-------
I I....
SMB
4.190 gal
71883!
96" 48' 36" 2-T / 30"
i i i i / i
~ Overflow 5o
Sanitary
Sewer
Recycle Wate
Iniaka Pom!
T
Note: Intake line 24-in
above tank bottom
Figure 4-16a. Initial Float Switch Levels in Recycle Tank
1
3'
9
.
S"R?
,
S*fi
,
7" 4 7
,
ntake *
Line!
s-
Recycle Wa!@
Note: Intake line 47. 5 -in
above tank bottom
lake
POII
T
I 60
L
I
@ t |
flT) A SJSS^aS
928 gal 2 364 gal
© *
© j
.
r
i
.,
TH-
""•"" ™**™ Overflow to
San&tary
Sewer
84~
Backwash Wastewater
Dischaftjift Lifts
^Iftto Recycle Tank)
Not to Sca/a
Figure 4-16b. Revised Float Switch Levels in Recycle Tank
33
-------
Based on the adjusted levels, the working range of the recycle system was reduced from 4,190 to 2,364
gal. These adjustments reduced the likelihood of reintroducing solids into the pressure filters, however,
increased the possibility of overflowing wastewater into the sanitary sewer in the event of sequential
backwashes.
Total operation hours of the recycle booster pump were estimated based on the total amount of
wastewater generated and the booster pump flowrate of 14 gpm, assuming the amount of wastewater
overflowing into the sanitary sewer was negligible. The total amount of wastewater generated during the
performance evaluation study was 671,148 gal, which was calculated based on the average wastewater
production rate of 724 gal/vessel/cycle and a total of 927 backwash cycles. Therefore, the recycle system
operated for 799 hr, or 29.4% of the time the treatment system was in operation.
4.4.4 Residual Management. Residual requiring disposal consisted of only backwash solids,
which accumulated at the bottom of the recycle tank. Approximately 850 kg of backwash solids were
produced during the performance evaluation study based on 927 backwash events (Table 4-5) and 920 g
of backwash solids produced per backwash event (Section 4.5.2). Sludge accumulating in the recycle
tank was pumped to the sanitary sewer.
4.4.5 System/Operation Reliability and Simplicity. There was no downtime for the treatment
system during the performance study. After all items on the system inspection punch list (Section 4.3.3,
Table 4-4) were fixed, no major operational problems were encountered. The simplicity of system
operation and operator skill requirements are discussed according to pre- and post-treatment
requirements, levels of system automation, operator skill requirements, preventative maintenance
activities, and frequency of chemical/media handling and inventory requirements.
4.4.5.1 Pre- and Post-Treatment Requirements. Pre-treatment consisted of chemical additions to
improve arsenic removal. A 12.5% NaOCl solution was added using the pre-existing equipment to
oxidize As(III) and Fe(II), and provide chlorine residuals to the distribution system. In addition to
tracking levels of the NaOCl solution in the day tank, the operator measured chlorine concentrations to
ensure that residuals existed throughout the treatment train. A 37% FeCl3 solution diluted six times was
added upstream of the contact tanks. Solution levels in the day tank were tracked daily. No post-
treatment was required.
4.4.5.2 System Automation. The C/F system was automatically controlled by the PLC in the central
control panel. The control panel contained a modem and a touch screen OIP that facilitated monitoring of
system parameters, changing of system setpoints, and checking the alarm status. System run time,
standby time, and Ap settings (Table 4-6) automatically determined when the pressure filters needed to be
backwashed. The touch screen OIP also enabled the operator to manually initiate a backwash sequence.
4.4.5.3 Operator Skill Requirements. Under normal operating conditions, the daily demand on the
operator was about 45 min for visual inspection of the system and recording of operational parameters
such as pressure, volume, flowrate, and chemical usage on field log sheets. After receiving proper
training during system startup, the operator understood the PLC, knew how to use the touch screen OIP,
and was able to work with the vendor to troubleshoot problems and perform minor onsite repairs.
