Technologies and Costs for Removal of Arsenic From Drinking Water

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Table C26.1 - Base Costs Obtained from the WATERCO$T Model for Tube Settling ModulesCost ComponentTube Module Area (ft2)280 2,800 14,000 28,000 56,000Manufactured Equipment $4,200 $31,000 $147,000 $282,000 $504,000 pSteel $2,000 $19,500 $95,000 $155,000 $300,000 pLabor $2,500 $11,200 $49,000 $95,000 $224,000 cContingencies $1,300 $9,300 $43,700 $79,800 $154,200 cTotal $10,000 $71,000 $334,700 $611,800 $1,182,200Table C26.2 - WATERCO$T Model Base Construction Cost Analysis for Tube Settling ModulesCapital CostCategoryCost Component280 2,800Tube Module Area (ft2)Average14,000 28,000 56,000 PercentManufactured Equipment 42.00% 43.66% 43.92% 46.09% 42.63% 43.66%Steel 20.00% 27.46% 28.38% 25.34% 25.38% 25.31%Labor 25.00% 15.77% 14.64% 15.53% 18.95% 17.98%Contingencies 13.00% 13.10% 13.06% 13.04% 13.04% 13.05%Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%International Consultants, Inc.Contract 68-C6-0039 C-26February 1999W/W Cost Model Capital Cost Breakdown
Table C27.1 - Base Costs Obtained from the WATERCO$T Model for Wash Water Surge BasinsCost ComponentCapacity (gal)Capital Cost10,000 50,000 100,000 500,000 CategoryExcavation & Sitework $200 $520 $1,250 $4,400 cConcrete $11,560 $39,310 $71,480 $143,680 pSteel $7,990 $25,170 $44,680 $70,770 pLabor $18,270 $58,500 $107,590 $182,150 cPipes and Valves $5,500 $7,500 $11,000 $16,000 pElectrical $1,300 $1,300 $6,000 $6,000 pContingencies $6,720 $19,850 $36,300 $63,450 cTotal $51,540 $152,150 $278,300 $486,450Table C27.2 - WATERCO$T Model Base Construction Cost Analysis for Wash Water Surge BasinsCost ComponentCapacity (gal)Average10,000 50,000 100,000 500,000 PercentExcavation & Sitework 0.39% 0.34% 0.45% 0.90% 0.52%Concrete 22.43% 25.84% 25.68% 29.54% 25.87%Steel 15.50% 16.54% 16.05% 14.55% 15.66%Labor 35.45% 38.45% 38.66% 37.44% 37.50%Pipes and Valves 10.67% 4.93% 3.95% 3.29% 5.71%Electrical 2.52% 0.85% 2.16% 1.23% 1.69%Contingencies 13.04% 13.05% 13.04% 13.04% 13.04%Total 100.00% 100.00% 100.00% 100.00% 100.00%International Consultants, Inc.Contract 68-C6-0039 C-27February 1999W/W Cost Model Capital Cost Breakdown
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United StatesEnvironmental Protecti
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ACKNOWLEDGMENTSThis document was pr
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2.5.7 Reverse Osmosis .............
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5.0 POINT-OF-ENTRY/POINT-OF-USE TRE
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LIST OF FIGURES2-1 Pressure Driven
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LIST OF ACRONYMSAAAWWAAWWARFBLSBVC/
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POUpoint-of-useppbparts per billion
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# Alternative treatment processes s
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ends up as ferric hydroxide. In alu
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Optimization Hierarchy for Coagulat
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Substantial arsenic removal has bee
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Vickers et al. (1997) reported that
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was reduced to 0.05 mg/L when the i
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Field StudiesSurveys of lime soften
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Effect of pHpH may have significant
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RegenerationRegeneration of AA beds
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een developed provide important inf
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applicability of IX at a particular
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TABLE 2-1Typical IX Resins for Arse
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solution strength. Arsenic elutes r
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2.4.12 Typical Design ParametersThr
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2.5.2 Important Factors for Membran
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arsenic size distribution to correl
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AWWARF (1998) also performed UF pil
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presumably due to changes in electr
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RO performance is adversely affecte
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TABLE 2-10Arsenic Removal with RO a
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eversal is the decreased potential
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2.6 ALTERNATIVE TECHNOLOGIES2.6.1 I
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20 mg As per gram of iron was remov
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The most significant weakness of th
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3.0 TECHNOLOGY COSTS3.1 INTRODUCTIO
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included in the estimates presented
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Table 3-3Water Model Capital Cost B
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3.2.3 Implementing TDP Recommended
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sources. The September 1998 index v
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Amortization, or capital recovery,
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3.3 ADDITIONAL CAPITAL COSTSThe cos
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PilotingThe Technology Design Panel
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The 1993 Technology and Cost Docume
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cause disinfection by-product (DBP)
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Figure 3-1Pre-oxidation - 1.5 mg/L
