-------
Monthly to Bimonthly
pHW, temperature'3',
DO, QRPW, C12 (free and; total) W
As (total and soluble),!As (III),
As (V), Fe (total and (soluble),
Mn (total and soluble),I Ca, Mg,
F, NO3! SO4! SiO2, P (tirtal), Ti,
turbidity, alkalinity
Klamath Falls, OR
60-gpm Adsorbsia™ GTO™ System at College
Union
DISTRIBUTION MAIN
AND ENTRY PIPING
pH, TSS, TDS,
As (total and soluble),
Fe (total and soluble),
Mn (total and soluble)
pH'2', temperature'2),
DOW, ORPW, C12 (free and total)W,
As (total and soluble), As (III),
As (V), Fe (total and soluble), <
Mn (total and soluble), Ca, Mg,
F, NO3, SO4, SiO2, P (total), Ti,
turbidity, alkalinity
pHW, temperature^),
DOW, ORPW, C12 (free and total)W,
As (total and soluble), As (III),
As (V), Fe (total and soluble),
Mn (total and soluble), Ca, Mg,
F, NO3, SO4, SiO2, P (total), Ti,
turbidity, alkalinity
Biweekly to Quarterly
pHW, temperature'3),
DOW, ORPW,
C12 (free and total)'2),
As (total)
LEGEND
Influent
Media Vessel Effluent
(TA and TB)
Total Combined Effluent
Backwash Sampling Location
Backwash Solid
Sampling Location
WELL NO. 1 Unit Process
DA: C12 Chlorine Disinfection
^- Process Flow
^~ BackwashFlow
pHW, temperature'2',
DO'2', ORP'2),
C12 (free and total)'2',
As (total)
pH'2), temperature'2',
DO'2', ORP'2),
C12 (free and total)'2),
As (total)
HYDRO PNEUMATIC
TANK (132 GAL)
Footnote
(a) Onsite analyses
BUILDING
DISTRIBUTION
SYSTEM
Figure 3-3. Process Flow Diagram and Sampling Locations for
Adsorbsia™ GTO™ System
14
-------
STORAGE
TANK
(250,000 GAL)
Klamath Falls, OR
POU ARM 200/E33-S Units
DISTRIBUTION MAIN
AND ENTRY PIPING
LEGEND
\ Water Sampling Location
After Filter
Unit Process
Chlorine Disinfection
POU CARTRIDGE
(AF
As (total)
Monthly
01/12/06-06/06/07
Quarterly
08/01/07-12/16/09
USER
Figure 3-4. Process Flow Diagram and Sampling Locations for POU Units
the other sampling events. On November 16, 2006, the sampling frequency was reduced to
bi-monthly for total arsenic only leading up to rebedding with ARM 300 media on January
24, 2007. Following rebedding, samples were collected monthly until June 1, 2007. On July
11, 2007, the system was placed in bypass until rebedding with E33-S on October 3, 2007.
The system was sampled quarterly between December 18, 2007, and August 26, 2009.
• College Union (Figure 3-3). On March 1, 2006, samples were collected at IN, TA, and TB
for total arsenic (note that Vessel A was in the lead position). After the first sampling event,
samples were collected bi-weekly on an eight-week cycle with speciation performed at all
locations at the beginning of the cycle and total arsenic during the remaining three bi-weekly
sampling events. Starting on May 9, 2006, samples were collected bi-weekly for six four-
week cycles with speciation performed at all locations at the beginning of the cycle and total
arsenic during the other sampling events. Samples were collected bi-monthly from January 1,
2007 through May 5, 2007. On August 1, 2007, samples were collected quarterly until
August 26, 2009.
For all sampling events, pH, temperature, DO, and ORP were measured onsite using a VWR SymPhony
handheld meter. Free chlorine residuals also were measured onsite using a Hach handheld colorimeter.
DO and ORP were not measured from February 13, 2008, through August 26, 2009.
Three of the eight POU units located in the University Advancement building (POU 1), Snell Hall (POU
2), and the Facility Services building (POU 3) were designated for monthly sampling from January 12,
2006, through June 6, 2006 and quarterly from August 1, 2007, through December 16, 2009. On
15
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February 13, 2008, the POU unit at Snell Hall was moved to Cornett Hall. Samples were collected after
cartridge filters for total arsenic analyses. Total flow measurements for the three POU units were
recorded through Kent meters. On November 15, 2007, May 25, 2008, and August 15, 2008, the three
Kinetico POU units were replaced with AdEdge POU units loaded with E33-S.
3.3.3 Backwash Wastewater and Solids. During the performance evaluation study, the three
POE systems were backwashed once on May 16 or 17, 2006. One backwash wastewater sample was
collected from each adsorption vessel. The procedure involved diverting a portion of backwash
wastewater from the backwash discharge line to a 32-gal plastic container over the duration of the
backwash for each vessel. After the content in the container had been thoroughly mixed, a composite
sample was collected and/or filtered onsite with 0.45-(im disc filters. Analytes for the backwash
wastewater samples are listed in Table 3-3.
The content in the 32-gal plastic container was allowed to settle and the supernatant was carefully
siphoned using a piece of plastic tubing to avoid agitation of settled solids in the container. The
remaining solids/water mixture was then transferred to a 1-gal plastic jar. After solids in the jar were
settled and the supernatant was carefully decanted, one aliquot of the solids/water mixture was air dried
before being acid-digested and analyzed for the metals listed in Table 3-3.
3.3.4 Distribution System Water. Water samples were collected from the distribution system to
determine the impact of the three POE arsenic treatment systems on its water chemistry, specifically, the
arsenic, lead and copper levels. Prior to system startup, four monthly baseline distribution water samples
were collected from three locations within the distribution system from July to September 2005.
Following system startup, distribution system sampling continued on a monthly basis at the same three
locations from January 25, 2006 to April 4, 2007. Analytes for the distribution system sampling are
presented in Table 3-3.
The three distribution system sampling locations were at Purvine Hall, the Residence Hall, and the
College Union. These three locations were part of OIT's historic sampling network for the Lead and
Copper Rule (LCR). The system operator collected the first draw distribution system samples following
an instruction sheet developed by Battelle in accordance with the Lead and Copper Monitoring and
Reporting Guidance for Public Water Systems (EPA, 2002). The operator recorded the date and time of
last water use before sampling and the date and time of sample collection for calculation of the stagnation
time. 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. The samples were analyzed for the analytes listed in Table 3-3.
Arsenic speciation was not performed for the distribution system water samples.
3.3.5 Residual Solids. Three ARM 200 spent media samples were collected from the lead vessel
(Tank B) during media changeout at the Residence Hall on January 24, 2007. Spent media was sampled
from the top (i.e., 0 to 4 in into the bed), middle (i.e., 22 to 26 in), and bottom (i.e., 35 to 39 in) of the
media bed using a 6.5-horsepower (hp) wet/dry shop vac that had been thoroughly cleaned and
disinfected before sampling. The media collected from each target layer was transferred from the shop
vac to a clean 5-gal bucket and mixed carefully with a small garden spade. A composite sample from
each layer was collected into a wide-mouth, 1-gal plastic container and sent to Battelle for analysis.
Metal analyses were conducted on air dried and acid digested samples (see analytes in Table 3-3) and
toxicity characteristic leaching procedure (TCLP) tests were conducted on unprocessed samples following
the protocol described in the QAPP (Battelle, 2004).
16
-------
3.4 Sampling Logistics
All sampling logistics, including arsenic speciation kit preparation, sample cooler preparation, and sample
shipping and handling are discussed below.
3.4.1 Preparation of Arsenic Speciation Kits. The arsenic field speciation method uses an anion
exchange resin column to separate soluble arsenic species, i.e., As(V) and As(III) (Edwards et al., 1998).
Resin columns were prepared in batches at Battelle laboratories in accordance with the procedures
detailed in Appendix A of the QAPP (Battelle, 2004).
3.4.2 Preparation of Sampling Coolers. For each sampling event, a sample cooler was prepared
with the appropriate number and type of sample bottles, disc filters, and/or speciation kits. All sample
bottles were new and contained appropriate preservatives. Each sample bottle was affixed with a pre-
printed, colored-coded, waterproof 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 for designating the arsenic speciation bottle (if
necessary). The sampling locations at the treatment plant were color-coded for easy identification. The
labeled bottles for each sampling location were placed in separate zip loc bags (each corresponding to a
specific sample location) and packed in the cooler. When needed, the sample cooler also included bottles
for the distribution system sampling.
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 placed in each cooler.
The chain-of-custody forms and airbills were complete except for the operator's signature and the sample
dates and times. After preparation, the sample cooler was sent to the site via FedEx for the following
week's sampling event.
3.4.3 Sample Shipping and Handling. After sample collection, samples for offsite analyses were
packed carefully in the original coolers with wet ice and shipped to Battelle. Upon receipt, the sample
custodian checked sample IDs against the chain-of-custody forms and verified that all samples indicated
on the forms were included and intact. The Battelle Study Lead addressed discrepancies noted by the
sample custodian with the plant operator. The shipment and receipt of all coolers by Battelle were
recorded on a cooler tracking log.
Samples for metal analyses were stored and analyzed at Battelie'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 American Analytical Laboratories (AAL) in Columbus, OH and
Belmont Labs in Englewood, OH, both of which were under contract with Battelle for this demonstration
study. The chain-of-custody forms remained with the samples from the time of preparation through
analysis and final disposition. All samples were archived by the appropriate laboratories for the
respective duration of the required hold time, and disposed of properly thereafter.
3.5 Analytical Procedures
The analytical procedures described in Section 4.0 of the QAPP (Battelle, 2004) were followed by
Batte lie's ICP-MS laboratory, AAL, 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
17
-------
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.
18
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4.0 RESULTS AND DISCUSSION
4.1
Site Description
4.1.1 Pre-existing Facility. The OIT-Klamath Falls campus (Figure 4-1) is located just east of the
Cascade Mountains in southern Oregon. The non-transient, non-community water system supplies water
to a population of 3,315 via 15 connections to individual buildings. The average daily use for the year of
2003 to 2004 was 167,000 gpd and the peak daily use was 350,000 gpd. A large quantity of water was
used for outdoor irrigation and landscaping due to the dry climate. Only 20,000 to 60,000 gpd was used
by facilities such as dormitories, classrooms, laboratories, and offices for drinking, sanitary, and
teaching/research purposes.
Source water is groundwater supplied by two wells, Wells No. 1 and No. 4, located on the east side of the
campus. Well No. 1 is the primary supply well and Well No. 4 is a backup well. Figure 4-2 shows the
Well No. 1 pump house. Well No. 1 was drilled to a depth of 1,205 ft below ground surface (bgs) with a
screen interval from 455 ft to 1,205 ft bgs. The well casings are 8-in in diameter from the surface to 685
ft bgs and 6-in in diameter from 685 ft to 1,205 ft bgs. Well No. 1 is equipped with a 60-hp closed line
shaft turbine pump rated for 300 gpm at a total dynamic head (TDH) of 600 ft of water or 260 lb/in2 (psi).
Well No. 4 has a total depth of 1,224 ft with a screen interval from 300 ft to 1,221 ft bgs. The well
casings are 12-in in diameter from the surface to 732 ft bgs, 10-in in diameter from 732 ft to 1,037 ft bgs,
and 8-in in diameter from 1,037 ft to 1,224 ft bgs. It is equipped with a 75-hp submersible pump rated for
250 gpm at a TDH of 530 ft of water or 230 psi. The static water level was measured at 449 ft bgs in
Well No. 1 and 315 ft bgs in Well No. 4. Well No. 1 typically operates approximately 2.5 hr/day in
winter and 12 hr/day in summer to meet the water demand.
Figure 4-1. View of OIT Campus
19
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Figure 4-2. Well No. 1 Pump House at OIT
The existing water treatment includes wellhead chlorination using chlorine gas to maintain a free chlorine
residual level of 0.25 to 0.35 mg/L (as C12). Figures 4-3 and 4-4 show an existing chlorine gas storage
unit and a chlorine addition system for Well No. 1. The chlorinated water is stored in a 250,000-gal
aboveground storage tank located near the pump house (Figure 4-5) before being distributed to the
campus.
Figure 4-3. Well No. 1 Chlorine Gas Storage Unit at OIT
20
-------
Figure 4-4. Close-up View of Well No. 1 Chlorine Addition System at OIT
Figure 4-5. 250,000-gal Aboveground Storage Tank at OIT
21
-------
4.1.2 Distribution System. The distribution system at OIT supplies water to 13 buildings on the
campus. Chlorinated water from the Well No. 1 pump house flows to the 250,000 gal storage tank before
entering the distribution system. Chlorinated water from the Well No. 4 pump house feeds directly into
the distribution system with excess water going to the storage tank. The distribution piping consists of
10-in asbestos cement, 8-in polyvinyl chloride (PVC), and 6-in ductile iron piping. The size and material
of the plumbing as well as the system pressure at each building inlet are presented in Table 4-1. Once
entering a building, the system pressure is reduced to 50 to 76 psi by a pressure reducing valve. Figure 4-
6 shows a photograph of a pressure reducing valve at one building inlet.
Figure 4-6. Pressure Reducing Valve at a Building Entry Point
The routine distribution system sampling at OIT included coliform (once a month), lead and copper (once
every three years), and asbestos (once every nine years). In December 2004, OIT conducted lead and
copper sampling at 20 locations. The 90th percentile results were below the respective action levels of 15
and 1,300 ug/L. As part of the EPA demonstration study, one location each in Purvine Hall, the
Residence Hall, and the College Union was selected for monthly distribution sampling before and after
installation of the POE treatment systems. These locations are part of OIT's historic LCR sampling
network. In addition, OIT conducted routine sampling at the distribution system entry points of Well No.
1 and Well No. 4 for arsenic, inorganic chemicals (IOC), nitrate, nitrite, volatile organic compounds
(VOCs), synthetic organic compounds (SOCs), and disinfection byproducts (DBP) from yearly to once
every nine years as directed by the Oregon DHS DWP.
4.1.3 Source Water Quality. Source water samples were collected from Well No. 1 on
October 27, 2004, and analyzed for the analytes shown in Table 3-3. The analytical results are presented
in Table 4-2 and compared to the data (for both Wells No. 1 and No. 4) provided by OIT to EPA for the
demonstration site selection and the data independently collected by Kinetico. Based on the data
presented in Table 4-2, water quality of the two wells was similar.
22
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Table 4-1. Source Water Quality Data for OIT Site
Parameter
Unit
Sampling Date
pH
Temperature
DO
ORP
Total Alkalinity (as aCO3)
Hardness (as CaCO3)
Turbidity
TDS
TOC
Nitrate (as N)
Nitrite (as N)
Ammonia (as N)
Chloride
Fluoride
Sulfate
Silica (as SiO2)
Orthophosphate (as PO4)
As (total)
As (soluble)
As (paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
U (total)
U (soluble)
V (total)
V (soluble)
Na
Ca
Mg
-
°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
Hg/L
^g/L
^g/L
^g/L
HB/L
^g/L
HB/L
^g/L
^g/L
^g/L
^g/L
HB/L
^g/L
mg/L
mg/L
mg/L
Facility Data
Well No. 4(a)
NA
7.6
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
23.0
NA
NA
29.0-35.0
NA
NA
NA
NA
ND
NA
ND
NA
NA
NA
NA
NA
23.0
NA
NA
Well No. 1
07/30/01
7.6
NA
NA
NA
NA
NA
NA
NA
NA
0.8, 0.7(b)
<0.01tb)
NA
NA
0.1
22.7
NA
NA
29.0, 27.0(c)
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
22.9
NA
NA
Kinetico
10/28/03
8.0
NA
NA
NA
112
80
NA
NA
NA
NA
NA
NA
3.9
0.2
22.0
34.2
<0.5
36.0
NA
NA
NA
NA
<30
NA
0.01
NA
NA
NA
NA
NA
25.0
23.0
5.8
Battelle
Well No. 1
10/27/04
7.9
23.0
4.2
82.0
107
81.0
0.6
200
<0.7
0.6
<0.01
O.05
2.6
<0.1
21.0
30.3
<0.06
32.8
33.0
0.1
0.5
32.5
<25
<25
0.2
O.I
0.3
0.2
35.0
35.8
31.9
20.8
7.0
(a) Provided by the facility to EPA for site selection.
(b) Sample taken on July 21, 2004.
(c) Sample taken on September 9, 2004.
DO = dissolved oxygen; NA= not available; ND = not determined; ORP = oxidation-
reduction potential; TDS = total dissolved solids; TOC = total organic carbon
Arsenic. Total arsenic concentrations in source water (from both wells) ranged from 27.0 to 36.0 (ig/L.
Based on the October 27, 2004, speciation results, out of 32.8 |o,g/L of total arsenic, 32.5 |o,g/L existed as
As(V). Although pre-chlorination was not required, the existing wellhead chlorination system continued
to be used to disinfect water throughout the study period.
Iron and Manganese. Iron and manganese concentrations in source water were low, typically less than
their MDLs of 25 and 0.1 |o,g/L, respectively. In general, AM technologies are best suited to water with
23
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low iron levels (i.e., less than 300 |o,g/L, which is the secondary maximum contaminant level [SMCL] for
iron).
pH. The pH of raw water ranged from 7.6 to 8.0. Typically, the target pH range for the use of AM for
arsenic removal is between 5.5 to 8.5. A pH value of 7.6 to 8.0 is within this range; therefore, pH
adjustment was not included for the arsenic treatment system.
Competing Anions. Arsenic adsorption could be influenced by the presence of competing anions such as
silica and phosphate. Analysis of source water indicated silica levels at 30.3 to 34.2 mg/L (as SiO2) and
orthophosphate levels below 0.5 mg/L (as PO4). Concentrations of these anions were monitored on a
regular basis during the system performance evaluation.
Other Water Quality Parameters. Nitrate was measured between 0.6 and 0.8 mg/L (as N). Nitrite,
ammonia, and fluoride were either below or close to their respective detection limits.
Table 4-3 presents historical treated water quality data from July 2001 through August 2005 obtained
from the Oregon DHS DWP. These treated water quality data were similar to the source water quality
data presented in Table 4-2. Total arsenic concentrations of the treated water ranged from 27 to 38 |o,g/L.
No arsenic speciation data were available.
Table 4-3. Treated Water Quality Data for OIT Site
Parameter
Unit
Date
Nitrate
Sulfate
As(total)
Na
mg/L (as N)
mg/L
W?/L
mg/L
Oregon DHS Treated Water Data
07/30/01-08/08/05
0.45-0.76
21.9-22.7
27-38
22.9-29.0
4.2
Treatment Process Description
4.2.1 POE/POU Approaches. Kinetico originally proposed a centralized treatment system at the
wellhead. This approach was replaced with one using three smaller POE systems during the January 19,
2005, project planning meeting attended by OIT, Kinetico, EPA, and the Oregon DHS DWP. The POE
approach was selected because (1) a POE system can be placed in an existing maintenance room in each
building, thus eliminating the need for a new treatment building to house a wellhead treatment system and
(2) a POE system only treats the water entering the building, not the water for irrigation and landscaping,
thus reducing the amount of water treated and the associated operational cost. Water usage and flowrate
information was not available during the system sizing and design phase of the project due to the lack of
water meters in any of the buildings. Weber Elliot Engineers and Kinetico provided flow estimates based
on fixture counts in each building. Table 4-3 summarizes these estimates.
To more accurately estimate flowrates, a portable ultrasonic flow meter (Greyline Instruments, Inc.) was
used for 24-hr real-time flow measurements in two buildings: the Residence Hall from March 28 to 29,
2005 (Figure 4-7) and Purvine Hall from April 4 to 5, 2005 (Figure 4-8). Flow measurements were made
by strapping the ultrasonic flow meter onto the entry piping in each building. The measurements
indicated that the total water usage at the Residence Hall was 14,456 gal with flowrates ranging from 0 to
156 gpm and averaging 19.4 gpm. The total water usage at Purvine Hall was 2,073 gal with flowrates
ranging from 0 to 62 gpm and averaging 8.4 gpm. Although these one-time measurements might not be
24
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Table 4-3. POE Locations and Estimated Flowrates at OIT
No.
1
2
3a
3b
4a
4b
4c
4d
5a
5b
6
7a
7b
8
9
Building Name
Residence hall
University Advancement
College Union South
College Union North
Snell Hall
Owens Hall
Semon Hall
Boivin Hall
Physical Education (PE)
Learning Resource Center
Purvine Hall
Cornett Hall South
Cornett Hall North
Facility Services
Stadium
Pipe Size
and
Material
4-in cast iron
NA
3-inPVC
4-in iron
1.5 -in copper
2-in copper
2-in copper
3 -in steel
2. 5 -in copper
3 -in copper
3 -in copper
1 -in/3 -in copper
2-in copper
2. 5 -in copper
NA
Pressure
after
Pressure
Reducing
Valves
(psi)
65
NA
72
76
62
65
75
60
68
70
60
65
NA
50
NA
Total (based on total fixture counts)
Peak Demand Based
on Fixture Count
(gpm)
Weber
Elliot
Engineers'3'
NA
NA
NA
NA
36
59
80
72
110
NA
57
85
33
41
310
Kinetico
NA
NA
NA
NA
33-63
58-83
95-120
70-95
100-125
NA
60-85
73-97
35-60
46-48
270
Design
Flowrate
Based on
Flow
Measurement
(gpm)(b)
60
1POU
60
1POU
1POU
N/A
N/A
1POU
1POU
30
N/A
1POU
1POU
NA
(a) From uniform plumbing code demand curves.
(b) Each POE system equipped with a 132-gal hydro tank.
N/A = not applicable/not available; POE = point of entry; POU = point of use; PVC = poly vinyl chloride
representative of the year-long use, they appeared to be more accurate than the estimates based on
building fixture counts provided by Weber Elliot Engineers and Kinetico. A decision was then made by
EPA to install three POE AM systems and eight POU AM units for this demonstration study. The size
and location of the POE systems are listed as follows:
• A 30-gpm ArsenXnp system in Purvine Hall
• A 60-gpm ARM 200 system in the Residence Hall
• A 60-gpm Adsorbsia™ GTO™ system in the College Union
Due to early arsenic breakthrough, ARM 200 media was changed out on two occasions with ARM 300
and E33-S. The eight Kinetico POU units were replaced with AdEdge POU units loaded with E33-S;
another 40 AdEdge POU units also were installed in various campus buildings.
4.2.2 Adsorptive Media. The three POE systems initially employed one of three adsorptive
media: (1) ArsenXnp, an iron-modified/resin-based media manufactured by Purolite; (2) ARM 200
(Ultrasorb-F as branded by Kinetico), an iron-based media manufactured by Engelhard Corporation; and
(3) Adsorbsia™ GTO™, a titanium dioxide-based media manufactured by Dow Chemical. The system
loaded with ARM 200 was rebedded with ARM 300, an iron-based media also manufactured by
Engelhard Corporation, and then E33-S, an iron-based media manufactured by Lanxess (formerly Bayer
AG). The eight POU units used ARM 200 media initially, but were replaced with AdEdge POU units
loaded with E33-S. All adsorptive media are listed by NSF International (NSF) under Standard 61 for use
in drinking water, and their physical and chemical properties are summarized in Table 4-4. More detailed
descriptions of the media are provided below.
25
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Residence Hall 24-Hour Realtime Flowrate Measurement
(15:00 3/28/05-15:00 3/29/05)
180
160
^ 140
a.
O
0)
•4-1
2
o
3/28/05 14:24 3/28/05 19:12 3/29/05 0:00 3/29/05 4:48 3/29/05 9:36 3/29/05 14:24
Time
Figure 4-7. Twenty-Four-Hour Real-Time Flowrate Measurements at Residence Hall
Purvine Hall Realtime Flowrate Measurement
(04/04/05 11:00 AM-04/05/05 11:00 AM)
4/4/0510:04 4/4/0516:04 4/4/0522:04 4/5/054:04 4/5/0510:04
Figure 4-8. Twenty-Four-Hour Real-Time Flowrate Measurements at Purvine Hall
26
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Table 4-4. Adsorptive Media Properties
Property
ArsenXnp(a)
Adsorbsia™
GTO™(b)
ARM 200(c)
ARM300(C)
E33-S(d)
Physical Property
Color
Matrix
Physical Form
Color
Bulk Density (g/cm3)
Bulk Density (Ib/fV)
BET Surface Area ( m2/g)
Pore Volume (mL/g)
Moisture Content (% by wt.)
Particle Size
(U.S. standard mesh)
Attrition (%)
Crystal Size (A)
Crystal Phase
Brown
Macro-porous
polystyrene/
divinylbenzene
Uniform
spherical
Beads
Reddish Brown
0.79-0.84
49-52
NA
NA
55-60
16 x50
NA
NA
NA
White
Nano-
crystalline
Titanium
oxide
Dry
granules
White
0.8
50
200-300
0.20-0.25
<15
10 x60
NA
NA
NA
Brown
Iron oxide/
hydroxide
Dry
granules
Dark Brown
0.72-0.80
45-50
225
NA
8
12 x40
<1
NA
NA
Brown
Iron oxide/
hydroxide
Dry
granules
Dark Brown
0.56
35-40
NA
NA
NA
12 x50
NA
NA
NA
Amber
Iron oxide
composite
Dry
granules/
pellets
Amber
0.47/0.56
28/35
120-200
NA
<15
10 x35
0.3
70
A-FeOOH
Chemical Property
Active Ingredient
Constituents
Titanium Dioxide (%)
Binder (%)
Metal Oxide (%)
pH Range
Hydrous iron
oxide
NA
NA
35-65
4-9
Titanium
dioxide
89.0-99.0
1.0-10.0
0.01-1.0
4-9
Iron oxide/
hydroxide
NA
NA
NA
5-6
Iron oxide/
hydroxide
NA
NA
NA
NA
Iron oxide
composite
0.11
NA
91.97
NA
(a) Provided by SolmeteX.
(b) Provided by Dow Chemical.
(c) Provided by Engelhard.
(d) Provided by Bayer AG.
BET = Brunauer, Emmett, and Teller; NA = not available
ArsenXnp. ArsenXnp media was developed by SolmeteX, Inc. and manufactured and distributed by
Purolite, Inc. under an exclusive license from Lehigh University. It has a base structure of macro-porous
polystyrene/divinylbenzene impregnated with nanoparticles containing hydrous iron oxide functional
groups. The media adsorbs both As(V) and As(III), with a higher capacity for As(V). It also removes
other contaminants, such as vanadium, molybdenum, chromium, and uranium. The media has good
mechanical strength and attrition resistance and does not generate fines during long-term vessel operation.
The media can handle water with a pH range from 4 to 9. ArsenXnp media can be regenerated multiple
times with a dilute caustic NaOH/NaCl solution. However, media regeneration and reuse were not
planned for the OIT site.
ARM 200 and ARM 300 Media. Developed by Engelhard Corporation, ARM 200 media is a granular
iron oxide/hydroxide media designed to remove dissolved arsenic from drinking water supplies via
adsorption onto its surface. Kinetico marketed the media as Ultrasorb-F. ARM 200 adsorbs both
As(V) and As(III) in a pH range from 5 to 9. The media is less effective for As(III) and at the upper
27
-------
end of the pH range. ARM 300 media is similar to ARM 200, but has a lighter bulk density (i.e., 35 to
40 vs. 45 to 50 lb/ft3) and somewhat broader size distribution (12 x 50 vs. 12 x 40 U.S. standard mesh).
Adsorbsia™ GTO™ Media. Adsorbsia™ GTO™ is a white, free-flowing granular titanium oxide-based
media manufactured by Dow Chemical. The media is capable of adsorbing both As(V) and As(III), with
a higher capacity for As(V). It adsorbs arsenic at a pH range of 6.5 to 8.5, but the adsorption is less
effective at the upper end of the range. According to the vender, the media's capacity for arsenic may be
independent of anion ions such as sulfate, phosphate, and vanadium. However, the presence of silica can
reduce arsenic removal. Source water at OIT contained 30.3 to 34.2 mg/L of silica (as SiO2); its impact
on arsenic adsorption was closely monitored. Adsorbsia™ GTO™ cannot be regenerated.
E33-S. Bayoxide E33-S media (branded as AD-33 by AdEdge), is an iron-based AM developed by
Lanxess (formerly Bayer AG) for the removal of arsenic from drinking water supplies. The media is
available in both granular and pelletized forms and delivered in a dry, crystalline form. The pelletized
media is 25% denser than its granular counterpart (i.e., 35 vs. 28 lb/ft3).
4.2.3 Treatment Process Description
4.2.3.1 Key Process Steps/System Components. The major process steps and system components of
the water system at OIT are discussed as follows:
• Intake. Raw water was supplied by two wells, with Well No. 1 being the primary well and
Well No. 4 being the backup well. Based on the water meter at the Well No. 1 pump head,
the total water consumption during the first year of performance evaluation study was
approximately 55,085,000 gal, compared to the 8,184,000 gal of water treated by the three
POE systems combined. The majority of water consumption on campus was for irrigation.
• Prechlorination. The pre-existing wellhead chlorination system was used to disinfect water.
Gas chlorine was used to maintain a target free chlorine residual level of 0.35 to 0.4 mg/L (as
C12). Chlorine gas cylinders (150 Ib) were kept in a room partitioned from the rest of the Well
1 pump house. The chlorine gas feed rate was regulated at 2.4 Ib/day using a panel-mounted
VI00 chlorinator (Wallace & Tiernan). A dual-cylinder scale was used to monitor the
chlorine gas consumption. Chlorine gas was injected to a side stream where an injector was
used to create a venturi effect to mix chlorine gas with carrier water. Chlorinated water then
was blended with source water prior to entering a 250,000-gal aboveground storage tank.
• Water storage. Chlorinated water was temporarily stored in the existing 250,000-gal
aboveground storage tank located on a hill near the Well No. 1 pump house before being
distributed to the campus.
• Distribution main and entry piping. The distribution main delivered water by gravity from
the storage tank to the 13 buildings on campus. Upon entering a building, the system pressure
was reduced to between 50 to 76 psi using pressure reducing valves (see Table 4-1). The inlet
piping to Purvine Hall, the Residence Hall, and the College Union consisted of 3-in copper, 4-
in copper, and 3-in copper, respectively, which was plumbed separately to the 30- gpm
ArsenXnp, 60 gpm ARM 200, and 60-gpm Adsorbsia™ GTO™ systems. Figure 4-9 shows
the inlet and exit piping to and from the 30-gpm ArsenXnp system at Purvine Hall.
28
-------
Figure 4-9. Inlet and Exit Piping to ArsenXnp System in Purvine Hall
POE/POU adsorptive media systems. The POE treatment systems and POU units are
discussed in detail in Sections 4.2.3.2 and 4.2.3.3, respectively.
Hydropneumatic tank. A 132-gal hydropneumatic tank (Amtrol Model WX-450-C) was
installed downstream of each POE treatment system to meet demand and provide water for
backwashing. The 24-in x 865/8-in tank had a steel shell coated with blue enamel paint on top
of red oxide primer and an inner bladder constructed of heavy duty butyl rubber. The tank
was pre-charged at the factory with air at 25 psi, a pressure lower than the inlet piping
pressure (i.e., the pressure after the respective pressure reducing valve).
Building distribution system. The effluent piping from each POE system and
hydropneumatic tank was tied into the exit piping to provide treated water to the distribution
system inside each building.
29
-------
4.2.3.2 POE Treatment Systems. All three POE arsenic removal systems are fixed-bed adsorption
systems, each consisting of one or two parallel treatment trains. Each treatment train consisted of two
adsorption vessels configured in series.
For series operation, the media in the lead vessel is removed and disposed of when it completely exhausts
its capacity or when the effluent from the lag vessel reaches 10 (ig/L of arsenic. Upon rebedding, the lead
vessel is switched to the lag position and the lag vessel is switched to the lead position. In general, the
series operation better utilizes the media capacity when compared to parallel operation because the lead
vessel may be allowed to exhaust completely prior to changeout.
When comparing the performance of the lead vessel (series operation) with that of two smaller in-parallel
vessels of a similarly-sized system (parallel operation), the number of BV treated by the system is
calculated based on the media volume in the lead vessel for the series operation and in both vessels for the
parallel operation. The calculation does not use the media volume in the lead and lag vessels because this
approach considers the two vessels as one large vessel, which has twice as much media than the in-
parallel system. The media volume in the lead vessel is equal to the sum of the media volume in each of
the two vessels in parallel; the flow through the lead vessel is equal to the sum of the flow through each of
the two vessels in parallel; and the empty bed contact time (EBCT) in the lead vessel is the same as the
EBCT in each of the two vessels in parallel. BV following the lag vessel were calculated based on the
combined media volume in both the lead and lag vessels.
ArsenX"p System. The ArsenXnp system installed in Purvine Hall had two parallel treatment trains, each
consisting of two pressure vessels configured in series. The process equipment included four 18-in x 65-
in vessels and associated piping/valves, sample ports, and pressure and flow instrumentation. Rated at
150 psi working pressure, the pressure vessels featured a fiber reinforced plastic (FRP) outer shell and
polyethylene inner shell. Each vessel had a 6-in top and bottom flange opening and was equipped with a
diffuser-style upper distributor and a hub and lateral-style lower distributor.
The system performance was monitored by inlet and outlet pressure, pressure differential across each
vessel, treated water flowrate and volume through each train, and wastewater flowrate and volume during
backwash. The flowrate was monitored through an inline vertical rotameter with a polysulphone tube
housing. The volume of treated water or backwash wastewater was measured using an Amco Bronze
water meter (Model C-700-1.5). The system also featured schedule 80 PVC solvent bonded plumbing,
valves, and sampling ports. The wall-mounted, pre-plumed plumbing was l!/2-in in diameter, which inter-
connected various system components. The piping size at the tie-in point to the water inlet, outlet, and
sewer were 3, 3, and l!/2-in, respectively. Figure 4-10 shows the wall-mounted plumbing and pressure
and flow instrumentation.
The treatment system was an on-demand system and the flowrate and volume of water treated were based
on user consumption. Each treatment train was equipped with a 15-gpm flow-limiting device to prevent
overrun. Thus, actual flowrates through each treatment train could range from 0 to 15 gpm based on
demand. The system was manually operated and there was no electrical connection associated with the
system. All flow meters and pressure gauges were mechanical and all valves were manual.
Table 4-5 presents the system's design specifications. Each tank was filled with 5 ft3 of ArsenXnp media
without underbedding support. At the design flowrate of 30 gpm, it yielded a hydraulic loading rate of
8.5 gpm/ft2 and an EBCT of 2.5 min/vessel. However, actual hydraulic loading rates and EBCTs could
vary significantly because this was an on-demand system. The working capacity as projected by the
vendor was 52,750 BV, which is equivalent to 3,945,700 gal of water treated (1 BV = 5 ft3 = 37.4
gal/train or 74.8 gal for both trains). Based on a daily use rate of 2,000 gal from the 24-hr real-time flow
measurement performed on April 4 and 5, 2005 (see section 4.1), arsenic breakthrough at 10 ug/L
30
-------
Figure 4-10. Wall-mounted Plumbing and Pressure and Flow
Instrumentation for ArsenXnp System in Purvine Hall
following the lead vessels would occur after 65 months of system operation. During the system
performance evaluation study, the vessels were not rebedded as arsenic concentrations from the lag
vessels were <1.0 (ig/L.
Media backwash was an entirely manual process, involving physically opening and closing 2-in ball
valves. The vendor recommended that the treatment system be backwashed on a regular basis to remove
particulate accumulating in the media beds. Backwash can be initiated when the differential pressure
(Ap) of any tank is 10 psi greater than that of a clean bed, after processing 10,000 BV of water, or after 60
days of operation. Each train in parallel can be backwashed independently or together. A manual valve
on the treated water line of each train (HV-7 for Train 1 and HV-20 for Train 2) was closed to isolate the
train for backwash; the other train continued to treat water and meet the demand along with the
hydropneumatic tank. Further, only one vessel in a train was backwashed at a time while the other vessel
in that train continued to treat water. The recommended backwash flowrate was 12 gpm, equivalent to a
hydraulic loading rate of 6.8 gpm/ft2. The backwash flowrate was monitored through the rotameter on the
wastewater outlet and adjusted using the metering valve on the wastewater discharge line. The flowrate
should be reduced if full-sized media granules were observed to escape the vessels. At a recommended
31
-------
Table 4-5. Design of 30-gpm ArsenXnp Adsorptive Media System
Parameter
Value
Remarks
Adsorption Vessels
Vessel Size (in)
Cross-Sectional Area (ft2/vessel)
No. of Vessels
Configuration
Media Type
Media Volume (ft3/vessel)
Media Bed Depth (in)
18 D x65H
1.8
4
2 parallel trains,
each with 2 vessels in series
ArsenXnp
5
34
-
-
-
Vessel B 1 and B2 in lead position;
Vessel Al and A2 in lag position
-
10 ft3 in both lead vessels; 20 ft3 total
-
Service Mode
Design Flowrate (gpm)
Hydraulic Loading Rate (gpni/ft2)
EBCT (min/vessel)
Estimated Working Capacity (BV)
Estimated throughput to 10 ug/L
Arsenic Breakthrough Following
Lead Vessel (gal)
Average Use Rate (gal/day)
Estimated Media Life (month)
30
8.5
2.5
52,750
3,945,700
2,000
65
15 gpm per train
Based on 15-gpm flowrate per lead/lag
train
Based on 15-gpm flowrate per lead/lag
train; 5 min EBCT per train
To 10 ug/L Arsenic Breakthrough
from Lead Vessel
1 BV = 5 fVVtrain = 37.4 gal/train or
74.8 gal for both trains
Based on 24-hr real time flowrate
measurement at Purvine Hall during
04/04/05-04/05/05
Estimated frequency of media change-
out in lead vessels based on average
use rate
Backwash Mode
Backwash Frequency
Backwash Duration (min/vessel)
Backwash Flowrate (gpm)
Hydraulic Loading Rate (gpm/ft2)
Wastewater Production (gal)
Every 60 days
12
12
6.8
576
Backwash conducted only once during
system performance evaluation
-
-
-
-
backwash duration of 12 min for each vessel, approximately 144 gal of backwash wastewater would be
produced during each vessel backwash. A total of 576 gal of wastewater would be discharged to the
sanitary sewer during each backwash event. During the system performance evaluation, the vessels were
backwashedonce.
ARM 200 System. The ARM 200 system installed in the Residence Hall consisted of two 36-in x 72-in
vessels configured in series. Each vessel had a 6-in top and a 6-in bottom flange opening and was
equipped with a diffuser-style upper distributor and a hub and lateral-style lower distributor. The pressure
vessels were constructed of FRP and rated at 150 psi working pressure. The vessels were bolted to the
concrete floor. The piping size was 2-in within the system, 4-in at the system inlet and outlet tie-ins, and
2-in at the tie-in to the sewer. Similar to the ArsenXnp system, flowrates were monitored through inline
vertical rotameters and volumes of treated water and backwash wastewater were measured using Amco
Bronze water meters (Model C-700-2). Figure 4-11 presents a photograph of the ARM 200 system.
32
-------
Figure 4-11. ARM 200 System in Residence Hall
Table 4-6 presents key design features of the system. At the start of the study, each vessel was loaded
with 20 ft3 of ARM 200 media with no underbedding media support. The system was operated on-
demand with a minimum combined EBCT of 2.5 min and a maximum hydraulic loading rate of
8.5 gpm/ft2, both based on a design flowrate of 60 gpm. Switching of the lead and lag vessel positions
was controlled by a series of 2-in PVC ball valves.
The working capacity estimated by the vendor was 62,600 BV (or approximately 9,365,000 gal of water
[1 BV = 20 ft3 = 149.6 gal in lead vessel]). Based on a daily use rate of 15,000 gal (from the 24-hr real
time flow measurement performed prior to the demonstration study [see section 4.2]), arsenic
breakthrough at 10 (ig/L following the lead vessel would occur after approximately 21 months of system
operation.
Due to unexpectedly rapid arsenic breakthrough from the adsorption vessels, ARM 200 media in the lead
vessel was rebedded with ARM 300 and the newly rebedded lead vessel was placed in the lag position.
Both the lead and lag vessel were rebedded with E33-S media due to a short run length again. The short
run length observed is discussed in detail in Section 4.5.2.2.
Manual backwash was recommended by the vendor to remove particulate using water in the
hydropneumatic tank. The backwash triggers were the same as those used by the ArsenXnp system. Only
one vessel was backwashed at a time while the other vessel continued to treat water used for backwash.
The recommended backwash flowrate was 50 gpm (or 7.0 gpm/ft2) and the recommended backwash
duration was 12 min for each vessel. Therefore, approximately 600 gal of backwash wastewater would be
33
-------
Table 4-6. Design of 60-gpm ARM200 and Adsorbsia™ GTO™ Adsorptive Media Systems
Parameter
Value
Remarks
Adsorption Vessels
Vessel Size (in)
Cross-Sectional Area (ft2/vessel)
No. of Vessels
Configuration
36 D x 72 H
7.1
2
in series
-
-
-
Vessel B in lead position for
ARM 200 system;
Vessel A in lead position for
Adsorbsia™ GTO™ system
ARM 200 Adsorptive Media
Media Quantity (Ib)
Media Volume (ft3/vessel)
Media Bed Depth (in)
1,800-2,000
20
34
Data source: Engelhard
40 ft3 total
-
Adsorbsia™ GTO™ Adsorptive Media
Media Quantity (Ib)
Media Volume (ft3/vessel)
Media Bed Depth (in)
1,760
20
34
Data source: Dow Chemicals
40 ft3 total
-
Service Mode
Design Flowrate (gpm)
Hydraulic Loading Rate (gpm/ft2)
EBCT (min)
Estimated Working Capacity
(BV)
Throughput to 10 ug/L Arsenic
Breakthrough Following Lead
Vessel (gal)
Average Use Rate (gal/day)
Estimated Media Life (months)
60
8.5
2.5
62,600 (ARM 200)
60,150 (Adsorbsia™ GTO™)
9,364,960 (ARM 200)
8,998,440 (Adsorbsia™ GTO™)
15,000
21 (ARM 200)
20 (Adsorbsia™ GTO™)
-
Based on design flowrate of 60
gpm
Based on 60 gpm design flowrate;
5 min total EBCT for both vessels
To 10 ug/L arsenic breakthrough
following lead vessel
1 BV = 20 ft3 = 149.6 gal in lead
vessel
Based on 24-hr real time flowrate
measurement at Residence Hall
on 03/28/05 and 03/29/05
Estimated frequency of media
changeout in lead vessel based on
average use rate
Backwash Mode
Backwash Frequency
Backwash Flowrate (gpm)
Backwash Duration (min/vessel)
Hydraulic Loading Rate (gpm/ft2)
Wastewater Production (gallons)
Every 60 days of operation
50
12
7.0
1,200
-
-
-
-
-
produced during backwash of each vessel. A total of 1,200 gal of wastewater would be produced from
backwashing both vessels.
