R-99-04

WATER TREATMENT ESTIMATION

ROUTINE (WATER) USER MANUAL

Water Desalination Research &

Development Program Report No. 43

August 1999

U.S. DEPARTMENT OF THE INTERIOR

Bureau of Reclamation

Technical Service Center

Environmental Resources Services

Denver, Colorado

and

Lower Colorado Regional Office

Boulder City, Nevada
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REPORT DOCUMENTATION PAGE mm APProYed fM”R Ah rl70d.Ol.QR I

)IlhliC rannnina burden to,

1 August 1999 Final

t. TrnE FIND SUSTITLE

Water Trwment Estimation Routine (WaTER)

User Mamu

Michelle Chapman Wilbert, John Pellegrino, Jennifer Scott, Qian Zhang

Bureau of Fkclamation

Denver Federal Center

PO Box 25007

Denver CO 80225-0007

3. SPDNSDRlNO,MDNlTDRlNG AGENCY NAMW, AND ADDRESSESI

Bureau of Fkclamation

Denver Federal Center

PO Box 25007

Denver CO 80225-OCO7

11. S”PPLEMENTARY NOTES

ksalR&D No. 43

12% D,STR,S”TIDN,~“AI~S,lLlTY STATEMENT

Available from the National Technical Information Service, Operations Division,

5285 Port Royal Road, Springfield, Virginia 22161

As with anything else, water treatment cost estimates are difficult to get a handle on without somewhere to begin. This document and

the spreadsheet program it describes are just that - a place to begin. With minimal information, such as a rough idea of the water

analysis and the capacity of the treatment systems, this program provides cost estimates based on theoretical equipment sizes and

chemical requirements. It is not intended to be a final design cost estimate. It is intended as a tool for comparing different process

options at a” early phase in the planning process. Processes included in the program are microfiltration, reverse osmosislnanotiltration.

elecuodi~lysis, ion exchange, gravity filtration, granular activated carbon, disinfection and chemical feed systems.

14. SmJEC1’TERMS-- 15. NWVISER OF P*GES

water treatment cost/membrane cost model/microfiltration/reverse osmosis/nanofiltration/ion 70

exchange/electrodialysislchlorine/chloraminelozonelacidl~~fe~ic sulfate/polymer/potassium

pamangaa~tellimelsoda ash/granular activated carbon/gravity filtration/upflow solids contact 16. PRICE CODE

clarifier/pumpslcleanvell storage
R-99-04

WATER TREATMENT ESTIMATION ROUTINE (WATER)

USER MANUAL

Water Desalination Research & Development Program Report No. 43

Michelle Chapman Wilbert’

John Pellegrino’

Jennifer Scott2

Qian Zhang’

Technical Service Center

Environmental Resources Services

Denver, Colorado

and

Lower Colorado Regional Office

Boulder City, Nevada

‘Environmental Resources Team

‘National institute of Standards and Technology

August 1999

UNITED STATES DEPARTMENT OF THE INTERIOR * BUREAU OF RECLAMATION
U.S. Department of the Interior

Mission Statement

The mission of the Department of the Interior is to protect and provide access to our

Nation’s natural and cultural heritage and honor our trust responsibilities to tribes.

Bureau of Reclamation

Mission Statement

The mission of the Bureau of Reclamation is to manage, develop, and protect water and

related resources in an environmentally and economically sound manner in the interest of

the American public.

Disclaimer

The information contained in this report regarding commercial products or firms may not be used

for advertising or promotional purposes and is not to be construed as an endorsement of any

product or firm by the Bureau of Reclamation.

The information contained in this report was developed for the Bureau of Reclamation: no

warranry as IO the accuracy, usefulness, or completeness is expressed or implied.

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ACKNOWLEDGEMENTS

Several people have been vitally important to the success of this project. Bill Boegli has been a

fount of information; I must thank him for the loan of his water treatment books, and advice on

determining dosage rates (without a water sample). Pat Giarrantano, now retired from the National

Institute of Standards and Technology (NET), provided the loan of her personnel for the start of

this effon:. Kim Linton’s review resulted in many improvements in the user experience which

were sorely needed, as any who tried to review the draft product will appreciate. Most of all, this

final product would not be possible without funding from the Water Desalination Research and

Development (DesalR&D) Program.

“1
CONTENTS

Introduction.. ........................................................................................................................................... 1

Overview of Water Treatment Estimation Routine ................................................................................. 3

Input Requirements.. ............................................................................................................................... 5

Production and Index Input ........................................................................................................... 5

Water Analysis Input..................................................................................................................... 5

Water Data Reports ....................................................................................................................... 5

Cost Indices ................................................................................................................................... 5

Cost Reports.. ................................................................................................................................ 5

Microfiltration ........................................................................................................................................ I

hmoduction ................................................................................................................................... I

Microfiltration Input...................................................................................................................... 7

Process input from Micro input worksheet .......................................................................... 7

Operation and maintenance cost input.. ............................................................................... 8

Process flow calculation ...................................................................................................... 8

Microfiltration Output ................................................................................................................... 9

Capita1 cost estimation:........................................................................................................ 9

Indirect capita1 cost.. ............................................................................................................ 9

Operation and maintenance cost estimation. ........................................................................ 10

Reverse Osmosis and Nanotiltration ....................................................................................................... 13

Introduction ................................................................................................................................... 13

RO&NF Input ............................................................................................................................... 13

Process input ....................................................................................................................... 13

Data from membrane product specifications ...................................................................... 14

Determination of operating pressure .................................................................................... 17

Membrane system size estimation ....................................................................................... 17

Operation and maintenance cost input parameters............................................................... 17

RO,&NF Output ............................................................................................................................. 17

Capital cost estimation ......................................................................................................... I7

indirect capital cost.. ............................................................................................................ 21

Operation and maintenance cost estimation. ........................................................................ 21

ion Exchange .......................................................................................................................................... 25

Introduction ................................................................................................................................... 25

Design ........................................................................................................................................... 25

Re!;in Medium ............................................................................................................................... 26

Ve:ssel cost .................................................................................................................................... 27

Regeneration ................................................................................................................................. 21

Regeneration and Backwashing Pump .......................................................................................... 27

output ........................................................................................................................................... 28

Electrodialysis.. .......................................................................................................................................

Design ...........................................................................................................................................

Input .............................................................................................................................................

Cost Computation ..........................................................................................................................

”

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29

30

31
CONTENTS

Disinfection and Chlorine and Choramine. ............................................................................................. 33

Design ........................................................................................................................................... 33

Input ............................................................................................................................................. 33

Cost Computation.. ........................................................................................................................ 34

Output ........................................................................................................................................... 35

Links ............................................................................................................................................ 35

Assumptions.. ................................................................................................................................ 35

Ozone Disinfection ................................................................................................................................. 37

Introduction ................................................................................................................................... 37

Purpose.. ........................................................................................................................................ 37

Links ............................................................................................................................................. 37

Cost Computation.. ........................................................................................................................ 37

Acid Feed ............................................................................................................................................. 39

Design ........................................................................................................................................... 39

Input ............................................................................................................................................. 39

Cost Computation.. ........................................................................................................................ 41

Output ........................................................................................................................................... 41

Links ............................................................................................................................................. 41

Assumptions .................................................... . ............................................................................. 41

Improvements ................................................................................................................................ 41

Alum or Ferric Sulfate Feed .................................................................................................................... 43

Design ........................................................................................................................................... 43

Input ............................................................................................................................................. 43

Cost Computation.. ........................................................................................................................ 43

Output ........................................................................................................................................... 44

Links ............................................................................................................................................. 44

Assumptions .................................................................................................................................. 44

Polymer Feed .......................................................................................................................................... 45

Design ........................................................................................................................................... 45

Input ............................................................................................................................................. 45

Cost Computation.. ........................................................................................................................ 45

Output ........................................................................................................................................... 45

Links ............................................................................................................................................. 45

Assumptions .................................................................................................................................. 45

Potassium Permanganate.. ....................................................................................................................... 47

Input ............................................................................................................................................. 47

Cost Computation .......................................................................................................................... 47

Output ........................................................................................................................................... 47

Links ............................................................................................................................................. 41
CONTENTS

Lime & Soda Ash Feed ........................................................................................................................... 4 9

Design ........................................................................................................................................... 49

Input ............................................................................................................................................. 50

Cost Computation .......................................................................................................................... 50

Output ........................................................................................................................................... 50

Links ............................................................................................................................................. 50

Assumptions.. ................................................................................................................................ 50

lm~provements ................................................................................................................................ 50

Granular Activated Carbon ..................................................................................................................... 5 1

Introduction ................................................................................................................................... 51

Cost estimate ................................................................................................................................. 51

Gravity Filtration ..................................................................................................................................... 53

Introduction ................................................................................................................................... 53

Design ........................................................................................................................................... 53

Cost estimation .............................................................................................................................. 53

Improvements ................................................................................................................................ 53

Upflow Solids Contact Clarifier. ............................................................................................................. 55

Introduction. .................................................................................................................................. 55

Design ........................................................................................................................................... 55

Cost Computation .......................................................................................................................... 55

Pumps ............................................................................................................................................. 57

Introduction.. ................................................................................................................................. 57

Design ........................................................................................................................................... 57

Dilrect costs.. .................................................................................................................................. 57

Operating Costs ............................................................................................................................. 58

Ou.tput ........................................................................................................................................... 58

Clearwell Storage .................................................................................................................................... 59

Introduction ................................................................................................................................... 59

Input ............................................................................................................................................. 59

Ca,st Computation .......................................................................................................................... 59

Output ........................................................................................................................................... 60

Water Analysis.. ...................................................................................................................................... 61

Bibliography .......................................................................................................................................... 63

Appendix ............................................................................................................................................. A-l

vii
CONTENTS - continued

Tables

Tllhle Page

1 Valid Dose ranges for chemical addition processes.. ........................................................... 4

2 Indices used in updating water treatment costs .................................................................... 6

3 Membrane Data ................................................................................................................... 14

4 Default values for ion exchange operational parameters ..................................................... 25

5 Default values for resin parameters ..................................................................................... 25

6 Default parameters for Electrodialysis cost estimates .......................................................... 30
INTRODUCTION

One of the primary concerns in updating an older water treatment plant, or building a new one is: “How

much will it cost?” These days, there are many alternative water treatment processes in use, with pros and

cons for each. Before one gets mired in the differences, similarities, and potential for success, it is

reassuring to look at the price tags. Cost is one tangible way to eliminate options. Yet cost is one of the

most difficult aspects of a process to get a handle on before the design process has begun. According to

Peters and Timmerhaus, in Plant Design and Economicsfor Chemical Engineers (1980), an order of

magnitude estimate should cost about $4000 (1979$). It requires knowledge of the water composition,

plant capacity, location and site requirements, utility requirements, raw materials and finished product

handling and storage requirements. Yet, the cost is needed before any agreements are made.

In 1994, the Bureau of Reclamation built a mobile Water Treatment Plant Trailer for the purpose of

exploring ‘water treatment alternatives. One of the questions most frequently asked is “How much will

these systems cost?’ Because of that, we have tried to automate the cost estimation process so that we can

provide a reasonable answer based on production capacity, and the water analysis. Sure, there are many

ways to specify which equipment is used, but when you step back and look at a long history of water

treatment system costs, it is possible to come up with a set of good generalizations.

Back in 1979, the EPA published a very thorough study on water treatment costs (EPA-60012-79-162). It

separates costs into different categories for manufactured equipment, labor, pipes and valves, electrical and

instrumentation, housing, etc. Then costs are repotted and graphed for different sizes of plants. The

trouble is {that you cannot use the graphs until you know the size of the process. For instance, chlorine feed

cost is based on the number of kg/day of chlorine needed. Chlorine demand is usually determined through

jar tests, which require money, time, and a fresh water sample. In addition, if you wanted to compare

chlorination with ozonation, you would need to have the size of the ozone contact chamber. These items

are not generally included in a standard water analysis.

In a joint effort between the Bureau of Reclamation, and the National Institute of Standards and

Technology, a water treatment design spreadsheet program has been developed to address this problem.

This Excel spreadsheet estimates the design parameters needed to drive the EPA cost estimates, then

updates cost information for several water treatment processes to current dollars. The capacity

requirements and minimal input about the process are entered on Capacity worksheet. Also, the water data

report based on water analysis is shown on the Capacity worksheet. The water analysis is entered in the

H20 Analysis worksheet. Cost indices based on the Engineering news Record construction cost index and

Bureau of Labor Statistics (February, 1999 built in) are entered on the Cost Index worksheet and may be

updated b:y the user. Cost and sizing calculations for the different processes are performed on linked

worksheets. These worksheets contain the parameters that may be refined when the equipment is specified

more exactly. Cost and relevant design parameters are reported back to the Report worksheet.

The program calculates dosage rates and cost estimates for the following water purification processes:

. pH adjustment with sulfuric acid.

. Disinfection with chlorine, chloramine, and ozone.

. Coagulation/Flocculation with alum, ferric sulfate, and lime/soda ash using upflow solids

contact clarifiers.

. Filtration enhancement with polymer feed.

. Filtration with granular activated carbon, and granular media.

. Microtiltration as pretreatment to remove particulate materials

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. Demineralization with ion exchange, electrodialysis, and reverse osmosis

. Pumping: raw water, backwash, and finished water pumping.

