Technologies and Costs for Removal of Arsenic From Drinking Water

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TABLE 3-9Chemical CostsChemical Cost UnitsAlum, Dry Stock $300 per tonCarbon Dioxide, Liquid $340 per tonChlorine, 1 ton cylinder $350 per tonChlorine, 150 lb cylinder $400 per tonChlorine, Bulk $280 per tonFerric Chloride $350 per tonHexametaphosphate $1276 per tonLime, Quick Lime $95 per tonPhosphoric Acid $300 per tonPolymer $2.25 per lbPotassium Permanganate $2700 per tonSoda Ash $400 per tonSodium Hypochlorite, 12% $1100 per tonSodium Chloride $99 per tonSodium Hydroxide, 50% solution $371 per tonSulfuric Acid $116 per tonThe models present total capital costs and annual O&M costs. Annual O&M costs include thecosts for materials, chemicals, power, and labor. Annual costs can be determined using the followingequations:Total annual cost (¢/kgal) =Annualized Capital Cost (¢/kgal) + O&M Cost (¢/kgal)Where:Annualized Capital Cost = Capital Cost ($) * Amortization Factor * 100 ¢/$Average Daily Flow (mgd)*(1000 kgal/mgal)*365 days/yearO&M Cost (¢/kgal) = Annual O&M ($) * 100 (¢/$)Average Daily Flow (mgd)*1000 kgal/mgal*365 days/year3-10
Amortization, or capital recovery, factors for interest rates of 3, 7, and 10 percent for 20 yearsare reported in Table 3-10. Alternative capital recovery factors can be calculated using the formulapresented below.Capital Recovery Factor =(1 + i) N((1 + i) N - 1)/i)Where:i = interest rateN = number of yearsTable 3-10Amortization FactorsInterest Rate (%) Amortization Period AmortizationFactor3 20 0.06721577 20 0.094392910 20 0.11745963.2.5 Re-Basing Bureau of Labor Statistics Cost IndicesThe Water Model and W/W Cost Model uses BLS cost index information based in 1967dollars. In 1986, the BLS conducted a comprehensive overhaul of the industrial price methodologyresulting in a re-basing of all index information to a base year of 1982 (i.e., 1982=100). The BLSindex information must be re-based to 1967 to use the indices in the models. A sample re-basecalculation is presented below.Sample Re-base Calculation:Machinery =1982 Base Factor / Re-base Factor = 1967 Base Factor= 146.4 / 0.32895016 = 445.13-11
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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
Page 27 and 28: Substantial arsenic removal has bee
Page 29 and 30: Vickers et al. (1997) reported that
Page 31 and 32: was reduced to 0.05 mg/L when the i
Page 33 and 34: Field StudiesSurveys of lime soften
Page 35 and 36: Effect of pHpH may have significant
Page 37 and 38: RegenerationRegeneration of AA beds
Page 39 and 40: een developed provide important inf
Page 41 and 42: applicability of IX at a particular
Page 43 and 44: TABLE 2-1Typical IX Resins for Arse
Page 45 and 46: solution strength. Arsenic elutes r
Page 47 and 48: 2.4.12 Typical Design ParametersThr
Page 49 and 50: 2.5.2 Important Factors for Membran
Page 51 and 52: arsenic size distribution to correl
Page 53 and 54: AWWARF (1998) also performed UF pil
Page 55 and 56: presumably due to changes in electr
Page 57 and 58: RO performance is adversely affecte
Page 59 and 60: TABLE 2-10Arsenic Removal with RO a
Page 61 and 62: eversal is the decreased potential
Page 63 and 64: 2.6 ALTERNATIVE TECHNOLOGIES2.6.1 I
Page 65 and 66: 20 mg As per gram of iron was remov
Page 67 and 68: The most significant weakness of th
Page 69 and 70: 3.0 TECHNOLOGY COSTS3.1 INTRODUCTIO
Page 71 and 72: included in the estimates presented
Page 73 and 74: Table 3-3Water Model Capital Cost B
Page 75 and 76: 3.2.3 Implementing TDP Recommended
Page 77: sources. The September 1998 index v
Page 81 and 82: 3.3 ADDITIONAL CAPITAL COSTSThe cos
Page 83 and 84: PilotingThe Technology Design Panel
Page 85 and 86: The 1993 Technology and Cost Docume
Page 87 and 88: cause disinfection by-product (DBP)
Page 89 and 90: Figure 3-1Pre-oxidation - 1.5 mg/L
Page 91 and 92: 3.6 PRECIPITATIVE PROCESSES3.6.1 Co
Page 93 and 94: enhanced coagulation treatment plan
Page 95 and 96: Figure 3-4Enhanced Coagulation/Filt
Page 97 and 98: Small Systems (Less than 1 mgd)The
Page 99 and 100: Figure 3-6Coagulation Assisted Micr
Page 101 and 102: 3.6.6 Enhanced Lime SofteningEnhanc
Page 103 and 104: Figure 3-8Enhanced Lime SofteningO&
Page 105 and 106: 3. Empty Bed Contact Time (EBCT) is
Page 107 and 108: For design flows greater than 1 mgd
Page 109 and 110: Figure 3-9Activated AluminaCapital
Page 111 and 112: Figure 3-11Activated Alumina (pH 8
Page 113 and 114: Figure 3-13Activated Alumina (pH Ad
Page 115 and 116: 3.7.2 Granular Ferric HydroxideGran
Page 117 and 118: 6. The capital costs include a redu
Page 119 and 120: Figure 3-15Bed Volumes to Arsenic B
Page 121 and 122: Figure 3-17Anion Exchange (< 20 mg/
Page 123 and 124: Figure 3-19Anion Exchange (20-50 mg
Page 125 and 126: quality feed stream and often requi
Page 127 and 128: 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 4-5Coagulation Assisted Micr
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Figure 4-7Coagulation Assisted Micr
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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
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Le, X.C., and M. Ma (1998). “Dete
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Scott, K., J. Green, H.D. Do and S.
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Appendix AVery Small Systems Capita
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Table A4 - VSS Document Capital Cos
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Table B1.1 - Base Costs Obtained fr
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Table B11.1 - Base Costs Obtained f
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Table B13.1 - Base Costs Obtained f
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Appendix CW/W Cost Model Capital Co
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Table C2.1 - Base Costs Obtained fr
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Table C10.1 - Base Costs Obtained f
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APPENDIX D: BASIS FOR REVISED ACTIV
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Company case study is 18 minutes (2
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egressed against their respective v
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costs for small systems is as follo
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were based on $40/sq ft). The proce
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Basis. Capital cost components incl
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The source water at Plant D has the
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equation y = (2*10 -8 )x 2 + 0.0002
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The maximum run length is 18,500 be
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Since the available arsenic capacit
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If the first column can be operated
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which includes lighting, ventilatio
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disposal costs, if needed, are cove
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Appendix EBasis for Revised Anion E
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2. The estimated cost of the anion
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9. The capital costs have been esti
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Thus, the cost of a road and fence
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length when sulfate is at or below
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the labor rates for both large and
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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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