Adsorbsia™ GTO™ System. The 60-gpm system at the College Union was designed and built in the
same fashion as the system in the Residence Hall. The only difference was that it was used to evaluate a
different type of media (i.e., Adsorbsia™ GTO™). Based on the vendor-estimated working capacity and
a daily use rate of 15,000 gal, the media would last for 20 months, after treating approximately 8,998,400
gal of water (1 BV = 20 ft3 = 149.6 gal in the lead vessel). The system was backwashed in a similar
34
-------
Figure 4-12. Adsorbsia™ GTO™ System in College Union
manner as the 60-gpm ARM 200 system at the Residence Hall. Table 4-6 summarizes the system design
specifications. Figure 4-12 presents a photograph of the system.
4.2.3.3 POU Units. Each Kinetico POU unit used a single cartridge to house 600 mL of ARM 200
media for arsenic removal. The cartridge housing had exterior dimensions of 70 mm x 320 mm and %-in
female National Pipe Thread (NPT) threads for direct connections to an incoming cold water line and an
exit line. Treated water was delivered from the exit line to a separately installed faucet. The POU units
were installed either under a sink or inside a drinking water fountain as shown in Figure 4-13.
As untreated water flowed into the feed water inlet, it was allowed to past a turbine, which was connected
to a gear to gradually close a measured shut-off assembly. An indicator on the outside of the filter head
showed the relative remaining cartridge capacity, based on a maximum capacity of 500 gal. When 500
gal of water was processed, the measured shut-off assembly was completely closed, preventing any more
water from passing through the cartridge. Eight POU systems were installed in eight buildings on campus
as summarized in Table 4-7.
35
-------
Figure 4-13. POU Systems Installed Under a Sink (top) and Inside a Drinking
Water Fountain (bottom)
36
-------
Table 4-7. Kinetico POU System Locations (2006-2008)
Building Name
University Advancement
Snell Hall
Owens Hall
Learning Resource Center
Physical Education
Facility Services
Cornett South
Stadium
Location
Sink in the break room
Drinking Fountain
Drinking Fountain
Drinking Fountain
Drinking Fountain
Drinking Fountain
Drinking Fountain
Drinking Fountain
About 11 months into the performance evaluation study, OIT began to replace the Kinetico ARM 200
POU units with AdEdge E33-S POU units. On November 15, 2007, May 25, 2008, and August 15, 2008,
AdEdge POU units were installed at the University Advancement, Cornett Hall, and the Facility Services
building, respectively. Overall, OIT replaced the eight Kinetico units with AdEdge units and installed 40
additional units.
The AdEdge POU units were comprised of a polypropylene housing. They had a 3/s-in inlet and a %-in
outlet. The approximate flowrate with a system inlet pressure of 60 psi was 1 gpm. The working
pressure ranged from 20 to 125 psi. The unit had a height of 13 in and a diameter of 6.75 in. Figure 4-14
shows the AdEdge housing and filter cartridge. Table 4-8 summarizes design specifications of the
Kinetico and AdEdge POU units.
o-rln
BlueAirvent
small o-rings
washer
^.As-08 05/25/08
ART 742 GALLONS
Figure 4-14. AdEdge POU Housing and Cartridge
37
-------
Table 4-8. Design Specifications of Kinetico and AdEdge POU Units
Parameter
Housing Material
Cartridge Dimensions (mm)
Housing Dimensions
Height (mm)
Width (mm)
Diameter (mm)
Unit Weight (Ib)
Media Type
Media Volume (mL)
Inlet Connection
Outlet Connection
Paniculate Retention (um)
Water Pressure (psi)
Flowrate (gpm)
Treatment Capacity (gal)
Kinetico Unit
Polypropylene
54 x 265
(Slightly tapered)
-
425
150
100
11
ARM 200
600
!/4-in Female NPT
!/4-in Female NPT
5.0
20-120
0.7-1.0
490
AdEdge Unit
Polypropylene
—
-
330
-
171
4
E33-S
-
3/8in
!/4in
0.5
30-125
1.0@60psi
-
4.3
Treatment System Installation
This section provides a summary of system installation, startup, and shakedown activities and the
associated prerequisites including permitting and building preparation.
4.3.1 System Permitting. Engineering plans for the system permit application were prepared by
Weber Elliott Engineers, a Kinetico subcontractor (also serving as the engineer for OIT) located in
Eugene, OR. The plans included diagrams and specifications of the three POE systems and eight POU
units, as well as drawings detailing the connections of the new systems/units to the tie-ins in each
building. The engineering package was certified by a Professional Engineer registered in the State of
Oregon and submitted to Oregon DHS for review and approval on October 13, 2005. The permit was
issued by Oregon DHS on October 31, 2005, and was received by Battelle on November 1, 2005.
4.3.2 Building Construction. The three POE systems were placed into the existing mechanical or
storage room of each building. Necessary arrangements were made to accommodate the treatment
systems and pipe/conduit supports were hung from the ceiling and/or attached to the walls. Plumbing was
modified to provide connections from the new treatment systems to the building distribution entry points
and sewer system. In particular, the two connections (i.e., south and north) to the campus water
distribution network in the College Union were combined for a single inlet tie-in to the Adsorbsia™
GTO™ system in that building.
4.3.3 System Installation, Startup, and Shakedown. The treatment systems arrived at OIT on
October 28, 2005. Quality Water Systems, a local subcontractor to Kinetico, performed off-loading and
installation of the systems. The installation activities, which lasted about one week, included placing the
POE systems and 132-gal hydropneumatic tanks in each of the three buildings and connecting system
piping at the tie-in points.
Upon completion of system installation, JOB Consulting, a subcontractor to Kinetico, traveled to the site
on December 5 through 10, 2005, to perform system inspections, hydraulic testing, and media loading.
Before media loading, empty vessels were hydraulically tested to check pressure loss at normal flowrates
and observe the flow patterns for uniformity. The media were then loaded separately through the 6-in
38
-------
flange openings on top of the vessels. No underbedding media support was used for any of the vessels.
Figure 4-15 shows loading of media into one of the vessels in the Residence Hall. After media loading,
the vessels were backwashed one at a time to remove media fines. For the 30-gpm ArsenXnp system in
the Purvine Hall and the 60-gpm ARM 200 system in the Residence Hall, backwash wastewater ran clear
within a few BV. The Adsorbsia™ GTO™ media in the College Union, however, would not run clear.
Figure 4-15. Media Loading into an Adsorption Vessel
Freeboard measurements for the ArsenXnp and ARM 200 systems were taken after media backwash and
the results are summarized in Table 4-9. Freeboards were measured from the top of the flange to the top
of the media beds. For the ArsenXnp system, 31.0 to 33.3 in freeboards were measured; these freeboard
measurements resulted in a bed depth of 36.7 to 39.0 in. (Note that bed depths were measured by
subtracting the freeboard from the distance from the bottom of the tank to the top of the flange [i.e., 70
in].) Measurements for the bed depth appeared to be inflated when compared with the design value of 34
in (see Table 4-5). This was caused by the displacement of media by the lower distributor at the bottom
of each vessel. The ARM 200 system had a bed depth of 48.5 to 50.0 in, compared to the design value of
34 in (see Table 4-6). The higher actual bed depth values were caused, again, by the displacement of
media by the laterals at the bottom of each vessel. Note that both ArsenXnp and ARM 200 media were
loaded directly into the adsorption vessels without the use of any underbedding support. Because of
issues related to backwashing of Adsorbsia™ GTO™ media, the freeboard measurements and resulting
bed depths obtained during the initial media loading were not considered valid.
After the freeboard measurements, the vendor inspected the systems for leaks, tested individual vessels
and treatment trains for balanced flows, and sanitized the systems with a strong NaOCl solution to a
minimum chlorine residual of 40 mg/L (as C12). By late afternoon on December 10, 2005, the three POE
systems were put online for a test run over the weekend. On the following Monday, "milky" water was
found in the Adsorbsia™ GTO™ system effluent and the system was immediately taken offline. The
39
-------
Table 4-9. Freeboard Measurements and Media Bed Depths for ArsenXnp and ARM 200 Systems
Location
Purvine
Hall(b)
Residence
Hall(c)
Media
Loading
Date
12/20/05
12/20/05
01/24/07
10/03/07
Media
Volume
ft3
5.0
5.0
5.0
5.0
20.0
20.0
20.0
20.0
20.0
Media
Type
ArsenXnp
ARM 200
ARM 300
E33-S
Media
Vessels
TB1 (Lead)
TAl(Lag)
TB2 (Lead)
TA2 (Lag)
B (Lead)
A (Lag)
B (Lag)
A (Lead)
B (Lag)
Freeboard
at Initial
Loading'3'
(in)
31.5
31.3
31.0
33.3
26.0
27.5
27.0
NA
NA
Under-
bedding
Depth
(in)
None
None
None
None
None
None
None
None
None
Bed
Depth
(in)
38.5(d)
38.7(d)
39.0(d)
36.7(d)
50.0(d)
48.5(d)
49.0(d)
NA
NA
Freeboard
at
Removal
(in)
-
-
-
-
25.8
NA
NA
NA
NA
(a) Freeboard measured from surface of media bed to top of flange.
(b) For 30 gpm system, tank height was 65 in; distance from bottom of tank to top
(c) For 60 gpm system, tank height was 72 in; distance from bottom of tank to top
(d) Calculated bed depth appeared inflated due to displacement of media by lateral
NA = not available
of flange was 70 in.
of flange was 76 in.
at bottom of tank.
other two POE systems continued to be online and the performance evaluation of these systems officially
began on December 12, 2005.
After discussing the milky white effluent issue with the media manufacturer, Dow Chemical, Kinetico
informed Battelle that Dow Chemical's decision was to rebed the vessels (thinking that the media could
have come from "a bad batch"). Dow Chemical also requested that a garnet underbedding support be
provided in the vessels before rebedding (thinking that the media could have leaked through the bottom
laterals).
According to Kinetico, an underbedding support should have particle sizes between 8 and 50 mesh and a
density over 75 lb/ft3. The underbedding support also should be installed to a depth about 1 to 2 in above
the bottom laterals. On January 5, 2006, Dow Chemical visited OIT to rebed the vessels at the College
Union. Prior to rebedding, the previously installed Adsorbsia™ GTO™ media was vacuumed out of the
two vessels and sent to a local landfill for disposal. The acceptance of the waste was based on Dow
Chemical's TCLP and California Waste Extraction Test (WET) test results using challenge water. Figure
4-16 shows the Adsorbsia™ GTO™ media after being removed from the adsorption vessels.
Before media loading, 30 x 40 mesh garnet was installed to provide media support in both vessels.
Following media loading, the lead vessel (Vessel A) was backwashed at 30 gpm for 4 hr and 8.8 gpm for
2 hr for a total of 55 BV (see Table 4-10). The bed expansion at 30 gpm was roughly 25%.
Approximately 3.5 ft3 of media (or 17% of the total bed volume) was lost even though the bed expansion
was much less than the 66% projected expansion before any media was lost. Non-uniform flow was
suggested by Dow Chemical as a possible cause for the media loss. The lag vessel (Vessel B) was
backwashed the next day at 20 gpm for 1.5 hr before it was terminated due to concerns over high pressure
drop (twice the projected value) across Vessel A in the service mode (Vessel A was in the service mode
when Vessel B was being backwashed). The backwash wastewater appeared turbid from both vessels.
The system remained offline.
40
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Figure 4-16. Adsorbsia™ GTO™ Taken Out of Adsorption Vessels
Table 4-10. Adsorbsia™ GTO™ Media Backwash During Rebedding
Date
01/05/06
02/17/06
Sum
Tank A
Flowrate
(gpm)
30/8.8
55-60
-
Throughput
(BV)
48/7
60
115
Media
Loss
(ft3)
3.5
0.5
4.0
TankB
Flowrate
(gpm)
20
55-62
-
Throughput
(BV)
12
96
108
Media
Loss
(ft3)
-
0.5
0.5
Two Battelle staff members traveled to Klamath Falls, OR to conduct system inspections and provide
operator training on data and sample collection on January 10 and 11, 2006. During the visit, Battelle
collected effluent samples from the newly rebedded Adsorbsia™ GTO™ system at four different service
flowrates, i.e., 5, 30, 45, and 60 gpm. As shown in Figure 4-17, the effluent samples became cloudier as
system flowrates increased incrementally from 30 to 60 gpm. Turbidity measurements also increased
correspondingly from 3 nephelometric turbidity unit (NTU) (at 45 gpm) to 64 NTU (at 60 gpm) (see
Table 4-11). Ap readings across both vessels increased significantly from 5 to 6 psi (at 45 gpm) to 8 to 11
psi (at 60 gpm), indicating that the media was not sufficiently cleaned of fines during the backwash
attempts on January 5 and 6, 2006. Backwashing the lead vessel was attempted using treated water from
the lag vessel at approximately 20 gpm. However, after about 1 min into the backwash, the backwash
effluent water turned milky and bulk media were seen entering the bottom of the backwash flowmeter
(Figure 4-18). The backwash attempt was terminated immediately.
41
-------
Figure 4-17. Effluent Samples from Rebedded Adsorbsia™ GTO™ System
at Different Service Flowrates
Table 4-11. Effluent Turbidity and Ap Readings from
Rebedded Adsorbsia™ GTO™ System
Flowrate
(gpm)
5
30
45
60
Turbidity
(NTU)
0
0
3
64
Ap Reading
(psi)
Vessel A
0
1
5
8
Vessel B
0
1
6
11
On February 17, 2006, Dow Chemical returned to the site to perform media backwash again. The visit
followed a media backwash pilot-scale study conducted at its Midland facilities in Michigan. The lead
vessel (Vessel A) was backwashed at 55 to 60 gpm (or 7.7 to 8.5 gpm/ft2) for 2.5 hr for atotal of 60 BV
(see Table 4-10). To achieve the target backwash flowrate of 60 gpm, the flowrate was slowly increased
over a few minutes. At this flowrate, bed expansions would range between 30 to 35%. The backwash
effluent showed signs of clearing, but maintained a cloudy appearance over the course of the backwash.
Following backwash, the lead vessel was put into the downflow service mode (to drain) at 60 gpm and the
effluent was visibly clear with the turbidity measured at <1 NTU after 10 min. Due to the various
episodes happening to Vessel A, approximately 4 ft3 of the media was lost from the vessel.
The lag vessel (Vessel B) was then backwashed at 55 to 62 gpm (7.7 to 8.7 gpm/ft2) for 4 hr for a total of
96 BV. A turbidity of <1 NTU was measured from the effluent after the lag vessel was put into service
42
-------
Figure 4-18. Bulk Media Entering Flow Meter (right) During Backwash Attempt
(to drain) at 60 gpm for 10 min. The amount of media lost from the vessel was 0.5 ft3, or 1 in of the
media bed. The pressure loss across the two vessels was 8 psi at a service flowrate of 60 gpm.
The system was then placed in the lead/lag position (inlet to Vessel A, to Vessel B, and then to the
distribution system) on February 17, 2006, and the performance evaluation study on the Adsorbsia™
GTO™ system officially began on the same day.
4.4
System Operation
4.4.1 Service Operation. Operational parameters of the treatment systems were tabulated and are
attached as Appendix A. Key parameters are summarized in Table 4-12, and discussed in detail below.
4.4.1.1 ArsenX"p System. The performance evaluation study on the ArsenXnp system in Purvine Hall
began on December 12, 2005, and ended on August 26, 2009. The system operated for a total of 1,353
days, treating 1,814,428 gal (or 24,254 BV) of water (1 BV = 5 ft3/train = 37.4 gal/train or 74.8 gal for
both trains; see arsenic breakthrough behavior in Section 4.5.2.1). Significantly imbalanced flow between
the two parallel trains was observed, with 878,214 gal treated by Train 1 and 936,214 gal treated by Train
2. More detailed discussions about this imbalanced flow are provided in Section 4.4.5.
During the first year of system operation, the average daily demand was 2,077 gal, very close to the
2,073 gal use rate measured during the 24-hr real-time flow measurement on April 4 and 5, 2005. The
daily demand dropped to 1,542 gal after 2 years of system operation. The average daily demand through
the entire study period was 1,341 gal. The higher daily demand during the first year of system operation
was due to a higher setting on a trap primer, a solenoid valve that discharged treated water to the drain to
prevent sewer gas from entering the building.
43
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Table 4-12. Operational Parameters of Treatment Systems
Parameter
Media Evaluated
Operating Period
Total Operating time (hr)
Total Operating Days (day)
Throughput (gal)
Average Daily Demand (gpd)
Range (Average) of Flowrates
(gpm)
Range (Average) of Hydraulic
Loading Rates (gpm/ft2)
Range (Average) of EBCT (min)
Range (Average) of System Inlet
Pressure (psi)
Range (Average) of System Outlet
Pressure (psi)
Range (Average) of Ap Readings
Across System (psi)
Range (Average) of Ap Readings
Across Each Vessel (psi)
Values
Purvine
Hall
System
ArsenXnp
12/12/05-
08/26/09
NAW
1,353
Train 1:
878,214
Train 2:
936,214
Combined:
1,814,428
1,341
1.0-27
(7.0)
0.3-7.5
(1.9)
2.8-74.8
(10.7)
45-67
(57.0)
40-65
(57.4)
0-11
0
Residence Hall
System
ARM 200
12/12/05-
01/22/07(a)
NA(b)
406
6,698,103
16,498
1.0-60
(20.0)
0.1-8.5
(2.8)
2.5-150
(7.5)
50-62
(58.5)
30-62
(54.9)
0-20
0
ARM 300
01/24/07-
07/09/07
NA(b)
166
5,325,660
32,082
14-58
(35.3)
2.0-8.2
(5.0)
2.6-10.7
(4.2)
40-62
(53.6)
28-61
(45.4)
0-20
0
E33-S
10/03/07-
08/26/09
NAlb)
693
12,170,210
17,562
1.0-60
(18.8)
0.1-8.5
(2.6)
2.5-150
(8.0)
50-62
(57.8)
32-62
(52.6)
0-18
0
College
Union
System
Adsorbsia™
GTO™
02/17/06-
08/26/09
NAW
1,286
5,889,749
4,580
1-34
(6.7)
0.1-4.8
(0.9)
3.5-120
(17.9)
55-64
(60.8)
28-64
(59.7)
0-32
0
(a) System went on being rebedded twice with ARM 300 and E33-S media.
(b) System on-demand; operating time not tracked.
Instantaneous on-demand flowrates to each of the parallel trains ranged from 0.5 to 15 gpm with
combined flowrates ranging from 1 to 27 gpm and averaging 7 gpm. At these flowrates, hydraulic
loading rates ranged from 0.3 to 7.5 gpm/ft2 and averaged 1.9 gpm/ft2, compared to the design value of
8.5 gpm/ft2. Based on the flowrates to the individual trains and system, EBCTs in each vessel varied
from 2.8 to 74.8 min (or 10.7 min on average).
Inlet pressure readings for Trains 1 and 2 ranged from 45 to 67 psi with both averaging 57.0 psi. Outlet
pressure readings for Trains 1 and 2 ranged from 40 to 65 psi with both averaging 57.4 psi. The Ap
across each adsorption vessel remained at 0 psi throughout the performance evaluation study.
4.4.1.2 ARM 200/ARM 300/E33-S System. The evaluation of ARM 200 media in the Residence
Hall began on December 12, 2005. In 406 days, the system treated 6,698,103 gal (or 44,767 BV) of
water. (Bed volumes were calculated based on 20 ft3 of media in the lead vessel; see Section 4.5.2.2 for
arsenic breakthrough.) The average daily demand was 16,498 gal, compared to the 14,456 gpd measured
during the 24-hr real-time flow measurement on March 28 and 29, 2005. Due to the on-demand system
configuration, the flowrates through the ARM 200 system ranged from 1 to 60 gpm and averaged 20.0
44
-------
gpm. Based on the flow to the system, EBCTs varied from 2.5 to 150 min ( 7.5 gpm [on average]);
hydraulic loading rates varied from 0.1 to 8.5 gpm/ft2 (2.8 gpm/ft2 [on average]).
Inlet pressure readings for the system ranged from 50 to 62 psi and averaged 58.5 psi; outlet pressure
readings ranged from 30 to 62 psi and averaged 54.9 psi. The average Ap across the system was 3.6 psi.
Pressure drops across each ARM 200 vessel were negligible.
The lead vessel (Vessel B) was rebedded with ARM 300 media on January 24, 2007, due to early arsenic
breakthrough from the lead and lag vessels (see Section 4.5.2.2). Upon rebedding, the vessel containing
ARM 300 was placed in the lag position and the vessel containing partially exhausted ARM 200 media in
the lead position. The ARM 200/ARM 300 test lasted from January 24, 2007, through July 9, 2007, with
the system treating 5,325,660 gal of water (or 35,595 BV). (Bed volumes, again, were calculated based
on 20 ft3 of media in the lead vessel; see discussions of arsenic breakthrough in Section 4.5.2.2) The
average daily demand was 32,082 gal, which was about twice the amount experienced previously during
the ARM 200 test run. A pipe break at the Residence Hall apparently contributed to the higher water
demand experienced during the ARM 200/ARM 300 test.
As expected, flowrates measured during the ARM 200/ARM 300 test run were higher than the ARM 200
test run, ranging from 14 to 58 gpm and averaging 35.3 gpm. Correspondingly, EBCTs were shorter
(ranging from 2.6 to 10.7 min and averaging 4.2 min) and hydraulic loading rates were higher (ranging
from 2.0 to 8.2 gpm/ft2 and averaging 5.0 gpm/ft2). Inlet and outlet pressure readings for the system
averaged 53.6 and 45.4 psi, respectively. The resulting pressure drop across the system was 8.2 psi (on
average), which is higher than that observed previously for the ARM 200 system. Pressure losses across
the vessels remained to be negligible, most likely due to errors associated with the pressure gauges.
On July 11, 2007, the system was placed in bypass as the system effluent had exceeded the arsenic MCL
in May 2007. On October 3, 2007, the lead and lag vessels were rebedded with E33-S media. The E33-S
test ran began on October 3, 2007, and ended on August 26, 2009. In 693 days, the system treated
approximately 12,170,210 gal of water (or 81,341 BV). The average daily demand was 17,562 gal, close
to that observed during the ARM 200 test run.
Operational parameters, including flowrates, EBCTs, hydraulic loading rates, system inlet/outlet pressure
and system differential pressure, measured during the E33-S test run were very close to those measured
during the ARM 200 test run.
4.4.1.3 Adsorbsia™ GTO™ System. Due to the difficulties encountered during the initial media
backwash, the Adsorbsia™ GTO™ system wasn't placed online until February 17, 2006. During the
1,286 days of system performance evaluation, the system treated 5,889,749 gal of water. This total
throughput corresponded to 49,212 BV based on 16 ft3 of media in the lead vessel (the lag vessel had 19.5
ft3 of media [see Table 4-12].) The average daily demand was 4,580 gal. The average daily demand
appeared to increase over time, with 3,776 gal treated, for example, during the first six months of system
operation and 5,162 gal treated during the last year of system operation.
The instantaneous flowrates ranged from 1 to 34 gpm and averaged 6.7 gpm. Because of the low
flowrates, EBCTs were long (ranging from 3.5 to 120 min and averaging 17.9 min) and hydraulic loading
rates were low (ranging from 0.1 to 4.8 gpm/ft2 and averaging 0.9 gpm/ft2). Inlet and outlet pressure
readings averaged 60.8 and 59.7 psi, respectively, resulting in only 1.1 psi pressure loss across the
system. Pressure drops across the vessels were 0 psi throughout the study.
4.4.2 Media Loading and Removal. After the initial media loading, only the ARM 200 system
was rebedded with its lead vessel replaced with ARM 300 media and then placed in the lag position. The
45
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ARM 200/ARM 300 system was then rebedded with E33-S media. Rebedding of the lead vessel with
ARM 300 media was performed by Kinetico's local subcontractor, Quality Water System. Before the
removal of spent media, the freeboard was measured as 25.8 in from the top of the flange to the media
surface, which was close to the freeboard (26 in) measured during initial media loading in December 2005.
Spent media samples were collected at the top, middle, and bottom sections of the media bed at depths of 0
to 4, 22 to 26, and 35 to 39 in., respectively. The vessel was rinsed and any remaining media removed
from the bottom of the vessel. The vessel was then half filled with water before virgin media was poured
through a large funnel from the top of the tank. After the vessel was completely filled with water and the
media was soaked for 1 hr, the vessel was backwashed with 1,440-gal of treated water from Vessel A.
After backwashing, freeboard measurements were taken, and the newly-rebedded Vessel B was placed in
the lag position. The freeboard was 27 in after ARM 300 media loading. On October 3, 2007, the ARM
200/ARM 300 media in the lead and lag vessels were rebedded with E33-S. The same local subcontractor
rebedded the vessels following the procedure used during the first media changeout.
4.4.3 Backwash Operation. Kinetico recommended that the three POE systems be backwashed
on a regular basis to remove particulates and media fines accumulating in the media beds. Backwash
could be initiated when the pressure differential of any tank was 10 psi greater than that of a clean tank,
after processing 10,000 BV of water, or after 60 days of operation. Due to negligible pressure drops
across adsorption vessels, the three POE systems were backwashed only once on May 16 or 17, 2006.
Table 4-13 summarizes backwash flowrates and durations and amounts of wastewater produced during
backwash of each of the POE systems. Backwash flowrates for the two 60-gpm systems ranged 8 to 40
gpm (or 1.1 to 5.7 gpm/ft2), which were significantly lower than the design value of 50 gpm (7.0 gpm/ft2).
The operator used lower backwash flowrates to avoid losing any media during backwash. When
backwashing Adsorbsia™ GTO™ media at 40 gpm, backwash wastewater looked slightly milky. After 4
min into backwash, the operator reduced the flowrate from 40 to 8 gpm.
Table 4-13. Summary of Backwash Flowrate and Duration
Vessel
Flowrate
(gpm)
Hydraulic
Loading
(gpm/ft2)
Duration
(min)
Wastewater
Produced at
Different
Flowrate
(gal)
Wastewater
Produced
from Each
Vessel
(gal)
ArsenX"p System
TB1 (lead)
TA1 (lag)
TB2 (lead)
TA2 (lag)
12
12
12
12
6.8
6.8
6.8
6.8
12
12
12
12
144
144
144
144
144
144
144
144
ARM 200 System
TB (lead)
TA (lag)
20
30
20
10
8
2.8
4.2
2.8
1.4
1.1
1
11
o
J
2
7
20
330
60
20
56
350
136
Adsorbsia™ GTO™ System
TA (lead)
TB (lag)
40
8
40
8
5.7
1.1
5.7
1.1
4
10
4
10
160
80
160
80
240
240
46
-------
4.4.4 Residual Management. Residuals produced by the operation included backwash water and
spent media. There was only one backwash event for each of the three POE systems during the system
performance evaluation. Approximately 1,540 gal of wastewater was generated, with 580, 480, and 480
gal from the ArsenXnp, ARM 200, and Adsorbsia™ GTO™ systems, respectively. The backwash
wastewater was discharged to the city sanitary sewer.
On January 24, 2007, approximately 20 ft3 of spent ARM 200 media in the lead vessel at the Residence
Hall was rebedded with ARM 300. The spent media passed TCLP tests (Section 4.5.8), and was disposed
of by Waste Management, Inc. On October 3, 2007, spent ARM 200 and ARM 300 in the lead and lag
vessels were rebedded with E33-S. The spent media was stored at OIT. In December 2009, the operator
sent an ARM 300 spent media sample to Battelle for TCLP analysis by Belmont Labs. The spent ARM
300 media passed the TCLP test.
4.4.5 System/Operation Reliability and Simplicity. During the system performance evaluation,
there were no major operational issues except for a few minor leaks, imbalanced flow from the parallel
treatment trains, and a malfunctioned totalizer. Water-dripping leaks were noticed at several union/valve
thread connections of the 30-gpm ArsenXnp system at Purvine Hall right after the system startup and were
repaired on February 28, 2006.
Imbalanced flow was observed between the two treatment trains of the ArsenXnp system, with each train
treating 878,214 and 936,214 gal of water. Before the flow restriction valve on each train was adjusted
on February 1, 2006, approximately 40% and 60% of the flow passed through Trains 1 and 2,
respectively. Following the adjustment, the flows through both trains were close with an average of
47.3% and 52.7% passing through Trains 1 and train 2, respectively.
A totalizer malfunction occurred on the Adsorbsia™ GTO™ system at the College Union on May 18,
2006. The flow totalizer (Kent positive displacement meter) installed on the treated water side of the 60-
gpm system failed to register any flow when the water flowrate was at or below 10 gpm. Clogging of the
meter with particles was thought to be the problem. The system was restarted in an attempt to flush away
any particles that might have been present; however, the problem persisted until the vendor replaced the
malfunctioned totalizer on July 18, 2006. During the period of totalizer malfunction, the average daily
flow rate calculated based on the meter reading was 2,108 gal, compared to 4,580 gal prior to the totalizer
malfunctioning. Because the number of consumers and their daily activities remained essentially
unchanged during these two periods, the 54% decrease in average daily usage was likely caused by the
malfunctioning totalizer. The average daily water usage of 4,580 gal also was supported by additional
data collected after replacement of the totalizer. As such, the treated water throughput during the period
from May 18 to July 18, 2005, was adjusted based on an average daily water usage of 4,580 gal.
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. There was no pre- or post-treatment required for
the systems. The pre-existing centralized chlorination system at the wellhead continued to be used for
disinfection purposes.
4.4.5.2 System Automation. The POE systems were designed for complete manual operation. There
was no electrical connection associated with the system; all flow meters and pressure gauges were
mechanical and all valves were manual. Pressure was the driving force for water flowing through the
treatment systems. During system backwash, manual valves had to be physically opened and closed to
change flow paths and adjust flowrates.
47
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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, and flowrate on field log sheets. The O&M of the POE systems required
minimal additional operator skills beyond those required for small system operators, such as a solid work
ethic, basic mathematical skills, ability to understand chemical properties, familiarity with electronic and
mechanical components, and ability to follow written and verbal instructions. Understanding of and
compliance with all occupational and chemical safety rules and regulations also were required. Since all
systems were of complete manual operation, the operator was required to understand system piping and
be able to follow the valve chart to operate the system under service and backwash modes after receiving
proper training by the vendor.
All Oregon public water systems, both community and non-transient non-community water systems, must
be under the supervision of a certified operator. The Oregon DHS Drinking Water Program classifies
water distribution systems and treatment plants into two types according to their complexity or size and
establishes minimum standards for personnel responsible for operating these systems. Systems with 149
and fewer connections, either using groundwater as their only source or purchasing all their water from
another public water system without adding any additional treatment, require an "S" certification; those
with 150 or more connections require certification at "Levels 1 to 4" for treatment and/or distribution.
The operators of systems with "S" certification are required to attend a small water system training course
once every three years and submit a new Small Water System Operator Application with proof of training
attendance. The OIT Water System is classified as an "S" system and the plant operator attends a training
course once every three years to be qualified as a small water system operator.
4.4.5.4 Preventive Maintenance Activities. Preventive maintenance tasks recommended by the
vendor included daily to monthly visual inspection of the piping, valves, tanks, flow meters, pressure
gauges, and other system components. Chlorine residual across the treatment train also was checked on a
regular basis using a Hach colorimeter, even though the addition of chlorine was only for disinfection
purposes, and not required by the systems.
4.4.5.5 Chemical Handling and Inventory Requirements. No chemicals were required for the
system operation.
4.5 System Performance
Performance of the three POE systems was evaluated based on analyses of water samples collected across
the treatment trains, from the media backwash, and from the distribution system. The three POU units
were evaluated by collecting effluent water samples for arsenic analysis. The performance evaluation
studies began on December 12, 2005, for the ArsenXnp system in Purvine Hall and the ARM 200 system
in the Residence Hall, and on February 17, 2006, for the Adsorbsia™ GTO™ system at the College
Union. The evaluations for all three POE systems were completed on August 26, 2009.
For the ArsenXnp system in Purvine Hall, water samples were collected at six locations: IN, TB1, TA1,
TB2, TA2, and TT (with Vessels TB1 and TB2 at the lead position). Sampling was conducted on 36
occasions (including three duplicate sampling events) with field speciation performed at IN and TT for
eight of the 36 occasions.
Sampling in the Residence Hall was conducted on 28 occasions (including three duplicate sampling
events) during the ARM 200 test from January 11, 2006, through January 10, 2007, with field speciation
performed for eight of the 28 occasions. On January 24, 2007, ARM 200 media in the lead vessel (Vessel
B) was replaced with ARM 300 and the newly-rebedded vessel was placed in the lag position. Sampling
was conducted on five occasions for the ARM 200/ARM 300 test from February 7, 2007, through June 1,
48
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2007, with no field speciation performed during the test. On July 11, 2007, the system was placed in
bypass until media rebedding. On October 3, 2007, ARM 200 and ARM 300 media in the lead (Vessel
A) and lag vessels (Vessel B) were replaced with E33-S. Sampling was conducted on eight occasions
from December 18, 2007, through August 26, 2009, with no field speciation performed. Water samples
were collected at IN, TB, and TA for all sampling events.
The late system startup for the Adsorbsia™ GTO™ system at the College Union did not limit the number
of sampling events during the system performance evaluation study. Sampling was conducted on 32
occasions (including three duplicate sampling events) from March 1, 2006, through August 26, 2009,
with field speciation performed on seven of the 32 occasions. Water samples were collected at the
wellhead and following Vessels A and B at IN, TA, and TB for all sampling events.
Tables 4-14 through 4-16 summarize arsenic, iron, manganese, and/or titanium analytical results for the
ArsenXnp, ARM 200/ARM 300/E33-S, and Adsorbsia™ GTO™ systems, respectively. Tables 4-17
through 4-19 summarize other water quality parameter results for the three systems. Appendix B contains
a complete set of analytical results collected during the system performance evaluation. The results of the
water samples collected are discussed below.
Table 4-14. Summary of Arsenic, Iron, and Manganese Analytical Results at Purvine Hall
Parameter
As (total)
As (soluble)
As
(paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Sample
Location00
IN
TB1
TA1
TB2
TA2
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
Unit
Mg/L
HS/L
W/L
^g/L
HS/L
Hg/L
Hg/L
Hg/L
Mfi/L
W/L
^g/L
^g/L
HS/L
^g/L
Hg/L
^g/L
Mg/L
HS/L
^g/L
HS/L
^g/L
^g/L
Sample
Count
36
28
28
28
28
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
Concentration
Minimum
25.2
0.1
0.1
0.1
0.1
0.1
27.6
0.1
0.1
0.5
0.1
0.1
27.4
0.5
<25
<25
<25
<25
0.1
0.1
0.2
0.2
Maximum
35.5
21.6
1.4
30.6
0.8
1.9
33.9
1.9
1.7
0.5
0.6
0.5
33.6
1.6
<25
28
<25
<25
0.6
0.5
0.5
0.5
Average
29.8
5.7
0.4
6.0
0.4
0.6
30.5
0.6
0.8
0.5
0.3
0.3
30.2
0.6
<25
<25
<25
<25
0.4
0.5
0.5
0.5
Standard
Deviation
2.3
7.1
0.3
9.2
0.2
0.5
2.0
0.5
0.6
0.0
0.2
0.2
2.0
0.4
0.0
0.0
0.0
0.0
0.2
0.1
0.1
0.1
(a) Vessels B1 and B2 in lead position; Vessels Al and A2 in lag position.
One-half of detection limit used for samples with concentrations less than detection limit for
calculations.
Outliers excluded from average if all other values are less than the detection limit.
49
-------
Table 4-15. Summary of Arsenic, Iron, and Manganese Analytical Results
at Residence Hall
Parameters
As (total)
As (soluble)
As
(paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn
(soluble)
Sample
Location
IN
TA(b)
TA(a)
TA(a)
TBW
TB(b)
TB(b)
IN
TAw
TB(a)
IN
TA(b)
TBta)
IN
TA(b)
TBta)
IN
TA(b)
TB(a)
IN
TA(b)
TB(a)
IN
TA(b)
TB(a)
IN
TA(b)
TB(a)
IN
TA(b)
TB(a)
Unit
^g/L
^g/L
^g/L
^g/L
^g/L
^g/L
HS/L
HS/L
HS/L
^g/L
^g/L
^g/L
Hg/L
^g/L
^g/L
HS/L
^g/L
HS/L
^g/L
^g/L
^g/L
^g/L
HS/L
HS/L
HS/L
^g/L
^g/L
Sample
Count
28
5
8
28
5
8
28
5
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
Concentration
Minimum
25.7
25. 4
24.7
<0.1
22.2
1.1
0.2
0.4
<0.1
26.6
0.1
0.2
<0.1
0.1
<0.1
0.1
0.1
O.I
26.3
O.I
0.1
<25
<25
<25
<25
<25
<25
0.
O.
0.
O.
0.
0.
Maximum
33.2
32.5
32.8
19.5
27.8
19.2
30.3
77.7
3.1
30.6
1.8
18.7
2.1
0.8
0.6
0.6
0.4
0.5
30.5
1.8
18.5
<25
45
<25
<25
<25
<25
0.6
1.0
0.6
0.3
1.1
0.1
Average
29.6
29.4
29.1
2.8
25.3
12.5
10.5
9.1
1.3
29.1
0.5
9.9
0.7
0.1
0.2
0.2
0.2
0.2
28.9
0.4
9.7
<25
<25
<25
<25
<25
<25
0.2
0.3
0.1
0.1
0.2
0.1
Standard
Deviation
1.8
3.1
2.6
5.4
2.3
6.4
9.0
7.6
1.2
1.3
0.6
5.4
0.8
0.3
0.2
0.1
0.1
0.1
1.3
0.6
5.4
0.0
11.3
0.0
0.0
0.0
0.0
0.2
0.4
0.2
0.1
0.4
0.0
(a) Vessel in lead position.
(b) Vessel in lag position.
Regular font for results of ARM 200 test run; italic font for results of ARM 2007ARM 300 test
run; bold font for results of E33-S test run.
One-half of detection limit used for samples with concentrations less than detection limit for
calculations; duplicate samples included in calculations.
Outliers excluded from average if all other values are less than the detection limit.
4.5.1 Inlet Water to POE Systems. Inlet water data were extracted from Tables 4-14 to 4-19 and
summarized in Table 4-20. The historic source water data (before chlorination) also were reproduced
from Table 4-3 for comparison. As expected, results of inlet water sampling in each of the three buildings
were similar, as all three buildings received their inlet (chlorinated) water from the same storage tank.
50
-------
Table 4-16. Summary of Arsenic, Iron, Manganese, and Titanium Analytical
Results at College Union
Parameter
As (total)
As (soluble)
As
(paniculate)
As(III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
Sample
Location(a)
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
Unit
ug/L
Mfi/L
Mfi/L
Mfi/L
^g/L
ug/L
ug/L
ug/L
ug/L
Mfi/L
Mfi/L
Mfi/L
ug/L
ug/L
ug/L
ug/L
Mfi/L
ug/L
Mfi/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Mfi/L
ug/L
Mfi/L
ug/L
ug/L
Sample
Count
32
32
32
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
Concentration
Minimum
25.1
0.2
0.1
27.4
0.2
0.1
0.2
0.5
0.5
0.1
0.1
0.1
27.2
0.2
0.5
<25
<25
<25
<25
<25
<25
0.1
0.5
0.1
0.1
0.1
0.2
1.7
1.6
1.8
Maximum
35.8
24.3
1.5
35.7
0.5
0.5
1.6
0.5
0.5
0.5
0.5
0.5
35.6
0.5
0.5
<25
<25
<25
<25
<25
<25
0.5
0.5
0.5
0.5
0.5
0.5
9.7
10.2
10.6
Average
29.9
3.7
0.3
30.7
0.4
0.2
0.7
0.5
0.5
0.2
0.3
0.3
30.5
0.4
0.5
<25
<25
<25
<25
<25
<25
0.4
0.5
0.4
0.4
0.4
0.5
3.1
3.3
o o
J.J
Standard
Deviation
2.4
7.1
0.3
3.0
0.1
0.2
0.5
0.0
0.0
0.1
0.2
0.2
3.0
0.1
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.2
0.0
0.1
0.1
0.1
0.1
2.9
3.0
3.2
(a) Vessel A in lead position; Vessel B in lag position.
Outliers excluded from average if all other values are less than the detection limit.
Total arsenic concentrations in inlet water (with samples collected from all three buildings) ranged from
24.7 to 35.8 |o,g/L and averaged 29.7 |o,g/L. Soluble As(V) was the predominating species, ranging from
26.3 to 35.6 ug/L and averaging 29.8 ug/L. Soluble As(III) and particulate arsenic concentrations were
low, averaging 0.2 and 0.7 ug/L, respectively. The concentrations of arsenic species in inlet water
sampled during the system performance evaluation were consistent with those of the historical source
water sampling. Because the inlet water was chlorinated (with 0.3 mg/L of free chlorine [as C12], on
average), it was highly oxidizing, as reflected by high ORP readings (498 mV [on average]) and high DO
levels (3.4 mg/L [on average]).
Similar to the historic results, iron and manganese concentrations in inlet water were low, typically less
than the MDLs at 25 and 0.3 ug/L, respectively. pH values of the inlet water ranged from 7.3 to 8.5 and
averaged 8.0, which is at the higher end of the commonly recommended range of 5.5 to 8.5 for arsenic
removal by adsorptive media. Media run lengths at pH 8.0 most likely would be shorter than the runs at
51
-------
Table 4-17. Summary of Other Water Quality Parameter Results at Purvine Hall
Parameter
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate
(asN)
Total P
(asP)
Silica
(as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
(as C12)
Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Sample
Location00
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TT
IN
TB1
TA1
TB2
TA2
TT
IN
TB1
TA1
TB2
TA2
TT
IN
TB1
TA1
TB2
TA2
TT
IN
TB1
TA1
TB2
TA2
TT
IN
TB1
TA1
TB2
TA2
TT
IN
TT
IN
TT
IN
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
HB/L
^g/L
mg/L
mg/L
NTU
NTU
s.u.
s.u.
s.u.
s.u.
s.u.
s.u.
°c
°c
°c
°c
°c
°c
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mV
mV
mV
mV
mV
mV
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
8
8
8
8
8
8
8
8
7
7
8
8
8
8
32
24
24
24
24
8
32
24
24
24
24
8
24
17
17
17
17
7
25
17
17
17
17
8
32
24
24
24
24
8
8
8
8
8
8
8
Concentration
Minimum
112
101
<0.1
<0.1
21.0
20.0
0.5
O.05
<10
<10
27.9
11.4
0.1
0.1
7.3
7.3
7.0
7.4
7.2
6.9
12.8
12.9
13.0
12.1
12.2
12.8
2.4
2.9
2.3
3.0
3.0
2.7
319
255
264
253
257
264
0.2
0.0
0.0
0.0
0.0
0.0
72.3
74.2
53.9
53.7
16.5
20.4
Maximum
122
123
<0.1
0.2
35.0
30.0
1.0
0.9
12
<10
31.2
31.5
0.6
0.9
8.4
8.4
8.4
8.4
8.3
8.4
26.3
25.2
24.8
24.5
24.5
23.1
5.1
5.0
4.5
6.6
4.6
3.5
586
488
491
483
484
568
0.4
0.2
0.2
0.1
0.1
0.1
107
106
79.1
78.5
27.6
27.4
Average
116
113
<0.1
<0.1
23.9
23.0
0.7
0.6
<10
<10
29.9
26.9
0.4
0.5
8.0
8.1
8.0
8.0
8.0
7.9
19.3
19.0
19.4
18.9
19.0
19.9
3.7
3.4
3.4
3.6
3.5
3.1
488
409
430
419
420
400
0.3
0.0
0.0
0.0
0.0
0.0
82.8
84.2
61.5
61.4
21.3
22.9
Standard
Deviation
3.6
6.5
0.0
0.1
4.9
3.6
0.1
0.3
2.7
0.0
1.4
6.6
0.2
0.3
0.2
0.2
0.3
0.2
0.2
0.4
4.5
4.2
4.0
4.4
4.3
4.4
0.7
0.5
0.6
0.9
0.5
0.4
76.8
73.3
59.8
58.1
58.3
93.0
0.1
0.0
0.0
0.0
0.0
0.0
10.7
9.6
7.9
7.6
3.6
2.3
(a) Vessels Bl and B2 in lead position; Vessels Al and A2 in lag position.
