EPA/600/R-11/060
May 2011
Arsenic Removal from Drinking Water by Coagulation/Filtration
U.S. EPA Demonstration Project at Town of Arnaudville, LA
Final Performance Evaluation Report
by
Abraham S.C. Chen§
Wendy E. Conditf
Brian J. Yates1^
Lili Wang§
^attelle, Columbus, OH 43201-2693
§ALSA Tech, LLC, Powell, OH 43065-6938
Contract No. 68-C-00-185
Task Order No. 0029
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 0029 of Contract 68-C-00-185 to Battelle. It has been subjected to the Agency's
peer and administrative reviews and has been approved for publication as an EPA document. Any
opinions expressed in this paper are those of the author(s) and do not, necessarily, reflect the official
positions and policies of the EPA. Any mention of products or trade names does not constitute
recommendation for use by the EPA.
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FOREWORD
The 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
subsurface resources; protection of water quality in public water systems; remediation of contaminated
sites, sediments and ground water; 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 environmental problems by: developing and promoting technologies that protect and improve
the environment; advancing scientific and engineering information to support regulatory and policy
decisions; and providing the technical support and information transfer to ensure implementation of
environmental regulations and strategies at the national, state, and community levels.
This publication has been produced as part of the Laboratory's strategic long-term research plan. It is
published and made available by EPA's Office of Research and Development to assist the user
community and to link researchers with their clients.
Sally Gutierrez, Director
National Risk Management Research Laboratory
in
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ABSTRACT
This report documents the activities performed during and the results obtained from the arsenic removal
treatment technology demonstration project at the United Water Systems' facility in Arnaudville, LA.
The objectives of the project were to evaluate: (1) the effectiveness of Kinetico's FM-284-AS pressure
filtration system using Macrolite® media in removing arsenic to meet the maximum contaminant level
(MCL) of 10 ug/L, (2) the reliability of the treatment system for use at small water facilities, (3) the
required system operation and maintenance (O&M) and operator skill levels, and (4) the capital and
O&M cost of the technology. The project also characterized water in the distribution system and
residuals generated by the treatment process. The types of data collected included system operation,
water quality, process residuals, and capital and O&M cost.
Upon approval of the engineering plan by the Louisiana Department of Health and Hospitals (LADHH),
the treatment system was installed and became operational on June 23, 2006. The system consisted of a
5,000-gal contact tank (converted from a pre-existing aeralater) and two 84-in x 96-in steel pressure tanks
configured in parallel. Each pressure tank was loaded with 75 ft3 of Macrolite® media, a spherical, low
density, and chemically inert ceramic media, to which filtration rates up to 10 gpm/ft2 (at a design
flowrate of 770 gal/min [gpm]) might be applied (the actual flowrate was 335 gpm [on average]). Due to
the presence of ammonia (1.9 mg/L [as N]) and total organic carbon (TOC) (1.3 mg/L) in source water,
potassium permanganate (KMnO4) was selected as the oxidantto oxidize As(III) (24.4 ug/L [on average])
and Fe(II) (1,906 ug/L [on average]). After arsenic-laden iron solids had been removed by the pressure
filters, the treated water was softened, with 30% bypass, and chlorinated before entering the distribution
system.
Source water was supplied by two 10-in production wells, i.e., Wells No. 1 and No. 2, at 350 and 375
gpm, respectively. Quality of well water from both wells was similar, containing 24.1 to 43.0 ug/L of
arsenic (existing mostly as soluble As[III]), 1,477 to >3,000 ug/L of iron (existing almost entirely in the
soluble form), and 96.2 to 196 ug/L of manganese (also existing almost entirely in the soluble form).
Because the aeralater was used not only as a contact tank, but also for aeration (although unintentionally),
a number of operational and performance issues occurred during the performance evaluation study. After
approximately five months into system operation, extensive biofouling became evident, causing the filters
to be backwashed up to eight times per day (from one to two times per day after system startup).
Aeration in the aeralater, with an average dissolved oxygen (DO) level of 5.5 mg/L, apparently had
caused biological activities, including nitrification, to occur. To curb continuing biological activities in
the filters, several actions were taken, including performing a hydrochloric acid (HCl)/caustic wash of the
filter media, replacing KMnO4 with gas chlorine, and turning off the blower of the aeralator. Due to the
presence of elevated soluble As(V) in the filter influent/effluent, a system modification application
package was prepared and submitted to LADHH for supplemental iron addition. While the benefit of
supplemental iron usage was inconclusive, extra solids loading to the filters caused them to be
backwashed more frequently (from one to two times per day to two to three times per day). Iron addition
was discontinued after 19 months.
Although the ratio of soluble iron to soluble arsenic in source water was over 65 (on average) — a value
higher than the rule-of-thumb value of 20 — elevated soluble As(V) (close to or over 10 ug/L) continued
to be measured through the most of the 4-year study period. Factors affecting removal of soluble As(V)
in the filter influent might include elevated phosphorus levels (648 ug/L [on average]), elevated silica
levels (42.5 mg/L [as SiO2] [on average]), and elevated DO levels due to aeration in the aeralater.
Aeration continued even after shutting-down of the blower (DO levels reduced from 5.5 to 2.4-3.4 mg/L)
and removal of aluminum trays (DO levels further reduced to 2.4 mg/L). Aeration discontinued only after
IV
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the aeralater had been bypassed (DO levels further reduced to 0.5 mg/L). The presence of oxygen might
have caused some soluble iron to precipitate (even though KMnO4 or chlorine was added ahead of the
aeralater), rendering it ineffective to remove soluble As(V) via adsorption and/or co-precipitation. A
series of jar tests were conducted onsite to examine the authenticity of this postulation.
Results of distribution system water sampling before and after system startup indicated that the water
quality in the distribution system was comparable to that of the pressure filter effluent. Thus, the
treatment system appeared not to have beneficial effects on arsenic, iron, and manganese concentrations.
Arsenic concentrations remained essentially unchanged from baseline levels; iron and manganese
concentrations actually increased slightly. Alkalinity, pH, and lead concentrations also increased slightly.
Copper concentrations increased rather significantly from the average baseline level of 108 |o,g/L to
267 ng/L.
Analyses of backwash wastewater samples indicated that approximately 4.9 Ib of solids (including 0.01 Ib
of arsenic, 1.8 Ib of iron, and 0.08 Ib of manganese) would be disharged, assuming that 87.8 mg/L of total
suspended solids (TSS) and 6,752 gal of wastewater would be generated during each backwash event.
The capital investment for the treatment system was $427,407, including $281,048 for equipment,
$50,770 for site engineering, and $95,589 for installation, shakedown, and startup. Using the system's
rated capacity of 770 gpm (or 1,108,800 gal/day [gpd]), the capital cost was $555/gpm (or $0.38/gpd).
This calculation did not include the cost of the building to house the treatment system. O&M cost,
estimated at $0.07/1,000 gal, included only the incremental cost for chemicals, electricity, and labor.
Since chlorine addition already existed prior to the demonstration study, the incremental cost for chemical
usage was for iron addition only.
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CONTENTS
DISCLAIMER ii
FOREWORD iii
ABSTRACT iv
APPENDICES vii
FIGURES vii
TABLES viii
ABBREVIATIONS AND ACRONYMS x
ACKNOWLEDGMENTS xii
Section 1.0 INTRODUCTION 1
1.1 Background 1
1.2 Treatment Technologies for Arsenic Removal 2
1.3 Project Objectives 2
Section 2.0 SUMMARY AND CONCLUSIONS 5
Section 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 12
3.3.4 Distribution System Water 12
3.3.5 Residual Solids 12
3.4 Special Studies 12
3.4.1 Filter Run Length Studies 12
3.4.2 Jar Tests 13
3.4.2.1 Raw Water Collection 13
3.4.2.2 Jar Test Procedures 14
3.4.2.3 Aeralater Bypass 13
3.5 Sampling Logistics 14
3.5.1 Preparation of Arsenic Speciation Kits 14
3.5.2 Preparation of Sampling Coolers 15
3.5.3 Sample Shipping and Handling 15
3.6 Analytical Procedures 15
Section 4.0 RESULTS AND DISCUSSION 16
4.1 Site Description 16
4.1.1 Pre-existing Facility 16
4.1.2 Distribution System 19
4.1.3 Source Water Quality 19
4.2 Treatment Process Description 21
4.3 System Installation 28
4.3.1 Permitting 28
4.3.2 Building Construction 28
4.3.3 System Installation, Startup, and Shakedown 28
4.3.4 Iron Addition Modification 30
4.4 System Operation 32
VI
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4.4.1 Service Operation 37
4.4.2 KMnO4, Chlorine, and Iron Additions 42
4.4.3 Backwash Operation 43
4.4.3.1 PLC Settings 46
4.4.3.2 Acid and/or Caustic Washes 47
4.4.4 Residual Management 50
4.4.5 Reliability and Simplicity of Operation 50
4.4.5.1 Pre- and Post-Treatment Requirements 50
4.4.5.2 System Automation 51
4.4.5.3 Operator Skill Requirements 51
4.4.5.4 Preventative Maintenance Activities 51
4.5 System Performance 51
4.5.1 Treatment Plant Sampling 51
4.5.1.1 Arsenic 54
4.5.1.2 Iron 58
4.5.1.3 Manganese 61
4.5.1.4 pH, DO, andORP 63
4.5.1.5 Ammonia and Nitrate 64
4.5.1.6 Other Water Quality Parameters 64
4.5.2 Special Studies 64
4.5.2.1 Filter Run Length Studies 65
4.5.2.2 Aeralater Bypass Test 65
4.5.2.3 Jar Tests 67
4.5.2.4 Filter Run Length Study During January 2010 Site Visit 69
4.5.3 Backwash Wastewater Sampling 69
4.5.4 Distribution System Water Sampling 70
4.6 System Cost 70
4.6.1 Capital Cost 73
4.6.2 O&MCost 74
5.0 REFERENCES 75
APPENDICES
APPENDIX A: OPERATIONAL DATA A-l
APPENDIX B: ANALYTICAL DATA TABLES B-l
FIGURES
Figure 3-1. Process Flow Diagram and Sampling Schedule and Locations 11
Figure 4-1. Pre-existing Treatment Train 16
Figure 4-2. Pre-existing Aeralater 17
Figure 4-3. Pre-existing Water Softener 17
Figure 4-4. Pre-existing Storage Tank (center) with Hydropneumatic Tank at Its Side (left) 18
Figure 4-5. Pre-existing Hydropneumatic Tank 18
Figure 4-6. Pre-existing Transfer Pumps 19
Figure 4-7. Schematic of Kinetico's Macrolite® Arsenic Removal System 22
Figure 4-8. Intake Piping to Aeralater 24
Figure 4-9. Chemical Metering Pumps for KMnO4 Addition 24
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Figure 4-10. KMnO4 Injection Point at Wellhead 25
Figure 4-11. Chemical Storage Tanks and Secondary Containments 25
Figure 4-12. Macrolite Pressure Filters and Valve Rack 26
Figure 4-13. Backwash Wastewater Pond with Storage Tank in Background 27
Figure 4-14. New Building Constructed Adjacent to Pre-existing Aeralater 28
Figure 4-15. Off-Loading of Pipe Rack for Macrolite® Filtration System 29
Figure 4-16. Placement of Vessels and Pipe Rack on Concrete Pad Prior to Building
Construction 29
Figure 4-17. Completed Treatment Systems 30
Figure 4-18. Piping Bypassing Pre-existing Aeralater 33
Figure 4-19. Replacement Steel Pipe (Vertical Section on Right) After Pipe Break 33
Figure 4-20. Daily Run Time 37
Figure 4-21. Daily Demands During Study Period 39
Figure 4-22. System Flowrates 40
Figure 4-23. System Inlet/Outlet Pressure and Differential Pressure 41
Figure 4-24. Differential Pressure Across Macrolite® Pressure Filters 41
Figure 4-25. KMnO4 Dosages over Time 42
Figure 4-26. Backwash Frequency 44
Figure 4-27. Macrolite® Media After Backwash 48
Figure 4-28. Macrolite® Media After Being Soaked in 10%HC1 Solution 48
Figure 4-29. HCl-Soaked Media After Drying 49
Figure 4-30. Arsenic Speciation Results at IN, AC, and TT Sampling Locations 56
Figure 4-31. Total Arsenic Concentrations at IN, AC, TA, TB, and TT Sampling Locations 59
Figure 4-32. Soluble and Particulate Iron Across Treatment Train 59
Figure 4-33. Soluble and Particulate Manganese Concentrations Across Treatment Train 62
Figure 4-34. Ammonia Concentrations Across Treatment Train 65
Figure 4-35. Arsenic Speciation Results for Samples Collected During Jar Tests 68
Figure 4-36. Arsenic, Iron, and Manganese Breakthrough During Filter Run-length Study 70
TABLES
Table 1-1. Summary of the Arsenic Removal Demonstration Sites 3
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 Analyses 9
Table 3-4. Test Matrix for Run Length Studies 12
Table 3-5. Test Matrix for Determining Optimal Oxidant Doses 14
Table 3-6. Test Matrix for Arsenic and Iron Removal 14
Table 4-1. Source Water Quality Data 20
Table 4-2. Properties of 40/60 Mesh Macrolite® Media 22
Table 4-3. Design Features of Macrolite® System 23
Table 4-4. System Inspection Punch-List Items from August 9 to 11, 2006, Site Visit 31
Table 4-5. Key Events During Performance Evaluation Study at Arnaudville, LA 34
Table 4-6. Treatment System Operational Parameters 38
Table 4-7. Waste to Production Ratios for Macrolite® Pressure Filters 46
Table 4-8. Snapshots of PLC Backwash Settings 47
Table 4-9. Analytical Results (without Iron Addition) 52
Table 4-10. Analytical Results (with Iron Addition) 55
Table 4-11. Results of Samples Taken Before and After Aeralater Bypass 66
Table 4-12. Jar Test Results for Optimal Oxidant Doses 67
Vlll
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Table 4-13. Jar Test Results for Arsenic and Iron Removal 68
Table 4-14. Backwash Wastewater Sampling Test Results 71
Table 4-15. Distribution System Sampling Results 72
Table 4-16. Capital Investment for Kinetico's FM-284-AS System 73
Table 4-17. O&M Costs for Kinetico's FM-284-AS System 74
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ABBREVIATIONS AND ACRONYMS
Ap
AAL
Al
AM
As
ATS
differential pressure
American Analytical Laboratories
aluminum
adsorptive media
arsenic
Aquatic Treatment Systems
C/F coagulation/filtration
Ca calcium
Cl chlorine
CRF capital recovery factor
Cu copper
DBF Disinfection Byproducts
DI deionized
DO dissolved oxygen
EPA U.S. Environmental Protection Agency
F fluoride
Fe iron
FeQ3 ferric chloride
GFH granular ferric hydroxide
gpd gallons per day
gph gallons per hour
gpm gallons per minute
F£AA heloacetic acid
HIX hybrid ion exchanger
hp horsepower
ICP-MS inductively coupled plasma-mass spectrometry
ID identification
IX ion exchange
LADHH Louisiana Department of Health and Hospitals
LCR (EPA) Lead and Copper Rule
MCL maximum contaminant level
MDL method detection limit
MEI Magnesium Elektron, Inc.
Mg magnesium
jam micrometer
Mn manganese
mV millivolts
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Na sodium
NA not analyzed
NaOCl sodium hypochlorite
ND not detected
NRMRL National Risk Management Research Laboratory
NS not sampled
NSF NSF International
NTU nephelometric turbidity units
O&M operation and maintenance
OIP operator interface panel
OIT Oregon Institute of Technology
OPH Office of Public Health
ORD Office of Research and Development
ORP oxidation-reduction potential
P phosphorus
Pb lead
pCi/L picocuries per liter
psi pounds per square inch
psig pounds per square inch gauge
PLC programmable logic controller
PO4 phosphate
POU point-of-use
PVC polyvinyl chloride
QA quality assurance
QA/QC quality assurance/quality control
QAPP Quality Assurance Project Plan
RPD relative percent difference
RO reverse osmosis
Sb antimony
SDWA Safe Drinking Water Act
SiO2 silica
SMCL secondary maximum contaminant level
SO4 sulfate
STS Severn Trent Services
TDS total dissolved solids
THM trihalomethanes
TOC total organic carbon
TSS total suspended solids
UPS uninterruptible power supply
V vanadium
XI
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ACKNOWLEDGMENTS
The authors wish to extend their appreciation to United Water Systems in the Town of Arnaudville, LA
for its willingness to participate in this arsenic removal demonstration project. United Water Systems
provided manpower to collect samples from the treatment and distribution systems during the
performance evaluation study. United Water Systems also assisted in several onsite special studies.
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 |^g/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 in order to reduce compliance costs. As
part of this Arsenic Rule Implementation Research Program, EPA's Office of Research and Development
(ORD) proposed a project to conduct a series of full-scale, on-site demonstrations of arsenic removal
technologies, process modifications, and engineering approaches applicable to small systems. Shortly
thereafter, an announcement was published in the Federal Register requesting water utilities interested in
participating in 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 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, and the United Water Systems' facility in Arnaudville, LA was one of those selected.
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. Kinetico's Macrolite® arsenic removal technology was selected for
demonstration at the Arnaudville facility.
As of May 2011, all 40 systems were operational and the performance evaluation of 39 systems was
completed.
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1.2 Treatment Technologies for Arsenic Removal
The technologies selected for the Round 1 and Round 2 demonstration host sites included 25 adsorptive
media (AM) systems (the Oregon Institute of Technology [OIT] site has three AM systems), 13 coagula-
tion/filtration (C/F) systems, two ion exchange (IX) systems, 17 point-of-use (POU) units (including nine
under-the-sink reverse osmosis [RO] units at the Sunset Ranch Development site and eight POU-AM
units at the OIT site), and one system modification. Table 1-1 summarizes the locations, technologies,
vendors, system flowrates, and key source water quality parameters (including As, iron [Fe], and pH) at
the 40 demonstration sites. An overview of the technology selection and system design for the 12 Round
1 demonstration sites and the associated capital cost is provided in two EPA reports (Wang et al., 2004;
Chen et al., 2004), which are posted on the EPA Web site at
http: //www. epa. gov/ORD/NRMRL/wswrd/dw/arsenic/index.html.
1.3 Project Objectives
The objective of the arsenic demonstration program was to conduct full-scale arsenic treatment
technology demonstration studies on the removal of arsenic 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 Kinetico system at Arnaudville, LA from July 17, 2006,
through September 16, 2010. The types of data collected include system operation, water quality (both
across the treatment train and in the distribution system), residuals, and capital and preliminary O&M
cost.
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Table 1-1. Summary of Arsenic Removal Demonstration Sites
Demonstration
Location
Site Name
Technology (Media)
Vendor
Design
Flow rate
fepm)
Source Water Quality
As
(Mg/L)
Fe
(Mg/L)
PH
(S.U.)
Northeast/Ohio
Wales, ME
Bow,NH
Goffstown, NH
Rollinsford, NH
Dummerston, VT
Felton, DE
Stevensville, MD
Houghton, NY(d)
Buckeye Lake, OH
Springfield, OH
Springbrook Mobile Home Park
White Rock Water Company
Orchard Highlands Subdivision
Rollinsford Water and Sewer District
Charette Mobile Home Park
Town of Felton
Queen Anne's County
Town of Caneadea
Buckeye Lake Head Start Building
Chateau Estates Mobile Home Park
AM (A/I Complex)
AM(G2)
AM(E33)
AM(E33)
AM (A/I Complex)
C/F (Macrolite)
AM(E33)
C/F (Macrolite)
AM (ARM 200)
AM(E33)
ATS
ADI
AdEdge
AdEdge
ATS
Kinetico
STS
Kinetico
Kinetico
AdEdge
14
70(b)
10
100
22
375
300
550
10
250(e)
38W
39
33
36W
30
30W
19W
27W
15W
25W
<25
<25
<25
46
<25
48
270W
l,806(c)
1,312W
l,615(c)
8.6
7.7
6.9
8.2
7.9
8.2
7.3
7.6
7.6
7.3
Great Lakes/Interior Plains
Brown City, MI
Pentwater, MI
Sandusky, MI
Delavan, WI
Greenville, WI
Climax, MN
Sabin, MN
Sauk Centre, MN
Stewart, MN
Lidgerwood, ND
City of Brown City
Village of Pentwater
City of Sandusky
Vintage on the Ponds
Town of Greenville
City of Climax
City of Sabin
Big Sauk Lake Mobile Home Park
City of Stewart
City of Lidgerwood
AM(E33)
C/F (Macrolite)
C/F (Aeralater)
C/F (Macrolite)
C/F (Macrolite)
C/F (Macrolite)
C/F (Macrolite)
C/F (Macrolite)
C/F&AM(E33)
Process Modification
STS
Kinetico
Siemens
Kinetico
Kinetico
Kinetico
Kinetico
Kinetico
AdEdge
Kinetico
640
400
340(e)
40
375
140
250
20
250
250
14w
13W
16W
20W
17
39W
34
25W
42W
146W
127w
466W
l,387(c)
l,499(c)
7827(c)
546W
l,470(c)
3,078(c)
l,344(c)
1,325W
7.3
6.9
6.9
7.5
7.3
7.4
7.3
7.1
7.7
7.2
Midwest/Southwest
Amaudville, LA
Alvin, TX
Bruni, TX
Wellman, TX
Anthony, NM
Nambe Pueblo, NM
Taos, NM
Rimrock, AZ
Tohono O'odham
Nation, AZ
Valley Vista, AZ
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
Town of Taos
Arizona Water Company
Tohono O'odham Utility Authority
Arizona Water Company
C/F (Macrolite)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
AM(E33)
AM (AAFS50/ARM 200)
Kinetico
STS
AdEdge
AdEdge
STS
AdEdge
STS
AdEdge
AdEdge
Kinetico
770(e)
150
40
100
320
145
450
90(b)
50
37
35W
19w
56(a)
45
23(a)
33
14
50
32
41
2,068(c)
95
<25
<25
39
<25
59
170
<25
<25
7.0
7.8
8.0
7.7
7.7
8.5
9.5
7.2
8.2
7.8
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Table 1-1. Summary of Arsenic Removal Demonstration Sites (Continued)
Demonstration
Location
Site Name
Technology (Media)
Vendor
Design
Flow rate
fepm)
Source Water Quality
As
(ug/L)
Fe
(Mg/L)
PH
(S.U.)
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 Cffi-A
Golden Hills Community Service District
C/F (Macrolite)
IX (A300E)
POU RO(1)
C/F (Electromedia-I)
POE AM (Adsorbsia/ARM 200/ArsenXnp)
And POU AM (ARM 200)®
IX (Arsenex II)
AM (GFH/Kemiron)
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; C/F = coagulation/filtration; GFH = granular ferric hydroxide; HTX = hybrid ion exchanger; IX = ion exchange; 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% after system was switched from parallel to serial configuration.
(c) Iron existing mostly as Fe(II).
(d) Selected originally to replace Village of Lyman, NE site, which withdrew from program in June 2006; withdrew from program in 2007 and replace with a home system
in Lewisburg, OH.
(e) Facilities upgraded Springfield, OH system from 150 to 250 gpm, Sandusky, MI system from 210 to 340 gpm, and Amaudville, LA system from 385 to 770 gpm.
(f) Including nine residential units.
(g) Including eight under-the-sink units.
-------
2.0 SUMMARY AND CONCLUSIONS
Based on the information collected from operation of Kinetico's FM-286-AS pressure filtration system
using Macrolite® media at United Water Systems' facility in Arnaudville, LA from July 17, 2006, through
September 16, 2010, the following summary and conclusions are provided relating to the overall
objectives of the treatment technology demonstration study.
Performance of the arsenic removal technology for use on small systems:
• KMnO4 was effective in oxidizing soluble As(III) to soluble As(V) and soluble Fe(II) to iron
solids. Chlorine also was effective in oxidizing soluble As(III) and soluble Fe(II) even with
the presence of 1.9 mg/L of ammonia (as N) (on average).
• Unintentional aeration in the aeralater caused extensive biofouling in filter beds. An acid and
a caustic wash using 10% HC1 and 10% NaOH can restore the filter media. Biological
activities, including nitrification, can be controlled by minimizing aeration.
• Aeration in the aeralater apparently caused some soluble iron to precipitate, rendering it
ineffective in removing soluble As(V) via adsorption and/or co-precipitation. As a
consequence, elevated soluble As(V) levels (close to or over 10 |o,g/L) were measured in the
filter effluent during most of the 4-year study period, regardless of the choice of oxidants.
• Aeration can be eliminated by bypassing the aeralater. Without oxygen, soluble As(V) can
be reduced to <6 |o,g/L based on results of a series of jar tests.
• The effect of supplemental iron addition on arsenic removal was inconclusive, due, in part, to
operational issues, such as the use of an oversized pump and a corroding/dissolving
impeller/mixer. The use of supplemental iron added extra loading to the filters, thus
requiring more frequent backwash.
• Backwash can restore the filter media, but useful filter run lengths were short, averaging <4
hr (at an average filtration rate of 4.4 gpm/ft2). The backwash frequency went from once to
twice a day a few months into the study, to as many as eight times a day after the media was
fouled, to as many as 16 times a day when supplemental iron was added.
Required system O&M and operator skill levels:
• The daily demand on the operator was short, averaging 30 min for routine O&M. However,
the operator spent a significant amount of time assisting in troubleshooting system
operational issues (such as biofouling of filter media and corrosion/dissolution of mixing
equipment) and repairing the system (such as pipe breaks).
Characteristics of residuals produced by the technology:
• The amount of wastewater generated was equivalent to 5.5% of the water production, which
is much higher than that at other Macrolite® pressure filtration sites.
• Approximately 4.9 Ib of solids was produced during each backwash event, including 1.8 Ib of
iron, 0.08 Ib of manganese, and 0.01 Ib of arsenic.
-------
Capital and O&Mcost of the technology:
• The capital investment for the system was $427,407, including $281,048 for equipment,
$50,770 for site engineering, and $95,589 for installation, shakedown, and startup.
• The unit capital cost was $555/gpm (or $0.38/gpd) based on a 770-gpm design flowrate. This
calculation does not reflect the building cost as it was funded by United Water Systems.
• The O&M cost was $0.07/1,000 gal including incremental cost for KMnO4, electricity, and
labor.
-------
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 Kinetico treatment system began on July 17, 2006, and ended on September 16, 2010. Table 3-2
summarizes the types of data collected and considered as part of the technology evaluation process. The
overall system performance was based on its ability to consistently remove arsenic to below the target
MCL of 10 |og/L through the collection of water samples across the treatment train. The reliability of the
system was evaluated by tracking the unscheduled system downtime and frequency and extent of repair
and replacement. The unscheduled downtime and repair information were recorded by the plant operator
on a Repair and Maintenance Log Sheet.
The O&M and operator skill requirements were assessed through 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
water produced during each backwash cycle. Backwash wastewater was 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
cost for equipment, engineering, and installation, as well as the O&M cost for media replacement and
disposal, chemical supply, electricity usage, and labor.
Table 3-1. Predemonstration Study Activities and Completion Dates
Activity
Introductory Meeting Held
Project Planning Meeting Held
Final Letter of Understanding Issued
Request for Quotation Issued to Vendor
Vendor Quotation Received b Battelle
Purchase Order Completed and Signed
Engineering Plan Submitted to LADHH/OPH
System Permit Issued by LADHH/OPH
Pre-construction Meeting Held
Notice to Proceed Issued to Building Contractor
Treatment Equipment Arrived
System Installation Complete
System Start-up and Shakedown Completed
Performance Evaluation Begun
Final Study Plan Issued
Request for FeCl3 Addition Submitted to LADHH/OPH
Request Granted by LADHH/OPH
Date
November 3, 2004
March 2 1,2005
April 8, 2005
April 13, 2005
May 3, 2005
May 23, 2005
August 19, 2005
September 16, 2005
February 27, 2006
March 6, 2006
April 10, 2006
June 7, 2006
June 23, 2006
July 17, 2006
August 7, 2006
June 2 1,2007
August 8, 2007
LADHH = Louisiana Department of Health and Hospitals; OPH = Office of Public
Health
-------
Table 3-2. Evaluation Objectives and Supporting Data Collection Activities
Evaluation Objective
Performance
Reliability
System O&M and Operator
Skill Requirements
Residual Management
System Cost
Data Collection
-Ability to consistently meet 10 (og/L of arsenic in treated water
-Unscheduled system downtime
-Frequency and extent of repairs including a description of problems,
materials and supplies needed, and associated labor and cost
-Pre- and post-treatment requirements
-Level of automation for system operation and data collection
-Staffing requirements including number of operators and laborers
-Task analysis of 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
3.2
System O&M and Cost Data Collection
The plant operator performed daily, weekly, and/or monthly system O&M and data collection upon
Battelle's requests. On a daily basis, the plant operator recorded system operational data, such as
pressure, flowrate, totalizer, and hour meter readings on a Daily System Operation Log Sheet, checked
potassium permanganate (KMnO4), ferric chloride (FeCl3), and/or sodium hypochlorite (NaOCl) levels,
and conducted visual inspections to ensure normal system operations. If any problem 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 problem
encountered, course of actions taken, materials and supplies used, and associated cost and labor incurred,
on a Repair and Maintenance Log Sheet. To the extent possible, the plant operator measured several
water quality parameters onsite, including temperature, pH, dissolved oxygen (DO), oxidation-reduction
potential (ORP), and residual chlorine, and recorded them on an Onsite Water Quality Parameters Log
Sheet. Monthly backwash data also were recorded on a Backwash 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 chemical usage, electricity consumption, and
labor. Consumption of KMnO4, FeCl3, and/or NaOCl was tracked on the Daily System Operation Log
Sheet. Electricity consumption was determined from utility bills. Labor for various activities, such as
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, replenishing the chemical solutions, ordering supplies, 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 the cost analysis.
3.3
Sample Collection Procedures and Schedules
To evaluate system performance, water samples were collected at the wellhead, across the treatment
plant, during Macrolite® filter backwash, from the distribution system and during one hydrant flush event.
Table 3-3 presents the sampling schedule and analytes measured during each sampling event. In addition,
-------
Table 3-3. Sampling Schedule and Analyses
Sample
Type
Source Water
Treatment
Plant Water
(Regular)
Treatment
Plant Water
(Speciation)
Backwash
Wastewater
Residual
Solids
Distribution
Water
Sample
Locations'3'
IN
IN, AC,
TA, and TB
IN, AC, and
TT
BW
Backwash
Solids from
Each Tank
Three LCR
Residences
No. of
Samples
1
4
3
2
2
3
Frequency
Once
Varying
Varying
Varying
Once
Monthly(d)
Analytes
Onsite: pH, temperature,
DO, and ORP
Offsite: As(III), As(V),
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble),
U (total and soluble),
V (total and soluble),
Na, Ca, Mg, F, Cl, NO2,
NO3, NH3, SO4, SiO2,
PO4, TDS, TOC,
turbidity, and alkalinity
Onsite: pH, temperature,
DO, ORP, and/or total
Cl2(b)
Offsite: As (total),
Fe (total), Mn (total),
SiO2, P, turbidity, and
alkalinity
Onsite: pH, temperature,
DO, ORP, and/or total
C12(C)
Offsite: As(III), As(V),
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble),
Ca, Mg, F, NO3, NH3,
SO4, SiO2, P, TOC,
turbidity, and/or
alkalinity
pH, TSS, TDS,
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble)
Total Ag, As, Ba, Cd, Cr,
Hg, Pb, and Se
pH, alkalinity, As (total),
Fe (total), Mn (total), Pb,
andCu
Collection
Date
11/03/04
See Appendix B
See Appendix B
See Table 4-14
Not performed
See Table 4-15
(a) Abbreviations corresponding to sample locations in Figure 3-1, i.e., IN = at wellhead; AC = after
contact tank; TA = after Vessel A; TB = after Vessel B; TT = after Vessels A and B combined; BW:
at backwash discharge line; SS = sludge sampling location.
(b) At AC, TA, and/or TB only.
(c) At AC and/or TT only.
(d) Discontinued on 04/03/07.
-------
Figure 3-1 presents a flow diagram of the treatment system along with the analytes and schedule for each
sampling location. 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, 2004). The procedure for arsenic speciation is described in Appendix A of
the QAPP.
3.3.1 Source Water. During the initial site visit on November 3, 2004, one set of source water
samples from Wells 1 and 2 was collected and speciated using arsenic speciation kits (Section 3.4.1).
Before sampling, sample taps were flushed for several minutes; special care was taken to avoid agitation,
which might cause unwanted oxidation. The samples were analyzed for analytes listed in Table 3-3.
Arsenic speciation kits and containers for water quality samples were provided by Battelle and American
Analytical Laboratories (AAL), respectively. Sample containers for total organic carbon (TOC) were
provided by TCCI Laboratories, Inc.
3.3.2 Treatment Plant Water. The Battelle Study Plan (Battelle, 2006) called for the collection
of weekly treatment plant water samples on a four-week cycle. For the first week of each four-week
cycle, samples were collected at the wellhead (IN), after the contact tank (AC), and after Vessels A and B
combined (TT), speciated onsite, and analyzed for the analytes listed under "Treatment Plant Speciation
Sampling" in Table 3-3. For the next three weeks, samples were collected at IN, AC, after Vessel A
(TA), and after Vessel B (TB) and analyzed for the analytes listed under "Treatment Plant Regular
Sampling" in Table 3-3.
Due to various operational issues encountered during the performance evaluation study, speciation and
regular sampling were performed as scheduled only between August 10, 2006, through April 30, 2007
(except for five sampling events on November 28, 2006, December 19, 2006, January 1, 2007, February
21, 2007, and April 30, 2007, when biweekly samples were collected due to holidays and other logistic
issues). After April 30, 2007, sampling discontinued and resumed a number of times for the following
reasons:
• Poor system performance led the project team to believe that supplemental iron addition was
necessary to enhance soluble arsenic removal by the treatment system. Sampling
discontinued after April 30, 2007, to await the installation of an iron addition system.
Sampling resumed on January 23, 2008, with onsite speciation for arsenic, iron, and
manganese only. Five additional sampling events followed on January 28, March 11, March
19, March 24, and April 17, 2008. For the March 19 and March 24 samples, total phosphorus
also was analyzed.
• Irregularities on iron dosing occurred after implementation of iron addition. Sampling
discontinued after April 17, 2008 to await results of a run length study by the operator.
Despite the fact that irregular iron dosing continued, sampling with onsite speciation for
arsenic, iron and manganese resumed on November 18, 2008, and lasted until March 30,
2009. During this period, seven sampling events took place, with one each in November and
December 2008, two in January 2009, and three in March 2009.
• Upon conferring with the operator, it was determined that aeration in the aeralater in fact
continued. To minimize aeration, the operator agreed to remove aluminum trays in the
aeralater and cut the standpipe 4 ft below the high-level sensor in the aeralater. Meanwhile,
supplemental iron addition was suspended. Speciation sampling as noted in Table 3-3
resumed on August 18, 2009, and lasted until August 5, 2010. A total of 19 sampling events
took place, with one in August 2009, four each in September and October 2009, three in
November 2009, one in December 2009, three in January 2010, two in February 2010, and
one in August 2010.
10
-------
INFLUENT
(WELLS 1 AND 2)
Monthly
pHW temperature^), DOW,
As (total and soluble), As(III), As(V),
Fe (total and soluble), Mn (total and soluble),-
Ca, Mg, F, NO3, NH3, SO4, SiO2, P,
TOC, turbidity, and alkalinity
HW, temperature^), DOW, ORPW, total Cl2(a),
As (total and soluble), As(III), As(V),
Fe (total and soluble), Mn (total and soluble),-
Ca, Mg, F, NO3, NH3, SO4, SiO2, P,
TOC, turbidity, and alkalinity
Total Ag, As, Ba,
Cd, Cr, Hg, Pb, Se
pH, TSS, TDS,
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble)
Arnaudville, LA
Macrolite® Arsenic Removal System
Design Flow: 770 gpm
1
r
CONTACT TANK
pHW, temperature^, DO^,
-As (total), Fe (total), Mn (total),
SiO2, P, turbidity, and alkalinity
SANITARY
SEWER
A
e ^.—^
'-*• /BWJ
*
1
/FIL'
i
1
FER\
J
^ 1
/FIL1
pHW, temperature^, DO
^total Cl2(a), As (total), Fe (total),
"Mn (total), SiO2, P,
turbidity, and alkalinity
, temperature^, DO^,
total Cl2(a), As (total), Fe (total),
Mn (total), SiO2, P,
turbidity, and alkalinity
HW, temperature^, DOW, ORPW, total Cl2(a),
As (total and soluble), As(III), As(V),
Fe (total and soluble), Mn (total and soluble),"
Ca, Mg, F, NO3, NH3, SO4, SiO2, P,
TOC, turbidity, and alkalinity
Footnote
(a) Onsite analyses
\
T)
r
WATER SOFTENER
\
^ DA:C12
1
DISTRIBUTION
SYSTEM
J ' J
Water Sampling Locations
LEGEND
(JNJ At Wellhead
(AC) After Contact Tank
(lAj After Tank (A,B)
( TT J After Tanks A and B Combined
( BWJ Backwash Sampling Location
f SS J Sludge Sampling Location
INFLUENT Unit Process
DA: C12 Chlorine Disinfection
_ A -r--. f _ Potassium Permanganate
DA: KMnO, ^ . , . &
4 Oxidation
Figure 3-1. Process Flow Diagram and Sampling Schedule and Locations
11
-------
3.3.3 Backwash Wastewater. Monthly backwash wastewater samples were collected six times by
the plant operator between September 19, 2006, and March 25, 2007. Backwash wastewater samples
were collected by directing a portion of backwash wastewater at approximately 1 gpm to a clean, 32-gal
container over the duration of backwash for each vessel. This sidestream was produced via plastic tubing
connecting to a tap on the backwash wastewater discharge line. After the content in the container was
thoroughly mixed, composite samples were collected and/or filtered onsite with 0.45-(im disc filters.
Analytes for the backwash wastewater samples are listed in Table 3-3.
3.3.4 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, arsenic, lead, and copper levels. Prior to system startup from August 2005 to January 2006,
four monthly baseline distribution system water samples were collected from three residences within the
town's historic Lead and Copper Rule (LCR) sampling network. Following system startup, distribution
system water sampling began in September 2006 and ended in April 2007 on a monthly basis at the same
three locations.
Homeowners collected samples following an instruction sheet developed according to the Lead and
Copper Monitoring and Reporting Guidance for Public Water Systems (EPA, 2002). The dates and times
of last water usage before sampling and of actual sample collection were recorded for determination of
the stagnation time. Except for one on November 30, 2005, all samples were collected from a cold-water
faucet that had not been used for at least 6 hr to ensure that stagnant water was sampled.
3.3.5 Residual Solids. Residual solids produced consisted of only backwash wastewater solids.
Per the Battelle Study Plan, solid samples would be collected on two occasions after solids in backwash
wastewater had settled (in a 32-gal container) and supernatant had been carefully decanted. A portion of
each of the solids/water mixtures would then be air-dried for metals analyses. Residual solid sampling
was planned but never actually performed during the performance evaluation study.
3.4
Special Studies
Due to on-going problems with system performance, several special studies were conducted to examine
possible causes and solutions to improve performance. The studies performed included several filter run
length studies and a series of jar tests.
3.4.1 Filter Run Length Studies. Filter run length studies were conducted by collecting a series
of effluent samples from one or both pressure filters to determine useful run lengths between two
consecutive backwash events. Filtered (with 0.45 um disc filters) and unfiltered samples collected at
predetermined time intervals were analyzed for total and soluble metals and/or some or all of the other
analytes listed in Table 3-4.
Table 3-4. Test Matrix for Run Length Studies
a
OJ O
t'l
C« 0
C/3 — 1
IN
AC
TA/TB
a S
Filter Ru
Length (1
0
0
X
M
8.
X
X
X
£
-^-1
Tempera
X
X
X
o
0
X
X
X
o
X
X
X
Total
Chlorine
X
X
X
aj
Is
ll
X
X
X
Q> -Q
3 a
£ £
X
X
X
hH
hH
X
X
s
X
X
PA
Ammoni
X
X
1
X
X
U
g
X
X
12
-------
3.4.2 Jar Tests. A series of jar tests were conducted from January 18 to 22, 2010, to determine (1)
the most effective oxidant, (2) a proper dosage, and (3) arsenic and iron removal using select doses of
oxidants. During system startup and until March 29, 2007, KMnO4 had been used for oxidizing arsenic,
iron, and manganese. Although effective, concerns about biofouling of the filter media prompted the use
of chlorine. Residual chlorine levels in system effluent (or influent to the softening unit) had to be kept
below 1.0 mg/L (as C12) because the synthetic zeolite in the softening unit might be sensitive to chlorine.
The first part of the jar tests used three doses of NaOCl and three doses of KMnO4 to gain information
about an optimal dosage for each oxidant. One dose of NaOCl and all three doses of KMnO4 were then
used to examine their effectiveness in treating arsenic, iron, and manganese in source water. Due to the
presence of ammonia in source water, NaOCl would react with ammonia to form chloramines, which
would reduce oxidation kinetics. Breakpoint chlorination could not be used because it would result in
unacceptably high chemical use. When using KMnO4, colloidal MnO2 particles might form due to the
presence of TOC in source water; colloidal particles might not be removed by the filter media (Pellitier,
2010). Additional KMnO4 might be added to "offset" effects exerted by TOC, based on observations
made during studies at arsenic demonstration sites such as Sauk Centre, MN (Shiao et al., 2009) and
Waynesville, IL (Chen et al., 2011; 2010c). Specific procedures developed for the jar tests are described
below.
3.4.2.1 Raw Water Collection. Raw water was collected from the wellhead sample tap in a manner
that minimized oxidation of source water and preserved its in-well characteristics throughout its use.
After turning off the gas chlorine addition valve and thoroughly flushing the sample tap for at least 15
min, raw water was filled into a 2.5-gal partially opaque jug at a low flowrate from the bottom using
Tygon® tubing. Once the jug was filled, it was allowed to overflow to remove layers of potentially
oxidized water. Thus, potential oxidation of raw water was diffusion-limited to a small layer near the
air/water interface within the jug and relatively far away from the sample tap located near the bottom of
the jug. The last 1 gal of water from the jug was not used for the studies. pH, DO, ORP, and temperature
were measured directly from the bottom of the overflowing jug.
In addition to the sample tap, the jug also was equipped with a small hole on its top to provide pressure
during sampling. When the sampling tap was not open, the hole was covered with a piece of tape to
reduce air intrusion. The water just below the interface was periodically observed during the experiment
for signs of oxidation (light attenuation and scattering caused by the precipitation of oxidized metals);
however, this proved difficult, since the sample jug was partially opaque. No signs of significant
oxidation were noted during the study, although a slight yellow hue was noted in the jug approximately
60 min after collection. Water with an appreciably noticeable yellow hue was disposed of and fresh raw
water was used in its place.
3.4.2.2 Jar Test Procedures. The jar tests were carried out using raw water collected as described in
Section 3.4.2.1. 1-L amber glass jars were spiked with appropriate amounts of an oxidant and then filled
with raw water from the 2.5-gal jug. The actual oxidant dose was determined by spiking 1-L amber jars
filled with deionized (DI) water and measuring respective oxidant concentrations. Care was taken to
minimize agitation when filling the jars. The jars were mixed by inverting them with the aid of stainless
steel weights added prior to raw water addition.
To determine an appropriate contact time, a simple calculation was made using the contact tank volume
and average flowrate to the contact tank; the ratio of these provided the hydraulic detention time within
the contact tank. The contact time within the tank was found to be about 20 min; therefore, a 20-min
contact time was used for all jar tests.
13
-------
After the 20-min contact time, contents in some 1-L jars were measured for residual chlorine or KMnO4
to determine optimal doses (see Table 3-5). For arsenic and iron removal, an extended suite of analytes,
including metal speciation, ammonia, TOC, pH, temperature, DO, and ORP also were analyzed (see
Table 3-6). The order of the sampling/measurements (as presented herein) was important to ensure that
minimal oxygen dissolution occurred while the 1-L jars were open to the atmosphere. All samples were
taken with a sterile 25-mL pipette from the bottom of the jars.
Table 3-5. Test Matrix for Determining Optimal Oxidant Doses
Oxidant
NaOCl
KMnO4
0)
2 S g
0 >§ o
0.0
2.2
4.2
7.1
0.0
1.9
4.2
6.6
Reaction
Time (min)
20
20
20
20
20
20
20
20
Total
Chlorine
X
X
X
X
o
=
X
X
X
X
Table 3-6. Test Matrix for Arsenic and Iron Removal
•^
sS
2
'H
o
None
NaOCl
KMnO4
0)
** LJ ' "*
'H =B .
0
2.2
1.9
4.2
6.6
^~>
Reaction
Time (mir
-
20
20
20
20
M
X
X
X
X
X
0)
•_
s
Temperat
X
X
X
X
X
O
X
X
X
X
X
o
X
X
X
X
X
Total
Chlorine
X
X
-
-
-
o
X
-
X
X
X
-------
3.5.2 Preparation of Sample 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, colored-coded label consisting of the 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 the demonstration site, the 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 were separated by sampling location, placed in zip-lock bags, and packed into 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 sam-
pling event.
3.5.3 Sample Shipping and Handling. After sample collection, samples for offsite analyses were
packed carefully in the original coolers with wet ice and shipped back 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 metal analyses were stored at Battelle's inductively coupled plasma-mass spectrometry (ICP-
MS) laboratory. Samples for other water quality analyses were packed in separate coolers and picked up
by couriers from AAL in Columbus, OH and TCCI Laboratories in New Lexington, OH, which were both
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.
3.6 Analytical Procedures
The analytical procedures described in Section 4.0 of the QAPP (Battelle, 2004) were followed by
Battelle's ICP-MS laboratory, AAL, and TCCI Laboratories, and Belmont Labs. 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
handheld field meter, which was calibrated for pH and DO prior to use following the procedures provided
in the user's manual. The ORP probe also was checked for accuracy by measuring the ORP of a standard
solution and comparing it to the expected value. The plant operator collected a water sample in a clean,
plastic beaker and placed the probe in the beaker until a stable value was obtained. The plant operator
also performed free and total chlorine measurements using Hach chlorine test kits following the user's
manual.
15
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4.0 RESULTS AND DISCUSSION
4.1
Site Description
4.1.1 Pre-existing Facility. Located at 1004 Twin Oaks Drive in Arnaudville, LA, United Water
Systems Treatment System served approximately 1,200 service connections in rural areas of Arnaudville,
Cecilia, Breaux Bridge, and Bayou Portage in St. Landry and St. Martin Parishes. The system was
supplied by two 10-in production wells, i.e., Wells No. 1 and No. 2, drilled to a depth of approximately
560 ft. Each well was equipped with a 15 -horsepower (hp) submersible pump rated for 350 or 375 gpm
against a 90-lb/in2 (psi) head. Prior to the demonstration project, the wells alternated with each well
operating approximately four times per day for a total daily operating time of 15 to 23 hr. The typical
daily water usage was between 280,000 to 380,000 gpd with an estimated peak daily demand of 400,000
The pre-existing treatment system consisted of aeration, prechlorination, sand filtration, softening, post-
chlorination, and zinc orthophosphate addition (Figure 4-1). Aeration was performed at the top section of
an 1 1-ft diameter aeralater (Figure 4-2) to oxidize soluble iron. Chlorine addition occurred within the
aeralater to achieve further oxidation. The chlorinated water passed through a gravity filter within the
aeralater and to a separate pressure filter to remove precipitated iron particles. Seventy percent of the
water from the pressure filter was then treated by a synthetic zeolite water softener for hardness removal
(Figure 4-3). The other 30% bypassed the softener and was blended with the softened water before post-
chlorination and storage onsite in a 127,000-gal storage tank (Figure 4-4). Treated water in the storage
tank was transferred to a 10,000-gal hydropneumatic tank (Figure 4-5) before entering the distribution
system.
System piping and flow path/control were arranged so that raw water was fed from one of the two wells
into a manifold and a 6-in standpipe leading toward the top of the aeralater. The well pumps were
UNITED WATER SYSTEM, INC
Figure 4-1. Pre-existing Treatment Train
16
-------
Figure 4-2. Pre-existing Aeralater
Figure 4-3. Pre-existing Water Softener
17
-------
Figure 4-4. Pre-existing Storage Tank (center) with Hydropneumatic Tank at Its Side (left)
Figure 4-5. Pre-existing Hydropneumatic Tank
18
-------
controlled by a set of high- and low-level sensors within the top section of the aeralater. Water
discharged from the standpipe splashed downward through a series of aluminum trays where air was
forced from a blower to aerate the water. After passing the gravity filter within the aeralater, water was
pumped by two transfer pumps (Figure 4-6) to the pressure filter and water softener before entering the
127,000-gal storage tank. The transfer pumps were controlled by a set of high- and low-level sensors in
the storage tank. Treated water in the storage tank was transferred by two high service pumps to a
10,000-gal hydropneumatic tank before entering the distribution system. A pair of high- and low-level
sensors in the hydropneumatic tank controlled the flow from the storage tank to the hydropneumatic tank.
Figure 4-6. Pre-existing Transfer Pumps
For the arsenic removal technology demonstration, the pre-existing aeralater was used as a contact tank
(instead of an aerator and a gravity filtration unit) and two Macrolite® pressure filters were installed to
replace the pre-existing pressure filter. Other pre-existing system components and piping and flow
path/control arrangements remained mostly unchanged.
4.1.2 Distribution System. The distribution system was a closed looped distribution line supplied
via the 127,000-gal storage tank by Wells No. 1 and No. 2. The distribution line was constructed of 2-in
to 6-in Schedule 40 and Class 160 polyvinyl chloride (PVC) piping. United Water Systems sampled daily
for chlorine residuals, monthly for bacterial analysis, and once every three years at 10 residences under
the LCR. The facility also performed regular sampling for volatile organic compounds (VOCs), metals,
and pesticides approximately once every three years or as directed by the LADFiFi/OPH.
4.1.3 Source Water Quality. Source water samples from Wells No. 1 and No. 2 were collected
and speciated by Battelle on November 3, 2004. Analytical results from the source-water sampling are
presented in Table 4-1 and compared to those taken by the facility, Kinetico, and the Louisiana
Department of Health and Hospitals/Office of Public Health (LDHH/OPH).
19
-------
Table 4-1. Source Water Quality Data
Parameter
Unit
Date
PH
Temperature
DO
ORP
Total Alkalinity^
Hardness^
Turbidity
TDS
TOC
Nitrate (as N)
Nitrite (as N)
Ammonia (as N)
Chloride
Fluoride
Sulfate
Silica (as SiO2)
Orthophosphate
As (total)
As (soluble)
As (particulate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
U (total)
U (soluble)
V (total)
V (soluble)
Pb (total)
Cu (total)
Na (total)
Ca (total)
Mg (total)
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
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
mg/L
mg/L
mg/L
Facility
Data
Well
No. 1
-
7.3
NA
NA
NA
309
NA
NA
NA
NA
NA
NA
NA
42.0
NA
0.3
NA
NA
18.0
NA
NA
NA
NA
1,840
NA
110
NA
NA
NA
NA
NA
NA
NA
27.0
NA
NA
Well
No. 2
-
7.2
NA
NA
NA
315
NA
NA
NA
NA
NA
NA
NA
6.0
NA
0.6
NA
NA
24.0
NA
NA
NA
NA
1,630
NA
100
NA
NA
NA
NA
NA
NA
NA
15.0
NA
NA
Dist.
System
-
NA
NA
NA
NA
NA
42
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
19.0
NA
NA
NA
NA
70
NA
NA
NA
NA
NA
NA
NA
NA
NA
113.0
NA
NA
Kinetico
Data
Well
-
7.0
NA
NA
NA
312
290
NA
NA
NA
NA
NA
NA
43.3
0.4
<4.0
44.9
0.8
22.0
NA
NA
NA
NA
2,520
NA
140
NA
NA
NA
NA
NA
NA
NA
33.0
78.5
23
Battelle
Data
Well
No. 1
Well
No. 2
11/03/04
7.0
21.1
0.4
-105
308
316
25.0
392
2.1
O.04
O.01
1.9
37.0
0.1
<1.0
41.0
0.06
33.6
33.1
0.5
32.8
0.3
2,136
2,140
133
133
0.1
O.I
1.7
0.6
NA
NA
41.7
78.5
29.0
7.0
20.7
0.7
-101
308
294
20.0
336
1.5
O.04
O.01
1.8
11.0
O.I
<1.0
42.4
0.06
35.9
35.8
0.1
34.6
1.2
1,999
2,004
120
125
O.I
O.I
0.5
0.7
NA
NA
25.0
73.0
27.1
LDHH/OPH
Data
Well
No. 1
Well
No. 2
Dist.
System
04/26/99-07/07/03
7.1-7.3
NA
NA
NA
298-305
173-243
0.6-3.2
396^16
NA
O.014
NA
NA
30.7-53.2
0.1-0.2
O.014
NA
NA
17.0-33.0
NA
NA
NA
NA
2,020-2,530
NA
120-150
NA
NA
NA
NA
NA
NA
<5
3.6-36.9
NA
NA
7.0
NA
NA
NA
302-313
170-224
3.1-7.0
354-364
NA
O.014
NA
NA
4.2-9.0
0.2
O.014
NA
NA
25.0-37.0
NA
NA
NA
NA
1,910-2,240
NA
120-140
NA
NA
NA
NA
NA
NA
<5
0.5-23.1
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
-------
should be at least 20 times the soluble arsenic concentration for effective arsenic removal via adsorption
and co-precipitation with iron solids (Sorg, 2002). Based on the data shown in Table 4-1, natural soluble
iron levels were approximately 60 times the soluble arsenic levels in source water, indicating that there
would be no need to supplement the natural iron levels for effective arsenic removal.
Manganese. Total manganese levels in source water ranged from 100 to 150 (ig/L, which exceeded the
50-(ig/L SMCL for manganese. Of the total manganese present in source water, all of it was in the
soluble form, owing to the reducing nature of the source water.
Ammonia. Ammonia concentrations measured in source water ranged from 1.8 to 1.9 mg/L (as N). Due
to the presence of ammonia and TOC in source water, Kinetico proposed the use of KMnO4 to oxidize
soluble As(III) to soluble As(V) rather than NaOCl. NaOCl is known to react with ammonia to form
chloramines, which is not very effective in oxidizing soluble As(III) (Chen et al., 2009; Ghurye and
Clifford, 2001). NaOCl also is known to react with TOC to form disinfection byproducts (DBFs), such as
trihalomethanes (THMs) and haloacetic acids (HAAS). However, chloramines most likely will not react
with TOC to form DBFs (Bougeard et al, 2010; Amy et al., 1984).
