EPA/600/R-11/070
July 2011
Arsenic Removal from Drinking Water by Adsorptive Media
U.S. EPA Demonstration Project at
Hot Springs Mobile Home Park in Willard, Utah
Final Performance Evaluation Report
by
Lili Wang*
Abraham S.C. Chen*
Vivek Lal§
Lydia J. dimming8
§Battelle, Columbus, OH 43201-2693
JALSA Tech, LLC, Powell, OH 43065-6082
Contract No. EP-C-05-057
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 was funded by the United States Environmental Protection Agency
(EPA) under Task Order 0019 of Contract EP-C-05-057 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 U.S. 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 sub-
surface 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 to anticipate emerging problems. NRMRL's research provides solutions to envi-
ronmental problems by developing and promoting technologies that protect and improve the environment;
advancing scientific and engineering information to support regulatory and policy decisions; and provid-
ing 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 activities performed for and results obtained from the arsenic removal treatment
technology demonstration project at the Hot Springs Mobile Home Park (HSMHP) in Willard, UT. The
objectives of the project were to evaluate the effectiveness of Adsorbsia GTO adsorptive media
combined with Birm®/Filox oxidizing media (as a pretreatment) in removing arsenic to meet the new
arsenic maximum contaminant level (MCL) of 10 |o,g/L. Additionally, this project evaluated (1) the
reliability of the treatment system, (2) the required system operation and maintenance (O&M) and
operator skill levels, and (3) the capital and O&M cost of the technology. The project also characterized
the water in the distribution system and process residuals produced by the treatment process.
The water system at HSMHP was supplied by a supply well (Well No. 2) and a backup well (Well No. 1).
Arsenic concentrations in source water from Well No. 2 ranged from 9.4 to 21.1 |o,g/L and averaged 13.2
(ig/L. Of the soluble fraction, As(III) and As(V) each accounted for almost half of the concentrations.
Source water also contained, on average, 276 (ig/L of total iron and 116 (ig/L of total manganese.
Therefore, pretreatment was needed to remove iron and manganese and oxidize soluble As(III) to soluble
As(V) prior to adsorption by Adsorbsia GTO .
The 30-gal/min (gpm) arsenic treatment system consisted of two integral parts. The oxidation/filtration
unit consisted of two 24-in x 72-in vessels, each containing 5 ft3 of Birm® and 5 ft3 of Filox media; the
adsorption unit consisted of one 24-in x 72-in vessel containing 10 ft3 of Adsorbsia GTO media (the
actual amount was 10.3 ft3). Birm® is a manganese dioxide-coated media and Filox is a manganese
dioxide-based media; both are commonly used for iron and manganese removal. Adsorbsia GTO is a
granular titanium oxide media manufactured by the Dow Chemical Company for arsenic removal.
Operation of the treatment system began on December 11, 2008. The types of data collected included
system operation, water quality (both across the treatment train and in the distribution system), process
residuals, and capital and O&M cost. During the performance evaluation study period from December
11, 2008, through October 18, 2010, the system treated 5,629,000 gal (or 73,010 bed volumes [BV]) of
water based on a flow meter/totalizer installed on the adsorption vessel and 10.3 ft3 (or 77.1 gal) of
Adsorbsia GTO media in the vessel. Daily run times averaged 23.4 hr/day and daily water demands
averaged 8,354 gpd. Flowrates to the adsorption vessel varied extensively from 0.7 to 24.0 gpm and
averaged 7.3 gpm. Due to the fluctuating flowrates, empty bed contact times (EBCTs) in the adsorption
vessel varied extensively from 3.2 to 110 min and averaged 10.6 min. The average EBCT was four times
the vendor recommended value of 2.5 min.
Pretreatment with Birm®/Filox™ removed approximately 21% of total arsenic, leaving 10.4 (ig/L (on
average) in the influent to the adsorption vessel. Total arsenic at this point existed mainly as soluble
As(V), indicating effective oxidation of soluble As(III) by Birm®/Filox™. Birm®/Filox™ also was
effective in removing iron and manganese, reducing their concentrations to <25 and 4 (ig/L (on average),
respectively. Daily backwashing appeared to be effective in maintaining Birm®/Filox™ performance; no
sign of iron leakage or media fouling was observed during the performance evaluation study.
Adsorbsia™ GTO™ further removed soluble As(V) to below the 10-(ig/L arsenic MCL throughout the 22-
month study period. By the end of the performance evaluation study, the total arsenic concentration in
the system effluent was 6.2 (ig/L. At this point, the system had treated approximately 69,200 BV of
water, compared to the vendor estimated media life of 168,000 BV.
IV
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Each pre-oxidation vessel was backwashed daily at 47 gpm for 8 min, producing 376 gal of wastewater
(752 gal for two vessels). The wastewater contained 29.8 mg/L (on average) of total suspended solids
(TSS); therefore, 85 g (0.2 Ib) of solids were discharged daily. As expected, the solids were comprised
mainly iron (8.9 g).
Comparison of the distribution system sampling results before and after system startup showed significant
reductions in total arsenic, iron, and manganese concentrations. Total arsenic concentrations decreased
from an average of 11.2 to 3.2 (ig/L; total iron from 70 (ig/L to less than the method detection limit
(MDL) of 25 ug/L; total manganese from 19.5 to 8.8 (ig/L. Neither lead nor copper concentrations at the
consumers' taps appeared to have been impacted by system operation.
The capital investment cost for the system was $66,362, including $46,267 for equipment, $3,850 for site
engineering, and $16,245 for installation. Using the system's rated capacity of 30 gpm (43,200 gal/day
[gpd]), the normalized capital cost was $2,212/gpm ($1.54/gpd). The O&M cost included the cost for
media replacement and disposal, electricity consumption, and labor. Neither the oxidizing nor the
adsorptive media required replacement during the study period. The media replacement and disposal cost
would represent the majority of the O&M cost and was estimated to be $8,175 for 20 ft3 of Birm®/Filox™
and $8,440 for 10 ft3 of Adsorbsia™ GTO™. It was estimated that both Birm®/Filox™ media would have a
life expectancy of 10 years.
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CONTENTS
DISCLAIMER ii
FOREWORD iii
ABSTRACT iv
APPENDICES vii
FIGURES vii
TABLES viii
ABBREVIATIONS AND ACRONYMS ix
ACKNOWLEDGMENTS xii
Section 1.0: INTRODUCTION 1
1.1 Background 1
1.2 Treatment Technologies for Arsenic Removal 2
1.3 Project Objectives 2
2.0 SUMMARY AND CONCLUSIONS 6
3.0 MATERIALS AND METHODS 7
3.1 General Project Approach 7
3.2 System O&M and Cost Data Collection 8
3.3 Sample Collection Procedures and Schedules 8
3.3.1 Source Water 10
3.3.2 Treatment Plant Water 10
3.3.3 Backwash Wastewater and Solids 10
3.3.4 Spent Media 11
3.3.5 Distribution System Water 11
3.4 Sampling Logistics 11
3.4.1 Preparation of Arsenic Speciation Kits 11
3.4.2 Preparation of Sampling Coolers 12
3.4.3 Sample Shipping and Handling 12
3.5 Analytical Procedures 12
4.0 RESULTS AND DISCUSSION 13
4.1 Facility Description and Pre-existing Treatment System Infrastructure 13
4.1.1 Source Water Quality 15
4.1.2 Distribution System 17
4.2 Treatment Process Description 17
4.2.1 Technology Description 17
4.2.2 Birm® and Filox™ 18
4.2.3 Adsorbsia™ GTO™ Media 18
4.2.4 System Design and Treatment Process 18
4.3 System Installation 27
4.3.1 Permitting 27
4.3.2 Building Preparation 27
4.3.3 Installation, Shakedown, and Startup 27
4.4 System Operation 34
4.4.1 Operational Parameters 34
4.4.2 Residual Management 36
4.4.3 System/Operation Reliability and Simplicity 36
4.5 System Performance 37
VI
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4.6
4.5.1 Treatment Plant Sampling 37
4.5.2 Backwash Residual Sampling 45
4.5.3 Distribution System Water Sampling 46
System Cost 48
4.6.1 Capital Cost 48
4.6.2 O&MCost 49
Section 5.0: REFERENCES 52
APPENDICES
Appendix A: OPERATIONAL DATA
Appendix B: ANALYTICAL DATA
FIGURES
Figure 3-1. Backwash Sampling 11
Figure 4-1. Existing Pump House at HSMHP 13
Figure 4-2. Wellhead Cavity and Piping in Pump House 14
Figure 4-3. Hydropneumatic Tanks in Pump House 14
Figure 4-4. Schematic of Pre-Oxidation and Adsorptive Media System 20
Figure 4-5. Cross Sections of Pre-Oxidation and Adsorptive Media Vessels (As Built) 21
Figure 4-6. Process Flow Diagram and Sampling Locations 23
Figure 4-7. Composite Fiberglass Vessels (top) and Associated Piping (bottom) 24
Figure 4-8. PLC Panel 25
Figure 4-9. Strainer Installed Before Adsorption Vessel 25
Figure 4-10. 550-gal Backwash Supply Tank 26
Figure 4-11. Backwash Discharge Point Behind Treatment Building 27
Figure 4-12. New Treatment Building 28
Figure 4-13. Treatment System Installed 28
Figure 4-14. Backwash Supply Tank and Inlet Piping 29
Figure 4-15. Wastewater Collected After First (Left) and Fifth Backwashes (right) 30
Figure 4-16. Appearance of Backwash Wastewater After First (left) and Twelfth
Backwashes (right) 31
Figure 4-17. Backwash Wastewater Samples Collected at Beginning, Middle, and End of a
Backwash Cycle 33
Figure 4-18. Comparison of IN (right) and AP (left) Samples Collected During Refill of
Backwash Supply Tank 33
Figure 4-19. Concentrations of Various Arsenic Species at IN, AP, and TC Sampling Locations 40
Figure 4-20. Total Arsenic Breakthrough Curves 41
Figure 4-21. Total Iron Concentrations at IN, AP, and TC Sampling Locations 41
Figure 4-22. Concentrations of Iron Species at IN, AP, and TC Sampling Locations 42
Figure 4-23. Total Manganese Concentrations at IN, AP, and TC Sampling Locations 43
Figure 4-24. Total Phosphorus Breakthrough Curves 44
Figure 4-25. Total Phosphorus Percent Removal 44
Figure 4-26. O&M Costs for HSMHP System 51
vn
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TABLES
Table 1-1. Summary of Rounds 1, 2, and 2a Arsenic Removal Demonstration Locations,
Technologies, and Source Water Quality 3
Table 1 -2. Number of Demonstration Sites Under Each Arsenic Removal Technology 5
Table 3-1. Predemonstration Study Activities and Completion Dates 7
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities 8
Table 3-3. Sampling Schedule and Analytes 9
Table4-l. HSMHP Well No. 2 Source Water Data 15
Table 4-2. HSMHP Historic Water Quality Data 16
Table 4-3. Physical and Chemical Properties of Birm® and Filox™ Media 18
Table 4-4. Physical and Chemical Properties of Adsorbsia™ GTO™ Media 19
Table 4-5. Design Features of Arsenic Removal System at HSMHP 22
Table 4-6. Backwash Settings and Measurements 32
Table 4-7. Flowrates Measured During Refill of Backwash Supply Tank 32
Table 4-8. Summary of System Operation 35
Table 4-9. Summary of Arsenic, Iron, and Manganese Analytical Results 38
Table 4-10. Summary of Other Water Quality Parameter Results 39
Table 4-11. Birm®/Filox™ Vessel Backwash Wastewater Sampling Results 45
Table 4-12. Birm®/Filox™ Vessels Backwash Solid Sample Total Metal Results 46
Table 4-13. Distribution System Sampling Results 47
Table 4-14. Capital Investment for HSMHP System 49
Table 4-15. O&M Costs for HSMHP System 50
Vlll
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ABBREVIATIONS AND ACRONYMS
Ap differential pressure
AAL American Analytical Laboratories
Al aluminum
AM adsorptive media
As arsenic
ATS Aquatic Treatment Systems
bgs below ground surface
BV bed volume
Ca calcium
CA WET California Waste Extraction Test
Cd cadmium
C/F coagulation/filtration
cm3/g cubic centimeters per gram
CWS community water system
DDW Division of Drinking Water
DO dissolved oxygen
EBCT empty bed contact time
EPA U.S. Environmental Protection Agency
Fe iron
g/cm3 grams per cubic centimeter
g/L grams per liter
gpd gallons per day
gpm gallons per minute
H2SO4 sulfuric acid
HC1 hydrochloric acid
HIX hybrid ion exchanger
FiNO3 nitric acid
hp horsepower
HSMHP Hot Springs Mobile Home Park
ICP-MS inductively-coupled plasma/mass spectroscopy
ID iron addition
IR iron removal
IX ion exchange
m2/g square meters per gram
MCL maximum contaminant level
MDL method detection limit
MEI Magnesium Elektron, Inc
Mg magnesium
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ABBREVIATIONS AND ACRONYMS (Continued)
mg/L
Mn
MnO2
Na
NA
NaOCl
NaOH
Na2S2O3
NH3
Ni
NO3
NO2
NRMRL
NS
NSF
NTU
O&M
OIT
ORD
ORP
P
Pb
pCi/L
PLC
PO43
POU
psi
PVC
PWS
QAPP
QA/QC
RFP
RO
RPD
SDWA
SiO2
SMCL
SO42
STS
milligrams per liter
micrograms per liter
manganese
manganese dioxide
sodium
not available
sodium hypochlorite
sodium hydroxide
sodium thiosulfate
ammonia
nickel
nitrate
nitrite
National Risk Management Research Laboratory
not sampled
NSF International
nephelometric turbidity unit
operation and maintenance
Oregon Institute of Technology
Office of Research and Development
oxidation-reduction potential
Phosphorus
lead
pico Curies per liter
programmable logic controller
orthophosphate
point of use
pounds per square inch
polyvinyl chloride
Performance Work Statement
Quality Assurance Project Plan
Quality Assurance/Quality Control
Request for Proposal
reverse osmosis
relative percent difference
Safe Drinking Water Act
silica
secondary maximum contaminant level
sulfate
Severn Trent Services
TCLP
Toxicity Characteristic Leaching Procedure
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ABBREVIATIONS AND ACRONYMS (Continued)
TDS total dissolved solids
Ti titanium
TOC total organic carbon
TSS total suspended solids
U uranium
V vanadium
VOC volatile organic compound
Zn zinc
XI
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ACKNOWLEDGMENTS
The authors wish to extend their sincere appreciation to Dan Dimick of Hot Springs Mobile Home Park in
Willard, UT, for monitoring operation of the arsenic removal system and collecting samples from the
treatment and distribution systems throughout the performance evaluation study.
xn
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1.0 INTRODUCTION
1.1 Background
The Safe Drinking Water Act (SDWA) mandates that the 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 (As) 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). In order 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 (ig/L) (EPA, 2003). The final rule required 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 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 Round 1 of this EPA-sponsored demonstration program to provide information on their
water systems. In June 2002, EPA selected 17 out of 115 sites to host the demonstration studies.
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 from 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 project. 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.
In 2003, EPA initiated Round 2 arsenic technology demonstration projects that were partially funded with
Congressional add-on funding to the EPA budget. In June 2003, EPA selected 32 potential demonstration
sites. In September 2003, EPA again solicited proposals from engineering firms and vendors for arsenic
removal technologies. EPA received 148 technical proposals for the 32 host sites, with each site
receiving from two to eight proposals. In April 2004, another technical panel was convened by EPA to
review the proposals and provide recommendations to EPA with the number of proposals per site ranging
from none (for two sites) to a maximum of four. The final selection of the treatment technology at the
sites that received at least one proposal was made, again, through a joint effort by EPA, the state
regulators, and the host site. Since then, four sites have withdrawn from the demonstration program,
reducing the number of sites to 28.
With additional funding from Congress, EPA selected 10 more sites for demonstration under Round 2a.
Among the sites selected was the Hot Springs Mobile Home Park (HSMHP) in Willard, Utah. Somewhat
different from the Round 1 and Round 2 process, Battelle, under EPA's guidance, issued a Request for
Proposal (RFP) on February 14, 2007, to solicit technology proposals from vendors and engineering
firms. Upon closing of the RFP on April 13, 2007, Battelle received from 14 vendors a total of 44
proposals, which were reviewed by a three-expert technical review panel convened at EPA on May 2 and
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3, 2007. Copies of the proposals and recommendations of the review panel were later provided to and
discussed with representatives of the 10 host sites and state regulators in a technology selection meeting
held at each host site during April through August 2007. Final selections of the treatment technology
were made, again, through a joint effort by EPA, the respective state regulators, and the host sites.
Adsorbsia™ GTO™ adsorptive media combined with a Birm®/Filox™ oxidizing media pretreatment was
selected for demonstration at HSMHP in Willard, UT. The treatment system was provided by Filter Tech
Systems, Inc. (Filter Tech) in Grand Junction, CO.
As of July 2011, all 50 systems were operational and the performance evaluations of 49 systems were
completed.
1.2 Treatment Technologies for Arsenic Removal
Technologies selected for Rounds 1, 2, and 2a demonstration included adsorptive media (AM), iron
removal (IR), coagulation/filtration (C/F), ion exchange (IX), reverse osmosis (RO), point-of-use (POU)
RO, and system/process modification. Table 1-1 summarizes the locations, technologies, vendors, system
flowrates, and key source water quality parameters (including As, iron [Fe], and pH). Table 1-2 presents
the number of sites for each technology. AM technology was demonstrated at 30 sites, including four
with IR pretreatment. IR technology was demonstrated at 12 sites, including four with supplemental iron
addition. C/F, IX, and RO technologies were demonstrated at three, two, and one sites, respectively. The
Sunset Ranch Development site that demonstrated POU RO technology had nine under-the-sink RO
units. The Oregon Institute of Technology (OIT) site classified under AM had three AM systems and
eight POU AM units. The Lidgerwood site encompassed only system/process modifications. An
overview of the technology selection and system design for the 12 Round 1 demonstration sites and the
associated capital costs 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/arsenic/resource.htm.
1.3 Project Objectives
The objective of the arsenic demonstration program was to conduct full-scale performance evaluations of
treatment technologies for arsenic removal from drinking water supplies. The specific objectives were 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 arsenic removal system at the HSMHP in Willard, UT
from December 11, 2008, through October 18, 2010. The types of data collected included system
operation, water quality (both across the treatment train and in the distribution system), residuals, and
capital and O&M cost.
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Table 1-1. Summary of Rounds 1, 2, and 2a Arsenic Removal Demonstration
Locations, Technologies, and Source Water Quality
Demonstration
Location
Site Name
Technology (Media)
Vendor
Design
Flow rate
(gpm)
Source Water Quality
As
(ug/L)
Fe
(HS/L)
PH
(S.U.)
Northeast/Ohio
Carmel, ME
Wales, ME
Bow,NH
Goffstown, NH
Rollinsford, NH
Dummerston, VT
Houghton, NY(C)
Woodstock, CT
Pomfret, CT
Felton, DE
Stevensville, MD
Conneaut Lake, PA
Buckeye Lake, OH
Springfield, OH
Carmel Elementary School
Springbrook Mobile Home Park
White Rock Water Company
Orchard Highlands Subdivision
Rollinsford Water and Sewer District
Charette Mobile Home Park
Town of Caneadea
Woodstock Middle School
Seely -Brown Village
Town of Felton
Queen Anne's County
Conneaut Lake Park
Buckeye Lake Head Start Building
Chateau Estates Mobile Home Park
RO
AM (A/I Complex)
AM (G2)
AM(E33)
AM(E33)
AM (A/I Complex)
IR (Macrolite)
AM (Adsorbsia)
AM (ArsenXnp)
C/F (Macrolite)
AM(E33)
IR (Greensand Plus) with ID
AM (ARM 200)
IR & AM (E33)
Norlen's Water
ATS
ADI
AdEdge
AdEdge
ATS
Kinetico
Siemens
SolmeteX
Kinetico
STS
AdEdge
Kinetico
AdEdge
l,200gpd
14
70™
10
100
22
550
17
15
375
300
250
10
250(e)
21
38W
39
33
36W
30
27w
21
25
30W
19W
28W
15(a)
25W
<25
<25
<25
<25
46
<25
l,806(d)
<25
<25
48
270™
157™
1,312™
1,615™
7.9
8.6
7.7
6.9
8.2
7.9
7.6
7.7
7.3
8.2
7.3
8.0
7.6
7.3
Great Lakes/Interior Plains
Brown City, MI
Pentwater, MI
Sandusky, MI
Delavan, WI
Goshen, IN
Fountain City, IN
Waynesville, IL
Geneseo Hills, IL
Greenville, WI
Climax, MN
Sabin, MN
Sauk Centre, MN
Stewart, MN
Lidgerwood, ND
Lead, SD
City of Brown City
Village of Pentwater
City of Sandusky
Vintage on the Ponds
Clinton Christian School
Northeastern Elementary School
Village of Waynesville
Geneseo Hills Subdivision
Town of Greenville
City of Climax
City of Sabin
Big Sauk Lake Mobile Home Park
City of Stewart
City of Lidgerwood
Terry Trojan Water District
AM(E33)
IR (Macrolite) with ID
IR (Aeralater)
IR (Macrolite)
IR&AM(E33)
IR (G2)
IR (Greensand Plus)
AM(E33)
IR (Macrolite)
IR (Macrolite) with ID
IR (Macrolite)
IR (Macrolite)
IR&AM(E33)
Process Modification
AM (ArsenXnp)
STS
Kinetico
Siemens
Kinetico
AdEdge
US Water
Peerless
AdEdge
Kinetico
Kinetico
Kinetico
Kinetico
AdEdge
Kinetico
SolmeteX
640
400
340(e)
40
25
60
96
200
375
140
250
20
250
250
75
14W
13(a)
16W
20W
29W
27W
32W
25W
17W
39W
34W
25W
42W
146W
24
127™
466™
l,387(d)
1,499™
810(d)
1,547™
2,543(d)
248™
7,827™
546™
1,470™
3,078(d)
1,344™
1,325™
<25
7.3
6.9
6.9
7.5
7.4
7.5
7.1
7.4
7.3
7.4
7.3
7.1
7.7
7.2
7.3
Midwest/Southwest
Willard, UT
Amaudville, LA
Alvin, TX
Bruni, TX
Wellman, TX
Anthony, NM
Nambe Pueblo, NM
Hot Springs Mobile Home Park
United Water Systems
Oak Manor Municipal Utility District
Webb Consolidated Independent School District
City of Wellman
Desert Sands Mutual Domestic Water Consumers
Association
Nambe Pueblo Tribe
IR & AM (Adsorbsia)
IR (Macrolite)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
Filter Tech
Kinetico
STS
AdEdge
AdEdge
STS
AdEdge
30
770(e)
150
40
100
320
145
15.4W
35W
19W
56W
45
23(a)
33
332(d)
2,068(d)
95
<25
<25
39
<25
7.5
7.0
7.8
8.0
7.7
7.7
8.5
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Table 1-1. Summary of Rounds 1, 2, and 2a Arsenic Removal Demonstration
Locations, Technologies, and Source Water Quality (Continued)
Demonstration
Location
Taos, NM
Rimrock, AZ
Tohono O'odham
Nation, AZ
Valley Vista, AZ
Site Name
Town of Taos
Arizona Water Company
Tohono O'odham Utility Authority
Arizona Water Company
Technology (Media)
AM(E33)
AM(E33)
AM(E33)
AM (AAFS50/ARM 200)
Vendor
STS
AdEdge
AdEdge
Kinetico
Design
Flow rate
(gpm)
450
90(»)
50
37
Source Water Quality
As
(ug/L)
14
50
32
41
Fe
(ug/L)
59
170
<25
<25
PH
(S.U.)
9.5
7.2
8.2
7.8
Far West
Three Forks, MT
Fruitland, ID
Homedale, ID
Okanogan, WA
Klamath Falls, OR
Vale, OR
Reno, NV
Susanville, CA
Lake Isabella, CA
Tehachapi, CA
City of Three Forks
City of Fruitland
Sunset Ranch Development
City of Okanogan
Oregon Institute of Technology
City of Vale
South Truckee Meadows General Improvement
District
Richmond School District
Upper Bodfish Well CH2-A
Golden Hills Community Service District
C/F (Macrolite)
IX (A300E)
POU RO(1)
C/F (Electromedia-I)
POE AM (Adsorbsia/
ARM200/ArsenXnp)
and POU AM (ARM 200)(B)
IX(ArsenexII)
AM (GFH)
AM (A/I Complex)
AM(HIX)
AM (Isolux)
Kinetico
Kinetico
Kinetico
Filtronics
Kinetico
Kinetico
Siemens
ATS
VEETech
MEI
250
250
75gpd
750
60/60/30
525
350
12
50
150
64
44
52
18
33
17
39
37w
35
15
<25
<25
134
69W
<25
<25
<25
125
125
<25
7.5
7.4
7.5
8.0
7.9
7.5
7.4
7.5
7.5
6.9
AM = adsorptive media process; C/F = coagulation/filtration; EHX = hybrid ion exchanger; IR = iron removal; IR with ID = iron removal with iron addition; IX = ion exchange
process; RO = reverse osmosis
ATS = Aquatic Treatment Systems; MEI = Magnesium Elektron, Inc.; STS = Severn Trent Services
(a) Arsenic existing mostly as As(III).
(b) Design flowrate reduced by 50% due to system reconfiguration from parallel to series operation.
(c) Selected originally to replace Village of Lyman, NE site, which withdrew from program in June 2006; withdrew from program in 2007 and replaced with a home system in
Lewisburg, OH.
(d) Iron existing mostly as Fe(II).
(e) Facilities upgraded systems in Springfield, OH from 150 to 250 gpm, Sandusky, MI from 210 to 340 gpm, and Amaudville, LA from 385 to 770 gpm.
(f) Including nine residential units.
(g) Including eight under-the-sink units.
-------
Table 1-2. Number of Demonstration Sites Under Each Arsenic
Removal Technology
Technologies
Adsorptive Media(a)
Adsorptive Media with Iron Removal Pretreatment
Iron Removal (Oxidation/Filtration)
Iron Removal with Supplemental Iron Addition
Coagulation/Filtration
Ion Exchange
Reverse Osmosis
Point-of-Use Reverse Osmosis(b)
System/Process Modifications
Number
of Sites
26
4
8
4
o
J
2
1
1
1
(a) OIT site at Klamath Falls, OR had three AM systems and
eight POU AM units.
(b) Including nine under-the-sink RO units.
-------
2.0 SUMMARY AND CONCLUSIONS
Based on the information collected during the 22 months of system operation, the following summary and
conclusions were made relating to the overall objectives of the treatment technology demonstration study.
Performance of the arsenic removal technology for use on small systems:
• The use of Birm® in combination with Filox™is effective in removing iron and manganese
and oxidizing soluble As(III). No chemical addition or regeneration is required for Birm® or
.. TM
Filox .
• A daily backwash for 8 min appears to be adequate to maintain Birm®/Filox™ media
performance and prevent media fouling. Adsorbsia™ GTO™ media does not require
backwash.
• Adsorbsia™ GTO™ media can effectively remove soluble As(V) to below 10 (ig/L. By the
last sampling event, total arsenic concentrations following Adsorbsia™ GTO™ reached 6.2
(ig/L after treating approximately 69,200 bed volumes (BV) of water.
Required system O&Mand operator skill levels:
• The system is simple to operate. The daily demand on the operator was typically 30 min to
visually inspect the system and record operational parameters.
Process residuals produced by the technology:
• The only residual produced from system operation was Birm®/Filox™ backwash wastewater.
The amount of wastewater produced amounted to about 10% of the water production, caused
by a high backwashing frequency (i.e., daily).
• Based on an average of 29.8 mg/L of total suspended solids (TSS) in 752 gal of wastewater
produced by backwashing the two vessels daily, approximately 85 g of solids would be
discharged daily. The solids contained 102 mg of arsenic, 8.9 g of iron, and 1.6 g of
manganese.
Capital and O&M cost of the technology:
• The unit capital cost was $0.40/1,000 gal of water treated if the system operated at a 100%
utilization rate. The system's actual unit cost was $2.05/1,000 gal, based on a daily average
water production of 8,354 gal (i.e., about 19% utilization).
• The O&M cost per 1,000 gal of water treated would be $2.20 plus the Adsorbsia™ GTO™
media replacement cost per actual run length.
-------
3.0 MATERIALS AND METHODS
3.1
General Project Approach
Following the predemonstration activities summarized in Table 3-1, the performance evaluation study of
the dual oxidizing media and Adsorbsia GTO arsenic removal system began on December 11, 2008,
and ended on October 18, 2010. Table 3-2 summarizes the types of data collected and considered as part
of the technology evaluation process. The overall system performance was evaluated based on its ability
to consistently remove arsenic to below the MCL of 10 (ig/L through the collection of water samples
across the treatment train, as described in the Study Plan (Bartelle, 2008). The reliability of the system
was evaluated by tracking the unscheduled system downtime and frequency and extent of repair and
replacement. The plant operator recorded unscheduled downtime and repair information on a Repair and
Maintenance Log Sheet.
Table 3-1. Predemonstration Study Activities and Completion Dates
Activity
Introductory Meeting Held
Technology Selection Meeting Held
Project Planning Meeting Held
Draft Letter of Understanding Issued
Final Letter of Understanding Issued
Request for Quotation Issued to Vendor
Vendor Quotation Received by Battelle
Purchase Order Completed and Signed
Engineering Package Submitted to Utah DDW
Permit Issued by Utah DDW
Equipment Arrived at Site
Final Study Plan Issued
System Installation Completed
System Shakedown Completed
Performance Evaluation Begun
Date
November 30, 2006
June 20, 2007
September 18, 2007
November 5, 2007
November 2 1,2007
January 30, 2008
April 5, 2008
May 27, 2008
July 7, 2008
August 7, 2008
September 16, 2008
September 24, 2008
October 24, 2008
October 3 1,2008
December 11, 2008
DDW = Division of Drinking Water
The O&M and operator skill requirements were evaluated based on a combination of quantitative data
and qualitative considerations, including the need for pre- and/or post-treatment, level of system
automation, extent of preventative maintenance activities, frequency of chemical and/or media handling
and inventory, and general knowledge needed for relevant chemical processes and related health and
safety practices. The staffing requirements for the system operation were recorded on an Operator Labor
Hour Log Sheet.
The quantity of aqueous and solid residuals generated was estimated by tracking the volume of backwash
wastewater produced during each backwash cycle. Backwash wastewater and solids were sampled and
analyzed for chemical characteristics.