The State of Delaware requires all operators of public water treatment and distribution systems to have a
valid base-level license, which requires the operator to have:
• High school diploma or equivalent and one year of acceptable operating experience, or;
• Three years of acceptable operating experience, and;
• Successful completion of base-level written examination.
34
-------
4.4.5.4 Preventative Maintenance Activities. The vendor recommended several routine maintenance
activities to prolong the integrity of the treatment system (Kinetico, 2005). Daily preventative
maintenance tasks included recording pressure and flowrate readings and chemical drum levels and
visually checking for leaks, overheating components, proper manual valve positioning and pumps'
lubricant levels, and any unusual conditions. The vendor recommended weekly checking for trends in the
recorded data that might indicate a decline in system performance, and semi-annually servicing and
inspecting ancillary equipment and replacing worn components. Cleaning and replacement of sensors and
replacement of o-ring seals and gaskets of valves were performed as needed.
4.4.5.5 Chemical Handling and Inventory Requirements. Chlorine and iron additions were
required for effective arsenic removal. The operator tracked usage of the chemical solutions daily (by
solution levels), coordinated supplies, and refilled the day tanks as needed. A 12.5% NaOCl solution,
supplied in 55-gal drums by Wilbur-Ellis, was transferred to the day tank and injected without dilution. A
37% FeCl3 solution, supplied in 180-lb drums by Hawkins Chemical, was diluted by a factor of six in the
66-gal day tank prior to injection into the chlorinated water. Speed and stroke settings of the chemical
pumps were adjusted, as needed, to acquire the target chlorine residuals as measured regularly with a
Hach pocket colorimeter and iron concentrations after the contact tanks.
4.5 System Performance
The performance of the Macrolite® Arsenic Removal System was evaluated based on analyses of water
samples collected from the treatment plant, system backwash, and distribution system.
4.5.1 Treatment Plant Sampling. Treatment plant water was sampled on 57 occasions (including
four duplicate events) during the 13.5 months of system operation. Field speciation also was performed
for 14 of the 57 occasions. Table 4-7 summarizes the analytical results for arsenic, iron, and manganese.
Five outliers with either significantly low (on November 29, 2006) or significantly high arsenic, iron,
and/or manganese concentrations (on March 21, April 18, and August 8, 2007) at the AC sampling
location were not included in statistical calculations shown in Table 4-7. These significantly elevated
arsenic, iron, and manganese concentrations probably were due to introduction of backwash solids from
the recycle tank. The August 8 event took place even after the level float switches in the recycle tank and
the intake line from the recycle tank had been moved up from the bottom of the tank in May 2007
(Section 4.4.3.3). It was not clear, however, what had caused the low concentrations to be measured on
November 29, 2006. Table 4-8 summarizes the results of the other water quality parameters. Appendix B
contains a complete set of analytical results. The results of the water samples collected across the
treatment train are discussed below.
4.5.1.1 Arsenic. Figure 4-17 shows total arsenic concentrations measured across the treatment train
and Figure 4-18 presents the results of the 14 speciation events. Total arsenic concentrations in source
water ranged from 27.2 to 43.3 (ig/L and averaged 34.4 (ig/L with soluble As(III) existing as the
predominant species at 29.1 (ig/L (on average) (Table 4-7 and Figure 4-18). Low concentrations of
particulate arsenic and soluble As(V) also were present in source water, with concentrations averaging
3.4 and 2.1 (ig/L, respectively. The arsenic concentrations measured during the 13.5-month performance
evaluation study were consistent with those of source water collected during the initial site visit on
October 7, 2004.
