132 MGD Water Treatment Plant Expansion Conventional Treatment Expansion Conceptual Design

Transcription

1 132 MGD Water Treatment Plant Expansion Conventional Treatment Expansion Conceptual Design 1.0 Summary Description of Improvements Under Scenario 4, the City of Evanston (Evanston) will increase the capacity of the Evanston Water Treatment Plant (WTP) from 108 million-gallons-per-day (mgd) to 132 mgd utilizing conventional treatment processes. The following improvements are assumed to be included as part of Scenario 4: Replace Existing 1909 Raw Water Intake Replace Two Existing Raw Water Pumps Implement New Distributed Rapid Mix Improvements with New Chemical Application Points Implement Flocculator Improvements Retrofit Sedimentation Basins with Tube Settlers Implement Filtration Improvements Replace Existing Finished Water Storage Reservoir Replace Two Existing High-Lift Water Pumps Chemical Storage and Feed System Improvements 2.0 Raw Water Systems To provide a maximum day design net water treatment capacity of 132 mgd, the required maximum raw water flow to the conventional treatment system is projected to be 136 mgd to accommodate lost water (estimated at 3 percent) from filter backwash water at maximum day flow. 2.1 Intake The existing 36/42-inch intake pipe installed in 1909 is projected to have reached the end of its reliable life. It is assumed that this intake will be abandoned and replaced. A new 54-inch diameter intake pipe is assumed to be constructed to replace the capacity of the 36/42-inch intake as well as provide the additional capacity needed to meet the proposed increase in raw water demand. The new 54-inch intake will consist of a concrete cylinder pipe of approximately 5,940 ft in length to provide the conveyance capacity required while preventing excessive pipeline velocities. The intake will be configured similar to the existing 54-inch intake, with a crib intake structure that includes a low-velocity intake cone, a chemical feed/application system to protect the intake from zebra and quagga mussel colonization, and an electric resistance heating system to mitigate icing. C-1

2 It is assumed that new 54-inch on-shore raw water piping will connect the new intake to the raw water pumping system at the existing North and South Screen Wells and the Low Lift Pump 4 Suction Well. Onshore piping from the existing 36-inch intake is proposed to be demolished to make room for the new 54-inch raw water piping. 2.2 Raw Water Pump Station The existing raw water pump station (i.e., Low Lift Pump Station) contains six pumps that provide a firm rated capacity of approximately 108 mgd. The existing Pumps 5 and 6 (15 mgd capacity, each) were installed in 1956 and are projected to have reached the end of their reliable life. It is assumed that Pumps 5 and 6 will be replaced with two new 30 mgd pumps to increase the reliability of the existing pumping system as well as to increase the firm capacity of the pump station to 136 mgd. The two new pumps will be vertical turbine-type low lift pumps with electric motors and directengine drives to allow for the operation of these pumps in the event of loss of utility power. Preliminary design criteria for the new raw water pumps are shown in Table C-1. Table C-1 New Raw Water Pumping Design Criteria Characteristic Design Value Comments/Assumptions Number of New Pumps 2 Replace Existing Pumps 5 & 6 Pump Type Vertical Turbine Pump Capacity 30 mgd (20,800 gpm) Discharge Head 20 psi (45 ft TDH, nominally) Motor Horsepower 300 HP Voltage 4160 VAC Drive Type 18 Pulse Variable Frequency 3.0 Pretreatment The existing rapid-mix, flocculation, and clarification systems are assumed to be modified to enable the increase in capacity of the pretreatment facilities. 3.1 Rapid Mix The existing rapid mix process consists of a single chamber, single mixer, system located a considerable distance from the flocculation basins. Historically, as production rates approached the current rated capacity of the WTP, a partial bypass of the rapid mix process has been employed to relieve the hydraulic bottleneck through the rapid mix chamber. Improvements to this existing rapid mix process are proposed to (1) address hydraulic limitations of the existing rapid mix system that is undersized for the existing peak design capacity, (2) eliminate the single-point of failure within the treatment process, and (3) reduce the long distance between the rapid mix basin and the flocculation basins. It is assumed that the existing single chamber, single mixer, rapid mix system is to be replaced with four new in-line rapid mix systems located closer to the flocculation basins. In-line rapid mixers ( Water Champs or equivalent) are assumed to be constructed within the flocculation basin influent channels. The proposed distributed rapid mix system will provide increased capacity, better process control, and reduced headloss compared to the existing arrangement, while also avoiding potential deterioration of floc formed prior to entering the flocculation basins. Additionally, the proposed arrangement will eliminate the single point of failure situation that the existing rapid mix C-2