The cost of the system was evaluated based on the capital cost per gal/min (gpm) (or gal/day [gpd]) of
design capacity and the O&M cost per 1,000 gal of water treated. This task required tracking the capital
-------
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities
Evaluation
Objectives
Performance
Reliability
System O&M and
Operator Skill
Requirements
Residual Management
Cost-Effectiveness
Data Collection
-Ability to consistently meet 10-|ag/L arsenic MCL in treated water
-Unscheduled system downtime
-Frequency and extent of repairs including a description of problems
encountered, materials and supplies needed, and associated labor and
cost incurred
-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 preventative 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, engineering, and installation
-O&M cost for chemical usage, electricity consumption, and labor
cost for equipment, engineering, and installation, as well as the O&M cost for media replacement and
disposal, chemical supply, electrical usage, and labor.
3.2
System O&M and Cost Data Collection
The plant operator performed daily, biweekly, and monthly system O&M and data collection according to
instructions provided by the vendor and Battelle. On a regular basis, the plant operator recorded system
operational data such as pressure, flowrate, totalizer, and hour meter readings on a System Operation Log
Sheet and conducted visual inspections to ensure normal system operations. When problems occurred,
the plant operator contacted the Battelle Study Lead, who determined if the vendor should be contacted
for troubleshooting. The plant operator recorded all relevant information, including the problems
encountered, course of actions taken, materials and supplies used, and associated cost and labor incurred
on the Repair and Maintenance Log Sheet. On a regular basis, the plant operator also measured
temperature, pH, dissolved oxygen (DO), and oxidation-reduction potential (ORP) and recorded the data
on an Onsite Water Quality Parameters Log Sheet.
The capital cost for the arsenic removal system consisted of the cost for equipment, site engineering, and
system installation. The O&M cost consisted of the cost for electricity consumption, and labor. Labor
for various activities, such as the routine system O&M, troubleshooting and repairs, and demonstration-
related work, was tracked using an Operator Labor Hour Log Sheet. The routine system O&M included
activities such as completing field logs, performing system inspections, and others as recommended by
the vendor. The labor for demonstration-related work, including activities such as performing field
measurements, collecting and shipping samples, and communicating with the Battelle Study Lead and the
vendor, was recorded, but not used for cost analysis.
3.3
Sample Collection Procedures and Schedules
To evaluate system performance, samples were collected from the wellhead, across the treatment plant,
during oxidation/filtration vessel backwash, and from the distribution system. Table 3-3 presents the
-------
Table 3-3. Sampling Schedule and Analytes
Sample
Type
Source
Water
Treatment
Plant Water
Distribution
System
Water(f)
Backwash
Wastewater
Backwash
Solids
Sample
Locations'3'
IN
IN, TA, TB,
AP, and TC
Mobile
homes
Backwash
discharge
line (BW)
Wastewater
container
No. of
Samples
1
5(b>
3
2
2
Frequency
Once (during initial
site visit)
Monthly(c'd)
(Speciation
sampling)
Weekly from
01/28/09 to
/,\
ll/04/09(e), none in
12/09 and 01/10,
and monthly
thereafter
(regular sampling)
Monthly to
11/04/09
Monthly
Once
Analytes
Onsite: pH, temperature,
DO, and ORP
Offsite: As (III), As(V),
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble),
Sb (total and soluble),
V (total), Na, Ca, Mg, Cl,
F, NO3, NO2, NH3, SO4,
SiO2, turbidity, alkalinity,
TDS, and TOC
Onsite: pH, temperature,
DO, and/or ORP
Offsite: As(III), As(V),
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble),
Ti (total and soluble),
Ca, Mg, F, N03, S04,
SiO2, P (total), turbidity,
and alkalinity
Onsite: Same as above
Offsite: As (total),
Fe (total), Mn (total),
Ti (total), SiO2, turbidity,
and alkalinity
Total As, Fe, Mn, Cu, and
Pb, pH, and alkalinity
pH, TDS, TSS,
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble), and
Ti (total and soluble)
Al, As, Ba, Ca, Cd, Cu, Fe,
Mg, Mn, Ni, P, Pb, Si, Zn
Sampling Date
11/30/06
See Appendix B
See Appendix B
See Table 4-13
See Table 4-11
06/29/09
(a) Abbreviations in parenthesis corresponding to sample locations shown in Figure 4-6, i.e., IN = at wellhead;
TA= after pre-oxidation vessel A; TB = after pre-oxidation vessel B; AP = after Vessels A and B combined;
TC= after adsorption vessel; DS = distribution system; BW = backwash discharge line
(b) Sampled at IN, TA, TB, AP, and TC from 12/17/08 through 02/18/09 and at IN, AP, and TC thereafter.
(c) Except for June 2009 and June 2010 (with two speciation sampling events taking place in each month) and
August 2010 (with no speciation sampling taking place).
(d) On 03/10/09, samples collected at IN, TA, TB and TC.
(e) On 12/17/08, only total metals were sampled.
(f) Four baseline sampling events taking place from July 16 to September 2, 2008, before system startup.
DO = dissolved oxygen; ORP = oxidation-reduction potential; TDS = total dissolved solids; TSS = total
suspended solids
-------
sampling schedules and analytes measured during each sampling event. 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, 2007). The procedure
for arsenic speciation is described in Appendix A of the QAPP.
3.3.1 Source Water. During the introductory meeting on November 30, 2006, one set of source
water samples was collected from Well No. 2 and speciated using an arsenic specitation kit (see Section
3.4.1). The sample taps were flushed for several minutes before sampling; special care was taken to avoid
agitation, which might have caused unwanted oxidation. Analytes for the source water samples are listed
in Table 3-3.
3.3.2 Treatment Plant Water. The first treatment-plant sampling event occurred on December
17, 2008, when samples were collected for only total metal analysis. The next sampling event occurred
on January 22, 2009, during Battelle's site visit and operator training. Since then through the end of the
performance evaluation study, treatment plant water samples were collected from weekly to monthly,
somewhat different from the schedule laid out in the Battelle Study Plan (2008). The Study Plan called
for weekly sampling, with "speciation sampling" performed during the first week of each four-week cycle
at the wellhead (IN), after the two pre-oxidation vessels (AP), and after the adsorption vessel (TC); and
"regular sampling" performed during the second, third, and fourth weeks at IN, after Pre-oxidation Vessel
A (TA), after Pre-oxidation Vessel B (TB), and TC. Speciation sampling included onsite speciation for
total and soluble arsenic, iron, manganese, and titanium, and a suite of analytes as listed under
"Speciation Sampling" in Table 3-3; regular sampling included total arsenic, iron, manganese, and
titanium and silica, turbidity and alkalinity as listed in Table 3-3.
Actual speciation sampling occurred monthly, with three exceptions for the month of June 2009 and June
2010 (with two speciation sampling events taking place in each month) and the month of August 2010
(with no speciation sampling taking place). Actual regular sampling occurred as called for by the Study
Plan from February 22, 2009, through November 18, 2009, except for the weeks of July 21 and
November 11, 2009, when no sampling took place during these two weeks. Regular sampling was
discontinued during the months of December 2009 and January 2010 but resumed in February 2010 with
a monthly frequency until the end of the performance evaluation study.
Treatment plant water samples were collected at IN, TA, TB, AP, and TC from December 17, 2008,
through February 18, 2009, and at IN, AP, and TC thereafter (except for the week of March 10, 2009,
when samples were taken from IN, TA, TB, and TC).
Beginning on April 19, 2010, only total arsenic, iron, manganese, and titanium were analyzed during each
regular sampling event.
3.3.3 Backwash Wastewater and Solids. The plant operator collected backwash wastewater
samples from each oxidation/filtration vessel on 12 occasions. During backwash, a side stream of
backwash wastewater was directed from the tap on the backwash water discharge line to a clean, 32-gal
plastic container at approximately 1 gpm (Figure 3-1). After the contents in the container were
thoroughly mixed, one aliquot was collected as is and the other filtered with 0.45-(im disc filters. The
samples were analyzed for analytes listed in Table 3-3.
Once during the study period, the contents in the 32-gal plastic container were allowed to settle and the
supernatant was carefully siphoned using a piece of plastic tubing to avoid agitation of settled solids in
the container. The remaining solids/water mixture was then transferred to a 1-gal plastic jar. After solids
in the jar settled and the supernatant was carefully decanted, one aliquot of the solids/water mixture was
air-dried before being acid-digested and analyzed for the metals listed in Table 3-3.
10
-------
Figure 3-1. Backwash Sampling
3.3.4 Spent Media. The media in the oxidation/filtration and adsorption vessels were not
replaced during this demonstration study, therefore, no spent media were produced as residual solids.
3.3.5 Distribution System Water. Water samples were collected from the distribution system to
determine the impact of the arsenic treatment system on the water chemistry in the distribution system,
specifically, the arsenic, lead and copper levels. Prior to the system startup from July 16 to September 2,
2008, four sets of baseline distribution system water samples were collected at three locations (845 West
8700 South House, 845 West 8700 South No. 1, and 845 West 8700 South No. 2). Following system
startup, distribution system sampling continued periodically at the same sampling locations.
The plant operator collected the samples following an instruction sheet developed in accordance with the
Lead and Copper Monitoring and Reporting Guidance for Public Water Systems (EPA, 2002). The date
and time of last water usage before sampling and of actual sample collection were recorded for
calculation of stagnation time. All samples were collected from a cold-water faucet that had not been
used for 6 hr or greater to ensure that stagnant water was sampled.
3.4
Sampling Logistics
3.4.1 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).
Resin columns were prepared in batches at Battelle laboratories in accordance with the procedures
detailed in Appendix A of the EPA-endorsed QAPP (Battelle, 2007).
11
-------
3.4.2 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 affixed with a pre-
printed, color-coded label consisting 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 designating the arsenic speciation bottle (if necessary). The
sampling locations at the treatment plant were color-coded for easy identification. The labeled bottles for
each sampling location were placed in separate zip-lock bags and packed in the cooler.
In addition, all sampling- and shipping-related materials, such as disposable gloves, sampling
instructions, chain-of-custody forms, prepaid/addressed FedEx air bills, and bubble wrap, were included.
The chain-of-custody forms and air bills were complete except for the operator's signature and the sample
dates and times. After preparation, the sample cooler was sent to the site via FedEx for the following
week's sampling event.
3.4.3 Sample Shipping and Handling. After sample collection, samples for offsite analyses were
packed carefully in the original coolers with wet ice and shipped to Battelle. Upon receipt, the sample
custodian 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. Discrepancies noted by the sample custodian were addressed with the plant
operator by the Battelle Study Lead.
Samples for metals analyses were stored at Battelie's inductively coupled plasma-mass spectrometry
(ICP-MS) laboratory. Samples for other water analyses were packed in separate coolers and picked up by
couriers from American Analytical Laboratories (AAL) in Columbus, OH, which was 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 disposition. All samples were archived by the appropriate
laboratories for the respective duration of the required hold time and disposed of properly thereafter.
3.5 Analytical Procedures
The analytical procedures described in detail in Section 4.0 of the EPA-endorsed QAPP (Battelle, 2007)
were followed by Battelle's ICP-MS laboratory and AAL. Laboratory quality assurance/quality control
(QA/QC) of all methods followed the prescribed guidelines. Data quality in terms of precision, accuracy,
method detection limits (MDLs), 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 upon completion of the Arsenic Demonstration Project.
Field measurements of pH, temperature, DO, and ORP were conducted by the plant operator using a
VWR Symphony SP90M5 Handheld Multimeter, 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 Symphony SP90M5 probe in the beaker
until a stable value was obtained.
12
-------
4.1
4.0 RESULTS AND DISCUSSION
Facility Description and Pre-existing Treatment System Infrastructure
HSMHP is located at 845 West 8700 South in Willard, UT. The facility is a community water system
(CWS) supplied by two artesian wells, i.e., Wells No. 1 and No. 2. Well No. 1 has not been used for the
past 10 years and is intended only as a backup well. Designated for this demonstration study, Well No. 2
served a population of 110 to 125 residents. Prior to the study, this well typically operated 5 to 6 hr/day
to meet the average daily demand of approximately 11,000 gal.
Well No. 2 was 10-in in diameter and 288 ft deep with a screened interval extending from 200 to 250 ft
below ground surface (bgs). The static water level was 8 ft bgs. The well was equipped with a 2-
horsepower (hp) submersible pump rated for 30 gpm. The pre-existing Well No. 2 pump house was a 8 ft
x 10 ft x 8 ft wooden shed (Figure 4-1), which housed the wellhead cavity, piping, and a sample tap
(Figure 4-2). Various instrumentation, including pressure gauges and a wellhead totalizer, also was
located inside the pump house. There was no pre-existing treatment at this site. Two hydropneumatic
tanks (Figure 4-3) were used to maintain the line pressure at 35 to 60 lb/in2 (psi). Water entered the
distribution system via a 500-gal underground storage tank (that was also pressurized).
?;-X 3
i^f-^-k'^
^i*.
Figure 4-1. Existing Pump House at HSMHP
13
-------
Figure 4-2. Wellhead Cavity and Piping in Pump House
Figure 4-3. Hydropneumatic Tanks in Pump House
14
-------
4.1.1 Source Water Quality. Source water samples from Well No. 2 were collected on November
30, 2006, when Battelle staff traveled to the site to conduct an introductory meeting for this demonstration
project. The source water was filtered for soluble arsenic, iron, manganese, and antimony, and then
speciated for As(III) and As(V) using field arsenic speciation kits. In addition, pH, temperature, DO, and
ORP also were measured onsite using a field meter. Table 4-1 presents analytical results from the source
water sampling, which are compared to the data provided by EPA and Utah DDW. Table 4-2 presents
year 2000 to 2005 source water quality data provided by Utah DDW.
Table 4-1. HSMHP Well No. 2 Source Water Data
Parameter
Date
pH
Temperature
DO
ORP
Total Alkalinity (as CaCO3)
Total Hardness (as CaCO3)
Turbidity
Total Dissolved Solids (TDS)
Total Organic Carbon (TOC)
Nitrate (as N)
Nitrite (as N)
Ammonia (as N)
Chloride
Fluoride
Sulfate
Silica (as SiO2)
Orthophosphate (as PO4)
P (as PO4)
Al (total)
As (total)
As (soluble)
As (paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Sb (total)
Sb (soluble)
V (total)
Na (total)
Ca (total)
Mg (total)
Unit
S.U.
°c
mg/L
mV
mg/L
mg/L
NTU
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
^g/L
^g/L
^g/L
^g/L
Hg/L
^g/L
HB/L
^g/L
^g/L
^g/L
^g/L
Hg/L
^g/L
mg/L
mg/L
mg/L
EPA
Data
03/20/06
NA
NA
NA
NA
NA
112
NA
NA
NA
NA
NA
NA
NA
NA
6.8
13.4
0.2
0.4
<25
12
NA
NA
NA
NA
213
NA
130
NA
NA
NA
NA
31.9
37.5
4.6
Battelle
Data
11/30/06
7.5
15.5
2.3
285
137
108
2.6
172
<1
0.2
0.05
0.05
23
0.1
6.0
13.3
NA
NA
NA
15.4
13.6
1.8
6.0
7.6
332
129
180
165
O.I
0.1
4.3
32.2
35.6
4.7
Utah DDW
Historical
Data(a)
12/00-12/05
NA
NA
NA
NA
NA
NA
1.4-1.7
180-288
NA
0.2-0.3
0.1
NA
NA
0.1
7.0-9.0
NA
NA
NA
NA
13-14
NA
NA
NA
NA
NA
NA
NA
NA
O.5
NA
NA
28-48
NA
NA
(a) See Table 4-2 for detailed data
DDW = Division of Drinking Water; NA = not available
15
-------
Table 4-2. HSMHP Historic Water Quality Data
Parameter
Unit
Date
Fluoride
Sulfate
Nitrate (as N)
Nitrite (as N)
Turbidity
TDS
Antimony
Arsenic
Barium
Beryllium
Cadmium
Chromium
Cyanide
Mercury
Nickel
Selenium
Sodium
Thallium
Gross Alpha
Gross Beta
mg/L
mg/L
mg/L
mg/L
NTU
mg/L
Mfi/L
^g/L
mg/L
^g/L
^g/L
^g/L
^g/L
Mfi/L
Mfi/L
Mfi/L
mg/L
^g/L
pCi/L
pCi/L
Well No. 2
12/19/00
0.10
7
0.2
0.01
1.4
180
O.5
14
0.07
<1.0
<1
<5.0
<2.0
0.2
<10.0
0.5
28
0.5
NS
NS
12/12/01
NS
NS
0.3
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
12/13/02
NS
NS
0.2
0.10
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
12/08/03
0.10
9
0.2
NS
1.7
288
O.5
13
0.12
<1.0
<1
<5.0
<2.0
0.2
<10.0
0.9
48
0.5
<2
<3
12/07/05
NS
NS
0.2
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
NS
Source: Utah Division of Drinking Water
NS = not sampled
Several factors, such as arsenic concentration and species, natural iron concentration, pH, natural organic
matter, and competing anions, affected the treatment train chosen. The results of the source water
assessment and implications for water treatment are discussed briefly below.
Arsenic. Historically, total arsenic concentrations of source water ranged from 13 to 14 |og/L. Based on
Battelle's sampling results, out of 15.4 |o,g/L of total arsenic, 1.8 |o,g/L existed as particulate arsenic. For
the soluble fraction, 6.0 |o,g/L existed as As(III) and 7.6 |o,g/L existed as As(V). A pre-oxidation step,
therefore, was needed to convert soluble As(III) to soluble As(V) for more effective arsenic removal. No
prior information on arsenic speciation was available. Battelle and EPA's total arsenic results were
slightly higher and lower, respectively, than the historical range provided by Utah DDW.
Iron and Manganese. No historical data on iron concentrations existed. Battelle's data indicated that,
out of 332 |og/L of total iron measured (which was over the 300-|o,g/L secondary maximum contaminant
level [SMCL]), only 129 |o,g/L (or 38%) existed as soluble iron, which was about 10 times higher than
soluble arsenic. EPA's March 20, 2006 sampling event indicated 213 |o,g/L of iron in raw water, which
was slightly lower than Battelle's data (EPA's data did not include soluble iron concentration).
Manganese concentrations of 130 and 180 |o,g/L obtained by EPA and Battelle, respectively, also exceed
the SMCL of 50 |o,g/L. The presence of iron and manganese as well as soluble As(III) in raw water
required pre-oxidation of water prior to Adsorbsia™ GTO™ adsorption.
Competing Anions. Depending on the treatment technology, removal of arsenic potentially can be
influenced by competing anions such as silica and phosphorus. Concentrations of silica at 13.3 to 13.4
mg/L (as SiO2) in raw water is not considered high enough to impact adsorption by Adsorbsia™ GTO™
16
-------
media. Phosphorus concentrations were 0.2 mg/L (as PO4) or 0.4 mg/L (as P) based on EPA data. This
level of phosphorus could impact arsenic removal by iron-based media, but not by Adsorbsia™ GTO™
according to the media manufacturer, The Dow Chemical Company (Dow).
Other Water Quality Parameters. Battelle's data indicate a moderate pH of 7.5, which is within the
commonly-agreed target range of 5.5 to 8.5 for arsenic removal. The raw water samples also were
analyzed for additional parameters as listed in Tables 4-1 and 4-2. Collectively, total hardness
concentrations ranged from 108 to 112 mg/L (as CaCO3); turbidity from 1.4 to 2.6 nephelometric
turbidity unit (NTU); total dissolved solids (TDS) from 172 to 288 mg/L; nitrate from 0.2 to 0.3 mg/L;
barium from 0.07 to 0.12 mg/L; selenium from <0.5 to 0.9 |o,g/L; and sodium from 28 to 48 mg/L. All
other analytes were below detection limits and/or anticipated to be low enough not to adversely affect the
arsenic removal process.
4.1.2 Distribution System. The distribution system for HSMHP consisted of 46 connections.
According to the park owner, the distribution system material is comprised of 2-in diameter galvanized
main with %-in galvanized connections to each home. Three residences within the mobile home park
were selected for monthly baseline and distribution system water sampling to evaluate the effect of the
treatment system on the distribution system water quality.
For compliance purposes, HSMHP samples water periodically from the distribution system for several
parameters: monthly for bacterial analysis; yearly for nitrate; once every three years for lead and copper,
volatile organic compounds (VOCs), and inorganics; and once every three to five years for pesticides.
4.2 Treatment Process Description
4.2.1 Technology Description. Adsorbsia™ GTO™ media was proposed by Filter Tech to remove
arsenic at HSMHP. To protect the media from fouling and to extend media life, a decision was made to
pretreat iron and manganese and to oxidize soluble As(III) to soluble As(V). Because HSMHP preferred
not to use any chemicals, such as chlorine, to oxidize and disinfect water due to its concerns over
changing the taste of water and chemical handling, a pretreatment system of Birm® over Filox™ was
added to the originally proposed Adsorbsia™ GTO™ system. The use of an iron sequester, such as
polyphosphate, had been suggested, but not adopted because it would not oxidize soluble As(III) and
could potentially impact arsenic adsorption with Adsorbsia™ GTO™. Based upon results of a pilot study
conducted at Licking Valley High School in Newark, OH under a separate EPA Task Order, EPA/Battelle
proposed to use the dual oxidizing media, Birm® and Filox™, to remove iron and manganese and
simultaneously oxidize soluble As(III) in source water. Upon acceptance of the approach by all project
stakeholders, including UTAH DDW, HSMHP, and Filter Tech, Filter Tech revised its original design to
include Birm®/Filox™ as a pretreatment.
The treatment system at HSMHP consisted of two steps: oxidation/filtration of iron and manganese and
oxidation of soluble As(III) with Birm® and Filox™ followed by adsorption of soluble As(V) with
Adsorbsia™ GTO™. Backwashing as frequently as daily would be required to remove iron and
manganese solids accumulated in the Birm® and Filox™ media bed and maintain the effectiveness of the
media. This high backwashing frequency was considered important because of the high levels of iron and
manganese. After the oxidation of soluble As(III), water containing soluble As(V) was introduced
downward through the Adsorbsia™ GTO™ bed. When the media reached its capacity, the spent media
would be removed and subject to EPA's Toxicity Characteristic Leaching Procedure (TCLP) before
disposal. The media life depends upon soluble As(V) concentration, pH, and concentrations of competing
anions in source water.
17
-------
4.2.2 Birm* and Filox™. Birm® is an acronym that stands for the "Burgess Iron Removal
Method" and is a proprietary product manufactured by the Clack Corporation (Windsor, Wisconsin).
Birm® is produced by impregnating manganous salts to near saturation on aluminum silicate sand, a base
material, followed by oxidizing manganous ions to solid manganese dioxide using potassium
permanganate. Filox is a brand name for pyrolusite, a naturally-occurring manganese dioxide (MnO2)
in granular form. Both media can oxidize soluble Fe(II) and soluble Mn(II) and trap precipitated particles
in media beds. Both media have NSF International (NSF) Standard 61 approval for use in drinking water.
Table 4-3 presents physical and chemical properties of Birm® and Filox . When used in a mixed bed,
Filox™ stays in the lower half of the bed and Birm® over the upper half because the density of Filox™ is
over double the density of Birm®. As well water is applied downward through the bed, Birm® will
oxidize most of the soluble Fe(II) and soluble Mn(II), leaving soluble As(III) to be oxidized by Filox .
This is based on observations made during the above-mentioned pilot study.
Table 4-3. Physical and Chemical Properties of Birm® and Filox™ Media
Media
Color
Active Ingredient (wt%)
Mesh Size
Effective Size (mm)
Bulk Density (g/L)
Bulk Density (Ib/ft3)
Specific Gravity
Uniformity Coefficient
pH Range
Source
Birm®
Black
0.01% MnO2
10x40
0.48
681
40-45
2
2.7
6.8-9.0
Clack Corporation
Filox™
Black
75-85% MnO2
20x40
Not Available
1,826
114
NA
1.45
5.0-9.0
Matt-Son, Inc.
4.2.3 Adsorbsia™ GTO™ Media. Adsorbsia™ GTO™ is a white, free flowing granular titanium
oxide-based media manufactured by Dow. The media is capable of adsorbing both soluble As(V) and
soluble As(III), with a higher capacity for soluble As(V). Commonly mentioned adsorption pH values
range from 6.5 to 8.5, but the adsorption is less effective at the upper end of the range. According to
Dow, the media capacity for arsenic may be independent of anions such as sulfate, phosphate, and
vanadium. However, the presence of silica can reduce arsenic removal. Adsorbsia™ GTO™ is designed
for non-regenerative applications. When exhausted, it is removed from the vessel and replaced with
virgin media. Spent media from Dow's arsenic loading tests have been shown to pass both the TCLP and
California Waste Extraction Test (CA WET). Table 4-4 presents physical and chemical properties of
Adsorbsia™ GTO™. The media is NSF/ANSI 61 certified and delivered in dry granular form.
4.2.4 System Design and Treatment Process. The 30-gpm treatment system consisted of two
Birm®/Filox™ vessels, one Adsorbsia™ GTO™ vessel, one backwash water supply tank, and two pressure
tanks (pre-existing). Figure 4-4 presents a schematic of the treatment system. Figure 4-5 shows as-built
cross sections of a pre-oxidizing and an adsorption vessel. Table 4-5 specifies key system design
parameters of the treatment system. Figure 4-6 shows a process flowchart, along with the sampling/
analysis schedule. The key process components of the treatment system are discussed as follows:
• Intake - Raw water was fed to the treatment system by a 2-hp submersible pump with a
maximum flowrate of 30 gpm. The reported deadhead pump pressure was 50 psi (on
average), based on a pre-existing pressure gauge installed at the wellhead. A pre-existing
flow meter/totalizer was used to monitor flowrates and volume throughputs. A sample tap
was used to collect raw water samples for chemical analysis.
18
-------
Table 4-4. Physical and Chemical Properties of Adsorbsia™ GTO™ Media
Parameter
Product Type
Particle Size Range (mesh)
Moisture Content (%)
Bulk Density (g/L)
Bulk Density (lb/ft3)
Specific Surface Area (m2/g)
Pore Volume (cnrVg)
Equilibrium Capacity(a) (@ 50 ppb, pH 7)
Arsenic (V) (mg/g)
Arsenic (III) (mg/g)
Value
Titanium oxide based granulation
10-60
<15
705
44
200-300
0.20-0.25
12-15
3-4
Source: The Dow Chemical Company
(a) Static equilibrium capacity measured at room temperature in NSF Standard
53 challenge water.
• Pre-Oxidation - Prior to adsorption, raw water was allowed to flow through two 24-in x 72-
in, in-parallel composite vessels, each containing 19 in of Birm® and 19 in of Filox™. At a
design flowrate of 15 gpm/vessel, it corresponds to a filtration rate of 4.8 gpm/ft2, which is
within the recommended range of 3 to 5 gpm/ft2. During media backwashing, a 15-gpm/ft2
backwash rate was applied to the bed, resulting in >40% and <10% bed expansion for Birm®
and Filox™, respectively. These anticipated bed expansions were well within the 30 in
available freeboard in each pre-oxidation vessel (actual freeboard was <30 in).
The anticipated pressure drop across a clean bed was 4 psi, and the maximum pressure drop
allowed was 14 psi. Pressure gauges and sample taps located before and after each pre-
oxidation vessel were used to monitor pressure drop and effectiveness of pre-oxidation,
respectively. Flowrates and volume throughputs of filtered water were monitored with two
1 !/2-in Signet battery-operated insertion turbine meters/totalizers located on the effluent side
of the two pre-oxidation vessels. Figure 4-7 shows the two pre-oxidation vessels (Vessels A
and B) and one adsorption vessel (Vessel C) and piping connections. Figure 4-8 shows the
programmable logic controller (PLC) panel with a close-up view of the touch screen for the
filter operation.
• Adsorption - Following pre-oxidation, water was fed to a 24-in x 72-in composite vessel
containing 10 ft3 of Adsorbsia™GTO™ underlain by 2 ft3 of garnet. At the design flow rate of
30 gpm, the empty bed contact time (EBCT) was 2.5 min and the hydraulic loading rate was
9.5 gpm/ft2. The anticipated pressure drop across a clean bed was 8 psi, and the maximum
pressure drop was 18 psi. Flowrates and volume throughputs of treated water were monitored
using a 1 !/2-in Signet battery-operated insertion turbine meter/totalizer located on the effluent
side of the vessel. The head loss across the vessel was monitored by a pair of pressure
gauges. A strainer (Figure 4-9) was installed before the adsorption vessel to capture fines
exiting the pre-oxidation vessels. Sample taps were located before and after the pressure
vessel to allow for the collection of water samples for chemical analyses.
• Pressure Tanks - Treated water from Vessel C was temporarily stored in the two pre-
existing pressure tanks (Figure 4-3) in the Well No. 2 pump house. These pressure tanks
were used to maintain the line pressure between 35 and 60 psi.
