiring a direct connection to the Internet which could lead to potential
vulnerabilities, however, mitigating these vulnerabilities is not a part of this project and will
need to be addressed by the Owner’s IT consultant.
The PICS will not include any type of building security, access controls, or CCTV systems.
Any other building management and alarm systems will be provided as a part of the
Membrane Filtration building design.
Process Control
The following systems will be evaluated during design development to determine if
SCADA HMI screens exist and provide adequate functionality for plant operators:
Marco Lakes raw water pumps: Provide On/Off, Speed, and Flow Setpoint
functionality from SCADA HMI. Requires an Ethernet connection between the WTP and
WWTP control systems. Ethernet connection is shown to be provided as part of the
Marco Island RWPF Phase III design and the existence of this connection will need to be
confirmed during design.
Existing Lime Reactor System: Automate influent valve and add Lime reactor drive and
rake control to the SCADA HMI.
Membrane Filtration Package System: Duplicate package system control screens on the
SCADA HMI System.
New Chemical Systems (Alum, Lime, Carbon Dioxide, Sodium Hypochlorite,
Phosphoric Acid, and Ammonia): Provide remote manual control of all chemical
systems from the SCADA HMI. Determine which chemical systems require automatic
PID, Trim, or flow pacing control during design development.
NWTP High Service Pumps: Provide SCADA HMI screens for monitoring and control.
SWTP High Service Pumps: Provide SCADA HMI screens for monitoring and control.
No other systems at the NWTP or SWTP are planned to be added or modified to the
Owner’s SCADA HMI or PLC system. Process systems added to SCADA HMI not currently
connected to the PLC system will have available equipment I/O connected to the new plant
PLC in the Membrane Filtration building or to the new Remote I/O located at the Chemical
Storage facilitiy to allow incorporation onto the SCADA HMI screens.
PLC and SCADA Systems
Koyo DirectLogic PLCs will be used for all PICS PLC and RIO applications. New systems
will be controlled by a Koyo DirectLogic 405 PLC which will be located in the main control
panel located in the Membrane Building Electrical Room. The PLC will interface with field
devices and Package System controllers via hardwired I/O and control functions will be
accessed from SCADA via Ethernet.
The Owner’s existing Invensys Wonderware HMI software and the Owner’s existing HMI
servers and workstations will be used for SCADA. The Owner’s SCADA system will be
updated to incorporate new systems including additional reporting requirements for
MARCO ISLAND MF IMPROVEMENTS PROJECT ELECTRICAL AND I&C DESIGN
MARCO MF PROJECT ELECTRICAL-I&C REPORT 12-22-10.DOCX 3
systems added as a part of this project. The HMI software will be updated as required to
support new systems and communications.
The PLC for the packaged Membrane Filtration system will be an Allen-Bradley
ControlLogix PLC which will be housed in the Membrane Filtration system Main Control
Panel in the Membrane Building. The PLC will interface with field equipment via
hardwired I/O and with Membrane trains via Ethernet/IP connected Pneumatics remote
I/O units. Any communications required between the Plant PLC and the Membrane
Filtration system PLC will be via hardwired I/O.
In-Plant Communications Networks
The primary network used for communications across the PLC/HMI networks will be
10/100/1000BASE-TX Ethernet over Category 6 copper Ethernet cables and Gigabit
Ethernet over fiber optic cable. Loose buffer gel-free Multimode 62.5/125 micron fiber is
currently being used and new fiber optic data links will use the same type of fiber. Sixnet
industrial managed switches and media converters will be used to match the existing
network components at the plant. Cable routing and outlet locations will be discussed
further in the Electrical Section.
The existing network is connected with main nodes in a star configuration to the existing
switch in the NWTP Operations Building. New major links will be added using the same
configuration. This configuration does not provide fault tolerant communications. If a link
is disconnected or damaged, all data associated with that link will not be available on the
network, but other links will still be available.
New communications connections include a fiber optic Ethernet connection between the
new fiber optic Ethernet switch located in the plant PLC enclosure and the existing gigabit
switch in the NWTP Operations Building. Additional communications connections include
connection to the Pall System switch, Pall System remote I/O units, and Remote I/O at the
Chemical Storage facility. No other new communications are planned to be added.
Existing fiber optic Ethernet connections currently terminated in the Sand Filter
Electrical/Control Room will be evaluated and re-terminated to the WTP Operations
Building if it is determined that they are still required for proper Plant communications.
These connections include communications to the onsite Trailers, Lime System, and to the
County WAN external to the plant. These connections need to be evaluated with the Owner
and the Owner’s IT manager to determine requirements including construction scheduling,
equipment preferences, and interface preferences.
Existing plant Ethernet and Radio communications paths at the Plant will be utilized for all
other plant communications, such as communications with equipment at the Marco Lakes
location.
The current NWTP control system network also has several connections to business, public,
and city wide area networks (WAN). It is not currently known if these connections are
through a local internet service provider (ISP) or are private City maintained
communications service connections. Control Systems connected to Business networks
and/or the Internet face an increased risk of being adversely affected by malicious software
and of being penetrated by attackers. It is not currently known if the network, SCADA
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servers, or PLCs at the NWTP have security measures in place and is network security
measures are not being investigated as a part of this project. However unless the City is
confident that current network security provisions are adequate, evaluation of the entire
City SCADA network is recommended to determine if additional security improvements
are required such as network segmentation using Virtual Local Area Networks (VLANs) or
addition of Demilitarized Zones (DMZs). For example, current standards such as the latest
draft standard of NIST SP 800-82, Guide to Industrial Control Systems Security, also
recommends Firewall blocking of email (SMTP) and internet (HTTP) protocols on process
control networks. However a detailed network risk assessment would be required to
determine security measures applicable to the City of Marco Island Water Treatment System
SCADA network.
Raceways will be provided for Telephone connections, if required. Telephone circuits will
be designated and provided by the Owner.
Field Networks
Field networks are device level networks that connect multiple signals from devices, such as
variable speed drives and electric motor operators, to the PLC via a serial data
communications link instead of hardwired I/O. No Field networks are being provided as a
part of this project.
Provisions For Future Expansion
Two membrane trains and related process equipment are planned to be provided in the
future for expansion of the NWTP membrane filtration system. PICS and Package Control
systems will be provided with sufficient installed I/O and spare space to allow
incorporation of these items into the systems provided as a part of this project. Software
will be designed to allow incorporation of these items into the PLC and HMI programs
without major re-programming.
The PICS PLC system will also be provided with a minimum of 15% spare installed I/O in
addition to the I/O reserved for known future equipment.
Drawings
The PICS drawings included with the schematic design report are organized as follows:
EXHIBIT 1
Summary of PICS Drawings
Marco Island Membrane Filtration Improvements Project Engineering Report
Drawing Number Description
01-G-10 & 01-G-11 PICS Legend Sheets define symbols and abbreviations.
10-I-1 thru 10-I-13 Process & Instrumentations Diagrams (P&ID).
10-I-14 & 10-I-15 PICS Block Diagrams
The PICS drawings graphically depict the proposed PICS. Refer to the PICS drawings when
reviewing the PICS portion of the schematic design report. The legend sheets (01-G-10 & 01-
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G-11) along with notes and legends on individual drawings define symbols used on
drawings and clarify design intent.
Control Modes & Levels of Automation
General philosophy
The PICS will provide automatic and manual control of equipment.
Control Modes & Selection
Both LOCAL, primarily manual, and REMOTE controls will be provided as follows.
Local Control
All equipment will have manual local control devices located at the motor controller
location for emergency operation, maintenance, and testing. In LOCAL operation, PLC
control will be bypassed. Controllers will need to be set for REMOTE operation to allow
PLC control. Local controls will be independent of the PLC except for hardwired interlocks
for personnel safety and equipment protection such as motor overloads, emergency stop,
low/high liquid level protection, etc.
PLC Control
PLC control is accomplished from any PC workstation having the appropriate HMI
software using HMI graphic displays. This is the control level for normal system operation.
Any PC workstation on the PLC/HMI network can be used for process monitoring and
control of any process in the facility. Any equipment that is controlled automatically by the
PLC system will also be provided with a PLC manual control mode. This will allow
individual equipment to be manually controlled from PC workstations. The membrane
filtration package system may not have the same manual control mode.
The Owner’s existing SCADA workstations and servers will be used for this project. No
new workstations, servers, or standard PC software will be provided as a part of this
project.
Automatic and manual control logic will be implemented in the PLCs. Control logic will not
be performed in PC workstations.
The Owner’s existing control for PC workstation access and applications software user
levels will be followed for all new HMI programming.
Tag Numbering System
Equipment, Control Valves, and Instrument Numbering System
A standard numbering scheme will be used for this project, except for Package Control
System equipment, that will include equipment, instrumentation, and control loops. The tag
number consists of, device identification letters, followed by a sequential “loop” number, a
unit number, and an optional letter suffix. This numbering scheme is described below.
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EXHIBIT 2
Tag Numbering Scheme
Marco Island Membrane Filtration Improvements Project Engineering Report
Format ISALLUUS[BB] Where:
ISA = 1 to 4-letter device ISA identifier for equipment and instruments
(e.g. P for pump, T for tank, FIT for flow indicating transmitter)
LL = 2-digit loop number; 01 to 99.
Loop numbers are assigned sequentially to devices within a unit process or facility.
UU = 2-digit unit number, e.g. pump 1, pump 2, etc.
S = Optional suffix letter (A to Z) for devices in the same loop and associated with the same unit.
(e.g. two level indicators which indicate the level of the same tank, but are located at two
different locations).
BB = 1 to 4-letter clarifying abbreviation
(e.g. OO for ON/OFF, PH for pH, etc.)
Panel Numbers
Control panels with PLCs will be assigned the identifier CP and use the same numbering
system as the equipment.
Local control panels used to communicate I/O to PLCs but do not perform computing
processes will be assigned the identifier LCP and use the same numbering system as the
equipment.
Design Criteria and Standards
PLC Input/Output Signals
Standard Signals
Use the following PLC I/O signal types:
Discrete Inputs: Dry contact in field powered from 120 Vac source in the PLC cabinet.
24 Vdc contacts will be allowed for package system I/O.
Discrete Outputs: 24 Vdc high-density, terminal block integrated interposing relays in
the PLC cabinet, relay contacts rated for 5 A at 120 Vac, minimum.
Analog Inputs: 4 to 20 mAdc at 24 Vdc. 2-wire transmitters powered from independent
DC power supplies in the PLC cabinet.
Analog Output: 4 to 20 mAdc at 24 Vdc into 750 ohms, powered from the PLC.
Instrumentation
Listed below are instrument types that are planned to be used. Listing a single manufacturer
and model number is assumed to be acceptable. The PICS design will be based on the listed
manufacturer and model number. The Contractor will be required to provide all additional
work including engineering required to incorporate substitute manufacturers and models
and to complete the selection and installation of the named device.
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EXHIBIT 3
Tag Numbering Scheme
Marco Island Membrane Filtration Improvements Project Engineering Report
Field Instrument Application Manufacturers
Electromagnetic Flow Meters Liquid Flow Measurement. Use
pulsed DC excitation. Liners: NSF
61 elastomer type approved for
drinking water.
ABB Magmaster
Rosemount
Endress & Hauser
Rotameters Flow measurement and control for
analyzer feed water.
Brooks
ABB
Pump Check Valve Limit Switch Pump Flow (valve open) and No-
Flow Status (valve closed)
Indication.
Use switches securely mounted on
valve bodies to provide reliable,
low-maintenance operation.
Provided by valve manufacturer
RTD Temperature Sensors Temperature Measurement. Use 2-
wire, 100 Ohm units with
thermowells.
Not required when temperature
measurements are available from
analytical instruments such as pH
at the same location.
Rosemount
Temperature Switches Temperature Alarm. Use vapor
pressure elements where
applicable.
Ashcroft
Temperature Gauges Temperature Indication. Use vapor
pressure elements where
applicable; liquid temperature.
Ashcroft
Free or Total Chlorine Residual
Analyzer and Transmitter
Finished Water Free or Total
Chlorine Residual based on
reagent used. Colorimetric type.
Hach CL17
Turbidity Meter Process Liquid Turbidity
Measurement; low-level
compliance.
Hach 1720E
pH Process Liquid Potential Hydrogen
Measurement; process control
monitoring.
Hach pHD sc Digital Differential pH
Sensor and sc Controller
Ethernet Switches Copper and Multi-mode fiber optic
managed Ethernet Switches to
connect equipment communicating
via Ethernet.
Sixnet.
PLC – Main Control Panel Monitoring and Control Koyo DirectLOGIC 405 series.
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Design Practices and Guidelines
This section describes process control design practices and guidelines for the project.
Emergency Stop Control
When required for personnel safety, equipment will have a mushroom-type emergency stop
(E-STOP) pushbutton. This pushbutton will be hardwired to the motor controller or the
breaker supplying the motor controller. The E-STOP pushbutton must be surrounded by a
metal guard and be capable of being locked in the STOP position.
Personnel Safety
Use switches and relays hardwired to the equipment starter or controller, for personnel
safety interlocks such as E-STOP pushbuttons. These interlocks must be independent of the
PLC.
Equipment Protection
Use switches and relays hardwired to the equipment starter or controller, for protective
interlocks such as motor overload and critical process conditions. These interlocks must be
independent of the PLC. Provide local RESET capabilities to reset lockout functions at the
motor controllers.
Construction Considerations
The existing control panel and network equipment in the Sand Filter Electrical/Control
room will be uninstalled and turned over to the Owner as spares.
Instrumentation at the Sand Filter Electrical/Control room will be uninstalled and provided
to the Owner as spares.
Equipment remaining previously controlled by the existing control panel in the Sand Filter
Electrical/Control room will be controlled by the new Plant PLC located in the Membrane
Building. This equipment includes only those items listed in the section entitled Process
Control.
PICS contractor will need to obtain an understanding of the existing SCADA system
including network interfaces and standard graphics. Information will be included to inform
the potential PICS integrator that the SCADA system is existing and needs to be modified to
maintain the current integrity.
Coordination will be required with the Owner’s IT consultant to identify telephone circuits,
obtain IP addressing schemes, VPN setup, and for general network coordination and
configuration.
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Electrical Systems
Description of Power Distribution
The North Water Treatment Plant Membrane Filtration Facility one line drawings show the
basic power distribution scheme for the facility. Below is a description of the major
electrical distribution system features:
The power feeds to the Existing Zenon System #1 and Existing MCC-5 located in the
Sand Filter Electrical Room will be demolished with conductors removed and conduit
abandoned in place. Feeder breakers for these equipment will be either reused or
marked as spare.
Power will be fed from the existing Low Voltage Switchgear LVSG-2 located in the
Operations Building Electrical Room. The ratings and trip settings of the Existing
breakers in the switchgear will be evaluated to meet the needs of the new electrical loads
in the Membrane Filtration Facility.
MCCs will be rated for 800 Amps, 480Vac, 65kAIC to match existing feeder breakers in
LVSG-2 and Interrupt Current capacity selected based on the Power System Study
performed by GE. Fault currents will be increased as appropriate based on calculations
performed during design development. The number of MCCs required will be
determined during design development to accommodate all electrical loads, including
known future loads, and providing some spare capacity for future modifications.
A new 480Vac panelboard, transformer, and 208Y/120Vac panelboard will be located at
the new Chemical Storage facility for local power distribution. The 480Vac panelboard
will be fed from one of the new MCCs in the Membrane Filtration Building.
The existing MCC-6 building will be demolished and circuits powered from MCC-6 will
be re-fed from new Chemical Storage Area panelboards.
Equipment currently powered from existing MCC-5 that is still required to be in
operation will be re-located into the new MCCs located in the Membrane Filtration
Building.
Equipment performing similar functions will be fed from separate MCCs to allow
continued operation of similar equipment during MCC maintenance or failure such that
taking a single MCC out of service will not disable processes that have lead/lag or
duty/standby type operation. Equipment that is part of the same process train will be
located in the same MCC where feasible.
All 480V distribution for the Membrane Filtration Facility will be provided from the new
MCCs. Power feeds to other new equipment not located at the Membrane Filtration
Facility will be obtained from the nearest suitable electrical power source.
Motor Starters, AFDs, and Equipment requiring over 100Amp, 480Vac breaker feeds will
be fed from the MCCs. All other equipment will fed from panelboards.
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Low Voltage Transformers and panelboards will be provided at the Membrane
Filtration Facility as required to power 240/208/120V equipment. Transformers and
panelboards will be located external to MCCs.
Existing 240/208/120V equipment being powered out of the existing Sand Filter
building will be coordinated with the Owner during design development and any
equipment that will remain in service will be powered from the new Membrane
Filtration Facility.
Conduit runs will be underground and below slab where possible.
The existing 1500kW Generator system will be re-evaluated during design development
to determine if additional capacity is required and what loads, if any, may need to have
starting staggered or be locked out of operation during Generator operation.
Drawings
The Electrical drawings included with the schematic design report are organized as follows:
EXHIBIT 4
Summary of Electrical Drawings
Marco Island Membrane Filtration Improvements Project Engineering Report
Drawing Number Description
G-9 & G-10 Electrical Legend Sheets define symbols and abbreviations.
E-1 through E-2 Electrical One-Line Diagrams
The Electrical drawings depict the proposed Electrical power distribution system. Refer to
the Electrical drawings when reviewing the Electrical portion of the schematic design
report.
Electrical Load Calculations and Preliminary Equipment Ratings
Using preliminary process equipment horsepower and estimating other facility loads, the
connected load was calculated to be 1285kVA. Adding in known future process loads and
estimating other possible future process loads, the total connected load including future
equipment was calculated to be 1560kVA. Based on initial electrical loading, (3) MCCs
being fed from LVSG-2 will be required to distribute power to equipment.
Standby Generation
The existing Standby Generation system will be evaluated during design development to
verify that the existing 1500kW generator has sufficient capacity to provide standby power
to new loads provided at the Membrane Filtration Facility. Options such as staggering the
restarting of large electrical loads, locking out electrical loads, and providing additional
standby power will be evaluated during design development.
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Equipment Preferences
The following is a list of equipment manufacturers designed around and included in
contract specifications:
1. 480 V Motor Control Centers: Eaton/Cutler-Hammer, Schneider Electric/Square D, or
Allen-Bradley.
2. Adjustable Frequency Drives (Stand-alone): Yaskawa.
3. Adjustable Frequency Drives (MCC mounted): Same manufacturer as MCC supplier or
Yaskawa.
4. Lighting and Power Panels: Eaton/Cutler-Hammer, Schneider Electric/Square D, or GE.
5. Dry-type Transformers: Eaton/Cutler-Hammer, Schneider Electric/Square D, or GE.
6. Motors: Toshiba, Emerson/U.S. motors, Baldor, or Reliance.
Hazardous and Corrosive Locations
There are no Hazardous locations associated with the Membrane Filtration Facility.
The Corrosiveness of chemicals will be evaluated during design development and
equipment and materials selected accordingly to protect against corrosion.
Inside Building (non-Air Conditioned, Ventilated): Control and electrical enclosures will
have a minimum NEMA 12 rating.
Inside Building (Air Conditioned): Control and electrical enclosures will have a minimum
NEMA 1 rating.
Outside Building: Control enclosures will have a NEMA 4X, 316 Stainless Steel rating and
electrical equipment will have a minimum NEMA 3R, Stainless Steel rating.
Basic Electrical Materials
The project consists of areas which will be exposed to many different environments.
Therefore, the electrical materials proposed on the project have been selected in order to
provide the maximum physical protection from the environment in which the equipment is
installed while still attempting to minimize the overall construction costs of the project. The
following is a list of the proposed conduit materials to be utilized on the project based on
the area in which it will be installed:
Inside Exposed Corrosive Areas: PVC Schedule 40
Inside Exposed: Rigid Galvanized Steel, EMT, or PVC Schedule 40
Outside Exposed: PVC-coated rigid galvanized steel
Concrete encased: PVC Schedule 40
Direct Burial: PVC Schedule 40
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Adjustable Frequency Drives
Adjustable frequency drives (AFDs) will be provided as required to vary the speed of a
motor within a particular process. Bypasses for drives will not be provided for drives of
any size.
The physical size of the drive can vary significantly depending on the size of the motor
which the drive is powering. Drives 100 hp and smaller will be installed within the motor
control center. Any drives larger than 100 hp will be provided in a stand-alone cabinet. All
drives shall be provided with a local drive front mounted keypad and handswitches for
control, drive front mounted ON/OFF and FAIL indicator lights, and a lockable
Enable/Disable switch located near the motor location.
Drives are also one of the major contributors to harmonics within an electrical distribution
system. These harmonics can have adverse effects on sensitive electrical equipment such as
computers and PLCs. Therefore, the drives will be designed to meet following
requirements:
1. Drives less than 100 hp:
a. Minimum 6 pulse drives with 3-5% input line reactors and output filters.
b. Drives rated based on motor full load current, not on horsepower. Drive rating =
1.0*motor FLA minimum.
c. Input P.F > 0.95 at all speeds.
2. Drives 100 hp and above:
a. Minimum 18 pulse drives to minimize generation of harmonics.
b. Drives rated based on motor full load current, not on horsepower. Drive rating =
1.0*motor FLA.
c. Input P.F > 0.95 at all speeds.
d. Drives provided with output filters to minimize over-voltages at motor terminals.
3. All drives shall include a diode bridge converter front end with a pulse width
modulated (PWM) inverter to generate the adjustable frequency output.
4. Drives on a common bus shall meet the guidelines of IEEE 519 at the point of common
coupling.
Motor Protection and Control
Each motor will be provided with a suitable controller and devices that will protect the
equipment and perform the functions required.
MCC-type construction will be used.
MCCs powered by distribution transformers or remote distribution equipment will have a
main circuit breaker.
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MCC enclosures will be NEMA 1 gasketed. Circuit breakers 225 amps and smaller and
motor starters NEMA size 4 and smaller will be the drawout type with auto disconnect of
control and motor power conductors.
MCCs will include feeder circuit breakers and motor starters. Motor starters for motors
through 50 hp will be the full voltage, non-reversing, combination type with magnetic-only
circuit breaker. Motor starters for motors larger than 50 hp will be the solid-state, soft-start,
reduced voltage, combination type with thermal-magnetic-only circuit breaker with
adjustable trip. The feeder breakers to variable frequency drives for motors larger than 50
hp shall be thermal-magnetic breakers with adjustable trips.
Motor starters will include an ON/OFF/REMOTE or HAND/OFF/REMOTE selector
switch with control devices (START/STOP pushbuttons) for operation in the HAND mode,
RED motor ON light, GREEN motor OFF light, and AMBER abnormal condition and/or
BLUE fault or alarm lights, as required. Lights will be the LED push-to-test type. These
devices will be mounted on the front of the motor starter control center cubical.
Each constant speed motor, 25 hp and larger, and all adjustable frequency drive motors will
be provided with thermal overload protection in ungrounded phases. Controller-mounted
relays will be provided with external manual reset.
All motors 250 hp and larger will be provided with motor protective relays mounted in the
unit starters or AFDs.
Oil-tight pilot devices will be specified for mounting on unit starters.
Motor control circuits will be designed at 120 volts and an individual control power
transformer with 120 volt control voltage will be provided in each motor starter.
Electrical motor starter controls will consist of red and green lights, pushbuttons, or
switches, devices such as timers and auxiliary relaying connected with process control as
required, safety interlock logic, and other non-process controls (motor protection shutdowns
and trouble alarms) as required.
Package Systems
Package systems are integrated equipment provided by a single manufacturer that is self-
contained such as the Membrane Filtration system and Chemical Metering skids. Package
systems will be provided with integral control or motor starter panels to provide local
control of package system operations. A single power feed will be provided to Package
Systems and major components of package systems from either the MCC or distribution
panelboards depending on power requirements. The following is a listing of major Package
Systems:
Membrane Filtration System.
Air Compressor System.
Chemical Feed Systems.
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Distribution System Protection
Equipment will be selected with adequate momentary and interrupting capacity for the
point in the system where it is used. Series-rated criteria will not be used, except for self-
contained equipment.
Phase and ground fault protective devices and device settings will be selected that will
function selectively to disconnect that portion of the system that is malfunctioning with as
little disturbance to the rest of the system as possible.
A preliminary analysis of the fault duty will be made to produce a design that can be
accurately bid by the contractor.
Maximum fault duty will be analyzed with sufficient accuracy to establish the required
interrupting ratings of circuit protection devices specified.
Final coordination studies based on actual equipment purchased will be made by the
contractor to establish the range of protective device settings that will result in reasonable
selectivity of device operations for both three-phase and ground faults. The following
protective device characteristics will be specified:
Protective relay type, coil tap range, and time dial range
Circuit breaker frame size, trip setting range, time delay ranges
Current transformer ratios
Surge Protective Devices (SPDs)
SPDs will be specified on all 480V MCC buses. All power and lighting panel boards will be
equipped with SPDs.
Motors
Generally, all motors 25HP and larger will be provided with space heaters in order to
prevent condensation from accumulating in the motor. Additionally, temperature protection
systems to prevent motors from operating outside normal operational temperature limits
will be provided as follows:
Motors for constant speed application 25 hp through 70 hp and adjustable speed
application 10 hp through 70 hp: Bi-metal disk or rod type thermostats embedded in
stator windings.
Motors for constant speed and adjustable speed applications 100 hp through 200 hp:
thermistor embedded in each stator winding. With a control module installed in the
motor terminal box to generator alarm contact.
Motors for constant speed and adjustable speed applications above 200 hp: 100-ohm 3-
wire platinum RTD embedded in stator winding and on motor bearings.
Alternating current (AC) induction motors will be the premium efficiency type with the
following:
Motors will have a 1.15 service factor, when supplied by sinusoidal power supply.
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NEMA design letter to fit the application (usually NEMA design B), and locked rotor
kVA Code G or lower.
Motors will be cast iron.
Bearings for horizontal and vertical motors will be grease-lubricated, with grease
addition and relief fittings.
Motor windings will be copper wire. Aluminum windings are not acceptable.
Motor insulation system will be Class F with a Class B temperature rise.
Motor supplied power by adjustable frequency drive will be inverter duty rated with 1.0
service factor.