3 arrangement presents. Minor modifications of the existing rapid mix structure will be necessary to allow the rated capacity of the expanded WTP to be conveyed without experiencing appreciable headloss (e.g., removing existing weir structure). New alum and polymer application points will be provided at the new in-line rapid mixers. It is assumed that chlorine will continue to be fed at the existing rapid mix, along with carbon, when needed. It is assumed that fluoride feed will be relocated to finished water lines as part of a separate project. New raw water flow meters are proposed to be installed on the influent conduits to each sedimentation basin for flow pacing of the alum and polymer application. 3.2 Flocculation The existing flocculation basins have an average detention time of approximately 27 minutes at the 132 mgd net design flow, which is slightly less than the recommended 30 minute detention time per the Recommended Standards for Water Works by the Great Lakes Upper Mississippi River Board (commonly called the Ten State Standards). The Illinois EPA has indicated that Evanston could likely obtain a variance to the 30 minute flocculation time requirement by demonstrating good performance of the pretreatment system at elevated loading rates. Good flocculation has been demonstrated at several Lake Michigan water plants with detention times less than 30 minutes. In order to optimize the flocculation conditions, reduce shearing, and equalize flow-through distribution, it is assumed that the influent ports, baffle wall openings, and effluent ports are increased in cross-sectional area. New VFD drives are proposed to be installed on the flocculators for Basins 1 and 2 to provide better control of flocculator speed. In addition, the existing flocculator paddles are proposed to be reconfigured to improve the flocculation energy (i.e., Gt value) for the basins. 3.3 Sedimentation The existing sedimentation basins have an average detention time of approximately 2.4 hours at the 132 mgd net design flow, which is less than the recommended 4 hour detention time per the Ten State Standards. In addition, the flow through velocity and surface loading rate for the sedimentation basins at the 132 mgd net design flow are higher than that recommended by Ten State Standards as shown in Table C-2. Table C-2 Sedimentation Basin Design Criteria Characteristic Design Value Comments/Assumptions Recommended Detention Time 4 hours Ten State Standards Detention 132 mgd net flow 2.4 hours Recommended Flow Through Velocity 0.5 feet / minute Ten State Standards Flow Through 132 mgd net flow 2.4 feet / minute Recommended Surface Loading Rate 0.5 gpm / square foot Ten State Standards Surface Loading mgd net flow 0.7 gpm / square foot The Ten State Standards allows higher capacities for sedimentation basins that are equipped with tube or plate setter units. Thus, it is assumed that tube settlers will be installed in the upper section of the four existing sedimentation basins at a design surface loading rate of 2 gpm/sf per the recommendations of Ten State Standards. At the increased flow of 132 mgd, hydraulic losses between the pretreatment basins and the filter complexes will elevate the water surface within the pretreatment basins that will surcharge the concrete roof. This additional force will require a 10-in (+/-) thick reinforced concrete slab covering both the flocculation and sedimentation basins. A preliminary C-3