Following prechlorination and the contact tanks, total arsenic concentrations remained essentially
unchanged at 35.1 (ig/L (on average). Arsenic, however, existed mostly as particulate arsenic (26.1 (ig/L
[on average]) with only a small fraction remaining in the soluble form (8.9 (ig/L). Of the soluble fraction,
35
-------
Table 4-7. Summary of Arsenic, Iron, and Manganese Analytical Results
Parameter
As
(total)
As
(soluble)
As
(paniculate)
As(III)
As(V)
Fe
(total)
Fe
(soluble)
Mn
(total)
Mn
(soluble)
Sampling
Location
IN
AC
TA
TB
TC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TA
TB
TC
TT
IN
AC
TT
IN
AC
TA
TB
TC
TT
IN
AC
TT
Unit
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
Number
of
Samples
57
52W
43
43
43
14
14
14
14
14
14
14
14
I3(b>
13(0
14
13(d)
14
57
52(e)
43
43
43
14
14
13W
14
57
52(g)
43
43
43
14
14
14
14
Minimum
Concentration
27.2
27.0
3.1
3.4
3.4
1.8
26.1
3.6
2.5
<0.1
19.5
<0.1
19.9
<0.1
<0.1
<0.1
3.1
2.2
<25
704
<25
<25
<25
<25
<25
<25
<25
<0.1
5.1
<0.1
<0.1
<0.1
<0.1
1.3
<0.1
<0.1
Maximum
Concentration
43.3
53.7
15.9
17.2
17.6
13.4
38.1
18.1
13.0
5.8
33.6
2.5
38.3
2.2
1.8
8.8
15.9
10.6
62.5
4,699
290
327
217
148
50.0
<25
<25
2.9
23.7
1.7
1.9
1.5
1.6
3.0
1.0
1.6
Average
Concentration
34.4
35.1
7.5
7.4
7.2
8.3
31.2
8.9
7.2
3.4
26.1
1.2
29.1
0.7
0.6
2.1
8.1
6.0
26.1
1,905
45.6
48.4
37.1
37.9
21.6
<25
<25
1.4
10.1
0.2
0.3
0.2
0.3
1.7
0.3
0.3
Standard
Deviation
3.6
4.9
2.9
2.7
2.8
3.6
3.1
4.3
3.1
1.9
4.2
0.9
3.9
0.6
0.5
2.1
4.2
2.7
13.6
709
61.6
57.2
44.8
41.9
13.4
-
-
0.4
3.6
0.3
0.4
0.3
0.4
0.5
0.4
0.5
(a) Five outliers (i.e., 12.2 ug/L on 11/29/06, 210 and 174 ug/L on 03/21/07, 142 ug/L on 04/18/07, and 104
ug/L on 08/08/07) omitted.
(b) One outlier (i.e., 8.6 ug/L on 01/31/07) omitted.
(c) One outlier (i.e., 10.1 ug/L on 01/31/07) omitted.
(d) One outlier (i.e., 0.9 ug/L on 01/31/07) omitted.
(e) Five outliers (i.e., 279 ug/L on 11/29/06, 13,646 and 10,937 ug/L on 03/21/07, 8,962 ug/L on 04/18/07,
and 6,632 ug/L on 08/08/07) omitted.
(i) One outlier (i.e., 177 ug/L on 12/6/06) omitted.
(g) Five outliers (i.e., 1.6 ug/L on 11/29/06, 59.2 and 48.8 ug/L on 03/21/07, 37.7 ug/L on 04/18/07, and 35.2
ug/L on 08/08/07) omitted.
36
-------
Table 4-8. Summary of Other Water Quality Parameter Results
Parameter
Alkalinity
(as CaCO3)
Fluoride
Sulfate
Nitrate
(asN)
Silica
(as SiO2)
Phosphorous
(asP)
Turbidity
pH
Temperature
Sampling
Location
IN
AC
TA
TB
TC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TA
TB
TC
TT
IN
AC
TA
TB
TC
TT
IN
AC
TA
TB
TC
TT
IN
AC
TA
TB
TC
TT
IN
AC
TA
TB
TC
TT
Unit
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
NTU
NTU
NTU
NTU
NTU
NTU
s.u.
s.u.
s.u.
s.u.
s.u.
s.u.