Motors will also be provided with an enclosure which is suitable for operating in the
environment in which it is installed. The following is a list of the enclosures proposed and
the area in which they will be installed:
Chemical Industry, Severe-Duty (CISD-TEFC) – Suitable for indoor and outdoor severe-
duty applications including high humidity, corrosive, dirty, or salty atmospheres.
Totally Enclosed, Fan Cooled (TEFC) – Suitable for most indoor and outdoor
applications in which the environment is not corrosive or hazardous.
Grounding
The majority of the building grounding system will be provided as part of the Membrane
Filtration Building Design. Grounding system additions for the electric distribution system
and equipment shall be provided as required for the Membrane Treatment system design.
Copper-clad steel ground rods and tinned copper ground loops shall be provided around
new structures. The grounding system shall also include connection to reinforcing steel in
the footing walls of the building and connection to exposed vertical metal structural
elements of the new structures where they exist.
Noncurrent-carrying parts of all electrical equipment, devices, panelboards, and metallic
raceways shall be grounded. A separate equipment ground conductor sized in accordance
with applicable requirements of the NEC shall be installed in all raceways for all power and
control circuits. The ground conductor shall be connected to the ground bus in the
equipment feeding the circuit and shall be bonded to all metal enclosures throughout the
raceway system to assure grounding continuity back to the power source.
Lighting
Lighting will be provided as part of the Membrane Filtration Building Design.
Lightning Protection
Lightning protection systems will be provided as part of the Membrane Filtration Building
Design.
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Fire Alarm System
Fire Alarm System will be will be provided as part of the Membrane Filtration Building
Design.
Telephone Systems
This project will not include installation of any telephone cables or telephone equipment.
All Telephone circuits will be provided by the Owner. Raceways will be provided for the
installation of known telephone connections.
Standards and Codes
The electrical design will conform to the latest applicable editions of the following standards
and codes:
National Fire Protection Association (NFPA)
NFPA-70, National Electrical Code (NEC)
NFPA-70E, Standard for Electrical Safety in the Workplace.
Standards and codes of the following shall govern where applicable:
American National Standards Institute (ANSI)
National Electrical Manufacturers Association (NEMA)
Institute of Electrical and Electronic Engineers (IEEE)
Insulated Cable Engineers Association (ICEA)
Occupational Safety and Health Act (OSHA)
American Society for Testing and Materials (ASTM)
Local codes and ADA standards shall be applied as appropriate. Where the requirements of
more than one code or standard are applicable, the more restrictive shall govern.
TECHNICAL MEMORANDUM
10. Marco Island NWTP MF Improvements Project
Engineering Report Drawings
TAB III Experience and Capacity of FirmTAB IIIExperience and Capacity of Firm
III‐1
CH2M Team Abilities and Capabilities
CH2M’s proven, available team is prepared to deliver on its promise of providing Collier County with efficient,
coordinated services for the Variable TDS Reverse Osmosis Conceptual Design Project. Our team consists of two
firms, each with a strong track record of successful project delivery for Collier County, bringing to this project
familiarity with your preferred methods of project delivery and standards for quality. Just as important, the
individual members of our project team have the technical expertise and the professional experience on similar
projects which will allow our team to be efficient in addressing key challenges affecting project success. We
routinely work together and offer an “integrated” team approach to providing successful project solutions.
CH2M, founded in 1946, is a global engineering and project delivery company partnering
with public and private clients to tackle the world's most complex infrastructure and natural
resource challenges. The firm's work is concentrated in the water, transportation, energy, environment and
industrial markets. CH2M has gross revenues of $5.4 billion, has 22,000 employees and is a specialist in program,
construction and operations management and design.
CH2M has been registered as a Florida corporation since 1951. The firm’s Naples office will be responsible for
managing the County’s project and offers a management team that is comprised of locally based experts. Project
Manager, Joe Elarde, and Principal‐in‐Charge Bill Beddow, represent decades of experience in successfully
delivering water infrastructure projects throughout Southwest Florida, the state of Florida and around the world,
as well as direct experience with the County. The County will benefit from having this high level of global expertise
as the primary points of contact and project accountability located within close proximity to County offices.
Capacity
CH2M is a global engineering firm and will provide the County
access to our global network of more than 22,000 multi‐disciplined
staff members, as needed. It is anticipated that our team will
manage all scope of services items from our Naples office,
supported by the specialized skills of our Florida team members.
On a firmwide basis, CH2M has more than adequate capacity to
provide the required services. If additional resources are needed for
any reason, Project Manager Joe Elarde, can reach out and procure
skilled personnel to assist the County. Representative CH2M staff
members include 690 Water Resources Engineers, 424 Process
Engineers, 174 Geologists, and 86 Hydrologists.
Financial Strength
CH2M had gross revenues of $5.4 billion ($5,361,505,369) in 2015. We would be happy to provide the County
with our annual financial statements or you may view our SEC filings at http://ir.ch2m.com/financial‐
information/sec‐filings/default.aspx.
Water Science Associates is a hydrogeological consulting firm that was
established by Kirk Martin and Brian Barnes to leverage over 50 years of
combined experience in providing creative, sustainable, and scientifically based solutions to our Client’s water
CH2M’s Florida offices house
more than 800 full time staff
members possessing a broad
range of technical skills to
support the County’s RO Design
project.
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resource challenges. Kirk Martin, PG was the former lead hydrologist with a nationally recognized engineering and
infrastructure firm and Brian Barnes was the former director of South Florida operations for an international
infrastructure and environmental consulting firm. Water Science Associates staff provide exceptional experience
in water resource evaluation, permitting, and facility design and construction throughout Florida and the
Caribbean.
The firm specializes in serving Public and Private Water and Wastewater Utilities, high quality Land Development
projects, Construction Contractors, Mining Industry, and Agricultural interests. We provide water resource
management and development services from planning, investigation, design, implementation, and compliance.
Water Science Associates takes pride in its reputation for responsive, Client‐focused and solutions oriented
services. We believe in listening carefully to project needs and client objectives, collaborating effectively with
project team members, and delivering appropriate and cost effective solutions to our Clients’ most challenging
water resource issues.
Water Science Associates specializes in:
Groundwater resource evaluations and water supply development
Saline water intrusion evaluations and mitigation
Wellfield planning, design, permitting, and construction
Aquifer Storage and Recovery design, permitting, and construction
Deep well injection well design, permitting, and construction
Dewatering plans, permitting, and impact assessments
Groundwater/Surface Water flow modeling and impact assessments
Seepage assessment and mitigation design
Mounding analysis for land disposal of wastewater
Managing Project Risks
As‐built and operations information is not available or is not accurate requiring re‐work by/change orders
to the engineer or contractor: mitigate by reviewing existing information in detail, developing a gap analysis
and collecting the outstanding information. CH2M and WSA are familiar with the NCRWTP system and will
incorporate our existing understanding of data gaps into the planned scope and analysis.
Use of innovative, unproven technologies without testing, and if not successful, requiring equipment
modifications after startup: mitigate by doing due diligence and perform additional testing if the proposed
technology is not proven yet on this type of water.
Future raw water quality variations differ from the projections, either in TDS or other water quality
constituents, requiring equipment or operational modifications after startup: mitigate by doing detailed
projections, verify with other utilities who have experienced variable TDS and provide flexibility in design. Use
recent CH2M experience and lessons learned in variable TDS evaluation and design to anticipate and account
for likely issues.
Finished water quality is different from projections due to different raw water quality or use of different
types of membranes/treatment regime requiring additional post conditioning chemicals and corrosion
control testing: mitigate by conducting post‐treatment evaluation early and provide flexibility in post‐
treatment process.
Existing well/pipeline/fittings and process equipment are over 15 years old, and may fail due to condition
during the startup and/or operation with the higher salinity water: mitigate by conducting a condition
assessment, review material compatibility with higher TDS water, and include upgrades as part of this project.
Combined concentrate water chemistry changes as part of this project leading to precipitation of scales in
pipe or injection well: mitigate by performing desktop water chemistry modeling and bench scale testing
using CH2M’s in‐house Applied Sciences Laboratory to predict scale formation in concentrate and develop
III‐3
methods to mitigate. Use CH2M experience at several facilities where potentially incompatible waste waters
have been combined before deep well injection.
Client is not able to make a selection of the preferred alternative delaying the project: mitigate by involving
the client in every step/decision during the project. Use a clearly defined, documented and defensible
decision making process as successfully completed on several project using CH2M decision making tools.
Cost of implementation of preferred alternative is above the budget requiring rework to get within budget
costing time and money: mitigate by developing detailed and reliable capital and operating cost opinions
using CH2M’s CPES™ cost model early in the alternatives evaluation and conceptual design phases and
developing a financing and phasing plan.
Conversion of existing BWRO trains to variable TDS RO trains requires multiple and extensive plant
shutdowns impairing ability to make water: mitigate by providing constructability reviews and by working
together with the County to develop phased implementation plan, with potential temporary utilities/facilities.
The TDS in the affected wells declines over time and matches the other wells resulting in an unutilized asset
for variable TDS treatment: mitigate by providing a flexible treatment solutions capable of treating low TDS
water even if less efficient. Identify process that provide multiple benefits like energy reduction or
concentrate minimization to offset potential inefficiencies. Design flexibility into the overall treatment
process by selecting components that can be used for multiple scenarios if anticipated early.
Benefits the CH2M Team offers the County
CH2M brings to this project a history of working in Collier County since 1977. We know the Collier County’s
systems and operations, and bring an acute understanding of local conditions as well as the County’s staff, local
subcontractors, contractors, and consultants. CH2M has worked at the NCRWTP facility upgrading water
treatment systems and working the local facility staff giving us recent in‐depth water treatment process
familiarity. WSA personnel are the designers have been central to work on the NCRWTP wellfield and understand
the issues contributing to the increasing source water TDS. This unparalleled recent source and treatment
experience at the NCRWTP gives CH2M an incomparable understanding of the issues faced during analysis and
design of the treatment facility.
Our proposed Project Manager, Joe Elarde, P.E., is known to County staff and is well qualified to serve as the
Project Manager and Task Leader. Based in our Naples office, he is a nationally recognized specialist in membrane
technologies—more than 19 years of water treatment planning and design experience, and 21 years of
membrane process experience working on projects that include study, design, permitting, construction, startup,
and operation of membrane filtration, nanofiltration, brackish water reverse osmosis, and seawater desalination
facilities all over the U.S., including many in Florida.
CH2M has established an international reputation in developing and applying desalination technology for
municipal facilities. A leader in the study and design of desalination facilities, we have an extensive knowledge of
alternative desalination treatment processes and what will be critical for additional support and optimization. We
are confident that no other firm in the nation has the pilot‐, demonstration‐, and full‐scale operational experience
History of working with Collier County and institutional knowledge of your systems,operations,
and staff allows us to start work immediately upon NTP
Project organization that provides all required resources under the direction of a
proven, experienced Project Manager streamlines project delivery and minimizes schedule
Proven methodologies and lessons learned on the successful delivery of similar projects
ensures the County that you will receive the best option for a viable and cost effective process
1
2
3
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with desalination treatment that CH2M has to offer the County. This experience gives us a unique insight into the
strengths and weaknesses of the process, and it will allow us to evaluate and identify the most appropriate and
cost‐effective process for local requirements.
Proven Facility Modeling and
Costing Tools
Our proprietary technology and costing models
effectively capture our best practices and will
help the County quickly and cost effectively find
true optimum solutions. CH2M has developed
and successfully applied a variety of simulation
and optimization modeling tools that estimate
cost, carbon footprint, treatment performance,
and system control. Our models include CPES™
(our proprietary costing tool), Replica™ (our
dynamic treatment simulation model), Source™
(our water treatment mass balance tool),
Preview™ (our facility visualization tool),
Voyage™ (complex decision support model), and
SI Port™ (our sustainability tool).
Local and Global Construction Experience
With more than 18 years of experience constructing water and wastewater projects – including $1.5 billion of
constructed value since 1997 – CH2M is an industry leader in constructing water and wastewater treatment
plants. Our projects represent the range of challenges we help owners address and also demonstrate our ability to
deliver quality facilities with highly constructible solutions. Local construction of multiple water treatment
facilities including the Bonita Springs lime softening WTP expansion, RO WTP and Floridan wellfield, the Ave Maria
membrane softening facility, and the Fort Myers RO WTP and Floridan wellfield provide local lessons learned
about the costs, constructability and challenges associated with SW Florida constructability. Furthermore,
construction of retrofit systems into the existing Bonita Springs and Fort Myers
facilities helps our team understand constructability issues and how to keep existing
facilities on‐line during construction. Our DB experience also provides an
understanding of the information needed in a 30 percent design criteria package that
will provide clear future direction.
In‐House Treatability Testing and Experience
CH2M HILL’s Applied Sciences Laboratory (ASL) provides the County with direct
access to decades of direct water treatment evaluation and testing experience to
cost‐effectively help understand treatment performance at the bench‐ and pilot‐
scale level before making an investment on a full‐scale facility. If schedule and
budget permits, short bench‐scale testing can be conducted at the NCRWTP or at the
ASL using water shipped from the NCRWTP to confirm water quality and process
treatability requirements to reduce full‐scale facility cost associated with overly
conservative design using limited information.
World Leader in Desalination Innovation
CH2M’s history delivering desalination projects both in the around the world is
extensive. We have been researching, pilot testing, designing and installing
desalination systems for nearly 40 years, dating back to the design of the original
Cape Coral, Florida brackish water desalination plant in 1977.
The CH2M HILL Applied
Sciences Lab is a full‐
service water quality and
treatability facility with
decades of direct water
treatment testing
experience to help in
process decision making.
CPES is a proprietary conceptual design and cost estimating
tool that generates quick, accurate, and detailed cost
estimates at the conceptual stage of any WTP, WWTP, or
conveyance project.
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CH2M is an international leader in desalination. As an integrated project delivery company, we offer a single point
of service and responsibility for all desalination‐related needs, be it feasibility and pilot studies, conceptual and
detailed design or facility construction and operation, in order to optimize constructability, reliability and cost
efficiency by designing right the first time.
No matter how complex the project, our staff brings focused expertise—with the know how to apply membrane
desalination technologies for brackish water similar to Collier County’s supply. We take pride in having
successfully delivered hundreds of projects, both big and small, for our clients throughout the world.
Within the last 10 years, we have designed and delivered more than $125 million of desalination projects in the
Middle East, Asia, Australia and United States.
Exhibit III‐a illustrates the breadth and depth of our desalination experience in which a variety of selected
desalination projects completed within the United States and throughout the world have been successfully
completed for municipalities as well as State and National governmental agencies. These include projects treating
brackish surface and ground water, seawater and wastewater (for reuse) as well as groundwater high in hardness
and organic matter using nanofiltration. Beyond those shown in the figure, CH2M has also completed desalination
projects for a variety of industrial clients, including those in high‐volume, oil and gas and mining sectors.
CH2M is known for our leadership in the water and wastewater industry and for pioneering desalination
innovations and technologies, including membrane pretreatment, dissolved air flotation (DAF) pretreatment,
large‐diameter RO technology, capital and operational cost minimization, SWRO energy recovery optimization and
green technology innovations.
Since the 1970’s, we have been a leading proponent in the design and advancement of RO technology. While we
liaise closely with membrane suppliers, due to our dedicated internal RO specialists, we are not limited to relying
on their design. Instead, we utilize our global RO specialists to ensure our clients receive a facility that is leading
edge and provides the best long‐term value. CH2M has:
Designed the world’s first dual‐membrane (microfiltration and RO) plants to challenging surface waters
Engineered the world’s first large diameter seawater RO installation at Power Seraya in Singapore
Pioneered the use of microfiltration as a pretreatment for the advanced reuse of secondary effluent using RO
Conducted comprehensive cost analysis that served as the basis for adoption of 16” as standardized size for
large diameter seawater and brackish water RO elements
Served as Program Manager for the world’s first zero carbon, zero waste, 100% renewable energy
development, including desalination, at Masdar City, Abu Dhabi.
Produced an energy recovery device tool for the WateReuse Research Foundation that allows users to
identify, which, if any, commercially available and proven energy recovery devices are suitable for their
brackish and seawater RO systems.
CH2M’s commitment and leadership in brackish water RO is evident in the projects we work on. CH2M has
successfully completed more than 200 desalination studies and pilots and has been instrumental in the delivery of
more than 30 operating brackish water RO and 10 operating seawater RO facilities worldwide. Exhibit III‐b
provides a list representative CH2M’s desalination projects. Additional information about these projects is
included at the end of this section.
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EXHIBIT III‐a CH2M Global Desalination Experience
III‐7
EXHIBIT III‐b CH2M RO Desalination Projects
Project
Plant
Size
(mgd)
Membrane
Process Services Provided Nanofiltration Brackish Water RO Seawater RO Engineering Study Pilot; Demo Testing Design Construction SiStartup/Operations Management Consulting Design‐Build Representative Brackish Water Projects
RO WTP, Fort Pierce, FL 5.3
Yuma Desalting Plant, Yuma, AZ 7
Northwest River WTP, Chesapeake, VA 12
Cypress WTP Expansion, Wichita Falls, TX 10
Southside WTP, Abilene, TX 7.5
Menifee Desalter, Eastern MWD, CA 3.5
Perris I Desalter, Eastern MWD, CA 2.5
Robert Dean RO WTP, Florida City, FL 6
RO WTP Expansion, Fort Myers, FL 13.3
RO WTP, Dunes Com. Development District, FL 0.65
Perris II Desalter, CA 4.5
RO WTP, Bonita Springs, FL 6
North Springs Improvement District, FL 7.5
Coral Springs Improvement District, FL 7.5
Cherry Point, NC 6
Ave Maria WTP, FL 2.0
Reynolds Desalter, CA 11
Green Meadows WTP, Fort Myers, FL 16
Representative Seawater Projects
SWRO Planning Study, MAWC, MA Study
Desalination Feasibility Study, Port St. Lucie, FL Study
SWRO WTPs, Stock Island/Marathon, FL 2/1
Dependability Study, New York DEP, NY Study
Seawater Desalination Feasibility Study, Hong Kong Pilot
SWRO Pilot, Marin MWD, CA Pilot
Co‐Located SWRO/Power Feasibility Study, Mexico Study
Palau Power Seraya Station WTP, Singapore 2.4
Layyah/Khor Fakkan/Kalba SWRO WTPs, Sharjah, UAE 15
Seawater Desal Demo Facility, Long Beach, CA Demo
Desal Plant, Melbourne Water Corp., Australia 120
Southern Seas Seawater Desal Plant, Australia 38
Pilbara Seawater Study, Water Corp. of Western Australia Study
Forward Osmosis/RO Hybrid Feasibility Study, TWDB, TX Study
Integrated PV‐SWRO Demo, Middle East Demo
Marina East Variable Salinity Project, Singapore 36
Mirfa Independent Water and Power Project, UAE 36
ACWA Power Barka, Oman 15
Tuas Desalination Plant III, Singapore 36
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Previous Performance with Similar Jobs
CH2M has extensive RO/Membrane experience in Florida and worldwide that is directly applicable to the Collier
County variable TDS RO Conceptual Design project. While Exhibit III‐b shows a wide range of desalination
projects that demonstrate our knowledge of the issues and wide range of design feed TDS conditions, Exhibit III‐c
summarizes projects with similar scopes of work to this project. Detailed project descriptions showcasing our
relevant project work with variable TDS source water, desalination evaluation and desalination design.
EXHIBIT III‐c CH2M Representative Similar Projects
Project Description Start Date End Date
Original
Budget
Final Project
Cost
Number of
Change Orders
Reference Projects
Marco Island Expansion Evaluation & 30% Design 10/2009 12/2010 $174,721 $174,721 0
Ave Maria Expansion Planning 09/2015 01/2016 $24,835 $24,835 0
North Springs Improvement District RO WTP Design
& SDC 2010 2016 $19.45M $19.45 <3%
Bonita Spring Design Build 3 Lower Hawthorn Wells
and Wellheads 04/2015 06/2016 $2.4M $2.4M 0
Lee County Class I Injection Well Acidization
Professional Engineering Support 02/2015 04/2016 $25,900 $25,900 0
Other Similar Projects
Marina East Variable Salinity 36 mgd RO Project,
Singapore 2014 2015 Confidential Confidential 0
Green Meadows WTP Expansion, Lee County, FL 2012 2016 $56M $70M* N/A*
Bonita Springs RO WTP Design‐Build 2003 2004 $40.8M $40.8M 0
Bonita Springs Energy Recovery Upgrades 2011 2012 $1.2M $1.2M 0
Ave Maria Membrane WTP Design‐Build‐Operate 2003 2005 $20.2M $20.2M 0
Pilbara Seawater Study, Water Corp. of Western
Australia
2009 2010 $750,000 $750,000 0
Olga Variable Salinity Surface WTP Expansion
Evaluation, Lee County, FL
2009 2011 $900,000 $900,000 0
Energy Recovery Model Development for
Desalination, WateReuse Foundation
2010 2012 $250,000 $250,000 0
Dependability Study, New York DEP, NY 2004 2006 $1M $1M 0
*Client driven scope change when changing the facility expansion from 12 to 16 mgd. Currently under construction.
III‐9
MARINA EAST VARIABLE SALINITY DESALINATION PLANT,
SINGAPORE
Client Name: Public Utilities
Board, Singapore
Size: 36 mgd
Project Value: Confidential
Project Duration: 2014‐2015
Key Highlights/Relevant Features:
VSP technology offers the
potential to treat brackish
water and seawater cost‐
effectively in the same plant
Comprehensive cost
estimating
Architecture and landscaping
designed both to integrate
with the surroundings and
offer a point of interest to the
general public
Innovative layout occupying 3
levels
Environmental impact
assessment (EIA) study for the
30MIGD desalination plant
Singapore and its neighbors, most relevantly Malaysia, have recently
experienced drought and this has resulted in challenges for the Public
Utilities Board (PUB) total water management approach. Availability of
imported water is becoming less certain than in the past due to climate
change and the sustainability of this source is uncertain.
PUB continues to investigate other sources of supply and recently engaged
CH2M to undertake an investigation and conceptual design of the 36 mgd
Marina East Variable Salinity Plant (MEVSP). This high profile desalination
plant is located in a prominent location near the CBD of Singapore. The
constrained 3 hectare site within public parkland necessitated an
innovative layout occupying 3 levels and incorporating DAF and UF pre‐
treatment and two‐pass Reverse Osmosis.
Seawater and brackish water will be abstracted through dedicated intakes
drawing from the Singapore Straits and the Marina Reservoir, respectively.
This will allow PUB to choose on a daily basis between the treatment of
seawater or brackish water, which requires a much lower specific energy
consumption and results in a significantly lower cost of treatment.
The treatment process for MEVSP has been developed to meet World
Health Organization (WHO) and PUB drinking water quality guidelines
based on an analysis of water quality data from both the Marina Reservoir
(post‐barrage construction) and the Singapore Straits. Due to inherently
different plant losses when operating on Marina Reservoir water
compared to seawater, the MEVSP will be capable of converting a higher
percentage of Marina Reservoir water into potable water than seawater.
As a result, the plant output will be higher when treating Marina Reservoir
water than seawater.
CH2M Role/Responsibilities:
CH2M is providing the full spectrum of conceptual design services
including;
Boundary Limits Workshops
Environmental Impact Assessment Studies
Concept Process Design Development
First Cut Infrastructure Development
Process Design Development
Equipment Sizing
Electrical System Design
Plant Layout Option Development
Preliminary Cost Estimation & Constructability Assessment
Option Screening
Design Refinement
Cost Estimation
Design Report
III‐10
GREEN MEADOWS WTP EXPANSION, LEE COUNTY, FL
Client Name: Lee County Utilities
Size: 16 MGD
Project Value: $70 million USD
Project Duration: 2012‐2016
Key Highlights/Relevant Features:
Feasibility and pilot studies
identified the best value
option using a benefit cost
analysis and CH2M tools ‐
provided Lee County
exceptional value.
The RO building incorporates
space‐saving concepts like a
center‐trench design and
train‐specific roll‐up doors and
includes operator facilities.
Evaluation identified the
benefits of alternative ion
exchange regeneration using
RO concentrate and seawater
wells.
The design includes
concentrate and regenerant
disposal by two injections
wells.
The existing Lee County Utilities Green Meadows lime softening facility
treats a blend of fresh surficial and intermediate aquifer groundwater
sources. The existing facility was nearing the end of its useful life and
needed to be replaced to maintain reliability and to continue to meet
regulations. To limit the demand on fresh water sources, the larger new
facility uses a brackish groundwater well source in addition to the existing
wells for expansion.
The new 16‐mgd facility uses reverse osmosis for desalinating brackish
well water in parallel with cation and anion exchange used to remove iron,
hardness and organics from a surficial aquifer fresh water source. A new
seawater well provides an alternative source of brine for cation exchange
resin regeneration to reduce operational costs. The estimated $35M
facility is part of a $70M project that includes new wells, wellfield
pipeline/roadway, and concentrate disposal wells.
CH2M Role/Responsibilities:
CH2M conducted a process evaluation and subsequent 1‐year pilot study
to determine the most economical and efficient treatment system to make
use of all three water sources. The treatment process’s identified were
cation and anion ion exchange as the most cost effective and reliable
process to treat a blend of the existing fresh water sources and a new RO
system that will treat the brackish source before blending with the treated
freshwater sources. The studies identified and subsequently verified
through pilot testing that RO concentrate and/or seawater wells could
effectively regenerate the cation exchange resin to significantly reduce
operating cost of the new facility.
CH2M conducted a desktop analysis of blending three different
groundwater supplies using our Source™ water quality and treatment
modeling tool to quickly identify impacts of blending on treatment and
optimize options for further proof pilot testing to confirm and develop
design criteria. Our CPES™ tool was used to develop costs for several
different treatment variations and capacities to help the County define the
best value option for the facility. Our Bridge™ design tool allowed the
project team to quickly and cost effectively complete the design to meet a
limited design budget and project schedule. CH2M used its Preview™ tool
into provide 3‐D representations early in the design process to help freeze
design decisions early. Dynamic simulation using Replica™ was also
conducted during the project to optimize energy efficiency and hydraulics.
