EPA/600/R-10/152
November 2010
Arsenic Removal from Drinking Water by Ion Exchange
U.S. EPA Demonstration Project at Fruitland, ID
Final Performance Evaluation Report
by
Lili Wang§
Abraham S.C. Chen§
Anbo Wang*
^attelle, Columbus, OH 43201-2693
§ALSA Tech, LLC, Columbus, OH 43219-0693
Contract No. 68-C-00-185
Task Order No. 0019
for
Thomas J. Sorg
Task Order Manager
Water Supply and Water Resources Division
National Risk Management Research Laboratory
Cincinnati, Ohio 45268
National Risk Management Research Laboratory
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, Ohio 45268
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DISCLAIMER
The work reported in this document is funded by the United States Environmental Protection Agency
(EPA) under Task Order 0019 of Contract 68-C-00-185 to Battelle. It has been subjected to the Agency's
peer and administrative reviews and has been approved for publication as an EPA document. Any
opinions expressed in this paper are those of the author(s) and do not, necessarily, reflect the official
positions and policies of the EPA. Any mention of products or trade names does not constitute
recommendation for use by the EPA.
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FOREWORD
The United States Environmental Protection Agency (EPA) is charged by Congress with protecting the
nation's land, air, and water resources. Under a mandate of national environmental laws, the Agency
strives to formulate and implement actions leading to a compatible balance between human activities and
the ability of natural systems to support and nurture life. To meet this mandate, EPA's research program
is providing data and technical support for solving environmental problems today and building a science
knowledge base necessary to manage our ecological resources wisely, understand how pollutants affect
our health, and prevent or reduce environmental risks in the future.
The National Risk Management Research Laboratory (NRMRL) is the Agency's center for investigation
of technological and management approaches for preventing and reducing risks from pollution that
threaten human health and the environment. The focus of the Laboratory's research program is on
methods and their cost-effectiveness for prevention and control of pollution to air, land, water, and
subsurface resources; protection of water quality in public water systems; remediation of contaminated
sites, sediments and groundwater; prevention and control of indoor air pollution; and restoration of
ecosystems. NRMRL collaborates with both public and private sector partners to foster technologies that
reduce the cost of compliance and anticipate emerging problems. NRMRL's research provides solutions
to environmental problems by developing and promoting technologies that protect and improve the
environment; advancing scientific and engineering information to support regulatory and policy
decisions; and providing the technical support and information transfer to ensure implementation of
environmental regulations and strategies at the national, state, and community levels.
This publication has been produced as part of the Laboratory's strategic long-term research plan. It is
published and made available by EPA's Office of Research and Development to assist the user
community and to link researchers with their clients.
Sally Gutierrez, Director
National Risk Management Research Laboratory
in
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ABSTRACT
This report documents the activities performed and the results obtained from this 32-month demonstration
study, which evaluated a Kinetico ion exchange (IX) system to remove arsenic and nitrate from source
water at the City of Fruitland in Idaho. The 250-gal/min (gpm) IX system consisted of a bank of five
sediment filters, two 48-in x 72-in pressure vessels (configured in parallel), one 15-ton saturator, one 685-
gal day tank, and ancillary equipment. Each resin vessel contained 50 ft3 of A300 E strong base anionic
exchange resin manufactured by Purolite.
The 32-month demonstration study was divided into three major study periods with Study Period I
extending from June 14, 2005, through July 25, 2006; Study Period II from July 25, 2006, through June
18, 2007; and Study Period III from June 18, 2007 to February 11, 2008. Study Period I evaluated
performance of the IX system in a co-current regeneration mode. Due to leakage of both arsenic and
nitrate after regeneration, attempts were made to switch the regeneration process from co- to counter-
current mode in Study Period II. However, a series of mechanical failures was encountered while
switching from co- to counter-current regeneration, causing the IX resin to foul. Therefore, Study Period
III was devoted to resin cleaning using a caustic/brine mixture before returning to regular but brief system
performance evaluation.
Routine system performance evaluation was conducted in Study Period I, when the IX system operated in
the co-current regeneration mode. During this period, the IX system operated for a total of 6,836 hr,
averaging 17.4 hr/day. The system treated approximately 65,423,000 gal of water with an average daily
production of 166,895 gal/day (gpd). The average flowrate was 157 gpm, which was 63% of the 250-
gpm design flowrate. This average flowrate yielded an empty bed contact time (EBCT) of 4.8 min and a
hydraulic loading rate of 6.2 gpm/ft2to each IX resin vessel.
Total arsenic concentrations in raw water ranged from 33.6 to 60.8 ug/L and averaged 42.5 ug/L, which
existed primarily as As(V). Nitrate concentrations ranged from 6.9 to 11.5 mg/L (as N) and averaged
10.0 mg/L (as N). The water also contained, on average, 19.4 ug/L of uranium, 39.3 ug/L of vanadium,
59 mg/L of sulfate, 0.32 mg/L of phosphorus (as P), 57 mg/L of silica (as SiO2), and 387 mg/L of
alkalinity (as CaCO3). After treatment, total arsenic and nitrate were reduced to below the respective
maximum contaminant levels (MCLs), except when the system was freshly regenerated or experiencing
mechanical problems. Near complete removal of uranium, vanadium, and molybdenum by the IX system
also was observed.
Sulfate, the most preferred anion by the IX resin, was removed from an average of 59 mg/L in raw water
to less than 1 mg/L in the treated water for most sampling events, except when the system was
experiencing mechanical problems. Raw water pH values ranged from 6.7 to 7.9. A significant reduction
in pH in the treated water was observed immediately after resin regeneration, presumably due to the
removal of bicarbonate ions by the freshly regenerated IX resin, as evidenced by the corresponding
decrease in total alkalinity.
In addition to routine sampling, six run length and two regeneration (or elution) special studies were
performed during Study Periods I and II. The purpose of the run length studies was to delineate arsenic
and nitrate breakthrough behavior and determine the resin run length between two consecutive
regeneration cycles. Based on the results of these special studies and routine sampling across the
treatment train, the resin run length was upwardly adjusted from the initial factory setting of 214,000 gal
(or 286 bed volume [BV]) to 335,000 gal (or 448 BV), then downwardly adjusted several times to
316,000 gal (or 422 BV), 275,000 gal (or 368 BV), 260,000 gal (or 348 BV), and finally 220,000 gal (or
IV
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294 BV) by the end of evaluation study. Effluent samples collected from the IX vessels indicated arsenic
and nitrate leakage during the first 50,000 to 60,000 gal (or 67 to 80 BV) of throughput.
The IX system was regenerated in a downflow, co-current mode during Study Period I using brine at a
target salt level of 10 lb/ ft3 of resin. Triggered automatically by a pre-set throughput in the
programmable logic controller (PLC), the two IX vessels were regenerated sequentially, each cycling
through the steps of brine draw, slow rinse, and fast rinse before returning to service. A total of 202
regeneration cycles took place during Period I, consuming approximately 271,640 lb of salt. Depending
on regeneration settings, average salt usage per regeneration cycle increased from 1,129 lb to as high as
1,736 lb and then decreased to 945 lb, equivalent to a regeneration level of 11.3, 17.4, or 9.5 lb/ft3. The
regeneration settings were adjusted multiple times to reach 9.5 lb/ft3 regeneration level, which was within
5% of the target value of 10 lb/ft3. Key settings included brine concentration, brine draw time, and brine
draw flowrate. The system production efficiency was 98% considering the amount of treated water used
for regeneration.
The purpose of the two regeneration (or elution) studies was to evaluate the effectiveness of the IX resin
regeneration process and characterize the residuals produced. Although the majority of arsenic and
nitrate on the resin was eluted during the brine draw and slow rinse steps, arsenic concentrations as high
as 35 ug/L were still measured towards the end of the fast rinse step. Therefore, it was not surprising to
detect over 10 ug/L of arsenic during subsequent service runs. Extending the fast rinse time from 6 to 15
min did not resolve the problem because the leakage was found to continue up to 52,000 gal (or 70 BV)
of throughput, or approximately 3 to 4 hr into service runs. The regeneration waste stream discharged to
the sewer contained an average of 1.9 mg/L of arsenic and 0.31 g/L of nitrate, equivalent to amass
loading of 47 g for arsenic and 7.9 kg for nitrate per regeneration cycle, based on the wastewater samples
collected during nine regeneration events.
Attempts were made in Study Period II to convert the IX system from co- to counter-current regeneration.
The conversion, however, was unsuccessful due to various mechanical difficulties. Improper IX resin
regeneration for an extended period during Study Period II resulted in resin fouling, which caused
deteriorating resin performance. The fouled IX resin was cleaned with a 5% NaOH/10% brine mixture
followed by regular co-current regeneration. Although the analytical data of IX resin samples showed
some effectiveness, the system performance did not improve after the caustic/brine cleaning. The early
leakage of arsenic and nitrate continued to exist after the system was reverted back to the co-current
regeneration mode.
The capital investment cost was $286,388, which included $173,195 for equipment, $35,619 for site
engineering, and $77,574 for installation. This capital cost was normalized to the system's rated capacity
of 250 gpm (360,000 gpd), which resulted in $1,146 per gpm ($0.80 per gpd). Funded separately by the
City of Fruitland, the cost associated with the new building, sanitary sewer connection, and other
discharge-related infrastructure was not included in the capital cost.
The operation and maintenance (O&M) cost for the IX system included the incremental cost associated
with the salt supply, electricity consumption, and labor. Over the first year of system operation, the cost
for salt supply was $0.49/1,000 gal of water treated, which could be reduced to $0.35/1,000 gal if a target
salt usage rate of 3.16 lb/1,000 gal was reached. The majority of the O&M cost was incurred by salt
supply.
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CONTENTS
DISCLAIMER ii
FOREWORD iii
ABSTRACT iv
APPENDICES vii
FIGURES vii
TABLES viii
ABBREVIATIONS AND ACRONYMS x
ACKNOWLEDGMENTS xii
1.0: INTRODUCTION 1
1.1 Background 1
1.2 Treatment Technologies for Arsenic Removal 1
1.3 Project Objectives 2
2.0 SUMMARY AND CONCLUSIONS 3
3.0: MATERIALS AND METHODS 5
3.1 General Project Approach 5
3.2 System O&M and Cost Data Collection 6
3.3 Sample Collection Procedures and Schedules 7
3.3.1 Source Water 7
3.3.2 Treatment Plant Water 7
3.3.3 Regeneration Wastewater 7
3.3.4 Distribution System Water 10
3.4 Real-Time Arsenic Monitoring with ArsenicGuard 11
3.5 IX Resin Run Length and Spent IX Resin Regeneration Studies 11
3.5.1 IX Resin Run Length Studies 11
3.5.2 Spent IX Resin Regeneration Studies 14
3.6 IX Resin Cleaning and Analysis 15
3.7 Sampling Logistics 16
3.7.1 Preparation of Arsenic Speciation Kits 16
3.7.2 Preparation of Sampling Coolers 16
3.7.3 Sample Shipping and Handling 17
3.8 Analytical Procedures 17
4.0: RESULTS AND DISCUSSION 18
4.1 Facility Description 18
4.1.1 Source Water Quality 18
4.1.2 Distribution System and Treated Water Quality 21
4.2 Treatment Process Description 21
4.2.1 Ion Exchange Process 21
4.2.2 Treatment Process 23
4.3 System Installation 29
4.3.1 Building Construction 29
4.3.2 Installation of Replacement Well 29
4.3.3 Permitting 30
4.3.4 System Installation, Shakedown, and Startup 30
4.4 System Operation 32
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4.4.1 Operational Parameters 33
4.4.2 Regeneration 34
4A.2.1 Regeneration Settings 35
4.4.2.2 Regeneration Parameters 35
4.4.2.3 Salt Usage 38
4.4.3 System Operational Issues 40
4.4.3.1 Period I (June 14, 2005 to July 25, 2006) 40
4.4.3.2 Study Period II (July 25, 2006, to June 18, 2007) 41
4.4.3.3 Study Period III (June 18, 2007 to February 11, 2008) 43
4.4.4 Residual Management 44
4.4.5 System Operation Requirement 46
4.4.5.1 Required System Operation and Operator Skills 46
4.4.5.2 Preventive Maintenance Activities 46
4.4.5.3 Chemical/Media Handling and Inventory Requirements 47
4.5 System Performance 47
4.5.1 Treatment Plant Sampling 47
4.5.1.1 Arsenic and Nitrate Removal 47
4.5.1.2 Arsenic Speciation 53
4.5.1.3 Uranium, Vanadium, and Molybdenum Removal 53
4.5.1.4 Other Water Quality Parameters 53
4.5.2 Resin Run Length Studies 56
4.5.2.1 Study Period I Run Length Studies 58
4.5.2.2 Period II Run Length Study 62
4.5.3 Regeneration Studies 62
4.5.3.1 Regeneration Study 1 (July 30, 2005) 62
4.5.3.2 Regeneration Study 2 (September 22, 2005) 62
4.5.4 Regeneration Wastewater Sampling 66
4.5.5 Analyses of Fouled IX Resin 70
4.5.6 Distribution System Water Sampling 71
4.6 System Cost 73
4.6.1 Capital Cost 73
4.6.2 Operation and Maintenance Cost 74
5.0 REFERENCES 76
APPENDICES
APPENDIX A: A SUMMARY OF MAJOR SYSTEM OPERATIONAL PROBLEMS
APPENDIX B: OPERATIONAL DATA
APPENDIX C: ANALYTICAL DATA
FIGURES
Figure 3-1. Process Flow Diagram and Sampling Locations/Analyses for Fruitland, ID IX
System 9
Figure 3-2. A Garden Hose Used for Residual Sampling from IX Resin Vessel 10
Figure 3-3. Real-Time Arsenic Analyzer- ArsenicGuard 12
Figure 3-4. Field Setup for Arsenic/Nitrate Regeneration Study 16
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Figure 4-1. Historic Well No. 6 Nitrate Concentrations 20
Figure 4-2. Purolite A-300E Simulation 23
Figure 4-3. Process Schematic of Kinetico's IX-248-As/N Removal System 24
Figure 4-4. 20-um Bag Filter Assembly 26
Figure 4-5. Ion Exchange System at Fruitland, ID 26
Figure 4-6. Sampling Taps, Pressure Gauges, and Valves 27
Figure 4-7. Photograph of Brine System 28
Figure 4-8. Salt Delivery to Fill Salt Saturator 28
Figure 4-9. New Addition to Old Well House 29
Figure 4-10. Equipment Offloading 31
Figure 4-11. Cutting and Soldering a Salt Saturator 31
Figure 4-12. Snapshot from ArsenicGuard on May 9 and 10, 2007 42
Figure 4-13. Total Arsenic Concentration in System Effluent - An ArsenicGuard Display
Snapshot 44
Figure 4-14. Total Arsenic Concentrations Measured During Study Period I: (a) Temporal Plot;
(b) Composite Breakthrough Curves 51
Figure 4-15. Nitrate Concentrations Measured Over the Period I Demonstration Study: (a)
Temporal Plot; (b) Composite Breakthrough Curves 52
Figure 4-16. Concentrations of Arsenic Species at Wellhead and Combined Effluent 54
Figure 4-17. Composite Breakthrough Curves for Total U, V, and Mo 55
Figure 4-18. Composite Breakthrough Curves for Sulfate 56
Figure 4-19. Composite Breakthrough Curves for pH and Total Alkalinity 57
Figure 4-20. Total Arsenic and Nitrate Breakthrough Curves of Run Length Studies 59
Figure 4-21. Total Alkalinity, pH, Sulfate, and Vanadium Breakthrough Curves from Run
Length Study 3 (December 7 to 8, 2005) 61
Figure 4-22. Vessel B Regeneration Curve 63
Figure 4-23. Vessels A and B Regeneration Curves of Arsenic, Nitrate, and Sulfate 64
Figure 4-24. Vessels A andB Regeneration Curves of TDS andpH 65
Figure 4-25. Regeneration Flowrates 66
Figure 4-26. Comparsion of Total Arsenic Concentrations in Distribution System Water and
Treatment Plant Effluent 73
TABLES
Table 1-1. Summary of Round 1 Arsenic Removal Demonstration Sites 2
Table 3-1. Pre-Demonstration Study Activities and Completion Dates 5
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities 6
Table 3-3. Sampling and Analysis Schedule at Fruitland, ID 8
Table 3-4. Sampling and Analysis Schedules for Resin Run Length Studies 13
Table 3-5. Sampling and Analysis Schedules for Spent Resin Regeneration Studies 15
Table 4-1. Source Water Quality Data of Old and Replacement Wells 19
Table 4-2. Historic Well No. 6 Heavy Metals and Fluoride Data 20
Table 4-3. Historic Well No. 6 Radiological Data 21
Table 4-4. Typical Physical and Chemical Properties of Purolite A300E Resin 22
Table 4-5. Design Specifications of IX System 25
Table 4-6. Key Demonstration Study Activities and Start/Complete Dates 33
Table 4-7. Summary of System Operational Data During Study Period I 34
Table 4-8. IX System Regeneration Settings at Fruitland, ID 36
Table 4-9. IX System Regeneration Parameters Collected During Study Period 1 37
Vlll
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Table 4-10. IX System Salt Usage Calculations 39
Table 4-11. Comparison of Wastewater Production Under Different IX Regeneration Settings 45
Table 4-12. Summary of Arsenic, Nitrate, Uranium, Vanadium, and Molybdenum Data 48
Table 4-13. Summary of Other Water Quality Parameters 49
Table 4-14. Regeneration Sampling Results in Study Period 1 67
Table 4-15. Mass Balance Calculations for Total Arsenic, Nitrate, and Sulfate 68
Table 4-16. IX Resin Analysis Results 70
Table 4-17. Summary of Distribution System Sampling Results in Period I Demonstration
Study at City of Fruitland 72
Table 4-18. Cost Breakdowns of Capital Investment for Fruitland IX System 74
Table 4-19. O&M Cost for Fruitland, ID Treatment System 75
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ABBREVIATIONS AND ACRONYMS
Ap differential pressure
AAL American Analytical Laboratories
Al aluminum
AM adsorptive media
As arsenic
ASV anodic stripping voltammetry
AZW Arizona Water Company
bgs below ground surface
BV bed volume(s)
Ca calcium
C/F coagulation/filtration
Cl chlorine
CRF capital recovery factor
Cu copper
DO dissolved oxygen
EBCT empty bed contact time
EMCT multi-component chromatography theory
EPA U.S. Environmental Protection Agency
F fluoride
Fe iron
FRP fiberglass reinforced plastic
gpd gallons per day
gpm gallons per minute
hp horsepower
HC1 hydrochloric acid
ICP-MS inductively coupled plasma-mass spectrometry
ID identification
IDEQ Idaho Department of Environmental Quality
IX ion exchange
LCR Lead and Copper Rule
MCL maximum contaminant level
MDL method detection limit
MDWCA Mutual Domestic Water Consumer's Association
Mg magnesium
Mn manganese
Mo molybdenum
mV millivolts
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Na sodium
NA not applicable
NaOCl sodium hypochlorite
NIST National Institute of Standards and Technology
NRMRL National Risk Management Research Laboratory
NSF NSF International
NTU nephelometric turbidity units
OIP operator interface panel
O&M operation and maintenance
ORD Office of Research and Development
ORP oxidation-reduction potential
P&ID piping and instrumentation diagrams
PLC programmable logic controller
Ppb part per billion
psi pounds per square inch
PVC polyvinyl chloride
QAPP quality assurance project plan
QA/QC quality assurance/quality control
RPD relative percent difference
SBA strong-base anionic exchange
SDWA Safe Drinking Water Act
SM system modification
STMGID South Truckee Meadows General Improvement District
STS Severn Trent Services
TBD
TDS
TOC
U
UPS
uv
to be determined
total dissolved solids
total organic carbon
uranium
uninterrupted power supply
ultraviolet
V vanadium
WRWC White Rock Water Company
XI
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ACKNOWLEDGMENTS
The authors wish to extend their sincere appreciation to the staff of the City of Fruitland Public Works in
Fruitland, Idaho. The Fruitland Public Works staff monitored the treatment system daily and collected
samples from the treatment and distribution systems on a regular schedule throughout this reporting
period. This performance evaluation would not have been possible without their efforts.
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1.0 INTRODUCTION
1.1 Background
The Safe Drinking Water Act (SDWA) mandates that U.S. Environmental Protection Agency (EPA)
identify and regulate drinking water contaminants that may have adverse human health effects and that
are known or anticipated to occur in public water supply systems. In 1975 under the SDWA, EPA
established a maximum contaminant level (MCL) for arsenic at 0.05 mg/L. Amended in 1996, the
SDWA required that EPA develop an arsenic research strategy and publish a proposal to revise the
arsenic MCL by January 2000. On January 18, 2001, EPA finalized the arsenic MCL at 0.01 mg/L (EPA,
2001). To clarify the implementation of the original rule, EPA revised the rule text on March 25, 2003, to
express the MCL as 0.010 mg/L (10 ug/L) (EPA, 2003). The final rule requires all community and non-
transient, non-community water systems to comply with the new standard by January 23, 2006.
In October 2001, EPA announced an initiative for additional research and development of cost-effective
technologies to help small community water systems (< 10,000 customers) meet the new arsenic standard,
and to provide technical assistance to operators of small systems in order to reduce compliance costs. As
part of this Arsenic Rule Implementation Research Program, EPA's Office of Research and Development
(ORD) proposed a project to conduct a series of full-scale, on-site demonstrations of arsenic removal
technologies, process modifications, and engineering approaches applicable to small systems. Shortly
thereafter, an announcement was published in the Federal Register requesting water utilities interested in
participating in the first round of this EPA-sponsored demonstration program to provide information on
their water systems. In June 2002, EPA selected 17 of 115 candidate sites to host the demonstration
studies. The facility at City of Fruitland in Idaho was selected to participate in this demonstration
program.
In September 2002, EPA solicited proposals from engineering firms and vendors for cost-effective
arsenic-removal treatment technologies for the 17 host sites. EPA received 70 technical proposals for the
17 host sites, with each site receiving one to six proposals. In April 2003, an independent technical panel
reviewed the proposals and provided its recommendations to EPA on the technologies that it determined
were acceptable for the demonstration at each site. Because of funding limitations and other technical
reasons, only 12 of the 17 sites were selected for the demonstration program. Using the information
provided by the review panel, EPA, in cooperation with the host sites and the drinking water programs of
the respective states, selected one technical proposal for each site. An ion exchange (IX) system proposed
by Kinetico was selected for demonstration at the Fruitland, ID, site for the removal of arsenic and nitrate
from drinking water supplies.
1.2 Treatment Technologies for Arsenic Removal
The technologies selected for the 12 Round 1 arsenic removal demonstration host sites included nine
adsorptive media (AM) systems, one IX system, one coagulation/filtration (C/F) system, and one process
modification with iron addition. Table 1-1 summarizes the locations, technologies, vendors, and key
source water quality parameters of the 12 demonstration sites. An overview of the technology selection
and system design for the 12 demonstration sites and the associated capital cost is provided in two EPA
reports (Wang, et al., 2004; Chen, et al, 2004), which are posted on the EPA Web site at
http: //www. epa. gov/ORD/NRMRL/wswrd/dw/arsenic/index.html.
As of February 2010, all 12 systems were operational and the performance evaluation of all 12 systems
was completed.
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Table 1-1. Summary of Round 1 Arsenic Removal Demonstration Sites
Demonstration
Site
WRWC (Bow), NH
Rollinsford, NH
Queen Anne's County, MD
Brown City, MI
Climax, MN
Lidgerwood, ND
Desert Sands MDWCA, NM
Nambe Pueblo Tribe, NM
AWC (Rimrock), AZ
AWC (Valley Vista), AZ
Fruitland, ID
STMGID, NV
Technology
(Media)
AM(G2)
AM (E33)
AM (E33)
AM (E33)
C/F (Macrolite)
SM
AM (E33)
AM (E33)
AM (E33)
AM (AAFS50)
IX (A-300E)
AM (GFH)
Vendor
ADI
AdEdge
STS
STS
Kinetico
Kinetico
STS
AdEdge
AdEdge
Kinetico
Kinetico
USFilter
Design
Flowrate
(gpm)
70(a)
100
300
640
140
250
320
145
90(a)
37
250
350
Source Water Quality
As
(Hg/L)
39
36(b)
19(b)
14(b)
39(b)
U6(b>
23(b>
33
50
41
44
39
Fe
(Hg/L)
<25
46
270(c)
127W
546(c)
1,325W
39
<25
170
<25
<25
<25
pH
7.7
8.2
7.3
7.3
7.4
7.2
7.7
8.5
7.2
7.8
7.4
7.4
AM = adsorptive media; C/F = coagulation/filtration; IX = ion exchange; SM = system modification
AWC = Arizona Water Company; MDWCA = Mutual Domestic Water Consumer's Association;
STMGID = South Truckee Meadows General Improvement District; WRWC = White Rock Water
Company; STS = Severn Trent Services
(a) Design flowrate reduced by 50% due to system reconfiguration from parallel to series operation.
(b) Arsenic existing mostly as As(III).
(c) Iron existing mostly as Fe(II).
1.3
Project Objectives
The objective of the arsenic demonstration program is to conduct full-scale arsenic removal technology
demonstration studies on the removal of arsenic from drinking water supplies. The specific objectives are
to:
Evaluate the performance of the arsenic removal technologies for use on small systems
• Determine the required system operation and maintenance (O&M) and operator skill levels
• Characterize process residuals produced by the technologies
• Determine the capital and O&M cost of the technologies.
This report summarizes the performance of the Kinetico IX system at the City of Fruitland, ID, from June
14, 2005, through February 11, 2008. The types of data collected included system operation, water
quality (both across the treatment train and in the distribution system), residuals characterization, and
capital and O&M cost.
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2.0 SUMMARY AND CONCLUSIONS
Based on the information collected during the 32-month demonstration study, the following summary and
conclusions were made relating to the overall objectives of the treatment technology demonstration study.
Performance of the IX arsenic/nitrate removal technology for use on small systems:
• A300E IX resin was effective at removing arsenic and nitrate, provided that the system was
regenerated properly. The system achieved a useful run length of approximately 220,000 gal
(294 bed volumes [BV]) for nitrate, which was shorter than that for arsenic.
• A300E IX resin also was effective at removing uranium, vanadium, and molybdenum.
• After the system was freshly regenerated, elevated arsenic and nitrate concentrations were
detected in the treated water up to 50,000 to 60,000 gal (67 to 80 BV) of throughput (or 3 to 4
hr into service runs), indicating incomplete regeneration. Attempts, including converting the
IX system from co- to counter-current regeneration, were made to eliminate the early leakage.
However, various mechanical difficulties encountered during the system conversion
prevented the counter-current mode from being evaluated for its effectiveness. The early
leakage continued through the end of the demonstration study.
• Freshly regenerated IX resin removes bicarbonate ions, causing reduction in pH and total
alkalinity during the initial 100 BV of service runs.
• Arsenic and nitrate peaking could occur if the system operated beyond exhaustion. To avoid
peaking, the IX system must be regenerated in a timely manner.
• Improper resin regeneration in the counter-current mode resulted in resin fouling and
deteriorating IX resin performance through the end of the demonstration study. Cleaning the
fouled IX resin with a 5% caustic/10% brine mixture was somewhat effective in restoring
resin capacity based on measurements such as volumetric and strong base capacity, moisture
content, and total organic fouling. However, the IX resin run length did not improve.
Required system O&Mand operator skill levels:
• Under normal operating conditions, the skill requirements to operate the system were
minimal with a typical daily demand on the operator of 30 min. Other skills needed
for performing O&M activities included replacing filter bags periodically, using a
hydrometer to check brine concentrations, monitoring salt inventory levels,
scheduling salt delivery, and working with the vendor to troubleshoot and perform
minor on-site repairs.
• It was important to monitor salt usage during a regeneration cycle to ensure that the IX resin
was properly regenerated.
Process residuals produced by the technology:
• Residuals produced by the IX system included spent brine and rinse water. The volume of
wastewater produced was dependent upon regeneration frequency and settings.
• Discharging spent brine to the sewer caused problems to the city's sewage lagoons,
prompting the city to shorten the daily operating time to 3 hr/day. High salt content in
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sewage was thought to have stressed duckweeds in the lagoons. Shorter daily operating time
and less frequent system regeneration appeared to alleviate the problems.
Cost of the technology:
• Using the system's rated capacity of 250 gal/min (gpm) (or 360,000 gal/day [gpd]), the
capital cost was $l,146/gpm (or $0.80/gpd) of the design capacity.
• Cost of salt supply was the most significant add-on to the previous plant operation. The
actual salt supply during the first year of system operation cost $0.49/1,000 gal of water
treated, which could be lowered to $0.35/1,000 gal if a salt usage rate of 3.16 lb/1,000 gal
was reached.
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3.0 MATERIALS AND METHODS
3.1
General Project Approach
Following the pre-demonstration activities summarized in Table 3-1, the performance evaluation of the
IX system began on June 14, 2005, and ended on February 11, 2008. Table 3-2 summarizes the types of
data collected and/or considered as part of the technology evaluation study. The overall performance of
the system was evaluated based on its ability to consistently remove arsenic and nitrate to below their
respective MCLs of 10-|o,g/L and 10-mg/L (as N) through the collection of water samples across the
treatment train, as described in a Performance Evaluation Study Plan (Battelle, 2004). The reliability of
the system was evaluated by tracking the unscheduled system downtime and frequency and extent of
equipment repairs and replacement. The plant operator recorded unscheduled downtime and repair
information on a Repair and Maintenance Log Sheet.
Table 3-1. Pre-Demonstration Study Activities and Completion Dates
Activity
Introductory Meeting Held
Request for Quotation Issued to Vendor
Vendor Quotation Received by Battelle
Purchase Order Completed and Signed
Letter Report Issued
Draft Study Plan Issued
Engineering Package Submitted to IDEQ
Concrete Pad Poured
Building Construction Begun
Final Study Plan Issued
IX-248-As/N System Shipped
Building Construction Completed
IX-248-As/N System Arrived
Excessive Sediment Production in Well No. 6 Occurred
Well Investigation on Sediment Production Conducted
Replacement Well No. 6-2004 Drilled
Treatment System Permit Issued
System Installation Completed
System Shakedown Halted due to Positive Coliform Test Results
Well Sanitization Continued due to Positive Coliform Test Results
Incorrect IX Resin Replaced with A300E Resin
Negative Coliform Test Results Obtained and Submitted to IDEQ
New Pump Installed in Well No. 6-2004
Request for Discharging Treated Water to Distribution System
Approved by IDEQ
System Shakedown Completed
Performance Evaluation Begun
Date
August 2 1,2003
August 26, 2003
September 19, 2003
October 16, 2003
October 17, 2003
November 26, 2003
January 25, 2004
February 6, 2004
February 10, 2004
February 25, 2004
March 3, 2004
March 3, 2004
March 8, 2004
March 25 to 26, 2004
April 1 to 13, 2004
May to July 2004
May 10, 2004
July 27, 2004
July 28, 2004
July 2004 to April 2005
April 2 1,2005
May 4, 2005
May 19, 2005
June 7, 2005
June 13, 2005
June 14, 2005
IDEQ = Idaho Department of Environmental Quality
The required system O&M and operator skill levels were evaluated through quantitative data and
qualitative considerations, including the need for pre- and/or post-treatment, level of system automation,
extent of the preventive maintenance activities, frequency of chemical and/or media handling and
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Table 3-2. Evaluation Objectives and Supporting Data Collection Activities
Evaluation Objective
Performance
Reliability
System O&M and Operator
Skill Requirements
Residual Management
System Cost
Data Collection
Ability to consistently meet 10 (o,g/L of arsenic and 10 mg/L of nitrate (as
N) in treated water
Unscheduled system downtime
Frequency and extent of repairs, including a description of problems,
materials and supplies needed, and associated labor and cost
Pre- and post-treatment requirements
Level of automation for system operation and data collection
Staffing requirements, including number of operators and laborers
Task analysis of preventive maintenance, including number, frequency, and
complexity of tasks
Chemical handling and inventory requirements
General knowledge needed for relevant chemical processes and health and
safety practices
Quantity and characteristics of aqueous and solid residuals generated by
system operation
Capital cost for equipment, site engineering, and installation
O&M cost for chemical usage, electricity consumption, and labor
inventory, and general knowledge needed for relevant chemical processes and health and safety practices.
The staffing requirements for the system operation were recorded on an Operator Labor Hour Log Sheet.
The cost of the system was evaluated based on the capital cost per gpm (or gpd) of design capacity and
the O&M cost per 1,000 gal of water treated. This required tracking the capital cost for equipment, site
engineering, and installation, as well as the O&M cost for salt supply, electrical power use, and labor.
The quantity of residuals generated was estimated by monitoring the flowrate and duration of each
regeneration step (i.e., brine draw, slow rinse, and fast rinse) and tracking the number of regeneration
cycles during the study period. Spent regenerant samples were collected and analyzed for chemical
characteristics.
3.2
System O&M and Cost Data Collection
The plant operator performed daily, weekly, and monthly system O&M and data collection according to
instructions provided by Kinetico and Battelle. The plant operator recorded system operational data, such
as pressure, flowrate, system throughput, hour meter, and regeneration counter readings on a Daily
System Operation Log Sheet; checked brine day tank and salt saturator levels; and conducted visual
inspections for leaks or faults. If any problems occurred, the plant operator contacted the Battelle Study
Lead, who would then determine if Kinetico should be contacted for troubleshooting. The plant operator
recorded all relevant information, including problem encountered, course of action taken, materials and
supplies used, and associated cost and labor incurred, on the Repair and Maintenance Log Sheet. On a
weekly basis, the plant operator measured water quality parameters, including pH, temperature, dissolved
oxygen (DO), and oxidation-reduction potential (ORP), and recorded the data on a Weekly Water Quality
Parameters Log Sheet. During the study period, the system was regenerated automatically when triggered
by a pre-determined throughput setpoint. Occasionally, system regeneration was initiated by the operator
for sampling purposes.
The capital cost for the arsenic-removal system consisted of the cost for equipment, site engineering, and
system installation. The O&M cost consisted primarily of the cost for salt use, electricity consumption,
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and labor. Salt was delivered in bulk quantities by a company, Western Step Saver, Inc. in Boise, ID, on a
weekly or as-needed basis to the treatment plant. Salt usage was tracked through monthly invoices.