Competing Anions. Silica and phosphate may compete with arsenic for available adsorption sites on
iron solids. Silica also may lower the point of zero charge of precipitated iron particles and/or form
networks with other adsorbed anions of the same species (Smith and Edwards, 2005; Meng, 2000; Meng,
2002). Typically, silica at levels greater than 40 mg/L and phosphate at levels greater than 1 mg/L may
impact arsenic adsorption onto iron particles or iron-based adsorption media. Silica levels in source water
were high, ranging from 41.0 mg/1 to 44.9 mg/L. Orthophosphate levels in the source water collected by
Battelle were less than its MDL of 0.06 mg/L (as PO4). However, the data collected by Kinetico showed
orthophosphate at 0.8 mg/L (as PO4). Orthophosphate levels were monitored over the course of the
demonstration study to determine if they were significant enough to have an effect on the arsenic removal
process.
Other Water Quality Parameters. pH values of source water samples ranged between 7.0 and 7.3. DO
levels were low at 0.4 to 0.7 mg/L and ORP readings ranged from -101 mV to -105 mV, suggesting
reducing conditions for the well water, which explained the metals speciation results. Source water had
high alkalinity and hardness, which measured between 298 and 313 mg/L and between 173 and 316
mg/L, respectively. Total dissolved solids (TDS) levels ranged from 336 to 416 mg/L. Fluoride
concentrations ranged from <0.1 to 0.4 mg/L, well below the MCL of 4 mg/L. Chloride, nitrate, and
nitrite were all below their respective SMCLs. Source water also was sampled by the LDHH/OPH for
antimony, barium, beryllium, cadmium, chromium, mercury, nickel, selenium, silver, thallium, and zinc.
Concentrations of these metals were all below their respective MCLs or SMCLs, and were typically less
than their MDLs.
4.2 Treatment Process Description
The treatment process at Arnaudville, LA consisted of oxidation of soluble As(III) and soluble Fe(II)
using KMnO4, adsorption/coprecipitation of soluble As(V) onto/with iron solids, and Macrolite® pressure
filtration to remove arsenic-laden particles. The pre-existing aeralater was "emptied" and used as a
contact tank in front of the Macrolite® pressure filters. (Because the aeration feature of the aeralater was
not completely removed and because of repeated miscommunications between the operator and the
project team concerning this fact, the aeralater continued to be used as an aerator during most of the
performance evaluation study. As a result, the system failed to consistently remove arsenic to less than
the 10-(ig/L MCL despite repeated attempts to troubleshoot this during the study period.) The pre-
existing pressure filter (120-in x 92-in) was emptied and converted to a softener after the Macrolite®
filters.
21
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Macrolite®, a ceramic media manufactured by Kinetico, was approved for use in drinking water
applications under NSF International (NSF) Standard 61. The spherical, low density and chemically inert
media were designed to allow for filtration rates up to 10 gpm/ft2. The physical properties of the media
are summarized in Table 4-2.
Table 4-2. Properties of 40/60 Mesh Macrolite® Media
Property
Color
Sphere Size Range (mm)
Bulk Density (g/mL)
Specific Gravity
Collapse Strength (for 30/50 mesh) (psi)
Value
Variable
23-36
0.86
2.05
7,000 to 8,000
Figure 4-7 is a schematic of the installed Macrolite® FM-284-AS arsenic removal system. The treatment
system consisted of two chemical feed systems for KMnO4 addition at both wellheads, a pre-existing
aeralater to provide contact time, two pressure vessels with hub and lateral stainless steel underdrains, and
associated instrumentation. The treatment system also was equipped with a central control panel that
housed a touch screen operator interface panel (OIP), a programmable logic controller (PLC), a modem,
and an uninterruptible power supply (UPS). The control panel was connected to various instruments used
to track system performance including inlet and outlet pressure for each filter, system flowrate, and
backwash flowrate and turbidity. All plumbing for the system was schedule 80 PVC and the skidded
units were pre-plumbed with the necessary isolation valves, check valves, sampling ports, and other
features. A 15-hp, 120-gal air compressor was provided with the system for air sparging of the media
during the backwash cycle. Table 4-3 specifies the key system design parameters of the treatment system.
Kinetico FM-284-AS Arsenic Removal System
I
FeedWater
atSO-tOOpsi
Existing
and
Modified
Equipment
ackuuash Waste
to _agoon
^
n
To Existing SpJit Stream
Softening System
Figure 4-7. Schematic of Kinetico's Macrolite® Arsenic Removal System
22
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Table 4-3. Design Features of Macrolite® System
Parameter
KMnO4 dosage (mg/L)
Value
2.6
Remarks
-
Contact
No. of Vessel
Vessel Size (ft)
Contact Time (min)
1
HDx7H
6.5
-
5,000 gal capacity
-
Filtration
No. of Vessels
Configuration
Vessel Size (in)
Vessel Cross-sectional Area (ft2)
Media Volume (ft3/vessel)
Hydraulic Loading Rate (gpm/ft2)
2
Parallel
84 D x 96 H
38.5
75
10
-
-
-
-
24-in bed depth of Macrolite®
385 gpm/vessel
Backwash
Pressure Drop (psi)
Initiating Pressure (psi)
Initiating Standby Time (hr)
Initiating Service Time (hr)
Hydraulic Loading Rate (gpm/ft2)
Duration (min/vessel)
Turbidity Set point (NTU)
Wastewater Production (gpd)
10-12(a)
20(a)
48(a)
24(a)
8-10
Variable(a)
20(a)
Variable(a)
Across a clean bed
Across bed at end of filter run
-
-
308 to 385 gpm/vessel
Based on minimum and maximum
backwash time, pressure and turbidity
setpoints
To terminate backwash
Based on PLC set points shown above
Design Specifications
Peak Flowrate (gpm)
Maximum Daily Production (gpd)
Hydraulic Utilization (%)
770
1,108,800
36%
-
Based on peak flow, 24 hr/day
Estimate based on maximum
demand(b)
(a) Initial expected values of PLC.
(b) Based on a peak daily demand of 400,000 gpd.
The treatment technology includes the following major process steps and system components:
• Intake - Raw water was pumped from both Wells No. 1 and No. 2 to provide a design
flowrate of 770 gpm against a 90-psi head. After combined, raw water from both wells flow
through a 6-in intake pipe (see Figure 4-8) to a 6-in standpipe inside the aeralater.
• Oxidation - Two KMnO4 feed systems were used to oxidize soluble As(III) to soluble As(V)
and soluble Fe(II) to Fe(III) solids. Prior to the study, the KMnO4 demand was estimated to
be 2.6 mg/L, which was delivered by one 0.42-gal/hr (gph) LMI (A171-155S) and one 0.58-
gph LMI (P141-352SI) metering pumps (Figure 4-9) to Wells No. 1 and No. 2 wellheads (see
an injection point at wellhead in Figure 4-10). Each chemical feed system also included an
impeller/mixer and a 66-gal polyethylene storage tank in a secondary containment (Figure 4-
11). KMnO4 was selected because of the elevated ammonia levels (up to 2 mg/L), which
were expected to form chloramines upon chlorine addition. Chloramines would result in
incomplete oxidation of soluble As(III) to soluble As(V). KMnO4 system operations were
tracked by measuring KMnO4 consumption in the storage tank.
23
-------
Figure 4-8. Intake Piping to Aeralater
Figure 4-9. Chemical Metering Pumps for KMnO4 Addition
24
-------
.
Figure 4-10. KMnO4 Injection Point at Wellhead
Figure 4-11. Chemical Storage Tanks and Secondary Containments
Retention - After KMnO4 addition, water flowed through the 6-in standpipe before being
discharged at the top of the aeralater. The original system design called for the use of the
aeralater as a contact tank (not as an aeration unit), which, with its 5,000-gal volume, would
25
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provide approximately 6.5 min of contact time to presumably improve the formation of iron
floes prior to pressure filtration.
Inconsistent to what was planned, the aeralater was used as an aerator during a large part of
the performance evaluation study. At system startup, the blower at the top of the aeralater
was allowed to operate, causing significant biofouling in the Macrolite® filters due to
biological activities. The blower was turned off in March 2007, but some aeration apparently
continued as water discharged from the standpipe splashed downward through a series of
aluminum trays at the top section of the aeralater. In July 2009, the aluminum trays were
removed and the 6-in standpipe was cut 4-ft below the high-level sensor in the aeralater.
Even with these changes, aeration continued until the aeralater was completely bypassed in
March 2010 as discussed in Section 4.5.2.2.
Pressure Filtration - Removal of arsenic-laden iron particles from the aeralater was
achieved via downflow filtration through two 84-in x 96-in pressure vessels. The steel
vessels were floor mounted, arranged in parallel, and piped to a valve rack mounted on a
welded, stainless steel frame (Figure 4-12). Each vessel contained approximately 24 in (or 75
ft3) of 40/60 mesh Macrolite® media supported by fine garnet underbedding filled to 1 in
above a stainless steel wedge-wire underdrain with 0.006-in slots. The steel vessels were
coated on the exterior with an epoxy base and the interior was coated with a NSF-approved
epoxy coating. The downflow through each vessel was regulated to 385 gpm with a flow-
limiting device to prevent filter overrun or damage to the system. The normal system
operation with both vessels online provided a total system flowrate of 770 gpm.
Figure 4-12. Macrolite Pressure Filters and Valve Rack
(Before Completion of Enclosure)
26
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• Filter Backwash - At a 10-gpm/ft loading rate and 24 in of depth, the anticipated pressure
drop across a clean Macrolite® filter was 10 to 12 psi in the service mode. When the pressure
drop across a filter reached 20 psi, both filters were automatically backwashed in an upflow
configuration. Backwash also might be triggered by the length of time the filters had been in
service and/or in stand-by mode. During a backwash cycle, one filter was backwashed while
the other was still in service. Water was drained from the first filtration vessel, which was
then sparged with air. After a brief settling period, the filtration vessel was backwashed with
treated water until the turbidity of backwash wastewater reached a desired setpoint, as
measured by an inline Hach™ turbidimeter. The filtration vessel underwent a filter-to-waste
cycle before returning to feed service, and then the second filter was backwashed. The
backwash wastewater was sent to a sump that emptied by gravity into a pond (Figure 4-13)
located just outside of the treatment plant building.
Figure 4-13. Backwash Wastewater Pond with Storage Tank in Background
• Softening and Post-Chlorination - Approximately 70% of the treated water from the
Macrolite® filter was fed into the pre-existing water softener. Synthetic zeolite was used to
remove hardness from the water and the softened water was subsequently blended with the
approximately 30% of the bypass water. The pre-existing pressure filter (120-in x 92-in) was
emptied and converted to a softener. After softening, post-chlorination occurred and the
water was transferred to the 127,000-gal storage tank for distribution.
• Storage and Distribution - Treated water in the 127,000-gal storage tank was transferred by
two high service pumps to the 10,000-gal horizontal hydropneumatic tank before entering the
distribution system. On/off of the pumps was controlled by a set of high- and low-level
sensors in the hydropneumatic tank.
27
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4.3
System Installation
Kinetico completed installation and shakedown of the system on June 23, 2006. The following briefly
summarizes system/building installation activities, including permitting, building preparation, system
offloading, installation, shakedown, and startup.
4.3.1 Permitting. Design drawings and a process description of the proposed treatment system
were submitted on August 19, 2005, by William Jarrell, P.E. of Morgan Goudeau and Associates to
LADHH/OPH. LDHH/OPH issued the permit with a letter of no objections on September 16, 2005. Due
to elevated As(V) levels in the filter effluent, a permit modification also prepared by William Jarrell, P.E.
was submitted on June 21, 2007, and granted on August 8, 2007 for the use of FeCl3 addition.
4.3.2 Building Construction. Building construction began on March 6, 2006, utilizing a pre-
engineered metal building extension to house the filtration and softener vessels. A 6-in thick concrete pad
was installed from March 6 to 27, 2006, and after allowing time for the concrete pad to cure, a go-ahead
was given to the vendor to ship the equipment. Upon arrival on April 10, 2006, the filtration vessels and
pipe rack were placed on the concrete pad followed by completion of the building enclosure. The
building was 53 ft x 25 ft with a roof height of 16 ft. A 12-ft-wide by 14-ft tall overhead door enabled
access to the building. Wastewater discharge was through a 12-in PVC drain line that emptied by gravity
from a sump into a 4-ft deep pond (Figure 4-13). Figure 4-14 shows the pre-engineered metal building
extension that housed the treatment system, which was placed adjacent to the existing aeralater unit.
Figure 4-14. New Building Constructed Adjacent to Pre-existing Aeralater
4.3.3 System Installation, Startup, and Shakedown. Upon arrival of the system components,
Kinetico, through its subcontractor Twico, performed off-loading, placement of the filter vessels and pipe
rack onto the concrete pad, and piping modifications (Figures 4-15 and 4-16). Further system installation
work was temporarily halted so that building construction could proceed around the system. Kinetico
28
-------
Figure 4-15. Off-Loading of Pipe Rack for Macrolite® Filtration System
Figure 4-16. Placement of Vessels and Pipe Rack on Concrete Pad Prior to Building Construction
-------
returned to the site from May 22, 2006, to June 7, 2006, to complete installation and shakedown
activities, including inlet and distribution piping tie-ins, electrical interlocking, PLC testing, instrument
calibration, and media loading and backwashing to remove fines. The system (Figure 4-17) was manually
started up on June 7, 2006, to test the pressure filters. Automatic startup was not performed at the time
because of several outstanding issues related to the conversion of the pre-existing aeralater to a contact
tank (e.g. filter media removal, cleaning, disinfection, as well as chemical feed point and bypass line
installation). After United Water Systems addressed these action items, Kinetico returned to the site to
continue shakedown activities during the week of June 19, 2006. Operator training occurred on June 22,
2006. The system was started in automatic mode on June 23, 2006.
Battelle performed system inspections and operator training on sample and data collection from August 9
to 11, 2006. As a result of the system inspections, several punch-list items were identified. Table 4-4
summarizes the items identified and corrective actions taken.
Figure 4-17. Completed Treatment Systems
4.3.4 Iron Addition Modification. A permit modification for an iron addition system was
prepared by William Jarrell, P.E. and submitted to LADFiFi/OPH on June 21, 2007, because of higher-
than-MCL levels of arsenic in the filter effluent. Approval for iron addition was granted by
LADFiFi/OPH on August 8, 2007, and iron addition was initiated by the operator on December 12, 2007.
30
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Table 4-4. System Inspection Punch-List Items from August 9 to 11, 2006, Site Visit
Item
No.
Description
Corrective Action(s) Taken
Resolution
Date
1
Move KMnO4 injection to a single point
just prior to aeralater
Action item for Kinetico removed on
11/14/06 due to proposed switch to pre-
chlorination
11/14/06
Change scale of outlet pressure gauge (PI-
5) to a 30 psi max range for better reading
accuracy
A 0 to 30 psi pressure gauge shipped and
installed by operator
01/15/07
Determine cause(s) of 2 to 4 psi
discrepancies observed between manual
gauges and pressure transducers and take
necessary measures to fix problems
Manual gauges next to transducers PT2 and
PT3 replaced by Kinetico; confirmed with
operator that these manual gauges were
working and within 1 to 2 psi of pressure
transducer (PT2/PT3) readings
12/13/06
Determine cause(s) of different backwash
flowrate readings observed between PLC
panel and digital readouts on meter;
perform meter calibration if needed
Three manual backwashes performed by
Kinetico and proper calibration of
backwash flow meter confirmed; data
provided to show comparable PLC readings
and digital readouts on meter
11/27/06
Adjust backwash flowrates to within
design specifications; elevated backwash
flowrate at 400 gpm (or 10.4 gpm/ft2)
observed, which might result in media loss
based on observations at other arsenic
demonstration sites
Backwash flowrate lowered by Kinetico to
approximately 380 gpm (inside range of
design values of 308 to 385 gpm/vessel [or
8 to 10 gpm/ft2])
11/28/06
Determine cause(s) of system warning
light on Hach Turbidimeter, which was lit
up on the instrument readout panel during
system operation
Hach warning light cleared
11/27/06
Determine cause(s) of low flow alarms
during backwash, which caused backwash
to fail and system to go out of service.
Problems reported by operator to Kinetico
on August 15, 2006; operator had to
acknowledge the alarm and manually
backwash system prior to returning to
service
Alarm was due to a bad solenoid valve on
air bank; lack of backwash flow due to
valve not opening. A spare solenoid on the
panel was used to fix the valve in question
08/31/06
Determine if a flow restrictor should be
installed to regulate fast rinse flowrate to
ensure proper fast rinse operation; flow
restrictors only installed on service line
An orifice plate to control fast rinse flow
rate shipped on October 20, 2006, and
installed by Kinetico later. Fast rinse
flowrate controlled to be within design
specification at 280 gpm
11/27/06
10
Determine cause(s) of elevated arsenic
levels in filter effluent. On 09/28/06,
Kinetico was notified by Battelle that filter
effluent was not reaching below 10 ug/L
arsenic due to presence of elevated soluble
As(V) concentrations
Iron addition initiated on December 12,
2007, but with little improvement; arsenic
levels in filter effluent remained elevated
for the duration of study
Not
resolved
31
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4.4 System Operation
The treatment process as designed would consist of oxidation of soluble As(III) and soluble Fe(II) using
KMnO4, adsorption/co-precipitation of soluble As(V) onto iron solids, and Macrolite® pressure filtration
for removal of arsenic-laden iron particles. The existing aeralater would be emptied of all internal
components and used as a contact tank upstream of the Macrolite® pressure filters. The existing pressure
filter would be converted to a softener in its pre-study configuration for hardness removal.
Upon completion of system installation in July 2006, the project team believed that the aeralater had been
properly modified to function as a contact tank. It was not until late 2006 and early 2007 when the
project team discovered that the aeralater, in fact, had been functioning as an aerator, causing extensive
biofouling of the filter media due to microbial activities, including nitrification. Accumulation of bio-
solids in the filters significantly increased backwash frequency (from one or two times/day to as many as
eight times/day). Efforts to rectify the problems included an acid and a caustic wash of the fouled media
in December 2006 and turning off the blower to stop air flow to and aeration in the aeralater in March
2007. To better control biological growth in the filters, both KMnO4 and chlorine (in gas form) were used
in late January 2007 and then only chlorine (in gas form) in March 2007 (exacting timing for
KMnCVchlorine and chlorine usage could not be verified). While these changes appeared to alleviate, to
some extent, frequent backwash issues, filter effluent continued to contain >10 ng/L of arsenic, existing
mostly as soluble As(V), during most sampling events. This prompted a decision to add supplemental
iron to raw water, starting on December 12, 2007, to aid in the adsorption/co-precipitation process.
The effect of iron addition was inconclusive due to erratic FeCl3 dosage caused by problems with the
chemical feed pump and corrosion and dissolution of the mixing equipment within the day tank. As a
result, iron addition not only did not significantly reduce soluble arsenic concentrations, but also added
extra solids loading to the pressure filters, resulting in even more frequent backwash. This, along with the
fact that piping in the aeralater was modified in July 2009 to minimize aeration of source water in the
aeralater, led to the termination of supplemental iron addition in July 2009. Because system performance
did not appear to improve, the filter media were acid-washed three times in March, July, and October
2009. Meanwhile, the two flow restrictors located downstream of the filters were unclogged and rubber
grommets in the restrictors removed to enhance water flow through the filters (from -250 to -450 gpm).
While the system continued to produce effluent with elevated arsenic and iron concentrations, two
members of the project team visited the site from January 18 through 22, 2010, to inspect the system and
conduct three separate, yet connected tests relating to the performance of and potential future
modifications to the system. The tests performed included sampling at the AC sampling location after
physical bypass of the aeralater, a series of jar tests relating to oxidant selection and optimal oxidant dose,
and a filter run length study to determine useful run length between two consecutive backwash events.
The test results led to two recommendations by the project team to permanently bypass the aeralater to
minimize aeration prior to the pressure filters and to return to the use of KMnO4 as the oxidant for soluble
As(III) and soluble Fe(II) oxidation.
During a following trip from March 17 through 19, 2010, made by Accurate Water Solutions under
contract with Battelle, it was noted that the facility had gone ahead to install piping to bypass the aeralater
(Figure 4-18). Upon its inspections, Accurate Water Solutions reported, among other issues, potential
water hammer problems. After replenishing the filter beds with Macrolite® media, the facility began to
operate the system with KMnO4 and performed another acid wash to both filters thereafter in April 2010.
A pipe break (Figure 4-19) took place on May 5, 2010, and forced the system to be shut down until May
20, 2010. Soon after the system resumed operation, the facility was issued an administrative order by
LDFIFI/OPH on June 2, 2010 due to exceedance of running annual average of arsenic compliance samples
collected during October 1, 2008, through September 30, 2009.
32
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Figure 4-18. Piping Bypassing Pre-existing Aeralater
Figure 4-19. Replacement Steel Pipe (Vertical Section on Right) After Pipe Break
33
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The two project team members returned to the site again during July 26 through 31, 2010 to perform two
run length tests with the use of bypass piping and KMnO4. While soluble As(V) concentrations were
reduced as anticipated, total arsenic concentrations were at or just over the 10-(ig/L MCL. In addition,
iron broke though the pressure filters within 2 hr of filter runs. A follow-on meeting was convened at
EPA National Risk Management Research Laboratory (NRMRL) on September 16, 2010, with
representatives from EPA, United Water Systems, and Battelle in attendance. Recommendations were
made by meeting attendees to the facility operator concerning ways to verify his observations that the
system had produced effluent with arsenic concentrations below the MCL. A decision also was made to
immediately end the performance evaluation study due to expiration of the Round 2 demonstration
contract between EPA and Battelle. Table 4-5 chronologically summarizes key events that took place
during the performance evaluation study.
Table 4-5. Key Events During Performance Evaluation Study at Arnaudville, LA
Date
10/10/06
11/06
12/04/06
12/08-
12/06
Late
January-
02/19/07
02/21/07
03/08/07
03/19/07
04/10/07
04/18/07
08/08/07
09/24/07-
10/15/07
11/05/07
Problems Encountered
Higher than MCL levels of soluble As(V) in
filter effluent observed since start of study
System experienced increasing backwash
frequency (from 2 to 3 times/day to 2 to 8
times/day)
Battelle informed by Kinetico possible
media fouling observed during its site visit
in late November 2006
Battelle informed Kinetico of decreased
filter bed depths (4.0 to 7.5 in)
Actions Taken
Kinetico agreed to include iron addition to
system
Operator performed an acid and a caustic
wash on Macrolite® pressure filters; backwash
frequency back to 1 to 2 times/day
Operator began to use gas chlorine for pre-
oxidation (possibly also with the use of some
KMnO4)
Battelle met with Kinetico and EPA to discuss
operational issues; nitrification determined as
cause for biofouling. Measures recommended
included:
• Stop aeration in aeralater
• Apply chlorine shock to filter media
periodically
• Chlorinate raw water and/or backwash water
Operator turned off aeralater blower
Battelle placed a P.O. with Morgan Goudeau
and Assoc. for preparation of an iron addition
submittal package for LADHH
Kinetico shipped media to facility on 04/26/07
to top off filter beds
Temporarily suspended regular weekly sampling
due to on-going operational issues
Received approval from LADHH for iron
addition
Operator replenished 7.5-in media into Vessel A
and 4-in media into Vessel B; system taken
offline
Resumed normal system operation
34
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Table 4-5. Key Events During Performance Evaluation Study at Arnaudville, LA (Continued)
Date
11/19/07
12/12/07
01/23/08
02/08-
04/08
05/29/08
06/08-
09/08
10/20/08
11/08-
12/08
01/09-
05/09
06/29/09
07/13-
20/09
09/09-
10/09
10/26-
28/09
11/09-
01/10
Problems Encountered
Impeller/mixer corroded, leading to
stratification within day tank and
inconsistent chemical dosing
System flowrate gradually reduced to
250 gpm
System continued to experience low flowrate
System continued to have early iron and
arsenic breakthrough
Actions Taken
Operator conducted a 3.2-hr run length study;
arsenic at 11.4 to 12.9 ug/L measured in filter
effluent with no paniculate iron breakthrough
Began supplemental iron addition (EPA TOM
visited site on 12/1 1/07)
Resumed weekly sampling; results indicated
similar treatment results as compared to no iron
addition
Increased iron dosage from -0.5 to 1.2 mg/L (as
Fe); total arsenic level reduced to 5.6 ug/L
Operator conducted a run length study; results
indicated insufficient chlorine addition during
testing (i.e., no arsenic oxidation/co-
precipitation/removal occurred)
Battelle attempted to contact operator regarding
need to repeat special study; operator indicated
in 09/08 that mixing unit was down and that he
would repeat the study once a new mixing unit
was installed
Operator repeated run length study; results
indicated that ion dose rates were too low
Operator worked on iron dose rates, which were
either too low or too high; mixing equipment
continued to be corroded/dissolved
Battelle attempted to contact operator regarding
status of mixing unit and another acid wash,
which was carried out in early March; Battelle
purchased a new pump and an impeller/mixer
for FeCl3 mixing; operator called on 05/14/09
indicating receipt of new mixing equipment and
low system flowrate (250 gpm)
Operator informed Battelle that aeration
continued in aeralater; Battelle emphasized that
aeration must be stopped and that iron addition
can be discontinued once aeration is stopped
Performed acid wash on media; aluminum trays
in aeralater removed and standpipe in aeralater
cut approximately 4 ft below high level sensor
(explained to Battelle during site visit for jar
tests in 01/10)
Performed acid wash on media; little
improvement on flowrate; identified cause to be
a clog in flow restrictors; worked with Kinetico
to unclog flow restrictors (by removing
sediment and rubber grommets); restored
flowrate to -450 gpm
35
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Table 4-5. Key Events During Performance Evaluation Study at Arnaudville, LA (Continued)
Date
Problems Encountered
Actions Taken
01/18-
22/10
Battelle onsite to perform jar tests, realizing
that:
• Aeration in aeralater continued (2 to 4 mg/L
of DO at AC)
• System settings significantly deviated from
design settings
• Media beds needed replenishment Jar test
results indicated that:
• Without air, soluble As(V) reduced down to
~5 ug/L with use of KMnO4, suggesting
bypassing aeralater could be a solution
• Chlorine would leave higher levels of
As(III) and Fe(II) at AC
03/17-
19/10
Low Ap across vessels (possible
channeling?)
Tom Jadach of Accurate Water Solutions visited
site to inspect system and observed the
following:
• Media has bio- and iron fouling; back-to-
back acid washes using 10% muriatic acid
needed
• Media beds are only ~17 in deep; need ~24
ft3 per vessel
• Aeralater bypassing piping already installed;
had concerns over water hammer
04/14/10
24 ft3 media ordered by Battelle (another 24 ft3
ordered by United Water Systems)
04/19/10
Operator indicated the following:
• Both vessels acid washed
• Bypassing plumbing completed
• System changes made for KMnO4
injection
05/05-
20/10
Pipe break at site; system taken offline
Replacement steel piping installed
06/02/10
Administrative order issued by LDH
07/26-
31/10
Battelle onsite to perform run length studies
with use of bypass piping and KMnO4:
• Experienced early iron breakthrough from
filters (within 2 hr)
• Soluble As(V) reduced to about 6 ug/L,
consistent with results from jar tests
• Actual backwash steps not following PLC
settings
09/16/10
Meeting convened at EPA/NRMRL with
representatives from United Water Systems,
EPA, and Battelle:
• Operator indicated that system effluent had
low iron concentrations due to use of both
KMnO4 and chlorine
• Recommendations provided by meeting
participants to operator regards ways to
verify his claims
• System performance evaluation study to end
immediately due to end of Round 2 contract
between EPA and Battelle
36
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4.4.1 Service Operation. The system operational parameters are tabulated and attached as
Appendix A with the key parameters summarized in Table 4-6. The performance evaluation study began
on July 17, 2006, and ended on September 16, 2010, when the project team met with representative of
United Water System at EPA/NRMRL in Cincinnati, OH. The operational parameters were logged only
until February 21, 2010. Between July 17, 2006, and February 21, 2010, the system operated for 17,800
(Vessel B) to 18,329 hr (Vessel A) based on two hour meters interlocked with the well pumps. Average
daily run times ranged from 4.2 to 23.6 hr/day and averaged 14.0 hr/day for Vessel A and ranged from 4.4
to 23.6 hr/day and averaged 13.9 hr/day for Vessel B. As shown in Figure 4-20, no obvious seasonal
variation was observed during the study period.
Daily Run Time
Q TA Daily Run Time
OTB Daily Run Time
0.0
03/24/06 10/10/06 04/28/07 11/14/07 06/01/08 12/18/08 07/06/09 01/22/10 08/10/10
Figure 4-20. Daily Run Time
Daily demands varied between 89,635 and 505,714 gpd and averaged 277,128 gpd, compared to the
280,000 to 380,000 gpd reported by the facility prior to the performance evaluation study. Daily demands
were calculated based on incremental readings of a flow meter/totalizer installed at the effluent side of the
pressure filters normalized for a 24-hr day. Similar to daily system run times, no obvious seasonal
variation was observed during most of the study period. As shown in Figure 4-21, the only clear
increasing trend on daily demands appeared to occur during the 2009 summer (before July 2009), but
similar increasing trends also were observed during the 2007 to 2008 and 2009 to 2010 winters. At
277,128 gpd, the system operated at 25% of the design capacity (i.e., 770 gpm).
37
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Table 4-6. Treatment System Operational Parameters
Parameter
Operating Period
Value
07/17/06-09/16/10(a)
Pretreatment Operation
KMnO4 Dosage (mg/L)(b)
Chlorine Dosage (mg/L [as C12])(C)
FeCl3 Dosage (mg/L [as Fe])(d)
1.8 [0.04-4.7]
NA
NA
Service Operation
Total Operating Time (hr)
Daily Operating Time (hr)
System Throughput(e) (gal)
Daily Demand (gal)
Instantaneous Flowrate (gpm)
Calculated Flowrate(f) (gpm)
Contact Time in Aeralater(8) (min)
Hydraulic Loading over Pressure Filter(g) (gpm/ft2)
System Inlet Pressure (psi)(h)
System Outlet Pressure (psi)(h)
Tank A Outlet Pressure (psi)(h)
Tank B Outlet Pressure (psi)(h)
Ap Across System (psi)(h)
Ap Across Vessel A (psi)(h)
Ap Across Vessel B (psi)(h)
Filter Run Time between Backwashes (hr)
18,329 (Vessel A)
17,800 (Vessel B)
14.0 [4.2-23. 6] (Vessel A)
13. 9 [4.4-23.6] (Vessel B)
363,096,450
277,128 [89,635-505,714]
335 [136-509]
352 [130-673]
14.9 [9.8-36.8]
4.4 [1.8-6.6]
33.0 [18-48]
15.8 [10-30]
24.7 [12-44]
24.2 [10-44]
16.9 [1-42]
7.8 [1-34]
8.1 [1-38]
3. 9 [0-22.6] (Vessel A)
3. 6 [0-22.5] (Vessel B)
Backwash Operation
Backwash Frequency (time/vessel)
Number of Backwash Cycles (Vessels A/B)
Flowrate(1) (gpm)
Hydraulic Loading Rate(1) (gpm/ft2)
Duration (min/tank)(1)
Backwash Volume (gal/vessel)
Filter-to -Waste Volume (gal/vessel)
Wastewater Produced (gal/vessel)
2.2 [0-10] (Vessel A)
2.3 [0-16] (Vessel B)
2,876/3,000
NA
NA
NA
3,376
250
724 [596-1,157]
Note: Data presented included average and [range].
(a) Operational data recorded since system startup on 07/17/06 through 02/21/10.
(b) KMnO4 used from system startup in 07/06 through 02/07 and then from 04/10
through end of performance evaluation study in 09/10; tracking of KMnO4
performed only during 07/06 through 02/07.
(c) Gas chlorine used between 02/07 through 04/10; chlorine dosages not tracked.
(d) FeCl3 added during 12/07 through 07/09; iron dosages tracked sporadically
during testing.
(e) Estimated based on average instantaneous flowrate (335 gpm) and average
filter operating time ([17,800 + 18,329]/2).
(f) Calculated flowrates based on incremental throughput and incremental
operating hours.
(g) Based on instantaneous flowrate readings.
(h) After outliers removed.
(i) Data not available due constant changes of flowrate and other backwash
settings on PLC.
38
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Daily demand
600,000
500,000
100,000
03/24/06
10/10/06
01/22/10
08/10/10
Figure 4-21. Daily Demands During Study Period
System flowrates were tracked by both instantaneous readings of the flow meter and calculated values
based on hour meter and flow totalizer readings on the control panel. Instantaneous flowrate readings
varied from 136 to 509 gpm and averaged 335 gpm. Calculated flowrate values varied from 130 to
673 gpm and averaged 352 gpm. Although large variations were observed for both instantaneous and
calculated flowrates, these flowrate readings/values appeared to agree with one another for the most part
as shown in Figure 4-22.
Flowrates during the periods from February 10 through June 5, 2007, from January 29 through February
27, 2008, and from June 20 through August 24, 2008, were significantly reduced to an average of 283,
260, and 250 gpm, respectively, due to failure and/or shutdown of one of the wells caused by various
operational issues. Flowrates were gradually reduced from approximately 400 gpm in September 2008 to
below 280 gpm by the end of January 2009, and then suddenly increased to over 370 gpm in February
2009. The reason for the sudden increase was an acid wash of the filter media by the operator per
Kinetico recommendation. Thereafter, flowrates were gradually decreased again from about 370 gpm to
below 270 gpm by October 2009 despite two consecutive acid washes of the filter media in July and
October 2009. On October 29, 2009, with Kinetico's assistance, it was determined that the decreasing
flowrates were caused by clogged flow restrictors. Upon removal of large flakes of precipitated iron and
rubber grommets from the flow restrictors, flowrates were restored to above 400 gpm throughout the
remainder of the performance evaluation study.
Using the average instantaneous flowrate of 335 gpm and total number of filter operating time (i.e.,
average of Vessel A and B operating times -18,065 hr), the total system throughput was estimated to be
363,096,450 gal.
39
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System Flowrates
03/24/06 10/10/06 04/28/07 11/14/07 06/01/08 12/18/08 07/06/09 01/22/10 08/10/10
Figure 4-22. System Flowrates
The 335-gpm instantaneous flowrate (on average) corresponded to a contact time of 14.9 min in the
aeralater and a filtration rate of 4.4 gpm/ft2 through the pressure filters. These values were much higher
than the design contact time of 6.5 min, but much lower than the design filtration rate of 10 gpm/ft2.
As shown in Figure 4-23, system outlet pressure readings stayed relatively constant, ranging from 10 to
30 psi and averaging 15.8 psi. System inlet pressure readings, however, varied significantly, ranging
from 18 to 48 psi and averaging 33 psi. Variations observed were caused primarily by factors such as
number of wells operating, system flowrate, installation of orifice plates, removal of rubber grommets
from the flow restrictors, extent of media fouling, depth of filter media, addition of supplemental iron,
and stage of filtration runs (e.g., just before or just after backwash), etc. System differential pressure (Ap)
readings generally varied according to the system inlet pressure readings, ranging from 1.0 to 42 psi and
averaging 16.9 psi.
Ap readings across both pressure filters also varied extensively (Figure 4-24), ranging from 1 to 34 psi for
Vessel A and from 1 to 38 psi for Vessel B. As shown in the figure, Ap readings generally decreased
from the range of 5 to 20 psi at the beginning of the performance evaluation study to the range of 1 to 5
psi by the end of performance evaluation study. Factors contributing to the decreases included primarily
washing away of filter media from the pressure filters (note that the pressure filters were replenished with
4 to 7.5 in of media in April 2007 and 7.5 in of media in April 2010) and especially removal of rubber
grommets in October 2009. Due to constant changing of PLC settings and other system operating
conditions by the operator as mentioned earlier, it was difficult to pinpoint what exactly had happened
during system operation and to interpret system performance using the recorded data such as vessel Ap
readings.
40
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System Pressure
O system inlet pressure
n system outlet pressure
delta p across system
03/24/06 10/10/06 04/28/07 11/14/07
06/01/08 12/18/08
Date
07/06/09 01/22/10 08/10/10
Figure 4-23. System Inlet/Outlet Pressure and Differential Pressure
Differential Pressure
03/24/06 10/10/06 04/28/07 11/14/07 06/01/08 12/18/08 07/06/09 01/22/10 08/10/10
Figure 4-24. Differential Pressure Across Macrolite® Pressure Filters
41
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4.4.2 KMnO4, Chlorine, and Iron Additions. KMnO4 was used initially as an oxidant to oxidize
soluble As(III) and soluble Fe(II). Due to biofouling in the pressure filters, KMnO4 was used in
conjunction with chlorine in February 2007. In an attempt to more effectively curb biological growth, gas
chlorine was used to replace KMnO4 soon afterwards. Meanwhile, FeCl3 was added to supplement
natural iron for better soluble As(V) removal in December 2007. After it became clear that aeration in
fact was the reason for biofouling and ineffective soluble As(V) removal, addition of FeCl3 was
discontinued in July 2009 and KMnO4 was used again as the oxidant in April 2010.
KMnO4 dosages were tracked by measuring daily consumption through solution level changes in the
chemical day tanks and daily flow based on the system effluent totalizer. Solution levels in both day
tanks were measured daily starting on August 16, 2006, for Tank 1 and on September 25, 2006, for Tank
2. Measurements continued through February 13, 2007, when KMnO4 was replaced with gas chlorine.
After KMnO4 was used again as the oxidant in April 2010, changes of solution levels were not recorded.
As shown in Figure 4-25, KMnO4 dosages ranged from 0.042 to 4.7 mg/L (as KMnO4) and averaged 1.8
mg/L (as KMnO4). This average dosage was about 30% lower than the target dosage of 2.6 mg/L.
KMnO4 Dosage
^"
O
c
re
60
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After switching from KMnO4 to gas chlorine, chlorine dosages were not tracked. Total chlorine residuals
at the AC and TB sampling locations were monitored by the operator using a field Hach meter. Because
reporting of the data to Battelle was sporadic and because communications with the operator had been a
great challenge, no chlorine usage or residual data could be presented in this report.
Initial sampling results across the treatment train appeared to suggest that there was a need for iron
addition in order to reduce arsenic concentrations to below 10 (ig/L (although it became evident later that
poor arsenic removal observed was caused primarily by the aeration process in the aeralater). Upon
LADHH's approval, iron addition was implemented in December 2007. According to the plan, iron
dosages should have been tracked by measuring daily consumption of FeCl3 in a day tank and daily flow
read from the effluent totalizer. However, tank levels were measured so sporadically (during the period
from February 26, 2008, through May 29, 2009) that iron dosages could not be calculated and plotted.
Based on the metal analyses as discussed in Section 4.5.1, iron dosages scattered quite extensively, which,
among others, might have been caused by an oversized pump and a corroding/dissolving impeller/mixer
due to the corrosivity of FeCl3 solution. By May 2009, a more adequately sized pump and a new impeller
and a mixer were installed, but logging of daily consumption did not resume. By July 2009, iron addition
was discontinued.
4.4.3 Backwash Operation. The two Macrolite® pressure filters were backwashed 2,876 and
3,000 times, respectively. Backwash was triggered mainly by a Ap setpoint. Occasionally, manual
backwashes were initiated, but only for testing and sampling of backwash water and solids.
After system startup in July 2006, the pressure filters generally were backwashed once or twice a day (see
Figure 4-26). The backwash frequency gradually increased to up to eight times a day by late November
2006. Examination of the filter media indicated significant biofouling, apparently caused by microbial
activities as a result of aeration in the aeralater. Immediately after an acid and a caustic wash in early
December 2006, the backwash frequency was restored to once or twice a day. Thereafter, the backwash
frequency was maintained to mostly once or twice a day through 2007. The use of gas chlorine (to
replace KMnO4) in February 2007 and shutting-off of the blower (in the aeralater) in March 2007
apparently helped slow down the biofouling. The acid and caustic wash is discussed in details in
Section 4.4.3.2.
Starting from December 2007, iron was added to well water; the backwash frequency increased
correspondingly to mostly one to three times a day. Occasionally, the backwash frequency spiked to six
or even seven to 16 times a day. By January and February 2009, the backwash frequency increased rather
consistently to six to 11 times a day and system flowrates decreased to about 280 gpm. Bio- and iron-
fouling were believed to be the main reason for more frequent backwashing. Under Kinetico's
instructions, the operator performed the second acid wash to the filter media in early March 2009. Upon
completion, the backwash frequency was reduced to mostly three to four times per day, which was
somewhat higher than those experienced with iron addition in 2008.
Due to deteriorating flow through the pressure filters after the March 2009 acid wash (from 350 to 270
gpm by October 2009), two additional acid washes were performed in mid-July and late October 2009.
These acid washes appeared to be less effective in reducing the backwash frequency and restoring the
system flowrates.
The backwash duration for each tank was affected by the minimum and maximum backwash time settings
and the ability of the backwash water to meet the turbidity threshold setting as measured by an inline
Hach™ turbidimeter. If the backwash water failed to meet the set threshold prior to reaching the
maximum backwash time, the backwash failure alarm had to be acknowledged and a successful backwash
cycle had to be conducted before the tank could return to the service mode. Backwash was followed by a
43
-------
No. of Backwashes/day from August 2006 Through August 2008
07/02/06 10/10/06 01/18/07 04/28/07 08/06/07 11/14/07 02/22/08 06/01/08 09/09/08
Date
Figure 4-26. Backwash Frequency
-------
No. of Backwashes/day from August 2008 Through February 2010
06/01/08 09/09/08 12/18/08 03/28/09 07/06/09
Date
10/14/09
01/22/10
05/02/10
Figure 4-26. Backwash Frequency (Continued)
-------
filter-to-waste step to remove any participates from the filter. The amount of wastewater produced totaled
19,834,500 gal (or 3,376 gal/vessel), equivalent to 5.5% of the total amount of water treated. This waste
to production ratio is significantly higher than those of several similar Macrolite® pressure filtration
systems evaluated at other EPA arsenic removal demonstration sites (see Table 4-7). Media fouling and
resulting higher backwash frequency apparently contributed to the higher backwash water usage.
Table 4-7. Waste to Production Ratios for Macrolite® Pressure Filters
Site
Arnaudville, LA
Pentwater, MI
Felton, DE
Sabin, MN
Climax
Design
System
Flowrate
(gpm)
770
400
375
250
140
No. of
Vessels
2
2
o
J
2
2
Vessel
Size
(in)
84 x96
60 x96
48 x?2
48 x?2
36 x?2
Waste to
Production
Ratio
(%)
5.5
1.9
1.5
2.5
1. 9-2 A
References
-
Valigore et al., 2008
Chenetal.,2010b
Chenetal., 2010a
Condit and Chen, 2006
Assuming a backwash flowrate of 385 gpm, the backwash duration would be 8.8 min. During the
performance evaluation study, however, backwash flowrates and other backwash settings were frequently
changed by the operator. This, in conjunction with the fact that the inline turbidimeter was not
functioning properly during most of system operation, prevented a meaningful estimate of the backwash
duration during the study period.
Because of frequent backwashes, filter run times between two consecutive backwashes were short,
averaging 3.9 and 3.6 hr for Vessels A and B, respectively. Varying system operating conditions caused
filter run times to vary significantly from 0 to 22.6 hr and from 0 to 22.5 hr, for Vessels A and B,
respectively.
4.4.3.1 PLCSettings. Table 4-8 presents the PLC backwash settings at system startup on August 10,
2006, and during a site visit on January 18, 2010. One of the most visible discrepancies was the Ap
trigger, which was set at 3 psi for both tanks. According to the vendor, the expected clean-bed Ap would
be 8 to 10 psi and the recommended Ap trigger should be approximately 10 psi larger than the clean-bed
Ap (i.e., -20 psi). The 3-psi Ap trigger could cause the filters to be backwashed far too frequently.
The actual pressure drop across the pressure filters at the time of data recording was 2.0 psi. The low
pressure drop observed might have been caused by factors such as shallow filter beds (indicative of media
loss), crusty bed surface, and/or channeling. It was determined later during a site visit by Accurate Water
Solutions on March 17 and 18, 2010, that the low pressure drop actually was caused by the removal of
rubber grommets in the flow restrictors in October 2009. This was supported by observation of a sudden
decrease in inlet pressure and Ap (see Figures 4-23 and 4-24), and a sudden increase in system flowrate
(see Figure 4-22).
Both minimum and maximum backwash times were set at 6 min; thus, all backwashes were terminated in
6 min. The filter beds most likely were not completely backwashed in 6 min, as evidenced by the large
amount of solids still present in backwash wastewater. The turbidimeter apparently was not working
properly. For example, the turbidity reading of a backwash wastewater sample taken by the end of a
backwash event showed approximately 40 nephelometric turbidity units (NTU) using a Hach handheld
46
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turbidimeter, while the inline turbidimeter read only 5 to 6 NTU. The operator cleaned the turbidimeter
with dilute HNO3, but the cleaning did not seem to solve the problem.
The backwash flowrate observed was 445 gpm (11.7 gpm/ft2), which was significantly higher than the
design value of 310 to 385 gpm (8 to 10 gpm/ft2). High backwash flowrates could lead to loss of media
and need to replenish the filter beds. In fact, both filter beds were replenished twice in April 2007 and
April 2010. Nonetheless, the 445-gpm flowrate appeared to be insufficient to fluidize the beds based on
an observation made by Accurate Water Solutions during its March 2010 visit.
As noted earlier, backwash settings and other system operating conditions were changed constantly by the
operator. The changes were not recorded in the field logs or reported to Battelle's Study Lead.
Therefore, it was difficult to track system performance and interpret treatment results based on PLC
settings and system operating conditions.
Table 4-8. Snapshots of PLC Backwash Settings
Parameter (for Each Tank)
Drain Time (min)
Service Time Trigger (hr)
Standby Time Trigger (hr)
Ap Trigger (psi)
Minimum Backwash Time (min)
Maximum Backwash Time (min)
Turbidity Threshold (NTU)
Low Flowrate Threshold (gpm)
Filter-to -Waste Time (min)
Recorded Date
08/10/06
4
24
48
20
5
16
20
200
2
01/18/10
6
24
48
3
6
6
30
200
2
4.4.3.2 Acid and/or Caustic Washes. When the high backwash frequency was observed in
November 2006, samples of Macrolite® media were collected from both pressure filters and sent to
Kinetico for analysis. One aliquot of the media was placed in a column, backwashed at 100% bed
expansion to remove suspended solids, and removed from the column for visual observation and
photographing (Figure 4-27). One portion was then vacuum-filtered and 1.135 g of the moist media was
placed in 36 mL of 1% sulfuric acid and heated to nearly boiling. The solution was then filtered and
analyzed for iron, manganese, silica, and phosphorus. The results showed 10.6, 1.7, 2.4, and 2.2 mg/g of
media for iron, manganese, silica, and phosphorus, respectively. One aliquot each of the vacuum-filtered
media was allowed to soak for approximately 67 hr in 10% HC1, 10% NaOH, saturated NaCl, Liquinox,
mineral spirits, and methanol. No significant changes to the media were observed except for the HC1-
soaked media, which seemed to be coated in an opaque gelatinous substance (Figure 4-28). After the
HCl-soaked media was dried at 105 °C for 1 hr, it exhibited a glazed appearance with some of the
gelatinous substance flaking off from the media and attaching to the watch glass (Figure 4-29). Placing
the HCl-soaked media in a 20% NaOH appeared to break up the gelatinous coating.
After the laboratory testing, Kinetico recommended to proceed with the acid/caustic washes, but only
after it determined that the system components were chemically compatible with the strong acid/base
used. A teleconference with the operator on December 8, 2006, however, indicated that the operator had
initiated the acid wash. Without recourse, Kinetico agreed to allow the acid to stay in the vessel for 24 hr
and the operator performed a system backwash the following morning on December 9, 2006. Because no
47
-------
Figure 4-27. Macrolite® Media After Backwash
Figure 4-28. Macrolite® Media After Being Soaked in 10% HC1 Solution
48
-------
Figure 4-29. HCl-Soaked Media After Drying
written instructions had been provided by Kinetico and no reliable communications had been established
between the operator and Battelle, it was not clear how the acid and caustic washes were actually
performed at the site.
By March 2007, a set of written procedures was received from Kinetico. Key steps of the procedures are
summarized as follows:
• Begin the 10% HC1 wash with two back-to-back backwashes on both vessels.
• Isolate the vessel to be washed by disabling the vessel with the touch screen. Also close the
hand valves for all service lines so that nothing can enter the vessel during the wash.
• Drain water in the vessel to approximately 1 ft above the media bed.
• Dispense 150 gal of 30% HC1 to the media bed. Afterwards, close the top of the vessel and
airsparge the media for a minimum of 5 min.
• Continue to airsparge the media for 5 min per hour while the media is being soaked in the
acidic solution.
• Allow the media to sit in the acidic solution overnight (more than 20 hr of contact, however,
may cause damage to the lower distributors).
• Slowly fill the vessel completely with water; perform backwash to rinse out any remaining
acid in the vessel.
• Continue the 10% NaOH wash by repeating the acid wash procedure.
• Dispense 100 gal of 50% caustic into the vessel and allow the media to soak for 2 hr.
49
-------
• Airsparge the media bed every 15 min.
• Rinse out any remaining NaOH in the vessel with backwash.
• Ensure that all valves are in the correct positions before enabling the vessels on the touch
screen and bring the system back online.
Because the media continued to show signs of biofouling and required more frequent backwashing, three
additional acid washes were performed by the operator in March, July and October 2009. The amounts of
HC1 used were 25 and 50 gal for the March and July washes, respectively. The amount used for the
October wash was unknown. The amounts used for the March and July washes were significantly lower
than the amount (i.e., 150 gal of 30% HC1) recommended by Kinetico; this probably was the reason why
these washes were not as effective (in terms of restoring the system flowrate and backwash frequency) as
the one performed in December 2006.
4.4.4 Residual Management. Residuals produced by the Macrolite® arsenic removal system
included backwash wastewater and filter to waste water, which contained arsenic-laden solids as
discussed in Section 4.5.2. Wastewater from backwash was discharged to the building sump, which was
emptied by gravity to a pond as shown in Figure 4-13. According to the backwash flow totalizer,
19,834,500 gal of wastewater was produced during the entire study period.
4.4.5 Reliability and Simplicity of Operation. Inability to consistently remove arsenic to <10
(ig/L was the main issue encountered during the performance evaluation study. This was caused
primarily by the unintended aeration in the pre-existing aeralater and resulting biofouling of the filter
media in the pressure filters. Another unfortunate consequence of the unintended aeration was
misinterpretation of the above-the-MCL treatment results, which led the project team to conclude that
supplemental iron would be needed to enhance arsenic removal. While addition of FeCl3 resulted in little
improvement to arsenic removal, additional solid loading to the pressure filters required them to be
backwashed even more frequently. Further, chlorine gas was used to replace KMnO4 due to chlorine's
ability to better curb biological growth in the pressure filters, but the use of chlorine might not be a good
choice due to the presence of ammonia and TOC in source water. The iron addition process was
interrupted a number of times due to erratic dosing rates caused by an oversized pump and a
corroding/dissolving piece of mixing equipment (i.e., an impeller and mixer). These, in conjunction with
the constantly changing PLC settings/operating conditions and lack of timely communications between
the operator and Battelle caused the source water (with a complex chemistry) to be inadequately treated
and the treatment system to be improperly operated.
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.
4.4.5.1 Pre- and Post-Treatment Requirements. Pretreatment consisted of chemical additions to
improve arsenic removal. KMnO4 after proper dilutions was added using two LMI metering pumps to
oxidize As(III) and Fe(II). KMnO4 was replaced with gas chlorine using the pre-existing addition system
from February 2007 through April 2010. Gas chlorine also was used for post-chlorination to provide
chlorine residuals to the distribution system. During December 2007 through July 2009, iron addition
was performed using one of the KMnO4 addition systems. The other post-treatment was softening (with
30% bypass). In addition to tracking the depth of the KMnO4, chlorine, and iron solution in the day
tanks, the operator measured chlorine concentrations to ensure that residuals existed prior to entering the
distribution system.
50
-------
4.4.5.2 System Automation. The Macrolite® pressure filtration system was automatically controlled
by the PLC in the central control panel. The control panel contained a modem and a touch screen OIP
that facilitated monitoring of system parameters, changing of system setpoints, and checking the alarm
status. Service time, standby time, and Ap settings (Table 4-3) automatically determined when the tanks
were backwashed. Due to media fouling and solids loading, Ap setting was responsible for all 3,000
backwashes for each filter. The touch screen OIP also enabled the operator to manually initiate the
backwash sequence.
Because the PLC settings and system operating conditions such as backwash flowrate were constantly
changed by the operator during system operation, it was difficult to troubleshoot system operational and
performance issues and to interpret data, both operational and analytical, for performance improvements.
4.4.5.3 Operator Skill Requirements. Under normal operating conditions, the daily demand on the
operator was about 30 min for visual inspection of the system and recording of operational parameters,
such as pressure, volume, flowrate, and chemical usage on field log sheets. Due to operational and
performance issues, the operator spent a significant amount of time working with the vendor and/or
Battelle to assist in troubleshooting and performing special studies.
In Louisiana, an operator of any public water system must hold current and valid professional
certification(s) of required categories (i.e., water production, water distribution, and water treatment) at or
above the level required for the total system and individual facility. Required levels (classes) of
certification for an operator, based on facility classification, are from Classes 1 to 4, with Class 1 being
the lowest (serving <1,000 population) and Class 4 the highest (over 25,000 population). Because the
system at Arnaudville, LA serves approximately 1,200 connections, the operator needs to have a Class 2
certification (serving 1,001 to 5,000 population).
After receiving proper training during the system startup, the operator understood the PLC, knew how to
use the touch screen OIP, and was able to work with the vendor to troubleshoot problems and perform
onsite repairs.
4.4.5.4 Preventative Maintenance Activities. The vendor recommended several routine maintenance
activities to prolong the integrity of the treatment system (Kinetico, 2005). Daily preventative
maintenance tasks included recording pressures, flowrates, chemical drum levels, and visually checking
for leaks, overheating components, proper manual valve positioning and pumps' lubricant levels, and any
unusual conditions. The vendor recommended weekly checking for trends in the recorded data that might
indicate a decline in system performance, and semi-annually servicing and inspecting ancillary equipment
and replacing worn components. Cleaning and replacement of sensors and replacement of o-ring seals
and gaskets of valves were performed as needed.
4.5 System Performance
The performance of the Macrolite® Arsenic Removal System was evaluated based on analyses of water
samples collected from the treatment plant, backwash line, and distribution system.