One-half of detection limit used for samples with concentrations less than detection limit for
calculations; duplicate samples included in calculations.
52
-------
Table 4-18. Summary of Other Water Quality Parameter Results at Residence Hall
Parameter
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as N)
Phosphorus
(asP)
Silica
(as SiO2)
Turbidity
pH
Temperature
DO
Sample
Location
IN
TAw
TB(a)
IN
TAw
TB(a)
IN
TAw
TB(a)
IN
TAw
TB(a)
IN
TA(b)
TB(a)
IN
TA(b)
TB(a)
IN
TA(b)
TB(a)
IN
TA(b)
TA(a)
TA(a)
TB(a)
jgCb)
TB(b)
IN
TA(b)
TA(a)
TA(a)
TB(a)
TgO)
TBW
IN
TA(b)
TA(a)
TA(a)
TB(a)
TBtb)
-pgO)
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
HS/L
Mfi/L
HS/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
s.u.
s.u.
s.u.
°c
°c
°c
mg/L
mg/L
mg/L
Sample
Count
8
8
8
8
8
8
8
8
8
8
8
8
7
7
7
8
8
8
8
8
8
24
5
8
24
5
8
24
5
8
24
5
8
24
5
8
24
5
8
22
5
1
22
5
1
22
5
1
Concentration
Minimum
110
106
110
0.1
0.1
0.1
21.0
21.0
21.0
0.5
0.5
0.5
<10
<10
<10
28.5
2.2
18.6
0.1
0.1
0.1
7.3
7.9
8.0
6.9
7.9
8.0
7.1
7.9
8.0
13.2
18.5
16.1
13.5
18.5
15.9
13.6
18. 4
15.9
2.3
3.2
3.7
2.2
2.8
3.1
2.5
3.0
4.7
Maximum
123
122
125
0.1
0.1
0.1
26.0
26.0
24.0
0.9
0.9
0.9
<10
<10
<10
31.2
31.7
31.6
1.1
0.7
0.5
8.3
8.0
8.3
8.5
8.1
8.3
8.5
8.0
8.8
24.3
22.4
24.2
24.3
23.1
24.5
24.1
23.1
24.6
4.9
5.2
3.7
4.3
4.2
3.1
5.1
4.2
4.7
Average
116
115
117
0.1
0.1
0.1
22.5
22.2
21.8
0.7
0.7
0.7
<10
<10
<10
30.1
25.7
28.2
0.4
0.3
0.2
7.9
8.0
8.2
8.0
8.0
8.2
8.0
8.0
8.2
19.6
20.5
20.8
19.7
20.7
20.8
19.7
20.6
20.8
3.2
4.3
3.7
3.0
3.6
3.1
3.1
3.8
4.7
Standard
Deviation
5.1
5.2
4.6
0.0
0.0
0.0
1.7
1.6
1.0
0.1
0.1
0.1
0.0
0.0
0.0
0.9
9.6
4.0
0.3
0.2
0.2
0.2
0.1
0.1
0.3
0.1
0.1
0.3
0.1
0.3
3.3
1.9
3.0
3.3
2.1
3.1
3.3
2.1
3.1
0.6
0.9
0.0
0.6
0.7
0.0
0.7
0.5
0.0
53
-------
Table 4-18. Summary of Other Water Quality Parameter Results at Residence Hall (Continued)
Parameter
ORP
Free Chlorine
(as C12)
Total
Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Sample
Location
IN
TA(b)
TA(a)
TA(a)
TB(a)
-pgO)
-pgCb)
IN
TA(b)
TA(a)
TA(a)
TB(a)
-j-gCb)
ra(b)
IN
TAw
TB(a)
IN
TAw
TB(a)
IN
TA(b)
TB(a)
Unit
mV
mV
mV
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
24
5
1
24
5
1
24
5
1
24
5
8
24
5
8
24
5
8
8
8
8
8
8
8
8
8
8
Concentration
Minimum
276
503
562
326
555
596
405
574
546
0.2
0.3
0.4
0.1
0.3
0.4
0.1
0.2
0.3
77.6
76.2
78.5
54.7
54.9
55.1
21.2
21.0
21.5
Maximum
570
564
562
600
579
596
609
613
546
0.4
0.4
0.4
0.3
0.3
0.4
0.3
0.3
0.4
93.8
91.6
103
66.9
65.5
75.8
26.9
26.0
26.9
Average
494
529
562
522
570
596
542
586
546
0.3
0.3
0.4
0.2
0.3
0.4
0.3
0.3
0.4
84.3
82.9
85.2
60.7
60.0
61.7
23.5
22.9
23.5
Standard
Deviation
71.2
22.1
0.0
63.9
9.1
0.0
50.5
75.5
0.0
0.0
0.0
0.0
0.1
0.0
0.0
0.1
0.0
0.1
5.9
5.1
8.0
4.5
3.6
6.6
1.7
1.8
1.7
(a) Vessel in lead position.
(b) Vessel in lag position.
Regular font for results of ARM 200 test run.
Italic font for results of ARM 200/ARM 300 test run.
Bold font for results of E33-S test run.
One-half of detection limit used for samples with concentrations less than detection limit
calculations.
for
lower pH values. Lowering pH values prior to adsorption can prolong the adsorption runs, but often is
avoided by small system operators because of the need to handle acids and bases. When benefits of
lowering pH values are out-weighed by concerns over the handling of acids and bases, pH adjustments
are not performed.
Competing anions such as silica and phosphorus were measured in source water during the initial site
visit and in inlet water during the performance evaluation study. Analysis of inlet water showed silica
levels at 27.8 to 31.5 mg/L (as SiO2), compared to 30.3 to 34.2 mg/L (as SiO2) in source water during the
initial site visit. Silica adsorption by the five adsorptive media tested is discussed in detail in
Section 4.5.2. Total phosphorus in inlet water was below its MDL of 10 (ig/L, consistent with the
measurements of orthophosphate levels measured (below the MDL of 0.06 mg/L [as PO4]) during the
initial site visit.
Other analytes measured were either low or close to or below their respective MDLs. Their effects on
arsenic removal by the media evaluated were expected to be minimal.
54
-------
Table 4-19. Summary of Other Water Quality Parameter Results at College Union
Parameter
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate (as
N)
Phosphorus
(asP)
Silica
(as SiO2)
Turbidity
pH
Temperature
ORP
DO
Free
Chlorine
(as C12)
Total
Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg
Hardness
(as CaCO3)
Sample
Location'3'
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
IN
TA
TB
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
Mfi/L
W?/L
HB/L
mg/L
mg/L
mg/L
NTU
NTU
NTU
s.u.
s.u.
s.u.
°c
°c
°c
mV
mV
mV
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
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
29
29
29
29
29
29
22
22
22
20
20
20
29
29
28
7
7
7
7
7
7
7
7
7
Concentration
Minimum
110
104
103
<0.1
<0.1
<0.1
21.0
21.0
<1.0
0.5
0.6
0.6
<10
<10
<10
27.8
28.2
27.3
0.1
0.2
0.1
7.8
7.2
7.4
12.1
11.9
11.9
315
474
460
2.5
2.7
2.4
0.3
0.2
0.1
67.0
63.9
68.6
54.8
46.8
50.1
12.2
17.1
18.5
Maximum
127
122
122
<0.1
<0.1
0.7
28.0
26.0
26.0
0.9
0.9
1.0
<10
<10
<10
31.5
32.3
31.7
1.5
0.5
0.7
8.5
8.6
8.6
25.1
25.3
25.4
575
600
611
5.4
3.9
7.1
0.4
0.4
0.4
106
107
103
78.2
80.0
75.9
27.3
27.0
27.0
Average
118
116
114
<0.1
<0.1
0.1
22.5
22.1
19.4
0.7
0.7
0.7
<10
<10
<10
29.9
29.9
29.8
0.6
0.3
0.3
8.0
8.0
8.0
20.1
20.1
20.1
505
554
563
3.3
3.1
3.3
0.3
0.3
0.3
83.8
83.5
83.0
62.9
61.2
60.8
20.9
22.3
22.3
Standard
Deviation
6.4
6.6
8.0
0.0
0.0
0.2
2.5
1.8
8.6
0.1
0.1
0.1
0.0
0.0
0.0
1.4
1.6
1.7
0.5
0.1
0.2
0.2
0.2
0.2
4.2
4.2
4.3
59.6
33.6
36.3
0.7
0.4
1.0
0.1
0.1
0.1
11.5
12.6
10.9
7.5
9.7
8.4
5.3
3.1
2.8
(a) Vessel A in lead position and Vessel B in lag position.
55
-------
Table 4-20. Comparison of Water Quality Between Building Inlet and Historic Results
Parameter
pH
DO
ORP
Total
Alkalinity
(as CaCO3)
Total
Hardness
(as CaCO3)
Turbidity
Nitrate
(asN)
Fluoride
Sulfate
Silica
(as SiO2)
Phosphorus
(asP)
As
(total)
As
(soluble)
As
(paniculate)
As(III)
As(V)
Unit
S.U.
mg/L
mV
mg/L
mg/L
NTU
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Building
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Sample
Count
32
37
29
24
28
20
25
30
22
8
8
7
8
8
7
8
8
7
8
8
7
8
8
7
8
8
7
8
8
7
7
7
7
36
41(b)
32
8
8
7
8
8
7
8
8
7
8
8
7
Concentration Range (Average)
At Each Building
7.3-8.4 (8.0)
7.3-8.3 (8.0)
7.4-8.5 (8.0)
2.4-5.1(3.7)
2.3-5.2 (3.4)
2.5-5.4 (3.3)
319-586(488)
276-570 (502)
315-575(505)
112-122(116)
110-123(116)
110-127(118)
72.3-107 (82.8)
77.6-93.8 (84.3)
67.0-106 (83.8)
0.1-0.6(0.4)
0.1-1.1(0.4)
0.1-1.5(0.6)
0.5-1.0 (0.7)
0.5-0.9 (0.7)
0.5-0.9 (0.7)
0.1-0. 1(0.1)
0.1-0.1(0.1)
0.1-0.1(0.1)
21.0-35.0 (23.9)
21.0-26.0 (22.5)
21.0-28.0 (22.5)
27.9-31.2(29.9)
28.5-31.2(30.1)
27.8-31.5(29.9)
<10-12.0 (<10)
<10-<10 (<10)
<10-<10 (<10)
25.2-35.5 (29.8)
24.7-33.2 (29.4)
25.1-35.8(29.9)
27.6-33.9 (30.5)
26.6-30.6(29.1)
27.4-35.7 (30.7)
0.1-1.7(0.8)
0.1-2.1(0.7)
0.2-1.6 (0.7)
0.1-0.6(0.3)
0.1-0.6(0.2)
0.1-0.5(0.2)
27.4-33.6 (30.2)
26.3-30.5 (28.9)
27.2-35.6 (30.5)
Across Three
Buildings
7.3-8.5 (8.0)
2.3-5.4 (3.4)
276-586 (498)
110-127(117)
67.0-107 (83.6)
0.1-1.5 (0.5)
0.5-1.0 (0.7)
0.1-0.1
(0.1)
21.0-35.0 (23.0)
27.8-31.5(30.0)
<10-12.0 (<10)
24.7-35.8 (29.7)
26.6-35.7(30.1)
0.1-2.1(0.7)
0.1-0.6(0.2)
26.3-35.6 (29.8)
Historic
Data(a)
7.6-8.0
4.2
82
107-112
80-81
0.6
0.6-0.8
0.1-0.2
21.0-23.0
30.3-34.2
<60(c>
29.0-36.0
33.0
0.1
0.5
32.5
56
-------
Table 4-20. Comparison of Water Quality Between Building Inlet and Historic Results (Continued)
Parameter
Fe (total)
Fe (soluble)
Mn (total)
Mn
(soluble)
Ti (total)
Unit
ug/L
ug/L
ug/L
ug/L
ug/L
Building
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Purvine Hall
Residence Hall
College Union
Sample
Count
8
8
8
8
8
7
8
8
7
8
8
7
NA
NA
7
Concentration Range (Average)
At Each Building
<25-<25 (<25)
<25-<25 (<25)
<25-<25 (<25)
<25-<25 (<25)
<25-<25 (<25)
<25-<25 (<25)
0.1-0.6(0.4)
<0. 1-0.6 (0.2)
0.1-0.5(0.4)
0.2-0.5 (0.5)
<0. 1-0.3 (0.1)
0.1-0.5(0.4)
NA
NA
1.7-9.7(3.1)
Across Three
Buildings
<25-<25 (<25)
<25-<25 (<25)
<0. 1-0.6 (0.3)
<0. 1-0.5 (0.3)
NA
Historic
Data(a)
<25
<25
<0. 1-0.2
<0.1
NA
(a) See Table 4-2 (data reflect results before chlorination).
(b) Including all three tests.
(c) Concentration of orthophosphate (as PO4).
4.5.2
Treated Water Following Media Adsorption
4.5.2.1 ArsenX"p. Figure 4-19 presents arsenic breakthrough curves at TB1, TA1, TB2, TA2, and
TT. Arsenic breakthrough at 10 (ig/L following the lead vessels (TB1 and TB2) occurred after treating
approximately 594,440 and 609,700 gal of water (or 15,900 and 16,300 BV), respectively. (BV was
calculated based on 5 ft3 of media in a lead vessel.) These run lengths represented only approximately
30% of the 52,750-BV run length estimated by the vendor. By the end of the performance evaluation
study, arsenic levels following the two lead vessels were approaching those in inlet water. At this time,
the system had treated 1,814,428 gal (or 24,254 BV [1 BV = 10 ft3 of media in both lead vessels]) of
water. The run-length differences observed between the two trains were caused by the imbalanced flow
experienced during the initial stage of system operation (see Section 4.4.5).
At the end of the performance evaluation study, arsenic concentrations following the lag vessels (TA1 and
TA2) were 0.4 ug/L. Since then, the system continued to treat and provide drinking water to taps in
Purvine Hall.
Figure 4-20 presents silica breakthrough curves from the treatment system. Silica broke through from the
treatment system soon after system startup. Complete silica breakthrough occurred at approximately
5,000 BV (1 BV = 10 ft3 of media in both lead vessels). Silica adsorption has been observed at a number
of arsenic demonstration sites using AM; a review of silica adsorption at these sites was documented in a
system performance evaluation report authored by Chen et al. (2010).
57
-------
40.0
35.0
30.0
25.0
3 20.0
•-B
I
I 15'°
o
o
1/3
^ 10.0
5.0
0.0
AsMCL=10ng/L
1 BV = 5 ft3 or 37.4 gal of
media in lead vessel
-n
10 12 14 16 18 20 22 24 26 28 30
Throughput (BV) xlOOO
Influent (IN) —#— Train 1 Lead Vessel (TB1) —0— Train 2 Lead Vessel (TB2)
- Train 1 Lag Vessel (TA1) -D- Train 2 Lag Vessel (TA2) -•- Combined Effluent (TT)
35.0
30.0
J
W'
s
o
•s
20.0
10.0
5.0
Figure 4-19. Total Arsenic Breakthrough from ArsenXnp Media
2.0
1 BV = 10 ft3 or 74.8 gal of media
in both lead vessels
4.0 6.0
Throughput (BV) xlOOO
-«-IN -B-TT
8.0
Figure 4-20. Silica Breakthrough from ArsenXnp Media
100
58
-------
4.5.2.2 ARM200/ARM300/E33-SMedia. Figure 4-21 presents breakthrough curves following the
lead and lag vessels. Total arsenic concentrations exceeded 10 (ig/L after the lead vessel (TB) containing
ARM 200 had treated 2,085,000 gal (or 13,940 BV) of water. (BV was calculated based on 20 ft3 of
media in the lead vessel.) The BV was only 22% of the vendor-estimated run length of 62,600 BV.
Since then, total arsenic concentrations following the lead vessel fluctuated between 9.9 and 12.6 (ig/L
before spiking to 17.6, 28.5, and 30.3 (ig/L at 27,800, 36,200, and 39,400 BV, respectively. By the end of
the ARM 200 test, total arsenic concentrations following the lead vessel had reached the inlet water level
of approximately 30 (ig/L. At this time, the lead vessel had treated approximately 6,698,000 gal of water
(or 44,770 BV [1 BV = 20 ft3 = 149.6 gal]).
40.0
35.0
30.0
^ 25.0
20.0
u
§
U
15.0
10.0
5.0
-IN
-ARM 200 (Lead)
-ARM 200 (Lag)
Partially Spent ARM 200 (Lead)
-ARM 300 (Lag)
ARM 200 in lead
vessel replaced with
ARM 300 at 44,767
BV and placed in lag
position
J15,557BV
1 BV = 20 ft3 = 149.6 gal
10
20
30 40 50
Throughput (BV) xlOOO
60
70
Figure 4-21. Total Arsenic Breakthrough from ARM 200 and/or ARM 300 Media
Breakthrough of total arsenic at 10 (ig/L following the lag vessel (TA) containing ARM 200 media
occurred at 34,078 BV (1 BV = 20 ft3 of media in one vessel). Considering the lead and lag vessels as
one large vessel, breakthrough at 10 (ig/L in system effluent would occur at 17,039 BV (1 BV = 40 ft3 of
media in both vessels). The difference between the two-vessel and one-vessel run lengths (17,039 vs.
13,940 BV) likely was caused by twice as long EBCT for the lead/lag system. By the end of the ARM
200 test, the total arsenic concentration in the system effluent had reached 19.5 (ig/L.
Because of the unexpected early arsenic breakthrough, the system was taken offline and the lead vessel
was rebedded with ARM 300 when the lag vessel had an arsenic effluent concentration of 19.5 (ig/L.
After vessel switching (with partially spent ARM 200 in the lead position and virgin ARM 300 in the lag
position), the system was put online on January 24, 2007. The lead vessel containing partially spent
ARM 200 (TA) continued to remove arsenic but the percentage removal was diminishing from about 21%
59
-------
at 3,200 BV (since rebedding and vessel switching) to <9% at 31,300 BV (1 BV = 20 ft3 = 149.6 gal).
Total arsenic concentrations from the lag vessel (TB) reached 9.5 (ig/L on April 4, 2007 after treating
2,327,650 gal (or 15,557 BV) of water. This run length was very close to that (13,940 BV) for ARM 200.
Because of the short run lengths experienced with both ARM 200 and ARM 300 media, the system was
put in the standby mode on July 11, 2007, pending results of a series of rapid small-scale column tests
(RSSCTs) funded under another EPA task order. The RSSCTs evaluated the run lengths of five different
adsorptive media (i.e., ArsenXnp, ARM 200, GFH [a granular ferric hydroxide media developed by GEH
Wasserchemie Gmbh and marketed by Siemens], Metsorb [a titanium dioxide-based media developed by
HydroGlobe], and E33-S) using 100 x 140 U.S. standard mesh media fractions packed separately in 1.1-
cm x 30.5-cm glass columns. The results indicated that E33-S was able to achieve a useful run length of
approximately 40,000 BV, while the rest would achieve only 12,000 to 20,000 BV. As such, E33-S was
used to rebed both lead and lag vessels on October 3, 2007, and the system was put back online
immediately for additional testing.
E33-S media treated approximately 7,480,000 gal (or 50,000 BV [1 BV = 20 ft3 = 149.6 gal]) of water
before effluent concentrations from the lead vessel exceeded the 10-(ig/L MCL (see Figure 4-22). This
run length was 20% longer than the RSSCT-projected run length and much longer than those achieved by
ARM 200 (13,940 BV), ARM 300 (16,200 BV [with 8.6 to 20.1% of arsenic already removed by ARM
200 media]), and ArsenXnp (16,000 BV). During the last sampling event on August 26, 2009, the arsenic
concentration following the lag vessel was 3.1 (ig/L. By now, the system had treated 12,170,210 gal of
water (equivalent to 40,670 BV based on 40 ft3 of media in both vessels).
40.0
35.0
30.0
"a 20.0
15.0
U
10.0
5.0
0 0
As MCL = 10 fig 1
1 BV = 20 ft3 = 149.6 gal
10
20
30 40 50 60
Throughput (BY) xlOOO
90
100
-E33 (Lead)
-E33 (Lag)
Figure 4-22. Arsenic Breakthrough from E33-S Media
60
-------
Removal of silica (as SiO2) by ARM 200 was observed during the initial stage of the ARM 200
adsorption run. Because only two samples were collected during the first three months of system
operation and because silica concentrations had already reached inlet levels during the second sampling
event (at approximately 9,400 BV), precise silica breakthrough behavior may not be determined using the
available data (see Figure 4-23).
35.0
30.0
25.0
ff
I
20.0
15.0
10.0
5.0
0.0
1 BV = 20 ft3 = 149.6 gal
6 S 10 12 14 16 IS 20 22 24 26 28 30
Throughput (BV) xlOOO
-•-IN -B-Lead Vessel (TB) -*~Lag Vessel (TA)
Figure 4-23. Silica Breakthrough from ARM 200 Media
4.5.2.3 Adsorbsia™ GTO™. Figure 4-24 shows total arsenic breakthrough from Adsorbsia™
GTO™ media. Total arsenic concentrations following the lead vessel (TA) remained below 1.1 (ig/L
after the system had treated 2,571,229 gal of water (or 21,484 BV based on 16 ft3 of media in the lead
vessel). Since then, total arsenic concentrations rose sharply to 10 (ig/L after treating an additional
12,000 BV of water. Afterwards, total arsenic concentrations continued to increase to 24.3 ug/L in 7,200
BV. During the last sampling event of the system performance evaluation study, the arsenic
concentration following the lead vessel was 21.1 ug/L, which was within 22% to the inlet level; the
arsenic concentration following the lag vessel (TB) was 0.6 ug/L. At this time, the system had treated
5,889,749 gal of water (equivalent to 21,872 BV based on 36 ft3 of media). The vendor-estimated media
life was 60,150 BV, which was about 80% higher than the run length achieved by the lead vessel.
Silica did not seem to compete with arsenic for adsorption sites, as evidenced by the same level of silica
in the treated water.
61
-------
a
40.0
35.0
30.0
23-1'
•a 20.0
K
I
§ 15.0
U
I
10.0
5.0
0 0
1BV = 20 ft3 = 149.6 gal
10 15 20 25 30
Throughput (BY) xlOOO
40
45
50
-IN
-Lead(TA)
-•-Las(TB)
Figure 4-24. Total Arsenic Breakthrough from Adsorbsia™ GTO™ Media
4.5.2.4 POE System Performance Comparison. Table 4-21 summarizes the run length data of the
three POE systems. Among the media evaluated, E33-S performed the best, achieving approximately
50,000 BV. Adsorbsia™ GTO™ was the next best performer, achieving 33,500 BV. ARM 200, ARM
300, and ArsenXnp had a media life of around 16,000 BV.
Table 4-21. Summary of Media Run Lengths
Run Length(a)
POE Systems
RSSCT
Purvine
Hall
ArsenXnp
16,000
15,000
Residence
Hall
ARM 200
13,940
14,000
ARM 300
16,200(b)
NA
E33-S
50,000
40,000
College
Union
Adsorbsia™
GTO™
33,500
NA
(a) To 10 ug/L arsenic breakthrough.
(b) Before contacting ARM 300, 8.6 to 20.9% of arsenic in inlet water already removed by
partially spent ARM 200 media.
The full-scale system data seemed to match the RSSCT data rather well, with projected run lengths within
6.3%, 0.4%, and 20% of the actual run lengths for ArsenXnp, ARM 200, and E33-S, respectively.
62
-------
4.5.2.5 POU Units. Figures 4-25 and 4-26 show total arsenic concentrations following three POU
units loaded with ARM 200 media and three POU units loaded with E33-S, respectively. Total arsenic
was consistently removed to less than 1.0 (ig/L from ARM 200 Units 1 and 2 after treating approximately
400 and 740 gal of water, respectively. ARM 200 Unit 3 effectively removed arsenic to <2.1 (ig/L after
treating 500 gal, but the effluent arsenic concentrations rose steadily to 6.0 after treating approximately
1,000 gal. Arsenic was consistently removed to the MDL level by the three E33-S POU units after
treating approximately 500 gal. A follow-on study that allowed inlet water to flow through an E33-S
POU unit at about 1 gpm showed the concentration reduction to <10 ug/L by the unit during the first
3,000 gal of throughput (Figure 4-27).
10.0
8.0
6.0
4.0
2.0
As MCL 10 (ig L
POU 2 moved from
SnellHalltoComett
Hall at -600 gal oil
February 13. 2008.
0 100 200 .WO 400 500 600 "00 800 900 1,000
Throughput (gal)
—»-POUl(ARM200) -»-POU2(ARM200) -n- POU 3 (ARM 200)
Figure 4-25. Arsenic Breakthrough Curves for Three ARM 200 POU Units
4.5.6 Backwash Wastewater Sampling. Table 4-22 summarizes analytical results of the
backwash wastewater sampling during backwash of the three POE systems on May 16 or 17, 2006. The
unfiltered samples were analyzed for pH, TDS, TSS, and total arsenic, iron, and manganese. Filtered
samples using 0.45-|o,m disc filters were analyzed for soluble arsenic, iron, and manganese. Backwash
solid results are presented in Table 4-23.
4.5.6.1 ArsenX"p System. The lead vessels (TB1 and TB2) were backwashed using treated water
from the lag vessels (TA1 and TA2) in the same train. Similarly, the lag vessels (TA1 and TA2) were
backwashed using treated water from the lead vessels (TB1 and TB2) in the same train. The treated water
from the lag and lead vessels contained, at the time, no more than 0.1 |o,g/L of total arsenic. Wastewater
collected from the two lead vessels contained 15.2 and 14.3 (ig/L of total arsenic, respectively, existing
primarily in the soluble form (this is contrary to what would be expected). Wastewater collected from the
two lag vessels contained only 0.2 (ig/L of total arsenic, similar to the level in the treated water. Solids in
63
-------
10.0
8.0
6.0
4.0
AsMCL lOjisL
0.0
100
200
-POU1(E33)
300
Throughput (gil
-«-POU2(E33)
400
POU3(E33)
500
600
Figure 4-26. Arsenic Breakthrough Curves for Three AdEdge E33-S POU Units
12.0
10.0
8.0
2 6.0
1
4.0
2.0
As MCL 10 jig L
500
1,000
1.500 2,000 2,500 3,000
Throughput (gnl)
Figure 4-27. Results of AdEdge E33-S POU Unit Run Length Study
3,500
64
-------
Table 4-22. Backwash Sampling Results
Sampling
Location
M
a.
S.U.
!/5
0
H
mg/L
!/5
!/5
H
mg/L
"3
-*^
§
%
•<£
fig/L
As (soluble)
fig/L
As (particulate)
fig/L
/^•js
CS
-*^
§
0)
u.
Hg/L
Fe (soluble)
fig/L
"3
-*^
§
I
fig/L
Mn (soluble)
Hg/L
ArsenXnp System in Purvine Hall
TB1 (Lead/Train 1)
TA1 (Lag/Train 1)
TB2 (Lead/Train 2)
TA2 (Lag/Train 2)
7.9
7.8
7.9
7.9
174
188
164
172
48
18
4
60
15.2
0.2
14.3
0.2
12.5
0.1
13.7
0.1
2.7
0.1
0.7
0.1
2,758
1,867
389
2,499
<25
<25
<25
<25
19.1
3.9
3.6
5.1
0.1
0.3
0.1
0.2
ARM 200 System in Residence Hall
TB (Lead)
TA (Lag)
7.9
8.0
188
180
6
34
19.0
13.9
18.2
10.4
0.8
3.5
1,280
3,637
<25
<25
19.4
29.0
0.1
0.2
Adsorbsia™ GTO™ System in College Union
TA (Lead)
TB(Lag)
7.8
7.9
184
162
120
62
10.9
1.3
12.3
1.9
0.1
0.1
421
137
<25
<25
7.3
3.1
0.1
0.1
TDS = Total Dissolved Solids
TSS = Total Suspended Solids
the backwash wastewater, as reflected by TSS at 4 to 60 mg/L, most likely were media fines measured as
particulate iron (at 389 to 2,758 (ig/L). The unusually low TSS value (4 mg/L) measured at TB2 might
have been the result of sampling errors caused by insufficient mixing of the solids/water mixtures in the
backwash water collection containers immediately before sampling. Based on an average TSS level of 42
mg/L (excluding the 4 mg/L outlier) and the quantity of backwash wastewater produced (144 gal/vessel),
approximately 91.6 g of solids was discharged during the backwash event. The discharged solids
contained negligible amount of arsenic (due to the low particulate arsenic concentrations in the
wastewater) and 5.2 g of iron (5.6% by weight), which does not reconcile well with the 91.6-g TSS
measured in the wastewater sample or the 18.7% iron measured in the backwash solids (see Table 4-25).
The solids analysis showed low arsenic and manganese loadings at 0.04% and 0.11%, respectively.
4.5.6.2 ARM200 System. Backwash was performed using treated water from the other vessel in the
treatment system. At the time of backwash, the treated water from the lead and lag vessels contained no
more than 11.1 and 0.3 (ig/L of arsenic, respectively. However, the backwash water from the lead and lag
vessels contained 19.0 and 13.9 (ig/L of arsenic, respectively. Again, the majority of arsenic in the
wastewater existed as soluble arsenic. As expected, more arsenic was found from the lead than the lag
vessel, due the higher arsenic loading in the lead vessel (even though the treated water from the lag vessel
used for backwashing the lead vessel contained less arsenic). The TSS levels were 6 and 34 mg/L for the
lead and lag vessels, respectively. The low TSS value found for the lead vessel might be the result of
sampling errors as discussed above. Based on the TSS levels (6 and 34 mg/L) and the quantity of
backwash water produced (350 and 136 gal), approximately 25.4 g of solids was discharged during the
backwash event. The discharged solids contained 3.6 g of iron (or 14.1% by weight) but negligible
amounts of arsenic and manganese. Similar to the ArsenXnp solid results, the individual elemental results
do not reconcile well with the TSS results or backwash solids results (i.e., 41% iron, 0.3% manganese,
and 0.04% arsenic).
4.5.6.3 Adsorbsia™ GTO™ System. Similar to the ARM 200 system in the Residence Hall,
backwash of the Adsorbsia™ GTO™ system was performed using treated water from the other vessel in
65
-------
Table 4-23. Backwash Solids Results
Sample ID
Mg
Hg/g
Si
Hg/g
P
Hg/g
Ca
Hg/g
Mn
Hg/g
Fe
Hg/g
As
Hg/g
Ba
Hg/g
Ti
Hg/g
ArsenX"p System in Purvine Hall
BW1-A (TA1)
BW1-B (TA1)
BW1-C (TA1)
Average
BW2-A(TB1)
BW2-B (TB1)
BW2-C(TB1)
Average
BW3-A (TA2)
BW3-B (TA2)
BW3-C (TA2)
Average
BW4-A (TB2)
BW4-B (TB2)
BW4-C (TB2)
Average
1,350
1,331
1,307
1,329
462
458
469
463
956
928
933
939
1,746
1,716
1,783
1,748
541
<250
284
412
<250
293
<250
293
473
<250
419
446
429
441
<250
435
348
362
332
347
640
625
639
634
343
354
358
352
519
515
543
526
5,384
5,489
5,761
5,545
2,065
2,100
2,148
2,104
4,362
4,298
4,360
4,340
11,608
11,369
11,925
11,634
939
976
954
956
,271
,276
,281
,276
,068
,065
,018
,051
994
950
1,001
982
184,546
187,074
186,709
186,110
196,535
195,133
196,798
196,155
200,127
190,703
196,192
195,674
177,617
171,429
171,784
173,610
7.8
8.9
8.3
8.3
923
942
947
937
26.7
19.9
18.8
21.8
784
763
790
779
11.6
12.4
12.2
12.0
16.4
17.1
16.7
16.7
12.7
13.6
12.7
13.0
15.5
14.9
18.5
16.3
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
ARM 200 System in Residence Hall
BW1-A (TA)
BW1-B (TA)
BW1-C (TA)
Average
4,953
5,046
4,786
4,929
846
938
1,074
953
328
353
374
352
24,469
25,360
25,280
25,036
3,008
2,966
3,005
2,993
424,855
398,674
408,767
410,765
434
434
421
430
8.1
8.6
7.7
8.1
NA
NA
NA
NA
Adsorbsia™ GTO™ System in College Union
BW1-A (TA)
BW1-B (TA)
BW1-C (TA)
Average
BW2-A (TB)
BW2-B (TB)
BW2-C (TB)
Average
3,177
3,221
3,157
3,185
4,920
4,868
4,781
4,856
441
534
324
433
849
886
917
884
106
98.7
72.3
92.3
158
154
155
156
20,867
21,530
21,352
21,249
28,276
28,197
27,810
28,094
40.5
38.9
42.0
40.5
62.4
59.9
62.7
61.7
,294
,418
,251
,321
,735
,753
,746
,745
2.0
0.6
<0.5
1.0
<0.5
<0.5
<0.5
<0.5
19.4
20.0
20.1
19.8
13.2
13.6
13.2
13.3
211,113
189,643
NA
200,388
340,379
343,268
NA
341,824
the treatment system. At the time of backwash, the treated water from the lead and lag vessels contained
no more than 0.6 and 0.1 (ig/L of arsenic, respectively. Backwash water analytical data indicated more
arsenic from the lead vessel (i.e., 10.9 vs. 1.3 ug/L) due to more arsenic loading. The majority of the total
arsenic in the backwash water was in the soluble form. Based on the TSS levels (120 and 62 mg/L) and
the quantity of backwash water produced (240 gal/vessel), approximately 165g of solids was discharged
during the backwash event. Because titanium was not analyzed, its amount in backwash wastewater
could not be estimated. However, based on the amounts measured in backwash solids, over 34% of the
solids could be present as titanium.
4.5.7 Distribution System Water Sampling. Prior to the installation/operation of the three POE
treatment system, first draw baseline distribution system water samples were collected at three locations
on July 13, August 4, August 24, and September 14, 2005. Following the installation of the treatment
system, distribution water sampling continued on a monthly basis until April 4, 2007. Table 4-24
summaries results of the distribution system sampling.
66
-------
Table 4-24. Distribution System Sampling Results
No. of
Sampling
Events
BL1
BL2
BL3
BL4
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
Address
Sample
Type
Flushed /
1st Draw
Sampling
Date
07/13/05
08/04/05
08/24/05
09/14/05
01/25/06
03/02/06
03/30/06
04/26/06
05/25/06
06/21/06
08/17/06
08/31/06
09/13/06
10/11/06
11/16/06
12/13/06
01/10/07
02/07/07
03/08/07
04/04/07
DS1
Purvine Hall
LCR
1st Draw
o>
H
a ^
0 !-
••g-S-
a
.s
to
14.8
17.0
15.7
15.3
10.3
10.2
15.1
14.9
15.0
14.9
19.6
NA
15.3
15.3
15.3
15.0
16.0
14.8
15.0
15.4
$
S£
M
7.6
7.5
7.8
7.7
7.7
7.9
7.9
7.9
7.7
7.9
7.7
7.9
7.8
7.8
7.6
7.7
8.0
8.1
8.0
8.0
6
^
.5 w
T2 *
If
110
110
110
110
119
112
112
112
112
112
111
124
137
124
135
115
124
121
124
124
*
*t,
27.0
26.6
35.4
25.6
1.7
1.5
1.4
0.7
0.7
0.6
0.5
0.8
0.6
0.6
0.7
O.I
0.8
0.7
0.6
7.3
Fe (ng/L)
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
1
§
O.I
O.I
1.2
O.I
1.0
0.4
1.1
0.4
0.5
0.4
0.5
0.6
0.4
O.I
0.3
0.4
0.3
0.3
O.I
O.I
1
e
0.4
1.4
0.4
0.8
0.2
0.1
1.5
0.9
0.1
0.1
1.3
1.4
1.3
0.5
0.1
O.I
0.5
0.5
0.4
1.0
1
5
98
94
63
101
155
40
160
106
53
100
137
167
171
106
89
44
94
73
126
77
DS2
College Union
LCR
1st Draw
U
H
I*
« ^
=
M
.s
to
15.1
16.4
16.0
15.7
NS
15.8
16.3
15.1
15.0
15.0
19.8
7.8
15.5
15.3
15.3
14.1
15.3
14.8
15.7
15.6
d
i—; cs
^
&d
M
7.7
7.6
7.8
7.7
NS
7.5
7.7
7.8
7.7
7.8
7.9
7.9
7.9
7.8
7.7
7.8
8.1
8.1
8.1
8.0
]3
-i
~<
110
128
114
106
NS
104
108
112
108
112
117
120
123
120
124
119
123
123
124
117
d
sp
(X)
<
36.0
26.3
33.0
28.3
NS
0.8
1.3
0.5
0.2
0.2
1.4
0.7
1.0
0.3
0.4
O.I
0.4
0.4
3.6
0.5
£
&
<25
<25
<25
<25
NS
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
<25
1
§
0.3
0.2
0.6
0.2
NS
O.I
0.8
O.I
O.I
O.I
0.4
0.2
0.2
O.I
O.I
O.I
O.I
O.I
O.I
O.I
1
e
0.6
0.5
0.4
0.6
NS
0.1
1.3
0.4
0.1
0.1
1.6
1.2
1.4
0.3
0.1
O.I
0.6
0.5
0.7
0.5
1
5
224
138
81
208
NS
97
448
223
41
98
119
121
199
165
135
72
129
101
92
126
DS3
Residence Hall
LCR
1st Draw
U
H
I?
O ja
03 * — '
=
M
.s
to
15.2
16.3
13.9
16.0
9.8
16.0
16.1
15.6
15.2
15.6
19.8
7.6
18.0
16.6
15.5
15.3
15.3
14.6
15.1
15.3
pH (S.U.)
7.3
7.6
7.8
7.7
7.7
7.9
8.0
8.0
7.8
7.8
7.9
7.8
7.8
7.8
7.8
7.8
8.0
8.0
8.0
8.1
Alkalinity
(mg/L as CaCO3)
110
110
110
114
114
112
112
112
112
112
113
118
123
129
133
126
124
123
124
117
(X)
-------
The most noticeable change in the distribution water samples after system startup was decreases in
arsenic concentration at all three locations. Baseline arsenic concentrations for all three locations ranged
from 25.6 to 36.0 (ig/L and averaged 29.2 (ig/L. After system startup, arsenic concentrations ranged from
<0.1 to 1.7 (ig/L and averaged 0.8 (ig/L (excluding one outlier at 7.3 (ig/L on April 4, 2007) in Purvine
Hall and ranged from <0.1 to 1.4 (ig/L and averaged 0.6 (ig/L (excluding one outlier at 3.6 (ig/L on March
8, 2007) in the College Union. Distribution system water samples in the Residence Hall essentially
mirrored ARM 200 system effluent (although arsenic concentrations in the distribution system water
samples taken during the first several months of system operation were, in general, higher than those in
the system efflent, suggesting resuspension, solublization, and/or desorption of arsenic-laden
particles/scales in the distribution system). Arsenic concentrations exceeded the 10 (ig/L MCL on
December 13, 2006 and January 10, 2007, before the lead vessel was rebedded with ARM 300 on January
24, 2007.
Post-baseline lead concentrations ranged from <0.1 to 1.6 (ig/L, with none of the samples exceeding the
action level of 15 (ig/L. Post-baseline copper concentrations ranged from 39.7 to 448 (ig/L across all
sampling locations, with no sample exceeding the 1,300 (ig/L action level. The arsenic treatment systems
do not seem to affect lead or copper concentrations in the distribution system.
Measured pH values ranged from 7.5 to 8.1 and averaged 7.9 at all three locations. Alkalinity levels
ranged from 104 to 137 mg/L (as CaCO3). The arsenic treatment systems do not seem to affect these
water quality parameters in the distribution system.
4.5.8 Spent Media Sampling. Three ARM 200 spent media samples were collected from the top,
middle, and bottom of the lead vessel in the Residence Hall during the media changeout on January 24,
2007. Tables 4-25 and 4-26 present metals and TCLP results, respectively. Arsenic, barium, and
chromium were detected at concentrations slightly higher than their respective detection limit. The other
TCLP metals were less than the respective MDLs. Because the media passed the TCLP test, it can be
disposed of as non-hazardous waste.
The ICP-MS results of the spent media indicated that the media contained mostly iron at 569 mg (as Fe)/g
of dry media or 56.9% by weight. The chemical formula that best represents the iron media was not
available from the product literature. The spent media also contained trace levels of Al, Ca, Cu, Mg, Mn,
P, and Si at 0.58, 11.8, 0.65, 1.0, 1.7, 0.54, and 0.42 mg/g, respectively. Some of these elements were
detected in inlet water and apparently were removed by ARM 200 media. The spent media also removed
some Al, Cu, Pb, and Zn from inlet water, as evidenced by the decreasing loadings from the top to the
bottom of the media bed. It is not clear what mechanisms were involved in the removal of these cations.
The arsenic loading on the spent media based on the ICP-MS results was 0.83 mg/g (average across bed
from Table 4-25). For comparison to the spent media results, the adsorptive capacity was calculated by
dividing the arsenic mass removed by the amount of dry media in the lead vessel. The arsenic mass
removed was estimated by multiplying the average throughput to the 10-(ig/L breakthrough (15,490 BV,
see Table 4-21) by the average arsenic level in inlet water (29.7 ug/L). The dry weight of the media, i.e.,
874 Ib, was calculated based on a wet weight of 950 Ib (i.e., 20 ft3 of media at 47.5 lb/ft3) and a moisture
content of 8% (Table 4-3). Using this approach, the arsenic loading for the spent media was 0.66 mg/g of
dry media. The ICP-MS analysis appeared to over-recover by 26%.