Electricity consumption was obtained from utility bills for the reporting period. Labor hours for routine
system O&M, system troubleshooting and repairs, and demonstration-related work, were recorded daily
on an Operator Labor Hour Sheet. Routine O&M included activities such as filling field logs and
performing system inspections. Demonstration-related work, including activities such as performing field
measurements, collecting and shipping samples, and communicating with the Battelle Study Lead, was
recorded, but not used for cost analysis.
3.3 Sample Collection Procedures and Schedules
System operation during the performance evluation study underwent three distinct periods as discussed in
Section 4.4. The plant operator collected water samples from the treatment plant/distribution system
and/or during the IX resin regeneration process either on a regular basis as summarized in Table 3-3 or
through special run length and regeneration studies as described in Sectgion 3.5.1. Table 3-3 provides the
sampling schedule and analytes measured during each regular sampling event. Figure 3-1 presents a
process flow chart, along with the sampling/analysis schedule, for the IX system. Specific sampling
requirements for analytical methods, sample volumes, containers, preservation, and holding times are
presented in Table 4-1 of the EPA-endorsed Quality Assurance Project Plan (QAPP) (Battelle, 2003).
3.3.1 Source Water. During the initial visit to the site on August 21, 2003, one set of source water
samples was collected from Well No. 6 for detailed water quality analyses. Because it had not been in
use due to elevated nitrate concentrations, the well was purged for several hours before the samples were
taken from a temporary sample tap on a hose that discharged the purged water to the ground. The source
water also was speciated onsite for particulate and soluble As, As(III) and As(V), and particulate and
soluble iron (Fe), manganese (Mn), and aluminum (Al). Special care was taken to avoid agitation, which
might cause unwanted oxidation. After completion of a replacement well, Well No. 6-2004, Battelle
arranged source water samples to be taken from the new well by the plant operator on July 13, 2004.
3.3.2 Treatment Plant Water. Routine treatment plant water samples were collected only during
Period I extending from June 14, 2005, through July 25, 2006. The plant operator collected water
samples across the treatment train weekly on a 4-week cycle (exception for six sampling events that took
place biweekly and one sampling event that took place in 3 weeks). For the first week of each 4-week
cycle, water samples were collected for arsenic speciation at two locations (i.e., at the wellhead [IN] and
at the combined effluent from Vessels A and B [TT]) and analyzed for the analytes listed under the
monthly treatment plant analyte list in Table 3-3. For the other three weeks, treatment plant samples were
collected at three locations (i.e., IN, after Vessel A [TA], and after Vessel B [TB]) and analyzed for the
analytes listed under the weekly treatment plant analyte list in Table 3-3.
3.3.3 Regeneration Wastewater. Similar to treatment plant sampling, routine regeneration
wastewater samples were collected only during Study Period I when the IX system was regenerated in a
co-current mode. Co-current regeneration introduced brine solution and rinse water downward through
each IX resin bed with spent brine/rinse water discharged from the bottom of the vessel to a floor drain.
Starting from November 15, 2005, on eight separate occasions, one composite sample from each of the
three regeneration steps (i.e., brine draw, slow rinse, and fast rinse) was collected during regeneration of
each IX resin vessel. When the IX resin beds were regenerated, a portion of the effluent from each of the
three regeneration steps was diverted to a 32-gal plastic container through a garden hose over the duration
of each step (Figure 3-2). At the end of the regeneration, the content in the three containers was
thoroughly mixed, and a portion of the liquid was transferred to sample bottles for total As, nitrate,
sulfate, total dissolved solids (TDS), and pH analyses. Arsenic speciation was not performed on the
wastewater samples.
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Table 3-3. Sampling and Analysis Schedule at Fruitland, ID
Sample
Type
Source Water
Treatment
Plant Water
Distribution
Water
Regeneration
Wastewater
Sampling
Locations'50
IN
IN, TA, and
TB
IN and TT
One Non-
LCR
Residence
and Two
Non-
Residential
Locations
Drain Pipe
off Vessels
AandB
No. of
Sampling
Locations
1
o
5
2
o
5
6(c)
Frequency
Three
Times
Weekly
Monthly
Monthly
8 times
Analytes
As (total and paniculate),
As(III), As(V),
Fe (total and soluble),
Mn (total and soluble),
Al (total and soluble),
V (total and soluble),
Mo (total and soluble),
Sb (total and soluble),
Na, Ca, Mg, Cl, F, NO3,
S2; SO4, SiO2, PO4, TOC,
alkalinity, turbidity, and
pH
Onsite: pH, temp., DO,
andORP
Offsite: As (total),
Fe (total), Mn (total),
U (total), V (total),
Mo (total), F, NO3, SO4,
SiO2, PO4, P (total),
alkalinity, and/or turbidity
Same as those for weekly
samples plus following:
Offsite: As (soluble),
As(III), As(V),
Fe (soluble), Mn (soluble),
U (soluble), V (soluble),
Mo ( soluble), Ca, Mg,
andTDS
pH, alkalinity, As (total),
Fe (total), Mn (total), Pb
(total), Cu (total), and NO3
As (total), NO3, SO4,
TDS, and pH
Sampling
Date
Well No. 6:
08/21/03
Well No. 6-2004:
07/13/04, 04/17/07
06/23/05, 06/29/05, 07/06/05,
07/20/05, 08/03/05, 08/10/05,
08/24/05, 08/31/05, 09/07/05,
09/21/05, 09/28/05, 10/05/05,
10/26/05, 11/02/05, 11/16/05,
11/30/05, 01/04/06, 01/10/06,
01/25/06, 02/01/06, 02/08/06,
02/15/06, 03/01/06, 03/15/06,
03/29/06, 04/05/06, 04/26/06,
05/03/06, 05/09/06, 05/24/06,
05/31/06, 06/07/06, 06/21/06,
06/28/06, 07/06/06
06/15/05, 07/13/05, 08/17/05,
09/14/05, 10/12/05, 11/09/05,
12/14/05, 01/18/06, 02/22/06,
03/22/06, 04/19/06, 05/17/06,
06/14/06, 07/12/06
Baseline sampling:(b)
12/08/03, 01/06/04, 02/02/04,
03/02/04
Monthly Sampling:
06/29/05, 08/03/05, 08/24/05,
09/21/05, 10/26/05, 11/30/05,
12/15/05, 01/25/06, 02/22/06,
03/23/06, 04/19/06, 05/24/06,
06/14/06, 07/12/06
11/15/05,01/11/06,02/15/06,
04/04/06, 04/13/06, 05/09/06,
06/07/06, 07/06/06
(a)
Abbreviations in parentheses corresponding to sample locations in Figure 3 -1: IN = at wellhead, TA = after
Vessel A, TB = after Vessel B, and TT = conbined effluent.
(b) Four baseline sampling events performed before system placed online.
Three composite samples from each vessel for each regeneration steps (i.e.,brine draw, slow rinse, and fast
rinse).
(c)
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INFLUENT
(WELL No. 6-2004)
Monthly
pH
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Figure 3-2. A Garden Hose Used for Residual Sampling from IX Resin Vessel
3.3.4 Distribution System Water. Water in the distribution system was sampled at three locations
to determine the impact of the IX system on the water chemistry in the distribution system, specifically,
the arsenic, nitrate, lead, and copper levels. Since the City of Fruitland had 11 wells to supply the
distribution system, sampling locations were selected from a small area of homes that received water
primarily from Well No. 6-2004. The sampling locations selected included one residence (the operator's
house) and two non-residential locations, even though none of them was part of the city's Lead and
Copper Rule (LCR) sampling locations.
The operator collected all of the samples following an instruction sheet developed according to the Lead
and Copper Rule Monitoring and Reporting Guidance for Public Water Systems (EPA, 2002). First-draw
samples were collected from a cold-water faucet that had not been used for at least six hours to ensure
that stagnant water was sampled. The sampler recorded the date and time of last water use before
sampling and the date and time of sample collection for calculation of the stagnation time. Arsenic
speciation was not performed on these samples.
From December 2003 to March 2004 prior to system startup, four monthly samples were collected
from the locations within the distribution system to establish the baseline condition. Following system
startup in June 2005, distribution system sampling continued on a monthly basis at the same three
locations during Study Period I. Analytes for the distribution system sampling are presented in
Table 3-3.
10
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3.4 Real-Time Arsenic Monitoring with ArsenicGuard
On May 7, 2007, a real-time total arsenic analyzer, ArsenicGuard, was installed to monitor total arsenic
concentrations in IX system effluent at the TT location.
The ArsenicGuard analyzer (Figure 3-3) was developed by TraceDetect, Inc. to measure total inorganic
arsenic in drinking and groundwater via Anodic Stripping Voltammetry (ASV) using a gold-coated Nano-
Band™ electrode. The normal measurement range is 1 to 25 (ig/L. The analyzer also supports dilution
up to 50:1, so the measurement range can be extended upwards to 50 to 1,250 (ig/L. As claimed by the
vendor, the accuracy in the normal range is 1 (ig/L or ±20% (whichever is larger), and 50 (ig/L or ±20%
for the extended range. Because the sensor is only sensitive to arsenite, sample treatment is required prior
to actual measurements. Each measurement starts with acidification of a sample to pH ~0.7 with 2M
hydrochloric acid (HC1), followed by reduction of all arsenate to arsenite via a reducer not specified by
the vendor. The instrument then makes calibrated measurements by first scanning for arsenic in the
treated sample, followed by adding a metered quantity of arsenite (the spike) and re-scanning. From these
steps, a two-point calibration curve is derived for each sample tested. The result of each measurement is
displayed on the front screen of the analyzer.
The ArsenicGuard utilizes electrochemical plating and a stripping technique to measure part-per-billion
(ppb) quantities of arsenic. The treated sample is drawn into a measurement cell, which houses a sensor,
a reference electrode, and an auxiliary electrode. The voltage of this electrochemical cell is manipulated
so that arsenic is first plated on to the tip of the sensor during an accumulation phase, and then stripped
off the sensor during a stripping phase. The duration of the accumulation phase is adjusted to ensure a
good stripping signal, i.e., high concentrations are measured using a short accumulation time and low
concentrations using a longer accumulation time. The sensing action occurs during the stripping phase of
the measurement. During this phase, the voltage of the electrochemical cell is ramped from the
accumulation potential, past the stripping potential for arsenic. When arsenic is stripped off the sensor, it
dissolves back into the test solution. This stripping process releases three electrons per arsenic atom and,
therefore, the amount of arsenic accumulated on the tip of the sensor is proportional to the current
measured during the stripping operation. This current is recorded for the treated sample as well as for the
spiked sample to calculate the arsenic concentration in the original sample stream.
3.5 IX Resin Run Length and Spent IX Resin Regeneration Studies
3.5.1 IX Resin Run Length Studies. Because the routine weekly samples collected from the
treatment plant only represented discrete data points from multiple service runs, it was necessary to
collect samples from several complete service runs to delineate arsenic and nitrate breakthrough curves
and to determine the appropriate run length of the IX system. The results of the studies were used to
optimize system performance. Table 3-4 summarizes sampling and analytical schedules of six run length
studies, during which effluent samples were collected from either one or both vessels throughout the set
service runs. A combined effluent totalizer was used to track the volume of water treated between two
consecutive regeneration cycles. The totalizer was automatically reset to "zero" when regeneration of
Vessel A was complete and regeneration of Vessel B just began. The reset of the totalizer also signaled
the beginning of the service run. The service run ended when the totalizer reached a preset throughput
value, which triggered the next regeneration cycle. Additional information for each of the studies is
provided below.
Run Length Study 1. Between July 28 and 30, 2005, a vendor technician was onsite to collect samples of
the combined effluent from both resin vessels during one service run and perform field measurements for
the analytes shown in Table 3-4. Sampling began when Vessel A had completed regeneration and gone
into service and when Vessel B had just begun regeneration. Hourly samples were collected until
11
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Figure 3-3. Real-Time Arsenic Analyzer - ArsenicGuard
392,000 gal (524 BV) of water was processed. In addition, operational parameters, such as system inlet
and outlet pressure, flowrate, and throughput were recorded every hour. Arsenic was analyzed onsite
using a Quick arsenic test kit (Industrial Test Systems) and a 28°C water bath to maintain the required
sample temperature between 24 and 30°C. Nitrate was measured using Hach nitrate test tubes (CAT No.
14037-00). pH was measured using Macerey-Nagel pH 0-14 test strips. Conductivity was taken using a
Myron-L, National Institute of Standards and Technology (NIST)-certified meter. Because effluent
arsenic and nitrate concentrations reached detectable levels of 2 ug/L and 5 mg/L, respectively, at
approximately 400 BV (see Section 4.5.2), the regeneration throughput setpoint was upwardly adjusted
from 214,000 gal (or 286 BV) to 335,000 gal (or 448 BV) on July 30, 2005.
12
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Table 3-4. Sampling and Analysis Schedules for Resin Run Length Studies
No.
1
2
3
4
5
6
Date
07/28/05-
07/30/05
08/16/05-
08/17/05
12/07/05-
12/08/05
04/11/06-
04/12/06
08/09/06-
08/10/06
01/17/07-
01/18/07
Run Length
Setpoint
(gal)
214,000(a)
335,000
316,000
316,000
316,000
316,000
(BV)
286
448
422
422
422
422
Regeneration
Mode
Co-current
Co-current
Co-current
Co-current
Counter-
current
Counter-
current
Sampling
Location
IN(b), TT
IN(b),
TA
INtb),
TA, TB
IN(b),
TA, TB
INtb),
TA, TB
TA, TB
Number
of
Samples
30
11
20
20
20
20
Analytes
As (total), NO3, conductivity, pH, and
temperature (onsite measurements only)
As (total) and NO3
As (total), U (total), V (total), Mo
(total), NO3, SO4, alkalinity, and pH
As (total) and NO3
As (total), V (total), NO3, and pH
As (total) and NO3
Reason for Study
To determine proper service run
length/regeneration frequency after
system startup
To further delineate breakthrough
behavior after run length had been
increased
To further delineate breakthrough
behavior after run length had been
slightly decreased
To further delineate breakthrough
behavior after brine concentration
had been reduced from 8% to 6%
To further delineate breakthrough
behavior after regeneration had
been changed from co- to counter
current mode
To further delineate breakthrough
behavior after brine eductor had
been replaced with a brine injection
pump per vendor recommendation
(a) Although set at 214,000 gal, system regeneration not taking place until 392,000 gal (524 BV).
(b) Inlet sample collected once at beginning of respective run length studies.
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Run Length Study 2: On August 16 and 17, 2005, the plant operator collected a series of samples from
Vessel A to help construct arsenic and nitrate breakthrough curves. Sampling at TA began approximately
30 min after regeneration of Vessel A had been completed, and continued by intervals of 1 to 3 hr, except
during the night. Flowrates and throughput values were recorded at the time of sampling for calculations
of the run length. The samples collected were sent to Battelle for arsenic and nitrate analyses.
Run Length Study 3: Following another adjustment to the throughput setpoint from 335,000 gal (or 448
BV) to 316,000 gal (or 422 BV) on September 19, 2005, Battelle staff and the plant operator collected 10
samples from each IX resin vessel during September 22 through 23, 2005, to further examine arsenic and
nitrate breakthrough from the IX system. Sampling from each vessel was repeated on December 7 and 8,
2005, because, for unknown reasons, arsenic and nitrate concentrations in all samples collected on
September 22 and 23, 2005, were similar to those in raw water. The first TA and TB samples on
December 7, 2005, were collected approximately 30 min after completion of Vessels A and B
regeneration. Subsequent samples were taken every 1 to 3 hr thereafter, except during the night. The last
sample was collected at 288,000 gal before reaching the 316,000-gal setpoint. The samples collected
were sent to Battelle for the analytes listed in Table 3-4.
Run Length Study 4: Following reduction of brine concentrations from 8% to 6% on March 5, 2006, the
plant operator collected 10 samples from each IX resin vessel during April 11 through 12, 2006, to
examine arsenic and nitrate breakthrough from the IX system. An inlet sample was collected once at the
beginning of the study. The first TA and TB samples were collected approximately 20 min after
regeneration of the respective vessels. Subsequent samples were taken every 1 to 4 hr thereafter, except
during the night. The last sample was collected just before the 316,000-gal setpoint. The samples
collected were sent to Battelle for the analytes listed in Table 3-4.
Run Length Study 5: After switching from co-current to counter-current mode on July 25, 2006 (Section
4.4.3.1), the plant operator collected 10 samples from each IX resin vessel during August 9 through 10,
2006, to investigate arsenic and nitrate breakthrough after the system had been regenerated in a counter-
current mode. The first TA and TB samples were collected immediately after regeneration of the
respective vessels. Subsequent samples were taken every 1 to 4 hr thereafter, except during the night.
The last sample was collected just before the 316,000-gal setpoint. The samples collected were sent to
Battelle for the analytes listed in Table 3-4.
Run Length Study 6: Another run length study was conducted on January 16 and 17, 2007, after a brine
injection pump was installed (to replace the originally installed eductor) and modifications to counter-
current regeneration were completed (Section 4.4.3.1). The plant operator collected samples from each
IX resin vessel to examine arsenic and nitrate breakthrough following regeneration in a counter-current
mode. Similar to Run Length Study 5, the first TA and TB samples were collected immediately after
regeneration. Subsequent samples were taken every 1 to 4 hr thereafter (except during the night). The
last sample was collected just before the 316,000-gal setpoint. The samples collected were sent to
Battelle for the analytes listed in Table 3-4.
3.5.2 Spent IX Resin Regeneration Studies. The regeneration scheme was adjusted several times
to improve brine regeneration efficiency and minimize waste production. Two elution studies were
performed to evaluate the effectiveness of the IX resin regeneration process and determine the quantity
and chemical characteristics of the residuals. Table 3-5 summarizes sampling schedules, analytes
measured, and corresponding regeneration settings.
14
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Table 3-5. Sampling and Analysis Schedules for Spent Resin Regeneration Studies
No.
1
2
Date
07/30/05
09/22/05
Throughput
of Previous
Service Run
(gal)
392,000
316,000
Regeneration
Steps
Brine Draw
Slow Rinse
Fast Rinse
Brine Draw
Slow Rinse
Fast Rinse
Duration
(min)
32
64
30
32
64
6
Number
of Grab
Samples
31
61
28
8
6
2
Number
of
Composite
Samples
Not
collected
1
1
1
Analytes
specific gravity and
conductivity
TDS, pH, alkalinity,
total As, U, V, and
Mo, NO3, and SO4
Elution Study 1. During a trip to Fruitland in July 2005, a vendor technician changed the brine
concentration from 4% to 8% and the brine draw time from 64 to 32 min in an attempt to maintain a
target regeneration level of 10 Ib NaCl/ft3 resin. Upon completion of Run Length Study 1 as described
above, the technician continued to perform the regeneration study by monitoring the conductivity and
specific gravity of regeneration wastewater using a Myron-L NIST-certified meter and a hydrometer
every minute. Regenerant and rinse samples were not taken for arsenic and nitrate analyses.
Elution Study 2. To further characterize regeneration residuals, Battelle staff conducted an elution study
on both IX resin vessels on September 22, 2005. The test apparatus used was similar to that described in
Section 3.3.3 except that a flow-through cell attached to the inner rim of a 32-gal plastic container
(Figure 3-4) was used to receive regeneration wastewater continuously during each of the three
regeneration steps. Probes/electrodes associated with a Hanna HI 9635 conductivity/TDS meter (Hanna
Instruments, Inc., Woonsockett, RI) and a WTW Multi 340i handheld meter (VWR) were placed in the
flow-through cell for continuous measurements of conductivity/TDS, pH, and temperature during
regeneration. The time elapsed and flow totalizer readings also were recorded every 1 to 2 min once
regeneration began. Grab samples were collected every 4 to 6 min by filling up sample bottles with the
overflow from the flow-through cell. At the end of the regeneration cycle, the content in each 32-gal
container was thoroughly mixed and a composite sample was collected from each container. The samples
were shipped to Battelle for the analytes listed in Table 3-5.
3.6
IX Resin Cleaning and Analysis
The IX resin was fouled due to the presence of total organic carbon (TOC) and repeatedly unsuccessful
regenerations of the IX resin in the counter-current mode. Core samples were collected from Vessels A
and B by Kinetico on March 28, 2007. The samples were sent to Purolite, cleaned in its laboratory with a
mixture of 2% NaOH and 10% brine, and analyzed before and after the caustic/brine cleaning. Analytes
included moisture content, volumetric capacity, strong base capacity, and total organic fouling. The
results are discussed in Section 4.5.5.
The IX resin in both vessels was washed with a 5% caustic/10% brine mixture on June 19, 2007. The
caustic/brine mixture was prepared by dispensing 55 gal of a 50% NaOH concentrate to the brine day
tank using a drum pump followed by filling the day tank with brine up to 550 gal. The specific gravity of
the mixture was 1.045, corresponding to a 6% brine solution. The caustic/brine mixture was drawn
downward through the vessels (one at a time) at 48 gpm for about 25 min. By the end of brine draw, a
hand valve was closed manually to allow the IX resin to soak in the caustic/brine mixture for 30 min.
Slow rinse was then conducted at 38 gpm for about 40 min. Following the slow rinse, fast rinse was
conducted at 72 to 74 gpm for about 15 min. Upon completion, the IX vessels were subject to another
15
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round of regular co-current regeneration. Co-current regeneration was used due to the difficulties
encountered in the counter-current regeneration mode (Section 4.4.3).
Upon completion of the regeneration with caustic/brine, a core sample was then taken from Vessel B and
sent to Purolite for analysis. The same set of analytes above was analyzed for this sample.
3.7
Sampling Logistics
All sampling logistics including arsenic speciation kit preparation, sample cooler preparation, and sample
shipping and handling are discussed as follows.
3.7.1 Preparation of Arsenic Speciation Kits. The arsenic field speciation method used an anion
exchange resin column to separate the soluble arsenic species, As(V) and As(III) (Edwards et al., 1998).
Arsenic speciation kits were prepared in batches at Battelle laboratories according to the procedures
detailed in Appendix A of the EPA-endorsed QAPP (Battelle, 2003).
3.7.2 Preparation of Sampling Coolers. For each sampling event, a sample cooler was prepared
with the appropriate number and type of sample bottles, disc filters, and/or speciation kits. All sample
bottles were new and contained appropriate preservatives. Each sample bottle was taped with a pre-
printed, colored-coded, and waterproof label. The sample label consisted of sample identification (ID),
date and time of sample collection, collector's name, site location, sample destination, analysis required,
and preservative. The sample ID consisted of a two-letter code for a specific water facility, sampling
date, a two-letter code for a specific sampling location, and a one-letter code for the specific analysis to be
performed. The sampling locations were color-coded for easy identification.
Figure 3-4. Field Setup for Arsenic/Nitrate Regeneration Study
16
-------
For example, red, yellow, green, and blue were used for IN, TA, TB, and TT sampling locations. Pre-
labeled bottles for each sampling location were placed in separate zip-lock bags (each corresponding to a
specific sampling location), which were then packed in a sample cooler. When arsenic speciation
samples were to be collected, arsenic speciation kits also were included in the cooler.
When appropriate, the sample cooler was packed with bottles for the three distribution system sampling
locations. In addition, a packet containing all sampling and shipping-related supplies such as latex
gloves, sampling instructions, chain-of-custody forms, prepaid FedEx air bills, and bubble wrap also was
placed in the cooler. Except for the operator's signature, the chain-of-custody forms and prepaid FedEx
air bills had already been completed with the required information. The sample coolers were shipped via
FedEx to the facility approximately 1 week prior to the scheduled sampling date.
3.7.3 Sample Shipping and Handling. After sample collection, samples for off-site analyses were
packed carefully in the original coolers with wet ice and shipped to Battelle. Upon receipt, sample
custodians verified that all samples indicated on the chain-of-custody forms were included and intact.
Sample IDs were checked against the chain-of-custody forms and the samples were logged into the
laboratory sample receipt log. Any discrepancies were addressed with the field sample custodian, and the
Battelle Study Lead was notified.
Samples for metal analyses were stored at Battelle's inductively coupled plasma-mass spectrometry (ICP-
MS) laboratory. Samples for other water quality analyses were packed in coolers and picked up by
couriers from American Analytical Laboratories (AAL) in Columbus, OH, or TCCI Laboratories in New
Lexington, OH, both of which were under contract with Battelle for this demonstration study. The chain-
of-custody forms remained with the samples from the time of preparation through analysis and final
disposal. All samples were archived by the appropriate laboratories for the respective duration of the
required hold time and disposed of properly thereafter.
3.8 Analytical Procedures
The analytical procedures described in detail in Section 4.0 of the EPA-endorsed QAPP (Battelle, 2003)
were followed by Battelle ICP-MS, AAL, and TCCI Laboratories. Laboratory quality assurance/quality
control (QA/QC) of all methods followed the prescribed guidelines. Data quality in terms of precision,
accuracy, method detection limit (MDL), and completeness met the criteria established in the QAPP, i.e.,
relative percent difference (RPD) of 20%, percent recovery of 80% to 120%, and completeness of 80%.
The QA data associated with each analyte will be presented and evaluated in a QA/QC summary report to
be prepared under separate cover and to be shared with the Arsenic Demonstration Project.
Field measurements of pH, temperature, DO, and ORP were conducted by the plant operator using a
WTW Multi 340i handheld meter, which was calibrated for pH and DO prior to use following the
procedures provided in the user's manual. The ORP probe also was checked for accuracy by measuring
the ORP of a standard solution and comparing it to the expected value. The plant operator collected a
water sample in a clean, plastic beaker and placed the Multi 340i probe in the beaker until a stable value
was obtained.
17
-------
4.0 RESULTS AND DISCUSSION
4.1 Facility Description
The City of Fruitland is located in southwest Idaho, approximately 50 miles northwest of Boise on
Highway 1-95. It has multiple production wells (Wells No. 1, 5, 6, 9, 10, 11, 12, 14, 15, 16, and 20) that
supply water to approximately 4,000 residents. Well No. 6, originally selected for this demonstration
project, is located on South Utah Street between Southwest 4th and 7th Streets. Drilled in 1973 using a
rotary drilling method, the well was installed in a 24-in-diameter by 204-ft-deep borehole to a total depth
of 199 ft below ground surface (bgs). The well was lined with a 12-in-diameter steel casing extending
from 3 ft above ground to 109 ft bgs and a 10-in-diameter steel casing extending from 109 to 199 ft bgs.
The well had four screened sections: 44 to 54 ft bgs, 58 to 68 ft bgs, 109 to 119 ft bgs, and 179 to 189 ft
bgs. The static water level was 36.4 ft bgs. A submersible pump placed at 105 ft bgs was rated at 250
gpm. A downhole camera survey on October 29, 1998, indicated that 90% of the third screen (109-119 ft
bgs) was plugged and that the fourth screened section was completely buried in sediment. Well No. 6
was taken offline since January 2000 due to levels higher than the nitrate MCL in the well water. There
was no water treatment in place prior to the installation of the IX system.
Problems with sediment production were encountered with Well No. 6 during the shakedown of the IX
system in March 2004. A replacement well, Well No. 6-2004, was installed in June 2004 in a 20-in-
diameter by 140-ft-deep borehole to a total depth of 125 ft bgs using a cable tool drilling method at a
location approximately 25 ft from the existing well (see more details in Section 4.3). The well was
constructed of a 12-in-diameter steel casing with three screened sections: 50 to 70 ft bgs, 95 to 105 ft bgs,
and 110 to 120 ft bgs. The submersible pump from the old Well No. 6 was placed into the new well at
105 ft bgs. Well pumping tests indicated that this well could produce about 200 gpm of water while
maintaining a similar static water level at 36.3 ft bgs (aggressive pumping was not desired by the city due
to its concern over potential subsidence of the ground).
4.1.1 Source Water Quality. Source water samples were collected from the old Well No. 6 on
August 21, 2003, and from the replacement well, Well No. 6-2004, on July 13, 2004, and then April 17,
2007, about 22 months into the performance evaluation study to confirm the source water quality. Table
4-1 presents the analytical results of both wells and compares them with the data provided by the city to
EPA for the demonstration site selection and with the data independently collected by EPA and the
vendor. Figure 4-1 plotted historic nitrate data for Well No. 6 obtained from IDEQ. Tables 4-2 and 4-3
summarize historic data of several heavy metals, fluoride, and radiological analytes for Well No. 6.
Based on the data, water quality of Well No. 6-2004 was very similar to that of Well No. 6 and remained
rather consistent during the entire study period.
Arsenic Species. Total arsenic concentration in the new well (Well No. 6-2004) ranged from 48.5 to 49.7
ug/L, existing mostly in a soluble form (39.9 ug/L according to July 13, 2004, data). Although total
arsenic concentrations in the new well were higher than those in the old well (Well No. 6, which ranged
from 32 to 46 ug/L as shown in Tables 4-1 and 4-2), soluble arsenic concentrations were comparable
between the two wells (i.e., 39.9 vs. 40.1 ug/L). The higher particulate arsenic concentration observed
(i.e., 9.8 vs. 3.4 ug/L) might be caused by insufficient well purging or sample tap flushing. Some
particulate arsenic and/or well sediment might be removed by the bag filters (with 20 um nominal pore
size) located upstream of the IX resin vessels. Removal of particulate matter and sediment can help
alleviate adverse effects on the resin beds. Similar to the old well, most soluble arsenic existed as As(V)
(i.e., H2AsO4" at 39.0 ug/L) with only a small amount existing as As(III) (i.e., H3AsO3 at 1.0 ug/L).
Because IX resin is effective at removing arsenate, pre-oxidation of the water upstream of the IX process
was not required.
18
-------
Table 4-1. Source Water Quality Data of Old and Replacement Wells
Parameter
Unit
Well ID
Sampling Date
pH
Total Alkalinity (as CaCO3)
Hardness (as CaCO3)
Chloride
Fluoride
Nitrate (as N)
Sulfate
Silica (as SiO2)
Orthophosphate (as PO4)
TOC
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Al (total)
Al (soluble)
Mn (total)
Mn (soluble)
V (total)
V (soluble)
Mo (total)
Mo (soluble)
Sb (total)
Sb (soluble)
Na
Ca
Mg
S.U.
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
W?/L
HB/L
Mfi/L
^g/L
^g/L
^g/L
^g/L
Mfi/L
HB/L
W?/L
HB/L
^g/L
^g/L
^g/L
W?/L
HB/L
W?/L
Mg/L
Mg/L
Mg/L
Facility
Data
No. 6
NA
7.4
357
252
14.0
NS
5.2-13.9
60.0
57.8
0.1
0.1
37.0
NS
NS
8.0
34.0
10-190
NS
NS
NS
50.0
NS
NS
NS
NS
NS
NS
NS
107
60.5
25.4
U.S.
EPA
Data
No. 6
08/28/02
NS
NS
251
NS
NS
NS
57.3
54.3
NS
NS
41.0
NS
NS
NS
NS
744
NS
120
NS
32.0
NS
NS
NS
NS
NS
<25
NS
104
60.0
24.6
Kinetico
Data
No. 6
NA
7.6
388
271
17.8
0.72
8.7
64.0
57.8
0.3 (as P)
NS
44.0
NS
NS
NS
NS
450
NS
NS
NS
50.0
NS
NS
NS
NS
NS
NS
NS
118
66.0
26.0
\Battelle Data
No. 6
08/21/03
7.4
381
233
16.0
1.0
NS
58.0
55.1
0.1
<1.0W
43.5
40.1
3.4
0.8
39.3
<30
<30
21
<10
1.6
0.5
36.2
35.1
9.7
9.2
0.1
O.I
97
55.0
23.1
No. 6-2004
07/13/04
7.4
379
240
12.0
0.6
14.0
53.0
57.4
0.1
2.2
49.7
39.9
9.8
1.0
39.0
268
<25
151
<10
28.3
18.0
34.0
33.7
6.2
6.6
0.1
O.I
114
51.3
27.2
04/17/07
NS
418
269
NS
NS
10.8
57.0
59.1
NS
1.6
48.5
NS
NS
NS
NS
<25
NS
NS
NS
12.5
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
(a) Sample collected on October 14, 2003.
NS = Not sampled
Nitrate. Nitrate concentrations in the new well were 14.0 mg/L (as N) on July 13, 2004, and 10.8 mg/L
(as N) on April 17, 2007, which were comparable to the levels over the higher end in the old well (Figure
4-1). As shown in the figure, nitrate concentrations in the old well increased from 5.2 mg/L in July 1986
to 13.9 mg/L in November 2001. According to the vendor, the A300E IX resin selected for Fruitland had
a similar run length for both arsenate and nitrate, thus maximizing system efficiency.
Sulfate. Sulfate concentrations in the new well were 53.0 mg/L on July 13, 2004, and 57.0 mg/L on April
17, 2007. These concentrations were slightly lower than those (from 57.3 to 64.0 mg/L) in the old well
(see Table 4-1). Because sulfate is more preferred by the A300E IX resin than arsenate and nitrate and
because of its higher concentrations, sulfate is a strong competing anion for arsenic and nitrate removal.
19
-------
t
2
w
o
16.0 -|
1 A n
1 9 n
10 0 -
6 0 -
4 0 -
2 0 -
Fruitland Nitrate Concentrations Over Time
(July 1986 through November 2001)
+ *
X* » +4* *
T%J * *
* *A * W% *
A, ,****
» * »
^
A A.