°c
°c
°c
°c
°c
°c
Number
of
Samples
57
57
43
43
43
14
14
14
14
14
14
14
14
14
14
57
57
43
43
43
14
57
57
43
43
43
14
57
57
43
43
43
14
39W
39(b)
29(c>
29(d)
29(e>
I0(t>
41
41
30
30
30
11
Minimum
Concentration
276
283
280
274
270
300
1.0
1.0
1.0
9.0
8.8
8.8
0.05
0.05
0.05
8.5
8.6
8.4
8.3
8.3
8.5
23.3
21.7
<10
<10
<10
<10
0.2
0.9
0.2
0.2
0.3
0.3
7.8
7.7
7.7
7.7
7.7
7.9
14.7
14.7
14.7
14.8
14.8
18.1
Maximum
Concentration
349
339
341
339
331
327
2.0
1.8
2.8
21.0
18.0
18.0
0.05
0.05
0.05
11.6
13.7
11.1
11.3
11.2
10.3
110
298
47.9
48.1
49.3
79.0
4.8
20.0
5.1
4.5
3.6
3.3
8.9
8.9
8.9
9.0
9.0
8.5
20.8
20.2
21.0
20.3
19.9
19.3
Average
Concentration
321
315
313
312
311
316
1.4
1.4
1.6
10.8
10.4
10.3
0.05
0.05
0.05
9.5
9.7
9.2
9.1
9.1
9.2
44.7
57.3
11.5
11.2
10.8
16.6
1.2
3.1
1.3
1.1
1.1
1.0
8.3
8.3
8.3
8.3
8.3
8.3
19.2
18.8
18.9
18.8
18.7
18.8
Standard
Deviation
11.8
11.7
10.8
12.7
11.7
8.2
0.3
0.2
0.5
3.0
2.3
2.3
-
-
-
0.6
0.9
0.6
0.6
0.6
0.5
13.4
48.2
9.7
9.5
8.9
19.7
1.1
3.5
1.2
1.0
0.9
0.8
0.2
0.2
0.3
0.3
0.3
0.2
1.1
0.8
1.0
0.9
1.2
0.4
37
-------
Table 4-8. Summary of Other Water Quality Parameter Results
Parameter
DO
ORP
Free
Chlorine
(as C12)
Total
Chlorine
(as C12)
Total
Hardness
(as CaCO3)
Ca Hardness
(as CaCO3)
Mg Hardness
(as CaCO3)
Sampling
Location
IN
AC
TA
TB
TC
TT
IN
AC
TA
TB
TC
TT
AC
TA
TB
TC
TT
AC
TA
TB
TC
TT
IN
AC
TT
IN
AC
TT
IN
AC
TT
Unit
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
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Mg/L
Number
of
Samples
41
41
30
30
30
11
41
41
30
30
30
11
41
30
30
30
11
41
30
30
30
11
14
14
14
14
14
14
14
14
14
Minimum
Concentration
0.5
0.4
0.6
0.6
0.5
0.6
216
251
277
287
486
335
0.2
0.2
0.2
0.2
0.4
0.3
0.3
0.3
0.3
0.5
35.4
34.6
36.1
13.9
14.1
14.1
20.0
18.6
19.7
Maximum
Concentration
.4
.7
2.6
.9
.7
.1
444
630
651
652
673
572
.7
.3
.4
.4
.2
.8
.4
.4
.4
.3
41.3
42.6
40.6
19.4
20.2
19.8
25.2
24.9
23.9
Average
Concentration
1.0
1.1
1.2
1.0
1.0
0.9
320
456
500
536
580
490
0.8
0.7
0.74
0.77
0.83
0.83
0.76
0.76
0.81
0.86
39.3
39.1
38.6
16.8
17.0
16.8
22.4
22.1
21.8
Standard
Deviation
0.2
0.3
0.4
0.3
0.3
0.2
72.7
97.3
101
96.1
47.1
71.5
0.3
0.3
0.2
0.3
0.2
0.3
0.3
0.2
0.2
0.2
1.8
1.9
1.3
1.7
1.5
1.4
1.3
1.7
1.3
(a) Two outliers (i.e., 9.3 on 06/13/07 and 9.8 on 06/20/07) omitted.