4 structural review indicates that the existing sedimentation basins are expected to be able to accept this additional concrete loading with minimal additional modifications. Per the recommendations of the CTL Group report Inspection of Finished Water Reservoir and Settling Basins No. 1 & 2 (December 2012), full-height replacement of the above-grade concrete access manholes to Sedimentation Basins 1 and 2 using air-entrained concrete are proposed to be completed concurrently with the proposed rapid-mix improvements. An allowance of $25,000 was assumed for the hatch repairs 4.0 Filtration The existing filtration process consists of two filter complexes (East and West) and 24 granular media filtration units. 4.1 East Filter Complex Improvements Filters 13 through 24, in the East Filter Complex, have undergone improvements which include new underdrains and new filter media. Recent stress testing has allowed the IEPA to approve the operation of these filters at a hydraulic loading rate of 5 gpm/sf, or the equivalent of 110 mgd with one of the 12 filters out of service. Improvements are required to the East Filter Complex to replace aging facilities and to increase system reliability. Improvements for the 1948 filter rate of flow controllers (ROFCs) are assumed to consist of replacement of the Venturis and valve actuators. The ROFC butterfly valves on these filters were replaced in Improvements for the 1964 filters are assumed to consist of replacement of the Venturis, butterfly valves, and valve actuators. The existing control valves and limit switches on the filter control valves in the East Filter Complex have reached the end of their useful life and need to be replaced in order to reliably maintain control of the filtration process. The filter influent piping and control valves are proposed to be increased in size from 24-inch to 30-inch to improve system hydraulics. The modulating actuator on the master backwash water butterfly valve that regulates backwash water to the 12 East Plant filters has reached the end of its reliable life and is in need of replacement. In addition, the butterfly valves and actuators need to be replaced on the dedicated 30 backwash supply and 6 surface wash supply pipes to each of the filters within the East Filter Complex. Limit switches will be included on all valves. Recent improvements to Filters 19 through 24 included new s style surface wash sweep arms. WTP staff has noticed a significant improvement in the filter backwash process as a result of this change. It is assumed that these same, improved, surface wash sweep arms will be installed in Filters 13 through West Filter Complex Improvements The West Filter Complex includes existing filters Conveyance channels from the sedimentation basins to Filters 1-12 limit the capacity of these filters to approximately 36 mgd or a filter loading rate of 3.0 gpm/sf. This provides more than enough filtration capacity to supplement the firm 110 mgd capacity of the East Filter Complex. Therefore, no improvements are assumed for the West Filter Complex. C-4

5 5.0 Finished Water Storage Systems The existing finished water storage capacity at the WTP totals 9.4 million gallons (MG), which provides an average detention time of 1.7 hours at the 132 mgd net design capacity. This capacity meets the Illinois Rules & Regulations requirement for 1 hour of chlorine contact detention time post filtration. The existing finished water storage arrangement also meets the disinfection credit (Ct) requirement of 0.5 log removal of Giardia and 2.0 log removal of viruses at cold water temperatures under normal chlorine residual levels. (This assumes a 2.5 log removal credit for Giardia and 2.0 log removal credit for viruses is received by the conventional coagulation/sedimentation/filtration process at the Evanston WTP according to the LT1ESWTR Disinfection Profiling and Benchmarking Technical Guidance Manual for a total removal credit of 3.0 log for Giardia and 4.0 log for viruses.) The total existing finished water storage capacity represents roughly 7 percent of the daily production at the 132 mgd design flow. This is less than 10 to 15 percent of design production that is typically recommended to provide sufficient volume for operational flexibility and to accommodate diurnal flow variations, backwash water demands and other plant dynamics. However, at this time, space constraints at the Evanston WTP limit the options for implementing additional finished water storage at the WTP site. It is assumed that implementation of any additional finished water storage would be the responsibility of wholesale water customers within their delivery systems. A condition assessment of the existing 5 MG finished water storage reservoir located south of Lincoln Street has indicated that the roof slab of the 80-year old structure is in poor condition. The assessment recommended a series of structural improvements including replacement of the roof slab and drop panels. Additional evaluations of the reservoir are ongoing to determine whether it is better to rehabilitate or replace the reservoir. For the purposes of this evaluation, it is assumed that the existing reservoir will be replaced with a new 7 MG reservoir, located to the south of Lincoln Street. 6.0 High Lift Pumping and Distribution The existing High Lift Pump Station capacity is proposed to be increased to 132 mgd firm capacity by replacing the existing Pump 2 (10 mgd capacity) with a new 20 mgd pump and replacing the existing Pump 5 (15 mgd capacity) with a new 25 mgd pump. The two new pumps will be horizontal split-case type pumps with electric motors. Pump 2 would also be equipped with a direct-engine drive to allow for the operation of this pump in the event of loss of utility power. Preliminary design criteria for the new high-lift pumps are shown in Table C-3. Table C-3 New High-Lift Pumping Design Criteria Characteristic Design Value Comments/Assumptions Number of New Pumps 2 Replace Existing Pumps 2 & 5 Pump Type Horizontal Split Case Centrifugal Pump Capacity Pump 2: 20 mgd (13,900 gpm) Pump 5: 25 mgd (17,350 gpm) Discharge Head 65 psi (150 ft TDH, nominally) Motor Horsepower Pump 2: 700 HP Pump 5: 800 HP Voltage 4160 VAC Drive Type 18 Pulse Variable Frequency An assessment of the finished water distribution systems is not included under the scope of this study. C-5