Date
Source: IDEQ
Figure 4-1. Historic Well No. 6 Nitrate Concentrations
Table 4-2. Historic Well No. 6 Heavy Metals and Fluoride Data
Analyte
Arsenic
Antimony
Barium
Beryllium
Cadmium
Chromium
Mercury
Nickel
Selenium
Sodium
Thallium
Fluoride
10/24/95
07/28/98
03/30/00
06/26/00
11/05/01
Concentration (mg/L)
0.046
0.005
0.05
0.0005
0.0005
0.002
0.0005
0.02
0.005
85.8
0.002
0.68
0.043
0.005
0.06
0.0005
0.0005
0.002
0.0002
0.02
0.005
67.7
0.002
0.68
0.034
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
0.032
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
0.039
0.005
0.06
0.0005
0.0005
0.002
0.0002
0.02
0.005
110
0.002
0.65
Source: IDEQ
NS = Not sampled
Other Water Quality Parameters. TDS concentration in source water was not measured, but estimated to
be 560 mg/L based on 114 mg/L sodium, 51.3 mg/L of calcium, 27.2 mg/L of magnesium, 379 mg/L of
bicarbonate, 12.0 mg/L of chloride, 0.6 mg/L of fluoride, 14.0 mg/L of nitrate, 53.0 mg/L of sulfate, and
57.4 mg/L silica after taking into account the loss of CO2 and H2O upon evaporation of Ca(HCO3)2 and
Mg(HCO3)2. This estimated TDS value agreed with the average TDS of 580 mg/L measured during the
performance evaluation study (see Table 4-13). Other dissolved ions present included 33.7 ug/L of
vanadium and 6.6 ug/L of molybdenum. The uranium concentration measured on December 6, 2000 was
20
-------
Table 4-3. Historic Well No. 6 Radiological Data
Sampling
Date
10/24/95
12/06/95
03/04/96
06/06/96
09/17/96
06/08/00
09/29/00
12/06/00
06/25/01
11/05/01
03/08/02
Radium
226
(pCi/L)
NS
0.0±0.2
O.OiO.l
0.0±0.2
0.1±0.2
NS
NS
NS
NS
NS
0.2
Uranium
(Hg/L)
NS
NS
NS
NS
NS
NS
NS
22.4
NS
NS
NS
Gross
Alpha
Activity
(pCi/L)
12.8±4.3
NS
NS
NS
NS
19.7
23.2
21.7
11.2
17.5
NS
Gross
Beta
Activity
(pCi/L)
6.3
NS
NS
NS
NS
6.6
13.9
13.4
14.3
15.1
NS
Source: IDEQ
NS = Not sampled; pCi/L = picoCuries per liter
22.4 ug/L (Table 4-3), lower than its MCL of 30 ug/L. Iron and aluminum were present primarily as
particulates; the dissolved species were below the respective detection limits. The pH value of raw water
was 7.4. Unlike adsorptive media, IX resins are not sensitive to water pH.
4.1.2 Distribution System and Treated Water Quality. The City of Fruitland has a looped
drinking water distribution system with water from multiple production wells entering the distribution
system at various locations. During the performance evaluation study, water produced from Wells No. 5,
9, and 10 was pumped into a reservoir, which was then connected to the distribution network. Water
from Wells No. 14 and 20 was blended prior to entering the distribution system. The distribution system
was constructed of asbestos cement pipe in the area of Well No. 6, but some sections in other areas of the
city were constructed of polyvinyl chloride (PVC) pipe. During periods in which production exceeded
demand, the excess was stored in one 1,000,000-gal ground level storage tank and one 200,000-gal
elevated storage tank. The well pumps were controlled by level sensors in the storage tanks.
Process water from the IX treatment system entered the distribution system via a 6-in-diameter line, from
which a branch line delivered water to a small area of homes receiving primarily Well No. 6-2004 water.
Service lines to these individual homes were mainly copper, while the lines within these homes were
constructed of galvanized iron, copper, and polyethylene. Three sampling locations were selected from
this area for the distribution system sampling (Section 3.3.4).
The City of Fruitland sampled water from the distribution system for several analytes. Four monthly
samples were collected from six locations for fecal coliform analysis. Samples also were taken for
asbestos analysis every three years. Under the EPA LCR, samples were collected from customer taps at
10 locations every three years.
4.2
Treatment Process Description
4.2.1 Ion Exchange Process. IX is a proven technology for removing arsenic and nitrate from
drinking water supplies (Clifford, 1999; Ghurye et al., 1999; and Wang et al., 2002). It is a
physical/chemical process that removes dissolved arsenate and nitrate ions from water by exchanging
them with chloride ions on anionic IX resins. Once its exchange capacity is exhausted, IX resins are
21
-------
regenerated with a brine solution containing high concentrations of chloride ions to displace the arsenate
and nitrate ions. Strong-base anionic (SBA) exchange resins are commonly used for arsenate and nitrate
removal. Resin capacity is not sensitive to water pH (in the range of 6.5 to 9.0). An SBA exchange resin
tends to have a higher affinity for more highly charged anions, resulting in a general hierarchy of
selectivity as follows:
SO2 >HAsO2
4 4
>NO >NO
>HAsO ,HCO
2 4 3
» Si(OH) ; H AsO
^ V 3 4
Because sulfate is more preferred over arsenic and nitrate and because its concentrations are at least three
orders of magnitude higher than those of arsenic, it is a key competing anion to arsenic and nitrate
removal by the IX process. High TDS levels also can significantly reduce arsenic and nitrate removal
efficiencies. In general, the IX process is not economically attractive if source water contains >500 mg/L
of TDS and >150 mg/L of sulfate. Also, particulates in feed water can potentially foul the SBA IX resin,
and must be removed by bag filters upstream of an IX vessel.
The Fruitland IX system used Purolite A300E, a Type II SBA exchange resin in chloride form, to remove
arsenic and nitrate from source water. The resin is NSF International (NSF) Standard 61 approved for use
in drinking water treatment and its typical physical and chemical properties are presented in Table 4-4.
According to Purolite's computerized simulation on the Fruitland water, the A300E resin has a relatively
higher capacity for arsenic and nitrate than A520E, a nitrate-selective resin. As shown in Figure 4-2,
A300E reaches 10-mg/L nitrate (as N) and 10-ug/L arsenic breakthrough at approximately 700 and 880
BV, respectively (note that this simulation significantly over-predicts the actual resin run length, which
was less than 422 BV as discussed in Sections 4.4 and 4.5). Because nitrate breaks through before
arsenate, nitrate will determine the resin run length (Ghurye et al., 1999). Using Clifford's equilibrium
multi-component chromatography theory (EMCT) model, the run length to the 10-mg/L nitrate (as N)
breakthrough was estimated to be about 580 BV when using a type II SBA exchange resin (like A300E)
for the Fruitland Well No. 6-2004 water. The estimated run length was further refined to about 450 BV
after taking into consideration mass transfer (Clifford, 2006). This run length was close to the 350 to 422
BV actually experienced at the Fruitland, Idaho site.
Table 4-4. Typical Physical and Chemical Properties of Purolite A300E Resin
Property
Polymer Structure
Functional Groups
Physical Appearance
Ionic Form
Mesh Size Range (U.S. Standard Mesh) (Wet)
Uniformity Coefficient
Water Retention (%)
Swelling (%)
pH Limitations
Temperature Limitations (°F)
Chemical Resistance
Whole Clear Beads (%)
Shipping Weight (lb/ft3 or g/L)
Total Capacity (meq/mL or meq/g)
Values
Macroporous styrene-divinylbenzene
Quaternary ammonium: R(CH3)2(C2H4OH)N+
Clear spherical beads
Chloride
16 x 50 (+16 mesh <5%; -50 mesh <1%)
1.7 maximum
40-45
Salt -OH, 10%
None
185 (maximum)
Unaffected by dilute acids, alkalis, and most solvents
92 (minimum)
44 or 705 g/L
1.45-1.6 meq/mL minimum volumetric (wet);
meq/g minimum weight (dry)
3.5-3.7
Source: Purolite
22
-------
IX-SIM Removal of Arsenic(V) with A-300E
Kinetico - Fruitland, ID
CO
o
o
I
o
O
o
Q.
Q.
45
40
35
30
25
20
15
10
5
0
1— Sulfate
Nitrate
Arsenic(V)
virgin resin
/
/
lO O lO O lO
oo m co o
i- C\l CO
/
Z /
jf
_^— """ _^,>s
70
60
50
40
3D
?0
10
0
OU1OU1OU1OUOO
ooiocoooomcoooo
cOTj-mcocoi — oooo)
Bvs
>"
(/)
^f
Q.
Source: Purolite
Figure 4-2. Purolite A-300E Simulation
4.2.2 Treatment Process. The Fruitland IX system utilized the packed-bed IX technology to
remove arsenic and nitrate from source water. Figure 4-3 is a process schematic of the system. The
process equipment included one bank of five skid-mounted bag filters, two skid-mounted resin vessels,
one central control panel, one salt saturate system, one pre-wired brine transfer pump, one brine tank,
one air compressor, as well as associated valves, sample ports, pressure gauges, and flow
elements/controls. The IX system was fully automated and controlled by a central control panel that
consisted of a programmable logic controller (PLC), a touch screen operator-interface-panel (OIP), and a
data communication modem. The OIP allowed the operator to monitor system flowrate and volume
throughput since last regeneration, change system setpoints as needed, and check the status of alarms.
The modem allowed the vendor to remotely dial in for monitoring and troubleshooting purposes. All
pneumatic valves were constructed of PVC and all plumbing was Schedule 80 PVC solvent bonded.
Table 4-5 summarizes the design specifications of the IX system.
The major process steps and system components are presented as follows:
• Sediment Filtration. Prior to entering the FX resin vessels, raw water was filtered through a
bag filter assembly to remove well sediment, if any. The bag filter assembly consisted of five
parallel FSIXI00 polypropylene housing units, each lined with a 20-um filter bag. Filter
bags in the assembly were replaced when pressure gauges on the inlet and outlet of the
assembly indicated a head loss of over 6 lb/in2 (psi). Figure 4-4 presents a photograph of the
bag filter assembly.
• Ion Exchange. After passing through the bag filters, water flowed downward through two
48 in x 72 in pressure vessels configured in parallel. Mounted on a polyurethane coated,
welded steel frame, the pressure vessels were of fiber reinforced plastic (FRP) construction,
23
-------
I Flow |
—•—^- Backwash/Regen
Waste to Sewer
by Others
Treated Water to
Storage / Distribution
by Others
Figure 4-3. Process Schematic of Kinetico's IX-248-As/N Removal System
rated for 150 psi working pressure. Each vessel had a 6-in top and bottom flange and two 4-
in side flanges, and was equipped with a diffuser-style upper distributor and a hub and lateral-
style lower distributor. Each vessel was filled with 3 ft3 of flint gravel support media, 50 ft3
of A300E resin, and 3 ft3 of polypropylene filler beads on the top (to prevent resin from being
washed away in an upflow, counter-current regeneration). The IX system was designed for a
flowrate of 250 gpm, yielding a hydraulic loading rate of 10 gpm/ ft2 and an empty bed
contact time (EBCT) of 3 min. Each IX resin vessel was equipped with a 125-gpm flow-
limiting device to prevent overrun. However, these devices were removed later because they
overly restricted the flow through the IX system.
An insertion-type paddle wheel flow element was installed on the combined effluent line to
register flowrate and volume throughput of the IX system since last regeneration. When a
pre-determined throughput setpoint was reached, Vessel A was automatically taken out of
service for regeneration, whereas Vessel B remained on the line for treatment. The amount of
water treated by Vessel B at this time would not be registered on the totalizer during Vessel A
regeneration. Once Vessel A regeneration was complete, the totalizer was automatically reset
to zero and began to register the amount of water treated by Vessel A. Meanwhile, Vessel B
was taken out of service for regeneration. After Vessel B regeneration was complete, the
totalizer registered the amount of water treated by both vessels. Figure 4-5 presents a
photograph of the FX system at Fruitland. Figure 4-6 provides a close-up view of sampling
taps, pressure gauges, and valves.
24
-------
Table 4-5. Design Specifications of IX System
Parameter
Value
Remarks
Pretreatment-Bag Filter Assembly
Bag Filter Size (in)
Number of Bag Filters
Configuration
Nominal Pore Size (urn)
6x20
5
Parallel
20
-
-
-
-
IX Vessels and Media Beds
Vessel Size (in)
Cross-Sectional Area (ft2/vessel)
Number of Vessels
Configuration
IX Resin Quantity (ft3/vessel)
Bed Depth (in)
Resin Type
Flint Gravel Support Media (ft3/vessel)
Polypropylene Filler Beads (ft3/vessel)
48 D x 72 H
12.6
2
Parallel
50
48
Purolite A300E
3
3
-
-
-
-
Total of 100 ft3 for two vessels
-
-
12-in bed depth
12-in bed depth
Service
System Design Flowrate (gpm)
Hydraulic Loading (gpm/ft2)
EBCT (min)
Estimated Working Capacity (BV)
Volume Throughput (gal)
250
10
3.0
400-500
299,200-374,000
125 gpm/vessel
-
Based on design flowrate
-
!BV=100ft3=748gal
Regeneration
Regeneration Mode
Regeneration Level (Ib of salt/ft3 of resin)
Brine Draw Duration (min)
Brine Draw Flowrate (gpm)
Slow Rinse Duration (min)
Slow Rinse Flowrate (gpm)
Fast Rinse Duration (min)
Fast Rinse Flowrate (gpm)
Wastewater Production (gal)
Salt Consumption (Ib/regeneration)
Co-current
10
64
23
64
23
30
75
3,500 to 5,250
500 (per vessel)
Downflow
-
Based on 4% brine
Based on 4% brine
-
-
-
-
-
1,000 Ib (total)
Brine System
Brine Day Tank Size (in)
Brine Day Tank Material
Brine Transfer Pump Size
Salt Saturator Size (in)
Salt Saturator Material
61Dx64H
HOPE
!/2hp
96 D x 180 H (original)
96 D x 148 H
(shortened)
Fiberglass
Capacity = 685 gal
-
-
Saturator shortened by 32 in
(straight height) to fit to building;
corresponding capacity reduced
from 15 to 12.3 ton
-
Post- Treatment
None
D = diameter; H = height.
25
-------
Figure 4-4. 20-um Bag Filter Assembly
Figure 4-5. Ion Exchange System at Fruitland, ID
26
-------
Figure 4-6. Sampling Taps, Pressure Gauges, and Valves
• Resin Regeneration. Regeneration can be initiated automatically based on a throughput
setpoint or manually by pressing a push-button on the PLC. Once regeneration was initiated,
the PLC controlled the sequence of three regeneration steps, i.e., brine draw, slow rinse, and
fast rinse. To achieve a regeneration level of 10 Ib NaCl/ft3 of resin, the original design
called for 64 min of brine draw at 23 gpm using a 4% brine solution. During the study, the
regeneration scheme was adjusted several times to optimize the regeneration efficiency,
reduce waste production, and minimize arsenic and nitrate leakage (Section 4.4.2). In doing
so, the duration of each regeneration step was reset on the PLC; the brine concentration was
adjusted using a hand valve located upstream of the eductor to change the brine draw rate;
and a hydrometer was used to measure the specific gravity of the brine solution to confirm its
concentration.
Brine was drawn from a brine day tank (Figure 4-7) into the resin vessels via a Venturi
eductor. The brine day tank was equipped with high/low level sensors interlocked with a
brine transfer pump to fill the tank with saturated brine (about 23 to 26%) from a 15-ton salt
saturator. The salt saturator was sized to hold 30 days of salt supply for daily regeneration
and was re-filled by a salt delivery truck on a weekly or as-needed basis (Figure 4-8).
Treated water was used to make the brine solution and rinse the beds. Wastewater produced
was discharged to a floor drain and a 6-in drain line to a lift station outside of the building.
Wastewater was then pumped to a city sewer.
The system was designed to regenerate in either a co-current or counter-current mode. The
vendor decided to use downflow, co-current regeneration, which was thought to be superior
to upflow, counter-current regeneration for arsenic and nitrate. Upflow regeneration would
27
-------
Figure 4-7. Photograph of Brine System
Figure 4-8. Salt Delivery to Fill Salt Saturator
28
-------
4.3
force the contaminants concentrated at the bottom of the IX resin beds back through the entire
resin beds, thus leaving more contaminants in the IX resin beds. Clifford et al. (1987, 2003)
recommended co-current downflow regeneration for arsenic removal because it was easier to
implement. For nitrate removal, co-current "complete" regeneration (i.e., removing over
95% of exchanged nitrate) is recommended only when bypass blending is allowed, which
was not the case in Fruitland. Due to the arsenic/nitrate leakage problems detected at
Fruitland, the co-current regeneration was converted to upflow counter-current regeneration
during the period from July 25, 2006 to May 18, 2007. A series of mechanical problems
occurred, however, under the counter-current regeneration mode (Section 4.4.3.2). The
system was switched back to downflow, co-current regeneration mode after May 18, 2007.
System Installation
From the time the system was installed in March 2004 through June 2005, a series of events took place
that seriously delayed the startup of the demonstration study. The events included the production of
excessive sediment from the old well (Well No. 6), installation of a replacement well, repeated failures of
bacterial testing, replacement of the IX resin already loaded in the IX vessels, and replacement of a well
pump. These events are discussed in detail in the following sections.
4.3.1 Building Construction. The City of Fruitland constructed an addition to the existing pump
house for the IX system. The 17-ft tall addition covered 360 ft3 of floor space and had a wood frame,
steel siding and roofing, and a roll-up door. The total cost was approximately $18,000. The building
construction began on February 6, 2004, when the concrete pad was poured. Construction of the wood
frame began on February 10, 2004, and the building was completed (with the exception of the electrical
and the final siding) on March 3, 2004. Figure 4-9 shows a photograph of the new structure, adjacent to
the existing well house.
Figure 4-9. New Addition to Old Well House
4.3.2 Installation of Replacement Well. After the IX system was delivered to the treatment
building on March 8, 2004, system installation began immediately. The installation was nearly complete
29
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when excessive accumulation of sediment was noted in the bag filters and the empty IX resin vessels (as
much as 3 in) during a hydraulic test on March 25 and 26, 2004. As a result, loading of the IX resin was
put off to allow the facility to examine the sand production problem. The city performed an investigation
of Well No. 6 from April 1 through 13, 2004, including an initial video surveying, cleaning, bailing, and
pumping, and final video surveying. The investigation revealed the presence of two holes in the well
casing, with each hole having an associated void in the adjacent sand pack. On April 13, 2004, the city
council voted to replace Well No. 6 with a new well on the same lot, located approximately 25 ft from the
existing well.
The initial design for Well No. 6-2004 called for a 12-in-diameter steel casing completed to 95 ft bgs,
with a screened interval from 50 to 70 ft bgs. Installation of the replacement well commenced on May 5,
2004, after the well location had been approved by IDEQ and a well drilling permit had been issued by
the Idaho Department of Water Resources. Well installation continued through May 26, when well
development and pump testing indicated that the well was unable to produce an adequate supply of water,
presumably caused by the shorter screen interval installed. On May 28, the city council voted to increase
well depth to 120 bgs with two additional screened sections extending from 95 to 105 ft bgs and from 110
to 120 ft bgs (see Section 4.1). Modifications to Well No. 6-2004 were completed in July 2004, and
water samples were collected for coliform tests. The first water sample tested positive for coliform,
requiring another chlorine shock and a second round of coliform sampling. Following the second
chlorine shock and a negative coliform test result, the vendor proceeded with the loading of the IX resin
in the vessels on July 23, 2004, and the shakedown/startup and operator training activities were scheduled
for July 28, 2004.
4.3.3 Permitting. Engineering plans for the system permit application were prepared by Holladay
Engineering, a Kinetico subcontractor (also serving as the engineer for the city) located in Payette, Idaho.
The plans included general arrangement diagrams, specifications of the IX system, and drawings detailing
the connections of the new unit to the existing facility and new building. After incorporating comments
from the vendor and Battelle, the plans were submitted on January 25, 2004, by the city to IDEQ for
review and approval. Review comments provided by IDEQ on February 25, 2004, were addressed by the
city and Holladay Engineering within a week. On May 10, 2004, IDEQ sent an e-mail stating that the
submittal for the demonstration was generally acceptable, and that the project was approved to proceed
once the new well was installed.
4.3.4 System Installation, Shakedown, and Startup. The IX system was delivered to the site on
March 8, 2004. Mechanical Installation, Inc., a subcontractor to Kinetico, performed the off-
loading and installation of the system, including connections to the existing entry and distribution piping
(Figure 4-10). Because the salt saturator had the same height, i.e., 17 ft, as the building, it had to be
shortened before it could be brought into the building. As such, the top section of the fiberglass vessel
was cut off and a 32-in long section of the straight shell was removed. After the shortened vessel was
brought into the building, the top section was placed back and soldered on March 18, 2004 (Figure 4-11).
Following the installation of the replacement well, the vendor proceeded with the loading of the IX resin
in the vessels on July 23, 2004. Battelle staff arrived at Fruitland on July 28, 2004, to provide data and
sample collection training to the operator. The vendor engineer also was onsite to install a new touch
screen on the control panel. However, the city learned on the same day that the latest sample taken from
the system had failed the bacterial test and that the system would require further sanitation. This was
complicated by the fact that the IX resin had already been loaded into the vessels and that the resin could
not be exposed to any chlorine treatment. The city re-shocked the well with chlorine and bypassed the IX
system by pumping water to the ground. Battelle and Kinetico proceeded with the operator training as
scheduled and left the site on July 29, 2004.
30
-------
Figure 4-10. Equipment Offloading
Figure 4-11. Cutting and Soldering a Salt Saturator
31
-------
Immediately following the completion of operator training, the city began a series of activities involving
chlorine shock, pumping, and sampling for Well No. 6-2004. The city administered multiple cycles of
chlorine treatment, but samples taken continued to test positively for coliform. The well driller
remobilized to the site in December 2004 to redevelop the well, clean the screens, and disinfect the pump
and the well. However, intermittent positive coliform results continued after the redevelopment effort. In
light of the positive coliform data, IDEQ agreed to a post-chlorination system at Well No. 6-2004 for the
period of the demonstration. However, chlorination was not desired by the city due to concerns over taste
and odor and resistance from a local beverage bottling facility.
The city continued to chlorine-shock and pump the well from December 2004 through April 2005, but
intermittent positive results for coliform persisted during this period. To allow water to enter the
distribution system, the city contemplated several pre- and/or post-treatment options, including
prechlorination (upstream of the IX system), postchlorination (prior to entering the distribution system),
and ultraviolet (UV) treatment. Before any of these treatment options was implemented, the city
collected water samples from the outlet of the IX resin vessels in March 2005, and the results were
negative for coliform. The vendor, therefore, determined that a specialized sanitization method most
likely would not be needed for treating the IX resin and that a brine solution would be sufficient to
intoxicate/kill coliform if they were actually present in the IX system.
In April 2005, samples collected at the IX system effluent during a short test run (while the treated water
was discharging to the ground) indicated that arsenic breakthrough had already occurred. Examination of
relevant information led the vendor to conclude that a nitrate-specific resin, A-520E (also manufactured
by Purolite), had been erroneously delivered to the site and loaded into the IX vessels. A vendor
technician arrived onsite on April 20, 2005, to remove A-520E resin and load A300E resin into the
vessels. After resin replacement and upon IDEQ's request, water samples were collected from the
wellhead and the system effluent for a bacterial test, which showed negative coliform results. The sample
results were submitted to IDEQ on May 4, 2005.
Meanwhile, it was discovered that the pump in Well No. 6-2004, which had been salvaged from the
original well, Well No. 6, was out of order and had to be replaced. The new pump was installed on May
19, 2005, and was disinfected and began pumping to waste on May 20, 2005. Samples collected on May
23 and 24, 2005, indicated the absence of coliform. Holladay Engineering sent a letter to IDEQ on June
1, 2005, reporting the negative coliform results and requesting permission to send the treated water to the
distribution system. IDEQ provided an approval in an e-mail dated June 7, 2005. As such, the
performance evaluation study officially began on June 14, 2005. After Battelle reviewed the data and
sample collection procedures with the operator via telephone, the first set of samples was collected from
the IX system on June 15, 2005.
4.4 System Operation
The 32-month demonstration study (from June 14, 2005, through February 11, 2008) can be divided into
three study periods. Study Period I, extending from June 14, 2005 through July 25, 2006, focused on
treatment system performance evaluation as the system was set in the co-current regeneration mode. The
activities carried out in Study Period II, extending from July 25, 2006, through June 18, 2007, involved
solving various mechanical problems encountered when efforts were made to convert IX resin
regeneration from the co-current to counter-current mode (Section 4.4.3.2). The conversion efforts were
made as an attempt to address issues relating to arsenic and nitrate leakage after regeneration. In spite of
repeated trials, these efforts were not successful and the system was reverted back to the co-current
regeneration mode. Improper IX resin regeneration during this period was thought to have resulted in
resin fouling due to the presence of dissolved organic matter in source water (Section 4.4.3.2).
Deteriorating resin performance as reflected by shorter system run lengths prompted efforts to clean the
32
-------
fouled IX resin in Study Period III starting on June 18, 2007 and ending on February 11, 2008. After the
fouled IX resin was washed with a caustic/brine solution, the performance evaluation sampling was
resumed for a short period. Appendix A chronologically summarizes all operational issues and corrective
actions taken during the 32-month demonstration study. Table 4-6 provides an overview of key
demonstration study activities throughout the study period.
Table 4-6. Key Demonstration Study Activities and Start/Complete Dates
Demonstration Study Activities
Study Period I. Evaluation of IX System Performance with Co-
current Regeneration Mode
• Run Length Study 1
• Elution Study 1
• Run Length Study 2
• Elution Study 2
• Run Length Study 3
• Run Length Study 4
Study Period II. Conversion from Co- to Counter-current
Regeneration Mode
• Run Length Study 5
• Run Length Study 6
• Meeting with Kinetico and EPA in Columbus, OH
• Installation of ArsenicGuard
Study Period III. Caustic/Brine IX Resin Cleaning Followed with
Short Performance Evaluation
• Caustic/Brine IX Resin Cleaning
• Performance Evaluation with Co-current Regeneration Mode
• Reduced Daily Run Time
• Equipment Transfer Letter Signed by City Council
Date
06/14/05-07/25/06
07/28-30/05
07/30/05
08/16-17/05
09/22/05
12/07-08/05
04/11-12/06
07/25/06 to 06/18/07
08/09-10/06
01/16-17/07
02/07/07
05/07/07
06/18/07-02/11/08
06/18-21/07
06/21/07-01/25/08
09/2007-02/11/08
02/11/08
(a) Operating time reduced to 3 hr/day due to concern over high salt content in regeneration
waste discharge, which might have caused stress to duckweeds in city's sewage lagoons.
4.4.1 Operational Parameters. Operational data were collected during weekdays from June 14,
2005, through July 25, 2006 (Study Period I), and are attached as Appendix B after tabulation. After July
25, 2006, the demonstration study focused primarily on solving mechanical problems associated with
conversion of system regeneration from the co- to counter-current mode and on addressing IX resin
fouling issues. Therefore, the treatment system operated only periodically and operational data were
recorded only on an as-needed basis.
Table 4-7 summarizes key operational parameters collected during Study Period I. Based on well pump
hour meter readings, the IX system operated for a total of 6,836 hr in 392 days, resulting in an average
daily operating time of 17.4 hr. Well No. 6-2004 operated longer between June and September, i.e., 22
hr/day (on average), compared to 13 hr/day between December and March. The throughput during the
study period was 65,400,000 gal based on wellhead totalizer readings. The average daily demand was
166,895 gpd; the peak daily demand was 255,000 gpd, which occurred on September 14, 2005.
The IX system was equipped with an insertion paddle wheel flow meter/totalizer on the product water
discharge line to monitor the combined flow from both IX vessels. During the first week of system
operation, flowrates from both IX vessels ranged from 130 to 144 gpm (except for the 73 gpm on June
33
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Table 4-7. Summary of System Operational Data During Study Period I
Parameter
Demonstration Study Period I
Total Operating Time (hr)
Total Operating Days (day)
Average Daily Operating Time (hr/day)
Throughput to Distribution (gal)
Average Daily Use (gpd)
Peak Daily Use (gpd)
Number of Regeneration Cycles
Service Flowrate (gpm)
Empty Bed Contact Time (min)
Hydraulic Loading to Each Resin Vessel (gpm/ft2)
Pressure Loss Across Each Resin Vessel (psi)
Pressure Loss Across Entire System (psi)
Value
June 14, 2005 to July 25, 2006(a)
6,836
392
17.4
65,423,000(b)
166,895
255,000
202W
126-179(d) (average 157)
4.2-5.9 (average 4.8)
5.0-7.1 (average 6.2)
4-13w
8-18w
(a) System regeneration in co-current mode.
(b) Based on wellhead totalizer readings.
(c) Including 35, 31, 39, 33, and 64 regeneration cycles at initial regeneration setting
and four subsequently modified settings, respectively (Section 4.4.2.1).
(d) Excluding lower flowrates during system regeneration and before flow restrictors
were removed on July 7, 2005.
(e) Not include data during system regeneration (pressure loss could increase up to
20 psi during regeneration of one vessel).
(f) Not include data during system regeneration (pressure loss could increase up to
26 psi during regeneration of one vessel).
16, 2005, when one IX vessel was regenerating), which was 28% to 35% lower than the 200-gpm well
capacity and 42% to 48% lower than the 250-gpm system design flowrate. Meanwhile, the pressure drop
(Ap) across the system also was elevated, with values ranging from 20 to 30 psi (excluding the 42 psi on
June 16, 2005, when one IX vessel was regenerating). It was determined that the 100-gpm flow
restrictors at the outlet side of the IX vessels had overly restricted the flow, causing the unexpectedly low
flowrates. The flow restrictors were modified on June 21, 2005, with a wider opening, which resulted in a
higher flowrate of 170 gpm and a lower Ap of 6 psi. The flow restrictors were later removed on July 7,
2005, but the removal did not appear to further increase system flowrates. Since then, product water
flowrates ranged from 126 to 179 gpm and averaged 157 gpm; system Ap readings ranged from 8 to 18
psi and averaged 11 psi (excluding those recorded during regeneration). Based on this average flowrate,
the IX system had been operating at an average hydraulic loading rate of 6.2 gpm/ft2 (compared to the
design value of 10 gpm/ft2) and an average EBCT of 4.8 min (compared to the design value of 3 min).
As noted above, when one IX vessel was being regenerated, the second IX vessel continued to be in
service. Under the circumstances, service flowrates through one IX vessel increased to 109 to 145 gpm,
which were significantly higher than those (i.e., 63 to 89.5 gpm/vessel) when both IX vessels were in
service. Also, some service flowrates had exceeded the design value of 125 gpm most likely due to the
removal of the flow restrictor. This flowrate range represents a hydraulic loading rate of 8.7 to 11.5
gpm/ft2 and an EBCT of 3.4 to 2.6 min. The pressure drop across the vessel in service also could spike to
21 psi during regeneration.
4.4.2 Regeneration. The system PLC automatically initiated a regeneration cycle based on a
throughput setpoint. The duration of each regeneration step, e.g., brine draw, slow rinse, and fast rinse,
was controlled by a timer in the PLC. During Study Period I, a total of 202 regeneration cycles took
place. The treatment system operated sporadically during Study Periods II and III; therefore, the number
34
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of regeneration cycles that took place was not tracked. Table 4-8 summarizes the regeneration settings set
during the entire performance evaluation study.
4.4.2.1 Regeneration Settings. As shown in Table 4-8, during June 14 through July 26, 2005, IX
system regeneration was triggered based on a factory throughput setpoint of 214,000 gal. A 4% brine
solution was used to regenerate the IX resin at 23 gpm for 64 min to achieve a target regeneration level of
10 Ib of salt/ft3 of resin. Based on the results of arsenic/nitrate breakthrough and resin run length studies
(see Section 4.5.2), regeneration settings were modified four times during Study Period I. On July 30,
2005, a Kinetico technician was onsite to change the brine concentration from 4% to 8%, the brine draw
time from 64 to 32 min, and the throughput setpoint from 214,000 to 335,000 gal based on field arsenic
and nitrate measurements. On September 19, 2005, the operator was given the instructions to reduce the
throughput setpoint from 335,000 to 316,000 gal and the fast rinse time from 30 to 6 min based on the
results of an arsenic/nitrate run length study conducted on August 16 and 17, 2005 (Run Length Study 2).
On December 5, 2005, the brine draw time was reduced again from 32 to 25 min, slow rinse time reduced
from 64 to 40 min, and fast rinse time increased from 6 to 15 min. On March 5, 2006, the brine
concentration was reduced from 8% to 6%. By this time, the averaged regeneration level achieved was
9.5 lb/ft3, very close to the design value of 10 lb/ft3.
Upon completion of Study Period I, the IX system was converted from the co- to counter-current
regeneration mode beginning on July 25, 2006, as an attempt to address the arsenic and nitrate leakage
issues. On March 14, 2007, the throughput setpoint was further reduced from 316,000 to 275,000 gal due
to shorter run lengths experienced during February 1 and 7, 2007 (Appendix A). The attempt to convert
to the counter-current regeneration mode was unsuccessful and the regeneration flow direction was
reverted back to co-current after caustic/brine resin cleaning on June 21, 2007. On July 7 and October 16,
2007, throughput setpoints were further reduced to 260,000 and 220,000 gal, respectively, based on even
shorter run lengths observed for arsenic and nitrate. Rationales of these setting modifications are further
discussed in Sections 4.4.3 and 4.5.2.
4.4.2.2 Regeneration Parameters. Regeneration parameters were monitored on 13 occasions during
Study Period I (from June 14, 2005, to July 25, 2006). Table 4-9 summarizes the monitoring results. The
volume of treated water used for each regeneration step was recorded via a totalizer installed upstream of
the Venturi eductor and was used to calculate the average flowrate of each step. Brine usage was
recorded from the 685-gal brine day tank with 50-gal graduations. The volume of brine draw (i.e., diluted
brine) was calculated using Equation 1:
'brine, d f }'brine, s * brine, s ~^~ 'water/ / }'brine, d \*)
where:
Vbrine, d= volume of diluted brine (gal)
Vbrine, s = volume of saturated brine (gal)
Vwater, s= volume of water used (gal)
Vbrine, s = specific gravity of saturated brine, i.e., 1.160 for 21% brine
Vbrine, d= specific gravity of diluted brine, i.e., 1.061 for 8% brine.
As shown in Table 4-9, 350 to 375 gal, 250 to 325 gal, and 200 to 325 gal of saturated brine was used to
regenerate each vessel under Regeneration Settings 2, 3, and 4, respectively. The average brine draw
flowrate under Regeneration Setting 2 was 36 gpm, which is approximately 56% higher than the design
value of 23 gpm (see Tables 4-5 and 4-8). This higher flowrate resulted in higher salt consumption as
discussed in Section 4.4.3. Average brine draw flowrates under Regeneration Settings 3 and 4 were 37
and 43 gpm, respectively, which were even higher than the average brine draw flowrate under
Regeneration Setting 2.
