november 2015 anion exchange for drinking water treatment michael poulios, aqua north carolina...
TRANSCRIPT
![Page 1: November 2015 Anion Exchange for Drinking Water Treatment Michael Poulios, Aqua North Carolina William Dowbiggin, CDM Smith 2015 Annual Conference Raleigh,](https://reader033.vdocument.in/reader033/viewer/2022051216/5697bffb1a28abf838cc1229/html5/thumbnails/1.jpg)
November 2015
Anion Exchange for Drinking Water TreatmentMichael Poulios, Aqua North Carolina
William Dowbiggin, CDM Smith
2015 Annual Conference Raleigh, NC
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• Use a substitution reaction to remove ions
• DefinitionDescription:• Undesirable ions are captured on reactive sites of resin• Ions initially attached to resin are released into treated
water• Reversible reaction is most useful (recharge the resin)• Cation exchange uses H+ or Na+
• Anion exchange uses OH- or Cl-
• Water treatment applicationsExamples: • Softening(Ca2+, Mg2+) or other cation exchange
Ion Exchange Description and Examples
• Organics removal (Anion Exchange)• Anion Removal (Nitrate, Perchlorate, Arsenic,
Selenium, Chromium)• Wastewater/Industrial applications
• Other uses include chemical recovery• Contaminant (i.e. heavy metals) removal
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Inside of the Ion Exchange Bed • Typical arrangement
• Freeboard for bed expansion during a backwash
• Gravel and underdrain or other media support system
AIR RELEASE LINE
BAFFLE
FREEBOARD
GRAVEL BED
UNDERDRAIN
VERTICAL SOFTENER TANK
" DIAMETER
" FILTER SAND, SIZE TO MM.
STANDARD SOFTENER
" GRADED GRAVEL, SIZE 1/4" x 10" GRADED GRAVEL, SIZE 1/2" x 1/4"" GRADED GRAVEL, SIZE 3/4" x 1/2"" GRADED GRAVEL, SIZE 1 1/2 x 3/4"
" SIDE SHELL HEIGHT
P.S.I. W.P.
"ZEOLITE = CU.FT.
• Specified cubic feet of ion exchange resin (e.g. zeolite for softening)
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Raw Water NaCl to Regenerate
Low Organic MatterTreated WaterBackwash
Water Spent BrineTo Waste
DOCChromatePhosphatePerchlorateSulfateCarbonateBromideIodideArsenateNitrateChlorateHydroxideBromateNitriteChlorideBicarbonateFluoride
SpentBackwash
Water
Anion Exchange Process
Anion Exchange
Resin
Anions in decreasing order of selectivity:
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Example Order of Anion Elution from another CDM Smith Project
0
50
100
150
200
0 200 400 600 800 1000 1200Bed Volumes
Con
centr
atio
n (m
g/L o
r mg/
L)
ChlorideBicarbonateNitrateArsenicSulfate
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The Aqua Castle Bay Subdivision Water System is a 150 gpm Groundwater System near Hampstead NC just north of Wilmington
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Castle Bay Anion Exchange Project Drivers
• High concentrations of disinfection byproducts
• A desire to avoid chloramines and associated nitrification control issues given the system has high residence time
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Castle Bay Anion Exchange Project Phases• Bench study and testing of resin isotherms to
screen resins and obtain data for planning pilot testing
• Pilot testing of two short-listed resins to confirm suitability and determine guarantees for bidding
• Design• Construction and Start-up
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Bench Test Results - TOC mg/L vs. mL Resin Added
0 0.2 0.4 0.6 0.8 1 1.2 1.40
0.5
1
1.5
2
2.5
3
3.5
R.Tech SIR-22R.Tech SBACRThermax A-72Thermax A-30Purolite A-860
mL of Resin Added
TOC(mg/L)
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Bench Test Results - UV-254 Absorbance vs. mL Resin Added
UV-254 Abs. (cm-1)
mL of Resin Added
0 0.2 0.4 0.6 0.8 1 1.2 1.40.000
0.020
0.040
0.060
0.080
0.100
0.120
0.140
0.160
R.Tech SIR-22R.Tech SBACRThermax A-72Thermax A-30Purolite A-860
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0 0.2 0.4 0.6 0.8 1 1.2 1.40.000
5.000
10.000
15.000
20.000
25.000
30.000
35.000
40.000
45.000
R. Tech SIR-22R.Tech SBACRThermax A-72Thermax A-30Purolite A-860
Bench Test Results - Color vs. mL Resin Added
Color (PCU)
mL of Resin Added
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Bench Isotherm Preliminary Calculated Values
Resin K 1/N R2
Ld DR VR
(mg/g) (g/mL) (L/L)
R.Tech SIR-22P-HP 10.28 0.98 0.76 39.85 1.200 3288
R.Tech SBACR-HP 3.42 1.28 0.85 20.19 1.200 3029
Thermax A-72 3.26 0.93 0.64 11.84 1.100 1254
Thermax A-30 10.62 1.35 0.87 68.86 1.100 7291
Purolite A-860 9.39 1.45 0.79 70.00 1.065 6710
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0 100 200 300 400 500 600 700 800 9000
0.2
0.4
0.6
0.8
1
1.2
1.4
1.6
1.8
2
f(x) = 0.00178212670051135 x + 0.215922981555568R² = 0.843446434497524
f(x) = 0.00191764319258326 x + 0.260362589266843R² = 0.718620356613872
Pilot Test - Raw Water Feed TOC vs Run Time
TOC Purolite Linear (TOC Purolite)TOC Tonka Linear (TOC Tonka)
Cumulative Run Time, hr
TOC
(mg/
L)
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0 50 100 150 200 250 300 350 400 4500
0.2
0.4
0.6
0.8
1
1.2
1.4
1.6
1.8
2
f(x) = 0.00324905261850034 x − 0.0570065229545879R² = 0.922705538377324
f(x) = 0.00385393122241286 x + 0.545993602920621R² = 0.816982341212327