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BONITA SPRINGS RO WTP, BONITA SPRINGS, FL
Client Name: Bonita Springs
Utilities
Size: 6 MGD expandable to 12
MGD Desalter
Project Value: 40.8 Million USD
Project Duration: 1993‐2013
Key Highlights/Relevant Features:
CH2M successfully managed
more than 22 subconsultants
and delivered the RO WTP on
time and within budget
Saved BSU $500,000 from
direct contracting for
equipment features,
eliminated 3 weeks from the
original schedule, and reduced
construction costs by $50,000
by developing a unique
installation method for the RO
feed pump cans
20‐year relationship, providing
water and wastewater
treatment, regional irrigation
planning, and general
engineering services to BSU
Located in a popular resort and tourism area, the Bonita Springs Utilities
(BSU) service area is subject to peak seasonal water demands due to
visiting tourists and part‐time residents.
CH2M Role/Responsibilities:
CH2M began assisting BSU in 1993 with a wide range of utility engineering,
construction, and specialty evaluation services for water, wastewater, and
reclaimed water systems. As part of this, CH2M prepared a water quality
study for the potable water system. The study reviewed short‐ and long‐
term options for expanding the existing potable water system to meet
emerging water quality regulations. In 1997, we implemented a 3‐mgd
expansion to the existing potable water lime softening WTP using the
traditional design‐bid‐build delivery process. In 2000, to respond to rapid
continued growth in the area, CH2M completed a second expansion to this
lime softening plant, increasing operating capacity to 13 mgd; this second
expansion also used the design‐build delivery process.
In 2002, CH2M commenced a design‐build of a new 6‐mgd (expandable to
12 mgd) RO water treatment facility constructed on the existing lime
softening facility site. This new RO WTP project included installation of
three cartridge filters; four RO feed pumps; four RO membranes trains;
chemical systems; degasifier and odor scrubber system; 2‐million‐gallon
ground storage tank; five brackish water production wells with pumps and
wellhead; three new high‐service pumps; new finished water transmission
main; raw water meter and new yard piping; plant generator; seven
wellhead generator; electrical upgrades; instrumentation and controls
software upgrades; and lime softening water plant slaker. The
demineralization facility was constructed to treat the brackish water and
the treated water was blended with the existing lime softened water prior
to storage and distribution. The RO WTP was designed conservatively, so
that its processes and equipment can accommodate potential degradation
of source water quality over the next 20 years. The project involved a new
4,160‐volt electrical service and ductbank loop to existing and new site
facilities and a new sodium hypochlorite generation system for both the
lime softening facility and new RO facility.
In 2012, CH2M completed an upgrades study, design and construction
project that optimized membrane replacement, new energy recovery
devices (ERDs), potential train expansion and overall wellfield and RO train
control that saved the utility more than $150,000 in annual power costs.
The project featured a Replica model of the complete RO and wellfield
system that was used to find operational strategies that could save the
utility additional power cost.
“CH2M is one of the few consultants I can count on to act as an extension of my
staff. When I need help and need it now, I know that CH2M will deliver.” —Fred
Partin, Executive Director, BSU
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NORTHWEST RIVER WTP, CHESAPEAKE, VA
Client Name: City of Chesapeake
Public Utilities
Size: 12 MGD
Project Value: $56.9 million
Project Duration: 1993‐1999
Key Highlights/Relevant Features:
This project won the top
award, Engineering Excellence
Award, in the Water and
Wastewater category from the
Consulting Engineers Council
of Virginia.
The first completed operating
ASR system in the state of
Virginia
For several years the City of Chesapeake considered alternatives for
upgrading the Northwest River WTP. The raw water is highly colored river
water with characteristics that include high concentrations of total organic
carbon and manganese, low alkalinity, and low pH. Saltwater intrusion into
the river during low flow, summer periods and a need to comply with
future regulations restricting disinfection by‐products (DBPs) were the two
main drivers behind the upgrade.
CH2M Role/Responsibilities:
The City selected CH2M to design upgrades to the existing conventional
treatment processes – rapid mix, flocculation, sedimentation, and high‐
rate filtration – and to design a new membrane treatment facility. The new
membrane treatment facility is designed to treat conventionally treated
surface water or brackish water from deep wells. The surface water and
groundwater reverse osmosis (RO) systems have capacities of 8 mgd and
4 mgd, respectively.
Previously, CH2M conducted a membrane pilot test program to help
determine the most feasible approach to removing DBP precursors and
protect against saltwater intrusion. The pilot programs confirmed the
feasibility of upgrading the Northwest River plant. The proposed design for
the upgrade included separate facilities for membrane treatment of
filtered water from the river and of brackish water from deep wells. Pilot
testing was also used to confirm suitability of the combined RO
concentrate (from the surface and brackish water RO trains) for discharge
to the south branch of the Elizabeth River. This required concurrent
operation of two separate RO pilot units to produce representative
concentrate from which toxicity and trace metal analyses could be
performed.
The design, which resulted in one of the most sophisticated WTPs in the
U.S., includes conventional and membrane processes that allow maximum
flexibility for treating the variable water sources. Four process trains fitted
with low fouling, RO membranes effectively handle saltwater intrusion into
the river. Two separate trains using high rejection RO membranes treat the
higher‐salinity brackish groundwater from the production wells. Under the
worst‐case operating scenario, all membrane trains operate on flow from
the river, and all wells are in service. Under typical (non‐brackish)
conditions, only one or two membrane trains operate, saving energy.
“The 10‐mgd upgrade of our surface water conventional treatment plant to
surface and groundwater RO was a huge undertaking for the City of Chesapeake...
The design by CH2M was extraordinarily complex, requiring not only a sound
design but the need for an integrated upgrade that would allow an existing plant
to remain in continuous operation during construction. Virtually every design and
construction challenge was overcome in a way that best combined the input of the
design engineer, contractor, and the City...” —A. Craig Maples, Water Production
Superintendent, City of Chesapeake, Water Production Division
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RO WATER TREATMENT PLANT, CITY OF FT MYERS, FL
The City of Fort Myers WTP was designed and built (by others) in the early
1990s as a membrane softening facility treating surficial groundwater.
The facility was designed for a capacity of 12 mgd with an ultimate future
expansion to 20 mgd. The facility was converted by others to a brackish
water RO facility in 2002 because of feed water quality problems. The
conversion reduced WTP capacity to 8 mgd due to feed water pumping
and post‐treatment limitations.
As the designer and general contractor, CH2M provided pre‐design, final
design, procurement, permitting, construction management, and startup
services, as well as services during construction. This project expanded the
raw water supply, expanded the RO WTP capacity from 8 to 13.3 mgd, as
well as resolved existing post‐treatment water quality issues. Specific
treatment components included a transmission main; two degasifers;
membrane feed pumps; RO equipment; production wells; raw water sand
strainers; upgraded plant control; and upgraded plant electrical.
CH2M HILL subsequently provided design‐build services to design and for this design‐build project,
The project was delivered under budget and within schedule in spite of delays as a result of four hurricanes.
MEMBRANE SOFTENING WTP, AVE MARIA UTILITY
COMPANY
Located on 5,000 acres of former farmland, Ave Maria is a new city
development consisting of a university and surrounding community of
residential units, retail stores, medical facilities, hotels, public schools, and
parks. CH2M HILL began work on this design‐build‐operate project in 2005
and was responsible for design, permitting, construction, and operation of
the located water facility, including a natural treatment wetlands treatment
system being developed on the greenfield site. The WTP design is a 1.67‐
mgd membrane softening facility. Concentrate from the WTP is sent to the
1.25‐mgd WRF for disposal. Three water supply wells provide raw water for
the system.
CH2M HILL met the overall development schedule by preparing preliminary
engineering reports that met FDEP requirements for permitting early in the
development of the construction documents. While FDEP reviewed the
permit applications, construction document preparation continued, saving
time in the schedule. Early discussions and presentations to the permitting
agencies helped to streamline the process. Procurement of equipment was
also started early in the schedule, prior to completion of the final construction documents so that delivery of key
equipment wouldn‘t slow construction.
Completed in 2006, CH2M HILL OMI is contracted to operate the newly constructed facilities for up to 20 years
based on four recurring 5‐year contracts.
“We are extremely pleased with our relationship with CH2M HILL. They delivered on all facets of the design,
construction, and operation of our facilities and within the timeframe and budget established. Their
professionalism, technical expertise, and dependability have earned them a place on our team – now and in the
future.” David B. Genson, PE, Director, Ave Maria Utility Company
For the RO WTP project, we saved
the City of Fort Myers more than
$1,290,000 through diligence of
scheduling, well design changes,
and controlling labor costs during
construction.
This Ave Maria project was the
winner of the 2007 Design‐Build
Institute of America Merit
Award for water/ wastewater
projects over $15 million.
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FORWARD OSMOSIS / RO HYBRID FEASIBILITY STUDY,
TEXAS WATER DEVELOPMENT BOARD, TX
CH2M HILL worked with the TWDB to evaluate a hybrid forward osmosis/reverse osmosis (FO‐RO) process to
recover water from high salinity water for beneficial use. The study sought to examine the mechanics of forward
and reverse osmosis water treatment; assess the feasibility of using high salinity streams to extract water out of
water streams; and, determine characteristics required for cost‐effective application of this hybrid process.
Bench‐scale pilot testing was completed to evaluate feasibility while cost modeling was also conducted to
determine viability compared to other treatment options. Assuming that membranes can be commercially
produced at a reasonable price point, it is anticipated that use of FO‐RO may be viable at some point in the future.
This study provided several recommendations for continuing the development of the hybrid FO‐RO process.
CALIFORNIA SEAWATER DESALINATION
DEMONSTRATION FACILITY CITY OF LONG BEACH, CA
CH2M HILL provided senior level process consulting in conjunction with construction and operation of the
Seawater Desalination Prototype Demonstration Facility. The Facility utilizes a unique two pass nanofiltration (NF)
system, developed and patented by the Long Beach Water Department (LBWD), for the purpose of seawater
desalination. CH2M HILL served as a technical advisor to LBWD for both low pressure MF and high pressure RO
membrane process engineering support during construction of the Facility. Once operational, CH2M HILL
participated in a study entitled Ultraviolet (UV) Light and Chlorine Dioxide Seawater Pretreatment Systems for
Biogrowth Control and Pathogen Inactivation, funded in part by Proposition 50 grant from the California
Department of Water Resources. The study investigated, on both a bench‐ and demonstration‐scale, the
suitability of UV and chlorine dioxide for controlling biofouling of nanofiltration and reverse osmosis systems used
to desalinate seawater and to achieve virus inactivation requirements as mandated by the CA Department of
Health Services. CH2M HILL prepared a research work plan that served as the basis for testing conducted under
the study. A draft research plan was first developed with the input of a panel of outside technical advisory panel
and LBWD in a workshop and finalized following subsequent review by LBWD and the panel. CH2M HILL also
provided oversight during the testing, in part conducted by UCLA, and reviewed test data and reports.
OLGA VARIABLE SALINITY SURFACE WTP EXPANSION
EVALUATION, LEE COUNTY, FL
CH2M HILL conducted a study and preliminary design charged with finding the optimum source water and
treatment expansion option for an aging conventional surface water treatment. The study examined current and
anticipated water treatment and water supply regulations, raw water availability and storage options, treatment
options, and operation and maintenance costs. A benefit‐cost analysis helped identify the optimum solutions that
were then benched‐tested on the project site. Bench testing of new membrane filtration and reverse osmosis
processes was conducted on existing and potential new raw water sources to examine treatability and costs
effectiveness on multiple process options.
WEST PILBARA SWRO FEASIBILITY SITING AND COSTING
STUDY, WATER CORPORATION OF WESTERN AUSTRALIA
CH2M HILL conducted a feasibility study and concept design for the construction of
a desalination plant as part of the West Pilbara Water Supply Scheme. Using our
experience in cutting edge technologies, several options and processes were
evaluated to produce an innovative solution.
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The existing seawater in the proposed area was originally discounted due to the reportedly poor and variable
water quality near the existing intake facility. CH2M HILL reviewed the operation of this intake and found that an
improvement in water quality could be achieved through upgraded works and that
full replacement of the intake facility would not be required for several years.
CH2M HILL also looked at the treatment process selection as part of this study. The
pretreatment and desalination technologies were chosen based on an impartial
analysis of monetary and non‐monetary criteria. A decision making framework was
created which ranked and weighted all of the "success criteria" which were
important to the Water Corporation. This was combined with cost estimates to
determine the best outcome from a cost ‐ benefit perspective.
CH2MHILL created a generic design, complete with layout drawings and equipment sizing based on its global
design experience. This information will guide the Water Corporation in their land acquisition negotiations
EVALUATION AND OPTIMIZATION OF EMERGING AND
EXISTING ENERGY RECOVERY DEVICES FOR
DESALINATION AND WASTEWATER MEMBRANE
TREATMENT PLANTS, WATEREUSE FOUNDATION
CH2M HILL developed a computer based tool to evaluate current and emerging energy recovery devices based on
their performance, applicability and life cycle costs. The model covers all known and applicable commercially
available energy recovery device and all associated systems that impact it. The tool allows the user to develop an
optimum RO system design based on feed water quality and desired product water quality.
SEAWATER AND BRACKISH WATER DESALINATION
SITING, FEASIBILITY AND COSTING STUDY, NEW YORK
DEPARTMENT OF ENVIRONMENTAL PROTECTION, NY
CH2M conducted a feasibility and costing study for 200 mgd BWRO and 50 mgd
SWRO facilities for the City of New York. The project included the site planning,
conceptual design, and cost development of a 200 mgd brackish water RO
facilities treating a tidally influenced river water source and a 50 mgd seawater
facility with dual pressure filter pretreatment system and post treatment
facilities treating an open intake seawater source. The study examined site
constraints, raw water quality, treatment options, residuals disposal, capital
costs, and operation and maintenance costs.
CH2M as the technical member of the team that studied alternatives for development of up to 400 mgd of
emergency supply, including brackish and seawater desalination, as part of New York City’s long‐term water
supply strategy. CH2M was responsible for an in‐depth evaluation of brackish and seawater desalination at
various sites along the Hudson River and in New York Harbor, including the development of cost models for these
processes.
The study included an analysis of intakes, pretreatment, membrane treatment, energy recovery, post‐treatment,
and residual management technologies. Cost models were developed for the “highest cost and largest footprint”
design and the “lowest cost and smallest footprint” design at each location. A total of 14 cost scenarios were
developed for four sites, capacity options, and high and low cost alternatives.
CH2M then performed a statistical analysis of raw water quality, current and future water quality regulations,
recommendations for finished water quality parameters, and detailed analysis of treatment alternatives for
intakes, pretreatment, desalination technologies, post‐treatment alternatives, and brine return. Alternatives were
reviewed on a site‐by‐site basis to determine the most feasible processes for each potential site. The benefits and
costs for each alternative were evaluated and facility plans were developed for three desalination facilities (50
mgd, 200 mgd, and 400 mgd).
CH2M helped the Water
Corporation prove the
feasibility of Seawater
Reverse Osmosis as a
sustainable option.
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Other CH2M Desalination Project Examples
SEAWATER DESALINATION SITING, FEASIBILITY AND PILOT STUDY
HONG KONG WATER SUPPLIES DEPARTMENT, HONG KONG
CH2M designed and managed a 30‐month study to establish technical, engineering, environmental, and
budgetary information required to enable the Hong Kong Water Supplies Department to reach an informed
decision on how best to implement SWRO, in preparation for their 140 MLD facility.
The scope of the study included identifying prospective plant sites and conducting pilot trials to define RO design
requirements, identification of the most effective pre and post treatment processes, and development of capital
and operating cost estimates for one or more full scale facilities. The pilot program was comprehensive and
involved testing for a continuous 12‐month period at two separate locations (24 months total), selected to
represent the two types of marine water quality characteristics.
Three types of pretreatment were evaluated: granular media filtration, pressurized ultrafiltration and submerged
ultrafiltration. Three types of RO membranes were also evaluated: Dow FilmTec, Hydranautics, and Toray. Post‐
treatment blending with existing water supply was also evaluated to ensure smooth introduction of desalinated
water into the current supply. A complete capital and operating cost evaluation was included in the project.
SEAWATER DESALINATION FEASIBILITY STUDY
City of Port St. Lucie, Port St. Lucie, FL
CH2M conducted a planning study that investigated water supply alternatives to meet future water supply
demands for the City of Port St. Lucie including reverse osmosis desalination of seawater with an anticipated
capacity of up to 50 mgd. The scope of work included capital and operation and maintenance cost estimates for
the selected primary supply and treatment alternatives.
Seawater Desalination Plant
Melbourne Water Corporation, Australia
CH2M HILL provided Melbourne Water Corporation (MWC) with expert advice relative to their seawater
desalination plant. The planning, permitting, design and construction of the 120 mgd desalination facility, the
world’s largest RO plant at commissioning, included cost, environmental, and public acceptance issues that were
integral to the project’s success. We have worked closely with MWC and their consultants to resolve technical
issues regarding finished water quality, cost implications of low total dissolved solids (TDS) requirements, post‐
treatment alternatives for blending purposes, and public acceptance. Of particular sensitivity is TDS levels, boron
and bromide concentrations in the finished water while maintaining overall low corrosivity relative to the long
transmission lines.
Southern Seas Seawater Desalination Plant
Water Corporation of Western Australia
The Southern Seas Seawater Desalination Plant is the second large‐scale seawater desalination plant in Perth at
commissioning utilizes renewable energy to provide all the power for this 38 mgd facility. CH2M HILL, the owner’s
engineer, worked hand‐in‐hand with the utility to develop specifications, evaluate proposers, and then guide the
two shortlisted proposers through the full proposal process prior to award. In our role as owner’s engineer, we
have assisted Water Corporation to determine the ‘short list’ and to make recommendations on numerous
significant technical issues, which impacted the final design of the facility. The white papers created include
Advancements in SWRO; Post Treatment with Lime and Turbidity in Product Water; Oil and Grease Testing in
Seawater for RO Membranes; and RO Concentrate for Granular Media Filter Backwash.
Layyah, Khor Fakkan, and Kalba Seawater Reverse Osmosis (SWRO) Plants
Sharjah Electricity and Water Authority, United Arab Emirates
CH2M HILL served as the single source of responsibility for EPC services for turnkey delivery of three SWRO
treatment plants with a total capacity of 16 mgd and expandable to 32 mgd. The Layyah Seawater RO plant is
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located within the Arabian Gulf, which is known for seawater that is warm in temperature and high in salinity. To
ensure adequate pre‐treatment, the process design includes 3‐millimeter (mm) screening, dilution/ attenuation,
and two‐stage media filtration. Both Kalba and Khor Fakkan plants are located on the Indian Ocean coast of the
United Arab Emirates. Pre‐treatment at Khor Fakkan includes passive 3 mm screening and two‐stage media
filtration, while at Kalba pre‐treatment is achieved through UF membranes with upstream protection by passive
screening and pre‐filtration screens. Onsite pilot testing was conducted to verify UF performance and design
parameters.
SWRO Plant
Power Seraya, Singapore
In late 2005, Power Seraya engaged CH2M HILL to conduct a feasibility study and functional design for a new
SWRO desalination WTP at the Pulau Power Seraya Station. After the successful delivery of the feasibility study
and functional design and positive experiences working with the CH2M HILL team, Power Seraya requested that
we continue with the new SWRO desalination plant, utilizing a design‐build delivery model.
The Power Seraya Seawater Desalination Plant project is the world’s first full‐scale desalination plant to use large‐
diameter SWRO technology. CH2M HILL designers took advantage of the existing infrastructure at the neighboring
power station to maximize efficiency and cost savings while maintaining technical performance. The Power Seraya
plant produces two qualities of water: high‐grade service water at a rate of 2.4 million gallons per day (mgd) and
domestic drinking water at 0.26 mgd.
SWRO Pilot Plant
Marin Municipal Water District, California
CH2M HILL, in partnership with Kennedy Jenks Engineers, served as the technical advisor for planning, design and
operation of an 85,000 gpd seawater RO pilot plant for the Marin Municipal Water District, California. The pilot
plant comprised two screening systems (wedge wire and compressed disc), three separate pretreatment trains
two submerged hollow fiber membrane systems (MEMCOR CS MF and ZeeWeed 1000 UF) and conventional
(coagulation/flocculation/sedimentation/granular media filtration) and two full‐recovery seawater RO trains, each
containing ultra‐high rejection elements from three different suppliers. The purpose of the pilot study was
several‐fold: (1) to assess and compare performance of two screening systems and three pretreatment systems
(relative to downstream RO performance and fouling control), (2) demonstrate the ability of seawater RO to
produce finished water complying with EPA drinking water standards and local requirements for un‐regulated
trace contaminants, (3)characterize the RO concentrate relative to sewer discharge requirements and (4) prepare
costs for full‐scale (~40 mgd) desalination plant. The pilot plant was also used to gauge public opinion on the
taste of desalinated water through a public outreach event in which samples of desalinated water and the
MMWD’s current drinking water supply were made available for tasting. In addition to that for the pilot plant,
extensive source water sampling was conducted at three sites considered most suitable for full‐scale plant
construction in order to understand differences and their impact on full‐scale plant design. Results of the study
were used to assess feasibility, cost and public acceptance of SWRO desalination as a means of supplementing
and ‘drought proofing’ Marin County’s water supply.
Demonstration Project for Integrated Concentrated Photovoltaic‐SWRO System
Confidential Client, Middle East
CH2M HILL is under contract to assist in the development of a demonstration project that integrates a
commercially‐available concentrated photovoltaic (CPV) system for power generation with a commercial SWRO
desalination facility for drinking and industrial water production. The goal of the project is to demonstrate that a
seawater desalination system can be powered by renewable energy using solar energy. The CPV system will have
an output of 5‐10 megawatts while the SWRO system will be sized to produce approximately 5 mgd of desalinated
water. Under our contract, we will develop a scoping document that defines the capacity of the CPV/SWRO
system and the manner in which the two technologies will be integrated, prepare a conceptual‐level design and
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associated order‐of‐magnitude cost for the facility, identify and define parameters and issues associated with
scale‐up of the two technologies and conduct a market study to identify potential applications for the CPV/SWRO
system within the Middle East region.
Desalinated Water Quality Blending Study
San Diego County Water Authority, California
CH2M HILL conducted executed a water quality study for the San Diego County Water Authority (SDCWA) to
define the interaction between desalinated seawater containing varying levels of bromide to be produced by the
Carlsbad Seawater Desalination Facility with two different existing treated surface waters distributed by the
SDCWA throughout their service area. An initial review focused on the impact of desalinated water bromide on
degradation of chloramine residual and the impact of the desalinated water on blended water pH, alkalinity and
TOC. Results from the review were used to prepare a bench‐scale testing protocol that defined a comprehensive
series of experiments to both quantify chloramine reduction following blending at different ratios, desalinated
water bromide level, residence time between desalinated water chloramination and blending and point of re‐
chlorination. The results were used to establish design criteria for design and construction of additional chlorine
(and ammonia) boosting facilities at SDWCA’s Twin Oaks Valley WTP as necessary to maintain a target chloramine
residual in the blended and distributed waters.
Stock Island and Marathon SWRO Water Treatment Plants
Florida Keys Aqueduct Authority, FL
CH2M HILL successfully delivered the Authority’s two RO seawater WTPs on budget and schedule.
Since 1984, CH2M HILL has worked closely with FKAA and a multitude of stakeholder groups to seek ways to
improve the water systems in the Keys. We worked with FKAA to design and construct two RO desalination plants
that treat seawater to drinking water standards as an emergency source of water for the Keys; one is located on
Marathon to supply the Middle Keys and one is on located Stock Island to supply Key West and the Lower Keys.
CH2M HILL designed and provided engineering services during construction for these two seawater RO plants,
which have a total capacity of 3 mgd. We also recently provided design, permitting, bid phase, and construction
management services for a 6 mgd brackish water RO WTP in Florida City to improve the sustainability of the FKAA
water system.
Seawater Desalination Facility Planning Study
Massachusetts American Water Company, Hingham, MA
CH2M HILL conducted a planning study for a 500,000 gpd SWRO facility treating open intake surface seawater in
Massachusetts. The project included the site planning, conceptual design, and cost development of a seawater
facility with intake, dual pressure filter pretreatment system, and post treatment facilities. Study examined
current and anticipated water treatment and water supply regulations, site constraints, raw water quality,
treatment options, residuals disposal, capital costs, and operation and maintenance costs.
Menifee, Perris I and Perris II Desalters
Eastern Municipal Water District, Sun City, CA
CH2M HILL planned, piloted, designed and provided engineering construction services for the 2.5 mgd Menifee,
the 4.5 mgd Perris I, and the 3.5 mgd Perris II desalination facilities. All three facilities are located on the same
site and consist of a number of facilities including feed water flow control facilities, RO buildings, bulk chemical
storage and pumping areas, brine pump station, chlorine contact tank, and administration building. The RO
buildings house cartridge filters, RO feed pumps, two‐stage RO skids and permeate decarbonation facilities. The
RO systems are designed to accommodate the anticipated range of groundwater TDS (3,000 to 7,000 ppm).
Hydraulic turbochargers extract and transfer residual pressure energy from second stage concentrate to second
stage feed, reducing first stage feed pressure and flux as well as reducing energy use and first stage fouling
potential
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RO Water Treatment Plant
Coral Springs Improvement District, FL
The CSID RO Facility is designed with the flexibility to soften and remove organics from an existing freshwater
facility with the capability to treat brackish water in the future.
CH2M HILL designed a new 7.5‐mgd RO facility that treats existing Biscayne freshwater wells and is designed to
treat future brackish Floridan well water. The new facility replaces an existing lime softening treatment process at
the existing Coral Springs WTP site while using the existing finished water storage and pumping, wellfield, and
chlorination facilities.
The new treatment process includes sand strainers, cartridge filters and chemical pretreatment, bypass blending,
three RO trains, degasifiers, finished water clearwell, post‐treatment chemical stabilization, and transfer pumping
to existing finished water storage.
CH2M HILL helped the District find a cost‐effective and sustainable treatment solution that met project drivers
such as the need to replace aging water treatment infrastructure and ability to treat alternative Floridan brackish
water in the future.