The Water Treatment Estimation Routine (WaTER) is based primarily on the EPA report Esrimaring

Water Treatment Cosrs, Vol. 2, Cost Curves Applicable m 200 mgd Treatment Plants (EPA-600/2-79-

1626, August 1979). For estimates using cost curves from this EPA report, or from Qasim et al. (AWWA,

Aug. 1992). the assumptions used in the EPA report are pertinent. The EPA report details the

configuration of each process, and what is not included. The EPA is working on an update to that cost

study. When it is published, we hope to incorporate the new cost curves and parameters into this program.
OVERVIEW OF WATER TREATMENT ESTIMATION ROUTINE

The Water Treatment Estimation Routine is an Excel workbook. WTCOSTxls is the name for this Excel

workbook. Computer requirements are as follows:

. Windows 95 or higher

. Microsoft Excel Office 97.

. Pentium Co-processor is desirable.

Open the workbook by double clicking on the file name. To bring a desired worksheet into the window,

single-click on the name of the worksheet tab at the bottom of the screen. To navigate through the

worksheets, simply, click on the name of the worksheet tab. Remember that the worksheets are linked so

that changes in one worksheet will be reflected in the other worksheets. The worksheets included are:

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Capacity-Production capacity and water data report.

H20 Analysis -Water analysis

Cost Index -Current cost indices

Report-Reports for water treatment processes

Micro Input-Input for Microfiltration sizing

Micro Output - Output for Microfiltration cost

RO&NF Input - Input for Reverse Osmosis or Nanofiltration sizing

Rejection -Calculates observed rejection for given water and recovery rates

RO&NF Output - Output for Reverse Osmosis or Nanofiltration cost.

ION-EXH - Ion exchange resin volume and cost

ED2 - Electrodialysis sizing and cost

CL2 -Chlorination dosage and cost

NHCl - Chloramine dosage and cost

OZONE -Ozone dosage and cost

DG&ACID - Acid dosage

ACID -Acid feed cost

ALUMFD - Alum dosage and cost

LRONFD -Ferric sulfate dosage and cost

POLYFD -Polymer dosage and cost

KMn04 - Potassium permanganate dosage and cost

LlMEFD -Lime and soda ash dosage and cost

GAC -Granular activated carbon cost

GRAVFILT - Granular media filter sizing and cost

UFSCC - Upflow solids contact clarifier sizing & cost

PUMPS -Pump sizing and cost

CLEARWELL - Below ground and ground level clearwell cost

Water Analyses - A collection of general water analyses in case you need one.

Most worksheets contain a set of data that have been used to create graphs to demonstrate the relationship

between cost and capacity for a range of dosage rates, or sizes, depending on the appropriated parameter

for the process. You may perform sensitivity studies with these worksheets to determine how the cost is

effected by the various process parameters.

3
To create a new set of data for the worksheet of interest, first, erase the old set of data, then change the

desired parameters, click on the Macro command button with the name of the worksheet on it located on

top of the data set. Repeat this process to generate the data. The graphs incorporated into the worksheets

will update automatically when data are changed. Samples of the graphs are included in the appendix.

The applicable ranges for some treatment process are listed in Table 1. If the calculated values for your

system are outside these ranges, the cost values may not be representative.

Table 1. Valid Dose ranges for chemical addition processes.

Name Range Metric Units Range English

Units

CL

NHCL

ACID

ALUM (Dry)

ALUM (Liquid)

IRONFD

POLYMER

4 - 4500

110-2300

0.04 - 20

4 - 2300

2 - 2500

6 - 3000

0.5 - 100

0.5 - 100

kg/day

kg/day

ml/day

kglhr

kglhr

kg/day

kg/day

kg/day

9 - 9921

243-5071

11 -5264

9 - 5071

4-5512

13-6614

1 - 220

l-220

lb/day

lb/day

gal/day

Iblhr

lblhr

lb/day

lb/day

lb/day

LIME 4 - 4500 kg/hr 9 - 9921 Ibihr

4
INPUT REQUIREMENTS

You may refer to the copy of [WTCOST.XLS] Capacity, H20 Analysis, and Cost Index worksheets in the

appendix or, better yet, the screen version on your computer.

Production and Index InpUt: The Capacity, H20 Analysis, Cost Index, and Report worksheets

allow the user to estimate costs for each treatment process separately. It requires following general

information:

. Required plant feed flow rate in Llsec

. Desired plant product flow rate in Usec

. Water analysis

. Cost Indices: February 1999 included.

Water halysis Input: This table summarizes metals and inorganic components. Water analysis data

is entered in the shaded column labeled “Water Analysis” in the units specified. Concentration is

compared with the USEPA Drinking Water Standards Maximum Contaminant Level (MCL). If there is an

exceedance, it is calculated and appears in BOLD in the next column, labeled “Amount over MCL.”

Equivalents per liter, and concentration in moles/liter, are calculated for your convenience, and for

bookkeeping purposes.

Water Data RepOttS: Vita1 data from the water analysis are listed in the Capacity worksheet. These

data, calculated or repeated from the water analysis, are used in the design algorithms.

Cost Indices: The cost components are based on those used by Qasim (1992). Each is tied to one of

the Engineering News Record (ENR) or Bureau of Labor Statistics (BLS) indices. Table 2 lists the cost

components from February 1999 used in updating water treatment costs. Cost curves from the Qasim

paper were updated from April 1992. Cost curves developed directly from the EPA report were updated

from October 1978.

Cost Reports: The Report worksheet is set up with sections for each process. Each contains the name

of the process in the upper left comer. Variables are listed that are either taken from the Capacity

worksheet, or are entered in the colored or shaded cells.

Conshuction cost, and operation and maintenance costs are reported in each section. This represents the

first level of generalization. To refine the estimates further, it is necessary to adjust process design

parameters that have assumed values on their separate worksheets.

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Table 2. Indices used in updating water treatment costs.

Cost Component

Excavation & site work

Index 1999

1967=100 Value

ENR Skilled Labor Wage Index 548.67

Manufactured equipment

Concrete

Steel

Labor

Pipes and valves

Electrical equipment and

instrumentation

Housing

Energy requirements Local $/kWh

Maintenance material BLS Producer Price Index for Finished Goods

requirements Code SOP3000

Labor requirements Local $/hr

BLS General Purpose Machinery & Equipment

Commodity Code 114

BLS Concrete Ingredients

Commodity Code 132

BLS Steel Mill Products

Commodity Code 1017

ENR Skilled Labor Wage Index

BLS General Purpose Equipment

Producer Price Index 1149

BLS Electrical Machinery 8 Equipment

Commodity Code 117

ENR Building Cost Index

149.10

150.20

106.60

548.67

164.30

120.60

505.81

0.07

131.30

3 0

Now we get to the major drawback of using a spreadsheet for this type of application. The costs reported

here are based entirely on the water analysis and production data as they are entered in the water analysis

tables. If you want to use only one of the processes, that would be fine. However, the composition of the

water will change after it has left any one of the processes. Then, the next process cost is based on the

wrong water composition. You, the user, will have to pick the process flow scheme for your application,

and adjust water analysis accordingly. The cost report should then be copied to another area of the

spreadsheet and converted to values so that it will not change when you adjust the water analysis. In this

way you can build a more accurate report for your application.

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MICROFILTRATION

(MF INPUT & OUTPUT)

Introduction:

Microfiltmtion is used as pretreatment to remove particulate material from water, including

microorganisms such as protozoa, bacteria (Giardia and Cqptosporidium) to meet new and future

environmental requirements. The purpose of this section is to provide cost estimation for Microfiltration.

This section consists of two worksheets: Micro-input and Micro-output. The cost estimation is based on

factory-a:;sembled hollow fiber Microfiltration units.

Most of the Microfiltration membranes system includes the following equipment:

. Membrane module skids - membrane modules, backwash manifold pipework, integral valves

and instruments, support legs, control panels.

. Air supply system - air compressors, air dryers, coalescers and air filters, process air receiver,

air regulator, plant pneumatic control enclosure, solenoid valves and instruments.

. Clean in place - concentrate tank, concentrate transfer pump, solution tank, solution tank

heater and control panel, re-circulation pump, valves and instruments.

. Control system main control panel, master PLC, plant I/O, man-machine interface.

.

The Microfiltration membrane manufacturers can provide more details on the scope of supply.

Micro input worksheet consists of:

. Process input

. Operation and maintenance cost input

. Process flow calculation

Micro output worksheet consists of:

. Capital cost estimation(direct and indirect)

. Operation and maintenance cost estimation

Microfilltration Input:

Process input from Micro input worksheet:

The following parameters are needed for cost estimation:

Design product flow rate (gpd)

Plant availability (%)

Microfilters system equipment cost ($)

Cost per MF membrane ($)

MF modular system flow rate (gpm)

No. membranes per microfilter

Pump efticiency (%)

Motor efficiency (%)

Design feed pressure (psi)
. Backflush pressure (psi)

. Backwash intervals (minutes)

. Backwash and backflush duration (minutes)

Operation and maintenance cost input:

. Electricity rate ($/kwh)

. Chemical costs (sodium hypochlotite, $/L)

. Design dosage (II@)

. Specific gravity of sodium hypochlorite

. Solution concentration (76)

. Membrane life (year)

. Staff days/day

. Labor rate (salary and benefits, $/lx)

. Amortization time (year)

. Interest rate (7%)

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Processflow calculation: All values in this section are calculated from inputs listed above. MF feed flow

is the total feed flow to the Microfiltration plant. It is calculated by:

Where: MFF = Microfiltration feed flow (Wsec)

MFP = Microfiltration product flow (L/SK)

Y = Recovery rate

MF reject flow (MFR (L/SK)) is the amount of water used for backwash and cleaning of the membranes.

It is calculated by:

MFR = BBD * BBF

BI

Where: BBD = backwash and backflush duration (set)

BBF = backwash flow rate (L/set)

BI = backwash interval (set)

Recovery rate (R) is calculated by:

Feed pump brake horsepower (HP) is calculated by:

Hp=MFF*DFP*2.31

PP% * 3960

Where: DFP = design feed pressure (psi)

8
PP% = pump efficiency (%)

2.31 = conversion factor for feet of vertical head of water per lb/in’

3960 = another English-Metric conversion factor.

Feed pump kilowatt-hour (kwh) is calculated by:

kWh = MFF * DFP * 2.31* 0.00315

PP%*M%*looo

Where: M% = motor efficiency (%)

0.00315 = conversion factor for consumption of electrical energy

Building area in square meter is estimated to be 1.23 percent of the design product flow rate in cubic meter

per day.

Microfiltration Output:

The cost estimate does not include concentrate disposal, National Environmental Policy Act (NEPA)

compliance, or water system storage and distribution cost.

Capital coot estimation:

Direct capital costs are the sum of microfilters, building, MF installation, miscellaneous, plant

interconnecting piping, engineering. These cost elements are discussed below:

Microfilters: The actual price for microfilters is obtained from membrane manufacturers. The price will

vary upon the type of microtilters and quantities involved. The total microfilters cost is estimated as the

cost per skid unit times the number of units.

Building: The building cost is estimated $1076 per square meter times the total building area in square

meter.

MF installlation: The microfilter installation cost is estimated $70,000 per unit for a large system (at

37.85 L/s flow rate).

Miscekmeous: This cost includes that any miscellaneous items needed to complete the project. It is

estimated 5 percent of the total microfilter cost.

Plant interconnecting piping: This cost estimated 5 percent of the sum of total microfilter and

miscellaneous costs.

Engineering: Engineering cost is estimated 10 percent of the sum of total microfilter and miscellaneous

costs.

Indirect capital cost:

The indirect capital costs are the sum of:

. Interest during construction (6% of total direct capital cost)

. Contingencies (20% of total direct capital cost)

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. A&E fees and project management (10% of total direct capital cost)

. Working capital (4% of total direct capital cost)

Operation and maintenance cost estimation:

Operation and maintenance costs include:

. Electricity

. Labor

. Chemicals (sodium hypochlorite)

. Membrane replacement

. Cleaning chemicals

. Repairs and replacement and miscellaneous

Total annual cost equals the capital recovery cost plus the total operation and maintenance costs. These

major O&M cost elements are discussed below:

Electricity: Electricity cost is the total kilowatt-hour for the feed pump and backflush pump times the

electricity cost ($/kwh).

Labor: This cost is estimated by the number of staff days times the going rate per day.

Chemicals: The cost of Sodium hypochlorite for disinfection is estimated based on the correlated formula

from the Microfiltration membrane quotation data:

SHC * (.0025 * MFP - 333.33)

Wh-Ze: SHC = sodium hypochlorite cost ($/L)

Membrane replacement: The cost is estimated by

Elements * $ I Element

Cleaning chemicals: Sodium hypochlorite cost is estimated based on the correlated formula from the

Microfiltration membrane quotation data:

(0.00005 * MFP + 66.67) * SHC

Repairs and replacement and misc.: The cost for repairs and replacements assumed to be 0.5% of the

total direct capital cost.

10
Capital recovery cost: The capital recovery cost equals

TCC *

i * (l+ i)” [ 1(1+ i)“”

Where: TCC = total construction cost

i = interest rate

n = number of years

1 1

REVERSE OSMOSIS AND NANOFILTRATION

(RO&NF INPUT, REJECTION AND RO&NF OUTPUT)

Introduction:

The purpose of this section is to provide cost estimation for Reverse Osmosis (RO) and Nanofiltration

(NF). This section is made up of three worksheets: RO&NF Input, Rejection and RO&NF Output.

