Technologies and Costs for Removal of Arsenic From Drinking Water

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APPENDIX D: BASIS FOR REVISED ACTIVATED ALUMINA COSTSD.1 OVERVIEWFour sets of costs were developed for disposable activated alumina (no regeneration) - twofor unadjusted pH and two where the pH has been adjusted to the optimal pH of 6. The costs for pHadjustment to optimal pH 6.0 are included as a separate module in these cost estimates since it is onlyused for two of the options. The costs in the cost models routinely used to estimate unit costs are allbased on regeneration of the media, operation at optimal pH, and use of single columns. Most of thecosts are based on fluoride removal rather than arsenic removal. It was determined that the existingcost models could not be used to estimate costs for disposable activated alumina. A similar summaryto this was prepared for the proposed rule for the disposable activated alumina costs. It was includedin Appendix G of the November 1999 Technology and Cost Document (1). The main change betweenthat design and the design used for the final rule is that smaller columns operated in series will be usedinstead of a single column. This will provide greater utilization of the media before disposal and ismore consistent with the designs used by commenters in evaluating disposable activated alumina.D.2 DESIGN ASSUMPTIONS AND BASISD.2.1Capital Costs - Natural pH1. The pH will not be adjusted to operate the process at the optimal pH between 5.5 and 6.0.The activated alumina process will be operated at the natural pH of the system to simplify theprocess and avoid potential problems with lowering the pH. Two pH ranges will beevaluated 7.0 #pH < pH 8.0 and 8.0 # pH #8.3.Basis. Comments from AWWA Arsenic Technical Workgroup Meeting on TreatmentTechnology. EPA expressed a concern about small systems adjusting pH downward and theAWWA Technical Workgroup agreed that there were significant risks if small systems wereadjusting pH downward (the water could become very acidic if the treatment chemicals areoverdosed). The AWWA Technical Workgroup believed that lowering the pH would requireD-1
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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
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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.
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 244 and 245: much more oversight than most small
Page 246 and 247: Basis. An old activated alumina des
Page 248 and 249: Basis. The Water Model provided con
Page 250 and 251: systems could underestimate the nee
Page 252 and 253: For design flows greater than 1 mgd
Page 254 and 255: The source water at Plant C has the
Page 256 and 257: length of 10,000 BV for 7 # pH < 8
Page 258 and 259: The arsenic loaded onto the column
Page 260 and 261: column. The Phase 3 Report noted th
Page 262 and 263: The lower bound run length at pH 6
Page 264 and 265: Basis. The labor requirements when
Page 266 and 267: 23. The disposal cost for the spent
Page 268 and 269: 8. US EPA. Guide for Implementing P
Page 271 and 272: APPENDIX E: BASIS FOR REVISED ANION
Page 273 and 274: 6. The capital costs include a redu
Page 275 and 276: Table E-2Percentage of Ground Water
Page 277 and 278: 12. The building cost to house the
Page 279 and 280: 15. The second major component in t
Page 281 and 282: Arsenic in the regeneration brine w
Page 283 and 284: 12. Clifford, D.A. G. Ghurye et al.
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Technologies and Costs for Removal of Arsenic From Drinking Water

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