4.5.1 Treatment Plant Sampling. Treatment plant water was sampled on a total of 69 occasions,
including three duplicate events and 41 speciation events. From August 10, 2006, through April 30 2007,
37 sampling occasions took place, including three duplicate events and nine speciation events. After
April 30, 2007, sampling was suspended to await the implementation of supplement iron addition. Once
iron addition began in December 2007, sampling resumed on January 23, 2008, but was on again and off
again until March 30, 2009. During this period, 13 speciation sampling events took place. After
supplemental iron addition ended in July 2009, sampling resumed in August 2009 and continued until
51
-------
February 9, 2010. A single sampling event took place on August 5, 2010, after piping to bypass the
aeralater had been installed. From August 18, 2009, through February 9, 2010, 19 speciation sampling
events took place.
Tables 4-9 summarizes analytical results of all analytes without iron addition (excluding the August 5,
2010, data after aeralater bypassing). Table 4-10 summarizes analytical results of all analytes with iron
addition. The results shown in these two tables represent data impacted, to a varying degree, by aeration
in the aeralater. Appendix B contains a complete set of analytical results. The results of the water
samples collected across the treatment plant are discussed below.
Table 4-9. Analytical Results (without Iron Addition)(:
Parameter
As (total)
As (soluble)
As
(paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Sampling
Location
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
Unit
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Sample
Count
55
55
29
29
27
27
27
1
1
27
27
27
1
1
27
27
27
1
1
27
27
27
1
1
27
55
55
29
29
27
27
27
1
1
27
Concentration
Minimum
24.1
25.3
8.7
9.5
1.4
11.1
2.2
9.6
9.8
0.3
<0.1
3.6
0.1
1.1
0.1
0.4
O.I
1.5
1.4
0.1
O.I
1.3
8.0
8.4
O.I
1,477
1,385
<25
<25
<25
<25
<25
<25
<25
<25
Maximum
43.0
41.8
27.7
28.5
19.0
37.7
30.9
9.6
9.8
16.2
22.7
30.2
0.1
1.1
9.8
35.2
27.2
1.5
1.4
5.6
19.9
19.0
8.0
8.4
14.1
2,939
2,701
92.7
149
1,037
3,276
1,956
<25
<25
<25
Average
32.7
33.8
13.8
14.3
11.7
29.1
13.3
9.6
9.8
10.1
2.7
19.7
0.1
1.1
1.8
24.4
2.5
1.5
1.4
1.2
4.7
10.8
8.0
8.4
9.0
2,059
1,995
17.6
21.6
166
1,906
97
<25
<25
<25
Standard
Deviation
4.9
4.2
4.0
3.9
4.3
4.7
5.2
-
-
3.3
4.6
5.2
-
-
2.7
7.2
5.4
-
-
1.2
5.1
3.6
-
-
3.1
279
285
17.2
32.2
264
683
373
0.0
0.0
0.0
52
-------
Table 4-9. Analytical Results (Without Iron Addition)^ (Continued)
Parameter
Mn (total)
Mn (soluble)
Total
Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Fluoride
Nitrate
(asN)
Ammonia
(asN)
Sulfate
Silica
(as SiO2)
Sampling
Location
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
Unit
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
Sample
Count
55
55
29
29
27
27
27
1
1
27
26
26
1
1
26
26
26
1
1
26
26
26
1
1
26
27
27
1
1
27
27
27
1
1
27
27
27
1
1
27
27
27
1
1
27
55
55
29
29
27
Concentration
Minimum
96.2
90.2
21.3
101
99.9
28.9
21.4
135
136
20.2
193
198
215
222
187
104
107
128
133
100
77.1
75.8
86.2
89.0
72.3
0.1
0.1
0.2
0.2
0.1
0.05
0.05
0.05
0.05
0.05
1.5
0.9
1.9
1.9
0.2
0.1
0.1
0.1
0.1
0.1
38.4
40.3
39.6
38.0
39.8
Maximum
196
932
605
1,443
384
180
478
135
136
394
440
438
215
222
439
316
316
128
133
316
124.4
122.4
86.2
89.0
123.8
0.3
0.3
0.2
0.2
0.8
0.05
0.1
0.05
0.05
0.6
2.2
2.0
1.9
1.9
2.0
0.5
0.5
0.1
0.1
0.5
49.3
50.0
50.1
49.6
49.6
Average
133
334
240
316
151
130
166
135
136
151
278
271
215
222
267
182
178
128
133
175
95.5
92.4
86.2
89.0
92.0
0.2
0.2
0.2
0.2
0.2
0.05
0.05
0.05
0.05
0.1
.9
.7
.9
.9
.4
0.2
0.2
0.1
0.1
0.2
42.5
43.3
41.9
41.8
44.5
Standard
Deviation
20.4
262
144
263
78.1
28.2
126
-
-
85.8
55.1
54.1
-
-
54.5
47.1
46.6
-
-
46.6
11.4
11.2
-
-
10.4
0.05
0.05
-
-
0.2
0.0
0.0
-
-
0.2
0.1
0.2
-
-
0.5
0.2
0.2
-
-
0.2
2.6
2.5
1.9
2.0
3.1
53
-------
Table 4-9. Analytical Results (Without Iron Addition)^ (Continued)
Parameter
Phosphorus
(asP)
TOC
Alkalinity
(as CaCO3)
Turbidity
pH
Temperature
DO
ORP
Sampling
Location
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
IN
AC
TA
TB
TT
Unit
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
NTU
NTU
s.u.
s.u.
s.u.
s.u.
s.u.
°c
°c
°c
°c
°c
mg/L
mg/L
mg/L
mg/L
mg/L
mV
mV
mV
mV
mV
Sample
Count
38
38
28
28
10
24
24
2
2
23
55
55
29
29
27
55
55
29
29
27
27
27
19
20
7
27
26
20
20
7
26
26
19
19
7
26
27
19
19
7
Concentration
Minimum
474
585
149
112
177
<1.0
1.0
1.2
1.2
<1.0
290
294
312
317
302
9.2
1.7
0.1
0.1
0.1
6.0
7.0
7.2
7.2
7.3
14.6
16.6
17.3
17.5
16.8
0.9
3.1
2.1
1.6
3.1
-6.7
140
207
213
247
Maximum
873
819
278
298
323
1.9
2.4
1.4
1.4
1.7
368
368
359
371
354
38.0
16.0
7.2
4.4
2.1
7.0
7.4
7.5
7.5
7.5
25.0
25.0
24.9
25.0
25.0
4.7
7.2
6.2
6.1
5.6
428
479
479
463
415
Average
648
714
199
199
225
.3
.4
.3
.3
.2
333
337
336
337
326
25.1
4.2
0.8
0.7
0.7
6.8
7.3
7.3
7.3
7.4
20.9
21.3
21.3
21.3
21.0
2.8
5.5
3.8
3.7
4.1
266
335
347
358
353
Standard
Deviation
94.8
51.6
27.7
34.2
43.5
0.4
0.3
0.1
0.1
0.4
14.1
17.1
11.2
11.8
15.6
5.6
2.7
1.3
0.8
0.5
0.2
0.1
0.1
0.1
0.1
2.5
2.3
2.0
2.0
3.2
0.8
0.8
1.2
1.4
1.0
188
93.0
87.5
78.2
70.3
(a) Excluding the event on August 5, 2010 (after piping to bypass aeralater had been installed).
4.5.1.1 Arsenic. Figure 4-30 presents the results of all 41 speciation events, including nine, 13, and
19 before, during, and after iron addition, respectively. As shown on the first bar chart (for samples
collected at the wellhead [IN]) and Tables 4-9 and 4-10, total arsenic concentrations in raw water ranged
from 24.1 to 43.0 |o,g/L and averaged 33.1 |o,g/L with 91% (on average) existing in the soluble form. Of
the soluble fraction, As(III) (scarlet on bar charts) was the predominant species with concentrations
ranging from 0.4 to 35.2 |o,g/L and averaging 24.2 |o,g/L. Low levels of As(V) (blue on bar charts) also
were present, ranging from <0.1 to 33.3 |o,g/L and averaging 5.9 |o,g/L. The range of total arsenic
54
-------
Table 4-10. Analytical Results (with Iron Addition)
Parameter
As (total)
As (soluble)
As
(paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn
(soluble)
P (as P)
Sampling
Location
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
Unit
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Sample
Count
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
13
3
3
3
Concentration
Minimum
28.5
18.7
5.6
28.3
2.5
4.7
0.1
7.7
0.2
1.6
0.3
0.2
0.5
1.7
3.9
1,768
701
<25
<25
<25
<25
107
106
76.3
109
90.8
76.4
726
779
108
Maximum
41.3
41.8
22.8
36.6
14.9
12.6
7.0
34.4
10.2
34.0
1.3
1.2
33.3
14.0
11.8
8,045
9,399
1,763
6,314
32.2
<25
195
170
156
199
155
157
832
1,718
172
Average
34.8
34.1
11.0
32.3
9.5
8.1
2.6
24.7
2.9
23.9
0.8
0.8
8.4
8.6
7.3
2,629
3,173
360
2,188
16.5
<25
130
129
116
133
117
117
787
1,106
143
Standard
Deviation
3.9
5.5
4.4
2.7
3.6
2.2
2.5
7.0
3.0
9.3
0.3
0.3
9.8
3.6
2.2
1,641
2,216
587
1,473
7.7
0.0
23.0
18.6
22.6
23.2
18.6
20.2
55.1
530
32.5
concentrations measured was slightly higher than that of historic data, i.e., 17.0 to 37.0 |o,g/L, as shown in
Table 4-1.
As shown on the second bar chart (for samples collected after the contact tank [AC]), KMnO4 was
effective in converting soluble As(III) to either soluble As(V) or particulate arsenic, with soluble As(V)
concentrations ranging from 6.9 to 16.2 |o,g/L and averaging 10.8 |o,g/L and particulate arsenic
concentrations ranging from 13.0 to 28.1 |o,g/L and averaging 20.4 |o,g/L. The high soluble As(V)
concentrations measured were contrary to what would be anticipated because of a high soluble iron to
soluble arsenic ratio (i.e., 1,998 |o,g/L:30.1 |o,g/L = 66.4 [see Tables 4-9 and 4-10]) in source water. In
fact, soluble As(V) concentrations at the AC location were found to be higher or close to the 10-|a,g/L
MCL during 16 of the 28 speciation events (whether KMnO4 or chlorine was used as an oxidant). The
rule of thumb was that soluble As(V) formed from soluble As(III) oxidation would be attached to iron
solids via adsorption and/or co-precipitation as long as the soluble iron concentration is at least 20 times
the soluble arsenic concentration (Sorg, 2002). The presence of high amounts of soluble As(V) in the
filter influent were not desirable because the Macrolite® media presumably would remove only particulate
arsenic, leaving soluble As(V) and residual soluble As(III) in the filter effluent. This was what prompted
55
-------
Arsenic Species at Wellhead (IN)
45
40
35
30
E 25
20
15
10
Date
Arsenic Species after Contact Tank (AC)
^i
a so
20
15
10
5
^ VMnn
with
Aeration)
.
•
< n
•
•
•^ Iron Addition >
•
•
KMnO4 /^
•
w
'oa
era
tTo"
i
-
0 l^-r"-
^^^^<^^/'^^^^^/\^^/'^^^^^^^f^f^s/>
-------
Arsenic Species After Filter Effluent Combined (TT)
Figure 4-30. Arsenic Speciation at IN, AC, and TT Sampling Locations (Continued)
the decision, made almost immediately after the treatment plant water sampling had begun, to add
supplemental iron to the inlet water to enhance arsenic removal.
On October 3, 2006, as much as 10.5 ug/L of soluble As(III) was measured after the contact tank,
presumably caused by an unusually low KMnO4 dosing rate as reflected by the low manganese
concentration, i.e., 361 ug/L [as Mn] or 1.0 mg/L [as KMnO4] measured in the same sample. The target
KMnO4 dosage was 2.6 mg/L (as KMnO4).
Due to concerns over biofouling in the media beds, gas chlorine was used to replace KMnO4 by late
January 2007. Immediately after the oxidant replacement, soluble As(III) concentrations at the AC
location increased to 4.4 and 3.2 (ig/L on January 30 and March 6, 2007. Incomplete soluble As(III)
oxidation might have been caused by the presence of ammonia (1.9 mg/L [as N]), which formed
chloramines with chlorine. Chloramines are known to react less effectively with As(III) (Frank and
Clifford, 1986; Ghurye and Clifford, 2001). Elevated As(III) concentrations did not reoccur after the
sampling event on March 6, 2007.
On October 5, 2009, as much as 27.0 ug/L of soluble As(III) was measured at the AC location. This
uncharacteristically high soluble As(III) concentration was thought to have been caused by the lack of
chlorine addition, although the operator did not report any irregularity during this study period. Because
the soluble iron concentration in the same sample also was unusually high (1,956 ug/L), malfunctioning
of the gas chlorine addition system most likely was the case. Aeration in the aeralater did not appear to
have oxidized much of the soluble iron either when comparing its concentration with that of total iron.
57
-------
No DO or ORP data were available to support or refute this. Onsite measurements for pH, temperature,
DO, and ORP were discontinued by the operator on April 30, 2007.
A number of factors potentially could affect soluble As(V) adsorption onto and co-precipitation with iron
solids. Competing anions, such as phosphorus and silica, could use up some adsorption sites.
Phosphorus concentrations in source water ranged from 474 to 873 ug/L (as P) and averaged 658 ug/L (as
P) (see Tables 4-9 and 4-10). Phosphorus concentrations at the AC location ranged from 585 to 819 ug/L
(as P) and averaged 714 ug/L (as P) (see Table 4-9). Although phosphorus concentrations at the AC
location were similar to those in source water, its concentrations were significantly reduced after
Macrolite pressure filters (to 199 and 225 ug/L [as P], on average, at the TA/TB and TT locations,
respectively). Silica concentrations in source water ranged from 38.4 to 49.3 mg/L (as SiO2) and
averaged 42.5 mg/L (as SiO2). Its concentrations at the AC, TA, TB, and TT locations remained
relatively constant at 43.3, 41.9, 41.8, and 44.5 mg/L (as SiO2). Based on the concentrations at the TA
and TB locations, some silica might have been removed along with iron solids, similar to what had
occurred for phosphorus.
The other factor that might have impacted soluble As(V) removal was aeration in the aeralater. Although
KMnO4 or chlorine was added to either the wellheads or the 6-in standpipe prior to the aeralater, some
soluble iron might have reached the aeralater and precipitated upon aeration. Based on field
measurements, DO concentrations at the wellhead were 2.8 mg/L (note that results of two special studies
conducted onsite showed <0.2 mg/L of DO at the wellheads); DO concentrations after the aeralater
increased significantly to 5.5 mg/L. According to the results of the same special studies, soluble As(V)
concentrations were reduced to below 5.9 mg/L after KMnO4 oxidation (with most converted to
particulate arsenic) if DO levels were kept at the wellhead levels (see Section 4.5.2.3).
Without supplemental iron addition, total arsenic concentrations following the pressure filters at the TA,
TB, and TT locations ranged from 1.4 to 28.5 ug/L and averaged 13.3 ug/L (Table 4-9 and Figure 4-31).
Arsenic existed primarily in the soluble form with concentrations ranging from 0.3 to 16.2 ug/L and
averaging 10.1 ug/L. As expected, soluble As(V) was the predominant species, with concentrations
ranging from <0.1 to 14.1 ug/L and averaging 9.0 ug/L (see the third bar chart in Figure 4-30) . It is
obvious that soluble As(V) must be converted to particulate arsenic before it can be removed by the
pressure filters. The amount of particulate arsenic was low, ranging from <0.1 to 9.8 ug/L and averaging
1.7 ug/L (light yellow on the bar chart). Elevated particulate arsenic concentrations usually were
associated with elevated particulate iron concentrations (see Appendix B for particulate arsenic and
particulate iron data at the TT location: 9.8 and 790 ug/L, respectively, on October 5, 2009; 7.8 and 732
ug/L, respectively, on October 13, 2009; and 8.5 and 1,037 ug/L, respectively, on January 5, 2010) and
thus iron leakage through the pressure filters.
The effect of iron addition was minimal, slightly decreasing the average soluble arsenic concentration
from 13.3 (without iron addition) to 9.5 ug/L (with iron addition) and average soluble As(V)
concentration from 10.8 (without iron addition) to 8.6 ug/L (with iron addition) at the AC location
(Tables 4-9 and 4-10 and the second bar chart in Figure 4-30). After the Macrolite® pressure filters, total
arsenic concentrations were reduced to 11.0 ug/L (on average), with 7.3, 0.8, and 2.9 ug/L existing as
soluble As(V), soluble As(III), and particulate arsenic. Although more soluble arsenic was converted to
particulate arsenic due to iron addition, extra solids loading to the pressure filters caused more particulate
arsenic to penetrate through the filters. As a result, little or no benefit was realized from the use of
supplemental iron.
4.5.1.2 Iron. Figure 4-32 presents three bar charts showing soluble and particulate concentrations
measured at the IN, AC, and TT locations. Total iron concentrations in source water ranged from 1,477
to 8,045 ug/L and averaged 2,168 ug/L, existing almost entirely in the soluble form. The amounts of
58
-------
Total Arsenic Concentrations
KMnO4
(with
Aeration)
CI2 (with Aeration)
A
•
As MCL 10 (jg/L
—•—At Wellhead (IN)
• After Chlorination (AC)
A After Combined Effluent (TT)
• After Tank A (TA)
• After Tank B (TB)
07/22/06
02/07/07
08/26/07
03/13/08
04/17/09
11/03/09
05/22/10
Figure 4-31. Total Arsenic Concentrations at IN, AC, TA, TB, and TT Sampling Locations
9,500
9,000
8,500
8,000
7,500
7,000
6,500
1 6,000
^ 5,500
o
is 5,000
1 4,500
0 4,000
u
£ 3,500
3,000
2,500
2,000
1,500
1,000
500
0
Soluble and Particulate Fe at Wellhead (IN)
^
*S^
n n
.
oV\^
s\<$>\<$\<$\<$\<$>N
i^K^%* x1^
1
*:
p.
•
.
,-,
• Fe soluble)
DFe(part culate
1
^^|4§^^^^^
Date
p.
-,
n
1
>? \P \^ \^ \^ \^ \^
^^^Vt^'T^V5
Figure 4-32. Soluble and Particulate Iron Across Treatment Train
59
-------
9,500
9,000
8,500
8,000
7,500
7,000
6,500
B) 6,000
~£ 5,500
o
is 5,000
«j 4,500
o 4,000
O
£ 3,500
3,000
2,500
2,000
1,500
1,000
500
4
Soluble and Participate Fe After Contact Tank (AC)
n _
1
< —
D
n
ron
Addit on
•
p.
i n n
> BFefsoluble
OFe(particulate
R n
1 n
1
1
• n
•
Date
Soluble and Participate Fe After Filter Effluent Combined (TT)
9 500
9,000
8,500
8,000
7,500
7,000
6,500
? 6,000
O)
3.
— 5,500
| 5,000
| 1,500
1 4,000
o
«) 3,500
3,000
2,500
2,000
1,500
1,000
500
- (with
aeration)
i-i
"
• n n
<£figti*K*g£*
"¥^
^
J
_...JLn
Date
KMnO4
(w/o aeration) '
• Fe(soluble)
• Fe(particulate)
n =
J*
/
^_m^
>
Figure 4-32. Soluble and Particulate Iron Across Treatment Train (Continued)
60
-------
soluble iron in source water were at least 66 times (on average) the amounts of soluble arsenic. This
soluble iron to soluble arsenic ratio was much higher than the 20:1 rule-of-thumb value needed for
effective arsenic removal via adsorption/co-precipitation with iron solids. This is why it became
suspicious that some soluble iron might, in fact, be precipitated via aeration, rendering it less effective in
turning soluble As(V) into arsenic-laden solids. An unusually high iron concentration of 8,045 |o,g/L
(with 6,314 |o,g/L existing in the soluble form) was measured on January 28, 2008 (see the first bar chart
in Figure 4-32). It was not clear what caused this to occur. Out of the 41 speciation events, the ones on
October 3, 2006, January 30, 2007, March 11, 2008, January 19, 2009, and October 5, 2009, had
particulate iron as the predominant species. This most likely was caused by aeration during sampling.
As expected, soluble iron was precipitated to become iron solids after oxidant addition/aeration in the
aeralater (see the second bar chart in Figure 4-32). On October 5, 2009, iron at the AC location existed
only as soluble iron. As discussed earlier, this most likely was caused by malfunctioning of the chlorine
addition system.
With iron addition, total iron concentrations varied from 701 to 9,399 |og/L and averaged 3,173 |og/L,
compared to 1,995 |o,g/L without iron addition. Increases in iron concentration occurred during three
sampling events on April 17, 2008, December 3, 2008, and March 13, 2009. As discussed in Section
4.4.2, iron dosages were not well controlled because of the use of an over-sized pump and a
corroding/dissolving impeller/mixer. Stratification of iron crystals in the chemical day tank very much
could have been a source of errors contributing to the erratic results.
Iron leakage could be seen in the filter effluent as shown in the third bar chart in Figure 4-32. With iron
addition, iron concentrations as high as 1,763 |o,g/L were measured (on March 13, 2009) in the filter
effluent. Because of continuing aeration and iron addition, the Macrolite® filters became increasingly
fouled and iron leakage became even more significant and frequent during the most of year 2009. This
was the reason for the flow dropping even with three consecutive acid washes (although the washes were
done with much less amounts of HC1 than recommended by the vendor) in March, July and October 2009.
Flowrates were "restored" only after rubber grommets in the flow restrictors were removed in October
2009. Iron addition discontinued in July 2009.
4.5.1.3 Manganese. Figure 4-33 presents three bar charts showing soluble and particulate
manganese concentrations measured at the IN, AC, and TT locations. Total manganese concentrations in
source water ranged from 96.2 to 196 |o,g/L and averaged 132 |o,g/L, existing almost entirely in the soluble
form (see Tables 4-9 and 4-10). Due to KMnO4 addition, manganese concentrations increased to as high
as 787 ug/L at the AC location during the first six speciation events (and the seventh event apparently
with the use of both KMnO4 and gas chlorine). KMnO4 reacted with reducing species in source water and
formed a significant amount of manganese solids, presumably MnO2, as shown by the blue bars in the
second bar chart. After KMnO4 was replaced with gas chlorine, manganese concentrations remained
relatively unchanged. Chlorine was not effective in oxidizing soluble manganese, as shown by the mostly
scarlet bars in the bar chart. Studies have found that incomplete oxidation of soluble Mn(II) occurs using
free chlorine at pH values less than 8.5 (Knocke et al., 1987 and 1990; Condit and Chen, 2006; McCall et
al., 2007).
Particulate manganese was removed by the pressure filters (see the third bar chart), leaving mostly soluble
manganese in the filter effluent. Four of the first six speciation events showed elevated soluble
manganese, probably caused by overdosing of KMnO4 or formation of colloidal manganese particles due
to the presence of TOC in source water.
61
-------
900
800
Soluble and Particulate Mn at Wellhead (IN)
DMn (Particulate)
• Mn (Soluble)
700
3- 600
o 500
1
| 400
o
O
1 300
200
100
0
_
HI [|j|j]
1
11
n
liiiliiu
in
li
i
i
^v\\<%%^
^44t4^
Date
900 r
800
700
2- 600
1
I 5°°
8 400
o
O
S 300
200
100
#1
Soluble and Particulate Mn After Contact Tank(AC)
K
f
Mn04
with
eratio
n)
CI2
with A
t
KMnO4 -^
^ Iron Add t
•
n
1
in
"\
m
HI
II
(w/o Aeration)
111111
OMn (Particulate)
• Mn (Soluble)
ll
11
|
1
>
/>^^^^^^^^>^>>^/>^>
M^^^W^^^^/^^^^^W^W^MM^^^
Date
Figure 4-33. Soluble and Particulate Manganese Concentrations Across Treatment Train
62
-------
Soluble and Particulate Mn After Filter Effluent Combined (TT)
700
300
200
100
KMnO,
"(with
Aeration)
CI2 (with Aeration)
KMnO, —'
(w/o Aeration)
Iron Addition
Figure 4-33. Soluble and Particulate Manganese Concentrations Across Treatment Train
(Continued)
4.5.1.4 pH, DO, and ORP. pH, temperature, DO, and ORP were measured after system startup
through April 17, 2007. Based on the data collected, pH values of source water ranged from 6.0 to 7.0
and averaged 6.8 (Table 4-9). This pH range was somewhat lower than that measured historically (see
Table 4-1) and was ideal for arsenic adsorption onto iron solids. DO levels in source water ranged from
0.9 to 4.7 mg/L and averaged 2.8 mg/L. This average value was much higher than the DO levels
measured during the first several sampling events, i.e., 1.5, 0.9, 2.2, and 1.7 mg/L on August 10, August
15, August 22, and August 29, 2006, respectively. Higher DO levels measured most likely were caused
by aeration during sampling and measurements. Similar to DO, ORP readings taken during the first
several events were much lower than the average value (266 mV) measured during the entire sampling
period. For example, -2.7, -6.7, 6.1, 5.4, 3.1, and 5.7 mV were measured during the first six of seven
sampling events. Aeration again was thought to be the main contributing factor for the high readings.
Great caution must be taken during DO and ORP measurements, although the project team did experience
frequent malfunctioning of DO probes and excessive drifting when taking ORP measurements at this and
a large number of other arsenic demonstration sites.
After oxidant addition and the aeralater, the average pH value increased to 7.3 but remained constant
across the pressure filters. DO levels increased significantly to an average of 5.5 mg/L, indicating
aeration. After the blower in the aeralater were turned off, DO levels remained elevated at 2.4 to 3.4
mg/L, indicating continuing aeration (but at a lesser extent). As noted earlier, aeration might have
adversely affected soluble As(V) removal by iron solids. No routine DO measurement was made after the
aluminum trays had been removed and the standpipe in the aeralater was cut in July 2009. Therefore, the
effect of this action was not clear. However, the DO measurements performed during the January 2010
special study indicated an elevated DO level of 2.4 mg/L at the AC location. After the aeralater was
63
-------
bypassed, the DO level was reduced to 0.5 mg/L. Results of this special study are discussed in detail in
Section 4.5.2.2.
4.5.1.5 Ammonia and Nitrate. As shown in Table 4-9, ammonia concentrations ranged from 1.5 to
2.2 mg/L (as N) and averaged 1.9 mg/L (as N). Ammonia concentrations were reduced to 1.7 and 1.4
mg/L (as N) at the AC and TT locations, respectively. Nitrification and/or chlorination were primarily
responsible for the concentration reduction. Before gas chlorine was used to replace KMnO4 by the end
of January 2007, nitrification was the only process consuming ammonia. Ammonia concentrations were
reduced from 2.0 mg/L (as N), on average, at the wellhead to 1.8 mg/L (as N), on average, after the
aeralater. After the pressure filters, its concentrations were further reduced to 0.9 mg/L (as N), on
average.
With the blower on, nitrification was active seven weeks into system operation, as evidenced by a lower
ammonia concentration, i.e., 1.3 mg/L (as N), in the filter effluent on August 10, 2006 (see Figure 4-34).
Ammonia concentrations after the filters were further reduced to 1.1, 0.6. 0.5, and 0.8 mg/L (as N) by
September 6, October 3, November 7, and December 5, 2006, respectively. This was when the backwash
frequency increased to as many as eight times per day and an acid and a caustic wash were recommended
by the vendor. At this point, nitrate concentrations had increased to 0.6 mg/L (as N). The increase in
nitrate concentration, however, was less than the stoichiometric amount.
After the acid and caustic washes, biological activities apparently were under control, as reflected by the
essentially "constant" level of ammonia (i.e., 1.5, 1.7, and 1.7 mg/L [as N]) and less than the MDL of
nitrate (0.05 mg/L [as N]) across the treatment train. To curb biofouling, gas chlorine was used to replace
KMnO4 by the end of January 2007, and the blower was turned off by March 2007. From late January
through April 30, 2007, when the routine sampling was temporarily discontinued, ammonia levels were
reduced, on average, from 1.9 mg/L (as N) at the wellhead to 1.7 mg/L (as N) after the aeralater, and then
to 1.4 mg/L (as N) after the filters. Assuming that the 0.2 mg/L (as N) of concentration reduction (from
1.9 down to 1.7 mg/L [as N]) was caused by chlorination, the 0.3-mg/L (as N) reduction across the filters
could have been caused, again, by nitrification (note that 0.1 mg/L of nitrate [as N] was measured on
April 10, 2007). The extent of nitrification, if any, definitely was much less significant than before.
After the aluminum tray was removed and standpipe was cut in July 2009, ammonia concentration
reduction was observed only across the aeralater (i.e., from 2.0 mg/L [as N] at the wellhead to 1.7 mg/L
[as N] after the aeralater), presumably caused by chlorination. Ammonia concentrations remained
unchanged at 1.7 mg/L (as N) after the filters. Therefore, little or no nitrification would occur at this
point. Nitrate concentrations measured in this study period were either less than the MDL or at 0.1 mg/L
(as N).
4.5.1.6 Other Water Quality Parameters. Hardness, fluoride, sulfate, silica, TOC, and alkalinity
levels remained constant across the treatment train and were not affected by the treatment process
(Table 4-9). Phosphorus levels after the aeralater, which were slightly higher than the average raw water
concentration of 648 |og/L (possibly due to trace quantities in the pretreatment chemicals), decreased to an
average of 225 |o,g/L after the pressure filters (see discussion in Section 4.5.1). Turbidity also decreased
significantly with treatment (i.e., from 25.1 NTU in source water to 0.7 NTU after the TT location).
4.5.2 Special Studies. Several special studies were conducted to attempt to improve system
performance during the performance evaluation study. Results of these studies are discussed in detail
below.
64
-------
Ammonia Across Treatment Train
Ammonia (IN)
Ammonia (AC)
Ammonia (IT)
Date
Figure 4-34. Ammonia Concentrations Across Treatment Train
4.5.2.1 Filter Run Length Studies. Three filter run length studies were performed. The first was
conducted on November 19, 2007, before the implementation of supplemental iron addition. The test run
was short (3.2 hr), with 11.4 to 12.9 ug/L of soluble arsenic but less than the MDL of particulate iron in
the filter effluent.
After iron addition had begun, a second filter run length study was conducted on May 29, 2008. The
results showed no As(III) oxidation nor arsenic-laden iron solids removal based on total and soluble
arsenic and iron data, apparently caused by a problem with the chlorine addition system.
A repeat run length study was conducted on October 20, 2008, but the results indicated that iron dosage
was too low due to an on-going problem with the mixing equipment, which continued to corrode and
dissolve. No additional run length studies were attempted after the three rather unsuccessful tests.
4.5.2.2 Aeralater Bypass Test. Aeration in the aeralater might have caused ineffective soluble As(V)
removal by iron solids using either KMnO4 or chlorine. For the IR process to be effective, iron must be
precipitated in the presence of soluble As(V), as this induces co-precipitation and/or adsorption of soluble
As(V) and forms arsenic-laden iron particles prior to filtration. Although KMnO4 or chlorine was added
just before water entered the aeralater, soluble iron and soluble As(III) could still exist as water exited the
standpipe. This might result in precipitation of soluble iron and contact of iron solids with soluble As(V)
and soluble As(III), thus hindering the adsorption/co-precipitation process.
65
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To verify the adverse effect of aeration, the aeralater was bypassed by diverting well water directly to the
pressure filters after chlorination. Samples were taken at the AC sampling location for DO and arsenic
speciation measurements. It was postulated that bypassing the aeralater would eliminate aeration, thus
decreasing soluble As(V) concentrations and increasing particulate arsenic concentrations prior to the
pressure filters. However, the presence of ammonia could skew the results due to formation of
chloramines, which were less effective in oxidizing soluble As(III) and soluble Fe(II).
Table 4-11 compares results of the samples taken before and after aeralater bypass. As measured during
the initial site visit on November 3, 2004 and the first several sampling events after system startup, source
water was highly reducing, with an ORP reading of -42 mV and a DO concentration of 0.1 to 0.2 mg/L
(note the method of source water sample collection in Section 3.4.2.1). Before aerator bypass, water
taken at the AC location contained 2.4 mg/L of DO, indicating aeration despite removal of the aluminum
trays and shortening of the standpipe. The ORP reading increased, as expected, to as high as 483.0 mV
due to chlorination. About 0.9 mg/L of total chlorine (as C12) was measured, presumably existing as
chloramines. This level of total chlorine was acceptable for protection of the synthetic zeolite in the
downstream softening unit.
Table 4-11. Results of Samples Taken Before and After Aeralater Bypass
Analytes
pH
Temperature
DO
ORP
Total Chlorine (as C12)
NH3 (as N)
As (total)
As (soluble)
As (particulate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Unit
S.U.
°c
mg/L
mV
mg/L
mg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Hg/L
Sampling Locations
IN
Before
6.9
20.9
0.1
-42
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
After
NA
NA
0.2
-42.4
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
AC
Before
7.1
20.8
2.4
483
0.9
1.1
29.5
11.8
17.7
0.9
10.9
1,824
33.2
109
111
After
6.9
20.3
0.5
327
1.6
0.9
29.8
12.5
17.3
0.5
12.0
1,943
45.6
113
103
TT
Before
7.2
20.8
3.8
406
0.8
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
After
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
DO = dissolved oxygen; NA = not available; ORP = oxidation-reduction potential
Metals analyses for samples taken at the AC location before aerator bypass showed 29.5 (ig/L of total
arsenic with about one third (11.8 (ig/L) present as soluble arsenic. Of the soluble arsenic fraction, most
(10.9 (ig/L) was present as As(V), similar to what had been observed during the entire study period. This
soluble fraction was not removed by the filters and was in the filter effluent. As expected, manganese
existed entirely in the soluble form.
After aeralater bypass, DO in water sampled from the AC location remained low (0.5 mg/L). Contrary to
what would be anticipated, the low DO level did not result in a lower level of soluble arsenic or As(V)
(which were measured at 12.5 and 12.0 (ig/L, respectively). It was not clear if the formation of
chloramines had played a role on these unexpected results. Additional examination on jar test results
would be needed to verify these results.
66
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4.5.2.3 Jar Tests. Tables 4-12 and 4-13 present results of optimal oxidant dose and arsenic and iron
removal tests, respectively. Figure 4-35 shows arsenic speciation results obtained during the arsenic and
iron removal tests. The use of 2.2 to 7.1 mg/L NaOCl (as C12) left 0.8 to 3.9 mg/L (as C12) of residual in
glass jars after 20 min of contact time, indicating a demand of 1.4 to 3.2 mg/L (as C12). The increasing
chlorine demand was contrary to the assumption that a finite and consistent amount of reducing species
existed in raw water. At higher chlorine doses, more chlorine may react with TOC in water, thus
resulting in higher chlorine demands. However, reactions between chlorine and TOC may or may not
result in lower TOC levels in the treated water.
To protect the downstream synthetic zeolite in the softening unit, the 2.2-mg/L (as C12) dose was selected
for the follow-on arsenic and iron removal jar test (because it resulted in a residual level below 1.0 mg/L
[as C12] as shown in Table 4-12). However, after 20 min of contact time, only 0.1 mg/L (as C12) of
residual was measured in the glass jar (see Table 4-13). This, in conjunction with the high levels of
soluble arsenic (22.3 (ig/L), soluble As(III) (4.8 (ig/L), and soluble iron (730 (ig/L), suggest that the 2.2-
mg/L (as C12) dose was not enough to react with all reducing species in the water tested. As shown in
Table 4-13, more than 2.1 mg/L of total iron (existing entirely as soluble iron) was present in water
collected for the NaOCl jar test and more than 2.6 mg/L of total iron present in water for the KMnO4 jar
tests (raw water quality not measured). Water quality apparently had changed during the 2-day study
period, thus causing insufficient addition of chlorine during the jar test.
Table 4-12. Jar Test Results for Optimal Oxidant Doses
Oxidant
NaOCl
KMnO4
Dose
(mg/L)
0.0
2.2
4.2
7.1
0.00
1.9
4.2
6.6
Contact
Time
(min)
20
20
20
20
20
20
20
20
Residual
Oxidant
(mg/L)
0
0.8
2.3
3.9
0.00
0.9
2.8
5.0
Oxidant
Demand
(mg/L)
NA
1.4
1.9
3.2
NA
1.0
1.4
1.6
NA = not applicable
As shown in Table 4-13, TOC levels remained unchanged at 1.4 mg/L during the NaOCl jar test.
Manganese levels also remained constant. Ammonia levels increased from 1.3 to 1.6 mg/L (as N). There
is no plausible explanation for such an increase, and analytical errors may be the only probable cause.
DO levels remained low at 1.0 mg/L (versus 0.9 mg/L in raw water); DO levels in the KMnO4 jars also
remained low at 1.1 to 1.2 mg/L. These, together with the presence of only soluble iron in raw water,
suggest that the water collection method adequately preserved raw water quality during the study period.
The KMnO4 demand study used 1.9, 4.2. and 6.6 mg/L of KMnO4 (as KMnO4) in three separate jars. As
shown in Table 4-12, KMnO4 residual levels ranged from 0.9 to 5.0 mg/L, reflecting a demand of 1.0 to
1.6 mg/L (as KMnO4). This demand was somewhat lower than the amounts (from 1.6 to 2.2 mg/L)
measured during the follow-on jar tests, probably because of the lower iron level in raw water (i.e., 2.1
versus 2.6 mg/L). In the presence of ammonia, KMnO4 is a stronger and more effective oxidant than
NaOCl because NaOCl reacts with ammonia to form chloramines.
67
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Table 4-13. Jar Test Results for Arsenic and Iron Removal
Analytes
Unit
Contact Time
pH
Temperature
DO
ORP
Residual Oxidant
Oxidant Demand
NH3 (as N)
TOC
As (total)
As (soluble)
As (paniculate)
As(III)
As(V)
Fe (total)
Fe(soluble)
Mn (total)
Mn (soluble)
S.U.
°c
mg/L
mV
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Oxidant Dosage
NaOCl
0
20
7.4
19.5
0.9
-42
0
NA
1.3
1.4
29.9
30.8
0.0
29.7
1.1
2,117
2,111
121
126
2.2
20
7.0
19.5
1.0
63
0.1
>2.1
1.6
1.4
30.7
22.3
8.4
4.8
17.5
2,150
730
122
123
KMnO4
0
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
NM
1.9
20
7.0
19.6
1.2
237
0.3
1.6
1.2
1.4
31.0
7.4
23.6
1.5
5.9
2,677
<25
951
178
4.2
20
7.1
19.8
1.2
373
2.4
1.7
1.2
1.2
28.1
6.2
21.9
0.7
5.5
2,654
<25
1,926
426
6.6
20
7.1
19.9
1.1
463
4.4
2.2
1.1
1.1
29.1
6.6
22.5
0.9
5.7
2,663
<25
2,746
1,133
DO = dissolved oxygen; NA =
oxidation-reduction potential;
= not available; NM = not measured; ORP =
TOC = total organic carbon
40.0
35,0
5.0
0.0
Baseline NaOCl @ 2.2 mg/L KMnCM <6> 1.88 mg/L KMnCM 4.15 mg/L KMnCW (ffl 6.61 mg/L
Figure 4-35. Arsenic Speciation Results for Samples Collected During Jar Tests
68
-------
After 20 min of contact time, KMnO4 reduced soluble arsenic, soluble As(III), and soluble As(V) to
levels below 7.4, 1.5, and 5.9 (ig/L, respectively. Soluble iron was converted in its entirety to arsenic-
laden iron solids, which can be removed by the Macrolite filters. As expected, ammonia concentrations
remained constant at 1.1 to 1.2 mg/L, since it does not react with KMnO4. TOC levels were reduced
somewhat, from 1.4 to 1.1 mg/L, as the KMnO4 dosage increased from 1.9 to 6.6 mg/L.
Two key issues related to the use of KMnO4 involved selecting and maintaining an initial dose and coping
with changing water quality. With 2.6 mg/L of iron, 1.5 mg/L of KMnO4 (as KMnO4) would be
recommended, assuming that raw water would bypass the aeralater. Because TOC levels in raw water
were marginally elevated, the need to increase KMnO4 dose to "overcome" the TOC effect, as discussed
in Section 2.3, might not exist. Also, overdosing KMnO4 would impart pink color to and elevated
manganese levels in the filter effluent. Any untreated soluble Mn(II) might be removed by the
downstream synthetic zeolite.
4.5.2.4 Filter Run Length Study During January 2010 Site Visit. Figure 4-36 shows a time-series
plot of arsenic, iron, and manganese breakthrough from Tank A, along with flowrate (Q) and Ap data
shown next to the iron data points. Also present on the plot are horizontal lines indicating the arsenic
MCL (10 (ig/L), manganese SMCL (50 (ig/L), and iron SMCL (300 (ig/L).
Total arsenic was measured at 14.8 (ig/L before the first hour of filter runtime, with most of the
concentration (13.1 (ig/L) present in the soluble form. Total arsenic concentrations decreased slightly
over the next 5 hr, with concentrations ranging from 11.6 to 12.4 (ig/L. Particulate arsenic concentrations
remained relatively constant and ranged from 1.1 to 2.2 (ig/L. The quick breakthrough was obviously
caused by the fact that arsenic existed primarily in the soluble form before entering the filters.
Total iron was measured at 270 (ig/L after the first hour of filter runtime. In contrast to the breakthrough
of arsenic, almost all of the iron was in the particulate form. Total manganese was measured above the
SMCL of 50 (ig/L after the first hour of filter runtime. This was to be expected, as all of the manganese
present after chlorination was in the soluble form. Manganese measured throughout the run-length study
ranged from 116 to 121 (ig/L, all of which was present in the soluble form.
The poor filter performance was expected because most arsenic that broke through from the filters existed
as soluble arsenic and because iron particles prematurely broke through the filter beds most likely due to
bio- and iron fouling of the filter media and shallow bed depths of the filters. The result of this run length
study was consistent with what was observed during the performance evaluation study.
4.5.3 Backwash Wastewater Sampling. Table 4-14 presents analytical results of six backwash
wastewater sampling events taking place prior to implementation of iron addition. Concentrations of
TDS and total suspended solids (TSS) ranged from 326 to 474 mg/L and from 18 to 234 mg/L,
respectively. Concentrations of total arsenic, iron, and manganese ranged from 110 to 468 |o,g/L, from
13.8 to 74.0 mg/L, and from 592 to 3,689 |og/L, respectively. As expected, these metals existed primarily
in the particulate form. Average concentrations of particulate arsenic, iron, and manganese were 218
Hg/L, 31.8 mg/L, and 1,464 |og/L, respectively. Assuming that these average particulate results existed
during the production of 6,752 gal of wastewater per backwash event, approximately 0.01 Ib of arsenic,
1.8 Ib of iron, and 0.08 Ib of manganese would be disharged during each backwash event. Using the
average TSS concentration (87.8 mg/L), the total amount of solids discharged would be 4.9 Ib. For all
events, the backwash wastewater had a pH of 7.8 to 8.0.
69
-------
400
350
250
100
3 4
Elapsed Time (hr)
Figure 4-36. Arsenic, Iron, and Manganese Breakthrough During Filter Run-length Study
4.5.4 Distribution System Water Sampling. Table 4-15 summarizes the results of the
distribution system sampling events. The water quality was similar among the three residences except for
copper at the DS1 and DS3 residences, which exhibited higher concentrations than the other residence.
After the treatment system began operation, arsenic concentrations remained essentially unchanged from
the average baseline level of 15.6 |o,g/L to 15.3 |o,g/L. Iron and manganese concentrations increased
slightly from baseline levels of <25 and 65.3 |o,g/L to 47.2 and 96 |o,g/L, respectively. Alkalinity, pH, and
lead concentrations also increased slightly from average baseline levels of 296 mg/L (as CaCO3), 7.1
S.U., and 0.4 |o,g/L to 333 mg/L (as CaCO3), 7.4 S.U., and 0.8 ng/L, respectively. Copper concentrations
increased rather significantly from the average baseline level of 108 |o,g/L to 267 |og/L, due mainly to four
>1,000 |og/L hits, including one over the l,300-|o,g/L action level (1,317 ng/L). Otherwise, the water in
the distribution system was comparable to that of the treatment system effluent. Thus, the treatment
system appeared to have no beneficial effects on arsenic, manganese, and iron concentrations of the
distribution system 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 cost for
equipment, site engineering, and system installation, shakedown, and startup. O&M cost included cost
for chemicals, electricity, and labor. Cost associated with the building including the sump, sanitary sewer
connections, and water system telemetry was not included in the capital cost because it was not included
in the scope of this demonstration project and was funded separately by United Water Systems.
70
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Table 4-14. Backwash Wastewater Sampling Test Results
Sampling
Event
No.
1
2
3
4
5
6
Date
09/19/06
10/31/06
01/15/07
02/14/07
02/26/07
03/25/07
BW1
Vessel 4
D.
s.u.
7.5
7.2
7.5
7.6
7.7
7.5
H
mg/L
470
392
360
360
340
392
VI
VI
mg/L
56
65
45
32
136
234
4s (total)
Hg/L
110
165
213
137
279
468
4s (soluble)
Hg/L
17.5
13.0
16.4
24.6
19.8
14.8
U
&
X
Hg/L
72.5
152
197
113
259
453
1
Hg/L
14,232
19,391
28,167
15,439
35,973
73,957
S
1
Hg/L
33.8
54.7
59.9
52.3
<25
<25
f
|
Hg/L
1,312
3,689
1,334
592
956
1,965
Mn (soluble)
Hg/L
119
126
32.1
58.8
87.8
86.9
BW2
Vessel B
X
S.U.
7.4
7.3
7.4
7.5
7.8
7.5
H
mg/L
474
410
374
362
326
400
VI
VI
mg/L
48
50
18
102
113
154
4s (total)
Hg/L
114
128
224
225
418
348
4s (soluble)
Hg/L
18.9
13.6
15.6
28.3
19.0
14.8
U
&
X
Hg/L
95.5
114
208
197
399
363
1
Hg/L
14,373
13,779
29,562
26,083
59,262
51,976
S
1
Hg/L
56.7
81.2
68.4
22.8
<25
<25
Mn (total)
Hg/L
1,222
2,732
1,446
896
1,308
1,222
^
1
1
Hg/L
134
145
86.5
52.0
95.4
88.1
TDS = total dissolved solids; TSS = total suspended solids
-------
Table 4-15. Distribution System Sampling Results
No. of
Sampling
Events
BL1
BL2
BL3
BL4
1
2
3
4
5
6
7
8
Address
Sample
Type
Flushed/
1st Draw
Sampling
Date
08/03/05
-------
4.6.1 Capital Cost. The capital investment for the FM-284-AS system was $427,407 (Table 4-16).
The equipment cost was $281,048 (or 66% of the total capital investment), which included cost for two,
84-in x 96-in steel pressure vessels and associated distributors, 150 ft3 of Macrolite® media, process
valves and piping, air scour system, chemical feed, instrumentation and controls, turbidimeter, and
additional sample taps and totalizer/meters, shipping, labor, and system warranty. The system warranty
covered the cost for repair and replacement of defective system components and installation workmanship
for 12 months after system startup.
Table 4-16. Capital Investment for Kinetico's FM-284-AS System
Description
Cost
% of Capital
Investment Cost
Equipment
Welded Stainless Steel Frame
84-in x 96-in Steel Pressure Vessels
Wedge Wire Distributors - 84 in Vessels
Macrolite® Media (150 ft3)
Process Valves and Piping
Air Scour System
Chemical Feed System
Instrumentation and Controls
Turbidimeter
Additional Sample Taps and Totalizers/Meters
Labor
Freight
Equipment Total
$13,951
$59,579
$16,543
$37,500
$47,797
$9,830
$6,750
$18,556
$6,612
$1,700
$54,824
$7,406
$281,048
-
-
-
-
—
—
—
—
66%
Engineering
Labor
Subcontractor
Engineering Total
$44,520
$6,250
$50,770
—
—
12%
Installation, Shakedown, and Startup
Labor
Subcontractor
Travel
Installation, Shakedown, and Startup
Total Capital Investment
$90,804
$0
$4,785
$95,589
$427,407
—
—
—
22%
100%
The site engineering cost covered the cost for preparing the required permit application submittal,
including a process design report, a general arrangement drawing, piping and instrumentation diagrams,
electrical diagrams, interconnecting piping layouts, tank fill details, and a schematic of the PLC panel,
and obtaining the required permit approval from LADFiFi/OPH. The engineering cost of $50,770 was
12% 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. All activities were performed by the vendor with the operator's
assistance. The installation, startup, and shakedown cost of $95,589 was 22% of the total capital
investment.
The total capital cost of $427,407 was normalized to $555/gpm ($0.38/gpd) of design capacity using the
system's rated capacity of 770 gpm (or 1,108,800 gpd). The total capital cost also was converted to an
73
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annualized cost of $40,343 gal/yr using a capital recovery factor (CRF) 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 770 gpm to produce 404,712,000 gal/yr, the unit capital cost would be $0.10/1,000 gal.
During the four-year study period, the system average daily demand was 277,128 gal, or 101,151,720 gal
annually, so the unit capital cost increased to $0.40/1,000 gal.
A 53 ft x 25 ft pre-engineered metal building with a roof height of 16 ft was installed by United Water
Systems to house the treatment system (Section 4.3.2). The cost of the building and supporting utilities
was not included in the capital investment.
4.6.2 O&M Cost. O&M costs included chemical usage, electricity consumption, and labor as
shown in Table 4-17. Three chemicals were used for treatment, including chlorine, KMnO4, and FeCl3.
Since chlorination already existed prior to the demonstration study, its incremental cost for pre- and/or
post-treatment was not tracked during the study. Addition of FeCl3 was implemented from December
2007 through July 2009. However, the effect of iron addition was inconclusive due to erratic FeCl3
dosage and aeration in the aeralater; the addition was terminated in July 2009. Thus, there was no need to
include FeCl3 addition in the cost analysis. KMnO4 had been used since system startup through the end
of January 2007 and its use resumed after the aeralater was bypassed in April 2010. Based on the average
KMnO4 dosage of 1.8 mg/L used in the study and a unit cost of $1.98/lb, the KMnO4 usage was estimated
to be $0.03/1,000 gal.
Table 4-17. O&M Costs for Kinetico's FM-284-AS System
Category
Annual Volume Processed
(gal x 106)
Value
101
Remarks
Based on daily demand of 277, 128 gal for study
period from 07/17/06 through 09/16/10
Chemical Usage
Chlorine Cost ($/l,000 gal)
FeCl3 Cost ($/l,000 gal)
KMnO4 Consumption (lb/1,000 gal)
Chemical Cost ($/l,000 gal)
NA
NA
0.015
0.03
Existed prior to the demonstration study
Inconclusive; terminated in July 2009
Based on an average dosage of 1.8 mg/L
Based on a unit cost of $1.98/lb
Electricity Consumption
Electricity Cost ($/l,000 gal)
Negligible
Labor
Labor (hr/week)
Labor Cost ($/l,000 gal)
Total O&M Cost ($/l,000 gal)
2.5
$0.04
$0.07
30 min/day, 5 day/week
Labor rate = $30/hr
Electrical power consumption associated with the chemical feed system was assumed to be negligible.
The routine, non-demonstration related labor activities consumed 30 min/day, five days a week. Based on
this time commitment and a labor rate of $30/hr, the labor cost was $0.04/1,000 gal of water treated. In
sum, the total O&M cost was estimated to be $0.07/1,000 gal. It should be noted that this low O&M cost
did not include any costs associated with the extensive system troubleshooting by the operator, such as
performing the acid/caustic wash of the fouled media, replenishing the Macrolite® media, and modifying
the existing aeralater piping configuration.
74
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5.0 REFERENCES
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in the Presence of Ammonia and Bromide." Environ. Sci. Technol, 18:781-786.
Battelle. 2004. Quality Assurance Project Plan for Evaluation of Arsenic Removal Technology.
Prepared under Contract No. 68-C-00-185, Task Order No. 0029, for U.S. Environmental
Protection Agency, National Risk Management Research Laboratory, Cincinnati, OH.
Battelle. 2006. System Performance Evaluation Study Plan: U.S. EPA Demonstration of Arsenic
Removal Technology Round 2 at United Water Systems, Inc. in Arnaudville, LA. Prepared under
Contract No. 68-C-00-185, Task Order No. 0029, for U.S. Environmental Protection Agency,
National Risk Management Research Laboratory, Cincinnati, OH.
Bougeard, C.M., E.H. Goslan, B. Jefferson, and S.A. Parsons. 2010. "Comparison of the Disinfection
By-product Formation Potential of Treated Waters Exposed to Chlorine and Monochloramine,"
Water Research, 44: 729-740.
Chen, A.S.C., A.M. Paolucci, B.J. Yates, and L. Wang. 2011. Arsenic Removal from Drinking Water by
Coagulation/Filtration, U.S. EPA Demonstration Project at Village of Waynesville, IL, Final
Performance Evaluation Report. Report 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., W.E. Condit, B.J. Yates, and L. Wang. 2010a. Arsenic Removal from Drinking Water by
Iron Removal, U.S. EPA Demonstration Project at Sabin, MN, Final Performance Evaluation
Report. EPA/600/R-10/033. U.S. Environmental Protection Agency, National Risk Management
Research Laboratory, Cincinnati, OH.
Chen, A.S.C., G.M. Lewis, L. Wang, and A. Wang. 2010b. Arsenic Removal from Drinking Water by
Coagulation/Filtration, U.S. EPA Demonstration Project at Town ofFelton, DE, Final
Performance Evaluation Report. EPA/600/R-10/039. U.S. Environmental Protection Agency,
National Risk Management Research Laboratory, Cincinnati, OH.
Chen, A.S.C., L. Wang, T.J. Sorg, and A.M. Paolucci. 2010c. "Design and Operation of Arsenic
Removal Systems Treating High TOC and Ammonia Waters," Paper presented at the Seventh
Annual EPA Drinking Water Workshop in Cincinnati, OH.
Chen, A.S.C., L. Wang, and W.E. Condit. 2009. Arsenic Removal from Drinking Water by Iron
Removal, U.S. EPA Demonstration Project at Vintage on the Ponds in Delavan, WI, Final
Performance Evaluation Report. EPA/600/R-09/066. 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.
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Research Laboratory, Cincinnati, OH.
Clark, J.W., W. Viessman, and M.J. Hammer. 1977. Water Supply and Pollution Control. IEP, aDun-
Donnelley Publisher, New York, NY.