RO&NF Input worksheet consists of:

. Process input

. Data from membrane product specification

. Determination of operating pressure

. Membrane system size estimation

. Pump size estimation

. Operation and maintenance cost input parameters

The Rejection worksheet calculates the actual membrane rejection and water permeation rates from the

membrant: specifications for the present water quality. These values are used to calculate the osmotic

pressure differential and the membrane area needed.

RO&NF Output worksheet consists of:

. Capital cost estimation (direct and indirect)

. Operation and maintenance cost estimation

RO&NF Input:

Process in@: The calculation routine is based on desired product or permeate flow rate. Desired product

flow rate i.s the value entered on the Capacity worksheet. The percent recovery, the ratio of product flow

rate to feed flow rate, is entered on the Report worksheet in the Reverse Osmosis section. If the recovery

value is too high, there will be problems with the cost estimate. To give you an idea of what recovery rates

should be, first check the delta G value in the water data report section in Capacity worksheet. If it is

negative or close to zero, or if you plan to use acidification and/or antiscalants, you can use the following

estimates.

Seawater 50 %

15,000 to 20,000 TDS 75 %

5,000 to 15,000 TDS 85 %

Nanofiltration 90 %

These values are only estimates; the maximum recovery possible depends on the composition of the feed

water.

If the product water concentration is lower than necessary, as is often the case with RO, it may be possible

to decreze the membrane system capacity by blending the product water with pretreated feed water. The

blending aoption is specified in the RO and NF section of the Report worksheet. If the response is yes (Y).

the ratio of blend water to product will be calculated based on the target product water TDS. The

membrane system will be sized for the resulting smaller capacity. If no (N) is entered, this value will be

13
zero. The maximum portion of blend water that can be used, assuming the blend water has the same TDS

as the feed water is calculated as follows:

c,v, = c,v, + c,v,

v, = G-C,

c, -c,

Where C stands for concentration in mg/L, V is flow, with VT = 1. Subscripts T is for target, p is for RO

permeate and b is for blend water.

Datafrom membrane product specijications: Information for this section is obtained from the membrane

product specification sheets provided by membrane manufacturers. Table 3 lists data needed. This data

should be on all manufacturers specification sheets.

Table 3: Membrane Data

Type of membrane Film Tee. BW30-400

Productivity 40 m’lday

Area per module 37 m2

Operating pressure, P,, 1550 kPa

Test solution TDS 2000 mglL

MW of test salt 58.44 mglmmol NaCl

Chloride Rejection 0.995

Sulfate Rejection 0.998

Recovery Rate 15 %

Temperature 25 “C

These parameters are used to calculate the water transport coefficient, A, and the intrinsic and actual

rejection rate. The water transpon coefficient measures the permeation of water through a membrane for a

unit of applied pressure. It is calculated by:

J

A=----

NDP,

Where: A = water transport coefficient, m3m-2 sec.‘Pa-’

J” = initial module productivity taken from the specification sheet, m3/day

mp0 = net driving pressure under test conditions, kPa

NDP, = P,, Pm

Net driving pressure under test conditions, NDP,:

Where: P app = operating pressure at test conditions, Wa

Posrr = osmotic pressure of the feed water, Wa

14
Osmotic p~ressure of the feed water, Posm:

P o,,=0.99*2*R*(273.15iT)*~,/1000

Where: R = universal gas constant, n?.Pa/mole.K

T = temperature, “ C

C, = concentration at the membrane surface. As a first approximation this is take,” as

the average of the feed and concentrate concentrations, mole/m3

0.99 = NaCl dissociation constant.

Concentration of salt in feed water, Ct:

Where: TIX, = feed TDS, mg/L

Avg MW = feed average molecular weight, assuming NaCl is used to test the membranes, this

would be 58.4 g/mole.

Osmotic pressure of the feed solution, concentration polarization and the resulting decrease in productivity

are accounted for using a model method developed by Rao and Sirkar (1978) for the perfectly mixed feed

and permeate model, with concentration polarization

Let C, = boundaty layer concentration at the membrane interface caused by concentration polarization.

Assume that no gel formation occurs. Because the feed side is perfectly mixed, C, = C,, where C, = bulk

concentration.

Then: C, =

c, - ec,

l-0

where 9 = recovery rate of water. The intrinsic rejection of a membrane is defined as R”= l-C&. This is

different from the apparent rejection, R, = I CJC,. The intrinsic rejection is a characteristic of the

membrane. The apparent rejection is determined by the operating conditions. For lack of anything better,

we assum’: that the reported rejection, most likely measured under optimum conditions with a minimum

chalienge., is close to the intrinsic rejection. We can then use this to estimate C,, the wall concentration

and the C,, the product concentration to be expected with the current operating conditions.

From the simple boundary layer model for concentration polarization and assuming that R” is constant, the

following relationship for C, is obtained:

15
The wall concentration is

C,=C,

I

exp[+]

R”+(l-R”)exp +

l 1.

From the material balance C, = C,, is defined by:

c, =c, =

CJ

(l-l?)+

8(1- R”)enp+

R’+(l-R”)exp+

With k = the boundary layer mass transfer coefficient. The variable ‘k’is obtained via a correlation that

assumes that J, <<(I,, where U, is the average cross flow velocity. The correlation used in this model is

from Schock & Miquel(l987) for RO membrane in spacer filled flat channels.

k = 0.065 * Re’.“’ SC~-=~

Re is the Reynolds number and SC is the Schmidt number.

Re = prCd

r7

d zz representative channel or tube dimension for flow (i.e., diameter)

a = average cross flow velocity

P = density

rl = shear viscosity

D = solute diffusivity

Now we can calculate the actual rejection, R,

The actual permeation rate J, is now:

As calculated above with the new estimation for C,. This group of relationships is non-linear because of

the exponential term and must be solved iteratively (using successive substitutions). There is a graph of R,

and J, on the Rejection sheet showing the solution progress through much iteration. If the solution fails to

stabilize, check the inputs for accuracy.

16
Determimztion of operatingpressure: The NDP used for the specification testing is the default NDP used

to determine the recommended operating pressure. The user can change this value. The osmotic pressure

of the feed water is calculated as described above and then the operating pressure is calculated as follows:

P app = NDPi f Pa,

Where: P,,, = applied operating pressure under the conditions of interest for the cost estimate,

kPa

NDPi = net driving pressure entered by the user (may chose to enter the manufacturer’s test

NDP,), kPa

P Own = osmotic pressure difference between the bulk stream and product stream based on

the membrane rejection and recovery rate and the water analysis provided, kPa

It is assumed that the water transport coefficient, A, is constant under all conditions, independent of feed

water TDS and operating pressure. The new J,is calculated as above using the new pressure conditions.

Membrane system size estimation: With J, calculated for the water quality and operating pressure, the

number of membrane modules can be calculated. There are user inputs for the number of modules per

vessel and number of vessels per block. The required number is rounded up to tit into the specified

configuration. The number of blocks determines the number of chemical feed systems and pressure

pumps. The user specifies the number of product water pumps, transfer pumps, raw water pumps and the

administrative building area.

There are three different types of pumps: single stage turbine (SST), centrifugal single speed (CSS) or

variable speed turbine (VST). There is a different cost correlation for each type based on horsepower. All

of the pumps sizing calculations are the same. Pomp horsepower is based on the capacity per block,

pressure differential, pipe diameter, length of piping and vertical lift needed. Pipe diameter is tied in with

the capacity per block. The lengths of piping and vertical lift have default values. Pressure differential for

the high pressure pumps is based on the calculated operating pressure. The other pumps have default

V&K?&

Operation and maintenance cost inputparameters: Chemical costs, membrane life, cleaning rate, and

operation!; labor can be input in this section. Number of labor hours includes only hours required for the

reverse osmosis system. Electrical costs and labor cost are brought over from the Cost Index sheet.

RO&NF Output:

Capital cost estimation:

The relations for most of the direct capital costs are extracted from technical paper presented by Suratt

(1995). Direct capital costs are the sum of membranes, RO skids, building, electrical, instrumentation &

controls, high pressure pumps, raw water transfer pumps, product water pumps, degasifiers, odor control,

process p:lping, yard piping, chemical feed with pumps, cartridge filters, membrane cleaning equipment,

contractor engineering & training, concentrate treatment & pipin,,e c1oenerators, and sitework. These major

construction cost elements are discussed below:

17
Membranes: The actual price for membrane is obtained from membrane distributors. The price will vary

upon the type of membrane and quantities involved. The total membrane cost is estimated as:

$750 per high rejection RO element is used for membrane estimation.

RO skids: This cost is a function of the number of pressure vessels. The cost is estimated as

$/vessel * Number of vessels

RO skids include the pressure vessels supported by structural painted steel skid support frame, piping

connector sets for each vessel, and piping manifolds. $5000 per pressure vessel is assumed (Suratt, 1995).

Building: The cost is estimated as

Unir Cosr($/ m2 ) * Building Area( m2 )

Unit costs vary depending on the level of architectural treatment and the location of the plant being built.

$1,076 per m* is used for this spreadsheet (Suratt, 1995).

Electrical: The cost is estimated using a model adapted from Suratt, 1995.

$/m3 * product capacity0’6s

Product capacity is in m’/day. $614 per m3 of product water is used for this spreadsheet (Suratt, 1995).

Instrumentation & control: The formula for this cost is

$300,000 + $65,000 * Number of RO skids

$300,000 is for the central computer system. Additional of $65,000 is for the local instrumentation and

controls per skid.(Suratt, 1995)

High pressure, raw water transfer, product water pumps: The cost of equipment and installation is a

function of horsepower. An IF statement is built in this cell as follows: the cost for Single Speed Turbine

(SST) is

58,000 * (HP/I 00 p6’

The valid horsepower range for SST is 3 HF’ to 300 HP.

18
Variable Speed Turbine (VST) is

85,OOO*(HP/IOO fn5

The valid horsepower range for VST is 3 HP to 500 HP.

Centrifugal Single Speed (CSS) equals

35,OOO*(HP/IOO )'.'*

The valid horsepower range for CSS is 3 HP to 350 HP.

The horsepower (HP) is determined by using equation (10) in page 516 (Peters and Timmerhaus,1980) as:

Where: W = theoretical mechanical energy, hp

Z = vertical distance above datum plane, m

V = linear velocity of fluid, m/xc

gc = gravitational acceleration, 9.81 m/s*

P = absolute pressure, kPa

Y = specific volume of the fluid, m3/kg

Degasifiers: The equation used to estimate this cost is

1.5006 *X +3765.7

where X is product capacity in m’/day.

Product d’egasifiers are used when hydrogen sulfide exists in raw water and large amounts of carbon

dioxide are liberated when the raw water pH is lowered.

Odor conltrol: If odor control is specified yes (y) in the RO&NF input worksheet. The cost is estimated

by

320.9* xn6

where X is product capacity in m’/day. Otherwise, it is zero

19
Process piping: The size is a function of plant capacity and recovery rate. The cost is

15.852 * X/Y

Where X is product capacity in m3/day and Y is recovery rate in percent

Chemical feed with pumps (acid, antiscalant, chlorine): Pump size is a function of dose rates and flow

rate of feed water and product water. An IF statement is built into the cost of the acid system. It stated that

if acid concentration is greater than zero, the formula to calculate the cost is

where

AC = acid concentration, mL/L

S C = storage cost

N S = number of skids

X = product capacity, m31day

Y = recovery rate, %

P = density, g/mL

If concentration is less than zero, then cost is zero.

Cost formula for antiscalant and chlorine is

where

AS = antiscalant concentration, mglL

CCC = chlorine concentration, mg/L

S C = storage cost

N S = number of skids

X = product capacity, m’/day

Y = recovery rate, o/o

P = density, g/mL

Cartridge filters: cartridge filters are a function of feed water flow rate. The cost is estimated by

112,836 * CS"~80J'* NS *I.2

where CS is capacity per skid, m3/s. NS is number of skids.

Membrane cleaning equipment: Use $67,000 as an installed system price. This system is based upon

cleaning 14 tubes at one time at a flow rate of 50 gpm per tube.

20
Concentrate treatment & piping: The cost is

where COC is concentrate cost ($/n?), X is product capacity (&/day), and Y is recovery rate (%).

coc*x*(l-YyY

Generators: The cost is estimated at

150,000 * (kwRO/l 000 jOKS + 50,000

Where kwR0 is the RO & Building electricity usage estimated as

14 * (x/Y)/3785

X is product capacity (m3/day). Y is recovery rate (Q/o).

Sitework: The cost is

where TC is the feed flow in m3/day. SWC is sitework cost in $/m’.

TC * SWC

Indirect azpital cost:

The indirect capital costs are the sum of:

. Interest during construction (4% of total construction cost)

. Contingencies (6% of total construction cost)

. A&E fees and project management(lZ.% of total construction cost)

. Working capital(4% of total construction cost).