Tuas Desalination Plant, Singapore Public Utilities Board, Singapore
PUB is committed to providing its customers with a safe and reliable supply of
high‐quality drinking water. To further increase the availability and reliability of
supply of desalinated water, PUB has undertaken a third seawater reverse
osmosis (SWRO) desalination plant at Tuas (TDP3) using a design‐build approach.
TDP3 will deliver potable water into PUB’s distribution network and will occupy a
3.5‐ha plot of land located at the far western side of the island (fronting Tuas
South Avenue 3), which currently separates the SingSpring and Tuaspring
desalination plants.
The seawater quality at the intake is critical in designing the overall treatment process. Key considerations for
design and selection of the pre‐treatment process include suspended solids, turbidity, TOC and potential for algal
blooms. Key considerations for design of the RO process include total dissolved solids, boron and temperature.
There is a concern that TSS levels may increase in the future as a result of possible future dredging activities
associated with various land reclamation projects in the vicinity of the Johor Straits and the TDP3 intake. With the
current TSS levels, DAF followed by membrane filtration is proposed as the preferred pre‐treatment process as
typical practice has been to provide solids removal (such as sedimentation or dissolved air flotation (DAF))
upstream of membrane filtration when TSS levels exceed around 20 mg/L in order to maintain high design fluxes
and recoveries.
The plant has been designed for an effective operating range of 6.6 to 36 mgd. The treatment process for the
desalination plant consists of DAF followed by a dual membrane system using ultrafiltration (UF) followed by 1st –
and 2nd‐pass RO, then by disinfection and post treatment chemical addition. The treatment process includes
treatment screening, intake pumping, intake chlorination, treated water tanks and pumps, outfalls, and ancillary
systems.
CH2M is providing preliminary design, preparation of a design‐build tender, EIA studies and security assessments,
engineering services during construction, and site supervision. Preliminary design activities include:
Data analysis provided by PUB regarding feed water quality and product water quality objectives;
Collection and analysis of additional water samples
Engage global technology experts within CH2M and, in collaboration with PUB, select appropriate treatment
processes
Collect best practice and lessons learnt from similar projects globally and in Singapore
Conduct workshops on process design, value engineering and layout options with PUB and key stakeholders
Cost estimating in conjunction with PUB and key stakeholders
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Develop the preliminary design for the preferred design option
Develop and optimize the intake and outfall design and locations
Develop and optimize the security conceptual designs
Develop Preliminary Design Report for PUB
Barka I, Phase 2 Seawater Desalination Plant, ACWA Power Barka, Oman
ACWA Power Barka (APB) appointed CH2M to act as Owner’s Engineer for a
new 12.5 MiGD Seawater Reverse Osmosis (SWRO) plant near its existing
Barka 1 integrated water and power plant (IWPP) facility.
The SWRO Plant will be developed on the site adjacent to Barka 1 IWPP and
will be powered with electricity supplied by Barka 1 IWPP. Feed seawater
for the Plant will be sourced from the seawater heat reject from Barka1 IWPP through seawater supply facilities.
The owner engineer scope also encompasses associated infrastructure including, water pipeline, permeate water
filling station and seawater supply.
The project scope includes seawater desalination for potable use via two pass reverse osmosis with microfiltration
pretreatment
CH2M Role/Responsibilities:
Design Engineering Review;
Review of EPC Contractor’s preliminary engineering documents
Review of EPC design development drawings, documents and other submissions review
Procurement document review
Quality assurance plan review
Equipment and material submittal and shop drawing review
Project Site Supervision;
Project management on behalf of ACWA Power
Review of detailed network schedules and preparing revisions and updates to the master schedule
Field construction management and inspection services
Periodic specialty inspections
Change management
Advise on field safety
Commissioning;
Pre‐commissioning Services
Witness Performance Testing
Closeout Services
MIRFA Independent Water and Power Project
Mirfa International Power and Water Company, Abu Dhabi, UAE
CH2M was appointed as Owner’s Engineer for the review of the 30MIGD
SWRO desalination plant by MIRFA International Power and Water Company
(Project Company formed between Abu Dhabi Water and Electricity Company
and GDF Suez).
When finished, and with the existing and new facilities fully integrated, MIRFA
IWPP will have a total power capacity of 1,600 MW and a seawater
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desalination capacity of 52.5 MIGD. Manufacturers of main SWRO equipment include Degremont ‐ RO equipment
supplier, Hydranautics ‐ membranes, Torishima – high pressure pumps and ERI ‐ energy recovery devices
CH2M Role/Responsibilities:
CH2M is responsible for review of Hyundai Engineering and Construction Company Limited (Degremont is their
subcontractor) desalination plant design including DAF, 2 pass media filtration, 2 pass RO (Ten 1st pass RO Trains,
three 2nd pass RO Trains).
Supply of Seawater Desalination Plants, Sharjah, United Arab Emirates
Sharjah Electricity and Water Authority
The Layyah SWRO plant is located within the Arabian Gulf, characterized by
seawater that is high in temperature and salinity and subject to algal blooms
(red tie). To ensure adequate quality RO feed water, pre‐treatment includes 3‐
millimeter (mm) screening, dilution/attenuation, and two‐stage media
filtration. The Kalba and Khor Fakkan plants are located in the Gulf of Oman,
where seawater quality is less challenging.
The Layyah SWRO Desalination Plant produces 6 mgd of permeate from
Arabian Gulf seawater (TDS: 42,000 mg/L). Subject to frequent Red Tide
events, the plant uses a state‐of‐the‐art pre‐treatment system including using pre‐treatment consisting of
coagulation, flocculation, DAF and Dual‐Stage Pressure Sand Filters to mitigate the fouling effects of Red Tide.
The Khor Fakkan SWRO Desalination Plant also produces 6 mgd of permeate from seawater withdrawn from the
Gulf of Oman using pre‐treatment consisting of coagulation, inline flocculation and Dual‐Stage Pressure Sand
Filters. The Kalba SWRO Desalination Plant, located near Fujairah, produces 3 mgd of permeate from seawater
extracted from the Gulf of Oman using a pre‐treatment scheme consisting of coagulation, inline flocculation and
NORIT Seaguard UF Membrane Filtration.
CH2M Role/Responsibilities:
CH2M served as the single source of responsibility for EPC services for delivery of two seawater RO treatment
plants with a total capacity of 15 mgd, expandable to 32 mgd. CH2M was responsible for design, procurement,
mechanical/electrical design, guarantee of water output, guarantee of electricity consumed per m3 of produced
desalinated water.
Pre‐treatment at Khor Fakkan included passive 3‐mm screening and two‐stage media filtration, while at Kalba pre‐
treatment was achieved through UF membranes with upstream protection by passive screening and pre‐filtration
screens. Onsite pilot testing was conducted to verify UF performance and design parameters.
The Layyah and Khor Fakkan sites used dual‐stage media filters for treatment of the raw seawater prior to
reaching the high‐pressure SWRO system. The Layyah site incorporated a DAF system before the media filters for
enhanced removal of particulates, and better protection against accidental oil spills and seasonal algae blooms.
Instead of conventional media filters, the Kalba desalination plant used high‐performance ultrafiltration
membranes that are specifically designed for SWRO pre‐treatment applications.
All three plants incorporate the highest efficiency energy‐recovery devices available on the market. These
innovative technologies result in the production of desalinated seawater at lower capital and operating costs than
conventional systems.
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Wonthaggi Seawater Desalination Plant, Melbourne, Australia
Melbourne Water Corporation
The Melbourne Water Corporation (MWC) selected CH2M to provide expert
advice relative to the upcoming seawater desalination plant being procured
through the Department of Sustainability and Environment for MWC. Because
of the magnitude of the project, one of the world’s largest RO plants—cost,
environmental and public acceptance issues were integral to the project’s
success.
CH2M Role/Responsibilities:
CH2M has worked closely with MWC and their consultants to resolve technical
issues regarding finished water quality, cost implications of low total dissolved solids requirements, setting of
boron and bromide water quality limits, post‐treatment alternatives for blending purposes, and public
acceptance. Of particular sensitivity is TDS levels, boron and bromide concentrations in the finished water while
maintaining overall low corrosivity to long transmission lines and distribution systems, and minimization of
customer impacts from boron and TDS.
PowerSeraya Seawater Reverse Osmosis Plant, Jurong Island, Singapore
PowerSeraya
The PowerSeraya Seawater Desalination Plant Project is the world’s first full‐
scale desalination plant to use a large‐diameter SWRO technology.
The desalination plant is located on the site of PowerSeraya’s existing Pulau
Seraya Power Station, a 3,100 MW power plant. The desalination plant is
located on Jurong Island, a unique cluster of the major oil, petrochemical,
and specialty chemical industries of Singapore. The desalination plant
features granular media filtration pre‐treatment and a two‐pass RO system.
CH2M Role/Responsibilities:
In late 2005, PowerSeraya engaged CH2M in a consultancy assignment to
conduct a feasibility study and functional design for a new SWRO desalination plant at the Pulau Seraya
PowerStation. CH2M took advantage of the power station’s existing infrastructure of cooling water intake,
discharge out falls, and onsite tank age to co‐site the new desalination plant at the power station, resulting in an
estimated 25 per cent savings in capital costs for new infrastructure. CH2M also served as the EPC contractor
responsible for the design, procurement, construction, and commissioning of the new SWRO desalination plant in
Singapore.
Southern Seawater Desalination Plant, Binningup, Australia
Water Corporation
The Southern Seawater Desalination Plant, located in Binningup, was
constructed in 2 stages – each capable of producing 36 mgd of water per
year. The first stage began producing and supplying drinking water to the
Water Corporation’s Integrated Water Supply Scheme in March 2012 and
the plant is currently producing approximately 72 mgd. The plant’s energy
requirements are offset by energy purchased from various renewable energy
generators, including wind and solar farms near Geraldton.
CH2M Role/Responsibilities:
CH2M is the owner’s engineer and independent third‐party reviewer responsible for:
Independent technical advice during the Alliance Establishment Stage
III‐23
Advice and technical input to Water Corporation during workshops and design presentations during the
Alliance Development Stage
Preparation of a tender evaluation report to inform and assist Water Corporation with the shortlisting of four
proponents from a field of six during the Alliance Establishment Stage
Advice and guidance to select the final shortlist of two proponents to proceed to the Alliance Development
Stage
Preparation of proponent questionnaires and interview questions
Technical memos and key advice during the Alliance Establishment Stage
Independent third‐party reviews for all process design including, pre‐treatment, RO, and post‐treatment
processes
Independent third‐party reviews for geotechnical, structural, durability, mechanical, civil, electrical, and
instrumentation and controls. Subcontractors were engaged and managed by CH2M to perform these
independent third‐party reviews.
National Centre of Excellence in Desalination – Detailed Design, Western Australia,
Murdoch University
The detailed design of a world‐class desalination pilot‐scale testing and
research facility. The Facility has been designed to be a flexible, modular in
design to allow testing of multiple innovative and emerging technologies, it will
be highly instrumented providing advanced data acquisition.
Water supplied from brackish and seawater bores, mixing is through a flexible
tank arrangement and delivery to multiple points around the site. Chemical
cleaning and neutralization system with disposal to sewer and Managed Aquifer
Recharge of brine and product water.
CH2M Role/Responsibilities:
CH2M carried out the detailed design and procurement management for the center with capacity to deliver feed
water for use in multiple pilot scale technologies. A detailed smart piping model was prepared using Autodesk
Revit MEP to provide clarity of location and interactions of pipework. CH2M also used its contacts to find and
encourage sponsorship of the facility through vendors providing equipment for use in the center.
Feed waters to the facility for testing and research come from two extraction bores located on site. The bores
provide freshwater and seawater directly to the tank farm location. Construction of the bores was supervised by
CH2M during the conceptual phase of the project. The bore water is delivered to a tank farm consisting of three
(3) feed water tanks and a service water tank to allow mixing of constitute parts to achieve a wide range of water
characteristics. Brine and product water collected from pilot trial area can be discharged to a re‐injection bore via
a managed aquifer recharge system.
The feed water is distributed around the facility by three (3) delivery mains. Service water is delivered through a
fourth main.
There are nine (9) Tie‐In points available for pilot plants around the facility, power and control cables are also
available from three test bay supply boxes.
Data from the pilot plants is measured via an instrumentation skid, the skids include multiple instruments
measuring flow, pH, conductivity, ORP, temperature etc.
III‐24
QGC Value Engineering Independent Review, Queensland, Australia
QGC
QGC are in the process of ramping up gas production in line with their
program to begin exporting LNG. The ability to manage the treatment and
disposal / re‐use of the associated water is critical to ensure gas production
targets are met. QGC required certainty that the water management and
treatment facilities will be sufficient in terms of capacity, availability and
reliability.
The four water treatment plants include an RO system as a critical process
unit, were reviewed at various stages of operation, commissioning,
construction and design. At the commencement of the engagement, the
online treatment plants (two of four) were operating well below design capacity due to water quality and
operational constraints.
The two treatment plants under design and commissioning at the time of CH2M’s review (i.e. review underway
prior to operation) had a combined design capacity of 48 mgd.
CH2M Role/Responsibilities:
CH2M completed a value engineering independent review of QGC’s water treatment system that will receive coal
bed seam water from the QGC Queensland Curtis liquefied natural gas (QCLNG) development in the Surat Basin,
Queensland.
Reynolds Desalter Expansion
Sweetwater Authority
The Sweetwater Authority is expanding the capacity of the Richard A. Reynolds
Groundwater Desalination Facility. Built in 1999, the facility’s current
production capacity is 5 million gallons per day (mgd) from six wells. This
consists of 4 MGD reverse osmosis product water blended with 1 mgd of water
treated only for iron and manganese removal via pyrolusite filters.
The expansion will double the production to 10 mgd, with the addition of five
new wells and three new RO treatment trains. The new RO trains are to
include turbochargers for energy savings and flux balancing. The upgrades
also include the implementation of upgraded system controls and automation
enhancements to the existing and new groundwater wells. 15,700 feet of new pipelines are being installed to
convey groundwater to the new treatment facility and the concentrate control disposal pipeline is being
relocated. In addition, the RO clean in place and neutralization systems are being replaced.
CH2M Role/Responsibilities:
CH2M is owners engineer for the expansion with the following responsibilities:
Design and construction phase services of the iron and manganese treatment system added in 2009.
Environmental Services for CEQA/NEPA Compliance
Preliminary design of the expansion
Final Design of the Desalter Expansion including Construction Phase Services
Well drilling, equipment and buildings
SCADA and Automation Coordination
III‐25
Menifee and Perris I Desalters, Eastern Municipal Water District
Eastern Municipal Water District
The Menifee and Perris I Desalter Facilities treat groundwater extracted from the
Menifee and Perris sub‐basins, and produce 7.5 mgd of desalinated water
(product water), with Menifee producing 3 mgd and the Perris I facility 4.5 mgd.
The product water is then blended with 1.5 mgd of brackish groundwater for a
total treated water flow of 9 mgd. By pumping and treating brackish
groundwater, the facility reduces salinity within the San Jacinto Basin and helps
the District reduce their dependence on imported water from the Colorado River
and State Project water systems. Salinity reduction is achieved through the use of
RO, a pressure‐driven membrane process that retains the salts using a semi‐permeable membrane.
The Desalter Facility is located in Sun City, California. The facility’s process building houses the two desalters in
separate but adjacent areas. Each area includes cartridge filters, high pressure pumps and RO trains, as well as a
chemical cleaning system. Facilities for neutralization of spent cleaning solutions are also housed within the
building but in a separate room. Enclosed chemical storage and feed systems are provided for scale inhibitor,
sulfuric acid, caustic, and onsite hypochlorite generation. Outside facilities include decarbonators to remove
excess carbon dioxide from the RO permeate; a chlorine contact basin to provide for virus inactivation of the
combined RO product and bypassed well water; and a brine pump station. Following disinfection and storage, the
treated water is delivered to the water distribution system and combined with other treated water supplies. The
facility also has a separate administration building with a control and operations room, conference room and rest
rooms.
Each RO train at the Perris I Desalter includes a PEI hydraulic turbocharger to reduce energy consumption by
recovering residual energy in the RO concentrate. After entering the brine pump station, the RO concentrate is
pumped into the Santa Ana Regional Interceptor brine line for ultimate discharge to the Pacific Ocean.
The Menifee Desalter was commissioned in 2001 and the Perris I Desalter in 2007. Both desalters have operated
nearly continuously since commissioning. CH2M provided operational assistance during commissioning and start‐
up of the Perris I Desalter and follow‐on tailored training of desalter facility operations staff. We also assisted
District staff in conducting testing to increase the recovery of the desalters from 70 to 75 percent, resulting in
additional treated water production and, more importantly, reduced cost for RO concentrate disposal.
CH2M Role/Responsibilities:
CH2M developed the project design, performed structural, mechanical, process and electrical engineering,
construction management and prepared environmental documents & permits.
J. Robert Dean WTP
Florida Keys Aqueduct Authority, FL
For decades, South Florida has relied on the Biscayne Aquifer, a thin lens of fresh
water 30 to 100 feet below the surface, for its drinking and irrigation water. But
an ever‐growing population, combined with long spells of dry weather, prompted
Southwest Florida Water Management District to limit the amount of fresh water
drawn from the Biscayne Aquifer. The desalination facility was added to the
Florida Keys Aqueduct Authority’s (FKAA's) existing 23‐mgd treatment plant to tap
into brackish waters of the Upper Floridan Aquifer, located approximately 1,200
to 1,300 feet below the surface. The RO system is designed to desalt feed water
with salinities from about 5,000 to 8,000 mg/L TDS.
CH2M Role/Responsibilities:
CH2M designed, permitted, and provided construction management services for the project. Additionally, we
provided the control programming services. The design of the RO facility included supply wells and raw water
III‐26
transmission mains; pretreatment; brackish water RO membrane treatment; disinfection; post‐treatment and
blending; and concentrate disposal transmission and injection wellhead facilities.
The RO facility is designed to be fully integrated with the existing lime softening treatment process at the plant,
which treats "fresh" Biscayne Aquifer groundwater. The blended lime softening and RO desalted product waters
from the two treatment processes continue to meet FKAA’s potable water production and water quality goals.
The new facilities include 6 mgd of membrane permeate capacity.
The RO system consists of four 1.5‐mgd, two‐stage process trains, each with dedicated feed pumps and energy
recovery hydraulic turbochargers. The turbochargers transfer excess energy from the waste concentrate flow
streams to boost the feed pressure to the second stage RO membranes. This not only minimizes energy
consumption but better balances the flows through the system and improves RO performance.
“CH2M has a long‐standing history of providing high‐quality professional engineering and multi‐discipline utility
services to support the Florida Keys Aqueduct Authority's water resources needs, including several desalination
projects. …They are very technically competent and have cost‐effectively and efficiently managed and delivered
our projects. I highly recommend CH2M for any organization looking for engineering services to carry them into
the future.” —James C. Reynolds, PE, Executive Director, FKAA
TAB IV Specialized Expertise of Team Members TAB IVSpecialized Expertise of Team Members
IV-1
The CH2M Team and Their Roles on this Project
CH2M team members were selected on the basis of their knowledge and familiarity with Collier County, their
industry expertise and applicable experience in their assigned role, and their ability to commit to deliver on
this project. As noted in Tab III, CH2M and our partner, Water Science Associates (WSA), will provide all the
services necessary to successfully complete this project. The organizational chart on the following page shows
the highly qualified team members we have chosen to support the County and their selected project roles.
Successful Experience Working Together on Previous Projects
The CH2M team was assembled to combine recognized industry experts with highly skilled local staff who
bring the requisite technical skills and institutional knowledge of the County, South Florida and regional
Reverse Osmosis (RO) facilities. Many of our management team and task leads are located in CH2M’s Naples
and Ft. Lauderdale offices. As such, our team members have a history of collaborating together on projects
similar to the County’s RO Conceptual Design project. Our team members work closely on a regular basis on
dozens of project and have developed seamless working relationships. Examples of our team’s experience
working together on similar projects is show in Exhibit IV-1 below.
EXHIBIT IV-1 CH2M team members have a long history of working together on projects relevant to the
County’s Scope of Services
REPRESENTATIVE RELEVANT PROJECT KEY TEAM MEMBER PARTICIPATION
Green Meadows Water Treatment Plant in Lee County Joe Elarde, Bill Beddow, Nick Easter, Mike Witwer,
Larry Van Dyk
Bonita Springs RO WTP Joe Elarde, Bill Beddow, Nick Easter, PY Keskar
Marco Island RO and Membrane Filtration projects Joe Elarde, Bill Beddow, GJ Schers, Nick Easter,
Mike Witwer
North Springs Improvement District RO WTP Joe Elarde, GJ Schers, Nick Easter, Cristina Ortega-
Castineiras, Mike Witwer, Larry Van Dyk
WTP projects, Seminole Tribe Joe Elarde, GJ Schers, Cristina Ortega-Castineiras,
Mike Witwer,
North Miami Beach WTP GJ Schers, Cristina Ortega-Castineiras, Mike
Witwer, Larry Van Dyk
Marina East Variable Salinity Project, Singapore Jim Lozier, Steve Alt, Mike Hwang
Team Member Resumes
The CH2M team has extensive similar experience, unparalleled technical expertise, an understanding of the
kind of responsive, high-quality services the County demands, and stands ready to begin this project now! Our
Team Organization Chart, Exhibit IV-2 shows the group of experienced professionals CH2M is committing to
the County’s Variable TDS RO Conceptual Design project. Our team is composed of the optimal combination
IV-2
of industry leading expertise with local, knowledgeable and highly skilled personnel, resulting in a project that
will be delivered in a technically superior and highly responsive manner.
Resumes for the CH2M team members that will be assigned to the County’s project, including subconsultants
can be found at the end of this section. Short bios for key team leaders follow the organization chart.
Subconsultant Letters of Intent
A Letter of Intent from our subconsultant team member, Water Science Associates, can be found at the end of
this Tab.
EXHIBIT IV-2
Team Organization
Chart
IV-3
CH2M offers Collier County a Team of Project Leaders with a Proven
Record of Successfully Implementing RO projects in Florida
Our Team will be led by Joe Elarde, PE, who will serve as CH2M Project
Manager and Task Leader for Tasks 1 and 3.
Joe is a nationally recognized specialist in membrane technologies—more than 18 years of
water treatment planning and design experience, and 20 years of membrane process
experience working on projects that include study, design, permitting, construction,
startup, and operation of membrane filtration, nanofiltration, brackish water RO, and
seawater desalination facilities in the U.S. and globally, including many in Florida. Joe has a
long history of performing services similar to those detailed in the County’s RFP, notably in South Florida.
Representative projects include serving as the Lead Process Engineer on the New York Dependability and
Pilbara variable desalination feasibility studies, Senior Process/Mechanical Designer for Lee County’s Green
Meadows new 16 mgd RO and Ion Exchange WTP. In addition, he was the Senior Consultant and Project
Engineer for a new 7.5 mgd RO WTP North Springs Improvement District, Coral Springs, FL; was involved in the
RO WTP Design/Build Upgrade and Expansion for Bonita Springs Utilities, FL; and Lead Process Designer and
Resident Engineer for RO WTP Design/Build Upgrade and Expansion for the City of Fort Myers, FL.
Key Personnel Qualifications to Serve in their Assigned Roles on the County’s RO Project
TEAM MEMBER
Jim Lozier, PE
QUALIFICATIONS FOR THIS ROLE
Specializes in the application of membrane processes for water
treatment, desalination and water reuse, as well as associated
preliminary and post-treatment processes, including coagulation,
clarification, oxidation, and various chemical treatments
Lead Process Engineer on several variable salinity desalination projects
including Marina East Variable Salinity Desalination WTP in Singapore.
Published more than 60 articles and book chapters on the use of
membrane processes in drinking water production, desalination, and
water reuse
In his position as the Global Desalination Technology Leader for CH2M, is
responsible for the development of the CH2M knowledge base and
application of new and innovative technologies.
ROLE
QA/QC
YEARS OF EXPERIENCE
35
REGISTRATIONS
PE: FL (#46999)
EDUCATION
MS, Civil Eng.; BA, Biology
TEAM MEMBER
Steve Alt, PE
QUALIFICATIONS FOR THIS ROLE
Specialist in membrane treatment, both ultrafiltration/microfiltration
(MF) and reverse osmosis (RO) with experience in application, full scale
design and pilot testing of membrane processes on water sources.
Process designer of several desalination facilities including the Marina
East Variable Salinity Desalination WTP in Singapore.
Author of more than 10 membrane based water treatment research
papers/presentations
Prior to CH2M, experience as a process and applications engineer for a
major membrane manufacturer followed by serving as a consulting
engineer designing membrane based water and waste water treatment
systems.
ROLE
QA/QC
YEARS OF EXPERIENCE
20
REGISTRATIONS
PE: CA
EDUCATION
BS, Chemical Engineering
IV-4
=
TEAM MEMBER
GJ Schers, PMP
QUALIFICATIONS FOR THIS ROLE
Expertise in design of advanced water treatment processes, including ion
exchange, ozonation, advanced oxidation, activated carbon filtration,
membrane filtration, and ultraviolet light disinfection as well as
conventional treatment processes like coagulation, softening,
clarification, sand filtration, pumping systems, chemical feed systems,
washwater recovery, and sludge treatment and dewatering systems
Experience with Collier County as a Project Technical Lead for the design
and bidding for a new raw water valving and metering station at the
South Regional Water Treatment Plant
Serving as Senior Technologist/Owners Representative for the Seminole
Tribe of Florida’s CIP Program focused on improvements to the Brighton
and Big Cypress water treatment plants, which utilize reverse osmosis
membrane and degasification technologies
ROLE
Treatment Lead; Task
Leader, Tasks 2 & 5
YEARS OF EXPERIENCE
25
REGISTRATIONS
PMP (PMI, #428825)
EDUCATION
MS, Civil Eng.; BS, Civil Eng.
TEAM MEMBER
Michael Hwang, PE
QUALIFICATIONS FOR THIS ROLE
Environmental engineer with 10 years of experience in conceptual and
preliminary design of water and wastewater treatment facilities utilizing
both conventional and membrane treatment technologies
Instrumental to the development and refinement of membrane costing
modules in CH2M’s costing tool CPES™
Process Engineer supporting the Marina East Variable Salinity
Desalination WTP.