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Condit, W.E. and A.S.C. Chen. 2006. Arsenic Removal from Drinking Water by Iron Removal, U.S. EPA
Demonstration Project at Climax, MN, Final Performance Evaluation Report. EPA/600/R-
06/152. U.S. Environmental Protection Agency, National Risk Management Research
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Edwards, M., S. Patel, L. McNeill, H. Chen, M. Frey, A.D. Eaton, RC. Antweiler, and H.E. Taylor.
1998. "Considerations in As Analysis and Speciation." J. AWWA, 90(3): 103-113.
EPA. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic.
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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.
Frank, P.L. and D.A. Clifford. 1986. Arsenic (III) Oxidation and Removal from Drinking Water.
EPA/600/S2-86/021. U.S. Environmental Protection Agency, National Risk Management
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Ghurye, G.L. and D.A. Clifford. 2001. Laboratory Study on the Oxidation of Arsenic III to Arsenic V.
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Knocke, W.R., J.E. Van Benschoten, M. Kearney, A. Soborski, and D.A. Reckhow. 1990. "Alternative
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OH, Six-Month Evaluation Report. EPA/600/R-07/016. U.S. Environmental Protection Agency,
National Risk Management Research Laboratory, Cincinnati, OH.
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Removal by Ferric Chloride." Water Research, 34(4): 1255-1261.
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Removal by Iron Hydroxides." Toxicology Letters, 133(1): 103-111.
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Centre, MN, Final Performance Evaluation Report. EPA/600/R-09/013. U.S. Environmental
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Surfaces." Journal of Water Supply: Research and Technology -AQUA,54(4): 201-211.
Sorg, T.J. 2002. "Iron Treatment for Arsenic Removal Neglected." Opflow, 28(11): 15.
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by Coagulation/Filtration, U.S. EPA Demonstration Project at Village ofPentwater, MI, Final
Performance Evaluation Report. EPA/600/R-08/011. U.S. Environmental Protection Agency,
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77
-------
APPENDIX A
OPERATIONAL DATA
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet
Week
No.
0
0
1
2
3
4
5
6
7
8
Day of
Week
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Wed
Thu
Fri
Sun
Mon
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Wed
Thu
Fri
Sun
Date
07/1 7/06
07/1 8/06
07/19/06
07/20/06
07/21/06
07/23/06
07/24/06
07/26/06
07/28/06
07/29/06
07/30/06
07/31/06
08/01/06
08/02/06
08/03/06
08/04/06
08/05/06
08/06/06
08/07/06
08/08/06
08/10/06
08/11/06
08/12/06
08/13/06
08/14/06
08/15/06
08/17/06
08/18/06
08/19/06
08/21/06
08/22/06
08/23/06
08/24/06
08/25/06
08/27/06
08/28/06
08/29/06
08/30/06
08/31/06
09/01/06
09/02/06
09/03/06
09/04/06
09/06/06
09/07/06
09/08/06
09/10/06
09/11/06
09/13/06
09/14/06
09/15/06
09/16/06
09/18/06
09/19/06
09/20/06
09/21/06
09/22/06
09/23/06
09/24/06
09/27/06
09/28/06
09/29/06
10/01/06
Time
7:33 AM
10:23 AM
8:30 AM
7:50 AM
7:03 AM
9:47 AM
NR
10:00 AM
9:00 AM
7:30 AM
7:30 AM
7:10AM
7:20 AM
7:26 AM
7:27 AM
7:55 AM
8:40 AM
9:30 AM
7:20 AM
7:30 AM
1 1 :46 AM
7:33 AM
9:00 AM
10:46 AM
7:03 AM
7:04 AM
8:00 AM
7:30 AM
7:00 AM
7:03 AM
7:11 AM
7:09 AM
7:14 AM
6:55 AM
9:00 AM
6:54 AM
7:08 AM
6:53 AM
6:56 AM
7:03 AM
8:58 AM
9:21 AM
8:35 AM
7:05 AM
6:58 AM
7:00 AM
7:05 AM
6:59 AM
7:20 AM
6:59 AM
6:57 AM
10:00 AM
7:42 AM
7:08 AM
4:25 AM
7:03 AM
7:00 AM
9:00 AM
9:45 AM
7:04 AM
6:59 AM
6:53 AM
7:25 AM
Tank A Hour
hrs
279.3
293.4
NR
315.4
325.2
351.2
NR
386.7
410.4
419.9
433.9
446.0
458.3
469.5
481.7
494.2
506.7
519.3
529.7
541.5
569.1
578.6
590.5
604.1
614.4
631.6
653.2
662.8
671.5
697.2
711.1
722.6
732.9
742.0
774.1
786.9
799.0
811.7
822.5
833.0
843.7
853.9
876.2
886.8
899.0
919.5
931.6
953.6
963.0
973.6
988.3
1.006.5
1,016.6
1,030.2
1,041.0
1,051.4
1,061.7
,072.6
,107.0
,119.6
,130.0
,151.8
Tank B Hour
Meter
hrs
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
570.4
579.8
591.6
605.2
616.0
624.8
641.0
650.5
659.2
681.2
688.1
696.4
706.0
715.1
768.1
759.6
772.3
784.5
795.0
805.4
816.1
844.3
860.0
872.4
892.9
904.9
927.0
936.4
947.4
962.1
981.1
990.9
1,004.4
1,015.2
1,025.7
1,035.9
1,047.1
1,080.8
1,093.9
1,125.5
TARun
Time
hrs
NA
14.1
NA
22.0
9.8
14.0
NA
12.3
13.8
9.5
14.0
12.1
12.3
11.2
12.2
12.5
12.5
12.6
10.4
11.8
14.9
9.5
11.9
13.6
10.3
17.2
10.6
9.6
8.7
14.6
13.9
11.5
10.3
9.1
12.8
12.1
12.7
10.8
10.5
10.7
10.8
10.6
10.9
12.1
10.8
9.4
10.6
14.7
7.9
10.1
13.6
10.8
10.4
10.3
10.9
12.4
12.6
12.1
TB Run
Time
hrs
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
9.4
11.8
13.6
10.8
8.8
10.2
9.5
8.7
10.9
6.9
8.3
9.6
9.1
12.7
12.2
.5
.
Z
7
i
:
',
i
.7
;
.5
:
.5
.2
.2
.3
KMnO4
Tankl
Lever3'
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
31.5
29.3
23.5
31.0
28.0
22.0
23.5
22.0
27.0
24.3
29.5
27.5
24.5
25.0
24.5
24.5
27.0
27.0
27.0
25.0
34.0
26.0
25.0
20.0
22.0
23.0
19.8
14.0
18.0
16.5
15.0
18.5
8.0
9.5
7.0
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
10.0
7.0
9.0
Estimated
KMnO4
Dosage
H3/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
509
1078
497
Pressure Filtration
Influent
psig
34
35
34
34
35
37
NR
32
35
35
32
34
38
33
35
30
34
NR
34
36
NR
36
37
34
37
37
30
25
30
26
5
30
25
30
31
32
28
28
34
29
33
29
31
29
28
30
29
33
36
33
37
37
30
33
32
29
37
35
31
40
32
Outlet
Tank A
psig
25
19
NR
25
22
0
NR
22
19
19
22
22
23
26
22
24
22
NR
23
22
NR
26
20
21
19
28
17
18
17
21
2
16
19
17
16
19
20
20
18
20
18
20
20
21
22
20
19
19
17
18
17
27
20
12
20
21
36
17
19
31
20
Outlet
TankB
psig
24
19
NR
24
21
28
NR
23
19
20
23
22
22
26
21
22
21
NR
22
21
NR
26
19
22
20
55
16
18
17
16
11
18
19
17
17
18
20
19
17
19
17
20
11
19
19
19
18
19
19
18
19
18
1
19
11
17
19
26
17
20
27
30
18
Effluent
psig
20
19
NR
23
19
18
NR
22
20
20
22
22
23
21
20
20
21
NR
21
21
NR
19
Inlet-TA
psig
9
16
NA
9
13
NA
NA
10
16
16
10
12
15
7
13
6
12
11
14
NA
10
17
18
9
13
7
13
5
NA
14
6
13
15
13
8
8
16
9
15
9
NA
11
8
6
10
10
14
19
15
20
10
10
21
12
8
NA
18
12
NA
9
12
Inlet-TB
psig
10
16
NA
10
14
9
NA
9
16
15
9
12
16
7
14
8
13
NA
12
15
NA
10
18
NA
14
7
13
10
NA
12
6
13
14
14
8
9
17
10
16
9
NA
12
10
9
12
10
14
18
14
19
NA
11
22
15
10
11
18
11
10
10
14
Inlet-
Effluent
psig
14
16
11
16
19
NA
10
15
15
10
12
15
12
15
10
13
NA
13
15
NA
17
25
26
27
30
25
30
26
NA
30
25
31
27
23
23
29
24
28
24
NA
26
24
23
25
24
28
31
28
32
32
25
28
27
24
32
30
26
32
35
27
27
Flow
rate
gpm
377
340
430
370
346
296
NR
400
340
355
390
362
285
375
340
412
356
420
370
331
NR
330
325
323
305
411
440
424
466
NR
432
470
400
399
434
361
425
377
417
0
470
425
426
416
425
382
340
393
343
315
417
391
378
422
400
327
420
306
268
406
382
Totalizer to
Distribution
kgal
179.9
467.7
NR
976.6
1,198.9
1,785.2
NR
2,593.6
3,077.1
10,016.7
10,291.8
10,569.0
10,832.4
11,079.9
11,350.5
11,621.2
11,898.6
12,178.9
12,408.9
12,653.0
13,256.2
20,183.9
20,441.2
20,963.0
21,285.3
21,780.9
22,029.4
22,254.9
22,877.2
23,178.0
30,171.6
30,430.5
31,191.8
31,433.8
31,732.9
32,029.1
32,319.1
32,575.2
32,823.7
33,082.4
40,047.1
40,600.3
40,864.2
41,159.2
41,663.7
41,953.6
42,472.4
42,690.6
42,954.5
50,018.3
50,455.5
50,698.6
51,015.0
51,279.2
51,525.3
51,774.3
52,038.5
52,296.8
52,835.5
53,148.4
60,128.9
60,635.0
Gallon
Usage
gal
NA
287,800
NA
508,900
222,300
310,300
NA
282,100
261,300
NA
275,100
277,200
263,400
247,500
270,600
270,700
277,400
280,300
230,000
244,100
324,200
NA
257,300
295,500
226,300
322,300
281,700
248,500
225,500
341,900
300,800
NA
258,900
262,600
242,000
299,100
296,200
290,000
256,100
248,500
258,700
NA
271,200
263,900
295,000
266,700
289,900
260,200
218,200
263,900
NA
263,900
243,100
316,400
264,200
246,100
249,000
264,200
258,300
289,500
312,900
NA
263,500
Daily
Average
Flowrate
gpm
NA
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
WALUE
362
362
358
461
452
434
432
457
544
WALUE!
434
419
253
WALUE!
398
388
401
396
403
WALUE!
580
348
400
408
401
402
387
407
WALUE!
468
389
408
393
405
399
402
394
406
WALUE!
376
Backwash
Tank
A
No.
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
68
69
70
72
73
80
92
94
95
3
4
6
7
20
22
24
26
27
29
0
2
3
7
9
1
4
8
9
50
52
54
58
59
0
-.4
16
17
19
1
4
7
9
3
Tank
B
No.
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
69
70
72
74
75
77
78
81
81
81
83
84
87
88
90
92
93
95
96
98
99
103
105
07
12
15
16
18
20
23
24
26
30
32
34
35
37
41
43
45
49
Total
Volume
kgal
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
556.4
564.3
572.6
604.1
614.9
630.1
678.2
692.1
699.6
739.4
770.5
777.3
791.3
798.3
819.9
831.7
846.6
863.8
874.1
891.5
900.0
914.4
921.9
958.0
975.0
993.0
1043.2
1079.0
1090.2
1116.2
1138.7
1179.5
1201.9
1253.4
1274.8
1295.1
1310.2
1333.1
1376.2
1400.4
1418.2
1456.4
Daily
Volume
kgal
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
7.9
8.3
31.5
10.8
15.2
14.4
13.9
7.5
25.0
31.1
6.8
14.0
7.0
7.6
11.8
14.9
17.2
10.3
17.4
8.5
14.4
7.5
17.0
18.0
23.2
20.5
11.2
26.0
22.5
18.0
22.4
24.5
21.4
20.3
15.1
22.9
25.5
24.2
17.8
Since Last BW
Run
Time
hrs
3.7
8.3
0.3
3.9
5.7
0.3
NR
2.6
8.2
7.1
NR
5.3
8.2
1.5
5.2
0.1
5.2
1.9
2.8
6.7
0.8
3.0
6.6
4.0
6.3
1.2
2.7
1.5
2.9
0.9
0.0
4.0
0.7
3.2
4.3
2.8
1.1
1.3
5.1
1.5
3.9
1.2
5.2
0.7
0.5
1.8
3.2
5.5
4.1
5.1
0.1
3.2
1.5
0.0
4.8
3.5
0.0
2.8
2.8
2.8
Run
Time
hrs
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
1.4
3.0
7.2
3.4
5.8
0.0
3.3
0.9
3.5
0.1
0.1
0.3
1.3
3.6
3.6
3.4
0.5
1.3
5.7
1.5
4.5
0.1
4.6
1.4
1.1
1.8
2.5
4.9
3.5
4.4
0.0
3.9
2.2
0.4
5.4
2.8
0.0
3.3
3.4
3.4
Standby
Time
hrs
5.9
9.0
0.4
6.5
7.8
0.0
NR
0.9
6.0
9.0
NR
6.5
8.0
0.0
5.7
0.0
7.2
0.2
5.6
7.8
0.4
3.7
8.4
5.0
6.0
0.0
6.5
0.6
7.0
0.0
0.0
5.4
0.0
6.7
7.9
6.2
0.0
1.3
5.6
3.3
8.2
1.6
8.3
5.8
0.8
0.0
1.1
5.3
6.7
6.0
1.9
0.0
5.6
5.4
0.0
8.1
6.2
0.0
5.5
6.3
7.4
Standby
Time
hrs
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
0.4
4.4
8.1
4.9
6
0.0
6.6
0.6
7.0
0.0
0.2
0.0
0.0
6.7
7.9
6.2
0.0
0.7
5.6
3.9
8.2
1.4
8.3
5.8
0.7
0.0
1.8
5.4
6.7
6.0
1.9
0.0
4.9
5.6
5.5
0.0
8.1
6.2
0.1
5.5
6.1
7.4
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
9
11
13
14
15
16
17
18
Day of
Week
Tue
Thu
Fti
Sat
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Date
0/03/06
0/05/06
0/06/06
0/07/06
0/08/06
0/09/06
0/10/06
0/11/06
0/13/06
0/14/06
0/15/06
0/16/06
0/17/06
0/18/06
0/19/06
0/21/06
0/23/06
0/24/06
0/25/06
0/27/06
0/28/06
0/29/06
0/31/06
1/01/06
1/02/06
1/03/06
1/04/06
1/05/06
1/06/06
1/07/06
1/08/06
1/09/06
1/10/06
1/11/06
1/12/06
1/13/06
1/14/06
1/15/06
1/16/06
1/17/06
1/19/06
1/20/06
1/21/06
1/22/06
1/23/06
1/24/06
1/25/06
1/26/06
1/27/06
1/28/06
1/29/06
1/30/06
2/02/06
2/03/06
2/04/06
2/05/06
2/06/06
2/07/06
2/09/06
2/10/06
2/11/06
2/12/06
2/13/06
2/15/06
2/16/06
2/17/06
Time
7:03 AM
6:50 AM
7:04 AM
9:50 AM
9:04 AM
7:00 AM
6:42 AM
7:00 AM
7:05 AM
8:30 AM
9:33 AM
7:10AM
7:28 AM
7:30 AM
7:30 AM
7:05 AM
7:10AM
7:30 AM
7:00 AM
6:50 AM
7:00 AM
9:20 AM
6:50 AM
7:02 AM
6:50 AM
6:47 AM
7:00 AM
8:45 AM
6:54 AM
6:56 AM
6:56 AM
7:47 AM
7:05 AM
7:15AM
7:10AM
7:10AM
7:00 AM
7:12AM
6:47 AM
6:54 AM
10:00 AM
7:33 AM
6:53 AM
7:16AM
9:00 AM
8:45 AM
8:30 AM
9:54 AM
7:01 AM
6:51 AM
8:30 AM
7:03 AM
7:15AM
7:00 AM
8:10AM
6:59 AM
1 1 :30 AM
7:00 AM
NR
NR
7:00 AM
6:48 AM
7:03 AM
9:20 AM
MA
MA
Tank A Hour
Meter
hrs
,174.0
,198.5
,209.5
,221.5
,232.6
,244.8
,256.1
,267.2
,289.9
,301.1
,313.0
,324.6
,334.8
,345.7
,356.9
,376.6
,399.8
,410.2
,421.3
,440.7
,453.8
,468.7
,483.8
,494.5
,503.2
,517.5
,527.1
,539.1
,550.3
,562.0
,572.6
,584.4
,595.5
,606.1
,617.5
,630.9
,642.7
,655.6
,668.5
,681.6
,716.8
,723.5
,739.0
,755.7
,771.0
,784.9
,797.3
,809.7
,822.2
,835.7
,850.2
,861.0
,888.5
,900.5
,918.5
,933.5
NR
,965.2
NR
NR
NR
NR
,991.6
,012.4
,023.4
,034.4
Tank B Hour
Meter
hrs
,148.5
,172.4
,183.4
,194.2
,206.6
,219.1
,230.2
,241.5
,263.7
,274.6
,286.9
,298.0
,307.9
,318.7
,330.0
,340.4
,372.8
,383.1
,393.6
,413.5
,426.6
,441.2
,456.9
,468.0
,478.8
,489.9
,499.4
,511.7
,534.6
,545.5
,557.1
,568.6
,578.5
,590.3
,603.4
,615.0
,628.2
,641.3
,654.2
,690.4
,697.4
,712.7
,729.7
,745.6
,758.6
,771.4
,783.5
,795.5
,809.2
,823.6
,861.0
,874.5
,891.7
,906.3
NR
,937.7
NR
NR
NR
NR
,963.1
,984.4
,994.8
,006.6
TARun
Time
hrs
1 .3
.7
1
i ;
1
1 .7
1
1
1
1
1
1
1
1
— \
_
15.5
1 i.7
1
1
1
1
1
1
1 .5
12.5
18.0
15.0
NA
NA
NA
NA
NA
NA
NA
10.4
11.0
11.0
TBRun
Time
hrs
11.0
12.1
11.0
10.8
12.4
12.5
11.1
10.9
12.3
9.9
10.8
11.3
NA
12.5
10.3
10.5
8.8
13.1
14.6
11.3
11.1
10.8
11.1
9.5
12.3
11.5
10.9
11.5
9.9
11.8
13.1
11.6
13.2
13.1
12.9
20.1
7.0
15.3
17.0
15.9
13.0
12.8
12.1
14.4
2.5
7.2
4.6
NA
NA
NA
NA
NA
NA
NA
10.7
10.4
11.8
KMnO4
Tankl
Lever3'
inches
8.0
9.0
7.5
7.0
7.0
7.5
6.5
14.0
15.0
11.0
11.0
13.0
12.0
10.0
14.0
12.5
10.0
11.5
18.0
19.0
15.0
15.0
16.0
10.0
14.0
16.0
16.5
17.0
15.0
15.0
15.0
18.5
18.0
18.0
18.0
18.0
19.0
16.5
17.0
16.0
18.0
16.0
17.0
17.0
17.8
14.0
15.0
17.0
17.0
NR
6.5
NR
NR
NR
NR
NR
17.0
7.0
6.0
KMnO4
Tank 2
Level
inches
6.0
7.0
5.8
7.5
7.5
6.5
10.0
13.5
18.0
24.5
20.0
14.5
13.5
10.0
8.0
12.0
17.0
11.5
14.0
14.0
14.5
11.0
13.5
16.5
15.0
16.0
16.0
15.5
17.0
17.0
15.0
17.0
17.5
17.0
18.0
14.5
19.5
17.0
17.5
19.0
14.5
14.0
14.0
15.0
17.0
17.0
15.0
NR
3.0
NR
NR
NR
NR
NR
11.0
12.0
Estimated
KMnO4
H3/L as Mn
437
470
410
399
417
387
369
716
705
766
735
970
1145
NA
912
NA
567
849
878
1647
918
907
948
654
967
NA
951
1009
963
993
956
950
986
910
937
NA
1197
668
815
667
748
923
826
NA
736
NA
NA
774
925
NA
NA
NA
NA
NA
NA
NA
947
579
553
Pressure Filtration
Influent
psig
34
30
39
35
38
30
34
35
29
32
27
31
30
29
34
33
30
30
37
34
30
32
33
39
33
36
29
27
30
28
33
32
34
36
43
30
39
7
41
37
36
35
28
38
46
46
15
43
NR
27
NR
NR
NR
NR
35
36
34
Outlet
psig
8
9
',2
5
9
1
9
22
20
23
19
20
22
20
19
24
22
23
20
19
4
20
19
22
24
21
23
19
19
20
20
18
18
48
12
1
23
1
16
19
26
1
19
12
12
15
56
NR
22
NR
NR
NR
NR
20
20
Outlet
psig
18
20
31
27
19
21
20
19
19
18
20
20
22
19
17
19
18
18
28
18
18
19
23
17
16
18
20
20
19
19
18
17
16
12
21
24
11
19
17
28
19
23
50
17
11
14
16
NR
0
NR
NR
NR
NR
20
21
psig
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
NR
5
NR
NR
NR
NR
5
20/22
20/20
26/20
psig
16
11
7
10
19
9
NA
10
16
7
12
4
12
10
7
14
14
6
8
NA
14
7
12
14
NA
17
7
9
5
14
13
14
16
25
12
NA
NA
NA
14
NA
19
12
NA
20
34
34
0
-13
NA
5
NA
NA
NA
NA
15
16
14
psig
16
10
8
8
19
9
NA
11
17
15
10
14
7
11
8
10
17
14
12
12
9
12
14
14
16
20
11
10
9
14
14
17
20
31
9
15
NA
22
20
8
16
NA
26
18
NA
35
1
27
NA
27
NA
NA
NA
NA
15
15
Inlet-
psig
29
25
34
30
33
25
38
25
29
30
38
24
27
22
26
25
24
29
28
25
25
32
25
27
28
34
31
24
22
25
23
28
27
29
31
38
25
34
NA
36
32
31
30
33
38
34
31
41
41
10
38
NA
22
NA
NA
NA
NA
30
NA
NA
NA
Flow
gpm
363
409
279
300
320
429
318
365
412
418
381
440
407
402
417
386
381
409
418
335
352
396
379
389
286
342
402
381
437
415
420
382
379
350
346
398
400
0
413
337
361
400
416
348
345
322
276
400
NR
272
NR
NR
NR
NR
355
330
358
429
Totalizer to
kgal
61,180.1
61,740.1
62,004.2
62,301.4
62,585.5
62,881.0
63,147.1
70,148.8
70,692.9
70,971.2
71,254.2
71,526.9
71,771.3
72,039.1
2,294.9
2,783.9
69.5
324.2
583.9
1,077.2
1,403.1
1,554.6
1,862.3
2,120.7
2,382.1
2,645.3
2,907.9
3,140.6
158.9
703.0
970.5
1,236.8
1,500.0
1,751.1
2,024.9
2,330.6
2,604.2
2,918.8
3,228.7
259.8
890.1
1,269.5
1,636.0
2,040.9
2,429.0
2,739.3
3,051.2
373.4
694.0
1,047.0
1,286.2
NA
2,244.6
2,603.9
2,886.7
NR
146.6
NR
NR
NR
NR
687.3
1,161.1
1,429.5
1,666.3
Gallon
gal
262,200
278,600
264,100
297,200
284,100
295,500
266,100
274,200
278,300
283,000
272,700
244,400
267,800
NA
219,600
NA
254,700
259,700
226,400
325,900
151,500
307,700
258,400
261,400
263,200
262,600
232,700
NA
273,200
270,900
267,500
266,300
263,200
251,100
273,800
305,700
273,600
314,600
309,900
NA
252,800
379,400
366,500
404,900
388,100
310,300
311,900
295,900
320,600
353,000
239,200
359,300
282,800
NA
NA
NA
NA
NA
NA
NA
241,900
268,400
236,800
Daily
Average
gpm
397
378
400
436
404
399
396
10,420
392
390
WALUE!
405
411
WALUE!
WALUE!
WALUE!
410
401
439
415
171
1,258
381
400
455
350
406
WALUE!
403
389
415
379
388
409
394
385
390
402
397
WALUE!
210
924
397
401
415
385
413
403
393
407
367
WALUE!
WALUE!
340
319
WALUE!
WALUE!
WALUE!
WALUE!
WALUE!
WALUE!
WALUE!
382
418
347
Backwash
Tank
No.
187
192
194
197
200
205
208
213
218
221
223
226
228
232
246
249
252
254
256
259
261
263
265
269
272
275
279
282
286
289
293
297
301
306
311
316
329
333
340
346
354
359
365
376
381
388
390
401
408
414
418
NR
431
NR
NR
NR
NR
437
438
439
440
Tank
No.
153
158
160
163
166
171
174
179
184
187
189
192
194
199
204
206
209
214
217
221
222
224
227
230
233
236
239
242
245
249
252
256
259
263
267
271
276
281
286
300
305
312
318
326
332
338
350
362
364
376
383
390
395
NR
407
NR
NR
NR
NR
414
415
416
417
Total
kgal
1496.6
1545.8
1564.8
1586.3
1608.1
1644.9
1704.1
1739.3
1761.4
1776.7
1807.3
1825.9
1865.7
1908.4
1923.5
1944.5
1981.0
2006.8
2032.3
2043.2
2064.5
2092.6
2116.9
2140.5
2159.5
2186.7
2211.0
2242.5
2277.8
2304.0
2339.8
2362.9
2397.3
2428.5
2461.7
2575.7
2571.7
2623.7
2700.4
2817.4
2900.6
3020.2
3084.7
3123.0
3166.1
3249.3
8.2
55.8
88.0
294.0
352.6
388.3
NR
463.1
NR
NR
NR
NR
499.6
509.2
517.4
525.3
Daily
kgal
19.2
19.0
19.0
21.5
21.8
15.8
14.6
22.1
15.3
30.6
18.6
20.9
25.8
15.1
21.0
14.6
25.8
25.5
10.9
21.3
28.1
24.3
23.6
19.0
27.2
24.3
31.5
35.3
26.2
35.8
23.1
34.4
31.2
33.2
114.0
NA
52.0
7.3
117.0
83.2
119.6
64.5
38.3
43.1
37.4
NA
47.6
32.2
66.5
58.6
35.7
NA
NA
NA
NA
NR
NR
NA
9.6
8.2
7.9
Since Last BW
Run
Time
hrs
4.8
2.5
2.7
4.6
1.9
4.7
2.9
1.4
1.8
0.6
2.4
2.6
1.2
2.8
2.7
0.7
1.5
0.0
0.5
2.6
1.6
2.4
2.6
0.0
2.5
1.8
2.3
0.8
2.4
0.0
1.3
0.2
2.3
2.8
1.3
1.5
2.0
1.4
0.0
1.4
0.0
0.2
0.0
1.7
0.5
0.0
1.9
0.0
0.0
0.0
0.0
NR
0.1
NR
NR
NR
NR
4.6
9.2
8.1
2.4
Run
Time
hrs
5.3
2.5
3.4
5.3
1.9
0.0
3.4
1.6
1.7
2.1
1.2
3.0
1.1
1.8
3.4
2.3
2.4
2.0
0.0
1.1
3.3
2.2
2.3
2.0
1.3
3.1
2.4
2.9
0.0
2.4
0.6
1.2
0.8
2.3
2.8
2.1
2.3
3.2
0.8
0.0
0.7
0.0
0.9
0.0
0.8
0.0
1.2
1.2
0.0
0.0
0.1
0.8
NR
0.0
NR
NR
NR
NR
5.2
8.4
8.5
4.0
Standby
Time
hrs
6.6
5.1
5.5
6.3
3.8
6.0
5.0
0.9
1.7
3.4
0.0
5.3
6.0
2.3
6.2
5.0
0.7
0.9
0.0
0.0
6.2
1.8
4.2
5.1
0.0
3.7
4.8
6.0
0.0
4.4
0.0
1.9
0.0
4.6
3.2
0.7
2.5
0.0
0.0
0.3
0.2
1.5
0.0
0.0
0.8
0.0
0.0
0.0
0.0
1.6
0.0
0.0
0.0
NR
0.0
NR
NR
NR
NR
5.3
12.1
12.6
5.5
Standby
Time
hrs
6.6
5.6
5.5
6.3
4.3
0.0
5.0
1.4
1.9
3.6
0.0
5.1
4.4
2.3
6.2
5.0
5.2
0.9
0.0
6
1.
3
5.
3
4
5
2/
0.
5
3
0
2
0.0
0.0
0.0
0.2
0.0
0.0
0.0
0.8
0.0
0.9
0.0
0.0
0.0
0.0
0.0
0.0
NR
0.0
NR
NR
NR
NR
5.3
12.0
12.6
10.3
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
22
23
25
26
27
28
29
30
Day of
Week
Tue
Wed
Fri
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Tnu
Sat
Sun
Mon
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Tnu
Fri
Sun
Mon
Wed
Tnu
Fri
Sun
Date
2/19/06
2/20/06
2/22/06
2/24/06
2/25/06
2/26/06
2/27/06
2/29/06
2/30/06
2/31/06
1/01/07
1/02/07
01/04/07
01/05/07
01/06/07
01/07/07
01/08/07
01/09/07
01/10/07
01/11/07
01/12/07
01/14/07
01/15/07
01/16/07
01/17/07
01/19/07
01/20/07
1/21/07
1/22/07
1/23/07
1/24/07
1/25/07
1/26/07
1/27/07
1/28/07
1/30/07
1/21/07
02/01/07
02/03/07
02/04/07
02/05/07
02/07/07
02/08/07
02/09/07
02/10/07
02/11/07
02/12/07
02/13/07
02/14/07
02/15/07
02/16/07
02/18/07
02/19/07
02/20/07
02/21/07
02/22/07
02/23/07
02/25/07
02/26/07
02/28/07
03/01/07
03/02/07
03/04/07
Time
7:00 AM
7:00 AM
1:00 AM
8:43 AM
10:00 AM
8:30 AM
6:52 AM
7:15AM
10:50 AM
2:10AM
1:00 AM
7:40 AM
6:55 AM
7:05 AM
6:51 AM
8:00 AM
7:03 AM
6:50 AM
7:05 AM
7:25 AM
6:59 AM
7:00 AM
7:00 AM
7:07 AM
8:00 AM
7:00 AM
7:01 AM
7:15AM
7:02 AM
7:50 AM
8:30 AM
6:57 AM
7:18AM
7:00 AM
7:15AM
7:00 AM
6:57 AM
7:05 AM
7:21 AM
8:15 AM
7:45 AM
9:00 AM
7:01 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
9:00 AM
7:00 AM
11:45 AM
7:15AM
6:50 AM
6:58 AM
9:45 AM
6:49 AM
7:18 AM
7:05 AM
7:00 AM
7:10AM
Tank A Hour
Meter
hrs
2,055.8
2,067.3
2,092.4
2,112.6
2,127.7
2,137.4
2,148.2
2,171.3
2,184.6
2,198.5
2,210.1
2,217.8
2,241.2
2,251.9
2,286.5
2,298.7
2,309.5
2,319.0
2,331.0
2,352.6
2,364.9
2,376.6
2,387.1
2,410.4
2,430.5
2,438.6
2,471.0
2,484.1
2,497.2
2,509.4
2,522.9
2,550.9
2,565.6
2,579.3
2,615.2
2,631.9
2,649.7
2,678.8
2,692.2
2,706.3
2,716.7
2,751.4
2,770.9
2,791.4
2,814.1
2,834.7
2,869.8
2,887.7
2,911.4
2,929.1
NR
2,963.6
2,995.1
3,011.0
3,037.5
3,051.3
3,065.6
3,092.6
Tank B Hour
Meter
hrs
2,027.3
2,039.3
2,064.1
2,084.3
2,098.6
2, 08.3
2, 19.2
2, 43.1
2, 56.6
2, 70.7
2, 81.1
2, 88.8
2,212.6
2,222.7
NR
2,270.9
2,281.6
2,291.8
2,303.2
2,324.5
2,336.8
2,348.4
2,359.4
2,382.4
2,402.1
2,409.8
2,442.3
2,455.2
2,468.4
2,481.0
2,494.1
2,521.7
2,536.3
2,550.0
2,585.9
2,602.4
2,621.2
2,650.1
2,665.3
2,679.0
2,690.1
2,725.2
2,744.3
2,764.5
2,786.7
2,807.1
2,842.1
2,860.7
2,884.9
NR
2,937.0
2,985.0
3,011.6
3,025.4
3,039.3
3,066.8
TARun
Time
hrs
10.7
11.5
14.5
13.6
15.1
9.7
10.8
11.4
13.3
13.9
.6
7
.3
.5
2.2
.8
i .5
2.0
.3
2.3
7
•5
.8
20.1
8.1
0.4
3.1
3.1
2.2
3.5
3.9
4.7
3.7
9.6
6.7
7.8
4.7
3.4
4.1
0.4
9.6
9.5
20.5
22.7
20.6
18.5
NA
23.7
NR
NA
15.9
15.2
13.8
14.3
15.3
TBRun
Time
hrs
11.0
12.0
14.3
14.0
14.3
9.7
10.9
12.3
13.5
14.1
10.4
7.7
11.5
10.1
NA
NA
10.7
10.2
11.4
10.5
12.3
11.6
11.0
11.5
19.7
7.7
11.8
10.8
12.9
13.2
12.6
13.1
13.4
14.6
3.7
9.5
6.5
8.8
4.0
5.2
3.7
1.1
20.3
19.1
20.2
22.2
20.4
18.3
NA
24.2
NR
NA
6.7
5.4
3.8
3.9
6.0
KMnO4
Tankl
Lever3'
inches
6.0
7.0
7.0
7.0
8.0
4.5
7.0
6.0
6.5
10.0
6.0
5.0
6.0
6.0
9.0
9.0
9.0
8.0
9.0
9.0
9.0
7.0
6.0
7.0
12.0
6.0
16.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
12.0
9.0
17.0
0.0
0.0
7.0
8.0
2.0
2.0
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
KMnO4
Tank 2
Level
inches
9.0
11.0
13.0
10.0
12.0
8.0
9.0
10.0
11.0
11.0
8.0
6.5
9.0
9.0
8.0
10.0
10.0
9.0
9.0
9.0
9.0
9.0
9.0
8.0
9.0
13.0
7.0
17.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
17.0
12.0
12.0
7.0
9.0
9.0
13.0
20.0
2.0
2.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
3.0
Estimated
KMnO4
H3/L as Mn
505
567
529
NA
514
489
546
499
476
551
480
527
472
519
NA
457
587
539
591
591
549
547
528
488
445
474
442
575
448
1072
495
499
515
482
NA
467
471
541
467
569
181
NA
427
686
733
128
204
0
0
0
0
NA
0
0
0
0
0
0
0
NA
Pressure Filtration
Influent
psig
40
34
34
34
10
34
34
34
40
33
12
32
9
36
31
34
9
33
32
32
33
33
34
34
39
41
35
35
34
34
32
33
40
29
35
33
33
33
35
32
35
32
33
41
33
38
35
33
32
30
24
32
28
24
NR
28
30
32
25
27
25
Outlet
psig
20
22
24
24
11
16
23
16
36
24
11
20
11
18
19
18
11
25
17
26
17
19
23
18
24
58
16
17
22
21
25
17
23
18
17
16
17
17
19
19
20
17
24
19
48
17
16
14
14
15
16
17
19
16
NR
18
1
1
1
1!
Outlet
psig
0
17
17
17
10
12
17
16
17
10
24
12
20
24
20
10
15
23
17
22
22
16
19
0
19
18
20
15
16
16
21
NR
11
19
20
22
20
22
20
21
20
16
22
21
20
17
18
17
16
19
14
14
8
NR
13
13
19
17
15
psig
20/0
22/17
28/17
25/18
11/12
17/22
25/19
23/19
30/30
24/17
11/11
21/27
10/11
16/21
18/25
17/21
11/11
10/13.5
17/25
27/22
23/18
23/19
23/16
19/21
25/2
0/21
20
22
23/17
22
18/25
18/23
24/3
19/12
1720
19/23
17/24
10
24/19
22/19
21/22
18/21
25/18
20/24
NA
NA
18/12
15/20
15/20
15/19
16/21
18/15
14
8
NR
14/17
17/14
15/20
15/19
20/15
psig
20
12
10
10
NA
18
11
18
9
NA
12
NA
18
12
16
NA
8
A
psig
40
17
17
17
NA
22
17
18
16
NA
8
NA
16
7
14
NA
18
9
15
11
11
18
15
39
NA
17
15
19
16
18
16
12
NA
18
16
13
11
16
11
15
11
15
16
11
20
13
23
18
15
15
14
5
18
14
16
NR
4
17
19
6
10
10
Inlet-
psig
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Flow
gpm
363
364
360
0
335
355
378
365
0
401
0
340
380
0
352.7
394.8
401.5
389.8
414.9
380
385
303
392
307
365
353
360
384
280
450
375
400
370
375
420
385
412
377
383
405
380
328
163
267
269
283
325
268
294
322
NR
292
310
272
269
309
287
305
Totalizer to
kgal
2,146.5
2,406.1
2,962.4
129.2
447.2
656.1
895.7
1,412.6
1,713.1
2,024.9
2,263.5
2,442.1
2,960.5
3,197.1
206.8
439.4
704.3
992.8
1,242.1
1,477.3
1,745.5
2,255.5
2,534.3
2,802.6
3,060.1
334.0
796.6
981.5
1,200.7
1,482.3
1,734.1
2,326.9
2,612.8
2,918.1
273.1
588.3
901.0
1 ,266.4
1,705.1
2,073.2
2,489.7
3,134.3
192.4
498.9
749.3
1,084.0
1,338.9
1,499.2
1,817.0
2,167.9
2,489.7
3,076.3
101.3
520.4
815.5
865.3
1,151.2
1,678.0
1,925.8
2,409.9
2,655.4
2,901.4
110.8
Gallon
gal
243,100
259,600
309,200
NA
318,000
208,900
239,600
262,400
300,500
311,800
238,600
178,600
260,100
236,600
NA
232,600
264,900
288,500
249,300
235,200
268,200
269,200
278,800
268,300
257,500
276,200
462,600
184,900
219,200
281,600
251,800
285,900
305,300
NA
315,200
312,700
365,400
438,700
368,100
416,500
317,100
NA
306,500
250,400
334,700
254,900
160,300
317,800
350,900
321,800
303,800
NA
419,100
295,100
49,800
285,900
291,800
247,800
255,500
245,500
246,000
NA
Daily
Average
gpm
373
368
358
ft/ALUE!
361
359
368
370
374
371
363
387
365
79
ft/ LUE!
75
ft/ LUE!
ft/ LUE!
; 37
; 98
;82
. 12
78
384
399
395
387
390
381
384
396
384
383
ft/ALUE!
359
380
372
374
370
380
369
ft/ALUE!
368
389
373
213
138
260
261
262
275
ft/ALUE!
292
277
ft/ALUE!
ft/ALUE!
284
254
278
296
291
ft/ALUE!
Backwash
Tank
No.
441
442
444
446
447
448
50
53
55
57
58
462
465
66
. 68
. 70
. 71
. 73
. 74
. 77
. 79
480
482
485
488
489
491
492
494
499
501
504
506
508
510
513
515
518
522
525
526
527
529
530
530
531
532
533
535
536
538
539
NR
540
542
543
545
546
547
550
Tank
No.
419
420
421
424
426
427
428
431
435
441
444
445
447
448
450
451
453
456
457
459
460
464
467
468
469
471
472
477
479
483
485
487
489
492
494
497
501
503
505
506
508
508
509
511
512
514
516
516
518
519
NR
521
523
523
525
527
528
530
Total
kgal
536.4
546.5
569.5
595.3
622.9
640.5
676.5
719.9
771.2
802.5
811.6
830.2
845.0
859.3
874.6
889.3
917.8
930.5
943.9
958.4
995.3
1020.4
1029.1
1041.3
1055.0
069.0
121.8
144.0
181.9
202.4
1221.3
1241.0
1282.1
1318.7
1373.2
1442.9
1495.6
1517.1
528.6
548.5
554.5
557.8
568.7
599.7
601.7
633.5
640.8
662.6
674.3
NR
1684.5
1702.7
1714.5
1722.9
1734.4
1741.6
1759.0
Daily
kgal
7.5
10.1
12.0
20.8
7.6
9.7
21.1
1.0
.1
3.6
4.8
4.3
5.3
4.7
k5
2.7
3.4
k5
7.0
25.1
8.7
12.2
13.7
14.0
22.3
15.4
22.2
17.7
20.5
18.9
19.7
41.1
36.6
54.5
39.3
52.7
21.5
11.5
19.9
6.0
3.3
10.9
31.0
2.0
16.6
NA
21.8
11.7
NA
NA
13.6
11.8
8.4
11.5
7.2
10.5
Since Last BW
Run
Time
hrs
10.7
5.8
4.1
2.1
2.4
2.1
2.1
5.0
4.1
6.7
2.4
1.2
5.3
0.0
5.0
4.7
2.1
6.2
2.9
0.0
5.0
6.2
1.8
7.6
2.6
0.5
3.1
1.7
6.5
5.9
5.6
7.2
6.3
3.0
5.1
1.0
6.5
NR
5.4
3.2
22.6
19.2
22.6
19.9
11.2
8.0
3.4
2.6
NR
13.1
9.2
6.2
7.6
8.3
9.5
2.7
Run
Time
hrs
10.4
12.0
12.3
8.2
7.2
6.8
5.9
1.1
1.1
4.1
0.9
5.3
1.6
4.7
1.8
1.9
6.8
3.9
0.0
4.1
2.2
3.3
6.5
4.0
6.4
4.7
0.0
5.5
3.8
2.3
1.7
3.3
1.7
3.0
2.0
2.6
5.0
2.1
4.2
2.3
22.5
17.6
6.9
6.9
8.6
0.1
18.7
11.4
13.3
NR
2.7
0.3
15.6
14.4
1.9
5.0
4.5
Standby
Time
hrs
0.0
5.4
3.7
4.8
8.2
5.4
5.0
0.7
5.7
6.1
5.3
0.0
4.6
0.0
6.3
8.8
6.1
6.0
5.2
0.0
1.7
6.0
3.1
5.7
4.9
0.0
4.7
1.6
4.8
5.3
4.0
3.7
5.0
2.3
4.8
0.0
5.3
0.0
6.0
0
2.6
2.4
0.5
2.5
5.1
3.1
0.0
NR
6.7
7.6
4.6
4.3
5.3
4.9
6.0
Standby
Time
hrs
0.0
10.7
12.9
9.9
4.3
8.2
6.8
7.8
5.2
1.9
0.0
0.3
5.7
1.0
6.6
5.3
7.1
9.1
5.6
0.0
5.3
0.4
0.6
6.5
5.1
6.6
5.2
0.0
7.2
4.8
4.0
0.9
3.7
4.9
1.8
4.9
4.5
2.4
6.3
0.9
1.1
25
2.1
0.0
1.4
0.0
3.1
2.4
1.3
NR
4.7
0.0
5.4
7.9
0.8
4.7
6.9
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
31
32
33
34
35
36
37
38
39
41
42
Day of
Week
Mon
Tue
Wed
Thu
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Mon
Tue
Thu
Fri
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Mon
Wed
Tnu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Date
03/05/07
03/06/07
03/07/07
03/08/07
03/10/07
03/12/07
03/13/07
03/14/07
03/15/07
03/16/07
03/17/07
03/18/07
03/19/07
03/20/07
03/21/07
03/22/07
03/24/07
03/26/07
03/27/07
03/29/07
03/30/07
04/01/07
04/02/07
04/03/07
04/04/07
04/05/07
04/07/07
04/08/07
04/10/07
04/11/07
04/12/07
04/13/07
04/14/07
04/16/07
04/18/07
04/19/07
04/20/07
04/21/07
04/22/07
04/24/07
04/25/07
04/26/07
04/27/07
04/28/07
04/29/07
05/01/07
05/02/07
05/03/07
05/04/07
05/05/07
05/07/07
05/08/07
05/09/07
05/11/07
05/12/07
05/13/07
05/15/07
05/16/07
05/17/07
05/18/07
05/19/07
05/20/07
05/22/07
05/23/07
05/24/07
05/25/07
05/26/07
05/27/07
Time
7:00 AM
6:59 AM
6:59 AM
7:00 AM
9:15AM
7:00 AM
7:00 AM
7:22 AM
7:01 AM
7:00 AM
7:40 AM
NR
7:00 AM
7:00 AM
7:00 AM
7:00 AM
10:00 AM
7:05 AM
6:55 AM
7:05 AM
7:21 AM
9:20 AM
7:00 AM
7:00 AM
7:00 AM
6:55 AM
7:45 AM
7:15 AM
7:15AM
7:20 AM
7:03 AM
MA
10:00 AM
7:00 AM
7:15 AM
7:00 AM
7:00 AM
9:00 AM
8:00 AM
7:00 AM
7:05 AM
7:02 AM
7:00 AM
7:05 AM
7:05 AM
7:10AM
7:00 AM
7:00 AM
7:00 AM
7:10AM
6:55 AM
7:00 AM
7:00 AM
7:00 AM
4:00 PM
9:00 AM
7:00 AM
6:50 AM
8:00 AM
7:30 AM
7:15AM
7:00 AM
7:05 AM
7:00 AM
7:00 AM
7:00 AM
8:45 AM
8:35 AM
Tank A Hour
Meter
hrs
3,108.1
3,122.6
3,150.3
3,183.3
3,216.0
3,230.9
3,246.0
3,259.4
3,275.1
3,290.3
,308.8
; ,328.4
; ,343.1
,358.3
,373.1
,407.3
; ,442.0
; ,457.7
3,492.3
3,509.9
3,547.6
3,567.8
3,586.8
3,603.5
3,620.1
3,650.6
3,666.7
3,697.8
3,713.0
3,728.8
3,744.7
3,754.3
3,791.5
3,825.3
3,840.0
3,853.5
3,871.1
3,887.3
3,922.9
3,938.3
3,954.2
3,969.4
3,982.6
3,999.9
4,036.1
4,052.5
4,068.5
4,084.4
4,099.8
4,135.2
4,151.8
4,169.5
4,204.3
4,236.2
4,240.5
4,275.5
4,291.8
4,309.5
4,328.3
4,342.1
,362.3
,394.0
,410.1
,425.0
,437.5
,453.4
Tank B Hour
Meter
hrs
3,081.8
3,095.8
3,110.1
3,124.1
3,157.2
3,190.4
3,204.9
3,220.1
3,233.5
3,249.3
3,264.3
3,282.4
3,302.4
3,317.0
3,332.3
3,346.9
3,381.3
3,416.5
3,432.2
3,466.6
3,484.3
3,522.0
3,542.0
3,561.1
3,578.2
3,594
3,625.
3,640,
3,671. I
3,687.
3,702.!
3,718.
3,733
3,764..
3,797
3,812
3,827.4
3,844.3
3,859.9
3,896.4
3,911.0
3,926.8
3,942.7
3,955.5
3,972.0
4,009.8
4,027.0
4,043.0
4,059.1
4,074.4
4,110.1
4,126.0
4,143.7
4,179.2
4,203.1
4,215.0
4,250.8
4,266.5
4,284.3
4,303.6
4,317.3
4,337.5
4,369.4
4,384.6
4,399.4
4,411.8
4,427.7
TARun
Time
hrs
15.5
14.5
MA
MA
15.7
15.7
14.9
15.1
13.4
15.7
15.2
8.5
9.6
4.7
5.2
4.8
9.0
7.6
5.7
7.1
7.6
8.5
0.2
9.0
6.7
6.6
6.0
6.1
4.6
5.2
5.8
5.9
6
.9
5.4
.7
3.5
7.6
.2
5.8
5.4
5.9
5.2
.2
7.3
7.5
.4
;.o
5.9
5.4
.8
I.6
7.7
7.7
; .9
3
i.9
i.3
7.7
.8
.8
2 .2
.8
1.1
.9
2.5
5.9
TBRun
Time
hrs
5.0
4.0
4.3
4.0
6.2
6.0
4.5
5.2
3.4
5.8
5.0
8.1
0.0
4.6
5.3
4.6
9.2
8.3
5.7
7.2
7.7
7.0
0.0
9.1
7.1
6.3
6.5
5.3
4.7
5.5
5.8
5.1
5.2
5.5
5.8
5.0
4.7
6.9
5.6
6.6
4.6
5.8
5.9
2.8
6.5
8.2
7.2
6.0
6.1
5.3
9.2
5.9
7.7
7.7
3.9
1.9
7.7
5.7
7.8
9.3
3.7
0.2
4.8
5.2
4.8
2.4
5.9
KMnO4
Tankl
Lever3'
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
H3/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
23
26
23
26
26
32
32
31
31
30
31
28
29
29
32
30
30
29
26
29
31
32
24
24
29
27
27
27
29
36
48
26
29
28
23
23
41
25
26
29
38
27
27
25
24
26
23
19
18
27
28
28
28
24
28
26
28
31
26
25
29
26
32
37
29
7
7
29
Outlet
psig
6
6
1
9
2
7
7
8
9
8
8
5
0
9
9
9
5
1
5
6
5
0
6
1
9
2
1
6
7
1
2
6
7
9
7
6
5
2
7
9
2
7
0
7
7
1
0
4
2
2
0
6
6
3
2
7
1
6
7
8
9
0
1
5
8
2
2
7
Outlet
psig
20
18
15
15
13
13
13
13
14
14
14
20
13
14
14
14
19
13
22
18
18
14
21
15
15
14
15
19
18
2
10
21
18
15
21
18
32
15
19
15
20
20
16
21
19
15
17
10
11
15
16
20
19
16
16
22
16
19
22
23
16
15
14
15
16
10
10
18
psig
5
5
5
5
5
4
4
4
4
4
8
5
4
5
5
5
5
5
5
5
4
5
5
5
5
5
5
5
5
4
1
5
5
5
5
5
0
5
5
5
4
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
4
5
5
5
5
5
5
1
1
5
psig
7
10
2
7
4
15
15
13
12
12
13
13
9
10
13
11
15
8
11
13
16
12
8
3
10
5
6
11
12
15
NA
10
12
9
6
7
6
3
9
10
NA
10
7
8
7
5
3
5
6
5
8
12
12
1
6
9
7
15
9
7
10
6
11
22
11
NA
NA
12
p g
i ft
22
13
NA
NA
11
Inlet-
psig
8
11
8
11
11
8
8
7
7
6
3
3
5
4
7
5
5
4
1
4
7
7
9
9
14
12
12
12
14
22
37
11
14
13
8
8
11
10
11
14
24
12
12
10
9
11
8
3
12
13
13
13
9
13
11
13
16
12
10
14
11
17
22
14
NA
NA
14
Flow
gpm
321
297
300
301
301
265
251
263
275
275
252
297
270
280
268
275
280
280
310
285
275
270
305
285
269
295
289
294
290
215
0
308
297
268
305
270
297
NR
280
380
300
290
304
305
285
291
290
280
286
260
275
302
280
265
260
265
302
298
271
289
298
200
280
0
0
265
Totalizer to
kgal
385.8
632.6
880.5
1,129.1
1,646.7
2,181.7
2,420.0
2,668.1
2,893.0
3,149.3
124.7
428.5
746.8
994.8
1,252.0
1,498.7
2,075.1
2,651.8
2,924.6
211.2
501.5
1,135.7
1,423.9
1,745.7
2,028.2
2,311.2
2,843.5
3,109.6
365.6
627.4
892.9
1,162.1
1,471.4
1,953.5
2,473.9
2,724.5
2,968.3
3,266.5
260.3
871.8
1,131.7
1,403.7
1,666.2
1,891.9
2,192.1
2,814.5
3,089.0
349.6
603.2
1,184.5
1,456.0
1,740.0
2,307.8
2,582.6
2,890.4
184.7
443.5
735.2
1,045.6
1,279.0
1,647.3
2,368.8
2,614.6
2,876.9
3,139.3
15.3
445.0
Gallon
gal
275,000
246,800
247,900
248,600
291,000
255,600
238,300
248,100
224,900
256,300
NA
303,800
318,300
248,000
257,200
246,700
322,400
296,500
272,800
NA
290,300
299,200
288,200
321,800
282,500
283,000
279,400
266,100
253,900
261,800
265,500
269,200
309,300
255,500
268,300
250,600
243,800
298,200
NA
274,200
259,900
272,000
262,500
225,700
300,200
299,400
274,500
271,600
253,600
303,800
271,500
284,000
285,500
274,800
307,800
NA
258,800
291,700
310,400
233,400
368,300
320,000
245,800
262,300
262,400
NA
429,700
Daily
Average
gpm
301
289
WALUE!
WALUE!
304
269
270
273
280
271
ft/ALUE!
277
268
282
281
280
281
275
290
WALUE!
274
281
239
282
279
287
287
283
289
284
280
290
438
280
287
281
289
288
WALUE!
282
289
286
281
289
296
280
272
283
275
274
279
267
269
168
812
WALUE!
270
274
272
283
304
360
262
294
351
WALUE!
423
Backwash
Tank
No.
551
552
554
555
558
560
561
562
563
564
565
566
568
569
570
571
573
576
577
579
580
583
584
586
587
589
592
593
596
598
599
601
602
606
609
610
612
614
615
619
620
622
624
624
627
630
631
634
637
638
639
643
644
646
650
651
653
655
656
659
666
666
667
669
670
670
Tank
No.