Operation and maintenance cost estimation:

Operation and maintenance costs include:

. Electricity

. Labor

. Chemicals (acid, caustic, antiscalant, and chlorine)

. Membrane replacement

. Cleaning chemicals

. Cartridge filters

. Repairs and replacement

21
. Insurance

. Lab fees

Total annual cost equals to capital recovery cost plus the total operation and maintenance costs. These

major O&M cost elements are discussed below:

Electricity: Electricity is the largest operating cost. It is estimated by:

kwR0 is the RO &Building electricity usage. X is product capacity (&/day). Y is recovery rate (%)

(kwRo+kwHPP+(kwRWT +kwPWP))* PA*365* 24* 2

kwHPP equals: 746 * NS * PYI 000

kwHPP is the high pressure. pump electricity usage. NS is number of skids. PS is the pump size (hp).

kwRWT and kwPWP equal

746 * NP * PS/lOOO

kwRWT is raw water transfer pump electricity usage. kwPWP is product water pump electricity usage.

NP is number of pumps. PS is pump size (hp).

Labor: This cost is estimated by

SD*LR*8*365

where SD is staff days. LR is labor rate.

Chemicals: IF statements are built in for both acid and caustic. If acid concentration is less than zero, then

cost is zero. Otherwise, acid cost equals

Where: AC = acid concentration, mL/L

X = product capacity, &/day

Y = recovery rate, %

PA = % availability

ACC = acid cost, $/kg

PZid = density of acid, g/ml

2 2
If caustic Iconcentration is less than 1, then cost is zero. Otherwise, caustic cost equals

CC * TC * 1000 * 365 * PA * CAC/( p * 1000’ )

Where: cc = caustic concentration, mLiL

TC = total capacity, m3/day

PA = % availability

CAC = caustic cost, $/kg

Pb2S = density, g/mL

Antiscalant cost is

AS * TC * 1000 * 365 * PA * AK/( p * 1000’ )

WUtZ: AS = antiscalant concentration, mg/L

TC = total capacity, &/day

PA = plant % availability

ASC = antiscalant cost, $/kg

pAr = density, g/mL

Chlorine cost equals

CCC * TC * 1000 * PA * 365 * CLC/f per, * 10002 )

Where: ccc = chlorine concentration, mg/L

TC = total capacity, m’/day

PA = % availability

CLC = chlorine cost, $/kg

PG = density, g/mL

Membrane replacement: The cost is estimated by

(Number of elements * $/element)/membrane life

Cleaning chemicals: Cleaning chemicals are H2P04 and NaOH. H2P04 solution concentration is 0.05%

F* NM *(D’*~*102/4)*1.15*(0.005* PHC+O.OOI*SDC*2)/1000

NaOH solution concentration is 0.1%. The cost equals

F = cleaning frequency

NM = number of modules

D = membrane diameter, cm

PHC = HzP04 cost, $/kg

23
SDC = NaOH cost, $/kg

iT = .3.14

1.15 = correction factor for pipe tilling

Cartridge filters: The cost is estimated by

23097 * CPS - 6.245 * NS * 12

Where: CPS = capacity per skid, m’/sec

N S = number of skids

Repairs and replacements, insurance: The cost for repairs and replacements assumed to be 0.5% of the

total capital cost and 0.2% of the total capital cost for insurance.

Lab fee: The cost equals

$800 * 12 * NS

where $800 is the cost for one water analysis sample test and 12 samples per year. NS is number of skids.

The install cost in ($/m’ per day and $/gallon per day) and total annual cost in ($ per m3, $ per acre-foot, $

per 1000 gallons) of product water also can be found in the RO&NF Output worksheet.

TCC*i*(l+i)“/((l+i)“-I)

Capital recovery: Capital recovery cost equals

Where: TCC = total construction cost

i = interest rate

” = number of years

24
ION EXCHANGE

(ION-EXH)

Introduc:tion:

Ion exchange resins are insoluble granular materials which have free cationic, or anionic radicals in their

structure. These ions can be exchanged for ions of the same sign in the solution. Ion exchange is used for

de-mineralization.

Design:

The purpo:je of this worksheet is to provide a cost estimation for an ion exchange unit based on available

design pammeters. Data required from the Capacity worksheet includes:

. Desired flow rate Usec

. Equivalents/L of Cation > +I in water Equiv/L

. Equivalents/L of Anion > -1 in water Equiv/L

Parameters with default values can be modified on the ion exchange worksheet. They are shown in the

table 4. Table 5 lists suggested ranges for resin parameters.

Table 4: Default values for ion exchange operational parameters.

Parameter Value Unit

Desired run cycle 7 Days

Resin expansion coefficient 200 %

Cost factor for pressure 1

Aspect ratio 2 Height/diameter

Cost of NaCl $0.02 /kg

Table 5: Default values for resin parameters.

-

Parameter Value Unit

13equired service flow rate Range 16-40 U(hr’L resin)

Cation equivalents/L of Resin 1.9 Equiv/L

Anion equivalents of Resin 1.4 Equiv/L

Resin price $6700 Id

‘Jobme NaCl/volume resin for regeneration 483 kg/m’

l?egeneration fluid concentration 10 %

2 5
Resin Medium:

The minimum resin volumc(n?) is calculated by:

Min resin Volume( m3 ) = Desired flow rate(Lf..)

Service jlow rate(LJhr * L resin)

Time until resin exhaustion (days) is calculated by:

Time until Resin exhaustion(days) =

MRV * (EQC + EQA)

FR * (ECR f EAR)

Where: MRV = minimum resin volume, m3

EQC = Equivalents/L of Cation > +l in water, EquivYL

EQA = Equivalents/L of Anion > -1 in water, EquivYL

ERC = Cation Equivalents/L of Resin, EquivYL

EAR = Anion Equivalents/L of Resin, Equiv/L

FR = Desired flow rate (L/s)

An lF statement is built in for the resin volume required to meet exhaustion time. It states that if time

until resin exhaustion is greater than the desired run cycle, then the resin volume required to meet

exhaustion time is equal to the minimum resin volume. Otherwise, the resin volume required to meet

exhaustion time is calculated by:

RVET= RC*FR*(EQC+EQA)

(ECR + EAR)

Where: RVET = resin volume required to meet exhaustion time, days

RC = desired run cycle, days

Resin manufacturers recommend an expansion coefficient of two to provide ample room for the resin to

expand during upflow regeneration.

Total Vessel Volume (TVV) is calculated by:

TW = RVET * Resin expansion coeflcient

Resin Cost (RC) is calculated by:

RC=MRV*RP

Where: RP = nominal resin price, $/m’

2 6
Vessel Cost:

The fiber glass pressure vessel cost is calculated by the following formula:

Log($)=3.44609+0.561757*Log(TW)

Regeneration:

NaCl is used for the resin regeneration. Amount of NaCl required is calculated by the following equation:

NaCl required = pNon * RVET

WhtTe: PNKl = density of N&I, kg/m’

The total chemical cost per year is calculated by:

WhtXe: NaCl,,,,= sodium chloride cost, S/kg

DRC = desired run cycle, days

365 = days per year

Storage tank cost is calculated by:

Tank Cost = 0.1427 X3 - 5.6691 X2+257.56X - 467.45

where X is the tank volume in m3. This formula is developed from the Snyder cone bottom tank, HDLPE

model tank prices.

Regeneration and Backwashing Pump:

Construct~ion cost and O&M cost formulas for regeneration and backwashing pump are developed from the

1979 EPA report (EPA-600/2-79-162b).

Construction cost(CC):

CC=36000+1254.21X -0.1212~~

2 7
Operating and Maintenance cost (O&M):

Where X is the filter area in m2

output:

Total construction costs include resin cost, resin operating tank cost, storage tank cost, and regeneration

and backwashing pump cost. This total construction cost and Operating cost are output to the Report

worksheet.

28
ELECTRODIALYSIS

(EW

Design::

The design model for electrodialysis is from a paper presented by Thomas D. Wolfe of HPD Inc. at the

American Water Works Association meeting in August, 1993. It is a simplified version of the complex

calculations required to design an ED system but, according to Mr. Wolfe, it is adequate for one pass

desalination of brackish water. If the desalination ratio (input TDS/output TDS) is less than 3.6, the model

Kwh AM*26.8*1/,. IkW

In3 Curr eff IOOOW

gives a good estimate of power and membrane requirements as follows:

~ = Feed TDS (g/m’) Diluate TDS (g/m”)

Ave.EqWt. (g/eq)

Current Eff = [XC’ Eff + XA- off]- -oo~~o~cIDzfi8

Where: 26.8 Amp*hrs/eq is Faraday’s constant.

C’ and A- represent each cation and anion species.

0.006 (eq/(cmz*hr*eq/m3) is the Salt Diffusion Coefficient.

Total Resistance, Rt = Rd + R, + R,

Where: & is the dilute side resistance,

R, is the concentrate side resistance,

R, is the membrane resistance,

V,=R,*CD+V,

V, is the electric potential per cell pair,

V, is the membrane electric potential,

CD is current density.

2 9
Power requirement is given by:

KWatts =

m3 treated *$&z

hr m3

Membrane area requirements:

AreacmZ)= watts

Amps per ,,,’ *Volts

The number of pairs required:

No. of Pairs =

Area ( m2 )

Area (m2)/pair

Input:

There are several input requirements for this model which are taken from the Capacity and Cost Index

worksheets:

. Feed and product TDS: mg/L

. Average equivalent weight: g/eq

. Flow rate: &/day

. Percent recovery: %

. Cost of electricity: SlkWh

The following table includes variables that are entered on the electrodialysis worksheet. The current

values are approximations. More exact information can be obtained from the membrane manufacturer for

the membrane in question.

Table 6: Default parameters for Electrodialysis cost estimates.

Variable Value Unit

Cost of Membrane $100 m2

Cation and Anion transport efficiencies 0.874

Area per membrane pair 0.862 m2/pair

Resistances (Rt) 2.5 Ohms/cm’

Current density 38 Amp/dm’

Membrane electric potential per pair 0.25 Volt/pair

Electra-osmotic coefficient 0.003 mllma’hr

30
Cost Computation:

Capital cost is determined by multiplying the membrane cost by the construction factor. The construction

factor used here is 1.65. This value was arrived at by adjusting the membrane operation variables till the

electrical and membrane requirements matched those listed in a published cost estimate (Pittner, 1993) and

then multiplying by an appropriate construction factor so that the costs matched also.

Operation and maintenance costs are the sum of chemical addition, maintenance, membrane replacement,

labor, electricity and capita1 recovery costs. Chemical addition costs are dependent on the TDS of the feed

water and are indexed to the “Maintenance Material Index.” General maintenance is 5% of the capital cost

and is also indexed to Maintenance Material. Membrane replacement is the amortized cost of replacing the

membranes in 15 years at the given interest rate. Labor cost is simply S/year at the given labor wage rate.

Electricity requirements are calculated above. Capita1 recovery is the amortized cost of the capital over the

life of the plant at the given interest rate.

31

DISINFECTION WITH CHLORINE AND CHLORAMINE

(CL2 AND NHCL)

Design:

Cost estimation for chlorine and/or chloramine disinfection is based on the amount of chemicals used per

day. Chlorine demand is determined from the concentration of nitrite and reduced inorganic transition

metals, such as chromium, copper, iron, and manganese, present in the water. These metals are oxidized

from +2 charge to +3 by the hypochlorite ion by the following reaction (Snoeyink & Jenkins, 1980, pp.

391-395):

Hypochlo:rite reacts with nitrite to form nitrate:

HCIO- + NO; - NO; + Cl- + H’

Therefore, one mole of aqueous chlorine is needed for each two moles of divalent transition metal, and one

mole for each mole of nitrite, before the required chlorine residual will accumulate.

For disinfection with chloramine, ammonia is reacted with free chlorine in the water to form mono- and dichloramine:

NHj,,,,+HOCl-NH?Cl+H,O

NHzCl+HOCl-NHClz+HzO

The ratio of ammonia to hypochlorite used for maintenance of a combined chlorine residual is 1:l

Input:

The concentration of chromium, copper, iron, manganese, and nitrite is taken from the H20 Analysis

worksheet. Chlorine demand is given by:

3 3
Chlorine residual and chloramine residual are input from the Report worksheet. The volume of water

treated is input from the Capacity worksheet. The kilograms of chlorine needed per day is then:

where Clzd is the chlorine demand and Clzr is the free chlorine residual.

If chloramine disinfection is used, chlorine demand is determined as for chlorine disinfection, then

ammonia and chlorine are added in a one to one molar ratio to produce the required residual.

mgNH3 _ mg NH z Cl/L 17mg NH3

L-- 51.4 mg NH~ Chmole * mm& NHz Cl

mg Chuqj = mg CIZd + mg NHzCfi .+ 71 w Cllcaql

L L 51.4 mg NH 2 Cl/mmole mm& NH 2 Cl

Cost Computation:

Capital cost, and operation and maintenance costs are calculated from the formulas for chlorine storage and

feed with cylinder storage in Qasim et al. (1992).

Where X = kg Cl? per day.

Cost formulas for ammonia addition are based on anhydrous ammonia feed:

cc = 3849.2 * xD.MR * e-J.5E.5-x

0 + MC = - 28063 * e1-Z.4’E-4*X’+ 36160

Where X = kg NH, per day (Qasim, et al, 1992).