Experience includes development of an operations and monitoring
guidance manual for a RO concentrate wetlands pilot system, as well as
alternatives evaluations and optimizations strategies for RO facilities
ROLE
Concentrate Lead
YEARS OF EXPERIENCE
10
REGISTRATIONS: PE: CA
EDUCATION
MS & BS, Environ. Eng
TEAM MEMBER
Kirk Martin, PG (WSA)
QUALIFICATIONS FOR THIS ROLE
Experienced in managing complex integrated water resource programs
with expertise in water supply development, groundwater hydraulic
interpretations, and fresh/saline water relationships in coastal aquifers
Completed over 300 reports on regional and local geology/hydrology in
Florida
Provided the primary technical direction on development of over 500
mgd of raw water supply and over 100 mgd of aquifer recharge and
wastewater disposal projects
Served as the lead technical resource for the Collier County Wellfield
Reliability Improvements and Expansion Program that included the
planning, evaluation, design, permitting, construction, and operations of
the County’s water supply facilities.
ROLE
Hydrogeology Lead; Task 4
Lead
YEARS OF EXPERIENCE
30
REGISTRATIONS: PG: FL
EDUCATION
Graduate Geophysics; B.S.,
Geology
IV-5
TEAM MEMBER
Mike Witwer, PE
QUALIFICATIONS FOR THIS ROLE
Experienced with bench and pilot testing design, construction and
operation including clarification, media filtration, membrane processes,
ion exchange, ozonation, and disinfection at water and advanced
wastewater treatment facilities
Served as a process and mechanical engineer in the design of facilities
including clarification, microfiltration, reverse osmosis, chemical
injection and disinfection processes
Project experience includes Process Lead, Project Technologist, and Pilot
Plant Manager for the Green Meadows Water Treatment Plant
Expansion in Lee County
Lead Project Technologist for the Seminole Tribe of Florida Water
Treatment Plant Evaluations and Expansion Alternatives
ROLE
Equipment/Layout; Task
Leader, Tasks 7 & 8
YEARS OF EXPERIENCE: 21
REGISTRATIONS:
PE: FL (#69262)
EDUCATION
ME & BS, Environmental
Engineering
TEAM MEMBER
Richard Giani, PE
QUALIFICATIONS FOR THIS ROLE
State certified instructor for water and wastewater operation classes in
various states
Supported numerous AWWARF projects related to lead corrosion in
drinking water, including effects of partial lead service line replacement
and effects of chlorine and chloramine disinfectant
Current Chair of AWWA’s Distribution Water Quality Committee and
chair for developing the latest addition of AWWA’s industry manual of
practice for Internal Corrosion Control Treatment for Drinking Water
Distribution Systems
Background includes Drinking Water Compliance Coordinator for CH2M;
Manager for the City of Portland’s Water Quality Division; and Manager
of the Drinking Water Division of the District of Columbia Water and
Sewer Authority.
ROLE
Corrosion Control Lead
YEARS OF EXPERIENCE
27
REGISTRATIONS
Water and Wastewater
Operation Classes: FL
EDUCATION
BS, Environmental Studies;
AAS, Biotechnology
Support Staff
TEAM MEMBER
PY Keskar, PhD, PE
QUALIFICATIONS FOR THIS ROLE
Recognized expert in electrical and instrumentation and control systems
design and implementation with significant expertise in I&C systems
design, including distributed control systems, PLCs, and SCADA systems
Performed numerous energy and process optimization studies for clients
nationwide, including Bonita Springs and Palm Beach County, Florida
Authored a significant number of papers in the fields of electrical power
and control systems engineering, which have been presented at ISA,
IEEE, EPRI, and TAPPI conferences and have appeared in the transactions
of ISA and IEEE; two of the papers received ISA national level awards
ROLE
Electrical/I&C
YEARS OF EXPERIENCE: 46
REGISTRATIONS
PE: FL (#29288)
EDUCATION
PhD, MS, BE, Electrical
Engineering
IV-6
TEAM MEMBER
Larry Van Dyk
QUALIFICATIONS FOR THIS ROLE
Experience includes both design and construction phases of many
different categories of buildings, including process plants
Design and field experience in new construction projects, as well as
refurbishment and extensions to existing buildings
Tasks performed include preparation of all structural design plans and
reports; attends coordination meetings for structural issues; and
coordinates structural issues and schedule reviews
Lead Structural Designer for the Wastewater Treatment Plant Expansion
for North Springs Improvement District in Coral Springs, FL.
ROLE
Structural
YEARS OF EXPERIENCE:
52
EDUCATION
Witwatersrand College of
Engineering
TEAM MEMBER
Adam Ahmad, PE
QUALIFICATIONS FOR THIS ROLE
Skilled in civil engineering site and roadway design/mapping and
surveying, computer information science, management, cartography,
and graphic design
Diverse experience includes serving as the project manager for the
Seminole Tribe of Florida Long Range Transportation Plan, Collier Area
Transit’s Facility Design Guide and the preparation of over a hundred
million dollars in grant applications including TIGER grants
Design Engineer responsible for development and coordination of the
Collier County Master Mobility Plan
ROLE
Civil
YEARS OF EXPERIENCE: 10
REGISTRATIONS
PE: FL (#72472)
EDUCATION
BS, Civil Engineering
TEAM MEMBER
Ralph Myers, CGC
QUALIFICATIONS FOR THIS ROLE
Experience of managing delivery and estimating the construction of
water, wastewater treatment and conveyance systems
Specializes in hard bid and design-build management, estimate
preparation, budgeting, purchasing, planning, scheduling, subcontract
management and close out of construction projects.
Proficient in equipment, material and subcontract procurement
Former Owner/General Contractor who has delivered successful projects
for over 30 years in hard bid and design-build in Florida
ROLE: Cost Estimating
YEARS OF EXPERIENCE: 31
REGISTRATIONS
Certified Gen. Contractor- FL
EDUCATION
Allstate Construction
College- Florida
WSA Letter of Intent
Associates
13620 Metropolis Avenue, Suite 110, Fort Myers, FL 33912 O 239.204.5300 F 866.398.2426
June 10, 2016
Ms. Sue Diuk
CH2MHILL
4350 West Cypress Street
Suite 600
Tampa, Florida 33607
Letter of Intent: Collier County CCNA Solicitation 16-6639 Variable TDS Reverse Osmosis
Conceptual Design Project
Dear Sue,
Water Science Associates is pleased to be part of the CH2MHILL team on the Collier County Variable TDS
Reverse Osmosis Conceptual Design Project and pleased to provide this Letter of Intent indicating our
participation.
Please don’t hesitate to contact me if you have any questions or need additional information. Yours
Sincerely,
W. Kirk Martin, P.G.
Principal Scientist
Water Science Associates, Inc.
Mobile: 239.218.1043
Office: 239.204.5301
Email: kirk@wsaconsult.com
Key Team Member Resumes
Joe Elarde, PE
Representative Project Experience
Senior Process/Mechanical Designer, Green Meadows WTP
Expansion Pilot Study, Master Plan, Design and Construction, Lee
County Utilities, Fort Myers, FL. Mr. Elarde served as the senior
process designer for the pilot study and master planning of an
expansion of the existing 9-mgd WTP. Piloted processes include
low-pressure reverse osmosis for softening multiple fresh water
sources, reverse osmosis for desalinating brackish well water, ion
exchange for organics and iron removal, and strainers for sand and
silt reduction. The master planning work evaluated the piloted
process options to determine the most robust and cost effective
option for expansion, as well as the expanded facility capacity. Mr.
Elarde served as the senior process/mechanical designer of the
selected 16 mgd RO and Ion Exchange WTP. The new facility will
use reverse osmosis for desalinating brackish well water in parallel
with cation and anion exchange used to remove iron, hardness and
organics from a surficial aquifer fresh water source. The estimated
$35M facility is part of a $70M project with completion in 2018.
Lead Process Designer, RO WTP Energy Recovery and Membrane
Upgrades Evaluation and Design/Build Improvements, Bonita
Springs Utilities, Bonita Springs, FL. Lead process/mechanical
designer for the evaluation and design of a new energy recovery
system and membrane replacement of a 6.6-mgd brackish water
desalting RO WTP. The project included evaluation of multiple
combinations of energy recovery and membrane element options.
The project saved more than $150,000 annually in power cost.
Process Designer, RO WTP Design, Construction and
Commissioning, North Springs Improvement District, Coral
Springs, Florida. Process designer and commissioning lead for a
new 7.5 mgd RO WTP. The new facilities include the RO facility,
sand strainers, cartridge filters, chemical pretreatment, bypass
blending, degasifier systems, biological odor control, post
treatment chemical stabilization, and transfer pumping to existing
finished water storage.
Lead Process/Mechanical Engineer, Marco Island NWTP
Membrane Filtration and Improvements Design and Services
During Construction, City of Marco Island, Marco Island, FL. Mr.
Elarde was the process/mechanical lead and client liaison for the
study, design and construction services of a new 6.7-mgd
membrane filtration system and other facility improvements. The
project scope included an evaluation of existing water treatment
facilities, planning and design of a new 6.7-mgd membrane
filtration facility. The final design included a new membrane
Role on Project
Project Manager; Task Leader – Tasks 1 &
3
Years of Experience
21
Relevant Experience
Nationally recognized specialist in
membrane technologies—more than
18 years of water treatment planning
and design experience, and 20 years
of membrane process experience
working on projects that include
study, design, permitting,
construction, startup, and operation
of membrane filtration, nanofiltration,
brackish water reverse osmosis, and
seawater desalination facilities all over
the U.S. and internationally, including
many in Florida
Strong background in membrane
piloting, research, data analysis,
design, startup, and operation
Conducted several membrane
filtration, softening, brackish water
desalting, and seawater desalting
feasibility studies
Education
MS, Environmental Engineering,
University of Illinois, 1998
BS, Civil Engineering Technology,
University of Illinois, 1995
Professional Registration
Professional Engineer: Florida
(#59309)
JOE ELARDE, PE
building, membrane filtration system, transfer pumping system, new chemical storage and feed
facilities, and lime softening rehabilitation.
Project Engineer, Brackish Water and Seawater Desalination Facility Planning Studies, NYDEP, New
York, NY. Mr. Elarde conducted a feasibility and costing study for 200 mgd BWRO and 50 mgd SWRO
facilities New York. The project included the site planning, conceptual design, and cost development of
a 200 mgd brackish water RO facilities treating a tidally influenced river water source and a 50 mgd
seawater facility with dual pressure filter pretreatment system and post treatment facilities treating an
open intake seawater source. The study examined site constraints, raw water quality, treatment
options, residuals disposal, capital costs, and operation and maintenance costs.
Project Manager and Process Lead, RO WTP Energy Recovery and Membrane Upgrades Evaluation and
Pilot Study, City of Melbourne Utilities, Melbourne, FL. Project manager and process lead for the
evaluation and pilot study for membrane replacement and chemical/energy optimization study of a 5-
mgd brackish water desalting RO WTP. The project included evaluation of multiple combinations of
membrane elements and energy recovery options, as well as the evaluation of other WTP upgrades to
reduce chemical and power cost including feed pump modification, installing adjustable frequency
drives, eliminating acid, adjusting scale inhibitor dose and type, adjusting RO system pretreatment, and
alternative concentrate treatment with ozone.
Project Manager, Olga Surface WTP Expansion, Lee County Utilities Department, Fort Myers, FL.
Project manager and process lead for a study and preliminary design charged with finding the optimum
source water and treatment expansion option for an aging conventional surface water treatment. The
examined current and anticipated water treatment and water supply regulations, raw water availability,
treatment options, and operation and maintenance costs. Bench testing of new membrane filtration and
reverse osmosis processes was conducted on existing and potential new raw water sources to examine
treatability and costs effectiveness on multiple process options.
Project Engineer, Green Meadows WTP Expansion, Lee County Utilities Department, Fort Myers, FL.
Project engineer for a study and preliminary design that determined the optimum expansion option for
an aging water treatment facility. Study examined raw water availability, treatment options, and
operation and maintenance costs. Bench testing of process options was conducted on potential new raw
water sources to examine treatability and costs effectiveness of multiple process options.
Lead Process Designer, RO WTP Design/Build Expansion, Bonita Springs Utilities, Bonita Springs, FL.
Senior technology consultant and process designer for the expansion of a 6.6-mgd brackish water
desalting RO WTP to 10 mgd. The project included a new wellfield, expanded pretreatment processes,
feed pumps, RO trains, installation of energy recovery on the new and existing RO trains, and expanded
post-treatment processes.
Senior Technology Consultant, Membrane Softening WTP Design/Build/Operate, Ave Maria Utilities,
Ave Maria, FL. Senior technology consultant during the design, commissioning and continued operation
of a new 2.5-mgd (expandable to 6 mgd) membrane softening WTP. Performed process QC during the
design of the new facility and worked on-site during the commissioning of the facility. Led tasks that
included verification of membrane system performance, control system design, plant operations,
operator training, system troubleshooting, and data collection and analysis.
Lead Process Designer/Resident Engineer, RO Water Treatment Plant (WTP) Design/Build Upgrade
and Expansion, City of Fort Myers, FL. Lead process designer for the upgrade and expansion of the 12-
mgd (expandable to 20 mgd) brackish water desalting RO WTP. The existing membrane facility was
upgraded from membrane softening of shallow wells by NF to the desalting of deep brackish wells by
RO. The upgrade and expansion included the design and installation of 4-mgd of additional RO
membrane capacity, as well as upgrades to the raw water wells, membrane feed pumps, and
degasification systems required by the conversion to RO.
Bill Beddow, PE
Representative Project Experience
Project Manager/Principal-in-Charge, Green Meadows WTP
Expansion, Lee County, FL. Design, permitting and services during
construction for a 16-mgd RO/IX treatment facility. The new facility
will use RO for desalinating brackish well water in parallel with
cation and anion exchange used to remove iron, hardness, and
organics from a surficial aquifer fresh water source. The project
provided the full evaluation of treatment alternatives, piloting and
design for a new WTP desalinating a brackish well water source and
blending with other treated waters within the facility and with other
nearby treatment facilities.
Engineering Manager, RO WTP and Production and Deep Injection
Wells (Design-Build), Bonita Springs Utilities, FL. Design-build
project involving a new $36 million RO WTP. The new facility is
located at the site of the existing lime softening WTP and was
designed for an initial capacity of 6 million gallons per day (mgd).
The facility was designed to be expandable to 12 mgd. Raw water is
supplied to the plant from eight brackish water wells tapping the
Lower Hawthorn formation of the Upper Floridan aquifer, raw water
transmission main, and two DIWs. Because of a critical need for
additional water, the project was delivered using a design-build
delivery approach that saved BSU approximately 8 months of
construction time and allowed BSU to meet its 2003 peak water
demands. Also engineer-of-record for the Class I industrial injection
well, which was used to dispose concentrate water from the RO
WTP.
Engineering Manager, East Water Reclamation Facility (WRF)
(Design-Build), Bonita Springs Utilities, FL. Design-build project that
included the design and construction of a new 4-mgd advanced
WRF, expandable to 8 mgd. At the time of construction, it was the
largest membrane bioreactor facility of its type in Florida. Residuals
management was designed to meet future regulations and is
accomplished by means of a rotary drum dryer system producing
Class AA biosolids. Odor control systems include tower biofilters.
Also served as the engineer-of-record for the Class I municipal
injection well that was designed to dispose excess reclaimed water
during extended wet weather periods.
Principal-in-Charge/Officer-in-Charge, Water Treatment
Improvement Projects Involving RO and Membrane Filtration (MF)
Water, City of Marco Island, FL. Principal-in-charge of several WTP
expansion and improvement projects for the City. Projects included
a new water storage facility, high-service pumping upgrades, odor
control repairs, and water treatment process evaluations.
Role on Project
Principal in Charge
Years of Experience
23
Relevant Experience
Specializes in water resources and
water treatment including public
supply wellfields, water treatment
facilities, deep injection wells (DIWs),
aquifer storage and recovery (ASR)
systems, water use permitting, and
construction management
Served as engineering manager for
three water and wastewater design-
build facilities totaling more than $120
million, including a new 6-million-
gallon-per-day (mgd) reverse osmosis
(RO) water treatment plant(WTP), 8-
mgd RO WTP expansion, and new 4-
mgd membrane bioreactor water
reclamation facility (WRF).
Education
ME, Environmental Engineering,
University of Florida, 1994
Graduate Certificate in Hydrologic
Sciences, 1992
B.S., Environmental Engineering
Professional Registration
Professional Engineer: Florida
(#0052581)
BILL BEDDOW, PE
Principal-in-Charge/Engineer-of-Record, Class I Deep Injection Well, FKAA, Cudjoe Key, FL. Technical
lead and principal-in-charge for design, permitting, and services during construction of a 3,000 foot Class
I Deep Injection well for the Cudjoe Regional Water Advanced Water Reclamation System. This
wastewater effluent disposal well was built to higher Class I standards to even though no USDW was
present in this location.
Principal-in-Charge, Water Treatment Plant (WTP) Expansion Program, City of Fort Myers, FL. Led the
City’s water treatment expansion program, which involved the conversion of the City’s raw water supply
from surface water to the Floridan aquifer. Project included the design and construction of membrane
feed pumps, reverse osmosis (RO) skids, process mechanical, electrical and instrumentation upgrades,
degasifiers, post treatment chemical feed system, 18 Floridan aquifer production wells, Class I deep
injection and monitor well system, and site improvements.
Project Manager, Wellfield Quality, City of Fort Myers, FL. Led an investigation examining the City’s
wellfield water quality and its compatibility with its 12-mgd membrane softening water treatment plant.
The focus of the investigation was to identify the wellfield water quality changes that have led to
premature membrane failure and to find solutions that still utilized the new membrane WTP. The
investigation provided the City with ways to optimize the current raw water supply and treatment
process, and identified new raw water sources more compatible with membrane water treatment
process.
Senior Consultant, Wellfield Protection Services, FKAA, Florida City, FL. Project involved wellfield
protection services at the J. Robert Dean WTP. As senior consultant, provided QC review, technical
guidance, data interpretation on the project, and review during construction.
Senior Consultant, RO DIW and Floridan Supply Wells at J. Robert Dean WTP, FKAA, Florida City, FL.
Project involved an RO DIW and Floridan supply wells at the J. Robert Dean WTP. Served as a senior
consultant. Advised project team on injection well testing and well completion decisions and
interpretations, as well as provided review during construction.
Project Manager/Engineer-of-Record, Brackish Water Wellfield, City of Fort Myers, FL. Design,
permitting, and construction of a new 16-mgd brackish water wellfield. Helped the City obtain a 20-year
water use permit for the new wellfield. The permitting included development of future water demand
projections, providing impact assessments, and investigation of new water source alternatives.
Project Manager, Public Supply Wellfield (Design-Build), City of Fort Myers, FL. New public supply
wellfield for the City’s RO WTP. This fast-tracked project included seven new 14-inch-diameter deep
production wells withdrawing water from the Upper Floridan Aquifer. Project included two test wells
used to verify water quality and to confirm production capacity. The test wells were also used to
supplement the City’s water supply during a critical water shortage and were later converted to
production wells.
Jim Lozier, PE
Representative Project Experience
Project Manager/Lead Process Engineer, RO Plant, City of
Scottsdale, AZ. Project manager and lead process engineer for pilot
testing, preliminary and final design of a 2.8-mgd RO plant to
improve the quality of brackish groundwater for the southern
service area of the City of Scottsdale. The RO plant will improve
quality by reducing TDS, hardness and nitrate levels in a series of
groundwater wells, the water of which has received prior
treatment by packed column air stripping to remove
trichloroethylene. The facility will consist of fine (10-um) screening,
cartridge filtration, chemical conditioning, high pressure pumping
and reverse osmosis. The product water from the RO plant will be
stabilized through the addition of caustic soda blended with
existing stripper effluent prior to disinfection. Responsibilities
include management of all pilot and design phase activities,
including: design of pilot plant, development of pilot plant
protocol; oversight of pilot plant operation, data collection and
analysis; preparation of pilot report; pre-selection of large
diameter (18 inches) RO membrane elements and pressure vessels;
development of preliminary design criteria and order of magnitude
costs options for feedwater pretreatment and RO system; and
development of detailed design plans and specifications.
Lead Process Engineer/Assistant Project Manager, RO Plant, Fort
Pierce Utilities Authority, FL. Lead process engineer and assistant
project manager for a reverse osmosis (RO) pilot study conducted
for the Fort Pierce Utilities Authority, Florida. Obtained data for the
design of a 3-mgd (expandable to 18-mgd) RO facility to treat
groundwater that is high in hardness, dissolved solids, and
dissolved organic compounds, and to treat waste residuals for
surface or deep well disposal. Responsible for and supervised
preparation of test plans and monitoring software; data collection
and analysis; training of plant operating and data processing
personnel; report preparation; unit set-up, shakedown, and start-
up; and supervision of client operating personnel.
Senior Technical Consultant, Perris II Desalter, Eastern Municipal
Water District, CA. Senior process consultant for design of a new
5.0-mgd RO plant for the Eastern Municipal Water District,
Riverside County, California. The plant will be fed by new brackish
groundwater wells containing TDS ranging from 1,500 to 3,000
mg/L, with variable and high levels of silica, calcium, bicarbonate
and iron. The desalter will comprise an iron and manganese
removal system, chemical conditioning including acid and scale
inhibitor addition, cartridge filtration, two 2.25 mgd RO trains
Role on Project
QA/QC
Years of Experience
35
Relevant Experience
Specializes in the application of
membrane processes for water
treatment, desalination and water
reuse, as well as associated
preliminary and post-treatment
processes, including coagulation,
clarification, oxidation, and various
chemical treatments
Internationally recognized authority
on membrane technologies for
potable water treatment,
desalination, and water reuse
Published more than 60 articles and
book chapters on the use of
membrane processes in drinking
water production, desalination, and
water reuse
Serves as member of Project Advisory
Committee for several Water Research
Foundation, WateReuse Research
Foundation, and Water Environment
Research Foundation projects on
membrane bioreactors for wastewater
reclamation
Education
MS, Civil Engineering, University of
Arizona, 1983
BA, Biology, State University of New
York, 1975
Professional Registration
Professional Engineer: Florida
(#46999); Arizona (#46341)
JIM LOZIER, PE
including high pressure pumps and hydraulic turbocharger energy recovery devices, product water
decarbonator and treated water chemical addition (chlorine, ammonia, caustic and corrosion
inhibitor), concentrate pump station, chlorine contact tank and high service pumping; and
administration and process equipment buildings. Responsibilities included review and approval of
preliminary design report, plans (drawings) and specifications at 30-, 50- and 90-percent design, and
presentation of process design materials at client workshops.
Senior Technical Advisor for Design of the Perris I Desalter 5.0-mgd RO Plant for the Eastern
Municipal Water District, Southern California. The plant includes three new wells tapping deep
groundwater having variable TDS ranging from 3,000 to 7,000 mg/L and high silica, associated
transmission mains, preliminary treatment of acid and scale inhibitor addition and cartridge
filtration, two 2.25 mgd RO trains including high pressure pumps and hydraulic turbocharger energy
recovery devices, product water decarbonator and chemical feeds (chlorine, ammonia, caustic and
corrosion inhibitor and process equipment building. Responsibilities included review and approval
of preliminary design report, plans (drawings) and specifications at 30-, 50- and 90-percent design,
and presentation of process design materials at client workshops.
Senior Technical Consultant, Northern Advanced Water Treatment Plant (NAWTP), NAVFAC, Camp
Pendleton, CA. Senior technical consultant for design and construct of a new 5-mgd RO WTP
comprising groundwater conveyance pipelines from existing wells to treatment facility, RO
pretreatment (acidification, antiscalant addition and cartridge filtration), high pressure pumps, RO
trains and post-treatment (chlorination and stabilization) to remove iron, TDS and TOC from
groundwater. RO concentrate undergoes oxidation and pyrolusite filtration to remove iron before
deep well injection. Responsible for review of design documents at 30-, 60- and 90-percent,
including piping and instrumentation diagrams, hydraulic profile, process flow diagram, equipment
calculations and specifications.
Lead Process Engineer, Beenyup Advanced Water Recycling Plant, Water Corporation, Perth,
Australia. Lead process engineer for design/build of the 10 mgd, expandable to 20-mgd. The facility,
consisting of coarse and fine screening, hollow fiber ultrafiltration, reverse osmosis, degasification
and ultraviolet disinfection, is currently under construction in the Perth metropolitan area. Treating
secondary effluent, the facility will produce a finished water meeting all potable standards for
groundwater replenishment through direct injection. In addition to the main treatment processes,
the plant includes chemical storage and dosing facilities for pre-formed chloramines for membrane
biofouling control, sulfuric acid and antiscalant for scale prevention and caustic addition for finished
water pH adjustment. During design phase, responsible for preparation (for each design) of plant
mass balance, RO design projections, antiscalant dosing, specifications and bid documents (with
assistance by the commercial team) for MF skids and modules and RO skids as well as review and
oversight on all other chemical design calculations, pumping and bulk storage calculations and MF
and RO power usage estimates.
Lead Process Engineer, Northwest River Water Treatment Plant, Chesapeake, VA. Lead process
engineer for pilot testing for two reverse osmosis (RO) pilot studies. Both studies use RO: one for
reduction of disinfection byproduct precursors and control of salinity intrusion in surface water and
the other for demineralization of a highly brackish (8,000 mg/L) deep groundwater. Results from the
studies were used to design a new 10-mgd RO plant to treat conventionally-treated brackish surface
water and a 4-mgd brackish groundwater RO plant, both located at the Northwest River WTP to
meet current and future drinking water regulations. Responsibilities included design and
construction oversight of pilot facilities; preparation of test plans, data collection and analytical
requirements; selection of RO membranes; management of pilot system start-up and operation;
training of operating personnel; monitoring and review of test data; and preparation of project
reports. Also served as QA/QC for design of both RO facilities.