532
533
534
535
538
540
541
542
544
545
548
549
550
551
554
556
558
560
561
563
566
567
568
570
573
575
578
581
583
585
588
592
593
594
596
598
601
603
605
606
608
610
612
613
619
621
622
625
627
629
632
634
636
638
638
641
648
649
650
652
653
654
Total
kgal
769.5
776.8
787.3
794.1
814.9
830.8
838.7
875.5
903.9
913.0
922.1
931.2
955.2
981.2
993.4
2017.8
2030.1
2061.0
2085.0
2102.2
2110.9
2127.8
2149.2
2159.1
2179.3
2191.8
2208.4
2220.5
2237.8
2260.9
2290.3
2299.1
2312.2
2328.0
2340.0
2367.2
2382.7
2394.3
2406.8
2418.1
2434.1
2469.3
2481.8
2518.6
2544.6
2556.1
2565.6
2602.0
2615.0
2627.5
2652.6
2663.0
2678.2
2693.8
2698.7
2719.0
2766.9
2770.8
2779.8
2794.7
2803.8
2811.1
Daily
kgal
10.5
7.3
10.5
6.8
10.7
8.0
7.9
13.4
9.1
9.1
9.1
14.4
16.3
12.2
12.8
12.3
11.9
24.0
17.2
8.7
16.9
10.3
9.9
6.9
12.5
16.6
12.1
17.3
12.1
16.7
8.8
13.1
15.8
12.0
11.8
15.5
11.6
12.5
11.3
16.0
22.9
12.5
10.4
12.1
11.5
9.5
16.2
13.0
12.5
10.7
10.4
15.2
15.6
4.9
20.3
14.1
3.9
9.0
14.9
9.1
7.3
Since Last BW
Run
Time
hrs
7.3
9.9
0.1
3.8
0.8
7.2
6.9
3.8
4.9
6.0
6.6
11.1
3.0
10.6
12.3
14.4
6.6
2.4
6.2
1.6
2.0
8.0
9.7
5.1
0.0
7.2
5.3
4.0
5.3
9.7
3.7
0.9
7.6
0.0
6.3
2.6
6.0
5.8
2.7
2.5
4.0
4.8
9.8
17.4
0.0
4.5
7.2
2.9
10.3
7.1
1.3
3.5
2.5
4.8
20.8
11 7
2.6
4.2
21.6
Run
Time
hrs
0.2
3.7
.5
! .3
1.8
4.8
1.5
. .1
3.7
9.2
.8
1. 4
.7
.8
.8
5.2
.9
8.5
13.4
7.2
8.3
3.4
5.5
5.3
5.9
1.3
1.2
10.3
0.1
5.1
9.4
6.5
5.8
2.9
8.3
7.1
2.3
9.7
12.5
13.3
11.1
4.8
8.1
6.8
0.0
1.6
8.6
5.9
1.1
3.4
11.2
7.7
12.5
15.2
13.7
3.1
15.0
10.3
Standby
Time
hrs
5.5
8.5
0.0
5.5
0.0
3.9
4.9
5.2
5.2
1.5
12.6
4.1
5.8
4.6
1.8
4.0
3.6
4.2
5.4
0.0
3.3
3.7
0.3
3.2
5.9
6.0
0.0
0.0
3.6
1.1
3.9
4.3
4.0
4.7
0.0
5.9
0.0
4.7
3.7
6.1
5.0
2.2
2.7
5.2
3.3
3.6
5.0
0.0
5.0
4.0
5.2
4.1
2.4
0.0
5.1
1.4
3.9
11.3
8.1
6.4
4.1
10.3
Standby
Time
hrs
0.0
5.9
4.9
6.5
7.5
3.9
8.3
7.9
8.9
8.4
1.5
7.2
7.6
8.1
2.5
1.8
0.0
5.8
2.9
5.4
0.0
3.8
4.8
3.0
6.0
5.9
5.2
0.0
4.4
1.5
0.0
4.6
0.0
4.0
5.5
4.7
6.0
3.6
5.1
4.5
3.7
2.8
5.0
2.2
3.3
3.0
6.9
7.3
3.3
3.6
3.1
2.0
3.7
0.0
5.3
4.1
0.0
1.3
5.1
1.4
5.8
7.3
8.1
6.3
7.8
6.0
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
43
44
45
46
47
48
49
53
Day of
Week
Mon
Tue
Wed
Thu
Fti
Sun
Mon
Wed
Thu
Fti
Sat
Mon
Tue
Thu
Fti
Sat
Sun
Mon
Tue
Wed
Thu
Fti
Sat
Sun
Tue
Wed
Thu
Fti
Sat
Sun
Tue
Wed
Thu
Fti
Sat
Sun
Mon
Tue
Wed
Tnu
Fti
Sat
Sun
Mon
Wed
Fri
Sat
Mon
Tue
Wed
Fti
Sun
Mon
Tue
Wed
Fti
Sat
Sun
Mon
Tue
Wed
Tnu
Fti
Sat
Sun
Date
05/28/07
05/29/07
05/20/07
05/31/07
06/01/07
06/03/07
06/04/07
06/06/07
06/07/07
06/08/07
06/09/07
06/11/07
06/12/07
06/14/07
06/15/07
06/16/07
06/17/07
06/18/07
06/19/07
06/20/07
06/21/07
06/22/07
06/23/07
06/24/07
06/26/07
06/27/07
06/28/07
06/29/07
06/30/07
07/01/07
07/03/07
07/04/07
07/05/07
07/06/07
07/07/07
07/08/07
07/09/07
07/10/07
07/11/07
07/12/07
07/13/07
07/14/07
07/15/07
07/16/07
07/18/07
07/20/07
07/21/07
07/23/07
07/24/07
07/25/07
07/27/07
07/29/07
07/30/07
07/31/07
08/01/07
08/03/07
08/04/07
08/05/07
08/06/07
08/07/07
08/08/07
08/09/07
08/10/07
08/11/07
Time
9:00 AM
7:05 AM
7:00 AM
9:00 AM
7:40 AM
9:15 AM
7:00 AM
7:05 AM
7:05 AM
7:05 AM
7:10 AM
6:55 AM
7:00 AM
7:00 AM
7:05 AM
8:50 AM
7:13AM
7:10AM
8:55 AM
1 1 :00 AM
7:00 AM
7:00 AM
7:15AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:05 AM
6:57 AM
10:00 AM
9:15 AM
NR
7:00 AM
7:00 AM
7:00 AM
7:05 AM
10:00 AM
7:10AM
10:00 AM
7:00 AM
7:10AM
7:10AM
7:10AM
7:05 AM
NR
1:00 AM
7:30 AM
7:00 AM
10:00 AM
NR
7:20 AM
7:30 AM
7:30 AM
7:05 AM
7:05 AM
7:10AM
Tank A Hour
Meter
hrs
4.490.9
4,507.9
4,523.0
4,535.5
4,545.4
4,570.9
4,582.0
4.603.4
4.614.8
4.626.9
4.636.6
4.664.8
4,677.5
4,702.6
4,713.8
4,725.6
4,782.3
4.795.1
4.809.0
4,822.7
4.844.7
4,856.3
4,867.2
4,878.9
4,890.2
4,900.0
4,923.3
4,944.6
4,954.6
4,965.3
4,976.9
NR
5.003.5
5.019.1
5,034.6
5,050.9
5,070.0
5,097.7
5,129.5
5,151.6
5,161.7
5,186.4
5,198.5
5.210.9
5.234.7
5,258.5
5,266.5
5,310.7
5,324.8
NR
5,349.0
5,361.5
5,374.0
5.386.6
5.400.1
5.412.8
Tank B Hour
Meter
hrs
. .464.6
. ,481.5
. ,496.5
. ,508.8
. ,518.6
. ,543.8
554.9
. .576.6
. .587.7
. .599.7
. .609.6
. .637.3
649.9
674.8
685.6
697.4
. ,754.6
. .768.3
. .789.2
. ,795.5
. .818.0
. ,829.7
. ,840.1
. ,851.9
. ,862.6
. ,873.4
896.7
918.1
929.1
. ,940.6
950.2
NR
. .962.1
. ,962.1
962.1
962.1
962.1
. ,962.1
. ,962.1
. ,981.2
. ,991.4
016.7
028.6
040.5
065.1
089.5
097.8
140.7
155.5
NR
179.7
191.6
204.3
216.6
230.5
242.7
TARun
Time
hrs
2 1
7.0
5.1
2.5
i .9
;
2.
.8
.3
2.8
.9
.7
.6
.6
.9
.7
.3
_8
.6
.9
.0
.7
.6
ft
2 i.6
5.6
.5
.3
.1
.3
7.1
.9
.1
.9
2.1
2.4
2.2
.1
0
.0
.1
ft
ft
2.5
2.5
2.6
.5
2.7
TBRun
Time
hrs
20.4
6.9
5.0
2.3
9.8
3.2
1.1
1.3
1.1
2.0
9.9
14.6
12.6
12.5
10.8
11.8
.4
.7
2 .9
i.3
7
.7
.4
.8
.7
.8
.4
.0
.0
.5
6
ft
.9
.0
o
o
0
.0
.0
.4
•2
2.6
.9
.9
2.5
.9
3
.8
.8
ft
ft
.9
2.7
2.3
.9
2.2
KMnO4
Tankl
Lever3'
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
H3/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
26
7
27
40
32
38
7
7
34
7
6
31
37
40
40
33
31
31
33
33
32
31
6
32
33
32
6
29
29
6
6
32
29
NR
46
39
38
46
38
38
36
30
31
33
33
33
29
NR
39
NR
38
31
NR
40
30
29
33
38
32
Outlet
psig
23
13
21
37
21
12
12
19
11
12
21
1
22
34
18
29
22
20
21
28
19
12
19
19
23
11
28
21
11
12
21
22
NR
3
24
25
47
25
23
29
29
25
24
21
18
28
NR
24
NR
24
24
28
NR
40
23
28
20
26
20
Outlet
psig
15
11
15
34
16
26
10
10
24
10
10
27
30
6
38
28
20
26
25
19
17
24
11
23
22
12
20
27
6
6
14
27
NR
1
0
0
0
0
0
19
20
20
19
25
20
NR
3
NR
1
21
NR
40
25
21
22
2
25
psig
5
5
5
5
5
4
0
0
5
0
0
7
5
2
0
2
8
9
8
7
7
7
5
1
5
5
1
5
6
6
5
0
5
=?
1
2
5
0
4
4
5
5
7
8
6
8
R
4
R
4
7
R
0
7
7
6
4
5
psig
3
NA
6
3
11
NA
NA
NA
15
NA
NA
10
NA
18
6
6
2
9
13
12
4
12
NA
13
14
NA
1
8
8
NA
NA
11
NA
43
15
NA
15
7
1
6
9
12
15
1
NA
15
NA
14
7
NA
NA
7
1
13
12
12
psig
11
NA
12
6
16
12
NA
NA
10
NA
NA
4
7
34
2
11
11
5
8
14
15
7
9
11
13
NA
9
2
2
NA
NA
18
NA
NA
39
46
38
38
36
11
11
13
14
8
9
NA
36
NA
37
10
NA
NA
5
8
11
NA
7
Inlet-
psig
11
NA
12
25
17
24
NA
19
NA
NA
14
22
28
0
15
2
6
6
5
6
14
17
18
NA
14
13
13
NA
NA
17
NA
NA
27
36
11
24
22
15
16
16
15
17
11
NA
25
NA
24
14
14
NA
NA
3
12
17
24
17
Flow
gpm
298
0
295
200
433
275
0
409
445
340
235
223
475
476
435
380
400
400
385
370
390
0
429
451
0
0
456
NR
262
0
262
175
267
305
414
410
400
386
374
447
NR
276
NR
260
422
NR
204
444
447
379
285
415
Totalizer to
kgal
785.7
1,072.1
1,329.3
1,629.0
1,887.5
2,504.3
2,785.7
63.6
346.9
910.5
1,614.2
1,929.1
2,568.8
2,853.8
296.8
815.9
1,364.3
1.666.0
1.999.1
2,324.2
2.864.2
3,140.2
123.1
398.3
657.2
914.6
1,469.1
2,241.0
2,781.7
NR
34.0
297.2
1,407.1
1,647.0
2,187.2
2,713.2
2,959.8
292.1
587.3
882.0
1.457.4
2,052.5
2,243.6
2,534.3
2,780.4
30.3
363.7
NR
952.8
1,251.9
1,555.5
1.859.2
2.181.4
2.482.3
Gallon
gal
340.700
286,400
257,200
299,700
258,500
321,500
281,400
NA
283.300
258.100
367.500
314,900
322,900
285,000
323,500
NA
273,400
289,900
301.700
333.100
325,100
277.400
276,000
NA
275,200
258,900
257,400
270,500
254,600
290,100
NA
NA
263.200
331,900
232,400
239,900
279,900
265,200
246,600
NA
295,200
294.700
288.000
295,000
191,100
290,700
246,100
NA
333,400
NA
589,100
299,100
303,600
303.700
322.200
300,900
Daily
Average
gpm
280
282
285
403
437
400
423
WALUE!
420
439
418
415
422
432
457
WALUE!
424
426
380
333
628
397
395
WALUE!
390
393
417
392
405
460
WALUE!
WALUE!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
ffilV/0!
#DIV/0!
397
405
WALUE!
410
404
389
428
391
404
407
385
WALUE!
WALUE!
409
402
407
392
403
Backwash
Tank
No.
I72
I73
I74
I76
I77
680
681
685
686
688
690
694
696
700
702
704
707
710
712
714
716
717
720
721
722
724
725
727
729
733
735
NR
739
741
744
751
754
757
765
769
770
773
775
776
780
783
784
786
787
792
NR
794
795
797
798
800
801
Tank
No.
656
656
657
659
661
664
665
668
672
673
678
680
683
686
688
693
696
697
699
701
704
705
706
707
709
710
713
716
719
NR
720
720
720
720
720
720
720
723
724
727
729
731
734
738
738
740
741
746
NR
749
750
751
753
754
756
Total
kgal
2833.2
2842.0
2848.9
2862.7
2873.2
2895.7
2908.3
2968.3
2978.9
3000.0
3023.8
3048.1
3079.2
3097.4
3119.2
3136.8
3155.1
3170.0
3181.4
3203.2
3211.3
3218.9
3239.5
3245.9
3257.8
3276.2
25.5
43.7
NR
62.3
70.0
109.5
130.7
159.8
184.6
191.7
212.5
224.8
237.0
262.6
288.2
291.9
307.1
314.2
376.6
NR
391.7
410.2
438.7
453.4
468.3
479.8
Daily
kgal
22.1
8.8
6.9
13.8
10.5
8.1
12.6
NA
14.1
10.6
7.2
23.8
13.9
13.9
18.2
14.9
7.3
18.3
14.9
11.4
10.6
8.1
7.6
20.6
11.9
10.9
10.9
9.6
NA
18.6
NA
13.5
10.8
14.6
10.8
7.1
10.7
12.3
12.2
13.0
14.7
3.7
15.2
7.1
37.8
NA
NA
18.5
28.5
14.7
14.9
11.5
Since Last BW
Run
Time
hrs
2.6
5.1
5.0
1.7
5.5
0.0
11.6
0.8
5.6
2.2
4.0
0.0
3.3
5.3
1.0
0.0
8.9
4.1
1.3
6.9
9.1
7.8
9.9
5.8
7.7
0.0
5.3
0.7
4.6
NR
0.0
9.0
3.7
4.0
1.9
0.1
3.1
3.5
0.0
8.4
0.2
3.1
4.2
1.0
3.5
1.1
NR
7.8
7.0
0.2
7.1
4.4
8.1
Run
Time
hrs
11.8
14.3
13.2
5.2
2.1
6.1
6.3
4.9
0.4
4.4
0.8
1.1
0.0
0.8
4.1
0.0
5.3
4.1
7.4
7.2
2.8
0.9
4.4
6.0
7.8
2.1
5.6
0.0
8.8
0.3
NR
1.2
1.2
1.2
1.2
1.2
10.1
9.2
7.3
5.6
2.2
4.7
0.8
0.0
5.0
0.0
5.2
NR
2.7
3.9
4.7
4.5
0.0
3.4
Standby
Time
hrs
0.9
3.7
4.2
0.8
8.1
0.0
8.1
0.6
4.7
7.1
5.8
0.0
5.0
6.8
0.8
6.0
0.0
10.0
6.1
0.0
7.2
6.3
6.7
10.8
0.3
9.2
0.0
5.7
6.8
1.7
8.7
NR
0.0
4.1
2.1
3.9
0.0
0.0
6.8
6.4
0.0
8.9
0.0
1.0
5.4
0.0
6.6
0.0
NR
6.5
6.7
0.0
5.7
4.1
6.3
Standby
Time
hrs
3.3
3.7
7.2
6.1
5.3
7.0
6.8
7.1
5.6
0.0
8.1
0.9
0.5
0.0
0.0
1.3
0.0
6.0
6.4
6.0
6.3
2.7
0.4
5.2
7.5
8.6
5.6
9.0
0.0
0.0
9.3
5.8
0.0
NR
1.8
1.8
1.8
1.8
1.8
1.8
1.8
1.8
9.6
11.5
7.8
9.0
5.5
5.0
8.1
0.0
6.8
0.0
6.3
NR
4.7
6.8
5.0
5.7
0.0
5.2
7.2
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
54
55
57
58
59
60
62
63
64
Day of
Week
Mon
Tue
Wed
Thu
Fti
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Fti
Sat
Sun
Mon
Tue
Wed
Thu
Fti
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Mon
Tue
Wed
Thu
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Mon
Tue
Wed
— pjf—
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Tnu
Fti
Sat
Sun
Mon
Tue
Wed
Thu
Fti
Sat
Sun
Date
08/1 3/07
08/14/07
08/15/07
08/16/07
08/17/07
08/18/07
08/19/07
08/20/07
08/21/07
08/22/07
08/23/07
08/24/07
08/25/07
08/26/07
08/28/07
08/29/07
08/31/07
09/01/07
09/02/07
09/03/07
09/04/07
09/05/07
09/06/07
09/07/07
09/08/07
09/09/07
09/10/07
09/11/07
09/12/07
09/13/07
09/15/07
09/17/07
09/18/07
09/19/07
09/20/07
09/22/07
09/23/07
09/24/07
09/25/07
09/26/07
09/27/07
09/29/07
10/01/07
10/02/07
10/03/07
10/05/07
10/06/07
10/07/07
10/08/07
10/09/07
10/10/07
10/11/07
10/12/07
10/14/07
10/15/07
10/16/07
10/17/07
10/18/07
10/19/07
10/20/07
10/21/07
10/22/07
10/23/07
10/24/07
10/25/07
10/26/07
10/27/07
10/28/07
Time
6:55 AM
6:55 AM
7:05 AM
7:05 AM
7:05 AM
10:00 AM
10:00 AM
7:15 AM
7:10AM
7:30 AM
7:10AM
7:30 AM
7:00 AM
6:55 AM
7:00 AM
7:00 AM
9:30 AM
10:00 AM
NR
7:10AM
7:40 AM
7:10AM
8:30 AM
8:00 AM
7:00 AM
7:00 AM
6:55 AM
7:05 AM
8:30 AM
7:05 AM
7:20 AM
7:35 AM
8:06 AM
8:00 AM
7:40 AM
7:00 AM
7:19AM
7:00 AM
7:00 AM
8:30 AM
7:50 AM
7:27 AM
8:52 AM
7:15AM
8:30 AM
9:00 AM
NR
NR
NR
NR
NR
NR
NR
:05AM
:20AM
:20AM
:15AM
:OOAM
:45AM
:OOAM
:OOAM
:45AM
NR
7:00 AM
8:30 AM
9:30 AM
Tank A Hour
Meter
hrs
5.440.5
5,451.9
5,471.0
5,483.8
5,500.9
5,512.4
5,526.0
5,538.1
5,549.3
5.561.4
5.585.8
5.596.9
5.610.4
5,634.9
5,646.5
5,678.0
5,696.6
5,717.0
5,735.2
5,792.9
5.809.0
5.827.5
5,841.7
5.856.0
NR
5,885.8
5,896.7
5,919.7
5,943.5
5,955.6
5,968.5
5,981.3
6,008.6
6,029.2
6.033.6
6.036.5
6.036.5
6,036.5
6,036.5
6,036.5
6,036.5
6,036.5
6,036.5
6,047.5
6,066.8
6,067.0
6,097.8
6.112.4
6.124.9
6,137.1
6,160.9
6,175.4
6,191.4
6,205.2
6,218.6
26.4
38.2
51.6
66.9
84.3
100.7
114.3
127.8
141.5
156.6
Tank B Hour
Meter
hrs
5.270.5
5,282.5
5,301.6
5,313.1
5,330.4
5,342.9
5,355.6
5,367.4
5,379.6
5.391.2
5.416.7
5.427.8
5.440.9
5,464.4
5,475.9
5,507.5
5,525.3
5,545.9
5,563.7
5,582.0
5,621.8
5.637.6
5.656.5
5,670.6
5.684.8
NR
5,714.6
5,724.9
5,747.2
5,771.4
5,784.3
5,797.1
5,808.9
5,836.3
5,855.4
5.861.3
5.876.5
5.892.6
5,905.0
5,935.2
5,965.7
5,980.4
5,995.1
6,022.6
6,035.4
6,054.2
6,073.7
6, 84.2
6. 98.5
6. 10.5
6, 22.6
6, 46.8
6/60.9
6 61.0
6, 61.0
6, 61.0
6, 61.0
6, 61.0
6, 61.0
6, 61.0
6, 61.0
6, 61.0
6. 61.0
6. 61.0
6, 61.0
6 61.0
TARun
Time
hrs
14.8
11.4
19.1
12.8
17.1
11.5
3.6
2.1
1.2
2.1
1.8
1.1
3.5
'0.3
1.6
20.3
18.6
20.4
18.2
8.1
9.1
0.5
6.1
8.5
4.2
8.5
•iA
9.8
0.9
2.6
3.2
2.1
2.9
2.8
1.8
0.6
4.4
2.9
0.0
0.0
0.0
0.0
0.0
0.0
0.0
11.0
19.3
0.2
30.8
14.6
12.5
12.2
10.2
14.5
16.0
13.8
13.4
NA
11.8
13.4
15.3
17.4
16.4
13.6
13.5
13.7
15.1
TBRun
Time
hrs
14.5
12.0
19.1
11.5
17.3
12.5
2.7
1.8
2.2
1.6
2.5
1.1
3.1
10.0
11.5
20.5
17.8
20.6
17.8
18.3
19.3
20.5
15.8
18.9
14.1
28.3
NA
29.8
10.3
12.0
12.9
12.9
12.8
11.8
11.7
.1
9
5.2
1.1
2.4
.9
5.7
.7
.7
.8
2.8
.8
.5
.3
2.0
2.1
.2
' .1
1
.0
.0
.0
.0
.0
.0
.0
.0
0.0
KMnO4
Tankl
Lever3'
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
H3/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
32
32
27
33
25
32
31
32
32
32
30
33
33
30
31
27
22
23
15
31
24
25
32
31
31
26
28
41
33
20
30
31
33
32
NR
32
31
38
38
36
34
38
39
35
36
32
30
26
36
31
29
31
41
40
36
37
37
38
37
45
36
38
37
46
36
Outlet
psig
21
26
21
20
15
29
21
20
25
18
29
25
20
23
23
18
15
16
21
23
20
19
2
30
30
16
15
43
26
23
20
30
27
22
NR
20
26
4
4
6
6
7
6
6
6
6
30
27
23
21
27
33
30
29
29
31
58
32
26
30
52
28
Outlet
psig
24
20
14
29
20
19
27
25
19
26
19
19
24
28
25
13
20
20
14
24
14
14
17
20
18
16
18
39
19
28
25
20
19
29
NR
29
21
31
32
23
29
30
31
27
31
28
50
22
27
23
23
1
1
1
4
4
4
5
4
29
36
35
23
psig
7
;
5
5
3
7
i
5
6
i
t
7
;
• ;
6
I
3
3
?
7
3
2
2
2
7
•
I
i
7
i
7
7
6
R
6
;
5
5
2)
6
7
t
9
9
9
i
i
7
i
3
5
;
;
;
;
>
i
5
i
5
2
i
psig
11
6
6
13
10
3
10
12
7
14
NA
8
13
7
8
9
7
7
NA
8
4
6
30
1
1
10
13
-2
7
-3
10
1
6
10
NA
12
5
NA
NA
NA
NA
NA
NA
NA
NA
NA
6
4
6
10
NA
13
3
7
8
9
6
-13
4
12
7
-6
8
10
psig
8
12
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Inlet-
psig
15
16
2
8
2
5
5
7
6
6
2
6
7
'4
5
3
9
10
NA
14
11
13
20
19
14
12
14
41
17
3
14
14
16
16
NA
16
15
23
23
16
18
21
21
16
17
13
11
20
15
12
15
28
14
25
20
21
21
22
21
34
21
22
22
34
20
21
Flow
gpm
399
404
244
494
273
404
418
428
379
404
412
318
370
425
407
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
345
386
335
363
348
364
NR
356
373
276
277
136
245
281
262
248
274
468
201
223
281
378
404
363
233
387
253
295
265
260
260
272
NR
275
237
264
365
254
253
Totalizer to
kgal
3.138.3
153.3
453.8
749.6
1,047.0
1,339.5
1,639.4
1,921.1
2,192.1
2.474.1
2.785.1
3.066.8
47.5
351.3
899.0
1,161.9
1,587.5
1,587.9
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
1,746.6
2,216.9
2,714.6
2,974.6
3,240.0
228.5
1,172.6
1.284.7
1.530.0
1.778.4
1,913.6
2,342.2
2,715.1
2,915.4
3,114.3
218.2
356.0
733.0
988.8
1,234.1
1.489.9
1.733.3
1,977.0
2,490.4
2,757.3
3,010.7
3,222.5
161.8
349.8
530.3
725.2
9473
1,191.8
1,384.6
1.591.6
1.782.0
1.964.0
2,181.2
Gallon
gal
656.000
NA
300,500
295,800
297,400
292,500
299,900
581,600
271,000
311.000
281.700
NA
303.800
234,400
262,900
171,400
400
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
158,700
255,100
264,900
260,000
265,400
NA
429,000
112.100
245.300
248.400
135,200
175,800
194,300
200,300
198,900
188,700
137,800
377,000
255,800
245,300
255.800
243.400
243,700
236,300
266,900
253,400
211,800
NA
188,000
180,500
194,900
222 100
244,500
192,800
207.000
190.400
182,000
217,200
Daily
Average
gpm
746
WALUE!
262
407
288
407
381
811
387
405
387
WALUE!
381
385
379
140
0
WALUE!
WALUE!
WALUE!
WALUE!
WALUE!
WALUE!
ft/ALUE!
WALUE!
WALUE!
WALUE!
WALUE!
250
346
338
347
344
361
371
839
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
ffilV/0!
#DIV/0!
194
330
10,768
261
295
331
334
369
311
21,249
#DIV/0!
ft/ALUE!
ft/ALUE!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
ffilV/0!
Backwash
Tank
No.
804
806
807
808
810
812
813
815
816
819
821
822
823
826
827
829
830
831
832
833
834
835
836
838
840
841
842
844
845
847
849
851
858
858
858
858
858
858
858
858
858
859
859
860
862
863
864
865
868
869
871
874
876
879
881
884
886
890
892
895
897
900
903
Tank
No.
759
760
761
764
766
767
769
770
771
775
776
111
779
782
783
785
787
788
790
791
792
794
795
797
799
801
802
803
806
808
809
817
821
826
828
836
840
843
845
851
852
853
855
856
858
860
861
864
Total
kgal
503.0
515.8
533.7
552.5
567.5
578.3
588.7
596.7
606.4
628.1
641.8
648.8
659.2
681.3
690.4
720.3
733.6
743.0
751.0
762.0
774.3
782.0
793.8
821.0
831.4
842.0
853.2
860.3
886.7
917.3
944.1
078.2
091.0
107.1
113.8
140.5
156.1
165.9
173.2
194.0
201.0
204.3
224.8
236.9
246.0
256.6
263.1
283.9
320.8
328.2
338.4
345.3
356.2
1365.2
377.3
389.3
394.9
404.4
412.0
422.5
Daily
gal
1 1
2.8
7.9
8.8
5.0
0.8
0.4
3.0
9.7
0.8
10.4
8.1
9.1
16.6
13.3
9.4
8.0
11.0
12.3
7.7
11.8
NA
41.0
10.4
10.6
11.2
7.1
19.0
12.5
26.8
9.2
12.8
16.1
6.7
10.0
12.2
9.8
7.3
10.1
7.0
3.3
20.5
12.1
9.1
10.6
6.5
10.5
13.1
7.4
10.2
6.9
10.9
9.0
12.1
12.0
5.6
9.5
7.6
10.5
Since Last BW
Run
Time
hrs
8.0
3.2
3.8
6.2
13.3
1.0
4.7
8.0
3.9
4.3
8.8
7.0
6.5
5.9
1.0
11.9
5.9
7.0
4.7
5.1
0.0
0.0
0.2
9.1
18.8
0.6
3.4
5.0
9.0
0.5
3.3
6.2
6.2
6.2
6.2
6.2
6.2
6.2
6.2
1.3
2.0
16.7
2.1
3.6
4.9
7.0
0.0
0.7
2.2
2.7
3.5
0.7
0.0
0.4
4.5
1.9
0.0
1.9
2.2
Run
Time
hrs
4.8
7.1
17.6
0.0
3.3
5.7
0.8
3.1
8.1
1.1
4.2
0.0
2.7
14.3
1.9
1.5
11.2
4.3
13.1
16.7
6.2
11.1
4.2
6.2
6.6
6.6
9.2
0.0
4.1
7.2
5.7
1.0
0.7
5.2
1.6
2.5
0.8
3.6
0.7
6.1
0.0
5.9
0.0
6.5
0.1
4.0
4.9
0.6
0.6
0.6
0.6
0.6
0.6
0.6
0.6
0.6
0.6
0.6
0.6
Standby
Time
hrs
5.6
5.9
0.9
6.7
4.5
0.0
6.8
6.0
5.1
6.0
5.9
7.3
7.3
7.5
0.0
3.5
4.0
0.0
3.3
1.9
2.9
0.0
0.0
0.0
5.4
3.9
0.2
6.5
5.4
8.2
0.0
5.8
5.7
6.6
6.6
6.6
6.6
6.6
6.6
6.6
6.6
0.9
5.7
0.3
3.8
5.4
5.2
4.2
0.0
0.0
2.9
4.8
6.1
0.6
0.0
0.0
5.9
2.0
0.0
2.4
0.8
Standby
Time
hrs
5.2
6.6
3.5
0.0
3.8
8.0
0.0
4.8
6.4
6.1
0.0
5.7
6.1
0.0
6.3
0.0
0.0
0.0
0.0
3.3
2.0
2.8
3.2
3.9
6.2
5.4
0.0
6.7
11.5
0.0
6.1
6.5
5.4
0.0
5.8
5.7
0.0
0.0
6.2
0.9
3.6
0.0
1.2
0.0
8.0
0.0
0.7
0.0
5.3
0.0
4.2
8.5
0.0
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
65
66
67
68
69
70
71
72
73
74
75
Day of
Week
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sun
Date
0/30/07
0/31/07
1/01/07
1/02/07
1/03/07
1/04/07
1/05/07
1/06/07
1/07/07
11/08/07
1/09/07
1/10/07
1/11/07
1/12/07
1/13/07
1/15/07
1/16/07
1/17/07
1/18/07
1/19/07
1/20/07
1/22/07
1/23/07
1/25/07
1/26/07
1/27/07
1/28/07
1/29/07
1/30/07
2/01/07
2/02/07
2/04/07
2/05/07
2/06/07
2/07/07
2/08/07
2/09/07
2/10/07
2/11/07
2/12/07
2/13/07
2/14/07
2/15/07
2/17/07
2/18/07
2/19/07
2/20/07
2/21/07
2/22/07
2/23/07
2/24/07
2/25/07
2/26/07
2/27/07
2/28/07
2/30/07
2/31/07
1/01/08
1/02/08
1/03/08
1/04/08
1/05/08
1/06/08
1/07/08
1/08/08
1/09/08
1/10/08
1/11/08
1/13/08
Time
7:30 AM
7:00 AM
7:00 AM
7:00 AM
8:25 AM
10:30 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:30 AM
7:30 AM
7:20 AM
7:00 AM
7:00 AM
NR
8:30 AM
8:00 AM
6:50 AM
7:00 AM
NR
8:00 AM
8:00 AM
9:47 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
9:00 AM
7:05 AM
7:00 AM
7:00 AM
7:00 AM
8:30 AM
9:00 AM
7:20 AM
7:00 AM
7:01 AM
7:00 AM
7:15 AM
7:00 AM
7:00 AM
7:00 AM
7:05 AM
7:00 AM
7:00 AM
8:30 AM
8:13 AM
12:30PM
10:30 AM
7:00 AM
7:05 AM
7:00 AM
8:30 AM
7:00 AM
1 :00 PM
7:00 AM
7:00 AM
7:00 AM
10:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
9:00 AM
Tank A Hour
Meter
hrs
186.1
200.5
214.4
233.1
247.7
264.9
278.0
293.7
308.8
321.9
332.6
344.7
356.3
368.9
379.1
400.3
NR
422.1
431.9
442.7
454.3
476.5
487.3
508.4
518.3
530.2
541.0
552.3
564.4
573.7
584.4
605.3
616.5
626.5
637.3
648.0
659.7
675.1
687.7
702.5
716.3
731.4
741.2
774.6
787.2
798.3
808.8
820.0
830.2
842.9
866.5
876.5
888.6
899.3
920.9
931.8
947.4
956.0
969.0
983.0
998.1
1,020.5
1,032.2
1,042.9
1,053.2
1,064.2
1,085.2
Tank B Hour
Meter
hrs
6,161.0
6,161.0
6,161.0
6,161.0
6,161.0
6,161.0
6,161.0
6,175.6
6,191.4
6,204.5
6,216.5
6,228.9
6,240.2
6,252.3
6,261.8
6,283.6
NR
6,304.4
6,314.4
6,325.9
6,337.5
6,359.9
6,371.6
6,390.9
6,402.5
6,414.4
6,424.9
6,437.2
6,448.6
6,458.0
6,469.1
6,489.6
6,500.6
6,511.2
6,522.6
6,533.8
6,544.4
6,544.1
6,546.8
6,546.8
6,546.8
6,546.8
6,554.4
6,555.9
6,567.2
6,577.3
6,587.6
6,598.8
6,608.6
6,621.7
6,644.6
6,655.0
6,667.2
6,678.4
6,700.8
6,712.0
6,727.0
6,736.0
6,749.0
6,764.0
6,778.7
6,801.9
6,812.6
6,823.1
6,834.2
6,844.8
6,865.9
TARun
Time
hrs
15
14..
8
4. ;
7
3.
5
5.
3.
0
12.
11. I
12.6
•2
2.0
ft
2 .8
i .8
.8
.6
Tj
•8
j
_9
.9
.8
.3
2.1
i .3
•7
.6
.2
.0
.8
.7
.7
5.4
2.6
.8
.8
5.1
i .8
.2
2.6
.1
.2
2.7
.2
.1
.9
5.6
.6
.0
.0
5.1
8
.7
.7
.3
.0
7
TBRun
Time
hrs
.0
.0
.0
.0
.0
o
.6
5.8
.1
2.0
2.4
.3
2.1
5
2.0
ft
2 .8
.0
.5
.6
4
.7
.3
.6
.9
.3
.4
i .4
.1
J
.0
.6
.4
.2
.6
- .3
7
.0
.0
.0
6
.3
.2
i .8
.1
.4
.2
.2
.0
.4
.2
5.0
i .0
.0
.0
9
.7
.5
.1
•6
8
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jj.g/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
36
39
37
37
36
36
36
29
33
30
32
40
31
32
34
33
NR
41
33
32
32
33
33
32
32
41
34
33
30
38
30
30
34
33
32
32
40
31
38
39
38
38
33
46
35
33
34
33
32
32
32
40
6
8
31
5
5
8
33
33
33
43
32
5
29
5
30
Outlet
Tank A
psig
31
25
27
27
30
23
28
21
20
22
22
27
26
28
19
28
NR
1
21
21
21
24
27
21
22
1
22
28
24
11
25
25
19
21
22
22
28
27
34
31
34
34
26
4
23
24
24
21
26
21
22
1
11
11
23
11
11
11
27
21
21
26
42
22
11
25
11
24
Outlet
TankB
psig
29
35
35
5
7
4
4
24
19
26
26
0
22
20
27
19
NR
25
24
26
27
20
19
25
24
25
22
18
26
10
25
24
26
25
25
25
4
21
3
3
3
0
21
3
21
21
21
26
21
28
27
29
10
10
25
10
10
10
20
25
25
21
39
24
9
25
10
25
Effluent
p g
?
8
Inlet-TA
p g
-6
4
-6
6
Inlet-TB
psig
NA
NA
NA
NA
NA
NA
NA
5
14
4
6
40
9
12
7
14
NA
16
9
6
5
13
14
7
8
16
12
15
4
28
5
6
8
8
7
7
36
10
35
36
35
38
12
43
14
12
13
7
11
4
5
11
-4
-2
6
-5
-5
-2
13
8
8
12
4
8
-4
4
-5
5
Inlet-
Effluent
psig
20
23
21
21
19
20
19
13
18
14
15
25
15
17
19
17
NA
27
17
16
15
18
16
15
15
26
18
17
13
22
13
14
18
17
16
16
25
15
21
24
22
21
16
34
19
17
17
-6
16
15
NA
15
25
-8
-3
14
-8
-3
16
16
18
17
33
15
5
12
-6
12
Flow
rate
gpm
275
217
240
246
260
280
251
378
340
403
401
270
393
400
386
396
NR
268
390
397
400
377
404
386
394
247
367
380
418
392
418
404
382
393
408
402
267
381
302
285
290
310
370
0
369
383
380
0
380
395
413
413
288
11
11
423
0
0
0
384
374
398
392
196
400
0
436
0
430
Totalizer to
Distribution
kgal
2,565.6
2,777.5
2,977.3
3,187.1
117.8
361.3
552.0
833.1
1,121.3
1,374.7
1,552.1
1,923.1
2,187.2
2,467.1
2,696.9
3,204.7
NR
441.6
668.1
924.4
1,191.9
1,717.3
1,972.4
2,468.5
2,701.1
2,979.5
3,234.7
231.0
506.5
722.2
985.0
1,418.0
1,693.9
1,942.3
2,195.1
2,444.0
2,695.6
2,954.7
3,181.1
142.3
362.0
602.4
822.1
1,373.3
1,644.8
1,908.8
2,146.6
2,399.9
2,633.4
2,927.7
398.0
400.0
686.1
257.0
529.4
783.7
1,033.8
1,388.2
1,585.1
1,889.5
2,219.1
2,562.0
2,915.5
3,112.0
109.4
317.4
636.3
894.2
1,443.4
Gallon
Usage
gal
188,700
211,900
199,800
209,800
-3,069,300
243,500
190,700
281,100
288,200
253,400
177,400
371,000
264,100
279,900
229,800
275,300
NA
NA
226,500
256,300
267,500
254,300
255,100
231,900
232,600
278,400
255,200
NA
275,500
215,700
262,800
213,500
275,900
248,400
252,800
248,900
251,600
259,100
226,400
NA
219,700
240,400
219,700
264,300
271,500
264,000
237,800
253,300
233,500
294,300
NA
2,000
286,100
-429,100
272,400
254,300
250,100
354,400
196,900
304,400
329,600
342,900
353,500
196,500
NA
208,000
318,900
257,900
261,800
Daily
Average
Flowrate
gpm
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
#DIV/0!
ffilV/0!
310
311
322
261
505
384
378
389
382
WALUE!
ft/ALUE!
381
383
384
406
379
424
363
390
399
391
385
402
334
414
402
380
379
377
-7,057
849
WALUE!
#DIV/0!
#DIV/0!
428
ffilV/0!
380
416
381
377
389
380
386
3
392
-653
419
380
377
386
373
390
379
384
394
417
WALUE!
327
497
398
448
Backwash
Tank
A
No.
909
911
914
917
920
923
926
927
929
931
933
935
937
939
940
944
NR
947
949
951
953
957
959
963
964
966
968
974
976
978
982
983
985
987
989
991
996
1000
1004
009
014
015
022
024
026
027
028
029
031
034
035
037
039
041
1041
1043
1044
1046
1047
1049
1052
1054
1056
1059
1062
1064
1070
Tank
B
No.
867
868
870
872
873
875
877
879
882
NR
885
887
889
891
896
897
901
903
905
907
912
913
916
919
921
923
925
927
928
928
928
928
928
928
928
928
928
928
929
931
932
933
937
938
939
941
942
943
945
946
947
949
951
953
955
958
961
964
967
975
Total
Volume
kgal
NR
449.8
471.3
481.8
492.7
503.0
512.1
524.7
538.3
541.3
562.7
576.5
590.5
600.1
623.9
NR
644.9
658.4
672.0
685.7
726.1
726.8
752.8
763.6
777.7
791.5
829.2
839.9
857.4
880.8
891.4
904.6
918.6
932.7
942.8
960.7
975.3
989.7
2007.5
2024.9
2028.5
2052.8
2060.1
2070.3
2077.4
2087.9
2094.6
2105.0
2129.7
2136.7
8.2
25.0
32.1
35.6
53.0
60.1
70.9
81.7
96.0
113.8
128.1
146.4
168.0
189.3
206.9
255.2
Daily
Volume
kgal
NA
17.3
I
24.5
Since Last BW
Run
Time
hrs
0.3
5.4
1.3
3.2
1.5
8.7
6.0
3.4
4.0
2.5
0.6
0.4
5.0
0.7
NR
0.0
4.2
3.6
4.1
3.2
0.7
3.5
4.0
0.0
5.5
1.0
0.6
1.1
1.0
6.5
4.5
3.8
3.2
2.6
1.0
0.3
1.1
0.3
0.1
3.2
0.0
6.2
4.2
7.2
8.2
2.4
7.9
1.8
7.9
5.5
6.1
1.8
7.3
2.0
1.0
2.8
1.8
0.9
2.3
1.3
Run
Time
hrs
0.6
0.6
0.6
0.6
0.6
4.3
8.7
0.3
1.4
0.0
4.6
4.3
0.8
5.5
NR
4.2
1.6
0.8
0.1
4.8
1.0
1.6
3.6
0.1
4.5
0.6
1.1
1.4
1.1
0.7
1.0
0.0
0.0
0.0
0.0
0.0
0.0
7.7
0.0
8.7
1.1
2.7
6.4
0.7
0.8
3.8
1.5
1.3
7.1
3.6
6.3
2.7
1.8
0.3
0.0
0.8
0.6
Standby
Time
hrs
0.0
4.0
0.5
0.0
0.0
5.5
6.1
5.1
6.6
4.3
1.8
0.0
6.0
0.6
NR
0.0
8.1
6.6
5.1
— oj~~
1.1
6.8
7.6
0.0
0.0
0.6
0.4
0.0
5.8
6.3
6.6
6.5
4.5
0.0
0.0
0.0
0.0
0.0
7.0
0.0
7.2
10.3
0.0
8.1
8.3
1.9
8.4
7.4
5.5
0.0
4.5
1.1
0.0
4.8
2.3
0.6
0.8
0.0
Standby
Time
TankB
hrs
0.3
0.3
0.3
0.3
0.3
5.6
7.0
0.0
2.3
0.0
8.2
6.4
0.0
6.5
NR
7.3
3.8
0.2
0.0
7.3
8.1
0.7
5.4
6.5
0.0
6.6
0.0
0.8
1.2
0.8
0.7
0.7
0.0
0.0
0.0
0.0
0.0
0.0
10.9
0.0
7.6
7.9
0.2
3.9
7.5
8.4
0.0
1.3
0.2
7.6
1.1
1.5
3.4
1.8
2.8
4.3
2.6
0.6
0.1
0.7
0.0
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
76
77
79
80
82
83
84
85
86
Day of
Week
Mon
Wed
Thj
Fti
Sat
Mon
Tue
Wed
Thu
Fti
Sat
Sun
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fti
Sat
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Fti
Sat
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Tnu
Fti
Sat
Sun
Tue
Thu
Sat
Sun
Mon
Tue
Wed
Tnu
Sat
Mon
Wed
Thu
Fri
Sat
Sun
Date
01/14/08
01/16/08
01/17/08
01/18/08
01/19/08
01/21/08
01/22/08
01/23/08
01/24/08
01/25/08
01/26/08
01/27/08
01/29/08
01/30/08
02/01/08
02/02/08
02/03/08
02/04/08
02/05/08
05/06/08
02/07/08
02/08/08
02/09/08
02/11/08
02/12/08
02/14/08
02/15/08
02/16/08
02/17/08
02/18/08
02/19/08
02/20/08
02/22/08
02/23/08
02/25/08
02/26/08
02/27/08
02/28/08
02/29/08
03/02/08
03/03/08
03/04/08
03/05/08
03/07/08
03/08/08
03/09/08
03/11/08
03/13/08
03/15/08
03/16/08
03/17/08
03/19/08
03/20/08
03/22/08
03/24/08
03/26/08
03/27/08
03/28/08
03/29/08
03/30/08
Time
7:00 AM
7:00 AM
7:00 AM
7:00 AM
1 1 :00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
8:30 AM
7:10AM
7:00 AM
8:00 AM
6:00 AM
12:OOPM
7:00 AM
12:OOPM
7:00 AM
7:00 AM
7:30 AM
8:30 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
9:12 AM
NR
7:00 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
7:30 AM
7:45 AM
7:30 AM
8:00 AM
5:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
10:00 AM
10:00 AM
7:10AM
7:10 AM
9:00 AM
9:00 AM
7:00 AM
8:20 AM
7:10AM
7:40 AM
7:00 AM
7:10AM
7:05 AM
7:00 AM
7:40 AM
7:30 AM
Tank A Hour
Meter
hrs
1,096.3
1,117.4
1,127.7
1,139.3
1,151.8
1 1747
1,192.0
1,201.9
1,215.0
1,230.3
,243.6
,258.4
,285.6
,304.3
,344.4
,362.2
,386.5
,401.6
,422.2
,436.8
,456.2
,477.3
,496.6
,535.6
,553.8
,591.6
,610.8
,629.6
,647.4
,666.8
,684.9
,702.3
,735.5
,751.9
,791.6
,804.4
,828.4
,839.5
,859.5
,873.6
,885.3
,896.9
,920.4
1,931.9
,946.0
,966.2
,988.3
,010.0
,020.9
,034.0
,059.6
,069.0
,091.5
,114.9
,139.9
,151.0
,162.3
,172.7
,184.0
Tank B Hour
Meter
hrs
6,877.1
6,898.1
6,908.9
6,919.8
6,931.2
6,951.6
6,966.8
6,975.5
6,983.8
6,999.6
7,009.3
7,022.9
7,048.1
7,065.4
7,104.9
7,122.8
7,147.3
7,162.0
7,181.6
7,196.1
7,215.5
7,236.3
7,255.4
7,294.6
7,313.1
7,351.5
7,370.7
7,388.6
7,406.3
7,426.5
7,444.6
7,461.5
7,495.1
7,511.7
7,551.6
7,564.1
7,589.4
7,601.3
7,621.8
7,636.0
7,648.5
7,659.9
7,682.9
7,694.8
7,708.4
7,728.4
7,750.3
7,772.2
7,783.3
7,796.8
7,822.1
7,832.0
7,854.7
,878.0
,902.3
,913.3
,925.3
,935.2
,947.1
TARun
Time
hrs
11.1
10.5
0.3
1.6
2.5
0.7
7.3
9.9
13.1
15.3
13.3
14.8
12.0
18.7
19.5
17.8
24.3
15.1
20.6
14.6
19.4
21.1
19.3
20.1
18.2
18.7
19.1
19.2
18.8
17.8
19.4
18.1
17.4
15.3
16.4
18.5
12.8
11.9
11.1
10.9
14.1
11.7
11.6
10.0
11.5
14.1
12.0
10.9
10.9
10.9
13.1
12.6
9.4
10.7
11.3
11.7
11.1
11.3
10.4
11.3
TBRun
Time
hrs
11.2
10.6
10.8
10.9
11.4
8.5
15.2
8.7
8.3
15.8
9.7
13.6
10.9
17.3
18.8
17.9
24.5
14.7
19.6
14.5
19.4
20.8
19.1
9.5
3.5
9.0
9.4
9.2
7.9
7.7
2D.2
3.1
6.9
5.7
6.6
3.6
2.5
2.7
.9
.5
.2
2.5
.4
i .8
.9
.6
.1
.2
.1
.1
.5
.1
9
.9
.2
2.1
.0
2.0
9
.9
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
10.0
NR
NR
NR
NR
NR
NR
NR
5.0
2.0
NR
12.5
11.3
11.3
11.3
8.0
8.0
7.0
NR
10.0
10.5
NR
8.0
11.0
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
31
30
5
30
43
31
7
32
40
42
29
8
39
32
21
21
23
38
21
22
22
32
23
22
24
23
21
26
21
23
22
22
24
22
23
28
31
31
35
36
31
33
33
32
38
31
6
31
39
32
41
32
43
36
34
32
41
32
31
4
Outlet
Tank A
psig
23
25
1
24
39
24
11
28
1
50
24
11
27
11
14
17
19
36
16
21
19
1
15
15
15
20
16
15
16
19
20
20
16
16
19
25
24
24
27
32
22
29
20
28
27
20
11
22
31
21
1
21
43
24
20
28
25
24
23
11
Outlet
TankB
psig
25
23
10
22
38
22
10
29
29
24
25
10
3
20
19
5
4
3
6
4
5
9
0
0
9
4
8
7
8
4
5
5
7
8
5
1
7
26
18
18
26
19
28
20
0
22
10
27
0
28
25
27
40
19
25
20
4
23
28
8
Effluent
p ig
_
?
R
R
Inlet-TA
psig
8
5
4
6
4
7
-4
4
39
-8
5
-3
12
21
7
4
4
2
5
1
3
31
8
7
9
3
5
11
5
4
2
2
8
6
4
3
7
7
8
4
9
4
13
10
4
11
11
-5
9
8
11
40
8
11
0
12
14
4
16
8
8
-7
Inlet-TB
psig
-4
Inlet-
Effluent
psig
19
13
-6
14
13
14
-4
10
25
28
12
-4
25
20
7
6
10
NA
7
7
8
17
8
7
9
8
6
11
7
8
7
7
9
7
8
10
14
26
12
20
21
14
17
17
17
15
23
15
-4
14
25
15
28
38
NA
NA
20
17
15
26
15
14
-6
Flow
rate
gpm
417
414
0
394
188
406
710
406
304
180
440
300
299
NR
273
262
255
146
260
260
270
201
251
253
252
248
256
238
273
250
254
252
241
250
253
371
409
242
418
355
375
386
366
385
401
394
274
360
NR
399
305
388
252
318
397
152
358
360
377
267
380
406
0
Totalizer to
Distribution
kgal
1,720.6
2,252.2
2,504.4
2,787.6
3,077.9
323.1
NR
975.0
1,277.5
1,660.7
1,980.3
2,300.5
2,899.9
3,283.8
522.7
783.3
1,143.4
1,360.3
1,717.7
1,928.9
2,211.6
2,520.1
2,800.7
86.9
351.6
627.0
908.7
1,189.4
1,471.1
1,753.4
2,035.7
2,307.3
2,562.6
3,064.1
22.7
648.4
941.8
1,218.2
1,488.6
1,736.2
2,122.3
2,479.2
2,738.2
2,980.9
3,276.3
207.9
476.2
776.6
1,251.2
1,768.1
2,293.7
2,567.9
2,883.3
3,192.3
NR
412.9
906.7
1,429.2
1,981.1
2,229.0
2,488.8
2,736.8
2,995.1
Gallon
Usage
gal
277,200
267,600
252,200
283,200
290,300
217,500
NA
NA
302,500
383,200
319,600
320,200
281,700
383,900
285,100
260,600
360,100
216,900
357,400
211,200
282,700
308,500
280,600
NA
264,700
275,400
281,700
280,700
281,700
282,300
271,600
255,300
237,900
NA
321,300
293,400
276,400
247,600
188,100
356,900
259,000
242,700
295,400
NA
268,300
300,400
261,300
259,300
275,600
274,200
315,400
309,000
NA
NA
232,200
242,800
267,000
247,900
259,800
248,000
258,300
Daily
Average
Flowrate
gpm
414
423
399
420
406
383
WALUE!
WALUE!
496
411
475
376
411
356
248
243
246
243
297
242
243
245
244
WALUE!
240
244
244
244
256
238
250
248
256
WALUE!
289
387
373
359
280
420
357
352
369
WALUE!
382
362
378
391
418
415
395
393
WALUE!
WALUE!
358
360
374
374
372
407
371
Backwash
Tank
A
No.
073
80
82
87
89
94
96
99
01
05
08
10
14
15
18
20
22
23
25
26
27
29
31
34
35
37
38
39
41
45
147
148
52
54
61
66
69
74
77
78
80
81
83
85
87
90
95
01
210
215
220
225
227
229
232
236
242
244
247
249
251
Tank
B
No.