34
output:

The worksheet for chlorine disinfection returns the capital, and O&M cost for chlorine addition sufficient

to supply the chlorine demand, and provide the indicated chlorine residual. The chloramine disinfection

worksheet returns capital cost and O&M cost for addition of both chlorine and ammonia, sufficient to

produce the combined chlorine residual specified. This cost estimate may be high if there are overlapping

costs associated with the combination of chlorine addition and ammonia addition formulas.

Links:

. Transition metal and nitrite concentration is taken from the water analysis table on the H20

Analysis worksheet.

. Treatment requirements input from the Report worksheet.

. Costs output to Report worksheet.

Assumptions:

There are three important assumptions made in the cost modeling for chlorine and chloramine disinfection:

. The sum of the concentrations of metals and nitrite will give an adequate estimate of chlorine

demand. The oxidation state of these metals is not usually given in a water analysis, so it is

assumed that the whole concentration is at a +fI state. This is probably not accurate, but it

may balance out other chlorine demand that is not accounted for in this model.

. A 1:l ratio of residual chlorine to ammonia will produce the necessary combined chlorine

residual. According to V.L Snoeyink and D. Jenkins (Water Chemistry, p 395, 1980, John

Wiley & Sons), the ratio of residual chlorine, as Cl?, to initial NH, oxidized is 1 at a ratio of

1 :I, Cl2 dose:NH3 initial. The combined residual at this point is composed of NHzCl with a

trace of NH&

. For chloramine disinfection, Qasim’s cost models for chlorine addition and ammonia addition

are added together using the amounts of each needed for the required residual. This may give

a high cost estimate due to overlap in cost items in the two models. It is assumed that the

overlap is insignificant. Manufactured equipment is the highest component for each of the

processes. Housing is second for chlorine feed and storage. The two chemicals would need

their own equipment for feed and storage, so these components are not highly overlapping.

The portion that may be significant is the labor cost for O&M. This cost may need

modification in the future.

35

OZONE DISINFECTION

(OZONE)

Introduc:tion:

Ozone (O,), an allotrope of oxygen (O?), is one of the most powerful oxidizing agents available for water

treatment. A substantial amount of energy is required to split the stable oxygen-oxygen covalent bond to

form ozone. The resulting Oj molecule is highly unstable. It was thought that ozone might be a suitable

replacement for chlorine, which forms tri-halomethanes. Ozone has the potential to form the same

byproducts though, as long as halides are available to react with the oxidized organic compounds. Ozone

decomposes rapidly, however, which makes it a safer choice for pretreatment ahead of chlorine sensitive

membrane processes.

Purpose!:

This work:;heet provides an estimation of capital costs and yearly power costs for an ozone system. The

capital cost estimation includes costs associated with the ozone generator and the contact chamber.

Estimates are derived from equations found in Qasim et al. (1992). Electricity costs are computed using a

nominal power requirement per kilogram of ozone produced, and the local cost of electricity per kWh.

Links:

Ozone dor,age in mg/L, and contact time in minutes, are taken from the Report worksheet. Values of 3

mg/L, and 2 minutes, are suggested as normal levels. Flow rate is taken from the Capacity worksheet.

Electrical ,:ost is taken from the Cost Index worksheet.

Cost Co’mputation:

Ozone generation, and contact chamber costs are calculated by the following equations for 1992 dollars,

then updated with the current index values.

o~~c~,r~ = 392.4 * x0.919 + 68000

Where x = chlorine feed capacity in kg/day

Where x = chamber volume in m’.

Operation and maintenance costs for the contact chamber are included with those for ozone generation.

31

ACID FEED

(DG&ACID AND ACID)

Acid feed may be used in reverse osmosis to lower the pH of the feed water to levels compatible with the

membranes used. With cellulose acetate membranes, this 1s about pH 5.5. Thin film composite

membranes are not as sensitive to pH as cellulose acetate, but acid feed still may be used to control scaling

Design:

The Langelier Saturation Index (LSI) is normally used to predict the carbonate scaling tendency of water.

In this model the Gibbs Free Energy (AG) is used instead. The AG calculations can be used for

determining other solubility equilibria whereas, LSI is only for determining carbonate solubility. LSI can

be calculated from AG as follows.

L‘.yI= AG

2.3* RT

Where: R = 1 .987x1U3 kcal/mol*‘K

T = Temperature in “K

2.3 is a factor for converting from natural log to log base 10

The reaction equations of interest in carbonate solubility are:

CO2,,,+ Hz 0 tf COz,,,, : 1% KH = - 1.41

CaCOa,, ff Ca” f CO;- : log K,, = - 8.15 (1)

and

I

H‘ + CO;- W HCO; : log - = 10.49

K”J

(2)

Summations of equation (1) and (2 ) equal:

cacox,, + H’ tf ~a’+ + HCO; : log K = 2.34

3 9
Activity coefficients are calculated for calcium and bicarbonate ions from the ionic strength taken from the

Capacity worksheet. .

log 1: = 0.5091* z’ * [+$-0.2*PJ

p=o.5*zci*z:

WheK?: cj = Concentration of the i” ionic species,

ZI = charge of the i” ionic species,

!J = ionic strength,

Y = activity coefficient of the ith ionic species

Gibbs Free Energy is given by:

AG=AG”+RT*lnQ

Where: R = 1 .987xIU3 kcaVmol*“K, is the universal gas constant.

AG” = theoretical solubility of calcium carbonate at 298°K and,

RT*lnQ = solubility under the pH, temperature conditions with the reported

concentrations of Ca” and HC03., adjusted for ionic strength.

If AG is positive, the water is over-saturated, and will tend to deposit calcium carbonate scale.

The following charge balance equation is used to calculate the amount of acid needed to change the pH:

[Cations]+ [H+]= [Amons ] [+ OH -1 [ + HCO; ] * +2[ CO2‘~1

All terms are expressed as functions of [H+], solubility constants, ionization fractions, and concentrations

adjusted with their activity coefficients. This equation is solved for the target pH.

Input:

Ca2+ and HCO< concentrations, total cations and anions, water temperature, and current pH, are input from

the water analysis table of t.he H20 Analysis worksheet. Ionic strength is input from the water data report

section on the Capacity worksheet.

40
Cost Computation:

Cost computations are done with ACID worksheet. Liters/second treated is input from the Capacity

worksheet, and acid feed/day from DG&ACID worksheet. Formulas for capital and O&M costs are from

Qasim et al, 1992.

cc= 61,010.6 * x0.79” + 8,818O

0 + MC = - 42,397.4 * ei-6.82E-3*XJ + 43,670

Where X = m3 of sulfuric acid per day.

Output::

AG is output to the water data report section in the Capacity worksheet. Capital cost, O&M cost and liters

96% H*SO? per day is output to the Report worksheet.

Links:

DG&AC:[D worksheet is linked to ACID worksheet, H20 Analysis, water data report in the Capacity

worksheet and the Report worksheet. ACID worksheet cost reports to the Report worksheet.

Assumptions:

Ionic strength is accounted for, but the only scaling tendency checked is that of calcium carbonate. The

system is assumed to be at equilibrium with the atmosphere. Assumptions used in the EPA report are in

effect for this estimate as well.

Improvements:

Scaling tendencies for other constituents should be calculated. The AG calculation could be modified for

this purpose by entering the proper solubility constants. Some good candidates would be silica, calcium

sulfate, b,arium sulfate, strontium sulfate, and ferric hydroxide.

41

ALUM OR FERRIC SULFATE FEED

(ALUMFD AND IRONFD)

Alum or ferric sulfate coagulation is used for clarification. It is another process, like lime softening, that is

designed t,o lower turbidity through precipitation of a sparingly soluble salt.

Design:

Alum or ferric sulfate react with alkalinity in the water to produce a hydroxide precipitate. Both react

according to the following formula:

Fe>( Sod jj f 6 HCO; tf 2 Fe(OH Jj J + 3 so:- + 6 COT

Commercial grade alum and ferric sulfates are available as Al~(S0~)~*18H~O (MW: 666.41), and

Fe2(S0&9Hz0 (MW: 562), respectively.

Input:

Alkalinity is taken from the water analysis section of the H20 Analysis worksheet. Volume of water

treated is taken from the Capacity worksheet.

Cost Colmputation:

Formulas For ferric and alum sulfate feed capital and O&M costs we from Qasim et al. (1992). There are

formulas for both dry, and liquid (50% by weight), alum sulfate feed. Generally, the dose of liquid alum

needed is twice that for dry alum.

Ferric Sulfate : CC = 10613 * x”“~ * e0.93f-4*XJ

FerricSulfate: O+MC= 1,260,926*~‘-‘94E-S’XJ- 1,257,710

43
Liquid Alum : CC = 13,223.3 * x”*j * &J.nE-4*x)

Dry Alum : 0 +MC = 1,205,293 * e(‘.W33E-5*X’ - 1,202,070

Liquid Alum : 0 + MC = - 6880.7 * &6.59E-4’x’ + 8,700

X = kg per hour of Alum.

output:

Capital and operation and maintenance costs are output to the Report worksheet

Links:

The links are to the Capacity, H20 Analysis, Cost Index, and Report worksheets.

Assumptions:

Those assumptions made in the EPA report on which the cost formulas are based are made here

44
POLYMER FEED

(POLYFD)

Polymer is added to prevent scaling in RO and NF systems. It is also used for clarification and as a

coagulant or flocculant aid.

Design:

The amount of polymer needed depends on the type of polymer and the purpose for adding it. In any case,

very little is needed. The precise amount is determined through jar testing. For design purposes, we will

use 0.5 grams per cubic meter as suggested in the Water Treafment Handbook (0.05 to 0.5 g/m’,

Degremont, 1991, ~144) for a combination of synthetic flocculant and coagulant for clarification of surface

waters.

Input:

Volume of water treated is taken from the Capacity worksheet

Cost Computation:

Formulas for polymer feed capital and operation and maintenance costs are from Qasim et al, 1992:

Where X equals Kg polymer per day.

output:

Capital and operation and maintenance costs are output to the Report worksheet

Links:

The links are to the Capacity, H20 Analysis, Cost Index, and Report worksheets.

Assumptions:

The only assumption, other than those made in the EPA report on which the cost formulas are based, is

that 0.5 mg per liter is a representative dosage of polymer.

4 5

POTASSIUM PERMANGANATE

WMNOJ

Potassium permanganate is an oxidizing agent. It is used for iron, manganese removal

A combination of KMnOJ oxidation and manganese-greensand filtration was selected for testing.

Manganese-greensand provides effective filtration and also controls under and over dosing of KMn04

(prevents the development of pink water breakthrough). Manganese (II) removal depends on the

precipitation of MnOz(s)(manganese[IV] [manganic dioxide], as follows:

Manganic dioxide is insoluble over the entire pH range of interest in drinking water treatment. Also, the

oxidation of both Mn” and Fet2(ferrous iron) using KMn04 is reported to be quite rapid at pH 7 and

higher (Glase, 1990).

The stoichiometry for manganese and iron oxidized with permanganate is:

I,.92 mg/L KMn04 per mg/L of Md’ removed

0,94 mg/L KMn04 per mglL of Fe” removed

Input:

Volume of water treated is taken from the Capacity worksheet.

Cost Computation:

Formulas for potassium permanganate feed capital and operation and maintenance costs are from Qasim et

al, 1992:

0+ MC = -2125.9e-0.0'689X +5600

Where X equals dry potassium permanganate feed in kg/day.

output:

Capital and operation and maintenance costs are output to the Report worksheet.

Links:

The links are to the Capacity, H20 Analysis, Cost Index, and Report worksheets

47

LIME & SODA ASH FEED

(LIMEFD)

Design:

Lime and soda ash are added to precipitate excess carbonate, and in the process, removes metals and

constituents that cause turbidity. Lime, Ca(OH)>, and soda ash, NaKO,, react with carbonate hardness to

precipitate calcium carbonate and magnesium hydroxide.

Ca”+2HCa+Ca(OH),~2CaC~~+2Hz0

Mg’+ + 2 HCO; + 2Ca(OH )* fs Mg(OH )z J +2 CaCOj J + Hz 0

The sum of these two reactions is:

Ca2++ Mg”+4HCO;+ 3Ca(OH )? tt4CaC0, .h +Mg(OH )z J +3H20

This react.ion is used when all components are available. The Mg’+ and Ca”’ are reacted with alkalinity

and lime [to form CaCO; and Mg(OH)z.

The limiting reagent is determined by the mole ratio of each component. Then the amount of lime required

for the initial reaction is calculated. The remaining Mg2+ or Ca” is reacted with remaining alkalinity. If

carbonate alkalinity is zero, no more lime is needed. If Mg’+ is zero, formula (1) is used to calculate

amount off lime to complete softening. Reaction (1) requires one mole of Ca(OH)? per mole of Cazi.

If Mg’+ is not zero, the Ca” is zero, formula (2) is used to calculate amount of lime needed to complete

softening,, Reaction (2) requires 2 moles of ca(OH)? per mole of Mg”.

If HCO&02 were the limiting reagent, which means that Ca” and Mg’+ are in excess of alkalinity. The

soda ash j&z used to precipitate Ca” and Mg*+. The following reactions demonstrate the relationship

between soda ash and Ca” and Mg*‘:

Ca” + NazC03 tf CaCO3 J + 2 Na’

Mg” + Naz CO3 f Ca(OH )J c+ Mg(OH )z J + CaCOj J

4 9
Input:

Calcium, magnesium, carbon dioxide and alkalinity content of the water are taken from the water analysis

in the H20 Analysis worksheet. If the percent reduction column is blank or zero for these values, the cost

estimate will consider the total hardness, resulting in high cost estimates. Volume of water treated is taken

from the Capacity worksheet.