4.6 System Cost
The system cost was evaluated based on the capital cost per gpm (or gpd) of the design capacity and the
O&M cost per 1,000 gal of water treated. Capital cost for the treatment system included the expenditure
for equipment, site engineering, and system installation, shakedown, and startup. O&M cost included the
68
-------
Table 4-25. ARM 200 Media Metals Results
Metals
Aluminum
Arsenic
Cadmium
Calcium
Copper
Iron
Lead
Magnesium
Manganese
Nickel
Phosphorus
Silica
Zinc
Unit
VS/S
vs/s
vs/s
vs/s
vs/s
vs/s
vs/s
ng/g
vs/s
vs/s
ng/g
vs/s
vs/s
Sampling Location
Top
1,191
1,244
854
926
<0.5
<0.5
12,098
13,056
1,806
1,871
403,334
436,097
11.9
12.8
943
1,009
1,745
1,880
130
143
570
603
463
498
724
765
Middle
175
143
825
837
<0.5
<0.5
11,652
11,925
71.6
73.6
403,582
413,431
5.9
6.4
927
941
1,692
1,711
146
151
514
548
423
472
196
208
Bottom
320
396
779
726
<0.5
<0.5
11322
10617
45.3
41.6
407,958
378,185
3.8
3.5
1231
1171
1702
1587
126
116
487
488
382
293
133
123
Table 4-26. Spent Media TCLP Results
Analyte
Concentration (mg/L)
As
0.18
Ba
0.84
Cd
< 0.010
Cr
0.012
Pb
< 0.050
Hg
< 0.0020
Se
<0.10
Ag
< 0.010
expenditure for media replacement and labor. The cost associated with the plumbing modification was
not included in the capital cost because it was out of the scope of the demonstration project, and was
funded separately by OIT.
4.6.1 Capital Cost. The total capital investment for the Kinetico POE systems and POU units was
$198,958, which included $142,448 (71.6%) for equipment, $33,560 (16.9%) for site engineering, and
$22,950 (11.5%) for installation. Table 4-27 presents cost breakdowns provided by the vendor. The
equipment cost was broken down for major cost components such as adsorptive media, filter vessels,
hydropneumatic tank, process valves and piping, labor, and shipping for each system.
The site engineering cost included the cost for preparing a process design report and required engineering
plans, including a general arrangement drawing, piping and instrumentation diagram (P&ID), inter-
connecting piping layouts, tank fill details, and other associated drawings. After being certified and
stamped by an Oregon-registered professional engineer, the plans were submitted to Oregon DHS for
permit review and approval.
69
-------
Table 4-27. Capital Investment Cost for Kinetico POE/POU Treatment Systems
Description
Quantity
Cost
% of Capital
Investment Cost
Equipment Cost
30-gpm ArsenXnp System in Purvine Hall
Fiberglass Adsorption Tanks & Internals
ArsenXnp Media
132-gal Hydropneumatic Tank
Process Valve and Piping
Additional Sample Taps/Totalizer/Meters
Subtotal
2
20ft3
1
1
1
-
$6,901
$12,728
$4,246
$5,597
$7,465
$36,937
-
-
-
-
60-gpm ARM 200/ARM 300/E33-S System in Residence Hall
Fiberglass Adsorption Tanks & Internals
ARM 200 Media
132-gal Hydropneumatic Tank
Process Valve and Piping
Additional Sample Taps/Totalizer/Meters
Subtotal
2
40ft3
1
1
1
-
$7,237
$20,002
$4,246
$3,543
$4,349
$39,377
-
-
-
-
60-gpm Adsorbsia™ GTO™ System in College Union
Fiberglass Adsorption Tanks & Internals
Adsorbsia Media
132-gal Hydropneumatic Tank
Process Valve and Piping
Additional Sample Taps/Totalizer/Meters
Subtotal
2
40ft3
1
1
1
-
$7,237
$29,093
$4,246
$3,543
$4,349
$48,468
-
-
-
-
POU Units
Kinetico POU Cartridges
AdEdge POU Cartridges
Subtotal
Shipping
Labor
Equipment Total
8
48
-
-
-
-
$1,216
$9,120
$10,336
$4,250
$3,080
$142,448
PaidbyOIT
-
71.6%
Engineering Cost
Vendor Labor
Vendor Travel
Subcontractor Labor
System Startup Vendor Labor
System Startup Vendor Travel
Site Engineering Total
-
-
-
$20,760
$2,150
$3,000
$5,500
$2,150
$33,560
-
16.9%
Installation Cost(a>
Vendor Labor
Vendor Travel
Subcontractor Labor
Installation Total
Total Capital Investment
-
-
-
-
-
$3,300
$1,650
$18,000
$22,950
$198,958
-
-
-
11.5%
100%
(a) Not including cost for installing 48 AdEdge POU units.
The installation cost included labor and materials for system unloading and anchoring, plumbing,
mechanical connections, media loading, system startup and shakedown, and operator's training (see
Section 4.3).
70
-------
To calculate the normalized capital cost based on the design capacity of each POE system, the composite
engineering cost and installation cost provided by the vendor were broken down proportionally for each
system based on the ratio calculated from their equipment cost breakdown. The rearranged cost
breakdowns for each POE system are summarized in Table 4-28.
Table 4-28. Rearranged Capital Investment Cost for Each Kinetico POE System
Location
Purvine Hall
Residence Hall
College Union
POE System
30-gpm ArsenXnp
60-gpm ARM 200
60-gpm Adsorbsia™
GTO™
Total
Capital Cost
Equipment'3'
$39,108
$41,689
$51,314
$132,111
Engineering
$9,941
$10,587
$13,032
$33,560
Installation
$6,798
$7,240
$8,912
$22,950
Total
$55,847
$59,516
$73,258
$188,621
(a) Including shipping and labor cost.
4.6.1.1 ArsenX"p System. The capital cost of $55,847 was normalized to $l,862/gpm ($1.29/gpd) of
design capacity using the system's rated capacity of 30 gpm (or 43,200 gpd). The capital cost also was
converted to an annualized cost of $5,271/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/wk, and
365 day/yr at the design flowrate of 30 gpm, the unit capital cost would be $0.33/1,000 gal. During the
system performance evaluation, the system treated an average of 489,480 gal/yr (see Table 4-12); at this
reduced rate of usage, the unit capital cost increased to $10.77/1,000 gal.
4.6.1.2 ARM200 System. The capital cost of $59,516 was normalized to $992/gpm ($0.69/gpd) of
design capacity using the system's rated capacity of 60 gpm (or 86,400 gpd). The capital cost also was
converted to an annualized cost of $5,618/yr using a 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/wk, and 365 day/yr at the design
flowrate of 60 gpm, the unit capital cost would be $0.18/1,000 gal. The system was operated on demand,
producing 6,698,103 gal of water in 406 days during the ARM 200 test (see Table 4-12). At this reduced
rate of operation (i.e., 6,021,694 gal/yr), the unit capital cost increased to $0.93/1,000 gal.
4.6.1.3 Adsorbsia™ GTO™ System. The capital cost of $73,258 was normalized to $l,221/gpm
($0.85/gpd) of design capacity using the system's rated capacity of 60 gpm (or 86,400 gpd). The capital
cost also was converted to an annualized cost of $6,915/yr using a 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/wk, and 365 day/yr at
the design flowrate of 60 gpm, the unit capital cost would be $0.22/1,000 gal. During the evaluation
study, the system produced 5,889,749 gal of water in 1,286 days (or 1,671,663 gal/yr; see Table 4-12); at
this reduced rate of usage, the unit capital cost increased to $4.14/1,000 gal.
4.6.2 Operation and Maintenance Cost. The O&M cost included the cost for replacing media
and the cost of labor to operate the systems, as summarized in Table 4-29 for the three POE systems.
Media replacement is a major cost for operating an adsorptive media system. According to vendor
estimates, it would cost $11,900 to replace 20 ft3 of ArsenXnp, $18,700 to replace 40 ft3 of ARM 200,
$12,000 to replace 40 ft3 of E33-S, and $27,100 to replace 40 ft3 of Adsorbsia™ GTO™. Therefore, the
unit cost from the lowest to the highest would be $300/ft3 for E33-S, $468/ft3 for ARM 200, $595/ft3 for
ArsenXnp, and $678/ft3for Adsorbsia™ GTO™. These estimates do not include the cost for labor, travel,
freight, spent media analysis, and media disposal. These costs are expected to be similar regardless of the
media type.
71
-------
Table 4-29. Operation and Maintenance Cost for POE systems
POE Location
Purvine
Hall
Residence Hall
College Union
Media Replacement Costa)(b)
Media Type
Media Volume (ft3)
Media Cost ($)
Media Unit Cost ($/ft3)
Normalized Media Cost ($71,000 gal)
ArsenXnp
20
$11,900
$595
ARM 200
40
$18,700
$468
E33-S
40
$12,000
$300
Adsorbsia™ GTO™
40
$27,100
$678
See Figure 4-36
Labor Cost
Average Weekly Labor (hr/wk)
Average Annual Labor (hr/yr)
Labor Rate ($/hr)
Annual Labor Cost ($/yr)
Annual Throughput (gal/yr)
Unit Labor Cost ($71,000)
2.5
130
$21
$2,730
489,480
$5.58
2.5
130
$21
$2,730
6,021,694
$0.45
2.5
130
$21
$2,730
6,410,130
$0.43
2.5
130
$21
$2,730
1,671,662
$1.63
(a) Cost for labor, travel, freight, spent media analysis, and media disposal fee not included in quote,
but expected to be similar regardless of media type.
(b) Media quote provided by Kinetio in August 2005 except for E33-S, which was provided by a local
vendor.
Based on the actual cost incurred to replace 20 ft3 of ARM 200 at the Residence Hall in February 2007,
the media cost was $7,700 and the labor and travel cost for emptying one vessel, disposing spent media,
and reloading the new media was $3,500. The labor cost could be less if a local vendor was hired for the
job with the assistance of the operator. To help select the most cost-effective media, a cost curve was
constructed for each media type in terms of media cost per 1,000 gal of water treated as a function of the
projected media run length to the 10-|o,g/L arsenic breakthrough (Figure 4-28). For example, the average
ARM 200 media run length at the Residence Hall was 13,490 BV (Table 4-21), so the media cost based
on Figure 4-28 was approximately $4/1,000 gal. The actual media replacement cost incurred was
$11,200, which translated to $5.55/1,000 gal.
Under normal conditions, routine labor activities to operate and maintain each POE system consumed 30
min per day on average, or 2.5 hr for a five-day week. Based on this time commitment and a labor rate of
$21/hr, the annual labor cost was estimated to be $2,730 to operate each POE system. Depending on the
annual water production of each POE system, the normalized labor cost was $5.58/1,000 gal for the
Purvine Hall system and $1.63/1,000 gal for the College Union system. At Residence Hall, the estimated
labor cost was similar for the ARM 200 and E33-S media runs, which was $0.45/1,000 gal and
$0.43/1,000 gal, respectively.
72
-------
E33-S
ARM 200
ArsenXnp
Adsorbsia™GTO™
» $7.00 H
M
O
10 20 30 40 50 60 70
Media Working Capacity, Bed Volumes (xlOOO)
80
90
100
Figure 4-28. Media Replacement Cost Curves for POE System
73
-------
5.0 REFERENCES
Battelle. 2004. Revised 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 at Oregon Institute of Technology at Klamath Falls, OR. 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.
Chen, A.S.C., J.P. Lipps, R.J. Stowe, B.J. Yates, V. Lai, and L. Wang. 2010. Arsenic Removal from
Drinking Water by Adsorptive Media, U. S. EPA Demonstration at LEADS Head Start Building in
Buckeye Lake, OH, Final performance Evaluation Report. Prepared under Contract No. 68-C-OO-
185, Task Order No. 0029, for U.S. Environmental Protection Agency, National Risk
Management Research Laboratory, Cincinnati, OH.
Chen, A.S.C., L. Wang, J.L. Oxenham, and W.E. Condit. 2004. Capital Costs of Arsenic Removal
Technologies: U.S. EPA Arsenic Removal Technology Demonstration Program Round 1.
EPA/600/R-04/201. U.S. Environmental Protection Agency, National Risk Management
Research Laboratory, Cincinnati, OH.
Edwards, M., S. Patel, L. McNeill, H. Chen, M. Frey, A.D. Eaton, R.C. Antweiler, and H.E. Taylor.
1998. "Considerations in As Analysis and Speciation." JAWWA, 91: 103-113.
EPA. 2001. National Primary Drinking Water Regulations: Arsenic and Clarifications to Compliance
and New Source Contaminants Monitoring. Fed. Register, 66:14:6975.
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. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic.
Federal Register, 40 CFRPart 141.
Wang, L., W.E. Condit, and A.S.C. Chen. 2004. Technology Selection and System Design: U.S. EPA
Arsenic Removal Technology Demonstration Program Round 1. EPA/600/R-05/001. U.S.
Environmental Protection Agency, National Risk Management Research Laboratory, Cincinnati,
OH.
Westerhoff, Paul. 2007. Rapid Small Scale Column Tests: Arsenic Removal from Ground water from
Klamath Falls, OR. Prepared by Arizona State University, Tempe, AZ.
74
-------
APPENDIX A
OPERATIONAL DATA
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet
Week
No.
1
2
3
4
5
6
7
8
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
12/12/05
12/13/05
12/14/05
12/15/05
12/16/05
12/19/05
12/20/05
12/21/05
12/22/05
12/23/05
12/27/05
12/28/05
12/29/05
01/03/06
01/04/06
01/05/06
01/06/06
01/09/06
01/10/06
01/11/06
01/12/06
01/13/06
01/17/06
01/18/06
01/19/06
01/20/06
01/23/06
01/24/06
01/25/06
01/26/06
01/27/06
01/30/06
01/31/06
02/01/06
02/02/06
02/03/06
Time
7:50
8:00
13:45
11:30
9:00
15:05
8:40
8:10
8:40
8:15
8:55
22:20
22:15
10:00
16:04
8:30
15:00
9:10
15:00
13:40
15:17
8:35
11:50
14:00
12:15
12:15
16:10
9:07
10:30
9:50
8:15
10:40
10:00
8:05
7:42
11:45
Treatment System
Train 1
Flow
Rate
gpm
15 Test
2
0
0
0
15 Test
0
0
0
0
0
0
0
0
1 3. 5 Test
0
0
0
0
1
0
0
0
2
0
0
0
13 Test
0
0
0
0
2
5 Test
4
0.5
Totalizer
gal
3,521
4,026
4,591
5,029
5,590
7,039
7,542
7,906
8,408
8,834
10,389
10,780
11,566
16,085
16,543
16,984
17,382
18,785
19,692
20,573
21,600
22,050
24,218
25,198
25,802
26,500
28,195
28,600
29,492
30,190
30,854
32,545
33,324
33,930
35,135
35,387
Daily
Water
Treated
gal
NA
505
565
438
561
1,449
503
364
502
426
1,555
391
786
4,519
458
441
398
1,403
907
881
1,027
450
2,168
980
604
698
1,695
405
892
698
664
1,691
779
606
1,205
252
Cum.
Throughput
gal
NA
505
1,070
1,508
2,069
3,518
4,021
4,385
4,887
5,313
6,868
7,259
8,045
12,564
13,022
13,463
13,861
15,264
16,171
17,052
18,079
18,529
20,697
21,677
22,281
22,979
24,674
25,079
25,971
26,669
27,333
29,024
29,803
30,409
31,614
31,866
Bed
Volume
#BV
NA
14
29
40
55
94
107
117
131
142
184
194
215
336
348
360
371
408
432
456
483
495
553
580
596
614
660
670
694
713
731
776
797
813
845
852
Train 2
Flow
Rate
gpm
15 Test
2
0
0
0
15 Test
0
0
0
0.5
0
0
0
0
1.5 Test
0
0
0
0
1
0
0
0
2
0
0
0
15 Test
0
0
0
0
2
12 Test
3
0.5
Totalizer
gal
3,691
4,276
4,932
5,550
6,008
7,768
8,220
9,018
9,972
10,820
13,113
13,688
14,744
20,693
21,322
21,781
22,480
24,485
25,846
26,925
28,654
29,072
32,342
33,671
34,472
35,354
37,948
38,720
39,980
41,092
42,081
44,564
45,690
46,630
48,100
48,240
Daily
Water
Treated
gal
MA
585
656
618
458
1,760
452
798
954
848
2,293
575
1,056
5,949
629
459
699
2,005
1,361
1,079
1,729
418
3,270
1,329
801
882
2,594
772
1,260
1,112
989
2,483
1,126
940
1,470
140
Cum.
Throughput
gal
NA
585
1,241
1,859
2,317
4,077
4,529
5,327
6,281
7,129
9,422
9,997
11,053
17,002
17,631
18,090
18,789
20,794
22,155
23,234
24,963
25,381
28,651
29,980
30,781
31,663
34,257
35,029
36,289
37,401
38,390
40,873
41,999
42,939
44,409
44,549
Bed
Volume
#BV
NA
16
33
50
62
109
121
142
168
191
252
267
295
455
471
484
502
556
592
621
667
679
766
801
823
846
916
936
970
1,000
1,026
1,093
1,123
1,148
1,187
1,191
Train2-Train1
Daily
Water
Treated
gal
NA
80
91
180
(103)
311
(51)
434
452
422
738
184
270
1,430
171
18
301
602
454
198
702
(32)
1,102
349
197
184
899
367
368
414
325
792
347
334
265
(112)
Cum.
Throughput
gal
80
171
351
248
559
508
942
1,394
1,816
2,554
2,738
3,008
4,438
4,609
4,627
4,928
5,530
5,984
6,182
6,884
6,852
7,954
8,303
8,500
8,684
9,583
9,950
10,318
10,732
11,057
11,849
12,196
12,530
12,795
12,683
Bed
Volume
#BV
2
5
9
7
15
14
25
37
49
68
73
80
119
123
124
132
148
160
165
184
183
213
222
227
232
256
266
276
287
296
317
326
335
342
339
Combined
Total
Flow
gpm
30 Test
4
0
0
0
30 Test
0
0
0
1
0
0
0
0
28 Test
0
0
0
0
2
0
0
0
4
0
0
0
27 Test
0
0
0
0
4
17 Test
7
1
Cum.
Throughput
gal
NA
1,090
2,311
3,367
4,386
7,595
8,550
9,712
11,168
12,442
16,290
17,256
19,098
29,566
30,653
31,553
32,650
36,058
38,326
40,286
43,042
43,910
49,348
51,657
53,062
54,642
58,931
60,108
62,260
64,070
65,723
69,897
71,802
73,348
76,023
76,415
Bed
Volume
#BV
NA
15
31
45
59
102
114
130
149
166
218
231
255
395
410
422
436
482
512
539
575
587
660
691
709
730
788
803
832
856
879
934
960
980
1,016
1,021
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
9
10
11
12
13
14
15
16
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
02/06/06
02/07/06
02/08/06
02/09/06
02/10/06
02/13/06
02/14/06
02/17/06
02/20/06
02/21/06
02/22/06
02/23/06
02/24/06
02/27/06
02/28/06
03/01/06
03/02/06
03/03/06
03/06/06
03/07/06
03/08/06
03/09/06
03/10/06
03/13/06
03/14/06
03/15/06
03/16/06
03/17/06
03/20/06
03/21/06
03/22/06
03/23/06
03/24/06
03/27/06
03/28/06
03/29/06
03/30/06
03/31/06
Time
10:46
8:19
7:45
8:09
11:15
9:24
9:48
8:19
8:30
13:50
8:57
7:50
8:00
8:50
9:10
10:20
7:55
11:15
8:50
8:28
9:05
8:15
10:14
9:00
9:25
8:13
8:00
9:00
9:10
8:15
9:40
13:40
8:35
8:33
13:05
12:15
15:00
9:05
Treatment System
Train 1
Flow
Rate
gpm
1
0
0
0
8.5 Test
0.5
2.5
4
1
1
8
3
4
1
1
9
7
1
2
2
2
2
1
1
0
0.5
3
1
0
0
2
0
0
0
0
0
7.5
7.5
Totalizer
gal
38,243
39,183
40,136
41,075
42,050
43,835
44,855
47,512
49,402
50,575
51,220
52,210
53,025
55,030
56,090
57,001
58,031
59,051
60,971
62,074
62,934
63,920
64,805
66,800
68,002
68,808
69,868
70,812
72,812
73,606
74,364
75,172
75,670
77,140
77,700
78,252
78,880
79,390
Daily
Water
Treated
gal
2,856
940
953
939
975
1,785
1,020
2,657
1,890
1,173
645
990
815
2,005
1,060
911
1,030
1,020
1,920
1,103
860
986
885
1,995
1,202
806
1,060
944
2,000
794
758
808
498
1,470
560
552
628
510
Cum.
Throughput
gal
34,722
35,662
36,615
37,554
38,529
40,314
41,334
43,991
45,881
47,054
47,699
48,689
49,504
51,509
52,569
53,480
54,510
55,530
57,450
58,553
59,413
60,399
61,284
63,279
64,481
65,287
66,347
67,291
69,291
70,085
70,843
71,651
72,149
73,619
74,179
74,731
75,359
75,869
Bed
Volume
#BV
928
953
979
1,004
1,030
1,078
1,105
1,176
1,227
1,258
1,275
1,302
1,323
1,377
1,405
1,430
1,457
1,485
1,536
1,565
1,588
1,615
1,638
1,692
1,724
1,745
1,774
1,799
1,852
1,874
1,894
1,916
1,929
1,968
1,983
1,998
2,015
2,028
Train 2
Flow
Rate
gpm
1
0
0
0
i.5 Test
0.5
5.5
4
1
1
8
3
2
1
1
9
7
1
2
2
2
2
1
1
0
1
3
1
0
0
2
0
0
0
0
0
7.5
7.5
Totalizer
gal
51,347
52,370
53,410
54,432
55,515
57,361
58,435
61,222
63,175
64,418
65,100
66,115
66,958
69,012
70,071
71,150
72,255
73,352
75,560
76,532
77,460
78,510
79,455
81,561
82,850
83,709
84,827
85,842
87,942
88,792
89,600
90,458
90,968
92,502
93,082
93,654
94,322
94,848
Daily
Water
Treated
gal
3,107
1,023
1,040
1,022
1,083
1,846
1,074
2,787
1,953
1,243
682
1,015
843
2,054
1,059
1,079
1,105
1,097
2,208
972
928
1,050
945
2,106
1,289
859
1,118
1,015
2,100
850
808
858
510
1,534
580
572
668
526
Cum.
Throughput
gal
47,656
48,679
49,719
50,741
51,824
53,670
54,744
57,531
59,484
60,727
61,409
62,424
63,267
65,321
66,380
67,459
68,564
69,661
71,869
72,841
73,769
74,819
75,764
77,870
79,159
80,018
81,136
82,151
84,251
85,101
85,909
86,767
87,277
88,811
89,391
89,963
90,631
91,157
Bed
Volume
#BV
1,274
1,301
1,329
1,357
1,385
1,435
1,464
1,538
1,590
1,623
1,642
1,669
1,691
1,746
1,775
1,803
1,833
1,862
1,921
1,947
1,972
2,000
2,026
2,082
2,116
2,139
2,169
2,196
2,252
2,275
2,297
2,320
2,333
2,374
2,390
2,405
2,423
2,437
Train2-Train1
Daily
Water
Treated
gal
251
83
87
83
108
61
54
130
63
70
37
25
28
49
(1)
168
75
77
288
(131)
68
64
60
111
87
53
58
71
100
56
50
50
12
64
20
20
40
16
Cum.
Throughput
gal
12,934
13,017
13,104
13,187
13,295
13,356
13,410
13,540
13,603
13,673
13,710
13,735
13,763
13,812
13,811
13,979
14,054
14,131
14,419
14,288
14,356
14,420
14,480
14,591
14,678
14,731
14,789
14,860
14,960
15,016
15,066
15,116
15,128
15,192
15,212
15,232
15,272
15,288
Bed
Volume
#BV
346
348
350
353
355
357
359
362
364
366
367
367
368
369
369
374
376
378
385
382
384
386
387
390
392
394
395
397
400
401
403
404
404
406
407
407
408
409
Combined
Total
Flow
gpm
2
0
0
0
17 Test
1
8
8
2
2
16
6
6
2
2
18
14
2
4
4
4
4
2
2
0
2
6
2
0
0
4
0
0
0
0
0
15
15
Cum.
Throughput
gal
82,378
84,341
86,334
88,295
90,353
93,984
96,078
101,522
105,365
107,781
109,108
111,113
112,771
116,830
118,949
120,939
123,074
125,191
129,319
131,394
133,182
135,218
137,048
141,149
143,640
145,305
147,483
149,442
153,542
155,186
156,752
158,418
159,426
162,430
163,570
164,694
165,990
167,026
Bed
Volume
#BV
1,101
1,127
1,154
1,180
1,208
1,256
1,284
1,357
1,408
1,441
1,458
1,485
1,507
1,562
1,590
1,617
1,645
1,673
1,729
1,756
1,780
1,807
1,832
1,887
1,920
1,942
1,971
1,998
2,052
2,074
2,095
2,118
2,131
2,171
2,186
2,201
2,219
2,233
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
17
18
19
20
21
22
23
24
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
04/03/06
04/04/06
04/05/06
04/06/06
04/07/06
04/10/06
04/11/06
04/12/06
04/13/06
04/14/06
04/17/06
04/18/06
04/19/06
04/20/06
04/21/06
04/24/06
04/25/06
04/26/06
04/27/06
04/28/06
05/01/06
05/02/06
05/03/06
05/04/06
05/05/06
05/08/06
05/09/06
05/10/06
05/11/06
05/12/06
05/15/06
05/16/06
05/17/06
05/18/06
05/19/06
05/22/06
05/23/06
05/24/06
05/25/06
05/26/06
Time
9:40
9:00
8:10
11:03
8:10
8:15
8:20
9:22
7:55
8:30
8:45
8:10
8:30
8:10
13:52
9:10
8:30
11:35
14:17
8:20
9:00
8:15
10:15
10:00
8:35
8:26
9:03
15:21
7:23
7:45
8:40
9:00
14:15
15:30
14:35
10:55
10:00
9:30
13:50
9:18
Treatment System
Train 1
Flow
Rate
gpm
2
12
9
8.5
7.5
11
4
8.5
2
6.5
9.5
3
5
3
9
5
4
8.5
1
1
4
10.5
0
2
4
4
11.5
2
0
0
4
7
2
1
0
0
0
0
0
1
Totalizer
gal
81,812
83,100
84,040
86,870
87,671
91,000
92,534
94,565
95,935
97,381
100,565
102,290
103,985
105,400
107,670
110,386
111,800
113,770
115,810
117,990
119,770
121,728
123,728
124,824
125,380
128,738
130,802
133,330
133,400
134,625
138,420
140,108
141,500
142,445
143,412
145,210
146,310
147,130
148,750
148,970
Daily
Water
Treated
gal
2,422
1,288
940
2,830
801
3,329
1,534
2,031
1,370
1,446
3,184
1,725
1,695
1,415
2,270
2,716
1,414
1,970
2,040
2,180
1,780
1,958
2,000
1,096
556
3,358
2,064
2,528
70
1,225
3,795
1,688
1,392
945
967
1,798
1,100
820
1,620
220
Cum.
Throughput
gal
78,291
79,579
80,519
83,349
84,150
87,479
89,013
91,044
92,414
93,860
97,044
98,769
100,464
101,879
104,149
106,865
108,279
110,249
112,289
114,469
116,249
118,207
120,207
121,303
121,859
125,217
127,281
129,809
129,879
131,104
134,899
136,587
137,979
138,924
139,891
141,689
142,789
143,609
145,229
145,449
Bed
Volume
#BV
2,093
2,127
2,153
2,228
2,250
2,339
2,380
2,434
2,471
2,509
2,594
2,641
2,686
2,724
2,784
2,857
2,895
2,947
3,002
3,060
3,108
3,160
3,214
3,243
3,258
3,348
3,403
3,470
3,472
3,505
3,606
3,652
3,689
3,714
3,740
3,788
3,817
3,839
3,883
3,888
Train 2
Flow
Rate
gpm
2
12
9
8.5
7.5
11
4
8.5
2
6.5
9.5
3
5
3
9
5
4
8.5
1
1
4
10.5
0
2
4
4
11.5
2
0
0
4
7
2
1
0
0
0
0
0
1
Totalizer
gal
97,360
98,710
99,685
102,610
103,430
106,909
108,512
110,631
112,048
113,550
116,865
118,920
120,355
121,860
124,182
126,986
128,433
130,465
132,570
134,747
136,660
138,005
140,705
141,390
142,385
145,877
148,005
150,580
150,650
151,980
155,832
157,585
159,190
160,078
161,065
162,800
164,018
165,190
166,030
166,790
Daily
Water
Treated
gal
2,512
1,350
975
2,925
820
3,479
1,603
2,119
1,417
1,502
3,315
2,055
1,435
1,505
2,322
2,804
1,447
2,032
2,105
2,177
1,913
1,345
2,700
685
995
3,492
2,128
2,575
70
1,330
3,852
1,753
1,605
888
987
1,735
1,218
1,172
840
760
Cum.
Throughput
gal
93,669
95,019
95,994
98,919
99,739
103,218
104,821
106,940
108,357
109,859
113,174
115,229
116,664
118,169
120,491
123,295
124,742
126,774
128,879
131,056
132,969
134,314
137,014
137,699
138,694
142,186
144,314
146,889
146,959
148,289
152,141
153,894
155,499
156,387
157,374
159,109
160,327
161,499
162,339
163,099
Bed
Volume
#BV
2,504
2,540
2,566
2,645
2,666
2,759
2,802
2,859
2,897
2,937
3,026
3,081
3,119
3,159
3,221
3,296
3,335
3,389
3,446
3,504
3,555
3,591
3,663
3,681
3,708
3,801
3,858
3,927
3,929
3,964
4,067
4,114
4,157
4,181
4,207
4,254
4,286
4,318
4,340
4,360
Train2-Train1
Daily
Water
Treated
gal
90
62
35
95
19
150
69
88
47
56
131
330
(260)
90
52
88
33
62
65
(3)
133
(613)
700
(411)
439
134
64
47
0
105
57
65
213
(57)
20
(63)
118
352
(780)
540
Cum.
Throughput
gal
15,378
15,440
15,475
15,570
15,589
15,739
15,808
15,896
15,943
15,999
16,130
16,460
16,200
16,290
16,342
16,430
16,463
16,525
16,590
16,587
16,720
16,107
16,807
16,396
16,835
16,969
17,033
17,080
17,080
17,185
17,242
17,307
17,520
17,463
17,483
17,420
17,538
17,890
17,110
17,650
Bed
Volume
#BV
411
413
414
416
417
421
423
425
426
428
431
440
433
436
437
439
440
442
444
443
447
431
449
438
450
454
455
457
457
459
461
463
468
467
467
466
469
478
457
472
Combined
Total
Flow
gpm
4
24
18
17
15
22
8
17
4
13
19
6
10
6
18
10
8
17
2
2
8
21
0
4
8
8
23
4
0
0
8
14
4
2
0
0
0
0
0
2
Cum.
Throughput
gal
171,960
174,598
176,513
182,268
183,889
190,697
193,834
197,984
200,771
203,719
210,218
213,998
217,128
220,048
224,640
230,160
233,021
237,023
241,168
245,525
249,218
252,521
257,221
259,002
260,553
267,403
271,595
276,698
276,838
279,393
287,040
290,481
293,478
295,311
297,265
300,798
303,116
305,108
307,568
308,548
Bed
Volume
#BV
2,299
2,334
2,359
2,436
2,458
2,549
2,591
2,646
2,684
2,723
2,810
2,861
2,902
2,941
3,003
3,077
3,115
3,168
3,224
3,282
3,331
3,375
3,438
3,462
3,483
3,574
3,630
3,699
3,701
3,735
3,837
3,883
3,923
3,947
3,974
4,021
4,052
4,078
4,111
4,124
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
25
26
27
28
29
30
31
32
Day of
Week
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Tue
Wed
Thu
Fri
Date
05/30/06
05/31/06
06/01/06
06/02/06
06/05/06
06/06/06
06/07/06
06/08/06
06/09/06
06/12/06
06/13/06
06/14/06
06/15/06
06/16/06
06/19/06
06/20/06
06/21/06
06/22/06
06/23/06
06/26/06
06/27/06
06/28/06
06/29/06
06/30/06
07/03/06
07/05/06
07/06/06
07/07/06
07/10/06
07/11/06
07/12/06
07/1 3/06
07/19/06
07/20/06
07/21/06
07/22/06
Time
8:00
8:40
4:05
7:30
2:42
7:15
8:14
2:15
10:24
8:53
8:10
8:16
8:28
8:35
10:30
8:20
8:00
7:55
8:10
11:00
11:50
9:30
8:35
9:32
14:04
10:48
8:24
8:11
7:20
7:25
8:30
7:45
14:10
10:35
10:00
8:00
Treatment System
Train 1
Flow
Rate
gpm
8
6
0
2
7.5
0
12
0
2
4.4
4
0
4.4
4
1
4
7
3
4
2
1
9.5
4
0
1
0
4
4
0
2
5
0
1
2
1
4
Totalizer
gal
152,065
153,605
155,600
156,370
160,450
161,720
162,970
164,935
166,143
169,633
170,875
172,280
173,300
174,400
177,630
178,595
181,345
181,422
181,500
185,730
186,800
187,870
188,912
190,200
193,040
195,100
195,950
197,180
200,275
201,390
202,612
203,685
209,980
210,756
211,620
212,700
Daily
Water
Treated
gal
3,095
1,540
1,995
770
4,080
1,270
1,250
1,965
1,208
3,490
1,242
1,405
1,020
1,100
3,230
965
2,750
77
78
4,230
1,070
1,070
1,042
1,288
2,840
2,060
850
1,230
3,095
1,115
1,222
1,073
6,295
776
864
1,080
Cum.
Throughput
gal
148,544
150,084
152,079
152,849
156,929
158,199
159,449
161,414
162,622
166,112
167,354
168,759
169,779
170,879
174,109
175,074
177,824
177,901
177,979
182,209
183,279
184,349
185,391
186,679
189,519
191,579
192,429
193,659
196,754
197,869
199,091
200,164
206,459
207,235
208,099
209,179
Bed
Volume
#BV
3,971
4,012
4,066
4,086
4,195
4,229
4,263
4,315
4,348
4,441
4,474
4,512
4,539
4,568
4,655
4,680
4,754
4,756
4,758
4,871
4,900
4,928
4,956
4,991
5,067
5,122
5,144
5,177
5,260
5,290
5,323
5,351
5,520
5,540
5,563
5,592
Train 2
Flow
Rate
gpm
8
6
0
2
7.5
0
12
0
2
4
4
0
4.4
4
1
4
7
3
4
2
1
9.5
4
0
1
0
4
4
1
2
5
0
1
2
1
4
Totalizer
gal
169,890
171,554
173,580
174,365
178,535
179,922
181,100
183,089
184,300
187,829
189,888
190,600
191,715
192,900
196,409
197,235
199,355
200,032
200,610
205,201
206,365
207,520
208,652
210,046
213,130
215,370
216,290
217,625
220,000
222,180
223,522
224,680
231,820
232,345
233,280
234,550
Daily
Water
Treated
gal
3,100
1,664
2,026
785
4,170
1,387
1,178
1,989
1,211
3,529
2,059
712
1,115
1,185
3,509
826
2,120
677
578
4,591
1,164
1,155
1,132
1,394
3,084
2,240
920
1,335
2,375
2,180
1,342
1,158
7,140
525
935
1,270
Cum.
Throughput
gal
166,199
167,863
169,889
170,674
174,844
176,231
177,409
179,398
180,609
184,138
186,197
186,909
188,024
189,209
192,718
193,544
195,664
196,341
196,919
201,510
202,674
203,829
204,961
206,355
209,439
211,679
212,599
213,934
216,309
218,489
219,831
220,989
228,129
228,654
229,589
230,859
Bed
Volume
#BV
4,443
4,488
4,542
4,563
4,674
4,711
4,743
4,796
4,828
4,923
4,978
4,997
5,027
5,058
5,152
5,174
5,231
5,249
5,265
5,387
5,418
5,449
5,480
5,517
5,599
5,659
5,684
5,719
5,783
5,841
5,877
5,908
6,099
6,113
6,138
6,172
Train2-Train1
Daily
Water
Treated
gal
5
124
31
15
90
117
(72)
24
3
39
817
(693)
95
85
279
(139)
(630)
600
500
361
94
85
90
106
244
180
70
105
(720)
1,065
120
85
845
(251)
71
190
Cum.
Throughput
gal
17,655
17,779
17,810
17,825
17,915
18,032
17,960
17,984
17,987
18,026
18,843
18,150
18,245
18,330
18,609
18,470
17,840
18,440
18,940
19,301
19,395
19,480
19,570
19,676
19,920
20,100
20,170
20,275
19,555
20,620
20,740
20,825
21,670
21,419
21,490
21,680
Bed
Volume
#BV
472
475
476
477
479
482
480
481
481
482
504
485
488
490
498
494
477
493
506
516
519
521
523
526
533
537
539
542
523
551
554
557
579
573
575
580
Combined
Total
Flow
gpm
16
12
0
4
15
0
24
0
4
8
8
0
9
8
2
8
14
6
8
4
2
19
8
0
2
0
8
8
1
4
10
0
2
4
2
8
Cum.
Throughput
gal
314,743
317,947
321,968
323,523
331,773
334,430
336,858
340,812
343,231
350,250
353,551
355,668
357,803
360,088
366,827
368,618
373,488
374,242
374,898
383,719
385,953
388,178
390,352
393,034
398,958
403,258
405,028
407,593
413,063
416,358
418,922
421,153
434,588
435,889
437,688
440,038
Bed
Volume
#BV
4,207
4,250
4,304
4,325
4,435
4,470
4,503
4,556
4,588
4,682
4,726
4,754
4,783
4,813
4,903
4,927
4,992
5,003
5,011
5,129
5,159
5,189
5,218
5,254
5,333
5,390
5,414
5,448
5,521
5,566
5,600
5,630
5,809
5,827
5,851
5,882
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
33
34
35
36
37
38
39
40
41
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
07/24/06
07/25/06
07/26/06
07/27/06
07/28/06
07/31/06
08/01/06
08/02/06
08/03/06
08/04/06
08/07/06
08/08/06
08/09/06
08/10/06
08/11/06
08/15/06
08/16/06
08/17/06
08/18/06
08/25/06
08/28/06
08/29/06
08/30/06
08/31/06
09/01/06
09/05/06
09/08/06
09/11/06
09/12/06
09/13/06
09/14/06
09/15/06
09/18/06
09/19/06
09/20/06
09/21/06
09/22/06
Time
9:20
15:00
15:10
15:00
8:00
8:00
7:30
8:05
14:30
8:30
10:34
7:45
14:05
16:55
10:00
8:35
10:00
8:30
8:15
15:55
7:55
7:50
12:20
8::55
7:50
7:55
14:50
9:42
10:04
11:51
11:00
15:00
8:05
7:35
9:00
7:55
8:15
Treatment System
Train 1
Flow
Rate
gpm
4
2
0
0
0
1
1
2
0
4
0
0
0
0
0
4
6
3
0
0
0
0
0
4
2
0
0
4
0
7.5
0
0
0
0
3
0
0
Totalizer
gal
215,770
217,070
218,160
219,350
220,218
223,109
224,530
225,640
227,410
228,400
231,430
232,125
233,010
234,525
235,270
239,500
240,655
241,540
242,739
250,210
252,740
253,730
254,937
255,710
256,730
260,760
264,505
267,340
268,310
269,575
270,555
271,560
274,580
275,630
276,760
277,750
278,770
Daily
Water
Treated
gal
3,070
1,300
1,090
1,190
868
2,891
1,421
1,110
1,770
990
3,030
695
885
1,515
745
4,230
1,155
885
1,199
7,471
2,530
990
1,207
773
1,020
4,030
3,745
2,835
970
1,265
980
1,005
3,020
1,050
1,130
990
1,020
Cum.
Throughput
gal
212,249
213,549
214,639
215,829
216,697
219,588
221,009
222,119
223,889
224,879
227,909
228,604
229,489
231,004
231,749
235,979
237,134
238,019
239,218
246,689
249,219
250,209
251,416
252,189
253,209
257,239
260,984
263,819
264,789
266,054
267,034
268,039
271,059
272,109
273,239
274,229
275,249
Bed
Volume
#BV
5,674
5,709
5,738
5,770
5,793
5,871
5,909
5,938
5,986
6,012
6,093
6,112
6,135
6,176
6,196
6,309
6,340
6,363
6,395
6,595
6,663
6,689
6,721
6,742
6,769
6,877
6,977
7,053
7,079
7,113
7,139
7,166
7,247
7,275
7,305
7,331
7,359
Train 2
Flow
Rate
gpm
4
2
0
0
0
1
1
2
0
4
0
0
0
0
0
4
6
3
0
0
0
0
0
4
2
0
0
4
0
7.5
0
0
0
0
3
0
0
Totalizer
gal
237,800
239,205
240,375
241,660
242,620
245,760
247,020
248,580
250,420
251,500
254,800
255,548
256,300
258,135
259,025
263,555
264,820
265,920
267,080
275,170
277,915
278,985
280,290
281,120
282,225
286,585
290,630
293,700
294,750
296,100
297,165
298,250
301,650
302,660
303,870
304,900
305,600
Daily
Water
Treated
gal
3,250
1,405
1,170
1,285
960
3,140
1,260
1,560
1,840
1,080
3,300
748
752
1,835
890
4,530
1,265
1,100
1,160
8,090
2,745
1,070
1,305
830
1,105
4,360
4,045
3,070
1,050
1,350
1,065
1,085
3,400
1,010
1,210
1,030
700
Cum.
Throughput
gal
234,109
235,514
236,684
237,969
238,929
242,069
243,329
244,889
246,729
247,809
251,109
251,857
252,609
254,444
255,334
259,864
261,129
262,229
263,389
271,479
274,224
275,294
276,599
277,429
278,534
282,894
286,939
290,009
291,059
292,409
293,474
294,559
297,959
298,969
300,179
301,209
301,909
Bed
Volume
#BV
6,259
6,296
6,328
6,362
6,388
6,472
6,505
6,547
6,596
6,625
6,713
6,733
6,753
6,802
6,826
6,947
6,981
7,011
7,042
7,258
7,331
7,360
7,395
7,417
7,446
7,563
7,671
7,753
7,781
7,817
7,846
7,875
7,966
7,993
8,025
8,053
8,071
Train2-Train1
Daily
Water
Treated
gal
180
105
80
95
92
249
(161)
450
70
90
270
53
(133)
320
145
300
110
215
(39)
619
215
80
98
57
85
330
300
235
80
85
85
80
380
(40)
80
40
(320)
Cum.
Throughput
gal
21,860
21,965
22,045
22,140
22,232
22,481
22,320
22,770
22,840
22,930
23,200
23,253
23,120
23,440
23,585
23,885
23,995
24,210
24,171
24,790
25,005
25,085
25,183
25,240
25,325
25,655
25,955
26,190
26,270
26,355
26,440
26,520
26,900
26,860
26,940
26,980
26,660
Bed
Volume
#BV
584
587
589
592
594
601
597
609
611
613
620
622
618
627
631
639
641
647
646
663
668
671
673
675
677
686
694
700
702
705
707
709
719
718
720
721
713
Combined
Total
Flow
gpm
8
4
0
0
0
2
2
4
0
8
0
0
0
0
0
8
12
6
0
0
0
0
0
8
4
0
0
8
0
15
0
0
0
0
6
0
0
Cum.