978
985
988
993
997
007
014
021
031
040
046
050
058
060
065
066
068
069
072
073
077
079
082
083
084
086
087
090
093
095
097
101
102
109
115
116
22
25
27
28
30
32
33
35
39
43
50
58
64
69
73
76
77
80
85
90
92
95
98
200
Total
Volume
kgal
276.0
325.2
342.4
377.3
398.1
450.2
481.1
516.0
557.3
606.2
633.3
633.8
695.4
NR
733.5
744.2
758.3
765.3
782.7
789.7
814.0
828.0
848.9
901.5
925.3
939.1
949.3
976.7
987.2
1035.3
1073.3
1094.5
1125.0
145.1
154.9
188.9
199.4
1213.2
1237.2
1268.1
1311.6
368.5
405.5
441.5
4734
499.7
520.3
550.0
589.6
603.0
623.9
640.9
653.1
Daily
Volume
kgal
20.8
28.4
17.2
34.9
20.8
20.8
30.9
34.9
41.3
48.9
27.1
0.5
20.8
NA
10.4
10.7
14.1
_0
7.4
0
.9
.0
.3
.0
.8
•2
.5
.5
34.2
38.0
21.2
10.5
9.5
13.4
10.5
13.8
24.0
16.8
27.1
34.1
37.0
36.0
31.9
10.1
10.3
10.2
17.5
13.4
20.9
17.0
12.2
Since Last BW
Run
Time
hrs
1.7
1.0
0.0
3.4
3.8
2.4
5.9
0.8
0.0
0.0
1.1
3.4
2.6
0.0
8.5
3.1
2.3
2.9
5.2
1.0
0.0
7.7
9.5
0.6
0.4
8.3
6.8
2.3
0.1
0.6
0.0
1.6
1.5
1.9
3.7
0.3
3.1
6.5
1.0
1.5
0.4
0.7
0.0
0.5
0.6
3.1
4.2
0.3
3.3
3.9
2.1
Run
Time
hrs
1.0
0.0
1.5
2.7
2.3
1 1
0.9
0.2
0.3
1.4
0.3
2.1
0.0
5.2
0.6
7.1
10.1
11.3
3.1
8.4
3.9
1.1
0.5
8.0
6.6
5.5
1.6
1.8
1.5
0.0
2.1
0.8
0.0
0.6
0.8
0.0
0.0
4.3
2.9
0.1
0.0
0.0
1.5
0.0
4.6
7.9
1.4
3.1
0.0
4.7
0.0
Standby
Time
hrs
0.8
1.5
0.0
4.7
2.5
4.9
3.6
0.0
0.0
0.0
0.0
4.9
4.6
0.0
2.8
2.7
0.0
1.8
3.2
0.0
0.0
3.1
1.8
0.0
0.0
3.5
4.3
8.3
0.0
0.0
0.0
0.9
0.6
2.0
5.8
2.4
4.4
0.0
6.0
0.2
1.7
0.0
0.0
0.0
0.0
0.0
7.3
7.1
0.0
5.0
5.1
5.4
Standby
Time
TankB
hrs
0.8
5.4
2.3
4.7
0.6
2.6
0.2
0.0
0.0
0.0
0.0
3.0
0.0
1.5
0.0
2.7
3.8
3.6
0.0
3.4
2.8
1.3
0.0
0.0
1.1
1.8
3.6
3.5
0.5
4.2
0.0
0.0
2.6
0.0
0.0
0.3
1.7
6.8
0.0
0.0
4.8
0.0
0.8
5.5
0.0
0.0
0.0
2.2
0.0
0.0
5.7
9.4
3.6
4.7
0.0
5.1
0.0
6.2
>
oo
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
87
88
89
90
91
92
93
94
95
96
97
Day of
Week
Mon
Tue
Wed
Thj
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Mon
Tue
Wed
Tnu
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Tnu
Fri
Sat
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Thu
Sat
Sun
Date
03/31/08
04/01/08
04/02/08
04/03/08
04/04/08
04/05/08
04/06/08
04/07/08
04/08/08
04/09/08
04/10/08
04/11/08
04/12/08
04/13/08
04/14/08
04/15/08
04/16/08
04/17/08
04/18/08
04/19/08
04/20/08
04/21/08
04/22/08
04/23/08
04/24/08
04/25/08
04/26/08
04/27/08
04/28/08
04/29/08
04/30/08
05/01/08
05/03/08
05/04/08
05/05/08
05/06/08
05/07/08
05/08/08
05/10/08
05/12/08
05/13/08
05/14/08
05/15/08
05/16/08
05/17/08
05/18/08
05/20/08
05/22/08
05/23/08
05/24/08
05/26/08
05/27/08
05/29/08
05/30/08
05/31/08
06/01/08
06/02/08
06/03/08
06/04/08
06/05/08
06/06/08
06/07/08
06/08/08
06/09/08
06/10/08
06/12/08
06/14/08
06/15/08
Time
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:10 AM
8:30 AM
8:30 AM
7:00 AM
7:00 AM
6:55 AM
7:00 AM
6:55 AM
10:15AM
9:15 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:40 AM
7:00 AM
7:00 AM
6:55 AM
7:00 AM
7:00 AM
8:00 AM
8:00 AM
7:00 AM
7:00 AM
8:30 AM
8:50 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:10AM
7:40 AM
7:05 AM
NR
8:30 AM
6:55 AM
6:50 AM
7:00 AM
7:45 AM
7:00 AM
7:00 AM
7:00 AM
7:10 AM
8:40 AM
8:30 AM
6:50 AM
7:00 AM
7:15AM
7:10AM
7:00 AM
8:00 AM
8:00 AM
7:00 AM
6:50 AM
6:55 AM
9:00 AM
6:30 AM
Tank A Hour
Meter
hrs
2,196.7
2,208.1
2,219.5
2,229.9
2,240.9
2,251.1
2,262.4
2,274.3
2,286.7
2,297.9
2,309.6
2,321.4
2,333.1
2,345.6
2,356.4
2,368.0
2,407.6
2,417.7
2,429.2
2,444.3
2,457.3
2,483.4
2,495.6
2,507.1
2,518.6
2,530.3
2,543.9
2,595.7
2,607.3
2,618.6
2,630.7
2,642.4
2,655.6
2,682.2
2,712.0
2,725.1
2,737.0
2,748.1
2,760.0
2,771.2
2,782.6
2,804.7
2,826.5
2,836.9
2,845.8
2,869.5
2,882.6
2,908.5
2,920.6
2,932.5
2,945.7
2,957.0
2,969.2
2,982.3
2,993.6
3,005.2
3,016.6
3,030.1
3,042.2
3,055.8
3,078.3
3,102.7
3,112.8
Tank B Hour
Meter
hrs
7,959.6
7,971.2
7,982.5
7,992.8
8,004.1
8,014.4
8,024.7
8,037.3
8,049.2
8,061.6
8,074.4
8,086.9
8,098.3
8,111.1
8,122.5
8,133.6
8,171.0
8,181.0
8,193.2
8,207.8
8,220.9
8,248.3
8,259.8
8,271.0
8,282.7
8,294.5
8,308.3
8,354.8
8,370.9
8,381.8
8,393.2
8,404.9
8,418.3
8,. 44.6
8,. 73.0
8,. 36.8
8,. 98.8
8,509.2
8,520.5
8,531.4
8,543.9
8,567.0
8,589.0
8,599.1
8,608.0
8,631.6
8,644.7
8,670.5
8,683.2
8,695.0
8,706.8
8,718.5
8,730.5
8,742.7
8,753.8
8,766.2
8,779.3
8,791.4
8,803.8
8,816.0
8,637.9
8,862.1
8,872.6
TARun
Time
hrs
2.7
.4
.4
.4
.0
.2
.3
.9
2.4
.2
.7
.8
.7
2.5
.8
.6
2.9
.1
.5
5.1
.0
.2
2.2
.5
.5
.7
.6
.3
.6
.3
2.1
.7
.2
.3
5.3
.1
.9
.1
.9
.2
.4
.0
7
.4
.9
.6
.1
3.0
2.1
.9
3.2
.3
2.2
.1
.3
.6
.4
3.5
2.1
.6
2.2
2.6
.1
TBRun
Time
hrs
12.5
11.6
11.3
0.3
1.3
0.3
0.3
2.6
1.9
2.4
2.8
2.5
1.4
2.8
1.4
1.1
1.7
0.0
2.2
4.6
3.1
3.1
1.5
1.2
1.7
1.8
13.8
8
.1
.9
.4
.7
.4
.0
.6
.8
2.0
.4
.3
.9
2.5
.5
g
.9
.0
.1
3.0
2.7
.8
.8
.7
2.0
2.2
.1
24
.1
2.1
2.4
2.2
- 7.9
2.0
.5
KMnO4
Tankl
Level(a)
inches
11.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
6.0
11.0
15.0
NR
8.0
6.0
5.0
5.0
5.0
NR
8.0
4.0
9.0
8.0
8.0
8.0
8.0
10.0
11.0
8.0
9.0
9.0
8.0
8.0
7.0
8.0
4.0
7.0
7.0
10.0
10.0
10.0
9.0
9.0
8.0
0.0
NR
NR
7.0
33.0
NR
NR
NR
NR
9.0
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
42
42
39
36
36
38
31
43
34
34
31
32
36
4
31
34
41
5
32
4
34
33
35
39
32
36
4
32
44
34
32
39
34
4
35
32
32
34
34
33
33
33
35
34
32
35
32
35
31
30
32
32
5
35
31
34
32
31
33
30
33
38
32
30
38
33
33
Outlet
Tank A
psig
25
51
30
21
23
33
22
44
22
22
24
30
33
11
28
20
1
11
25
11
25
21
21
30
22
20
12
23
42
24
28
27
11
25
27
29
27
27
29
30
26
21
27
25
22
31
21
25
25
23
23
13
22
25
24
30
30
24
25
25
33
31
30
48
22
10
Outlet
TankB
psig
3
22
45
21
25
0
28
41
24
26
27
20
NR
9
22
28
26
10
24
9
20
28
23
50
27
26
10
28
44
21
20
21
9
21
21
21
20
20
20
19
21
24
20
24
23
21
23
27
28
29
26
10
23
21
24
21
22
24
27
27
0
20
23
32
28
10
Effluent
P 9
.
;
;
5
;
i
7
i
i
7
7
i
I
8
)
7
7
1
6
6
5
7
)
1
?
7
7
6
)
5
7
1
i
;
7
7
7
i
i
7
i
i
i
7
6
7
7
)
i
t
6
i
7
7
t
8
5
;
;
5
7
NR
Inlet-TA
psig
17
-9
9
15
13
5
9
-1
12
12
7
2
3
-7
3
14
-6
7
-7
9
12
14
12
9
16
-8
9
2
10
4
7
-7
10
5
3
7
7
4
3
7
14
7
7
13
1
14
6
5
9
9
-8
13
6
10
2
1
9
5
8
5
1
0
-10
11
23
Inlet-TB
psig
39
20
-6
15
11
38
3
2
10
8
4
12
NA
-5
9
6
-5
8
-5
14
5
12
6
-11
10
-6
4
0
13
12
39
13
-5
14
11
11
14
14
13
14
12
11
14
8
12
11
12
4
2
3
6
-5
12
10
10
11
9
9
3
6
38
12
7
6
5
23
Inlet-
Effluent
psig
28
26
23
21
20
22
14
43
18
18
14
15
20
-1
13
16
-5
15
-5
15
19
17
24
-6
14
NA
17
15
24
18
-6
20
15
14
8
8
6
6
6
9
8
5
9
16
9
4
4
5
5
-5
19
13
8
6
4
6
5
3
6
4
3
6
NA
Flow
rate
gpm
256
224
368
340
381
315
405
126
382
378
407
388
315
0
416
384
0
394
0
395
350
385
296
386
372
NR
401
122
363
390
386
0
367
388
381
370
383
381
395
386
354
370
404
347
390
367
410
422
408
403
0
351
396
383
402
411
398
400
318
402
422
312
391
NR
Totalizer to
Distribution
kgal
0.8
264.4
521.4
750.5
1,000.6
1,240.4
1,429.1
1,758.3
2,030.7
2,293.1
2,566.8
2,834.7
3,139.6
142.0
346.0
601.0
1,198.5
1,488.5
1,715.7
2,328.9
2,611.6
2,936.8
3,225.3
217.4
473.8
731.5
996.1
1,297.2
1,593.4
1,915.6
2,728.6
2,978.6
3,247.1
242.4
556.2
1,153.5
1,805.1
2,119.7
2,394.7
2,644.1
2,907.0
3,180.2
165.6
705.3
1,223.6
1,461.9
1,685.1
2,229.0
2,532.2
3,139.4
155.2
437.8
719.8
993.1
1,261.3
1,551.0
1,811.1
2,381.1
2,646.7
2,930.8
3,228.2
493.7
1,054.6
1,287.2
Gallon
Usage
gal
NA
263,600
257,000
229,100
250,100
239,800
188,700
329,200
272,400
262,400
273,700
267,900
304,900
NA
204,000
255,000
318,200
290,000
227,200
341 ,900
282,700
325,200
288,500
NA
256,400
257,700
264,600
301,100
296,200
322,200
259,300
250,000
268,500
NA
313,800
286,000
338,600
314,600
275,000
249,400
262,900
273,200
NA
256,500
252,700
238,300
223,200
288,400
303,200
308,900
NA
282,600
282,000
273,300
268,200
289,700
260,100
300,400
265,600
284,100
297,400
292,000
287,900
232,600
Daily
Average
Flowrate
gpm
WALUE!
382
377
369
374
390
292
448
374
372
373
368
440
ft/A LIE!
307
375
382
394
377
384
361
384
381
WALUE!
377
370
375
366
371
391
320
375
381
WALUE!
393
363
378
390
384
387
378
412
WALUE!
417
390
388
418
391
386
396
ft/ALUE!
397
377
396
369
382
387
411
347
387
385
187
390
377
Backwash
Tank
A
No.
1254
1256
1259
1260
1262
1264
265
267
268
270
272
274
276
277
279
280
286
290
292
303
306
308
310
312
314
316
319
323
330
332
333
336
340
344
348
351
353
354
355
357
359
363
368
369
377
383
385
387
389
390
392
394
395
401
403
404
408
412
1414
Tank
B
No.
202
205
207
209
211
212
214
215
217
219
221
222
224
226
227
229
234
238
241
252
254
257
259
261
263
265
267
271
278
280
282
284
288
292
296
299
301
303
305
307
309
313
317
319
327
333
335
337
340
341
343
345
350
352
355
360
365
366
Total
Volume
kgal
670.9
691.0
707.3
714.0
727.2
737.4
748.1
758.5
769.2
782.9
796.9
806.9
818.1
829.8
839.3
848.9
886.5
914.0
930.6
009.5
061.4
080.0
093.6
108.2
127.7
154.3
182.9
211.5
2260.0
2274.0
2285.4
2313.9
2353.4
2399.8
2429.3
2461.2
2475.8
2486.2
2507.0
2529.1
2551.7
2579.5
2610.4
2620.8
2673.0
2715.7
2725.3
2738.4
2757.2
2766.8
2779.9
2789.5
2824.3
2837.0
2849.6
2880.6
2907.2
2916.8
Daily
Volume
kgal
17.8
20.1
16.3
6.7
13.2
10.2
0.7
0.4
0.7
3.7
4.0
10.0
11.2
11.7
9.5
9.6
23.9
27.5
16.6
24.9
51.9
18.6
14.6
19.5
26.6
28.6
28.6
14.0
11.4
28.5
39.5
16.2
18.7
31.9
14.6
10.4
20.8
22.1
22.6
14.2
16.7
10.4
13.0
22.9
9.6
13.1
9.6
13.1
9.6
9.4
12.7
12.6
17.9
12.5
9.6
Since Last BW
Run
Time
hrs
2.3
0.0
1.4
6.9
5.1
1.0
4.4
0.6
5.2
4.0
3.0
0.0
1.0
4.7
0.0
6.1
1.1
1.0
1.7
2.8
1.2
2.5
3.8
3.9
3.3
3.7
2.7
0.3
0.0
1.1
0.5
2.3
1.5
0.2
0.2
4.0
7.6
2.3
4.8
4.4
0.0
5.1
3.1
2.2
4.8
5.2
0.9
0.2
5.1
1.2
0.2
0.0
0.0
5.0
0.0
Run
Time
hrs
0.0
3.1
0.0
5.4
2.4
0.0
1.2
4.6
2.6
1.9
0.8
6.5
0.0
1.7
4.0
1.2
1.9
1.2
0.6
0.8
0.0
0.5
1.4
1.4
0.1
0.8
2.9
3.3
3.7
2.6
7.5
1.2
2.9
5.7
5.0
6.0
7.4
4.1
6.6
0.0
7.6
0.3
1.0
2.9
5.1
8.2
1.5
3.8
3.1
1.8
0.0
0.0
0.0
1.1
5.6
Standby
Time
hrs
5.0
0.0
1.1
7.1
4.7
0.0
6.5
0.0
6.3
5.5
5.5
0.0
0.0
7.5
0.0
1.5
0.1
0.0
5.7
5.5
5.0
0.9
4.4
8.2
5.5
4.5
0.0
15
0.0
0.0
0.0
4.9
5.8
0.0
0.0
5.7
3.5
4.8
5.6
2
3
3
1
5
4. ;
5 ;
7
6
7
0
6
— £
6.
2.2
0.6
7.8
0.4
Standby
Time
TankB
hrs
0.0
5.9
0.0
6.3
4.7
0.0
0.0
5.8
6.3
3.7
0.6
7.2
0.0
1.3
5.3
0.9
0.1
0.5
1.2
7.2
6.5
0.8
0.0
0.0
2.4
4.1
0.0
0.0
5.0
0.4
6.0
4.3
3.3
5.8
4.6
5.0
5.9
5.7
4.8
5.6
5.1
6.1
6.2
6.7
3.5
0.0
1.2
5.5
7.3
2.1
6.8
8.0
6.1
6.2
1.1
0.1
0.0
5.0
4.4
0.0
0.7
8.8
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
98
99
100
104
105
107
108
Day of
Week
Mon
Tue
Thj
Fri
Sat
Sun
Mon
Wed
Tnu
Fri
Sun
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Fri
Sat
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Fri
Sun
Mon
Wed
Thu
Sat
Sun
Mon
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Fri
Sat
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Date
06/16/08
06/17/08
06/19/08
06/20/08
06/21/08
06/22/08
06/23/08
06/25/08
06/26/08
06/27/08
06/29/08
07/01/08
07/02/08
07/03/08
07/04/08
07/06/08
07/07/08
07/08/08
07/09/08
07/11/08
07/12/08
07/14/08
07/15/08
07/16/08
07/18/08
07/20/08
07/21/08
07/22/08
07/23/08
07/25/08
07/27/08
07/28/08
07/30/08
07/31/08
08/02/08
08/03/08
08/04/08
08/06/08
08/07/08
08/08/08
08/09/08
08/10/08
08/11/08
08/12/08
08/13/08
08/15/08
08/16/08
08/18/08
08/19/08
08/20/08
08/21/08
08/22/08
08/23/08
08/24/08
08/26/08
08/27/08
08/28/08
08/29/08
08/30/08
08/31/08
Time
7:00 AM
8:30 AM
6:50 AM
7:00 AM
8:30 AM
9:00 AM
7:00 AM
7:05 AM
7:15AM
7:05 AM
8:00 AM
7:00 AM
7:05 AM
7:15 AM
7:15 AM
7:00 AM
7:15AM
6:50 AM
7:00 AM
7:00 AM
8:15 AM
7:30 AM
7:00 AM
6:50 AM
7:00 AM
10:00 AM
6:55 AM
7:05 AM
7:10AM
7:10AM
8:00 AM
7:00 AM
7:05 AM
7:10AM
10:00 AM
10:00 AM
7:00
6:55 AM
7:05 AM
6:50 AM
6:45 AM
7:30 AM
6:55 AM
7:00 AM
6:50 AM
7:50 AM
7:10AM
7:00 AM
7:00 AM
7:00 AM
7:10AM
9:50 AM
7:00 AM
7:00 AM
NR
1 1 :30 AM
8:00 AM
Tank A Hour
Meter
hrs
3,124.9
3,141.4
3,169.6
3,184.1
3,204.9
3,226.1
3,247.6
3,276.1
3,289.4
3,304.5
3,338.2
3,372.0
3,389.1
3,408.6
3,427.3
3,461.6
3,482.5
3,504.8
3,528.6
3,570.3
3,590.3
3,632.6
3,654.0
3,676.1
3,707.1
3,753.0
3,773.0
3,796.2
3,817.2
3,862.8
3,891.3
3,904.4
3,932.6
3,946.3
3,972.0
3,984.1
3,995.4
4,029.7
4,043.6
4,057.1
4,071.5
4,085.4
4,111.3
4,136.8
4,155.5
4,200.0
4,219.6
4,238.9
4,259.0
4,278.8
4,294.8
4,354.5
4,369.4
NR
4,402.4
4,415.1
Tank B Hour
Meter
hrs
8,884.7
8,900.2
8,928.9
8,942.2
8,962.2
8,983.3
9,004.1
9,032.7
9,045.7
9,060.1
9,092.1
9,125.9
9,141.4
9,161.0
9,179.9
9,214.2
9,234.5
9,257.3
9,280.9
9,321.9
9,341.1
9,383.7
9,405.6
9,428.0
9,462.3
9,507.6
9,527.7
9,550.0
9,570.5
9,616.5
9,644.5
9,656.6
9,683.7
9,697.2
9,722.0
9,733.5
9,744.5
9,778.8
9,792.4
9,804.6
9,818.5
9,832.2
9,857.7
9,882.7
9,901.5
9,945.1
9,963.8
9,983.2
10,002.4
10,022.0
10,037.4
10,096.4
10,110.8
NR
10,141.4
10,158.5
TARun
Time
hrs
2.1
5.5
4.2
4.5
2D.8
1.2
1.5
3.5
3.3
5.1
7.0
3.6
7.1
9.5
3.7
9.3
0.9
2.3
3.8
9.7
0.0
2D.8
1.4
2.1
5.1
21.9
20.0
23.2
21.0
23.7
13.0
13.1
14.6
3.7
3.3
2.1
1.3
4.0
3.9
3.5
4.4
3.9
2.0
3.2
8.7
3.1
9.6
9.3
0.1
9.8
6.0
6.6
4.9
NA
NA
12.7
TBRun
Time
hrs
2.1
5.5
4.0
3.3
0.0
1.1
0.8
3.4
3.0
4.4
6.4
8.7
5.5
9.6
8.9
9.3
0.3
2.8
3.6
9.7
9.2
20.6
21.9
22.4
15.2
21.9
20.1
22.3
20.5
23.1
12.3
12.1
13.6
3.5
2.5
1.5
1.0
3.4
3.6
2.2
3.9
3.7
1.9
2.5
8.8
2.5
8.7
9.4
9.2
9.6
5.4
7.0
4.4
NA
NA
17.1
KMnO4
Tankl
Level(a)
inches
NR
NR
6.0
10.0
1.0
NR
NR
NR
NR
9.0
NR
NR
NR
NR
3.5
NR
NR
NR
6.0
2.0
3.0
3.0
3.0
3.0
2.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
3.0
4.0
4.0
4.0
3.0
0.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
0.0
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
40
33
33
41
9
. 1
. 0
;2
5
39
38
23
26
28
33
24
22
21
26
24
41
46
30
28
22
22
25
22
25
20
27
28
7
29
6
30
30
39
30
29
28
28
28
40
32
23
22
29
26
23
30
42
31
29
44
NR
43
7
Outlet
Tank A
psig
28
23
31
5
17
36
40
23
13
55
33
22
16
18
24
19
18
22
22
21
42
38
28
24
22
17
18
17
17
18
18
27
25
13
24
13
22
24
6
29
28
28
28
28
3
16
18
17
24
20
18
22
44
23
27
44
NR
18
15
Outlet
TankB
psig
3
26
26
24
20
35
40
28
10
32
2
16
18
18
0
16
18
15
14
15
41
36
36
31
14
20
20
19
20
18
19
23
26
10
24
10
26
25
26
21
24
23
23
24
26
21
20
18
26
15
19
48
43
26
24
42
NR
0
13
Effluent
psig
15
16
15
15
NR
12
10
Inlet-TA
psig
12
10
2
36
12
5
0
9
-8
-16
5
1
10
10
9
5
4
-1
4
3
-1
8
2
4
0
5
4
8
5
7
2
0
3
-6
5
-7
8
6
8
33
1
1
0
0
0
37
16
5
5
5
6
5
8
-2
8
2
0
NA
25
-8
Inlet-TB
psig
8
NA
43
-6
Inlet-
Effluent
psig
25
17
18
26
14
41
40
-5
23
23
8
12
13
18
NA
7
6
11
9
41
46
16
13
8
6
5
10
7
10
5
11
12
-3
14
-4
15
14
17
25
15
14
12
11
26
17
8
7
13
11
8
15
25
15
13
44
NA
31
-3
Flow
rate
gpm
283
402
403
242
250
95
105
0
303
312
270
238
254
216
244
258
250
239
249
98
91
212
230
270
264
261
262
265
262
449
156
0
405
0
407
411
381
287
402
396
408
409
280
321
266
248
412
244
260
398
173
384
415
128
NR
165
0
Totalizer to
Distribution
kgal
1,564.0
1,935.4
2,566.5
2,880.0
3,204.5
248.8
557.0
1,524.2
1,863.5
2,603.9
3,271.7
266.8
560.8
833.0
1,414.8
1,733.1
2,049.1
2,381.9
2,973.9
3,273.9
608.2
908.7
1,181.2
1,815.8
2,161.1
2,779.4
3,112.1
141.1
810.0
1,527.6
1,855.2
2,535.4
2,873.3
232.1
514.3
777.1
1,284.0
1,604.6
1,928.9
2,227.9
2,550.8
3,158.1
154.1
733.1
1,025.7
166.8
2,017.2
2,312.5
2,597.2
2,880.6
3,219.8
893.6
1,267.3
1,586.9
NR
2,283.0
2,309.3
Gallon
Usage
gal
276,800
371,400
317,000
313,500
324,500
NA
308,200
317,800
339,300
382,300
296,700
NA
294,000
272,200
295,100
318,300
316,000
332,800
285,900
300,000
304,400
300,500
272,500
^5300
304,800
332,700
NA
341,100
326,100
327,600
344,800
337,900
NA
282,200
262,800
259,300
320,600
324,300
299,000
322,900
298,400
-3,004,000
295,500
292,600
-1,171,300
1,850,400
295,300
284,700
283,400
339,200
327,200
373,700
319,600
NA
NA
NA
Daily
Average
Flowrate
gpm
381
387
375
377
265
WALUE!
403
384
382
265
WALUE!
251
241
255
258
234
234
242
255
245
231
204
253
244
WALUE!
243
430
434
408
414
ft/ALUE!
399
393
422
390
393
389
380
362
-4,190
384
260
-856
1,611
254
242
240
360
367
371
364
ft/ALUE!
WALUE!
WALUE!
Backwash
Tank
A
No.
1415
1417
1422
1423
1424
1425
1432
1434
1439
1442
1442
1443
1445
1448
1449
1451
1452
1454
1455
1457
1460
1463
1475
1476
1477
1480
488
490
497
500
505
507
509
513
515
518
520
522
526
527
531
533
1536
1538
1539
1540
1541
1544
1546
1550
1553
NR
1574
1584
Tank
B
No.
368
371
376
378
380
381
390
394
399
403
405
406
407
4 3
4 4
4 5
4 8
420
422
424
425
435
437
438
441
451
455
464
467
474
477
479
483
486
489
492
495
501
503
509
511
515
518
519
521
522
526
528
534
537
NR
566
567
Total
Volume
kgal
2926.0
2941.6
2973.7
2983.4
2992.5
2999.0
3050.2
3070.1
3100.8
3137.5
3144.0
3152.3
3184.6
3194.3
3204.1
3210.8
3228.9
3238.6
3251.8
3268.1
4.1
51.8
74.6
84.4
90.7
110.0
167.2
185.6
235.9
254.4
290.6
305.8
318.0
342.2
357.1
375.3
391.1
406.1
436.8
445.7
475.5
488.1
524.4
565.8
581.9
606.7
624.6
715.5
798.1
847.6
NR
958.6
958.6
Daily
Volume
kgal
9.2
15.6
19.2
9.7
9.1
6.5
12.7
19.9
16.2
11.8
6.5
8.3
6.3
9.7
9.8
6.7
6.6
9.7
6.6
16.3
NA
18.6
6.6
9.8
6.3
9.7
25.8
18.4
15.5
18.5
15.2
5.2
2.2
2.2
4.9
8.2
5.8
5.0
5.4
8.9
4.8
2.6
27.6
41.4
16.1
24.8
17.9
33.9
NA
NA
0.0
Since Last BW
Run
Time
hrs
3.6
7.2
0.7
0.0
20.8
20.4
2.7
0.0
1.7
2.9
19.9
17.5
13.8
0.1
5.3
5.0
12.0
NR
5.6
3.0
1.0
14.2
13.3
14.0
8.0
0.2
1.7
2.6
2.2
3.3
3.5
4.3
0.0
0.3
0.5
0.1
0.1
0.0
0.0
6.8
8.5
2.9
6.6
10.6
8.0
NR
0.0
12.2
Run
Time
hrs
6.8
3.7
0.0
5.4
6.8
11.4
1.4
1.2
1.2
11.8
5.8
3.5
2.4
1.8
0.0
15.3
2.9
11.2
19.6
18.6
6.1
6.5
1.8
6.6
1.5
1.0
0.4
0.6
1.5
1.9
0.8
3.4
0.0
2.0
1.1
1.4
1.1
2.5
0.3
1.9
3.3
0.6
12.6
4.6
0.0
3.1
2.2
NR
0.0
17.2
Standby
Time
hrs
0.0
3.6
3.2
0.0
4.1
2.3
2.8
0.0
0.0
3.2
9.5
9.7
13.8
6.4
0.0
17.4
0.3
4.7
1.4
0.0
0.0
0.0
0.0
0.0
2.5
0.0
0.0
2.4
2.4
1.5
2.1
7.5
5.9
7.1
3.2
0.3
1.0
0.1
0.0
0.0
0.0
3.6
0.0
0.5
2.8
1.4
1.5
1.9
0.5
NR
0.0
6.2
Standby
Time
TankB
hrs
0.0
3.0
3.9
5.6
3.7
2.3
1.2
0.0
0.0
3.2
3.1
2.7
3.0
2.4
0.0
8.0
3.2
2.9
1.4
0.0
0.0
3.3
0.0
0.0
0.0
2.6
0.0
0.0
0.0
0.0
0.9
0.8
0.0
1.9
7.1
5.0
3.8
2.9
1.3
1.2
0.7
5.1
0.0
0.5
0.0
0.6
2.8
1.4
0.0
3.9
0.5
NR
0.0
6.2
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
110
111
112
114
116
117
118
119
Day of
Week
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Wed
Thu
Fri
Sat
Sun
Mon
Wed
Tnu
Sat
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Tue
Thu
Sat
Mon
Tue
Wed
Thu
Sat
Sun
Date
09/01/08
09/02/08
09/03/08
09/05/08
09/06/08
09/07/08
09/08/08
09/09/08
09/10/08
09/11/08
09/12/08
09/13/08
09/14/08
09/15/08
09/17/08
09/18/08
09/19/08
09/20/08
09/21/08
09/22/08
09/24/08
09/25/08
09/27/08
09/28/08
09/29/08
09/30/08
0/01/08
0/03/08
0/04/08
0/05/08
0/06/08
0/07/08
0/08/08
0/09/08
0/10/08
0/11/08
0/12/08
0/14/08
0/15/08
0/17/08
0/18/08
0/20/08
0/21/08
0/22/08
0/23/08
0/24/08
0/26/08
0/27/08
0/28/08
0/29/08
0/30/08
0/31/08
1/01/08
1/02/08
1/04/08
1/06/08
1/08/08
1/10/08
1/11/08
1/12/08
1/13/08
1/15/08
1/16/08
Time
NR
NR
NR
7:00 AM
5:30 AM
8:00 AM
NR
7:00 AM
7:00 AM
6:00 AM
6:55 AM
9:00 AM
9:00 AM
6:40 AM
6:55 AM
6:55 AM
8:30 AM
8:30 AM
6:55 AM
6:55 AM
7:00 AM
8:00 AM
8:10AM
7:05 AM
6:55 AM
6:50 AM
7:00 AM
8:30 AM
8:00 AM
7:00 AM
NR
6:50 AM
NR
NR
NR
NR
7:05 AM
7:00 AM
6:55 AM
6:45 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:30 AM
7:00 AM
6:50 AM
7:00 AM
7:00 AM
7:00 AM
7:30 AM
8:00 AM
6:55 AM
6:50 AM
NR
7:00 AM
8:15 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
Tank A Hour
Meter
hrs
NR
NR
NR
4,426.9
4,439.5
4,451.0
4,464.1
4,477.4
4,489.1
4,502.7
4,516.0
4,553.5
4,566.5
4,579.1
4,591.6
,604.6
,617.6
,644.7
,658.1
,682.0
,696.4
,711.6
,724.7
,738.5
,766.8
,785.2
,804.0
,824.3
4,834.2
4,845.7
4,862.4
4,882.0
. ,899.9
. ,914.0
. ,952.3
. ,969.3
4,996.7
5,013.7
5,052.3
5,070.2
5,088.2
5,105.6
5,168.0
5,189.1
5,211.5
5,227.6
5,240.8
5,253.5
5,264.5
5,279.0
5,303.6
5,328.1
NR
5,373.5
5,390.3
5,405.4
5,419.8
5,447.1
5,463.2
Tank B Hour
Meter
hrs
NR
NR
NR
0,165.3
0,175.0
0,175.2
0,186.4
0,198.6
0,211.2
0,222.9
0,236.0
0,249.4
0,286.3
0,299.1
0,311.4
0,324.5
0,336.7
0,349.3
0,375.9
0,388.7
0,413.0
0,426.9
0,442.1
0,455.6
0,469.0
0,497.8
0,516.4
0,535.2
0,555.1
0,564.8
0,576.2
0,592.7
0,612
0,629 I
0,643
0,681
0,698.0
0,725.2
0,741.8
0,780.4
0,798.1
0,816.3
0,833.3
0,895.7
0,916.5
0,939.2
0,955.5
0,969.1
0,981.3
0,991.9
1,006.4
1,030.9
1,055.4
NR
1,100.5
1,117.7
1,132.3
1,146.7
1,173.5
1,189.8
TARun
Time
hrs
NA
NA
NA
)
2.6
.5
.1
.3
.7
.6
.3
5
3.0
2.6
2.5
.0
0
4
4
.0
.4
5.2
3.1
.8
5.3
.4
.8
i .9
.5
i.7
.6
7.9
.1
4
7.0
.8
7.0
.7
9
.0
4
2
1
4
1
3.2
7
.0
5
3
7
NA
.9
8
1
.4
2.9
1
TBRun
Time
hrs
NA
NA
NA
)
i .7
.2
2.2
2.6
.7
.1
.4
4
2.8
2.3
3.1
2.2
6
2
8
2.5
.9
5.2
3.5
.4
5.2
.6
.8
.9
i .7
.4
i.5
.6
7.3
.1
2 .9
i.7
.7
_6
.2
7
.2
0
3
8
7
3
3.6
2
6
5
2
7
NA
11.7
17.2
14.6
14.4
12.8
16.3
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
19.0
29.0
NR
NR
NR
NR
21.0
NR
NR
NR
4.0
13.0
14.0
NR
15.0
15.0
15.0
15.0
15.0
15.0
15.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
24.0
NR
NR
NR
NR
3.0
13.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
NR
NR
NR
13
38
19
31
32
5
31
32
4
32
33
29
29
30
30
29
28
31
5
30
30
31
39
29
29
31
39
27
29
28
31
32
20
30
31
32
42
35
42
35
34
45
27
32
36
37
37
5
37
37
27
37
36
NR
36
38
6
Outlet
Tank A
psig
NR
NR
NR
8
16
24
25
25
13
24
24
13
25
23
28
26
25
24
27
28
22
11
23
27
23
28
25
26
20
18
27
23
18
23
23
22
27
30
29
24
38
27
27
46
22
30
32
32
29
10
31
30
29
31
32
NR
33
29
11
Outlet
TankB
psig
NR
NR
NR
10
13
22
21
21
22
10
26
25
11
25
24
24
26
25
27
23
25
26
10
26
23
26
36
20
20
22
17
23
21
14
24
22
16
22
20
22
26
1
29
44
23
25
32
28
34
10
30
32
32
30
30
NR
34
31
9
Effluent
psig
NR
NR
NR
5
;
2;.
?
?
?
?
?
?
?
;
7
7
7
7
6
7
I
)
7
;
5
3
;
;
;
7
;
5
;
?
5
7
;
7
6
5
6
5
2
8
;
6
i
6
7
6
6
;
?
6
;
Inlet-TA
psig
NA
NA
NA
5
22
-4
-4
6
7
-8
7
8
-9
8
7
10
1
3
5
6
2
0
9
-6
7
3
8
11
4
3
11
21
0
6
10
8
9
-2
3
1
3
11
4
8
-1
5
2
4
5
8
-5
6
7
-2
6
4
NA
3
9
-5
Inlet-TB
psig
NA
NA
NA
3
25
Inlet-
Effluent
psig
NA
NA
NA
-2
25
-3
NA
NA
NA
NA
NA
NA
NA
17
16
17
12
12
3
3
3
1
13
-5
13
12
15
24
16
13
15
23
10
13
13
15
NA
5
13
15
15
27
19
27
19
17
7
12
18
21
21
-5
21
20
11
21
20
NA
20
22
21
6
Flow
rate
gpm
NR
NR
NR
0
0
0
0
380
375
0
386
389
0
364
380
378
420
430
400
392
407
442
408
0
410
409
274
366
374
355
173
373
373
239
381
370
252
396
398
389
245
359
263
360
352
85
180
292
332
338
352
0
330
333
343
334
350
NR
315
311
315
0
Totalizer to
Distribution
kgal
NR
NR
NR
2,310.1
2,620.6
2,629.8
2,629.8
2,905.6
3,189.7
206.7
488.4
794.7
1 ,093.4
1,375.6
1,942.0
2,229.8
2,519.0
2,805.0
3,208.1
127.7
764.7
1,077.9
1,661.6
1,984.0
2,331.8
2,946.1
302.5
661.0
992.6
1,341.6
1,520.2
1,756.1
2,088.2
2,438.6
2,811.2
3,131.1
530.1
871.5
1,440.8
1,799.8
2,608.5
3,005.1
147.2
518.9
901.2
1,773.2
2,071.9
2,451.7
3,028.3
3,272.5
202.4
483.0
964.6
1,431.3
1,869.4
2,389.9
2,608.9
2,887.6
3,148.2
377.3
683.0
Gallon
Usage
gal
NA
NA
NA
0
310,500
9,200
NA
275,800
284,100
NA
281,700
306,300
298,700
282,200
282,100
287,800
289,200
286,000
403,100
NA
335,600
313,200
304,600
322,400
347,800
304,600
309,700
302,500
358,500
331,600
349,000
178,600
235,900
332,100
350,400
372,600
319,900
318,700
341,400
239,400
359,000
398,000
396,600
147,200
371,700
382,300
455,100
298,700
379,800
261,900
244,200
202,400
280,600
247,700
220,300
210,300
302,800
219,000
278,700
260,600
241,500
305,700
Daily
Average
Flowrate
gpm
WALUE!
WALUE!
WALUE!
#DIV/0!
472
#DIV/0!
WALUE!
405
375
WALUE!
383
373
381
378
372
387
373
534
WALUE!
391
399
434
380
381
382
380
331
323
294
289
304
343
333
298
353
378
240
338
340
356
350
371
136
360
330
341
238
281
326
327
312
323
337
314
WALUE!
428
215
313
302
313
315
Backwash
Tank
A
No.
NR
NR
NR
584
593
594
594
595
595
598
599
600
602
603
605
606
607
608
612
614
617
619
623
624
629
632
634
635
636
637
639
641
642
643
647
648
650
651
654
656
660
662
665
671
672
675
680
681
683
686
689
692
696
699
701
705
707
Tank
B
No.
NR
NR
NR
567
583
584
584
585
585
589
590
591
594
595
597
599
600
062
609
614
616
619
621
625
628
630
632
633
634
637
639
641
642
646
647
649
650
653
655
658
661
664
669
671
673
678
679
680
683
686
689
692
694
697
701
703
Total
Volume
kgal
NR
NR
NR
958.6
042.5
049.0
049.0
060.7
060.7
085.9
093.1
100.2
117.9
125.0
157.0
213.1
241.0
255.4
280.9
291.5
326.2
344.9
358.8
369.4
376.9
384.4
402.7
417.0
428.3
435.1
463.5
470.7
484.7
492.3
513.9
528.3
553.3
571.1
593.0
632.0
642.9
660.6
696.6
703.5
714.4
736.0
757.3
802.4
819.9
839.0
866.8
Daily
Volume
kgal
NA
NA
NA
0.0
83.9
D
7
.0
5
2
1
1
1
.6
7.3
.4
4
.6
2; .8
.6
5
5
.3
.3
11.3
6.8
14.0
7.2
7.2
11.0
14.4
25.0
17.8
21.9
10.9
17.7
10.6
6.9
10.9
7.2
7.2
-1750.9
13.6
17.5
19.1
7.2
Since Last BW
Run
Time
hrs
NR
NR
NR
0.0
0.0
0.4
8.9
22.0
10.6
10.9
11.2
11.7
6.9
0.0
5.2
6.3
0.2
5.4
2.7
10.6
0.6
0.8
5.6
1.8
8.9
11.1
0.0
3.9
0.1
0.0
9.0
1.0
5.7
5.7
3.0
16.4
0.4
1.5
6.8
8.9
5.3
5.8
6.4
5.2
2.0
0.0
5.1
7.0
Run
Time
hrs
NR
NR
NR
0.0
0.0
0.0
9.1
10.0
6.2
7.4
8.8
6.6
4.1
1.1
1.6
2.0
0.5
1.4
0.0
6.3
6.1
4.1
6.9
9.0
5.2
8.0
10.0
7.9
11.4
8.4
7.6
0.0
3.4
2.8
6.2
11.5
10.2
3.7
0.9
1.5
7.0
4.1
3.8
7.1
4.3
0.0
2.4
6.0
Standby
Time
hrs
NR
NR
NR
0.0
0.0
0.0
8.9
18.2
8.5
8.7
9.3
7.8
9.7
6.7
5.8
0.0
7.0
5.9
0.0
4.5
2.8
1.9
0.0
0.5
4.1
0.7
5.2
7.2
0.0
2.2
0.0
3.0
0.0
3.2
0.0
3.4
0.9
1.3
0.9
0.0
1.1
6.0
9.5
6.4
6.3
7.6
6.2
3.8
0.0
4.7
7.4
Standby
Time
TankB
hrs
NR
NR
NR
0.0
0.0
0.0
8.4
10.0
0.1
6.8
8.7
7.8
6.0
5.4
4.0
1.9
3.3
0.6
1.8
2.8
0.0
5.4
0.7
0.0
1.9
7.5
4.9
4.1
1.9
5.2
6.6
0.0
3.2
10.8
5.9
2.0
3.2
0.0
2.6
0.0
0.9
0.0
5.4
0.0
5.3
7.1
6.3
6.9
7.4
5.2
0.0
1.7
7.4
3.8
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
120
123
125
127
129
130
Day of
Week
Mon
Tue
Wed
Thj
Fri
Sat
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Sat
Sun
Mon
Wed
Fri
Sun
Tue
Wed
Tnu
Sat
Sun
Mon
Wed
Fri
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Sun
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Wed
Tnu
Fri
Sat
Sun
Mon
Wed
Thu
Fri
Sat
Sun
Date
11/17/08
11/18/08
11/19/08
11/20/08
11/21/08
11/22/08
11/23/08
11/24/08
11/25/08
11/26/08
11/28/08
1 1/29/08
11/30/08
12/02/08
12/03/08
12/05/08
12/06/08
12/07/08
12/08/08
12/09/08
12/10/08
12/11/08
12/13/08
12/14/08
12/15/08
12/17/08
12/19/08
12/21/08
12/23/08
12/24/08
12/25/08
12/27/08
12/28/08
12/29/08
12/31/08
01/02/09
01/03/09
01/04/09
01/05/09
01/06/09
01/07/09
01/08/09
01/09/09
01/10/09
01/11/09
01/12/09
01/13/09
01/14/09
01/16/09
01/17/09
01/18/09
01/19/09
01/21/09
01/22/09
01/23/09
01/24/09
01/25/09
01/26/09
01/28/09
01/29/09
01/30/09
01/31/09
02/01/09
Time
7:00 AM
7:30 AM
7:15AM
7:00 AM
7:30 AM
8:00 AM
8:00 AM
6:50 AM
7:00 AM
10:30 AM
9:00 AM
NR
7:00 AM
7:00 AM
7:00 AM
8:00 AM
8:00 AM
6:55 AM
7:05 AM
7:00 AM
7:00 AM
NR
NR
7:00 AM
7:00 AM
8:00 AM
9:00 AM
7:00 AM
NR
9:00 AM
NR
NR
7:00 AM
7:00 AM
7:00 AM
7:30 AM
8:00 AM
7:00 AM
6:55 AM
6:55 AM
7:00 AM
7:00 AM
8:00 AM
7:30 AM
7:15AM
7:10AM
7:10AM
7:05 AM
8:00 AM
8:00 AM
6:50 AM
6:50 AM
6:45 AM
7:00 AM
NR
NR
7:00 AM
7:30 AM
7:30 AM
7:15AM
7:30 AM
7:00 AM
Tank A Hour
Meter
hrs
5,477.8
5,496.6
5,510.5
5,523.8
5,537.7
5,550.4
5,564.9
5,593.6
5,607.0
5,640.7
5,655.1
5,668.7
5,699.3
5,713.5
5,741.3
5,755.9
5,769.6
5,785.3
5,798.9
5,812.8
5,828.2
5,856.1
5,870.3
5,886.7
5,914.1
5,945.3
5,974.5
6,002.8
6,018.5
6,035.6
6,066.5
6,078.4
6,092.4
6,125.6
6,154.7
6,170.0
6,185.6
6,201.2
6,216.7
6,230.7
6,247.3
6,263.5
6,279.7
6,293.8
6,310.4
6,325.4
6,341.1
6,375.1
6,391.4
6,409.6
6,424.5
6,456.2
6,473.7
6,492.1
6,510.2
6,528.2
6,545.2
6,579.4
6,597.6
6,615.5
6,632.2
6,645.0
Tank B Hour
Meter
hrs
,203.8
222.7
250.0
,264.3
276.8
,291.0
,319.7
333.0
,366.3
,380.3
394.0
,424.5
,438.8
,466.0
,480.9
,496.0
,510.2
,523.9
,537.7
,552.9
,581.2
,595.6
,611.3
,639.8
,670.1
,698.9
,727.2
,743.2
,759.8
,790.2
,802.6
,816.1
849.2
,878.1
,893.4
,909.5
,924.6
,939.7
,953.2
,968.9
,985.1
2,000.8
2,014.6
2,031.4
2,045.9
2,061.7
2,095.6
2,111.5
2,129.3
2,143.4
2,174.9
191.1
2,207.9
225.3
2,241.5
2,258.1
2,290.1
2,306.7
2,323.3
2,340.0
2,352.6
TARun
Time
hrs
4.6
8.8
3.3
.9
.7
.5
.5
.4
7.0
.4
.6
. .5
. .2
.3
.6
.7
5.7
.6
3.9
5.4
.3
.2
i.4
.4
5.9
i.O
2.7
5.7
7.1
.1
.9
. .0
.8
.0
5.3
5.6
5.6
5.5
.0
.6
i.2
2
, .1
.6
.0
.7
8.5
6.3
8.2
4.9
6.4
7.5
8.4
8.1
8.0
7.0
6.7
8.2
7.9
6.7
2.8
TBRun
Time
hrs
4.0
8.9
3.4
.3
5
.2
.5
.3
7.0
.0
.7
. .5
. .3
.8
.9
5.1
.2
.7
3.8
5.2
.9
.4
7
; .6
5.1
5.5
2.7
;.o
.6
7.9
2.4
; .5
7
.0
5.3
1.1
5.1
5.1
3.5
5.7
i.2
5.7
8
8
. .5
8
.9
5.9
7.8
.1
5.8
.2
i.8
.4
i.2
i.6
5
i.6
i.6
i.7
2.6
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
31.5
NR
NR
NR
NR
NR
NR
NR
NR
8.5
19.5
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
36
46
7
37
37
7
37
6
37
37
44
33
38
37
37
38
36
37
37
37
44
38
38
37
38
37
7
37
37
39
43
37
37
40
38
39
39
38
39
39
44
38
39
39
44
39
39
39
39
43
39
44
38
39
40
NR
39
39
39
40
40
44
26
Outlet
Tank A
psig
31
45
11
30
36
11
32
35
35
40
32
31
35
34
29
31
33
30
33
38
33
32
32
35
33
12
37
33
31
47
36
36
33
37
37
35
39
36
37
45
34
37
35
1
38
33
36
38
5
37
3
38
37
34
NR
38
38
34
33
32
4
23
Outlet
TankB
psig
33
44
10
35
31
10
32
33
35
32
36
31
11
35
33
34
36
34
33
34
35
36
34
34
35
37
42
35
34
37
41
32
32
39
33
34
35
41
35
37
33
NR
32
33
37
34
38
36
23
Effluent
P 9
7
)
6
7
7
~^~
R
24
Inlet-TA
psig
5
1
-4
1
-4
5
2
2
4
1
7
2
3
9
5
4
7
4
6
5
6
5
3
4
-5
0
4
8
-4
1
1
7
1
2
4
3
2
-1
4
2
4
43
1
6
3
1
38
2
41
0
2
6
NA
1
1
5
7
8
40
3
Inlet-TB
psig
8
3
Inlet-
Effluent
psig
19
46
-3
20
7
20
6
21
21
29
18
23
20
22
22
20
21
21
22
30
22
23
22
23
22
-3
21
21
22
30
21
22
24
23
24
24
23
-233
24
44
23
24
24
30
22
24
23
24
30
23
30
23
24
25
NA
24
24
24
25
25
29
2
Flow
rate
gpm
334
70
0
318
0
334
333
330
167
320
317
318
309
290
306
315
288
297
139
310
320
298
302
298
0
296
282
280
148
280
285
268
293
292
285
290
275
290
147
283
289
288
164
293
283
291
275
157
287
167
295
295
276
NR
285
277
288
268
0
0
0
Totalizer to
Distribution
kgal
947.6
1,298.3
1,555.7
1,798.8
2,054.6
2,284.2
2,549.3
307.0
40.1
649.3
906.6
1,152.0
1,706.3
1,950.1
2,440.9
2,696.2
2,930.9
3,196.1
151.1
392.1
640.8
1,095.0
1,343.2
1,630.2
2,120.8
2,647.2
3,131.9
325.9
585.4
871.7
1,367.4
1,539.3
1,764.7
2,304.9
2,794.1
3,048.0
31.8
279.3
533.0
769.2
1,041.5
1,312.9
1,578.2
1,808.1
2,087.5
2,332.1
2,584.1
3,139.5
125.2
421.9
654.0
1,184.1
1,459.5
1,745.1
2,045.6
2,327.9
2,582.2
3,122.0
125.7
312.7
322.3
323.0
Gallon
Usage
gal
264,600
350,700
257,400
243,100
255,800
229,600
265,100
307,000
40,100
307,900
257,300
245,400
264,000
243,800
245,000
255,300
234,700
265,200
151,100
241,000
248,700
205,000
248,200
287,000
234,000
257,100
262,800
208,800
259,500
286,300
291,800
171,900
225,400
292,100
173,100
253,900
31,800
247,500
253,700
236,200
272,300
271,400
265,300
229,900
279,400
244,600
252,000
302,900
125,200
296,700
232,100
273,300
275,400
285,600
300,500
282,300
254,300
266,500
-2,996,300
187,000
9,600
700
Daily
Average
Flowrate
gpm
309
310
309
303
302
304
308
353
50
302
302
300
303
285
291
289
272
296
184
290
271
251
289
298
301
277
278
274
273
283
270
236
273
274
289
276
33
269
276
286
281
279
277
275
279
276
267
270
130
275
267
283
273
271
282
276
252
276
-2,876
181
10
1
Backwash
Tank
A
No.
08
10
12
13
15
16
17
720
721
725
726
727
731
733
735
737
738
739
740
741
742
745
747
747
751
756
760
763
766
768
773
775
776
781
785
787
790
791
794
797
801
805
808
810
814
816
819
825
827
831
833
842
846
849
854
858
862
869
874
880
887
891
Tank
B
No.