Pilot Test - Filtered Water Feed to Resin TOC vs. Run Time
TOC Purolite Linear (TOC Purolite)TOC Tonka Linear (TOC Tonka)
Cumulative Run Time, hr
TOC
(mg/
L)
Regenerated at 163 hours
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600 650 700 750 800 8500
0.02
0.04
0.06
0.08
0.1
0.12
Pilot Test - Raw Water Fed to Resin Iron Removed vs Run Time
Iron Purolite Iron Tonka
Cumulative Run Time, hr
Iron
Rem
oved
by
the
Resi
n, m
g/L
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0 50 100 150 200 250 3000
0.05
0.1
0.15
0.2
0.25
0.3
0.35
0.4
0.45
0.5
0.360.34
Filtered Water Fed to Resin Iron Removed vs. Run Time
Iron Purolite Iron Tonka
Cumulative Run Time, hr
Iron
Rem
oved
by
the
Resi
n (m
g/L)
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The Resin is Piped for Raw Water or Filtered Water Feed-Initially to use Raw Water because:• Purolite ended up the selected media supplier, and they
recommended treating the raw water with the resin based on prior experiences, concern over the chlorine residuals, and the pilot data for this project.
• Chlorine degrades the anion exchange resin and chlorine residuals coming out of the iron filters have been highly variable and up to 1.63 mg/L reaching the pilot units which is far above Purolite’s recommended 0.2 mg/L max chlorine reaching the anion exchange resin.
• Even Tonka, who recommended trying downstream on filtered water, concurred that it should be on raw water after the pilot test on filtered water.
• After the iron removal filters, the Tonka unit had clogging (pressure increases) quickly dropping flows and requiring regeneration then had clogging again.
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The Resin is Piped for Raw Water or Filtered Water Feed-Initially to use Raw Water because (continued):
• Iron removal in the anion exchange resin was found to be low when operated on the raw water, but up to 0.44 mg/L in the Tonka unit and up to 0.34 mg/L in the Purolite unit when operated after the iron removal filter. These levels of iron removal in the AER resin indicate quick iron fouling potential and correspond to the observed clogging (pressure increases and flow decreases).
• Total run time on the log sheet is 817 hours for raw water. The run time for post iron filters was 588 hours. The Tonka unit reportedly also had a regen/wash before even reaching the 588 hours due to the clogging.
• Anion resin on the raw water helps DBPs by removing the organics before the first chlorine dose.
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Planning for the Anion Exchange Resin Operations
• Based on the pilot testing and prior projects, the vendors suggested planning on regenerating the media once a week typically. The necessary regeneration frequency will increase with age and fouling.
• The salt required for regeneration was reported to be 8 to 10 lb/cubic foot of media. The final installation is to have 87 cubic feet of media including all three vessels. Consequently, the amount of salt used per regeneration of all three vessels was estimated to be about 700 to 870 lb of salt per regeneration of all three vessels. Salt cost is about $ 0.12/lb, and the vendor indicated about 3,200 gallons of water would be used in each regeneration.
• The resin is guaranteed to last at least a week between regenerations.
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Design, Construction and Costs
• The design included plan and profiles and a detailed technical specification with performance requirements
• The purchase cost of the anion exchange system was approximately $ 140,000 with all items included.
• Potential cost saving measures could include strategies such as operating just one or 2 beds at a time pending DBP levels.
• In conclusion, the anion exchange resin should do an excellent job of removing the organic precursors of disinfection byproducts. Cost control for the resin will be influenced by careful operations to prevent fouling while still being frugal with respect to labor and chemical costs.
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Design - Anion Exchange Vessels
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The Anion Exchange Vessels at Castle Bay Water System
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Water Softening System at Castle Bay Water System
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42217 42125 42036 41944 41852 41760 41671 415790
0.01
0.02
0.03
0.04
0.05
0.06
0.07
0.08
0.09
0.1
Quarterly TTHM vs. TimeCastle Bay Water System
Date
TTHM
(mg/
L)
AER Started
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Conclusions
• The anion exchange resin should do an excellent job of removing the organic precursors of disinfection byproducts. Cost control for the resin will be influenced by careful operations to prevent fouling while still being frugal with respect to labor and chemical costs.
• Potential cost saving measures could include strategies such as operating just one or 2 beds at a time pending DBP levels.
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Questions?
Michael Poulios, PE LEEDAqua North Carolina
(919) 653-6965
William B. Dowbiggin, PE BCEECDM Smith
(919) 623-7964 [email protected]