(b) Two outliers (i.e., 9.3 on 06/13/07 and 10.0 on 06/20/07) omitted.
(c) One outlier (i.e., 9.3 on 06/13/07) omitted.
(d) One outlier (i.e., 9.4 on 06/13/07) omitted.
(e) One outlier (i.e., 9.3 on 06/13/07) omitted.
(f) One outlier (i.e., 10.0 on 06/20/07) omitted.
only 0.7 ug/L (on average) existed as As(III) (except for one data point at 8.6 (ig/L on January 31, 2007),
indicating effective oxidation of As(III) by chlorine. The reason for the exceptionally high As(III)
concentration on January 31, 2007, was unclear. Free and total chlorine concentrations measured in the
system effluent on that day were 0.8 and 0.8 mg/L, respectively, which were consistent with the
respective average values shown in Table 4-8. As much as 8.1 ug/L of As(V) was measured following
the contact tanks, suggesting the need for further increasing iron doses.
38
-------
60
50 -
40 -
20 -
10 --
11/15/06
10/18/06 11/29/06
10/25/06 AT-. , 12/20/06
702/21/07
05/02/07
04/11/071
08/22/07
10[jg/L
-------
Arsenic Species at Wellhead (IN)
AZ
As Concentration (\ig:L}
-^-"•ISJIVJWWJv-l
D010010010010C
=
=
.
-
-
-
=
-
.
=
•
nAs(particulate)
•As(V)
nAs(lll)
—
4
Arsenic Species after Conctact Tanks (AC)
v>
^x
DAs(particulate)
•As(V)
nAs(lll)
/ ^
^
„/ „/
^ " 4? ^' 'f ^V fV4 (V* cxl' c\3 oP* (SP csP cV r\o
J
./,/
# / A#
ANJ
<&"
0J
cr
x
\v
16
Arsenic Species after Tanks A, B, and C Combined (TT)
=d 14 -
0)
3 12 -
o 10-
S
o>
o
o
u
w
<
8 -
6 -
4 -
2 -
0 --
CT
. _10 ugiLMCL
s<^ .\<^ V<^ V^ A<^ v<^- x<^ ^
?3 yy -,'V ^C> r&y /^V ^ lA
/ vV ,\V \V ^\V \v \\ \^
Figure 4-18. Arsenic Speciation Results
40
-------
Table 4-9. Ineffective Arsenic Removal Due to Inadequate Iron Addition
Date
10/18/06
11/15/06
03/28/07
05/02/07
06/20/07
07/18/07
08/22/07
TA
Total
As
(MS/L)
10.6
11.8
NM
17.9
NM
10.3
NM
Total
Fe
(MS/L)
50.3
<25
NM
<25
NM
<25
NM
TB
Total
As
(MS/L)
10.4
12.2
NM
19.5
NM
11.3
NM
Total
Fe
(MS/L)
<25
<25
NM
<25
NM
<25
NM
TC
Total
As
(MS/L)
10.3
11.9
NM
19.3
NM
11.7
NM
Total
Fe
(MS/L)
<25
<25
NM
<25
NM
<25
NM
TT
Total
As
(MS/L)
NM
NM
12.8
NM
10.8
NM
12.8
As(V)
(MS/L)
NM
NM
8.5
NM
9.0
NM
10.6
Total
Fe
(MS/L)
NM
NM
<25
NM
<25
NM
<25
AC
Total
Fe
(MS/L)
1,252
1,017
788
704
1,268
1,528
1,111
Soluble
Fe
(MS/L)
NM
NM
<25
NM
<25
NM
<25
NM = not measured
species (66 to 83% of the total As), implying that more iron would need to be added for more complete
arsenic removal. Total iron concentrations measured following the contact tanks (AC) were all
significantly lower than the average concentration at AC (i.e. 1,905 (ig/L, Table 4-9), which further
supports the need for more iron addition.