• Filter Backwash - Frequent backwashing was required to maintain performance of the pre-
oxidizing media. Upon initiation by a time setpoint, backwash was done with Birm®/Filox™-
treated water stored in a 550-gal poly tank (Figure 4-10). During system startup and
shakedown, programming changes were made to include a time delay between
19
-------
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-------
C»VC SLOTTED —
DIS-^RUTOR
JISDniDRAII-,
(2 PLACES;
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ADSORBIA FILTER
Figure 4-5. Cross Sections of Pre-Oxidation and Adsorptive Media Vessels (As Built)
-------
Table 4-5. Design Features of Arsenic Removal System at HSMHP
Design Parameter
Value
Remarks
Pretreatment
No. of Vessels
Configuration
Vessel Size (in)
Depth of Birm® Media (in)
Quantity of Birm® Media (ft3)
Bum81 Design Filtration Rate (gpm/ft2)
Depth of Filox'™ Media (in)
Quantity of Filox™ Media (ft3)
Filox'™ Design Filtration Rate (gpm/ft2)
Clean Bed Pressure Drop (psi)
Maximum Pressure Drop (psi)
Underbedding
Maximum Freeboard (in)
Backwash Rate (gpm/ft2)
Bed Expansion for Birm®/Filox'M (%)
Backwash Flowrate (gpm)
Backwash Duration (min)
Backwash Wastewater Generated (gal/vessel)
Design Backwash Frequency (time/day)
2
Parallel
24 D x 72 H
19
5
4.8
19
5
4.8
4
14
Garnet
30
15
>40/<10
47
8
376
1
-
-
3. 14 ft2 cross sectional area
-
Per vessel (10 ft3 total)
3.0-5.0 gpm/ft2 recommended
-
Per vessel (10 ft3 total)
5.0 gpm/ft2 recommended
-
-
%-in x %-in, 2 ft3
-
Recommend:
10-12 (Birm®); 25-30 (Filox™)
Estimate
-
-
-
Required by manufacturer
Adsorption
No. of Vessels
Vessel Size (in)
Vessel Cross Sectional Area (ft2)
Type of Media
Quantity of Media (ft3)
Media Bed Depth (in)
Design Flowrate (gpm)
Design Hydraulic Loading Rate (gpm/ft2)
EBCT (min)
Clean Bed Pressure Drop (psi)
Maximum Pressure Drop (psi)
Underbedding
Maximum Freeboard (in)
Backwash Rate (gpm/ft2)
Bed Expansion (%)
Backwash Flowrate (gpm)
Backwash Duration (min)
Backwash Wastewater Generated (gal/vessel)
Design Backwash Frequency
1
24 D x 72 H
3.14
Adsorbsia'™
GTO™
-10
38
30
9.5
2.5
8
18
Garnet
28
9
50
27
8
216
As needed
-
-
-
—
-
-
-
-
-
-
-
%-in x %-in, 2 ft3
74% of bed expansion
6-10 gpm/ft2 recommended
Estimated
-
-
-
Filtration System
Average Throughput to System (gal/day)
Daily Throughput (BV/day)
Estimated Media Life (month)
10,800
144
38
Estimated based on 6 hr/day, 30
gpm flowrate
1 BV = 10 ft3 = 74.8 gal
168,000 BV (with pretreatment)
22
-------
Speciation Sampling
(Monthly)
pH, temperature^', DO/ORPW,
As (total and soluble), As (III),
As (V), Fe (total and soluble),
Mn (total and soluble),
Ti (total and soluble),
Ca, Mg, F, NO3, SO4, SiO2,
P (total), turbidity, and alkalinity
Willard,UT
Filter Tech Systems' Preoxidation
and Arsenic Adsorption System
Design Flow: 30 gpm
pH,TDS, TSS,
As (total and soluble),"
Fe (total and soluble), -
Mn (total and soluble), -
Ti (total and soluble)
Footnote
(a) Onsite analyses
Regular Sampling
(Weekly/Monthly)
, temperature'2',
DO/ORPW, As (total),
Fe (total), Mn (total),
Ti (total), SiO2,
turbidity, and alkalinity
BIRM®/
FILOX™
MEDIA
VESSEL A
BIRM®/
FILOX™
MEDIA
VESSEL B
GTO™
MEDIA
VESSEL
C
BACKWASH
WATER SUPPLY
STORAGE TANK
(5 50 GAL)
After Pre-Oxidation
(Combined effluent of
VesselsAandB)
After Vessel C
PRESSURE TANK
ProcessFlow
Backwash Flow
DISTRIBUTION
SYSTEM
Figure 4-6. Process Flow Diagram and Sampling Locations
23
-------
Figure 4-7. Composite Fiberglass Vessels (top) and Associated Piping (bottom)
24
-------
Figure 4-8. PLC Panel
Figure 4-9. Strainer Installed Before Adsorption Vessel
25
-------
Figure 4-10. 550-gal Backwash Supply Tank
completion of pre-oxidation vessel backwash and return of the freshly backwashed vessels to
service (to fill the 550-gal backwash supply tank first [see discussion in Section 4.3.3]). By
design, each pre-oxidation vessel was to be backwashed daily at 47 gpm for 8 min, producing
376 gal of wastewater per vessel.
The AM vessel was backwashed as needed. Once initiated, the vessel was backwashed at 27
gpm for 8 min, producing 216 gal of wastewater. The wastewater produced was discharged
to a septic system behind the treatment building (Figure 4-11). No permit was needed to
discharge the backwash wastewater to the septic system.
Media Replacement. When arsenic concentrations in Adsorbsia™ GTO™-treated water
approaches 10 |og/L, replacement of the media will be necessary. Based on the estimate
provided by the vendor, breakthrough of arsenic at 10 |o,g/L would be expected after treating
approximately 168,000 BV of water. The spent media can be disposed of as non-hazardous
waste in a sanitary landfill if it passes the EPA's TCLP. During the performance evaluation
study, neither the media in the pre-oxidation nor the adsorption vessel required a changeout.
26
-------
Figure 4-11. Backwash Discharge Point Behind Treatment Building
4.3 System Installation
4.3.1 Permitting. For the permit application, Filter Tech prepared an engineering package,
including design drawings and a process description of the proposed treatment system. After it was
reviewed and signed by a Utah-licensed professional engineer (Hansen, Allen & Luce, Inc.), the package
was submitted to and approved by Utah DDW on July 7 and August 7, 2008, respectively.
Following installation of the treatment system, Hansen, Allen & Luce, Inc. submitted an operating permit
request (that included final as-built drawings and bacteria test results) to Utah DDW. Utah DDW issued
on December 11, 2008, a temporary permit, which stipulated a monitoring and a quarterly reporting
requirement and remained effective through December 31, 2009. As opposed to a permanent permit, the
temporary permit was issue because Utah DDW needed to evaluate the data to be generated during the
EPA demonstration study and determine an appropriate monitoring schedule. The operator obtained a
permanent permit before the temporary permit had expired.
4.3.2 Building Preparation. To house the new treatment system, a 10-ft * 10-ft * 8-ft
prefabricated metal structure with a 6 ft * 6 ft roll-up door (Figure 4-12) was installed on a concrete pad
poured in late August 2008. The building installation began on September 6, 2008, and was completed
on September 11,2008.
4.3.3 Installation, Shakedown, and Startup. Installation of the treatment system began on
September 16, 2008. Installation activities included offloading, placing, and connecting the pre-
oxidation/adsorption vessels to influent, effluent and backwash tie-in points, and completing electrical
wiring for system controls. Several trips were required to complete the installation due to an inaccurate
estimate of the building height. The original system piping was pre-fabricated based on a ceiling/wall
height of 8 ft. Although the ceiling height was 8 ft, the walls were several feet shorter, resulting in
insufficient clearance over the vessels for the rigid, pre-fabricated piping to fit in. Therefore, flexible
tubing had to be used, instead, for vessel inlet and outlet connections (Figure 4-13). The pre-
27
-------
Figure 4-12. New Treatment Building
Figure 4-13. Treatment System Installed
28
-------
oxidation/adsorption vessels and a backwash pump were bolted to the floor with concrete anchors and
pipe supports mounted to ceiling joints.
Media Loading. A slotted polyvinyl chloride (PVC) underdrain was installed in the bottom of each
vessel with a l!/2-in Schedule 40 standpipe. Two ft3 of garnet (%-in x Mrin), 5 ft3 of Filox™, and 5 ft3 of
Birm® were then loaded sequentially through a 4-in opening at the top of each pre-oxidation vessel. The
amount of garnet was enough to cover the underdrain. The depth of each media layer was measured at
approximately 19.7 in, close to the calculated value of 19.1 in based on the media volume and vessel
diameter.
On October 4, 2008, 2 ft3 of garnet and 10 ft3 of Adsorbsia™ GTO™ were loaded into the adsorption
vessel. The media depth was measured at approximately 39.4 in, close to the calculated value of 38.2 in
based on the media volume and vessel diameter. Freeboard was measured from the top of the vessel to
the top of the media layer to ensure sufficient room for backwashing. The freeboard measured was 20 in
in the pre-oxidation vessels and 21 in in the adsorption vessel. Although smaller than the design values of
30 and 28 in, respectively (see Table 4-5), these freeboards provided more than 50% of bed expansion,
sufficient to meet media backwashing needs.
Media Backwashing. To prepare for media backwashing, the 550-gal backwash supply tank was first
filled with well water via piping that bypassed the treatment system (see Figure 4-14). Because the well
water contained a large amount of silt, a layer of sediment was found to deposit at the bottom of the tank.
Therefore, the piping to the tank had to be disconnected and the tank was rinsed out. The tank was then
refilled to approximately 460 gal.
Figure 4-14. Backwash Supply Tank and Inlet Piping
The pre-oxidation vessels were backwashed manually one at a time. Backwash flowrates were controlled
by throttling a 2-in PVC ball valve on the backwash line. The initial flowrate to a vessel was 8.5 gpm,
which was maintained until the vessel was completely filled. Afterwards, the flowrate was incrementally
increased to 20, 38, and 47 gpm (or 6.4, 12.1, and 15.0 gpm/ft2). The flowrate was then kept steady at 47
gpm until the backwash supply tank was almost empty. The amount of water in the backwash supply
tank (460 gal) was enough to allow for a complete backwash cycle at the design flowrate of 47 gpm and
the design duration of 8 min.
-------
Each pre-oxidation vessel was backwashed five times over a two-day period on October 22 and 23, 2008.
Although the backwash effluent was never completely cleared up after the five backwashes (Figure 4-15),
the vessel effluent looked clear, indicating a clean bed. The total amount of water used for backwash was
5,206 gal. The freeboard measured in both vessels after the fifth backwash was 21 in, indicating the loss
of approximately 1 in of media during backwash. The new bed depth was 18.7 in.
Figure 4-15. Wastewater Collected After First (left) and Fifth Backwashes (right)
To prepare Adsorbsia™ GTO™ media for backwashing, the backwash supply tank was cleaned and refilled
with 430 gal of treated water from the newly backwashed pre-oxidation vessels. The 430 gal of water in
the backwash supply tank would last for 16 min (or twice the design duration) if the backwash flowrate
was maintained at the design flowrate of 27 gpm.
The Adsorbsia™ GTO™ startup procedure called for backwashing the media with 75 to 90 BV (5,610 to
6,732 gal) of water at 6 to 10 gpm/ft2 (or 18.9 to 31.4 gpm). After filling the vessel at 6 gpm (or 2
gpm/ft2), the backwash flowrate was set at 14.5 gpm to determine if this flowrate would result in media
loss. During the first backwash (with approximately 430 gal of water), some media loss was observed;
the backwash flowrate was therefore reduced to 10 gpm. After three and six backwash cycles (each with
approximately 430 gal of water), the flowrate was increased to 19 and 27.5 gpm (or 6.1 and 8.8 gpm/ft2),
respectively. Upon completion of the twelfth backwash, backwash wastewater had gone from milky
(after the initial backwash) to cloudy (Figure 4-16) and a total of 5,558 gal (or 74.3 BV) of water had
been used for backwash. The vessels were backwashed one more time in preparation of disinfection. At
this point, a total of 12,233 gal of water had been used to backwash all three vessels.
Because the freeboard in the adsorption vessel was not re-measured after backwash, the pre-backwash
bed depth of 39.4 in was used to calculate BV, which was 10.3 ft3 or 77.1 gal. This bed depth also was
shown in the as-built cross section drawing in Figure 4-5.
Vessel Disinfection. The two pre-oxidation and one adsorption vessels were disinfected using a 185
mg/L (as C12) sodium hypochlorite (NaOCl) solution, prepared by adding 1.4 gal of Clorox® bleach
(containing 6% NaOCl) into 500 gal of treated water in the backwash supply tank. After 140 gal of the
-------
Figure 4-16. Appearance of Backwash Wastewater After
First (left) and Twelfth Backwashes (right)
chlorine solution was pumped upflow through each vessel at 6 gpm, the vessels were allowed to sit
overnight. Because the effluent from each vessel contained only a trace level of chlorine residuals, the
disinfection procedure was repeated. Upon applying additional 100 gal of the chlorine solution through
each vessel, greater than 20 mg/L (as C12) of chlorine residuals were measured in the vessel effluent. The
vessels were then rinsed with well water in the service mode (i.e., parallel through the pre-oxidation
vessels and then the adsorption vessel) until chlorine residuals in the vessel effluent were below its MDL.
A sample was collected downstream of the Adsorbsia™ GTO™ vessel for the Bac-T test.
Startup Issues. Soon after system startup on December 11, 2008, it was noted that when the system
pressure became low, the normally closed, hydraulically-operated diaphragm valves on the backwash line
would open (due to lack of pressure on the diaphragm to close the valves), causing water to constantly
leak and bypass the treatment system. To alleviate this concern, a small bladder tank was installed on the
treated water line and filled with pressurized water from the distribution system and a check valve was
installed to keep the tank pressurized if there was a loss of pressure in the system. Meanwhile,
the hydraulic line supplying the diaphragm valves was taken after the check valve but before the tank so
that there was always enough pressure in the bladder tank to open and close the diaphragm
valves. During normal operation, the bladder tank was kept at the same pressure as the system. However,
when the well pump went into sleep mode or if the system lost pressure, the bladder tank would maintain
the normal system pressure and keep the diaphragm valves closed.
In addition, the backwash supply tank refill line was separated from the service line so that it would not
cause the variable frequency drive (VFD) pump to run at a higher flowrate during refill of the backwash
supply tank. This modification reduced the well pump flowrate from approximately 30 to 20 gpm during
refill of the backwash supply tank.
31
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Issues Observed During Battelle's Site Visit. On January 21, 2009, two Battelle staff members visited
the site to inspect the system and provide operator training on the data and sample collection. When
onsite, the system was backwashed for observation and residual sampling. Table 4-6 summarizes PLC
settings and measurements taken during backwash. Table 4-7 presents flowrates measured during refill of
the backwash supply tank. The time delay between Vessels A and B backwashing was initially set at
2,150 sec (~36 min) for the backwash supply tank to be refilled. Since it took only 1,660 sec (~27 min) to
refill the tank, the time delay was shortened to 1,800 sec (30 min). The 27 min refill time was based on a
refill flowrate of 13 gpm. Based on the data presented in Table 4-7, refill flowrates could be as high as
17.2 gpm. Therefore, the refill time could be as short as 21 min.
Table 4-6. Backwash Settings and Measurements
Setting
Backwash Duration
Backwash Frequency
Backwash Flowrate
Backwash Tank High Mark
Backwash Tank Low Mark
Backwash Volume for TA
Backwash Volume for TB
Refill Rate to Backwash Tank
Actual Time Taken to Refill
Current Delay Setting
New Delay Setting
Control Mechanism
PLC Setting
PLC Setting
Valve Control (Manually adjusted)
High Float Switch (Pump on)
Low Float Switch (Pump off)
PLC Setting/Float Switches/Valve
PLC Setting/Float Switches/Valve
Valve Control (Manually adjusted)
None (Timed during backwash)
PLC Setting
PLC Setting
Value
8 min
Weekly (Fridays, 13:00)
-45-48 gpm
-470 gal
-110 gal
374 gal
383 gal
-13 gpm
1,660 sec (-27 min)
2,150 sec (-36 min)
1,800 sec (30 min)
Table 4-7. Flowrates Measured During Refill of Backwash Supply Tank
Time
NA
17:55
"IN"
Flowrate
19 gpm
23.6 gpm
TA
Flowrate
(= IN-TB)
11 gpm
15. 2 gpm
TB
Flowrate
8 gpm
8.4 gpm
TC
Flowrate
4.8 gpm
6.4 gpm
Refill Rate
(= IN-TC)
14.2 gpm
17.2 gpm
Samples of backwash wastewater were collected at the backwash discharge point at the beginning, during,
and the end of pre-oxidizing media backwashing. These samples were collected for visual observation of
water quality and signs of media loss. As shown in Figure 4-17, all three samples looked cloudy but
contained little media. This suggests that the media needed to be backwashed more frequently than
weekly and that bed expansion during backwash was within the available freeboard height. Water
samples collected at the AP sampling location during refill of the backwash supply tank also were cloudy
and contained a small amount of media (see photographs in Figure 4-18 for a water sample taken at AP
versus a water sample taken at IN). This indicates that the pre-oxidizing media had not been thoroughly
cleaned during backwashing and that the media was not given enough time to settle prior to being put
back into service to refill the backwash supply tank.
Based on the above-mentioned and other observations made during the site visit, a punch list was
developed and discussed with Filter Tech. Punch-list items included the following:
• Install a sediment filter prior to the inlet flow totalizer
32
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Figure 4-17. Backwash Wastewater Samples Collected at Beginning,
Middle, and End of a Backwash Cycle
Figure 4-18. Comparison of IN (right) and AP (left) Samples Collected During Refill of
Backwash Supply Tank
Install a high pressure cut-off switch for the well pump
Replace all pressure gauges with more accurate gauges
Install a flow totalizer for Tank A
Establish a delay after each filter has been backwashed to allow media to settle before putting
back into service to refill the backwash supply tank
33
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• Set timer to backwash daily
• Supply a revised schematic that reflects all system modifications that have been made
• Install a new backwash sample tap
• Develop a plan for backwashing Tank C.
Filter Tech ordered materials and parts and returned to the site on April 18 to 19, 2009 to complete all
punch-list items mentioned above. While onsite, a separate backwash supply line to Tank C was installed
to allow backwashing of Tank C. Tank C was backwashed; the backwash discharge showed no sediment
buildup.
4.4 System Operation
4.4.1 Operational Parameters. The operational parameters for the demonstration study were
tabulated and are attached as Appendix A. Table 4-8 summarizes key parameters. The performance
evaluation study began on December 11, 2008, and ended on October 18, 2010. During the study period,
the well pump operated for a total of 15,835 hr, averaging 23.4 hr/day (for 676 days). The well pump ran
almost around the clock, occasionally going into a sleep mode.
As noted in Section 4.2, flowrates and volume throughputs were tracked by five Signet insertion turbine
flow meters/totalizers located separately at the system inlet, after Vessels A, B, and C, and on the
backwash water supply line. The inlet flow meter/totalizer stopped registering incoming flow on March
30, 2010, rendering it useless for tracking the system flow. The flow meter/totalizer on Vessel A was not
installed until April 9, 2009; therefore, the flow through Vessel A prior to this date was estimated by
subtracting the flow through Vessel B from the flow through Vessel C. Although not done, this amount
should have been further adjusted by adding half of the flow used to refill the backwash supply tank prior
to April 9, 2009.
In theory, the inlet flow should be equal to the sum of the flow through Vessels A and B and equal to the
sum of the flow through Vessel C and the flow to refill the backwash supply tank. Based on the meters/
totalizers installed on the three vessels, the total amount of water treated by the two pre-oxidation vessels
was 5,198,000 gal (including 2,571,000 and 2,627,000 gal through Vessels A and B, respectively); the
total amount of water treated by the adsorption vessel (Vessel C) was 5,629,000 gal. Instead of being
lower, this amount (5,629,000 gal) was actually higher than the total flow through both pre-oxidation
vessels. While it was not clear what had caused this to occur, the way the flow meters/totalizers were
installed (i.e., flexible hoses with short straight length) could contribute, in part, to the discrepancies
observed. As specified by the meter manufacturer, depending on the piping configurations, the straight
length upstream from the flow sensor should be 10 to 50 times (15 to 75 in) the inner diameter of the pipe
and the straight length downstream from the flow sensor should be at least five times (7.5 in) the inner
diameter of the pipe. With all piping/valves/meters/gauges installed in a rather congested area as shown
in Figure 4-7, these requirements most likely were not met. The other possible cause was the ability of
the flow meters/totalizers to register flow with <4 gpm flowrates. This is discussed in detail in Section
4.4.3.
Based on the Vessel C flow meter/totalizer, the system treated 5,629,000 gal (or 73,000 BV) of water
(bed volumes were calculated based on 10.3 ft3 [or 77.1 gal] of media). Daily demands through the entire
study period ranged from 2,476 to 21,987 gal and averaged 8,354 gal, which was 24% lower than the
11,000 gpd provided by the operator prior to the demonstration study.
34
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Table 4-8. Summary of System Operation
Operational Parameter
Operating Period
Total Operating Time (day)
Value/Condition
12/11/08-10/18/10
676
Well Pump
Total Operating Time (hr)
Average Daily Run Time (hr/day)
15,835
23.4
Birnf/Filox™ Pre-Oxidation
Throughput (gal)
Instantaneous Flowrate (gpm)
Hydraulic Loading (gpm/ft2)
Vessel/System Pressure and Ap (psi)
Vessel A
2,571,000(a)
Vessel A
4.5 [0.6-13.8]
Vessel A
1.4 [0.2-4.4]
Vessel
A 61
B 61
Vessel B
2,627,000
Vessel B
4.6 [0.6-20.9]
Vessel B
1.5 [0.2-6.7]
Inlet Outlet
[50-92] 59 [48-9
[50-92] 59 [40-9
Combined
5,198,000
Combined
9.3 [1.2-27.1]
Ap.
4] 2 [0-14]
8] 2 [0-20]
Adsorbsia™ Adsorption System
Throughput (gal)
Daily Demand (gal/day)
Bed Volume (BV)
Instantaneous Flowrate (gpm)
EBCT (min)
Vessel/System Pressure and Ap (psi)
5,629,000
8,354 [2,476-21,987]
73,010(b)
7.3 [0.7-24.0]
10.6 [3.2-1 10]
Vessel
C 60
Inlet Outlet
[40-76] 54 [45-6
Ap.
2] 6 [0-22]
Birm "/Filox™ Backwash Operation
Backwash Frequency
Backwash Flowrate (gpm)
Number of Backwash Cycles
Duration (min)
Backwash Volume (gal/cycle)
Total Wastewater Produced (gal)
Wastewater Production Rate
Daily
47
676
8
776
511,800
10%
(a) Vessel A totalizer installed on April 9, 2009; throughput prior to April 9, 2008,
calculated based on Vessels B and C totalizer readings.
(b) Calculated based on 10.3 ft3 (or 77.1 gal) of media in vessel.
Instantaneous flowrates through Vessels A and B (as read from the respective Signet flow meters)
fluctuated extensively from 0.6 to 20.9 gpm. Instantaneous flowrates through Vessel C also fluctuated
extensively from 0.7 to 24 gpm. The higher flowrates occurred when the backwash supply tank was
being filled, either from the combined effluent of Vessels A and B or from the effluent of Vessel C. The
fill rate to the backwash supply tank was controlled by a PVC ball valve and could be manually
adjusted. The fill rate was set to be less than the system maximum flowrate because pumping at a high
flowrate over an extended period could cause an increase in the sediment content in well water.
The average flowrate through the two pre-oxidation vessels was 9.3 gpm; the average flowrate through
the adsorption vessel was 7.3 gpm. These flowrates were much lower than the 30-gpm design value as
shown in Table 4-5. At these average flowrates, hydraulic loading rates were 1.4 and 2.3 gpm/ft2,
respectively (compared to the design values of 4.8 and 9.5 gpm/ft2, respectively). EBCTs with the AM
ranged from 3.2 to 110 min and averaged 10.6 min, which was four times the vendor-recommended
EBCT of 2.5 min.
35
-------
System inlet pressure readings ranged from 50 to 92 psi averaging 61 psi. Pre-oxidation outlet pressure
readings ranged from 40 to 98 psi, averaging 59 psi. Differential pressure (Ap) across the pre-oxidation
vessels ranged from 0 to 20 psi and averaged 2 psi. These Ap readings reflect results of a daily backwash
schedule. Ap across the adsorption vessel ranged from 0 to 22 psi and averaged 6 psi. These Ap readings
reflect results of one backwash on April 18, 2009 throughout the study period.
From December 11, 2008, through October 18, 2010, 511,800 gal of backwash wastewater was produced.
Assuming that daily backwash began on December 11, 2008, 676 backwashes would have been done by
the end of the study period. Therefore, each backwash would have produced 776 gal of wastewater,
which is very close to the design value of 752 gal for both vessels (at 47 gpm for 8 min per vessel).
4.4.2 Residual Management. Residuals generated by the operation of the system included only
backwash wastewater. Neither the oxidation media (Birm®/Filox™) nor the AM (Adsorbsia™ GTO™)
were replaced during the study period. The wastewater produced was discharged to the septic tank
behind the treatment building (Figure 4-11). No permit was necessary to discharge the backwash
wastewater to the septic system.
4.4.3 System/Operation Reliability and Simplicity. There were no major operational issues
affecting the system; only minor repairs were made to the system. Filter Tech made a site visit on June
13, 2009, to calibrate all flow meters/totalizers. The issue was that the new flow totalizer on Vessel A
would not register flow when its flowrate was lower than 4 gpm. This was unlike the flow meters/
totalizers on both Vessel B and the backwash water supply line that were capable of registering flow
down to 3 gpm due to the use of a more sensitive sensor. Filter Tech switched the flow meter/totalizer on
Vessel A with one on the backwash water supply line so that both Vessels A and B had identical flow
meters/totalizers. On August 25, 2009, and June 22, 2010, the operator took the system offline to replace
a leaking nut on the piping leading to Vessel B. The system was offline for several days until the repair
work was complete.
The system O&M and operator skill requirements are discussed below in relation 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 oxidation/filtration with Birm®/Filox™
media for iron and manganese removal and soluble As(III) oxidation. Iron and manganese particles
formed were backwashed out of media beds. There was no post chlorination of the distribution water.
System Automation. The Birm®/Filox™ and Adsorbsia™ GTO™ system included automated controls for
service and backwash operations.
Operator Skill Requirements. Under normal operating conditions, the skills required to operate the
arsenic treatment system were minimal. The operator's duties were to monitor the pre-oxidation and
adsorption vessels, and initiate manual backwash when necessary.
Utah's Operator Certification Program is authorized by Section R3 09-105-11 of the Utah Public Drinking
Water Rules. The rules state that "all community and non-transient non-community water systems or any
public system that employs treatment techniques for surface water or ground water under the direct
influence of surface water shall have an appropriately certified operator." The specific requirements are
located in Section 309-300, Certification Rules for Water Supply Operators.
36
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All public drinking water systems within the state of Utah are assigned a complexity level (I, II, III, IV)
and discipline (Treatment or Distribution) for the certification requirements of their operators. Any
operator who makes independent decisions that affect the sanitary quality, safety, and adequacy of the
water to their system needs to be certified to the grade of the system. HSMHP was classified as a
"distribution" facility and designated as a "small system" serving a population between 25 and 500
persons. Operators running a "small system" are required to obtain 2.0 continuing education units within
a three-year period to renew certification.
Preventive Maintenance Activities. Preventive maintenance tasks included such items as periodic checks
of flow meters and pressure gauges and inspection of system piping and valves. Typically, the operator
performed these duties only when he was onsite for routine activities. The operator recorded flow,
volume, and pressure readings of the system daily.
Chemical/Media Handling and Inventory Requirements. No chemical was used as part of the treatment
system at the HSMHP.
4.5 System Performance
The performance of the HSMHP arsenic removal system was evaluated based on analyses of water
samples collected from the treatment plant, the media backwash residuals, and distribution system.
4.5.1 Treatment Plant Sampling. Water samples were collected on 64 occasions, including three
duplicate events, with field speciation performed on 22 occasions at the IN, AP, and TC sampling
locations. TA and TB also were sampled seven times between December 17, 2008, and February 18,
2009, and on March 10, 2009, and then discontinued thereafter. Sample location AP was not sampled on
March 10, 2009.
Table 4-9 presents a statistical summary of key analytical results of arsenic species, total and soluble iron,
and manganese measured at the IN, AP, and TC sampling locations across the treatment train. Table 4-10
summarizes the statistical summary of other water quality parameters at the same three locations. The
analytical data at TA and TB were not used for the statistical analysis due to small sample sizes (i.e., 3 to
7). Appendix B contains a complete set of analytical results for the demonstration study. The results of
the treatment plant sampling are discussed below.
Arsenic. The key parameter for evaluating the treatment effectiveness was the arsenic concentration in
treated water. Figure 4-19 contains three bar charts showing concentrations of arsenic species, including
particulate arsenic, soluble As(III), and soluble As(V) at the IN, AP, and TC locations for each of the 22
speciation events. Total arsenic concentrations in source water ranged from 9.4 to 21.1 (ig/L and
averaged 13.2 (ig/L (Table 4-9). Of the soluble fraction, As(III) and As(V) each accounted for about half
of the concentration at 6.0 and 5.8 (ig/L, respectively (on average). Except for one spike of 8.8 (ig/L on
September 23, 2009, particulate arsenic concentrations were low, averaging 1.3 (ig/L.
After the Birm®/Filox™ treatment, there was 21% reduction in total arsenic concentration to 10.4 (ig/L (on
average), indicating removal by Birm®/Filox™. The remaining arsenic existed primarily as soluble As(V)
with concentrations ranging from 8.7 to 11.1 (ig/L and averaging 10.0 (ig/L. Soluble As(III) and
particulate arsenic concentrations were low, averaging 0.3 and 0.2 (ig/L, respectively (on average).
Therefore, the Birm®/Filox™ treatment was effective in oxidizing soluble As(III) to soluble As(V)
throughout the study period.
The Adsorbsia™ GTO™ media further removed soluble As(V) to below the 10-(ig/L MCL. Figure 4-20
presents total arsenic breakthrough curves from the pre-oxidation and adsorption vessels. By September
37
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Table 4-9. Summary of Arsenic, Iron, and Manganese Analytical Results
Parameters
As (total)
As (soluble)
As
(paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Sample
Location
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
Unit
Hg/L
ug/L
Hg/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
Hg/L
ug/L
Hg/L
ug/L
Hg/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Sample
Count
64
60
64
22
21
22
22
21
22
22
21
22
22
21
22
64
63
64
22
21
22
64
63
64
22
21
22
Concentration
Minimum
9.4
5.4
<0.1
7.9
9.0
0.1
0.1
0.1
0.1
2.8
0.1
0.1
3.9
8.7
0.1
<25
<25
<25
36.9
<25
<25
87.6
0.1
0.1
83.3
0.1
0.1
Maximum
21.1
13.0
7.0
15.1
11.4
7.2
8.8
1.6
1.1
8.3
1.0
2.1
10.0
11.1
7.1
871
62.7
62.1
210
59
<25
286
45.1
50.1
130
0.3
38.8
Average
13.2
10.4
_(a)
11.8
10.3
_(a)
1.3
0.2
_(a)
6.0
0.3
_(a)
5.8
10.0
_(a)
276
<25
<25
93
<25
<25
116
4.0
2.6
109
0.1
2.4
Standard
Deviation
2.4
1.2
_(a)
1.5
0.7
_(a)
1.8
0.4
_(a)
1.5
0.2
_(a)
1.3
0.7
_(a)
198
6.3
7.2
42.9
10.2
0.0
25.7
8.4
8.6
13.0
0.1
8.5
One-half of detection limit used for concentrations less than detection limit for calculations.
Duplicate samples included in calculations.
(a) Statistics not meaningful; see arsenic breakthrough curves at TC location in Figure 4-20.
14, 2010, when the last set of samples was collected, total arsenic concentrations in treated water after
Adsorbsia™ GTO™ had reached 6.2 (ig/L. The amount of water treated at this point was 69,200 BV.