35
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Table 4-8. IX System Regeneration Settings at Fruitland, ID
Parameter
Operational Duration
Regeneration Mode (co-
or counter)
Run Length Setting (gal)
Run Length Setting (BV)
Regeneration Interval (hr)
Brine Concentration (%)
Brine Draw Time (min)
Slow Rinse Time (min)
Fast Rinse Time (min)
Total Regeneration Time
(min)
No. of Regeneration
Cycles
Salt Delivered (Ib)
Average Salt Usage
(lb/cycle)(a)
Average Regeneration
Level (Ib/ft3)(b)
Period I
Initial
Setting
06/14/05-
07/30/05
Co
214,000
286
22
4
64w
64
30
158
33
37,260(d)
1,129
11.3
Setting
1
07/30/05-
09/19/05
Co
335,000
448
34
8
32(o)
64
30
126
33
55,295(e)
1,675
16.8
Setting
2
09/19/05-
12/05/05
Co
316,000
422
32
8
32W
64
6
102
39
67,705(f)
1,736
17.4
Setting
3
12/05/05-
03/05/06
Co
316,000
422
32
8
25W
40
15
80
35
52,855fe)
1,510
15.1
Setting
4
03/05/06-
07/25/06
Co
316,000
422
32
6
25(c>
40
15
80
62
58,525(h)
945
9.5
Period II(b)
Setting
5
07/25/06-
03/14/07
Counter
316,000
422
32
6
25
40
15
80
_w
_(i)
_w
_(l)
Setting
6
03/14/07-
06/18/07
Counter
275,000
368
32
6
25
40
15
80
_w
_(i)
_w
_(l)
Period III(b)
Setting
7
06/18/07-
07/07/07
Co
275,000
368
32
6
25
40
15
80
_w
_(i)
_(i)
_(i)
Setting
8
07/07/07-
10/16/07
Co
260,000
348
32
6
25
40
15
80
.«
_(i)
_(i)
.«
Setting
9
10/16/07-
02/11/08
Co
220,000
294
32
6
25
40
15
80
_w
(i)
_(i)
_(i)
(a)
Calculated by dividing total amounts of salt delivered by number of regeneration cycles, assuming same salt storage levels in saturator at beginning and end
of each operational period; theoretical salt usage was 1,000 Ib/regeneration.
(b) Calculated based on 100 ft3 of resin in two vessels; design value was 10 lb/ft3.
With a constant brine draw flowrate of 23 gpm.
Delivered in 6 shipments with quantities varying from 3,945 to 9,035 Ib per shipment.
Delivered in 9 shipments with quantities varying from 3,205 to 8,970 Ib per shipment.
Delivered in 11 shipments with quantities varying from 5,955 to 7,240 Ib per shipment.
(g) Delivered in 11 shipments with quantities varying from 1,880 to 8,020 Ib per shipment.
(h) Delivered in 11 shipments with quantities varying from 1,320 to 8,755 Ib per shipment.
(i) Routine operational data not collected after 07/25/06.
(c)
(d)
(e)
(f)
-------
Table 4-9. IX System Regeneration Parameters Collected During Study Period I
Date
09/22/05
11/10/05
11/15/05
01/11/06
02/15/06
04/04/06
04/13/06
05/09/06
05/31/06
06/07/06
06/22/06
07/06/06
07/17/06
Regen
Setting
Setting
2
Setting
3
Setting
4
Tank
Being
Regen'd
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
A
B
Total
Brine Draw 1
Brine
Used
in
Day
Tank
(gal)
360
NA
NA
350
350
700
375
375
750
325
325
650
250
250
500
325
325
650
225
210
435
210
200
410
210
200
410
200
200
400
200
200
400
200
200
400
200
200
400
Treated
Water
Used for
Brine
Draw
(gal)
802
1.340M
l,604(b)
800
800
1,600
900
700
1,600
600
700
1,300
650
650
1,300
900
900
1,800
800
800
1,600
900
800
1,700
875
875
1,750
875
875
1,750
875
875
1,750
875
875
1,750
875
875
1,750
Brine
Draw
Volume
(gal)M
1,149
NA
2,29900
1,137
1,137
2,274
1,258
1,070
2,328
920
1,014
1,934
885
885
1,770
1,222
1,221
2,443
1,016
1,002
2,018
1,098
990
2,088
1,075
1,062
2,137
1,064
1,064
2,129
1,064
1,064
2,129
1,065
1,066
2,132
1,065
1,069
2,134
Brine
Draw
Time
(min)
32
32
64
32
32
64
32
32
64
25
25
50
25
25
50
25
25
50
25
25
50
25
25
50
25
25
50
25
25
50
25
25
50
25
25
50
25
25
50
Brine
Draw
Flowrate
(gpm)
36
NA
36W
36
36
36
39
34
37
37
41
39
35
35
35
49
49
49
41
40
40
44
40
42
43
42
43
43
43
43
43
43
43
43
43
43
43
43
43
8
0=
£o
Slow
Rinse
Volume
(gal)
1,519
1,542
3,061
1,900
1,600
3,500
1,900
1,600
3,500
1,000
1,200
2,200
1,040
1,040
2,080
1,400
1,400
2,800
1,400
1,500
2,900
1,440
1,440
2,880
1,440
1,440
2,880
1,440
1,440
2,880
1,440
1,440
2,880
1,440
1,440
2,880
1,440
1,440
2,880
Slow
Rinse
Time
(min)
64
64
128
64
64
128
64
64
128
40
40
80
40
40
80
40
40
80
40
40
80
40
40
80
40
40
80
40
40
80
40
40
80
40
40
80
40
40
80
Slow
Rinse
Flowrate
(gpm)
24
24
24
30
25
27
30
25
27
25
30
28
26
26
26
35
35
35
35
38
36
36
36
36
36
36
36
36
36
36
36
36
36
36
36
36
36
36
36
Fast Rinse 1
Fast
Rinse
Volume
(gal)
383
359
742
300
400
700
400
400
800
1,110
1,110
2,220
1,110
1,110
2,220
1,000
900
1,900
1,000
1,000
2,000
1,050
1,050
2,100
1,050
1,050
2,100
1,050
1,050
2,100
1,050
1,050
2,100
1,050
1,050
2,100
1,050
1,050
2,100
Fast
Rinse
Time
(min)
6
6
12
6
6
12
6
6
12
15
15
30
15
15
30
15
15
30
15
15
30
15
15
30
15
15
30
15
15
30
15
15
30
15
15
30
15
15
30
Fast
Rinse
Flowrate
(gpm)
64
60
62
50
67
58
67
67
67
74
74
74
74
74
74
67
60
63
67
67
67
70
70
70
70
70
70
70
70
70
70
70
70
70
70
70
70
70
70
Total Waste Production per Regeneration Cycle
Total
Waste
Generated
(gal)
6,100
6,500
6,650
6,354
6,070
7,143
6,918
7,068
7,117
7,109
7,109
7,112
7,114
Total
Waste
Produc
-tion
(BV)
16
17
18
17
16
19
18
19
19
19
19
19
19
Regen
Setpoint
(BV)
422
422
422
422
422
422
422
422
422
422
422
422
422
Water
Produc
-tion
Eff.
(%)
96.2
96
95.7
96
96.2
95.5
95.6
95.5
95.5
95.5
95.5
95.5
95.5
(a) Including an unknown amount of water that went into salt saturator.
(b) Assuming TB consumed same amount of brine and water as TA.
(c) Calculated using Equation 1 .
-------
Average slow rinse flowrates under Regeneration Settings 2 and 3 were 26 and 27 gpm, respectively, just
over the designed value of 23 gpm (see Table 4-5). Slow rinse flowrates under Regeneration Setting 4
averaged 36 gpm, significantly higher than the designed value. Average fast rinse flowrates under
Regeneration Settings 2, 3, and 4 were 62, 74, and 69 gpm, respectively, lower than the design value of
75 gpm. Each regeneration cycle produced 6,100 to 7,140 gal of wastewater, equivalent to 16 to 19 BV.
At a regeneration setpoint of 316,000 gal (or 422 BV), the water production efficiency was 96%.
4.4.2.3 Salt Usage. The amount of salt used by each regeneration cycle was calculated based on the
concentration and volumes of saturated and diluted brine solutions, respectively, according to Equation 2.
The results are presented in Table 4-10.
WsaU = Vbnm x ybme x dwater x Csah (2)
where:
Wsalt = weight of salt (Ib)
Vbrine = volume of brine (gal)
Jbrine = specific gravity of brine
db,ine = density of water, e.g., 8.34 (Ib/gal)
Csait= percent of salt (%).
The specific gravity of the saturated brine measured with a hydrometer on September 22, 2005, was 1.16,
corresponding to 21% of NaCl, which was lower than the ideal salt saturation level of 23 to 25%.
Specific gravities of diluted brine solutions measured ranged from 1.061 to 1.062 for Regeneration
Settings 2 and 3, and from 1.038 to 1.046 for Regeneration Setting 4, corresponding to 8% and 6% of
NaCl, respectively, as expected. Using the ideal salt saturation level for calculations, it yielded amounts
of salt usage (by weight) similar to those based on diluted brine solutions, as shown in Table 4-10.
Averaged amounts of salt usage under Regeneration Setting 2 were 1,647 and 1,628 Ib based on saturated
and 8% brine, respectively, which was over 60% higher than the design value of 1,000 Ib (derived from
10 Ib of salt/ft3 of IX resin and 100 ft3 of IX resin in the system). Adjustments made to regeneration
settings reduced amounts of salt usage to 1,297 and 1,312 Ib (based on saturated and 8% brine,
respectively) under Regeneration Setting 3, and then to 986 and 1,098 Ib (based on saturated and 6%
brine, respectively) under Regeneration Setting 4.
Amounts of salt usage also were estimated based on amounts of salt delivered and the number of
regeneration cycles taking place over the respective study periods. In doing so, it was assumed that the
same level of salt was maintained in the salt saturator at both the beginning and end of the study periods.
As presented in Tables 4-8 and 4-10, average salt usage based the amounts delivered increased from
1,129 Ib under the initial regeneration setting to 1,675 and 1,736 Ib under Regeneration Settings 1 and 2,
respectively, and then decreased to 1,510 and 945 Ib under Regeneration Settings 3 and 4, respectively.
Divided by 100 ft3 of IX resin in the system, these amounts corresponded to the regeneration levels of
11.3, 16.8, 17.4, 15.1, and 9.5 lb/ft3. The salt regeneration level was only 13% higher than the design
value of 10 lb/ft3 during and soon after system startup, but became 67%, 74%, and 51% higher through a
number of regeneration setting modifications. Under Regeneration Setting 4, the regeneration level based
on the amount salt delivered was within 5% of the target value of 10 lb/ft3.
38
-------
Table 4-10. IX System Salt Usage Calculations
Date
09/22/05
10/25/05
11/10/05
11/15/05
Based on Saturated Brine
Volume
of
saturated
brine
(gal)
720
750
700
750
Specific
gravity'3'
1.176
1.176
1.176
1.176
Percent
of salt
(%)
23
23
23
23
Average Under Regeneration Setting 2
01/11/06
02/15/06
650
500
1.176
1.176
23
23
Average Under Regeneration Setting 3
04/04/06
04/13/06
05/09/06
05/31/06
06/07/06
06/22/06
07/06/06
07/17/06
650
425
410
410
400
400
400
400
1.176
1.176
1.176
1.176
1.176
1.176
1.176
1.176
23
23
23
23
23
23
23
23
Average Under Regeneration Setting 4
Salt
usage
(Ib)
,624
,692
,579
,692
,647
,466
,128
,297
,466
959
925
925
902
902
902
902
986
Based on Diluted Brine
Volume
of
diluted
brine
(gal)
2,299
NA
2,273
2,328
Specific
gravity*10
1.061
NA
1.061
1.061
Percent
of salt
(%)
8
NA
8
8
1,934
1,770
1.062
1.062
8
8
2,443
2,018
2,088
2,137
2,129
2,129
2,132
2,134
1.046
1.043
1.042
1.042
1.04
1.04
1.039
1.038
6
6
6
6
6
6
6
5
Salt
usage
(Ib)
1,627
NA
1,609
1,648
1,628
1,370
1,254
1,312
1,279
1,053
1,089
1,114
1,108
1,108
1,108
924
1,098
Based
on Salt
Delivery
Salt
usage
(Ib)
1,736
1,510
945
(a) Ideal salt saturation level used for calculation.
(b) Measured using a hydrometer.
The higher than expected regeneration levels experienced during most of Study Period I probably were
triggered initially by over adjustment of the hand valve located upstream of the Venturi eductor. As noted
in Section 4.4.2.2, a higher brine draw flowrate (i.e., 36 gpm vs. the design flowrate of 23 gpm) was
observed during September 19 through December 5, 2005 (under Regeneration Setting 2). (Note that this
flowrate most likely also was the flowrate experienced during July 30 through September 19, 2005, under
Regeneration Setting 1 because of similar amounts of salt usage and the same brine concentration and
brine draw time between these two periods.) It was suspected that, when the brine strength in the day
tank was changed from 4% to 8% on July 26, 2005, the hand valve might have been overly adjusted, thus
resulting in higher brine draw flowrates.
After being notified of the brine draw flowrate issue, the vendor provided instructions to the operator to
shorten the brine draw time from 32 to 25 min on the PLC on December 5, 2005. Shortening the brine
draw time was done because it was easier to implement (compared to manipulating the hand valve).
Reduction of the brine draw time from 32 to 25 min, however, would decrease the salt usage by only
22%; further decrease in the brine draw time was not recommended by the vendor because of the concern
of incomplete regeneration. The actual reduction in salt usage (and regeneration level) due to the
decrease in brine draw time was 21% based on saturate brine, 20% based on 8% brine, or 13% based on
salt delivery (see Table 4-10).
39
-------
Further adjustment under Regeneration Setting 4 involved a 25% reduction in brine concentration from 8
to 4% in the brine day tank. The actual reduction in salt usage (and regeneration level) was 24% based on
saturate brine, 16% based on 8% brine, or 37% based on salt delivery.
Salt usage per 1,000 gal of water treated was calculated to be 5.5, 4.8, and 3.0 Ib under Regeneration
Settings 2, 3, and 4, respectively, based on the amounts of salt consumed per regeneration cycle (i.e.,
1740, 1510, and 945 Ib, respectively) and the run length setting of 316,000 gal (Table 4-8). The 5.5 and
4.8 lb/1000 gal usage rates under Settings 2 and 3 were caused by the 56% higher brine draw rate and
improper regeneration setting as discussed above. The 3.0 Ib salt usage value was slightly lower than the
3.19 lb/1000 gal stated in the vendor's proposal and those reported in the literature (Clifford et al., 1987;
2003). For example, in a nitrate study conducted at Glendale, Arizona, where similar run length to nitrate
breakthrough (-400 BV) was obtained from a type II resin, Clifford et al. (1987) reported a salt usage of
3.25 lb/1,000 gal for complete regeneration and 2.36 lb/1,000 gal for partial regeneration. Outer's work
on nitrate removal in McFarland, California (1981) produced an even lower salt consumption than
experienced in Glendale, Arizona.
4.4.3 System Operational Issues. Major operational issues encountered during Study Periods I,
II, and III of the demonstration study are discussed in the following sub-sections.
4.4.3.1 Period I (June 14, 2005 to July 25, 2006)
PLC Problems. A power outage occurred over the weekend of June 18 and 19, 2005, causing several
operational issues. First, the product water totalizer read 341,000 gal on June 20, 2005, exceeding the
regeneration setpoint of 214,000 gal. An examination of the system revealed that the brine transfer pump
had been reset to "off, preventing the scheduled regeneration from taking place. Second, due to the
power outage, the PLC regeneration setting was reverted from "co-current" to the factory default of
"counter-current." Although the system was designed with flexibilities to support both regeneration
modes, the plumbing and valving was configured only for the co-current regeneration. Therefore, it was
suspected that the system had not been properly regenerated for about 10 days, as indicated by higher-
than-expected arsenic and nitrate concentrations in the treated water on June 23 and 29, 2005 (Section
4.5). To rectify the situation, the PLC setting was changed back to "co-current" on June 29, 2005, after
sample collection. In addition, an uninterrupted power supply (UPS) was installed by the vendor on July
26, 2005, to provide a backup power to the PLC.
The system failed to regenerate again on August 3, 2005, due to a broken level sensor in the brine day
tank. The product water totalizer read 534,000 gal on that day, far exceeding the setpoint of 335,000 gal.
The prolonged service run resulted in higher-than-influent levels of arsenic and nitrate in the treated
water, known as "chromatographic effect" (see Section 4.5). The level sensor was repaired by the
operator on the same day.
Initial Arsenic and Nitrate Leakage after Regeneration. With co-current regeneration during Study
Period I, the IX system performed well (in terms of removing both arsenic and nitrate to below the
respective MCLs) except when it was freshly regenerated (Sections 4.5.1.1 and 4.5.2) or was
experiencing mechanical problems. Samples collected after the IX system had been freshly regenerated
during either weekly sampling or a special study on December 7 and 8, 2005 (i.e., Run Length Study 3 in
Table 3-4) contained elevated arsenic and nitrate concentrations until up to 50,000 to 60,000 gal of
throughput (or 3 to 4 hr into the service run). The early leakage of arsenic and nitrate was indicative of
incomplete regeneration of the IX resin via the downflow, co-current regeneration mode. To curb the
problem, a vendor's technician was onsite in March 2006 to (1) remove polyethylene beads from both IX
vessels, (2) backwash the vessels, and (3) replace the existing blue eductor with a larger, orange one in
March 2006 in the hope of achieving a higher brine draw flowrate. However, the leakage problem
40
-------
persisted afterwards. A run length study conducted on April 11 and 12, 2006 (i.e., Run Length Study 4 in
Table 3-4) again showed significant initial arsenic and nitrate leakage, which prompted the vendor to
recommend converting the regeneration from co- to counter-current mode.
4.4.3.2 Study PeriodII (July 25, 2006, to June 18, 2007)
Mechanical Problems Encountered During Counter-Current Regeneration. The first attempt to change
to counter-current regeneration took place on July 25, 2006, when a vendor's technician was onsite to
reload the polyethylene beads that were removed for IX vessel backwash in March 2006. Following the
modification and an upflow regeneration cycle on August 1, 2006, a run length study was conducted on
August 9 and 10, 2006 (i.e., Run Length Study 5 in Table 3-4). The results showed as high as 129 (ig/L
of arsenic and 17.6 mg/L of nitrate (as N) in the treated water long before the 316,000 gal throughput
setting, indicating improper regeneration (Section 4.5.2). As a result, the IX system was shut down on
August 18, 2006. On September 5, 2006, the IX system was changed back to co-current regeneration
temporarily and the results indicated proper regeneration. At this point, the vendor concluded that the
brine eductor had not functioned properly due to "fluctuating pressure" and recommended that the eductor
be replaced with a brine injection pump.
The second attempt took place on October 24, 2006, when a 1.5 horsepower (hp) close-coupled
centrifugal pump (Goulds Pumps Model #1BF21512) was installed at the suction side of the eductor.
Upon completion of two counter-current regeneration cycles, system operation resumed on December 5,
2006. Battelle conducted another run length study on January 17 to 18, 2007 (i.e., Run Length Study 6 in
Table 3-4). The analytical results showed essentially no arsenic or nitrate removal in the treated water
during the entire run length study. These results suggested that problems associated with counter-current
regeneration persisted even after the brine injection pump had been installed. Samples collected on
February 1 and 7, 2007 by the city and analyzed by the city's own laboratory and by a State-certified lab
showed nitrate concentration exceeding the 10-mg/L MCL, which prompted the city to shut down the
system again on February 13, 2007, and IDEQ to request for a public notice to be issued.
A meeting was held with the vendor and EPA at Battelle on February 21, 2007, to review the system
performance issues and formulate a course of action. Consensus was reached among the meeting
participants that the performance issues were caused mainly by mechanical failures of the brine injection
system. It was suspected that the suction port of the eductor, which was left online, might have restricted
the brine flow as brine was pulled (or, in this case, pumped) from the suction chamber to the
converging/mixing chamber in the eductor.
The vendor dispatched another technician to Fruitland on February 26, 2007. The technician opened the
tops of the vessels and discovered 8 in of freeboard in both vessels. The vendor speculated that the
presence of freeboard could have allowed the IX beds to rise and pack around the upper distributor,
resulting in excessive pressure drop as observed during regeneration. Additional packing media was
shipped to the site and loaded into the IX vessels on March 2, 2007. Meanwhile, the eductor was
removed and replaced with a tee and a diaphragm valve on the regeneration water inlet line before the tee
for flowrate adjustment. After these modifications, the brine injection pump was able to inject a proper
amount of saturated brine (-225 gal per vessel) into the IX system. Samples collected following a
regeneration cycle showed 1.5, 1.3, 1.3, 1.1, 4.5, and 7.5 mg/L of nitrate (as N) at 17,000, 40,000, 48,000,
53,000, 207,000, and 248,000 gal of throughput, respectively.
Resin Fouling. From April 12 to May 14, 2007, elevated arsenic and/or nitrate concentrations were
detected again in system effluent. For example, 13.8, 11.8, and 13.6 mg/L of nitrate (as N) were detected
at 204,000, 28,000, and 149,000 gal of throughput on April 4, April 13, and May 9, 2007. Significantly
elevated arsenic concentrations were detected throughout the service run on May 9 and 10, 2007, as
41
-------
shown on Figure 4-12, a snapshot from the inline arsenic analyzer, ArsenicGuard. Note that the inline
data (yellow dots) starting from the night of May 11, 2007, through ~ 10:30 a.m on May 14, 2007 were
invalid because the analyzer lost control of arsenic concentrations during this time period. Also note that
the analyzer would continue analyzing "samples" even when the IX system was not operating or the
analyzer was losing control of arsenic concentrations. Blue dots in the figure reflect the results of 0 and
10.0 (ig/L standards, which appear to be well on track.
StripChart: All Measurement*
Select Metal
JT Metal 1
r Metal 2
Select Parameter to Plot
ff Concentration (ppb) (~ Fit factor (r)
C Peak Voltage (mY) r 95% Confidence Interval
C Peak Width (mV) C Sensitivity
C Background Current (nA)
Select Interval
r 24 hours
C* 48 hours
ff 1 Week
(" 2 Weeks
C 4 Weeks
Update Graph
209 measurements attempted,
202 completed
Show Regens as vertical line
17 Y-Axis: Include Zero
F X-Axis: Include Zero
KEY:
Yellow dots: System Effluent at TT
Blue dots: Check standards (10 or 0 ppb)
Red dots: Failed or aborted measurement
Data plotted as of 11:20 a.m. on 05/14/07, which is 'zero' day on the plot
Figure 4-12. Snapshot from ArsenicGuard on May 9 and 10, 2007
The high arsenic and nitrate concentrations measured during service runs raised the suspicion of FX resin
fouling. Source water collected on April 17, 2007 showed 1.6 mg/L of TOC, slightly lower than the 2.2
mg/L of TOC measured three years ago during source water sampling on July 13, 2004 (Table 4-1). The
results of other analytes, including total As, Fe, Mn, P, and Ca were comparable to those measured
previously (Table 4-1), suggesting that the poor system performance and the suspected IX resin fouling
would not have been caused by any changes in water quality.
On May 18, 2007, a conference call was held by Battelle with EPA, Kinetico, and the facility to discuss
issues related to IX resin fouling. It was agreed that various mechanical issues associated with the brine
42
-------
injection system that caused improper resin regeneration for an extended period of time (i.e., since July
2006 after conversion of system regeneration from the co- to counter-current mode) might have resulted
in the suspected IX resin fouling. The vendor, therefore, recommended that the IX resin be cleaned with
a mixture of 5% NaOH and 10% brine followed by regular co-current regeneration, and that system
regeneration be switched back to co-current regeneration due to difficulties encountered in the counter-
current regeneration mode.
One additional item discussed during the May 18, 2007, teleconference was the 1.5-hp, close-coupled
centrifugal pump installed on October 24, 2006 for brine injection. Due to extensive corrosion, the
vendor recommended to order and send a 2-hp replacement pump (G&L model ICS [Investment Cast
Stainless 316SS]). Upon arrival, the pump was installed by the operator in mid-June 2007, but had to be
returned to the vendor for repair shortly after it was put in use. As such, the plant operator had to switch
back to the old pump during IX resin regeneration.
The IX resin fouling issue had been discussed in the February 21, 2007, meeting, during which
recommendations were made to pull core samples from each IX resin vessel and send them to Purolite for
laboratory cleaning and analysis. The core samples were collected on March 28, 2007, following a
regular field regeneration cycle with brine. The results of the resin analysis before and after caustic/brine
cleaning are discussed in Section 4.5.5.
4.4.3.3 Study Period III (June 18, 2007 to February 11, 2008)
Initial Arsenic and Nitrate Leakage after Regeneration. The IX resin was cleaned with a caustic/brine
mixture on June 19, 2007, and a core sample was taken from Vessel B and shipped to Purolite for
analysis. The IX system was then switched back to the co-current regeneration mode. The initial arsenic
and nitrate leakages observed during Study Period I continued, as evidenced by the results of field nitrate
measurements using nitrate test tubes (CAT No. 14037-00) and inline arsenic measurements using the
ArsenicGuard. For example, samples collected daily in July 2007 showed elevated nitrate concentrations
both at the beginning and end of service runs, although all were below 10 mg/L (as N). Similarly, arsenic
concentrations monitored by the ArsenicGuard were elevated during both the beginning and end of
service runs, as shown by a snapshot of the ArsenicGuard display in Figure 4-13.
Ineffective Resin Regeneration Caused by the Newly-installed Brine Injection Pump. Following the
resin cleaning on June 19, 2007, system performance continued to be erratic, largely depending on
success or failure of regeneration. For example, an automatic regeneration failed on June 26, 2007, with
29.8 (ig/L and 12.7 mg/L (as N) of arsenic and nitrate, respectively, measured at 21,000 gal of throughput.
A manual regeneration conducted on the following day was successful with 4.8 mg/L (as N) of nitrate
measured at 94,000 gal of throughput. Consistently elevated nitrate concentrations were measured again
on July 2, 3, and 5, 2007, at 12.7 mg/L (at 145,000 gal), 12.1 mg/L (at 10,000 gal), and 12.9 mg/L (at
160,000 gal), respectively. As a result, the IX system was shut down on July 5, 2007. The vendor
suspected that the failed regeneration cycles were caused by the newly installed 2-hp pump and, therefore,
asked the plant operator to switch back to the old brine injection pump (see Section 4.4.3.2). The
regeneration was manually triggered on July 6, 2007, and it was confirmed that each vessel used
approximately 250 gal of brine (SG = 1.043) as intended.
Impact of Spent Brine Discharge on City's Sewage Lagoons. The city experienced problems with its
sewage lagoons due to discharge of spent brine and rinse water, which apparently had caused duckweeds
in the lagoons to die. Therefore, the use of the IX system was cut back to 3 hr/day starting from
September 2007 to reduce any harmful impact on the biological activities in the lagoons. The city plans
to completely discontinue the use of the IX system after a new surface water treatment plant is put into
service. The IX system would be kept for emergency use only.
43
-------
StripChart: All Measurements
Select Metal
f? Metal 1
r Metal 2
Select Parameter to Plot
W Concentration (ppb) f~~ Fit factor (r)
C Peak Voltage (mV) r 95% Confidence Interval
r Peak Width (mV) C Sensitivity
C Background Current (nA)
Select Interval
C 24 hours
(~ 48 hours
(" 1 Week
4 Weeks
< prev. ext >
47S measurements attempted,
477 completed
Y-Axis: Include Zero
X-Axis: Include Zero
Show Regens as vertical line
KEY:
Yellow dots: System Effluent at TT
Blue dots: Check standards (10 or 0 ppb)
Red dots: Failed or aborted measurement
Figure 4-13. Total Arsenic Concentration in System Effluent - An ArsenicGuard Display Snapshot
Corrosion in IX Treatment Plant. The interior of the IX treatment plant experienced extensive corrosion
due to exposure to high salt contents in the plant. This was caused primarily by the presence of the salt
saturator and brine day tank and dusty conditions during salt loading in the plant.
4.4.4 Residual Management. Residuals produced by the IX system included spent brine and rinse
water, which were discharged to a floor drain. The volume of wastewater produced was determined by
the regeneration frequency and the volume of wastewater generated per regeneration cycle. Table 4-11
presents the calculations of wastewater production under different regeneration settings during Study
Period I, using the flowrates derived from Table 4-9.
The adjustments to the regeneration settings resulted in significant reductions in wastewater production.
For example, increasing the brine concentration from 4% to 8%, decreasing the brine draw time from 64
to 32 min, and increasing the brine draw flowrate reduced the spent brine volume from 2,944 to 2,304 gal
per regeneration cycle. The reduction in slow rinse and fast rinse time also decreased the wastewater
volume proportionally. Under Regeneration Setting 3, the total wastewater volume per cycle was reduced
to 6,230 gal, which was 60% of that under the initial setting. The monthly wastewater production was
estimated based on the number of regeneration cycles calculated by dividing the respective run length
44
-------
Table 4-11. Comparison of Wastewater Production Under Different IX Regeneration Settings
Parameter
Run Length Setting (gal)
Initial
Settings
214,000
Regeneration
Setting 1
335,000
Regeneration
Setting 2
316,000
Regeneration
Setting 3
316,000
Regeneration
Setting 4
316,000
Brine Draw
Brine Concentration (%)
Brine Draw Time (min)
Brine Draw Flowrate (gpm)(a)
Brine Draw Volume (gal)
4
64
23
1,472
8
32
36W
1,152
8
32
36
1,152
8
25
37
925
6
25
43
1,075
Slow Rinse
Slow Rinse Time (min)
Slow Rinse Flowrate (gpm)(a)
Slow Rinse Volume (gal)
64
23
1,472
64
26
1,664
64
26
1,664
40
27
1,080
40
36
1,440
Fast Rinse
Fast Rinse (min)
Fast Rinse Flowrate (gpm)(a)
Fast Rinse Volume (gal)
30
75
2,250
30
62
1,860
6
62
372
15
74
1,110
15
69
1,035
Total Waste Production
Wastewater Produced (gal/tank/cycle)
Wastewater Produced (gal/cycle)
Average Monthly Production (gal/month)(b)
No. of Regeneration Cycles per Month
Monthly Wastewater Production (gal/month)
Water Production Efficiency (%)
5,194
10,388
5,076,390
23
238,924
95.3
4,676
9,352
5,076,390
14
130,928
97.4
3,188
6,376
5,076,390
15
95,640
98.1
3,115
6,230
5,076,390
15
93,450
98.2
3,550
7,100
5,076,390
15
106,500
97.9
(a) Flowrates measured under Regeneration Setting 2 used for calculations under Setting 1.
(b) Based on an average daily demand of 166,895 gpd in Table 4-7.
(c) Higher brine draw flowrate caused by over adjustment of a hand valve.
-------
settings by average daily demand of 166,895 gpd. Depending on the settings, water production
efficiencies ranged from 95.3% to 98.2%.
4.4.5 System Operation Requirement
4.4.5.1 Required System Operation and Operator Skills. The required system operation and
operator skills are further discussed below according to pre- and post-treatment requirements, levels of
system automation, operator skill requirements, preventive maintenance activities, and frequency of
chemical/media handling and inventory requirements.
Pre- and Post-Treatment Requirements. Pretreatment included filtration with a bank of five bag filters
to remove sediment from source water. The bag filters were replaced when Ap readings across the bag
filters were greater than 6 psi. The bag filters were replaced eight times during the first 20 months of the
demonstration study from June 14, 2005 to February 9, 2007, and it took approximately one hour each
time to replace all five filter bags. There was no post-treatment employed, except for the provision of
post-chlorination in case of any bacterial outbreak.
System Automation. The IX system was fully automatic and controlled by the PLC in the central control
panel. The control panel also contained a touch screen OIP that allowed the operator to monitor system
flowrate and throughput since last regeneration. The OIP also allowed the operator to change system
setpoints, as needed, and check the status of alarms. Setpoint screens were password-protected so that
changes could only be made by authorized personnel. Typical alarms were for no flow, storage tank
high/low, and regeneration failure. The IX system was regenerated automatically based on a throughput
setpoint, except during the regeneration sampling events when the system was regenerated manually in
order to capture spent regenerant and rinse samples. Although the system required minimal operator
oversight and intervention, a number of operational issues with automated resin vessel regeneration and
associated equipment, as noted in Section 4.4.3 did arise.
Operator Skill Requirements. The O&M of the IX system required minimal additional operator skills
beyond those required for small system operators, such as solid work ethic, basic mathematical skills,
ability to understand chemical properties, familiarities with electronic and mechanical components, and
ability to follow written and verbal instructions. Understanding of and compliance with all occupational
and chemical safety rules and regulations also were required. Since all major system operations were
automated and controlled by the PLC, the operator was required to understand and learn how to use the
PLC and OIP to perform tasks after receiving training from the vendor.
The level of operator certification is determined by the type and class of the public drinking water
systems. IDEQ's drinking water rules require that all community and non-transient, non-community
public drinking water and distribution systems be classified based on potential health risks.
Classifications range from "Class I" (lowest) to "Class IV" (highest) for treatment systems and from
"Very Small" to "Class IV" for distribution systems, depending on factors such as system complexity,
size, and source water. There are 11 different types and classes of individual drinking water operator
classes for which licenses are issued. The City of Fruitland Public Water System is classified as a "Class
II" distribution system and the plant operator has a matching "Class II" license. After receiving proper
training by the vendor during system startup, the operator understood the PLC, knew how to use the OIP,
and worked with the vendor to trouble shoot and perform minor on-site repairs.
4.4.5.2 Preventive Maintenance Activities. Preventive maintenance tasks recommended by the
vendor included daily to monthly visual inspection of the piping, valves, vessels, flow meters, and other
system components. Routine maintenance also may be required on an as-needed basis for the air
compressor motor and the replacement of o-ring seals or gaskets on automated or manual valves and the
46
-------
brine transfer pump (Kinetico, 2004). During the demonstration study, maintenance activities performed
by the operator included replacing filter bags periodically, checking the brine concentration using a
hydrometer, adjusting regeneration frequency and setpoints as instructed by the vendor, and conducting
troubleshooting activities as described in Section 4.4.3 related to the malfunction of automated
regeneration operations.
4.4.5.3 Chemical/Media Handling and Inventory Requirements. Sodium chloride was the only
chemical required for IX system operation. The system has fully automated controls with IX resin
regeneration triggered by volume throughput. The salt truck delivered salt on a weekly or as-needed basis
with or without the operator's presence. The salt saturator was sized to hold 15 tons of salt supply; this
capacity, however, was reduced by 18% to 12.3 ton due to shortening of the tank height to fit the
building. Assuming that the system regenerated 15 times per month (see Table 4-10) and used 1,000 Ib of
salt per event (as designed), it would require 15,000 Ib or 6.8 tons of salt per month. Therefore, the salt
saturator held about seven weeks of salt supply.
4.5 System Performance
The performance of the IX system was evaluated based on analyses of water samples collected across the
treatment train, during IX vessel regeneration, and from the distribution system. To help provide
additional insight into system performance, samples also were collected during a number of IX resin run
length studies and elution studies.