705
707
09
11
12
13
715
718
719
723
725
726
730
732
735
737
738
739
740
741
743
745
747
748
751
756
761
764
766
769
774
776
777
782
786
788
793
797
801
808
812
816
819
822
825
828
834
837
841
844
854
861
868
875
883
888
900
909
918
926
930
Total
Volume
kgal
892.9
906.9
921.6
943.2
950.0
982.2
989.4
2018.1
2028.7
2035.9
2064.2
2078.6
2096.4
2110.8
2118.0
2125.2
2132.4
2139.5
2150.1
2164.2
2171.3
2186.4
2211.0
2247.0
2279.5
2300.3
2336.2
2336.2
2371.4
2385.4
2392.2
2428.9
2457.6
2471.6
2504.5
2528.8
2553.7
2593.0
2621.8
2646.4
2664.2
2684.5
2706.9
2728.0
2771.5
2789.2
2818.0
2837.2
2904.2
2944.2
2979.4
3022.1
3064.7
3096.4
3164.2
3214.9
3264.7
43.0
61.6
Daily
Volume
kgal
11.0
14.0
14.7
10.9
6.8
14.4
7.2
14.4
10.6
7.2
14.3
14.4
11.0
14.4
7.2
7.2
7.2
7.1
10.6
6.9
7.1
15.1
10.9
14.4
18.2
7.2
35.9
0.0
21.2
14.0
6.8
22.3
14.8
11.0
24.3
24.9
39.3
28.8
24.6
17.8
20.3
22.4
21.1
25.6
17.7
28.8
19.2
40.1
40.0
35.2
42.7
42.6
31.7
32.6
50.7
49.8
-3221.7
18.6
Since Last BW
Run
Time
hrs
9.2
8.1
3.4
0.5
NR
NR
0.9
3.3
3.3
7.4
9.9
1.7
3.7
9.7
6.6
8.5
9.9
10.0
8.4
8.4
8.1
8.9
5.2
5.3
2.8
0.1
5.5
11.0
0.0
2.0
0.6
7.6
1.5
1.5
8.1
1.8
1.6
2.3
1.4
2.9
0.0
0.9
5.1
1.4
1.1
0.0
1.7
0.0
0.2
1.0
3.1
NR
0.3
0.7
2.2
2.2
2.4
0.0
8.4
Run
Time
hrs
1.8
5.4
4.6
6.4
NR
3.4
7.4
0.0
4.1
9.0
3.2
6.1
4.6
1.5
4.5
8.4
10.7
0.0
0.6
0.8
10.1
2.0
7.8
5.6
0.7
5.0
5.9
7.0
2.7
1.0
7.3
1.9
2.1
4.2
0.7
2.0
0.8
2.6
1.0
0.6
3.5
5.6
2.4
4.0
3.6
2.4
0.0
0.6
0.0
1.3
NR
1.8
1.8
0.1
0.9
0.0
0.0
8.9
Standby
Time
hrs
4.8
4.0
5.5
0.0
3.9
5.8
0.8
4.5
1.6
5.1
6.8
2.0
0.0
7.9
6.1
6.6
4.7
6.4
5.7
4.9
4.5
6.1
4.6
5.3
1.6
0.0
4.5
7.9
0.0
0.6
0.7
5.4
0.8
.8
, .7
.5
.0
.7
.6
.6
.0
.0
. .0
.1
.0
.0
.0
.1
—
.0
.4
NR
.0
•0
.0
.4
.0
.2
8.5
Standby
Time
TankB
hrs
1.9
4.0
5.5
6.4
7.4
5.8
4.7
5.3
0.0
4.2
6.8
1.9
0.0
5.3
0.3
6.7
4.7
6.4
0.0
0.0
0.0
6.2
2.8
5.3
4.8
0.0
4.3
5.0
7.2
0.6
0.7
5.3
8.8
2.8
3.8
4.2
0.0
1.0
0.0
2.4
0.0
0.0
3.8
4.0
1.1
1.0
4.5
0.0
0.0
0.0
0.0
0.0
NR
0.0
1.3
0.1
0.0
0.0
1.1
8.7
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
131
132
133
134
135
136
138
139
140
Day of
Week
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
Sat
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Wed
Thu
Fri
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Fri
Sun
Date
02/02/09
02/03/09
02/04/09
02/05/09
02/06/09
02/07/09
02/08/09
02/09/09
02/10/09
02/11/09
02/12/09
02/13/09
02/14/09
02/15/09
02/16/09
02/17/09
02/18/09
02/19/09
02/20/09
02/21/09
02/22/09
02/23/09
02/24/09
02/25/09
02/26/09
02/27/09
02/28/09
03/01/09
03/02/09
03/03/09
03/04/09
03/05/09
03/07/09
03/09/09
03/10/09
03/11/09
03/12/09
03/13/09
03/15/09
03/16/09
03/17/09
03/18/09
03/20/09
03/21/09
03/23/09
03/24/09
03/25/09
03/26/09
03/27/09
03/28/09
03/29/09
03/30/09
04/01/09
04/02/09
04/03/09
04/04/09
04/05/09
04/07/09
04/08/09
04/09/09
04/10/09
04/11/09
04/12/09
04/13/09
04/14/09
04/15/09
04/17/09
04/19/09
Time
6:50 AM
7:00 AM
6:55 AM
7:20 AM
7:00 AM
8:00 AM
8:00 AM
7:30 AM
7:10AM
6:55 AM
6:55 AM
7:00 AM
6:00 AM
6:50 AM
6:45 AM
6:50 AM
6:50 AM
6:55 AM
7:15 AM
7:30 AM
6:48 AM
6:50 AM
6:48 AM
6:45 AM
6:55 AM
7:00 AM
7:00 AM
6:50 AM
6:38 AM
6:52 AM
6:50 AM
8:00 AM
7:15AM
7:00 AM
6:55 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
6:50 AM
7:00 AM
9:00 AM
6:45 AM
7:00 AM
7:10AM
7:10AM
6:45 AM
7:00 AM
10:00 AM
6:47 AM
7:00 AM
NR
NR
NR
6:55 AM
7:00 AM
7:00 AM
8:00 AM
8:00 AM
8:00 AM
6:55 AM
7:00 AM
8:00 AM
Tank A Hour
Meter
hrs
6,655.7
6,665.0
6,675.9
6,687.1
6,699.4
6,711.5
6,723.5
6,735.9
6,746.5
6,757.9
6,769.8
6,781.5
6,791.1
6,516.1
6,827.9
6,839.7
6,851.1
6,861.9
6,873.6
1,885.0
,897.2
1,909.7
NR
1,933.7
1,946.0
1,958.1
1,978.9
1,984.1
1,997.2
,009.1
,021.5
,047.1
,083.3
,087.2
,099.7
,112.7
,124.4
,150.0
,161.0
,174.0
,188.6
,216.0
,230.6
,256.6
,269.6
,282.4
NR
,294.0
,313.0
,327.2
,327.7
,339.4
,352.5
,365.4
,378.3
,391.4
,418.3
,430.9
,443.6
,456.6
,472.1
,488.2
,524.3
,552.7
,577.8
Tank B Hour
Meter
hrs
2,363.3
2,373.6
2,384.9
2,396.1
2,408.6
2,420.8
2,433.0
2,445.9
2,456.7
2,468.0
2,480.0
2,492.2
2,501.9
2,528.0
2,528.0
2,552.6
2,564.6
2,575.9
2,588.0
2,600.0
2,627.0
2,625.8
2,639.2
2,651.3
2,644.1
2,676.5
2,689.7
2,705.5
2,717.3
' 2,729.4
2,742.3
2,768.8
2,794.8
2,809.2
2,822.1
2,835.0
2,847.5
2,874.2
2,885.6
2,898.8
2,913.3
2,941.7
2,957.5
2,983.9
2,997.3
3,010.4
NR
3,022.3
3,041.5
3,055.8
3,056.3
3,068.1
3,081.3
3,094.4
3,107.3
3,120.1
3,148.2
3,161.3
3,174.7
3,188.7
3,205.4
3,222.2
3,260.3
3,290.0
3,315.8
TARun
Time
hrs
10.7
9.3
.9
.2
.7
.7
2.5
2
'
2
2.5
.7
i
;
2.7
.2
.7
;
2.7
5.5
.2
.2
TBRun
Time
hrs
0.7
0.3
1.3
1.2
2.5
2.2
2.2
2.9
0.8
1.3
2.0
2.2
9.7
NA
NA
0.0
24.6
12.0
11.3
12.1
12.0
NA
NA
13.4
12.1
NA
NA
13.2
5.8
1.8
'2.1
2.9
3.5
4.1
4.4
2.9
2.9
2.5
4.7
1.4
3.2
4.5
4.1
5.8
3.3
3.4
3.1
NA
NA
19.2
.3
.5
.8
.2
.1
2.9
.8
.8
.1
.4
.0
i.7
.8
2 7
2.1
5.1
.6
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
35.0
NR
NR
NR
NR
NR
NR
26.0
NR
NR
7.0
16.0
26.0
34.0
NR
NR
NR
NR
0.0
9.0
18.5
28.0
36.0
8.0
16.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
5.0
12.0
20.0
27.0
NR
36.0
36.0
NR
NR
NR
13.0
17.0
4.0
NR
10.0
13.0
16.0
19.0
24.0
25.0
26.0
28.0
NR
29.0
30.0
30.0
34.0
33.0
33.0
30.5
30.5
30.5
31.0
31.0
Estimated
KMnO4
Dosage
jj.g/L as Mn
Pressure Filtration
Influent
psig
26
34
33
34
35
33
30
28
33
35
33
41
9
NR
7
8
34
33
34
7
34
33
6
33
44
8
34
34
34
33
33
41
34
27
35
33
34
35
34
42
36
36
34
34
35
34
44
35
NR
39
46
33
33
33
34
34
33
34
33
7
34
30
30
31
48
40
28
33
Outlet
Tank A
psig
22
28
30
28
27
28
25
28
30
28
30
39
9
NR
10
11
28
31
32
10
29
29
30
42
11
29
28
28
29
29
36
31
22
29
30
28
29
29
51
26
30
33
32
33
33
44
33
20
15
32
30
31
28
30
31
31
31
10
31
29
30
31
50
37
26
29
Outlet
TankB
psig
21
31
30
30
27
31
25
16
30
32
29
1
9
10
10
29
29
29
10
31
31
31
42
10
31
31
30
28
30
50
27
18
25
27
30
26
32
38
30
26
29
30
27
28
43
30
23
48
32
31
27
29
29
31
28
29
10
30
20
30
20
49
1
25
30
Effluent
p g
3
;
;
;
;
i
5
?
i
i
i
5
?
0
0
;
7
I
)
7
7
6
?
?
i
7
7
;
' 7
5
7
3
i
i
i
i
5
5
5
5
5
5
5
5
5
5
?
5
5
i
7
I
;
;
7
6
9
)
7
7
1
|
5
.
7
Inlet-TA
p g
ft/A JE!
ft/A .UE!
Inlet-TB
psig
5
3
ft/A JE!
ft/A .UE!
Inlet-
Effluent
psig
3
18
17
18
19
17
15
ft/ALUE!
17
19
17
26
ft/ALUE!
ft/ALUE!
-3
-2
18
16
16
-3
17
16
17
ft/ALUE!
ft/ALUE!
18
17
17
17
16
26
17
14
19
17
18
19
19
27
21
21
19
19
20
19
29
20
ft/ALUE!
24
31
17
16
15
18
18
16
18
14
-3
17
13
12
13
48
25
14
16
Flow
rate
gpm
0
0
373
368
345
375
372
346
364
359
343
263
NR
NR
0
0
348
340
346
0
352
360
259
137
0
363
362
340
345
363
255
360
357
332
346
350
322
365
191
330
337
345
343
337
350
156
340
NR
245
362
365
368
335
340
353
370
355
342
0
334
336
344
350
0
250
395
345
Totalizer to
Distribution
kgal
323.0
323.0
536.6
775.0
1,027.5
1 ,274.8
1,523.2
1,778.1
2,011.4
2,245.6
2,488.0
2,732.4
2,942.7
NR
205.8
436.7
681.9
922.9
1,397.5
1,637.3
1,887.3
2,649.8
2,908.6
3,155.1
139.5
414.1
679.5
920.1
1,170.9
1,688.0
2,203.6
2,486.8
2,743.4
3,005.9
3,244.3
480.8
703.7
953.5
1,232.8
1,512.9
1,776.2
2,076.9
2,595.7
2,862.2
3,117.0
68.6
238.7
509.9
513.2
737.4
987.7
1,234.9
1 ,482.3
1,745.1
2,241.1
2,482.5
2,730.4
2,989.1
17.9
3130
800.3
1,041.3
1,577.8
2,085.1
Gallon
Usage
gal
0
0
213,600
238,400
252,500
247,300
248,400
254,900
233,300
234,200
242,400
244,400
210,300
ft/ALUE!
ft/ALUE!
230,900
245,200
241,000
237,900
239,800
250,000
259,000
239,600
258,800
246,500
-3,015,600
274,600
265,400
240,600
250,800
267,100
276,500
283,200
256,600
262,500
238,400
278,500
222,900
249,800
280,100
263,300
300,700
257,100
266,500
254,800
ft/ALUE!
ft/ALUE!
170,100
271,200
3,300
223,700
250,300
247,200
247,400
262,800
261,500
241,400
247,900
258,700
-2,971,200
295,100
253,400
241,000
258,500
235,500
Daily
Average
Flowrate
gpm
0
0
321
355
339
339
342
336
344
338
341
363
ft/ALUE!
ft/ALUE!
ft/ALUE!
256
344
333
342
ft/ALUE!
ft/ALUE!
ft/ALUE!
ft/ALUE!
ft/ALUE!
-3,112
585
356
334
331
334
259
769
337
338
329
324
332
318
330
319
330
330
337
328
ft/ALUE!
ft/ALUE!
148
317
110
317
317
317
320
338
317
313
317
320
-3,080
299
322
345
295
344
Backwash
Tank
A
No.
891
895
897
898
900
902
904
906
911
915
919
922
931
935
939
945
952
956
960
974
978
981
985
989
993
• 996
999
2005
2009
2013
2016
2019
2022
2029
2031
2034
2041
2045
2050
2058
2063
2067
2070
2070
2071
2071
2073
2075
2078
2 81
2 84
2 89
2 92
2 96
2 02
2 09
2 15
2 24
2 28
2 37
2 49
Tank
B
No.
1930
1933
1934
1935
1936
1938
1939
1940
1944
1946
1948
1951
1956
1959
1961
1964
1968
1970
1972
1977
1979
1981
1983
1985
1987
1989
1990
1994
1997
1999
2001
2003
2004
2008
2009
2010
2013
2015
2017
2022
2025
2027
2029
2029
2030
2030
2031
2033
2035
2037
2039
2042
2044
2046
2048
2051
2054
2058
2060
2066
2071
Total
Volume
kgal
NR
82.4
88.5
92.3
98.4
106.9
113.8
139.1
157.4
163.7
176.3
190.1
220.7
234.1
276.6
289.6
302.5
343.5
356.5
366.8
379.1
391.7
404.7
415.4
426.1
446.0
460.6
473.6
484.3
495.0
503.7
527.1
535.8
542.3
564.2
576.9
592.1
619.5
635.5
648.1
658.7
658.7
662.5
662.5
668.6
677.3
687.6
697.8
706.0
725.5
736.4
749.3
766.0
788.0
807.3
835.3
848.2
880.0
909.3
Daily
Volume
kgal
ft/ALUE!
ft/ALUE!
6.1
3.8
6.1
8.5
6.9
8.1
18.3
6.3
12.6
ft/ALUE!
ft/ALUE!
10.8
3.0
2.9
1.1
3.0
0.3
2.3
2.6
3.0
'0.7
0.7
11.1
6.1
13.0
10.7
10.7
8.7
13.0
8.7
6.5
13.0
12.7
15.2
15.2
16.0
12.6
ft/ALUE!
ft/ALUE!
0.0
3.8
0.0
6.1
8.7
10.3
10.2
8.2
10.3
10.9
12.9
16.7
22.0
9.3
2.9
2.9
6.6
14.5
Since Last BW
Run
Time
hrs
19.2
4.5
2.1
6.3
4.5
4.4
4.8
3.7
1.1
0.3
1.1
0.7
2.3
1.2
1.8
2.1
0.8
2.5
1.8
1.7
1.0
1.0
1.0
0.5
5.1
1.3
1.0
1.8
1.6
2.2
0.0
3.8
0.1
0.4
0.0
0.2
0.0
0.6
2.6
21.5
11.8
12.3
0.9
3.5
1.5
0.0
6.9
0.8
1.3
0.5
0.5
0.7
0.1
0.8
0.0
1.0
0.5
Run
Time
hrs
18.2
1.6
3.7
4.4
7.7
1.1
4.4
1.2
2.8
0.0
0.6
3.0
3.5
2.0
1.4
1.0
5.6
3.1
1.6
1.4
2.1
3.3
2.0
0.0
4.4
5.8
4.1
4.2
2.0
7.0
1.8
1.8
5.3
5.0
0.0
5.7
3.5
1.9
4.1
4.0
6.0
7.6
14.1
5.6
4.7
3.4
0.9
3.1
4.1
3.3
2.7
4.4
2.4
0.4
4.0
0.0
1.9
1.5
Standby
Time
hrs
20.6
5.5
1.7
7.7
6.8
7.4
6.7
6.2
1.0
0.0
3.1
NR
0.3
5.4
3.6
4.5
2.4
0.8
4.5
0.1
4.8
4.2
4.2
1.0
2.1
0.9
0.0
5.1
1.0
0.8
2.3
2.3
0.6
0.0
5.8
0.0
4.0
0.0
0.0
0.0
0.7
NR
5.1
23.3
7.6
8.9
0.8
5.7
1.2
0.0
1.0
0.0
1.8
0.0
0.7
0.7
00
0.0
0.0
0.0
1.1
Standby
Time
hrs
20.5
3.4
5.1
7.1
8.5
1.2
6.7
2.5
5.0
0.0
3.1
NR
5.6
1.5
3.4
6.2
5.2
4.5
2.4
0.8
6.3
5.2
3.5
4.2
4.2
4.5
2.1
0.0
6.3
5.1
5.2
5.6
2.5
5.9
0.6
2.3
5.8
5.2
4.7
5.3
2.7
2.4
5.8
NR
5.1
6.0
7.6
8.9
6.1
5.7
4.6
0.0
4.8
6.0
5.3
5.1
6.0
3.4
00
5.4
0.0
1.0
3.1
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
142
144
145
146
147
148
149
151
152
Day of
Week
Mon
Tue
Thj
Sat
Mon
Wed
Fti
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Fti
Sat
Sun
Mon
Tue
Wed
Tnu
Sat
Sun
Mon
Wed
Thu
Fti
Sat
Sun
Tue
Wed
Fti
Sat
Sun
Tue
Thu
Fti
Sun
Mon
Tue
Wed
Thu
Fti
Sun
Date
04/20/09
04/21/09
04/23/09
04/25/09
04/27/09
04/29/09
05/01/09
05/02/09
05/03/09
05/05/09
05/06/09
05/07/09
05/08/09
05/09/09
05/10/09
05/11/09
05/12/09
05/14/09
05/16/09
05/17/09
05/18/09
05/19/09
05/20/09
05/21/09
05/22/09
05/23/09
05/24/09
05/25/09
05/26/09
05/28/09
05/29/09
05/30/09
05/31/09
06/01/09
06/02/09
06/03/09
06/04/09
06/06/09
06/07/09
06/08/09
06/10/09
06/11/09
06/12/09
06/13/09
06/14/09
06/16/09
06/17/09
06/19/09
06/20/09
06/21/09
06/23/09
06/25/09
06/26/09
06/28/09
06/29/09
06/30/09
07/01/09
07/02/09
07/03/09
07/05/09
Time
7:00 AM
6:55 AM
8:30 AM
7:00 AM
7:00 AM
7:10AM
7:00 AM
9:00 AM
9:30 AM
7:00 AM
6:50 AM
7:00 AM
7:00 AM
8:00 AM
8:00 AM
7:00 AM
7:00 AM
6:55 AM
8:00 AM
8:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:15AM
10:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
9:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:30 AM
8:00 AM
7:00 AM
7:30 AM
7:30 AM
7:30 AM
7:00 AM
7:00 AM
7:00 AM
7:15AM
NR
NR
NR
10:00 AM
Tank A Hour
Meter
hrs
7,591.9
7,603.9
,630.2
,654.1
,681.6
,706.9
,731.7
,746.2
,760.7
,784.5
,880.0
,818.1
,835.0
,852.7
,869.3
,884.1
,897.7
,924.7
,950.4
,965.5
,978.2
,990.7
8,004.6
8,045.2
8,059.7
8,075.8
8,087.9
8,114.2
8,129.3
8,160.3
8,177.3
8,193.3
8,207.3
8,201.1
8,247.9
8,266.5
8,279.0
8,310.4
8,325.4
8,339.0
8,403.5
8,418.0
8,454.1
8,473.1
8,492.1
8,527.1
8,564.5
8,582.8
8,619.8
8,363.2
NR
8,656.3
8,679.1
8,740.5
Tank B Hour
Meter
hrs
13,330.8
13,343.1
3,370.0
3,394.8
3,422.8
3,448.4
3,473.3
3,488.0
3,502.1
3,525.8
3,540.9
3,559.1
3,576.0
3,593.5
3,609.9
3,625.0
3,638.4
3,665.2
3,690.9
3,704.9
3,718.3
3,730.9
3,744.8
3,786.3
3,800.7
3,816.6
3,828.5
13,854.2
13,869.0
13,900.5
13,917.5
3,933.3
3,947.1
3,960.7
3,987.1
4,005.4
4,018.0
4,049.8
4,064.9
14,077.8
14,141.8
14,157
14,193
14,212.
14,231
14,266
14,304.
14,322
14,359
14,375
NR
14,398
14,422.;
14,486
TARun
Time
hrs
14.1
12.0
12.9
11.8
14.7
12.4
12.3
14.5
14.5
11.4
NA
NA
16.9
17.7
16.6
14.8
13.6
12.9
13.0
15.1
12.7
12.5
13.9
13.0
14.5
16.1
12.1
14.3
15.1
NA
NA
17.0
16.0
14.0
NA
14.9
18.6
12.5
16.2
15.0
13.6
NA
NA
17.2
14.5
18.2
19.0
19.0
16.3
18.7
18.3
18.8
NA
NA
NA
22.8
NA
20.3
TBRun
Time
hrs
15.0
12.3
3.2
2.2
4.8
2.5
2.3
4.7
4.1
1.4
5.1
8.2
6.9
7.5
6.4
5.1
3.4
3.2
3.0
4.0
13.4
12.6
13.9
13.8
13.3
14.4
15.9
11.9
14.2
14.8
NA
NA
17.0
15.8
13.8
13.6
14.7
18.3
12.6
16.3
15.1
12.9
NA
NA
17.4
15.7
18.3
18.8
19.1
15.9
NA
18.3
18.8
16.2
NA
NA
23.9
NA
21.6
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
31.5
2.0
NR
NR
2.0
NR
9.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
8.0
28.0
30.0
36.0
28.0
0.0
0.0
3.0
6.0
8.0
12.0
16.0
19.0
27.0
32.0
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
Pressure Filtration
Influent
psig
33
34
32
34
33
32
32
33
34
33
33
33
32
32
33
32
32
6
33
34
33
45
33
33
7
34
42
34
32
30
33
NR
NR
33
32
32
32
42
32
43
34
32
20
NR
NR
33
32
33
34
33
34
34
32
35
10
NR
37
39
NR
34
Outlet
Tank A
psig
31
29
30
28
30
31
33
31
29
34
28
30
33
32
31
29
33
12
6
30
28
46
32
32
11
32
49
31
33
30
31
30
32
32
33
40
30
3
29
32
24
NR
31
32
32
26
30
26
30
31
28
7
31
37
25
Outlet
TankB
psig
30
32
29
27
27
30
30
28
30
30
32
29
31
31
31
32
30
11
13
31
32
44
31
31
9
29
38
31
30
27
33
31
31
31
30
43
30
36
30
31
22
30
29
32
33
32
32
32
31
29
5
21
15
28
Effluent
P 9
7
7
7
5
5
7
i
7
5
7
6
5
;
>
>
>
8
0
I
j
i
7
7
0
i
?
5
1
7
i
?
?
5
5
19
5
5
5
4
5
i
3
?
?
5
5
;
5
;
5
5
5
5
1
?
5
5
R
6
Inlet-TA
psig
2
5
2
6
3
1
-1
2
5
-1
5
3
-1
0
2
3
-1
-6
27
4
5
-1
1
1
-4
2
-7
3
-1
0
2
ft/ALUE!
ft/ALUE!
3
0
0
-1
2
2
40
5
0
-4
ft/ALUE!
ft/ALUE!
2
0
1
8
3
8
4
1
7
3
ft/ALUE!
6
2
ft/ALUE!
9
Inlet-TB
psig
ft/A JE!
ft/A .UE!
ft/A JE!
ft/A .UE!
ft/A JE!
ft/A UE!
Inlet-
Effluent
p ig
3
7
5
9
8
5
6
6
9
6
7
8
6
3
17
16
14
-4
22
16
17
45
16
16
-3
18
ft/ALUE!
19
14
13
17
ft/ALUE!
ft/ALUE!
18
17
-137
17
27
17
29
19
16
-3
ft/ALUE!
ft/ALUE!
18
17
17
19
17
19
19
17
20
-1
ft/ALUE!
22
24
ft/ALUE!
18
Flow
rate
gpm
339
340
361
342
345
351
352
348
342
343
344
342
367
356
351
340
342
0
330
347
330
71
353
351
0
349
186
336
334
340
368
NR
NR
340
363
343
352
350
343
198
198
350
NR
NR
NR
347
349
331
315
331
30
32
30
320
0
NR
288
227
320
Totalizer to
Distribution
kgal
2,361.5
2,601.7
3,113.3
323.3
892.4
1,399.2
1,887.8
2,177.4
2,444.1
2,914.5
3,207.7
264.8
932.5
1,255.9
1,541.5
1,816.7
2,333.8
2,827.5
3,102.5
85.9
332.6
611.1
1,153.5
1,409.2
1,691.3
2,004.0
2,234.6
2,736.5
3,027.3
NR
352.7
688.7
1,005.5
1,283.3
1,557.1
2,096.7
2,452.9
2,709.0
56.9
357.2
430.3
NR
NR
1,323.1
1,461.7
2,136.7
2,486.9
2,832.8
80.1
797.0
1,143.2
1,845.3
2,000.7
NR
2,272.4
2,592.8
NR
180.9
Gallon
Usage
gal
276,400
240,200
252,900
242,900
304,700
246,300
244,700
289,600
266,700
233,500
293,200
341,100
323,400
285,600
275,200
249,500
249,600
275,000
-3,016,600
246,700
278,500
277,700
264,700
255,700
282,100
312,700
230,600
272,800
290,800
ft/ALUE!
ft/ALUE!
336,000
316,800
277,800
273,800
295,000
356,200
256,100
-2,960,200
300,300
73,100
ft/ALUE!
ft/ALUE!
330,000
138,600
340,700
350,200
345,900
-3,093,000
357,200
346,200
355,400
155,400
ft/ALUE!
ft/ALUE!
320,400
ft/ALUE!
ft/ALUE!
Daily
Average
Flowrate
gpm
317
330
323
337
344
330
332
331
311
341
ft/ALUE!
323
327
318
340
319
320
315
-3,855
328
334
325
323
324
325
326
320
319
324
ft/ALUE!
ft/ALUE!
329
332
333
ft/ALUE!
332
322
340
-3,036
333
92
ft/ALUE!
ft/ALUE!
318
153
311
309
303
-3,202
ft/ALUE!
315
315
ft/ALUE!
ft/ALUE!
ft/ALUE!
229
ft/ALUE!
ft/ALUE!
Backwash
Tank
A
No.
2153
2157
2165
2172
2180
2186
2191
2193
2195
2199
2200
2208
2210
2212
2215
2220
2225
2228
2231
2235
2238
2242
2245
2249
2252
2256
2259
2265
2268
2278
2280
2283
2285
2287
2291
2294
2296
2302
2305
2307
2314
2322
2325
2326
2328
2330
2334
2336
2340
2342
2372
2376
2384
Tank
B
No.
2074
2077
2083
2088
2094
2 99
2 03
2 05
2 07
2 10
2 12
2119
2121
2 22
2 25
2 30
2 35
2 38
2 41
2 43
2 46
2 49
2 52
2 55
2 59
2 63
2 66
2 73
2 77
2 88
2 90
2 94
2 96
2 98
2203
2207
2209
2215
2218
2223
2232
2235
2239
2241
2243
2246
2250
2252
2256
2259
2283
2283
2287
Total
Volume
kgal
931.2
946.0
974.8
999.6
028.2
051.2
069.6
077.2
085.8
100.5
106.5
137.8
146.4
152.4
164.1
184.4
204.8
217.2
228.8
240.9
253.6
268.3
280.7
295.0
310.9
325.1
337.5
364.2
380.4
1413.1
1422.9
1435.3
443.6
451.9
470.7
485.0
4933.0
518.1
529.8
529.9
563.4
567.6
581.9
587.9
596.2
606.3
622.9
631.0
646.9
650.9
NR
656.7
665.5
1690.6
Daily
Volume
kgal
21.9
14.8
4.3
0.2
4.3
0.6
10.5
7.6
8.6
6.8
6.0
8.7
8.6
6.0
11.7
10.9
10.2
12.4
11.6
12.1
12.7
14.7
12.4
14.3
15.9
14.2
12.4
12.4
16.2
ft/ALUE!
ft/ALUE!
9.8
12.4
8.3
8.3
12.4
14.3
13448.0
12.4
11.7
0.1
ft/ALUE!
ft/ALUE!
14.2
4.2
8.3
6.0
8.3
3.7
8.1
8.1
7.8
4.0
ft/ALUE!
ft/ALUE!
8.8
ft/ALUE!
8.5
Since Last BW
Run
Time
hrs
0.5
1.1
1.2
2.7
1.1
2.2
0.3
1.4
5.3
0.3
7.8
6.3
3.6
4.0
0.0
2.4
3.1
3.2
4.7
1.1
0.3
0.0
2.6
1.0
0.0
2.4
0.7
0.6
2.2
0.0
5.6
0.6
0.0
0.4
1.7
3.3
0.0
3.9
1.1
8.2
3.8
2.9
4.4
11.1
6.1
10.3
6.0
5.7
6.7
8.2
4.9
2.2
8.0
Run
Time
hrs
0.9
0.1
1.5
4.9
3.3
3.2
1.8
3.1
3.6
3.9
0.6
1.8
1.7
0.0
1.8
2.6
2.3
1.5
0.8
4.5
0.6
1.0
1.5
3.2
1.1
2.0
1.1
3.0
0.0
0.0
2.0
0.1
0.4
2.1
2.6
1.1
3.1
2.8
0.7
8.3
NR
1.3
2.6
0.3
0.2
0.0
6.0
1.6
2.2
4.9
8.0
16.8
40.8
5.4
Standby
Time
hrs
0.0
1.0
0.9
4.8
0.8
5.9
0.0
1.0
7.4
0.0
4.9
0.6
2.5
3.5
0.0
5.5
5.4
4.4
3.2
0.8
0.0
0.0
4.9
3.3
0.0
1.6
1.0
0.7
2.5
NR
0.0
2.7
0.0
0.2
0.0
1.4
0.0
0.0
4.5
0.0
6.6
NR
NR
3.4
4.9
2.0
3.7
3.1
5.1
2.0
2.8
3.3
5.5
NR
3.1
0.0
NR
3.6
Standby
Time
hrs
0.0
0.0
0.9
5.4
3.6
6.0
3.0
5.3
6.7
6.1
0.0
0.0
0.5
0.0
0.0
2.3
5.5
5.4
2.7
0.0
5.4
0.0
0.0
3.1
5.8
2.9
1.5
1.0
3.9
0.0
0.1
2.6
0.0
0.4
2.8
2.8
0.0
5.1
3.2
0.0
6.6
NR
NR
0.6
5.0
0.0
0.0
0.0
5.0
0.9
2.8
3.2
5.5
NR
5.5
5.5
3.7
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
156
157
158
160
161
162
163
Day of
Week
Mon
Tue
Wed
Fri
Sat
Sun
Tue
Wed
Fri
Sat
Sun
Tue
Wed
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Mon
Tue
Wed
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Tnu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
07/06/09
07/07/09
07/08/09
07/10/09
07/11/09
07/12/09
07/14/09
07/15/09
07/17/09
07/18/09
07/19/09
07/21/09
07/22/09
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
08/13/09
08/14/09
08/15/09
08/17/09
08/18/09
08/19/09
08/21/09
08/22/09
08/24/09
08/25/09
08/26/09
08/27/09
08/28/09
08/29/09
08/30/09
08/31/09
09/01/09
09/03/09
09/04/09
09/05/09
09/06/09
09/07/09
09/08/09
09/1 1/09
09/12/09
09/13/09
09/14/09
09/15/09
09/16/09
09/17/09
09/18/09
09/19/09
09/20/09
Time
8:00 AM
7:00 AM
7:00 AM
7:00 AM
9:30 AM
1 1 :00 AM
7:00 AM
7:00 AM
7:00 AM
7:30 AM
7:30 AM
7:00 AM
7:00 AM
NR
7:00 AM
7:00 AM
6:50 AM
6:55 AM
7:00 AM
7:00 AM
8:00 AM
9:00 AM
7:10 AM
7:05 AM
7:10AM
7:05 AM
7:05 AM
NR
9:00 AM
7:25 AM
7:00 AM
6:48 AM
7:00 AM
7:30 AM
7:15 AM
7:15AM
6:55 AM
7:00 AM
7:30 AM
7:00 AM
7:00 AM
7:10AM
7:15AM
7:15AM
NR
7:15 AM
7:00 AM
7:00 AM
7:10 AM
7:30 AM
7:20 AM
7:30 AM
6:55 AM
7:10AM
8:00 AM
8:00 AM
7:05 AM
7:15AM
7:15AM
7:10AM
7:30 AM
NR
NR
Tank A Hour
Meter
hrs
8,757.5
8,775.2
8,792.4
8,825. I
8,845
8,867
8,900
8,917.
8,953 I
8,970 I
8,987
9,022
9,039
9,091.5
9,108.7
9,121.0
9,146.0
9,159.9
9,173.7
9,191.9
9,207.4
9,220.2
9,234.8
9,253.2
9,269.8
9,291.0
NR
9,328.8
9,344.3
9,360.6
9,393.7
9,413.6
9,431.5
9,465.2
9,479.9
9,497.7
9,522.5
9,533.7
9,564.4
9,580.9
9,602.5
9,620.5
9,640.4
NR
9,694.4
9,714.4
9,752.6
9,769.4
9,784.5
9,800.1
9,815.0
9,831.6
9,875.9
9,888.8
9,904.2
9,919.6
9,935.9
9,950.6
9,965.3
9,980.0
NR
NR
Tank B Hour
Meter
hrs
14,501.7
14,519.2
14,536.6
14,569.6
14,589.4
14,611.2
14,649.5
14,667.0
14,702.6
14,719.2
14,735.8
14,764.4
14,785.2
14,834.5
14,851.5
14,863.0
14,888.5
14,902.2
14,916.2
14,934.0
14,949.3
14,962.2
14,976.5
14,995.1
15,011.5
15,032.6
NR
15,069.9
15,085.5
15,101.7
15,134.2
15,153.3
15,171.1
15,204.6
15,219.9
15,234.2
15,261.4
15,272.6
15,303.4
15,319.7
15,341.1
15,359.4
15,379.4
NR
15,432.6
15,452.8
5,491.1
5,507.8
5,522.1
5,537.3
5,551.7
5,568.0
5,610.7
5,623.6
5,630.4
5,653.1
5,668.6
5,683.1
5,697.0
5,711.2
NR
NR
TARun
Time
hrs
17.0
17.7
7.2
9.1
0.1
1.5
6.4
7.5
7.9
7.0
6.6
8.2
6.8
6.5
7.2
2.3
1.3
3.7
3.9
3.8
8.2
5.5
12.8
14.6
18.4
16.6
21.2
NA
NA
15.5
16.3
17.9
19.9
17.9
17.2
14.7
17.8
3.8
1.2
2.0
6.5
1.6
8.0
9.9
^
6.6
0.0
8.9
6.8
5.1
5.6
4.9
6.6
4.6
2.9
5.4
5.4
4.7
4.7
4.7
NA
NA
TBRun
Time
hrs
15.7
17.5
7.4
8.7
9.8
1.8
1.6
7.5
7.7
6.6
6.6
1.2
0.8
6.3
7.0
1.5
1.8
3.7
3.7
4.0
7.8
5.3
12.9
14.3
18.6
16.4
21.1
NA
NA
15.6
16.2
17.6
19.1
17.8
17.2
15.3
14.3
13.5
11.2
12.4
16.3
21.4
18.3
20.0
NA
16.1
20.2
19.1
16.7
14.3
15.2
14.4
16.3
13.7
12.9
6.8
22.7
14.5
13.9
14.2
NA
NA
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Pressure Filtration
Influent
psig
34
32
33
34
43
35
35
34
33
43
42
34
42
33
33
33
33
5
33
6
33
33
41
7
34
35
35
33
NR
23
34
33
33
34
32
35
34
34
34
34
36
34
35
36
41
NR
37
35
36
41
37
35
36
36
44
35
37
36
43
36
NR
NR
Outlet
Tank A
psig
26
32
34
32
49
31
31
30
34
44
44
30
40
33
32
33
32
10
34
11
34
32
34
12
30
28
29
33
22
32
33
34
28
33
30
32
34
33
33
36
35
31
30
39
NR
35
36
42
31
31
30
30
44
35
21
35
36
35
Outlet
TankB
psig
28
27
27
29
38
28
28
31
32
42
41
31
39
30
28
27
31
11
30
10
27
32
1
11
32
31
33
31
22
31
32
33
32
31
32
30
30
33
31
29
33
33
29
1
33
31
4
36
34
34
36
41
32
33
30
4
33
Effluent
P 9
5
5
5
;
I
5
5
5
5
5
5
5
5
i
5
5
)
6
0
5
5
3
)
5
5
5
5
R
i
i
5
i
5
5
5
5
5
5
5
5
5
5
5
5
?
5
5
5
5
5
5
5
5
5
5
5
5
5
3
5
NR
NR
Inlet-TA
psig
8
NA
I <\
NA
NA
Inlet-TB
psig
NA
NA
Inlet-
Effluent
psig
19
17
18
18
29
20
20
19
18
28
27
19
42
18
17
18
18
-5
-4
18
18
28
19
20
20
18
NA
18
18
17
19
17
20
19
19
19
19
21
19
20
21
26
22
22
20
21
26
22
20
21
22
26
21
29
20
29
22
21
30
21
NA
NA
Flow
rate
gpm
321
342
340
349
186
328
322
320
322
119
123
311
108
334
315
320
322
0
318
0
323
320
185
0
320
308
328
324
NR
230
305
325
326
320
327
305
308
314
323
300
304
315
315
294
193
280
280
310
309
189
305
307
293
287
194
294
200
295
168
283
303
171
309
NR
NR
Totalizer to
Distribution
kgal
507.5
848.3
1,178.0
1 ,744.2
2,127.4
2,524.9
3,198.0
262.8
914.6
1,219.5
1,519.8
2,133.2
2,421.7
2,727.2
3,380.1
386.9
6,230.0
1,093.6
1,351.7
1,606.0
1,939.6
2,221.4
2,457.0
2,721.6
3,057.7
87.0
436.6
1,094.0
1,381.8
1,666.6
2,263.2
2,605.8
2,924.6
243.5
506.8
774.4
1,269.6
1 ,482.8
2,017.0
2,303.7
2,664.5
2,979.6
47.9
681.9
958.3
1,296.0
1,935.4
2,214.9
2,470.0
2,736.4
2,991.9
3,276.2
509.1
754.5
983.3
1 ,245.4
1,469.9
1,768.4
2,027.0
2,267.3
2,516.8
NR
Gallon
Usage
gal
326,600
340,800
329,700
357,900
383,200
397,500
360,600
-2,935,200
322,400
304,900
300,300
314,000
288,500
305,500
330,400
-2,993,200
5,843,100
256,600
258,100
254,300
333,600
281,800
235,600
264,630
336,070
87,000
349,600
NA
NA
284,800
319,500
342,600
318,800
243,500
263,300
267,600
246,500
213,200
218,800
286,700
360,800
315,100
47,900
276,400
337,700
324,100
279,500
255,100
266,400
255,500
284,300
249,600
245,400
228,800
262,100
224,500
298,500
258,600
240,300
249,500
NA
Daily
Average
Flowrate
gpm
333
323
318
316
320
306
322
-2,795
302
303
302
377
259
301
336
-2,917
8,193
312
312
305
309
305
306
305
303
88
275
ft/A LIE!
WALUE!
292
300
293
298
236
293
281
301
317
299
291
280
289
40
WALUE!
WALUE!
282
280
284
278
289
288
291
288
289
289
296
463
204
313
295
280
288
WALUE!
WALUE!
Backwash
Tank
A
No.
2386
2389
2391
2395
2397
2400
2405
2407
2411
2412
2414
2417
2418
2420
2424
2425
2426
2429
2430
2432
2434
2435
2437
2438
2440
2442
2445
2450
2454
2459
2461
2465
2468
2470
2472
2475
2476
2480
2484
2486
2489
2493
2495
2498
2503
2505
2508
2510
2512
2516
2517
2519
2521
2522
2524
2526
2527
2529
Tank
B
No.
2289
2292
2294
2298
2302
2304
2309
2312
2317
2319
2321
2328
2332
2335
2538
2340
2342
2345
2347
2348
2351
2352
2354
2356
2361
2364
2371
2376
2283
2387
2391
2395
2397
2399
2404
2405
2409
2415
2417
2420
2426
2429
2432
2438
2441
2448
2451
2454
2460
2464
2466
2470
2473
2477
2480
2483
2488
Total
Volume
kgal
1698.3
1709.4
1717.9
1733.6
1745.7
1754.8
1768.3
1777.7
795.4
801.7
809.8
823.6
826.0
835.2
859.1
855.5
874.3
880.7
887.1
896.6
900.7
909.0
914.7
932.8
945.3
968.8
981.3
2012.3
2024.8
2041.3
2055.1
2064.2
2072.5
2089.2
2093.4
2110.0
2139.2
2150.6
2172.2
2182.1
2195.0
2217.8
2227.2
2258.3
2268.9
2289.4
2299.3
2307.9
2319.4
2328.1
2342.2
2350.8
2359.1
2373.5
NR
NR
Daily
Volume
kgal
7.7
11.1
8.5
.0
2.1
i .1
7
i .4
9.9
6.3
8.1
5.5
2.4
9.2
-3.6
8.3
6.4
9.5
4.1
8.3
5.7
10.2
12.5
NA
NA
4.2
14.4
12.5
16.5
8.0
9.1
8.3
10.6
4.2
6.0
8.7
11.4
9.9
12.9
12.6
9.4
10.6
10.6
10.2
9.9
8.6
11.5
8.7
14.1
8.6
8.3
14.4
NA
NA
Since Last BW
Run
Time
hrs
8.4
0.4
0.4
1.7
0.0
3.6
5.5
6.4
2.2
8.9
4.4
8.6
12.9
3.0
2.0
0.6
2.2
7.5
2.9
9.3
8.3
2.6
6.4
2.4
1.1
6.7
0.8
7.4
4.6
2.0
3.0
5.3
0.9
7.7
3.4
7.2
7.3
2.3
0.7
0.4
5.6
6.6
1.2
9.9
4.5
2.5
0.0
6.9
6.7
9.4
4.1
Run
Time
hrs
5.4
4.2
5.2
3.8
0.6
6.1
7.2
1.3
0.9
3.1
5.3
0.3
2.3
1.9
7.7
7.2
1.2
0.0
4.3
2.2
2.1
0.8
0.1
0.7
1.3
3.1
3.8
3.5
0.1
4.8
0.0
3.3
1.4
3.9
4.0
1.9
4.0
0.0
1.0
4.2
0.6
4.5
3.9
1.9
0.0
1.8
5.9
4.5
1.3
Standby
Time
hrs
2.7
0.0
0.0
0.0
0.0
0.0
0.5
3.5
1.6
5.9
5.6
4.0
5.7
1.8
0.6
0.0
0.0
5.7
4.0
5.3
0.0
NR
3.6
0.0
2.9
0.6
3.4
5.0
6.0
4.6
7.0
0.0
7.1
0.0
NR
6.2
1.5
0.7
0.0
0.0
6.4
3.1
0.0
0.3
5.7
2.3
2.7
5.0
4.9
0.0
3.3
NR
NR
Standby
Time
hrs
2.7
4.0
3.5
1.9
0.0
0.8
0.5
0.5
0.6
2.9
5.5
0.0
1.9
0.4
4.6
4.2
4.7
2.8
5.8
0.0
0.0
4.0
2.1
0.0
0.5
0.0
0.0
0.6
2.5
5.0
4.6
0.0
7.1
0.0
0.0
3.2
0.0
NR
4.1
0.0
0.5
0.8
0.0
1.1
1.2
4.1
0.0
0.0
5.8
2.3
4.0
2.2
5.0
0.0
0.6
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
166
167
169
170
171
172
173
174
Day of
Week
Mon
Wed
Fri
Sat
Mon
Tue
Wed
Fri
Sat
Mon
Tue
Thu
Fri
Sun
Mon
Wed
Tnu
Fri
Sat
Sun
Mon
Wed
Fri
Sun
Mon
Tue
Wed
Tnu
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Date
09/21/09
09/23/09
9/25/09
9/2 6 /O 9
9/28/09
9/29/09
9/30 /O 9
0/02/09
0/03/09
0/05/09
0/06/09
0/08/09
0/09/09
0/11/09
0/12/09
0/14/09
0/15/09
0/16/09
0/17/09
0/18/09
0/19/09
0/21/09
0/23/09
0/25/09
0/26/09
0/27/09
0/28/09
0/29/09
0/31/09
1/01/09
1/02/09
1/03/09
1/04/09
1/05/09
1/06/09
1/08/09
1/09/09
1/10/09
1/11/09
1/12/09
1/14/09
1/15/09
1/16/09
1/17/09
1/18/09
1/19/09
1/20/09
1/21/09
1/23/09
1/25/09
1/26/09
1/27/09
1/28/09
1/29/09
1/30/09
2/01/09
2/02/09
2/03/09
2/04/09
2/05/09
2/06/09
Time
7:15AM
7:15AM
7:00 AM
6:30 AM
7:05 AM
7:00 AM
7:00 AM
8:00 AM
8:00 AM
7:15AM
7:10AM
6:15AM
7:00 AM
10:30 AM
6:50 AM
7:15AM
7:15AM
7:20 AM
8:45 AM
9:00 AM
7:00 AM
7:15AM
7:20 AM
7:00 AM
8:00 AM
NR
NR
NR
7:00 AM
8:00 AM
7:00 AM
8:00 AM
7:00 AM
7:20 AM
7:30 AM
7:00 AM
7:00 AM
7:00 AM
9:30 AM
7:00 AM
7:30 AM
7:30 AM
7:00 AM
7:15AM
7:15 AM
7:15 AM
7:30 AM
7:30 AM
7:00 AM
7:30 AM
9:00 AM
9:00 AM
1 1 :30 AM
9:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
8:00 AM
Tank A Hour
Meter
hrs
0,021.8
NR
0,081.0
0,100.6
0,141.4
0,158.1
0,175.3
0,206.4
0,220.9
NR
0,263.3
0,288.7
0,305.4
0,338.5
0,350.9
0,382.6
0,402.2
0,422.3
0,440.7
0,458.0
0,469.6
0,498.4
0,529.5
0,565.5
0,581.0
NR
NR
NR
0,635.8
0,648.9
0,660.0
0,673.7
0,684.2
0,696.0
0,707.3
0,727.7
0,739.7
0,750.1
0,760.3
0,769.0
0,788.4
0,800.3
0,811.5
0,828.7
0,846.8
0,858.1
0,868.6
0,879.0
0,900.4
0,922.3
0,933.1
0,944.0
0,955.8
0,964.0
0,984.6
0,995.8
1,007.6
1,011.1
1,033.7
1,050.9
Tank B Hour
Meter
hrs
15,751.6
NR
5,808.8
5,826.2
5,865.9
5,882.6
5,899.4
5,930.7
5,945.1
NR
5,987.7
6,013.2
6,028.8
6,061.0
6,073.0
6,103.6
6,122.8
6,143.1
6,161.0
6,178.4
6,190.9
6,220.0
6,250.9
6,287.9
6,303.2
NR
NR
NR
6,355.1
6,368.2
6,380.1
6,343.5
6,404.1
6,415.8
6,427.2
6,447.9
6,459.5
6,470.0
6,479.8
6,488.2
6,507.0
6,519.1
6,529.6
6,546.9
6,564.9
6,576.0
6,587.0
6,599.8
6,618.8
6,640.0
6,644.7
6,661.6
6,673.4
6,681.4
6,701.9
6,717.5
6,724.7
6,735.6
6,749.5
6,766.5
TARun
Time
hrs
NA
NA
15.4
9.6
0.5
6.7
7.2
5.1
4.5
•iA
NA
3.0
6.7
7.8
2.4
6.4
9.6
0.1
8.4
7.3
1.6
4.3
6.3
8.0
5.5
^
^
^
2.6
3.1
1.1
13.7
0.5
1.8
1.3
0.0
2.0
0.4
0.2
8.7
.9
.9
.2
7.2
.1
.3
5
•4
.5
j
.8
.9
.8
2
.2
.2
.8
5
.6
.2
TBRun
Time
hrs
NA
NA
14.7
17.4
0.4
6.7
6.8
5.3
4.4
•iA
NA
3.3
5.6
7.7
2.0
5.7
9.2
0.3
7.9
7.4
12.5
14.8
16.5
18.5
15.3
NA
NA
NA
10.0
13.1
11.9
-36.6
60.6
11.7
11.4
10.2
11.6
10.5
9.8
8.4
9.0
2.1
0.5
7.3
8.0
1.1
1.0
2.8
10.5
^
. .7
i.9
.8
0
i .0
.5
5.6
2
3.9
.0
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
HR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Pressure Filtration
Influent
psig
6
37
39
38
38
38
38
38
38
39
39
44
38
38
39
38
39
39
38
38
39
21
44
44
39
38
NR
NR
NR
33
33
35
8
8
8
8
8
28
29
29
7
25
27
26
19
18
8
8
35
7
26
27
27
26
27
27
26
26
26
25
21
15
Outlet
Tank A
psig
12
36
34
38
39
39
38
38
38
34
36
40
39
40
38
36
38
38
38
35
23
5
3
40
38
NR
NR
NR
31
28
27
11
11
11
11
11
21
22
21
10
22
23
23
17
15
10
10
44
9
22
21
22
22
22
21
25
22
24
24
17
15
Outlet
TankB
psig
9
36
33
35
33
37
38
38
38
34
35
37
36
37
36
39
38
36
36
38
22
41
40
36
38
NR
NR
NR
25
25
27
11
11
10
10
10
22
21
22
6
23
21
23
14
17
9
7
27
6
22
22
23
22
21
22
22
23
24
22
20
14
Effluent
p ig
0
6
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
5
3
2
3
5
5
R
R
R
6
5
5
0
D
0
0
0
5
5
5
0
5
5
5
5
5
1
0
5
0
5
5
5
5
5
5
8
3
7
7
4
4
Inlet-TA
psig
-6
1
5
0
-1
-1
0
0
0
5
3
-2
-1
-1
0
3
1
0
0
4
-2
39
41
-1
0
ft/ALUE!
ft/ALUE!
ft/ALUE!
2
5
8
-3
-3
0
-3
-3
7
7
8
-3
3
4
3
2
3
-2
-2
-9
-2
4
6
5
4
5
6
1
4
2
1
4
0
Inlet-TB
psig
-3
ft/A JE!
ft/A JE!
ft/A .UE!
Inlet-
Effluent
psig
-4
21
24
23
23
23
23
23
23
24
24
29
23
23
24
23
24
24
23
23
24
-2
32
31
24
23
ft/ALUE!
ft/ALUE!
ft/ALUE!
17
18
2
— : —
13
1
1
\
12
11
4
3
-3
-2
20
-3
11
12
12
11
12
12
8
10
9
8
1
Flow
rate
gpm
0
324
293
304
299
300
284
295
295
280
283
117
287
291
289
281
288
292
282
285
0
128
123
298
302
NR
NR
NR
366
348
326
0
0
0
0
0
409
393
410
0
445
430
450
257
265
0
0
318
0
423
. 25
. 30
. 26
11
. 27
440
409
449
266
Totalizer to
Distribution
kgal
3,029.7
266.1
786.2
1,110.1
1,788.0
2,060.0
2,337.0
2,846.4
3,090.9
283.5
505.3
719.6
940.6
1,199.5
1,733.5
1,931.2
2,443.7
2,752.4
3,070.0
3,382.1
396.6
877.7
1,377.3
1,966.9
2,208.1
NR
NR
NR
3,084.9
75.0
325.4
606.5
1,107.8
1,379.0
1,894.2
2,184.2
2,446.4
2,716.2
2,932.2
159.9
464.5
738.7
1,007.2
1,283.3
1,563.5
1,835.9
2,097.4
2,631.2
3,169.5
NR
441.6
736.2
952.1
1,185.2
1,740.7
2,018.2
2,308.9
2,975.8
Gallon
Usage
gal
NA
258,900
262,400
323,900
341,200
272,000
277,000
248,700
244,500
235,900
221,800
214,300
221,000
258,900
293,000
197,700
260,900
308,700
317,600
312,100
29,200
243,900
261,200
292,100
241,200
ft/ALUE!
ft/ALUE!
ft/ALUE!
195,900
75,000
250,400
281,100
274,500
271,200
251,700
290,000
262,200
269,800
216,000
159,900
304,600
274,200
268,500
276,100
280,200
272,400
261,500
272,000
262,900
ft/ALUE!
441,600
294,600
215,900
233,100
264,600
277,500
290,700
337,900
Daily
Average
Flowrate
gpm
ft/ALUE!
ft/ALUE!
291
293
278
271
272
273
282
ft/ALUE!
ft/ALUE!
290
280
267
275
270
271
265
262
287
40
279
265
267
261
ft/ALUE!
ft/ALUE!
ft/ALUE!
293
95
363
107
389
398
415
410
418
450
421
244
423
422
259
255
417
423
380
432
417
ft/ALUE!
555
416
444
422
338
517
914
329
Backwash
Tank
A
No.
2532
2535
2538
2541
2546
2548
2550
2554
2556
2559
2561
2563
2568
2573
2574
2579
2582
2585
2588
2590
2594
2598
2602
2608
2610
NR
NR
NR
2622
2623
2624
2626
2629
2630
2632
2633
2634
2636
2637
2640
2642
2644
2645
2646
2648
2650
2651
2654
2657
2659
2660
2662
2663
2664
2667
2669
2672
2682
Tank
B
No.
2495
2501
2508
2517
2526
2528
2531
2535
2537
2540
2542
2545
2553
2561
2563
2572
2576
2579
2581
2584
2586
2590
2593
2597
2599
NR
NR
NR
2622
2623
2624
2626
2628
2629
2632
2634
2635
2637
2639
2643
2645
2648
2649
2651
2653
2655
2657
2661
2665
2667
2669
2671
2672
2674
2679
2681
2685
2697
Total
Volume
kgal
2393.2
2411.8
2431.5
2456.1
2484.9
2494.8
2502.8
2519.5
2527.8
2540.7
2549.1
2560.1
2586.6
2613.5
2619.5
2648.3
2662.7
2675.3
2686.1
2696.1
2696.1
2712.4
2727.2
2748.7
2757.1
NR
NR
NR
2 74.2
2 78.4
2 82.6
2 91.3
2801.9
2806.1
2816.3
2822.8
2826.9
2835.3
2841.4
2856.2
2864.2
2874 .4
2878.6
2884.7
2893.0
2901.4
2909.5
2922.3
2937.1
2944.2
2951.5
2959.9
2964.1
2970.2
2986.2
2994.6
3009.0
Daily
Volume
kgal
NA
10.6
13.6
24.6
144
9.9
8.0
8.4
8.3
4.1
8.4
11.0
12.1
14.8
6.0
18.9
14.4
12.6
10.8
0.0
8.0
6.1
10.9
8.4
ft/ALUE!
ft/ALUE!
ft/ALUE!
3.8
4.2
4.2
8.7
4.2
4.5
6.5
4.1
8.4
6.1
6.1
8.0
10.2
4.2
6.1
8.3
8.4
8.1
6.1
6.4
7.1
7.3
8.4
4.2
6.1
3.9
8.4
14.4
Since Last BW
Run
Time
hrs
2.1
6.7
6.4
1.9
1.6
1.1
2.2
1.7
2.0
11.1
5.6
0.0
1.3
1.2
6.9
4.4
3.6
2.0
6.7
9.7
0.0
0.0
0.1
1.0
NR
NR
NR
2.9
5.5
7.1
4.6
1.9
4.9
7.9
7.9
1.1
1.9
3.6
3.1
2.3
4.4
8.0
5.5
3.4
0.0
6.2
4.7
3.6
5.4
3.7
5.3
7.0
11.6
4.4
0.3
Run
Time
hrs
7.8
0.8
1.9
0.9
3.4
1.5
1.1
0.7
1.6
10.7
5.3
2.1
1.4
1.7
2.3
5.7
0.1
0.7
2.8
9.8
4.5
7.9
0.0
0.4
NR
NR
NR
7.6
10.6
8.9
3.4
5.8
9.0
6.6
3.2
6.2
4.9
2.5
1.1
3.9
0.5
8.4
1.0
3.4
2.6
2.4
2.7
2.0
2.0
2.0
1.8
3.9
2.8
1.1
2.5
0.0
Standby
Time
hrs
4.6
5.2
4.2
1.1
0.0
0.0
0.8
0.0
1.9
6.0
4.2
0.0
0.0
0.0
0.0
0.7
4.4
0.0
1.5
6.8
0.0
0.0
5.9
0.0
NR
NR
NR
4.2
6.4
7.6
5.9
2.1
7.9
3.1
8.3
1.7
5.8
6.9
6.1
3.8
3.0
3.1
3.7
5.8
0.0
8.9
6.1
2.8
8.2
3.0
9.2
9.1
0.0
11.5
6.5
1.2
1.0
Standby
Time
hrs
6.9
0.0
2.5
0.0
1.2
0.0
0.0
0.0
1.9
6.1
4.2
2.9
1.3
0.0
0.0
4.7
0.0
0.0
2.7
4.3
6.9
5.0
6.0
4.8
0.0
NR
NR
NR
4.2
1C. 5
8.;
4
7_
9.;
6
6 ;
8.
6..