6 7.0 Chemicals The WTP utilizes various chemical storage and feed systems, including alum, polymer, carbon, chlorine, fluoride, and blended poly/ortho-phosphate. Alum and polymer are currently used in the pretreatment process. Powdered activated carbon is used periodically to control taste & odor events. Chlorine gas is currently used in solution for disinfection through a combination of pre and postchlorination application points and for mussel control at the existing raw water intake structures. Fluoride is currently used to help prevent dental decay. Blended phosphate is currently added to the finished water for lead & copper corrosion control. According to the Ten State Standards, bulk storage tanks are required to hold at least a 30-day supply of chemical. It is assumed that the existing bulk chemical tanks currently provide at least a 30-day chemical supply and would thus provide at least 25 days chemical storage at the 132 mgd WTP design capacity. The Illinois EPA has indicated that Evanston could likely obtain a variance to the 30-day bulk chemical storage requirement based upon demonstration of the ability to maintain adequate chemical supply with 25 days storage. In the future, the bulk storage tanks can be replaced as they reach their useful life with new tanks that provide the full 30 days storage. The following improvements are assumed for the chemical storage and feed systems to support the 132 mgd upgrade: Alum: The existing alum day tanks are adequate for the 132 mgd design flow. A new dedicated chemical feed pump is assumed to be installed to transfer alum to the each of the four new distributed in-line rapid mixers. A fifth chemical feed pump is assumed to be installed as a standby. Polymer: The existing polymer day tank is oversized for the needs of the 132 mgd design flow. A new, smaller polymer day tank is assumed to be installed to meet the needs of the system and to free up space for installation of additional polymer feed units. A new dedicated polymer feeder is assumed to be installed for each of the four new distributed in-line rapid mixers. A fifth polymer feeder is assumed to be installed as a standby. Carbon: The existing carbon storage and feed facilities are assumed to be adequate. No improvements are assumed for the carbon system at this time. Fluoride: Evanston staff indicated that a new day tank will be required for the fluoride system. Phosphate: New chemical feeders are assumed to be required for the blended poly/orthophosphate system. Chlorine: New chemical feeders are assumed to be required for the chlorine system. 8.0 Waste Backwash Water and Residuals Treatment The existing waste backwash water management system is assumed to be adequate to accommodate the increased flows from the 132 mgd design capacity. It is assumed that sludge from the sedimentation basins will continue to be discharged to the sanitary sewer. No improvements to the waste backwash water and residual treatment systems are assumed. C-6

7 9.0 Electrical Systems It is assumed that the existing electrical system is adequate to serve the expanded 132 mgd design capacity Capital Cost Estimate Table C-4 presents a summary of the capital cost estimate for the 132 mgd expansion of the conventional WTP system as defined herein. The cost estimate considers general condition costs, conceptual costs; undeveloped design detail costs; contractor fees, overhead, and profit costs; change order costs; and engineering and administration related costs. A cost breakdown for each unit process is presented at the end of Appendix C. Unit Process Table C-4 Capital Cost Estimate for Scenario C4 Cost Intake $24,200,000 Raw Water Pumping $5,700,000 Rapid Mix $1,200,000 Flocculation $300,000 Sedimentation $13,900,000 Filtration $2,900,000 Finished Water Storage $18,200,000 High Lift Pumping $3,800,000 Chemical Systems $1,600,000 Total Capital Cost Estimate for Scenario 4 $71,800,000 The American Association of Cost Engineers has established guidelines for cost estimate accuracy versus project definition development level. This estimate is a conceptual-level (0%-2% project definition) cost estimate for comparison purposes only. The expected accuracy range is -30% to +50% as shown in Table C-5. The Engineering News Record Construction Cost 20-City Average Index was equal to 9552 at the time of cost estimate preparation (July 2013). Table C-5 Expected Accuracy Range for Capital Cost Estimate Expected Accuracy Range Cost Plus 50% $107,700,000 Minus 30% $50,300,000 C-7