Throughput
gal
446,358
449,063
451,323
453,798
455,626
461,657
464,338
467,008
470,618
472,688
479,018
480,461
482,098
485,448
487,083
495,843
498,263
500,248
502,607
518,168
523,443
525,503
528,015
529,618
531,743
540,133
547,923
553,828
555,848
558,463
560,508
562,598
569,018
571,078
573,418
575,438
577,158
Bed
Volume
#BV
5,967
6,003
6,033
6,066
6,090
6,171
6,207
6,243
6,291
6,319
6,403
6,422
6,444
6,489
6,511
6,628
6,660
6,687
6,718
6,926
6,997
7,025
7,058
7,080
7,108
7,220
7,324
7,403
7,430
7,465
7,492
7,520
7,606
7,634
7,665
7,692
7,715
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
42
43
44
45
46
47
48
49
50
51
52
53
54
55
56
Day of
Week
Mon
Tue
Wed
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Wed
Wed
Thu
Fri
Mon
Wed
Mon
Thu
Tue
Wed
Fri
Mon
Wed
Mon
Wed
Fri
Mon
Wed
Mon
Wed
Fri
Tue
Tue
Fri
Tue
Wed
Fri
Date
09/25/06
09/26/06
09/27/06
09/29/06
10/02/06
10/03/06
10/04/06
10/05/06
10/06/06
10/10/06
10/11/06
10/12/06
10/13/06
10/18/06
10/25/06
10/26/06
10/27/06
10/30/06
11/01/06
11/05/06
11/07/06
11/14/06
11/15/06
11/17/06
11/20/06
11/22/06
11/27/06
11/29/06
12/01/06
12/04/06
12/06/06
12/11/06
12/13/06
12/15/06
12/19/06
01/02/07
01/05/07
01/09/07
01/10/07
01/12/07
Time
8:30
8:15
11:00
9:00
8:30
8:22
8:25
9:48
9:00
10:05
11:20
15:35
14:55
15:15
11:45
9:55
11:45
10:10
11:30
7:30
9:40
10:00
9:10
11:35
8:30
11:10
8:00
14:25
15:33
8:30
7:50
14:10
10:45
11:10
15:10
9:20
8:45
13:30
10:22
8:55
Treatment System
Train 1
Flow
Rate
gpm
3
1
9
6
0
0
0
6
0
2
0
1
2
0
3
1
2
2
0
0
0
0
0
0
4
0
0
0
12
4
2
0
0
3
0
0
0
0
0
3
Totalizer
gal
281,760
283,200
285,100
287,760
290,270
291,602
292,871
294,862
295,739
299,990
301,680
303,000
304,310
309,880
317,500
318,610
319,980
323,900
326,300
330,772
334,920
339,774
341,085
344,750
347,320
350,040
354,370
357,090
361,710
363,820
365,570
368,850
369,950
371,280
373,370
380,410
382,130
383,970
384,700
385,730
Daily
Water
Treated
gal
2,990
1,440
1,900
2,660
2,510
1,332
1,269
1,991
877
4,251
1,690
1,320
1,310
5,570
7,620
1,110
1,370
3,920
2,400
4,472
4,148
4,854
1,311
3,665
2,570
2,720
4,330
2,720
4,620
2,110
1,750
3,280
1,100
1,330
2,090
7,040
1,720
1,840
730
1,030
Cum.
Throughput
gal
278,239
279,679
281,579
284,239
286,749
288,081
289,350
291,341
292,218
296,469
298,159
299,479
300,789
306,359
313,979
315,089
316,459
320,379
322,779
327,251
331,399
336,253
337,564
341,229
343,799
346,519
350,849
353,569
358,189
360,299
362,049
365,329
366,429
367,759
369,849
376,889
378,609
380,449
381,179
382,209
Bed
Volume
#BV
7,439
7,477
7,528
7,599
7,666
7,702
7,736
7,789
7,812
7,926
7,971
8,006
8,041
8,190
8,394
8,424
8,460
8,565
8,629
8,749
8,860
8,990
9,025
9,123
9,191
9,264
9,380
9,452
9,576
9,632
9,679
9,767
9,796
9,832
9,888
10,076
10,122
10,171
10,191
10,218
Train 2
Flow
Rate
gpm
3
1
9
6
0
0
0
6
0
2
0
1
2
0
3
1
2
2
0
0
0
0
0
0
4
0
0
0
12
4
2
0
0
3
0
0
0
0
0
3
Totalizer
gal
309,250
310,790
312,840
315,720
318,432
319,865
321,222
323,365
324,308
328,870
330,475
332,100
333,490
337,370
347,475
348,650
350,100
354,330
356,840
361,640
366,030
NA
372,610
376,470
379,220
382,090
386,781
389,625
394,520
396,780
398,620
402,100
403,270
404,800
406,940
414,500
416,320
418,280
418,730
420,120
Daily
Water
Treated
gal
3,650
1,540
2,050
2,880
2,712
1,433
1,357
2,143
943
4,562
1,605
1,625
1,390
3,880
10,105
1,175
1,450
4,230
2,510
4,800
4,390
NA
NA
3,860
2,750
2,870
4,691
2,844
4,895
2,260
1,840
3,480
1,170
1,530
2,140
7,560
1,820
1,960
450
1,390
Cum.
Throughput
gal
305,559
307,099
309,149
312,029
314,741
316,174
317,531
319,674
320,617
325,179
326,784
328,409
329,799
333,679
343,784
344,959
346,409
350,639
353,149
357,949
362,339
NA
368,919
372,779
375,529
378,399
383,090
385,934
390,829
393,089
394,929
398,409
399,579
401,109
403,249
410,809
412,629
414,589
415,039
416,429
Bed
Volume
#BV
8,169
8,210
8,265
8,342
8,414
8,453
8,489
8,546
8,572
8,693
8,736
8,780
8,817
8,921
9,191
9,222
9,261
9,374
9,441
9,570
9,687
NA
9,863
9,966
10,040
10,116
10,242
10,318
10,449
10,509
10,558
10,651
10,683
10,723
10,781
10,983
11,031
11,084
11,096
11,133
Train2-Train1
Daily
Water
Treated
gal
660
100
150
220
202
101
88
152
66
311
(85)
305
80
(1,690)
2,485
65
80
310
110
328
242
NA
NA
195
180
150
361
124
275
150
90
200
70
200
50
520
100
120
(280)
360
Cum.
Throughput
gal
27,320
27,420
27,570
27,790
27,992
28,093
28,181
28,333
28,399
28,710
28,625
28,930
29,010
27,320
29,805
29,870
29,950
30,260
30,370
30,698
30,940
NA
31,355
31,550
31,730
31,880
32,241
32,365
32,640
32,790
32,880
33,080
33,150
33,350
33,400
33,920
34,020
34,140
33,860
34,220
Bed
Volume
#BV
730
733
737
743
748
751
753
757
759
768
765
773
776
730
797
799
801
809
812
821
827
NA
838
843
848
852
862
865
873
877
879
884
886
892
893
907
910
913
905
915
Combined
Total
Flow
gpm
6
2
18
12
0
0
0
12
0
4
0
2
4
0
6
2
4
4
0
0
0
0
0
0
8
0
0
0
24
8
4
0
0
6
0
0
0
0
0
6
Cum.
Throughput
gal
583,798
586,778
590,728
596,268
601,490
604,255
606,881
611,015
612,835
621,648
624,943
627,888
630,588
640,038
657,763
660,048
662,868
671,018
675,928
685,200
693,738
NA
706,483
714,008
719,328
724,918
733,939
739,503
749,018
753,388
756,978
763,738
766,008
768,868
773,098
787,698
791,238
795,038
796,218
798,638
Bed
Volume
#BV
7,804
7,844
7,896
7,970
8,040
8,077
8,112
8,168
8,192
8,310
8,354
8,393
8,429
8,556
8,792
8,823
8,861
8,970
9,035
9,159
9,273
NA
9,444
9,544
9,615
9,690
9,811
9,885
10,012
10,071
10,119
10,209
10,239
10,278
10,334
10,529
10,577
10,627
10,643
10,676
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73
Day of
Week
Tue
Thu
Fri
Mon
Mon
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Thu
Tue
Thu
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Fri
Mon
Wed
Mon
Wed
Mon
Wed
Fri
Date
01/16/07
01/18/07
01/19/07
01/22/06
01/29/07
02/02/07
02/05/07
02/07/07
02/09/07
02/12/07
02/14/07
02/16/07
02/19/07
02/21/07
02/23/07
02/26/07
02/28/07
03/05/07
03/07/07
03/09/07
03/12/07
03/14/07
03/16/07
03/19/07
03/22/07
03/27/07
03/29/07
04/02/07
04/04/07
04/06/07
04/09/07
04/11/07
04/13/07
04/16/07
04/20/07
04/23/07
04/25/07
04/30/07
05/02/07
05/07/07
05/09/07
05/11/07
Time
15:30
14:02
14:35
8:15
8:30
8:30
8:00
10:25
10:43
8:35
8:50
11:55
8:50
10:20
15:30
14:52
16:05
8:00
11:07
9:25
9:10
7:45
9:00
11:55
9:05
8:25
9:10
10:05
11:40
11:10
8:40
15:00
8:50
8:00
8:00
14:30
7:35
11:10
11:55
8:10
15:34
8:15
Treatment System
Train 1
Flow
Rate
gpm
0
0
0
0
0
0
2
0
0
0
2
1
0
0
0
1
0
0
2
2
2
0
0
1
0
0
0
0
2
1
0
0
0
4
0
0
0
0
1
0
0
0
Totalizer
gal
387,530
388,910
389,680
392,380
396,540
400,070
401,080
402,900
404,500
405,630
407,260
409,210
410,420
411,870
413,380
414,780
416,620
418,790
420,300
421,630
423,270
425,000
427,220
428,290
430,030
431,790
432,680
433,930
435,360
436,600
437,670
439,665
440,700
441,950
445,041
446,500
447,425
450,285
452,010
454,600
456,580
457,450
Daily
Water
Treated
gal
1,800
1,380
770
2,700
4,160
3,530
1,010
1,820
1,600
1,130
1,630
1,950
1,210
1,450
1,510
1,400
1,840
2,170
1,510
1,330
1,640
1,730
2,220
1,070
1,740
1,760
890
1,250
1,430
1,240
1,070
1,995
1,035
1,250
3,091
1,459
925
2,860
1,725
2,590
1,980
870
Cum.
Throughput
gal
384,009
385,389
386,159
388,859
393,019
396,549
397,559
399,379
400,979
402,109
403,739
405,689
406,899
408,349
409,859
411,259
413,099
415,269
416,779
418,109
419,749
421,479
423,699
424,769
426,509
428,269
429,159
430,409
431,839
433,079
434,149
436,144
437,179
438,429
441,520
442,979
443,904
446,764
448,489
451,079
453,059
453,929
Bed
Volume
#BV
10,266
10,303
10,324
10,396
10,507
10,601
10,628
10,677
10,720
10,750
10,794
10,846
10,878
10,917
10,957
10,995
11,044
11,102
11,142
11,178
11,222
11,268
11,327
11,356
11,402
11,450
11,473
11,507
11,545
11,578
11,607
11,660
11,688
11,721
11,804
11,843
11,868
11,944
11,990
12,059
12,112
12,136
Train 2
Flow
Rate
gpm
0
0
0
0
0
0
2
0
0
0
2
1
0
0
0
1
0
0
2
2
2
0
0
1
0
0
0
0
2
1
0
0
0
4
0
0
0
0
1
0
0
0
Totalizer
gal
422,010
423,430
424,240
427,090
431,380
435,000
436,060
437,930
439,570
440,760
442,430
444,460
445,730
447,240
448,840
450,300
452,050
454,580
456,180
457,580
459,330
461,180
463,530
464,660
466,400
468,360
469,100
470,640
472,160
473,480
474,620
476,735
477,838
479,180
482,435
483,890
484,980
487,990
489,810
492,550
494,660
495,580
Daily
Water
Treated
gal
1,890
1,420
810
2,850
4,290
3,620
1,060
1,870
1,640
1,190
1,670
2,030
1,270
1,510
1,600
1,460
1,750
2,530
1,600
1,400
1,750
1,850
2,350
1,130
1,740
1,960
740
1,540
1,520
1,320
1,140
2,115
1,103
1,342
3,255
1,455
1,090
3,010
1,820
2,740
2,110
920
Cum.
Throughput
gal
418,319
419,739
420,549
423,399
427,689
431,309
432,369
434,239
435,879
437,069
438,739
440,769
442,039
443,549
445,149
446,609
448,359
450,889
452,489
453,889
455,639
457,489
459,839
460,969
462,709
464,669
465,409
466,949
468,469
469,789
470,929
473,044
474,147
475,489
478,744
480,199
481,289
484,299
486,119
488,859
490,969
491,889
Bed
Volume
#BV
11,184
11,221
1 1 ,243
11,319
11,434
11,531
11,559
11,609
11,653
11,685
11,729
11,784
11,818
11,858
11,901
11,940
11,987
12,054
12,097
12,134
12,181
12,231
12,294
12,324
12,370
12,423
12,442
12,484
12,524
12,560
12,590
12,647
12,676
12,712
12,799
12,838
12,867
12,947
12,996
13,069
13,126
13,150
Train2-Train1
Daily
Water
Treated
gal
90
40
40
150
130
90
50
50
40
60
40
80
60
60
90
60
(90)
360
90
70
110
120
130
60
200
(150)
290
90
80
70
120
68
92
164
(4)
165
150
95
150
130
50
Cum.
Throughput
gal
34,310
34,350
34,390
34,540
34,670
34,760
34,810
34,860
34,900
34,960
35,000
35,080
35,140
35,200
35,290
35,350
35,260
35,620
35,710
35,780
35,890
36,010
36,140
36,200
36,200
36,400
36,250
36,540
36,630
36,710
36,780
36,900
36,968
37,060
37,224
37,220
37,385
37,535
37,630
37,780
37,910
37,960
Bed
Volume
#BV
917
918
919
923
927
929
931
932
933
935
936
938
939
941
943
945
943
952
955
957
959
963
966
968
968
973
969
977
979
981
983
986
988
991
995
995
999
1,003
1,006
1,010
1,014
1,015
Combined
Total
Flow
gpm
0
0
0
0
0
0
4
0
0
0
4
2
0
0
0
2
0
0
4
4
4
0
0
2
0
0
0
0
4
2
0
0
0
9
0
0
0
0
2
0
0
0
Cum.
Throughput
gal
802,328
805,128
806,708
812,258
820,708
827,858
829,928
833,618
836,858
839,178
842,478
846,458
848,938
851,898
855,008
857,868
861,458
866,158
869,268
871,998
875,388
878,968
883,538
885,738
889,218
892,938
894,568
897,358
900,308
902,868
905,078
909,188
911,326
913,918
920,264
923,178
925,193
931,063
934,608
939,938
944,028
945,818
Bed
Volume
#BV
10,725
10,762
10,783
10,858
10,971
11,066
11,094
11,143
11,186
11,217
11,262
11,315
11,348
11,387
11,429
11,467
11,515
11,578
11,620
11,656
11,701
11,749
11,810
11,840
11,886
11,936
11,958
11,995
12,035
12,069
12,098
12,153
12,182
12,217
12,301
12,340
12,367
12,446
12,493
12,564
12,619
12,643
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
74
75
76
77
78
79
80
81
82
83
84
85
86
87
88
89
90
91
92
94
Day of
Week
Mon
Thu
Fri
Mon
Wed
Tue
Wed
Fri
Mon
Wed
Thu
Tue
Fri
Mon
Wed
Fri
Mon
Fri
Mon
Wed
Mon
Wed
Mon
Wed
Fri
Mon
Wed
Mon
Wed
Mon
Wed
Fri
Tue
Fri
Mon
Wed
Mon
Tue
Mon
Mon
Wed
Fri
Date
05/14/07
05/17/07
05/18/07
05/21/07
05/23/07
05/29/07
05/30/07
06/01/07
06/04/07
06/06/07
06/07/07
06/12/07
06/15/07
06/18/07
06/27/07
06/29/07
07/02/07
07/06/07
07/09/07
07/11/07
07/16/07
07/18/07
07/23/07
07/25/07
07/27/07
07/30/07
08/01/07
08/06/07
08/08/07
08/13/07
08/15/07
08/17/07
08/21/07
08/24/07
08/26/07
08/28/07
09/04/07
09/11/07
09/17/07
10/01/07
10/03/07
10/05/07
Time
15:20
10:10
15:15
14:15
15:35
7:52
14:50
13:35
10:40
9:55
NA
10:45
15:20
NA
9:55
13:10
11:09
8:00
3:05
2:15
10:30
12:10
8:00
7:50
8:30
8:30
9:10
9:30
8:15
3:20
8:51
11:00
11:45
11:35
8:15
8:20
8:30
8:04
12:00
3:22
11:15
16:00
Treatment System
Train 1
Flow
Rate
gpm
0
0
0
0
0
0
0
0
2
0
4
0
0
0
0
0
1
0
0
0
0
0
0
0
0
0
0
1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
458,960
460,710
461,630
463,130
464,710
467,010
468,060
469,300
470,400
471,795
472,480
475,170
476,680
477,652
480,790
481,740
482,800
484,150
485,200
486,250
488,180
489,300
491,080
491,760
492,525
493,420
494,600
496,070
496,820
498,520
499,200
499,990
501,280
502,490
503,150
503,850
505,900
508,300
510,200
517,020
518,200
519,780
Daily
Water
Treated
gal
1,510
1,750
920
1,500
1,580
2,300
1,050
1,240
1,100
1,395
685
2,690
1,510
972
3,138
950
1,060
1,350
1,050
1,050
1,930
1,120
1,780
680
765
895
1,180
1,470
750
1,700
680
790
1,290
1,210
660
700
2,050
2,400
1,900
6,820
1,180
1,580
Cum.
Throughput
gal
455,439
457,189
458,109
459,609
461,189
463,489
464,539
465,779
466,879
468,274
468,959
471,649
473,159
474,131
477,269
478,219
479,279
480,629
481,679
482,729
484,659
485,779
487,559
488,239
489,004
489,899
491,079
492,549
493,299
494,999
495,679
496,469
497,759
498,969
499,629
500,329
502,379
504,779
506,679
513,499
514,679
516,259
Bed
Volume
#BV
12,176
12,223
12,247
12,287
12,330
12,391
12,419
12,452
12,482
12,519
12,537
12,609
12,650
12,676
12,759
12,785
12,813
12,849
12,877
12,905
12,957
12,987
13,035
13,053
13,073
13,097
13,129
13,168
13,188
13,233
13,252
13,273
13,307
13,340
13,357
13,376
13,431
13,495
13,546
13,728
13,760
13,802
Train 2
Flow
Rate
gpm
0
0
0
0
0
0
0
0
2
0
4
0
0
0
0
0
1
0
0
0
0
0
0
0
0
0
0
1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
497,170
499,030
500,000
501,600
503,240
505,680
506,790
508,110
509,290
510,630
511,440
514,370
515,940
516,990
520,365
521,370
522,600
523,965
525,170
526,191
528,270
529,440
531,320
532,050
532,849
533,840
534,880
536,660
537,450
539,270
540,000
540,831
542,220
543,300
544,230
544,970
547,170
549,735
551,770
558,950
560,140
561,670
Daily
Water
Treated
gal
1,590
1,860
970
1,600
1,640
2,440
1,110
1,320
1,180
1,340
810
2,930
1,570
1,050
3,375
1,005
1,230
1,365
1,205
1,021
2,079
1,170
1,880
730
799
991
1,040
1,780
790
1,820
730
831
1,389
1,080
930
740
2,200
2,565
2,035
7,180
1,190
1,530
Cum.
Throughput
gal
493,479
495,339
496,309
497,909
499,549
501,989
503,099
504,419
505,599
506,939
507,749
510,679
512,249
513,299
516,674
517,679
518,909
520,274
521,479
522,500
524,579
525,749
527,629
528,359
529,158
530,149
531,189
532,969
533,759
535,579
536,309
537,140
538,529
539,609
540,539
541,279
543,479
546,044
548,079
555,259
556,449
557,979
Bed
Volume
#BV
13,193
13,243
13,269
13,311
13,355
13,420
13,450
13,485
13,517
13,553
13,574
13,653
13,695
13,723
13,813
13,840
13,873
13,909
13,941
13,969
14,024
14,056
14,106
14,125
14,147
14,173
14,201
14,249
14,270
14,318
14,338
14,360
14,397
14,426
14,451
14,471
14,530
14,598
14,653
14,845
14,876
14,917
Train2-Train1
Daily
Water
Treated
gal
80
110
50
100
60
140
60
80
80
(55)
125
240
60
78
237
55
170
15
155
(29)
149
50
100
50
34
96
(140)
310
40
120
50
41
99
(130)
270
40
150
165
135
360
10
(50)
Cum.
Throughput
gal
38,040
38,150
38,200
38,300
38,360
38,500
38,560
38,640
38,720
38,665
38,790
39,030
39,090
39,168
39,405
39,460
39,630
39,645
39,800
39,771
39,920
39,970
40,070
40,120
40,154
40,250
40,110
40,420
40,460
40,580
40,630
40,671
40,770
40,640
40,910
40,950
41,100
41,265
41,400
41,760
41,770
41,720
Bed
Volume
#BV
1,017
1,020
1,021
1,024
1,026
1,029
1,031
1,033
1,035
1,034
1,037
1,043
1,045
1,047
1,053
1,055
1,059
1,060
1,064
1,063
1,067
1,069
1,071
1,073
1,073
1,076
1,072
1,081
1,082
1,085
1,086
1,087
1,090
1,086
1,094
1,095
1,099
1,103
1,107
1,116
1,117
1,115
Combined
Total
Flow
gpm
0
0
0
0
0
0
0
0
4
0
8
0
0
0
0
0
2
0
0
0
0
0
0
0
0
0
0
2
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Cum.
Throughput
gal
948,918
952,528
954,418
957,518
960,738
965,478
967,638
970,198
972,478
975,213
976,708
982,328
985,408
987,430
993,943
995,898
998,188
1,000,903
1,003,158
1,005,229
1,009,238
1,011,528
1,015,188
1,016,598
1,018,162
1,020,048
1,022,268
1,025,518
1,027,058
1,030,578
1,031,988
1,033,609
1,036,288
1,038,578
1,040,168
1,041,608
1,045,858
1,050,823
1,054,758
1,068,758
1,071,128
1,074,238
Bed
Volume
#BV
12,684
12,733
12,758
12,799
12,842
12,906
12,935
12,969
12,999
13,036
13,056
13,131
13,172
13,199
13,286
13,312
13,343
13,379
13,409
13,437
13,491
13,521
13,570
13,589
13,610
13,635
13,665
13,708
13,729
13,776
13,795
13,816
13,852
13,883
13,904
13,923
13,980
14,047
14,099
14,286
14,318
14,360
>
oo
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
95
96
97
98
99
100
101
102
103
104
105
106
107
108
109
110
111
113
115
116
118
120
121
123
124
125
127
129
132
138
Day of
Week
Tue
Fri
Wed
Mon
Wed
Fri
Tue
Fri
Tue
Mon
Wed
Tue
Wed
Wed
Fri
Wed
Tue
Fri
Thu
Fri
Mon
Mon
Tue
Fri
Wed
Tue
Wed
Thu
Tue
Thu
Mon
Thu
Tue
Thu
Fri
Mon
Wed
Fri
Date
10/16/07
10/19/07
10/24/07
10/29/07
10/31/07
11/02/07
11/05/07
11/07/07
11/20/07
12/03/07
12/12/07
12/18/07
12/26/07
01/09/08
02/01/08
02/1 3/08
02/26/08
02/29/08
03/06/08
03/07/08
03/10/08
03/17/08
03/25/08
03/28/08
04/09/08
04/22/08
04/30/08
05/01/08
05/1 3/08
05/29/08
06/02/08
06/19/08
06/24/08
07/03/08
07/18/08
07/28/08
08/20/08
1 0/03/08
Time
8:15
11:35
9:39
9:00
8:35
8:35
8:30
10:50
15:15
11:55
8:21
11:40
11:58
9:00
11:46
9:16
18:00
3:45
15:05
16:00
8:20
15:15
9:24
7:33
7:33
8:34
10:30
15:40
8:16
8:34
9:40
8:00
NA
15:10
14:00
8:00
14:00
9:45
Treatment System
Train 1
Flow
Rate
gpm
0
0
0
1
0
0
0
0
1
0
0
0
0
0
0
8
0
0
1
NA
NA
0
0
0
0
0
2
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
525,530
527,630
530,230
532,770
534,200
535,000
536,670
538,110
544,850
550,640
554,240
556,150
558,600
563,170
575,460
581,170
588,520
590,500
596,600
597,960
597,960
597,960
603,620
603,620
609,730
616,650
620,260
621,030
626,880
634,870
636,600
644,280
646,180
649,240
656,100
660,060
669,400
686,770
Daily
Water
Treated
gal
5,750
2,100
2,600
2,540
1,430
800
1,670
1,440
6,740
5,790
3,600
1,910
2,450
4,570
12,290
5,710
32,370
1,980
6,100
1,360
-
-
5,660
6,110
6,920
3,610
770
5,850
7,990
1,730
7,680
1,900
3,060
6,860
3,960
9,340
17,370
Cum.
Throughput
gal
522,009
524,109
526,709
529,249
530,679
531,479
533,149
534,589
541,329
547,119
550,719
552,629
555,079
559,649
571,939
577,649
584,999
586,979
593,079
594,439
594,439
594,439
600,099
600,099
606,209
613,129
616,739
617,509
623,359
631,349
633,079
640,759
642,659
645,719
652,579
656,539
665,879
683,249
Bed
Volume
#BV
13,956
14,012
14,081
14,149
14,187
14,209
14,253
14,292
14,472
14,627
14,723
14,774
14,840
14,962
15,290
15,443
15,640
15,693
15,856
15,892
15,892
15,892
16,043
16,043
16,207
16,392
16,488
16,509
16,665
16,879
16,925
17,130
17,181
17,263
17,446
17,552
17,802
18,266
Train 2
Flow
Rate
gpm
0
0
0
1
0
0
0
0
1
0
0
0
0
0
0
8
0
0
NA
MA
2
0
0
0
0
0
2
0
0
0
0
0
0
0
0
0
0
0
Totalizer
gal
567,540
569,630
572,330
574,910
576,340
577,610
578,910
580,420
587,570
593,550
597,260
599,270
601,845
606,700
619,420
625,340
632,990
634,930
634,935
634,935
636,640
644,620
644,620
646,450
652,810
660,000
663,720
664,520
670,500
678,960
680,770
688,820
690,860
694,110
701,220
705,480
715,500
733,580
Daily
Water
Treated
gal
5,870
2,090
2,700
2,580
1,430
1,270
1,300
1,510
7,150
5,980
3,710
2,010
2,575
4,855
12,720
5,920
33,720
1,940
5
-
1,705
7,980
1,830
6,360
7,190
3,720
800
5,980
8,460
1,810
8,050
2,040
3,250
7,110
4,260
10,020
18,080
Cum.
Throughput
gal
563,849
565,939
568,639
571,219
572,649
573,919
575,219
576,729
583,879
589,859
593,569
595,579
598,154
603,009
615,729
621,649
629,299
631,239
631,244
631,244
632,949
640,929
640,929
642,759
649,119
656,309
660,029
660,829
666,809
675,269
677,079
685,129
687,169
690,419
697,529
701,789
711,809
729,889
Bed
Volume
#BV
15,074
15,130
15,202
15,271
15,309
15,343
15,378
15,419
15,610
15,770
15,869
15,922
15,991
16,121
16,461
16,619
16,824
16,876
16,876
16,876
16,922
17,135
17,135
17,184
17,354
17,546
17,645
17,667
17,827
18,053
18,101
18,317
18,371
18,458
18,648
18,762
19,030
19,513
Train2-Train1
Daily
Water
Treated
gal
120
(10)
100
40
470
(370)
70
410
190
110
100
125
285
430
210
1,350
(40)
(6,095)
(1,360)
1,705
7,980
(5,660)
1,830
250
270
110
30
130
470
80
370
140
190
250
300
680
710
Cum.
Throughput
gal
41,840
41,830
41,930
41,970
41,970
42,440
42,070
42,140
42,550
42,740
42,850
42,950
43,075
43,360
43,790
44,000
44,300
44,260
38,165
36,805
38,510
46,490
40,830
42,660
42,910
43,180
43,290
43,320
43,450
43,920
44,000
44,370
44,510
44,700
44,950
45,250
45,930
46,640
Bed
Volume
#BV
1,119
1,118
1,121
1,122
1,122
1,135
1,125
1,127
1,138
1,143
1,146
1,148
1,152
1,159
1,171
1,176
1,184
1,183
1,020
984
1,030
1,243
1,092
1,140
1,147
1,154
1,157
1,158
1,162
1,174
1,176
1,186
1,190
1,195
1,202
1,210
1,228
1,247
Combined
Total
Flow
gpm
0
0
0
2
0
0
0
0
2
0
0
0
0
0
0
16
0
0
1
NA
2
0
0
0
0
0
4
0
0
0
0
0
0
0
0
0
0
0
Cum.
Throughput
gal
1,085,858
1,090,048
1,095,348
1,100,468
1,103,328
1,105,398
1,108,368
1,111,318
1,125,208
1,136,978
1,144,288
1,148,208
1,153,233
1,162,658
1,187,668
1,199,298
1,214,298
1,218,218
1,224,323
1,225,683
1,227,388
1,235,368
1,241,028
1,242,858
1,255,328
1,269,438
1,276,768
1,278,338
1,290,168
1,306,618
1,310,158
1,325,888
1,329,828
1,336,138
1,350,108
1,358,328
1,377,688
1,413,138
Bed
Volume
#BV
14,515
14,571
14,642
14,710
14,748
14,776
14,816
14,855
15,041
15,198
15,296
15,348
15,415
15,541
15,876
16,031
16,232
16,284
16,366
16,384
16,407
16,513
16,589
16,614
16,780
16,969
17,067
17,088
17,246
17,466
17,513
17,723
17,776
17,860
18,047
18,157
18,416
18,890
-------
Table A-l. EPA Arsenic Demonstration Project at Purvine Hall, Klamath Falls, OR - Daily System Operation Log Sheet (Cont.)
Week
No.
140
144
145
147
148
149
151
152
153
154
156
157
158
159
160
161
163
165
166
169
172
173
179
184
185
Day of
Week
Mon
Mon
Wed
Mon
Tue
Thu
Sun
Wed
Mon
Tue
Fri
Mon
Wed
Mon
Thu
Mon
Mon
Wed
Tue
Wed
Mon
Wed
Mon
Fri
Mon
Wed
Date
10/13/08
11/10/08
11/19/08
12/01/08
12/09/08
12/18/08
12/28/08
12/31/08
01/05/09
01/13/09
01/23/09
02/02/09
02/11/09
02/16/09
02/26/09
03/02/09
03/09/09
03/25/09
04/06/09
04/15/09
05/04/09
05/27/09
06/01/09
07/17/09
08/17/09
08/26/09
Time
14:01
15:35
13:50
11:03
15:30
7:59
15:30
14:55
9:57
11:08
13:05
8:10
8:52
15:10
14:30
8:20
9:48
11:46
9:22
8:15
12:10
9:30
11:35
8:22
8:30
11:10
Treatment System
Train 1
Flow
Rate
gpm
0
0
0
1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1
0
0
2
2
1
0
0
Totalizer
gal
692,415
722,960
729,530
734,490
738,380
744,340
748,150
748,900
750,840
756,400
762,610
775,240
781,830
784,960
791,310
793,080
797,330
805,150
811,360
815,900
827,240
840,180
842,880
862,360
878,540
881,735
Daily
Water
Treated
gal
5,645
30,545
6,570
4,960
3,890
5,960
3,810
750
1,940
5,560
6,210
12,630
6,590
3,130
6,350
1,770
4,250
7,820
6,210
4,540
11,340
12,940
2,700
19,480
16,180
3,195
Cum.
Throughput
gal
688,894
719,439
726,009
730,969
734,859
740,819
744,629
745,379
747,319
752,879
759,089
771,719
778,309
781,439
787,789
789,559
793,809
801,629
807,839
812,379
823,719
836,659
839,359
858,839
875,019
878,214
Bed
Volume
#BV
18,417
19,234
19,409
19,542
19,646
19,805
19,907
19,927
19,979
20,128
20,294
20,631
20,808
20,891
21,061
21,108
21,222
21,431
21,597
21,718
22,022
22,368
22,440
22,961
23,393
23,479
Train 2
Flow
Rate
gpm
0
0
0
1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
2
2
1
0
0
Totalizer
gal
739,490
772,300
779,380
787,550
788,670
795,020
799,120
799,920
802,010
807,830
814,345
828,582
834,740
837,900
844,570
846,450
850,870
859,140
865,590
870,440
882,880
895,730
898,600
919,110
936,520
NA
Daily
Water
Treated
gal
5,910
32,810
7,080
8,170
1,120
6,350
4,100
800
2,090
5,820
6,515
14,237
6,158
3,160
6,670
1,880
4,420
8,270
6,450
4,850
12,440
12,850
2,870
20,510
17,410
NA
Cum.
Throughput
gal
735,799
768,609
775,689
783,859
784,979
791,329
795,429
796,229
798,319
804,139
810,654
824,891
831,049
834,209
840,879
842,759
847,179
855,449
861,899
866,749
879,189
892,039
894,909
915,419
932,829
936,214
Bed
Volume
#BV
19,671
20,548
20,738
20,956
20,986
21,156
21,265
21,287
21,343
21,498
21,672
22,053
22,218
22,302
22,480
22,531
22,649
22,870
23,042
23,172
23,505
23,848
23,925
24,473
24,939
NA
Train2-Train1
Daily
Water
Treated
gal
265
2,265
510
3,210
(2,770)
390
290
50
150
260
305
1,607
(432)
30
320
110
170
450
240
310
1,100
(90)
170
1,030
1,230
NA
Cum.
Throughput
gal
46,905
49,170
49,680
52,890
50,120
50,510
50,800
50,850
51,000
51,260
51,565
53,172
52,740
52,770
53,090
53,200
53,370
53,820
54,060
54,370
55,470
55,380
55,550
56,580
57,810
NA
Bed
Volume
#BV
1,254
1,315
1,328
1,414
1,340
1,350
1,358
1,359
1,363
1,370
1,379
1,422
1,410
1,411
1,419
1,422
1,427
1,439
1,445
1,454
1,483
1,481
1,485
1,513
1,546
NA
Combined
Total
Flow
gpm
0
0
0
2
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1
0
0
4
4
2
0
0
Cum.
Throughput
gal
1,424,693
1,488,048
1,501,698
1,514,828
1,519,838
1,532,148
1,540,058
1,541,608
1,545,638
1,557,018
1,569,743
1,596,610
1,609,358
1,615,648
1,628,668
1,632,318
1,640,988
1,657,078
1,669,738
1,679,128
1,702,908
1,728,698
1,734,268
1,774,258
1,807,848
NA
Bed
Volume
#BV
19,044
19,891
20,073
20,249
20,316
20,481
20,586
20,607
20,661
20,813
20,983
21,342
21,513
21,597
21,771
21,820
21,935
22,150
22,320
22,445
22,763
23,108
23,182
23,717
24,166
NA
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet
Week
No.
1
2
3
4
5
6
7
8
9
10
11
12
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
12/12/05
12/13/05
12/14/05
12/15/05
12/16/05
12/19/05
12/20/05
12/21/05
12/22/05
12/23/05
12/27/05
12/28/05
12/29/05
01/03/06
01/04/06
01/05/06
01/06/06
01/09/06
01/10/06
01/11/06
01/12/06
01/13/06
01/17/06
01/18/06
01/19/06
01/20/06
01/23/06
01/24/06
01/25/06
01/26/06
01/27/06
01/30/06
01/31/06
02/01/06
02/02/06
02/03/06
02/06/06
02/07/06
02/08/06
02/09/06
02/10/06
02/13/06
02/14/06
02/15/06
02/16/06
02/17/06
02/20/06
02/21/06
02/22/06
02/23/06
02/24/06
02/27/06
02/28/06
03/01/06
03/02/06
03/03/06
Time
7:50
8:20
13:45
11:30
9:00
14:30
8:23
8:32
8:15
7:50
8:20
8:30
9:23
6:45
16:40
9:20
15:30
8:05
15:20
9:47
14:43
7:40
11:30
13:35
9:30
10:24
16:30
8:25
7:30
10:40
9:01
11:07
10:20
8:35
10:30
11:20
13:30
8:45
8:15
8:25
11:30
8:40
10:25
NM
NM
8:35
8:07
14:52
8:43
8:29
7:50
9:00
11:15
11:42
7:45
7:53
Tank Position
Lead
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
NM
NM
B
B
B
B
B
B
B
B
B
B
B
Lag
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
NM
NM
A
A
A
A
A
A
A
A
A
A
A
Treatment System
Flowrate|a|
gpm
NM
NM
NM
NM
NM
2
2
2
2
2
2
2
2
2
2
2
2
40
18
8
19
44
33
20
26.5
23
26
29
23
15
27.5
7.5
32.5
37.5
27
6.5
18.5
34
24
27.5
7
27
36
NM
NM
33
40
16
35
35
32.5
11.5
25
20
16
19
Totalizer
gal
12,600
17,215
22,230
26,278
30,012
40,502
43,780
48,414
53,151
56,871
67,821
72,152
76,142
91,952
97,840
99,312
105,535
133,780
157,530
172,392
195,920
208,715
288,550
311,410
330,351
351,550
417,758
429,880
450,555
474,440
494,580
553,555
571,915
592,250
614,280
636,405
695,035
709,660
727,225
749,750
776,820
831 ,640
852,936
NM
NM
916,000
971,850
1,000,422
1,001,650
1,033,620
1,053,980
1,111,775
1,134,870
1,156,580
1,172,037
1,193,930
Daily Water
Treated
gal
NA
4,615
5,015
4,048
3,734
10,490
3,278
4,634
4,737
3,720
10,950
4,331
3,990
15,810
5,888
1,472
6,223
28,245
23,750
14,862
23,528
12,795
79,835
22,860
18,941
21,199
66,208
12,122
20,675
23,885
20,140
58,975
18,360
20,335
22,030
22,125
58,630
14,625
17,565
22,525
27,070
54,820
21,296
NA
NA
63,064
55,850
28,572
1,228
31,970
20,360
57,795
23,095
21,710
15,457
21,893
Cum.
Throughput
gal
NA
4,615
9,630
13,678
17,412
27,902
31,180
35,814
40,551
44,271
55,221
59,552
63,542
79,352
85,240
86,712
92,935
121,180
144,930
159,792
183,320
196,115
275,950
298,810
317,751
338,950
405,158
417,280
437,955
461,840
481,980
540,955
559,315
579,650
601,680
623,805
682,435
697,060
714,625
737,150
764,220
819,040
840,336
NA
NA
903,400
959,250
987,822
989,050
1,021,020
1,041,380
1,099,175
1,122,270
1,143,980
1,159,437
1,181,330
Bed
Volume
#BV
NA
31
64
91
116
186
208
239
271
296
369
398
425
530
570
580
621
810
969
1,068
1,225
1,311
1,844
1,997
2,124
2,265
2,708
2,789
2,927
3,087
3,221
3,616
3,738
3,874
4,021
4,169
4,561
4,659
4,776
4,927
5,108
5,474
5,616
NA
NA
6,038
6,411
6,602
6,610
6,824
6,960
7,346
7,501
7,646
7,749
7,896
System Pressure
Inlet
psig
62
62
62
62
65
58
58
58
58
58
60
59
60
61
61
61
61
58
60
61
59
56
58
60
60
60
58
55
60
60
60
61
59
57
57
62
60
58
58
58
60
58
55
NM
NM
58
55
58
55
58
56
60
60
58
60
55
Outlet
psig
62
62
62
62
65
NA
NA
NA
NA
NA
NA
NA
NA
64
64
64
64
58
61
62
58
57
56
62
61
60
55
51
60
60
60
62
60
52
51
61
60
44
55
56
58
50
43
NM
NM
55
45
58
43
55
50
58
55
57
60
45
In-Out
psig
0
0
0
0
0
NA
NA
NA
NA
NA
NA
NA
NA
-3
-3
-3
-3
0
-1
-1
1
-1
2
-2
-1
0
3
4
0
0
0
-1
-1
5
6
1
0
14
3
2
2
8
12
NA
NA
3
10
0
12
3
6
2
5
1
0
10
Differential
Pressure
DP1 1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-ll
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
13
14
15
16
17
18
19
20
21
22
23
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
03/06/06
03/07/06
03/08/06
03/09/06
03/10/06
03/13/06
03/14/06
03/15/06
03/16/06
03/17/06
03/20/06
03/21/06
03/22/06
03/23/06
03/24/06
03/27/06
03/28/06
03/29/06
03/30/06
03/31/06
04/03/06
04/04/06
04/05/06
04/06/06
04/07/06
04/10/06
04/11/06
04/12/06
04/13/06
04/14/06
04/17/06
04/18/06
04/19/06
04/20/06
04/21/06
04/24/06
04/25/06
04/26/06
04/27/06
04/28/06
05/01/06
05/02/06
05/03/06
05/04/06
05/05/06
05/08/06
05/09/06
05/1 0/06
05/11/06
05/1 2/06
05/15/06
05/16/06
05/17/06
05/18/06
05/19/06
Time
8:10
8:02
8:57
8:43
10:32
8:50
11:13
7:45
7:50
8:00
8:10
8:02
8:57
8:43
10:32
8:25
14:00
9:55
7:58
8:10
9:00
8:45
7:45
10:51
7:42
7:47
7:45
10:26
7:45
8:00
8:00
9:10
8:55
7:45
13:43
8:42
8:24
9:12
7:54
7:43
8:45
7:50
13:35
8:36
3:10
8:54
11:34
15:15
8:30
8:55
8:00
7:55
13:15
13:50
15:00
Tank Position
Lead
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Lag
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Treatment System
Flowrate|a|
gpm
41.5
28.5
11.5
30
23
42.5
30
32
16
36
27
21
29
24
9
3
2
2
2
5
17.5
35
27
30
21
38
16.5
31
17
34
40
26
20
25
19
38
23
35
19
8
28
23
10
20
45
35
10
15
20
30
28
30
10
15
12
Totalizer
gal
1,251,520
1,271,665
1,295,728
1,315,705
1,341,000
1,398,950
1,422,650
1,439,200
1,459,310
1,483,530
1,541,235
1,564,375
1,585,740
1,606,560
1,619,912
1,636,650
1,643,545
1,647,346
1,651,345
1,656,105
1,683,720
1,700,440
1,719,900
1,742,390
1,758,191
1,812,690
1,813,632
1,857,315
1,872,480
1,895,000
1,945,150
1,965,915
1,987,550
2,005,600
2,039,935
2,097,485
2,116,550
2,141,010
2,158,860
2,182,490
2,242,424
2,261,210
2,291,775
2,307,180
2,331,700
2,387,958
2,436,220
2,437,333
2,453,200
2,474,080
2,525,170
2,545,130
2,573,540
2,596,940
2,620,505
Daily Water
Treated
gal
57,590
20,145
24,063
19,977
25,295
57,950
23,700
16,550
20,110
24,220
57,705
23,140
21,365
20,820
13,352
16,738
6,895
3,801
3,999
4,760
27,615
16,720
19,460
22,490
15,801
54,499
942
43,683
15,165
22,520
50,150
20,765
21,635
18,050
34,335
57,550
19,065
24,460
17,850
23,630
59,934
18,786
30,565
15,405
24,520
56,258
48,262
1,113
15,867
20,880
51,090
19,960
28,410
23,400
23,565
Cum.