Iron. Total iron concentrations in raw water ranged from <25 to 871 (ig/L and averaged 276 (ig/L. The
soluble fraction ranged from 37 to 210 (ig/L and averaged 93 (ig/L. Figure 4-21 presents total iron
concentrations at the IN, AP, and TC locations for all 64 sampling events. Figure 4-22 contains three bar
charts showing concentrations of particulate and soluble iron at the IN, AP, and TC locations for each of
the 22 speciation events. The data indicated that iron was mostly removed to below the MDL of 25 (ig/L.
Iron solids accumulated in the Birm®/Filox™ bed were removed via daily backwashing, which was able to
maintain media performance without any signs of iron leakage or media fouling after close to two years
of service.
Manganese. Figure 4-23 presents total manganese concentrations at the IN, AP, and TC locations for all
64 sampling events. Total manganese levels in source water ranged from 87.6 to 286 (ig/L and averaged
116 (ig/L, which existed almost entirely in the soluble form. Following the oxidation/filtration by
Birm®/Filox™, total manganese concentrations were reduced to 4.0 (ig/L (on average) with no
38
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Table 4-10. Summary of Other Water Quality Parameter Results
Parameters
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica
(as SiO2)
Turbidity
pH
Temperature
DO
ORP
Total
Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Ti (total)
Ti (soluble)
Sample
Location
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
IN
AP
TC
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
^g/L
^g/L
HB/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
s.u.
s.u.
s.u.
°c
°c
°c
mg/L
mg/L
mg/L
mV
mV
mV
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
Sample
Count
55
54
55
22
21
22
22
21
22
22
21
22
22
21
22
55
54
55
55
54
55
50
49
49
51
51
50
49
49
48
51
50
50
22
21
22
22
21
22
22
21
22
64
63
64
22
21
22
Concentration
Minimum
135
129
135
0.1
0.1
0.1
3.2
5.7
5.7
0.1
0.1
0.2
56.6
18.7
<10
13.3
13.9
14.0
0.7
O.I
O.I
7.4
7.5
7.1
9.0
9.3
9.1
1.6
1.3
1.1
112
47.1
41.2
96.8
103
98.0
73.4
78.0
73.8
16.7
16.2
16.4
1.1
0.9
0.9
0.9
0.5
0.8
Maximum
152
153
161
0.1
0.2
0.2
7.0
6.8
7.1
0.3
0.4
0.4
170
99.9
77.6
17.5
17.6
18.0
10.0
7.4
9.9
8.0
8.1
8.1
22.0
21.7
22.3
5.8
4.1
5.3
248
240
244
129
126
130
112
110
113
26.6
25.4
25.5
3.3
6.1
444
1.9
1.9
2.6
Average
143
143
143
0.1
0.1
0.1
6.1
6.2
6.3
0.2
0.3
0.3
112
67.1
36.7
15.4
15.4
15.5
2.9
0.8
1.4
7.6
7.7
7.8
17.2
17.4
17.6
2.4
2.0
2.1
199
191
187
114
115
113
93.8
94.5
93.2
20.4
20.1
20.1
1.8
1.7
16.3
1.4
1.3
1.4
Standard
Deviation
4.3
4.7
5.1
0.0
0.0
0.0
0.7
0.3
0.4
0.0
0.1
0.0
29.0
18.5
27.1
0.8
0.8
0.8
2.1
1.3
1.8
0.1
0.1
0.2
2.8
2.6
2.7
1.0
0.6
0.7
26.1
28.3
28.5
8.3
6.8
8.4
9.1
7.9
9.2
2.3
2.2
2.4
0.5
0.9
65.9
0.3
0.3
0.4
One-half of detection limit used for concentrations less than detection limit for calculations.
Duplicate samples included in calculations.
39
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As Speciation at Wellhead (IN)
20.0
15.0
10.0
0 0
•As(V)
nAs(particulate)
0
As Speciation After Pie oxidation (AP)
20.0
15.0
10.0
2 5.0
0 0
BAs(V) BAsdH) DAs(pailiculate)
As Speciatioii after Adsorption (TC)
g
g 15.0
I 10.0
3
U
! 5.0
n_As(Y) •A^(EI) nAs(paiticulate)
; _._n= .^nflnnnnnPnn
—
i^N^S^ ^^^^^^^N<^<^v^^N^ d^ ^d^^4^
Figure 4-19. Concentrations of Various Arsenic Species at IN, AP, and TC
Sampling Locations
40
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25.0
1000
10,000 20,000 30,000 40,000
Run Length (BV)
50,000 60,000 70,000
Figure 4-20. Total Arsenic Breakthrough Curves
12/01/08 03/31/09 07/29/09 11/26/09 03/26/10 07/24/10 11/21/10
Sampling Date
Figure 4-21. Total Iron Concentrations at IN, AP, and TC Sampling Locations
41
-------
1,000
^ 800
| 600
I
| 400
I 200
0
I
2
1
u
o
1,000
800
600
400
200
I
1,000
800
600
400
200
0
At Wellhead (IN)
iFe(soluble) •Fe(particulate)
idUlliiiilii
II
I
Pre-oxidation (AP)
I Fe(soluble) • Fe(particulate)
*^^^
^>>:44t^^^^^^^^
After Adsorption(TC)
I Fe(soluble) • Fe(particulate)
Figure 4-22. Concentrations of Iron Species at IN, AP, and TC Sampling
Locations
42
-------
300
12/01/08 03/31/09 07/29/09 11/26/09 03/26/10 07/24/10 11/21/10
Sampling Date
Figure 4-23. Total Manganese Concentrations at IN, AP, and TC Sampling Locations
concentration over the 50-(ig/L MCL. The data indicated that Birm®/Filox™ was effective in removing
manganese from raw water, preventing the downstream AM from being coated with MnO2.
Other Water Quality Parameters. Raw water pH values measured at the IN location varied from 7.4 to
8.0. pH values remained essentially unchanged after the dual oxidizing media treatment. Alkalinity also
did not vary, with values ranging from 129 to 161 mg/L (as CaCO3) across the treatment train. Treatment
plant samples were analyzed for fluoride, sulfate, nitrate, phosphorus, and hardness only when arsenic
speciation was performed. Fluoride and nitrate concentrations were low, averaging 0.1 and 0.2 mg/L (as
N), respectively, across the treatment train. Sulfate levels also were low, ranging from 3.2 to 7.1 mg/L
throughout the treatment train. Concentrations of total hardness, existing primarily as calcium hardness
(about 82%), ranged from 97 to 129 mg/L (as CaCO3), and remained essentially unchanged throughout
the treatment train. Silica (as SiO2) concentrations ranged from 13.3 to 18.0 mg/L, and appeared
unaffected by the treatment process.
Total phosphorus levels in raw water fluctuated between 57 and 170 (ig/L and averaged 112 (ig/L. The
pre-oxidation step removed 19 to 67% (40% on average) of total phosphorus, leaving 19 to 100 (ig/L in
the influent to the Adsorbsia™ GTO™ vessel. Adsorbsia™ GTO™ further removed total phosphorus to <10
to 78 (ig/L. Figure 4-24 presents total phosphorus breakthrough curves. Figure 4-25 plotted percentages
of total phosphorus removal by Birm®/Filox™ and Adsorbsia™ GTO™, respectively. For the first 22,000
BV, Adsorbsia™ GTO™ removed up to 90% of total phosphorus in the vessel influent. However, the
removal followed a decreasing trend and was reduced to <20% after approximately 36,000 BV.
Total titanium was monitored throughout the treatment train to evaluate if any Adsorbsia™ GTO™ media
had gotten into the treated water in either a soluble or a particulate form. Very little titanium was
43
-------
i
.S
180
160
140
120
I 100
1
§ 80
U
a.
•3 60
40
20
0
o
H
100%
90%
80%
-3 70%
t
g 60%
^ 50%
a.
| 40%
H
30%
20%
10%
0%
IN
•AP
TC
10,000 20,000 30,000 40,000
Run Length (BV)
50,000
60,000 70,000
Figure 4-24. Total Phosphorus Breakthrough Curves
AP
TC
10,000 20,000 30,000 40,000
Run Length (BV)
50,000 60,000
70,000
Figure 4-25. Total Phosphorus Percent Removal
44
-------
measured in raw water with concentrations averaging only 1.8 (ig/L. Total titanium concentrations
following the adsorption vessel were low, ranging from 0.9 to 444 (ig/L and averaging 16.3 (ig/L. There
were two instances where total titanium concentrations in the adsorption vessel effluent were high, i.e.,
268 (ig/L on March 10, 2009, and 444 (ig/L on November 18, 2009. For the November 18, 2009, sample,
the turbidity reading also was uncharacteristically high (9.9 NTU), indicating leakage of media fines into
the vessel effluent. Soluble titanium concentrations remained at the background level of 1.4 (ig/L
throughout the treatment train.
4.5.2 Backwash Residual Sampling. Backwash wastewater samples were collected 12 times from
each of the Birm®/Filox™ vessels. Table 4-11 presents analytical results of the Birm®/Filox™ backwash
wastewater sampling. The Adsorbsia™ GTO™ vessel was backwashed only once for a test purpose;
therefore, no samples were collected during its backwashing.
Table 4-11. Birm®/Filox™ Vessel Backwash Wastewater Sampling Results
Date
U
a.
S.U.
O
-^-1
1
Hg/L
Mn (soluble)
Hg/L
"3
-*^
£
H
Hg/L
Ti (soluble)
Hg/L
Vessel A
05/06/09
06/02/09
06/29/09
08/12/09
11/19/09
12/16/09
01/12/10
02/10/10
03/10/10
04/06/10
05/03/10
06/07/10
| Average \
05/06/09
06/02/09
06/29/09
08/12/09
11/19/09
12/16/09
01/12/10
02/10/10
03/10/10
04/06/10
05/03/10
06/07/10
| Average \
7.5
7.8
7.7
7.6
7.7
7.8
7.7
7.8
7.9
7.7
7.9
7.7
7.7
160
178
162
162
166
178
164
148
158
174
162
164
765
30.0
13.0
20.0
13.0
22.0
32.0
24.0
16.0
24.0
54.0
32.0
38.0
26.5
14.3
15.8
25.2
28.7
26.6
24.5
36.1
26.1
29.3
35.9
92.8
48.7
33.7
8.8
10.6
11.8
12.4
9.1
9.2
9.3
10.9
9.0
9.3
17.7
12.5
10.9
5.5
5.3
13.4
16.3
17.4
15.3
26.8
15.2
20.4
26.5
75.2
36.2
22.8
939
632
3,306
2,437
1,824
2,350
3,056
2,975
2,828
4,712
3,366
4,983
2,784
<25
96
372
37
<25
<25
<25
253
<25
<25
960
<25
344
1,022
516
614
720
519
229
513
458
189
650
526
180
511
1.7
138
122
33.6
11.6
10.7
22.3
64.7
17.3
24.2
153
22.2
51.8
653
3.4
12.4
6.5
5.2
410
6.5
3.8
3.8
6.7
7.4
8.5
93.9
1.9
1.4
2.3
1.7
1.7
1.8
NA
2.0
1.8
1.7
2.6
1.6
1.9
VesselB
7.6
7.8
7.7
7.5
7.6
7.7
7.7
7.7
7.7
7.6
7.6
7.6
7.6
170
180
154
170
158
176
162
148
146
168
142
180
163
86.0
26.0
20.0
16.0
24.0
33.0
14.0
18.0
48.0
42.0
37.0
32.0
33.0
26.9
29.3
24.7
27.1
34.8
25.7
34.0
31.7
40.3
30.8
102
48.7
38.0
9.9
9.7
9.5
19.2
8.8
9.4
13.9
9.4
9.5
9.4
17.8
10.8
11.4
17.0
19.6
15.2
7.9
26.0
16.3
20.1
22.3
30.8
21.5
84.5
37.9
26.6
3,258
2,415
3,135
2,253
2,628
2,599
2,760
3,745
4,964
3,423
4,747
5,421
3,446
<25
<25
60
990
<25
<25
710
<25
<25
<25
1,086
<25
711
1,422
672
657
744
490
241
364
422
240
492
626
658
586
16.0
4.6
11.7
695
12.6
11.5
194
26.3
48.1
18.4
193
21.8
104
379
19.0
19.9
6.6
5.6
349
4.8
4.8
4.9
5.8
8.9
8.7
68.1
1.9
1.1
1.6
3.8
1.7
2.4
NA
1.2
1.6
1.5
3.3
1.9
2.0
NA = not analyzed; TDS = total dissolved solids; TSS = total suspended solids
45
-------
As shown in Table 4-11, results for the two vessels were comparable. pH values of backwash wastewater
ranged from 7.5 to 7.9 and averaged 7.7, which was similar to that of the pre-oxidized water used for
backwashing. TDS concentrations ranged from 142 to 180 mg/L and averaged 164 mg/L. TSS
concentrations ranged from 13.0 to 86.0 mg/L and averaged 29.8 mg/L. TSS concentrations were low
because the pre-oxidizing media was backwashed daily.
The backwash wastewater samples contained 14.3 to 102 (ig/L of total arsenic, 632 to 5,421 (ig/L of total
iron, 180 to 1,422 (ig/L of total manganese, and 3.4 to 653 (ig/L of total titanium. As expected, the
majority of these metals were present in the particulate form. Assuming that 752 gal of wastewater was
produced when backwashing the two pre-oxidation vessels and that the wastewater contained 29.8 mg/L
of TSS, it would discharge 85 g (0.2 Ib) of solids. The waste stream would consist of 102 mg of arsenic,
8.9 g of iron, and 1.6 g of manganese based on 35.8 (ig/L of total arsenic, 3,115 (ig/L of total iron, and
548 (ig/L of total manganese in the backwash wastewater. According to Table 4-9, concentration
differences between the IN and AP locations were 2.8 (ig/L of total arsenic, 276 (ig/L of total iron, and
112 (ig/L of total manganese (on average). Therefore, based on a daily water demand of 8,354 gal, the
pre-oxidation vessels would remove 88.2 mg of total arsenic, 8.7 g of iron, and 3.5 g of manganese from
raw water. The daily backwash recovered 116% of total arsenic, 102% of total iron, and 46% of total
manganese from the pre-oxidation vessels. The low Mn recovery rate might be attributed to the fact that
some manganese (existing as MnO2) had attached to the oxidation media surface and was difficult to be
washed off.
One set of backwash solid samples was collected on June 29, 2009 and analyzed in duplicate for ICP/MS
metals. Table 4-12 presents the results of total metals analysis.
Table 4-12. Birm®/Filox™ Vessels Backwash Solid Sample Total Metal Results
Sample
BW1-A
BW1-B
Average
BW2-A
BW2-B
Average
Mg
5,469
5,545
5,507
5,140
5,436
5,288
Al
20,589
19,536
20,063
17,693
20,891
19,292
Si
15,629
17,277
16,453
12,842
17,728
15,285
P
2,584
2,512
2,548
2,103
2,071
2,087
Ca
8,573
8,191
8,382
8,247
8,531
8,389
Fe
42,466
43,475
42,971
37,512
37,821
37,667
Mn
17,006
13,940
15,473
13,412
15,674
14,543
Ni
34.0
33.1
33.6
26.6
30.0
28.3
Cu
60.0
58.6
59.3
38.8
39.6
39.2
Zn
172
169
777
132
231
182
As
130
124
727
100
99.0
100
Cd
<15
<15
<75
<15
<15
<75
Ba
529
500
575
452
456
454
Pb
17.9
16.3
77.7
12.2
13.6
12.9
Samples collected on 06/20/09; units in |ag/g.
Total arsenic, iron, and manganese concentrations in the solids averaged 113, 40,319, and 15,008 (ig/g.
Assuming that the daily backwashing discharged 85 g of solids (dry weight), the solids would contain 9.6
mg of total arsenic, 3.4 g of total iron, and 1.3 g of total manganese. The amounts of total arsenic and
iron were much lower than the values calculated based on the backwash wastewater data.
4.5.3 Distribution System Water Sampling. Prior to the installation/operation of the treatment
system, four first-draw baseline distribution system water samples were collected at three locations, i.e.,
South House, South #1, and South #2, on July 16, August 13, August 20, and September 2, 2008.
Following the installation of the treatment system, distribution water sampling continued on a monthly
basis from January 2009 to November 2009. Table 4-13 presents results of the distribution system water
sampling.
46
-------
Table 4-13. Distribution System Sampling Results
Sampling
Event
No.
BL1
BL2
BL3
BL4
1
2
o
5
4
5
6
7
8
9
10
11
Date
07/16/08
08/13/08
08/20/08
09/02/08
Average
01/14/09
02/18/09
03/19/09
04/15/09
05/13/09
06/10/09
07/08/09
08/05/09
09/02/09
10/07/09
11/04/09
Average
DS1
.0
-*^
sS
a jo
M a
st a
& N
•_
a
11.5
6.0
5.8
7.5
7.7
9.6
5.9
17.5
7.8
12.0
11.0
9.8
19.3
7.8
8.8
7.5
10.6
n
P
C/5
7.5
7.7
NA
7.6
7.6
7.8
7.4
7.6
7.8
8.0
7.6
7.6
7.7
7.6
7.7
7.7
7.7
Alkalinity
I
140
144
NA
144
143
141
144
145
138
142
145
146
139
138
143
136
142
t«
•3
1
14.2
10.2
10.9
10.7
77.5
2.2
1.3
0.4
4.8
3.3
4.9
5.7
6.0
2.9
3.4
3.3
3.5
1>
u.
-J
•a
391
48
<25
87
735
<25
<25
<25
55
76
<25
<25
<25
<25
<25
<25
<25
|
J
"SID
37.7
1.0
6.3
1.8
77.7
21.4
25.2
2.7
8.1
10.6
1.6
9.6
0.6
1.4
2.4
0.6
7.7
.a
a.
J
•a
0.2
<0.
<0.
<0.
<0.1
<0.
<0.
<0.
0.5
0.8
<0.
<0.
<0.
<0.
<0.
<0.
<0.1
u
1
5.7
2.0
5.5
1.3
3.6
6.6
8.1
47.1
5.3
269
6.5
6.2
1.7
0.7
3.6
3.0
32.5
DS2
Stagnation
Time
•_
a
4.0
8.0
9.3
10.0
7.8
9.0
9.5
8.7
8.3
12.0
7.8
10.6
11.3
11.0
10.3
9.8
9.8
n
c-s
P
C/5
7.6
7.6
NA
7.7
7.6
7.8
7.5
7.5
7.9
7.8
7.7
7.7
7.6
7.6
7.7
7.6
7.7
Alkalinity
I
142
137
NA
144
141
146
144
145
138
145
145
146
139
140
143
134
142
t«
•3
J
"SID
12.5
10.7
11.2
11.7
77.5
1.3
0.5
0.3
2.5
1.8
1.4
5.4
5.4
1.5
1.7
1.7
2.1
1>
u.
1
<25
41
<25
86
38
<25
<25
<25
132
<25
<25
<25
<25
<25
<25
<25
<25
|
1
45.9
57.9
24.1
17.7
36.4
3.2
0.4
0.2
29.1
0.9
0.2
20.6
12.9
6.3
4.1
16.0
8.5
.a
a.
1
<0.1
0.1
0.1
O.I
<0.1
0.4
0.1
O.I
0.1
0.3
0.1
O.I
0.1
0.3
0.1
O.I
<0.1
u
J
•a
18.2
52.8
20.5
11.2
25.7
48.7
13.5
10.7
5.3
22.1
11.2
8.4
30.0
57.7
10.6
18.4
27.5
DS3
.0
-*^
sS
a jo
M a
es B
£ N
•_
a
12.5
9.0
12.5
11.5
11.4
5.2
11.0
11.5
12.0
12.0
11.8
12.0
11.3
11.0
8.3
8.5
10.4
n
P
C/5
7.6
7.7
NA
7.8
7.7
8.0
7.4
7.7
8.0
7.9
7.6
7.7
7.5
7.5
7.9
7.7
7.7
Alkalinity
I
144
141
NA
142
142
141
144
135
134
140
145
148
137
138
143
138
140
t«
•3
1
11.1
10.2
10.0
10.6
70.5
5.1
3.9
3.7
5.1
4.1
3.8
5.1
5.2
3.0
3.6
3.0
4.1
1>
u.
J
"SID
<25
48
<25
68
36
<25
<25
<25
114
<25
<25
<25
<25
<25
<25
<25
<25
|
J
"SID
20.2
7.2
3.8
10.7
10.4
23.5
14.9
18.2
34.3
2.5
0.7
5.0
4.7
1.3
4.9
1.2
70.7
A
&
J
"SID
0.2
0.2
0.2
O.I
0.2
0.2
0.5
0.5
0.9
0.6
0.2
O.I
0.1
0.1
0.3
0.1
0.3
U
1
37.1
64.0
86.4
31.0
54.6
26.7
109
93.5
124
107
119
38.2
96.9
96.2
121
90.2
92. 8
NA = not available
-------
The most noticeable change in the distribution samples since system startup was a decrease in arsenic,
iron, and manganese concentrations. Baseline arsenic concentrations ranged from 10.0 to 14.2 (ig/L and
averaged 11.2 (ig/L. After system startup, arsenic concentrations were reduced to 0.3 to 6.0 (ig/L and
averaged 3.2 (ig/L. Baseline iron concentrations ranged from less than the MDL of 25 (ig/L to 391 (ig/L,
and averaged 70 (ig/L. After system startup, iron concentrations decreased to <25 (ig/L (on average).
Manganese had a similar trend with baseline concentrations averaging 19.5 (ig/L and after-startup
concentrations averaging 8.8 (ig/L.
Lead and copper concentrations of all water samples collected before and after the installation of the
treatment system were below the action level of 15 and 1,300 (ig/L, respectively. The arsenic treatment
system did not seem to have any effects on the lead or copper concentrations in the distribution system.
Measured pH values in distribution water ranged from 7.4 to 8.0 and averaged 7.7. Alkalinity levels
ranged from 134 to 148 mg/L (as CaCO3). The arsenic treatment system did not affect these water quality
parameters of the distributed water.
4.6 System Cost
The system cost 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. Capital cost of the treatment system included the expenditure
for equipment, site engineering, and system installation, shakedown, and startup. O&M cost included the
expenditure for chemicals, electricity, and labor. Cost associated with the building was not included in
the capital cost because it was outside the scope of this demonstration project and was funded separately
bytheHSMHP.
4.6.1 Capital Cost. The capital investment for the Birm®/Filox™ pre-oxidation and Adsorbsia™
GTO™ arsenic removal was $66,362 (Table 4-14). The equipment cost was $46,267 (or 70% of the total
capital investment), which included costs for three 24-in x 72-in composite vessels, 10 ft3 each of Birm®,
Filox™, and Adsorbsia™ GTO, 6 ft3 of garnet underbedding support, one backwash supply system, process
valves and piping, instrumentation and controls, shipping, and labor.
The site engineering cost covered the expenditure for preparing the required engineering submittal,
including a process design report, a general arrangement drawing, piping and instrumentation diagrams
(P&IDs), electrical diagrams, interconnecting piping layouts, and obtaining the required permit approval
from Utah DDW. The engineering cost of $3,850 was 6% of the total capital investment.
The installation, shakedown, and startup cost covered the labor and materials required to unload, install,
and test the system for proper operation. The installation, startup and shakedown activities were
performed by Filter Tech at a cost of $16,245 or 24% of the total capital investment.
The total capital cost of $66,362 was normalized to $2,212/gpm ($1.54/gpd) of design capacity using the
system's rated capacity of 30 gpm (or 43,200 gpd). The total capital cost also was converted to an
annualized cost of $6,264 gal/year using a capital recovery factor of 0.09439 based on a 7% interest rate
and a 20-yr return period. Assuming that the system operated 24 hr/day, 7 day/week at the design
flowrate of 30 gpm to produce 15,768,000 gal/yr, the unit capital cost would be $0.40/1,000 gal. During
the demonstration study, the system produced 8,354 gal of water daily (Table 4-8) or 3,049,000 gal
annually, the unit capital cost increased to $2.05/1,000 gal. These calculations did not include the
building construction cost.
48
-------
Table 4-14. Capital Investment for HSMHP System
Description
Quantity
Cost
% of Capital
Investment
Equipment
Adsorbsia™ GTO™ Media (ft3)
Bum® Media (ft3)
Filox™ Media (ft3)
Garnet (ft3)
24-in x 72-in Composite Vessels
Backwash Supply System
Process Valves and Piping
Instrumentation
Shipping
Labor
Equipment Total
10
10
10
6
o
J
1
1
1
-
-
—
$4,300
$500
$1,600
$35
$4,560
$7,600
$3,900
$6,875
$2,400
$14,497
$46,267
—
—
—
—
—
—
—
-
-
-
70%
Engineering
Labor
Engineering Total
1
—
$3,850
$3,850
-
6%
Installation, Shakedown, and Startup
Labor
Installation, Shakedown, and
Startup
Total Capital Investment
1
-
$16,245
$16,245
$66,362
-
24%
100%
4.6.2 O&M Cost. The O&M cost includes cost for media replacement and disposal, electricity,
and labor, as summarized in Table 4-15. Although neither the oxidizing nor the AM was replaced during
the performance evaluation study, the media replacement cost would represent the majority of the O&M
cost. It was estimated that the Birm®/Filox™ media would have a life expectancy of 10 years and that it
would cost $8,175 to replace 20 ft3 of media in two vessels (including the cost for media, labor, freight,
and media disposal). At the current water use rate (i.e., 3,049,000 gal for one year), the system would
treat 30,490,000 gal of water in a 10-yr period. Therefore, the Birm®/Filox™ media replacement cost
would be equivalent to $0.27/1,000 gal of water treated.
It also was estimated that it would cost $8,440 to change out 10 ft3 of Adsorbsia™ GTO™ media, including
the cost for media, labor, freight, and media disposal. This cost was used to estimate the media
replacement cost per 1,000 gal of water treated as a function of the projected media run length to the 10-
|o,g/L arsenic breakthrough (Figure 4-26).
No cost was incurred for repairs because the system was under warranty. Electrical power consumption
was calculated based on the difference between the average monthly cost from electric bills before and
after the building construction and system startup. The difference in cost was approximately $100/month
or $0.39/1,000 gal of water treated. The routine, non-demonstration related labor activities consumed
approximately 30 min a day, six days a week. Based on this time commitment and a labor rate of $30/hr,
the labor cost was $1.54/1,000 gal of water treated.
49
-------
Table 4-15. O&M Costs for HSMHP System
Category
Volume Processed (x 1,000 gal/year)
Media Re
Birm® Media
Filox™ Media
Freight
Subcontractor Labor Cost
Media Analysis and Disposal
Subtotal ($)
Birm®/ Filox™ Replacement and
Disposal Cost ($/l,000 gal)
Adsorbsia™ GTO™ Media
Freight
Subcontractor Labor Cost
Media Analysis and Disposal
Subtotal ($)
Adsorbsia™ GTO Replacement
and Disposal Cost ($/l,000 gal)
Value
3,049
Remarks
Based on average daily production
of 8,354 gal
placement and Disposal
$500
$1,600
$1,810
$2,765
$1,500
$8,175
$0.27
$4,300
$625
$2,765
$750
$8,440
See Figure
4-26
10ft3
10ft3
Estimate
Estimate
Estimate
Assuming 10-year media life
treating 30,490,000 gal of water
10ft3
Estimate
Estimate
Electricity Consumption
Electricity Cost ($/month)
Electricity Cost ($/l,000 gal)
$100
$0.39
Average incremental consumption
after system startup, including
building heating and lighting
-
Labor
Labor (hr/week)
Labor Cost ($71,000 gal)
Total O&M Cost ($/l,000 gal)
3.0
$1.54
See Figure
4-26
30 min/day, 6 day/week
Labor rate = $30/hr
Total O&M cost = $2.20 +
Adsorbsia™ GTO™ media
replacement cost
50
-------
$10.00
O&M cost
•Media replacement cost
$0.00
0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150
Adsorbsia Media Working Capacity, Bed Volumes (xlOOO)
Note: One bed volume equals 10ft3 (74.8 gal)
Figure 4-26. O&M Costs for HSMHP System
51
-------
5.0 REFERENCES
Battelle. 2008. System Performance Evaluation Study Plan: U.S. EPA Demonstration of Arsenic
Removal Technology Round 2a at Hot Springs Mobile Home Park in Willard, UT. Prepared
under Contract No. EP-C-05-057, Task Order No. 0019, for U.S. Environmental Protection
Agency, National Risk Management Research Laboratory, Cincinnati, OH.
Battelle. 2007. Quality Assurance Project Plan for Evaluation of Arsenic Removal Technology (QAPP
ID 355-Q-6-0). Prepared under Contract No. EP-C-05-057. Task Order No. 0019, for U.S.
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
Chen, A.S.C., L. Wang, J.L. Oxenham, and W.E. 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.
Edwards, M., S. Patel, L. McNeill, H.-W. Chen, M. Frey, A.D. Eaton, R.C. Antweiler, and H.E. Taylor.
1998. "Considerations in Arsenic Analysis and Speciation." JournalAWWA, 90(3): 103-113.
EPA. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic.
Federal Register, 40 CFR Part 141.
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, D.C.
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.
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, and K. Fields. 2000. Arsenic Removal from Drinking Water by Ion Exchange
and Activated Alumina Plants. EPA/600/R-00/088. U.S. Environmental Protection Agency,
National Risk Management Research Laboratory, Cincinnati, Ohio..
52
-------
APPENDIX A
OPERATIONAL DATA
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT
WK
No.