8 Scenario 4 Cost Breakdowns C-8

9 City of Evanston Wholesale Water Sales Services Intake (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $1,234,000 2 SITE WORK Trenching and Backfill $4,455,000 54" Pre-stressed Concrete Cylinder Pipe (5,940 ft) $2,970,000 54" PCCP From Shoreline to Shorewells $2,380,000 3 CONCRETE 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES 10 SPECIALTIES 11 PROCESS EQUIPMENT 12 FURNISHINGS 13 SPECIAL CONSTRUCTION Marine Dive Crew and Equipment $1,782,000 Zebra Mussel Control $182,000 Intake Cone Heater $520,000 54" Pipe Fittings $21, " x 54" Intake Cone with Crib Intake $30, CONVEYING SYSTEMS 15 MECHANICAL 16 ELECTRICAL SUBTOTAL $13,574,000 UNDEVELOPED DESIGN DETAILS (35%) $4,751,000 SUBTOTAL $18,325,000 CONTRACTORS FEES, OVERHEAD & PROFIT (10%) $1,833,000 CONTINGENCIES (5%) $1,008,000 ENGINEERING. LEGAL, AND ADMINISTRATIVE (15%) $3,024,000 TOTAL CAPITAL PROJECT COST $24,200,000 C-9

10 City of Evanston Wholesale Water Sales Services Low Lift Pumps (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $288,000 2 SITE WORK Demolish Existing Low Lift Pumps 5 & 6 $30,000 3 CONCRETE Concrete Pump Pad $16,000 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES Pipe Painting $10, SPECIALTIES 11 PROCESS EQUIPMENT Two Low Lift Pumps with VFDs $853,000 Two Direct Engine Drives $1,300, FURNISHINGS 13 SPECIAL CONSTRUCTION Instrumentation $66, CONVEYING SYSTEMS 15 MECHANICAL 36" Elbow $20,000 36"x 30" Reducer $29,000 30" Butterfly Valve $49,000 30" Check Valve $76, ELECTRICAL $431,000 SUBTOTAL $3,170,000 UNDEVELOPED DESIGN DETAILS (35%) $1,110,000 SUBTOTAL $4,280,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $430,000 CONTINGENCIES (5%) $240,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $710,000 TOTAL CAPITAL PROJECT COST $5,700,000 C-10

11 City of Evanston Wholesale Water Sales Services Rapid Mix (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $62,000 2 SITE WORK Remove Rapid Mix Weir $13,000 Remove Rapid Mixer $10,000 3 CONCRETE Concrete Pads for Davit Crane $5,000 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES 10 SPECIALTIES 11 PROCESS EQUIPMENT Four Water Champ Mixers $60, FURNISHINGS 13 SPECIAL CONSTRUCTION Four Raw Water Flow Meters $156, CONVEYING SYSTEMS Davit Crane $3, MECHANICAL Chemical Piping with Heat Tracing $95,000 Chemical & Plant Water Piping $105, ELECTRICAL Electrical and Instrumentation $170,000 SUBTOTAL $680,000 UNDEVELOPED DESIGN DETAILS (35%) $240,000 SUBTOTAL $920,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $90,000 CONTINGENCIES (5%) $50,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $150,000 TOTAL CAPITAL PROJECT COST $1,200,000 C-11

12 City of Evanston Wholesale Water Sales Services Flocculation Basins (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $14,000 2 SITE WORK Modify Influent and Effluent Ports $74,000 3 CONCRETE 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES 10 SPECIALTIES 11 PROCESS EQUIPMENT Flocculation Paddle Reconfiguration $35, FURNISHINGS 13 SPECIAL CONSTRUCTION 14 CONVEYING SYSTEMS 15 MECHANICAL 16 ELECTRICAL Flocculator VFDs (Basins 1 & 2) $28,000 SUBTOTAL $150,000 UNDEVELOPED DESIGN DETAILS (35%) $50,000 SUBTOTAL $200,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $20,000 CONTINGENCIES (5%) $10,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $30,000 TOTAL CAPITAL PROJECT COST $300,000 C-12

13 City of Evanston Wholesale Water Sales Services Sedimentation Basins (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $706,000 2 SITE WORK 3 CONCRETE 10-inch Concrete Slab over Pretreatment Basin Roof $1,624,000 Sedimentation Basins 1 & 2 Hatch Repairs $25,000 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES 10 SPECIALTIES 11 PROCESS EQUIPMENT Tube Settlers $5,411, FURNISHINGS 13 SPECIAL CONSTRUCTION 14 CONVEYING SYSTEMS 15 MECHANICAL 16 ELECTRICAL SUBTOTAL $7,770,000 UNDEVELOPED DESIGN DETAILS (35%) $2,720,000 SUBTOTAL $10,490,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $1,050,000 CONTINGENCIES (5%) $580,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $1,730,000 TOTAL CAPITAL PROJECT COST $13,900,000 C-13