Throughput
gal
1,238,920
1,259,065
1,283,128
1,303,105
1,328,400
1,386,350
1,410,050
1,426,600
1,446,710
1,470,930
1,528,635
1,551,775
1,573,140
1,593,960
1,607,312
1,624,050
1,630,945
1,634,746
1,638,745
1,643,505
1,671,120
1,687,840
1,707,300
1,729,790
1,745,591
1,800,090
1,801,032
1,844,715
1,859,880
1,882,400
1,932,550
1,953,315
1,974,950
1,993,000
2,027,335
2,084,885
2,103,950
2,128,410
2,146,260
2,169,890
2,229,824
2,248,610
2,279,175
2,294,580
2,319,100
2,375,358
2,423,620
2,424,733
2,440,600
2,461,480
2,512,570
2,532,530
2,560,940
2,584,340
2,607,905
Bed
Volume
#BV
8,280
8,415
8,576
8,709
8,878
9,266
9,424
9,535
9,669
9,831
10,217
10,371
10,514
10,653
10,743
10,854
10,901
10,926
10,953
10,985
11,169
11,281
11,411
11,561
11,667
12,031
12,037
12,329
12,431
12,581
12,916
13,055
13,200
13,320
13,550
13,935
14,062
14,225
14,345
14,503
14,903
15,029
15,233
15,336
15,500
15,876
16,199
16,206
16,312
16,452
16,793
16,926
17,116
17,273
17,430
System Pressure
Inlet
psig
54
58
60
58
58
55
55
58
60
58
56
59
59
59
60
61
60
61
60
60
60
55
59
55
61
55
59
59
61
56
54
58
56
60
55
58
58
58
59
57
59
58
60
60
57
58
60
60
58
59
58
56
61
60
56
Outlet
psig
40
52
61
57
57
50
50
53
59
48
50
57
56
58
60
61
61
61
60
60
59
48
57
52
59
40
58
58
60
50
43
54
52
59
48
49
50
56
57
52
56
55
59
58
42
44
60
58
52
48
52
48
60
60
57
In-Out
psig
14
6
-1
1
1
5
5
5
1
10
6
2
3
1
0
0
-1
0
0
0
1
7
2
3
2
15
1
1
1
6
11
4
4
1
7
9
8
2
2
5
3
3
1
2
15
14
0
2
6
11
6
8
1
0
-1
Differential
Pressure
DP1 1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-12
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
24
25
26
27
28
29
30
31
32
33
34
35
Day of
Week
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
05/22/06
05/23/06
05/24/06
05/25/06
05/26/06
05/30/06
05/31/06
06/01/06
06/02/06
06/05/06
06/06/06
06/07/06
06/08/06
06/09/06
06/12/06
06/1 3/06
06/1 4/06
06/15/06
06/16/06
06/19/06
06/20/06
06/21/06
06/22/06
06/23/06
06/26/06
06/27/06
06/28/06
06/29/06
06/30/06
07/03/06
07/05/06
07/06/06
07/07/06
07/10/06
07/11/06
07/12/06
07/13/06
07/18/06
07/19/06
07/20/06
07/21/06
07/24/06
07/25/06
07/26/06
07/27/06
07/28/06
07/31/06
08/01/06
08/02/06
08/03/06
08/04/06
08/07/06
08/08/06
08/09/06
08/10/06
08/11/06
Time
10:30
9:35
15:35
14:45
9:46
7:50
8:50
8:00
8:40
2:55
7:30
15:25
11:20
10:13
13:29
7:45
8:59
7:55
8:15
8:45
8:08
10:46
7:40
7:45
11:15
11:40
8:50
8:15
9:20
8:30
9:07
7:50
8:05
14:35
8:00
7:54
8:20
5:30
8:57
10:00
8:55
9:30
7:30
15:20
10:30
9:30
7:24
7:45
8:15
8:30
8:16
10:25
7:52
7:30
10:11
10:30
Tank Position
Lead
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Lag
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Treatment System
Flowrate|a|
gpm
25
35
10
35
30
25
23
25
40
12
12
10
20
28
24
18
38
20
10
10
2
10
4
2
2
2
2
8
2
5
4
45
3
1
4
2
5
10
12
10
5
12
0
0
2
8
0
2
1
2
12
4
2
5
12
16
Totalizer
gal
2,677,370
2,697,030
2,712,512
2,746,800
2,763,572
2,819,750
2,842,095
2,860,850
2,884,740
2,953,470
2,971,333
2,998,555
3,015,360
3,038,155
3,100,190
3,115,225
3,136,860
3,156,800
3,174,310
3,207,800
3,210,500
3,219,350
3,226,300
3,235,100
3,260,110
3,269,700
3,276,850
3,285,900
3,295,800
3,328,412
3,338,804
3,379,600
3,390,500
3,421,110
3,428,850
3,436,780
3,445,500
3,492,353
3,736
9,255
13,100
16,090
20,533
45,030
52,947
61,330
85,223
91,520
103,072
115,905
124,075
149,660
155,715
162,690
176,980
183,870
Daily Water
Treated
gal
56,865
19,660
15,482
34,288
16,772
56,178
22,345
18,755
23,890
68,730
17,863
27,222
16,805
22,795
62,035
15,035
21,635
19,940
17,510
33,490
2,700
8,850
6,950
8,800
25,010
9,590
7,150
9,050
9,900
32,612
10,392
40,796
10,900
30,610
7,740
7,930
8,720
46,853
3,436
5,519
3,845
2,990
4,443
24,497
7,917
8,383
23,893
6,297
11,552
12,833
8,170
25,585
6,055
6,975
14,290
6,890
Cum.
Throughput
gal
2,664,770
2,684,430
2,699,912
2,734,200
2,750,972
2,807,150
2,829,495
2,848,250
2,872,140
2,940,870
2,958,733
2,985,955
3,002,760
3,025,555
3,087,590
3,102,625
3,124,260
3,144,200
3,161,710
3,195,200
3,197,900
3,206,750
3,213,700
3,222,500
3,247,510
3,257,100
3,264,250
3,273,300
3,283,200
3,315,812
3,326,204
3,367,000
3,377,900
3,408,510
3,416,250
3,424,180
3,432,900
3,479,753
3,483,189
3,488,708
3,492,553
3,495,543
3,499,986
3,524,483
3,532,400
3,540,783
3,564,676
3,570,973
3,582,525
3,595,358
3,603,528
3,629,113
3,635,168
3,642,143
3,656,433
3,663,323
Bed
Volume
#BV
17,810
17,942
18,045
18,274
18,386
18,762
18,911
19,037
19,196
19,656
19,775
19,957
20,069
20,222
20,636
20,737
20,881
21,015
21,132
21,355
21,373
21,433
21,479
21,538
21,705
21,769
21,817
21,877
21,944
22,162
22,231
22,504
22,577
22,781
22,833
22,886
22,944
23,257
23,280
23,317
23,343
23,363
23,393
23,556
23,609
23,665
23,825
23,867
23,944
24,030
24,085
24,256
24,296
24,343
24,438
24,484
System Pressure
Inlet
psig
60
55
60
60
56
60
58
54
55
59
60
60
60
60
58
58
55
59
60
61
61
59
61
60
61
61
61
61
61
60
61
58
61
61
62
60
60
60
60
60
61
60
60
60
60
60
60
58
60
60
59
60
60
61
60
60
Outlet
psig
58
45
60
60
48
58
55
43
42
59
59
59
58
58
54
57
45
57
60
61
61
59
61
60
61
61
61
61
61
60
60
40
60
61
62
60
60
60
60
60
60
60
60
60
60
60
60
58
59
60
57
60
59
60
59
60
In-Out
psig
2
10
0
0
8
2
3
11
13
0
1
1
2
2
4
1
10
2
0
0
0
0
0
0
0
0
0
0
0
0
1
18
1
0
0
0
0
0
0
0
1
0
0
0
0
0
0
0
1
0
2
0
1
1
1
0
Differential
Pressure
DP1 1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-13
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
Day of
Week
Tue
Wed
Thu
Fri
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Wed
Wed
Thu
Fri
Mon
Wed
Fri
Mon
Thu
Tue
Wed
Thu
Fri
Mon
Wed
Mon
Wed
Fri
Date
08/15/06
08/16/06
08/17/06
08/18/06
08/25/06
08/28/06
08/29/06
08/30/06
08/31/06
09/01/06
09/05/06
09/06/06
09/07/06
09/08/06
09/11/06
09/12/06
09/13/06
09/14/06
09/15/06
09/18/06
09/19/06
09/20/06
09/21/06
09/22/06
09/25/06
09/26/06
09/27/06
09/29/06
10/02/06
10/03/06
10/04/06
10/05/06
10/06/06
10/10/06
10/11/06
10/12/06
10/13/06
10/16/06
10/18/06
10/25/06
10/26/06
10/27/06
10/30/06
11/01/06
11/03/06
11/05/06
11/08/06
11/14/06
11/15/06
11/16/06
11/17/06
11/20/06
11/22/06
11/27/06
11/29/06
12/01/06
Time
8:38
10:00
8:30
8:15
13:50
7:50
7:40
10:45
7:50
7:35
7:45
7:50
7:50
14:30
9:10
9:52
10:19
10:30
14:45
7:45
7:50
8:00
7:45
7:55
8:10
8:05
10:10
8:55
8:05
8:40
8:04
9:12
8:50
10:05
11:20
15:35
14:55
9:00
9:30
11:35
9:20
11:50
10:25
10:35
8:40
9:15
9:15
8:45
8:10
8:45
11:00
8:20
9:45
7:30
14:15
15:45
Tank Position
Lead
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Lag
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Treatment System
Flowrate|a|
gpm
8
5
0
10
4
4
3
5
5
4
8
5
4
8
5
10
5
8
5
30
15
18
19
17
60
50
30
20
42
25
54
13
56
28
25
8
15
30
24
16
22
35
30
28
35
20
15
30
45
35
16
42
30
45
15
18
Totalizer
gal
216,060
223,190
230,190
239,410
274,845
314,920
323,040
331,973
339,060
346,790
375,750
389,680
393,790
404,810
431 ,925
442,800
453,910
464,380
476,890
503,900
519,840
528,230
542,180
559,240
627,960
650,450
680,800
729,800
801,060
827,094
852,950
878,990
905,680
1,004,830
1,030,280
1,063,380
1,090,720
1,153,080
1,229,810
1,403,660
1,425,370
1,456,500
1,528,840
1,581,460
1,629,080
1,703,250
1,786,200
1,890,410
1,915,170
1,940,920
1,971,220
2,044,180
2,096,110
2,163,610
2,218,970
2,272,210
Daily Water
Treated
gal
32,190
7,130
7,000
9,220
35,435
40,075
8,120
8,933
7,087
7,730
28,960
13,930
4,110
11,020
27,115
10,875
11,110
10,470
12,510
27,010
15,940
8,390
13,950
17,060
68,720
22,490
30,350
49,000
71,260
26,034
25,856
26,040
26,690
99,150
25,450
33,100
27,340
62,360
76,730
173,850
21,710
31,130
72,340
52,620
47,620
74,170
82,950
104,210
24,760
25,750
30,300
72,960
51,930
67,500
55,360
53,240
Cum.
Throughput
gal
3,695,513
3,702,643
3,709,643
3,718,863
3,754,298
3,794,373
3,802,493
3,811,426
3,818,513
3,826,243
3,855,203
3,869,133
3,873,243
3,884,263
3,911,378
3,922,253
3,933,363
3,943,833
3,956,343
3,983,353
3,999,293
4,007,683
4,021,633
4,038,693
4,107,413
4,129,903
4,160,253
4,209,253
4,280,513
4,306,547
4,332,403
4,358,443
4,385,133
4,484,283
4,509,733
4,542,833
4,570,173
4,632,533
4,709,263
4,883,113
4,904,823
4,935,953
5,008,293
5,060,913
5,108,533
5,182,703
5,265,653
5,369,863
5,394,623
5,420,373
5,450,673
5,523,633
5,575,563
5,643,063
5,698,423
5,751,663
Bed
Volume
#BV
24,699
24,747
24,794
24,855
25,092
25,360
25,414
25,474
25,521
25,573
25,767
25,860
25,887
25,961
26,142
26,215
26,289
26,359
26,443
26,623
26,730
26,786
26,879
26,993
27,452
27,603
27,805
28,133
28,609
28,783
28,956
29,130
29,308
29,971
30,141
30,362
30,545
30,962
31,475
32,637
32,782
32,990
33,473
33,825
34,143
34,639
35,194
35,890
36,055
36,228
36,430
36,918
37,265
37,716
38,086
38,442
System Pressure
Inlet
psig
60
58
59
58
61
60
61
61
61
61
61
60
61
61
61
60
61
60
60
58
59
58
59
58
50
52
58
58
54
58
50
58
52
60
58
60
59
56
60
60
58
58
58
56
55
59
60
59
54
55
58
54
54
58
58
60
Outlet
psig
58
57
57
56
60
58
59
59
60
60
59
59
60
60
59
58
60
58
58
48
58
52
57
56
30
38
55
48
40
44
35
60
40
55
52
58
57
50
55
52
56
55
52
49
49
57
57
44
42
45
52
42
44
50
54
57
In-Out
psig
2
1
2
2
1
2
2
2
1
1
2
1
1
1
2
2
1
2
2
10
1
6
2
2
20
14
3
10
14
14
15
-2
12
5
6
2
2
6
5
8
2
3
6
7
6
2
3
15
12
10
6
12
10
8
4
3
Differential
Pressure
DP1 1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-14
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73
Day of
Week
Mon
Wed
Thu
Mon
Wed
Fri
Tue
Tue
Fri
Tue
Wed
Fri
Tue
Fri
Mon
Mon
Thu
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Thu
Fri
Tue
Thu
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Fri
Mon
Wed
Fri
Mon
Wed
Mon
Wed
Fri
Date
12/04/06
12/06/06
12/07/06
12/11/06
12/13/06
12/15/06
12/19/06
01/02/07
01/05/06
01/09/07
01/10/07
01/12/07
01/18/07
01/19/07
01/22/07
01/29/07
02/01/07
02/02/07
02/05/07
02/07/07
02/09/07
02/12/07
02/14/07
02/16/07
02/19/07
02/21/07
02/23/07
02/26/07
02/28/07
03/02/07
03/05/07
03/07/07
03/09/07
03/12/07
03/14/07
03/16/07
03/19/07
03/22/07
03/23/07
03/27/07
03/29/07
04/02/07
04/04/07
04/06/07
04/09/07
04/11/07
04/13/07
04/16/07
04/20/07
04/23/07
04/25/07
04/27/07
04/30/07
05/02/07
05/07/07
05/09/07
05/11/07
Time
8:10
8:35
8:50
10:50
9:10
10:35
14:45
9:05
10:40
9:00
12:00
16:10
14:10
14:30
8:10
8:37
10:30
9:50
7:50
8:35
8:40
7:57
8:40
11:45
8:40
10:45
15:15
14:42
15:40
15:20
7:50
7:53
9:15
9:10
7:45
NA
13:30
8:52
8:48
15:30
8:44
9:37
8:36
10:15
8:40
15:10
8:40
7:50
7:50
14:50
7:45
7:30
10:55
8:10
7:50
8:35
8:08
Tank Position
Lead
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Lag
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Treatment System
Flowrate|a|
gpm
14
36
24
5
10
5
15
5
12
42
25
20
16
32
40
45
40
34
42
50
40
40
48
30
40
32
38
14
18
22
45
44
45
52
26
18
32
28
22
16
15
38
55
34
44
28
46
48
24
30
48
58
30
52
45
40
52
Totalizer
gal
2,339,410
2,392,500
2,420,070
2,470,000
2,489,710
2,509,740
2,546,690
2,671,220
2,716,950
2,810,720
2,848,530
2,917,400
3,035,200
3,135,420
3,218,650
3,455,900
3,563,970
3,598,590
3,695,300
3,766,480
3,835,800
3,934,570
4,007,260
4,082,900
4,176,000
4,250,170
4,327,330
4,428,300
4,499,800
4,570,490
4,657,010
4,730,910
4,809,550
4,913,670
4,997,480
5,074,040
5,131,390
5,283,800
5,314,790
5,410,200
5,448,100
5,549,600
5,618,550
5,697,990
5,797,250
5,880,660
5,943,900
6,046,250
6,205,575
6,313,450
6,374,700
6,459,270
6,575,670
6,658,770
6,839,780
6,915,940
6,989,870
Daily Water
Treated
gal
67,200
53,090
27,570
49,930
19,710
20,030
36,950
124,530
45,730
93,770
37,810
68,870
117,800
100,220
83,230
237,250
108,070
34,620
96,710
71,180
69,320
98,770
72,690
75,640
93,100
74,170
77,160
100,970
71,500
70,690
86,520
73,900
78,640
104,120
83,810
76,560
57,350
152,410
30,990
95,410
37,900
101,500
68,950
79,440
99,260
83,410
63,240
102,350
159,325
107,875
61,250
84,570
116,400
83,100
181,010
76,160
73,930
Cum.
Throughput
gal
5,818,863
5,871,953
5,899,523
5,949,453
5,969,163
5,989,193
6,026,143
6,150,673
6,196,403
6,290,173
6,327,983
6,396,853
6,514,653
6,614,873
6,698,103
165,000
273,070
307,690
404,400
475,580
544,900
643,670
716,360
792,000
885,100
959,270
1,036,430
1,137,400
1,208,900
1,279,590
1,366,110
1,440,010
1,518,650
1,622,770
1,706,580
1,783,140
1,840,490
1,992,900
2,023,890
2,119,300
2,157,200
2,258,700
2,327,650
2,407,090
2,506,350
2,589,760
2,653,000
2,755,350
2,914,675
3,022,550
3,083,800
3,168,370
3,284,770
3,367,870
3,548,880
3,625,040
3,698,970
Bed
Volume
#BV
38,891
39,246
39,430
39,764
39,895
40,029
40,276
41,109
41,414
42,041
42,294
42,754
43,541
44,211
44,767
1,103
1,825
2,056
2,703
3,179
3,642
4,302
4,788
5,293
5,916
6,411
6,927
7,602
8,080
8,552
9,131
9,624
10,150
10,846
11,406
11,918
12,301
13,320
13,527
14,165
14,418
15,096
15,557
16,088
16,751
17,309
17,732
18,416
19,481
20,202
20,611
21,176
21,954
22,509
23,719
24,228
24,722
System Pressure
Inlet
psig
58
54
58
61
60
60
61
60
58
50
55
57
58
62
52
51
55
62
51
50
50
52
51
57
52
57
52
57
57
58
52
46
54
50
58
58
56
54
57
58
58
54
50
52
52
55
45
51
58
55
46
48
57
45
52
56
50
Outlet
psig
52
42
54
58
58
59
59
58
56
40
50
51
56
58
42
41
44
61
41
32
40
42
37
45
43
48
42
56
55
52
42
40
42
30
56
56
44
44
50
56
56
46
32
42
38
49
43
38
56
51
40
28
45
32
39
40
32
In-Out
psig
6
12
4
3
2
1
2
2
2
10
5
6
2
4
10
10
11
1
10
18
10
10
14
12
9
9
10
1
2
6
10
6
12
20
2
2
12
10
7
2
2
8
18
10
14
6
2
13
2
4
6
20
12
13
13
16
18
Differential
Pressure
DPI1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-15
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73
Day of
Week
Mon
Wed
Thu
Mon
Wed
Fri
Tue
Tue
Fri
Tue
Wed
Fri
Tue
Fri
Mon
Mon
Thu
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Thu
Fri
Tue
Thu
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Fri
Mon
Wed
Fri
Mon
Wed
Mon
Wed
Fri
Date
12/04/06
12/06/06
12/07/06
12/11/06
12/13/06
12/15/06
12/19/06
01/02/07
01/05/06
01/09/07
01/10/07
01/12/07
01/18/07
01/19/07
01/22/07
01/29/07
02/01/07
02/02/07
02/05/07
02/07/07
02/09/07
02/12/07
02/14/07
02/16/07
02/19/07
02/21/07
02/23/07
02/26/07
02/28/07
03/02/07
03/05/07
03/07/07
03/09/07
03/12/07
03/14/07
03/16/07
03/19/07
03/22/07
03/23/07
03/27/07
03/29/07
04/02/07
04/04/07
04/06/07
04/09/07
04/11/07
04/13/07
04/16/07
04/20/07
04/23/07
04/25/07
04/27/07
04/30/07
05/02/07
05/07/07
05/09/07
05/11/07
Time
8:10
8:35
8:50
10:50
9:10
10:35
14:45
9:05
10:40
9:00
12:00
16:10
14:10
14:30
8:10
8:37
10:30
9:50
7:50
8:35
8:40
7:57
8:40
11:45
8:40
10:45
15:15
14:42
15:40
15:20
7:50
7:53
9:15
9:10
7:45
NA
13:30
8:52
8:48
15:30
8:44
9:37
8:36
10:15
8:40
15:10
8:40
7:50
7:50
14:50
7:45
7:30
10:55
8:10
7:50
8:35
8:08
Tank Position
Lead
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Lag
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Treatment System
Flowrate(a|
gpm
14
36
24
5
10
5
15
5
12
42
25
20
16
32
40
45
40
34
42
50
40
40
48
30
40
32
38
14
18
22
45
44
45
52
26
18
32
28
22
16
15
38
55
34
44
28
46
48
24
30
48
58
30
52
45
40
52
Totalizer
gal
2,339,410
2,392,500
2,420,070
2,470,000
2,489,710
2,509,740
2,546,690
2,671,220
2,716,950
2,810,720
2,848,530
2,917,400
3,035,200
3,135,420
3,218,650
3,455,900
3,563,970
3,598,590
3,695,300
3,766,480
3,835,800
3,934,570
4,007,260
4,082,900
4,176,000
4,250,170
4,327,330
4,428,300
4,499,800
4,570,490
4,657,010
4,730,910
4,809,550
4,913,670
4,997,480
5,074,040
5,131,390
5,283,800
5,314,790
5,410,200
5,448,100
5,549,600
5,618,550
5,697,990
5,797,250
5,880,660
5,943,900
6,046,250
6,205,575
6,313,450
6,374,700
6,459,270
6,575,670
6,658,770
6,839,780
6,915,940
6,989,870
Daily Water
Treated
gal
67,200
53,090
27,570
49,930
19,710
20,030
36,950
124,530
45,730
93,770
37,810
68,870
117,800
100,220
83,230
237,250
108,070
34,620
96,710
71,180
69,320
98,770
72,690
75,640
93,100
74,170
77,160
100,970
71,500
70,690
86,520
73,900
78,640
104,120
83,810
76,560
57,350
152,410
30,990
95,410
37,900
101,500
68,950
79,440
99,260
83,410
63,240
102,350
159,325
107,875
61,250
84,570
116,400
83,100
181,010
76,160
73,930
Cum.
Throughput
gal
5,818,863
5,871,953
5,899,523
5,949,453
5,969,163
5,989,193
6,026,143
6,150,673
6,196,403
6,290,173
6,327,983
6,396,853
6,514,653
6,614,873
6,698,103
165,000
273,070
307,690
404,400
475,580
544,900
643,670
716,360
792,000
885,100
959,270
1,036,430
1,137,400
1,208,900
1,279,590
1,366,110
1,440,010
1,518,650
1,622,770
1,706,580
1,783,140
1,840,490
1,992,900
2,023,890
2,119,300
2,157,200
2,258,700
2,327,650
2,407,090
2,506,350
2,589,760
2,653,000
2,755,350
2,914,675
3,022,550
3,083,800
3,168,370
3,284,770
3,367,870
3,548,880
3,625,040
3,698,970
Bed
Volume
*BV
38,891
39,246
39,430
39,764
39,895
40,029
40,276
41,109
41,414
42,041
42,294
42,754
43,541
44,211
44,767
1,103
1,825
2,056
2,703
3,179
3,642
4,302
4,788
5,293
5,916
6,411
6,927
7,602
8,080
8,552
9,131
9,624
10,150
10,846
11,406
11,918
12,301
13,320
13,527
14,165
14,418
15,096
15,557
16,088
16,751
17,309
17,732
18,416
19,481
20,202
20,611
21,176
21,954
22,509
23,719
24,228
24,722
System Pressure
Inlet
psig
58
54
58
61
60
60
61
60
58
50
55
57
58
62
52
51
55
62
51
50
50
52
51
57
52
57
52
57
57
58
52
46
54
50
58
58
56
54
57
58
58
54
50
52
52
55
45
51
58
55
46
48
57
45
52
56
50
Outlet
psig
52
42
54
58
58
59
59
58
56
40
50
51
56
58
42
41
44
61
41
32
40
42
37
45
43
48
42
56
55
52
42
40
42
30
56
56
44
44
50
56
56
46
32
42
38
49
43
38
56
51
40
28
45
32
39
40
32
In-Out
psig
6
12
4
3
2
1
2
2
2
10
5
6
2
4
10
10
11
1
10
18
10
10
14
12
9
9
10
1
2
6
10
6
12
20
2
2
12
10
7
2
2
8
18
10
14
6
2
13
2
4
6
20
12
13
13
16
18
Differential
Pressure
DPI 1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-16
-------
Table A-2. EPA Arsenic Demonstration Project at Residence Hall, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
Ho.
1-i
153
1S3
15-
155
1E7
158
159
160
161
162
15-
1€€
170
173
173
17 =
184
185
Day of
Week
ue
Men
vVed
:'c"
~ut
Fri
Men
Wed
Man
~ue
i'cr-
~ue
~ue
}'•:!•
vVed
Men
Fri
:•:;-
vVed
Date
i2/C9;cs
I2;2s;cs
12.'3iyOS-
OI.'OS.'CS
oi;i3/c9
01/23.:.;-•::;
05/27/CS
C5,<'C1.--CS
07,.-17,.'C9
02,.'i7.-cs
Daaewa
Time
C- ^c
IMS
I*1S
S:-8
10:30
1*05
7:50
11:17
15:^5
15.13
7:5C
9:50
7:5C
S£l
11:50
1C:5S
15:35
8:CC
6:50
9'35
Tank Position
Lead
A'B
-
A
.A
-
A
A
A.
A
&
A
^
-
A
-
-
A
A
«
Lag
A.B
a
3
B
B
B
B
B
B
B
B
B
B
B
3
B
B
B
B
B
B
Treatment System
Flowrate1"
gpm
2;
2
o
n
2i
12
25
2
1
IS
30
3C
1
2i
10
18
12
12
-/
-
Totalizer
cial
17.3 5.220
17.- 2.C5C
17.- £.ic:
17,5 0.510
1 7,^7^.080
17.855.710
1S.Oi2.€7C
18.222.810
18.317. S5C
1 8.508.1 1C
1S.5s7.5SC
18,71i.52C
1S.5cC.1-C
15.102.750
1s.c17.1cC
2C.C32.-5C
2C.13-.3S
20. -88.78
2C.72E.S5
2C 75-'* 77
Daily IVater
Treated
gal
153. 52C
97 87C
5,010
32.810
143,170
1 1=30
1 5.9EC
1 0.1-0
5.1-C
1 :.:.:::
S.77C
115.8-0
2-5. :23
1-2.510
51 -.-1C
-15.2SC
1C1.9-C
35-. 390
2^0. C7C
57.920
Cum.
Throughput
gal
5.77;.E:::
S.S75.53C
8.881.5-0
S,91i.35C
9.057.520
9.23S.150
9. -25. 110
9.505.25:
9.701.390
9 592 oc:
9.9S1.120
10.097.950
10.3-3.5SC
io.ise.isc
11.CCO.SOC
11. -15.890
11.517.S3C
11.872.220
12.112.2SC
12.170.210
Bed
Volume
#BV
58.573
59.327
59.351
59.580
£p CT7
€1.751
53. CCO
5-.2C;
Ei.SiC
55.115
SS.71C
57.^91
59.132
70.085
73.52;
75.299
75. SSI
79,3-9
SC.S5-
81,341
System Pressure
Inlet
psig
5G
5C
61
61
!:S
58
S3
61
SC
c&
5;
58
61
Ei
5S
55
57
60
51
51
Outlet
psig
•
58
50
50
52
c^
50
51
5C
cc
is.
-2
50
-''
5S
54
52
CE
50
60
In-Out
psig
1C
2
1
1
6
-
8
0
C
3
1C
15
1
11
1
2
c
2
1
1
Differential
Pressure
DPI 1
psig
Q
C
C
Q
C
C
C
0
C
C
C
C
C
C
Q
C
C
C
C
C
DPI 2
psig
C
C
C
C
C
C
C
C
C
C
C
C
C
C
C
C
C
C
C
Note: System contains two vessels in series, each containing 20 ft3 of media.
Lead vessel (TB) rebedded with ARM 300 and put into lag position on January 24, 2007.
(a) From Week 5 through Week 20, flowrate readings recorded as a range; values recorded in table representing
midpoint of the range.
NA = not available
NM = not measured
A-17
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet
Week
No.
1
2
3
4
5
6
7
8
9
10
11
12
Day of
Week
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Date
02/17/06
02/20/06
02/21/06
02/22/06
02/23/06
02/24/06
02/27/06
02/28/06
03/01/06
03/02/06
03/03/06
03/06/06
03/07/06
03/08/06
03/09/06
03/10/06
03/13/06
03/14/06
03/15/06
03/16/06
03/17/06
03/20/06
03/21/06
03/22/06
03/23/06
03/24/06
03/27/06
03/28/06
03/29/06
03/30/06
03/31/06
04/03/06
04/04/06
04/05/06
04/06/06
04/07/06
04/10/06
04/1 1/06
04/12/06
04/13/06
04/14/06
04/17/06
04/18/06
04/19/06
04/20/06
04/21/06
04/24/06
04/25/06
04/26/06
04/27/06
04/28/06
05/01/06
05/02/06
05/03/06
05/04/06
05/05/06
Time
7:40
8:20
16:00
8:14
10:48
8:05
10:15
21:55
12:31
10:30
11:00
8:42
20:11
21:35
8:27
10:45
8:40
14:52
7:55
8:15
8:15
8:18
7:58
8:58
8:48
8:30
8:45
14:40
11:10
7:33
8:25
9:15
8:37
8:00
10:43
7:55
7:55
8:05
11:02
8:15
8:20
7:55
8:05
11:02
8:15
8:20
8:55
8:05
10:03
7:35
8:00
8:30
8:00
13:15
8:45
8:00
Tank Position
Lead
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Lag
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Treatments
Flow rate
gpm
7.5
11
5
14
11.5
6
11.5
12.5
11
15
10
5
5.5
8.5
4
23
4
4
2
2
1
3
3
3
3
1
2
1
1
3
3
7.5
11
12
17.5
2
2
2
2
4
3.5
10
4
8
3
26
1
3
28
2
2
2
4
4
2
4
Totalizer
gal
10,200
30,570
41,590
45,310
55,329
61,274
74,692
81,532
89,636
95,085
101,189
117,242
123,468
131,900
137,760
144,580
159,962
170,444
173,880
181,130
187,705
203,586
210,208
217,711
228,687
235,312
240,539
244,463
246,135
247,760
249,940
256,280
263,635
270,635
282,230
287,800
301,365
307,675
315,588
321,528
327,380
340,990
348,272
355,320
359,150
367,750
380,595
386,014
392,230
397,880
402,970
417,385
422,100
430,018
432,651
436,522
Daily Water
Treated
gal
NA
20,370
11,020
3,720
10,019
5,945
13,418
6,840
8,104
5,449
6,104
16,053
6,226
8,432
5,860
6,820
15,382
10,482
3,436
7,250
6,575
15,881
6,622
7,503
10,976
6,625
5,227
3,924
1,672
1,625
2,180
6,340
7,355
7,000
11,595
5,570
13,565
6,310
7,913
5,940
5,852
13,610
7,282
7,048
3,830
8,600
12,845
5,419
6,216
5,650
5,090
14,415
4,715
7,918
2,633
3,871
/stem
Cum.
Throughput
gal
NA
20,370
31,390
35,110
45,129
51,074
64,492
71,332
79,436
84,885
90,989
107,042
113,268
121,700
127,560
134,380
149,762
160,244
163,680
170,930
177,505
193,386
200,008
207,511
218,487
225,112
230,339
234,263
235,935
237,560
239,740
246,080
253,435
260,435
272,030
277,600
291,165
297,475
305,388
311,328
317,180
330,790
338,072
345,120
348,950
357,550
370,395
375,814
382,030
387,680
392,770
407,185
411,900
419,818
422,451
426,322
Bed Volume
#BV
NA
170
262
293
377
427
539
596
664
709
760
894
946
1,017
1,066
1,123
1,251
1,339
1,367
1,428
1,483
1,616
1,671
1,734
1,825
1,881
1,924
1,957
1,971
1,985
2,003
2,056
2,117
2,176
2,273
2,319
2,433
2,485
2,551
2,601
2,650
2,764
2,824
2,883
2,915
2,987
3,094
3,140
3,192
3,239
3,281
3,402
3,442
3,508
3,530
3,562
System Pressure
Inlet
psig
60
61
64
62
61
61
60
60
64
60
62
62
60
62
62
60
60
61
62
60
62
60
61
61
61
60
60
60
62
62
64
60
60
61
60
60
62
62
62
61
62
60
61
61
61
62
61
60
63
63
61
62
62
61
61
61
Outlet
psig
60
61
64
62
60
62
60
60
61
54
62
62
61
62
62
55
60
61
62
60
61
61
62
62
60
61
60
60
62
62
64
60
61
58
60
60
61
61
62
62
61
60
61
62
62
50
60
61
57
63
61
63
62
61
61
61
In-Out
psig
0
0
0
0
1
-1
0
0
3
6
0
0
-1
0
0
5
0
0
0
0
1
-1
-1
-1
1
-1
0
0
0
0
0
0
-1
3
0
0
1
1
0
-1
1
0
0
-1
-1
12
1
-1
6
0
0
-1
0
0
0
0
Differential
Pressure Across
Vessel
DPI1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-18
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet(Cont.)
Week
No.
13
14
15
16
17
18
19
20
21
22
23
Day of
Week
Mon
Tue
V\fed
Thu
Fri
Mon
Tue
V\fed
Thu
Fri
Mon
Tue
V\fed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Tue
Wed
Thu
Fri
Date
05/08/06
05/09/06
05/10/06
05/1 1/06
05/12/06
05/15/06
05/16/06
05/17/06
05/18/06
05/19/06
05/22/06
05/23/06
05/24/06
05/25/06
05/26/06
05/30/06
05/31/06
06/01/06
06/02/06
06/05/06
06/06/06
06/07/06
06/08/06
06/09/06
06/12/06
06/13/06
06/14/06
06/15/06
06/16/06
06/19/06
06/20/06
06/21/06
06/22/06
06/23/06
06/26/06
06/27/06
06/28/06
06/29/06
06/30/06
07/03/06
07/04/06
07/05/06
07/06/06
07/07/06
07/10/06
07/11/06
07/12/06
07/13/06
07/18/06
07/19/06
07/20/06
07/21/06
Time
8:43
1:29
15:00
8:42
8:05
8:20
8:10
10:40
13:20
15:40
8:10
9:20
11:01
14:05
9:27
8:10
9:10
7:30
7:45
2:36
7:40
10:45
13:55
9:57
9:08
8:15
10:16
8:15
8:25
8:30
8:00
10:00
7:46
7:50
10:40
11:10
8:10
8:00
8:15
7:45
NA
1:05
8:30
7:30
7:20
7:25
8:30
7:45
13:20
11:45
9:45
8:20
Tank Position
Lead
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Lag
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Treatments
Flow rate
gpm
2
32
2
2
2
2
2
0
10
0
0
0
20
20
20
18
0
0
0
0
0
24
20
32
0
0
15
0
0
10
0
0
0
0
20
0
0
0
0
30
NA
22
20
2
2
3
18
2
18
0
2
12
Totalizer
gal
445,242
450,262
454,444
456,220
459,565
468,132
470,860
473,066
475,590
477,452
481,444
484,755
490,100
494,360
496,865
504,712
507,636
510,512
512,885
520,581
522,705
524,909
528,330
529,690
535,801
538,887
541,660
543,975
546,231
551,045
552,128
552,642
553,035
553,286
554,000
554,234
554,279
554,325
555,708
560,240
NA
566,560
567,765
569,870
580,874
584,036
588,109
591,338
604,165
2,621
5,954
9,941
Daily Water
Treated
gal
8,720
5,020
4,182
1,776
3,345
8,567
2,728
2,206
2,524
1,862
3,992
3,311
5,345
4,260
2,505
7,847
2,924
2,876
2,373
7,696
2,124
2,204
3,421
1,360
22,916
3,086
2,773
2,315
2,256
4,814
1,083
514
393
251
714
234
45
46
1,383
4,532
NA
6,320
1,205
2,105
11,004
3,162
4,073
3,229
12,827
2,970
3,333
3,987
/stem
Cum.
Throughput
gal
435,042
440,062
444,244
446,020
449,365
457,932
460,660
462,866
465,390
467,252
471,244
474,555
479,900
484,160
486,665
494,512
497,436
500,312
502,685
510,381
512,505
514,709
518,130
519,490
525,601
528,687
531,460
533,775
536,031
540,845
541,928
542,442
542,835
543,086
543,800
544,034
544,079
544,125
545,508
550,040
NA
556,360
557,565
559,670
570,674
573,836
577,909
581,138
593,965
596,935
600,268
604,255
Bed Volume
#BV
3,635
3,677
3,712
3,727
3,755
3,826
3,849
3,868
3,889
3,904
3,938
3,965
4,010
4,045
4,066
4,132
4,156
4,180
4,200
4,265
4,282
4,301
4,329
4,341
4,392
4,418
4,441
4,460
4,479
4,519
4,528
4,532
4,536
4,538
4,544
4,546
4,546
4,546
4,558
4,596
NA
4,649
4,659
4,676
4,768
4,795
4,829
4,856
4,963
4,988
5,016
5,049
System Pressure
Inlet
psig
62
60
59
61
61
62
61
61
60
58
60
60
60
60
60
60
60
62
62
62
59
60
61
62
62
62
61
61
61
62
61
61
62
61
61
62
61
62
62
59
NA
62
60
62
61
61
60
61
60
62
62
62
Outlet
psig
62
48
59
61
61
62
61
61
58
58
60
60
58
58
60
58
59
57
60
62
58
54
55
54
60
60
58
60
60
61
61
61
62
61
59
55
58
61
61
48
NA
52
57
62
61
59
55
60
55
61
62
61
In-Out
psig
0
12
0
0
0
0
0
0
2
0
0
0
2
2
0
2
1
5
2
0
1
6
6
8
2
2
3
1
1
1
0
0
0
0
2
7
3
1
1
11
NA
10
3
0
0
2
5
1
5
1
0
1
Differential
Pressure Across
Vessel
DPI1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-19
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
24
25
26
27
28
29
30
31
32
33
34
35
36
Day of
Week
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Fri
Mon
Tue
Wed
Thu
Fri
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Tue
Wed
Thu
Fri
Mon
Wed
Date
07/24/06
07/25/06
07/26/06
07/27/06
07/28/06
07/31/06
08/01/06
08/02/06
08/03/06
08/04/06
08/07/06
08/08/06
08/09/06
08/10/06
08/11/06
08/15/06
08/16/06
08/17/06
08/18/06
08/25/06
08/28/06
08/29/06
08/30/06
08/31/06
09/01/06
09/05/06
09/06/06
09/07/06
09/08/06
09/11/06
09/12/06
09/13/06
09/14/06
09/15/06
09/18/06
09/19/06
09/20/06
09/21/06
09/22/06
09/25/06
09/26/06
09/27/06
09/28/06
09/29/06
10/02/06
10/03/06
10/04/06
10/05/06
10/06/06
10/09/06
10/10/06
10/11/06
10/12/06
10/13/06
10/16/06
10/18/06
Time
0:00
8:30
14:05
9:50
9:45
8:10
7:12
8:35
7:15
7:20
7:30
7:30
7:20
14:30
13:00
7:35
7:24
7:45
7:35
14:00
7:15
7:30
9:16
7:30
7:25
7:35
7:40
7:21
14:20
10:00
7:50
8:50
8:00
8:00
7:30
15:40
7:30
7:10
6:25
7:40
7:35
8:40
15:30
9:20
7:45
8:30
9:40
9:00
8:30
7:30
10:30
8:47
8:10
15:30
8:05
15:45
Tank Position
Lead
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Lag
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Treatments
Flow rate
gpm
8
4
2
2
1
12
2
2
1
1
1
2
2
2
2
0
4
2
2
2
2
1
20
2
2
1
3
2
2
4
2
3
3
2
4
8
2
3
3
3
2
6
2
3
16
2
14
0
8
25
4
3
5
2
2
33
Totalizer
gal
17,750
24,415
24,970
27,515
30,294
35,840
39,111
43,295
46,470
50,531
57,432
61,034
64,578
70,575
72,685
82,555
86,061
89,138
92,340
112,668
117,910
121,220
124,540
129,433
132,250
140,512
143,290
146,800
150,790
157,468
160,710
165,230
169,200
173,490
179,610
189,720
193,080
198,834
204,730
218,525
226,580
234,750
246,965
252,290
265,800
275,355
284,090
291,444
298,582
311,200
319,540
326,880
336,500
347,970
356,480
373,660
Daily Water
Treated
gal
7,809
6,665
555
2,545
2,779
5,546
3,271
4,184
3,175
4,061
6,901
3,602
3,544
5,997
2,110
9,870
3,506
3,077
3,202
20,328
5,242
3,310
3,320
4,893
2,817
8,262
2,778
3,510
3,990
6,678
3,242
4,520
3,970
4,290
6,120
10,110
3,360
5,754
5,896
13,795
8,055
8,170
12,215
5,325
13,510
9,555
8,735
7,354
7,138
12,618
8,340
7,340
9,620
11,470
8,510
17,180
/stem
Cum.