Steve Alt, PE
Representative Project Experience
Process Lead, Reverse Osmosis Energy Recovery, WateReuse
Energy Recovery Device Project. Process lead on the creation of
an Excel-based tool that guides the user on the cost and payback
period of implementing five different Energy recovery devices to
reverse osmosis trains. The tool permits utilities, engineers, and
plant operating staff to provide cost-based decisions on which, if
any, commercially available energy recovery device to implement
in their desalination facilities. User inputs water analysis and other
parameters, the tool runs an RO projection, creates a mass balance
and determines the capital cost and O&M cost of the RO system.
Lead Process Designer, Reynolds Groundwater Desalter Expansion
(Sweetwater Authority). Lead process designer for the expansion
of this potable water plant including the addition of 5 mgd RO,
replacement of cleaning and neutralization systems, and
modifications to existing RO trains. New RO trains have been
designed with turbocharger energy recovery devices. Process flow
diagram, detailed equipment specifications, and the mechanical
layout of the equipment in the RO building.
Senior Process Engineer Camp Pendleton Northern Advanced
Water Treatment Plant (NAWTP). Executing the process design of
the 6.7 mgd potable groundwater treatment system. System
includes low pressure reverse osmosis to remove iron, TDS and
TOC from groundwater. Concentrate undergoes oxidation and
pyrolusite filtration to remove iron before groundwater injection.
Detailed piping and instrumentation diagrams, hydraulic profile,
process flow diagram, equipment calculations and specifications.
Mechanical layout of RO building.
Process Lead, Goldsworthy Desalter, Torrance, CA. Process lead
on a feasibility study for the expansion of the Goldsworthy
Desalter. Study investigated the costs of doubling the capacity of
the facility and included a present worth analysis and payback
period for adding turbochargers to the RO trains.
Process Engineer, Chino II Desalter, Chino Basin Desalter
Authority,. Prepared plans and specifications for a 6 mgd RO
System to treat groundwater for potable use. Provided
construction oversight of the facility, including submittals, shop
and site inspections, and commissioning/acceptance testing
coordination. Assisted with plant startup and troubleshooting of
scale development in the post treatment system.
Process Engineer, Yucaipa Valley Water District, Yucaipa Valley
Regional Water Filtration Facility. Execution of bench scale
Role on Project
QA/QC
Years of Experience
20
Relevant Experience
Specialist in membrane treatment,
both ultrafiltration/microfiltration
(MF) and reverse osmosis (RO) with
over 20 years of experience in the
application, full scale design and pilot
testing of membrane processes on a
variety of water sources.
Process design and commissioning of
multiple waste water reclamation
systems using MF -> RO -> UVAOP
(ultraviolet light advanced oxidation).
Author of more than 10 membrane
based water treatment research
papers/presentations
Lead process designer of the
WaterReuse Energy Recovery Device
Tool
Well rounded knowledge base of
membrane technology from an
unusual employment history. Eight
years of experience as a process and
applications engineer for a major
membrane manufacturer followed by
twelve additional years as a consulting
engineer designing membrane based
water and waste water treatment
systems.
Education
BS, Chemical Engineering, University
of California San Diego
Professional Registration
Professional Engineer: California
STEVE ALT, PE
nanofiltration study that evaluated seven different membranes for DBP precursor and TDS removal.
Oversight of pilot testing of Pall ultrafiltration and Koch SR2 nanofiltration membranes.
Owner’s Engineer, Tuas 3 (PUB Singapore). As owner’s engineer, led CH2M team meetings with PUB
early in the project to discuss the treatment process, lessons learned on other seawater desalination
projects, and PUB preferences. Creation of specifications, piping and instrumentation diagrams and
layout for the microfiltration and reverse osmosis membrane treatment systems for design build tender
of 36 MGD potable water production facility. Plant energy evaluation and optimization. Review of DB
proposals and recommendation to PUB. TDP3 will include intake and outfall structures, dissolved air
flotation, membrane filtration, two-pass reverse osmosis and post-treatment.
Owner’s Engineer, MIRFA Independent Water and Power Project, Abu Dhabi. Design review of a 30
MIGD seawater reverse osmosis facility. Review of equipment sizing calculations, piping and
instrumentation diagrams, mass balances and mechanical arrangement drawings.
Process Reviewer, Victorian Desalination Project, Melbourne, Australia. A temporary reassignment to
Melbourne Australia to assist with the design of a 120 mgd open intake seawater desalination plant.
System P&ID and layout review. Created a process model that calculates the plant energy usage at
various water temperatures, feed water salinities and membrane life. Worked with the Operations and
Maintenance group to optimize plant operation and costs. Pilot plant commissioning and oversight.
Toured full scale Gold Coast and Sydney desalination plants.
West Basin Municipal Water District (WBMWD), Seawater Desalination Pilot Project. Analysis and
operations oversight of R&D effort to determine optimum operational parameters for the treatment of
seawater for potable use using MF and Ultrafiltration (UF) → RO. Managed on-site optimization studies
for pre-screening equipment, MF and UF and pretreatment to RO, an evaluation of low energy and high
rejection seawater membranes, and evaluation of a 2nd Pass RO for Boron reduction. Creation of
contractor bid packages including specification of equipment and process drawings for additional
equipment such as second pass RO unit high rate granular media filter unit. Worked with vendor to
install data collection system that allows remote data access and remote alarm notification to reduce
equipment down time. Evaluation of operation during severe red tide event. Data analysis and report
generation for funding agencies including NWRI and the US Bureau of Reclamation.
Senior Engineer, WBMWD, Seawater Desalination Demonstration Project. Senior engineer overseeing
the process design. Prepared plans and specifications for 300 gpm open intake desalination
demonstration plant consisting of UF followed by split partial two pass RO. Plant design included system
to inject preformed chloramines for biological fouling control. Construction oversight and start up
engineer. Data normalization and operations supervision. Design of an ocean water aquarium that
operates with source water from both the ocean and the reverse osmosis concentrate from the
demonstration plant. The aquarium enables the study of aquatic life in waters of elevated salinity.
Gerardus J. (GJ) Schers, PMP
Representative Project Experience
Senior Technologist; CIP Program; Seminole Tribe of Florida.
Providing expert water treatment technology services, as the
owner’s representative, for the improvements to the Brighton,
Immokalee and Big Cypress water treatment plants. These plants
utilize reverse osmosis membrane and degasification technologies
to treat ground waters which are highly mineralized and contain
elevated levels of hydrogen sulfide and color.
Senior Technologist; Deerfield Concentrate Disposal
Improvements; Deerfield Beach FL. Developing alternative methods
for transferring membrane concentrate streams to a deep injection
well. The solution involves an in-line booster pump station to
replace the existing wet-well station and was based on extensive
chemical sampling and modeling which determined that air-gap
aeration caused metal precipitation in the wet well, disposal
pipeline and injection well. The work also includes plant
optimizations to minimize the risk of future precipitation.
Senior Technologist; 4-Log Virus Treatment Compliance Study;
North Miami Beach FL. Identifying best methods to comply with the
Florida groundwater rule at the existing Norwood water treatment
plant containing three separate treatment trains involving lime
softening, nanofiltration and reverse osmosis treatment
technologies. The work will include bench test to define breakpoint
chlorination for this particular groundwater, chlorine demand and
decay tests and system distribution simulation test.
Reviewer; Timberlake OH WTP Upgrade Project. Providing
independent review services for an expansion to an existing iron and
manganese removal treatment system utilizing green sand pressure
filtration. The expansion encompasses the addition of two
nanofiltration membrane trains, including ancillary facilities, to
provide softening to the hard source water.
Prior to CH2M
Project Technical Lead; Membrane Replacement Study; Boynton
Beach, FL. Evaluated current condition of 12 years old
nanofiltration membrane elements at the existing 10 MGD East WTP
and analyzed element alternatives when/if re-membraning becomes
necessary. The work included assessment of membrane
performance and water quality data, and review of the membrane
autopsy report and existing operations. Software models were used
to analyze the performance of the overall membrane system and
verify results with the finished water quality goals at the WTP.
Follow-up discussions were held with membrane vendors.
Role on Project
Treatment; Task Leader – Tasks 2 & 5
Years of Experience
25
Relevant Experience
Specialized in sanitary engineering
with 25 years of experience in
design and management of water
treatment facilities and associated
infrastructure.
Expertise includes hydraulic, civil,
and process engineering during all
project stage
Responsible for the design of
advanced water treatment
processes, including ion exchange,
ozonation, advanced oxidation,
activated carbon filtration,
membrane filtration, and
ultraviolet light disinfection as well
as conventional treatment
processes.
Membrane expert with over 12
years’ experience in treating
Floridan Aquifer water
Education
MS, Civil Engineering, Delft
University of Technology,
Netherlands, 1991
BS, Civil Engineering, Delft
University of Technology,
Netherlands, 1989
Professional Registration
Project Management Professional
(PMI, No. 428825)
GERARDUS J. (GJ) SCHERS, PMP
Project Technical Lead; Valving and Metering Header; Collier County, FL. Finished the design and
bidding for a new raw water valving and metering station at the South Collier Regional Water Treatment
Plant in Collier County. The new facilities will be located above ground level on a slab-on-grade
reinforced concrete slab and will include magnetic flow meters and modulating valves to control the
backpressure and flow in each raw water pipeline.
Project Technical Lead; System 1A Reverse Osmosis WTP Expansion; Broward County, FL.
Implemented the planning phase of an alternative water supply system consisting of a 6 MGD brackish
groundwater Reverse Osmosis WTP expansion for Broward County. Completed activities include
wellfield siting, and investigations, permitting activities for the concentrate deep injection well,
preliminary engineering of the surface facilities of the production and injection wells and some
conceptual sizing of the treatment plant components.
Task Manager; RO System Refurbishment and Replacement; City of Venice, FL. Reviewed deliverables
of a Design/Build project to provide Refurbishment and Replacement (R&R) at the 4.4 MGD brackish
groundwater Reverse Osmosis WTP. Work included the replacement of RO feed pumps, RO trains and
cleaning/chemical facilities and replacement/upgrade of the SCADA system and incorporated a series of
process and controls enhancements to improve the water treatment process. The project was
successfully closed out by mid-2015.
Project Manager; Water Facilities Program; Cape Coral, FL. Implemented the City’s Water
Improvement Program, including the planning, design and construction of the following projects:
24 MGD ‘Green Field’ North Reverse Osmosis (RO) WTP. Design activities included field testing of
groundwater source to optimize location, depth, and capacity of production wells. The facilities
included new production wells, well surface facilities, raw water transmission systems, water
treatment plant utilizing RO and degasification processes, drinking water transmission mains, and
injection well for disposal of RO concentrate. Innovative design concepts were applied to ensure
water production can be maintained while raw water quality slowly degrades. The WTP was
designed for 24 MGD.
18 MGD Expansion of the Southwest Reverse Osmosis (RO) WTP. The designed facilities included
new brackish groundwater production wells, well surface facilities, new raw water collection and
transmission system, and hydraulic expansion of the plant utilizing RO. The design included specific
studies for the disposal of the RO concentrate, for odor emission and control, and included a full
standby power facility with two 2,250 kVa generators.
Project Technical Lead; Ion Exchange Study; Town of Davie, FL. Completed a project to identify the
origin of foul odor from a 4-mgd anion exchange system for color removal, develop alternatives to fix
the problem and implement the preferred alternative. The work included visits to other ion exchange
systems to review operational conditions, water quality data review and discussions with resin and
system integration vendors. Phase 2 involved the implementation of the short-term solution involving
the installation of a carbon dioxide system, and verification of its performance through bench-scale
testing. Phase 3 included the technical assistance during the start-up. The ion exchange system is now
operating successfully and has resolved the problem with foul odor.
Task Manager; Tippin WTP Filter Rehabilitation; City of Tampa, FL. Provided design and construction
oversight of the filter rehabilitation project for the 120 MGD Tippin WTP, which is the largest surface
water treatment plant in Florida. Activities included the verification and modification of the repair
techniques proposed by the design/build contractor and by the filter floor vendor Leopold, third party
construction inspection, and final signoff documentation of the construction.
Cristina Ortega-Castineiras, PE
Representative Project Experience
Project Engineer, City of North Miami Beach Water Treatment
Plant Master Plan, NMB Water, City of North Miami Beach, FL.
Involved in assessment of existing water treatment plant which
includes lime softening, nanofiltration and reverse osmosis
treatment trains. Performing evaluation of alternatives to expand
the treatment capacity to accommodate future demands.
Conducting cost-benefit comparison between lime softening and
nanofiltration.
Project Engineer, Sawgrass Water Treatment Plant (WTP)
Nanofiltration/Reverse Osmosis (NF/RO) Pilot, City of Sunrise, FL.
Pilot project that involved the construction, planning and testing
phases of the project. The purpose of the Sawgrass WTP NF acid
reduction pilot test was to determine the degree that sulfuric acid
usage at the plant could be reduced without negatively affecting
plant product water quality or damaging the existing NF
membranes and to estimate the overall chemical cost savings.
Conducted the data analysis and drafted the test report.
Project Engineer, West Water Treatment Plant Concentrate
Disposal Scaling Evaluation and Improvements, City of Deerfield
Beach, FL. Conducted evaluation of scale deposits on the NF and RO
concentrate disposal piping. Currently working on the design of
recommended improvements.
Project Engineer, Southwest WTP Groundwater Rule (GWR) Water
Treatment Improvements, City of Sunrise, FL. Involved in bench
testing and free chlorine residual monitoring investigations. The
results of these tests were used to determine Southwest WTP
facility improvements needed to meet the 4-log virus
removal/inactivation requirement of the Florida Department of
Environmental Protection (FDEP) so-called “Bird Rule” and the
Environmental Protection Agency’s (EPA’s) GWR based on free
chlorine disinfection. The proposed GWR improvements for the 2-
million-gallon-per-day (mgd) Southwest WTP included upgrade
plans for lime softening and filtration facilities to obtain 2-log virus
removal “credit,” as well as preliminary facility improvements
planned to obtain 2-log virus inactivation by free chlorine
disinfection.
Project Engineer, North Springs Improvement District Water
Treatment Plant, FL. Assisted with development of the facility
Operation and Maintenance Manual, and miscellaneous sampling to
develop a well field management plan.
Role on Project
Treatment
Years of Experience
7
Relevant Experience
Water process engineer with
experience in water/wastewater
engineering projects, including work
in assessment, design, pilot testing,
permitting, and master planning of
water and wastewater infrastructure
Involved in the planning, design, and
assessment of multiple membrane
and lime softening facilities
throughout Florida
Extensive experience with pilot
testing of membrane softening
technologies
Education
ME, Environmental Engineering;
BS, Civil Engineering;
BS, Environmental Engineering
Professional Registration
Professional Engineer: FL #77632
CRISTINA ORTEGA-CASTINEIRAS, PE
Process Consultant, WTP Lime Softening System Improvements, Town of Hillsboro Beach, FL. Acted as
process consultant during the construction and startup of a new lime softening WTP. Worked with
contractor, lime softening system supplier, controls subcontractor, and utility to verify process
performance and optimize operation. Compiled the facility Operation and Maintenance Manual.
Project Manager/Design Manager/Construction Manager/Water Process Engineer, Public Works
Department Capital Improvements Program, Seminole Tribe of Florida, FL. Served as project manager
for multiple water and wastewater treatment plant improvement projects at the Seminole Tribe of
Florida Brighton, Big Cypress, Immokalee, and Hollywood Reservations, including the following:
• Brighton WTP RO Train Improvements: Design manager and construction manager for a plant
upgrade project focused on the reverse osmosis treatment process. Project was completed within
budget, with no change orders.
• Brighton WTP Process Improvements: Conducted cost-benefit analysis of plant process upgrades,
rehabilitation preliminary design and provided piloting support services. Managed RO pilot project.
• New Hollywood WWTP and Deep Injection Wells: Managed the design of a new wastewater
treatment plant and deep injection wells system.
• Immokalee WWTP Improvements: Design manager for improvements to an existing wastewater
treatment facility.
• Immokalee WTP Expansion: Project manager for LPRO plant upgrade and expansion.
• Hollywood WTP Expansion and Improvement: Project manager and Construction Manager for plant
expansion and improvement project that added a new 1 MGD RO train to the existing facility. Also
managed design of improvements to plant’s chemical storage and conveyance systems.
• Big Cypress WTP Improvements: Managed the design of improvements to the plant, including
upgrades to the chemical storage, pumping and conveyance, post-treatment processes, RO trains
and CIP systems. Conducted an evaluation of post-treatment alternatives and provided
recommendations for short and long-term post-treatment improvements.
• Assisted in various capacities with the development of the Hollywood and Immokalee Water and
Wastewater Master Plans.
Project Engineer, Preston/Hialeah WTPs GWUDI Upgrades, Miami-Dade Water and Sewer
Department, Miami, FL. Led efforts on development, planning, and permitting of a NF/ ultraviolet (UV)
water treatment pilot study for the Hialeah-Preston GWUDI upgrades. Supervised construction and
installation of piloting facilities. Responsible for daily operations, as well as laboratory testing and data
collection/analysis. Compiled and digested information gathered during the testing period, in order to
produce a final summary of findings; and drafted the final Study Report.
Also involved with drafting specifications and drawings for the chemical building, including double
containment piping, chemical storage tanks, and coating materials. The Hialeah-Preston GWUDI
upgrades consist of a new water treatment facility with capacity for 165 mgd, which incorporates the
following processes: pre-filtration using media filters, sand separation, cartridge filtration,
nanofiltration, UV disinfection, and chlorine disinfection via onsite generation of chlorine gas.
Michael Hwang, PE
Representative Project Experience
Project Engineer, RO Concentrate Regulating Wetlands Pilot,
Goodyear, AZ. Developed operations and monitoring guidance
manual for a reclamation pilot wetlands system consisting of seven
wetland cells arranged in four train configurations to treat RO
concentrate at the Bullard Water Campus.
Project Engineer, Alternatives Evaluation for New Water Treatment
Plant, Freeport, TX. Reviewed Brazos River water quality and bench
testing data to support the evaluation of treatment alternatives for a
new 30 mgd plant. The first alternative assumed clarification
followed by pressurized MF/UF and the second alternative assumed
submerged UF.
Staff Engineer, Preliminary Design for the Expansion of Leo. J.
Vander Lans Advanced Water Treatment Facility, Long Beach, CA.
Assisted in the preliminary design of the expansion of the Leo. J.
Vander Lans Advanced Water Treatment Plant from 3 mgd to 6 mgd.
Assessing optimization strategies for operation of existing MF and
RO facilities.
Project Engineer, City of Glendale Zone 4 Groundwater Treatment
Plant and Conveyance Pipeline, Glendale, AZ. Performed water
quality review of ion exchange product and GWTP finished water to
verify removal rates arsenic and nitrate during startup and
commissioning.
Project Engineer, Chaparral Water Treatment Plant Bench and Full-
Scale Testing, Scottsdale, AZ. Performed bench testing and
developed a full scale test protocol to evaluate aluminum
chlorohydrate (ACH) as an alternative coagulant to ferric sulfate to
reduce the rate of short-term fouling in the City's Zenon ZeeWeed
500 UF system.
Project Engineer, Chaparral Water Treatment Plant Membrane
Integrity Improvements, Scottsdale, AZ. Performed preliminary
design of plant modifications needed to enable operation of the
Zenon ZeeWeed 500 UF in both feed-and-bleed mode (existing) and
batch mode to address the loss of membrane integrity.
Project Engineer, Yuma Desalting Plant Long-Term Operational
Alternatives Study, Yuma, AZ. Performed conceptual design and
preliminary cost estimates for 10 long-term operating alternatives
for the Yuma Desalting Plant to mitigate the imbalances between
supply and demand in the Colorado River Watershed.
Project Engineer, Reclaimed Water Master Plan, Chandler, AZ.
Performed an evaluation of the sources of system wastewater flows
Role on Project
Concentrate
Years of Experience
10
Relevant Experience
Environmental engineer with
experience in conceptual and
preliminary design of water and
wastewater treatment facilities
utilizing both conventional and
membrane treatment technologies
Expertise in hydraulic modeling for
water distribution systems
Specialized computer skills include RO
projection software, AutoCAD,
MicroStation, geographic information
system (GIS), H2OMAP® Water,
InfoWater®, InfoSewer, Hydra,
EPANET, and Goldsim®
Education
MS, Environmental Engineering, University
of California, Berkeley
BS, Environmental Engineering, University
of Southern California
Professional Registration
Professional Engineer: CA
MICHAEL HWANG, PE
and their relative contributions to TDS of reclaimed waters produced by Octotillo, Airport, and Lone
Butte water reclamation facilities.
Project Engineer, Water and Wastewater Reuse Master Plan and Programming, Chandler, AZ.
Completed a water and wastewater reuse master plan project for a confidential industrial client to
accommodate the expansion of existing production facilities.
Project Engineer, Water Distribution System Study at Marine Corps Air Station (MCAS), Yuma, AZ.
Updated the InfoWater hydraulic model and performed steady state and extended period simulations to
evaluate existing and future system demands. Recommendations were made based on identified
deficiencies in the water distribution system.
Staff Engineer, Groundwater Recharge Facilities Model, Orange County, CA. Assisted in developing a
groundwater-recharge operation model in GoldSim for approximately 1,200 acres of recharge spreading
facilities.
Staff Engineer, Regional Brine-Concentrate Management Study, Southern California. Helped conduct a
survey of the brine-concentrate management facilities, identify regulatory issues and trends, review
secondary and emerging constituents of concern, evaluate brine concentrate disposal options, and
identify potential brine-concentrate pilot/demonstration projects for further review.
Staff Engineer, Golden State Water Company Facility Master Plans, Southern California. Work included
field testing, model calibration, hydraulic analysis using H2OMAP, and storage/ supply analysis to
identify existing and future deficiencies in the water systems.
Staff Engineer, Advanced Water Treatment Pilot Study, Orange County, CA. Analyzed water quality
data for membrane filtration pilot units provided by Pall and Aqua. Collected additional water samples
from both units and performed water quality analysis.
Associates
W. Kirk Martin, P.G., CPG, CGWP
President/Principal Scientist
Mr. Martin has over 30 years of experience conducting groundwater resource investigations
and managing complex integrated water resource programs. He has special expertise in water
supply development, groundwater hydraulic interpretations, and fresh/saline water
relationships in coastal aquifers. He also has extensive experie nce in the application of
statistical analyses, computer models and geophysical methods to the solution of water
resource issues. He takes a “total water management” approach to water resource planning
and management challenges that provides for more creative solutions to address multiple level
issues. His project experience includes large-scale water supply, aquifer recharge, and
injection well design, construction, testing, and evaluation. He has extensive knowledge of
water policy and the regulations go verning water supply and water resource management.
Mr. Martin has completed over 300 reports on regional and local geology/hydrology in Florida
and has provided the primary technical direction on development of over 500 mgd of raw water
supply and over 100 mgd of aquifer recharge and wastewater disposal projects . Mr. Martin
served as the principal hydrologist for three projects winning awards from the Governor ’s
Commission for a Sustainable South Florida. He has worked with clients in the cities of Fort
Myers, Jacksonville, Marco Island, Boca Raton, Cape Coral, Sanibel, Hollywood, Titusville, and
Melbourne; and Palm Beach, Charlotte, Lee, Collier, St. Johns, Indian River, Hillsborough,
Brevard, Pinellas, Miami-Dade, and Seminole counties. He commonly serves as a technical
advisor to state, regional, and local governing bodies on water resource issues.
Water Supply
Technical Director, Collier County Wellfield Reliability Improvements and Expansion Prog ram,
Collier County, FL, 2004-2014. Recognizing the increasing uncertainty in securing critical raw
water resources in a rapidly growing community of 240 square miles, Collier County elevated
their water supply efforts to a programmatic status to ensure they could meet long-range needs
in an environmentally sustainable manner. Mr. Martin served as the lead technical resource for
the program that provides management and direction of multiple engineers, scientists, and
contractors in the planning, evaluation, design, permitting, construction, and operations of the
County’s water supply facilities. System elements include fresh, brackish and saline water
supplies, supplemental wastewater reuse, aquifer storage and recovery, and hy drologic and
operational monitoring and improvements.
Technical Director, Saltwater Intrusion Data Analyses. Florida Keys Aqueduct Authority, 2012-
2013. Saltwater intrusion was limiting withdrawals from the authority’s most efficient water
source. Mr. Martin directed a team in a detailed statistical evaluation of a wide range of
hydrogeologic data that showed that FKAA withdrawals were not the primary cause of saline
water migration but that regional operation of upgradient canal control infrastruc ture was the
critical factor in controlling salinity in the production aquifer.
Technical Director, Wellfield Performance Evaluation . City of Cape Coral Florida, 2013-2014.
The City of Cape Coral has a long and successful history of brackish water development for
reverse osmosis treatment. In addition, the City has planned reclaimed water ASR wells and
additional Floridan Aquifer supply wells to meet future growth demands. Mr. Mar tin provided
technical direction for a complete brackish wellfield performance evaluation to identify trends in
productivity and water quality and any issues with individual wells or wellfield areas.
Recommendations were provided for additional assessment of individual wells to determine
potential causes of water quality degradation and remedial actions.
Technical Director, Wellfield Performance Evaluation. St. Johns County Utilities, 2013. Mr.
Martin worked closely with SJCUD operations staff at the SR 214 brackish wellfield in
evaluating historic and ongoing operational data including production rates, static and
dynamic water levels, and production water salinity. Production wells with declining
Education
B.S. – Geology,
Florida Atlantic
University, 1981
Graduate
Geophysics, Wright
State University,
1984
Registration
Professional
Geologist: North
Carolina (1987),
Florida, Kentucky,
Texas, and
Alabama
Certifications
Certified
Professional
Geologist
Certified
Groundwater
Professional
W. Kirk Martin, P.G., CPG, CGWP
productivity or degraded water quality were identified for further analyses including dynamic video and geophysical
logging to identify primary production intervals, contributions to flow, and production water quality with depth. Specific
recommendations were provided for upgrades or modifications to well construction and operation of the most impacted
wells. Additionally, Mr. Martin provided ongoing services to the operations staff in periodic evaluation of production data
to optimize wellfield productivity and minimize raw water salinity over time. These efforts resulted in a more stabilized
production water quality and general operational improvements of the SR 214 wellfield.
Technical Director, Alternative Water Supply Evaluation and Implementation Plan Jacksonville Electric Authority, 2010 -2011.