Cost Computation:

Formulas for lime & soda ash feed capital, and operation and maintenance costs are developed from the

1979 EPA report (R.C. Gumerman, 1979)

CC= -24,950.92+20,424.67* In(x)

O+MC= 866.29 * x"'~~'

Where X equals Kg Lime per day

output:

Capital and operation and maintenance costs are output to the Report worksheet

Links:

The links are to the Capacity, H20 Analysis, Cost Index, and Report worksheets. Water analysis data is

taken from the H20 Analysis worksheet and cost data is returned to the Report worksheet.

It is assumed that calcium and magnesium react with bicarbonate ion and calcium hydroxide at the same

rate. If calcium was preferentially precipitated with bicarbonate before the magnesium, more soda ash

would be needed to precipitate the magnesium. This would mean higher capital and O&M cost.

Improvements:

Since lime and soda ash softening is not the technology of choice, cost estimates for this process are

primarily for comparison. Lime softening is not a precision process. As long as lime is added in excess,

the process works. Therefore, refinement of the cost estimate would have to come from new price

information, rather than improvements to the design of the cost model.

The cost estimate provided for lime feed is only for the lime feed system; it does not cover the cost a

clarifier, or sludge processing or disposal.

5 0
GRANULAR ACTIVATED CARBON

@AC)

Introduction:

Granular activated carbon (GAC) is used to remove color, odor, organic chemicals, disinfection byproducts, and chlorine from water through the process of adsorption. If the water has not been pre-tilwed,

the carbon bed may also serve as a granular filter, in which case, backwashing is a more significant design

criteria.

Cost Eetimate:

This worlcsheet provides estimates of the capital and operating costs of a granular activated carbon (GAC)

bed. Both are based entirely on flow rate and bed life. Costs are estimated using relationships derived

from cost data in the 1979 EPA repon. It is apparent from this data that there is a change in size versus

cost relat:ionship at 4000 m’/day. Capital costs for GAC are fairly constant with respect to capacity until a

production level of 4000 m’/day. Above this level, there are different cost curves for a bed life of 3, 6, and

12 months. Regeneration costs are not included. The cost parameter used in these equations is mg/day.

The composition of the water is not considered.

Cost equations are as follows.

3.6, or l:? month bed life, capacity 5 4000 m31day,

12 month! bed life:

cc>4wo = 1948.8 * xf’-.2569’ o~>~~ = 225.42 * ,“--‘”

6 month Ibed life:

cc>mJo = 150 * x OM >4mo = 235.91*x”-.‘~’

51
3 month bed life:

OM p4wo = 1563.45 * xrJ--3463)

CC>4WO = 200 * X OM><wo= 515.91* xi’-.z03j

52
GRAVITY FILTRATION

(SLOWSAND)

Introduc:tion:

Granular filtration removes particulate matter such as algae, colloidal humic compounds, viruses, asbestos

fibers, and colloidal clay from water. Matter accumulates on the surface, or is collected throughout the

depth of the bed. The purpose of this worksheet is sizing and cost estimation of granular filtration systems.

Design:

There are two components: the backwashing system and the gravity filter structure with sand as the media.

Costs for both are based on the area of the filter bed. Required input for area determination are:

. Flow rate (Wsec)

. Total suspended solids b@-)

. Backwash cycle (24 h&cycle)

. Density of suspended solids (35 gm

. Maximum media capacity (110 L TSS/m3 media)

. Media depth (1 4

Flow rate is input on the Capacity worksheet. Total suspended solids is input on the H20 Analysis

worksheet. The other parameters are input on the gravity filtration worksheet. Default values are listed

above.

Cost Estimation:

Costs estimates are derived from equations in Qasim et al. (1992):

OMsw=73.3 * p5 + 2,200

Where x is the area of the filter bed in meters.

Improvements:

Future developments may include modifications of the generalized cost estimation equations to

accommodate using different media.

53

UPFLOW SOLIDS CONTACT CLARIFIER

(UFSCC)

Upflow solids contact clarifiers can be used with lime softening, and alum, or ferric sulfate precipitation.

The chemical slurry is fed into the reaction zone in the center of the clarifier. Feed water flows up through

the precipitate at the bottom. Contact with the solids speeds precipitation so that a shorter detention time is

needed. As the water flows away from the center of the reactor, the solids settle out. Water is collected at

the sides from the surface. Sludge is pumped out periodically from the bottom.

Design:

The size of the clarifier is determined from the flow rate and the detention time. Flow rate is taken from

the Capacity worksheet, and detention time from the Report worksheet. The height of the tank is assumed

to be 4.8 meters. Operation and maintenance cost have three options based on the “rapid mix G value.”

The “rapid mix G value”, or mean velocity gradient is used to determine the size of the floes produced as a

function of the viscosity of the fluid at a certain temperature, and the rate of power dissipated into the tank

volume. These terms are used to calculate G.

where: G= mean velocity gradient, l/s

P = power requirement, Watt

p = dynamic viscosity, N.s/m’.

V= tank volume, m3

Costs for G values of 70, 110, and 150 are computed. Number of clarifiers can be specified in the Report

worksheet.

Cost Clomputation:

Cost curves were derived from data in EPA-600/2-79.162b. These are updated with current index values.

55

PUMPS

(PUMPS)

Introduction:

There are different types of pumps commonly employed in industrial operations. The ones examined in

this work:jheet are Single Speed Turbine (SST), Variable Speed Turbine (VST), and Centrifugal Single

Speed pomps.

Design::

For each type of pump, the horsepower (HP) required by the pump to deliver the volume the water has to

be determined. The horsepower is determined by using equation (10) in page 5 16 (Peters and

Timmerhaus,l980) as:

Where: W = theoretical mechanical energy, hp

z = vertical distance above datum plane, m

V = linear velocity of fluid, m/set

gc = gravitational acceleration, 9.81 m/s2

P = absolute pressure, kPa

” = specific volume of the fluid, m’/kg

Direct Costs:

The cost of these pumps are determined as follows,

Speed Turbine (SST):

5S,OOO*(HP/lOO )'."

The valid horsepower range for SST is 3 HP to 300 HP.

Variable Speed Turbine (VST):

85,000 *(HP/IO0 )'."

The valid horsepower range for VST is 3 HP to 500 HP

Centrifugal Single Speed (CSS):

35,000 *(HP/l00 )o.65
The valid horsepower range for CSS is 3 HP to 350 HP.

Operating Cost:

The operating costs are power consumption, lubrication, cooling water, and maintenance for the pump.

The cost information are based on the Pump Handbook (page 9-66) edited by Karassik, Krutzsch, Fraser,

and Messina. Lubricating oil consumption is based on 0.02 gal/l00 hp-hr for each pair of bearings. A

motor driven centrifugal pump results in 0.04 gal/l00 hp-hr total. Cooling water requirements are based

on 10 “F temperature rise and 2 percent ener,~ loss to the water for each pair of bearings.

The annual operating costs associated with each pump arrangement are developed from the following:

Lubricating oil 0.7 x 0.04 (bhp per 100) x 8760

Cooling water - (0.075 per 1,000) (bhp per 100) x 60 x 8760

Maintenance - 1.5 x bhp

Where bhp is brake horsepower.

output:

The direct costs and operating costs for the pumps are output to the Report worksheet.

58
CLEARWELL STORAGE

(CLEARWELL)

Introduction:

Product water is commonly stored at the plant site with clearwells. Clearwell storage can be constructed

by either below ground in reinforced concrete structures, or above ground in steel tanks. Instrumentation

and control of the clearwell water level is very important to pace the plant output.

Input:

The below ground and above ground level clearwell storage capacities are input on the clearwell storage

section of the Report worksheet.

Cost Computation:

Construction cost formulas for clearwell storage below ground and above ground costs are developed from

the 1979 EPA report (EPA-600/Z-79.162b.page 453-454).

Below ground:

CC=-0.0002X2+99.004X+37941

(for capacity less than or equal to 3785 m’)

CC = 49.084X + 224887

(for capacity greater than 3785 m’)

Ground level:

CC=-0.054X2+104.88X+21400

(for capacity less than or equal to 333 m’)

(for capacity greater than 333 m3)

CC = 0.0002 x ’ + 39.556X + 58237

59
Where X is the clearwell capacity in m3

output:

Construction costs for below ground and above ground level clearwell storage are output to the Report

worksheet.

60
WATER ANALYSIS

This work:sheet contains several different water analyses from locations around the country. These are

listed as desert well, brackish, desert surface, seawater intrusion, agricultural influence, seawater, alkaline

and range land. Feel free to use one of these that seems to tit your application if you do not have an actual

water analyses. Just copy the water analyses of interest and choose “Paste Special” from the edit menu on

the H20 Analysis sheet with your cursor at the top of the water analysis column and choose “paste as

dues”.

61

BIBLIOGRAPHY

Chapman-Wilbext, M. 1993. The Desalination and Water Treatment Membrane Manual. US Bureau of

Fteclamation Report R-93-I 5.

Degr&nont. 1991. Water Treatment Handbook. @Degr&nont, 1991

Engineering News Record. 3128194, p 40 & 49.

Gumennan, R.C., R.L. Gulp, & S.P. Hansen. 1979. Esrimating Water Treatment Costs, Vol. 2, Cost

Cuwes Applicable ro 200 mgd Treatment Plants. EPA-60012.79.1626, August 1919.

Peters, MS. & K.D. Timmerhaus. 1980. Plant Design and Economicsfor Chemical Engineers. McGrawHill Book company

Pittner, G.A. 1993. The Economics of Desalination Processes. Chapter in Membrane Technology, Water

Chemistq, and Indusrrial Applications. Z&id Amjad ed. Van Nostrand Reinhold, NY.

Qasim, S.R., S.W. Lim, E.M. Motley & K.G. Heung. 1992. Estimating Cosls for Treatment Plant

<:onstruction. J. AWWA, pp 57-62, Aug. 1992

Rao, G. and K.K. Sirkar. “Explicit flux expressions in tubular reverse osmosis desalination.”

Desalinarion, vol. 27, no. 99 (1978)

Ray, R. 1992. RO Cost Estimates. in Membrane Handbook. Ho and Sirkar, eds.

Schock, G and A. Miquel “Mass transfer and pressure loss in spiral wound modules.” Desalinarion,

6,4(1987) 339-352.

Snoeyink, V.L. &I). Jenkins. 1980. Waer Chemistq. @ 1980 John Wiley & Sons.

Wolfe, TED., 1993. Electrodialvsis Design Approaches. AWWA Proceedings; 1993 Membrane Technology

Conference. August I-4, 1993, Baltimore, Md. AWWA 1993.

Shields, C. Peter, DuPontpermasep Products, and Moth, Irving Jr., Moth & Associates, Evaluation of

<;lobal Seawater Reverse Osmosis Capital and OperatinE Costs, Technical Paper presented

at the American Desalting Association Conference, Monterey, CA, August, 1996.

Suratt, William B., Camp Dresser & McKee, Inc., Estimating the Cost of Membrane (RO or NF) Water

Treatment Plants, Technical paper presented at the 1995 AWWA membrane Technology

Conference, Reno, NV, August 13, 1995.

Max S. Peters and Klaus D. Timmerhaus, 1980. Plant Design and Economics for Chemical

Eneineers. Copyright 1980 by McGraw-Hill, Inc.

Glase, William H. “Chemical Oxidation,” Chapter 12 in Water Oualitv and Treatment A Handbook of

(:ommunitv Water Supplies, 4”edition, American Water Works Association, McGraw Hill

I:nc., New York, NY, 1990.

Pump Ha-, edited by Igor J. Karassik, Willian C. Kmtzsch, Warren H. Fraser, and Joseph P.