4.5.1 Treatment Plant Sampling. The treatment system performance was evaluated via routine
sampling only during Study Period I from June 14, 2005, to July 25, 2006. The treatment plant water was
sampled on 52 occasions, including three duplicate sampling events and 14 speciation events. Table 4-12
summarizes arsenic, nitrate, uranium, vanadium, and molybdenum analytical results. Table 4-13
summarizes results of other water quality parameters. Appendix C contains a complete set of analytical
results. The results obtained are discussed as follows.
4.5.1.1 Arsenic and Nitrate Removal. Arsenic and nitrate were the two primary contaminants of
concern in source water; thus, their removal was the key to assessing the performance of the IX system.
Figures 4-14 and 4-15 show total arsenic and nitrate concentrations, respectively, across the treatment
train. Each figure consists of two plots: the first one plots total arsenic (or nitrate) concentrations against
sampling dates; the second plots the same set of concentration data against system throughput at the time
of sample collection. Because the system was regenerated two to three times a week, these weekly
treatment plant samples were collected from multiple service runs. Typically, a breakthrough curve is
constructed with data from the same service run. To better understand IX system performance with data
collected from multiple service runs, the concentration data were plotted against the system throughput
(from low to high) when samples were collected. These "reconstructed" breakthrough curves are
presented in Figures 4-14b for total arsenic and 4-15b for nitrate. Note that Figures 4-14b and 4-15b do
not include the data collected on June 23, June 29, and August 3, 2005, because the IX system operated
improperly on those days.
Total arsenic concentrations in raw water ranged from 33.6 to 60.8 ug/L and averaged 42.5 ug/L (Table
4-13). Nitrate concentrations in raw water ranged from 6.9 to 11.5 mg/L (as N) and averaged 10.0 mg/L
(as N). After IX treatment, total arsenic concentrations were reduced from to below 10 ug/L in most TA,
TB, and TT samples (Figure 4-14b). However, over 10 ug/L of arsenic was measured in 10 samples
collected within 28,000 gal into the service runs and one sample collected after 314,000 gal into the
service run. Similarly, nitrate concentrations after the IX treatment were reduced to below 10 mg/L (as
N) in most TA, TB, and TT samples, except for seven samples collected after 269,000 gal into the service
runs (Figure 4-15b). As also shown in Figure 4-15b, somewhat elevated nitrate concentrations (above
47
-------
Table 4-12. Summary of Arsenic, Nitrate, Uranium, Vanadium, and
Molybdenum Data
Parameter
As
(total)
As
(soluble)
As
(paniculate)
As(III)
As(V)
Nitrate
(asN)
U
(total)
U
(soluble)
V
(total)
V
(soluble)
Mo
(total)
Mo
(soluble)
Sampling
Location(a)
IN
TA
TB
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TT
IN
TA
TB
TT
IN
TT
IN
TA
TB
TT
IN
TT
Unit
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Sample
Count
52
36(b)
36(b)
14
14
14
14
14
14
14
14
14
52
37
38
14
52
38
38
14
12
12
52
38
38
14
13
13
50
34(d)
34(d)
14
13
13
Minimum
33.6
<0.1
0.2
0.7
35.1
0.7
0.1
<0.1
0.4
0.4
33.7
<0.1
6.9
0.4
0.3
0.4
13.8
<0.1
<0.1
<0.1
15.9
<0.1
30.6
0.1
0.2
<0.1
36.6
<0.1
11.6
<0.1
<0.1
<0.1
11.4
<0.1
Maximum
60.8
41.4
46.3
o o
J.J
59.9
3.4
8.9
0.9
2.4
2.4
58.7
2.9
11.5
15.0
12.8
13.2
24.9
0.3
2.5
<0.1
20.4
<0.1
53.0
16.6
36.1
4.2
45.2
5.7
15.9
0.8
0.7
0.5
14.0
0.4
Average
42.5
_(<0
_(°>
_(<0
40.3
_(<0
3.5
_(<0
1.2
_(<0
39.0
_(<0
10.0
4.4
3.9
3.5
19.4
_(<0
_(°>
_(<0
18.6
_(<0
o r\ o
39.3
_(c)
_(°>
_(c)
39.6
_(c)
12.9
_(c)
_(c)
_(c)
12.7
_(c)
Standard
Deviation
6.0
_(<0
_(c)
_(c)
6.2
_(c)
3.2
_(c)
0.6
_(<0
6.2
_(c)
0.9
4.3
3.3
4.5
1.9
_(c)
_(<0
_(c)
1.4
_(c)
3.4
_(c)
_(c)
_(c)
2.2
_(c)
0.9
_(<0
_(c)
_(c)
0.8
_(c)
(a) See Figure 3-1 for sampling locations.
(b) Excluding data collected on 06/23/05 and 06/29/05, when system was not regenerated
properly.
(c) Not meaningful for concentrations related to breakthrough, see Figures 4-14 and 4-15 and
Appendix B for results.
(d) Excluding three outliers on 06/23/05, 06/29/05, and 11/30/05.
One-half of detection limit used for nondetect samples for calculations.
Duplicate samples included in calculations.
48
-------
Table 4-13. Summary of Other Water Quality Parameters
Parameter
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate
(asN)
Orthophosphate
(as PO4)
P (total)
Silica
(as SiO2)
Turbidity
TDS
pH
Temperature
Dissolved
Oxygen
ORP
Sampling
Location(a)
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
NTU
mg/L
mg/L
S.U.
S.U.
S.U.
S.U.
°C
°c
°c
°c
mg/L
mg/L
mg/L
mg/L
mV
mV
mV
mV
Sample
Count
52
37
38
14
15
1
1
14
52
37
38
13
53
37
38
18
28
19
20
8
31
22
22
9
50
38
38
13(b)
52
37
38
14
13
12
49
34
35
14
49
34
35
14
48
34
35
13
49
34
34(0)
14
Minimum
365
3.0
3.0
286
0.3
0.7
0.7
0.3
41
<1
<1
<1
6.9
0.4
0.3
0.4
0.05
0.05
0.05
0.05
0.03
0.03
0.03
0.03
47
53
53
46
0.1
0.1
0.1
0.1
542
498
6.7
6.8
6.0
7.2
14.6
14.6
14.6
14.8
1.9
1.8
1.3
1.7
191
180
186
172
Maximum
484
484
462
484
1.3
0.7
0.7
0.6
91
94
63
<1
11.5
15.0
12.8
13.2
0.56
0.23
0.25
0.85
0.40
0.28
0.50
0.09
63
62
63
62
1.4
1.5
1.8
1.6
610
584
7.9
7.9
7.9
7.9
15.7
15.9
15.7
15.9
4.3
3.4
3.5
3.6
314
319
296
288
Average
387
334
300
432
0.6
0.7
0.7
0.5
59
6.0
5.7
<1
10.0
4.4
3.9
3.9
0.11
0.05
0.05
0.13
0.32
0.03
0.07
0.02
57
57
57
56
0.4
0.6
0.6
0.5
580
547
7.6
7.5
7.3
7.5
15.1
15.1
15.0
15.1
2.7
2.5
2.5
2.6
244
241
239
240
Standard
Deviation
18
146
179
57
0.2
NA
NA
0.1
7.9
20
16
0.0
0.9
4.3
3.3
4.2
0.12
0.06
0.06
0.29
0.07
0.06
0.13
0.03
2.8
1.8
1.9
4.4
0.3
0.4
0.5
0.6
22
26
0.2
0.3
0.4
0.2
0.2
0.3
0.2
0.3
0.5
0.4
0.4
0.5
29
29
22
27
-------
Table 4-13. Summary of Other Water Quality Parameters (Continued)
Parameter
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Sampling
Location'3'
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TA
TB
TT
IN
TT
IN
TA
TB
TT
IN
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
Ug/L
Ug/L
Ug/L
Ug/L
Ug/L
Ug/L
Ug/L
Ug/L
Ug/L
ug/L
Sample
Count
15
1
1
14
16
3
3
13
15
1
1
14
50td)
38
38
14
14
14
52
38
38
14
14
14
Minimum
221
243
249
222
122
114
119
131
86
105
105
87
<25
<25
<25
<25
<25
<25
11.8
<0.1
0.2
0.2
10.0
0.2
Maximum
315
243
249
350
199
145
146
226
132
105
105
129
<25
<25
<25
<25
<25
<25
32.8
33.7
28.0
26.5
35.2
28.7
Average
249
243
249
249
146
130
129
150
101
105
105
100
<25
<25
<25
<25
<25
<25
22.1
11.9
13.9
11.4
21.5
11.6
Standard
Deviation
28
NA
NA
32
19
15
15
24
13
NA
NA
12
0.0
0.0
0.0
0.0
0.0
0.0
4.7
10.9
9.6
10.6
6.7
11.2
(a) See Figure 3-1 for sampling locations.
(b) Excluding an outlier on 07/16/06.
(c) Excluding an outlier on 08/10/05.
(d) Excluding two outliers on 06/23/05 and 9/28/05.
NA = not applicable.
One-half of detection limit used for nondetect samples for calculations.
Duplicate samples included in calculations.
~4 mg/L) also were measured within the first 50,000 gal of service run. Both arsenic and nitrate had
either leaked from freshly regenerated IX resin beds or broken through from the IX beds upon exhaustion.
These results are further discussed below:
Early Arsenic Leakage. On August 10, 2005, TA and TB samples collected at 28,000 gal (or 37 BV) of
throughput contained 25.6 and 15.1 ug/L of total arsenic, respectively, exceeding the 10-ug/L MCL. This
early arsenic leakage reoccurred on eight additional occasions on August 31, 2005, February 1, 2006,
May 9, 2006, June 7, 2006, and July 6, 2006, with concentrations as high as 40.5 ug/L measured at TA at
18,000 gal of throughput. The issues related to early arsenic leakage were discussed in Section 4.4.3.
Arsenic and Nitrate Breakthrough Upon IXResin Exhaustion. On September 28, 2005, the sample
collected at TA contained 17.6 ug/L of total arsenic and 9.7 mg/L of nitrate (as N), which were either
exceeding or approaching the respective MCLs. Sampling occurred after 314,000 gal (or 420 BV) of
water had been treated, which was close to the regeneration throughput setpoint of 316,000 gal (422 BV).
Because the TB sample contained only 2.1 ug/L of arsenic, the combined effluent from both vessels
would have contained arsenic just under the MCL.
50
-------
-------
ra
20
18
16
14
12
c
o
I 10
HI
§ 8
O
6
2
(a)
Sampling Date
20
18 -
16 -
o
210
o 8
O
2
£ 6
4 -
(b)
50,000 100,000 150,000 200,000
Water Treated (gal)
250,000 300,000 350,000
Note: 06/23y05,06/29/05, and 08/03/05 data not shown due to improper
Figure 4-15. Nitrate Concentrations Measured Over the Period I
Demonstration Study: (a) Temporal Plot; (b) Composite Breakthrough Curves
52
-------
Samples collected after 269,000 gal of throughput exceeded the nitrate MCL on a number of occasions
(including January 18, February 22, March 15, May 17, May 24, and June 21, 2006), indicating that the
regeneration setpoint of 316,000 gal (422 BV) was inadequate for nitrate removal. To ensure proper
removal of both arsenic and nitrate, a throughput value of 269,000 gal should have been used to trigger
regeneration.
Samples Collected When System Operating Improperly. TA and TB samples collected on June 23 and
29, 2005, after 212,000 gal (or 283 BV) and 147,000 gal (or 197 BV) of water had been treated,
respectively, showed almost no arsenic or nitrate removal (data not shown on the "reconstructed"
breakthrough curves). It was discovered later that, after a power outage on June 17, 2005, the system
PLC was reset automatically to the default "counter-current" regeneration mode. As a result, the system
was not properly regenerated during this period. The effluent water quality returned to normal after the
problem was corrected on June 29, 2005.
On August 3, 2005, TA and TB samples showed higher-than-raw-water levels of arsenic and nitrate (i.e.,
41.4 and 46.3 ug/L vs. 34.2 ug/L for total As and 9.7 and 9.7 mg/L vs. 9.3 mg/L [as N] for nitrate). This
occurred because the system had failed to regenerate at the setpoint of 335,000 gal (448 BV) and
continued to operate up to 534,000 gal (714 BV) due to a broken brine tank level sensor. The prolonged
service run forced previously exchanged arsenic and nitrate to be displaced, presumably, by more
preferred anions such as sulfate in raw water, resulting in "chromatographic peaking." According to the
selectivity sequence discussed in Section 4.2.1, an SBA resin such as A300E prefers sulfate over
HAsO42, nitrate, and H2AsO4"; HCO3" ion is less preferred than HAsO42, but has a similar affinity to the
resin as H2AsO4".
4.5.1.2 Arsenic Speciation. Figure 4-16 shows the arsenic speciation results of samples collected at
the wellhead and combined effluent during Study Period I. As(V) was the predominant species in raw
water, ranging from 33.7 to 58.7 ug/L and averaging 39.0 ug/L (Table 4-12). Only trace amounts of
particulate As and As(III) existed, with concentrations averaging 3.5 and 1.2 ug/L, respectively. After
treatment, As(III) concentrations remained essentially unchanged, averaging 1.2 ug/L. As expected, the
IX process did not remove the neutral species of arsenite.
4.5.1.3 Uranium, Vanadium, and Molybdenum Removal. Figure 4-17 presents the reconstructed
breakthrough curves of total U, V, and Mo during Study Period I. Total U concentrations ranged from
13.8 to 24.9 ug/L in raw water (Table 4-13), which was removed to less than 1 ug/L in treated water
except for July 6, 2005 at 2.5 ug/L (TB). Total V concentrations ranged from 30.6 to 53.0 ug/L and
averaged 39.3 ug/L in raw water. After treatment, total V was removed to less than 10 ug/L, except for a
few occasions with samples collected at 18,000 and 52,000 gal of throughput. The highest concentration
measured was 36.1 ug/L (TB) on July 6, 2005. Total Mo in raw water averaged 12.9 ug/L and was
removed to less than 1 ug/L, except for June 23 and 29, 2005, when the IX system was not operating
properly.
4.5.1.4 Other Water Quality Parameters. Figures 4-18 and 4-19 present "reconstructed"
breakthrough curves for sulfate, pH, and total alkalinity during Study Period I. As shown in Figure 4-18,
sulfate concentrations ranged from 41 to 91 mg/L in raw water (Table 4-13), which was removed to less
than 1 mg/L after treatment, except for June 23 and 29 and August 3, 2005, when the IX system
experienced mechanical problems and for three occasions on February 1, June 28, and July 6, 2006, when
sulfate concentrations spiked to 9 to 12 mg/L.
53
-------
Arsenic Species at Inlet (IN)
A* ^ J& ^ A# ^ ^
70
Arsenic Species after Tanks A and B Combined (TT)
60 -
50
40
30 -
20
10
„<&
Date
Figure 4-16. Concentrations of Arsenic Species at Wellhead and Combined Effluent
54
-------
g30
50,000 100,000
150,000 200,000
Water Treated (gal)
250,000 300,000 350,000
50,000 100,000 150,000 200,000
Water Treated (gal)
250,000 300,000 350,000
50,000 100,000 150,000 200,000 250,000 300,000 350,000
Water Treated (gal)
Figure 4-17. Composite Breakthrough Curves for Total U, V, and Mo
55
-------
100
50,000 100,000 150,000 200,000
Water Treated (gal)
250,000
300,000
350,000
Figure 4-18. Composite Breakthrough Curves for Sulfate
Raw water pH values ranged from 7.2 to 7.9 and averaged 7.6 (except for one outlier of 6.7 on July 6,
2005). Treated water pH values remained in the similar range, but reduction in pH values was observed
for a short duration after the system had been freshly regenerated. For example, pH values at IN, TA, and
TB locations were 7.8, 7.0, and 7.3, respectively, on August 10, 2005, after 28,000 gal of water was
treated; 7.7, 7.5, and 6.8, respectively, on August 31, 2005 after 28,000 gal of water was treated; and 7.8,
7.1, and 6.9, respectively, on February 1, 2006 after 11,000 gal of water was treated. This pH reduction
corresponded to the significant reduction in total alkalinity, i.e., from 383 to 3 and 3 mg/L (as CaCO3) on
August 10, 2005; from 374 to 158 and 7 mg/L (as CaCO3) on August 31, 2005; and from 393 to 60 and
12 mg/L (as CaCO3) on February 1, 2006.
The reduction in pH and alkalinity immediately after regeneration was attributed to the removal of
bicarbonate ions by the IX resin. As well documented in the literature, one disadvantage of the IX
process is reduction of pH by the freshly regenerated resin during the initial 100 BV of a service run
(Clifford, 1999). Afterwards, rapid breakthrough of bicarbonate ions raises the pH values to those similar
to raw water.
4.5.2 Resin Run Length Studies. Four run length studies (1 to 4) were conducted in Study Period
I when the IX system was regenerated in the co-current mode. Two run length studies (5 and 6) were
conducted in Study Period II after the system was switched to the counter-current mode. Figure 4-20
presents total arsenic and nitrate breakthrough curves from the six run length studies. Total alkalinity,
pH, sulfate, and total V also were measured during Run Length Study 3 conducted on December 7 and 8,
2005, and their breakthrough curves are presented in Figure 4-21.
56
-------
7 -
6 -
50,000 100,000 150,000 200,000
Water Treated (gal)
250,000
300,000
350,000
600
500 -
O400
50,000
100,000
150,000 200,000
Water Treated (gal)
250,000
300,000
350,000
Figure 4-19. Composite Breakthrough Curves for pH and Total Alkalinity
57
-------
4.5.2.1 Study Period I Run Length Studies
Run Length Study 1 (July 28-30, 2005). Combined effluent samples were collected and analyzed for
total arsenic and nitrate using field test kits (Section 3.5.1). Arsenic and nitrate reached the respective
detectable concentrations of 2 ug/L and 5 mg/L (as N), respectively, after 303,000 gal (-400 BV) of
throughput. Samples collected at 366,000 gal (489 BV) showed arsenic and nitrate breakthrough at 20
ug/L and 10 mg/L (as N), respectively. Subsequent samples were collected from individual vessels to
confirm the results. Total arsenic concentrations were measured at >50 ug/L in Vessel A effluent and 10
ug/L in Vessel B effluent. The higher arsenic breakthrough from Vessel A was expected because it had
been in service longer than Vessel B. Nitrate concentrations were measured at 10 mg/L for both vessels.
As a result of this study, the regeneration setpoint was adjusted from 214,000 gal (286 BV) to 335,000 gal
(448 BV) on July 30, 2005 (Table 4-8).
Run Length Study 2 (August 16-17, 2005). The first sample collected from Vessel A at 86,000 gal (115
BV) contained 5 ug/L of total arsenic and 1.5 mg/L of nitrate (as N). Total arsenic concentrations then
decreased to as low as 1.2 ug/L at 302,000 gal before rising again to as high as 5.4 ug/L before
approaching the 335,000-gal setpoint. Nitrate concentrations decreased to 0.1 mg/L (as N) at 250,000 gal,
and then increased steadily to 10 mg/L (as N) at 302,000 gal. Therefore, nitrate reached its MCL earlier
than arsenic, which was consistent with the hierarchy of selectivity of an SBA resin (i.e., the divalent
arsenate ion is more preferred than nitrate) as discussed in Section 4.2.1. The results of the study
prompted the throughput setpoint to be reduced to 316,000 gal (422 BV) on September 19, 2005.
Run Length Study 3 (December 7-8, 2005). In this study, samples were collected from each vessel with
more samples taken during the first 60,000 gal (or 80 BV) of throughput. Sampling results clearly
indicated initial arsenic and nitrate leakage from both IX resin vessels. Vessel A arsenic and nitrate
breakthrough curves were very similar to those of the second run length study. The initial arsenic leakage
from Vessel B was as high as 18.7 ug/L at 24,000 gal (or 32 BV). The initial nitrate leakage from either
vessel was as high as 4.3 mg/L (as N), which was below the MCL. The nitrate concentration in Vessel A
effluent reached 10 mg/L (as N) at 288,000 gal (or 385 BV).
As shown in Figure 4-21, total alkalinity and pH values were significantly reduced to as low as 11 mg/L
(as CaCO3) and a standard unit of 6, respectively, immediately after regeneration and then gradually
increased to the respective raw water levels at approximately 187,000 gal of throughput. Sulfate
concentrations were below the detectable level throughout the service run. Vanadium also showed initial
leakage, with more severe leakage observed at Vessel B. Total U and Mo levels were below the MDL of
0.1 ug/L throughout the service run.
Run Length Study 4 (April 11-12, 2006). Significant initial arsenic and nitrate leakage was observed
from both IX resin vessels. The first sample was collected from Vessel A at 2,000 gal (3 BV) and
contained 43 ug/L of total arsenic and 5.5 mg/L of nitrate (as N). Total arsenic concentrations then
decreased to as low as 1.1 ug/L at 216,000 gal before rising again to as high as 7.7 ug/L at the 316,000-
gal setpoint. Nitrate concentrations decreased to 0.2 mg/L (as N) at 216,000 gal, and then increased
steadily to exceed 10 mg/L (as N) around 279,000 gal. Again, nitrate reached its MCL earlier than
arsenic. Vessel B arsenic and nitrate breakthrough curves were similar to those of Vessel A. The first
sample collected from Vessel B was at 13,000 gal (17 BV) and contained 30.3 ug/L of total arsenic and
5.9 mg/L of nitrate (as N).
58
-------
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
20 H ' ' ' ' ' ' ' ' ' ' r 20
o
I
10 -
f
Run Length Study 1
Combined Effluent
(July 28-30, 2005)
- 15
- 10
o
O
I
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000 400,000
Water Treated (gal)
* Samples analyzed on site with test kits
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
20 H ' ' ' ' ' ' ' ' ' ' r 20
i 15 -
c
o
I
§ 10
c
o
o
re 5
o
Run Length Study 3
Vessel A Effluent
(December 7-8, 2005)
15
- 10
- 5
o
O
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000 400,000
Water Treated (gal)
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
Total As Concentration (^g/L)
D O1 O O1 C
-•—As
—»— Nitrate
Run LengthStudy2
Vessel A Effluent 7
(August 16-17, 2005) fy
m / f
D O1 -»•-»• N
O O1 C
Nitrate Concentration (mg/L as N)
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000 400000
Water Treated (gal)
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
Total As Concentration (^g/L)
D Ol O Ol C
^^As
Run Length Study 3 -»- Nitrate
j y
Vessel B Effluent
(December 7-8, 2005)
\ /
"-« • • *
D Ol -i -i f.
O Ol C
Nitrate Concentration (mg/L as N)
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000 400,000
Water Treated (gal)
Figure 4-20. Total Arsenic and Nitrate Breakthrough Curves of Run Length Studies
-------
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
50
40
c 30
o 20
o
O
-: 10 -
-As
-Nitrate
Run Length Study 4
Vessel A Effluent
(April 11-12, 2006)
100,000 200,000 300,000
System Throughput (gal)
20
15
10
00.
5 z
400,000
o
o
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
50
40
30
20
10
-As
-Nitrate
Run Length Study 4
Vessel B Effluent
(April 11-12, 2006) f
100,000 200,000 300,000
System Throughput (gal)
20
15 =•
u>
10 £
o
O
o S
400,000
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
150 H ' ' ' ' ' ' ' ' ' ' r 20
Run Length Study 5
Vessel A Effluent
(August 9-10,2006)
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000 400,000
System Throughput (gal)
Run Length (BV)
0 50 100 150 200 250 300 350 400 450 500
150 H ' ' ' ' ' ' ' ' ' ' r 20
3- 120 -
o>
c
I 90 -
i
0)
o 60
O
i 30 J
Run Length Study 5
Vessel B Effluent
(August 9-10,2006)
• 15
• 10 «
•s
o
o
• 5
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000 400,000
System Throughput (gal)
Figure 4-20. Total Arsenic and Nitrate Breakthrough Curves of Run Length Studies (Continued)
-------
Run Length (BV)
0 50 100 150 200 250 300 350 400 450
500 H ' ' ' ' '—: ' ' ' '—r 9.0
8 400 H
8
=! 300 -
O
E.
I 200 -
1
& 100 -
o
- 8.0
- 6.0
5.0
50,000 100,000 150,000 200,000 250,000 300,000 350,000
Water Treated (gal)
Run Length (BV)
0 50 100 150 200 250 300 350 400 450
500 H ' ' ' ' ' ' ' ' '—r 9.0
400 -
=! 300
O)
200 -
100 -
- 8.0
- 7.0
- 6.0
5.0
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000
Water Treated (gal)
Run Length (BV)
50 100 150 200 250 300 350 400 450
30
0
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000
Water Treated (gal)
Run Length (BV)
50 100 150 200 250 300 350 400 450
20 -
15 H
Vessel B
-SO4
20
- 15
- 10
o
O
5 O
0
0 50,000 100,000 150,000 200,000 250,000 300,000 350,000
Water Treated (gal)
Figure 4-21. Total Alkalinity, pH, Sulfate, and Vanadium Breakthrough Curves of Run Length Study 3 (December 7 to 8, 2005)
-------
4.5.2.2 PeriodIIRun Length Studies
Run Length Study 5 (August 9-10, 2006). This run length study was conducted after the mode of
regeneration had switched from co- to counter-current on July 25, 2006 (Table 4-8). For Vessel A,
breakthrough of arsenic and nitrate at the respective MCLs occurred at 210,000 and 140,000 gal,
respectively. For Vessel B, arsenic concentrations were above the 10 (ig/L MCL throughout the entire
run length study; nitrate concentrations were above the 10 mg/L (as N) MCL after approximately 133,000
gal of throughput. The highest arsenic and nitrate concentrations measured were 129 (ig/L and 17.6 mg/L
(as N), respectively. The result of the run length study indicated improper regeneration of the IX resin in
counter-current regeneration mode.
Run Length Study 6 (January 16-17, 2007). After the brine injection pump had been installed at the
suction side of the eductor, another run length study was conducted on January 17 to 18, 2007. The
analytical results showed little or no arsenic/nitrate removal throughout the entire run length study,
indicating lack of regeneration due to improper brine draw (Section 4.4.3).
4.5.3 Regeneration Studies
4.5.3.1 Regeneration Study 1 (July 30, 2005). Figure 4-22 presents the specific gravity and
conductivity of the wastewater discharged during Vessel B regeneration on July 30, 2005. Specific
gravity of the wastewater increased sharply soon after brine draw, leveled off, and then decreased sharply
a few minutes into slow rinse. Specific gravity measures percent concentration of salt in a brine solution.
It was verified that the brine solution entering Vessel B had a specific gravity of 1.06, corresponding to
8% of salt. Because neither the brine draw flow nor the day tank usage was monitored during this study,
the salt consumption could not be verified. Conductivity of the wastewater exceeded the range of the
meter during brine draw, dropped sharply during slow rinse, and then leveled off at about 1,200 uS after
about 65 min into regeneration. The data suggested that the slow rinse and fast rinse time could be
significantly reduced to minimize wastewater production. While the slow rinse time was unchanged, the
fast rinse time was reduced from 30 to 6 min on September 19, 2005 (Table 4-8).
4.5.3.2 Regeneration Study 2 (September 22, 2005)
Regeneration Curves. Figures 4-23 and 4-24 present concentrations of total arsenic, nitrate, sulfate,
TDS, and pH in/of the wastewater produced during IX system regeneration on September 22, 2005.
These regeneration curves were typical of an IX system and similar to those observed previously (Wang,
et al., 2002). TDS concentrations reflected salt concentrations in the wastewater. As the 8% brine
solution was drawn into an IX vessel, arsenic, nitrate, and sulfate on the exhausted IX resin were
displaced by the highly concentrated chloride ions. Peak arsenic (14.9 and 18.9 mg/L) and sulfate (51 and
49 g/L) concentrations were detected about 8 to 12 min into brine draw, slightly earlier than those for
nitrate (2.3 and 2.2 g/L [as N]). While nitrate concentrations dropped to below 10 mg/L (as N) towards
the end of fast rinse, arsenic concentrations were still around 35 ug/L, thus resulting in elevated
concentrations in the treated water after the IX system was returned to service. Extending the fast rinse
time to 15 min on December 5, 2005, did not appear to help because the leakage continued up to 52,000
gal (70 BV), or 3 to 4 hr into the service run.
As shown in Figure 4-24, pH values of the wastewater were close to neutral (i.e., 7.5) at the beginning of
brine draw, but rose sharply to about 9.0 due to the release of bicarbonate ions from the IX resin. pH
value dropped to between 5.5 to 6.0 by the end of fast rinse due to removal of bicarbonate s by the freshly
regenerated resin. This observation is consistent with the results obtained during the above-mentioned
run length studies and regular treatment plant sampling.
62
-------
Vessel B Elution Curve (07/30/05)
g. 1.020 -
10 20 30 40 50 60 70
-- 4,000
-- 3,000
-- 2,000 -
-- 1,500
Source: Kinetico
Figure 4-22. Vessel B Regeneration Curve
Regeneration Flowrate. As part of the September 22, 2005 regeneration study, regeneration flowrates
were monitored during regeneration and plotted in Figure 4-25. Due to concerns over the accuracy of
flowrate readings from a floater-type rotameter installed on the waste discharge line, readings of the
totalizer located upstream of the Venturi eductor also were recorded at 1 to 2 min intervals. Because the
totalizer did not register the volume of saturated brine drawn by the eductor, the brine draw flowrates
shown in Figure 4-25 were lower than the actual values. For Vessel A, flowrates varied from 22 to 29
gpm for brine draw, 22 to 28 gpm for slow rinse, and 56 to 75 gpm for fast rinse, producing 802, 1,519,
and 383 gal of wastewater (or 25, 24, and 64 gpm average flowrate for) in the respective steps. Adding
the volume of the saturated brine (i.e., 360 gal), the average flowrate for brine draw would be 36 gpm,
about 56% higher than the design value of 23 gpm.
For Vessel B, the flowrates were similar to those of Vessel A except for brine draw. A total of 1,340,
1,542, and 359 gal of water was used, corresponding to an average flowrate of 42, 24, and 60 gpm,
respectively. The higher brine draw flowrates for Vessel B were caused inadvertently by a chain of
events described below. The low-level sensor in the brine day tank was triggered during Vessel B
regeneration so that the brine transfer pump was turned on to transfer saturated brine from the salt
saturator to refill the day tank. Meanwhile, the level sensor in the salt saturator also reached a low level
so that it called for water to make up more saturated brine. The water filling the salt saturator was
registered on the same totalizer used for flowrate measurements, causing the seemly higher water usage
and flowrates during Vessel B regeneration.
Saturated Brine Usage. As shown in Table 4-9, approximately 360 gal of saturated brine (i.e., 730 Ib of
salt) was used for Vessel A regeneration on September 22, 2005, equivalent to 14.6 Ib of salt/ft3 of resin.
63
-------
Fruitland Vessel A Re gene ration Curve
Brine Draw
(32 min)
Slow Rinse + Fast Rinse
(64 min + 6 min)
100
80
0
10 20 30 40 50 60
Time (min)
70
80 90 100
Fruitland Vessel B Regeneration Curve
Slow Rinse + Fast Rinse
(64 min + 6 min)
-.40,000
IS
O
_,
"S. -E. ^30,000
100
80
60 —
8
40 H
20
0
0 10 20 30 40 50 60 70 80 90 100
Time (min)
Figure 4-23. Vessels A and B Regeneration Curves of Arsenic, Nitrate, and Sulfate
64
-------
Vessel A Regeneration (09/22/05)
100 -
80 -
in
P
40 -
20 -
Brine
0 10 20
Slow Rinse + Fast Rinse
(64 min + 6 min)
-- 9
30 40 50
Time (min)
10
70 80 90 100
100
Vessel B Regeneration (09/22/05)
10
20-
Slow Rinse + Fast Rinse
(64 min + 6 min)
-- 9
-- 7
-- 6
0 10 20 30 40 50 60 70
90 100
Time (min)
Figure 4-24. Vessels A and B Regeneration Curves of TDS and pH
65
-------
Rgeneration Flowrate (09/22/05)
100
90 -
80 -
70 -
60 -
50 -
1 40
30 -
20 -
10 -
0
0
Brine Draw
(32 min)
Slow Rinse + Fast Rinse
(64 min + 6 min)
10
20
30
* Higher flow rate for Vessel B caused by
inclusion of water used to fill salt saturator
40 50 60
Time (min)
70
80
90
100
Figure 4-25. Regeneration Flowrates
This regeneration level was 46% higher than the designed value of 10 Ib of salt/ft3 of resin. For a
throughput setpoint of 316,000 gal, the salt use is 4.6 lb/1,000 gal of water treated. The brine usage was
not recorded for Vessel B because the day tank was refilled automatically in the middle of the brine draw.
Although the 600-gal day tank was sized to supply 500 gal of brine for regeneration of both vessels, it had
to be refilled in the middle of the brine draw due to the higher usage. To track the brine usage by each
vessel, the day tank was refilled manually prior to the regeneration of each vessel and the data are
discussed in Section 4.4.2.3. To reduce the salt usage to close to the design level of 10 lb/ft3, the brine
draw time was shortened from 32 to 25 min and the diluted salt concentration was reduced from 8% to
6% (with the brine draw flowrate remaining unchanged). These modifications brought the regeneration
level down to 9.5 Ib of salt/ft3 of resin (Table 4-8) as discussed in Section 4.4.2.3.
4.5.4 Regeneration Wastewater Sampling. Composite samples were collected from both IX
vessels eight times during each of the three regeneration steps in Study Period I from November 15, 2005,
to July 6, 2006. Table 4-14 summarizes the analytical results. As expected, the majority of arsenic,
nitrate, and sulfate were eluted during brine draw, and more arsenic, nitrate, and sulfate were eluted
during slow rinse than fast rinse. For the eight sampling events, average total arsenic concentrations in
the spent brine were 29 times (on average) those in the slow rinse water. Average total arsenic
concentrations in the slow rinse water were 10 times (on average) those in the fast rinse water. Total
arsenic concentrations in the spent brine (averaged between Vessels A and B) ranged from 3,480 to 9,875
(ig/L and averaged 6,272 (ig/L. Arsenic concentrations in the slow rinse water ranged from 62 to 773
(ig/L and averaged 216 (ig/L. Arsenic concentrations in the fast rinse water were 6 to 34 (ig/L and
averaged 24 (ig/L.
Arsenic, nitrate, and sulfate concentrations measured at each regeneration step and the respective volumes
of the waste stream were used to calculate the mass of arsenic, nitrate, and sulfate recovered during
regeneration. Table 4-15 summarizes the results. Mass of arsenic, nitrate, and sulfate removed from raw
66
-------
Table 4-14. Regeneration Sampling Results in Study Period I
Sampling Event
No.