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3.6 PRECIPITATIVE PROCESSES3.6.1 Co
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enhanced coagulation treatment plan
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Figure 3-4Enhanced Coagulation/Filt
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Small Systems (Less than 1 mgd)The
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Figure 3-6Coagulation Assisted Micr
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3.6.6 Enhanced Lime SofteningEnhanc
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Figure 3-8Enhanced Lime SofteningO&
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3. Empty Bed Contact Time (EBCT) is
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For design flows greater than 1 mgd
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Figure 3-9Activated AluminaCapital
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Figure 3-11Activated Alumina (pH 8
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Figure 3-13Activated Alumina (pH Ad
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3.7.2 Granular Ferric HydroxideGran
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6. The capital costs include a redu
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Figure 3-15Bed Volumes to Arsenic B
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Figure 3-17Anion Exchange (< 20 mg/
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Figure 3-19Anion Exchange (20-50 mg
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quality feed stream and often requi
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Figure 3-20Greensand FiltrationCapi
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3.11 COMPARISON OF COSTSThe April 1
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4.0 RESIDUALS HANDLING AND DISPOSAL
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mechanical dewatering processes. Wh
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Storage lagoons are best suited for
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the current Industrial Pretreatment
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4.3.3 Dewatered Sludge Land Applica
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usually determined by the Paint Fil
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for arsenic toxicity by a substanti
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The solids content of the backwash
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carbonate hardness removal produces
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Domestic sewage means untreated san
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4.4.10 Reverse OsmosisReverse osmos
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Figure 4-1Anion Exchange (< 20 mg/L
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Figure 4-3Anion Exchange (20-50 mg/
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Figure 4-9Activated Alumina (pH 7 -
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Figure 4-11Activated Alumina (pH Ad
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Figure 4-13Greensand FiltrationWast
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5.0 POINT-OF-ENTRY/POINT-OF-USE TRE
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chromatographic peaking, which occu
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5.3.1 Case Study 1: Fairbanks, Alas
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Manufacturer and laboratory data su
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Figure 5-2POU Reverse OsmosisO&M Co
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# Installation time - 1 hour unskil
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Figure 5-3POU Activated AluminaTota
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6.0 REFERENCESAmy, G.L. and P. Bran
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Cooperative Research Centres for Wa
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Fuller, C.C., J.A. Davis, G.W. Zell
Page 187 and 188: Le, X.C., and M. Ma (1998). “Dete
Page 189 and 190: Scott, K., J. Green, H.D. Do and S.
Page 191: Appendix AVery Small Systems Capita
Page 194 and 195: Table A4 - VSS Document Capital Cos
Page 197 and 198: Table B1.1 - Base Costs Obtained fr
Page 207 and 208: Table B11.1 - Base Costs Obtained f
Page 209 and 210: Table B13.1 - Base Costs Obtained f
Page 211: Appendix CW/W Cost Model Capital Co
Page 214 and 215: Table C2.1 - Base Costs Obtained fr
Page 222 and 223: Table C10.1 - Base Costs Obtained f
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Page 243 and 244: APPENDIX D: BASIS FOR REVISED ACTIV
Page 245 and 246: Company case study is 18 minutes (2
Page 247 and 248: egressed against their respective v
Page 249 and 250: costs for small systems is as follo
Page 251 and 252: were based on $40/sq ft). The proce
Page 253 and 254: Basis. Capital cost components incl
Page 255 and 256: The source water at Plant D has the
Page 257 and 258: equation y = (2*10 -8 )x 2 + 0.0002
Page 259 and 260: The maximum run length is 18,500 be
Page 261 and 262: Since the available arsenic capacit
Page 263 and 264: If the first column can be operated
Page 265 and 266: which includes lighting, ventilatio
Page 267 and 268: disposal costs, if needed, are cove
Page 269: Appendix EBasis for Revised Anion E
Page 272 and 273: 2. The estimated cost of the anion
Page 274 and 275: 9. The capital costs have been esti
Page 276 and 277: Thus, the cost of a road and fence
Page 278 and 279: length when sulfate is at or below
Page 280 and 281: the labor rates for both large and
Page 282 and 283: 2. US EPA. Technologies and Costs f
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Technologies and Costs for Removal of Arsenic From Drinking Water

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