1
2
3
4
5
6
7
8
9
10
11
12
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Sat
Mon
Tue
Wed
Sat
Wed
Thu
Mon
Tue
Wed
Fri
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Sat
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Date
12/11/08
12/12/08
12/13/08
12/15/08
12/16/08
12/17/08
12/18/08
12/19/08
12/20/08
12/23/08
12/24/08
12/27/08
12/29/08
12/30/08
12/31/08
01/03/09
01/07/09
01/08/09
01/12/09
01/13/09
01/14/09
01/16/09
01/19/09
01/20/09
01/21/09
01/22/09
01/23/09
01/25/09
01/26/09
01/27/09
01/28/09
01/29/09
01/30/09
01/31/09
02/02/09
02/03/09
02/04/09
02/05/09
02/07/09
02/09/09
02/10/09
02/11/09
02/12/09
02/13/09
02/16/09
02/17/09
02/18/09
02/19/09
02/20/09
02/23/09
02/24/09
02/25/09
02/26/09
Hour Meter (hr)
Record
hr
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
1,467
1,492
1,582
1,612
1,629
1,677
1,751
1,771
1,795
1,819
1,846
1,892
1,914
1,937
1,956
1,983
2,007
2,024
2,080
2,103
2,124
2,148
2,192
2,235
2,264
2,281
2,310
2,331
2,402
2,428
2,451
2,472
2,495
2,571
2,590
2,614
2,637
Diff
hr
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
(b)
25
90
30
17
48
74
20
24
24
27
46
22
23
19
27
24
17
56
23
21
24
44
43
29
17
29
21
71
26
23
21
23
76
19
24
23
Pressure
IN
TA
TB
AP
TC
psi
55
59
60
65
65
62
65
60
70
65
65
75
65
65
65
NA
60
60
NA
60
60
60
60
60
60
60
61
60
62
58
61
58
58
58
60
58
61
60
60
59
60
57
58
60
63
59
58
60
58
60
62
63
60
58
57
57
55
59
57
57
55
60
56
60
65
60
60
59
59
59
59
60
60
56
59
58
56
56
57
58
56
57
57
58
56
56
56
56
56
58
57
59
56
56
56
60
57
59
57
56
57
56
59
59
59
56
55
55
57
55
57
57
59
55
60
56
57
65
58
57
57
57
59
58
59
57
56
56
56
55
55
56
58
55
56
57
57
55
55
55
56
56
56
56
58
56
56
56
60
57
58
57
56
57
56
59
59
58
56
NA
NA
NA
NA
NA
57
57
55
60
NA
57
57
57
56
56
56
59
59
59
59
58
59
58
56
56
57
59
58
57
59
58
58
58
58
57
56
58
57
59
57
57
57
60
58
59
58
57
58
56
60
60
59
57
57
59
60
55
56
57
58
55
59
55
55
57
56
56
55
56
54
54
54
53
52
53
54
52
52
53
54
54
53
54
54
53
53
56
56
53
53
53
53
53
53
53
54
53
53
53
53
58
53
54
54
53
54
Flowrate
IN
TA
TB
TC
gpm
4.8
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
14.0
8.1
10.8
4.4
5.8
27.1
0.0
0.0
(d)
10.8
12.6
7.2
6.7
9.0
10.8
3.1
6.7
6.9
8.4
8.8
12.8
6.9
9.9
1.4
11.6
1.8
31.1
6.4
14.4
8.3
4.5
3.4
9.2
11.5
14.4
13.8
18.0
NA
4.0
3.5
4.7
4.4
4.2
6.6
2.1
7.6
2.0
5.0
5.4
4.6
7.3
3.9
4.5
7.0
3.2
3.6
2.8
1.3
-1.1
-2.0
2.6
-1.3
1.9
3.7
3.6
3.8
8.9
3.1
3.5
0.4
2.9
3.1
2.4
3.3
2.8
3.1
2.5
2.4
-0.2
-1.8
2.6
4.1
0.7
2.3
3.4
-0.4
4.2
4.1
3.4
-5.1
NA
3.2
3.4
3.6
2.9
3.4
7.3
2.4
3.8
1.5
5.7
5.2
0.8
2.6
1.1
4.7
4.3
4.4
6.8
4.2
2.0
10.7
9.8
3.0
4.7
3.1
6.4
5.4
1.0
3.0
3.6
0.9
1.6
3.1
4.2
2.7
5.8
2.5
4.1
2.6
2.4
3.1
13.7
3.0
4.8
2.7
1.6
4.1
3.0
3.3
5.5
4.2
8.2
NA
7.2
6.9
8.3
7.3
7.6
13.9
4.5
11.4
3.5
10.7
10.6
5.4
9.9
5.0
9.2
11.3
7.6
10.4
7.0
3.3
9.6
7.8
5.6
3.4
5.0
10.1
9.0
4.8
11.9
6.7
4.4
2.0
6.0
7.3
5.1
9.1
5.3
7.2
5.1
4.8
2.9
11.9
5.6
8.9
3.4
3.9
7.5
2.6
7.5
9.6
7.6
3.1
Totalizer
IN
TA
g
238,989
238,989
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
253,142
265,945
312,648
327,048
335,912
358,116
362,364
362,364
(d)
362,403
375,683
398,155
410,702
423,328
432,162
445,683
456,843
463,684
489,359
499,959
509,572
522,686
545,835
565,499
579,087
585,689
599,723
609,242
638,738
651,918
662,115
670,692
680,106
714,925
723,048
732,213
740,375
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
TB
TC
al
4,142
8,430
11,172
19,284
23,895
27,380
31,679
37,150
40,763
52,158
55,308
68,370
79,578
81,267
83,751
96,554
118,075
124,168
145,973
152,937
157,443
168,713
183,006
186,938
NA(c)
197,314
202,992
212,992
218,350
221,890
224,801
230,005
234,714
237,471
247,608
252,250
256,345
262,037
272,255
280,133
285,855
288,649
294,875
298,988
308,648
314,470
318,818
322,634
326,065
340,933
344,462
348,304
351,610
7,924
16,925
22,715
38,547
47,975
55,094
63,583
73,731
83,568
109,740
116,171
146,430
168,646
178,705
187,370
225,967
277,336
287,804
326,870
339,198
346,792
365,864
394,674
402,209
410,667
421,446
431,629
451,057
461,327
472,235
479,682
490,221
499,577
504,841
526,337
534,898
542,498
552,914
571,440
587,353
598,582
604,539
615,699
623,764
648,991
659,791
667,976
675,207
683,206
712,148
718,562
726,378
733,418
Total
BVs|c|
BVs
103
220
295
500
622
715
825
956
1,084
1,423
1,507
1,899
2,187
2,318
2,430
2,931
3,597
3,733
4,240
4,399
4,498
4,745
5,119
5,217
5,326
5,466
5,598
5,850
5,983
6,125
6,222
6,358
6,480
6,548
6,827
6,938
7,036
7,171
7,412
7,618
7,764
7,841
7,986
8,090
8,418
8,558
8,664
8,758
8,861
9,237
9,320
9,421
9,513
BW
Totalizer
gal
12,566
NA(d)
NA(d)
NA(d)
13,083
13,083
13,083
13,083
13,083
13,083
13,083
13,083
13,083
13,083
13,083
13,083
13,955
13,955
14,721
14,721
14,721
15,100
15,482
15,482
15,482
15,482
17,010
17,010
17,544
17,544
17,544
18,197
18,968
19,743
21,049
21,708
22,482
23,206
24,696
26,254
27,030
27,030
28,574
28,574
30,027
30,802
31,577
32,351
32,894
34,569
35,348
36,125
36,516
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
13
14
15
16
17
18
19
20
21
22
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Fri
Sat
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Date
03/02/09
03/03/09
03/04/09
03/05/09
03/06/09
03/07/09
03/09/09
03/10/09
03/11/09
03/12/09
03/13/09
03/14/09
03/16/09
03/17/09
03/18/09
03/19/09
03/20/09
03/21/09
03/23/09
03/24/09
03/25/09
03/26/09
03/27/09
03/28/09
03/30/09
03/31/09
04/01/09
04/03/09
04/04/09
04/07/09
04/08/09
04/09/09
04/10/09
04/11/09
04/13/09
04/14/09
04/15/09
04/16/09
04/17/09
04/18/09
04/20/09
04/21/09
04/22/09
04/23/09
04/24/09
04/25/09
04/27/09
04/28/09
04/29/09
04/30/09
05/01/09
05/02/09
05/04/09
05/05/09
05/06/09
05/07/09
05/08/09
05/09/09
Hour Meter (hr)
Record
hr
2,735
2,749
2,781
2,803
2,821
2,843
2,893
2,914
2,940
2,962
2,983
3,007
3,055
3,077
3,102
3,125
3,147
3,171
3,219
3,243
3,265
3,290
3,313
3,336
3,384
3,407
3,431
3,477
3,500
3,572
3,593
3,619
3,641
3,665
3,710
3,734
3,757
3,790
3,804
3,827
3,875
3,898
3,920
3,947
3,968
3,993
4,038
4,060
4,084
4,108
4,131
4,156
4,204
4,234
4,246
4,269
4,294
4,317
Diff
hr
98
14
32
22
18
22
50
21
26
22
21
24
48
22
25
23
22
24
48
24
22
25
23
23
48
23
24
46
23
72
21
26
22
24
45
24
23
33
14
23
48
23
22
27
21
25
45
22
24
24
23
25
48
30
12
23
25
23
Pressure
IN
TA
TB
AP
TC
psi
61
60
60
62
60
60
66
64
64
60
60
62
62
60
62
60
64
60
64
62
60
60
62
60
62
60
60
56
60
80
92
60
58
58
56
56
60
60
60
60
60
56
58
56
58
58
58
58
58
58
56
56
56
56
56
60
60
56
58
56
57
58
58
56
60
58
60
60
58
60
60
58
60
56
60
56
58
56
56
58
58
56
56
56
56
56
58
70
94
58
58
58
56
56
56
58
56
58
56
56
56
58
56
58
56
56
58
56
56
56
56
56
56
58
56
56
57
56
58
58
56
50
60
58
60
60
58
60
58
58
60
56
58
56
58
56
56
56
58
56
56
54
54
56
58
70
98
58
58
56
56
56
56
58
56
58
56
56
56
56
56
56
56
56
58
56
56
56
56
56
54
58
56
54
58
58
59
60
58
40
60
60
60
60
58
60
60
60
58
56
60
56
60
58
58
56
58
58
58
56
56
56
60
70
98
60
58
58
56
58
56
60
58
60
58
58
58
58
58
58
58
58
58
58
58
56
56
56
56
58
58
56
55
56
56
55
52
52
54
52
52
52
52
54
54
54
52
52
52
52
52
52
52
52
52
52
52
52
52
54
54
52
54
54
54
54
52
54
52
56
56
54
56
52
54
54
54
54
54
54
54
54
52
56
55
54
54
52
54
52
Flowrate
IN
TA
TB
TC
gpm
12.0
9.3
9.5
12.3
8.0
10.5
10.9
6.0
11.8
4.6
10.1
14.3
12.4
8.2
13.1
3.5
15.5
0.0
16.0
4.4
5.2
8.4
8.0
4.1
10.8
4.1
2.8
4.8
4.1
8.1
10.0
9.7
2.3
2.9
3.4
4.6
1.9
4.8
0.0
NA(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
3.5
5.6
3.4
2.5
3.7
1.7
7.8
0.4
3.6
3.3
3.1
6.4
3.9
1.4
3.0
1.9
2.2
1.2
3.1
3.5
3.5
3.2
0.8
6.1
0.8
4.7
3.5
7.6
-0.4
5.5
2.0
6.0
0.8
2.0
1.9
3.5
1.4
5.1
3.7
3.6
4.8
3.5
3.3
2.7
1.2
2.0
-0.2
8.4
3.9
4.0
3.6
2.6
4.3
3.9
5.4
2.0
5.0
5.0
5.8
5.6
5.8
3.1
6.0
4.9
4.7
4.2
2.4
3.5
3.9
1.7
1.7
1.7
5.8
3.1
2.6
1.5
3.7
3.2
5.5
7.6
0.6
1.8
3.9
3.0
3.4
4.4
6.7
2.0
3.6
1.2
4.2
2.6
4.1
3.4
3.8
1.9
1.9
4.9
4.0
2.5
6.1
9.9
7.3
7.9
5.7
6.7
12.8
6.2
9.2
9.1
6.2
12.4
8.8
6.1
7.2
4.3
5.7
1.2
7.0
5.2
5.2
4.9
6.6
9.2
3.4
4.7
5.0
11.3
2.8
5.5
7.5
13.6
1.4
3.8
1.9
7.4
1.4
8.1
7.1
8.0
11.5
5.5
6.9
2.7
2.4
2.0
4.0
11.0
8.0
6.2
4.1
8.8
9.6
4.5
Totalizer
IN
TA
TB
TC
gal
784,112
789,256
802,374
811,459
818,509
825,876
847,139
854,460
863,344
872,265
881,322
891,451
917,138
927,076
936,716
945,813
954,761
964,647
984,484
995,771
1,004,384
1,015,995
1,024,715
1,034,259
1,052,554
1,062,249
1,072,099
1,078,723
1,085,487
1,098,548
1,104,066
1,116,714
1,125,172
1,133,069
1,147,963
1,153,312
1,157,902
1,157,902
1,157,902
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
NA(c)
17337
18745
20486
24093
26837
28582
31191
32319
33577
37635
39792
41857
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
NA(d)
61,800
64,213
64,605
64,918
65,231
65,231
66,550
69,381
72,140
370,011
372,163
377,898
382,003
385,148
388,424
397,822
400,998
404,826
408,919
412,912
417,419
428,815
433,388
437,762
441,835
445,743
449,981
458,922
464,094
467,951
473,102
476,971
480,921
488,523
492,823
497,228
500,375
503,426
504,856
506,052
512,102
515,390
518,931
525,085
529,456
533,271
539,230
541,076
544,611
552,091
556,136
559,969
564,607
568,323
572,558
583,002
587,296
591,889
595,872
600,470
600,984
601,350
601,725
601,725
604,064
608,311
612,911
769,162
773,307
784,152
791,584
797,078
803,352
820,976
827,803
835,404
842,664
850,206
858,416
878,879
887,054
894,880
902,245
909,400
917,267
933,756
942,769
949,870
958,999
966,787
974,112
990,423
998,516
1,006,633
1,011,586
1,017,244
1,028,231
1,033,210
1,043,175
1,049,954
1,057,259
1,071,107
1,079,430
1,086,555
1,098,374
1,102,347
1,109,191
1,122,055
1,130,118
1,138,100
1,147,483
1,155,045
1,163,713
1,183,843
1,192,689
1,201,841
1,210,121
1,219,059
1,219,711
1,219,914
1,219,914
1,219,914
1,224,404
1,233,634
1,243,138
Total
BVs|c|
BVs
9,976
10,030
10,171
10,267
10,338
10,420
10,648
10,737
10,835
10,929
11,027
11,134
11,399
11,505
11,607
11,702
11,795
11,897
12,111
12,228
12,320
12,438
12,539
12,634
12,846
12,951
13,056
13,120
13,194
13,336
13,401
13,530
13,618
13,713
13,892
14,000
14,093
14,246
14,298
14,386
14,553
14,658
14,761
14,883
14,981
15,094
15,355
15,469
15,588
15,695
15,811
15,820
15,822
15,822
15,822
15,881
16,000
16,124
BW
Totalizer
gal
39,234
40,012
40,791
41,570
42,348
43,126
44,492
44,492
44,878
45,646
46,425
47,204
48,760
49,539
50,317
51,095
51,874
52,652
53,434
54,210
54,988
55,766
55,766
56,609
56,609
57,127
57,872
59,044
59,426
59,852
59,852
60,625
61,016
61,016
61,019
61,433
62,060
62,060
62,510
65,934
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,082
65,115
66,746
68,391
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
23
24
25
26
27
28
29
30
31
32
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
05/11/09
05/12/09
05/13/09
05/14/09
05/15/09
05/16/09
05/18/09
05/19/09
05/20/09
05/21/09
05/22/09
05/23/09
05/25/09
05/26/09
05/27/09
05/28/09
05/29/09
05/30/09
06/01/09
06/02/09
06/03/09
06/04/09
06/09/09
06/10/09
06/11/09
06/12/09
06/13/09
06/15/09
06/16/09
06/17/09
06/18/09
06/19/09
06/20/09
06/22/09
06/23/09
06/24/09
06/25/09
06/26/09
06/27/09
06/30/09
07/01/09
07/02/09
07/03/09
07/04/09
07/06/09
07/07/09
07/08/09
07/09/09
07/10/09
07/13/09
07/14/09
07/15/09
07/16/09
07/17/09
07/18/09
07/19/09
Hour Meter (hr)
Record
hr
4,365
4,389
4,409
4,435
4,457
4,482
4,535
4,554
4,577
4,600
4,623
4,646
4,693
4,716
4,742
4,767
4,788
4,814
4,858
4,886
4,906
4,928
5,047
5,070
5,093
5,116
5,139
5,187
5,211
5,234
5,259
5,283
5,306
5,354
5,376
5,399
5,423
5,450
5,471
5,539
5,565
5,591
5,613
5,633
5,689
5,704
5,731
5,752
5,776
5,846
5,868
5,896
5,917
5,940
5,962
5,990
Diff
hr
48
24
20
26
22
25
53
19
23
23
23
23
47
23
26
25
21
26
44
28
20
22
119
23
23
23
23
48
24
23
25
24
23
48
22
23
24
27
21
68
26
26
22
20
56
15
27
21
24
70
22
28
21
23
22
28
Pressure
IN
TA
TB
AP
TC
psi
60
58
56
60
60
60
60
59
58
58
60
58
60
60
60
62
60
60
58
60
60
60
62
60
60
60
60
58
58
59
58
59
59
59
60
58
58
59
60
60
60
58
59
59
60
59
60
58
56
56
58
57
59
58
60
60
56
56
58
58
58
58
58
58
56
58
58
56
56
58
59
60
60
58
56
56
58
60
59
56
58
59
58
58
56
57
58
56
58
58
58
57
57
58
58
60
57
58
58
58
59
60
58
56
56
56
58
56
59
56
60
60
56
56
56
58
58
58
57
58
56
58
58
56
56
58
59
59
59
58
56
56
58
60
59
56
58
59
58
58
56
57
58
56
58
58
58
56
57
58
58
60
56
58
58
59
59
60
58
56
56
56
58
56
59
56
60
60
56
58
58
58
58
60
59
59
58
60
58
58
58
58
60
60
60
59
58
59
59
60
60
59
59
60
60
59
59
59
59
58
60
59
59
58
59
60
59
59
59
59
59
60
60
60
59
58
58
58
59
58
60
58
60
60
52
54
52
54
56
56
56
54
55
56
56
54
54
54
54
55
55
55
55
55
55
55
54
56
54
54
55
55
55
54
55
55
55
55
55
55
55
55
55
55
56
56
55
55
55
56
56
56
56
55
55
55
55
55
55
55
Flowrate
IN
TA
TB
TC
gpm
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
(a)
0.0
7.0
0.0
3.7
5.4
3.7
12.8
4.0
4.9
6.7
4.5
4.4
6.5
5.5
8.8
12.8
4.4
7.0
5.7
8.4
4.9
13.0
3.4
2.0
2.5
5.2
4.4
15.0
12.4
8.1
5.5
4.8
4.4
6.7
3.2
4.1
3.8
12.8
3.7
10.8
3.5
5.8
6.2
4.8
4.1
2.4
3.0
1.8
5.8
8.6
5.6
3.0
3.0
NA(d)
2.0
3.3
5.7
9.9
1.9
4.3
3.4
5.5
4.9
9.6
2.0
2.3
2.1
1.7
2.1
11.1
8.2
3.6
2.4
2.4
2.1
4.7
5.0
8.3
3.5
4.3
1.0
4.2
2.3
3.9
7.8
11.6
4.1
9.8
3.8
5.0
3.6
5.5
5.8
2.7
3.1
4.8
4.5
3.0
5.0
2.9
7.4
3.3
3.1
NA(d)
1.0
3.6
5.3
6.2
9.0
2.3
3.1
4.2
5.5
4.2
9.5
1.1
1.5
1.7
1.6
11.5
7.2
1.9
1.8
7.2
5.2
5.2
9.5
14.6
15.8
6.5
6.9
3.9
8.7
7.5
3.6
3.2
7.8
15.3
8.7
5.2
5.9
5.4
12.2
6.7
9.4
6.5
5.3
4.8
9.8
8.3
6.3
10.4
5.9
5.1
1.1
5.4
6.4
5.6
2.4
1.5
7.2
3.7
10.7
2.6
2.3
6.0
8.2
10.4
7.7
4.5
3.0
2.4
1.0
5.5
1.3
8.3
7.4
8.7
Totalizer
IN
TA
TB
TC
gal
NA(a)
NA(a)
1,161,268
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
1,161,538
1,165,258
1,166,656
1,171,437
1,178,226
1,184,201
1,189,195
1,194,099
1,204,901
1,209,644
1,214,828
1,220,939
1,227,402
1,232,434
1,248,724
1,255,563
1,261,976
1,266,747
1,270,845
1,286,390
1,289,335
1,296,466
1,301,399
1,306,989
1,323,608
1,328,491
1,335,522
1,340,779
1,345,891
1,350,847
1,359,665
77,024
81,038
83,976
NA(c)
91,631
94,112
101,879
105,411
108,938
112,666
117,445
121,072
128,306
132,269
143,311
140,171
142,871
146,487
151,306
155,244
157,207
161,638
177,910
180,358
183,383
185,828
NA
129,823
131,956
135,110
137,828
139,272
141,336
146,082
148,124
150,602
152,942
155,857
157,951
165,275
168,421
171,656
173,766
175,517
183,245
184,445
188,108
189,955
192,313
199,567
201,822
205,266
207,481
209,536
211544
216,412
621,374
626,795
630,939
637,309
641,713
645,853
657,090
662,028
667,418
672,456
678,415
683,218
694,573
700,067
704,969
710,826
714,759
720,088
727,956
733,063
736,943
743,011
767,742
771,549
776,724
780,718
783,105
787,522
789,576
792,289
794,594
796,042
797,626
801,214
802,943
804,887
806,937
809,357
810,841
815,840
818,354
821,097
822,947
824,561
831,356
832,255
835,539
837,221
839,578
845,911
847,831
850,835
851,544
853,215
855,406
859,522
1,261,264
1,270,399
1,280,981
1,293,501
1,302,555
1,311,662
1,334,494
1,344,785
1,355,330
1,366,010
1,378,043
1,388,417
1,410,796
1,422,128
1,433,124
1,445,012
1,453,850
1,465,447
1,483,268
1,494,543
1,503,067
1,514,847
1,565,286
1,573,514
1,583,769
1,592,245
1,597,186
1,607,923
1,612,710
1,619,184
1,624,333
1,628,475
1,632,578
1,641,879
1,646,574
1,651,270
1,656,613
1,661,882
1,666,666
1,680,680
1,686,390
1,691,840
1,696,041
1,699,775
1,713,930
1,716,500
1,722,777
1,727,035
1,732,017
1,746,337
1,750,767
1,756,439
1,761,151
1,765,451
1,769,999
1,777,955
Total
BVs|c|
BVs
16,359
16,477
16,615
16,777
16,894
17,012
17,309
17,442
17,579
17,717
17,873
18,008
18,298
18,445
18,588
18,742
18,857
19,007
19,238
19,384
19,495
19,648
20,302
20,409
20,542
20,652
20,716
20,855
20,917
21,001
21,068
21,122
21,175
21,295
21,356
21,417
21,487
21,555
21,617
21,799
21,873
21,943
21,998
22,046
22,230
22,263
22,345
22,400
22,465
22,650
22,708
22,781
22,842
22,898
22,957
23,060
BW
Totalizer
gal
71,684
73,333
74,981
76,632
78,277
79,925
84,879
84,879
86,537
88,196
89,855
91,511
94,824
96,475
98,125
100,614
101,432
103,919
106,383
109,342
109,342
110,970
119,567
120,891
122,546
124,199
NA
188,497
189,270
190,043
191,281
191,981
193,140
194,692
194,692
195,462
196,236
197,789
198,087
200,199
201,324
202,418
203,038
205,351
205,351
205,351
206,818
206,818
207,551
209,753
210,124
211,595
212,330
212,701
213,062
214,530
>
LtJ
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
33
34
35
36
37
38
39
40
41
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Date
07/20/09
07/21/09
07/22/09
07/23/09
07/24/09
07/25/09
07/26/09
07/27/09
07/28/09
07/29/09
07/30/09
07/31/09
08/01/09
08/02/09
08/03/09
08/04/09
08/05/09
08/06/09
08/07/09
08/08/09
08/09/09
08/10/09
08/11/09
08/12/09
08/13/09
08/14/09
08/15/09
08/16/09
08/17/09
08/18/09
08/19/09
08/20/09
08/21/09
08/22/09
08/24/09
08/25/09
08/26/09
08/27/09
08/28/09
08/29/09
08/31/09
09/01/09
09/02/09
09/03/09
09/04/09
09/05/09
09/07/09
09/08/09
09/09/09
09/10/09
09/11/09
09/12/09
09/14/09
09/15/09
09/16/09
09/17/09
09/18/09
09/19/09
Hour Meter (hr)
Record
hr
6,009
6,032
6,057
6,081
6,104
6,127
6,153
6,175
6,197
6,221
6,244
6,267
6,291
6,317
6,338
6,363
6,386
6,409
6,430
6,452
6,479
6,499
6,523
6,546
6,570
6,594
6,619
6,643
6,666
6,689
6,711
6,737
6,759
6,784
6,831
6,855
6,878
6,903
6,925
6,949
6,996
7,019
7,043
7,067
7,092
7,114
7,160
7,184
7,204
7,229
7,252
7,277
7,324
7,347
7,370
7,395
7,418
7,440
Diff
hr
19
23
25
24
23
23
26
22
22
24
23
23
24
26
21
25
23
23
21
22
27
20
24
23
24
24
25
24
23
23
22
26
22
25
47
24
23
25
22
24
47
23
24
24
25
22
46
24
20
25
23
25
47
23
23
25
23
22
Pressure
IN
TA
TB
AP
TC
psi
60
58
60
60
60
62
62
60
58
62
60
60
60
60
60
58
60
60
60
58
60
60
58
58
58
60
60
60
60
60
60
60
58
58
(d)
(d)
60
58
60
62
60
60
60
60
60
60
60
58
58
58
60
58
60
60
50
60
62
60
58
58
60
60
60
60
60
57
58
58
58
60
60
58
60
56
60
60
60
58
58
60
58
57
57
60
60
60
60
58
60
58
56
56
(d)
(d)
58
58
58
58
60
58
60
58
48
60
60
60
58
60
60
58
60
58
58
58
58
58
58
58
58
60
60
60
60
57
58
58
58
60
60
58
60
56
60
60
60
58
58
60
60
57
57
60
60
60
60
58
60
58
56
56
60
57
57
60
60
60
60
58
60
58
40
60
60
60
56
60
60
58
58
58
58
58
58
58
60
60
60
60
60
60
60
57
58
60
60
60
60
60
60
56
60
60
54
58
58
60
60
57
57
60
60
60
60
58
60
58
60
61
(d)
(d)
58
58
58
58
60
60
64
58
58
60
60
60
58
60
60
58
60
58
58
58
60
58
57
57
57
54
54
57
58
58
57
57
57
57
57
57
55
56
57
54
54
52
56
52
50
54
52
54
54
58
54
52
54
52
52
52
(d)
(d)
52
52
54
52
52
52
54
52
52
52
54
54
52
54
52
52
54
52
50
52
45
52
Flowrate
IN
TA
TB
TC
gpm
1.4
0.0
2.3
4.1
7.1
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
4.8
6.2
2.1
1.6
0.0
5.6
6.4
6.5
7.6
3.3
8.6
3.5
3.5
3.5
(d)
(d)
6.8
0.9
0.0
7.2
6.3
3.6
7.6
4.5
1.9
5.3
5.1
1.8
0.0
3.3
1.2
0.0
3.3
5.2
2.8
2.7
4.5
2.1
2.0
1.5
2.7
3.5
3.7
10.0
2.8
3.7
2.9
4.0
2.2
3.0
1.9
2.7
1.5
4.3
3.2
4.0
1.3
2.8
3.2
4.3
3.9
2.1
3.7
(d)
(d)
2.0
1.8
2.5
2.6
8.8
5.0
3.7
3.9
4.1
4.4
1.0
1.2
1.5
2.2
1.2
2.9
3.7
4.2
3.0
0.9
1.5
3.2
6.7
2.0
3.3
3.0
2.6
3.2
2.7
3.0
3.4
4.6
4.1
1.7
2.8
2.5
(d)
(d)
3.5
2.8
2.3
2.9
7.5
2.8
5.0
5.4
4.0
4.4
1.6
3.3
0.6
2.3
5.9
3.1
6.1
10.9
8.1
10.1
1.8
9.0
3.5
6.0
5.2
0.7
4.8
7.8
6.2
5.5
11.0
8.2
3.9
7.0
6.9
8.4
7.8
4.1
5.8
5.8
3.3
3.3
(d)
(d)
2.3
2.1
6.5
6.4
9.9
4.1
14.0
2.3
2.8
8.1
7.0
3.5
6.2
3.8
6.5
4.2
5.0
1.6
3.3
5.5
6.4
3.8
Totalizer
IN
TA
TB
TC
gal
1,359,987
1,359,987
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,359,988
1,364,697
1,370,433
1,376,340
1,382,067
1,387,845
1,394,182
1,399,110
1,403,574
1,408,281
1,414,000
1,420,707
1,430,939
1,436,068
1,442,023
(d)
(d)
1,445,458
1,450,117
1,451,072
1,452,109
1,474,550
1,480,183
1,485,303
1,490,714
1,496,128
1,499,994
1,510,371
1,514,906
1,518,865