Conversely, the six events shown in Table 4-10 seem to suggest particulate arsenic/iron breakthrough
being the main reason for the elevated arsenic concentrations observed. These samples were all collected
close to the end of a filter run before a backwash was triggered. As shown in Table 4-10, elevated iron
concentrations were measured in filter effluent for all samples except one on April 18, 2007, implying
particulate arsenic/iron leakage. Arsenic/iron leakage occurred occasionally even after the Ap trigger had
been decreased from 25 to 18 psi on January 17, 2007 (in an attempt to reduce run times and, therefore,
the likelihood of arsenic/iron particle breakthrough from the filters [Section 4.4.3.1]). Note that increases
in arsenic concentrations at the AC location on March 21, April 18, August 8, 2007, due to introduction
of backwash solids from the recycle tank did not cause excessive arsenic breakthrough from the pressure
filters.
Table 4-10. Ineffective Arsenic Removal Due to Arsenic/Iron Leakage
Date
10/25/06
11/29/06
12/20/06
02/21/07
04/11/07
04/18/07
TA
Total
As
(tig/L)
10.1
11.2
10.4
13.9
12.3
11.5
Total
Fe
(HB/L)
83.0
164.0
124
289
216
<25
TB
Total
As
(HB/L)
10.5
_(a)
10.2
10.3
_(a)
_(a)
Total
Fe
(HB/L)
85.1
<25
92.7
101
35.9
<25
TC
Total
As
(H8/L)
_(a)
_(a)
_(a)
12.1
_(a)
_(a)
Total
Fe
(HB/L)
57.4
<25
97.9
217
36.1
<25
(a) Data not presented since total arsenic concentration did not
exceed 10 ng/L MCL.
4.5.1.2 Iron. Figure 4-19 presents total iron concentration measured across the treatment train.
Total iron concentrations in source water ranged from <25 to 62.5 (ig/L and averaged 26.1 (ig/L, which
existed primarily in the soluble form.
41
-------
On 11/03/06 ,
stroke length
increased to 25%
fora target dosage
of 1.5 mg/L (as Fe).
On 09/17/07, chemical
feed pump switched
from flow-paced to
manual ope ration;
stroke length and speed
set at 75 & 25%,
respectively; iron
dosage targeted at
2.0 mg/L (as Fe).
On 01/17/07, stroke length
increased to 32% fora
target dosage of 2.0 mg/L
(as Fe).
# _V<*> v<$ _V<$
!\ XV rA
-•—AtWellhead (IN)
-.i-After Tank A (TA)
-6-After Tan kC(TC)
-AfterContact Tanks (AC)
-AfterTank B (TB)
-AfterTanks A, B, and C Combined (TT)
Figure 4-19. Total Iron Concentrations Across Treatment Train
Total iron concentrations after the contact tanks varied significantly, ranging from 704 to 4,699 (ig/L and
averaging 1,905 (ig/L (not including the five outliers noted in footnote e). Variations in iron
concentrations were caused primarily by the difficulties encountered operating the flow-paced iron
injection pump (Section 4.4.2). As expected, iron after the contact tanks existed solely as particulate iron
(except for one data point at 177 (ig/L on December 6, 2006).
Total iron concentrations in system effluent ranged from <25 to 327 (ig/L, and averaged 43.1 (ig/L.
Approximately 60% of the samples collected at the system outlet had total iron concentrations below the
method reporting limit of 25 (ig/L. The remaining 40% of samples had iron concentrations higher than 25
(ig/L, with one sample collected on August 29, 2007, containing 327 (ig/L. Iron in system effluent
existed only in the particulate form, indicating leakage through the pressure filters. The frequency of
particulate iron leakage did decrease after January 17, 2007, i.e. from 3 times during the initial 4 months
before January 17, 2007 to 3 times during the remaining 10 months afterwards. As described in Section
4.4.3.1, on January 17, 2007, the Ap backwash trigger was reduced to help shorten run times and reduce
iron breakthrough from the filters. As described in Section 4.5.1.1, particulate iron leakage often
occurred together with particulate arsenic leakage.