1
2
3
4
5
6
7
8
Date
11/15/05
01/11/06
02/15/06
04/04/06
04/13/06
05/09/06
06/07/06
07/06/06
Average
Vessel A
Brine Draw
Total As
Hg/L
2,602
3,531
3,930
8,400
6,430
1,272
4,836
5,812
4,602
^«
1
g
mg/L
1,230
1,490
265
176
988
994
979
891
877
Sulfate
mg/L
4,300
9,400
3,000
4,900
12,900
1,810
10,600
12,000
7,364
8
mg/L
-
-
-
-
56,800
59,600
55,500
48,700
55,150
D.
s.u.
-
-
-
-
8.5
8.2
8.3
8.5
8.4
Slow Rinse
Total As
Hg/L
62
199
92
90
204
92
201
235
147
^OJ
1
g
mg/L
22
103
53
77
102
60
136
183
92
Sulfate
mg/L
26
143
46
51.0
132
74
189
2,700
420
s
mg/L
-
-
-
-
8,240
5,080
10,600
12,300
9,055
a
s.u.
.
-
-
-
8.0
7.9
8.2
8.4
8.1
Fast Rinse
Total As
Hg/L
33
29
15
7
28
27
25
23
23
^«
1
g
mg/L
4.4
4.9
4.3
4.3
6.9
7.2
6.6
7.8
5.8
-------
Table 4-15. Mass Balance Calculations for Total Arsenic, Nitrate, and Sulfate
Parameter
Volume of Water Treated
Concentration in Brine Draw
Concentration in Slow Rinse
Concentration in Fast Rinse
Brine Draw Volume
Slow Rinse Volume
Fast Rinse Volume
Mass Recovered from Brine Draw
Mass Recovered from Slow Rinse
Mass Recovered from Fast Rinse
Total Mass Recovered
Average Cone, in wastewater
Mass Removed from Raw Water™
Percent Recovery
Cone. In Composite Brine Draw
Cone. In Composite Slow Rinse
Cone. In Composite Fast Rinse
Brine Draw Volume
Slow Rinse Volume
Fast Rinse Volume
Mass Recovered from Brine Draw
Mass Recovered from Slow Rinse
Mass Recovered from Fast Rinse
Total Mass Recovered
Average Cone, in wastewater
Mass Removed from Raw Water*'
Percent Recovery
Cone. In Composite Brine Draw
Cone. In Composite Slow Rinse
Cone. In Composite Fast Rinse
Brine Draw Volume
Slow Rinse Volume
Fast Rinse Volume
Mass Recovered from Brine Draw
Mass Recovered from Slow Rinse
Mass Recovered from Fast Rinse
Total Mass Recovered
Average Cone, in wastewater
Mass Removed from Raw Water*'
Percent Recovery
Unit
gal
09/22/05
316,000
Vessel
A
Vessel
B
Total
11/15/05
314,000
Vessel
A
Vessel
B
Total
01/11/06
316,000
Vessel
A
Vessel
B
Total
02/15/06
136,000
Vessel
A
Vessel
B
Total
04/04/06
96,000
Vessel
A
Vessel
B
Total
Arsenic Mass Balance
Hg/L
Hg/L
Hg/L
gal
gal
gal
mg
mg
mg
mg
mg/L
mg
%
6,014
293
35
1,149
1,519
383
26,155
1,685
51
27,890
2.4
6,082
271
36
1,149
1,542
359
26,450
1,582
49
28,081
2.4
6,048
-------
Table 4-15. Mass Balance Calculations for Total Arsenic, Nitrate, and Sulfate (Continued)
Parameter
Volume of Water Treated
Concentration in Brine Draw
Concentration in Slow Rinse
Concentration in Fast Rinse
Brine Draw Volume
Slow Rinse Volume
Fast Rinse Volume
Mass Recovered from Brine Draw
Mass Recovered from Slow Rinse
Mass Recovered from Fast Rinse
Total Mass Recovered
Average Cone. In waste water
Mass Removed from Raw Water*'
Percent Recovery
Concentration in Brine Draw
Concentration in Slow Rinse
Concentration in Fast Rinse
Brine Draw Volume
Slow Rinse Volume
Fast Rinse Volume
Mass Recovered from Brine Draw
Mass Recovered from Slow Rinse
Mass Recovered from Fast Rinse
Total Mass Recovered
Average Cone, in waste water
Mass Removed from Raw Water*'
Percent Recovery
Cone, in Composite Brine Draw
Cone, in Composite Slow Rinse
Cone, in Composite Fast Rinse
Brine Draw Volume
Slow Rinse Volume
Fast Rinse Volume
Mass Recovered from Brine Draw
Mass Recovered from Slow Rinse
Mass Recovered from Fast Rinse
Total Mass Recovered
Average Cone, in waste water
Mass Removed from Raw Water*'
Percent Recovery
Unit
gal
04/13/06
316,000
Vessel A
Vessel B
Total
05/09/06
297,000
Vessel A
Vessel B
Total
06/07/06
316,000
Vessel
A
Vessel
B
Total
07/06/06
309,000
Vessel A
Vessel B
Total
Arsenic Mass Balance
Hg/L
Hg/L
Hg/L
gal
gal
gal
mg
mg
mg
mg
mg/L
mg
%
6,430
204
28
1,016
1,400
1,000
24,727
1,081
106
25,914
2.0
4,668
77
39
1,002
1,500
1,000
17,704
437
148
18,288
1.4
5,549
-------
water were calculated using volume of water treated before each regeneration, average concentrations in
raw water, and average concentrations in treated water. Percent recovery of arsenic, nitrate, and sulfate
during regeneration was calculated using Equation 3:
%R=Mrf
(3)
where:
%R = percent recovery
Mrecovered = mass of arsenic, nitrate, or sulfate in regenerant waste (mg or g)
Mremoved = mass of arsenic, nitrate, or sulfate removed from raw water (mg or g)
Note that in addition to the eight monthly sampling events presented in Table 4-14, a set of composite
samples also was collected during the regeneration study on September 22, 2005 and analyzed for total
arsenic, nitrate, and sulfate. Mass balance calculations for the sample collected on September 22, 2005
also are presented in Table 4-15.
According to Table 4-15, 47.2 g of arsenic, 7.9 kg of nitrate, and 79.1kg of sulfate (on average) were
recovered and discharged to the sewer during a regeneration cycle. Average concentrations of arsenic,
nitrate, and sulfate in the waste stream were 1.9 mg/L, 0.31 g/L, and 3.1 g/L, respectively, for the nine
regeneration events presented in Table 4-15. Percent recoveries ranged 63% to 165% (averaged 116%,
not including an outlier on April 4, 2006) for arsenic, 99% to 235% (averaged 161%) for nitrate, and 73%
to 198% for sulfate (averaged 128%, not including an outlier on July 6, 2006). The percent recovery for
an IX system was reported to be 85% to 100% in the literature (Clifford, 1999).
4.5.5 Analyses of Fouled IX Resin. The IX resin samples taken especially from Vessel B were
visibly fouled with particulate and organic matter when viewed under a microscope. Table 4-16 presents
the analytical results provided by Purolite. Fouling resulted in significant losses in volumetric capacity,
with 19% and 35% reduction observed for Vessels A and B, respectively (when compared with Purolite's
A300E specifications). The reduction in resin capacity also was reflected by lower strong base capacity
(24% and 18%, respectively) and lower moisture content.
Table 4-16. IX Resin Analysis Results
Parameter
Moisture Content (%)
Volumetric Capacity (eq/L)
Volumetric Capacity (%)(a)
Strong Base Capacity (%)
TOC Fouling (mg of C/g of resin)
Purolite
A300E
Specs
40-45
1.4
-
100
NA
After
Normal Brine
Cleaning
Vessel
A
42
1.14
81
76
7.9
Vessel
B
38.3
0.91
65
82
12.7
After
Laboratory
Caustic/Brine
Cleaning
Vessel
A
41.8
1.2
86
94
7.2
Vessel
B
40.7
1.13
81
93
8.4
After Field
Caustic/Brine
cleaning
Vessel
B
41
1.24
88
84.1
4.0
(a) % = actual volumetric capacity/virgin volumetric capacity.
TOC = total organic carbon.
After laboratory cleaning, volumetric and strong base capacities improved significantly (to 86 and 81 %
for volumetric capacity and 94% and 93% for strong base capacity). TOC contents also were reduced
from 7.9-12.7 to 7.2-8.4 mg of C/g of resin.
70
-------
Table 4-16 also presents the analytical results of the core sample taken from Vessel B upon completion of
field caustic/brine cleaning. As shown in the table, field caustic/brine cleaning achieved somewhat
similar results to laboratory cleaning. The TOC content was reduced to 4 mg of C/g of resin, a level
viewed by Purolite as moderate fouling (i.e., <5 mg of C/g of resin).
Although the data showed some effectiveness of field cleaning, the IX resin run length for arsenic
removal did not improve. The throughput setpoint was scaled back from 275,000 gal before cleaning to
260,000 gal on July 7, 2007, after cleaning. It was reduced further to 220,000 gal on October 16, 2007
after the operator detected 10.3 mg/L of nitrate (as N) in samples collected at 233,000 gal.
4.5.6 Distribution System Water Sampling. Table 4-17 summarizes the results of the
distribution system sampling. The stagnation times for the first draw samples ranged from 5.8 to 24 hr,
which met the requirements of the EPA LCR sampling protocol (EPA, 2002).
During baseline sampling from December 2003 to March 2004, the old well (Well No. 6) was not in
service due to its higher-than-MCL nitrate concentrations; the distribution system was supplied by other
wells. Well No. 6-2004 was drilled in May 2004 and put online with the IX treatment system in June
2005. Since then, monthly distribution sampling resumed at the same locations to evaluate impacts of the
treatment system, if any, on the distribution water quality. Due to the use of a new well, different water
quality could become an issue. For example, average nitrate, alkalinity, and total Mn concentrations were
lower in the baseline samples than at inlet to the IX system (see Tables 4-12 and 13). In addition, the
average arsenic concentration (65 ug/L) of the baseline samples was higher than that (42.5 ug/L) in the
well samples.
Figure 4-26 compares arsenic concentrations measured in distribution system water and in system
effluent. Note that results of flushed samples at DS1 and DS2 were plotted because flushed samples
should be more representative of the plant effulent. Because no flushed samples were collected at DS3,
first draw samples were plotted in Figure 4-26. In general, total arsenic concentrations measured at DS1
and DS3 mirrored those in system effluent, except two apparent outliers measured at DS3 on October 26,
2005, and June 14, 2006. However, more than 50% of the data collected at DS2 had arsenic
concentrations significantly higher than those in system effluent, including some having arsenic
concentrations close to those in source water. It was suspected that DS2 might have received water from
other source wells at the time of sampling. During Study Period I, arsenic levels at DS1 and DS3 were
significantly reduced to below MCL when the IX system operated normally. Higher-than-MCL
concentrations were measured during the first two sampling events (June 29 and August 3, 2005) when
the system experienced operational problems.
No significant changes in pH values were observed in the distribution samples. pH values ranged from
7.3 to 7.7 in the baseline samples and 7.3 to 8.2 after system startup. On four occasions when the plant
effluent had a pH value below 7 (i.e., pH 6.0 on July 6, 2005; pH 6.8 on August 31, 2005; pH 6.9 on
February 1, 2006; and pH 6.3 on May 9, 2006), distribution samples were not collected. Therefore, there
was lack of evidence on whether low water pH produced by the freshly regenerated IX resin would
impact the pH in the distribution system. Alkalinity levels ranged from 200 to 304 mg/L and averaged
270 mg/L (as CaCO3) in the baseline samples. After system startup, alkalinity levels ranged from 198 to
467 mg/L (as CaCO3) and averaged 358 mg/L (as CaCO3). The higher values observed were likely
caused by the different water quality of the supply wells as discussed above. The freshly regenerated IX
system would reduce alkalinity for a short period of time due to exchange of bicarbonates onto the IX
resin. Unfortunately, no distribution water samples were taken when the plant effluent contained low
alkalinity.
71
-------
Table 4-17. Summary of Distribution System Sampling Results in Period I Demonstration Study at City of Fruitland
Sampling
Event
BLl
BL2
BL3
BL4
1
2
3
4
5
6
7
8
9
10
11
12
13
14
12/08/03
01/06/04
02/02/04
03/02/04
06/29/05
08/03/05
08/24/05
09/21/05
10/26/05
11/30/05
12/15/05
01/25/06
02/22/06
03/23/06
04/19/06
05/24/06
06/14/06
07/12/06
DS1
409 S Utah
Non-Residence
1st Draw
0)
H
C
o
1
M
sS
•^
t/3
NA
NA
NA
10.3
10.8
9.7
NA
NA
NA
12.5
NA
12.3
10.8
9.5
10.8
9.5
9.3
8.0
M
7.7
7.3
7.4
7.6
7.6
7.4
7.5
7.6
7.7
7.9
7.8
7.4
7.8
7.9
7.6
7.6
7.6
7.6
Alkalinity
264
292
258
279
383
374
427
396
440
431
462
352
357
435
278
456
467
NA
%
O
z
5 5
7.4
7.9
9.9
NA
NA
NA
NA
NA
NA
1.7
2.5
6.7
11.5
6.0
8.1
1.6
4.3
Flushed(a)
M
PI
NS
7.7
7.7
7.6
7.5
7.6
7.6
7.4
7.7
7.7
7.5
7.7
7.9
7.7
8.2
7.8
7.3
7.8
Alkalinity
NS
292
256
288
396
396
449
374
444
308
180
374
428
294
260
444
467
NA
O
z
NS
7.8
7.7
6.9
NA
NA
NA
NA
NA
NA
4.0
9.8
7.7
7.3
5.6
8.0
3 2
0.8
DS3
519 S Utah
Non-LCR
1st Draw
Stagnation Time
7.5
8.0
7.0
5.8
9.0
9.5
NA
NA
NA
12.3
NA
12.2
11.8
10.3
11.0
NA
9.8
NA
M
PI
7.8
7.8
7.7
7.6
7.5
7.5
7.7
7.4
7.7
7.7
7.4
7.5
7.9
8.2
7.6
7.8
7.6
7.6
Alkalinity
246
280
200
288
387
378
427
392
264
427
312
356
440
419
366
464
433
431
5«
^
45.9
58.5
43.9
73.7
42.6
42.9
2.0
2.7
17.7
3.3
4.7
3.8
2.7
2.9
1.9
3.5
11.4
1.9
£
<25
<25
26.0
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
I
<0.1
0.6
0.5
0.2
11.6
20.9
19.7
22.1
2.3
15.6
16.9
7.6
1.6
0.6
0.3
<0.1
0.2
0.3
.a
PH
0.3
0.7
0.8
0.2
0.5
0.4
0.2
0.6
0.10
0.05
<0.1
<0.1
<0.1
0.3
0.4
0.8
2.0
0.8
U
86.2
178
122
237
188
25.5
24.4
86.3
37.6
24.1
41.2
35.4
43.7
28.9
59.7
74.8
65.1
89.0
f>
O
z
4.6
7.4
5.7
7.9
NA
NA
NA
NA
NA
NA
1.6
1.4
9.3
12.0
2.3
5.1
1.3
1.6
(a) Stagnation times not applicable for flushed samples.
BL = baseline sampling; NS = not sampled; NA = data not available
Lead action level =15 |ig/L; copper action level =1.3 mg/L
Unit for analytical parameters is |ig/L except for pH and alkalinity (mg/L as CaCO3).
-------
Reduction in lead and copper levels was observed in the first draw samples at DS1 and DS2. For
example, before system startup, average lead concentrations in the first draw samples were 9.4, 8.3, and
0.5 ug/L at DS1, DS2, and DS3, respectively. After system startup, the concentrations were reduced to
3.4, 2.4, and 0.5 ug/L, respectively. Similarly, before system startup, average copper concentrations in
the first draw samples were 115, 231, and 156 ug/L at DS 1, DS2, and DS3, respectively. After system
startup, the concentrations were reduced to 45, 98, and 80 ug/L, respectively. Therefore, the lead and
copper levels in the distribution system appeared to be lowered by the operation of the IX system.
60
t>
* \
a
A
<>
0 DS1-Flushed
A DS3-1st Draw
^*-TB
n
I
I * °
I
a
D
D
^ 8
L-i^^i-^^br^^-L* * * ^
f~~-^W~~--^-~-^9 0 -°;:^0^==g=_ J g__ — 0
/ ^ 0T>M ^ ^ ^ $ ^
4.6
Figure 4-26. Comparsion of Total Arsenic Concentrations in Distribution System
Water and Treatment Plant Effluent
System Cost
The cost of the system was evaluated based on the capital cost per gpm (or gpd) of design capacity and
the O&M cost per 1,000 gal of water treated. This required tracking of the capital cost for the treatment
equipment, site engineering, and installation and the O&M cost for salt supply, electricity consumption,
and labor. The cost associated with the new building, sanitary sewer connection, and other discharge-
related infrastructure was not included in the capital cost because it was out of the scope of the
demonstration project, and was funded separately by the City of Fruitland.
4.6.1 Capital Cost. The capital investment for the Fruitland IX system was $286,388, which
included $173,195 for equipment, $35,619 for site engineering, and $77,574 for installation. Table 4-18
presents breakdowns of the capital cost provided by the vendor. The equipment cost included the cost for
the IX resin, filter skid, vessels, brine system, pre-filters, air compressor, instrumentation and controls,
engineering subcontractor, labor, and system warranty. The system warranty covered repairs and/or
replacement of any equipment or installation workmanship for a period of 12 months after system startup.
The equipment cost was 61% of the total capital investment.
73
-------
Table 4-18. Cost Breakdowns of Capital Investment for Fruitland IX System
Description
EC
IX Resin, Filter Skid, and Vessels
Brine System
Pre-treatment Filters
Air Compressor
Instrumentation & Controls
Engineering Subcontractor
Labor
Warranty
Equipment Total
Quantity
Cost
% of Capital
Investment Cost
luipment Cost
1
1
1
1
1
1
-
-
-
$63,673
$35,388
$3,540
$1,295
$11,524
$8,000
$32,870
$16,905
$173,195
-
-
-
-
-
-
61%
Engineering Cost
Labor
Engineering Total
-
-
$35,619
$35,619
-
12%
Installation Cost
Labor
Travel
Subcontractor
Installation Total
Total Capital Investment
-
-
-
-
-
$11,524
$4,095
$61,955
$77,574
$286,388
-
-
-
27%
100%
The site engineering cost included the cost for preparing a process design report and the required
engineering plans, including a general arrangement drawing, piping and instrumentation diagrams
(P&IDs), inter-connecting piping layouts, vessel fill details, a schematic of the PLC panel, an electrical
on-line diagram, and other associated drawings. After being certified and stamped by an Idaho-registered
professional engineer, the plans were submitted to IDEQ for permit review and approval. The
engineering cost was 12% of the total capital investment.
The installation cost included the cost for labor and materials for system unloading and anchoring,
plumbing, and mechanical and electrical connections (see Section 4.3). The installation cost was 27% of
the total capital investment.
The total capital cost of $286,388 was normalized to the system's rated capacity of 250 gpm (360,000
gpd), which resulted in $1,146 per gpm ($0.80 per gpd). The capital cost also was converted to an
annualized cost of $27,032/yr using a capital recovery factor of 0.09439 based on a 7% interest rate and a
20-year return. Assuming that the system operated 24 hr/day, 7 day/wk at the design flowrate of 250 gpm
to produce 131 million gal of water per year, the unit capital cost would be $0.21/1,000 gal. In fact, the
system operated an average of 17.4 hr/day at 157 gpm (see Table 4-7), producing 65.4 million gal of
water during the first 13-month demonstration study. At this reduced rate of operation, the unit capital
cost increased to $0.47/1,000 gal.
The City of Fruitland constructed an addition to its existing pump house to house the IX system. The 17-
ft tall addition covered 360 ft2 of floor space with a wood frame and steel siding and roofing, and a roll-up
door. The total cost for the material and electrical was approximately $18,000.
4.6.2 Operation and Maintenance Cost. The O&M cost included the cost associated with salt
supply, electricity consumption, and labor, as summarized in Table 4-19. Morton solar salt was used to
prepare brine solution for the resin regeneration. Over the first year of the demonstration study, a total of
74
-------
253,835 Ib of salt was consumed to treat 57,373,000 gal of water. The salt delivery charge totaled
$28,109 for the same period, which included fuel surcharges of $50 per delivery starting in October 2005.
The average salt use was 4.42 lb/1,000 gal, which corresponded to a salt cost of $0.49/1,000 gal.
However, this higher-than-expected salt usage was caused by improper flow control of the brine draw
during the initial regenerations as discussed in Section 4.4.2 and Table 4-10. If the target salt usage of
3.16 lb/1,000 gal was achieved, the salt cost would have been reduced to $0.35/1,000 gal.
Incremental electricity consumption associated with the IX system was not available, but was assumed to
be minimal. The actual power usage for operating the entire plant was obtained from utility bills and used
to estimate the electricity cost at $0.08/1,000 gal of water treated. The routine, non-demonstration related
labor activities consumed about 30 min/day, as noted in Section 4.4.4. Based on this time commitment
and a labor rate of $21/hr, the labor cost was estimated at $0.05/1,000 gal of water treated. In summary,
the total O&M cost was approximately $0.62/1,000 gal based on the actual salt usage and $0.49/1,000 gal
based on the target salt usage.
Table 4-19. O&M Cost for Fruitland, ID Treatment System
Cost Category
Annual Volume Processed (1,000 gal)
Value
57,373
Assumptions
From lune 14, 2005, through June 14, 2006
Salt Usage
Salt Unit Price ($/lb)
Total Salt Usage (Ib)
Salt Use (lb/1,000 gal)
Total Salt Cost ($)
Unit Salt Use Cost ($/l,000 gal)
0.11
253,835
4.42
28,109
0.49
Unit price increased progressively from $0.095
to$0.10and$0.11/lb
Quantity delivered
-
Based on total invoiced amounts, including a
$50 monthly fee for fuel surcharge
Based on target salt usage of 3. 16 lb/1,000 gal;
salt cost would be $0.35/1,000 gal
Electricity Consumption
Power Use ($/l, 000 gal)
0.08
Based on utility bills for entire treatment plant
Labor
Average Weekly Labor Hours (hr/wk)
Total Labor Hours (hr/year)
Total Labor Cost ($/year)
Labor Cost ($/l, 000 gal)
Total O&M Cost/1,000 gal
2.5
130
2,730
0.05
0.62
30 min/day; 5 day/wk
-
Labor rate = $2 1/hr
-
-
75
-------
5.0 REFERENCES
Battelle. 2003. Revised Quality Assurance Project Plan for Evaluation of Arsenic Removal Technology.
Prepared under Contract No. 68-C-00-185, Task Order No.0019, for U.S. Environmental
Protection Agency, National Risk Management Research Laboratory, Cincinnati, OH.
Battelle. 2004. Final System Performance Evaluation Study Plan: U.S. EPA Demonstration of Arsenic
Removal Technology at Climax, MN. Prepared under Contract No. 68-C-00-185, Task Order No.
0019 for U.S. Environmental Protection Agency, National Risk Management Research
Laboratory, Cincinnati, OH.
Chen, A., L. Wang, J. Oxenham, and W. Condit. 2004. Capital Costs of Arsenic Removal Technologies:
U.S. EPA Arsenic Removal Technology Demonstration Program Round 1. EPA/600/R-04/201.
U.S. Environmental Protection Agency, National Risk Management Research Laboratory,
Cincinnati, OH.
Clifford, D.A. 2006. Personal Communication.
Clifford, D.A. 1999. "Ion Exchange and Inorganic Adsorption." R. Letterman, ed., Water Quality and
Treatment, fifth edition, McGraw Hill, Inc., New York, NY.
Edwards, M., S. Patel, L. McNeill, H. Chen, M. Frey, A.D. Eaton, R.C. Antweiler, and H.E. Taylor.
1998. "Considerations in As Analysis and Speciation" JAWWA (March): 103-113.
EPA. 2001. National Primary Drinking Water Regulations: Arsenic and Clarifications to Compliance and
New Source Contaminants Monitoring. Federal Register, 40 CFR Parts 9, 141, and 142.
EPA. 2002. Lead and Copper Monitoring and Reporting Guidance for Public Water Systems.
EPA/816/R-02/009. U.S. Environmental Protection Agency, Office of Water, Washington, DC.
EPA. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic. Federal
Register, 40 CFR Part 141.
Ghurye, G.L., D.A. Clifford, and A.R. Tripp. 1999. "Combined Arsenic and Nitrate Removal by Ion
Exchange." JAWWA, 91(10): 85-96.
Kinetico. 2004. Operation and Maintenance Manual, Macrolite® Model FM-236-AS, Climax, Minnesota
Water Department.
Sorg, T.J. 2002. "Iron Treatment for Arsenic Removal Neglected." Opflow, AWWA, 28(11): 15.
Wang, L., W.E. Condit, and A.S.C. Chen. 2004. Technology Selection and System Design: U.S. EPA
Arsenic Removal Technology Demonstration Program Round 1. EPA/600/R-05/001. U.S.
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
Wang , L., A.S.C. Chen, T.J. Sorg, and K.A. Fields. 2002. "Field Evaluation of As Removal by IX and
C\ JAWWA, 94 1. (4): 161-173.
76
-------
APPENDIX A
A SUMMARY OF MAJOR SYSTEM OPERATIONAL PROBLEMS
-------
Fruitland IX System Chronology and Operational Problems
Date
06/14/05
06/14/05 to
07/07/05
06/15/05
06/18/05 to
06/29/05
08/03/05
09/22/05 to
09/23/05
August 2005,
to the end of
demonstration
study
07/25/06
08/09/06 to
08/11/06
Problem Encountered
Corrective Action
The demonstration study started.
System experienced low flow and elevated pressure loss.
Brine transfer pump malfunctioned.
After a power outage, IX system restarted but failed to initiate
regeneration because brine transfer pump had been reset to
"off; PLC returned to default "counter-current" regeneration
instead of "co -current".
Regeneration failed to occur after treating 534,000 gal of water
due to a broken low level sensor in brine day tank.
Brine draw rate and consumption rate were measured higher
than setting values.
Initial As and nitrate leakage during a service run was first
noticed in the water samples collected in August 2005. The run
length studies conducted on December 7 to 8, 2005 and April
11-12, 2006 also clearly indicated early leakage of arsenic and
nitrate (Section 4.5.2). The initial leakage persisted during the
demonstration study, and had reached as high as 40.5 ug/L of
arsenic on 02/0 1/06.
Flow restrictors were modified and subsequently replaced with blank pipe
sections on 07/07/05.
Pump was fixed on the same day by operator.
PLC setting was changed back to "co-current" on 06/29/05; an uninterrupted
power supply (UPS) was installed on 07/26/05 to provide back-up power.
Level sensor was fixed on the same day by operator.
On 12/05/05, brine draw time was shortened (from 32 to 25 min), slow rinse
time was reduced (from 60 to 40min), and fast rinse time was extended
(from 6 to 15 min) followed the instruction from Kinetico as a quick-and-
easy way to lower salt usage.
A series of efforts made to fix the problem was unsuccessful. Initial As and
nitrate leakages were not eliminated through the end of demonstration study.
The efforts made included:
• Replaced a brine eductor with a large one in March 2006 to obtain a
higher brine draw flow rate.
• Switched from co-current to counter-current regeneration from 07/25/06
to 06/18/07.
• Cleaned the resin with caustic and brine mixture on 06/21/07.
The system was switched to counter-current regeneration mode.
After switched from co-current to counter-current regeneration
on July 25, 2006, a run length study was conducted on August 9
to 10, 2006. Arsenic concentration in the effluent of Vessel B
was above MCL of 10 ug/L during the entire run length study,
with concentrations as high as 129 ug/L of As and 17.6 mg/L of
nitrate in the treated water (Figure 4-20).
• The system was shutdown on 08/18/06.
• On 09/05/06, system was changed back to co-current regeneration
temporarily. The results indicated proper regeneration could be obtained
in co-current mode.
• Kinetico suspected that incomplete regeneration was due to fluctuating
pressure that caused eductor not to work properly; thus, a regeneration
pump was installed on 10/24/06 to replace eductor to inject brine into the
vessels during regeneration.
-------
Fruitland IX System Chronology and Operational Problems (Continued)
Date
08/18/06 to
12/05/06
09/18/06
12/05/06
01/03/07 to
2/13/07
02/09/07
03/14/07
03/22/07
05/07/07
Problem Encountered
Corrective Action
The treatment system was taken offline to resolve the problems of significant arsenic and nitrate breakthrough caused by incomplete regeneration.
OIP screen was broken.
On 10/17/06, broken OIP screen was fixed by Kinetico.
The treatment system was resumed online after being generated twice in counter-current mode.
Higher than MCL levels of As and/or nitrate were detected in
system effluent during service runs:
• On 01/03/07, samples collected at 107,000 gal of throughput had
44 ug/L of As and 8.7 mg/L of nitrate, similar to raw water
quality.
• On 01/18/07, samples collected from a service run showed raw
water quality.
• A run length study was conducted on January 17 to 18, 2007.
The analytical results showed little or no arsenic/nitrate removal
in the effluent water from both Vessels A and B during the entire
run length study (Figure 4-20).
• On 02/01/07, samples collected at 232,000 gal showed less than
detection limit of As, but 14 mg/L of nitrate.
• On 02/07/07, samples collected at 224,000 gal showed less than
detection limit of As, but 13 mg/L of nitrate.
• On 02/13/07, system was shutdown. IDEQ requested a Public Notice to
be issued.
• On 02/21/07, Battelle, EPA, and Kinetico representatives had a meeting in
Columbus to discuss the performance issues with the IX system.
• 02/26/07-03/07/07: Kinetico 's technician made changes to the system
based on the decisions of the meeting on February 21, 2007, including:
• Taken out the eductor, which was left in the system when switched to the
brine injection pump on 10/24/06, and replaced it with a tee.
• Loaded additional packing media into the vessels, since the resin bed was
found not packed.
Daily operational data collection was discontinued. Since then through the end of demonstration study on February 11, 2008, the operational data
was recorded only twice on April 3 and 5, 2007.
The regeneration throughput setpoint was reduced from 3 16,000 gal to 275,000 gal.
System was manually regenerated at counter-current regeneration
mode. Regeneration flowrate for each step, however, was low
compared to the previous readings.
No response from the vendor about the low regeneration flowrate.
A online real-time arsenic analyzer, ArsenicGuard, was installed by TraceDetect to monitor total arsenic concentration in system effluent.
>
-------
Fruitland IX System Chronology and Operational Problems (Continued)
Date
Problem Encountered
Corrective Action
04/12/07 to
05/14/07
>
High As and nitrate concentrations were detected in system
effluent during service runs:
• On 04/04/07, sample collected at 204,000 gal throughput showed
13.8 mg/L of nitrate, the system was taken offline immediately.
• On 04/13/07, system was back on-line after manual regeneration.
Sample collected at 28,000 gal showed 11.8 mg/L of nitrate,
system was shutdown immediately.
• On 05/09/07, a sample taken at 149,000 gal of water treated had
a nitrate concentration of 13.6 mg/L (as N).
• From 05/09/07 to 05/14/07, monitoring data by ArsenicGuard
showed high arsenic concentrations in system effluent during
service runs.
It was suspected that the poor system performance was due to resin
fouling.
On 4/17/07, source water was collected, the result showed TOC, was
slightly lower than the historic data, and other analytes were comparable
to those measured previously, suggesting that the poor system
performance and the suspected resin fouling would not have been caused
by any changes in water quality.
On 05/18/07, a conference call was held with EPA, Kinetico, and the
facility to discuss various issues with the IX system.
- Kinetico concurred that various mechanical issues associated with the
brine injection system that caused improper resin regeneration for an
extended period of time (i.e., since July 2006 after the system was
switched from co- to counter-current regeneration) might have
resulted in the suspected resin fouling.
- Kinetico proposed to clean the resin with a 5% NaOH and 10% brine
mixture followed by regular co-current regeneration.
- Kinetico also decided to switch back to co-current regeneration due to
difficulties encountered in the counter-current regeneration mode.
06/18/07 to
06/21/07
Kinetico personnel were on-site to perform resin cleaning using caustic and brine mixture.
• Resin cleaning was conducted on both vessels on June 19, 2007.
• Upon completion on cleaning, a core sample was taken from Vessel B. The resin analysis results on the core sample indicated the field cleaned
resin had over 88% of its exchange capacity. The TOC content on the resin was reduced from the original 7.9 to 4 mg carbon per gram resin,
which represents going from severe to moderate fouling.
• System was switched back to co-current regeneration mode.
• The resin run length for arsenic removal after the caustic brine cleaning, however, did not improve.
06/26/07
The automatic regeneration failed on June 26, 2007. Samples
collected at 21,000 gal throughput contained 12.7 ug/L of nitrate
(as N) and 29.8 ug/L of arsenic.
• The system was turned off on June 26, 2007.
• On June 27, 2007, the plant operator manually triggered regeneration.
The regeneration was successful. A sample taken at 94,000 gal
throughput contained 4.8 mg/L of nitrate (as N).
-------
Fruitland IX System Chronology and Operational Problems (Continued)
Date
07/02/07 to
07/05/07
08/20/07 to
08/27/07
Early
09/2007
09/0 1/07 to
10/18/07
10/16/07
02/11/08
Problem Encountered
Consistently high nitrate concentrations were measured on July 2,
3, and 5, 2007, i.e., 12.7 mg/L (at 145,000 gal), 12.1 mg/L (at
10,000 gal), and 12.9 mg/L (at 160,000 gal), respectively.
Corrective Action
• The system was shutdown on July 5, 2007.
• Kinetico suspected that the system was not regenerated properly due to the
problematic, newly installed brine injection pump.
• The plant operator switched back to the old brine injection pump
• On July 7, 2007, the regeneration throughput setpoint was reduced from
275,000 to 260,000 gal.
- One or two water samples were collected daily to monitor the nitrate
concentrations. The nitrate concentrations were higher during the
beginning and end of the run, but all below 10 mg/L (as N).
- The arsenic concentrations monitored by the ArsenicGuard were below
10 ng/L most of the time, except during the beginning and end of the
run, which suggests that the early leakage still exists and that the run
length needs to be further shortened.
The City turned off the IX system due to a suspicion that the salt might be causing some problems with the biological activities in the lagoons.
The IX system was shut down to lower the salt discharge to see if it would change the water quality at the lagoon.
