Technologies and Costs for Removal of Arsenic From Drinking Water

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Figure 3-2Pre-oxidation - 1.5 mg/L ChlorineO&M Costs$1,000,000$100,000y = 4920.1x + 916.87O&M Costs ($)$10,000y = -1E-10x 2 + 4239.7x + 1161.8y = -0.3928x 2 + 823.35x + 19360$1,000$1000.001 0.01 0.1 1 10 100 1000Average Flow (mgd)3-22
3.6 PRECIPITATIVE PROCESSES3.6.1 Coagulation/FiltrationCoagulation/filtration (C/F) is a treatment process that alters the physical or chemicalproperties of colloidal or suspended solids, enhancing agglomeration, and allowing these solids tosettle out of solution by gravity or be removed by filtration. The C/F removal mechanism is discussedin greater detail in Chapter 2. A typical C/F process includes coagulant addition, which may befollowed by polymer addition to aid agglomeration, flocculation, sedimentation, and filtration.C/F is widely used as a treatment for removing suspended solids from surface water supplies.Most ground waters are low in turbidity and do not require this type of treatment. C/F is unlikely tobe installed solely for arsenic removal. Systems considering installation of this technology shoulddesign the process to operate in the optimal pH range if high removal efficiency is needed forcompliance. Source waters containing high As(III) concentrations may opt for oxidation as a pretreatmentfor C/F. Pre-oxidation options are presented in Section 3.5. Costs are not presented for thisoption. Key design parameters that can be used with the cost models are presented for systems thatwish to explore this option.Very Small Systems (Less than 0.10 mgd)Capital costs for very small systems can be developed using the VSS model. The designparameter most affecting capital cost is the filtration rate. It affects the size of the filter structure andvolume of filter media, the most cost intensive process in a C/F plant. The VSS model also makesprovisions for building (14.9-28.1 percent), fencing (2.1-7.5 percent) and road (1.2-4.7 percent) costsassociated with each of the technologies presented. The following design criteria can be used todevelop capital cost estimates for systems with a design flow of less than 0.10 mgd:# Coagulant dosage, ferric chloride, 25 mg/L;# Polymer dosage, 0.4 mg/L; and# Filtration rate, 2.5 gpm/ft 2 .O&M costs are most affected by chemical costs associated with coagulant and polymerdosages. As a result, the very small systems O&M cost estimates can be escalated using the BLSChemical and Allied Products Index. Labor requirements were estimated at 8 hours per week.3-23
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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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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
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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
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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 and 78: sources. The September 1998 index v
Page 79 and 80: Amortization, or capital recovery,
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: Figure 3-1Pre-oxidation - 1.5 mg/L
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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
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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
Page 129 and 130: 3.11 COMPARISON OF COSTSThe April 1
Page 131 and 132: 4.0 RESIDUALS HANDLING AND DISPOSAL
Page 133 and 134: mechanical dewatering processes. Wh
Page 135 and 136: Storage lagoons are best suited for
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Page 139 and 140: 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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