Os
-------
Table A-l. US EPA Arsenic Demonstration Project at Arnaudville, LA - Daily System Operation Log Sheet (Continued)
Week
No.
175
176
177
178
179
180
181
183
184
185
Day of
Week
Mon
Tue
Wed
Thj
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Fri
Sat
Mon
Tue
Wed
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Mon
Tue
Wed
Tnu
Fri
Sat
Mon
Tue
Thu
Fri
Sat
Mon
Tue
Wed
Fri
Sat
Sun
Mon
Tue
Thu
Fri
Sat
Sun
Mon
Tue
Wed
Thu
Sat
Sun
Tue
Wed
Thu
Fri
Sat
Sun
Date
2/07/03
2/08/09
2/09/09
2/10/09
2/11/09
2/12/09
2/13/09
2/14/09
2/15/09
2/16/09
2/17/09
2/18/09
2/19/09
2/20/09
2/21/09
2/22/09
2/23/09
2/24/09
2/25/09
2/26/09
2/28/09
2/29/09
2/30/09
2/31/09
1/01/10
1/02/10
1/03/10
1/04/10
1/05/10
1/06/10
01/07/10
01/09/10
01/10/10
01/11/10
01/12/10
01/13/10
01/14/10
01/15/10
01/16/10
01/18/10
01/19/10
01/21/10
01/22/10
01/23/10
01/25/10
01/26/10
01/27/10
01/29/10
01/30/10
01/31/10
02/01/10
02/02/10
02/04/10
02/05/10
02/06/10
02/07/10
02/08/10
02/09/10
02/10/10
02/1 1/1 0
02/13/10
02/14/10
02/15/10
02/16/10
02/17/10
02/18/10
02/19/10
02/20/10
02/21/10
Time
7:00 AM
6:50 AM
7:00 AM
7:00 AM
7:00 AM
10:00 AM
8:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
10:00 AM
7:00 AM
7:00 AM
7:00 AM
6:15 AM
7:30 AM
6:15AM
7:15AM
8:00 AM
7:00 AM
7:00 AM
NR
NR
NR
9:00 AM
7:00 AM
7:00 AM
7:00 AM
8:00 AM
7:00 AM
7:00 AM
7:00 AM
7:00 AM
6:30 AM
7:00 AM
8:00 AM
NR
NR
NR
NR
8:00 AM
7:00 AM
7:00 AM
7:00 AM
6:55 AM
7:33 AM
8:00 AM
7:00 AM
7:00 AM
7:30 AM
7:00 AM
8:30 AM
8:30 AM
7:00 AM
7:00 AM
7:00 AM
6:55 AM
8:00 AM
8:40 AM
7:30 AM
6:35 AM
9:00 AM
8:30 AM
Tank A Hour
Meter
hrs
,068.8
,081.8
,093.0
,106.2
,118.9
,131.1
,142.3
,158.7
1707
,183.3
,196.0
,207.6
,219.1
,233.9
,242.7
,254.1
,266.5
,279.1
,291.9
,335.0
,352.2
,367.3
,378.4
,389.2
,400.3
,418.0
,436.3
,451.3
,466.0
,478.6
,520.4
,526.1
,540.4
,559.9
,575.7
,590.0
,604.9
,619.9
,643.5
,655.6
,689.5
,694.8
,705.7
,733.2
,745.8
,758.8
,785.3
,799.0
,819.0
,834.9
,848.5
,877.1
,889.7
,903.6
,917.4
,933.7
,946.9
,960.9
,973.2
,999.7
,046.8
,055.3
,082.6
,099.5
,110.3
Tank B Hour
Meter
hrs
16,784.8
6,797.3
6,808.4
6,820.9
6,833.0
6,844.9
6,855.5
6,871.8
6,883.6
6,895.5
6,908.2
6,919.4
6,930.5
6,944.2
6,953.8
6,965.2
6,976.8
6,988.7
7,001.5
7,044.5
7,061.7
7,076.4
7,087.4
7,098.6
7,109.9
7,127.0
7,144.9
7,159.4
7,174.3
7,186.4
7,228.3
7,236.5
250.5
279.7
285.9
300.2
314.2
329.4
352.5
364.3
388.8
402.7
413.6
438.4
449.9
461.7
484.7
497.3
515.8
530.0
542.6
568.6
581.3
594.9
608.9
624.3
637.0
649.9
662.9
7,687.9
7,728.8
7,741.7
7,768.8
7,785.3
7,799.6
TARun
Time
hrs
17.9
3.0
1.2
3.2
2.7
2.2
1.2
6.4
2.0
2.6
2.7
11.6
11.5
14.8
8.8
11.4
12.4
12.6
12.8
12.6
17.2
15.1
11.1
10.8
11.1
17.7
18.3
15.0
14.7
12.6
17.9
7
.3
.5
5.8
.3
.9
5.0
.9
2.1
(\
3
.9
2.6
2.6
3.0
2.7
.7
2 .0
5.9
.6
.5
2.6
3.9
3.8
.3
.2
.0
.3
.6
.0
.5
.9
.9
TBRun
Time
hrs
18.3
2.5
1.1
2.5
2.1
1.9
0.6
6.3
1.8
1.9
2.7
11.2
11.1
.7
i i
.4
.6
.9
2.8
6
7.2
.7
.0
2
.3
7.1
7.9
.5
9
2.1
2
7
.2
.0
2< .2
i.2
.3
.0
5.2
.6
.8
.4
.9
.9
.4
.5
.8
7
2.6
.5
.2
6
3.3
2.7
3.6
.0
4
2.7
2.9
0
9
.5
2.9
5
5
3
KMnO4
Tankl
Level(a)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
KMnO4
Tank 2
Level
(Iron)
inches
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Estimated
KMnO4
Dosage
jxg/L as Mn
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
NR
Pressure Filtration
Influent
psig
15
8
25
26
8
8
26
8
27
42
8
8
25
26
25
8
26
8
26
8
8
26
27
26
25
25
26
25
16
26
16
17
8
26
33
26
26
26
8
8
25
8
8
26
26
25
25
33
33
32
25
25
25
25
25
25
33
24
25
8
8
25
8
25
24
8
34
27
Outlet
Tank A
psig
15
11
25
23
10
10
23
9
22
41
10
10
23
23
23
10
24
10
24
10
9
23
22
25
25
24
23
21
15
22
16
3
23
2
22
24
20
9
9
23
10
10
24
23
24
24
30
44
4
23
23
23
24
23
23
30
22
22
10
10
24
10
23
22
22
11
27
23
Outlet
TankB
psig
14
2
23
22
8
8
23
6
22
40
8
8
22
22
23
8
22
7
21
9
8
22
22
22
23
21
22
21
14
24
14
4
24
28
22
21
23
7
8
23
8
9
22
23
23
23
3
28
27
23
22
23
22
22
23
42
22
22
10
10
22
10
21
22
22
10
3
21
Effluent
P 9
.
5
;
7
)
)
5
)
5
)
)
;
;
i
)
7
)
1
0
)
5
5
8
i
4
7
1
5
1
8
9
5
i
5
i
)
)
1
)
)
i
1
t
9
5
5
5
1
8
1
t
t
t
Inlet-TA
P 9
- 1
Inlet-TB
psig
Inlet-
Effluent
p g
8
8
-3
-7
8
-3
9
9
10
-2
19
11
Flow
rate
gpm
262
0
448
412
0
0
425
0
424
187
0
0
428
423
440
0
436
0
426
190
0
0
435
427
430
454
448
407
256
445
267
509
NA
403
322
408
424
399
0
0
414
0
0
410
. 10
. 09
. 05
; 11
; 15
32
. 13
19
. 23
10
419
396
432
422
0
0
411
0
417
419
409
0
282
384
Totalizer to
Distribution
kgal
33.7
347.4
646.9
986.8
1,285.6
1,601.3
1,878.9
2,180.8
2,478.2
2,802.3
3,116.7
133.1
419.3
770.6
1,016.4
1,307.5
1,611.9
1,911.3
2,235.5
2,530.1
3,175.6
225.5
554.0
839.8
1,120.4
1 ,400.7
2,070.1
2,359.9
2,686.3
3,010.3
103.0
152.2
NA
804.4
1,261.5
1,647.7
1,986.7
2,327.8
2,700.2
6.9
321.8
939.4
1,284.0
1,576.2
2,202.4
2,510.8
2,832.5
178.2
509.1
863.9
1,248.1
1,588.4
2,293.0
2,598.3
3,272.1
330.0
652.6
973.4
1,304.7
1,932.3
2,264.0
2,584.1
2,936.6
3,248.7
295.5
959.3
1,258.3
Gallon
Usage
gal
33,700
313,700
299,500
339,900
298,800
315,700
277,600
301,900
297,400
324,100
314,400
133,100
286,200
351,300
245,800
291,100
304,400
299,400
324,200
294,600
332,900
225,500
328,500
285,800
280,600
280,300
335,100
289,800
326,400
324,000
103,000
49,200
NA
652,200
457,100
386,200
339,000
341,100
372,400
6,900
314,900
273,400
344,600
292,200
294,000
308,400
321,700
178,200
330,900
354,800
384,200
340,300
356,200
305,300
341 ,000
330,000
322,600
320,800
331,300
324,800
331,700
320,100
352,500
312,100
295,500
334,100
299,000
Daily
Average
Flowrate
gpm
31
410
448
441
402
437
425
308
417
441
413
195
422
411
446
426
423
408
422
341
440
219
368
431
425
309
328
368
437
95
34
NA
768
326
723
395
394
411
11
439
ft/ALUE!
748
447
409
427
433
256
420
308
427
434
428
402
403
409
347
415
398
437
409
414
385
357
508
365
333
405
Backwash
Tank
A
No.
2685
2687
2689
2691
2694
2696
2698
2702
2703
2705
2707
2709
2711
2713
2715
2717
2719
2721
2723
2726
2731
2733
2735
2737
2740
2746
2748
2751
2753
2756
2758
NA
2760
2763
2 66
2 68
2 69
2 72
2 76
2 79
2 84
2 86
2788
2792
2796
2801
2808
2811
2816
2821
2825
2833
2836
2838
2841
2845
2847
2849
2852
2856
2859
2861
2864
2866
2868
2875
2876
Tank
B
No.
2701
2 02
2 06
2 10
2 15
2 18
2 21
2 26
2 28
2 31
2 34
2 37
2740
2743
2746
2748
2751
2754
2757
2761
2771
2774
2777
2780
2786
2788
2791
2794
2798
2800
2803
NA
2806
2810
2813
2815
2818
2821
2827
2832
2839
2841
2844
2854
2861
2869
2883
2891
2900
2909
2917
2934
2837
2941
2946
2951
2956
2959
2963
2970
2974
2978
2981
2985
2989
2998
3000
Total
Volume
kgal
3068.6
3074.6
3086.8
3098.6
3114.5
3124.8
3135.0
3153.6
3159.7
3169.9
3180.2
3190.4
3201.0
3210.9
3221.5
3230.7
3240.5
3250.7
3261.0
3276.2
34.8
45.0
56.0
67.5
97.4
107.8
120.0
132.1
142.4
288.6
NA
162.1
176.1
188.7
197.0
205.0
217.5
238.3
255.4
299.1
316.4
339.8
397.1
444.1
500.0
589.8
637.5
696.8
757.5
808.5
914.6
940.4
966.3
040.6
068.5
089.9
119.3
166.6
196.0
221.5
246.8
272.3
297.7
353.2
Daily
Volume
kgal
14.4
6.0
12.2
11.8
15.9
10.3
10.2
18.6
6.1
10.2
10.3
10.2
10.6
9.9
10.6
9.2
9.8
10.2
10.3
15.2
10.3
10.2
11.0
11.5
9.1
10.4
10.3
146.2
NA
WALUE!
14.0
12.6
8.3
8.0
12.5
10.2
17.1
12.8
17.3
23.4
33.9
47.0
55.9
46.9
47.7
59.3
60.7
51.0
55.0
25.8
25.9
40.6
27.9
21.4
29.4
25.6
29.4
25.5
25.3
25.5
25.4
25.5
Since Last BW
Run
Time
hrs
3.9
6.7
0.0
3.6
1.8
3.4
2.1
0.7
6.1
4.7
3.7
2.2
1.5
3.6
1.7
1.1
1.7
0.6
0.5
0.8
2.1
3.1
4.5
0.3
5.2
4.2
0.7
5.2
0.0
4.6
0.0
2.6
1.1
8.1
3.9
4.4
2.6
7.1
4.3
1.4
3.5
0.0
0.1
0.3
0.0
0.0
2.3
1.8
2.5
0.3
0.7
2.0
4.0
0.5
4.6
0.3
2.5
0.6
2.6
4.4
5.2
Run
Time
hrs
3.1
6.6
0.0
0.0
0.9
4.1
2.4
0.0
4.1
4.0
3.0
3.3
2.0
2.9
0.2
3.5
2.7
3.5
4.0
1.6
1.3
1.8
2.3
2.7
5.0
2.4
0.9
0.0
0.0
0.4
0.7
1.8
4.2
0.1
2.5
2.9
0.8
2.3
3.4
4.0
1.5
1 1
1.5
0.0
0.0
0.1
1.1
1.2
0.1
2.0
0.0
0.4
2.8
2.4
2.3
1.3
0.3
3.8
1.1
0.8
0.0
Standby
Time
hrs
0.3
0.0
0.6
2.1
1.9
.9
.1
.8
.9
i.2
.8
.9
.5
; .0
.0
.2
.5
.2
.8
.2
.2
. .5
.1
6.6
1.6
5.1
3.6
0.0
0.0
8.2
1.5
0.0
2.0
0.6
3.7
3.4
4.7
4.3
6.0
5.5
1.2
4.8
0.0
0.0
0.0
11.0
0.0
1.7
1.0
1.4
0.0
0.5
2.6
4.7
0.0
5.0
0.0
3.0
0.5
2.4
5.0
3.4
Standby
Time
hrs
0.0
0.0
0.0
3.0
0.3
1.6
0.7
0.9
4.9
6.0
5.8
4.4
3.5
1.8
0.0
5.9
4.6
5.5
5.9
2.5
1.6
2.6
5.4
4.5
1.6
5.1
1.0
1.6
0.0
0.0
0.0
0.0
0.0
1.2
3.3
0.0
1.7
3.1
1.0
3.4
5.8
3.3
1.8
0.9
1.9
0.0
0.9
0.0
0.6
0.7
0.0
1.9
2.2
0.0
0.5
3.7
1.9
2.0
0.7
0.1
4.1
1.3
2.1
0.9
0.0
3.6
-------
APPENDIX B
ANALYTICAL DATA TABLES
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
08/10/06
IN
312
1.9
0.3
<1
<0.05
683
39.7
17.0
-
6.8
25.0
1.5
-2.7
-
264
170
93.6
38.2
32.4
5.9
28.7
3.6
2,138
1,998
138
141
AC
324
1.7
<0.1
<1
<0.05
740
40.7
3.7
-
7.3
25.0
7.2
244
-
252
163
88.7
38.8
10.7
28.1
0.4
10.3
2,058
<25
787
229
TT
316
1.3
<0.1
<1
0.1
196
39.8
0.1
-
7.3
25.0
3.2
258
-
251
162
89.0
11.8
10.5
1.3
0.4
10.1
<25
<25
147
147
08/15/06
IN
316
-
-
-
-
663
41.5
21.0
-
7.0
21.9
0.9
-6.7
-
-
-
-
28.8
-
-
-
-
2,304
-
132
-
AC
337
-
-
-
-
658
41.7
2.4
-
7.2
24.9
5.5
457
-
-
-
-
28.8
-
-
-
-
1,890
-
678
-
TA
312
-
-
-
-
186
41.2
0.2
-
7.2
24.4
2.1
436
-
-
-
-
8.7
-
-
-
-
<25
-
21
-
TB
324
-
-
-
-
185
40.6
0.3
-
7.2
24.9
1.6
424
-
-
-
-
9.5
-
-
-
-
<25
-
617(a)
-
08/22/06
IN
338
-
-
-
-
652
40.7
24.0
-
6.8
24.0
2.2
6.1
-
-
-
-
36.3
-
-
-
-
1,851
-
131
-
AC
353
-
-
-
-
766
41.7
3.1
-
7.3
23.7
6.5
255
-
-
-
-
38.3
-
-
-
-
1,938
-
600
-
TA
336
-
-
-
-
224
41.3
0.6
-
7.3
23.7
3.8
242
-
-
-
-
11.1
-
-
-
-
<25
-
73
-
TB
344
-
-
-
-
207
40.8
0.3
-
7.3
23.6
4.3
303
-
-
-
-
10.7
-
-
-
-
<25
-
1443(a)
-
08/29/06
IN
335
-
-
-
-
592
39.8
24.0
-
6.9
24.9
1.7
5.4
-
-
-
-
30.8
-
-
-
-
2,059
-
148
-
AC
350
-
-
-
-
815
40.3
3.1
-
7.4
24.9
7.0
306
-
-
-
-
36.3
-
-
-
-
2,602
-
932
-
TA
331
-
-
-
-
199
40.1
0.4
-
7.3
24.9
3.3
317
-
-
-
-
10.7
-
-
-
-
<25
-
358
-
TB
326
-
-
-
-
189
38.0
0.4
-
7.3
25.0
3.9
314
-
-
-
-
10.4
-
-
-
-
<25
-
202
-
09/06/06
IN
342
2.2
<0.1
<1
<0.05
650
39.3
18.0
-
6.9
23.6
2.3
46.2
-
264
170
94.1
28.5
28.5
<0.1
27.3
1.2
2,088
1,535
142
148
AC
354
2.0
<0.1
<1
<0.05
721
40.9
2.9
-
7.3
23.5
5.6
227
-
263
172
90.8
30.2
10.2
20.0
0.5
9.7
1,950
<25
750
424
TT
344
1.1
<0.1
<1
0.2
200
40.0
0.1
-
7.3
23.7
3.4
247
-
258
167
90.9
10.5
10.7
<0.1
0.5
10.2
<25
<25
384
394
(a) Samples re-run with similar results.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
09/12/06
IN
342
-
-
-
-
611
40.3
24.0
-
6.9
23.4
2.5
3.1
-
-
-
-
32.4
-
-
-
-
2,040
-
142
-
AC
356
-
-
-
-
692
41.0
2.8
-
7.4
23.4
5.7
254
-
-
-
-
31.9
-
-
-
-
2,031
-
700
-
TA
354
-
-
-
-
171
40.8
0.2
-
7.3
23.4
3.2
266
-
-
-
-
9.8
-
-
-
-
<25
-
355
-
TB
342
-
-
-
-
186
41.5
0.2
-
7.3
23.5
2.9
269
-
-
-
-
12.3
-
-
-
-
<25
-
403
-
09/19/06
IN
333
-
-
-
-
570
41.8
26.0
-
6.9
22.5
3.0
5.7
-
-
-
-
26.4
-
-
-
-
2,104
-
139
-
AC
342
-
-
-
-
666
43.2
3.7
-
7.3
22.3
5.5
174
-
-
-
-
28.7
-
-
-
-
2,001
-
346
-
TA
328
-
-
-
-
199
43.4
0.1
-
7.3
22.2
3.1
207
-
-
-
-
11.1
-
-
-
-
<25
-
382
-
TB
338
-
-
-
-
201
43.0
0.2
-
7.3
22.3
2.9
229
-
-
-
-
11.3
-
-
-
-
<25
-
491
-
09/26/06
IN
334
-
-
-
-
493
39.9
20.0
-
6.9
20.8
3.0
26.2
-
-
-
-
24.1
-
-
-
-
2,082
-
142
-
AC
357
-
-
-
-
585
41.5
3.7
-
7.3
20.6
5.3
198
-
-
-
-
25.3
-
-
-
-
2,115
-
440
-
TA
348
-
-
-
-
206
40.9
0.1
-
7.3
20.8
2.6
210
-
-
-
-
11.3
-
-
-
-
<25
-
470
-
TB
330
-
-
-
-
196
41.8
0.1
-
7.3
20.7
2.3
213
-
-
-
-
11.7
-
-
-
-
<25
-
463
-
10/03/06
IN
333
2.1
0.2
<1
<0.05
596
40.6
25.0
-
6.0
22.3
2.2
318
-
276
194
82.1
34.1
28.4
5.7
23.4
5.0
1,999
826
145
145
AC
348
1.9
0.2
<1
<0.05
700
41.8
2.5
-
7.3
22.8
4.8
319
-
263
182
81.2
35.0
17.4
17.6
10.5(a)
6.9
1,972
<25
361 (a)
331
TT
319
0.6
0.2
<1
0.4
265
41.7
0.3
-
7.3
23.1
3.1
404
-
263
173
89.7
15.7
13.8
1.9
0.6
13.2
<25
<25
333
351
(a) Incomplete oxidation due to low KMnO4 dosage.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
10/10/06
IN
328
-
-
-
-
642
42.3
23.0
-
6.9
22.3
NA(a)
NA(a)
-
-
-
-
32.6
-
-
-
-
1,878
-
141
-
AC
343
-
-
-
-
742
42.4
2.9
-
7.4
22.1
NA(a)
140
-
-
-
-
30.9
-
-
-
-
1,669
-
345
-
TA
332
-
-
-
-
278
42.0
0.7
-
7.3
22.3
NA(a)
NA(a)
-
-
-
-
14.4
-
-
-
-
<25
-
260
-
TB
317
-
-
-
-
298
42.2
0.7
-
7.3
22.2
NA(a)
NA(a)
-
-
-
-
17.7
-
-
-
-
<25
-
341
-
10/17/06
IN
337
-
-
-
-
606
40.0
19.0
-
6.8
22.6
2.5
32.8
-
-
-
-
33.1
-
-
-
-
2,012
-
153
-
AC
343
-
-
-
-
699
41.2
3.4
-
7.3
22.4
6.0
209
-
-
-
-
35.7
-
-
-
-
2,026
-
633
-
TA
335
-
-
-
-
199
42.9
0.5
-
7.3
22.5
2.7
232
-
-
-
-
12.3
-
-
-
-
<25
-
299
-
TB
333
-
-
-
-
201
41.8
0.5
-
7.3
22.6
2.4
232
-
-
-
-
12.2
-
-
-
-
<25
-
382
-
10/24/06
IN
337
337
-
-
-
-
646
627
41.0
40.3
24.0
22.0
-
6.9
19.2
3.4
371
-
-
-
-
39.1
36.9
-
-
-
-
2,457
2,509
-
138
138
-
AC
345
356
-
-
-
-
695
713
42.3
41.7
3.3
3.4
-
7.3
19.1
6.5
355
-
-
-
-
38.9
38.5
-
-
-
-
2,331
2,294
-
622
619
-
TA
337
333
-
-
-
-
195
195
41.3
40.9
0.5
0.4
-
7.3
19.1
3.5
363
-
-
-
-
12.6
12.8
-
-
-
-
<25
<25
-
383
384
-
TB
333
335
-
-
-
-
196
197
41.8
39.4
0.7
0.3
-
7.3
19.0
3.0
363
-
-
-
-
12.9
13.1
-
-
-
-
<25
<25
-
443
441
-
10/31/06
IN
348
-
-
-
-
636
40.7
23.0
-
6.9
21.7
2.1
424
-
-
-
-
32.9
-
-
-
-
2,261
-
154
-
AC
359
-
-
-
-
773
41.9
2.9
-
7.3
21.4
5.6
407
-
-
-
-
34.1
-
-
-
-
2,224
-
793
-
TA
348
-
-
-
-
221
41.9
0.5
-
7.3
21.6
2.2
412
-
-
-
-
11.0
-
-
-
-
<25
-
347
-
TB
346
-
-
-
-
230
41.0
0.6
-
7.3
21.6
2.2
408
-
-
-
-
11.1
-
-
-
-
<25
-
310
-
11/07/06
IN
328
1.8
0.2
<1
<0.05
595
39.8
23.0
-
6.9
21.7
3.4
373
-
308
196
112.0
26.8
27.7
<0.1
24.1
3.6
2,372
2,277
173
180
AC
336
1.7
0.2
<1
<0.05
734
41.1
3.0
-
7.4
21.6
5.8
388
-
293
187
106.0
30.7
10.2
20.5
1.3
8.9
2,375
<25
784
322
TT
328
0.5
0.2
<1
0.5
210
40.1
0.5
-
7.3
21.6
3.6
385
-
281
178
103.0
9.0
8.6
0.4
1.3
7.3
<25
<25
306
307
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
11/14/06
IN(a|
330
-
-
-
-
651
39.7
24.0
-
6.8
20.1
2.6
389(b)
-
-
-
-
36.5
-
-
-
-
1,981
-
141
-
AC(a>
336
-
-
-
-
748
40.3
3.1
-
7.3
20.1
5.5
359
-
-
-
-
36.6
-
-
-
-
1,920
-
755
-
TA
324
-
-
-
-
216
39.6
0.3
-
7.4
20.1
2.9
265
-
-
-
-
12.1
-
-
-
-
<25
-
225
-
TB
332
-
-
-
-
217
40.8
0.4
-
7.4
20.0
2.5
372
-
-
-
-
12.9
-
-
-
-
<25
-
187
-
11/28/06
IN
350
-
-
-
-
474
42.2
22.0
-
6.8
21.9
2.4
403
-
-
-
-
27.3
-
-
-
-
1,914
-
135
-
AC
363
-
-
-
-
632
43.2
2.5
-
7.3
21.6
4.9
313
-
-
-
-
31.7
-
-
-
-
1,939
-
545
-
TA
350
-
-
-
-
154
43.2
0.4
-
7.3
21.6
2.2
313
-
-
-
-
10.3
-
-
-
-
<25
-
232
-
TB
352
-
-
-
-
155
42.7
0.7
-
7.3
21.7
2.7
318
-
-
-
-
10.5
-
-
-
-
<25
-
238
-
12/05/06
IN
337
1.9
0.2
<1
<0.05
552
39.6
20.0
1.6
6.9
16.6
4.7
428
-
303
206
96.7
35.3
30.4
4.9
26.6
3.8
2,042
1,965
150
158
AC
361
1.8
0.2
<1
<0.05
717
40.5
4.6
1.3
7.4
16.6
4.7
389
-
282
188
93.8
37.6
14.2
23.4
1.7
12.5
2,065
<25
720
474
TT
333
0.8
0.2
<1
0.6
177
40.3
0.5
1.2
7.4
16.8
4.8
391
-
273
180
93.0
12.0
11.5
0.5
0.9
10.6
<25
<25
288
304
12/19/06
IN
347
-
-
-
-
581
41.7
25.0
-
7.0
20.8
-
-
-
-
-
-
29.9
-
-
-
-
2,207
-
155
-
AC
355
-
-
-
-
741
42.5
4.2
-
7.0
20.6
-
-
-
-
-
-
33.8
-
-
-
-
2,222
-
627
-
TA
351
-
-
-
-
220
42.8
0.9
-
NA(a)
20.7
-
-
-
-
-
-
13.1
-
-
-
-
93(b)
-
605(b)
-
TB
355
-
-
-
-
252
42.9
0.9
-
7.5
20.7
-
-
-
-
-
-
13.6
-
-
-
-
149(b)
-
564(b)
-
01/01/07
IN
361
-
-
-
-
569
41.7
20.0
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
36.8
-
-
-
-
2,230
-
145
-
AC
365
-
-
-
-
723
42.8
3.2
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
37.6
-
-
-
-
2,226
-
536
-
TA
359
-
-
-
-
213
41.1
0.7
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
14.4
-
-
-
-
31(b)
-
482(b)
-
TB
371
-
-
-
-
221
43.2
0.6
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
14.7
-
-
-
-
28(b)
-
394(b)
-
(a) Not measured.
(b) Mn and Fe levels elevated after acid/base wash and after system returned to service on 12/12/07.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
01/09/07
IN
332
1.5
0.2
<1
<0.05
542
41.3
23.0
1.3
NA(a)
NA(a)
NA(a)
NA(a)
-
288
181
106.6
30.3
30.1
0.2
10.2
19.9
2,013
1,788
147
152
AC
351
1.7
0.3
<1
<0.05
717
42.0
3.1
1.3
NA(a)
NA(a)
NA(a)
NA(a)
-
247
151
95.7
32.0
19.0
13.0
2.8
16.2
2,003
<25
536
478
TT
354
1.7
0.2
<1
<0.05
240
42.6
0.8
1.2
NA(a)
NA(a)
NA(a)
NA(a)
-
241
146
95.0
13.2
12.5
0.7
0.7
11.8
95
<25
129
156
01/16/07
IN
347
-
-
-
-
526
41.4
22.0
-
NA(a)
NA(a)
3.7
409
-
-
-
-
25.4
-
-
-
-
2,002
-
133
-
AC
351
-
-
-
-
700
42.9
3.3
-
NA(a)
NA(a)
5.6
392
-
-
-
-
28.4
-
-
-
-
1,974
-
475
-
TA
349
-
-
-
-
161
41.4
0.5
-
NA(a)
NA(a)
4.9
391
-
-
-
-
10.7
-
-
-
-
<25
-
57.7
-
TB
355
-
-
-
-
112
41.7
0.5
-
NA(a)
NA(a)
4.8
391
-
-
-
-
10.6
-
-
-
-
<25
-
128
-
01/24/07
IN
334
322
-
-
-
-
574
566
39.9
39.4
22.0
22.0
-
6.9
18.1
3.2
420
-
-
-
-
34.4
34.8
-
-
-
-
2,055
2,005
-
129
130
-
AC
339
334
-
-
-
-
657
668
41.2
40.5
3.3
3.3
-
7.3
18.3
5.9
384
-
-
-
-
35.9
36.6
-
-
-
-
1,822
1,826
-
468
482
-
TA
330
326
-
-
-
-
175
183
40.6
40.8
0.5
0.5
-
7.5
18.2
4.5
381
-
-
-
-
12.5
13.5
-
-
-
-
<25
<25
-
155
156
-
TB
339
335
-
-
-
-
179
176
40.1
40.7
0.6
0.6
-
7.5
18.0
3.8
386
-
-
-
-
13.6
13.5
-
-
-
-
<25
<25
-
208
209
-
01/30/07
IN
351
1.9
0.2
<1
<0.05
703
38.4
34.0
1.2
6.8
18.1
4.0
412
-
304
200
104.0
32.8
35.8
<0.1
26.5
9.3
1,285
902
105
28.9
AC
368
1.8
0.2
<1
0.1
643
40.8
4.5
1.4
7.4
18.1
6.2
387
-
286
188
97.8
31.8
14.6
17.2
4.4
10.2
904
<25
450
21.4
TT
347
1.3
0.2
<1
0.1
211
40.4
0.9
1.2
7.5
18.1
5.1
371
-
273
182
91.4
12.8
12.6
0.2
3.2
9.4
<25
<25
126
20.2
02/06/07|b|
IN
338
-
-
-
-
547
39.5
23.0
1.5
7.0
17.4
3.5
381
-
-
-
-
27.1
-
-
-
-
1,640
-
105
-
AC
357
-
-
-
-
662
40.5
3.9
1.6
7.0
17.7
4.1
376
-
-
-
-
27.6
-
-
-
-
1,558
-
180
-
TA
341
-
-
-
-
216
40.2
0.4
1.4
7.5
17.3
6.2
389
-
-
-
-
13.3
-
-
-
-
<25
-
135
-
TB
346
-
-
-
-
219
38.7
0.5
1.4
7.5
17.5
4.7
393
-
-
-
-
13.9
-
-
-
-
<25
-
150
-
(a) Not measured, (b) TOC samples analyzed out of hold time.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as
CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
02/21 /07|c|
IN
368
-
-
-
-
762
41.9
22.0
-
6.8
20.7
3.3
406
-
-
-
-
43.0
-
-
-
-
1,522
-
103
-
AC
339
-
-
-
-
755
42.8
7.4
-
7.2
20.6
3.1
386
-
-
-
-
41.6
-
-
-
-
1,460
-
90.2
-
TA
344
-
-
-
-
237
42.1
0.9
-
7.3
20.6
5.5
412
-
-
-
-
19.9
-
-
-
-
<25
-
101
-
TB
339
-
-
-
-
225
42.9
0.1
-
7.3
20.6
6.1
412
-
-
-
-
18.8
-
-
-
-
<25
-
101
-
02/27/07
IN
345
-
-
-
-
752
42.3
92(=)
-
6.9
14.6
2.9
416
-
-
-
-
32.8
-
-
-
-
1,618
-
196
-
AC
345
-
-
-
-
747
42.7
5.7
-
7.3
NA(a)
5.8
479
-
-
-
-
32.9
-
-
-
-
1,538
-
142
-
TA
338
-
-
-
-
243
41.7
0.6
-
7.4
19.8
4.8
445
-
-
-
-
17.5
-
-
-
-
<25
-
228(b)
-
TB
321
-
-
-
-
241
41.0
0.4
-
7.4
19.8
5.6
440
-
-
-
-
17.8
-
-
-
-
<25
-
211(b)
-
03/06/07
IN
346
1.9
0.2
<1
<0.05
808
41.5
12.0(c)
1.8
7.0
18.6
3.8
407
-
298
193
105.0
39.7
33.5
6.2
29.6
3.9
1,619
1,460
123
124
AC
339
1.7
0.2
<1
<0.05
795
41.7
8.1
1.7
7.3
18.7
5.6
416
-
302
194
108.0
41.1
22.2
18.9
3.2
19.0
1,548
<25
120
117
TT
346
1.4
0.2
<1
<0.05
241
41.2
1.0
1.7
7.4
18.6
5.6
415
-
263
170
92.8
19.0
15.6
3.4
2.3
13.3
<25
<25
138
139
03/13/07
IN
358
-
-
-
-
681
41.4
29.0
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
35.9
-
-
-
-
1,476
-
96.2
-
AC
351
-
-
-
-
671
41.7
12.0
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
37.0
-
-
-
-
1,385
-
96.9
-
TA
346
-
-
-
-
195
41.3
7.2
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
15.8
-
-
-
-
<25
-
195
-
TB
343
-
-
-
-
195
41.2
4.4
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
16.3
-
-
-
-
<25
-
198
-
03/21/07
IN
337
-
-
-
-
766
43.5
29.0
-
6.9
21.0
2.3
420
-
-
-
-
40.1
-
-
-
-
1,733
-
98.9
-
AC
332
-
-
-
-
770
43.7
7.2
-
7.2
20.9
4.8
448
1.6
-
-
-
39.9
-
-
-
-
1,726
-
101
-
TA
328
-
-
-
-
202
42.9
2.7
-
7.3
21.0
5.7
448
-
-
-
-
19.8
-
-
-
-
<25
-
110
-
TB
328
-
-
-
-
192
43.4
1.3
-
7.3
21.0
6.0
443
1.3
-
-
-
18.6
-
-
-
-
<25
-
103
-
(a) Not measured, (b) Samples rerun with similar results.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
03/26/07
IN
334
334
-
-
-
-
873
861
42.1
42.6
25.0
26.0
-
6.9
21.8
3.3
395
-
-
-
-
40.5
38.2
-
-
-
-
1,959
2,005
-
113
116
-
AC
329
324
-
-
-
-
788
818
41.8
41.4
5.9
6.0
-
7.1
21.6
5.3
334
1.7
-
-
-
36.5
37.8
-
-
-
-
1,869
1,886
-
115
116
-
TA
326
324
-
-
-
-
181
188
42.1
41.2
0.1
0.4
-
7.2
21.7
4.5
387
-
-
-
-
16.5
16.4
-
-
-
-
<25
<25
-
135
132
-
TB
324
329
-
-
-
-
180
186
41.9
42.1
0.4
0.3
-
7.3
21.8
5.5
423
0.5
-
-
-
16.6
16.4
-
-
-
-
<25
<25
-
130
129
-
04/03/07
IN
335
-
-
-
-
751
40.2
21.0
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
38.1
-
-
-
-
1,889
-
107
-
AC
335
-
-
-
-
729
41.3
6.7
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
36.9
-
-
-
-
1,810
-
109
-
TA
322
-
-
-
-
189
40.8
0.5
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
16.8
-
-
-
-
<25
-
109
-
TB
325
-
-
-
-
184
40.8
0.7
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
16.2
-
-
-
-
<25
-
112
-
04/10/07
IN
341
1.8
0.2
<1
<0.05
701
42.2
26.0
1.5
NA(a)
NA(a)
NA(a)
NA(a)
-
243
165
77.1
39.5
34.1
5.4
30.7
3.4
1,618
1,693
98
105
AC
334
1.6
0.2
<1
<0.05
684
41.8
11.0
1.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
246
166
80.4
38.8
17.5
21.3
0.8
16.7
1,521
<25
97
88.8
TT
336
1.4
0.2
<1
0.1
190
42.1
2.0
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
253
169
83.8
17.7
16.2
1.5
2.1
14.1
<25
<25
175
189
04/17/07
IN
338
-
-
-
-
688
43.2
28.0
-
6.9
19.8
3.4
409
-
-
-
-
40.5
-
-
-
-
2,595
-
163
-
AC
330
-
-
-
-
663
43.4
7.0
-
7.1
20.0
5.3
445
2.5
-
-
-
39.6
-
-
-
-
2,417
-
164
-
TA
326
-
-
-
-
181
43.5
0.8
-
7.2
19.9
4.2
479
-
-
-
-
15.9
-
-
-
-
<25
-
169
-
TB
330
-
-
-
-
192
43.6
1.3
-
7.2
20.0
3.8
463
0.9
-
-
-
18.4
-
-
-
-
<25
-
168
-
04/30/07
IN
340
-
-
-
-
826
43.1
25.0
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
39.8
-
-
-
-
2,453
-
151
-
AC
340
-
-
-
-
799
43.2
16.0
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
39.3
-
-
-
-
2,205
-
152
-
TA
340
-
-
-
-
183
42.9
0.7
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
34.3
-
-
-
-
<25
-
267
-
TB
335
-
-
-
-
176
43.2
0.9
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
32.5
-
-
-
-
<25
-
281
-
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
01/23/08
IN
-
-
-
-
-
-
-
:
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
28.5
28.3
0.2
12.5
15.8
2,303
2,462
133
142
AC
-
-
-
-
-
-
-
:
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
18.7
11.0
7.7
1.2
9.8
701
<25
127
127
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
9.4
7.9
1.6
0.8
7.1
45.0
<25
117
120
01/28/08
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
41.3
34.5
6.7
13.8
20.8
8,045
6,314
195
198
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
41.8
11.3
30.5
1.0
10.3
2,229
<25
108
90.8
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
10.7
9.2
1.5
0.9
8.3
<25
<25
76.3
76.4
03/11/08
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
35.1
34.3
0.8
24.2
10.0
2,445
2,391
144
146
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
36.1
9.0
27.1
0.9
8.2
2,520
<25
138
127
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
10.3
7.7
2.6
1.2
6.4
142
<25
128
125
03/19/08
IN
-
-
-
-
-
804
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
35.9
28.8
7.0
28.4
0.5
2,204
<25
134
130
AC
-
-
-
-
-
779
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
35.5
8.2
27.4
1.3
6.9
2,717
<25
131
122
TT
-
-
-
-
-
108
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
7.6
6.3
1.3
1.1
5.2
<25
<25
123
124
03/24/08
IN
-
-
-
-
-
832
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
38.6
33.8
4.9
27.8
6.0
2,274
2,410
134
141
AC
-
-
-
-
-
821
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
37.9
9.5
28.4
1.2
8.2
2,752
<25
133
129
TT
-
-
-
-
-
172
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
10.4
7.9
2.5
1.2
6.7
104
<25
128
133
04/17/08
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
35.2
33.9
1.3
24.2
9.7
2,364
2,307
140
141
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
35.6
6.6
29.0
0.3
6.4
3,573
<25
150
140
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
5.6
5.2
0.4
0.2
5.0
31.9
<25
137
134
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
11/18/08
IN
-
-
-
-
-
726
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
40.9
36.6
4.2
34.0
2.6
1,983
1,960
110
131
AC
-
-
-
-
-
1,717
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
37.6
14.9
22.7
0.9
13.9
2,132
<25
170
155
TT
-
-
-
-
-
148
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
10.5
8.5
2.0
0.9
7.6
135
<25
156
157
12/03/08
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
36.2
32.3
3.9
30.9
1.3
2,283
2,149
117
119
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
36.9
2.5
34.4
0.8
1.7
9,399
26
135
117
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
12.3
4.7
7.6
0.8
3.9
1,399
<25
109
107
01/19/09
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
33.0
34.9
<0.1
1.6
33.3
1,812
241
113
109
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
32.5
10.1
22.4
0.5
9.6
2,159
32
110
112
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
7.4
7.2
0.2
0.7
6.5
34
<25
105
109
01/27/09
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
29.7
29.3
0.3
27.5
1.9
1,768
1,851
107
112
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
30.9
10.0
20.9
0.7
9.3
2,159
<25
106
98.6
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
7.9
7.7
0.2
0.7
7.0
26
<25
99.4
101
03/13/09
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
32.9
31.7
1.2
30.5
1.2
2,317
2,228
124
122
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
34.4
3.8
30.5
0.9
2.9
6,003
31.2
135
102
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
22.8
12.6
10.2
0.9
11.8
1,763
<25
120
113
03/23/09
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
32.5
29.4
3.1
23.7
5.7
2,052
1,835
123
126
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
34.0
11.3
22.7
0.3
10.9
2,487
<25
122
111
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
11.1
9.2
1.9
0.4
8.8
146
<25
131
128
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
03/30/09
IN
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
32.7
32.7
0.1
31.9
0.8
2,332
2,280
112
112
AC
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
32.0
32.0
17.1
0.8
14.0
2,423
<25
107
93.5
TT
-
-
-
-
-
-
-
;
-
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
16.4
16.4
5.1
0.9
10.4
824
<25
111
97.9
08/18/09
IN
326
1.9
0.3
<0.1
<0.05
-
44.4
32.0
1.8
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
-
30.8
30.9
<0.1
12.3
18.5
1,854
1,904
164
165
AC
324
1.7
0.2
<0.1
<0.05
-
44.9
5.9
1.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
34.1
11.2
22.9
1.5
9.7
1,892
118
113
107
TT
315
1.5
0.7
<0.1
0.1
-
44.6
0.3
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
-
-
-
9.9
9.3
0.6
1.3
8.0
41
<25
110
106
09/01/09
IN
318
1.9
0.2
<0.1
<0.05
-
46.4
29.0
1.6
NA(a)
NA(a)
NA(a)
NA(a)
-
273
175
98.3
30.2
29.7
0.5
19.5
10.2
1,838
1,966
112
117
AC
323
1.6
0.3
<0.1
<0.05
-
46.8
2.3
1.6
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
281
183
97.8
33.6
11.6
22.0
0.5
11.1
1,790
<25
112
96.3
TT
316
1.6
0.2
<0.1
0.1
-
47.0
0.5
1.6
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
275
179
96.5
7.3
8.9
<0.1
0.3
8.6
<25
<25
103
105
09/09/09
IN
323
1.9
0.2
<0.1
<0.05
-
45.8
32.0
1.6
NA(a)
NA(a)
NA(a)
NA(a)
-
274
175
99.8
28.3
28.4
<0.1
20.1
8.4
1,775
1,857
110
113
AC
309
1.3
0.2
<0.1
<0.05
-
46.8
2.0
2.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
266
170
96.0
31.5
10.5
20.9
0.7
9.9
1,704
<25
107
25.2
TT
305
1.3
0.2
<0.1
<0.05
-
47.1
0.5
1.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
255
160
94.7
7.4
8.5
<0.1
<0.1
8.4
87
<25
103
111
09/15/09
IN
307
1.9
0.2
<0.1
<0.05
-
45.1
31.0
1.8
NA(a)
NA(a)
NA(a)
NA(a)
-
242
149
92.2
29.9
31.5
25.0
4.9
20.1
4.9
1,805
2,114
1,881
115
139
116
AC
294
1.4
0.2
<0.1
<0.05
-
45.3
2.3
1.7
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
231
142
89.2
32.4
30.9
2.2
30.2
0.9
1.3
1,758
2,067
<25
114
134
108
TT
302
1.6
0.2
<0.1
<0.05
-
45.3
0.4
1.6
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
225
138
87.7
1.4
0.3
1.1
0.4
<0.1
69
<25
107
107
09/28/09
IN
322
2.0
0.2
<0.1
<0.05
-
46.5
32.0
1.3
NA(a)
NA(a)
NA(a)
NA(a)
-
267
180
86.9
32.7
30.5
2.2
26.4
4.2
1,938
1,958
119
118
AC
314
0.9
0.2
<0.1
0.1
-
47.2
2.0
1.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
258
172
85.5
33.8
10.5
23.3
0.5
10.0
1,856
<25
116
99
TT
308
1.2
0.3
<0.1
0.1
-
47.3
0.1
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
256
172
84.9
9.4
9.6
<0.1
0.5
9.1
27
<25
110
116
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
10/05/09
IN
311
2.1
0.2
<0.1
<0.05
-
44.1
32.0
1.0
NA(a)
NA(a)
NA(a)
NA(a)
-
264
177
87.9
33.8
32.1
11, 11.5
22.7
0.4, 0.7
10.6
2,054
2,364
<25,
25.5
119
134
104, 119
AC
309
1.6
0.2
<0.1
<0.05
-
45.0
2.6
1.0
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
253
168
84.8
34.6
31.0,31.3
3.6
27.0, 30.2
3.7
1,825
1956,
2165
116
122, 135
TT
311
1.6
0.2
<0.1
<0.05
-
45.0
0.9
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
251
167
83.8
18.6
8.8
9.8
0.6
8.2
790
<25
116
113
10/13/09
IN
321
2.0
0.2
<0.1
<0.05
706
42.0
31.0
1.0
NA(a)
NA(a)
NA(a)
NA(a)
-
292
192
100
32.4
28.5
3.9
26.8
1.7
2,283
2,203
119
119
AC
308
1.4
0.2
<0.1
<0.05
715
42.6
2.7
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
277
181
96.0
32.2
9.6
22.6
<0.1
9.5
2,122
<25
115
110
TT
313
1.4
0.2
<0.1
<0.05
323
41.6
0.5
<1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
286
189
97.8
14.9
7.1
7.8
<0.1
7.0
732
<25
119
116
10/19/09
IN
310
2.0
0.1
<0.1
<0.05
-
41.8
32.0
<1.0
NA(a)
NA(a)
NA(a)
NA(a)
-
315
231
84.0
31.0
28.6
2.4
27.8
0.8
2,050
2,362
134
138
AC
308
1.8
0.2
<0.1
<0.05
-
42.6
2.1
1.0
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
307
231
76.2
32.2
15.4, 16.4
16.8
<0.1,0.52
15.4
2,305
<25, <25
136
111, 113
TT
314
1.9
0.2
<0.1
0.1
-
42.4
0.7
<1.0
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
309
225
83.3
10.5
8.5
1.9
0.3
8.2
120
<25
125
130
10/26/09
IN
290
2.0
0.2
<0.1
<0.05
-
45.9
30.0
1.1
NA(a)
NA(a)
NA(a)
NA(a)
-
420
302
118
27.2
26.5
0.7
24.2
2.3
2,005
2,176
108
114
AC
297
1.8
0.2
<0.1
<0.05
-
46.6
2.2
1.2
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
417
301
116
28.6
10.5
18.1
0.3
10.2
2,042
25
107
105
TT
305
1.9
0.2
<0.1
<0.05
-
47.7
1.0
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
415
298
117
10.8
8.9
1.9
0.1
8.8
191
<25
104
105
11/03/09
IN
329
2.0
0.2
<0.1
<0.05
-
44.0
26.0
1.1
NA(a)
NA(a)
NA(a)
NA(a)
-
440
316
124
26.4
25.8
0.6
24.0
1.9
2,072
2,155
111
115
AC
325
1.8
0.2
<0.1
<0.05
-
44.3
2.0
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
438
316
122
27.9
8.9
19.0
<0.1
8.8
2,134
<25
109
102
TT
320
1.6
0.2
<0.1
0.1
-
44.7
0.9
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
439
316
124
10.2
9.8
0.3
0.3
9.6
325
<25
104
90.8
11/09/09
IN
319
2.0
0.1
<0.1
<0.05
-
47.1
30.0
1.4
NA(a)
NA(a)
NA(a)
NA(a)
-
206
108
97.2
35.4
33.9
1.5
32.3
1.5
2,373
2,452
150
144
AC
326
1.6
0.2
<0.1
<0.05
-
48.5
2.0
1.5
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
206
111
95.1
35.5
12.4
23.1
1.2
11.2
2,411
28.0
142
129
TT
328
1.6
0.1
<0.1
<0.05
-
47.6
2.1
1.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
205
110
95.5
12.8
9.7
3.1
1.3
8.4
235
<25
133
135
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Cd
to
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
11/17/09
IN
342
1.8
0.2
<0.1
<0.05
-
48.3
26.0
1.2
NA(a)
NA(a)
NA(a)
NA(a)
-
193
103
89.4
42.4
37.7
4.7
35.2
2.5
2,255
2,337
138
131
AC
329
1.5
0.2
<0.1
<0.05
-
47.7
1.9
1.2
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
198
106
91.4
41.8
14.3
27.4
1.6
12.7
2,264
<25
136
116
TT
324
1.5
0.2
<0.1
<0.05
-
47.0
0.4
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
187
100
86.5
13.8
12.1
1.7
1.6
10.5
118
<25
117
113
12/08/09
IN
335
1.9
0.2
<0.1
<0.05
-
43.5
30.0
1.9
NA(a)
NA(a)
NA(a)
NA(a)
-
244
162
82.1
27.9
27.9
<0.1
24.0
3.8
1,959
1,903
123
125
AC
330
1.7
0.2
<0.1
<0.05
-
44.8
1.7
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
229
153
75.8
27.2
9.3
17.9
0.6
8.7
1,902
<25
114
114
TT
326
0.2
0.8
<0.1
<0.05
-
45.2
0.8
<1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
222
149
72.3
3.9
3.9
<0.1
0.8
3.1
52
<25
99.9
104
01/05/10
IN
334
2.1
0.3
<0.1
<0.05
-
46.7
38.0
<1.0
NA(a)
NA(a)
NA(a)
NA(a)
-
263
173
90.2
27.7
28.1
<0.1
28.1
<0.1
2,939
3,276
144
151
AC
343
1.8
0.2
<0.1
<0.05
-
47.9
2.4
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
253
168
85.0
31.1
10.8
20.3
1.2
9.5
2,701
35
132
124
TT
350
1.8
0.3
<0.1
<0.05
-
48.4
0.3
1.0
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
246
163
83.0
18.1
9.5
8.5
1.1
8.5
1037
<25
106
103
01/11/10
IN
336
1.9
0.2
<0.1
<0.05
-
45.0
31.0
1.2
NA(a)
NA(a)
NA(a)
NA(a)
-
277
180
96.2
28.3
28.1
0.2
27.9
0.2
2,076
2,238
121
127
AC
331
1.9
0.2
<0.1
<0.05
-
46.6
3.2
1.1
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
277
190
87.3
28.9
14.4
14.5
1.1
13.3
2,154
31
116
115
TT
340
1.9
0.2
<0.1
<0.05
-
46.9
1.4
<1.0
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
278
188
90.1
14.3
14.3
<0.1
2.2
12.1
117
<25
106
117
(a) Not measured.
-------
Table B-l. Analytical Results from Long-Term Sampling at Arnaudville, LA (Continued)
Cd
OJ
Sampling Date
Sampling Location
Parameter Unit
Alkalinity (as CaCO3)
Ammonia (as N)
Fluoride
Sulfate
Nitrate (as N)
P (as P)
Silica (as SiO2)
Turbidity
TOC
PH
Temperature
DO
ORP
Total Chlorine
Total Hardness (as CaCO3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO3)
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L
mg/L
mg/L
mg/L
mg/L
M9/L
mg/L
NTU
mg/L
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
01/22/10
IN
314
2.0
0.2
<0.1
<0.05
-
49.3
14.0
1.5
NA(a)
NA(a)
NA(a)
NA(a)
-
219
130
88.8
27.0
27.8
<0.1
27.3
0.5
2,386
2,403
143
149
AC
325
1.9
0.2
<0.1
<0.05
-
50.0
4.2
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
216
129
87.5
29.6
13.3
16.3
1.8
11.4
2,273
72
138
136
TA
332
1.9
0.2
<0.1
<0.05
-
50.1
0.3
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
214
128
86.2
9.4
9.6
<0.1
1.5
8.0
60
<25
132
135
TB
336
1.9
0.2
<0.1
<0.05
-
49.6
0.6
1.2
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
222
133
89.0
10.9
9.8
1.1
1.4
8.4
124
<25
124
136
TT
321
1.9
0.2
<0.1
<0.05
-
49.6
0.4
1.3
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
224
134
90.6
5.2
9.3
<0.1
5.6
3.7
83
<25
132
137
02/01/10
IN
316
2.0
0.2
<0.1
<0.05
-
48.2
31.0
1.5
NA(a)
NA(a)
NA(a)
NA(a)
-
211
128
82.3
25.1
26.2
<0.1
25.4
0.7
2,245
2,322
157
156
AC
332
1.9
0.2
<0.1
<0.05
-
49.0
4.9
1.7
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
226
141
84.5
27.9
13.3
14.5
2.0
11.4
2,271
111
149
143
TT
330
1.9
0.2
<0.1
<0.05
-
48.9
0.4
1.5
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
226
143
83.4
12.4
12.1
0.3
1.8
10.3
51
<25
137
140
02/09/10
IN
343
1.9
0.2
<0.1
<0.05
-
45.5
29.0
1.7
NA(a)
NA(a)
NA(a)
NA(a)
-
275
181
93.7
29.5
29.8
<0.1
29.0
0.8
2,270
2,404
133
144
AC
334
1.9
0.2
<0.1
<0.05
-
46.8
4.8
1.5
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
272
182
89.5
30.7
13.3
17.5
1.1
12.1
2,219
25
134
131
TT
352
2.0
0.2
<0.1
<0.05
-
46.4
0.6
1.4
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
282
189
92.3
12.4
11.1
1.3
1.0
10.2
192
<25
128
130
08/05/10
IN
318
2.0
0.2
<0.1
<0.05
-
47.0
31.0
1.6
NA(a)
NA(a)
NA(a)
NA(a)
-
100
1.8
98.6
31.9
33.0
<0.1
31.2
1.8
2,455
2,485
150
151
AC
327
1.8
0.2
<0.1
<0.05
-
47.8
33.0
1.7
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
93.9
2.1
91.8
32.9
11.8
21.1
0.3
11.5
2,573
<25
224
254
TT
313
1.8
0.2
<0.1
<0.05
-
48.7
0.4
1.6
NA(a)
NA(a)
NA(a)
NA(a)
NA(a)
93.5
0.4
93.2
6.7
7.2
<0.1
0.2
7.0
<25
<25
156
156
------- |