JEA had completed preliminary evaluations of several alternative water supply (AWS) options as part of their Total Water
Management Plans but needed a higher level of certainty as to the timing, quantity, type, and location of AWS alternatives .
The effort included evaluation of 18 separate AWS options with prioritization based on a variety of time horizons, demand
locations, and potential supply capacities. Evaluation criteria included environmental impacts, regulatory acceptability,
technical feasibility, and costs. Key implementation strategies and specific recommendations included a targeted reuse
program to displace competing water users and to develop a salinity barrier adjacent to wellfields experiencing salt water
encroachment, providing for recharge of the Upper Floridan Aquifer between the JEA wellfields and Keystone Heights, and
desalination of surface water at the Northside Generating Station.
Technical Director, Integrated Water Supply Plan, Lee County, Florida, 2009-2011. Mr. Martin provided the key technical
direction for a countywide integrated water supply plan, which included evaluation of all ground, surface, and reclaimed
water supplies, as well as opportunities for storage of seasonally or temporally available sources using aquifer and recovery
technology and surface water reservoirs where appropriate. Key recommendations were provided for numerous water
supply development options depending upon area specific demands, resources, constraints, and permitting challenges.
Technical Reviewer, Emerald Coast Utilities Authority (ECUA) Northern Wellfield Conceptual Design, Pensacola, Florida,
2009. As a means to provide needed expansion and reliability in the utility’s raw water supply system, ECUA sought to
develop a new wellfield north of their service area where potential competition for available resources was diminished, the
water supply source was less susceptible to urban and industrial contamination, and saline water intrusion was not of
concern. Conceptual wellfield design parameters were developed and potential wellfield sites screened for hydrogeologic
characteristics, parcel size, competing uses, land cover, ownership, potential environmental impacts, potential hydrologic
impacts, distance to existing infrastructure, and costs.
Lead Hydrogeologist, Wellfield Design, Construction, and Management, Collier County, Florida, 1984 to 2010. Mr. Martin
provided primary hydrogeologic expertise for all development activities for the Collier County wellfields, including over 35
freshwater wells and over 45 brackish water wells with depths of up to 1200 feet and with a combined capacity of over
80 mgd.
Lead Hydrogeologist, Water Supply Planning and Wellfield Design, Construction, and Management, Cape Coral, Florida,
1983 to 1994. Mr. Martin provided primary hydrogeologic expertise for planning and development activities for the city’s
wellfields, including wellfield layout for over 40 brackish supply wells and design and construction of over 20 brackish wate r
wells with an installed capacity of over 40 mgd.
Lead Hydrogeologist, Hobart Park and South County Brackish Supply Wellfields, Indian River County, Florida, 1992 to 2010.
Mr. Martin provided hydrogeologic oversight for expansion and rehabilitation of the county’s South County Reverse Osmosis
Water Treatm ent Plant (ROWTP) wellfield and design, permitting, and construction of the Hobart Park ROWTP wellfield
with capacities of 6 mgd and 4 mgd respectively.
Project Director, Irrigation Aquifer Storage and Recovery System , Collier County, Florida, 2012-2014. Mr. Martin provided
technical direction and hydrogeologic services for the design, permitting, and construction oversight fo r two irrigation quality
Aquifer Storage and Recovery wells to provide critical seasonal storage of large volumes of irrigation quality water that
allows more efficient and effective utilization of the county’s reclaimed water and supplemental irrigation sources. The wells
will provide for storage of up to 240 million gallons annually of a combination of municipal reclaimed water, raw groundwater,
and canal water to help in the overall integrated management of available water resources to the county.
Project Director, Feasibility Study of Salinity Barrier by Injection, Hollywood, Florida, 200 7. Mr. Martin served as project
director for this aquifer recharge and salinity management project that included testing the feasibility of using direct injection
of reclaimed water to control movement of the salinity interface threatening the City’s primary water supply. The project
established a program to test the feasibility of injecting highly treated effluent (reclaimed water) from a Class I wastewater
treatment facility into areas where saltwater intrusion contaminated the Biscayne Aquifer as a means to maintain and
possibly increase use of the Biscayne Aquifer for municipal supply.
Mike Witwer, PE
Representative Project Experience
Process Lead, Green Meadows Water Treatment Plant Expansion,
Lee County Utilities, Lee County FL. Design of a 16 mgd (60,500
m3/d) water treatment plant treating water from three sources.
The process trains include a combination of RO treatment of a
brackish groundwater with bypass blending of high quality
intermediate water and a separate treatment process for a surficial
ground water using cation and anion resin. The Ion exchange
system is designed to use bulk virgin brine or an alternative brine
source from a backup deep injection well for cation resin
regeneration.
Project Technologist, Olga Water Treatment Plant Arsenic
Removal Study, Lee County Utilities, Lee County FL. Responsible
for the evaluation and preliminary design of an arsenic removal
system for a 1 MGD (3,800 m3/d)ASR well using titanium based
adsorbents.
Lead Project Technologist and Pilot Plant Manager, Green
Meadows Water Treatment Plant Expansion, Lee County Utilities,
Lee County FL. Responsible for the design, construction, and
operation of a one-year pilot plant test program. The testing
included the operation of three pilot RO pilot skids, large and small
scale ion exchange columns, pressurized media filters, small scale
media columns and sand strainers.
Process Consultant, North Springs Improvement District, Coral
Springs, FL. Assisted in the development of a Basis of Design report
for a 10 mgd RO facility treating a blend of brackish and fresh
water wells.
Lead Project Technologist, Seminole Tribe of Florida Water
Treatment Plant Evaluations and Expansion Alternatives,
Seminole Tribe of Florida. These projects included an evaluation of
plant capacity and equipment assessments for four RO/NF water
treatment systems. The project included site visits, pilot testing,
and preliminary process selection for expansion at two of the
plants. Recommendations for plant improvements and the
development of baseline assessment and recommendation reports
for each plant were delivered.
Process and Process Mechanical Lead, Dyal Water Treatment
Plant LOX Conversion, City of Cocoa, FL. Conversion of the ozone
plant from air fed to liquid oxygen fed ozone generation. The
design included installation of liquid oxygen storage and feed
system and modification to existing system.
Role on Project
Equipment/Layout; Task Leader – Tasks 6
& 7
Years of Experience
21
Relevant Experience
Extensive experience with bench and
pilot testing design, construction and
operation including clarification,
media filtration, membrane processes,
ion exchange, ozonation, and
disinfection at water and advanced
wastewater treatment facilities
Experience as a process and
mechanical engineer in the design of
facilities including clarification,
microfiltration, reverse osmosis,
chemical injection and disinfection
processes
Education
ME, Environmental Engineering,
University of Florida, 2001
BS Environmental Engineering (with
Honors), University of Florida,
Gainesville, 1999
Professional Registration
Professional Engineer: FL (#69262)
MIKE WITWER, PE
Process/Start Up Consultant, Dunes RO WTP Design / Build / Operate, Dunes Development
Corporation, Palm Coast, FL. Process consultant during the commissioning and initial operation of a new
0.7-mgd (expandable to 1 mgd) brackish water RO WTP. Worked on-site during the commissioning of
the facility. Completed tasks that included verification of membrane system performance and operation,
system troubleshooting, and data collection and analysis.
Process Lead, Sunset Water Treatment Plant Expansion, Guntersville Water and Sewage Board,
Guntersville, AL. Process designer responsible for the design of the microfiltration and chemical feed
systems. Designed the microfiltration system to replace conventional media filtration for an 8 mgd
(30,300 m3/d) surface water treatment plant expansion. Designed the chemical feed systems for the
addition of sodium hypochlorite, sodium hydroxide, hydrofluosilicic acid, coagulant and coagulant aid.
Lead Process Designer; Seawater Reverse Osmosis Demonstration Plant; DesalNATE Inc., Catalina
Island, CA. Public-private agency consortium funded under the California Department of Water
Resources “Proposition 50” program. Designed a 200,000 gpd (757 m3/d) SWRO system utilizing
innovate RO large diameter elements and pumping-energy recovery components. Responsible for all
aspects of system design and coordination between various involved parties.
Startup and Performance Testing Consultant, Aloma and Magnolia Water Treatment Plants, Winter
Park Winter Park, FL. Assisted in the startup of two ozonation systems and monitoring and acceptance
of the ozone system performance testing.
Technologist, Murphree Water Treatment Plant Contingency Plan, Gainesville Regional Utilities,
Gainesville, FL. Performed a treatability study which tested various treatment technologies capability to
remove selected organic compounds from a spiked groundwater. Performed bench top testing to
evaluate the capabilities of ozonation, advanced oxidation, granular activated carbon, and air stripping
to meet treatment goals and developed preliminary designs and order of magnitude cost estimates for
the selected treatment technologies.
Task Lead, Southwest Water Treatment Plant Liquid Oxygen Conversion Evaluation, Orlando Utilities
Commission, Orlando, FL. Evaluated required system changes to support the conversion from air fed to
oxygen fed ozone generators at 40 mgd water treatment plant. The evaluation included changes
required to the existing system, analysis of operational changes, and preparation of a cost opinion.
Technical Report Writer and Data Analyst, Algal Toxin Treatability Study, American Water Works
Association Research Foundation. Assisted in the writing of a technical report and data analysis
associated with the treatment of surface waters containing algal toxins with activated carbon and
ozonation. This project is an AWWARF study to assess the occurrence and treatability of algal toxins in
surface waters.
Lead Technologist, Pinellas County Utilities South Cross Bayou Water Reclamation Facility Discharge
Effluent Limitations, FL. Performed process evaluation to evaluate cause of high disinfection by product
concentrations in plant effluent and develop recommended operational or process modifications to
alleviate DBP exceedences. Evaluation included the use of alternative disinfectants including
chloramines, ozone, UV radiation, ferrate, and peracetic acid and process modifications.
Technologist, Disinfection By Product Precursor Removal Pilot Testing at the Kanapaha Water
Reclamation Facility, Gainesville Regional Utilities, FL. Performed filter column pilot testing to evaluate
the capabilities of coagulant addition to unfiltered secondary effluent to remove disinfection by product
precursors. Additional pilot testing is ongoing. Responsibilities include the design, construction
oversight, start-up, operation, data analysis, and report writing.
Nick Easter
Representative Project Experience
Project Engineer, RO Membrane Replacement and Energy Recovery
Upgrades Project, Bonita Springs Utilities, Bonita Springs, FL.
Served as the lead during the membrane replacement and
commissioning of the new energy recovery devices. Duties included
analyzing membrane factory test data, arranging and loading
membranes to optimize performance, communicating with
construction workers and plant operators, overseeing start-up of the
RO trains, and confirming membrane and energy recovery device
performance in accordance with the contract documents.
Project Engineer, North Water Treatment Plant Membrane
Filtration System Services during Construction and Commissioning,
City of Marco Island, FL. Marco Island NWTP is a 6.7 mgd facility
lime softening facility. The most recent addition to the facility
includes installation of a new MF system following the lime softening
process. Provided assistance with submittal reviews, facilitated
communications between plant operations, contractors, and
manufacturer’s representatives during start-up, and helped to write
the standard operating procedures for the new facility.
Project Engineer, Coral Springs Improvement District Nanofiltration
WTP Commissioning, Coral Springs Improvement District, Coral
Springs, FL. Assisted during the commissioning of the new CSID NF
WTP. Duties included assembling the standard operating
procedures for new facility, conducting operator training for the
clean-in-place system, and creating an automated membrane data
normalization sheet.
Project Engineer, City of Cocoa Capital Improvement Program
Project Prioritization, City of Cocoa, FL. Assisted with the
development of City of Cocoa’s prioritization framework and
decision process model. Organized the five-year capital plan
schedule based on the capital improvement projects benefit-cost
analysis.
Project Engineer, City of Melbourne Reverse Osmosis Membrane
Pilot Study, City of Melbourne, FL. Assisted in pilot maintenance and
analyzed performance of multiple membrane elements and scale
inhibitors to replace the existing RO membranes and pretreatment
chemicals. Roles include purchasing necessary equipment,
communications with plant operators, collecting data, and preparing
samples for laboratory analysis.
Project Engineer, Reverse Osmosis Facility Conceptual Design,
Peace River Manasota Regional Water Supply Authority, Punta
Gorda, FL. Assisted with the conceptual design of a brackish water
Role on Project
Equipment/Layout
Years of Experience
5
Relevant Experience
Specializes in membrane treatment
process evaluation, preliminary
design, commissioning and data
analysis
Experienced in process cost estimation
Education
MS, Environmental Engineering in Civil
Engineering, University of Illinois at
Urbana-Champaign
BS, Chemical Engineering, Rose-Hulman
Institute of Technology
Professional Registration
N/A
NICK EASTER
reverse osmosis facility to serve as an alternative water source during drought periods. Duties included
preliminary treatment process design and cost development for the proposed RO system including
pretreatment and post treatment processes.
Project Engineer, Texas Desalination Feasibility Study, Confidential Client, TX. Assisted with the
feasibility evaluation of desalination membrane treatment of alternative water supplies for five separate
Texas drinking water markets. The evaluation included the identification of alternative water supplies,
development of treatment options in each market, and finished water conveyance to final distribution.
Duties included preliminary treatment process design and cost development for each of the overall
systems including both brackish and seawater desalination.
Project Engineer, Pasco County Lower Coastal Stormwater Survey, Pasco County, FL. Assisted in the
field surveying and data collection of stormwater infrastructure to provide information for a
hydrogeologic model. Duties include surveying with a TRIMBLE GPS unit and automatic level with rod,
DEM basin delineation correction and refinement using ARCGIS software, infrastructure
assessment/inventory and watershed evaluation on regional and local scale.
Project Engineer, Pasco County Master Reuse System (PCMRS) Master Plan, Pasco County, FL.
Developed the cost estimate and benefit analysis of the Boyette Reservoir high service pump station
upgrade. Assisted in writing the development and cost evaluation of PCMRS improvement alternatives.
Project Engineer, Pelican Bay Environmental Sampling, Pelican Bay, Naples, FL. Conducted monitoring
of water quality in the Pelican Bay area ponds. Responsibilities include water quality sampling, data
analysis, and report preparation.
Project Engineer, Marco Island Membrane Filtration System Performance Review, Marco Island
Utilities, Marco Island, FL. Evaluated MF operation data, created recommendations based on
operational issues and operator feedback. Duties include MF system data analysis, facility optimization
evaluation, clean-in-place support, report writing, and communicating with operations staff.
Richard Giani, PE
Representative Project Experience
Drinking Water Compliance Coordinator, CH2M HILL, Kansas City,
MO. Duties include assisting OMBG drinking water utilities with
ensuring regulatory compliance in all aspects of state and federal
drinking water regulations.
Also to provide technical assistance related to compliance of
drinking water treatment and distribution operations. This includes
surface and groundwater treatment, treatment techniques,
monitoring and maintaining/troubleshooting distribution water
quality. Additionally, high expertise related to corrosion control
treatment of drinking water and lead/copper optimization in the
distribution system.
Manager, Water Quality Group, Portland Water Bureau, Portland
OR. Responsible for managing the City of Portland’s Water Quality
Division, which includes oversight of two supervisory levels. The
Division houses four sections including the Field Inspectors section,
Water Quality Customer Service, Regulatory Compliance, and an
accredited Water Quality Laboratory. The Division encumbers water
quality sample collection, analysis and data review for drinking
water compliance and public health protection in the distribution
system and the watershed, engineering review of construction
plans, and cross connection permitting to name a few priorities. The
Division also houses the responsibility to monitor and maintain the
only watershed variance in the nation with respect to filtration and
ultraviolet (UV) treatment avoidance. He managed the division
during the LT2 variance negotiations with the state and the
development of the variance monitoring plan. He initiated
performance planning and goals to the Division to streamline
operations and provide a tracking mechanism to maintain
exceptional water quality. Mr. Giani instituted new monitoring
programs to help reduce lead levels in customer homes and identify
water quality degradation from nitrification. Mr. Giani instituted
more efficient and sanitary methods for collecting regulated
bacteria samples to reduce false positive readings.
Manager, Drinking Water Division, District of Columbia Water and
Sewer Authority, Washington, D. C. Responsible for managing the
District’s Drinking Water Division, which included oversight of two
supervisory levels. The Division encumbered the water quality
monitoring program, cross connection program, flushing program,
emergency response, and security monitoring. His primary
responsibility was to ensure safe, high water quality throughout the
District. Other responsibilities included submission of monthly
compliance reports to the U.S. EPA, providing expert testimony
Role on Project
Corrosion Control
Years of Experience
27
Relevant Experience
State certified instructor for water and
wastewater operation classes in
various states
Supported numerous AWWARF
projects related to lead corrosion in
drinking water, including effects of
partial lead service line replacement
and effects of chlorine and chloramine
disinfectant
Current Chair of AWWA’s Distribution
Water Quality Committee and chair
for developing the latest addition of
AWWA’s industry manual of practice
for Internal Corrosion Control
Treatment for Drinking Water
Distribution Systems
Education
BS, Environmental Studies, East
Stroudsburg University, East Stroudsburg,
Pennsylvania
AAS, Biotechnology, State University of
New York, Cobleskill, New York
Professional Registration
State certified instructor for water and
wastewater operation classes in Florida,
Level IV (highest level) operator’s licenses
for water treatment and water distribution
systems in the states of Washington and
Oregon
RICHARD GIANI, PE
involving litigation, budget and workplan and development, union negotiation and arbitration,
participate on national regulatory committees, provide guidance for public outreach documents and
press releases, and oversight of national research projects involving the authority. He brought the
authority back into compliance during the 2004 lead corrosion crisis. Mr. Giani reduced lead levels to
5 parts per billion (ppb) in 2011, the lowest recorded action level since the inception of the LCR for the
District. He reduced the District’s total coliform drinking water levels to below 0.5 percent. He
developed a water quality rapid emergency response program and an efficient and aggressive routine
monitoring and customer complaint program. He also developed national guidance for corrosion control
monitoring.
Environmental Research Specialist, Pennsylvania DEP, Harrisburg, PA. Responsible for conducting
environmental research, managing state funded research projects, providing technical guidance and
training to department staff, plant operators, and environmental engineers. He had 5 years of
experience in drinking water research. Mr. Giani’s primary focus was on the national lead and copper
rule and optimization of drinking water plant operations. He managed the technical outreach program.
His responsibilities included overseeing operations and supervising 30 technical specialists statewide
who focused on providing operator and management assistant to small utilities. He conducted research
for the biosolids program focusing on biosolids odor emissions, analysis of Vector Attraction Reduction
(VAR) options, development of national computer software for VAR and Pathogen treatments as well as
development, teaching, and oversight of the Commonwealth’s mandatory biosolids training program.
His duties also include publishing research papers and speaking at state and national conferences.
Field Sanitarian, Pennsylvania DEP, Stroudsburg, PA. Environmental Field Inspector for the
Commonwealth of Pennsylvania. His responsibilities included enforcement of the state drinking water
and public eating facilities regulations. His duties consisted of inspecting public water supplies,
conducting drinking water field sampling and analysis, determine drinking water health threats and
oversee compliance of water plant operations. He co-authored several major AWWARF projects related
to lead corrosion in drinking water including effects of partial lead service line replacement and effects
of chlorine and chloramines disinfectant.
PY Keskar, PhD, PE
Representative Project Experience
Lead Electrical/I&C Engineer, East Water Reclamation Facility
(WRF), Bonita Springs Utilities, FL. This $56.8 million design-build
wastewater treatment project includes state-of-the-art membrane
biological reactors, headworks, clarification, aeration, sludge
thickening, dewatering, and drying processes. Responsible for
complete power system and control systems design. Responsible for
design and implementation of a state-of-the-art 5kv power
distribution system, a 2-MW fully automatic standby generation
system featuring momentary paralleling with Bonita Springs Utilities,
and state-of-the-art A/B Control Logix PLC-based distributed plant
control system reporting to a central computer system using
Intellution iFix SCADA package. The site also includes a new 11-mgd
sludge dryer residuals management system.
Lead Electrical/I&C Engineer, Rehabilitation and Upgrade of a
Wastewater Treatment Plant, Orange Beach, FL. Project involved
heavy retrofit of electrical system and addition of a new UV
disinfection system.
Lead Electrical/I&C Engineer, Reverse Osmosis (RO) Water
Treatment Plant (WTP) (Design-Build), Bonita Springs Utilities, FL.
This new $50 million design-build facility is located at the site of the
existing lime softening WTP and used design-build delivery. It is
designed for an initial capacity of 6 million gallons per day (mgd),
but is expandable to 12 mgd. Raw water will be supplied to the plant
from eight brackish water wells tapping the Lower Hawthorn and
Suwannee aquifer portions of the Upper Floridan aquifer.
Responsible for the power systems and control systems design for
this project. Oversaw design and installation of electrical systems,
including power distribution and stand by generation.
Lead Electrical/I&C Engineer, Energy Management and
Optimization Study, Palm Beach County, FL. Energy management
and optimization study for the County’s four WTPs and one WWTP
to recommend ways to optimize energy usage thereby saving energy
dollars. Several key recommendations were made that will result in
savings with regard to energy dollars.
Lead Electrical/I&C Engineer, Stock Island RO WTP Rehabilitation,
Florida Keys Aqueduct Authority, Stock Island, FL. Stock Island
project includes the relocation of two high-pressure pumps and
membrane permeator racks from a 15-year-old RO plant. New
facilities include supply and disposal wells, cartridge filter, repair and
replacement of about 15 percent of the membrane permeators,
post-treatment facilities, chemical feed systems, computer-based
Role on Project
Electrical/ I&C
Years of Experience
46
Relevant Experience
Recognized expert in electrical and
instrumentation and control systems
design and implementation
Significant expertise in I&C systems
design, including distributed control
systems, PLCs, and SCADA systems
Performed numerous energy and
process optimization studies for
clients nationwide, including Florida
Authored a significant number of
papers in the fields of electrical power
and control systems engineering,
which have been presented at ISA,
IEEE, EPRI, and TAPPI conferences and
have appeared in the transactions of
ISA and IEEE; two of the papers
received national level awards from
ISA
Education
PhD, Electrical Engineering, University of
Missouri, 1972
MS, Electrical Engineering, University of
Missouri, 1968
Bachelors of Engineering, University of
Jodhpur, 1965
Professional Registration
Professional Engineer: FL (#29288), GA, AL,
LA, IL, AR
PY KESKAR, PHD, PE
I&C system, standby power generator, new diesel engines with right-angle drives for the membrane
feed pumps, and fuel storage system.
Lead Electrical/I&C Engineer, Brackish Groundwater Desalination Facility at J. Robert Dean WTP,
Florida Keys Aqueduct Authority, FL. This project involved design, permitting, and construction
management services for the RO plant at the J. Robert Dean WTP. Responsible for 5-kV power
distribution system design and I&C design for the 9.2-mgd RO supply wellfield mechanical design, pre-
treatment, membrane treatment, degasifier scrubber treatment, post-treatment blending and product
transfer pumping system with chemical treatment and storage facilities. Upgraded the plant-wide
electrical power distribution system and installed a state of the art SCADA system for the monitoring
and control of the RO plant. The project was completed on time and under budget, saving the client $1.4
million. Cost: $37.3 million (fee: $3.6 million).
Lead Electrical/I&C Engineer, RO WTP, Chesapeake, VA. Responsible for a plant-wide, 5-kilovolt power
distribution system with a capacity of 10 megavolt amperes (MVA) and onsite generation of 6.4 MW.
Also designed a state-of-the-art distributed control system (DCS) with approximately 3,000 input/output
points featuring Foxboro IA system and Allen Bradley programmable logic controllers (PLCs). The design
also included 800-horsepower (hp) adjustable frequency drives for the membrane feed pumps.
Lead Electrical/I&C Engineer, Wastewater Treatment Plant, Fort Pierce, FL. Upgrades and modifications
on this project. One portion of the design required an effluent pump station with four 250-hp adjustable
frequency drives.
Electrical Engineer, RO Facility and General Engineering Services Contract, Fort Pierce Utility Authority,
FL. This project involved five Floridan aquifer supply wells, 3-million-gallon (MG) aboveground storage
facility, approximately 3 miles of raw water distribution piping, new RO facility, and 3,045-foot-deep
concentrate disposal well. The completion of this plant represents more than 8 years of conceptual
planning, permitting, design, and construction. Cost: $30 million.
Lead Electrical/I&C Engineer, Sky Lake WTP Ozone Disinfection Project, Orlando Utilities Commission,
FL. This design-build project includes upgrade of plant power distribution system and standby
generation system. Project involved a $17 million facility expansion from 15 to 24 mgd. Designed
electrical and instrumentation systems for addition of an ozone system for taste and odor control, new
raw water well, upgrades to the plant chemical and electrical systems, site improvements, and site
security upgrades. Completed early release of design packages to support long-lead procurement of
electrical and I&C equipment and early start to construction activities.
Electrical Engineer, Swoope WTP Improvements, City of Winter Park, FL. Evaluated electrical systems
and oversaw I&C for the upgrades for this design-build project that consisted of upgrading and
expanding the City's 50-year-old WTP with a new $15 million, 10-mgd facility that features ozonation
with liquid oxygen supply for primary disinfection. Delivered on-time and on-budget in 2005 under a
design-build GMP contract with direct purchase of equipment by owner.
Electrical Engineer, Magnolia WTP Upgrade Phases 1 and 2, City of Winter Park, FL. Evaluated electrical
systems and oversaw I&C for the upgrades for this design-build project that consisted of upgrading and
expanding the 8.2-mgd Magnolia WTP. Phase 1 improvements include installation of new high service
pumps, replacement of gas chlorination with a sodium hypochlorite disinfection system and
replacement of all electrical equipment to provide surge protection. Phase 2 Improvements included
installing a new ozone system consisting of a 3,000-square-foot ozone building, contactor and
foundation with screen wall for liquid oxygen storage and feed system.
Lead Electrical/I&C Engineer, United Water WWTP Rehabilitation, Jacksonville, FL. Project involved the
construction of four sequential bath reactors, upgrade of influent/effluent pump stations, and sludge
dewatering facility. A distributed PLC-based control system with personal computers was designed and
implemented. This project included UV system for effluent disinfection.