The system was placed back on line in early September and ran about 3 hours a day on average.
Due to a clogged sample pressure regulator, the ArsenicGuard did
not work properly. Arsenic data were unavailable for the period.
On October 18, 2007, the ArsenicGuard was repaired by TraceDetect.
The regeneration throughput setpoint was further reduced from 260,000 gal to 220,000 gal, after the operator detected 10.3 mg/L of nitrate in
samples collected at 233,000 gal throughput.
The equipment transfer letter was approved and signed by the City Council.
>
-------
APPENDIX B
OPERATIONAL DATA
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation Log Sheet
1
2
3
4
5
6
Date
06/14/05
06/15/05
06/16/05
06/17/05
06/20/05
06/21/05
06/22/05
06/23/05
06/27/05
06/28/05
06/29/05
06/30/05
07/01/05
07/05/05
07/06/05
07/07/05
07/08/05
07/11/05
07/12/05
07/13/05
07/14/05
07/15/05
07/18/05
07/19/05
07/20/05
07/21/05
07/22/05
Pump House
Opt.
Hours
hr
NA
22.4
24.2
15.5
56.4
22.0
21.1
16.2
88.1
22.0
8.4
20.6
21.4
93.2
25.0
24.0
20.4
66.0
23.9
23.1
24.3
24.0
72.0
23.5
23.5
23.7
23.7
Cum.
Hours
hr
NA
22.4
46.6
62.1
118.5
140.5
161.6
177.8
265.9
287.9
296.3
316.9
338.3
431.5
456.5
480.5
500.9
566.9
590.8
613.9
638.2
662.2
734.2
757.7
781.2
804.9
828.6
Master
Flow
Meter
kgal
80,712
80,866
81,067
81,197
81,666
81,838
82,031
82,195
83,028
83,237
83,315
83,516
83,704
84,620
84,851
85,085
85,288
85,908
86,144
86,386
86,632
86,869
87,594
87,830
88,067
88,307
88,545
Treated
Volume
Kgal
NA
154
201
130
469
172
193
164
833
209
78
201
188
916
231
234
203
620
236
242
246
237
725
236
237
240
238
Product Water Flow Meter
Product
Water
Flow rate
gpm
130
144
73
142
142
142
170
171
167
155
156
160
150
167
165
122
164
163
168
170
170
168
164
167
169
167
167
Product
Water
Flow
Totalizer
kgal
111
37
NA
122
341
100
58
212
98
72
147
127
77
34
24
18
211
109
99
94
94
85
70
62
52
47
43
BV
Treated
BV
148
49
In
Regen
163
456
134
78
283
131
96
197
170
103
45
32
24
282
146
132
126
126
114
94
83
70
63
57
System Pressures
Combined
System
Inlet
Pressure
ON)
psig
74
72
84
73
64
65
52
62
63
62
64
62
60
62
60
70
60
60
60
60
60
60
60
60
60
60
58
Vessel A
Outlet
Pressure
(TA)
psig
65
64
78
68
62
62
52
58
55
58
56
56
54
56
54
60
52
54
50
48
48
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
62
62
In Regen
65
70
70
62
58
56
58
58
56
52
54
54
In Regen
52
54
50
48
48
50
48
48
50
50
50
Product
Water
Pressure
(TT)
psig
44
44
42
46
44
44
46
46
45
50
48
46
44
46
46
40
44
46
46
45
44
48
42
44
48
48
48
Regeneration
Regen.
Counter
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
13
14
15
15
18
19
20
21
22
25
26
27
28
29
Salt
Delivered
Ib
3,945
3,950
5,000
8,860
6,470
Cumulative
Salt
Delivered
Ib
3,945
7,895
12,895
21,755
28,225
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation Log Sheet (Continued)
7
8
9
10
11
12
13
Date
07/25/05
07/26/05
07/27/05
07/28/05
07/29/05
08/01/05
08/02/05
08/03/05
08/04/05
08/05/05
08/08/05
08/09/05
08/10/05
08/11/05
08/12/05
08/15/05
08/16/05
08/17/05
08/18/05
08/19/05
08/22/05
08/23/05
08/24/05
08/25/05
08/26/05
08/29/05
08/30/05
08/31/05
09/01/05
09/02/05
09/06/05
09/07/05
09/08/05
09/09/05
Pump House
Opt.
Hours
hr
69.5
23.2
23.6
24.0
49.9
42.8
23.3
23.2
24.4
21.0
72.0
23.8
23.9
22.0
23.8
69.5
23.5
24.4
21.8
23.7
68.9
22.8
23.3
22.7
23.2
70.5
22.7
23.3
23.0
23.3
87.4
23.1
22.1
21.5
Cum.
Hours
hr
898.1
921.3
944.9
968.9
1018.8
1061.6
1084.9
1108.1
1132.5
1153.5
1225.5
1249.3
1273.2
1295.2
1319.0
1388.5
1412.0
1436.4
1458.2
1481.9
1550.8
1573.6
1596.9
1619.6
1642.8
1713.3
1736.0
1759.3
1782.3
1805.6
1893.0
1916.1
1938.2
1959.7
Master
Flow
Meter
kgal
89,225
89,454
89,678
89,901
90,139
90,842
91,077
NM
91,543
91,760
92,387
92,631
92,882
93,111
93,349
93,984
94,223
94,477
94,699
94,939
95,626
95,846
96,078
96,294
96,520
97,179
97,411
97,652
97,893
98,131
99,035
99,267
99,487
99,696
Treated
Volume
Kgal
680
229
224
223
238
703
235
NA
466
217
627
244
251
229
238
635
239
254
222
240
687
220
232
216
226
659
232
241
241
238
904
232
220
209
Product Water Flow Meter
Product
Water
Flow rate
gpm
129
127
154
160
165
161
159
161
163
155
138
178
138
168
163
109
175
173
133
167
161
161
158
162
158
147
170
139
170
169
170
161
130
157
Product
Water
Flow
Totalizer
kgal
2
218
197
175
168
90
314
534
124
332
232
115
4
223
103
7
234
120
336
215
169
37
259
117
332
258
128
5
237
114
274
145
3
265
BV
Treated
BV
3
291
263
234
225
120
420
714
166
444
310
154
5
298
138
9
313
160
449
287
226
49
346
156
444
345
171
7
317
152
366
194
4
354
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
66
66
60
58
62
58
58
58
58
58
52
58
68
58
58
62
60
58
70
60
60
60
60
60
58
58
58
70
58
58
58
59
68
58
Vessel A
Outlet
Pressure
(TA)
Psig
50
In Regen
50
50
52
50
50
50
50
50
50
50
50
50
50
50
50
50
In Regen
60
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
In Regen
48
50
48
52
50
50
50
50
50
50
50
In Regen
50
50
In Regen
50
50
50
50
50
50
50
50
50
50
50
In Regen
50
50
50
50
In Regen
50
Product
Water
Pressure
(TT)
psig
44
44
46
42
46
48
46
46
46
46
42
44
46
46
46
46
46
46
46
46
46
46
48
46
48
46
46
44
46
46
48
48
48
48
Regeneration
Regen.
Counter
32
33
33
34
35
37
37
37
38
38
40
41
42
42
43
45
45
46
47
47
49
50
50
51
51
53
54
55
55
56
58
59
60
60
Salt
Delivered
Ib
9,035
8,970
3,985
5,485
6,010
3,205
8,425
8,025
5,860
Cumulative
Salt
Delivered
Ib
37,260
46,230
50,215
55,700
61,710
64,915
73,340
81,365
87,225
Cd
to
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation Log Sheet (Continued)
14
15
16
17
18
19
20
Date
09/12/05
09/13/05
09/14/05
09/15/05
09/16/05
09/19/05
09/20/05
09/21/05
09/22/05
09/23/05
09/26/05
09/27/05
09/28/05
09/29/05
09/30/05
10/03/05
10/04/05
10/05/05
10/06/05
10/07/05
10/11/05
10/12/05
10/13/05
10/14/05
10/17/05
10/18/05
10/19/05
10/20/05
10/21/05
10/24/05
10/25/05
10/26/05
10/27/05
10/28/05
Pump House
Opt.
Hours
hr
65.9
22.9
18.7
27.8
21.7
61.9
21.8
22.2
16.8
22.3
73.9
24.3
14.3
11.9
16.5
51.4
20.9
18.8
24.1
20.6
69.7
17.1
14.0
5.3
39.3
16.2
14.8
17.7
4.0
38.7
18.4
21.3
18.9
18.2
Cum.
Hours
hr
2025.6
2048.5
2067.2
2095.0
2116.7
2178.6
2200.4
2222.6
2239.4
2261.7
2335.6
2359.9
2374.2
2386.1
2402.6
2454.0
2474.9
2493.7
2517.8
2538.4
2608.1
2625.2
2639.2
2644.5
2683.8
2700.0
2714.8
2732.5
2736.5
2775.2
2793.6
2814.9
2833.8
2852.0
Master
Flow
Meter
kgal
100,303
100,547
100,802
101,025
101,255
101,904
102,129
102,356
102,534
102,760
103,511
103,757
103,906
104,018
104,193
104,753
104,943
105,133
105,367
105,566
106,296
106,475
106,624
106,678
107,094
107,264
107,415
107,630
107,640
108,050
108,243
108,463
108,661
108,846
Treated
Volume
Kgal
607
244
255
223
230
649
225
227
178
226
751
246
149
112
175
560
190
190
234
199
730
179
149
54
416
170
151
215
10
410
193
220
198
185
Product Water Flow Meter
Product
Water
Flow rate
gpm
140
175
171
168
165
175
170
170
170
164
170
170
170
170
174
167
125
165
165
147
167
173
173
179
170
169
170
170
170
145
170
164
173
168
Product
Water
Flow
Totalizer
kgal
81
314
209
73
294
216
106
130
300
187
264
172
314
94
261
127
NA
179
74
262
302
143
286
11
80
244
59
239
280
108
192
196
58
235
BV
Treated
BV
108
420
279
98
393
289
142
174
401
250
353
230
420
126
349
170
In Regen
239
99
350
404
191
382
15
107
326
79
320
374
144
257
262
78
314
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
54
58
58
58
58
58
58
58
58
58
58
58
58
58
58
58
68
58
58
58
58
58
59
58
58
59
59
59
59
68
58
59
60
59
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
49
50
In Regen
50
50
50
50
50
50
48
50
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
49
50
50
50
50
50
50
50
50
48
50
50
50
50
50
In Regen
50
50
50
50
Product
Water
Pressure
(TT)
psig
46
48
48
48
48
48
48
48
48
48
48
48
48
48
46
48
48
48
48
48
48
48
48
48
48
48
48
48
50
44
46
46
46
44
Regeneration
Regen.
Counter
62
62
63
64
64
66
67
68
68
69
71
72
72
73
73
75
76
76
77
77
79
80
80
80
82
82
83
83
83
85
85
86
87
87
Salt
Delivered
Ib
5,330
6,050
7,240
6,510
6,020
6,040
5,965
Cumulative
Salt
Delivered
Ib
92,555
98,605
105,845
112,355
118,375
124,415
130,380
Cd
OJ
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation Log Sheet (Continued)
21
22
23
24
25
26
27
Date
10/31/05
11/01/05
11/02/05
11/03/05
11/04/05
11/07/05
11/08/05
11/09/05
11/10/05
11/11/05
11/14/05
11/15/05
11/16/05
11/17/05
11/18/05
11/21/05
11/22/05
11/23/05
11/28/05
11/29/05
11/30/05
12/01/05
12/05/05
12/06/05
12/07/05
12/08/05
12/09/05
12/12/05
12/13/05
12/14/05
12/15/05
12/16/05
Pum
Opt.
Hours
hr
58.1
22.2
22.0
20.4
22.0
54.7
18.8
17.7
7.8
20.5
37.5
10.5
15.0
18.5
15.7
42.7
12.0
21.8
62.1
17.3
18.5
15.0
64.1
13.6
13.8
23.3
22.9
26.2
9.1
11.1
23.8
24.7
Cum.
Hours
hr
2910.1
2932.3
2954.3
2974.7
2996.7
3051.4
3070.2
3087.9
3095.7
3116.2
3153.7
3164.2
3179.2
3197.7
3213.4
3256.1
3268.1
3289.9
3352.0
3369.3
3387.8
3402.8
3466.9
3480.5
3494.3
3517.6
3540.5
3566.7
3575.8
3586.9
3610.7
3635.4
n House
Master
Flow
Meter
kgal
109,445
109,669
109,898
110,102
110,323
110,881
111,069
111,248
111,342
111,537
111,916
112,024
112,169
112,350
112,509
112,935
113,102
113,270
113,890
114,062
114,241
114,388
115,021
115,151
115,287
115,512
115,735
115,989
116,078
116,188
116,418
116,658
Treated
Volume
Kgal
599
224
229
204
221
558
188
179
94
195
379
108
145
181
159
426
167
168
620
172
179
147
633
130
136
225
223
254
89
110
230
240
Product Water Flow Meter
Product
Water
Flow rate
gpm
165
168
165
166
138
168
161
161
171
170
160
161
160
163
169
160
160
160
170
159
158
159
158
168
167
151
151
128
158
160
150
152
Product
Water
Flow
Totalizer
kgal
148
33
252
118
NA
203
54
224
314
178
212
314
125
302
168
199
30
190
135
299
103
283
233
32
102
193
83
NA
85
190
86
294
BV
Treated
BV
198
44
337
158
In Regen
271
72
299
420
238
283
420
167
404
225
266
40
254
180
400
138
378
311
43
136
258
111
In Regen
114
254
115
393
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
58
58
58
58
68
67
59
59
59
58
49
49
49
58
58
58
58
58
58
58
58
58
58
58
58
59
59
59
59
59
59
59
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
In Regen
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
In Regen
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
44
44
46
46
46
49
49
49
44
46
49
44
46
48
44
49
49
49
49
49
49
49
48
49
48
49
49
49
49
49
49
49
Regeneration
Regen.
Counter
89
90
90
91
92
93
94
94
94
95
96
96
97
97
98
99
100
100
102
102
103
103
105
106
107
107
108
109
109
109
110
110
Salt
Delivered
Ib
6,000
5,955
5,975
6,005
5,965
5,975
Cumulative
Salt
Delivered
Ib
136,380
142,335
148,310
154,315
160,280
166,255
Cd
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation Log Sheet (Continued)
28
29
30
31
32
33
34
Date
12/19/05
12/20/05
12/21/05
12/22/05
12/27/05
12/28/05
12/29/05
12/30/05
01/03/06
01/04/06
01/05/06
01/06/06
01/09/06
01/10/06
01/11/06
01/12/06
01/17/06
01/18/06
01/19/06
01/20/06
01/23/06
01/24/06
01/25/06
01/26/06
01/27/06
01/30/06
01/31/06
02/01/06
02/02/06
02/03/06
Pum
Opt.
Hours
hr
24.2
5.4
14.9
13.7
65.3
13.0
7.4
15.3
48.9
13.7
16.7
13.5
45.7
17.0
12.1
24.2
37.0
12.1
8.7
23.8
11.4
24.2
20.8
11.8
23.4
73.3
10.7
14.1
14.1
10.9
Cum.
Hours
hr
3659.6
3665.0
3679.9
3693.6
3758.9
3771.9
3779.3
3794.6
3843.5
3857.2
3873.9
3887.4
3933.1
3950.1
3962.2
3986.4
4023.4
4035.5
4044.2
4068.0
4079.4
4103.6
4124.4
4136.2
4159.6
4232.9
4243.6
4257.7
4271.8
4282.7
n House
Master
Flow
Meter
kgal
116,892
116,945
117,085
117,216
117,842
117,968
118,037
118,185
118,655
118,783
118,937
119,067
119,501
119,663
119,778
120,003
120,351
120,473
120,544
120,768
120,873
121,100
121,290
121,355
121,607
122,264
122,360
122,480
122,612
122,709
Treated
Volume
Kgal
234
53
140
131
626
126
69
148
470
128
154
130
434
162
115
225
348
122
71
224
105
227
190
65
252
657
96
120
132
97
Product Water Flow Meter
Product
Water
Flow rate
gpm
153
153
160
157
150
156
155
155
155
158
150
153
126
151
153
155
149
149
151
150
154
149
149
140
144
143
144
146
146
148
Product
Water
Flow
Totalizer
kgal
211
262
71
196
144
264
13
155
280
77
120
120
8
163
273
170
176
292
32
248
27
244
100
198
154
127
218
11
132
224
BV
Treated
BV
282
350
95
262
193
353
17
207
374
103
160
160
11
218
365
227
235
390
43
332
36
326
134
265
206
170
291
15
176
299
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
59
59
59
59
59
59
59
59
59
59
59
59
68
58
58
58
59
59
59
59
59
59
59
59
59
59
59
59
59
59
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
0
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
49
49
49
49
49
48
48
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
Regeneration
Regen.
Counter
111
111
112
112
114
114
115
115
116
117
118
118
120
120
120
121
122
123
123
123
124
124
125
125
126
128
128
129
129
129
Salt
Delivered
Ib
5,800
3,685
5,435
3,590
3,170
4,385
Cumulative
Salt
Delivered
Ib
178,190
181,875
187,310
190,900
194,070
198,455
Cd
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation and Operation Labor Log Sheet (Continued)
35
36
37
38
39
40
41
Date
02/06/06
02/08/06
02/09/06
02/10/06
02/13/06
02/14/06
02/15/06
02/16/06
02/17/06
02/21/06
02/22/06
02/23/06
02/24/06
02/27/06
02/28/06
03/01/06
03/02/06
03/03/06
03/06/06
03/07/06
03/09/06
03/10/06
03/13/06
03/14/06
03/15/06
03/16/06
03/17/06
03/20/06
03/21/06
03/22/06
03/23/06
03/24/06
Pum
Opt.
Hours
hr
70.0
14.3
8.3
0.1
18.8
10.5
9.0
17.4
12.0
27.5
11.9
23.9
13.2
21.6
9.0
23.7
6.2
8.8
41.6
11.5
29.2
15.0
39.1
12.4
11.0
11.9
7.6
27.7
5.9
10.0
6.9
24.0
Cum.
Hours
hr
4352.7
4367.0
4375.3
4375.4
4394.2
4404.7
4413.7
4431.1
4443.1
4470.6
4482.5
4506.4
4519.6
4541.2
4550.2
4573.9
4580.1
4588.9
4630.5
4642.0
4671.2
4686.2
4725.3
4737.7
4748.7
4760.6
4768.2
4795.9
4801.8
4811.8
4818.7
4842.7
3 House
Master
Flow
Meter
kgal
123,325
123,451
123,523
123,524
123,688
123,780
123,870
124,032
124,145
124,415
124,530
124,763
124,894
125,106
125,191
125,426
125,481
125,572
125,977
126,087
126,380
126,533
126,914
127,039
127,149
127,262
127,337
127,603
127,662
127,761
127,828
128,059
Treated
Volume
Kgal
616
126
72
1
164
92
90
162
113
270
115
233
131
212
85
235
55
91
405
110
293
153
381
125
110
113
75
266
59
99
67
231
Product Water Flow Meter
Product
Water
Flow rate
gpm
144
144
144
144
140
139
158
153
153
155
158
158
158
156
156
156
154
154
160
160
164
165
164
160
166
154
156
156
158
156
150
160
Product
Water
Flow
Totalizer
kgal
159
278
29
30
186
272
133
133
248
179
289
185
309
201
282
182
239
314
57
161
225
43
81
157
304
87
158
87
144
190
302
198
BV
Treated
BV
213
372
39
40
249
364
178
178
332
239
386
247
413
269
377
243
320
420
76
215
301
57
108
210
406
116
211
116
193
254
404
265
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
Regeneration
Regen.
Counter
131
131
132
132
132
132
133
134
134
135
135
136
136
137
137
138
138
138
140
140
141
142
143
143
143
144
144
145
145
145
145
146
Salt
Delivered
Ib
4,780
8,020
1,880
5,760
Cumulative
Salt
Delivered
Ib
203,235
211,255
213,135
218,895
Cd
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation and Operation Labor Log Sheet (Continued)
42
43
44
45
46
47
Date
03/27/06
03/28/06
03/29/06
03/30/06
03/31/06
04/03/06
04/04/06
04/05/06
04/06/06
04/07/06
04/10/06
04/11/06
04/12/06
04/13/06
04/14/06
04/17/06
04/18/06
04/19/06
04/20/06
04/21/06
04/24/06
04/25/06
04/26/06
04/27/06
04/28/06
05/01/06
05/02/06
05/03/06
05/04/06
05/05/06
Pump House
Opt.
Hours
hr
32.6
12.5
11.1
13.4
8.0
6.3
8.7
14.4
14.0
5.9
0.0
0.0
25.1
10.5
17.9
41.8
13.0
11.5
13.3
5.1
6.4
8.1
8.0
15.8
16.2
28.9
23.9
16.2
24.0
15.5
Cum.
Hours
hr
4875.3
4887.8
4898.9
4912.3
4920.3
4926.6
4935.3
4949.7
4963.7
4969.6
4969.6
4969.6
4994.7
5005.2
5023.1
5064.9
5077.9
5089.4
5102.7
5107.8
5114.2
5122.3
5130.3
5146.1
5162.3
5191.2
5215.1
5231.3
5255.3
5270.8
Master
Flow
Meter
kgal
128,377
128,500
128,605
128,734
128,817
128,885
128,961
129,101
129,249
129,297
129,297
129,297
129,538
129,639
129,810
130,211
130,334
130,440
130,570
130,619
130,679
130,754
130,834
130,985
131,340
131,418
131,649
131,803
132,090
132,177
Treated
Volume
kgal
318
123
105
129
83
68
76
140
148
48
0
0
241
101
171
401
123
106
130
49
60
75
80
151
355
78
231
154
287
87
Product Water Flow Meter
Product
Water
Flow rate
gpm
156
156
156
156
157
160
160
160
158
0
0
160
150
151
151
158
119
159
154
0
152
152
152
0
0
164
154
155
154
150
Product
Water
Flow
Totalizer
kgal
176
294
77
200
279
19
92
116
267
313
314
316
215
316
151
208
2
105
225
272
11
83
159
302
126
78
297
125
14
155
BV
Treated
BV
235
393
103
267
373
25
123
155
357
418
420
422
287
422
202
278
2
140
301
364
15
111
213
404
168
104
397
167
19
207
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
59
59
59
59
59
59
59
59
59
48
48
59
59
59
59
59
71
59
59
49
59
59
59
46
46
59
59
59
59
59
Vessel A
Outlet
Pressure
(TA)
psig
49
49
49
49
49
50
50
50
50
0
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
In Regen
50
50
50
50
50
50
50
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
50
50
50
50
50
49
49
49
49
50
0
49
49
49
49
49
49
49
49
49
49
49
49
46
46
49
49
49
49
49
Regeneration
Regen.
Counter
147
147
148
148
148
149
149
150
150
150
150
150
151
151
151
153
154
154
154
154
155
155
155
155
156
157
157
158
159
159
Salt
Delivered
Ib
5,920
3,920
6,200
1,320
Cumulative
Salt
Delivered
Ib
224,815
228,735
234,935
236,255
Cd
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation and Operation Labor Log Sheet (Continued)
48
49
50
51
52
53
54
Date
05/08/06
05/09/06
05/12/06
05/15/06
05/16/06
05/17/06
05/18/06
05/19/06
05/22/06
05/23/06
05/24/06
05/25/06
05/30/06
05/31/06
06/01/06
06/02/06
06/05/06
06/06/06
06/07/06
06/08/06
06/12/06
06/13/06
06/14/06
06/15/06
06/19/06
06/20/06
06/21/06
06/22/06
Pum
Opt.
Hours
hr
45.3
7.2
56.1
45.9
20.0
21.3
23.0
23.0
32.7
17.0
16.5
22.9
52.7
18.4
20.0
17.3
44.9
19.5
8.4
20.9
80.8
22.4
15.0
19.6
82.1
15.0
22.0
21.8
Cum.
Hours
hr
5316.1
5323.3
5379.4
5425.3
5445.3
5466.6
5489.6
5512.6
5545.3
5562.3
5578.8
5601.7
5654.4
5672.8
5692.8
5710.1
5755.0
5774.5
5782.9
5803.8
5884.6
5907.0
5922.0
5941.6
6023.7
6038.7
6060.7
6082.5
n House
Master
Flow
Meter
kgal
132,598
132,666
133,189
133,619
133,809
134,010
134,217
134,428
134,717
134,868
135,018
135,225
135,684
135,844
136,030
136,192
136,610
136,793
136,872
137,062
137,767
137,958
138,085
138,251
138,908
139,044
139,248
139,445
Treated
Volume
kgal
421
68
523
430
190
201
207
211
289
151
150
207
459
160
186
162
418
183
79
190
705
191
127
166
657
136
204
197
Product Water Flow Meter
Product
Water
Flow rate
gpm
153
155
153
152
153
152
153
152
146
144
144
148
144
142
141
160
165
153
158
149
140
142
142
140
140
146
143
150
Product
Water
Flow
Totalizer
kgal
231
297
158
244
103
293
164
39
312
130
269
168
257
84
150
302
173
228
302
174
183
39
157
312
276
80
180
132
BV
Treated
BV
309
397
211
326
138
392
219
52
417
174
360
225
344
112
201
404
231
305
404
233
245
52
210
417
369
107
241
176
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
59
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
48
48
48
49
49
49
46
46
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
49
Regeneration
Regen.
Counter
160
160
162
163
164
164
165
154
166
167
167
168
169
170
171
171
173
173
173
174
176
177
177
177
179
180
180
181
Salt
Delivered
Ib
6,900
4,520
5,660
4,840
Cumulative
Salt
Delivered
Ib
243,155
247,675
253,335
258,175
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation and Operation Labor Log Sheet (Continued)
55
56
57
58
59
60
61
62
Date
06/26/06
06/27/06
06/28/06
06/29/06
06/30/06
07/03/06
07/05/06
07/06/06
07/07/06
07/10/06
07/11/06
07/12/06
07/13/06
07/14/06
07/24/06
07/25/06
07/26/06
07/27/06
08/07/06
08/08/06
08/09/06
08/10/06
08/14/06
12/12/06
12/13/06
12/18/06
12/19/06
12/20/06
12/21/06
Pump House
Opt.
Hours
hr
84.0
22.7
21.7
23.7
22.9
66.5
47.9
14.4
26.2
71.2
23.6
24.1
24.3
23.6
-
-
23.2
24.6
185.9
25.4
2.9
26.9
74.9
203.3
1.1
48.6
17.1
13.2
11.8
Cum.
Hours
hr
6166.5
6189.2
6210.9
6234.6
6257.5
6324.0
6371.9
6386.3
6412.5
6483.7
6507.3
6531.4
6555.7
6579.3
-
6835.7
6858.9
6883.5
7069.4
7094.8
7097.7
7124.6
7199.5
7402.8
7403.9
7452.5
7469.6
7482.8
7494.6
Master
Flow
Meter
kgal
140,174
140,393
140,597
140,824
141,038
141,637
142,060
142,189
142,399
142,999
143,195
143,406
143,623
143,839
145,921
146,135
146,357
146,543
148,224
148,425
148,508
148,759
149,399
151,430
151,447
151,920
152,099
152,280
152,344
Treated
Volume
kgal
729
219
204
227
214
599
423
129
210
600
196
211
217
216
2,082
214
222
186
1,681
201
83
251
640
7,591
17
473
179
181
64
Product Water Flow Meter
Product
Water
Flow rate
gpm
160
160
150
150
153
148
148
164
140
140
130
142
149
154
144
151
160
148
157
158
158
151
117
159
156
160
160
159
159
Product
Water
Flow
Totalizer
kgal
25
233
101
315
190
102
175
299
184
98
279
154
34
236
45
127
144
49
38
230
314
230
200
87
105
9
180
303
89
BV
Treated
BV
33
311
135
421
254
136
234
400
246
131
373
206
45
316
60
170
193
66
51
307
420
307
267
116
140
12
241
405
119
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
59
59
59
59
59
59
59
59
59
59
59
59
59
59
58
58
52
54
58
58
58
58
59
60
60
60
60
60
60
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
46
45
44
49
49
49
49
49
46
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
50
50
46
45
44
49
49
49
49
49
46
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
49
49
49
49
49
49
49
49
49
49
49
49
49
49
48
44
42
48
46
46
46
46
48
50
50
50
50
50
50
Regeneration
Regen.
Counter
184
184
185
185
186
188
189
189
190
192
192
193
194
194
201
202
203
206
209
209
209
210
212
227
227
229
229
229
230
Salt
Delivered
Ib
8,755
4,730
Cumulative
Salt
Delivered
Ib
266,930
271,660
Cd
-------
US EPA Arsenic Demonstration Project at Fruitland, ID - Daily System Operation and Operation Labor Log Sheet (Continued)
63
64
65
66
67
68
69
70
71
72
73
Date
12/26/06
12/27/06
12/28/06
01/02/07
01/03/07
01/04/07
01/08/07
01/09/07
01/10/07
01/16/07
01/25/07
01/29/07
01/30/07
02/01/07
02/02/07
02/05/07
02/06/07
02/07/07
02/08/07
02/09/07
04/03/07
04/05/07
Pum
Opt.
Hours
hr
44.4
20.0
18.0
121.0
8.8
19.5
9.0
2.9
4.6
17.2
80.2
21.5
12.6
15.8
19.3
17.4
16.6
15.1
5.5
8.0
164.9
0.0
Cum.
Hours
hr
7539.0
7559.0
7577.0
7698.0
7706.8
7726.3
7735.3
7738.2
7742.8
7760.0
7840.2
7861.7
7874.3
7890.1
7909.4
7926.8
7943.4
7958.5
7964.0
7972
8136.9
8136.9
n House
Master
Flow
Meter
kgal
152,786
152,984
153,167
154,324
154,409
154,594
154,691
154,719
154,766
154,938
NA
155,938
156,063
156,223
156,403
156,587
156,748
156,896
156,946
157025
158593
158593
Treated
Volume
kgal
442
198
183
1,157
85
185
97
28
47
172
NA
NA
125
160
180
184
161
148
50
79
1568
0
Product Water Flow Meter
Product
Water
Flow rate
gpm
165
161
160
NA
NA
NA
163
160
166
161
158
158
NA
161
161
158
158
158
158
160
158
158
Product
Water
Flow
Totalizer
kgal
172
49
222
26
107
285
58
86
130
296
76
281
79
232
78
254
83
224
272
22
146000
146000
BV
Treated
BV
230
66
297
35
143
381
78
115
174
396
102
376
106
310
104
340
111
299
364
29
-
-
System Pressures
Combined
System
Inlet
Pressure
(IN)
psig
60
60
60
60
60
60
60
60
60
59
59
59
50
59
59
59
59
59
59
59
60
60
Vessel A
Outlet
Pressure
(TA)
psig
50
50
50
50
50
50
50
50
50
50
50
50
NA
50
50
50
50
50
50
50
50
50
Vessel B
Outlet
Pressure
(TB)
psig
50
50
50
50
50
50
50
50
50
50
50
50
NA
50
50
50
50
50
50
50
50
50
Product
Water
Pressure
(TT)
psig
49
49
49
49
49
49
49
50
50
49
49
49
49
49
49
49
49
49
49
49
49
49
Regeneration
Regen.
Counter
231
232
232
236
236
236
237
237
237
237
240
240
241
241
242
242
243
243
243
244
252
252
Salt
Delivered
Ib
Cumulative
Salt
Delivered
Ib
Cd
o
System regenerates every 316,000 gallons.
NM = Not measured
NA = Not available
-------
APPENDIX C
ANALYTICAL DATA
-------
Analytical Results from Long-Term Sampling at Fruitland, ID
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b>
mg/L(b)
mg/L
NTU
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
Hg/L
ng/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
6/15/2005
IN
-
-
484
0.5
52
10.0
<0.05
-
57.8
0.1
568
7.6
15.2
2.6
212
303
180
123
49.0
45.5
3.5
2.1
43.4
<25
<25
11.8
10.0
22.6
19.5
53.0
45.2
14.5
14.0
TT
37
49
484
0.5
<1
4.3
<0.05
-
57.2
<0.1
542
7.7
15.1
3.0
172
252
150
101
0.7
0.9
<0.1
0.8
<0.1
<25
<25
9.9
10.4
<0.1
<0.1
2.1
2.1
0.2
0.2
6/23/2005'c'a)
IN
-
-
374
-
59
10.3
<0.05
-
57.7
1.4
-
7.6
15.0
4.0
192
-
-
-
37.5
-
-
-
-
211
-
15.4
-
19.1
-
39.8
-
12.8
-
TA
TB
212
283
387
-
57
9.4
<0.05
-
57.3
0.1
-
7.5
15.2
3.4
204
-
-
-
38.2
-
-
-
-
<25
-
13.9
-
<0.1
-
0.9
-
8.2
-
387
-
59
9.8
<0.05
-
58.0
0.4
-
7.2
15.3
3.5
199
-
-
-
38.3
-
-
-
-
<25
-
14.3
-
<0.1
-
1.1
-
10.7
-
6/29/2005""
IN
-
-
396
0.7
58
10.1
0.2
-
59.3
0.7
-
7.4
14.9
2.4
225
-
-
-
38.0
-
-
-
-
<25
-
15.7
-
19.0
-
40.7
-
12.5
-
TA
TB
147
197
383
0.7
94
9.5
0.2
-
58.6
0.7
-
7.6
14.9
2.4
191
-
-
-
37.4
-
-
-
-
<25
-
14.5
-
<0.1
-
5.0
-
13.0
-
396
0.7
63
9.5
0.3
-
57.5
0.5
-
7.5
14.8
2.1
225
-
-
-
38.8
-
-
-
-
<25
-
15.1
-
<0.1
-
4.5
-
13.3
-
7/6/2005
IN
-
-
396
-
73
11.2
0.1
-
58.6
0.2
-
6.7
15.2
3.6
209
-
-
-
39.3
-
-
-
-
<25
-
19.4
-
20.6
-
39.2
-
12.1
-
TA
TB
29
39
176
-
<1
3.0
<0.05
-
58.4
0.2
-
6.8
15.8
2.2
180
-
-
-
3.6
-
-
-
-
<25
-
20.3
-
<0.1
-
8.4
-
<0.1
-
6
-
<1
6.6
<0.05
-
59.0
0.6
-
6.0
15.1
3.3
260
-
-
-
8.3
-
-
-
-
<25
-
20.9
-
2.5
-
36.1
-
0.2
-
7/13/2005
IN
-
-
387
0.5
75
9.6
<0.05
-
46.6
0.2
578
7.4
15.2
2.1
206
242
143
98.8
39.0
38.8
0.2
2.4
36.4
<25
<25
18.4
20.2
18.4
18.8
35.5
36.6
12.6
12.0
TT
94
126
286
0.5
<1
1.9
<0.05
-
48.1
<0.1
558
7.3
15.2
1.9
217
242
145
97.0
2.8
3.2
<0.1
2.4
0.8
<25
<25
19.8
20.2
<0.1
<0.1
4.2
5.7
0.3
0.2
7/20/2005
IN
-
-
374
-
59
9.4
<0.05
-
55.8
0.1
-
7.5
15.4
1.9
191
-
-
-
35.4
-
-
-
-
<25
-
25.4
-
18.6
-
38.7
-
13.7
-
TA
TB
52
70
264
-
<1
2.7
<0.05
-
56.6
<0.1
-
7.8
15.3
2.2
209
-
-
-
3.1
-
-
-
-
<25
-
20.8
-
<0.1
-
5.6
-
0.3
-
114
-
<1
4.1
<0.05
-
55.5
<0.1
-
7.3
15.3
2.5
198
-
-
-
5.8
-
-
-
-
<25
-
23.3
-
<0.1
-
11.9
-
<0.1
-
8/3/2005'e
IN
-
-
378
-
61
9.3
0.1
-
56.2
<0.1
-
7.7
15.4
3.1
199
-
-
-
34.2
-
-
-
-
<25
-
23.3
-
16.6
-
35.4
-
12.2
-
TA
TB
534
714"
383
-
55
9.7
0.2
-
56.1
<0.1
-
7.5
15.1
1.8
227
-
-
-
41.4
-
-
-
-
<25
-
23.1
-
<0.1
-
1.1
-
0.3
-
378
-
53
9.7
0.2
-
55.5
<0.1
-
7.4
14.8
2.5
186
-
-
-
46.3
-
-
-
-
<25
-
24.7
-
<0.1
-
2.1
-
0.7
-
(a) AsCaCO3. (b)AsPO4.