1,523,923
1,528,644
1,533,555
1,543,363
1,548,067
1,552,251
1,557,526
1,561,999
1,565,569
219,441
221,473
224,404
227,943
231933
235,200
240,052
242,872
245,551
248,560
251,233
253,821
257,229
259872
261,718
264,992
267,238
259,995
272,262
274,400
276819
279,661
282,561
285,192
287,912
290,653
292,499
294,254
296,294
298,927
302,851
308,574
311,311
313,308
(d)
(d)
316,095
319,578
323,269
328,021
338,763
343,120
347,100
350,956
354,817
357,443
356,731
367,874
370,698
374,352
377,651
381,838
382,785
391,260
394,394
398,037
401,326
403,713
861,352
863,882
866,783
869,836
873,436
877,125
880,795
883,291
885,893
888,347
890,840
893,122
896,190
898,470
900,132
902,940
905,004
907,157
908,498
910,659
912,770
915,071
917,705
920,032
922,633
925,267
927,227
928,730
930,660
933,289
937,003
943,205
945,496
947,491
(d)
(d)
949,958
953,416
957,096
961,590
972,029
976,168
979,526
983,084
986,560
989,108
995,847
998,858
1,001,646
1,005,113
1,008,215
1,011,228
1,017,436
1,020,530
1,023,389
1,027,123
1,030,164
1,032,305
1,782,389
1,787,916
1,793,999
1,800,635
1,808,420
1,816,454
1,823,765
1,829,522
1,835,060
1,840,810
1,846,173
1,851,456
1,858,135
1,863,366
1,867,128
1,873,525
1,878,021
1,882,320
1,887,825
1,891,713
1,896,336
1,902,032
1,907,540
1,912,533
1,917,955
1,923,682
1,927,931
1,931,346
1,935,462
1,940,651
1,947,954
1,959,826
1,964,904
1,969,582
(d)
(d)
1,975,402
1,982,889
1,990,531
1,999,872
2,021,022
2,029,599
2,037,292
2,045,330
2,053,403
2,058,904
2,074,428
2,081,181
2,086,852
2,094,285
2,101,305
2,108,505
2,123,085
2,130,385
2,136,741
2,145,002
2,152,252
2,157,519
Total
BVs|c|
BVs
23,118
23,190
23,268
23,355
23,456
23,560
23,655
23,729
23,801
23,876
23,945
24,014
24,100
24,168
24,217
24,300
24,358
24,414
24,485
24,536
24,596
24,670
24,741
24,806
24,876
24,950
25,006
25,050
25,103
25,171
25,265
25,419
25,485
25,546
NA(d)
NA(d)
25,621
25,718
25,818
25,939
26,213
26,324
26,424
26,528
26,633
26,704
26,906
26,993
27,067
27,163
27,254
27,348
27,537
27,631
27,714
27,821
27,915
27,983
BW
Totalizer
gal
214,530
215,263
215,995
216,730
217,466
218,999
219,584
219,668
220,401
221,135
221,869
222,602
223,335
224,440
224,804
225,530
226,271
227,005
227,376
228,110
229,581
229,581
230,314
231,049
231,971
232,523
233,255
233,987
234,721
235,454
236,187
236,921
237,653
238,384
(d)
(d)
238,384
239,118
239,852
240,860
242,052
242,785
243,518
244,250
245,353
245,715
247,179
247,911
248,643
249,374
250,107
250,839
252,302
253,036
253,768
254,500
255,230
255,961
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
42
43
44
45
46
47
48
49
50
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Date
09/21/09
09/22/09
09/23/09
09/24/09
09/25/09
09/26/09
09/28/09
09/29/09
09/30/09
10/01/09
10/02/09
10/03/09
10/05/09
10/06/09
10/07/09
10/08/09
10/09/09
10/10/09
10/12/09
10/13/09
10/14/09
10/15/09
10/16/09
10/17/09
10/19/09
10/20/09
10/21/09
10/22/09
10/23/09
10/24/09
10/26/09
10/27/09
10/28/09
10/29/09
10/30/09
10/31/09
11/02/09
11/03/09
11/04/09
11/05/09
11/06/09
11/07/09
11/09/09
11/10/09
11/11/09
11/12/09
11/13/09
11/14/09
11/16/09
11/17/09
11/18/09
11/19/09
11/20/09
11/21/09
Hour Meter (hr)
Record
hr
7,487
7,511
7,535
7,559
7,582
7,606
7,652
7,676
7,699
7,723
7,745
7,769
7,817
7,842
7,861
7,887
7,912
7,934
7,980
8,004
8,026
8,051
(d)
8,078
8,147
8,169
8,193
8,216
8,237
8,262
8,307
8,333
8,351
8,377
8,400
8,424
8,470
8,493
8,514
8,540
8,562
8,587
(d)
8,658
8,681
8,704
8,727
8,754
8,798
8,820
8,844
8,867
8,890
8,914
Diff
hr
47
24
24
24
23
24
46
24
23
24
22
24
48
25
19
26
25
22
46
24
22
25
69
22
24
23
21
25
45
26
18
26
23
24
46
23
21
26
22
25
23
23
23
27
44
22
24
23
23
24
Pressure
IN
TA
TB
AP
TC
psi
60
60
60
60
58
58
58
60
64
60
60
60
60
60
60
60
62
60
60
60
60
60
60
58
62
60
62
60
58
60
58
58
60
60
60
62
60
58
60
60
64
60
60
60
60
62
60
62
64
60
60
60
60
60
60
60
58
56
58
56
58
60
60
60
58
60
58
60
60
58
60
58
60
58
60
60
60
60
60
60
60
58
60
60
58
60
60
60
60
60
58
56
58
58
60
60
60
60
58
60
60
60
60
58
60
58
60
60
60
60
58
56
58
56
58
60
60
60
58
60
58
60
60
60
60
58
60
60
60
60
60
60
60
60
60
58
58
60
58
60
60
60
60
60
58
56
58
58
60
60
60
60
58
60
60
58
60
58
60
58
60
58
60
60
60
58
58
58
58
60
62
60
60
60
60
60
60
60
60
58
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
62
60
58
58
60
64
60
60
60
60
60
60
60
60
60
60
60
60
60
54
52
54
52
54
56
52
52
54
52
52
1.6
52
60
50
54
54
54
52
54
54
52
54
52
58
50
54
54
52
58
52
54
54
54
54
54
54
52
52
54
56
54
54
54
54
54
54
52
54
52
54
54
54
54
Flowrate
IN
TA
TB
TC
gpm
5.4
2.2
3.4
0.8
3.2
3.1
2.0
3.7
6.6
4.1
4.6
0.7
1.5
3.7
4.7
0.0
4.0
5.8
5.1
3.3
2.3
3.9
6.6
6.3
3.8
4.8
7.3
3.7
2.9
0.0
1.9
3.9
8.0
4.6
5.5
6.9
0.0
1.0
2.3
0.0
7.4
3.7
5.9
4.4
10.9
5.5
4.5
5.9
6.7
2.5
3.8
2.8
5.3
3.6
5.1
3.0
1.7
1.4
2.3
1.42
1.67
4.1
4.4
1.8
2.5
3.0
4.0
5.8
3.8
6.0
1.6
2.8
5.6
3.7
3.3
4.3
9.2
2.6
2.3
9.6
2.8
3.2
4.5
2.4
5.4
5.4
2.8
1.4
2.6
2.6
7.4
9.2
3.0
5.9
4.1
2.5
4.4
5.4
4.2
3.4
3.9
6.0
2.5
7.2
3.9
3.6
2.1
3.1
2.2
5.9
6.0
1.5
0.9
5.6
3.8
4.1
4.4
8.8
2.4
3.1
2.2
6.5
4.1
6.7
3.5
12.7
4.2
6.1
2.1
6.7
6.2
4.5
6.1
5.8
8.7
6.6
2.8
11.9
10.6
5.7
14.3
6.2
3.3
4.9
9.4
3.8
4.8
12.6
8.4
3.8
2.4
8.4
2.4
5.0
7.7
9.2
9.7
5.1
1.3
2.5
4.1
6.6
9.1
10.2
5.9
1.2
6.2
8.3
8.1
4.8
6.3
9.5
14.2
6.7
Totalizer
IN
TA
TB
TC
gal
1,574,687
1,579,868
1,584,197
1,588,336
1,593,647
1,597,223
1,605,783
1,610,121
1,613,813
1,618,263
1,622,056
1,627,122
1,636,148
1,640,896
1,645,322
1,649,693
1,654,777
1,658,826
1,668,071
1,672,510
1,676,206
1,680,579
1,683,951
1,687,983
1,697,054
1,701,056
1,705,500
1,709,506
1,713,671
1,717,717
1,726,030
1,732,734
1,738,257
1,746,157
1,753,132
1,759,780
1,768,067
1,773,087
1,777,097
1,781,489
1,785,839
1,790,114
1,799,415
1,804,352
1,808,710
1,812,856
1,817,130
1,822,319
1,831,719
1,836,562
1,841,679
1,845,715
1,850,118
1,854,130
410,318
413,893
417,491
420,545
424,891
427,373
430,800
434,139
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
434,429
437,605
440,743
444,079
447,377
453,761
459,230
467,315
470,303
476,092
481,627
488,271
491,448
494,347
497,332
500,449
503,701
511,136
514,827
517,935
521,306
524,675
528,472
535,047
538,809
542,738
545,795
548,995
552,220
1,038,723
1,042,069
1,045,212
1,048,009
1,051,993
1,054,394
1,060,515
1,063,513
1,066,102
1,069,040
1,071,692
1,075,152
1,081,492
1,084,793
1,087,960
1,091,113
1,094,556
1,097,555
1,103,991
1,106,915
1,109,271
1,111,934
1,114,109
1,116,829
1,122,944
1,125,776
1,128,843
1,131,367
1,134,374
1,137,264
1,142,910
1,149,532
1,159,160
1,158,507
1,164,308
1,169,808
1,176,314
1,179,588
1,182,563
1,185,646
1,188,641
1,191,723
1,199,145
1,203,061
1,206,517
1,209,596
1,213,160
1,217,117
1,223,991
1,227,093
1,231,382
1,234,774
1,238,314
1,241,329
2,172,051
2,179,535
2,187,124
2,193,683
2,202,246
2,207,880
2,221,534
2,228,222
2,234,274
2,241,442
2,247,711
2,255,837
2,270,696
2,278,637
2,285,753
2,293,098
2,301,482
2,308,202
2,323,452
2,330,707
2,336,480
2,343,501
2,348,754
235,038
2,369,435
2,375,824
2,382,650
2,388,941
2,395,582
2,402,054
2,415,037
2,426,015
2,434,871
2,447,950
2,459,509
2,470,782
2,485,974
2,493,313
2,499,812
2,507,134
2,514,145
2,521,232
2,537,113
2,545,364
2,550,347
2,559,116
2,566,105
2,574,426
2,590,710
2,599,530
2,607,937
2,614,507
2,621,729
2,628,168
Total
BVs|c|
BVs
28,172
28,269
28,367
28,452
28,564
28,637
28,814
28,900
28,979
29,072
29,153
29,259
29,451
29,554
29,647
29,742
29,851
29,938
30,136
30,230
30,305
30,396
30,464
3,048
30,732
30,815
30,903
30,985
31,071
31,155
31,323
31,466
31,581
31,750
31,900
32,046
32,244
32,339
32,423
32,518
32,609
32,701
32,907
33,014
33,078
33,192
33,283
33,391
33,602
33,716
33,825
33,911
34,004
34,088
BW
Totalizer
gal
257,424
258,154
258,887
259,619
260,351
261,082
262,548
263,279
264,010
264,742
265,475
266,206
267,668
268,603
269,130
269,862
270,593
271,326
272,790
273,519
274,250
274,981
275,712
276,444
277,903
278,632
279,364
280,095
280,827
281,557
283,019
283,745
284,479
285,210
285,943
286,673
288,133
288,862
289,591
290,321
291,049
291,775
293,230
293,958
295,053
295,413
296,138
297,371
297,905
297,911
299,007
299,371
300,103
300,829
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
51
52
53
54
55
56
57
58
59
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Date
11/23/09
11/24/09
11/25/09
11/26/09
11/27/09
11/28/09
11/30/09
12/01/09
12/02/09
12/03/09
12/04/09
12/05/09
12/07/09
12/08/09
12/09/09
12/10/09
12/11/09
12/12/09
12/14/09
12/15/09
12/16/09
12/17/09
12/18/09
12/19/09
12/21/09
12/22/09
12/23/09
12/24/09
12/25/09
12/26/09
12/28/09
12/29/09
12/30/09
12/31/09
01/01/10
01/02/10
01/04/10
01/05/10
01/06/10
01/07/10
01/08/10
01/09/10
01/11/10
01/12/10
01/13/10
01/14/10
01/15/10
01/16/10
01/18/10
01/19/10
01/20/10
01/21/10
01/22/10
01/23/10
Hour Meter (hr)
Record
hr
8,960
8,963
9,008
9,030
9,054
9,077
9,129
9,146
9,171
9,195
9,216
9,240
9,280
9,307
9,339
9,389
9,377
9,400
9,448
9,472
9,493
9,516
9,541
9,564
(d)
9,634
9,657
9,681
9,706
9,727
9,771
9,796
9,818
9,843
9,865
9,888
9,938
9,954
9,983
10,005
10,028
10,053
10,097
10,120
10,144
10,166
10,191
10,215
10,263
10,285
10,309
10,334
10,357
10,381
Diff
hr
46
3
45
22
24
23
52
17
25
24
21
24
40
27
32
50
-12
23
48
24
21
23
25
23
(d)
(d)
23
24
25
21
44
25
22
25
22
23
50
16
29
22
23
25
44
23
24
22
25
24
48
22
24
25
23
24
Pressure
IN
TA
TB
AP
TC
psi
64
58
65
70
64
58
60
60
64
60
62
60
62
64
62
62
62
66
56
56
62
62
60
60
60
60
60
58
60
62
62
62
60
62
64
64
62
60
64
64
60
60
60
58
62
66
64
70
62
64
60
58
64
60
60
58
62
68
60
58
54
58
60
56
64
60
60
61
62
60
60
60
54
54
60
60
60
58
58
58
58
58
60
60
60
60
60
58
60
60
60
60
60
58
58
60
58
58
58
62
62
66
60
60
58
58
58
60
60
56
60
64
60
58
54
60
60
59
64
60
60
60
60
60
60
60
54
54
60
60
60
58
58
58
58
58
60
60
60
60
60
58
60
60
60
60
60
58
58
60
58
58
58
62
62
66
60
60
58
58
58
60
60
60
62
66
64
60
58
58
60
60
64
60
62
60
60
62
60
60
54
54
60
64
60
58
58
60
60
58
60
60
60
60
60
58
60
62
62
60
60
60
60
60
58
60
60
62
64
66
60
60
60
60
58
62
54
52
54
56
54
54
52
55
54
54
62
54
54
54
54
54
54
56
48
52
52
54
54
54
54
54
54
54
54
48
54
54
54
54
54
56
56
54
50
54
52
54
55
54
55
56
56
58
54
54
54
54
54
52
Flowrate
IN
TA
TB
TC
gpm
5.8
1.9
7.0
16.3
1.6
1.4
0.0
3.3
0.0
0.0
1.4
5.0
4.1
6.0
2.6
5.6
5.6
9.9
5.0
9.7
7.3
8.5
7.0
2.0
5.0
5.3
12.9
0.0
6.0
14.0
7.5
7.5
7.3
16.6
8.8
8.6
4.6
6.3
14.5
7.7
6.5
5.1
3.1
4.6
1.7
10.6
8.0
11.2
17.5
6.8
3.7
4.4
15.9
5.1
1.0
5.9
5.6
6.6
3.5
2.2
3.5
4.4
2.6
3.1
5.1
5.1
5.2
4.7
5.8
7.0
6.1
3.6
3.7
1.0
12.8
4.3
13.7
4.8
5.2
5.2
10.7
7.3
7.3
7.7
4.5
12.2
4.9
3.0
6.7
7.0
7.6
13.8
5.2
3.7
13.0
5.2
6.0
5.4
7.5
4.7
6.6
1.0
5.8
3.7
4.6
3.2
3.3
3.5
5.5
3.8
5.0
4.4
7.0
6.2
4.2
3.2
1.6
12.6
5.2
13.4
4.0
8.8
5.2
11.1
7.5
4.0
7.9
4.5
12.6
7.2
4.2
3.4
5.7
2.0
7.5
8.2
20.9
12.7
6.0
12.9
3.4
12.3
10.7
13.8
8.7
3.3
6.5
8.8
9.3
7.8
9.9
6.2
6.0
7.7
9.2
11.1
5.6
2.6
4.2
15.0
5.0
4.9
6.4
5.7
12.0
6.5
10.7
14.2
7.8
16.6
8.8
7.1
14.0
19.0
15.8
9.6
15.6
10.1
8.1
8.5
3.9
4.4
16.4
14.3
22.3
12.0
10.3
2.2
6.4
11.8
6.5
Totalizer
IN
TA
TB
TC
gal
1,865,510
1,868,884
1,876,085
1,880,060
1,885,154
1,889,196
1,897,846
1,902,856
1,908,426
1,913,451
1,918,786
1,923,200
1,933,973
1,938,947
1,944,845
1,953,967
1,960,358
1,966,816
2,000,317
2,006,833
2,012,104
2,018,391
2,024,588
2,031,182
2,043,674
2,048,629
2,054,776
2,060,257
2,068,825
2,074,389
2,088,333
2,095,967
2,107,504
2,116,820
2,124,639
2,132,963
2,151,996
2,159,073
2,168,003
2,173,375
2,179,907
2,188,878
2,200,539
2,206,645
2,213,194
2,222,107
2,236,025
2,249,134
2,274,468
2,285,420
2,293,013
2,299,572
2,306,819
2,315,507
556,696
560,259
566,009
569,041
572,863
576,004
582,826
586,752
591,035
594,816
595,437
599,027
606,856
610,652
614,956
621,960
626,693
631,340
649,282
649,711
653,263
657,677
662,165
667,010
676,100
679,782
684,014
687,957
694,571
698,288
708,533
716,555
723,006
730,050
736,015
742,131
756,680
761,985
768,751
772,538
777,041
783,236
787,304
791,446
796,446
802,570
812,944
822,955
842,090
850,461
855,715
860,395
865,880
872,354
1,249,025
1,252,953
1,258,775
1,261,849
1,265,759
1,268,654
1,275,114
1,278,855
1,282,837
1,286,690
1,289,516
1,293,031
1,299,258
1,302,509
1,305,564
1,312,359
1,317,370
1,322,207
1,340,333
1,340,572
1,344,275
1,348,786
1,353,022
1,357,783
1,366,143
1,369,303
1,373,515
1,376,887
1,383,375
1,387,185
1,397,692
1,406,203
1,412,936
1,420,492
1,426,626
1,433,172
1,448,135
1,453,704
1,461,015
1,464,551
1,468,880
1,475,971
1,483,370
1,488,404
1,494,029
1,500,662
1,511,968
1,522,488
1,542,669
1,551,512
1,557,374
1,562,086
1,567,957
1,574,936
2,643,830
2,651,923
2,662,905
2,669,540
2,677,557
2,683,854
2,697,443
2,705,781
2,713,841
2,721,568
2,729,578
2,737,844
2,755,210
2,763,742
2,772,846
2,786,878
2,797,192
2,806,892
2,843,624
2,843,882
2,852,123
2,861,742
2,871,329
2,881,433
2,899,666
2,907,857
2,919,058
2,925,571
2,938,044
2,947,018
2,968,239
2,984,743
2,997,774
3,011,856
3,024,158
3,036,944
3,065,883
3,077,342
3,080,841
3,099,727
3,109,690
3,122,821
3,141,676
3,151,083
3,161,892
3,175,361
3,197,348
3,218,012
3,227,680
3,275,090
3,287,026
3,296,868
3,308,635
3,322,246
Total
BVs|c|
BVs
34,291
34,396
34,538
34,624
34,728
34,810
34,986
35,094
35,199
35,299
35,403
35,510
35,736
35,846
35,964
36,146
36,280
36,406
36,882
36,886
36,993
37,117
37,242
37,373
37,609
37,715
37,861
37,945
38,107
38,223
38,499
38,713
38,882
39,064
39,224
39,390
39,765
39,914
39,959
40,204
40,333
40,504
40,748
40,870
41,010
41,185
41,470
41,738
41,864
42,478
42,633
42,761
42,914
43,090
BW
Totalizer
gal
302,282
303,007
304,086
304,445
305,191
305,898
307,350
308,075
308,894
309,995
309,998
310,215
310,892
310,892
310,986
311,713
311,713
312,436
313,858
315,280
315,280
316,004
316,723
317,443
319,010
319,610
320,698
321,053
322,500
322,869
323,850
324,674
325,399
326,492
326,850
327,575
329,752
329,752
331,203
331,326
331,929
333,800
334,105
334,837
336,295
336,245
337,019
338,769
334,559
39,912
340,634
342,076
342,798
343,545
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
60
61
62
63
66
67
68
69
70
71
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Date
01/25/10
01/26/10
01/27/10
01/28/10
01/29/10
01/30/10
02/01/10
02/02/10
02/03/10
02/04/10
02/05/10
02/06/10
02/08/10
02/09/10
02/10/10
02/11/10
02/12/10
02/13/10
02/15/10
02/16/10
02/17/10
02/18/10
03/08/10
03/09/10
03/10/10
03/11/10
03/12/10
03/13/10
03/15/10
03/16/10
03/17/10
03/18/10
03/19/10
03/20/10
03/22/10
03/23/10
03/24/10
03/25/10
03/26/10
03/27/10
03/29/10
03/30/10
03/31/10
04/01/10
04/02/10
04/03/10
04/05/10
04/06/10
04/07/10
04/08/10
04/09/10
04/10/10
04/12/10
04/13/10
04/14/10
04/15/10
04/16/10
04/17/10
Hour Meter (hr)
Record
hr
10,428
10,451
10,474
10,498
10,523
10,, 546
10,593
10,615
10,640
10,661
10,686
10,708
10,754
10,779
10,801
10,825
10,849
10,872
10,918
10,940
10,965
10,987
11,408
11,438
11,457
11,480
11,503
11,527
11,570
11,594
11,624
11,641
11,668
11,689
11,736
11,765
11,783
11,806
11,833
11,855
11,900
11,928
11,948
11,975
11,997
12,022
12,064
12,087
12,110
12,137
12,150
12,179
12,225
12,249
12,273
12,295
12,319
12,344
Diff
hr
47
23
23
24
25
23
47
22
25
21
25
22
46
25
22
24
24
23
46
22
25
22
421
30
19
23
23
24
43
24
30
17
27
21
47
29
18
23
27
22
45
28
20
27
22
25
42
23
23
27
13
29
46
24
24
22
24
25
Pressure
IN
TA
TB
AP
TC
psi
62
60
66
58
62
62
62
62
60
64
60
62
68
60
60
62
64
60
62
58
60
60
58
58
60
58
60
62
60
58
64
62
58
58
62
62
58
62
62
60
60
60
60
60
60
70
60
60
60
60
62
62
62
60
62
62
60
60
60
60
62
58
58
58
60
62
60
64
60
58
60
58
60
60
58
58
58
60
56
60
60
60
60
56
58
60
58
58
64
60
58
58
58
60
58
60
60
60
58
60
58
60
60
60
58
58
58
60
60
60
60
60
60
60
60
60
60
60
62
58
58
58
60
62
60
64
60
58
60
58
60
60
58
58
58
60
56
60
60
60
60
56
58
60
58
58
64
60
58
58
58
60
58
60
60
60
58
60
58
60
60
60
58
58
58
60
60
60
60
60
60
60
60
60
60
60
64
60
60
60
60
64
60
64
60
60
60
60
60
60
60
60
60
60
60
60
60
60
60
56
60
60
60
58
64
60
58
58
60
60
60
60
60
60
58
60
58
60
60
60
58
58
58
60
60
60
60
60
60
60
60
60
54
54
54
54
54
50
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
52
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
Flowrate
IN
TA
TB
TC
gpm
14.4
5.3
10.9
5.0
3.0
13.5
6.0
8.7
13.0
8.7
3.5
2.7
6.7
11.8
2.6
5.1
12.7
4.3
4.1
3.5
0.0
3.2
3.8
6.9
3.6
0.0
5.2
6.4
1.2
3.6
4.5
6.5
0.0
3.8
6.4
6.1
0.6
5.7
7.7
0.0
0.0
2.5
0.0
7.4
9.6
0.0
16.5
18.9
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
11.4
5.2
7.2
2.1
13.4
8.9
7.3
11.9
7.1
2.3
3.2
6.2
10.9
2.0
5.3
10.9
1.5
6.4
3.5
5.1
1.1
6.0
3.9
2.5
3.3
5.9
3.9
1.2
2.1
4.9
4.9
3.5
2.7
4.9
2.2
5.8
1.0
3.6
1.9
1.4
3.2
3.3
4.7
4.0
4.5
3.2
2.4
3.8
11.5
5.4
6.5
6.7
2.3
13.2
7.2
11.8
7.0
5.0
2.6
6.5
4.8
5.6
6.0
10.1
6.6
3.2
6.2
2.9
3.0
6.4
3.4
6.2
2.9
4.3
3.1
2.6
5.0
4.2
4.1
4.4
4.4
2.4
12.1
14.1
4.7
4.2
3.2
3.7
5.0
2.8
4.1
3.9
5.5
13.0
9.4
13.1
7.4
5.2
12.6
9.0
15.6
10.3
13.6
8.9
4.7
13.5
5.2
11.1
10.5
9.8
12.9
9.5
10.6
5.1
6.3
9.6
8.1
24.0
3.4
3.7
11.6
6.8
3.7
9.1
11.2
6.6
7.1
5.9
5.9
2.6
6.1
6.0
8.0
3.5
9.1
2.2
8.1
6.6
3.1
9.3
6.5
9.7
5.9
12.6
7.6
7.4
11.9
Totalizer
IN
TA
TB
TC
gal
2,336,879
2,344,489
2,353,199
2,361,017
2,370,669
2,377,090
2,392,177
2,398,649
2,408,220
2,414,620
2,421,882
2,428,313
2,440,749
2,448,258
2,455,083
2,461,858
2,469,390
2,475,247
2,488,135
2,494,897
2,501,056
2,505,547
2,589,144
2,593,740
2,598,241
2,602,338
2,606,313
2,610,170
2,619,321
2,624,493
2,630,281
2,632,219
2,636,449
2,639,753
2,647,606
2,652,807
2,654,976
2,658,067
2,664,158
2,666,705
2,674,374
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
883,917
894,612
901,320
907,451
914,867
919,548
930,880
936,715
944,408
949,199
954,941
960,011
969,743
975,768
981,212
986,729
992,630
996,615
1,006,034
1,011,086
1,015,374
1,018,715
1,081,927
1,085,429
1,088,941
1,092,061
1,095,050
1,097,936
1,105,231
1,109,079
1,113,576
1,114,900
1,118,156
1,120,778
1,126,382
1,130,820
1,132,318
1,134,603
1,139,372
1,141,248
1,146,879
1,151,021
1,153,873
1,159,037
1,161,934
1,166,402
1,174,458
1,178,505
1,183,145
1,188,617
1,191,909
1,196,750
1,206,932
1,211,280
1,215,907
1,219,838
1,224,633
1,229,270
1,592,579
1,598,941
1,605,768
1,612,429
1,620,021
1,625,624
1,638,220
1,644,381
1,652,493
1,657,627
1,663,550
1,668,778
1,677,517
1,683,586
1,689,089
1,694,712
1,701,791
1,705,012
1,715,517
1,720,926
1,725,508
1,729,091
1,795,500
1,799,097
1,802,718
1,806,328
1,810,180
1,813,528
1,821,350
1,825,468
1,829,933
1,831,352
1,832,021
1,834,555
1,840,782
1,844,857
1,846,530
1,848,902
1,849,694
1,849,694
1,849,694
1,849,694
1,849,694
1,854,410
1,857,636
1,862,329
1,870,221
1,874,563
1,878,816
1,883,652
1,886,724
1,891,311
1,900,873
1,905,522
1,910,211
1,914,177
1,918,949
1,923,507
3,356,592
3,369,820
3,384,048
3,397,194
3,412,148
3,423,264
3,448,262
3,460,993
3,476,433
3,487,526
3,499,677
3,510,333
3,531,353
3,543,744
3,555,269
3,566,860
3,579,438
3,589,329
3,610,512
3,621,666
3,631,966
3,640,157
3,788,635
3,796,463
3,804,506
3,811,682
3,818,626
3,825,453
3,840,791
3,849,299
3,858,122
3,861,954
3,869,209
3,874,633
3,887,637
3,895,850
3,900,011
3,905,229
3,914,956
3,920,219
3,933,158
3,942,042
3,949,036
3,959,607
3,966,542
3,976,304
3,993,691
4,002,821
4,012,027
4,021,982
4,028,986
4,038,577
4,058,943
4,068,006
4,077,685
4,086,087
4,096,385
4,106,285
Total
BVs|c|
BVs
43,536
43,707
43,892
44,062
44,256
44,400
44,725
44,890
45,090
45,234
45,391
45,530
45,802
45,963
46,112
46,263
46,426
46,554
46,829
46,974
47,107
47,213
49,139
49,241
49,345
49,438
49,528
49,617
49,816
49,926
50,040
50,090