Larry Van Dyk
Representative Project Experience
Lead Structural Designer, Green Meadows WTP Expansion, Lee
County, FL. Design of facilities for a 16-mgd RO/IX treatment
facility. The new facility will use RO for desalinating brackish well
water in parallel with cation and anion exchange used to remove
iron, hardness, and organics from a surficial aquifer fresh water
source.
Structural Designer, Facility Conditional Surveys, Three Miami
Water Treatment Plants, Miami, FL.
Lead Structural Designer, Wastewater Treatment Plant
Expansions, North Springs Improvement District and Coral Springs
Improvement District, Coral Springs, FL. Responsible for the
structural design of the operations building expansion, new water
filter structures, and water-retaining structures.
Structural Designer, Installation of New Transfer Pumps, Miami
South District Water Treatment Plant, Miami, FL.
Structural Designer, Expansion to Sunrise Water Treatment Plant,
Davie, FL.
Structural Designer, Digester Upgrade and Refurbishment, Miami
South District Water Treatment Plant, Miami, FL.
Lead Structural Engineer, Crane Electrification Project, Port of
Miami, FL. Project involved the design of the Florida Power & Light
(FPL) Vault Building, which is 50 x 50 feet and is divided in half by a
fire-rated separation wall. The facility also stores FPL equipment
and crane electrical switchgear.
Lead Structural Designer, Public Safety Facility, City of Hollywood
Beach, FL. Participated in the design of this complex that consists
of a new two-story building with a three-bay fire rescue station and
offices and operations for Beach Safety. It also includes
incorporating an existing one-story historical structure located on
the south end of the site for community redevelopment agency
offices.
Lead Structural Designer, Fire Station No. 5 EOC, City of Boynton
Beach, FL. This state-of-the-art facility consists of two stories,
42,700 square feet, five apparatus bays, and training tower. It is
designed to resist a Category 5 hurricane and will be the main EOC
for the city.
Lead Structural Engineer, West Palm Beach Fire Station No. 2,
West Palm Beach, FL. 16,000 SF fire station. The station includes
three apparatus bays, living facilities for a three-shift crew of 12-
Role on Project
Structural
Years of Experience
52
Relevant Experience
Experience includes both design and
construction phases of many different
categories of buildings, including high-
rise condominiums, office blocks,
schools, factories, process plants,
aircraft hangars power stations, and
bulk materials handling
Design and field experience, in new
construction projects, as well as
refurbishment and extensions to
existing buildings
Tasks performed include preparation
of all structural design plans and
reports; attends coordination
meetings for structural issues; and
coordinates structural issues and
schedule reviews
Education
Witwatersrand College of Engineering,
Johannesburg, South Africa, 1967
Professional Registration
N/A
LARRY VAN DYK
plus firefighters, administrative offices, and private bunks for officers. Training and classroom space is
shared with a 600 SF community room and includes a multi-story training tower. An emergency
generator provides power for the entire facility and all window openings are secured by built-in, roll
down hurricane shutters, which are designed into the exterior wall system.
Lead Structural Engineer, Tequesta Public Safety Facility, Tequesta, FL. The $3.9 million facility
encompasses conference rooms, dormitories, a central dispatch room, physical conditioning area,
commercial kitchen facility, and apparatus bays. It is the headquarters for the Fire and Police
Departments and serves as Tequesta’s Emergency Operations Center. For this project, the Village
presented the firm with a plaque for Outstanding Architectural Work and Resilient Building Engineering.
Project Manager/Lead Structural Engineer, National Portland Cement, Port Manatee, FL. Responsible
for ship unloading conveyor design and restoration; mill building and feed conveyor modifications and
restoration; design of conveyor system for new unloading terminal; and design of new parking garages.
Lead Structural Engineer, Master Planning and Infrastructure Design for Industrial Cities: Salwa,
Rabigh, Water and Wastewater Infrastructure Master Planning and Design/Design Review, MODON,
KSA. Responsible for the design of all retaining walls, pond walls and pump stations.
Project Manager, Unit Paint/Blast Facility, Atlantic Marine Shipyards, Jacksonville, FL. This facility is
used for shot-blasting and painting of new ship hulls and hull sections and for the refurbishment of
existing ships. The facility is primarily used for the refurbishment of landing craft for the U.S. Navy. The
facility is approximately 110’-0” in width by 131’-0” in length and has a clear ceiling of 30’-0”. Spent shot
is collected in floor trenches, where it is conveyed to recycle hoppers by means of screw conveyors for
reuse. The air within the building is filtered and recycled at 100 foot per minute to remove paint vapors
and contaminants. The wall and ceiling panels house an extensive array of blast-proof strip lighting to
ensure that all hull surfaces are adequately illuminated. The blast cleaning equipment, dust collectors
and paint booth were supplied by Blast Cleaning Products Ltd, Canada.
Project Manager, New Covered Tankfarm, Atlantic Marine Shipyards, Jacksonville, FL. This new
structure enclosed large diesel fuel storage tanks. The structure was designed to serve as a retention
area in the event of a fuel leak or breach in the tank walls. Catch sumps were located to allow controlled
removal of spilled fuel to tanker truck for disposal. The tanker loading/offloading area is/was also
designed to capture fuel spillage to protect the environment.
Design Engineer, New Pump Station, Atlantic Marine Shipyards, Jacksonville, FL. This reinforced
masonry pump station was designed to house pumps for regulating storm drainage on the site.
Project Manager, New Floating Dry Dock Access Ramps and Gangways, Atlantic Marine Shipyards,
Jacksonville, FL. Height adjusting gangway and access ramps to the new floating dry dock.
Adam Ahmad, PE
Representative Project Experience
Design Engineer, Collier County Master Mobility Plan; Collier
County, Florida. Responsible for development and coordination of
the County's Master Mobility Plan. The grant was successfully
acquired to fund $472,799 of the project. He successfully
performed planning and engineering services as part of the Phase I
Project.
Design Engineer; LCCSI Design Build Criteria Packages; Lee County,
Florida. Performed field reviews and data evaluation of the
planned projects listed in the Complete Streets Initiative TIGER
Grant application; preparation of Conceptual Plans (horizontal
layout on aerial photos) which delineated the intent of the
proposed project(s), preparation of typical sections which defined
project features such as sidewalks, pathways, bike lanes and
shoulders; development of a Conceptual Report detailing the
criteria used as the basis for the conceptual plans; preparation of a
preliminary/conceptual design and construction schedule for
evaluation by the Lee County MPO.
Project Manager, Long Range Transportation Plan, Seminole Tribe
of Florida; Hollywood, Florida. He managed the 2035 Seminole
Tribe of Florida Long-Range Transportation Plan (LRTP). The 20-
year comprehensive study area included the boundary limits of the
six Seminole Tribe reservations (primarily comprised of trust lands)
within the state of Florida. A few services he managed were: An
evaluation of a full range of transportation modes and connections
between modes such as highway, rail, air, and water to meet
transportation needs; Social and economic development planning
to identify transportation improvements or needs to accommodate
existing and proposed land use in a safe and economical fashion;
Cultural preservation planning to identify important issues and
develop a transportation plan that is sensitive to Tribal cultural
preservation; Prioritized list of short and long-term transportation
needs; An analysis of funding alternatives to implement plan
recommendations.
Project Manager; Lee MPO Miscellaneous Planning Services; Lee
County, Florida. Provided a variety of transportation planning and
engineering services for the Lee County MPO. To date the following
services included: 1). Miscellaneous Planning Services: Validation of
Project Feasibility and Development of Project Estimates.
Preparation of conceptual designs along with quantity and cost
estimates for roadway and corridor improvements. 2) Grant
Preparation – Various TIGER I and TIGER III grant applications.
Role on Project
Civil
Years of Experience
10
Relevant Experience
Comprehensive experience of all
phases of planning and design and
production for civil/site work
projects
Experience in in a variety of
planning, engineering, technical,
analytical, statistical, graphical,
public involvement and project
review activities
Diverse experience includes
serving as the project manager for
the Seminole Tribe of Florida Long
Range Transportation Plan, Collier
Area Transit’s Facility Design Guide
and the preparation of over a
hundred million dollars in grant
applications including TIGER grants
Skilled in civil engineering site and
roadway design/mapping and
surveying, computer information
science, management,
cartography, and graphic design
Proficient in the use of state-of-
the-art engineering software
including Microstation and
GEOPAK, ICPR, Adobe Illustrator
and Photoshop, MathCAD, Leica
HDS Cyclone and ESRI ArcGIS.
Education
BS, Civil Engineering, University of Kansas
Professional Registration
Professional Engineer: FL (#72472)
ADAM AHMAD, PE
Roadway Design Engineer; Immokalee Road (CR 951 to 43rd Avenue NE); Collier County, FL. Assisted in
post design services for the widening of 8.1 miles of an existing two-lane rural roadway to a six-lane
urban facility. Services provided for this project included complete roadway design and permitting
services, drainage design, wetland mitigation, 8 miles of 36-inch water main design, 6 miles of 16-inch
force main design, signal design, roadway lighting, traffic studies, and services during construction.
Responsibilities included preparation of aerial exhibits, plan revisions, access management revisions and
field investigations and calculations.
Roadway Design Engineer; Vanderbilt Beach Road Widening; Collier County, FL. Assisted in post design
services for the widening of 5.5 miles of an existing two-lane roadway to a six-lane, urban divided
roadway. The project is located in a rapidly growing area of Collier County and required extensive
attention to public concerns regarding local access, circulation, traffic demand, impacts to businesses
and residential areas, and aesthetics. Responsibilities included preparation of utility designs, drainage
calculations and field investigations and calculations.
Roadway Design Engineer; Collier Boulevard Widening (Golden Gate Canal to Golden Gate Boulevard);
Collier County, FL. This project consisted of widening 3 miles of existing two-lane rural roadway to a six-
lane, urban divided roadway. The project is located in a rapidly growing area of Collier County and
required extensive attention to public concerns regarding local access, circulation, traffic demand,
impacts to businesses and residential areas, and aesthetics. Responsibilities included creation of
engineering exhibits, attendance at public meetings, and preparation of Gantt chart schedules in
Microsoft Project.
Roadway Design Engineer; Collier-Immokalee Intersection; Collier County, FL. Prepared utilities
designs, drainage calculations and field calculations. Provided aerial photography, attended public
meetings and performed modeling and computer simulations.
Design Engineer; Collier County Landfill; Collier County, FL. Prepared aerial exhibits assisted in plans
production, modeling and computer simulations.
Project Surveyor; Gordon River Water Quality Park; Collier County, FL. Involved in the hydrographic
survey of a portion of the Gordon River as part of the creation of this 50-acre constructed treatment
wetland and public park. Performed modeling and computer simulations for the hydrographic survey.
The project involved a rare consortium of government agencies and municipalities that have joined
together to design and build a constructed wetland facility that, once built, will provide flood
attenuation and stormwater treatment for a 2-square mile urban watershed.
Project Surveyor; Collier Boulevard Widening (US 41 to Golden Gate Boulevard); Collier County, FL.
Provided surveys for design of the 3 mile widening of an existing four-lane rural section to a six-lane
urban section.
Project Manager; 2009 Recovery Act - Energy Efficiency Conservation Block Grant for Facilities Power
Projects Priority; Collier County, FL. Responsible for development and coordination of the County's
Power Projects Priority. Approved for full funding of six new ice storage tanks, chiller replacement, 1,000
occupancy sensors, a computer power management system, and solar utility cart retrofits. The grant
was successfully acquired to fund $665,510 of the project.
Roadway Design Engineer; FPID 426836-1 Wildlife Crossing. Assisted in developing a design/build
criteria package for an Experimental Wildlife Underpass located on Immokalee Road. Provided aerial
photography, attended public meetings and performed modeling and computer simulations.
Project Lead; Collier County Facilities Grant Advisor; Collier County, FL. Duties include the evaluation
and assessment of literature dealing with funds available through grants from governmental agencies
and private foundations and submits grant proposals to officials for approval.
Ralph Myers, CGC
Representative Project Experience
Lead Estimator, Lane City Reservoir CMAR, Lower Colorado River
Authority (LCRA), Austin, TX. Led estimating effort and assisted with
Owner’s agent duties for negotiating for this $160-million, 100,000
Acre-Foot off Channel Reservoir & Pump Station project, via CMAR
delivery. The project includes construction of an earthen reservoir,
New Re-lift pump station, conveyance pipelines, conveyance canals,
Colorado River Outfall Facilities, Lane City Dam upgrades and
existing pump station facility upgrades.
Lead Estimator, C.W. Bill Young Regional Reservoir Renovation
Design-Build, Tampa, FL. Led estimating team in developing the
budgetary estimate to assist in evaluating the selection of the
design-build team to perform the rehabilitation of the $165,000,000
15 billion gallon regional reservoir for Tampa Bay Water.
Lead Estimator, JEA Total Water Management Plan (TWMP)
Design-Build, Jacksonville, FL. Led estimating effort and assisted the
Owner with review of the Design-Builder progressive estimates and
GMP for the river crossing segment as well as established baseline
budgets for traditional Design-Bid-Build projects. The program
included 43,000 linear feet (LF) of potable water transmission
pipeline including six projects or segments of large-diameter pipe
(36-inch, 30-inch, and 24-inch). The $23.3 million design-build
project (Segment 2) involved 7,800 LF of pipe, including
approximately 6,700 LF of 36-inch steel pipe under the St. Johns
River. This pipe was installed using HDD methods. The project also
included another 1,100 LF of 36-inch pipe on the east and west
banks of the river.
Project Management Assistant and Lead Estimator, Robindale
WWTP Expansion, Brownsville Public Utilities Board, Brownsville,
TX. Led estimating and GMP development as well as subcontractor
selection and negotiations for this $38-million, 14.5-million-gallons-
per-day (mgd) construction of this Wastewater Treatment Plant
Expansion project. The project included construction of (3)
Secondary Clarifiers, UV disinfection Facility, Mixed Liquor Pump
Station, Aerobic Digester, Headworks Structure, Odor Control
Facility, renovations to existing treatment units and related support
structures.
Lead Estimator, City of Tampa Utility Capital Improvements (UCAP)
CMAR/Design-Build, Tampa, FL. Responsible for developing timely
and accurate estimating and GMP contracting as well as
subcontractor bid packages and solicitation for this $250-million, 5+-
year design-build contract to resolve historical drainage, storm
water, and municipal pipeline problems for the City of Tampa. The
Role on Project
Cost Estimating
Years of Experience
31
Relevant Experience
Experience of managing delivery and
estimating the construction of water,
wastewater treatment and
conveyance systems
Specializes in hard bid and design-
build management, estimate
preparation, budgeting, purchasing,
planning, scheduling, subcontract
management and close out of
construction projects.
Proficient in equipment, material and
subcontract procurement.
Former Owner/General Contractor
who has delivered successful projects
for over 30 years in hard bid and
design-build in Florida
Education
Coursework for AA Degree, Miami-Dade
Community College
Allstate Construction College- Florida
Union Carpenter
Apprenticeship/Journeyman Training-
Local Union #1250-Miami
Professional Registration
State Certified General Contractor- Florida
(CH2M HILL Qualifier- 2014)
State Certified Underground Utility &
Excavation Contractor- Florida (CH2M HILL
Qualifier- 2014)
RALPH MYERS, CGC
project consists of over 12 miles of potable water transmission mains from the David L. Tippin WTP, as
well as numerous other water force main, wastewater force main, storm water drainage, river micro
tunneling and traffic signalization projects for the City of Tampa.
Estimator, Blue Plains WWTP Project, DC Water, Washington D.C. Performed discipline estimating and
GMP development for the $253,000,000 DC Water Blue Plains Advanced Clarification and Pump Station
Project. The project is a 250 mgd Tunnel Dewatering Pump Station and Clarification Facility expandable
to 500 mgd on a 5-acre site. The project includes two tunnel shafts a 132-foot diameter dewatering
shaft and a 76-foot diameter screening shaft each 100 feet deep, a new Tunnel Dewatering Pump
Station, new Headworks facility with screening and grit removal, solids processing and handling, chlorine
contact and odor control.
Estimator, Woodward Avenue WTP, City of Hamilton, Ontario Canada. Performed discipline estimating
and GMP development for the $332,000,000 Woodward Avenue Pump Station and Water Treatment
Plant. The plant included a Raw Wastewater Pumping Station, North and South Secondary Treatment
Plant Upgrades, a New Secondary & Tertiary Membrane Plants, an Aeration Plant Expansion, Railway
Alignment, Chlorine Contact Tank & Outfall, and a New Energy Centre for the Electrical & Power
Systems.
Prior to CH2M
Owner/Project Manager, South County Regional RO WTP, City of Naples, FL/Poole & Kent, Engineer-
Hazen & Sawyer. Developed firm fixed price and managed delivery of facility expansion to add 8 mgd of
RO water treatment process in a separate process building. Led self-performing general contractor in
concrete work supporting construction of new RO trains, high-service pump station, new electrical
building, degasifier structure, and expansion to existing overflow ponds.
Owner/Project Manager, Bonita Springs East WRF Expansion, Bonita Springs Utilities, FL. Developed
firm fixed price proposal and managed delivery for concrete, masonry, and metals fabrication associated
with the new dewatering and drying facility.
Owner/Project Manager, Sawgrass Wastewater Treatment Plant (WWTP) Expansion- Owner/Project
Manager, Client-City of Sunrise, FL/Poole & Kent. Developed firm fixed price proposal and managed
delivery including new clarifiers, ATAD facility, UV facility, and Aeration Basins for the $26-million
Sawgrass WWTP expansion project.
Owner/Project Manager, Sawgrass WTP Reverse Osmosis (RO) Membrane Facility, City of Sunrise,
FL/Poole & Kent. Developed firm fixed price proposal and managed project delivery including a new
Reverse Osmosis facility and support structures for the $24-million Sawgrass WTP expansion.
Owner/Project Manager, South Cary WWTP Expansion, Town of Cary, NC/Poole & Kent. Developed
firm fixed price proposal and managed delivery including new Deep Bed Filters, UV Facilities,
Aerobic/Anaerobic Digestion Basins, RAS/WAS Pump Station, Clarifiers and support structures for the
$22-million South Cary WWTP expansion project.
Owner/Project Manager, Palm Beach WTP No. 9 RO Membrane Facility, City of West Palm Beach,
FL/Poole & Kent. Developed firm fixed price proposal and managed delivery including a new Reverse
Osmosis Facility, Chemical Facilities, Ground Storage Tanks, Degasifiers and support structures for the
$21-million Water Treatment Plant #9 Expansion.
Owner/Project Manager, Norwood Oeffler WTP RO Membrane Facility, City of North Miami Beach,
FL/Poole & Kent. Developed firm fixed price proposal and managed delivery including a new Reverse
Osmosis Facility, Ground Storage Tanks, New Clearwell, Degasifiers and support structures for the $35-
million Norwood Oeffler WTP expansion.
TAB V ReferencesTAB VReferences
V-1
Client references are an excellent source of information about a firm’s project performance as well as the abilities
and responsiveness of the project management team. We encourage the County to contact the individuals
referenced in this section for an appraisal of the quality of our services. Per the instructions in the RFP, we have
included in this section five completed reference forms (Attachment 8: Reference Questionnaire) from clients
whose projects are of a similar nature to this solicitation.
RFP CCNA Template_01202016
RFP_CCNATemplate
40
Attachment 8: Reference Questionnaire
Solicitation: 16-6639 Variable TDS Reverse Osmosis Conceptual Design
Reference Questionnaire for:
(Name of Company Requesting Reference Information)
(Name of Individuals Requesting Reference Information)
Name: Company:
Email: FAX: Telephone:
Collier County is implementing a process that collects reference information on firms and their key personnel to be used in
the selection of firms to perform this project. The Name of the Company listed in the Subject above has listed you as a
client for which they have previously performed work. Please complete the survey. Please rate each criteria to the best of
your knowledge on a scale of 1 to 10, with 10 representing that you were very satisifed (and would hire the firm/individual
again) and 1 representing that you were very unsatisfied (and would never hire the firm/indivdiual again). If you do not
have sufficient knowledge of past performance in a particular area, leave it blank and the item or form will be scored “0.”
________________________
Project Budget: _______________________________ Project Number of Days: _______________________
Item Citeria Score
1 Ability to manage the project costs (minimize change orders to s cope).
2 Ability to maintain project schedule (complete on-time or early).
3 Quality of work.
4 Quality of consultative advice provided on the project.
5 Professionalism and ability to manage personnel.
6 Project administration (completed documents, final invoice, final product turnover;
invoices; manuals or going forward documentation, etc.)
7 Ability to verbally communicate and document information clearly and succinctly.
8 Abiltity to manage risks and unexpected project circumstances.
9 Ability to follow contract documents, policies, procedures, rules, regulations, etc.
10 Overall comfort level with hiring the company in the future (customer satisfaction).
TOTAL SCORE OF ALL ITEMS
Please FAX this completed survey to: _______________________________________ By ________________
CH2M HILL
Joe Elarde
Jeff Poteet
(Evaluator completing reference questionnaire)
Marco Island Utilities
(Evaluator’s Company completing reference)
jpoteet@marcoislandutilities.com 239-394-8137 239-389-5181
Ave Maria Expansion PlanningProject Description: _ __ Completion Date: _______January 2016_____________________
$24,835 120
10
10
10
10
10
10
10
10
10
10
100
6/29/16jelarde@ch2m.com
RFP CCNA Template_01202016
RFP_CCNATemplate
40
Attachment 8: Reference Questionnaire
Solicitation: 16-6639 Variable TDS Reverse Osmosis Conceptual Design
Reference Questionnaire for:
(Name of Company Requesting Reference Information)
(Name of Individuals Requesting Reference Information)
Name:
(Evaluator completing reference questionnaire)
Company:
(Evaluator’s Company completing reference)
Email: FAX: Telephone:
Collier County is implementing a process that collects reference information on firms and their key personnel to be used in
the selection of firms to perform this project. The Name of the Company listed in the Subject above has listed you as a
client for which they have previously performed work. Please complete the survey. Please rate each criteria to the best of
your knowledge on a scale of 1 to 10, with 10 representing that you were very satisifed (and would hire the firm/individual
again) and 1 representing that you were very unsatisfied (and would never hire the firm/indivdiual again). If you do not
have sufficient knowledge of past performance in a particular area, leave it blank and the item or form will be scored “0.”
Project Description: ___________________________ Completion Date: _____________________________
Project Budget: _______________________________ Project Number of Days: _______________________
Item Citeria Score
1 Ability to manage the project costs (minimize change orders to s cope).
2 Ability to maintain project schedule (complete on-time or early).
3 Quality of work.
4 Quality of consultative advice provided on the project.
5 Professionalism and ability to manage personnel.
6 Project administration (completed documents, final invoice, final product turnover;
invoices; manuals or going forward documentation, etc.)
7 Ability to verbally communicate and document information clearly and succinctly.
8 Abiltity to manage risks and unexpected project circumstances.
9 Ability to follow contract documents, policies, procedures, rules, regulations, etc.
10 Overall comfort level with hiring the company in the future (customer satisfaction).
TOTAL SCORE OF ALL ITEMS
Please FAX this completed survey to: _______________________________________ By ________________
CH2M HILL
Joe Elarde
Jason Vogel Ave Maria Utility Company
jvogel@amuc.com 239-348-3740 239-348-0248
Ave Maria Expansion Planning January 2016
$24,835 120
10
10
10
10
10
10
10
10
10
10
100
6/29/16jelarde@ch2m.com
RFP CCNA Template_01202016
RFP_CCNATemplate
40
Attachment 8: Reference Questionnaire
Solicitation: 16-6639 Variable TDS Reverse Osmosis Conceptual Design
Reference Questionnaire for:
(Name of Company Requesting Reference Information)
(Name of Individuals Requesting Reference Information)
Name:
(Evaluator completing reference questionnaire)
Company:
(Evaluator’s Company completing reference)
Email: FAX: Telephone:
Collier County is implementing a process that collects reference information on firms and their key personnel to be used in
the selection of firms to perform this project. The Name of the Company listed in the Subject above has listed you as a
client for which they have previously performed work. Please complete the survey. Please rate each criteria to the best of
your knowledge on a scale of 1 to 10, with 10 representing that you were very satisifed (and would hire the firm/individual
again) and 1 representing that you were very unsatisfied (and would never hire the firm/indivdiual again). If you do not
have sufficient knowledge of past performance in a particular area, leave it blank and the item or form will be scored “0.”
Project Description: ___________________________ Completion Date: _____________________________
Project Budget: _______________________________ Project Number of Days: _______________________
Item Citeria Score
1 Ability to manage the project costs (minimize change orders to s cope).
2 Ability to maintain project schedule (complete on-time or early).
3 Quality of work.
4 Quality of consultative advice provided on the project.
5 Professionalism and ability to manage personnel.
6 Project administration (completed documents, final invoice, final product turnover;
invoices; manuals or going forward documentation, etc.)
7 Ability to verbally communicate and document information clearly and succinctly.
8 Abiltity to manage risks and unexpected project circumstances.
9 Ability to follow contract documents, policies, procedures, rules, regulations, etc.
10 Overall comfort level with hiring the company in the future (customer satisfaction).
TOTAL SCORE OF ALL ITEMS
Please FAX this completed survey to: _______________________________________ By ________________
CH2M HILL
Jane Early
Ongoing - est. July 2016
TBD
North Springs Improvement District
10
10
10
10
10
10
10
10
10
10
100
Doug Hyche, District Manager
954-796-6603
$19,450,000.00 (RO Plant)
RO Plant
954-755-7237DougH@nsidfl.gov
TAB VI Acceptance of ConditionsTAB VIAcceptance of Conditions
VI-1
CH2M HILL takes no exception to the general terms and conditions of the RFP.
TAB VII Required Form SubmittalsTAB VIIRequired Form Submittals
VII-1
Per the RFP, CH2M has included in this section the following signed and notarized forms.
Attachment 2: Consultant Checklist
Attachment 3: Conflict of Interest Affidavit
Attachment 4: Consultant Declaration Form
Attachment 5: Immigration Affidavit and company’s E-Verify profile page and memorandum of understanding
Attachment 6: Consultant Substitute W9
Attachment 7: Insurance Requirements
Attachment 8: Reference Questionnaires are included in Tab V, References, of this submittal.