Throughput
gal
612,064
618,729
619,284
621,829
624,608
630,154
633,425
637,609
640,784
644,845
651,746
655,348
658,892
664,889
666,999
676,869
680,375
683,452
686,654
706,982
712,224
715,534
718,854
723,747
726,564
734,826
737,604
741,114
745,104
751,782
755,024
759,544
763,514
767,804
773,924
784,034
787,394
793,148
799,044
812,839
820,894
829,064
841,279
846,604
860,114
869,669
878,404
885,758
892,896
905,514
913,854
921,194
930,814
942,284
950,794
967,974
Bed Volume
#BV
5,114
5,170
5,174
5,196
5,219
5,265
5,293
5,328
5,354
5,388
5,446
5,476
5,505
5,556
5,573
5,656
5,685
5,711
5,737
5,907
5,951
5,979
6,006
6,047
6,071
6,140
6,163
6,192
6,226
6,282
6,309
6,346
6,380
6,415
6,467
6,551
6,579
6,627
6,677
6,792
6,859
6,927
7,029
7,074
7,187
7,267
7,340
7,401
7,461
7,566
7,636
7,697
7,778
7,873
7,944
8,088
System Pressure
Inlet
psig
62
60
61
61
61
60
61
61
61
62
62
60
62
60
62
62
61
61
61
60
60
60
55
61
62
60
55
61
62
61
61
60
60
61
61
60
60
60
60
60
61
60
60
61
60
61
60
62
60
60
60
61
60
61
60
58
Outlet
psig
61
60
61
61
61
58
61
60
61
62
61
60
61
60
61
61
59
60
60
58
60
60
60
60
61
60
60
60
61
59
60
60
60
60
60
58
59
59
59
48
59
60
60
60
58
61
58
62
58
54
58
59
58
60
60
50
In-Out
psig
1
0
0
0
0
2
0
1
0
0
1
0
1
0
1
1
2
1
1
2
0
0
-5
1
1
0
-5
1
1
2
1
0
0
1
1
2
1
1
1
12
2
0
0
1
2
0
2
0
2
6
2
2
2
1
0
8
Differential
Pressure Across
Vessel
DPI1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-20
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
37
38
39
40
41
51
52
53
54
55
56
57
58
59
60
61
62
63
64
Day of
Week
Wed
Thu
Fri
Mon
Wed
Fri
Mon
Wed
Thu
Tue
Wed
Fri
Mon
Wed
Mon
Tue
Wed
Fri
Mon
Tue
Wed
Mon
Wed
Fri
Mon
Tue
Fri
Tue
Thu
Fri
Tue
Wed
Fri
Tue
Thu
Fri
Mon
Wed
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Thu
Fri
Mon
Wed
Fri
Date
10/25/06
10/26/06
10/27/06
10/30/06
11/01/06
1 1/03/06
1 1/05/06
1 1/07/06
1 1/08/06
11/14/06
11/15/06
11/17/06
1 1/20/06
1 1/22/06
1 1/27/06
1 1/28/06
1 1/29/06
12/01/06
12/04/06
12/05/06
12/06/06
12/11/06
12/13/06
12/15/06
12/18/06
12/19/06
12/22/06
01/02/07
01/04/07
01/05/07
01/09/07
01/10/07
01/12/07
01/16/07
01/18/07
01/19/07
01/22/07
01/24/07
01/29/07
01/31/07
02/02/07
02/05/07
02/07/07
02/09/07
02/12/07
02/14/07
02/16/07
02/19/07
02/21/07
02/23/07
02/26/07
02/28/07
03/01/07
03/02/07
03/05/07
03/07/07
03/09/07
Time
11:55
9:40
11:35
7:35
9:50
8:52
9:00
9:30
9:30
9:00
8:30
11:25
9:20
9:00
7:15
8:30
14:00
14:15
8:00
8:30
8:10
7:35
10:35
9:50
10:10
13:45
NA
9:40
12:10
10:30
13:10
11:12
15:00
7:50
14:05
14:10
8:30
7:50
8:15
8:13
9:20
8:20
10:05
8:30
8:08
8:19
11:30
8:55
10:35
3:08
3:05
4:23
9:40
2:45
9:45
15:05
8:35
Tank Position
Lead
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Lag
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Treatments
Flow rate
gpm
12
25
3
3
2
3
4
12
18
0
4
5
8
0
0
2
12
1
2
10
4
1
3
2
1
2
1
4
3
4
20
18
8
14
3
0
2
11
3
4
1
3
2
1
10
4
3
3
2
2
4
2
8
2
2
1
2
Totalizer
gal
415,440
421,870
429,360
443,050
459,460
473,930
485,790
501,020
508,010
530,460
550,910
551,535
562,220
575,660
586,500
593,100
601,380
614,000
622,790
629,700
635,140
652,410
658,900
665,000
669,650
672,120
678,730
696,570
701,470
703,490
722,440
728,030
737,060
757,260
766,700
772,600
780,830
793,610
819,400
832,500
845,590
854,990
867,360
879,230
886,930
898,600
910,010
919,300
931,120
941,490
949,220
958,010
963,290
970,000
975,280
989,440
996,930
Daily Water
Treated
gal
41,780
6,430
7,490
13,690
16,410
14,470
11,860
15,230
6,990
22,450
20,450
625
10,685
13,440
10,840
6,600
8,280
12,620
8,790
6,910
5,440
17,270
6,490
6,100
4,650
2,470
6,610
17,840
4,900
2,020
18,950
5,590
9,030
20,200
9,440
5,900
8,230
12,780
25,790
13,100
13,090
9,400
12,370
11,870
7,700
11,670
11,410
9,290
11,820
10,370
7,730
8,790
5,280
6,710
5,280
14,160
7,490
/stem
Cum.
Throughput
gal
1,009,754
1,016,184
1,023,674
1,037,364
1,053,774
1,068,244
1,080,104
1,095,334
1,102,324
1,124,774
1,145,224
1,145,849
1,156,534
1,169,974
1,180,814
1,187,414
1,195,694
1,208,314
1,217,104
1,224,014
1,229,454
1,246,724
1,253,214
1,259,314
1,263,964
1,266,434
1,273,044
1,290,884
1,295,784
1,297,804
1,316,754
1,322,344
1,331,374
1,351,574
1,361,014
1,366,914
1,375,144
1,387,924
1,413,714
1,426,814
1,439,904
1,449,304
1,461,674
1,473,544
1,481,244
1,492,914
1,504,324
1,513,614
1,525,434
1,535,804
1,543,534
1,552,324
1,557,604
1,564,314
1,569,594
1,583,754
1,591,244
Bed Volume
#BV
8,437
8,491
8,553
8,668
8,805
8,926
9,025
9,152
9,211
9,398
9,569
9,574
9,664
9,776
9,866
9,922
9,991
10,096
10,170
10,227
10,273
10,417
10,471
10,522
10,561
10,582
10,637
10,786
10,827
10,844
11,002
11,049
11,124
11,293
11,372
11,421
11,490
11,597
11,812
11,922
12,031
12,110
12,213
12,312
12,377
12,474
12,570
12,647
12,746
12,833
12,897
12,971
13,015
13,071
13,115
13,233
13,296
System Pressure
Inlet
psig
60
59
60
61
61
60
59
60
60
61
60
60
56
59
61
61
60
60
60
60
60
63
58
62
62
61
61
61
62
61
60
61
59
60
61
61
62
59
62
61
60
61
61
61
60
59
60
61
61
62
61
61
61
60
63
63
63
Outlet
psig
58
54
60
61
61
60
58
58
58
61
57
60
57
59
61
60
58
60
60
58
60
62
58
61
62
61
61
60
60
61
55
58
58
58
60
60
61
58
61
61
60
60
61
61
60
58
61
61
61
62
60
61
60
60
62
62
62
In-Out
psig
2
5
0
0
0
0
1
2
2
0
3
0
-1
0
0
1
2
0
0
2
0
1
0
1
0
0
0
1
2
0
5
3
1
2
1
1
1
1
1
0
0
1
0
0
0
1
-1
0
0
0
1
0
1
0
1
1
1
Differential
Pressure Across
Vessel
DPI1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-21
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
65
66
67
68
69
70
71
72
73
74
75
76
77
78
79
80
81
82
83
84
85
86
87
88
89
90
Day of
Week
Mon
Wed
Fri
Mon
Thu
Mon
Thu
Mon
Tue
Wed
Fri
Mon
Wed
Fri
Mon
Fri
Mon
Wed
Fri
Mon
Wed
Wed
Fri
Mon
Wed
Thu
Fri
Mon
Wed
Tue
Wed
Fri
Mon
Thu
Tue
Fri
Mon
Wed
Fri
Mon
Thu
Fri
Mon
Wed
Mon
Wed
Mon
Thu
Fri
Mon
Wed
Fri
Mon
Wed
Mon
Wed
Thu
Fri
Tue
Fri
Mon
Wed
Tue
Date
03/12/07
03/14/07
03/16/07
03/19/07
03/22/07
03/26/07
03/29/07
04/02/07
04/03/07
04/04/07
04/06/07
04/09/07
04/11/07
04/13/07
04/16/07
04/20/07
04/23/07
04/25/07
04/27/07
04/30/07
05/02/07
05/09/07
05/11/07
05/14/07
05/16/07
05/17/07
05/18/07
05/21/07
05/23/07
05/29/07
05/30/07
06/01/07
06/04/07
06/07/07
06/12/07
06/15/07
06/18/07
06/27/07
06/29/07
07/02/07
07/05/07
07/06/07
07/09/07
07/09/07
07/16/07
07/18/07
07/23/07
07/25/07
07/27/07
07/30/07
08/01/07
08/03/07
08/06/07
08/08/07
08/13/07
08/15/07
08/16/07
08/17/07
08/21/07
08/24/07
08/26/07
08/28/07
09/04/07
Time
8:32
9:12
9:00
13:05
7:55
11:55
8:59
9:09
8:15
11:25
8:50
8:00
9:15
8:25
8:15
8:15
5:14
8:10
7:40
10:30
11:02
15:10
10:30
8:35
11:10
9:05
14:45
13:54
15:50
11:00
10:35
10:20
10:00
10:24
9:42
14:10
NA
8:40
11:50
11:00
8:15
8:32
8:05
2:00
9:40
12:35
7:45
8:50
8:20
8:30
10:26
10:19
9:05
8:00
10:25
8:10
9:50
10:20
8:32
10:25
8:05
8:40
8:20
Tank Position
Lead
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Lag
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Treatment System
Flow rate
gpm
15
2
4
2
2
1
4
2
2
15
1
0
2
18
4
10
20
16
0
10
12
2
3
2
30
2
15
18
3
4
4
15
0
8
20
1
8
4
11
3
1
0
0
5
0
8
5
10
6
28
10
4
2
3
3
2
3
12
2
0
0
0
0
Totalizer
gal
1,006,410
1,018,170
1,030,200
1,040,790
1,054,560
1,060,770
1,065,710
1,071,100
1,076,200
1,082,360
1,087,930
1,091,800
1,103,610
1,113,992
1,121,200
1,144,980
1,154,420
1,165,540
1,174,990
1,182,890
1,189,925
1,221,380
1,234,020
1,242,180
1,256,550
1,261,920
1,272,240
1,283,870
1,297,330
1,315,070
1,321,270
1,343,150
1,355,230
1,375,630
1,398,720
1,418,810
1,430,320
1,456,265
1,467,130
1,473,180
1,479,420
1,482,060
1,490,020
1,498,470
1,509,992
1,518,282
1,533,250
1,539,144
1,546,190
1,552,230
1,559,540
1,567,270
1,572,320
1,579,330
1,589,520
1,596,835
1,599,910
1,604,110
1,611,580
1,620,880
1,623,640
1,628,850
1,642,670
Daily Water
Treated
gal
9,480
1 1 ,760
12,030
10,590
13,770
6,210
4,940
5,390
5,100
6,160
5,570
3,870
11,810
10,382
7,208
23,780
9,440
11,120
9,450
7,900
7,035
31,455
12,640
8,160
14,370
5,370
10,320
11,630
13,460
17,740
6,200
21,880
12,080
20,400
23,090
20,090
11,510
25,945
10,865
6,050
6,240
2,640
7,960
8,450
11,522
8,290
14,968
5,894
7,046
6,040
7,310
7,730
5,050
7,010
10,190
7,315
3,075
4,200
7,470
9,300
2,760
5,210
13,820
Cum .
Throughput
gal
1,600,724
1,612,484
1,624,514
1,635,104
1,648,874
1,655,084
1,660,024
1,665,414
1,670,514
1,676,674
1,682,244
1,686,114
1,697,924
1,708,306
1,715,514
1,739,294
1,748,734
1,759,854
1,769,304
1,777,204
1,784,239
1,815,694
1,828,334
1,836,494
1,850,864
1,856,234
1,866,554
1,878,184
1,891,644
1,909,384
1,915,584
1,937,464
1,949,544
1,969,944
1,993,034
2,013,124
2,024,634
2,050,579
2,061,444
2,067,494
2,073,734
2,076,374
2,084,334
2,092,784
2,104,306
2,112,596
2,127,564
2,133,458
2,140,504
2,146,544
2,153,854
2,161,584
2,166,634
2,173,644
2,183,834
2,191,149
2,194,224
2,195,349
2,202,819
2,212,119
2,214,879
2,220,089
2,233,909
Bed Volume
#BV
13,375
13,473
13,574
13,662
13,777
13,829
13,871
13,916
13,958
14,010
14,056
14,089
14,187
14,274
14,334
14,533
14,612
14,705
14,784
14,850
14,908
15,171
15,277
15,345
15,465
15,510
15,596
15,693
15,806
15,954
16,006
16,189
16,290
16,460
16,653
16,821
16,917
17,134
17,225
17,275
17,327
17,349
17,416
17,486
17,583
17,652
17,777
17,826
17,885
17,936
17,997
18,061
18,104
18,162
18,247
18,308
18,334
18,343
18,406
18,484
18,507
18,550
18,666
System Pressure
Inlet
psig
61
62
60
62
60
62
62
62
62
58
62
0
0
60
60
60
61
60
60
60
60
60
62
61
61
60
60
60
60
60
60
58
62
60
60
60
60
62
60
60
60
58
61
62
62
62
60
61
61
60
62
63
60
62
61
61
62
61
63
62
63
62
62
Outlet
psig
61
62
61
61
59
62
61
61
61
60
61
0
0
58
60
60
58
28
61
58
58
60
61
61
54
60
58
58
60
60
60
55
61
59
58
60
60
61
58
60
60
58
59
60
60
60
63
62
62
50
60
61
60
61
60
62
61
61
62
61
62
61
61
In-Out
psig
0
0
-1
1
1
0
1
1
1
-2
1
0
0
2
0
0
3
32
-1
2
2
0
1
0
7
0
2
2
0
0
0
3
1
1
2
0
0
1
2
0
0
0
2
2
2
2
-3
-1
-1
10
2
2
0
1
1
-1
1
0
1
1
1
1
1
Differential
Pressure Across
Vessel
DP1 1
psig
0
0
0
0
0
0
0
0
0
0
0
63
64
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
64
63
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-22
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No.
91
92
93
94
95
96
97
98
99
100
101
102
103
104
105
106
107
108
109
110
111
113
114
115
116
117
118
120
121
123
124
126
127
129
131
132
133
139
140
144
145
147
148
149
150
151
Day of
Week
Mon
Tue
Wed
Fri
Mon
Wed
Fri
Mon
Wed
Tue
Wed
Mon
Wed
Fri
Mon
Wed
Tue
Mon
Wed
Tue
Thu
Wed
Fri
Wed
Mon
Tue
Fri
Wed
Tue
Fri
Tue
Fri
Mon
Mon
Tue
Fri
Wed
Mon
Wed
Tue
Thu
Thu
Tue
Thu
Mon
Thu
Tue
Mon
Fri
Mon
Thu
Fri
Wed
Fri
Fri
Mon
Wed
Mon
Tue
Thu
Mon
Wed
Mon
Date
09/10/07
09/11/07
09/12/07
09/14/07
10/01/07
10/03/07
10/05/07
10/15/07
10/19/07
10/23/07
10/24/07
10/29/07
10/31/07
11/02/07
11/05/07
11/07/07
11/20/07
12/03/07
12/12/07
12/18/07
12/20/07
12/26/07
12/28/07
01/09/08
01/28/08
01/29/08
02/01/08
02/13/08
02/26/08
02/29/08
03/04/08
03/07/08
03/10/08
03/17/08
03/24/08
03/28/08
04/09/08
04/14/08
04/22/08
04/29/08
05/01/08
05/08/08
05/13/08
05/29/08
06/02/08
06/19/08
06/24/08
07/07/08
07/18/08
07/28/08
08/07/08
08/15/08
08/20/08
10/03/08
10/10/08
11/10/08
11/19/08
12/01/08
12/09/08
12/18/08
12/29/08
12/31/08
01/05/09
Time
3:47
10:05
2:12
1:20
3:10
9:30
8:10
11:00
11:05
8:00
7:50
9:10
7:50
8:05
9:00
9:25
14:40
11:50
8:00
11:50
8:45
11:55
8:45
8:20
3:00
2:30
11:20
10:30
10:30
3:24
8:05
11:15
8:40
15:45
10:30
7:00
14:00
10:25
8:50
10:00
15:15
9:10
10:35
8:20
10:00
7:45
14:25
14:25
8:40
8:05
8:14
10:01
10:51
8:40
9:30
15:16
23:20
10:30
8:30
8:30
15:40
9:01
9:38
Tank Position
Lead
A/B
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
Lag
A/B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
B
Treatment System
Flow rate
gpm
3
3
8
3
4
20
0
0
0
0
0
8
3
2
0
0
5
4
1
18
4
2
1
0
0
5
0
0
2
15
2
5
5
5
1
3
2
12
10
4
18
12
12
2
14
2
2
4
2
5
2
14
4
3
4
15
3
10
0
2
1
1
4
Totalizer
gal
1,659,440
1,661,640
1,669,320
1,684,165
1,768,490
1,779,290
1,790,410
1,842,310
1,869,040
1,888,000
1,897,210
1,924,120
1,937,350
1,951,390
1,965,770
1,979,990
2,049,990
2,104,410
2,142,140
2,158,650
2,164,830
2,172,280
2,174,690
2,199,600
2,305,180
2,311,090
2,329,680
2,399,440
2,467,020
2,489,080
2,501,220
2,521,840
2,529,990
2,570,900
2,596,820
2,607,620
2,671,240
2,706,906
2,782,350
2,831,180
2,852,280
2,912,430
2,950,930
3,044,700
3,066,850
3,163,290
3,182,560
3,239,880
3,274,880
3,307,740
3,339,250
3,367,810
3,388,200
3,599,540
3,647,110
3,862,970
3,920,870
3,977,490
4,025,970
4,062,580
4,084,140
4,087,530
4,097,980
Daily Water
Treated
gal
16,770
2,200
7,680
14,845
84,325
10,800
11,120
51,900
26,730
18,960
9,210
26,910
13,230
14,040
14,380
14,220
70,000
54,420
37,730
16,510
6,180
7,450
2,410
24,910
105,580
5,910
18,590
69,760
67,580
22,060
12,140
20,620
8,150
40,910
25,920
10,800
63,620
35,666
75,444
48,830
21,100
60,150
38,500
93,770
22,150
96,440
19,270
57,320
35,000
32,860
31,510
28,560
20,390
211,340
47,570
215,860
57,900
56,620
48,480
36,610
21,560
3,390
10,450
Cum .
Throughput
gal
2,250,679
2,252,879
2,260,559
2,275,404
2,359,729
2,370,529
2,381,649
2,433,549
2,460,279
2,479,239
2,488,449
2,515,359
2,528,589
2,542,629
2,557,009
2,571,229
2,641,229
2,695,649
2,733,379
2,749,889
2,756,069
2,763,519
2,765,929
2,790,839
2,896,419
2,902,329
2,920,919
2,990,679
3,058,259
3,080,319
3,092,459
3,113,079
3,121,229
3,162,139
3,188,059
3,198,859
3,262,479
3,298,145
3,373,589
3,422,419
3,443,519
3,503,669
3,542,169
3,635,939
3,658,089
3,754,529
3,773,799
3,831,119
3,866,119
3,898,979
3,930,489
3,959,049
3,979,439
4,190,779
4,238,349
4,454,209
4,512,109
4,568,729
4,617,209
4,653,819
4,675,379
4,678,769
4,689,219
Bed Volume
#BV
18,806
18,824
18,888
19,012
19,717
19,807
19,900
20,334
20,557
20,716
20,793
21,017
21,128
21,245
21,365
21,484
22,069
22,524
22,839
22,977
23,029
23,091
23,111
23,319
24,201
24,251
24,406
24,989
25,554
25,738
25,839
26,012
26,080
26,422
26,638
26,728
27,260
27,558
28,188
28,596
28,773
29,275
29,597
30,381
30,566
31,371
31,532
32,011
32,304
32,578
32,842
33,080
33,251
35,017
35,414
37,218
37,701
38,175
38,580
38,886
39,066
39,094
39,181
System Pressure
Inlet
psig
60
60
60
59
62
60
63
62
60
61
62
62
62
62
60
61
61
62
62
60
62
63
62
61
61
61
60
63
60
61
62
61
61
62
61
61
62
61
61
61
60
60
61
60
60
61
61
59
60
61
61
60
62
62
62
60
62
59
60
62
62
63
63
Outlet
psig
59
59
60
58
61
58
62
61
58
62
61
60
61
61
60
59
60
61
62
55
62
64
63
62
60
60
61
62
60
60
62
61
61
61
62
61
61
59
60
60
57
58
58
60
58
61
61
58
59
60
60
58
60
61
62
58
61
59
60
62
62
62
62
In-Out
psig
1
1
0
1
1
2
1
1
2
-1
1
2
1
1
0
2
1
1
0
5
0
-1
-1
-1
1
1
-1
1
0
1
0
0
0
1
-1
0
1
2
1
1
3
2
3
0
2
0
0
1
1
1
1
2
2
1
0
2
1
0
0
0
0
1
1
Differential
Pressure Across
Vessel
DPI1
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
DPI 2
psig
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
A-23
-------
Table A-3. EPA Arsenic Demonstration Project at College Union, Klamath Falls, OR - Daily System
Operation Log Sheet (Cont.)
Week
No,
IE:
153
1SS
155
157
tsa
159
161
IK
1 = 5
187
170
17?
1 "^
154
IK
Day o'
Week
~LJ&
Fri
Men
firt
1.1 on
1.1 en
Men
Wed
~ue
re-
Man
•Ved
I'c-
Fri
"c-
vVed
Date
01/13/09
01/23/09
C2/C2/C9
02/06/09
C2.'tc/C9
02/26/09
C3/C2/C9
C3/C9/Cs
03/2E/OS
04/06/09
C4.'20/C9
C5,''C4.'C9
CE/27/C9
Cc'CI/CS
C7.'t7/C9
CSH7/C9
CS/26/C9
Time
9:55
13:2C
8:15
1E:3£
15:25
14;4C
T-CC
8:3 C
11:iC
£*37
11:2C
11:35
S:-1
15:5C
E:29
c:4C
jMg
Tank Position
Lead
AVB
A.
A
A
-
A
-
A
t.
1—
~
-
.
Lag
A'B
B
B
B
B
B
B
B
5
B
5
5
B
3
5
5
5
3
Treatment System
Flowrate
gpm
20
"
2
10
20
2
2
1
3
34
3
4
5
3
7
1
3
Totalizer
gal
4.14E.44C
4.2C1.C1C
-.2-i.--C
4.2S4.;;c
- ^-- -CC
-.-CS.23C
4.424. 3CC
4.4£;.S9C
4.E4T.42C
4.cc3.ia
-,-:7i.2C
4.7;o.cZ
4.5C£.:c
-.s;c.iC
?.17f.i7
;.2;;.;i
E.29£.EtC
Daily W ate r
Treated
qa
47 -"C
E5.57C
4E.43C
34.S2C
SC.CiC
:3.B3C
1 = .C7C
3S.5SC
S2.E3C
116.75
1 c.C2
1-C.2:
51.52
21 -.2-7
5C.2-
•>3 CC
Cum.
Throughput
gal
^.735.c79
4.752.2-S
^ s ^ r ^ "^ c
^ H7C C^C
4.53E.t35
4.999.4=9
E.C1E.E38
5.C55.129
E.137.SE9
c 25- 4 1 9
5.27C.4?:
E.EC:,315
5.552.135
5,766,506
"l.Ct 1.745
5. £59.749
Bed Volume
#BV
35.575
4C.C42
4C.4-7
4C.739
41.240
41.774
41. 90S
42.52S
4 .904
4 .G3B
-------
APPENDIX B
ANALYTICAL RESULTS
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as
CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
«3/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
01/11/06
IN
-
114
<0.1
21.0
0.5
<50(c)
31.1
0.4
7.3
13.7
4.2
340
0.3
77.0
53.9
23.1
29.8
29.7
0.1
0.6
29.1
<25
<25
<0.1
<0.1
TT
0.5
110
<0.1
30.0
0.2
<50(c)
11.4
0.7
6.9
13.5
3.3
334
0.0
82.2
57.9
24.3
0.1
0.1
<0.1
0.5
<0.1
28.4
<25
<0.1
<0.1
01/24/06
IN
-
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
31.2
-
-
-
-
-
-
-
-
TA1
0.7
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
0.1
-
-
-
-
-
-
-
-
TB1
0.7
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
0.1
-
-
-
-
-
-
-
-
TA2
0.9
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
0.9
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
<0.1
-
-
-
-
-
-
-
-
2/1/2006(d)
IN
-
-
-
-
-
-
-
-
7.5
13.3
3.3
491
0.3
-
-
-
32.4
-
-
-
-
-
-
-
-
TA1
0.8
-
-
-
-
-
-
-
7.0
14.4
3.3
466
0.0
-
-
-
0.3
-
-
-
-
-
-
-
-
TB1
0.8
-
-
-
-
-
-
-
7.3
13.4
3.6
462
0.0
-
-
-
0.4
-
-
-
-
-
-
-
-
TA2
1.1
-
-
-
-
-
-
-
7.2
13.9
3.9
472
0.0
-
-
-
0.3
-
-
-
-
-
-
-
-
TB2
1.1
-
-
-
-
-
-
-
7.4
13.3
3.4
462
0.1
-
-
-
0.5
-
-
-
-
-
-
-
-
02/14/06(e)
IN
-
-
-
-
-
-
-
-
8.1
73.3
3.5
428
0.4
-
-
-
26.5
-
-
-
-
-
-
-
-
TA1
1.1
-
-
-
-
-
-
-
7.9
13.8
3.2
444
0.0
-
-
-
0.1
-
-
-
-
-
-
-
-
TB1
1.1
-
-
-
-
-
-
-
8.1
13.5
2.9
448
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TA2
1.5
-
-
-
-
-
-
-
7.9
13.6
3.2
448
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
1.5
-
-
-
-
-
-
-
8.1
13.2
3.3
450
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
03/01/06
IN
-
-
-
-
-
-
-
-
7.7
13.6
3.5
319
0.3
-
-
-
27.0
-
-
-
-
-
-
-
-
TA1
1.4
-
-
-
-
-
-
-
7.8
13.3
3.5
326
0.0
-
-
-
0.1
-
-
-
-
-
-
-
-
TB1
1.4
-
-
-
-
-
-
-
8.0
13.5
3.3
320
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TA2
1.8
-
-
-
-
-
-
-
8.0
13.4
3.2
344
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
1.8
-
-
-
-
-
-
-
8.1
13.5
3.3
359
0.0
-
-
-
0.2
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) Result is measurement of orthophosphate as P.
(d) Water quality readings taken on 02/09/06.
(e) Water quality readings taken on 02/21/06.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L<"
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
03/14/06
IN
-
112
<0.1
21.5
0.7
<10
29.9
0.4
7.8
13.3
3.9
432
0.3
82.4
60.2
22.2
31.2
31.0
0.2
0.6
30.4
<25
<25
0.1
<0.1
TT
1.9
112
<0.1
22.3
0.6
<10
24.9
0.9
8.4
12.8
2.7
458
0.0
80.8
57.9
22.9
0.2
<0.1
<0.1
0.1
<0.1
<25
<25
0.1
<0.1
03/29/06
IN
-
-
-
-
-
-
-
-
8.0
17.7
4.2
476
0.2
-
-
-
30.2
29.6
-
-
-
-
-
-
-
-
TA1
2.0
-
-
-
-
-
-
-
8.2
13.0
4.2
456
0.1
-
-
-
<0.1
<0.1
-
-
-
-
-
-
-
-
TB1
2.0
-
-
-
-
-
-
-
8.4
12.9
3.3
446
0.1
-
-
-
<0.1
<0.1
-
-
-
-
-
-
-
-
TA2
2.4
-
-
-
-
-
-
-
8.3
12.8
3.6
445
0.1
-
-
-
<0.1
<0.1
-
-
-
-
-
-
-
-
TB2
2.4
-
-
-
-
-
-
-
8.4
12.9
3.3
442
0.1
-
-
-
<0.1
<0.1
-
-
-
-
-
-
-
-
04/12/06
IN
-
-
-
-
-
-
-
-
7.8
14.0
3.8
414
0.3
-
-
-
29.0
-
-
-
-
-
-
-
-
TA1
2.4
-
-
-
-
-
-
-
7.9
13.8
3.9
418
0.1
-
-
-
0.3
-
-
-
-
-
-
-
-
TB1
2.4
-
-
-
-
-
-
-
8.1
13.6
3.4
405
0.1
-
-
-
0.2
-
-
-
-
-
-
-
-
TA2
2.9
-
-
-
-
-
-
-
8.1
13.5
3.4
402
0.1
-
-
-
0.2
-
-
-
-
-
-
-
-
TB2
2.9
-
-
-
-
-
-
-
8.1
13.7
3.4
403
0.1
-
-
-
0.3
-
-
-
-
-
-
-
-
04/26/06
IN
-
-
-
-
-
-
-
-
8.1
16.1
4.8
581
0.3
-
-
-
27.4
-
-
-
-
-
-
-
-
TA1
3.0
-
-
-
-
-
-
-
8.3
16.7
2.8
471
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB1
3.0
-
-
-
-
-
-
-
8.3
16.0
3.2
456
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TA2
3.4
-
-
-
-
-
-
-
8.2
16.4
3.4
465
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
3.4
-
-
-
-
-
-
-
8.3
16.2
3.4
453
0.1
-
-
-
0.1
-
-
-
-
-
-
-
-
05/09/06
IN
-
122
<0.1
22
0.9
<10
31.2
0.6
8.1
20.6
4.0
433
0.3
107
79.1
27.6
28.7
28.6
<0.1
0.2
28.4
<25
<25
<0.1
<0.1
TT
3.6
109
<0.1
22
0.8
<10
29.6
0.8
8.0
19.0
3.4
364
0.1
106
78.5
27.4
<0.1
<0.1
<0.1
0.2
<0.1
<25
<25
<0.1
<0.1
(a) as CaCO3.
(b) as P.
Lead Vessels: TB1, TB2; Lag Vessels: TA1,
TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
05/24/06
IN
-
-
-
-
-
-
-
-
7.9
20.5
3.1
438
0.3
-
-
-
25.7
-
-
-
-
-
-
-
-
TA1
3.8
-
-
-
-
-
-
-
7.8
20.6
3.3
425
0.2
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB1
3.8
-
-
-
-
-
-
-
8.0
21.6
3.0
416
0.2
-
-
-
7.0
-
-
-
-
-
-
-
-
TA2
4.3
-
-
-
-
-
-
-
8.1
21.5
3.2
422
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
4.3
-
-
-
-
-
-
-
8.1
21.3
3.0
456
0.1
-
-
-
1.0
-
-
-
-
-
-
-
-
06/07/06
IN
-
118
<0.1
22
1.0
<10
31.0
0.3
7.9
22.8
3.8
397
0.3
86.7
63.4
23.3
29.3
27.6
1.7
0.2
27.4
<25
<25
<0.1
<0.1
TT
4.5
101
<0.1
21
0.9
<10
30.6
0.3
7.9
22.5
3.1
346
0.0
84.9
62.3
22.6
<0.1
<0.1
<0.1
0.2
<0.1
<25
<25
<0.1
<0.1
06/21/06
IN
-
-
-
-
-
-
-
-
8.0
22.6
3.1
508
0.3
-
-
-
32.4
-
-
-
-
-
-
-
-
TA1
4.8
-
-
-
-
-
-
-
8.0
22.7
2.8
457
0.0
-
-
-
0.2
-
-
-
-
-
-
-
-
TB1
4.8
-
-
-
-
-
-
-
8.0
22.0
3.4
473
0.0
-
-
-
5.3
-
-
-
-
-
-
-
-
TA2
5.2
-
-
-
-
-
-
-
7.9
22.0
3.6
454
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
5.2
-
-
-
-
-
-
-
8.0
21.9
3.3
449
0.0
-
-
-
0.9
-
-
-
-
-
-
-
-
07/05/06
IN
-
113
<0.1
21
0.7
<10
31.1
0.5
8.0
23.2
NA(C)
542
0.3
72.3
54.5
17.8
29.3
30.1
<0.1
<0.1
30.0
<25
<25
0.6
<0.1
TT
5.4
113
<0.1
20
0.8
<10
31.5
0.7
7.9
23.0
NA(C)
438
0.0
74.2
53.7
20.4
<0.1
<0.1
<0.1
<0.1
<0.1
<25
<25
0.5
<0.1
07/19/06
IN
-
-
-
-
-
-
-
-
8.0
23.8
3.1
524
0.3
-
-
-
30.7
31.3
-
-
-
-
-
-
-
-
TA1
5.5
-
-
-
-
-
-
-
8.2
23.4
2.3
436
0.1
-
-
-
<0.1
<0.1
-
-
-
-
-
-
-
-
TB1
5.5
-
-
-
-
-
-
-
8.0
23.4
3.0
419
0.1
-
-
-
3.6
3.8
-
-
-
-
-
-
-
-
TA2
6.0
-
-
-
-
-
-
-
7.9
23.4
3.2
414
0.1
-
-
-
<0.1
<0.1
-
-
-
-
-
-
-
-
TB2
6.0
-
-
-
-
-
-
-
8.0
23.7
3.0
404
0.0
-
-
-
0.8
0.8
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L("
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
08/02/06
IN
-
114
0.5
22
0.6
12.3
28.0
0.4
7.9
23.5
2.4
517
0.3
76.4
58.0
18.4
32.6
31.6
1.0
0.1
31.4
<25
<25
0.2
0.2
TT
6.2
114
0.5
22
0.8
<10
28.5
0.2
7.9
23.1
2.7
264
0.1
81.4
60.4
20.9
<0.1
<0.1
<0.1
0.1
<0.1
<25
<25
<0.1
0.2
08/16/06
IN
-
-
-
-
-
-
-
-
7.9
22.8
3.2
544
0.4
-
-
-
28.9
-
-
-
-
-
-
-
-
TA1
6.3
-
-
-
-
-
-
-
7.9
22.8
2.8
264
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB1
6.3
-
-
-
-
-
-
-
8.1
22.7
3.3
255
0.1
-
-
-
2.2
-
-
-
-
-
-
-
-
TA2
7.0
-
-
-
-
-
-
-
7.9
22.8
3.1
257
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
7.0
-
-
-
-
-
-
-
8.0
23.0
3.4
253
0.1
-
-
-
0.5
-
-
-
-
-
-
-
-
08/30/06
IN
-
116
<0.1
27
0.6
<10
27.9
0.1
8.1
23.0
3.0
485
0.2
77.8
61.4
16.5
35.5
33.9
1.6
0.3
33.6
<25
<25
<0.1
<0.1
TT
7.1
123
<0.1
27
0.8
<10
28.2
0.1
8.2
22.8
2.7
431
0.1
86.7
63.0
23.7
1.9
1.9
<0.1
0.3
1.6
<25
<25
<0.1
<0.1
09/13/06
IN
-
-
-
-
-
-
-
-
8.0
24.9
3.3
547
0.4
-
-
-
28.7
-
-
-
-
-
-
-
-
TA1
7.1
-
-
-
-
-
-
-
7.9
24.0
3.1
451
0.1
-
-
-
0.2
-
-
-
-
-
-
-
-
TB1
7.1
-
-
-
-
-
-
-
8.1
22.7
3.3
255
0.1
-
-
-
2.2
-
-
-
-
-
-
-
-
TA2
7.8
-
-
-
-
-
-
-
7.9
23.9
3.2
439
0.1
-
-
-
0.1
-
-
-
-
-
-
-
-
TB2
7.8
-
-
-
-
-
-
-
7.9
23.9
3.2
439
0.1
-
-
-
0.6
-
-
-
-
-
-
-
-
09/27/06
IN
-
120
<0.1
35
0.7
<10
28.9
0.2
8.0
22.5
4.5
563
0.3
83.0
61.3
21.7
30.3
31.5
<0.1
0.1
31.4
<25
<25
<0.1
<0.1
TT
7.9
118
0.2
20
<0.05
<10
30.1
0.2
7.9
22.5
3.5
568
0.0
77.8
57.0
20.7
<0.1
<0.1
<0.1
<0.1
<0.1
<25
<25
<0.1
<0.1
CO
(a) as CaCO3.
(b) as P.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
«3/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
10/11/06
IN
-
-
-
-
-
-
-
-
7.8
22.2
3.1
569
0.3
-
-
-
29.9
29.6
-
-
-
-
-
-
-
-
TA1
8.0
-
-
-
-
-
-
-
7.9
22.1
3.3
467
0.02
-
-
-
0.2
0.2
-
-
-
-
-
-
-
-
TB1
8.0
-
-
-
-
-
-
-
7.8
22.2
3.3
450
0.02
-
-
-
1.9
2.1
-
-
-
-
-
-
-
-
TA2
8.7
-
-
-
-
-
-
-
7.8
22.1
3.3
445
0.02
-
-
-
0.2
0.3
-
-
-
-
-
-
-
-
TB2
8.7
-
-
-
-
-
-
-
7.8
22.1
3.3
442
0.02
-
-
-
0.6
0.6
-
-
-
-
-
-
-
-
01/10/07
IN
-
-
-
-
-
-
-
-
8.2
15.6
5.1
474
0.3
-
-
-
32.1
-
-
-
-
-
-
-
-
TA1
10.2
-
-
-
-
-
-
-
7.5
16.8
4.5
416
0.05
-
-
-
0.4
-
-
-
-
-
-
-
-
TB1
10.2
-
-
-
-
-
-
-
8.1
16.5
5.0
381
0.05
-
-
-
2.0
-
-
-
-
-
-
-
-
TA2
11.1
-
-
-
-
-
-
-
7.7
16.5
4.3
385
0.05
-
-
-
0.3
-
-
-
-
-
-
-
-
TB2
11.1
-
-
-
-
-
-
-
8.2
18.1
6.6
372
0.05
-
-
-
1.2
-
-
-
-
-
-
-
-
03/07/07
IN
-
-
-
-
-
-
-
-
8.1
13.0
4.9
586
0.3
-
-
-
26.0
-
-
-
-
-
-
-
-
TA1
11.1
-
-
-
-
-
-
-
8.1
16.2
4.4
491
0.05
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB1
11.1
-
-
-
-
-
-
-
8.0
13.1
4.4
488
0.03
-
-
-
1.6
-
-
-
-
-
-
-
-
TA2
12.1
-
-
-
-
-
-
-
8.0
15.4
4.6
484
0.01
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
12.1
-
-
-
-
-
-
-
8.0
13.0
4.4
483
0.05
-
-
-
1.5
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Cd
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
H9/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
05/02/07
IN
-
-
-
-
-
-
-
-
8.0
18.7
3.7
585
0.3
-
-
-
31.4
-
-
-
-
-
-
-
-
TA1
12.0
-
-
-
-
-
-
-
7.9
21.6
3.4
479
0.05
-
-
-
0.3
-
-
-
-
-
-
-
-
TB1
12.0
-
-
-
-
-
-
-
7.9
19.6
3.6
469
0.05
-
-
-
2.6
-
-
-
-
-
-
-
-
TA2
13.0
-
-
-
-
-
-
-
7.9
20.8
4.0
459
0.05
-
-
-
0.2
-
-
-
-
-
-
-
-
TB2
13.0
-
-
-
-
-
-
-
7.9
19.2
4.0
457
0.05
-
-
-
3.3
-
-
-
-
-
-
-
-
08/01/07
IN
-
-
-
-
-
-
-
-
8.0
26.3
2.9
428
0.3
-
-
-
27.4
-
-
-
-
-
-
-
-
TA1
13.1
-
-
-
-
-
-
-
8.0
24.8
3.0
367
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB1
13.1
-
-
-
-
-
-
-
8.0
24.6
3.1
355
0.0
-
-
-
2.5
-
-
-
-
-
-
-
-
TA2
14.2
-
-
-
-
-
-
-
8.0
24.5
3.0
350
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
14.2
-
-
-
-
-
-
-
8.0
24.5
3.0
346
0.0
-
-
-
2.8
-
-
-
-
-
-
-
-
11/07/07
IN
-
-
-
-
-
-
-
-
8.2
19.5
3.8
583
0.4
-
-
-
32.0
-
-
-
-
-
-
-
-
TA1
14.3
-
-
-
-
-
-
-
8.1
20.8
3.2
472
0.1
-
-
-
0.2
-
-
-
-
-
-
-
-
TB1
14.3
-
-
-
-
-
-
-
8.2
20.0
3.3
463
0.1
-
-
-
3.6
-
-
-
-
-
-
-
-
TA2
15.4
-
-
-
-
-
-
-
8.1
20.5
4.1
458
0.1
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
15.4
-
-
-
-
-
-
-
8.1
20.0
4.1
454
0.1
-
-
-
5.1
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
(as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
02/13/08
IN
-
-
-
-
-
-
-
-
8.0
12.8
NA(C)
NA(C)
0.4
-
-
-
30.8
-
-
-
-
-
-
-
-
TA1
15.4
-
-
-
-
-
-
-
8.0
16.2
NA(C)
NA(C)
0.1
-
-
-
1.1
-
-
-
-
-
-
-
-
TB1
15.4
-
-
-
-
-
-
-
7.9
16.2
NA(C)
NA(C)
0.1
-
-
-
8.9
-
-
-
-
-
-
-
-
TA2
16.6
-
-
-
-
-
-
-
7.9
12.2
NA(C)
NA(C)
0.1
-
-
-
0.5
-
-
-
-
-
-
-
-
TB2
16.6
-
-
-
-
-
-
-
7.9
12.1
NA(C)
NA(C)
0.1
-
-
-
11.6
-
-
-
-
-
-
-
-
05/13/08
IN
-
-
-
-
-
-
-
-
8.2
18.7
NA(C)
NA(C)
0.3
-
-
-
29.3
-
-
-
-
-
-
-
-
TA1
16.7
-
-
-
-
-
-
-
8.2
19.6
NA(C)
NA(C)
0.0
-
-
-
0.9
-
-
-
-
-
-
-
-
TB1
16.7
-
-
-
-
-
-
-
8.2
19.9
NA(C)
NA(C)
0.0
-
-
-
12.0
-
-
-
-
-
-
-
-
TA2
17.8
-
-
-
-
-
-
-
8.2
19.6
NA(C)
NA(C)
0.0
-
-
-
0.4
-
-
-
-
-
-
-
-
TB2
17.8
-
-
-
-
-
-
-
8.2
19.8
NA(C)
NA(C)
0.0
-
-
-
14.4
-
-
-
-
-
-
-
-
08/20/08
IN
-
-
-
-
-
-
-
-
8.1
25.4
NA(C)
NA(C)
0.3
-
-
-
29.8
-
-
-
-
-
-
-
-
TA1
17.8
-
-
-
-
-
-
-
8.1
24.3
NA(C)
NA(C)
0.0
-
-
-
0.1
-
-
-
-
-
-
-
-
TB1
17.8
-
-
-
-
-
-
-
8.1
24.3
NA(C)
NA(C)
0.0
-
-
-
13.1
-
-
-
-
-
-
-
-
TA2
19.0
-
-
-
-
-
-
-
8.1
24.1
NA(C)
NA(C)
0.0
-
-
-
0.1
-
-
-
-
-
-
-
-
TB2
19.0
-
-
-
-
-
-
-
8.1
24.2
NA(C)
NA(C)
0.0
-
-
-
14.9
-
-
-
-
-
-
-
-
11/19/08
IN
-
-
-
-
-
-
-
-
8.3
22.2
NA(C)
NA(C)
0.4
-
-
-
33.1
-
-
-
-
-
-
-
-
TA1
19.4
-
-
-
-
-
-
-
8.2
20.7
NA(C)
NA(C)
0.0
-
-
-
0.2
-
-
-
-
-
-
-
-
TB1
19.4
-
-
-
-
-
-
-
8.2
20.5
NA(C)
NA(C)
0.0
-
-
-
20.0
-
-
-
-
-
-
-
-
TA2
20.7
-
-
-
-
-
-
-
8.2
20.6
NA(C)
NA(C)
0.0
-
-
-
0.1
-
-
-
-
-
-
-
-
TB2
20.7
-
-
-
-
-
-
-
8.2
20.5
NA(C)
NA(C)
0.0
-
-
-
21.9
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) DO/ORP not operating correctly.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-l. Analytical Results from Long-Term Sampling, Purvine Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
02/11/09
IN
-
-
-
-
-
-
-
-
8.4
13.9
NA(C)
NA(C)
0.4
-
-
-
30.5
-
-
-
-
-
-
-
-
TA1
20.8
-
-
-
-
-
-
-
8.4
16.8
NA(C)
NA(C)
0.0
-
-
-
0.3
-
-
-
-
-
-
-
-
TB1
20.8
-
-
-
-
-
-
-
8.3
16.1
NA(C)
NA(C)
0.0
-
-
-
21.6
-
-
-
-
-
-
-
-
TA2
22.2
-
-
-
-
-
-
-
8.2
16.2
NA(C)
NA(C)
0.0
-
-
-
0.3
-
-
-
-
-
-
-
-
TB2
22.2
-
-
-
-
-
-
-
8.2
15.6
NA(C)
NA(C)
0.0
-
-
-
23.1
-
-
-
-
-
-
-
-
05/27/09
IN
-
-
-
-
-
-
-
-
8.3
20.6
NA(C)
NA(C)
0.4
-
-
-
25.2
-
-
-
-
-
-
-
-
TA1
22.4
-
-
-
-
-
-
-
7.7
22.2
NA(C)
NA(C)
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB1
22.4
-
-
-
-
-
-
-
8.2
22.8
NA(C)
NA(C)
0.0
-
-
-
21.5
-
-
-
-
-
-
-
-
TA2
23.8
-
-
-
-
-
-
-
8.2
22.1
NA(C)
NA(C)
0.0
-
-
-
<0.1
-
-
-
-
-
-
-
-
TB2
23.8
-
-
-
-
-
-
-
8.2
22.4
NA(C)
NA(C)
0.0
-
-
-
20.8
-
-
-
-
-
-
-
-
08/26/09
IN
-
-
-
-
-
-
-
-
8.4
24.9
NA(C)
NA(C)
0.4
-
-
-
26.3
-
-
-
-
-
-
-
-
TA1
23.5
-
-
-
-
-
-
-
8.3
24.3
NA(C)
NA(C)
0.0
-
-
-
0.4
-
-
-
-
-
-
-
-
TB1
23.5
-
-
-
-
-
-
-
8.2
25.2
NA(C)
NA(C)
0.0
-
-
-
19.8
-
-
-
-
-
-
-
-
TA2(d)
24.9
-
-
-
-
-
-
-
8.2
24.3
NA(C)
NA(C)
0.0
-
-
-
0.4
-
-
-
-
-
-
-
-
TB2(d)
24.9
-
-
-
-
-
-
-
8.2
24.5
NA(C)
NA(C)
0.0
-
-
-
20.4
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) DO/ORP not operating correctly.