(c) Nitrate, turbidity, and Orthophosphate analyzed outside of holding time, (d) Vessels were not properly regenerated due to wrong settings caused by power outage on 6/17/05. The problem was fixed on
6/29/05 after sampling.
(d) Kinetico technician was on site 7/26/05 - 7/30/05 conducting an arsenic and nitrate breakthrough study and regeneration elution study. They changed the system regeneration setpoint from 214,000 gal
to 335,000 gal of water treated. The brine draw time was reduced from 64 to 32 min.
(e) Regeneration didn't start until 199,000 gallons past the setpoint at 355,000 gallons due to a problem with level sensor in the brine day tank.
-------
Analytical Results from Long-Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
8/10/2005
IN
Kgal
BV
mg/L<"
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b)
mg/L
NTU
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
Hg/L
ng/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
Mg/L
-
383
-
61
9.1
0.1
-
58.7
<0.1
-
7.8
15.4
3.0
216
-
-
-
40.6
-
-
-
-
<25
-
30.0
-
20.0
-
42.3
-
14.6
-
TA
TB
28
37
3
-
<1
2.5
0.1
-
58.4
<0.1
-
7.0
15.0
2.2
297
-
-
-
25.6
-
-
-
-
<25
-
25.8
-
0.3
-
16.6
-
0.2
-
3
-
<1
2.5
<0.05
-
58.6
<0.1
-
7.3
14.8
3.1
3.0
-
-
-
15.1
-
-
-
-
<25
-
26.4
-
0.2
-
15.7
-
0.1
-
8/17/2005
IN
-
-
365
0.5
55
8.5
0.1
-
48.3
0.1
598
7.7
15.3
-
240
247
145
102
39.4
38.2
1.1
2.0
36.3
<25
<25
28.0
29.0
17.7
17.9
39.3
40.0
13.7
13.2
TT
120
160
361
0.5
<1
0.6
<0.05
-
45.9
<0.1
552
7.5
15.2
-
244
249
145
104
2.4
2.7
<0.1
2.1
0.5
<25
<25
26.4
27.2
<0.1
<0.1
3.0
3.4
0.1
0.1
8/24/2005
IN
-
-
378
-
58
8.6
0.2
-
63.4
0.1
-
7.9
15.1
2.4
242
-
-
-
42.9
-
-
-
-
<25
-
26.5
-
19.5
-
39.7
-
12.8
-
TA
TB
259
346
440
-
<1
3.2
<0.05
-
61.6
0.1
-
7.9
14.7
2.6
235
-
-
-
1.4
-
-
-
-
<25
-
25.5
-
<0.1
-
1.4
-
0.3
-
462
-
<1
0.5
<0.05
-
63.2
0.1
-
7.9
14.9
2.6
244
-
-
-
1.1
-
-
-
-
<25
-
24.6
-
<0.1
-
1.1
-
0.1
-
8/31/2005
IN
-
-
374
378
-
62
61
9.5
9.5
0.2
0.2
-
58.7
57.1
0.2
0.3
-
7.7
14.9
3.7
265
-
-
-
52.0
51.5
-
-
-
-
<25
<25
-
25.2
25.1
-
17.6
17.5
-
35.7
36.5
-
12.2
12.7
-
TA
TB
28
37
158
158
-
<1
<1
1.6
1.7
<0.05
<0.05
-
57.6
57.3
0.3
0.2
-
7.5
15.0
2.1
207
-
-
-
3.0
2.9
-
-
-
-
<25
<25
-
25.7
25.2
-
<0.1
<0.1
-
3.4
3.2
-
0.8
0.7
-
7
8
-
<1
<1
2.4
2.3
<0.05
<0.05
-
58.3
57.7
0.1
0.4
-
6.8
14.7
2.8
246
-
-
-
11.4
10.8
-
-
-
-
<25
<25
-
25.5
25.7
-
<0.1
<0.1
-
8.9
8.4
-
0.5
0.5
-
9/7/2005
IN
-
-
374
-
60
8.9
0.3
-
57.5
0.2
-
7.8
15.1
3.8
247
-
-
-
60.0
-
-
-
-
<25
-
26.4
-
17.8
-
39.4
-
12.3
-
TA
TB
145
194
440
-
<1
0.4
<0.05
-
57.0
0.3
-
7.6
14.8
2.9
260
-
-
-
1.3
-
-
-
-
<25
-
26.2
-
<0.1
-
0.8
-
0.7
-
383
-
<1
0.7
<0.05
-
57.1
0.3
-
7.4
14.8
2.4
252
-
-
-
1.2
-
-
-
-
<25
-
28.0
-
<0.1
-
1.1
-
0.5
-
9/14/2005
IN
-
-
374
0.5
57
8.8
0.3
-
58.7
0.1
574
7.6
15.1
2.7
241
247
150
97.7
40.5
40.9
<0.1
1.1
39.8
<25
<25
30.8
30.4
17.2
16.2
38.7
38.4
12.9
12.4
TT
209
279
462
0.5
<1
0.4
<0.05
-
54.0
0.1
542
7.4
14.8
2.6
240
247
148
98.9
0.7
0.7
<0.1
1.1
<0.1
<25
<25
26.5
28.7
<0.1
<0.1
<0.1
<0.1
0.5
0.4
9/21/2005
IN
-
-
383
-
58
9.2
0.1
-
55.7
0.2
-
7.8
15.1
3.0
276
-
-
-
33.6
-
-
-
-
<25
-
27.4
-
19.7
-
36.5
-
-
-
TA
TB
130
174
422
-
<1
0.4
<0.05
-
55.3
0.5
-
NA(C)
NA(C)
NA(C)
NA(C)
-
-
-
1.3
-
-
-
-
<25
-
24.4
-
<0.1
-
2.6
-
-
-
365
-
<1
0.7
<0.05
-
55.8
0.1
-
7.5
14.8
2.3
253
-
-
-
2.1
-
-
-
-
<25
-
24.2
-
<0.1
-
4.4
-
-
-
(a) As CaCO3.
(b) As PO4.
(c) Operator did not record water quality measurement.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
9/28/2005
IN
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b>
mg/L
NTU
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
ng/L
ng/L
ng/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
Mg/L
-
396
-
47
8.4
<0.05
;
56.1
1.0
-
7.7
15.0
4.3
248
-
-
-
35.1
-
-
-
-
102
-
25.5
-
21.1
-
30.6
-
13.5
-
TA
TB
314
420
440
-
<1
9.7
<0.05
;
57.4
0.2
-
7.7
15.0
2.5
214
-
-
-
17.6
-
-
-
-
<25
-
33.7
-
<0.1
-
2.8
-
0.3
-
458
-
<1
4.8
<0.05
;
58.0
0.1
-
7.7
15.0
2.7
219
-
-
-
2.1
-
-
-
-
<25
-
15.6
-
<0.1
-
3.1
-
0.1
-
10/5/2005
IN
-
-
383
-
41
6.9
<0.05
;
53.8
<0.1
-
7.9
14.6
2.3
249
-
-
-
34.3
-
-
-
-
<25
-
24.8
-
16.6
-
38.7
-
12.1
-
TA
TB
179
239
462
-
<1
0.5
<0.05
;
53.8
0.5
-
7.8
14.6
2.4
242
-
-
-
0.8
-
-
-
-
<25
-
23.4
-
0.0
-
0.4
-
0.8
-
458
-
<1
0.4
<0.05
;
54.5
0.1
-
7.7
14.6
2.8
216
-
-
-
0.8
-
-
-
-
<25
-
23.1
-
0.2
-
0.7
-
0.4
-
10/12/2005
IN
-
-
383
0.5
52
9.4
0.6
0.4
56.7
0.2
566
7.6
14.9
3.2
242
232
134
97.1
60.8
59.9
0.9
1.2
58.7
<25
<25
23.2
21.8
19.4
19.7
38.5
40.0
12.0
13.3
TT
143
191
405
0.5
<1
0.6
0.9
<0.03
57.2
<0.1
524
7.4
15.0
2.9
260
241
142
99.2
1.3
1.2
<0.1
1.4
<0.1
<25
<25
23.0
24.0
<0.1
<0.1
0.9
0.9
<0.1
<0.1
10/26/2005
IN
-
-
374
-
58
9.7
0.1
0.4
NA(C)
<0.1
-
7.7
14.8
1.9
252
-
-
-
45.8
-
-
-
-
<25
-
22.9
-
19.4
-
41.8
-
12.0
-
TA
TB
196
262
NA(C)
-
NA(C)
NA(C)
NA(C)
<0.03
57.0
NA(C)
-
7.9
14.8
3.1
251
-
-
-
0.9
-
-
-
-
<25
-
22.2
-
<0.1
-
0.6
-
0.1
-
440
-
<1
0.4
<0.05
<0.03
58.5
<0.1
-
7.6
14.8
2.2
237
-
-
-
1.0
-
-
-
-
<25
-
22.9
-
<0.1
-
0.7
-
<0.1
-
11/2/2005
IN
-
-
365
-
54
9.6
<0.05
0.3
57.1
<0.1
-
7.3
14.8
2.1
248
-
-
-
35.0
-
-
-
-
<25
-
24.9
-
18.8
-
38.2
-
12.8
-
TA
TB
252
337
440
-
<1
3.4
<0.05
<0.03
58.3
0.2
-
7.5
14.8
2.9
260
-
-
-
0.7
-
-
-
-
<25
-
23.3
-
<0.1
-
0.3
-
0.1
-
462
-
<1
0.3
<0.05
<0.03
57.3
<0.1
-
7.2
14.8
2.4
220
-
-
-
0.5
-
-
-
-
<25
-
23.1
-
<0.1
-
0.3
-
<0.1
-
11/9/2005
IN
-
-
383
0.5
55.7
10.0
<0.05
0.4
56.2
<0.1
566
7.7
14.7
2.6
257
257
157
99.2
37.0
37.5
<0.1
1.6
35.9
<25
<25
21.8
21.7
18.5
18.3
41.7
40.7
13.1
13.0
TT
224
299
462
0.5
<1
0.5
<0.05
<0.03
56.1
<0.1
498
7.6
14.8
1.7
259
251
155
96.5
0.7
0.7
<0.1
1.2
<0.1
<25
<25
23.0
23.1
<0.1
<0.1
<0.1
<0.1
0.1
<0.1
o
(a) As CaCO3.
(b) As PO4.
(c) Sampling error
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
O
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b>
mg/L(b)
mg/L
NTU
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
LJg/L
LJg/L
M9/L
M9/L
LJg/L
Mg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
11/16/2005
IN
-
-
396
-
56
10.2
0.1
0.3
56.1
<0.1
-
7.6
15.2
2.2
252
-
-
-
44.0
-
-
-
-
<25
-
19.9
-
19.7
-
39.2
-
12.5
-
TA
TB
125
167
418
-
<1
0.5
<0.05
<0.03
56
<0.1
-
7.5
14.8
2.1
248
-
-
-
0.7
-
-
-
-
<25
-
20.3
-
<0.1
-
0.7
-
0.4
-
352
-
<1
0.7
<0.05
<0.03
55.9
0.2
-
7.5
14.8
2.8
250
-
-
-
0.7
-
-
-
-
<25
-
21.2
-
<0.1
-
1.2
-
0.2
-
11/30/2005
IN
-
-
383
-
55
10.3
0.1
0.3
57.0
<0.1
-
7.6
15.4
3.3
249
-
-
-
38.8
-
-
-
-
<25
-
21.9
-
19.2
-
43.2
-
12.6
-
TA
TB
103
138
440
-
<1
0.5
<0.05
<0.03
57.5
0.2
-
7.7
15.9
2.5
213
-
-
-
1.5
-
-
-
-
<25
-
21.4
-
<0.1
-
2.0
-
20.1
-
409
-
<1
0.5
<0.05
<0.03
57.6
0.1
-
7.5
15.4
2.4
221
-
-
-
2.3
-
-
-
-
<25
-
22.1
-
<0.1
-
4.6
-
20.1
-
12/14/2005
IN
-
-
396
0.5
76
10.5
0.1
-
56.8
0.8
-
7.7
15.1
2.3
248
227
141
86.2
46.3
37.3
8.9
0.9
36.4
<25
<25
15.0
14.8
20.0
19.1
39.2
40.4
12.3
11.8
TT
190
254
484
0.5
<1
0.7
<0.05
-
56.6
1.6
-
7.2
14.9
2.5
224
229
140
89.3
1.0
0.8
0.2
1.1
<0.1
<25
<25
14.6
14.1
<0.1
<0.1
0.5
0.3
0.2
0.1
(a) As CaCO3.
(b) As PO4.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TOC
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b>
mg/L
NTU
mg/L
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
LJg/L
LJg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
1/4/2006
IN
-
-
387
-
58
10.2
0.1
0.3
57.6
0.5
-
-
7.6
15.3
2.4
220
-
-
-
37.9
-
-
-
-
<25
-
22.6
-
20.2
-
39.9
-
13.7
-
TA
TB
77
103
312
-
<1
1.2
<0.05
<0.03
58.3
0.7
-
-
7.3
14.9
2.9
223
-
-
-
1.4
-
-
-
-
<25
-
13.9
-
<0.1
-
1.4
-
0.6
-
242
-
<1
1.9
<0.05
<0.03
57.4
0.7
-
-
7.3
15.0
2.1
223
-
-
-
1.4
-
-
-
-
<25
-
19.0
-
<0.1
-
1.9
-
0.3
-
1/10/2006
IN
-
-
400
-
53
9.4
<0.05
0.3
58.6
0.5
-
-
7.5
14.9
2.3
261
-
-
-
48.3
-
-
-
-
<25
-
30.1
-
24.9
-
45.4
-
15.9
-
TA
TB
163
218
484
-
<1
0.7
<0.05
0.3
58.8
0.8
-
-
7.7
14.9
2.4
222
-
-
-
1.2
-
-
-
-
<25
-
15.1
-
0.3
-
0.7
-
0.4
-
458
-
<1
0.9
<0.05
<0.03
58.9
0.6
-
-
7.8
14.9
2.2
244
-
-
-
0.7
-
-
-
-
<25
-
21.4
-
<0.1
-
0.7
-
<0.1
-
1/18/2006
IN
-
-
409
0.5
54
10
<0.06
0.2
58.6
0.7
-
542
7.7
15.5
2.25
268
221
129
91.7
35.9
35.1
0.8
1.4
33.7
<25
<25
21.3
21.8
21.9
-
41.3
41.3
13.4
13.8
TT
292
390
466
0.5
<1
10.3
<0.06
<0.03
58.8
1.3
-
572
7.5
15.9
2.4
260
241
146
94.9
1.5
1.4
0.1
1.4
<0.1
<25
<25
10.4
10.3
<0.1
-
0.7
1.0
<0.1
<0.1
1/25/2006
IN
-
-
405
-
54
10
0.1
0.3
57.7
0.6
-
-
7.5
15.2
2.3
279
-
-
-
36.6
-
-
-
-
<25
-
19.5
-
22.8
-
40.4
-
12.0
-
TA
TB
100
134
387
-
<1
1.1
<0.05
<0.03
56.7
1.1
-
-
7.8
15.2
2.4
222
-
-
-
2.5
-
-
-
-
<25
-
8.0
-
<0.1
-
2.9
-
0.2
-
330
-
<1
1.7
<0.05
<0.03
57.9
1.3
-
-
7.6
15.1
2.5
214
-
-
-
2.8
-
-
-
-
<25
-
17.1
-
<0.1
-
3.7
-
<0.1
-
2/1/2006
IN
-
-
393
-
54
9.9
-
0.3
58.7
0.2
-
-
7.8
15.4
2.4
227
-
-
-
46.6
-
-
-
-
<25
-
19.6
-
13.9
-
35.6
-
13.1
-
TA
TB
18
24
60
-
<1
3.4
-
<0.03
58.3
0.4
-
-
7.1
15.2
2.4
238
-
-
-
6.8
-
-
-
-
<25
-
4.8
-
<0.1
-
5.4
-
0.3
-
12
-
9
4.7
-
0.5
58.1
0.8
-
-
6.9
15.4
2.3
255
-
-
-
40.5
-
-
-
-
<25
-
16.5
-
<0.1
-
12.9
-
0.1
-
(a) As CaCO3. (b) As PO4.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TOC
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
2/8/2006
IN
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b>
mg/L
NTU
mg/L
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
LJg/L
LJg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
-
388
379
-
53
53
9.6
9.7
-
0.3
0.3
56.5
57.1
0.7
0.6
-
-
7.3
15.2
2.5
235
-
-
-
44.2
47.2
-
-
-
-
<25
<25
-
19.1
18.7
-
19.7
19.6
-
40.3
40.5
-
14.7
15.1
-
TA
TB
278
372
442
438
-
<1
<1
9.7
9.9
-
<0.03
<0.03
57.1
57.1
1.1
1.3
-
-
7.2
15.2
2.4
239
-
-
-
1.5
1.5
-
-
-
-
<25
<25
-
1.1
1.1
-
<0.1
<0.1
-
0.6
0.6
-
0.2
0.2
-
446
446
-
<1
<1
5.7
5.8
-
<0.03
<0.03
57.2
57.3
1.1
1.1
-
-
7.1
15.2
2.3
245
-
-
-
3.5
3.4
-
-
-
-
<25
<25
-
5.6
5.7
-
<0.1
<0.1
-
0.5
0.6
-
<0.1
<0.1
-
2/15/2006
IN
-
-
416
-
63
11.5
-
0.4
61.6
0.8
-
-
7.7
14.9
2.39
252
-
-
-
36.5
-
-
-
-
<25
-
22.0
-
19.1
-
42.8
-
13.8
-
TA
TB
133
178
96
-
<1
1.9
-
0.1
59.3
1.5
-
-
7.5
14.9
2.14
260
-
-
-
1.8
-
-
-
-
<25
-
4.6
-
<0.1
-
3.6
-
0.2
-
11
-
<1
3
-
<0.03
60.3
1.4
-
-
7.4
14.9
2.26
244
-
-
-
3.1
-
-
-
-
<25
-
11.4
-
<0.1
-
9.1
-
<0.1
-
2/22/2006
IN
-
-
386
0.5
62
11.5
-
0.3
58.5
0.3
-
582(c)
7.5
14.9
2.1
248
226
133
93.0
46.8
38.0
8.8
1.1
36.9
<25
<25
19.7
18.3
19.7
19.2
37.1
37.2
11.9
11.8
TT
289
386
436
0.5
<1
10.9
-
<0.03
59.4
1.2
-
520(c)
7.4
14.9
2.3
244
222
131
91.3
1.8
1.5
0.4
1.1
0.3
<25
<25
3.1
3.0
<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
3/1/2006
IN
-
-
381
-
59
10.2
-
0.4
55.2
1.4
-
-
7.6
15.4
2.8
254
-
-
-
50.2
-
-
-
-
<25
-
21.3
-
19.2
-
37.4
-
12.2
-
TA
TB
182
243
464
-
<1
0.6
-
<0.03
55.5
0.9
-
-
7.7
15.7
2.5
254
-
-
-
1.0
-
-
-
-
<25
-
4.0
-
<0.1
-
0.1
-
<0.1
-
439
-
<1
1.0
-
<0.03
53.9
1.5
-
-
7.6
15.7
2.6
223
-
-
-
0.9
-
-
-
-
<25
-
7.1
-
<0.1
-
0.3
-
<0.1
-
3/15/2006
IN
-
-
380
-
60
10.2
-
0.3
52.3
0.7
-
-
7.4
14.9
2.5
247
-
-
-
46.2
-
-
-
-
<25
-
19.3
-
19.9
-
37.5
-
12.2
-
TA
TB
304
406
422
-
<1
15
-
0.1
53.4
1
-
-
7.6
14.8
2.3
241
-
-
-
7.7
-
-
-
-
<25
-
1.0
-
<0.1
-
0.3
-
0.3
-
438
-
<1
12.8
-
0.1
53.0
1
-
-
7.4
14.9
1.3
246
-
-
-
7.8
-
-
-
-
<25
-
2.2
-
<0.1
-
0.2
-
0.1
-
(a) As CaCO3.
(b) As PO4.
(c) Sample reanalyzed outside of hold time.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TOC
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
3/22/2006
IN
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b>
mg/L
NTU
mg/L
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
ng/L
Hg/L
ng/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
Mg/L
ng/L
-
387
0.6
59
10.4
-
0.3
56.9
0.3
-
610
7.8
15.7
2.9
225
235
145
90.1
43.5
37.2
6.3
1.3
35.9
<25
<25
15.1
14.7
17.7
18.1
40.9
39.4
13.1
13.0
TT
190
254
473
0.6
<1
0.9
-
<0.01
57.0
1.3
-
584
7.9
15.1
2.2
234
227
140
87.0
0.9
0.9
<0.1
1.6
<0.1
<25
<25
0.5
0.5
<0.1
<0.1
0.6
0.7
<0.1
0.2
3/29/2006
IN
-
-
381
-
60
10.4
-
0.4
56.9
0.6
-
-
7.6
15.4
2.7
239
244
105
42.2
-
-
-
-
<25
-
17.2
-
21.4
-
40.3
-
12.1
-
TA
TB
77
103
298
-
<1
2.2
-
<0.01
57.1
1.2
-
-
7.2
15.2
2.3
271
243
105
1.9
-
-
-
-
<25
-
0.9
-
<0.1
-
1.6
-
0.2
-
282
-
<1
2.8
-
<0.01
56.4
0.7
-
-
7.3
15.0
2.4
238
249
105
2.1
-
-
-
-
<25
-
0.7
-
<0.1
-
1.8
-
0.1
-
4/5/2006
IN
-
-
380
-
59
10.3
-
0.3
57.4
0.4
-
-
7.8
15.2
2.7
235
-
-
-
44.0
-
-
-
-
<25
-
15.7
-
21.4
-
43.7
-
12.5
-
TA
TB
116
155
393
-
<1
1.1
-
<0.01
57.4
1.3
-
-
7.2
15.2
2.3
271
-
-
-
0.7
-
-
-
-
<25
-
0.4
-
<0.1
-
0.8
-
<0.1
-
384
-
<1
1.4
-
<0.01
57.0
1.3
-
-
7.4
15.1
2.4
240
-
-
-
0.9
-
-
-
-
<25
-
0.6
-
<0.1
-
0.7
-
<0.1
-
4/19/2006
IN
-
-
410
1.3
60
10.2
-
0.4
56.0
0.2
-
-
7.6
14.8
2.6
210
274
142
132
41.9
37.6
4.3
0.6
37.1
<25
<25
19.5
18.4
17.0
15.9
40.3
40.1
13.4
13.2
TT
105
140
379
0.3
<1
2.0
-
<0.01
55.6
0.4
-
-
7.5
14.9
2.8
253
270
141
129
1.1
0.9
0.2
0.6
0.4
<25
<25
0.3
0.3
<0.1
<0.1
1.0
0.9
<0.1
<0.1
4/26/2006
IN
-
-
383
-
64
11.5
-
0.4
56.8
0.5
-
-
7.3
14.9
2.3
224
-
-
-
42.9
-
-
-
-
<25
-
18.0
-
20.3
-
43.3
-
11.8
-
TA
TB
159
213
454
-
<1
1
-
<0.01
57.4
0.5
-
-
7.3
14.9
2.4
241
-
-
-
<0.1
-
-
-
-
<25
-
0.6
-
<0.1
-
0.3
-
<0.1
-
450
-
<1
1.1
-
<0.01
57.6
0.7
-
-
7.1
15.0
2.2
271
-
-
-
0.2
-
-
-
-
<25
-
0.9
-
<0.1
-
0.2
-
<0.1
-
o
(a) As CaCO3. (b) As PO4.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TOC
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b>
mg/L
NTU
mg/L
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
LJg/L
LJg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
5/3/2006
IN
-
-
391
-
58
10.0
-
0.3
59.4
0.5
-
-
7.3
14.9
2.3
212
-
-
-
43.9
-
-
-
-
<25
-
21.9
-
21.7
-
40.2
-
12.9
-
TA
TB
125
167
416
-
<1
1.2
-
<0.01
59.8
0.7
-
-
7.3
14.9
2.4
236
-
-
-
0.9
-
-
-
-
<25
-
0.5
-
<0.1
-
0.6
-
0.1
-
416
-
<1
1.4
-
<0.01
58.2
0.4
-
-
7.2
14.9
2.3
241
-
-
-
0.8
-
-
-
-
<25
-
0.8
-
<0.1
-
0.6
-
<0.1
-
5/9/2006
IN
-
-
376
-
62
10.9
-
0.4
60.4
0.4
-
-
7.6
15.1
3.2
307
-
-
-
47.4
-
-
-
-
<25
-
19.0
-
20.5
-
39.6
-
12.9
-
TA
TB
17
23
100
-
<1
4.9
-
<0.01
59
0.2
-
-
7.2
15.2
3.3
296
-
-
-
4.2
-
-
-
-
<25
-
0.8
-
<0.1
-
4.6
-
0.3
-
10
-
<1
5.9
-
0.2
59.9
0.3
-
-
6.3
15.2
3.4
262
-
-
-
29.7
-
-
-
-
<25
-
4.3
-
0.1
-
15.5
-
0.1
-
5/1 7/2006
IN
-
-
389
0.5
62
10.5
-
0.4
58.6
0.3
-
600
7.4
15.2
3.3
314
315
199
115
39.2
37.2
2.1
0.8
36.3
<25
<25
23.5
24.6
13.8
-
38.2
-
13.1
-
TT
293
392
432
0.5
<1
13.2
-
0.1
59
0.4
-
582
7.4
15.0
3.0
288
350
226
124
3.3
3.4
<0.1
0.5
2.9
<25
<25
0.4
0.3
<0.1
-
0.6
-
<0.1
-
5/24/2006
IN
-
-
381
381
-
61
60
10.6
10.7
-
;
57.2
57.9
0.3
0.3
-
-
7.3
15.0
3.0
311
-
132
122
-
40.0
41.1
-
-
-
-
<25
<25
-
19.3
19.3
-
19.2
19.1
-
32.1
33.7
-
13.0
12.7
-
TA
TB
269
360
435
444
-
<1
<1
12.6
12.7
-
;
57.9
56.5
0.7
0.7
-
-
7.3
15.0
3.1
319
-
114
131
-
2.1
2.4
-
-
-
-
<25
<25
-
<0.1
0.3
-
<0.1
<0.1
-
0.4
0.4
-
<0.1
<0.1
-
439
448
-
<1
<1
7.7
7.6
-
;
57.8
57.2
0.5
0.6
-
-
7.5
15.0
3.1
296
-
119
122
-
0.8
1.0
-
-
-
-
<25
<25
-
0.2
0.2
-
<0.1
<0.1
-
0.3
0.3
-
<0.1
<0.1
-
5/31/2006
IN
-
-
388
-
62
11.4
-
0.3
54.7
0.5
-
-
7.4
15.0
2.3
219
-
-
-
36.5
-
-
-
-
<25
-
22.3
-
20.1
-
40.3
-
13.3
-
TA
TB
84
112
371
-
<1
2.0
-
<0.01
54.9
0.7
-
-
7.3
14.9
2.8
239
-
-
-
1.1
-
-
-
-
<25
-
<0.1
-
<0.1
-
1.2
-
<0.1
-
271
-
<1
2.6
-
<0.01
56.5
0.9
-
-
7.2
15.2
2.8
244
-
-
-
1.8
-
-
-
-
<25
-
1.8
-
0.9
-
1.9
-
0.2
-
(a) As CaCO3. (b) As PO4.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TOC
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b>
mg/L
NTU
mg/L
mg/L
S.U.
UC
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
LJg/L
LJg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
6/7/2006
IN
-
-
388
-
60
10.8
-
;
59.1
0.3
-
-
7.3
14.9
2.3
240
-
-
-
40.6
-
-
-
-
<25
-
20.2
-
20.6
-
39.2
-
11.8
-
TA
TB
19
25
70
-
1
5.0
-
;
58.1
0.6
-
-
7.5
14.9
2.5
248
-
-
-
5.3
-
-
-
-
<25
-
2.1
-
<0.1
-
5.2
-
0.2
-
9
-
<1
6.2
-
;
58.3
0.4
-
-
7.2
14.9
2.4
250
-
-
-
38.1
-
-
-
-
<25
-
10.2
-
0.9
-
13.7
-
0.4
-
6/14/2006
IN
-
-
403
0.6
60
10.5
-
0.4
62.0
0.7
-
604
7.5
15.0
2.9
244
233
-
92.9
48.1
41.8
6.2
0.4
41.4
<25
<25
18.8
19.4
20.6
20.4
38.4
38.0
12.7
12.7
TT
157
210
480
0.6
<1
1.2
-
<0.01
61.5
0.4
-
534
7.6
15.2
3.6
228
228
-
91.0
0.8
0.8
<0.1
0.4
0.4
<25
<25
0.2
0.2
<0.1
<0.1
0.4
0.5
<0.1
<0.1
6/21/2006
IN
-
-
371
-
91
10.2
-
0.4
55.6
0.8
-
-
7.5
14.9
2.2
281
-
-
45.1
-
-
-
-
<25
-
30.6
-
20.6
-
38.9
-
12.6
-
TA
TB
276
369
433
-
<1
11.5
-
<0.03
54.4
0.9
-
-
7.3
14.9
2.4
256
-
-
2.1
-
-
-
-
<25
-
1.8
-
<0.1
-
0.5
-
0.3
-
441
-
<1
6.7
-
<0.01
54.8
0.9
-
-
7.6
15.0
2.5
256
-
-
1.3
-
-
-
-
<25
-
7.0
-
0.2
-
0.6
-
0.2
-
6/28/2006
IN
-
-
383
-
61
10.3
-
0.3
59.9
0.6
-
-
7.5
15.1
2.3
264
-
-
-
43.2
-
-
-
-
<25
-
28.4
-
20.6
-
37.8
-
13.2
-
TA
TB
101
135
379
-
<1
1.9
-
<0.01
61.6
1.1
-
-
7.4
15.4
2.5
240
-
-
-
1.0
-
-
-
-
<25
-
0.6
-
<0.1
-
0.8
-
0.2
-
338
-
12
2.3
-
<0.01
60
1.8
-
-
7.5
15.1
2.6
244
-
-
-
1.0
-
-
-
-
<25
-
8.6
-
<0.1
-
1.0
-
<0.1
-
7/6/2006
IN
-
-
385
-
75
10.2
-
0.3
57.3
0.4
-
-
7.2
15.0
2.3
302
-
-
-
42.1
-
-
-
-
<25
-
27.1
-
20.0
-
39.2
-
12.6
-
TA
TB
21
28
52
-
<1
5.8
-
<0.01
57.0
0.8
-
-
7.4
15.0
2.3
234
-
-
-
5.9
-
-
-
-
<25
-
1.5
-
<0.1
-
7.2
-
0.4
-
19
-
5
8.1
-
0.4
55.0
0.8
-
-
7.4
15.0
2.4
261
-
-
-
32.4
-
-
-
-
<25
-
5.0
-
<0.1
-
17.2
-
0.2
-
(a) As CaCO3. (b) As PO4.
-------
Analytical Results from Long Term Sampling at Fruitland, ID (Continued)
Sampling Date
Sampling Location
Parameter Unit
Water Treated
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Orthophosphate
Total P (as PO4)
Silica (as SiO2)
Turbidity
TOC
TDS
pH
Temperature
DO
ORP
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Total Fe
Soluble Fe
Total Mn
Soluble Mn
Total U
Soluble U
Total V
Soluble V
Mo (total)
Mo (soluble)
Kgal
BV
mg/L(a)
mg/L
mg/L
mg/L
mg/L(b)
mg/L(b)
mg/L
NTU
mg/L
mg/L
S.U.
C
mg/L
mV
mg/L
mg/L
mg/L
M9/L
Hg/L
Hg/L
LJg/L
Ljg/L
Mg/L
ng/L
Mg/L
Ljg/L
Mg/L
Mg/L
Mg/L
ng/L
Mg/L
Mg/L
7/12/2006
IN
-
-
381
0.3
43
10
-
0.3
55.6
0.1
-
602
7.5
15.2
2.8
210
239
140
99.0
43.8
38.5
5.3
0.5
38.0
<25
<25
32.8
35.2
19.1
19.8
37.7
37.8
11.6
11.4
TT
154
206
444
0.6
-
1.5
-
<0.01
553
0.3
-
560
7.5
15.1
3.2
233
231
139
91.3
1.6
0.7
0.9
0.4
0.3
<25
<25
1.2
0.2
<0.1
<0.1
0.7
0.6
<0.1
<0.1
(a) As CaCO3. (b) As PO4.
------- |