I\4essina, McGraw-hill, Inc., 1976

63

APPENDIX
APPENDIX

INPUT

General input and water data report ._.____.____.._.__._............................................................ Al

Water Analysis: Inorganic .__.___..__.___.____........................................................................... A2

COST WDICES

Current index values ____._______________................................................................................... A3

COST REPORT

Water treatment processes cost report _.__________________.............................................. A4.1 -A4.3

MF INPUT

Process, and O&M cost input .______._.__._._.___...................................................................... A5

Construction costs input __.___.______.______.............................................................................. A6

RO&NF INPUT

Process, construction cost, and O&M cost input ____._______________.......................................... A7

REJECTION

Notes _____...____.____........,..........................................,........................................................... A8

RO&NF OUTPUT

Output for Reverse Osmosis on Nanofiltration cost _.____._____________..................................... A9

DG&ACID

Acid dosage calculations .,..._.__.,_..____.....,.,.,.................................................................... Al 0

Notes and balance equation and Ionic strength calculation ___.___.___...._.___........................ Al 1

ACID

C,ost calculations ............................................................................................................ Al2

Construction cost for sulfuric acid feed.......................................................................... Al 3

O&M cost for sulfuric acid feed .................................................................................... A14

CL2

Chlorine dosage and cost calculations .._______...._..___........................................................ Al5

Construction and O&M Cost for chlorine disinfection at

different dosage rates _________,_________.____________________..................................... ; __._______ Al6
NHCL

Sizing, costs and notes .._.._._........................................................................................... Al7

Construction and O&M cost for chloramine disinfection at

different dosage ratesA 8

OZONE

Input and costs and ozone generator cost calculations ................................................... Al9

Construction cost for Ozone generation at different dosage rates .................................. A20

O&M cost for Ozone generation at different dosage rates.. ........................................... A21

ALUMFD

Sizing and costs ___._____._____._._........................................................................................... A22

Construction cost ,for dry alum and liquid alum feed at

different dosage rates ._______._____..___.................................................................... A23

O&M cost for dry alum and liquid alum feed at different dosage rates .._______.__._..... A24

RONFD

Sizing and Costs __.________.________......................................................................................... A25

Construction cost for ferric sulfate feed at different dosage rates ._________________________________ A26

O&M cost for ferric sulfate feed at different dosage rates _._____..___________......................... A27

POLYFD

Sizing and costs.............................................................................................................. A28

Construction cost for polymer feed at different dosage rates ......................................... A29

O&M cost for polymer feed at different dosage rates ................................................... A30

KMn04

Sizing and costs ____.__.._._________.......................................................................................... A31

Construction cost for potassium permanganate at different dosage rates ________.._____.._,.... A32

O&M cost for potassium permanganate at different dosage rates A33

LlMEFD

Sizing and costs.............................................................................................................. A34

Notes.. ............................................................................................................................ A35

Construction cost for lime softening at different dosage rates.. ...................................... A36

O&M cost for lime softening at different dosage rates ................................................... A37

ii
UFSCC

Sizing and Costs .._______.__............................................................................................ A38

Construction cost for upflow solids contact clarifier with different

detention time ___.__.__.__..._____.............................................................................. A39

O&M cost for upflow solids contact clarifier with different

detention time (G=150) .________.__._.__.__........................................................,....... A40

GAC

Si:zing and Costs ............................................................................................................. A41

Construction cost for carbon filtration .......................................................................... A42

O&M cost for carbon filtration ..................................................................................... A43

GRAVFILT

Sizing and cost repon . .._............................................................................................. A44

Cost calculations for backwashing and gravity filter structure ..___.._._______.___................... A45

Construction cost for gravity filtration at different suspended

solids dosage rates _______._.__._______......................................................................... A46

O&M cost for gravity filtration at different suspended solids dosage rates ..__._______.______ A47

ION_EXH

Design and regeneration system ..................................................................................... A48

Construction cost for Ion Exchange at different dosage rates ........................................ A49

O&M cost for Ion Exchange at different dosage rates ................................................... A50

ED2

Design and cost computation ........................................................................... A5 1.1 -A5 1.2

Construction cost for Electrodialysis at different TDS level .......................................... A52

O&M cost for Electrodialysis at different TDS Level .................................................... A53

PUMPS

Cost calculations ..__.__.____________........................................................................................ A54

CLEARWELL

Below ground level cost calculation .............................................................................. A55

Above ground level cost calculation .............................................................................. A56

Construction cost for below ground clearwell storage ................................................... A57

Construction cost for above ground clearwell storage.. .................................................. A58

WATER ANALYSIS

Generic analyses ..___________._............................................................................................. A59

111
Capacity

FLOW RATE INPUT PAGE, WATER DATA REPORT

lYellow colored cells are mandatory input cells

EnterAvailability.

Plant availability due to down time:’

*Plant availability is used to calculate energy and chemicals costs.

I 0.951

IL/M IGPH

I

IGPD

INPUT CELLS: enter flowrate in ONE of these cells, set rest cells to O=> 01 01

IMGD

5

Flow rate converted to Liters/second and entered in workbook calculations. 0.001 0.001

01

0.01 219.0

/Flow rates converted to a variety of units. I 131421 208,333 1 5.000,000 1 5.001

>

L PLANT FLOW RATES u s GPM

Required Plant Feed Flow Rate:” 292.1 4630

Desired Plant Product Flow Rate: 219.04 3472

“Feed Flow = Plant Product Flow I RO Recovery entered on cost report

WATER DATA REPORTS (based on Water Analysis)

Total dissolved solids (TDS): 700 mg/L

Average equivalent WI.: 26.0 g/equiv

Total equiv./L: 0.024 eq/L

Total aquiv./L (Valence >+l): 0.004 eq/L

Average MW 30.32 g/mol

Ionic Strength: 0.015 mole*charge”Z/L

Delta G: -0.409

2.09E-02 mol/L

1.78E-03 ~1 valence

LSI:

Tendancy to corrosion, may need remineralization.

-0.326

Cost Index

COST INDICES DATA:

Input Current Values

Feb

I999

548.67

149. I

150.2

106.6

JallUaN

1995 1 Source:

489

TBLS Oeneral &pose Machinery & Equipment WPU I 14 (I 91

130.2 IBLS Concrete In~~xiienls PPI 132 (1982 = 1001

115.7 III S str,:1 Mill l’mdII<!l~ WI’I, 1017 (19

IENR Skilled Labor Wage Index (1967=100)

12 = 100)

. ..82= 100)

164.3 I48

I xl h 1 127~4

‘ml 6

EMl Skilled Labor Wage Index (1967=100)

BLS Miscellaneous General Purpose Equipment WPU I 149 (I 982 = 100)

RI..? Elcclrical Machinerv & Equipmen( WPU I I7 (I 982 = 100)

ENR Building Cost Index (I967=100)

Local Energy Cost $kWhr

.l__

0.1

126.2 BLS: PPI Finished Goods (I 982 = 100)

2 0 lLocsl Skilled Labor Rates S/hr

1 I, L ,“Y...ly _“_._.

I) Enerp ($/kWhr) 0.07

.I) Maintenance Material 131.3

K) Lnhor($/hour) 3 0

Intws Rats 8

Amortization time (\T) 2 0

ENR Engineering News Record Construction Cost Index published monthly by McGraw Hill in New York City (212-512-2000)

BLS Bureau of Labor Statistics headquartered in Kansas City IDenver, Colorado Number: 303-844-17261

OR Check the EILS web site at http://stats.bls.govlsahome.html

Water Treatment Cost Estimation Program



Mhcroflltratlon Cost Estlmatlon Program

[Yellow colored cells are mandatory input cells

1
Total Construction Cost s 3.677.150

Cost per gpd capacity I 0.74 [
A-l
wrcost

Pu,re water permeability (m’ls) 4.63E-04

Feed Flow (m’ls) 3.09E-03

Transmembrane pressure (Pa) 1550000

Area (m’) 37

Channel height d,(m) 1.67E-03

C, (mol/m3) 34.22

Density (kg/m3) 1000

Viscosity (Pa s) 0.001

a (Pa m3mol~‘) 4908

Diffusivity of NaCl (m%) 1.20E-09

Calculated paramters determined by configuration and

operating conditions

J, (m/s) 1st pass 125E-05

PJt, (m3m”s.‘Pa.‘) 8.07E-12

>

Average U, (m/s) 9.99E-02

6.3 Schmidt Number 838

Renolds Number 166

t

0.875

0.250

C 0.065

k (m/s) for laminar flow 2.20G05

in flat channel

Solvlng the design equations

J& 0.57

Recovery 0.1500

Intrinsic Rejection R’ 0.996

Appartent Rejection R. 0.9917

C, (mol/L) 70.7728

C, (mol/L) 0.2831

C, (mol/L) 40.2126

J, Theoretical (m3m%.) 9.72G06

EXP (JJk) 1.77

,

0.997

0.996

0.995

0.994

0.993

0.992

0.991

0.990

0.989

l.O2E-05

-

i

t\~ ; ; ; ; s-q-,- l.OlE-05

l.OOE-05

il/- A + A A A A

9.90E-06

A 9.80E-06

r( 9.70E-06

9.60E-06

9.50E-06

r 9.40E-06

12 3 4 5 6 7 8 910

-A-Appartent Rejection Ra +-Intrinsic Rejection Ro

t Jv Theoretical (m3m-2s)

0.44 0.46 0.46 0.46 0.46 0.46 0.46

0.1165 0.1216 0.1209 0.1210 0.1210 0.1210 0.1210

0.996 0.996 0.996 0.996 0.996 0.996 0.996

0.9930 0.9928 0.9928 0.9928 0.9928 0.9928 0.9928

3.0lE+Ol 6,16E+Ol 6.13E+Ol 6.14E+Ol 6.14E+Ol 6.14E+Ol 6.14E+Oi

2.4OE-01 2.46E-01 2.45E-01 2.46E-01 2.45E-01 2.45E-01 245E-01

38.7050 38.9262 38.8950 36.8994 38.8988 38.8989 38.8989

l.OlE-05 l.OlE-05 l.OlE-05 1 .OlE-05 1 .Ol E-05 1 .Ol E-05 1 .Ol E-05

1.56 1.59 1.58 1.58 1.58 1.58 1.58
Cost per ml/day capacity

s ~325

Cost per gpd capacitys 1.23
DGACID
DGACID
Acid

Acid addition cost estimation

Litershec treated 292.05

HzS04 (96%) mL/L 0.03

H2S04 (96%) ma/day 0.77

Basis: 0.77 Applicable Range: 0.04 - 20 m?day

Acid Cost ($/ton): 7 5

1978 Current

index value index value

1978 Capital Cost: Percentages 13,052 basis 1999

A) Excavation and Site Wor 0 0 247 548.67

B) Manufactured Equipment 0.6 16,017 72.9 149.1

C) Concrete 0 0 71.6 150.2

D) Steel 0 0 7 5 106.6

E) Labor 0.16 4,639 247 548.67

F) Piping and Valves 0.07 2,138 70.2 164.3

G) Electrical Equip. and lnst 0.1 2,177 72.3 120.6

H) Housing 0.07 1,814 254.8 505.81

1999 Capital Cost: 1 .OO 1 ,,~$26,784 ~1

1978 O&M Cost: 1,445

I) Energy $IkW*h 0.05 169 0.03 0.07

J) Maintenance Material 0.04 106 71.6 131.3

K) Labor $/hour 0.91 3,945 1 0 3 0

Chemical Cost $/yr: 40,886

1999 0 & M Cost: 1.00 1 $45,105 1

Sulfuric Acid feed

Formula from Qasim. et al, Aug. 1992, AWWA

General Form: A’X”B + C

Capital Cost

A = 6010.6

B = 0.7934

c= 8180

O&M Cost A*eA(B’X) +C

A = -42397.4

B = -0.00682

c= 43670

Wafer Treatment Cost Estimation Program

A-12
Construction Cost for Sulfuric Acid Feed

1 5

1 0

5

0

0.0 0.5 1.0 1.5 2.0

Feed Capacity (m’/day)

2.5 3.0 3.5
O&M Cost for Sulfuric Acid Feed

160

160

140

6 0

40

2 0

0

0.0 0.5 1.0 1.5 2.0 2.5 3.0 3.5

Feed Capacity (m’/day)
A-15
Construction and O&M Cost for Chlorine Disinfection at Different Dosage Rates

2w

180

164l

140

60

4 c

2 c

c 0 200 400 600

Volume Treated (Usec)

800 1,000 1.200

-3mg/L CC -A-3 mglL08MC --F-S mg/L CC -I+5 mg/L 08MC
?z

MM cm!

A=
2,000

1,800

1,600

1.40(

s

g 1.20(

1

I

I -

I

60( I400

200

0

Construction and O&M Cost for Chloramine Disinfection at Different Dosage Rates

200 400 600

Volume Treated (Lfsec)

800 1000 1200

t3mglLCC -S-3mgiLO&MC 45mglLCC -X-SmgkO5MC

Construction Cost for Ozone Generator at Different Dosage Rates

$3.000

200 400 600 600 1000 1200

Volume Treated (Usec)

tl mgACC +3mg/LCC +-5mg/LCC
O&M Cost for Ozone Generator at Different Dosage Rates

$300

z $200

.E

z

> 0-I

IL

: $150

6

$50

Volume Treated (Usec)

+1 mg/L O&MC t3 mglL 08MC -4-5 mg/L O&MC
ALUMFD

Dry Alum Feed Cost Calculations.

Volume Treated USec:

Volume Treated (m31Hour):

Alternative dosage rate mg/L

292

105,

0 0 kg/hr

mg/L mmoles/L

I&carbonate Alkalinity: 212 3.5 I

I

Alum Feed Dry mg/L:

Calculated Alum Feed Dry kglhour:

Basis Feed Rate

0.576 Applicable Range 4 - 2,300 kglhr

I

Percentaaes

1976

index value

I

CUlElll

index value

1976 Capital Cost: $104,062 basis 1999

)A\ Excavation and Siie Work 0

Sj

$0 247 546.671

Manufactured Equipment 0.41 567.262 72.9 149.1

C) concrete 0 SO 71.6 150.2

D) Steel 0 SO 75 106.6

E) Labor 0.03 $6,935 247 546.67

F) Piping and Valves 0.04 99.742 70.2 164.3

Gl Electrical Equip. and lnstmnt. 0.05

Hj Housing

$6,679 72.3 120.6

0.47 $97,091 254.6 505.61

1999 cam4 cost: 1.00 1 $209.706 1

,976 O&M Cost: $12,744

I) Energy $IkW*h 0.17 $5,055 0.03 0.07

J) Maintenance Material 0.03 $701 71.6 131.3

K) Labor $/hour 0.6 $30,565 I O 3 0

Atum cost: $2.249.797

1999 Operation & Maintenance: 1.00 1 $2.266,136 1

A,“,,, Feed Liquid kg/hour:

Need twice as much as dry.