Lead Vessels: TB1, TB2; Lag Vessels: TA1, TA2
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b>
mg/L
NTU
S.U.
•c
mg/L
mV
mg/L
mg/L("
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
01/11/06
IN
-
114
<0.1
21
0.5
<50(c)
30.8
0.5
7.3
13.7
4.0
376
0.3
77.6
54.7
22.9
29.0
30.0
<0.1
0.6
29.4
<25
<25
<0.1
<0.1
TA
1.1
106
<0.1
21
0.5
<50(c)
2.2
0.5
6.9
14.6
3.3
442
0.1
83.7
59.1
24.5
0.9
0.1
0.8
0.4
<0.1
44.6
<25
1.0
1.1
TB
1.1
110
<0.1
21
0.5
<50(c)
18.6
0.5
7.1
14.4
4.0
459
0.1
78.9
55.1
23.9
0.2
0.2
<0.1
0.5
<0.1
<25
<25
<0.1
<0.1
01/24/06
IN
-
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
30.9
-
-
-
-
-
-
-
-
TA
2.8
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
0.1
-
-
-
-
-
-
-
-
TB
2.8
-
-
-
-
-
-
-
NM
NM
NM
NM
NM
-
-
-
0.2
-
-
-
-
-
-
-
-
02/01/06(d)
IN
-
-
-
-
-
-
-
-
7.5
18.1
2.9
506
0.3
-
-
-
30.2
-
-
-
-
-
-
-
-
TA
3.9
-
-
-
-
-
-
-
7.5
17.9
3.3
496
0.1
-
-
-
0.3
-
-
-
-
-
-
-
-
TB
3.9
-
-
-
-
-
-
-
7.6
17.9
3.4
533
0.2
-
-
-
0.5
-
-
-
-
-
-
-
-
02/14/06(e)
IN
-
-
-
-
-
-
-
-
7.9
17.1
3.2
403
0.4
-
-
-
26.7
-
-
-
-
-
-
-
-
TA
5.6
-
-
-
-
-
-
-
8.1
16.8
2.3
498
0.3
-
-
-
0.1
-
-
-
-
-
-
-
-
TB
5.6
-
-
-
-
-
-
-
8.1
16.6
3.8
511
0.2
-
-
-
0.9
-
-
-
-
-
-
-
-
03/01/06
IN
-
-
-
-
-
-
-
-
8.0
17.6
2.9
437
0.3
-
-
-
28.4
-
-
-
-
-
-
-
-
TA
7.6
-
-
-
-
-
-
-
8.2
17.3
2.7
472
0.3
-
-
-
0.1
-
-
-
-
-
-
-
-
TB
7.6
-
-
-
-
-
-
-
8.2
17.1
2.6
510
0.2
-
-
-
2.2
-
-
-
-
-
-
-
-
Cd
(a) as CaCO3.
(b) as P.
(c) Result is measurement of orthophosphate as P
NM = not measured.
Lead Vessel: TB; Lag Vessel: TA
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L("
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
03/14/06
IN
-
112
<0.1
21.7
0.7
<10
29.5
1.1
8.3
15.5
2.5
460
0.3
88.5
64.5
24.0
30.4
30.0
0.4
0.3
29.7
<25
<25
0.1
<0.1
TA
9.4
112
<0.1
21.7
0.7
<10
27.9
0.4
8.5
15.6
2.6
477
0.3
85.2
62.5
22.7
0.1
0.1
<0.1
0.3
<0.1
<25
<25
<0.1
<0.1
TB
9.4
116
<0.1
21.6
0.7
<10
28.7
0.3
8.5
15.6
2.6
520
0.3
86.3
63.2
23.1
5.0
5.0
<0.1
0.4
4.7
<25
<25
<0.1
<0.1
03/29/06
IN
-
-
-
-
-
-
-
-
7.6
13.2
3.7
438
0.3
-
-
-
30.0
30.0
-
-
-
-
-
-
-
-
TA
10.9
-
-
-
-
-
-
-
7.8
13.5
4.3
463
0.2
-
-
-
0.1
<0.1
-
-
-
-
-
-
-
-
TB
10.9
-
-
-
-
-
-
-
8.2
13.6
3.8
464
0.2
-
-
-
4.4
4.2
-
-
-
-
-
-
-
-
04/12/06
IN
-
-
-
-
-
-
-
-
7.9
17.4
2.9
513
0.3
-
-
-
29.2
-
-
-
-
-
-
-
-
TA
12.3
-
-
-
-
-
-
-
8.1
17.3
3.0
562
0.3
-
-
-
0.3
-
-
-
-
-
-
-
-
TB
12.3
-
-
-
-
-
-
-
8.1
17.3
2.9
571
0.3
-
-
-
8.1
-
-
-
-
-
-
-
-
04/26/06
IN
-
-
-
-
-
-
-
-
7.6
19.0
3.0
276
0.4
-
-
-
29.3
-
-
-
-
-
-
-
-
TA
14.2
-
-
-
-
-
-
-
8.0
19.0
2.9
326
0.3
-
-
-
0.2
-
-
-
-
-
-
-
-
TB
14.2
-
-
-
-
-
-
-
8.2
18.9
2.6
405
0.3
-
-
-
10.3
-
-
-
-
-
-
-
-
05/09/06
IN
-
110
<0.1
22
0.9
<10
31.2
0.5
8.0
21.5
2.9
461
0.3
93.8
66.9
26.9
30.2
28.6
1.6
0.2
28.5
<25
<25
<0.1
<0.1
TA
16.5
118
<0.1
22
0.9
<10
31.7
0.1
8.1
21.7
2.7
534
0.2
91.6
65.5
26.0
0.2
0.2
<0.1
0.1
<0.1
<25
<25
<0.1
<0.1
TB
16.5
114
<0.1
22
0.9
<10
31.6
0.1
8.1
22.0
2.7
566
0.3
103
75.8
26.9
10.8
10.3
0.5
0.2
10.2
<25
<25
<0.1
<0.1
05/24/06
IN
-
-
-
-
-
-
-
-
8.0
19.7
2.7
520
0.3
-
-
-
30.1
-
-
-
-
-
-
-
-
TA
18.0
-
-
-
-
-
-
-
8.0
19.6
2.2
570
0.3
-
-
-
0.3
-
-
-
-
-
-
-
-
TB
18.0
-
-
-
-
-
-
-
8.0
19.1
2.7
571
0.3
-
-
-
11.1
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
Lead Vessel: TB; Lag Vessel: TA
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
«3/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
06/08/06(c
IN
-
121
<0.1
24
0.8
<10
30.9
0.1
8.0
22.1
2.9
518
0.3
79.2
58.0
21.2
26.9
26.6
0.4
0.3
26.3
<25
<25
0.6
0.3
TA
20.1
121
<0.1
22
0.8
<10
30.0
0.2
7.9
21.8
2.6
531
0.3
78.5
56.7
21.9
0.6
0.5
<0.1
0.2
0.3
<25
<25
<0.1
<0.1
TB
20.1
117
<0.1
22
0.8
<10
30.0
0.2
7.9
21.9
2.7
537
0.3
79.3
57.3
21.9
11.8
11.8
<0.1
0.3
11.6
<25
<25
<0.1
<0.1
06/21/06
IN
-
-
-
-
-
-
-
-
8.0
22.8
NA(d)
539
0.2
-
-
-
30.1
-
-
-
-
-
-
-
-
TA
21.4
-
-
-
-
-
-
-
8.0
22.9
NA(d)
542
0.1
-
-
-
0.7
-
-
-
-
-
-
-
-
TB
21.4
-
-
-
-
-
-
-
8.0
22.9
NA(d)
550
0.2
-
-
-
12.2
-
-
-
-
-
-
-
-
07/05/06
IN
-
113
<0.1
21
0.8
<10
30.4
0.5
7.8
22.6
NA(d)
455
0.4
78.6
56.3
22.3
26.2
28.6
<0.1
0.1
28.5
<25
<25
0.5
<0.1
TA
22.2
113
<0.1
21
0.8
<10
28.9
0.7
8.0
22.6
NA(d)
418
0.2
76.2
54.9
21.3
0.4
0.3
<0.1
<0.1
0.2
<25
<25
0.9
0.4
TB
22.2
117
<0.1
21
0.8
<10
30.2
0.4
8.0
23.0
NA(d)
472
0.3
78.5
56.9
21.5
9.9
9.9
<0.1
<0.1
9.8
<25
<25
0.6
<0.1
07/19/06
IN
-
-
-
-
-
-
-
-
8.0
24.3
2.7
518
0.3
-
-
-
30.3
30.4
-
-
-
-
-
-
-
-
TA
23.3
-
-
-
-
-
-
-
8.0
24.3
2.2
549
0.3
-
-
-
0.6
0.6
-
-
-
-
-
-
-
-
TB
23.3
-
-
-
-
-
-
-
8.0
24.1
2.7
561
0.3
-
-
-
11.9
11.6
-
-
-
-
-
-
-
-
08/03/06(d)
IN
-
114
<0.1
22
0.7
<10
29.9
0.1
7.9
21.9
2.6
557
0.3
82.9
60.4
22.4
31.1
29.8
1.4
0.2
29.6
<25
<25
<0.1
0.1
TA
24.0
114
<0.1
22
0.7
<10
28.4
0.3
8.0
22.0
2.6
553
0.3
78.8
57.8
21.0
0.6
0.6
<0.1
0.1
0.5
<25
<25
<0.1
<0.1
TB
24.0
114
<0.1
22
0.7
<10
28.9
0.1
8.0
22.2
2.5
546
0.3
82.4
60.3
22.2
12.0
11.9
0.1
0.2
11.7
<25
<25
<0.1
<0.1
08/16/06
IN
-
-
-
-
-
-
-
-
8.0
22.4
2.7
559
0.3
-
-
-
25.7
-
-
-
-
-
-
-
-
TA
24.7
-
-
-
-
-
-
-
8.0
22.3
3.1
538
0.2
-
-
-
0.5
-
-
-
-
-
-
-
-
TB
24.7
-
-
-
-
-
-
-
8.0
21.9
2.7
571
0.3
-
-
-
10.4
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) Water quality readings taken on 06/07/06.
(d) DO probe not operational.
Lead Vessel: TB Lag Vessel: TA
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
'c
mg/L
mV
mg/L
mgfl.w
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
08/30/06
IN
-
123
<0.1
26
0.8
<10
28.5
0.2
7.9
22.4
2.3
561
0.3
90.1
65.7
24.5
30.9
28.9
2.1
0.3
28.6
<25
<25
<0.1
<0.1
TA
25.5
116
<0.1
26
0.8
<10
27.3
0.2
8.1
22.7
2.8
560
0.3
81.7
60.1
21.6
0.6
0.7
<0.1
0.2
0.4
<25
<25
0.1
0.2
TB
25.5
121
<0.1
24
0.8
<10
27.9
<0.1
8.0
22.7
2.7
563
0.3
88.8
65.1
23.7
12.0
11.3
0.6
0.3
11.0
<25
<25
<0.1
<0.1
09/13/06
IN
-
-
-
-
-
-
-
-
8.0
23.5
2.7
566
0.4
-
-
-
28.9
-
-
-
-
-
-
-
-
TA
26.3
-
-
-
-
-
-
-
8.0
23.7
2.5
583
0.3
-
-
-
0.9
-
-
-
-
-
-
-
-
TB
26.3
-
-
-
-
-
-
-
8.0
23.9
2.7
599
0.3
-
-
-
12.6
-
-
-
-
-
-
-
-
09/27/06
IN
-
122
<0.1
22
0.6
<10
29.3
0.2
8.0
23.9
4.9
570
0.3
83.6
59.4
24.2
29.3
30.6
<0.1
0.1
30.5
<25
<25
<0.1
<0.1
TA
27.8
122
<0.1
22
0.6
<10
29.5
0.1
8.0
23.9
3.8
600
0.3
87.4
63.1
24.3
1.7
1.8
<0.1
0.1
1.8
<25
<25
<0.1
<0.1
TB
27.8
125
<0.1
21
0.6
<10
29.4
0.2
8.0
24.1
3.9
609
0.3
84.6
60.2
24.4
17.6
18.7
<0.1
0.1
18.5
<25
<25
<0.1
<0.1
10/11/06
IN
-
-
-
-
-
-
-
-
7.9
22.6
4.0
542
0.4
-
-
-
28.1
29.4
-
-
-
-
-
-
-
-
TA
30.1
-
-
-
-
-
-
-
7.9
22.8
2.7
576
0.3
-
-
-
4.0
3.9
-
-
-
-
-
-
-
-
TB
30.1
-
-
-
-
-
-
-
7.9
23
2.7
586
0.3
-
-
-
0.2
0.2
-
-
-
-
-
-
-
-
11/16/06
IN
-
-
-
-
-
-
-
-
7.9
19.0
3.0
477
0.3
-
-
-
33.2
-
-
-
-
-
-
-
-
TA
36.2
-
-
-
-
-
-
-
7.9
18.9
3.5
521
0.2
-
-
-
13.2
-
-
-
-
-
-
-
-
TB
36.2
-
-
-
-
-
-
-
7.9
18.9
3.1
557
0.3
-
-
-
28.5
-
-
-
-
-
-
-
-
12/07/06
IN
-
-
-
-
-
-
-
-
7.9
18.0
3.4
530
0.3
-
-
-
33.1
-
-
-
-
-
-
-
-
TA
39.4
-
-
-
-
-
-
-
7.9
18.2
3.3
569
0.3
-
-
-
16.2
-
-
-
-
-
-
-
-
TB
39.4
-
-
-
-
-
-
-
7.9
18.1
3.4
580
0.3
-
-
-
30.3
-
-
-
-
-
-
-
-
(a) As CaCO3.
(b) As P.
Lead Vessel: TB Lag Vessel: TA
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
'c
mg/L
mV
mg/L
mgfl.w
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
12/13/06
IN
-
-
-
-
-
-
-
-
8.0
15.3
3.4
535
0.3
-
-
-
27.8
-
-
-
-
-
-
-
-
TA
39.9
-
-
-
-
-
-
-
8.0
15.2
3.9
571
0.3
-
-
-
11.8
-
-
-
-
-
-
-
-
TB
39.9
-
-
-
-
-
-
-
8.1
15.2
3.9
582
0.3
-
-
-
24.7
-
-
-
-
-
-
-
-
01/10/07
IN
-
-
-
-
-
-
-
-
8.0
17.2
4.3
550
0.4
-
-
-
31.8
-
-
-
-
-
-
-
-
TA
42.3
-
-
-
-
-
-
-
8.0
17.4
3.8
581
0.2
-
-
-
19.5
-
-
-
-
-
-
-
-
TB
42.3
-
-
-
-
-
-
-
8.0
17.4
5.1
594
0.3
-
-
-
30.1
-
-
-
-
-
-
-
-
02/07/07(c)
IN
-
-
-
-
-
-
-
-
8.0
18.6
5.2
564
0.3
-
-
-
31.1
-
-
-
-
-
-
-
-
TA
3.2
-
-
-
-
-
-
-
8.0
18.7
4.1
575
0.25
-
-
-
24.6
-
-
-
-
-
-
-
-
TB
3.2
-
-
-
-
-
-
-
7.9
18.7
4.2
582
0.2
-
-
-
0.4
-
-
-
-
-
-
-
-
03/07/07
IN
-
-
-
-
-
-
-
-
8.0
18.5
5.2
526
0.3
-
-
-
25.4
-
-
-
-
-
-
-
-
TA
10.2
-
-
-
-
-
-
-
8.0
18.5
4.2
568
0.3
-
-
-
22.2
-
-
-
-
-
-
-
-
TB
10.2
-
-
-
-
-
-
-
8.0
18.4
4.2
580
0.3
-
-
-
2.5
-
-
-
-
-
-
-
-
04/04/07
IN
-
-
-
-
-
-
-
-
7.9
20.8
3.2
520
0.3
-
-
-
31.4
-
-
-
-
-
-
-
-
TA
15.6
-
-
-
-
-
-
-
7.9
20.9
2.8
572
0.3
-
-
-
27.8
-
-
-
-
-
-
-
-
TB
15.6
-
-
-
-
-
-
-
7.9
20.8
3.9
580
0.3
-
-
-
9.5
-
-
-
-
-
-
-
-
05/02/07
IN
-
-
-
-
-
-
-
-
8.0
22.4
4.2
531
0.4
-
-
-
32.5
-
-
-
-
-
-
-
-
TA
22.5
-
-
-
-
-
-
-
8.1
22.4
4.1
579
0.3
-
-
-
27.5
-
-
-
-
-
-
-
-
TB
22.5
-
-
-
-
-
-
-
8.0
22.2
3.9
613
0.3
-
-
-
15.1
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) Lead vessel (TB) rebedded with ARM 300 and put into lag position on January 24, 2007. TA is the lead vessel for new test run.
Lead Vessel: TB Lag Vessel: TA
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
'c
mg/L
mV
mg/L
mgfl.w
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
06/01/07
IN
-
-
-
-
-
-
-
-
8.0
22.1
3.8
503
0.4
-
-
-
26.7
-
-
-
-
-
-
-
-
TA
31.3
-
-
-
-
-
-
-
8.0
23.1
2.9
555
0.3
-
-
-
24.4
-
-
-
-
-
-
-
-
TB
31.3
-
-
-
-
-
-
-
8.0
23.1
3.0
574
0.3
-
-
-
17.7
-
-
-
-
-
-
-
-
12/18/07(c)
IN
-
-
-
-
-
-
-
-
8.2
16.1
3.7
562
0.4
-
-
-
29.1
-
-
-
-
-
-
-
-
TA
18.3
-
-
-
-
-
-
-
8.2
15.9
3.1
596
0.4
-
-
-
1.1
-
-
-
-
-
-
-
-
TB
18.3
-
-
-
-
-
-
-
8.8
15.9
4.7
546
0.4
-
-
-
0.1
-
-
-
-
-
-
-
-
02/13/08
IN
-
-
-
-
-
-
-
-
8.0
19.0
NA(d)
NA(d)
0.4
-
-
-
30.7
-
-
-
-
-
-
-
-
TA
30.9
-
-
-
-
-
-
-
8.0
19.4
NA(d)
NA(d)
0.4
-
-
-
9.4
-
-
-
-
-
-
-
-
TB
30.9
-
-
-
-
-
-
-
8.0
18.9
NA(d)
NA(d)
0.3
-
-
-
1.2
-
-
-
-
-
-
-
-
05/13/08
IN
-
-
-
-
-
-
-
-
8.2
23.0
NA(d)
NA(d)
0.4
-
-
-
29.2
-
-
-
-
-
-
-
-
TA
42.8
-
-
-
-
-
-
-
8.1
23.0
NA(d)
NA(d)
0.4
-
-
-
9.5
-
-
-
-
-
-
-
-
TB
42.8
-
-
-
-
-
-
-
8.1
22.3
NA(d)
NA(d)
0.3
-
-
-
<0.1
-
-
-
-
-
-
-
-
08/20/08
IN
-
-
-
-
-
-
-
-
8.3
24.2
NA(d)
NA(d)
0.4
-
-
-
30.1
-
-
-
-
-
-
-
-
TA
47.8
-
-
-
-
-
-
-
8.2
24.5
NA(d)
NA(d)
0.4
-
-
-
8.4
-
-
-
-
-
-
-
-
TB
47.8
-
-
-
-
-
-
-
8.2
24.6
NA(d)
NA(d)
0.4
-
-
-
0.2
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) On October 3, 2007, both lead and lag vessels rebedded with E33-S media. Vessel A continued to be lead vessel and Vessel B lag vessel.
DO and ORP measurements not taken.
Lead Vessel: TA Lag Vessel: TB
-------
Table B-2. Analytical Results from Long-Term Sampling, Residence Hall, Klamath Falls, OR (Continued)
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
'c
mg/L
mV
mg/L
mgfl.w
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
11/19/08
IN
-
-
-
-
-
-
-
-
8.2
19.5
NA(C)
NA(C)
0.4
-
-
-
32.8
-
-
-
-
-
-
-
-
TA
56.5
-
-
-
-
-
-
-
8.1
19.3
NA(C)
NA(C)
0.4
-
-
-
16.3
-
-
-
-
-
-
-
-
TB
56.5
-
-
-
-
-
-
-
8.0
19.4
NA(C)
NA(C)
0.4
-
-
-
0.9
-
-
-
-
-
-
-
-
02/11/09
IN
-
-
-
-
-
-
-
-
8.3
18.0
NA(C)
NA(C)
0.4
-
-
-
30.2
-
-
-
-
-
-
-
-
TA
64.2
-
-
-
-
-
-
-
8.3
18.2
NA(C)
NA(C)
0.4
-
-
-
18.0
-
-
-
-
-
-
-
-
TB
64.2
-
-
-
-
-
-
-
8.3
18.2
NA(C)
NA(C)
0.4
-
-
-
1.6
-
-
-
-
-
-
-
-
05/27/09
IN
-
-
-
-
-
-
-
-
8.2
22.7
NA(C)
NA(C)
0.4
-
-
-
24.7
-
-
-
-
-
-
-
-
TA
76.3
-
-
-
-
-
-
-
8.2
22.6
NA(C)
NA(C)
0.4
-
-
-
19.1
-
-
-
-
-
-
-
-
TB
76.3
-
-
-
-
-
-
-
8.2
22.3
NA(C)
NA(C)
0.4
-
-
-
2.9
-
-
-
-
-
-
-
-
08/26/09
IN
-
-
-
-
-
-
-
-
8.3
23.7
NA(C)
NA(C)
0.4
-
-
-
26.2
-
-
-
-
-
-
-
-
TA
81.3
-
-
-
-
-
-
-
8.3
23.7
NA(C)
NA(C)
0.4
-
-
-
18.3
-
-
-
-
-
-
-
-
TB
81.3
-
-
-
-
-
-
-
8.3
23.6
NA(C)
NA(C)
0.4
-
-
-
3.1
-
-
-
-
-
-
-
-
(a) as CaCO3.
(b) as P.
(c) DO and ORP measurements not taken.
Lead Vessel: TA Lag Vessel: TB
-------
Table B-3. Analytical Results from Long-Term Sampling, College Union, Klamath Falls, OR
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L«
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
03/01/06
IN
-
-
-
-
-
-
-
-
8.1
13.1
3.3
530
0.4
-
-
-
27.7
-
-
-
-
-
-
-
-
-
TA
0.7
-
-
-
-
-
-
-
7.9
12.9
3.6
584
0.3
-
-
-
0.3
-
-
-
-
-
-
-
-
-
TB
0.7
-
-
-
-
-
-
-
7.8
12.9
3.4
607
0.3
-
-
-
<0.1
-
-
-
-
-
-
-
-
-
03/14/06
IN
-
112
<0.1
21.5
0.7
<10
29.9
0.7
8.2
12.1
3.4
500
0.3
85.6
62.3
23.3
30.4
30.2
0.2
0.5
29.7
<25
<25
0.1
<0.1
2.1
TA
1.3
112
<0.1
21.5
0.7
<10
32.3
0.4
8.6
11.9
2.8
562
0.3
80.4
58.8
21.6
0.4
0.4
<0.1
0.5
<0.1
<25
<25
<0.1
<0.1
2.6
TB
1.3
103
<0.1
21.6
0.7
<10
29.9
0.7
8.3
11.9
7.1
596
0.3
74.9
53.3
21.6
0.2
0.2
<0.1
0.5
<0.1
<25
<25
0.1
<0.1
2.5
03/29/06
IN
-
-
-
-
-
-
-
-
8.0
12.5
4.1
477
0.3
-
-
-
29.6
29.9
-
-
-
-
-
-
-
-
-
TA
2.0
-
-
-
-
-
-
-
7.8
11.9
3.7
474
0.3
-
-
-
0.4
0.4
-
-
-
-
-
-
-
-
-
TB
2.0
-
-
-
-
-
-
-
7.4
12.0
3.9
460
0.3
-
-
-
0.1
0.1
-
-
-
-
-
-
-
-
-
04/12/06
IN
-
-
-
-
-
-
-
-
8.1
13.6
3.6
546
0.3
-
-
-
29.1
-
-
-
-
-
-
-
-
-
TA
2.5
-
-
-
-
-
-
-
8.3
13.1
2.7
577
0.3
-
-
-
0.4
-
-
-
-
-
-
-
-
-
TB
2.5
-
-
-
-
-
-
-
8.0
13.0
3.7
611
0.3
-
-
-
0.2
-
-
-
-
-
-
-
-
-
04/26/06
IN
-
-
-
-
-
-
-
-
8.0
15.6
3.6
528
0.3
-
-
-
29.2
-
-
-
-
-
-
-
-
-
TA
3.2
-
-
-
-
-
-
-
8.2
15.8
3.2
538
0.3
-
-
-
0.2
-
-
-
-
-
-
-
-
-
TB
3.2
-
-
-
-
-
-
-
8.1
15.7
3.2
559
0.3
-
-
-
0.1
-
-
-
-
-
-
-
-
-
Cd
(a) as CaCO3.
(b) as P.
Lead Vessel: TA; Lag Vessel: TB
-------
Cd
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
10A3
mg/L(a)
mg/L
mg/L
mg/L
«3/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L(a)
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
05/09/06
IN
-
118
<0.1
22
0.9
<10
31.5
0.4
7.8
19.3
2.6
547
0.3
106
78.2
27.3
29.0
28.9
<0.1
0.2
28.8
<25
<25
<0.1
<0.1
2.4
TA
3.7
122
<0.1
22
0.9
<10
31.3
0.3
7.8
19.3
3.0
563
0.3
107
80.0
27.0
0.2
0.2
<0.1
0.1
<0.1
<25
<25
<0.1
<0.1
2.4
TB
3.7
118
<0.1
23
1.0
<10
31.7
0.3
7.7
19.3
3.0
554
0.3
103
75.9
27.0
0.1
0.1
<0.1
0.1
<0.1
<25
<25
<0.1
<0.1
2.2
05/24/06
IN
-
-
-
-
-
-
-
-
7.9
21.1
2.7
493
0.3
-
-
-
28.5
-
-
-
-
-
-
-
-
-
TA
4.0
-
-
-
-
-
-
-
7.9
20.9
2.9
576
0.3
-
-
-
0.6
-
-
-
-
-
-
-
-
-
TB
4.0
-
-
-
-
-
-
-
8.0
20.8
2.5
577
0.3
-
-
-
0.1
-
-
-
-
-
-
-
-
-
6/7/2006(c)
IN
-
127
<0.1
21
0.9
<10
31.4
1.5
7.9
21.7
2.6
509
0.3
83.5
60.8
22.7
28.5
27.4
1.1
0.2
27.2
<25
<25
<0.1
<0.1
9.7
TA
4.3
122
<0.1
21
0.9
<10
31.1
0.2
8.0
21.8
2.9
527
0.3
82.8
60.2
22.6
0.5
0.5
<0.1
0.2
0.3
<25
<25
<0.1
<0.1
10.2
TB
4.3
122
<0.1
21
0.9
<10
31.0
0.3
8.0
21.8
3.0
529
0.1
80.0
58.3
21.8
0.1
0.1
<0.1
0.1
<0.1
<25
<25
<0.1
<0.1
10.6
06/21/06
IN
-
-
-
-
-
-
-
-
7.9
21.3
NA(d)
452
0.3
-
-
-
34.0
-
-
-
-
-
-
-
-
-
TA
4.5
-
-
-
-
-
-
-
8.0
21.1
NA(d)
501
0.3
-
-
-
0.7
-
-
-
-
-
-
-
-
-
TB
4.5
-
-
-
-
-
-
-
7.9
21.2
NA(d)
522
0.3
-
-
-
0.2
-
-
-
-
-
-
-
-
-
07/05/06
IN
-
113
<0.1
21
0.8
<10
30.4
0.5
8.0
23.9
NA(d)
436
0.3
79.1
58.3
20.8
28.7
28.3
0.4
0.1
28.2
<25
<25
0.5
<0.1
1.7
TA
4.6
104
<0.1
21
0.7
<10
29.2
0.5
8.0
24.0
NA(d)
520
0.3
63.9
46.8
17.1
0.5
0.5
<0.1
<0.1
0.4
<25
<25
<0.1
<0.1
1.6
TB
4.6
104
<0.1
21
0.7
<10
31.3
0.4
8.0
24.0
NA(d)
524
0.3
68.6
50.1
18.5
0.1
<0.1
<0.1
<0.1
<0.1
<25
<25
0.5
<0.1
2.0
(a) As CaCO3.
(b) As P.
(c) Water quality readings taken on 06/08/06.
(d) DO probe not operational.
Lead Vessel: TA; Lag Vessel: TB
-------
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L<"
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
07/19/06
IN
-
-
-
-
-
-
-
-
8.0
23.9
2.7
540
0.3
-
-
-
30.4
30.4
-
-
-
-
-
-
-
-
-
TA
5.0
-
-
-
-
-
-
-
7.9
24.0
2.9
567
0.3
-
-
-
0.5
0.5
-
-
-
-
-
-
-
-
-
TB
5.0
-
-
-
-
-
-
-
7.9
24.0
2.5
560
0.2
-
-
-
0.2
0.1
-
-
-
-
-
-
-
-
-
08/02/06
IN
-
110
0.5
22
0.5
<10
28.3
0.1
8.2
23.3
3.0
475
0.3
67.0
54.8
12.2
35.8
35.7
<0.1
0.1
35.6
<25
<25
0.2
0.1
2.2
TA
5.3
114
0.5
22
0.6
<10
28.6
0.2
8.1
23.3
3.5
534
0.2
80.7
60.4
20.2
0.4
0.4
<0.1
0.2
0.3
<25
<25
<0.1
0.1
2.0
TB
5.3
114
0.7
20
0.7
<10
28.7
0.2
8.0
23.4
2.4
546
0.2
81.2
61.4
19.8
0.1
0.1
<0.1
0.1
<0.1
<25
<25
<0.1
0.2
1.8
08/16/06
IN
-
-
-
-
-
-
-
-
8.1
23.5
2.6
315
0.3
-
-
-
28.5
-
-
-
-
-
-
-
-
-
TA
5.7
-
-
-
-
-
-
-
8.0
23.5
3.1
544
0.3
-
-
-
0.4
-
-
-
-
-
-
-
-
-
TB
5.7
-
-
-
-
-
-
-
8.0
23.5
3.1
554
0.3
-
-
-
0.1
-
-
-
-
-
-
-
-
-
08/30/06
IN
-
123
<0.1
28
0.6
<10
27.8
<0.1
8.0
22.7
3.0
411
0.3
80.6
65.2
15.4
35.2
33.6
1.6
0.3
33.3
<25
<25
<0.1
<0.1
2.1
TA
6.0
121
<0.1
26
0.7
<10
28.2
0.2
8.1
23.0
2.8
492
0.3
85.3
61.8
23.4
0.5
0.5
<0.1
0.3
0.2
<25
<25
<0.1
<0.1
2.7
TB
6.0
118
<0.1
26
0.7
<10
27.3
0.1
8.2
22.9
2.9
521
0.3
87.8
64.0
23.8
0.1
0.1
<0.1
0.3
<0.1
<25
<25
<0.1
<0.1
2.1
09/13/06
IN
-
-
-
-
-
-
-
-
7.9
24.0
2.5
535
0.3
-
-
-
29.0
-
-
-
-
-
-
-
-
-
TA
6.4
-
-
-
-
-
-
-
8.0
24.0
2.7
565
0.3
-
-
-
0.6
-
-
-
-
-
-
-
-
-
TB
6.4
-
-
-
-
-
-
-
7.9
24.0
2.9
555
0.3
-
-
-
0.2
-
-
-
-
-
-
-
-
-
09/27/06
IN
-
122
<0.1
22
0.7
<10
29.9
0.2
7.9
21.9
3.9
528
0.3
85.0
60.5
24.5
29.6
30.7
<0.1
0.1
30.5
<25
<25
<0.1
<0.1
1.8
TA
6.9
118
<0.1
21
0.6
<10
28.8
0.2
7.2
21.7
3.9
600
0.3
84.6
60.6
23.9
0.4
0.5
<0.1
<0.1
0.4
<25
<25
<0.1
<0.1
1.8
TB
6.9
122
<0.1
24
0.6
<10
28.5
0.2
7.9
21.1
3.7
598
0.3
85.7
62.4
23.3
<0.1
<0.1
<0.1
<0.1
<0.1
<25
<25
<0.1
<0.1
1.8
Cd
oo
(a) as CaCO3.
(b) as P.
Lead Vessel: TA; Lag Vessel:
TB
-------
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L<"
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
10/11/06
IN
-
-
-
-
-
-
-
-
7.9
21.7
3.2
542
0.4
-
-
-
28.9
29.3
-
-
-
-
-
-
-
-
-
TA
7.7
-
-
-
-
-
-
-
7.9
21.9
2.8
576
0.3
-
-
-
0.7
0.7
-
-
-
-
-
-
-
-
-
TB
7.7
-
-
-
-
-
-
-
7.9
21.8
2.7
586
0.3
-
-
-
0.2
0.2
-
-
-
-
-
-
-
-
-
01/10/07
IN
-
-
-
-
-
-
-
-
8.1
15.5
3.6
534
0.3
-
-
-
31.7
-
-
-
-
-
-
-
-
-
TA
11.0
-
-
-
-
-
-
-
8.0
15.1
3.9
563
0.3
-
-
-
1.1
-
-
-
-
-
-
-
-
-
TB
11.0
-
-
-
-
-
-
-
8.0
14.6
3.9
579
0.3
-
-
-
0.4
-
-
-
-
-
-
-
-
-
03/07/07
IN
-
-
-
-
-
-
-
-
8.2
17.1
5.4
546
0.3
-
-
-
25.1
-
-
-
-
-
-
-
-
-
TA
13.2
-
-
-
-
-
-
-
8.2
17.2
3.7
582
0.2
-
-
-
0.6
-
-
-
-
-
-
-
-
-
TB
13.2
-
-
-
-
-
-
-
8.2
17.2
3.5
591
0.2
-
-
-
0.1
-
-
-
-
-
-
-
-
-
05/02/07
IN
-
-
-
-
-
-
-
-
8.0
23.1
2.5
575
0.3
-
-
-
32.2
-
-
-
-
-
-
-
-
-
TA
14.9
-
-
-
-
-
-
-
8.0
22.9
3.0
587
0.3
-
-
-
0.9
-
-
-
-
-
-
-
-
-
TB
14.9
-
-
-
-
-
-
-
8.0
22.8
3.8
596
0.3
-
-
-
0.3
-
-
-
-
-
-
-
-
-
08/01/07
IN
-
-
-
-
-
-
-
-
8.0
25.1
2.9
553
0.4
-
-
-
27.6
-
-
-
-
-
-
-
-
-
TA
18.0
-
-
-
-
-
-
-
8.1
25.3
2.9
582
0.4
-
-
-
0.6
-
-
-
-
-
-
-
-
-
TB
18.0
-
-
-
-
-
-
-
8.1
25.4
2.7
589
0.4
-
-
-
0.1
-
-
-
-
-
-
-
-
-
11/07/07
IN
-
-
-
-
-
-
-
-
8.2
20.1
4.3
547
0.4
-
-
-
32.4
-
-
-
-
-
-
-
-
-
TA
21.5
-
-
-
-
-
-
-
8.1
20.0
3.2
573
0.4
-
-
-
0.9
-
-
-
-
-
-
-
-
-
TB
21.5
-
-
-
-
-
-
-
8.2
20.2
3.1
581
0.4
-
-
-
0.2
-
-
-
-
-
-
-
-
-
Cd
(a) as CaCO3.
(b) as P.
Lead Vessel: TA; Lag Vessel: TB
-------
Sampling Date
Sampling Location
Parameter Unit
Bed Volume
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
Total P (as P)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine (as CI2)
Total Hardness
Ca Hardness
Mg Hardness
As (total)
As (soluble)
As (particulate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
Ti (total)
10A3
mg/L(a)
mg/L
mg/L
mg/L
ng/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L(a)
mg/L<"
mg/L(a)
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
02/13/08
IN
-
-
-
-
-
-
-
-
8.0
18.8
NA(C)
NA(C)
0.4
-
-
-
32.0
-
-
-
-
-
-
-
-
-
TA
25.0
-
-
-
-
-
-
-
8.0
18.0
NA(C)
NA(C)
0.3
-
-
-
3.0
-
-
-
-
-
-
-
-
-
TB
25.0
-
-
-
-
-
-
-
8.6
17.4
NA(C)
NA(C)
NA
-
-
-
1.3
-
-
-
-
-
-
-
-
-
05/15/08
IN
-
-
-
-
-
-
-
-
8.0
23.3
NA(C)
NA(C)
0.4
-
-
-
29.6
-
-
-
-
-
-
-
-
-
TA
29.6
-
-
-
-
-
-
-
8.1
23.5
NA(C)
NA(C)
0.4
-
-
-
7.2
-
-
-
-
-
-
-
-
-
TB
29.6
-
-
-
-
-
-
-
8.1
23.5
NA(C)
NA(C)
0.4
-
-
-
0.1
-
-
-
-
-
-
-
-
-
08/20/08
IN
-
-
-
-
-
-
-
-
8.3
24.4
NA(C)
NA(C)
0.4
-
-
-
29.9
-
-
-
-
-
-
-
-
-
TA
33.3
-
-
-
-
-
-
-
8.2
24.9
NA(C)
NA(C)
0.4
-
-
-
9.4
-
-
-
-
-
-
-
-
-
TB
33.3
-
-
-
-
-
-
-
8.1
25.1
NA(C)
NA(C)
0.4
-
-
-
0.3
-
-
-
-
-
-
-
-
-
11/19/08
IN
-
-
-
-
-
-
-
-
8.2
19.9
NA(C)
NA(C)
0.4
-
-
-
31.8
-
-
-
-
-
-
-
-
-
TA
37.7
-
-
-
-
-
-
-
8.2
19.9
NA(C)
NA(C)
0.4
-
-
-
19.7
-
-
-
-
-
-
-
-
-
TB
37.7
-
-
-
-
-
-
-
8.2
19.7
NA(C)
NA(C)
0.4
-
-
-
0.4
-
-
-
-
-
-
-
-
-
02/11/09
IN
-
-
-
-
-
-
-
-
8.5
13.6
NA(C)
NA(C)
0.4
-
-
-
30.6
-
-
-
-
-
-
-
-
-
TA
40.7(d)
-
-
-
-
-
-
-
8.2
15.1
NA(C)
NA(C)
0.4
-
-
-
24.3
-
-
-
-
-
-
-
-
-
TB
40.7(d)
-
-
-
-
-
-
-
8.1
14.6
NA(C)
NA(C)
0.4
-
-
-
0.5
-
-
-
-
-
-
-
-
-
05/27/09
IN
-
-
-
-
-
-
-
-
8.0
23.3
NA(C)
NA(C)
0.4
-
-
-
25.3
-
-
-
-
-
-
-
-
-
TA
46.0
-
-
-
-
-
-
-
8.0
23.5
NA(C)
NA(C)
0.4
-
-
-
20.2
-
-
-
-
-
-
-
-
-
TB
46.0
-
-
-
-
-
-
-
8.0
23.4
NA(C)
NA(C)
0.4
-
-
-
0.2
-
-
-
-
-
-
-
-
-
Cd
to
o
(a) as CaCO3.
(b) as P.
(c) DO/ORP probes not functioning properly.
Lead Vessel: TA; Lag Vessel: TB
-------