14 City of Evanston Wholesale Water Sales Services Filters (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $148,000 2 SITE WORK Demo Filter Influent Concrete $6,000 Demo Filter Influent Piping $45,000 Demo Filter Influent Valves $17,000 Demo Filter Influent 24-inch Wall Casting $12,000 Demo 6-inch Surface Wash & 30-inch Backwash Valves $25,000 3 CONCRETE 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES Pipe Painting $6, SPECIALTIES 11 PROCESS EQUIPMENT 12 FURNISHINGS 13 SPECIAL CONSTRUCTION Replace 1948 Venturis and Actuators $155,000 Replace 1964 Venturis, Valves and Actuators $175,000 Control Valves & Limit Switches (All Valves for East Filters) $120,000 Surface Wash Arms (Filters 13-18) $175, CONVEYING SYSTEMS 15 MECHANICAL 30-inch Filter Influent Valves & Actuators (East Filters) $150, inch Filter Wall Castings and Piping (East Filters) $118, inch Backwash Valves & Actuators (East Filters) $300,000 6-inch Surface Wash Valves & Actuators (East Filters) $80,000 Miscellaneous Piping for ROFC Improvements $50,000 Master Washwater Valve Actuator (East Filters) $10, ELECTRICAL Electrical & Instrumentation $33,000 SUBTOTAL $1,630,000 UNDEVELOPED DESIGN DETAILS (35%) $570,000 SUBTOTAL $2,200,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $220,000 CONTINGENCIES (5%) $120,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $360,000 TOTAL CAPITAL PROJECT COST $2,900,000 C-14

15 C-15

16 City of Evanston Wholesale Water Sales Services High Lift Pumps (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $196,000 2 SITE WORK Demolish Existing High Lift Pumps 2 & 5 $78,000 3 CONCRETE Concrete Pump Pad $16,000 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES Pipe Painting $10, SPECIALTIES 11 PROCESS EQUIPMENT Two High Lift Pumps with VFDs $711,000 One Direct Engine Drive $650, FURNISHINGS 13 SPECIAL CONSTRUCTION Instrumentation $66, CONVEYING SYSTEMS 15 MECHANICAL 36"x 30" Reducer $29,000 30" Butterfly Valve $49,000 30" Check Valve $76, ELECTRICAL $272,000 SUBTOTAL $2,150,000 UNDEVELOPED DESIGN DETAILS (35%) $750,000 SUBTOTAL $2,900,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $290,000 CONTINGENCIES (5%) $160,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $480,000 TOTAL CAPITAL PROJECT COST $3,800,000 C-16

17 City of Evanston Wholesale Water Sales Services Chemical Systems (132 MGD All Conventional Filtration) Capital Cost Breakdown DIVISION ITEM COST 1 GENERAL CONDITIONS (10%) $81,000 2 SITE WORK 3 CONCRETE 4 MASONRY 5 METALS 6 WOOD & PLASTICS 7 MOISTURE & THERMAL PROTECTION 8 DOORS & WINDOWS 9 FINISHES 10 SPECIALTIES 11 PROCESS EQUIPMENT Chlorine Chemical System Upgrade $181,000 Fluoride Chemical System Upgrade $55,000 Orthophosphate Chemical System Upgrade $181,000 Polymer and Alum Metering Pump Skids $70,000 Polymer Day Tank Modifications $12, FURNISHINGS 13 SPECIAL CONSTRUCTION Instrumentation $154, CONVEYING SYSTEMS 15 MECHANICAL 16 ELECTRICAL $154,000 SUBTOTAL $890,000 UNDEVELOPED DESIGN DETAILS (35%) $310,000 SUBTOTAL $1,200,000 CONTRACTORS FEES OVERHEAD & PROFIT (10%) $120,000 CONTINGENCIES (5%) $70,000 ENGINEERING, LEGAL & ADMINISTRATIVE (15%) $200,000 TOTAL CAPITAL PROJECT COST $1,600,000 C-17