Atternative dose rate mglL

Basis dose rate kglkhr:

810 -Applicable range 2 - 2500 kg/hour

0 0 kg/hr

610

1970 current

1976 capita1 cost:

tAn, Excavation and Site Work

index value index value

Percentages $121,006 basis 1999

0 $0 247 546.671

Ej Manufactured Equipment 0.64 $156,393 72.9 149.1

C) concrete 0 so 71.6 150.2

D) Steel 0 $ 0 7 5 106.6

E) Labor 0.12 $32.255 247 546.67

F) Piping and Valves 0.02 $5,664 70.2 164.3

Gl Electrical Equio. and Instmnt. 0.07 $14.129 72.3 120.6

H) Housing 0.15 $36,032 254.8 505.61

1999 Capital cost: 1.00 1 $246.4741

,976 OBM cost: $4,665

I) Energy $/kW’h 0.59 56,422 0.03 0.07

J) Maintenance Material 0.04 $342 71.6 131.3

K) Labor %,hour 0.37 $5,176 1 0 3 0

AlUrn cost: $4,499,594

1999 Operation 8 Maintenance: 1.00 1 $4.511.535 1

A-22
Construction Cost for Dry Alum and Liquid Alum Feed

1,000 1

900

i

800

I

700 .I

L

z 400 -

8

300 -

200

100,

0 1 , I 1 I I I

0 100 200 300 400 500 600

I

Volume Treated (Usec)

I

t385 mg/L CC (Dry Alum) -A-385 mg/L CC (Liquid Alum)
O&M Cost for Dry Alum and Liquid Alum Feed

20,000

18,000

16,000

6,000

100 200 300 400

Volume Treated (Usec)

t335 mg/L O&MC (Dty Alum) +335 m(l’L O&MC (Liquid Alum)

500

7

600
Coagulation With Ferric Sulfate

“Ol”me TEaled L&c

Ej Labor 0.02 s3.039 247 543.67

F) Piping an* “alYe* 0.05 s8.cc-s 70.2 164.3

G, Electrical Equip. and lnstm”t. 0.09 110.270 72.3 120.6

H, Housing 0.21 sx,520 x4.8 505.81

1999 capita, cost: l.c.3 1 1137.985 1

Ferric Sulfate Feed capita, cost

General Form: A’X%w(C’X)

A= 10613

B= 0.319

c= am393

O&M cost

General Form: A’eyl3’X)+C

A= 1250926

B= O.ooWI 394

C= -1257710

A-25
$400

$350

$300

c

0, $200

9

L2

I; 5

m

z

” $150

$100

$50

$ 0

Construction Cost for Ferric Sulfate Feed at Dierent Dosage Rates

0 100 200 300 400

Volume Treated (Usec)

-10mq/L CC Fentc Sulfate -A-30 mq/L CC Ferric Sulfate

500 600
O&M Cost for Ferric Sulfate Feed at Differe,ntD,osage Rates

0 100 200 300 400

Volume Treated (Lkec)

t10mg/L O&MC Ferric Sulfate -H-Jo mglL O&MC Feti Sulfate

500 600
POLYFD

Polymer Addition for Antiscalant

Volume Treated USec:

Volume Treated (m3/day):

Alternative dosage rate (default = 0.5 mg/L):

Polymer Feed kg/day:

Hypersperse AF200 $1500 lb.:

292

25233

0.3

7.6 Applicable range 0.5 - 100 kg/day

I::~~~~~~~-:9901

1978 current

1978 capita1 cost:

IA) Excavation and Site Work

index value indexvalue

Percentages $20,566 basis 1999

0 $0 247 546.671

Bj Manufactured Equipment 0.7 $29,447 72.9 149.1

C) concrete 0 $0 71.6 150.2

D) Steel 0 $0 75 106.6

E) Labor 0.04 $1,828 247 546.67

F) Piping and Valves 0.01 $461 70.2 164.3

G) Electrical Equip. and lnstmnt. 0.06 %2.056 72.3 120.6

H) Housing 0.19 $7.750 254.6 505.61

1999 Capital Cost: 1.00 1 $41,572 1

1978 O&M cost: $3.046

I) Energy $/kW’h 0.24 $1,707 0.03 0.07

J) Maintenance Material 0.1 $559 71.6 131.3

K) Labor $/hour 0.66 $6.035 1 0 30

Polymer Cost $11,567

1999 Oper?&on 8 Maintenance: 1.00 1 $19.869 J

Polymer Feed Capital Cost

General Form: A%‘(BX)+C

A =

B =

c =

11760.71

0.00665

6200

O&M cost

General Form: A’e^(B’X)

A = 3000.6

B = 0.00207

Water Treatment Cost Estimation Program

A-28
Construction Cost for Polymer Feed at IXfferent Dosage Rates

30

1

25 -I

20

0 100 200 300 400 500 600

Volume Treated (Usec)

to.3 mg/L CC -A-O.5 mg/L Cc
2 0

100

0 103 MO

Volume TEkd (Lkec)

400 500 600

-0.3 mg/L O&MC *OS mg/L O&MC
KMn04

Potassium Permanganate Oxidation

Mn 2+ concentration: 0.03 mg/L

Fe 2+ concentration: 0.00 mgR

Calculated KMn04 Dose: -0.042 mgR

Volume Treated USec: 292.1

Volume Treated (m3Iday): 25,233

Alternative dosage rate. mgll: 1

KMn04 kg/day: 25.2 Applicable range 0.5 - 100 kg/day

1978 Capital Cost:

A) Excavation and Site Work

6) Manufactured Equipment

C) concrete

D) Steel

E) Labor

F) Piping and Valves

G) Electrical Equip. and Instmnt.

Percentages

0

0.34

0

0

0.05

0.1

0.32

1978 current

indexvalue indexvalue

$11,014 basis 1999

$ 0 247 546.67

$7.659 72.9 149.1

$ 0 71.6 150.2

$ 0 7 5 106.6

$1,223 247 548.67

$2.576 70.2 164.3

$5,879 72.3 120.6

H) Housing 0.19 $4,154 254.8 505.81

1999 Capital Cost: 1.00 1 $21,493 J

1978 O&M Cost: $4,212

ilb Enerov $lkV\Ph 0.05 $491 0.03 0.071

IbIQ Main~knance $/hour Labor Material 0.03 0.92 $11.625 $232 71.6 10 131.3 30 I

KM”04 Cost: $23,563 I

1999 Operation & Maintenantie: 1 .oo 1 $35.911 1

Permanganate Feed Capital Cost

General Form: A’X”B’e”(C’X)

A =

B=

c =

9681.7

0.0304

0.00122

O&M Cost

General Form: A’e”(B’X)+C

A = -2125.9

B= -0.01689

c= 5600

Water Treatment Cost Estimation Program

A-31
0 100 200 300 400 500 600

Volume Treated (Usec)

41 mg/LCC 42mglLCC
O&M Cost for Potassium Permanganate at Different Dosage Rates

250

5 0

0

0 100 200 300

Volume Treated (Usec)

400

+I mglL 08MC +2 mglL 08MC

500 600

A-35
300

0

Construction Cost for Lime Softening at 30 mg/L Dosage

100 200 300

Volume Treated (Usec)

--C 30 mgll (Lime and Soda)

400 500 600
4 0

2 0

0

O&M Cost for Lime Softening at 30 mg/L Dosage

1

I

1

I

0 100 200 300

Volume Treated (Usec)

-H-30 mg/L (Lime and Soda) O&MC

400 500 600
UFSCC

Upflow Solids Contact Clarifier

Flow Rate L/ser:

Retention Time (min.)

Assumed Depth = 4.8 m

Calculated Settling Area (m’)

292 4630 gpm

180

Basis: 328.55903

Alternative settling Area (m’)

Construction Cost 1978 $

A) Excavation and Site Work

8) Manufactured Equipment

Percentages index value index value

229,695 basis 1999

0.046 23,471 247 548.67

0.509 239.122 73 ! a ,dcll .-.- .-,

C) Concrete 0.081 39;030 71.6 150.2

D) Steel 0.11 35,912 75 106.6

E) Labor 0.247 126,027 247 548.67

F ) Piping and Valves 0 0 70.2 164.3

G ) Electrical Equip. and Instmnt. 0.007 2,682 72.3 120~6

H) Housing 0 0 254.8 505.81

1999 Capital Cost: 1

>

466,2441

$2 % G=70 % G=llO % G=i50

1978 O&M Cost: 7,713 8,700 10,009

I) Energy $/kW’h 0.23 4,139 0.38 7,714 0.5 11,677 0.03 0.07

J) Maintenance Material 0.17 2,405 0.14 2,233 0.11 2,019 71.6 131.3

K) Labor $/hour 0.6 13,084 0.48 12,527 0.39 11,710 10 30

1999 Operation & Maintenance Cost: 1 _ ~~

,,: 20.428 1_~ 22,474 I

25,406

Construction Cost Equations (From EPAbOO/Z-79-162b)

$ = a+b’x a b

<400 mz 62801.114 416.77163

>400 m* 132264.71 244.33215

Operation 8 Maintenance Cost (From EPA-600/2-79-162b)

$=a+b’x a b

G = 70 5967.9519 5.3118202

G=llO 5806.5744 8.80491

G=150 5939.8245 12.384121

Water Treatment Cost Estimation Program
1,000

200

0

Construction Cost for Upflow Solids Contact Clarifier

0 200 400 600 800 1000 1200

Volume Treated (L/see)
O&M Cost for Upflow Solids Contact Clarifier wlth Different G values

200 400 600

Volume Treated (Usec)

800 1000 1200

tObMC(G=70) + 08MC(G=llO) t08MC(G=150)
GAC

Granular Activated Carbon Filtration

Desired Flow Rate: 292 L/s 4630 gpm

25233.33 m-3ldav

Bed Life (months) Construction Costs:

~operati”g cpJ

Water Treatment Cost Estimation Program

A-41
20.000

5,000

Construction Cost for Carbon Filtration

Volume Treated (Use@

--c 12 mon. bed lib cc -b-e mm. ted tire cc -3m. ted Iire cc
O&M Cost for Carbon Filtration

2,000 .I

1,000 1

OC

0

+I2 mm. bed life O&MC X6 mm. bed life O&MC t3mm. bed life 08MC


450

400

? E

2 =

200

;;

5

150

100

50

0

Construciion COSi for Gravity iihiion ai iiiffereni iiow Rates

0 100 200 300 400 500 600

Volume Treated (L/see)
450

4M)

350

300

153

loo

50

0

O&M Cost for Gravity Filtration at Different Flow Rates

0 103 203 3w 400 600

Volume Treated (Usec)

Construction Cost for Ion Exchange at Different Flow Rates

2,000

1,800

1,600

1,400

200 400 600 800 1.000

Volume Treated (Usec)

1.200
O&M Cost for Ion Exchange at Different Flow Rates

60

5 0

40

30

20

10

0

0 200 400 600 800 1000 1200

Volume Treated (Usec)


Construction Cost for Electrodialysis (1st and 2nd stage)

14,000

12,000

10,000

8,000

6,000

4,000

2,000

0

0 200 400 600 800 1000 1200

Volume Treated (L/se@
0&M Cost for Electrodialysis (1st and 2nd staae!

4.000

1,000

500

0

0 200 400 600 600 1000 1200

Volume Treated (L/see)
Pumps

Number of pumps:

Height differential:

Discharge pressure:

Full flow rate:

Basis flow rate

Pump Efficiency:

Pipe Diameter:

Motor Efficiency:

HP

Power consumption:

4

l m

1750 kPa

0.29 m3/s

0.07 m%

7 5 %

0.1 m

8 7 %

236

271 kWhr

2.9 n

254 psi

4630 gal/min

1157 gUmin

4 in

Direct Costs (material and labor)

Pump, drive, and driver

Piping

COlltrOlS

Total Direct Cost

Taxes

Total Capital Cost

SST VST css

405105 593689 244460

283816 283816 283816

16000

688921 893505 528276

5.0% 34446 44675 26414

1 $723,367 1 ,$938,1,80 1 $554.690,1

Operating Costs

Power Cost $/year

Lubrication ($/L oil)

Cooling water ($/m3 water)

Maintenance (hr/Hp)

631389

1 826

0.1 123904

1.5 10608

1 $766.727 [

A-54
CLEARWELL

Construction cost for clear well storage

Below Ground (concrete)

Storage Capacity (kgall 5677.5

m3 1500

Data from EPA-600/Z-79-162b, August 1979, pg453454. They are used in determining cost formula.

Water Treatment Cost Estimation Program
CLEARWELL

Ground Level Isteel)

Storage Capacity (kgal) 5677.5

m3 1500

modified I Current I

Water Treatment Cost Estimation Program
Construction Cost for Clearwell Be!ow Ground Storage

I

0

0 2w 4ml 600 Fm IWO 1200 i‘lm 16w

Capacity (m’)
Construction Cost for Clear-well Ground Level Storage

0 10 2w 400 Km 8w 1000 1233 1400 IMxl