50,184
50,255
50,423
50,530
50,584
50,651
50,778
50,846
51,014
51,129
51,220
51,357
51,447
51,573
51,799
51,917
52,037
52,166
52,257
52,381
52,645
52,763
52,888
52,997
53,131
53,259
BW
Totalizer
gal
344,959
344,959
345,680
346,689
347,837
348,203
349,884
349,996
351,431
351,431
352,147
352,865
354,300
355,381
355,736
356,461
357,542
354,895
359,328
360,048
361,122
361,476
374,365
375,081
375,825
376,411
377,125
377,838
379,972
379,988
381,422
381,422
382,399
(d)
384,287
385,716
385,716
386,430
387,857
387,857
389,285
390,706
390,706
392,128
392,841
393,552
394,264
394,972
395,091
397,109
397,109
397,813
399,218
399,917
400,621
401,329
402,021
402,718
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
72
73
74
75
76
77
78
79
80
81
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Fri
Sat
Date
04/19/10
04/20/10
04/21/10
04/22/10
04/23/10
04/24/10
04/26/10
04/27/10
04/28/10
04/29/10
04/30/10
05/01/10
05/03/10
05/04/10
05/05/10
05/06/10
05/07/10
05/08/10
05/10/10
05/11/10
05/12/10
05/13/10
05/14/10
05/15/10
05/17/10
05/18/10
05/19/10
05/20/10
05/21/10
05/22/10
05/24/10
05/25/10
05/26/10
05/27/10
05/28/10
05/29/10
05/31/10
06/01/10
06/03/10
06/04/10
06/05/10
06/07/10
06/08/10
06/09/10
06/10/10
06/11/10
06/12/10
06/14/10
06/15/10
06/16/10
06/17/10
06/18/10
06/19/10
06/25/10
06/26/10
Hour Meter (hr)
Record
hr
12,389
12,412
12,435
12,460
12,492
12,506
12,553
12,576
12,601
12,624
12,649
12,671
12,714
12,741
12,764
12,789
12,811
12,835
12,888
12,913
12,925
12,952
12,974
12,999
13,046
13,068
13,091
13,115
13,139
13,165
13,209
13,233
13,256
13,276
13,305
13,335
13,384
13,401
13,446
13,477
13,498
13,540
13,564
13,589
13,610
13,634
13,657
13,705
13,728
13,752
13,778
13,799
13,820
13,963
13,992
Diff
hr
45
23
23
25
32
14
47
23
25
23
25
22
43
27
23
25
22
24
53
25
12
27
22
25
47
22
23
24
24
26
44
24
23
20
29
30
49
17
45
31
21
42
24
25
21
24
23
48
23
24
26
21
21
143
29
Pressure
IN
TA
TB
AP
TC
psi
60
60
64
62
60
70
60
60
60
60
64
60
58
62
60
64
70
62
60
60
64
68
58
64
64
66
60
58
58
58
60
60
60
64
62
62
60
64
68
60
62
64
60
64
60
66
64
64
60
58
66
60
70
64
64
58
60
64
60
60
70
60
60
60
60
60
60
58
58
60
60
60
56
60
64
64
64
60
60
60
62
60
56
60
58
58
60
60
60
60
56
58
60
60
60
60
64
60
60
60
60
60
64
60
58
58
60
60
60
66
58
60
64
60
60
70
60
60
60
60
60
60
58
58
60
60
60
56
60
64
64
64
60
60
60
62
60
56
60
58
58
60
60
60
60
56
58
60
60
60
60
64
60
60
60
60
60
64
60
58
58
60
60
60
70
58
60
64
60
60
70
58
60
64
60
60
62
58
58
60
60
60
56
60
64
64
64
60
60
60
62
60
56
60
58
58
60
60
60
60
56
58
60
60
60
60
64
60
60
60
60
60
64
60
58
58
60
60
60
70
54
54
54
54
54
54
54
54
54
54
59
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
62
56
55
54
54
56
54
54
54
54
54
54
54
54
54
54
54
54
54
Flowrate
IN
TA
TB
TC
gpm
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
2.9
3.5
5.1
4.8
3.9
9.2
6.2
3.7
2.2
7.2
3.1
2.5
3.0
2.7
3.0
6.0
5.9
3.7
2.5
2.4
4.7
2.6
2.3
2.1
3.4
4.0
3.8
4.6
2.8
8.4
4.6
3.7
5.2
4.5
10.2
3.1
6.4
2.8
3.8
4.0
2.8
3.7
3.5
8.3
4.4
4.1
4.7
3.1
8.8
7.3
6.3
5.0
1.8
5.5
5.5
7.3
6.3
5.0
1.8
5.5
2.7
3.5
4.0
5.7
2.6
2.6
5.2
3.0
7.0
6.4
3.7
2.9
4.1
5.3
2.8
8.4
4.6
2.5
4.6
6.3
5.4
10.3
3.1
5.6
3.4
3.9
5.1
2.1
3.8
1.9
5.3
7.8
8.1
7.9
9.1
12.3
17.0
3.7
12.8
6.5
6.5
12.1
9.8
3.2
11.7
8.6
8.8
8.7
9.8
11.5
6.5
9.7
5.6
5.9
10.6
6.7
1.5
11.6
3.6
7.6
6.9
8.4
10.6
7.9
8.5
9.4
11.6
7.1
11.2
14.3
5.8
7.9
6.6
6.3
10.3
4.9
7.6
5.9
12.7
Totalizer
IN
TA
TB
TC
gal
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
1,238,575
1,242,915
1,247,693
1,252,446
1,259,346
1,262,211
1,270,344
1,274,466
1,278,622
1,282,966
1,287,971
1,294,428
1,302,729
1,306,496
1,309,384
1,313,279
1,318,228
1,321,047
1,328,468
1,331,217
1,333,666
1,337,833
1,342,089
1,344,911
1,352,316
1,355,781
1,358,789
1,361,262
1,363,695
1,366,344
1,370,965
1,374,797
1,378,544
1,383,379
1,389,999
1,344,846
1,402,946
1,406,231
1,415,761
1,420,380
1,423,045
1,428,909
1,432,578
1,436,602
1,438,842
1,442,310
1,444,921
1,449,748
1,452,565
1,455,828
1,459,673
1,461,476
1,463,916
1,472,595
1,482,454
1,932,920
1,937,052
1,942,022
1,946,923
1,953,930
1,956,698
1,964,720
1,969,083
1,973,435
1,977,765
1,982,933
1,989,581
1,997,853
2,001,432
2,004,467
2,008,627
2,013,580
2,016,302
2,023,138
2,025,600
2,027,836
2,032,445
2,037,130
2,039,877
2,047,318
2,050,775
2,053,600
2,055,861
2,057,977
2,060,470
2,064,938
2,068,149
2,072,605
2,077,536
2,084,298
2,089,180
2,097,465
2,100,593
2,110,030
2,114,161
2,116,832
2,122,533
2,126,139
2,130,040
2,132,104
2,135,484
2,138,113
2,142,822
2,145,500
2,148,727
2,152,419
2,153,834
2,155,662
2,161,647
2,171,192
4,126,103
4,135,333
4,145,437
4,155,662
4,169,751
4,176,270
4,193,125
4,202,038
4,211,428
4,220,892
4,231,339
4,244,442
4,261,452
4,269,426
4,275,925
4,284,305
4,294,384
4,300,460
4,315,555
4,321,530
4,326,720
4,335,941
4,345,605
4,351,825
4,367,957
4,375,487
4,382,143
4,387,545
4,392,810
4,398,698
4,409,818
4,416,480
4,425,983
4,436,850
4,450,553
4,461,645
4,481,095
4,488,416
4,508,539
4,517,488
4,522,970
4,536,322
4,544,139
4,552,147
4,557,362
4,564,887
4,570,568
4,580,966
4,587,272
4,594,719
4,601,812
4,606,153
4,610,622
4,625,600
4,644,302
Total
BVs|c|
BVs
53,516
53,636
53,767
53,900
54,082
54,167
54,386
54,501
54,623
54,746
54,881
55,051
55,272
55,375
55,459
55,568
55,699
55,778
55,973
56,051
56,118
56,238
56,363
56,444
56,653
56,751
56,837
56,907
56,975
57,052
57,196
57,282
57,406
57,547
57,724
57,868
58,121
58,216
58,477
58,593
58,664
58,837
58,938
59,042
59,110
59,207
59,281
59,416
59,498
59,594
59,686
59,743
59,801
59,995
60,237
BW
Totalizer
gal
404,109
404,803
465,497
406,194
407,590
407,590
408,984
409,679
410,373
411,065
411,761
412,458
413,847
414,549
415,239
416,282
416,621
417,313
419,377
420,063
420,750
420,750
421,437
422,119
423,480
424,189
424,839
425,520
426,204
427,237
428,260
428,947
429,631
430,313
430,990
432,350
433,710
439,394
435,677
436,435
437,110
437,783
438,463
439,811
439,811
440,488
441,167
442,530
443,206
443,882
445,231
445,231
445,908
447,590
448,935
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
82
83
84
85
86
87
88
89
90
Mon
Tue
Wed
Thu
Fri
Sat
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Date
06/28/10
06/29/10
06/30/10
07/01/10
07/02/10
07/03/10
07/06/10
07/07/10
07/08/10
07/09/10
07/10/10
07/12/10
07/13/10
07/14/10
07/15/10
07/16/10
07/17/10
07/19/10
07/20/10
07/21/10
07/22/10
07/23/10
07/24/10
07/26/10
07/27/10
07/28/10
07/29/10
07/30/10
07/31/10
08/02/10
08/03/10
08/04/10
08/05/10
08/06/10
08/07/10
08/09/10
08/10/10
08/11/10
08/12/10
08/13/10
08/14/10
08/16/10
08/17/10
08/18/10
08/19/10
08/20/10
08/21/10
08/23/10
08/24/10
08/25/10
08/26/10
08/27/10
08/28/10
Hour Meter (hr)
Record
hr
14,034
14,064
14,082
14,111
14,134
14,153
14,223
14,245
14,271
14,293
14,317
14,365
14,388
14,414
14,436
14,456
14,481
14,529
14,553
14,576
14,600
14,626
14,647
14,694
14,717
14,740
14,765
14,788
14,813
14,856
14,881
14,904
14,929
14,951
14,976
15,023
15,047
15,070
15,094
15,117
15,141
15,188
15,211
15,235
15,259
15,283
15,305
15,353
15,379
15,399
15,423
15,447
15,472
Diff
hr
42
30
18
29
23
19
70
22
26
22
24
48
23
26
22
20
25
48
24
23
24
26
21
47
23
23
25
23
25
43
25
23
25
22
25
47
24
23
24
23
24
47
23
24
24
24
22
48
26
20
24
24
25
Pressure
IN
TA
TB
AP
TC
psi
60
64
60
64
74
68
60
62
62
60
64
68
60
64
60
60
64
62
64
66
68
68
64
62
62
70
66
64
64
60
62
62
60
62
66
60
62
70
78
62
74
66
60
66
66
60
64
64
60
64
60
64
68
64
60
60
62
60
66
64
58
58
60
60
66
58
64
60
60
60
60
60
64
64
66
64
60
60
70
66
68
60
60
60
60
60
62
62
60
62
68
76
64
64
60
60
60
68
60
62
68
60
62
60
60
68
64
60
60
64
60
66
64
58
58
60
60
66
58
64
60
60
60
60
60
64
64
66
64
60
60
70
66
68
60
60
60
60
60
62
62
60
62
68
76
64
64
60
60
60
68
60
60
70
60
62
60
60
68
64
60
66
66
60
60
64
58
58
60
60
72
58
64
60
60
60
60
60
64
64
66
64
60
60
70
66
68
60
60
60
60
60
62
62
60
64
68
76
64
64
60
60
60
68
60
62
70
60
62
60
60
68
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
Flowrate
IN
TA
TB
TC
gpm
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
2.5
3.4
0.6
3.4
5.1
6.9
2.5
2.8
8.4
11.3
1.4
2.2
4.6
5.2
4.8
3.7
4.2
3.6
2.7
7.4
5.4
7.1
11.1
2.5
1.9
1.1
3.5
2.5
2.4
5.8
8.6
4.5
2.0
2.7
2.5
2.2
3.9
3.2
1.9
6.9
4.9
3.2
2.3
5.0
2.2
5.2
3.7
4.8
7.2
4.2
2.8
7.5
10.4
4.5
1.9
2.9
4.8
6.0
5.1
2.5
3.1
3.9
2.5
7.7
5.7
6.2
10.2
2.5
1.2
7.3
1.7
2.2
1.7
3.5
7.1
3.7
4.8
4.8
2.9
1.9
2.6
4.5
1.4
7.1
1.2
6.4
6.0
2.4
4.9
5.4
9.2
4.7
6.9
6.5
14.6
2.9
1.4
1.6
5.9
6.7
16.7
5.4
6.7
6.5
4.9
5.6
10.1
7.5
12.4
5.9
6.7
14.2
8.9
9.3
11.4
9.7
3.6
5.7
6.1
8.0
6.2
6.2
4.9
4.3
12.2
11.4
8.3
11.1
6.0
4.9
9.7
5.6
13.2
1.6
12.6
6.9
5.3
9.3
Totalizer
IN
TA
TB
TC
gal
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
1,492,925
1,500,761
1,503,177
1,508,457
1,512,976
1,517,819
1,517,819
1,517,819
1,517,819
1,517,819
1,517,819
1,517,819
1,517,819
1,547,806
1,551,148
1,555,802
1,559,469
1,559,734
1,573,786
1,577,444
1,580,660
1,585,679
1,588,583
1,596,177
1,601,036
1,606,355
1,610,805
1,614,072
1,617,559
1,625,406
1,630,386
1,634,564
1,638,521
1,644,194
1,647,872
1,651,936
1,651,936
1,655,095
1,659,536
1,664,521
1,669,829
1,678,053
1,681,565
1,686,344
1,690,732
1,693,935
1,696,711
1,706,792
1,711,860
1,715,092
1,719,967
1,724,583
1,728,302
2,180,743
2,188,124
2,196,379
2,195,475
2,199,674
2,204,383
1,522,801
1,522,801
1,522,801
1,526,797
1,530,306
1,539,227
1,543,766
2,243,428
2,246,342
2,250,609
2,254,013
2,264,243
2,267,869
2,271,200
2,274,131
2,279,220
2,282,104
2,288,603
2,292,737
2,297,217
2,301,206
2,303,794
2,306,978
2,314,151
2,318,983
2,322,888
2,326,280
2,331,751
2,335,062
2,341,139
2,344,917
2,348,213
2,351,976
2,356,583
2,360,901
2,368,684
2,372,131
2,376,342
2,380,734
2,383,848
2,386,490
2,396,452
2,401,433
2,405,341
2,410,653
2,415,350
2,419,185
4,665,540
4,680,284
4,685,629
4,696,270
4,703,089
4,713,266
4,734,597
4,742,804
4,752,056
4,760,829
4,769,146
4,786,917
4,795,434
4,803,358
4,810,782
4,820,373
4,828,115
4,849,237
4,857,426
4,865,672
4,871,001
4,882,020
4,888,929
4,904,263
4,913,954
4,924,687
4,934,266
4,940,001
4,948,595
4,965,611
4,976,066
4,984,658
4,992,707
5,003,952
5,012,279
5,026,727
5,035,077
5,042,801
5,051,745
5,061,742
5,072,309
5,089,546
5,097,614
5,107,525
5,117,275
5,123,894
5,130,029
5,150,622
5,159,925
5,168,028
5,178,735
5,188,296
5,196,354
Total
BVs|c|
BVs
60,513
60,704
60,773
60,911
61,000
61,132
61,409
61,515
61,635
61,749
61,857
62,087
62,198
62,300
62,397
62,521
62,621
62,895
63,002
63,109
63,178
63,321
63,410
63,609
63,735
63,874
63,998
64,073
64,184
64,405
64,540
64,652
64,756
64,902
65,010
65,197
65,306
65,406
65,522
65,652
65,789
66,012
66,117
66,245
66,372
66,458
66,537
66,804
66,925
67,030
67,169
67,293
67,398
BW
Totalizer
gal
449,612
450,963
450,963
452,311
452,987
452,987
455,024
455,702
456,379
457,055
457,728
459,071
460,744
460,759
461,090
461,764
462,436
463,777
464,446
465,120
465,789
467,131
467,131
468,472
469,142
469,810
470,478
471,146
472,154
473,151
473,818
474,484
475,152
475,518
476,483
477,817
478,484
479,151
479,817
480,485
481,155
482,488
483,156
483,801
484,484
485,147
485,811
487,136
488,469
488,469
489,135
489,801
490,464
-------
Table A-l. Operational Data for Hot Springs Mobile Home Park in Willard, UT (Continued)
WK
No.
91
92
93
94
95
96
97
98
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Date
08/30/10
08/31/10
09/01/10
09/02/10
09/03/10
09/04/10
09/06/10
09/07/10
09/16/10
09/17/10
09/18/10
09/20/10
09/21/10
09/22/10
09/23/10
09/24/10
09/25/10
09/27/10
09/28/10
09/29/10
09/30/10
10/01/10
10/02/10
10/04/10
10/05/10
10/06/10
10/07/10
10/08/10
10/09/10
10/11/10
10/12/10
10/13/10
10/14/10
10/15/10
10/16/10
10/18/10
Hour Meter (hr)
Record
hr
15,518
15,539
15,568
15,588
15,611
15,635
15,681
15,707
15,917
15,941
15,967
16,013
16,035
16,059
16,082
16,106
16,130
16,175
16,202
16,227
16,251
16,274
16,297
16,340
16,364
16,388
16,412
16,440
16,468
16,506
16,534
16,552
16,576
16,599
16,622
16,670
Diff
hr
46
21
29
20
23
24
46
26
210
24
26
46
22
24
23
24
24
45
27
25
24
23
23
43
24
24
24
28
28
38
28
18
24
23
23
48
Pressure
IN
TA
TB
AP
TC
psi
62
60
60
62
64
64
70
62
60
60
64
66
70
74
82
62
60
62
72
64
60
66
60
66
66
60
64
60
66
66
60
66
64
66
70
66
60
60
60
60
60
60
68
60
60
60
64
62
62
72
72
58
62
62
70
58
60
58
62
66
60
60
60
58
62
62
60
60
70
62
66
66
60
60
60
60
60
60
68
60
60
60
64
62
62
72
72
58
62
62
70
58
60
58
62
66
60
60
60
58
60
62
60
60
70
62
66
66
60
60
62
64
60
60
70
62
60
60
64
62
62
72
72
60
66
62
70
60
60
58
62
66
60
60
60
58
62
64
60
62
70
62
66
66
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
54
Flowrate
IN
TA
TB
TC
gpm
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
3.6
2.3
3.1
4.3
1.7
6.0
10.9
2.6
0.9
11.6
3.9
2.5
6.5
7.3
3.8
2.3
5.1
9.2
3.6
12.9
4.4
3.9
6.6
2.6
2.0
2.4
2.6
5.7
5.9
4.0
1.5
3.7
2.3
2.3
4.1
0.6
10.0
3.1
1.4
11.3
2.9
3.0
6.4
7.4
5.1
2.4
5.1
8.7
2.0
12.6
4.8
3.3
2.3
1.8
1.9
2.5
0.8
3.3
5.4
4.2
7.6
2.6
4.9
4.5
4.2
4.1
14.1
5.1
6.2
3.6
8.5
5.8
7.0
13.5
14.9
1.7
9.0
5.7
8.7
1.8
4.9
11.2
1.0
9.4
4.3
6.9
5.3
7.9
6.8
3.7
6.9
14.9
11.1
9.0
5.3
Totalizer
IN
TA
TB
TC
gal
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
2,675,326
1,735,636
1,738,493
1,743,200
1,745,277
1,748,358
1,751,917
1,758,472
1,762,797
1,800,677
1,804,937
1,810,799
1,820,920
1,825,142
1,829,326
1,833,410
1,837,411
1,841,651
1,852,732
1,859,198
1,865,135
1,869,872
1,874,905
1,880,065
1,886,122
1,889,694
1,892,505
1,896,106
1,899,851
1,903,708
1,908,418
1,912,492
1,914,399
1,918,055
1,921,459
1,925,158
1,932,197
2,426,383
2,429,221
2,434,228
2,436,163
2,439,426
2,443,036
2,449,872
2,454,511
2,492,226
2,496,799
2,503,069
2,513,341
2,517,758
2,522,016
2,526,110
2,530,143
2,534,555
2,540,132
2,552,877
2,559,221
2,563,901
2,569,259
2,574,454
2,580,576
2,584,287
2,587,406
2,591,391
2,595,462
2,599,374
2,604,084
2,608,203
2,610,001
2,613,476
2,616,710
2,620,219
2,626,768
5,211,545
5,217,389
5,227,084
5,231,880
5,238,286
5,245,618
5,259,726
5,268,552
5,348,708
5,357,876
5,370,062
5,391,588
5,400,667
5,409,378
5,417,731
5,426,100
5,435,763
5,459,307
5,473,145
5,485,611
5,495,253
5,506,165
5,516,548
5,530,060
5,537,757
5,544,338
5,552,616
5,560,461
5,569,139
5,580,105
5,588,320
5,592,901
5,600,449
5,607,709
5,615,502
5,629,084
Total
BVs|c|
BVs
67,595
67,670
67,796
67,858
67,941
68,037
68,220
68,334
69,374
69,493
69,651
69,930
70,048
70,161
70,269
70,377
70,503
70,808
70,988
71,149
71,274
71,416
71,551
71,726
71,826
71,911
72,018
72,120
72,233
72,375
72,481
72,541
72,639
72,733
72,834
73,010
BW
Totalizer
gal
491,791
492,458
493,794
493,794
494,461
495,727
496,453
497,460
503,119
503,786
504,789
505,779
506,441
507,105
507,768
508,431
509,094
510,417
511,076
512,072
513,056
513,718
514,377
515,038
515,697
516,358
517,019
518,846
519,010
519,674
521,002
521,002
521,667
522,331
522,995
524,319
(a) Meter required maintenance.
(b) Readings not taken initially.
(c) TA not having a dedicated flow totalizer.
(d) Data not recorded.
(e) Backwash flow meter/totalizer switched with TA flow meter/totalizer.
NA = not available
-------
APPENDIX B
ANALYTICAL DATA
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
^g/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
m/L
Mfl/L
Hfl/L
Hfl/L
^g/L
|jg/L
Hfl/L
^g/L
|jg/L
|jg/L
m/L
12/17/08
IN
-
NA
-
-
-
NA
NA
NA
NA
NA
NA
NA
-
-
-
11.7
-
-
-
-
185
-
100
-
1.6
-
TA
-
NA
-
-
-
NA
NA
NA
NA
NA
NA
NA
-
-
-
5.5
-
-
-
-
<25
-
1.0
-
1.5
-
TB
-
NA
-
-
-
NA
NA
NA
NA
NA
NA
NA
-
-
-
5.3
-
-
-
-
<25
-
0.9
-
1.5
-
AP
-
NA
-
-
-
NA
NA
NA
NA
NA
NA
NA
-
-
-
5.4
-
-
-
-
<25
-
0.7
-
1.7
-
TC
0.7
NA
-
-
-
NA
NA
NA
NA
NA
NA
NA
-
-
0.1
-
-
-
-
<25
-
0.6
-
1.6
-
01/22/09
IN
-
139
<0.1
6.9
0.2
117
14.7
1.7
7.5
15.1
5.0
189
117
95.8
21.0
13.5
11.9
1.6
5.8
6.1
339
118
109
110
1.3
0.96
TA
-
144
<0.1
6.8
0.2
57.6
14.7
<0.1
7.7
15.7
4.2
181
124
103
20.9
9.2
9.0
0.2
0.3
8.7
<25
<25
<0.1
<0.1
1.0
0.86
TB
-
139
<0.1
6.7
0.2
58.2
13.9
<0.1
7.7
15.9
NA
171
121
99.6
21.1
9.1
9.2
<0.1
0.3
9.0
<25
<25
<0.1
<0.1
1.0
0.93
AP
-
142
<0.1
6.9
0.2
58.0
14.8
<0.1
NA
16.1
4.1
167
122
100
21.5
9.2
9.0
0.1
0.3
8.7
<25
<25
<0.1
<0.1
1.0
0.94
TC
5.5
139
<0.1
7.0
0.2
<10
15.2
<0.1
7.7
16.0
3.9
169
121
99.5
21.4
0.1
0.2
<0.1
0.3
<0.1
<25
<25
<0.1
<0.1
0.9
0.8
01/28/09
IN
-
139
-
-
-
NA
15.3
3.5
NA
NA
NA
NA
-
-
-
15.3
-
-
-
-
361
-
117
-
1.9
-
TA
-
137
-
-
-
NA
15.2
0.1
NA
NA
NA
NA
-
-
-
10.2
-
-
-
-
<25
-
1.8
-
1.0
-
TB
-
137
-
-
-
NA
15.3
<0.1
NA
NA
NA
NA
-
-
-
10.9
-
-
-
-
<25
-
9.7
-
1.1
-
AP
-
139
-
-
-
NA
15.4
0.3
NA
NA
NA
NA
-
-
-
10.2
-
-
-
-
<25
-
25.7
-
1.2
-
TC
6.2
139
-
-
-
NA
15.5
<0.1
NA
NA
NA
NA
-
-
-
0.3
-
-
-
-
<25
-
<0.1
-
3.5
-
02/04/09 a|
IN
-
143
-
-
-
NA
15.6
3.6
7.6
9.0
5.8
128
-
-
-
15.5
-
-
-
-
283
-
109
-
1.4
-
TA
-
141
-
-
-
NA
15.8
0.7
7.7
9.8
4.8
103
-
-
-
11.8
-
-
-
-
<25
-
45.1
-
1.1
-
TB
-
141
-
-
-
NA
15.6
0.6
8.1
9.9
4.5
41
-
-
-
11.7
-
-
-
-
<25
-
0.9
-
0.9
-
AP
-
138
-
-
-
NA
15.6
0.9
8.1
9.3
4.1
47
-
-
-
11.8
-
-
-
-
<25
-
47.2
-
1.0
-
TC
7.0
143
-
-
-
NA
16.2
0.5
8.0
9.1
5.3
41
-
-
-
<0.1
-
-
-
-
<25
-
0.1
-
1.0
-
(a) Water quality parameters measured on 02/05/09.
NA = not available
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
|jg/L
ug/L
^g/L
ug/L
ug/L
|jg/L
Ug/L
|jg/L
ug/L
ug/L
ug/L
02/11/09
IN
-
149
<0.1
7.0
0.2
98.7
15.7
1.7
7.8
15.6
3.9
187
111
91.7
19.2
13.6
12.8
0.8
2.8
10.0
204
115
103
104
1.8
1.0
TA
-
149
<0.1
6.4
0.3
65.3
15.4
<0.1
7.9
16.5
3.0
188
112
92.3
19.3
11.1
11.0
0.2
0.7
10.3
<25
<25
4.5
<0.1
1.7
0.9
TB
-
147
<0.1
6.5
0.2
61.8
15.4
<0.1
8.0
16.5
2.7
187
105
86.7
18.5
10.5
10.3
0.1
0.5
9.8
<25
<25
4.3
0.1
1.5
0.9
AP
-
149
<0.1
6.7
0.3
62.4
15.4
<0.1
8.0
16.7
2.6
185
106
86.8
18.7
11.1
10.6
<0.1
0.5
10.2
<25
<25
0.2
<0.1
1.5
0.9
TC
7.8
147
<0.1
6.6
0.2
<10
15.8
0.2
8.0
16.5
2.6
183
108
88.7
19.0
0.2
0.2
<0.1
0.5
<0.1
<25
<25
3.0
0.2
23.7 (c)
0.8
2/18/09|a|
IN
-
147
-
-
-
;
14.6
2.2
7.8
15.2
3.9
224
-
-
-
13.5
-
-
-
-
277
-
102
-
1.7
-
TA
-
147
-
-
-
;
14.6
<0.1
7.8
15.6
3.6
178
-
-
-
10.3
-
-
-
-
<25
-
4.1
-
1.2
-
TB
-
144
-
-
-
;
14.4
<0.1
7.7
15.6
3.3
176
-
-
-
10.3
-
-
-
-
<25
-
2.3
-
1.3
-
AP
-
144
-
-
-
;
15
<0.1
7.7
15.8
3.4
174
-
-
-
10.3
-
-
-
-
<25
-
8.9
-
1.3
-
TC
8.7
142
-
-
-
;
14.4
0.1
7.1
15.6
3.5
175
-
-
-
0.2
-
-
-
-
<25
-
0.1
-
2.8
-
02/25/09
IN
-
138
140
-
-
-
;
15.1
15.0
10.0
9.5
7.7
14.0
5.4
248
-
-
-
20.5
20.1
-
-
-
-
863
839
-
134
133
-
3.3
3.3
-
AP
-
144
142
-
-
-
;
15.0
15.0
0.2
0.2
7.9
14.2
3.6
240
-
-
-
0.2
0.2
-
-
-
-
<25
<25
-
0.1
0.2
-
2.9
2.7
-
TC
9.4
140
140
-
-
-
;
15.4
14.9
0.3
0.3
NA
NA
NA
NA
-
-
-
0.1
0.1
-
-
-
-
<25
<25
-
<0.1
<0.1
-
1.6
1.7
-
03/04/09
IN
-
137
-
-
-
;
15.2
2.1
7.5
17.1
3.6
222
-
-
-
12.0
-
-
-
-
195
-
109
-
2.2
-
AP
-
139
-
-
-
;
15.2
<0.1
7.7
17.3
3.3
217
-
-
-
9.8
-
-
-
-
<25
-
17.8
-
1.8
-
TC
10.2
137
-
-
-
;
15.7
<0.1
7.7
17.3
3.3
204
-
-
-
0.1
-
-
-
-
<25
-
<0.1
-
1.7
-
3/10/09""
IN
-
147
<0.1
6.6
0.2
132
15.0
2.4
7.7
12.9
3.7
205
116
91.1
25.3
14.1
13.7
0.5
6.7
7.0
333
157
120
115
2.1
TA
-
145
<0.1
6.5
0.2
83.3
14.6
0.2
NA
NA
NA
NA
119
92.3
26.5
11.1
11.6
<0.1
1.4
10.2
<25
<25
0.8
0.1
1.8
TB
-
145
<0.1
6.4
0.3
79.9
15.0
<0.1
NA
NA
NA
NA
116
91.0
25.4
11.1
11.7
<0.1
0.5
11.2
<25
<25
0.3
0.2
1.6
TC
10.7
145
<0.1
6.5
0.3
<10
15.0
1.1
7.7
12.1
2.5
189
115
89.9
25.5
0.2
0.2
<0.1
1.2
<0.1
<25
<25
1.9
<0.1
268
(a) Water quality parameters measured on 02/19/09.
(b) Water quality parameters measured on 03/12/09.
(c) Sample was reanalyzed and the result was similar.
NA = not available
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
m/L
van.
|jg/L
|jg/L
Mfl/L
VglL
|jg/L
|jg/L
Hfl/L
VglL
Hg/L
03/18/09
IN
-
140
-
-
-
;
14.7
0.9
7.5
17.6
2.9
205
-
-
-
15.7
-
-
-
-
358
-
112
-
1.8
AP
-
142
-
-
-
;
14.6
0.1
7.6
17.6
2.5
208
-
-
-
11.8
-
-
-
-
<25
-
8.2
-
1.7
-
TC
11.6
140
-
-
-
;
15.1
5.1
7.6
17.8
2.4
212
-
-
-
<0.1
-
-
-
-
<25
-
<0.1
-
4.9
-
03/25/09
IN
-
144
-
-
-
;
14.0
1.9
7.7
12.9
NA
203
-
-
-
15.1
-
-
-
-
254
-
122
-
1.3
-
AP
-
141
-
-
-
;
13.9
0.8
7.6
13.0
NA
197
-
-
-
11.6
-
-
-
-
<25
-
3.2
-
1.2
-
TC
12.3
144
-
-
-
;
14.1
1.3
7.6
13.1
NA
195
-
-
-
0.2
-
-
-
-
<25
-
0.1
-
2.4
-
04/01/09
IN
-
148
-
-
-
;
14.1
4.8
7.6
13.8
NA
207
-
-
-
14.7
-
-
-
-
<25
-
110
-
2.5
-
AP
-
143
-
-
-
;
13.9
0.6
7.8
14.2
NA
211
-
-
-
11.9
-
-
-
-
<25
-
32.2
-
1.8
-
TC
13.1
146
-
-
-
;
14.4
2.4
7.7
14.3
NA
195
-
-
-
0.2
-
-
-
-
<25
-
9.9
-
2.5
-
04/08/09
IN
-
141
<0.1
6.6
0.2
135
14.7
2.4
7.6
16.1
2.8
218
115
96.0
18.8
15.2
15.1
<0.1
7.4
7.7
709
173
127
108
2.2
-
AP
-
143
<0.1
6.8
0.1
68.5
15.0
1.1
7.8
16.3
1.8
221
114
94.3
19.3
11.2
9.6
1.6
0.3
9.3
<25
<25
1.0
<0.1
1.5
-
TC
13.4
148
<0.1
6.7
0.2
<10
15.2
0.6
7.8
16.7
2.3
203
99.5
82.9
16.6
0.5
0.7
<0.1
0.3
0.4
<25
<25
0.9
0.2
3.2
-
04/15/09
IN
-
143
-
-
-
;
16.2
3.4
7.6
17.2
1.8
223
-
-
-
15.1
-
-
-
-
440
-
123
-
2.2
-
AP
-
134
-
-
-
;
16.4
0.8
7.5
17.4
2.3
190
-
-
-
10.9
-
-
-
-
<25
-
2.0
-
1.5
-
TC
14.1
141
-
-
-
;
16.7
1.9
7.6
17.6
1.9
186
-
-
-
0.5
-
-
-
-
<25
-
<0.1
-
1.6
-
04/22/09
IN
-
144
-
-
-
;
15.5
1.9
7.6
17.3
2.1
211
-
-
-
14.6
-
-
-
-
273
-
115
-
2.1
-
AP
-
143
-
-
-
;
15.7
0.2
7.7
17.5
2.0
191
-
-
-
13.0
-
-
-
-
<25
-
0.2
-
1.8
-
TC
14.8
146
-
-
-
;
15.9
0.5
7.7
17.7
2.0
189
-
-
-
0.9
-
-
-
-
<25
-
0.1
-
2.2
-
04/29/09
IN
-
138
-
-
-
;
17.5
3.6
7.6
17.5
2.6
213
-
-
-
12.7
-
-
-
-
235
-
125
-
1.8
-
AP
-
138
-
-
-
;
17.5
<0.1
7.7
17.5
2.0
193
-
-
-
10.2
-
-
-
-
<25
-
16.1
-
1.6
-
TC
15.6
140
-
-
-
;
18
3.8
7.7
18.8
2.0
185
-
-
-
0.4
-
-
-
-
<25
-
0.4
-
1.8
-
Cd
OJ
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity (as
CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
^g/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
m/L
|jg/L
Hfl/L
Hfl/L
^g/L
|jg/L
Hfl/L
^g/L
|jg/L
|jg/L
m/L
05/06/09
IN
-
138
<0.1
6.6
0.2
117
16.4
2.5
7.6
17.9
2.0
207
107
86.9
20.4
13.1
12.0
1.1
5.8
6.2
300
83
115
106
1.9
-
AP
-
140
<0.1
6.4
0.3
74.9
17.6
0.3
7.6
18.7
1.3
213
109
88.4
20.7
9.8
10.1
<0.1
0.1
9.9
<25
<25
0.5
0.3
1.6
-
TC
15.8
138
<0.1
6.6
0.3
34.5
15.8
1.0
7.6
19.1
1.1
190
110
89.6
20.5
2.5
2.5
<0.1
0.3
2.2
<25
<25
12.1
12.2
1.5
-
05/13/09
IN
-
142
-
-
-
-
17.0
2.9
7.6
15.0
2.6
187
-
-
-
12.3
-
-
-
-
189
-
118
-
1.6
-
AP
-
142
-
-
-
-
14.3
4.8
7.7
15.6
2.0
185
-
-
-
0.5
-
-
-
-
<25
-
2.0
-
5.1
-
TC
16.6
140
-
-
-
-
16.8
4.5
7.8
15.9
1.8
177
-
-
-
0.5
-
-
-
-
<25
-
0.5
-
1.6
-
05/20/09
IN
-
143
-
-
-
-
15.9
2.0
7.6
19.5
1.8
186
-
-
-
14.1
-
-
-
-
155
-
111
-
1.6
-
AP
-
143
-
-
-
-
16.2
0.4
7.8
19.5
1.6
188
-
-
-
12.0
-
-
-
-
<25
-
4.3
-
1.3
-
TC
17.6
145
-
-
-
-
16.2
0.4
7.7
19.6
1.7
181
-
-
-
0.5
-
-
-
-
<25
-
0.4
-
1.1
-
05/27/09
IN
-
144
-
-
-
-
15.7
5.2
7.6
19.4
2.1
205
-
-
-
12.5
-
-
-
-
109
-
106
-
1.2
-
AP
-
144
-
-
-
-
16.1
0.8
7.6
19.3
1.5
195
-
-
-
10.6
-
-
-
-
<25
-
0.5
-
0.9
-
TC
18.6
144
-
-
-
-
15.4
5.0
7.6
19.4
1.6
195
-
-
-
0.5
-
-
-
-
<25
-
0.4
-
2.6
-
06/03/09
IN
-
152
<0.1
3.2
0.1
115
15.9
1.3
7.6
20.1
1.8
205
116
96.6
18.9
12.8
12.8
<0.1
6.0
6.8
184
61
121
119
1.5
-
AP
-
147
<0.1
6.5
0.3
80.9
16.0
0.4
7.7
20.2
1.6
202
111
92.9
17.8
10.4
10.8
<0.1
0.2
10.6
<25
<25
0.3
<0.1
1.3
-
TC
19.5
149
<0.1
6.5
0.3
12.1
16.5
0.7
7.7
20.4
1.5
197
111
93.3
17.9
0.5
0.5
<0.1
0.2
0.3
<25
<25
0.1
0.1
1.1
-
06/10/09
IN
-
148
148
-
-
-
-
15.8
15.7
1.4
2.5
7.5
17.8
1.7
180
-
-
-
11.5
11.6
-
-
-
-
103
103
-
116
117
-
1.7
1.8
-
AP
-
148
146
-
-
-
-
16.0
15.8
1.6
0.5
7.7
17.8
1.5
171
-
-
-
10.3
10.1
-
-
-
-
<25
<25
-
1.3
3.9
-
1.6
1.6
-
TC
20.4
148
146
-
-
-
-
15.9
15.8
2.5
1.6
7.7
17.8
1.7
173
-
-
-
0.5
0.4
-
-
-
-
<25
<25
-
0.1
0.2
-
1.4
1.4
-
06/1 8/09 a|
IN
-
152
-
-
-
-
15.5
2.3
7.6
17.8
1.7
181
-
-
-
13.3
-
-
-
-
105
-
113
-
1.5
-
AP
-
150
-
-
-
-
15.7
4.0
7.7
17.9
1.6
177
-
-
-
12.1
-
-
-
-
<25
-
15.9
-
1.7
-
TC
21.1
152
-
-
-
-
15.9
4.1
7.8
17.8
1.7
172
-
-
-
0.6
-
-
-
-
<25
-
1.7
-
12.6
-
(a) Water quality parameters measured on 06/17/09.
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
|jg/L
Hfl/L
^g/L
Hg/L
Hfl/L
|jg/L
m/L
|jg/L
Hfl/L
^g/L
Hg/L
06/24/09
IN
-
142
-
-
-
;
15.2
1.8
7.6
19.6
2.2
112
-
-
-
13.0
-
-
-
-
222
-
103
-
1.6
-
AP
-
146
-
-
-
;
15.5
0.5
7.7
19.6
1.6
181
-
-
-
11.2
-
-
-
-
<25
-
1.5
-
1.5
-
TC
21.4
140
-
-
-
;
15.6
1.5
7.7
19.8
1.7
169
-
-
-
0.4
-
-
-
-
<25
-
0.4
-
1.4
-
06/29/09 a|
IN
-
135
<0.1
6.2
0.3
69.7
16.4
0.9
7.5
21.5
2.1
181
123
106
17.4
11.0
10.9
0.1
4.1
6.9
271
210
94.4
96.4
1.4
-
AP
-
149
<0.1
6.2
0.2
56.7
15.2
0.6
7.6
21.7
1.8
178
120
103
16.9
9.4
9.8
<0.1
<0.1
9.3
<25
<25
<0.1
<0.1
1.0
-
TC
21.8
146
<0.1
6.2
0.3
<10
15.8
0.5
7.7
22.2
1.7
178
123
106
17.1
0.1
0.3
<0.1
<0.1
0.2
62
<25
1.0
<0.1
1.2
-
07/08/09
IN
-
146
-
-
-
;
15.8
8.1
7.5
20.2
1.8
183
-
-
-
21.1
-
-
-
-
871
-
164
-
2.2
-
AP
-
148
-
-
-
;
16.0
0.7
7.6
20.1
1.5
180
-
-
-
11.8
-
-
-
-
<25
-
1.9
-
1.2
-
TC
22.3
150
-
-
-
;
16.2
0.4
7.7
20.2
1.5
185
-
-
-
0.6
-
-
-
-
<25
-
0.4
-
1.1
-
07/14/09
IN
-
142
-
-
-
;
15.8
0.7
7.5
19.8
1.7
167
-
-
-
11.0
-
-
-
-
65
-
87.6
-
1.1
-
AP
-
144
-
-
-
;
15.8
0.3
7.7
19.8
1.7
157
-
-
-
9.6
-
-
-
-
<25
-
1.1
-
1.0
-
TC
22.7
140
-
-
-
;
16.2
0.3
7.7
20.0
2.0
151
-
-
-
0.3
-
-
-
-
<25
-
0.5
-
0.9
-
07/29/09
IN
-
138
<0.1
6.3
0.3
167
15.4
3.7
7.5
22.0
2.3
166
96.8
73.4
23.4
13.5
11.5
2.1
5.1
6.4
361
73
124
126
2.1
-
AP
-
140
<0.1
6.3
0.3
99.9
15.3
0.2
7.7
21.5
1.9
156
103
78.7
24.4
9.1
10.2
<0.1
<0.1
10.1
<25
<25
0.3
<0.1
1.5
-
TC
24.0
138
<0.1
6.6
0.3
28.4
15.8
0.5
7.7
21.0
1.6
152
102
77.9
24.3
<0.1
<0.1
<0.1
<0.1
<0.1
<25
<25
<0.1
<0.1
1.4
-
08/05/09""
IN
-
139
-
-
-
;
15.5
0.9
7.6
20.6
1.7
190
-
-
-
10.8
-
-
-
-
107
-
109
-
1.5
-
AP
-
141
-
-
-
;
15.3
0.2
7.7
21.0
1.8
182
-
-
-
8.8
-
-
-
-
<25
-
0.2
-
1.4
-
TC
24.4
139
-
-
-
;
15.7
0.3
7.7
22.3
1.9
177
-
-
-
<0.1
-
-
-
-
<25
-
<0.1
-
1.5
-
08/12/09
IN
-
142
-
-
-
;
15.2
1.6
7.5
20.3
2.0
199
-
-
-
11.6
-
-
-
-
78.4
-
90.2
-
1.5
-
AP
-
142
-
-
-
;
15.3
1.3
7.6
19.9
1.8
206
-
-
-
10.3
-
-
-
-
<25
-
1.0
-
1.3
-
TC
24.8
144
-
-
-
;
15.2
0.9
7.6
20.1
1.8
207
-
-
-
0.6
-
-
-
-
<25
-
0.1
-
1.3
-
(a) Bed volume and WQP from 06/30/09.
(b) Water quality parameters from 08/06/09.
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
|jg/L
Hfl/L
^g/L
Hg/L
Hfl/L
|jg/L
m/L
|jg/L
Hfl/L
^g/L
Hg/L
08/18/09
IN
-
145
-
-
-
;
15.1
5.2
7.5
19.2
1.8
190
-
-
-
14.8
-
-
-
-
367
-
111
-
1.5
-
AP
-
145
-
-
-
;
14.8
0.4
7.7
19.1
1.7
185
-
-
-
11.4
-
-
-
-
<25
-
3.2
-
1.1
-
TC
25.2
142
-
-
-
;
15.1
0.8
7.8
19.3
1.6
182
-
-
-
1.2
-
-
-
-
<25
-
2.2
-
1.2
-
08/26/09
IN
-
145
0.1
6.5
0.3
170
15.8
9.5
NA
20.1
2.0
203
110
90.3
19.8
15.3
12.5
2.8
7.4
5.1
590
96
140
105
-
2.3
-
AP
-
142
0.2
6.2
0.3
91.5
15.7
7.4
NA
20.4
1.7
202
114
93.9
20.4
11.4
10.8
0.6
0.5
10.3
63
59
0.4
<0.1
-
1.4
-
TC
25.6
147
0.2
6.3
0.3
64.2
16.0
2.2
NA
20.0
1.6
199
108
88.6
19.5
0.8
0.7
0.1
0.3
0.4
39
<25
0.6
<0.1
-
5.9
-
09/02/09 a|
IN
-
140
-
-
-
;
15.5
2.1
7.7
19.5
1.7
191
-
-
-
10.9
-
-
-
-
146
-
110
-
1.3
-
AP
-
138
-
-
-
;
15.6
1.4
7.7
19.5
1.5
193
-
-
-
9.0
-
-
-
-
<25
-
0.6
-
1.3
-
TC
26.4
138
-
-
-
;
15.6
0.1
7.8
19.9
1.8
190
-
-
-
<0.1
-
-
-
-
<25
-
<0.1
-
1.3
-
09/09/09""
IN
-
144
142
-
-
-
;
15.8
15.7
1.1
1.5
7.5
18.8
1.6
182
-
-
-
10.6
10.3
-
-
-
-
129
123
-
107
107
-
1.2
1.3
-
AP
-
142
144
-
-
-
;
15.8
15.5
0.7
0.8
7.6
18.9
1.6
170
-
-
-
8.8
8.7
-
-
-
-
<25
<25
-
0.1
0.2
-
1.2
1.2
-
TC
27.1
142
146
-
-
-
;
15.9
15.9
0.2
0.4
7.6
18.9
1.6
171
-
-
-
<0.1
<0.1
-
-
-
-
<25
<25
-
<0.1
<0.1
-
1.2
1.2
-
09/16/09|c|
IN
-
142
-
-
-
;
15.4
2.6
7.8
18.9
1.8
180
-
-
-
13.7
-
-
-
-
197
-
116
-
2.4
-
AP
-
146
-
-
-
;
14.0
0.2
7.8
19.0
1.6
174
-
-
-
11.1
-
-
-
-
<25
-
0.9
-
2.1
-
TC
27.7
144
-
-
-
;
15.2
2.5
7.9
19.1
1.7
167
-
-
-
0.9
-
-
-
-
<25
-
0.4
-
2.6
-
09/23/09
IN
-
138
<0.05
5.9
0.2
150
14.3
4.3
7.6
19.4
2.3
185
102
81.9
19.8
16.7
7.9
8.8
3.3
4.6
462
56
124
108
2.4
-
AP
-
138
<0.05
5.8
0.3
71.9
14.1
0.2
7.7
19.2
1.8
182
110
90.8
19.7
11.5
11.2
0.3
0.3
10.8
<25
<25
9.3
<0.1
1.8
-
TC
28.4
140
<0.05
5.9
0.3
28.3
14.3
1.3
7.7
19.2
1.9
181
111
90.5
20.7
1.0
1.0
<0.1
0.3
0.7
<25
<25
0.2
<0.1
4.9
-
09/30/09
IN
-
136
-
-
-
;
15.5
3.3
7.7
16.4
2.0
187
-
-
-
13.4
-
-
-
-
172
-
105
-
1.6
-
AP
-
129
-
-
-
;
15.5
0.8
7.7
16.8
1.9
181
-
-
-
11.0
-
-
-
-
<25
-
0.1
-
1.4
-
TC
29.0
140
-
-
-
;
15.8
1.1
7.5
16.9
2.2
231
-
-
-
1.0
-
-
-
-
<25
-
<0.1
-
1.3
-
(a) Water quality parameters measured on 09/01/09.
(b) Water quality parameters measured on 09/08/09.
(c) Water quality parameters measured on 09/15/09.
NA = not available
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
|jg/L
Hfl/L
Hfl/L
Hg/L
Mfl/L
^g/L
Hfl/L
|jg/L
Hfl/L
^g/L
|jg/L
10/07/09
IN
-
139
-
-
-
;
13.3
1.4
7.7
16.7
1.8
186
-
-
-
13.3
-
-
-
-
119
-
107
-
1.4
-
AP
-
141
-
-
-
;
14.7
0.6
7.6
16.9
1.9
229
-
-
-
11.9
-
-
-
-
<25
-
0.3
-
1.4
-
TC
29.6
135
-
-
-
;
14.8
0.5
7.8
19.0
1.7
226
-
-
-
0.8
-
-
-
-
<25
-
<0.1
-
1.9
-
10/14/09
IN
-
144
-
-
-
;
13.8
1.2
7.5
17.9
1.6
207
-
-
-
10.8
-
-
-
-
120
-
96.4
-
1.8
-
AP
-
144
-
-
-
;
13.9
0.3
7.6
18.0
1.6
201
-
-
-
9.8
-
-
-
-
<25
-
0.2
-
1.7
-
TC
30.3
142
-
-
-
;
14.0
0.7
7.8
18.0
2.8
199
-
-
-
<0.1
-
-
-
-
<25
-
<0.1
-
1.6
-
10/1 9/09 |a|
IN
-
140
<0.1
5.7
0.3
76.7
14.4
3.0
7.6
17.8
1.9
218
129
112
16.7
13.7
12.1
1.6
7.1
5.0
351
42
124
126
2.5
-
AP
-
142
<0.1
5.9
0.4
26
14.4
0.3
7.8
17.8
1.8
239
126
110
16.2
10.9
10.9
<0.1
1.0
9.8
<25
<25
<0.1
<0.1
2.0
-
TC
30.7
140
<0.1
5.8
0.3
<10
14.3
0.2
7.8
17.9
1.7
244
130
113
16.4
1.9
0.8
1.1
<0.1
0.7
<25
<25
<0.1
<0.1
2.8
-
10/28/09
IN
-
151
-
-
-
;
15.8
3.3
7.9
15.8
2.2
212
-
-
-
11.7
-
-
-
-
238
-
103
-
2.2
-
AP
-
145
-
-
-
;
16.0
4.2
7.8
16.1
1.8
207
-
-
-
9.7
-
-
-
-
<25
-
0.6
-
2.0
-
TC
31.6
135
-
-
-
;
15.9
3.8
7.8
15.9
1.9
206
-
-
-
0.9
-
-
-
-
<25
-
0.3
-
2.9
-
11/04/09
IN
-
142
-
-
-
;
14.9
1.3
7.5
17.0
2.0
225
-
-
-
9.4
-
-
-
-
141
-
107
-
2.0
-
AP
-
138
-
-
-
;
14.9
0.7
7.6
17.1
2.1
228
-
-
-
8.7
-
-
-
-
<25
-
0.5
-
1.9
-
TC
32.4
136
-
-
-
;
15.0
0.6
7.7
16.8
2.2
229
-
-
-
0.8
-
-
-
-
<25
-
0.2
-
1.9
-
11/18/09
IN
-
145
<0.1
5.7
0.3
56.6
15.9
1.9
7.4
13.3
2.7
222
120
100
20.0
11.7
10.5
1.2
4.7
5.8
219
79
95.2
83.3
1.7
-
AP
-
147
<0.1
5.7
0.3
18.7
15.7
0.9
7.9
13.6
2.2
208
122
102
19.9
9.8
9.7
<0.1
0.3
9.4
<25
<25
17.6
<0.1
1.4
-
TC
33.8
143
<0.1
5.7
0.3
<10
15.9
9.9
7.9
13.5
2.5
211
121
101
19.9
1.4
1.4
<0.1
0.3
1.1
28
<25
50.1
0.1
444
-
12/15/09
IN
-
144
<0.1
5.8
0.3
110
15.9
2.6
7.5
14.2
2.2
231
123
103
20.1
11.5
10.9
0.6
6.0
4.9
257
93
129
125
2.2
-
AP
-
129
<0.1
6.0
0.3
70.5
15.6
0.4
7.6
14.4
2.0
200
120
101
18.7
9.8
10.0
<0.1
0.2
9.8
<25
<25
0.6
0.2
2.8
-
TC
36.7
138
0.1
6.0
0.3
56.7
15.6
0.5
7.7
14.4
2.1
197
116
97.8
18.6
4.9
4.7
0.3
2.1
2.6
<25
<25
29.3
38.8
3.8
-
(a) Water quality parameters from 10/17/09.
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
|jg/L
Hfl/L
|jg/L
|jg/L
Mfl/L
^g/L
|jg/L
|jg/L
Hfl/L
^g/L
|jg/L
01/12/10
IN
-
145
<0.1
5.5
0.2
101
16.0
2.0
7.5
12.5
2.7
211
126
104
21.7
11.1
10.3
0.8
4.4
6.0
199
56
90.3
92.9
2.3
-
AP
-
149
<0.1
5.9
0.2
74.3
15.9
0.5
8.0
13.6
1.6
206.6
126
105
21.9
9.6
9.5
<0.1
0.4
9.1
<25
<25
2.2
0.1
2.2
-
TC
40.9
136
<0.1
6.0
0.3
60.6
15.2
0.4
8.1
14.1
2.4
209
126
105
20.9
3.0
2.6
0.3
0.4
2.2
<25
<25
4.4
0.3
137
-
02/10/10
IN
-
149
<0.1
6.2
0.2
105
15.8
2.1
8.0
15.0
2.1
209
112
92.6
19.6
11.9
12.1
<0.1
8.1
3.9
247
90
115
92.9
1.4
1.3
AP
-
153
<0.1
6.1
0.3
73.9
15.5
0.3
8.0
15.3
2.3
195
118
97.2
20.4
9.9
9.9
<0.1
0.4
9.5
<25
<25
4.1
0.1
1.2
1.2
TC
46.1
153
<0.1
6.4
0.3
65.1
15.6
0.4
8.0
15.8
2.4
192
117
97.1
20.3
3.5
3.5
<0.1
0.4
3.2
<25
<25
0.1
<0.1
1.3
1.4
02/23/10
IN
-
;
-
-
.
;
-
;
NA
NA
NA
NA
-
-
-
11.5
-
-
-
-
221
-
107
-
2.0
-
AP
-
;
-
-
.
;
-
;
NA
NA
NA
NA
-
-
-
9.8
-
-
-
-
<25
-
1.0
-
4.4
-
TC
-48.0
;
-
-
-
;
-
;
NA
NA
NA
NA
-
-
-
3.5
-
-
-
-
<25
-
<0.1
-
1.9
-
03/09/10
IN
-
148
<0.1
6.1
0.3
101
14.4
3.1
7.6
14.5
2.8
171
110
90.2
19.9
10.9
9.9
0.9
5.7
4.2
327
56
128
101
1.9
1.4
AP
-
151
<0.1
5.8
0.3
54.1
14.3
0.4
7.7
14.7
2.2
174
108
88.1
19.5
8.8
9.4
<0.1
0.3
9.2
<25
<25
0.2
<0.1
1.5
1.4
TC
49.2
153
<0.1
6.5
0.4
44.0
14.4
1.9
7.8
14.3
2.3
167
110
89.9
19.6
3.3
3.3
<0.1
0.1
3.2
<25
<25
0.2
<0.1
3.4
1.4
03/22/10
IN
-
;
-
-
.
;
-
;
NA
NA
NA
NA
-
-
-
10.6
-
-
-
-
214
-
113
-
2.1
-
AP
-
;
-
-
.
;
-
;
NA
NA
NA
NA
-
-
-
9.0
-
-
-
-
<25
-
1.4
-
1.7
-
TC
50.4
;
-
-
-
;
-
;
NA
NA
NA
NA
-
-
-
3.1
-
-
-
-
<25
-
<0.1
-
1.6
-
04/06/10
IN
-
149
<0.1
5.8
0.2
87.8
16.0
1.8
7.6
13.1
2.7
237
115
93.1
21.7
11.5
11.8
<0.1
6.8
5.0
171
83
116
123
1.6
1.3
AP
-
138
<0.1
6.2
0.3
58.3
16.0
0.1
7.8
13.1
2.4
193
119
95.4
23.5
10.1
9.9
0.2
0.2
9.6
<25
<25
0.2
0.1
1.3
1.2
TC
51.9
142
<0.1
6.2
0.3
39.7
16.0
0.2
8.0
13.4
2.0
169
116
93.2
22.4
3.7
3.8
<0.1
0.2
3.6
<25
<25
<0.1
<0.1
1.4
1.3
04/19/10
IN
-
;
-
-
.
;
-
;
NA
NA
NA
NA
-
-
-
12.4
-
-
-
-
193
-
116
-
1.8
-
AP
-
;
-
-
.
;
-
;
NA
NA
NA
NA
-
-
-
10.0
-
-
-
-
<25
-
0.2
-
1.7
-
TC
53.5
;
-
-
-
;
-
;
NA
NA
NA
NA
-
-
-
4.0
-
-
-
-
<25
-
<0.01
-
1.6
-
NA = not available
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
|jg/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
m/L
m/L
|jg/L
Mfl/L
Mfl/L
^g/L
Mfl/L
M9/L
|jg/L
|jg/L
Hg/L
05/05/10
IN
-
143
<0.1
6.3
0.3
96.0
15.4
1.5
7.6
16.6
2.3
209
104
84.8
19.3
11.6
10.8
0.8
5.3
5.5
156
37
92.2
92.5
1.2
0.9
AP
-
143
<0.1
6.3
0.3
72.3
15.5
0.4
7.9
17.0
1.7
179
108
87.8
20.1
11.4
11.0
0.4
0.1
10.9
<25
<25
0.3
0.1
1.1
1.0
TC
55.5
143
<0.1
6.3
0.3
58.6
15.3
0.5
8.0
16.9
2.3
187
106
85.7
20.3
4.1
3.9
0.1
0.1
3.8
<25
<25
0.4
0.2
1.1
1.0
05/17/10
IN
-
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
10.7
-
-
-
-
179
-
101
-
1.7
-
AP
-
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
9.4
-
-
-
-
<25
-
0.2
-
1.5
-
TC
56.7
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
4.0
-
-
-
-
<25
-
0.2
-
1.7
-
06/07/10
IN
-
152
<0.1
6.2
0.3
111
15.3
3.3
7.6
20.2
2.0
151
127
107
20.7
13.9
12.7
1.1
7.8
4.9
234
126
128
123
1.9
1.5
AP
-
143
<0.1
6.3
0.4
73.8
15.2
1.2
7.8
20.2
1.8
179
116
96.8
19.4
11.7
11.4
0.3
0.4
11.0
<25
<25
0.4
0.3
1.6
1.5
TC
58.8
161
<0.1
6.2
0.3
72.4
14.9
0.6
7.8
20.3
2.1
178
124
103
21.0
5.4
5.3
0.1
0.3
5.0
<25
<25
0.2
0.2
1.6
1.4
06/14/10
IN
-
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
12.9
-
-
-
-
224
-
117
-
1.8
-
AP
-
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
10.9
-
-
-
-
<25
-
0.3
-
1.5
-
TC
59.4
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
5.1
-
-
-
-
<25
-
0.2
-
2.6
-
06/30/10
IN
-
143
<0.1
6.3
0.3
99.7
15.1
1.7
7.5
19.9
1.8
241
114
94.6
19.3
12.3
12.1
0.2
6.7
5.4
197
73.5
113
107
1.6
1.2
AP
-
143
<0.1
6.4
0.3
70.0
15.1
0.4
7.7
19.6
1.7
235
112
92.9
19.0
10.0
10.8
<0.1
0.2
10.6
<25
<25
0.4
0.1
1.3
1.3
TC
60.8
138
<0.1
7.1
0.4
77.6
15.4
0.6
7.9
19.8
1.7
228
111
92.3
18.4
4.9
4.8
<0.1
0.2
4.6
<25
<25
37.0
<0.1
2.0
1.3
07/12/10
IN
-
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
17.1
-
-
-
-
828
-
286
-
2.2
-
AP
-
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
12.1
-
-
-
-
<25
-
28.5
-
6.1
-
TC
62.1
-
-
-
-
-
-
;
NA
NA
NA
NA
-
-
-
5.6
-
-
-
-
<
25.0
-
0.9
-
36.6
-
07/27/10
IN
-
146
<0.1
5.8
0.2
149
15.0
5.0
7.6
20.2
2.2
223
108
89.0
19.1
14.6
12.9
1.6
8.3
4.7
690
89
158
130
2.6
1.1
AP
-
137
<0.1
6.8
0.3
69.4
14.6
0.5
7.9
19.5
1.8
205
113
93.6
19.2
9.9
10.7
<0.1
0.2
10.5
<25
<25
0.4
0.1
1.2
1.1
TC
63.7
151
<0.1
6.2
0.2
60.3
14.6
0.8
7.9
20.1
1.6
221
111
92.2
18.6
4.9
5.2
<0.1
0.2
5.0
<25
<25
0.3
<0.1
5.8
1.0
NA = not available
-------
Table B-l. Analytical Data from Long-Term Sampling at Hot Springs Mobile Home Park in Willard, UT (Continued)
Cd
o
Sampling Date
Sampling Location
Parameter
Bed Volume
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Total Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
As (total)
As (soluble)
As (particulate)
As(lll)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Ti (soluble)
Unit
10J
mg/L
mg/L
mg/L
mg/L
m/L
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
|jg/L
|jg/L
ug/L
ug/L
ug/L
|jg/L
ug/L
ug/L
ug/L
ug/L
ug/L
08/16/10
IN
-
-
-
-
-
-
;
-
NA
NA
NA
NA
-
-
-
11.4
-
-
-
-
190
-
103
-
1.3
-
AP
-
-
-
-
-
-
;
-
NA
NA
NA
NA
-
-
-
9.9
-
-
-
-
<25
-
0.3
-
1.2
-
TC
66.0
-
-
-
-
-
;
-
NA
NA
NA
NA
-
-
-
5.3
-
-
-
-
<25
-
<0.1
-
2.0
-
09/07/10
IN
-
147
<0.1
6.2
0.3
108
17.4
1.6
7.6
18.9
2.0
209
110
83.0
26.6
12.5
11.9
0.5
6.9
5.0
205
80
110
105
1.6
1.4
AP
-
145
<0.1
6.3
0.3
81.4
17.1
0.7
7.8
18.6
2.0
196
103
78.0
25.4
10.9
11.2
<0.1
<0.1
11.1
<25
<25
3.3
<0.1
1.9
1.4
TC
68.3
142
<0.1
6.1
0.3
69.8
17.4
1.7
7.8
18.8
2.0
193
98.0
73.8
24.2
7.0
7.2
<0.1
<0.1
7.1
<25
<25
<0.1
<0.1
2.2
1.4
09/14/10
IN
-
-
-
-
-
-
;
-
NA
NA
NA
NA
-
-
-
14.3
-
-
-
-
188
-
120
-
1.7
-
AP
-
-
-
-
-
-
;
-
NA
NA
NA
NA
-
-
-
11.9
-
-
-
-
<25
-
0.6
-
1.4
-
TC
-69.2
-
-
-
-
-
;
-
NA
NA
NA
NA
-
-
-
6.2
-
-
-
-
<25
-
0.4
-
1.3
-
NA = not available
------- |