4.5.1.3 Manganese. Figure 4-20 presents total manganese concentrations measured during the
demonstration study. In source water, manganese concentrations ranged from <0.1 to 2.9 |o,g/L and
averaged 1.4 (ig/L, existing primarily in the soluble form. After chlorination, iron addition, and contact
tanks, total manganese concentrations increased significantly to an average of 10.1 (ig/L, existing
42
-------
O)
3
O
ID
O
O
O
c
10 -
5 -
' / /
•& n^ •
X X X X X
° < *>
—•—At Wellhead (IN)
— &— After Tank A (TA)
-e- After Tank C (TC)
After Contact Tanks (AC)
— Q— After Tank B (TB)
—•—After Tanks A, B, andC Combined (TT)
Figure 4-20. Total Manganese Concentrations Across Treatment Train
primarily (over 97%) as particulate manganese. The increase in manganese concentration probably was
caused by trace amounts of manganese in the pretreatment chemicals. Particulate manganese apparently
was removed by the pressure filters, leaving only trace amounts (0.3 |og/L) in filter effluent.
4.5.1.4 pH, DO, and ORP. pH values in source water ranged from 7.8 to 8.9 and averaged 8.3. This
range was consistent with the pH measurements taken by Battelle during source water sampling on
October 7, 2004 (i.e., 8.2 in Table 4-1). DO levels of source water were low, ranging from 0.5 to 1.4
mg/L and averaging 1.0 mg/L. DO levels remained low across the treatment train, with average values
ranging from 0.9 to 1.2 mg/L. ORP readings of source water were uncharacteristically high, ranging from
216 to 444 mV and averaging 320 mV. These high values most likely were caused by the handheld
meter, which tends to drift during measurements. After prechlorination, average ORP readings increased
significantly to 456 mV after the contact tanks and to 527 mV after the pressure filters.
4.5.1.5 Chlorine. Figure 4-21 presents total and free chlorine residuals measured throughout the
treatment train. As shown in the figure, data were scattered extensively, with total chlorine residuals
ranging from 0.3 to 1.8 mg/L (as C12) and free chlorine residuals ranging from 0.2 to 1.7 mg/L (as C12).
Assuming that 4.3 mg/L of NaOCl (as C12) had been applied to source water, 0.044 mg/L (as C12) would
have reacted with As(III), Fe(II), and Mn(II) based on the respective average concentrations (i.e., 29.1,
21.6, and 1.7 (ig/L) in source water (Table 4-7), and 2.45 mg/L would have reacted with 0.32 mg/L of
ammonia (as N) to reach breakpoint chlorination. As such, 1.8 mg/L (as C12) would have been present as
free chlorine in treated water. These theoretical amounts appear to fall just inside (and outside) the
measured ranges for total and free residuals.
43
-------
2.0
1.6
O Total at AC
D Total at TA, TB, and TC
Total at TT
Free at AC
XFreeatTA, TB, and TC
O Free at TT
o
J
"a
1.2
1.0
I *
2
Ifl
&
0.8
0.6
0.4
0.2
" p A
:x a.
-tH»
X
«
» X
A*
0.0
10/01/06 10/31/06 11/30/06 12/30/06 01/29/07 02/28/07 03/30/07 04/29/07 05/29/07 06/28/07 07/28/07 08/27/07 09/26/07 10/26/07
Date
Figure 4-21. Chlorine Residuals Measured Throughout Treatment Train
4.5.1.6 Other Water Quality Parameters. Alkalinity, fluoride, sulfate, nitrate, silica, pH,
temperature, and hardness levels remained relatively constant across the treatment train and were not
affected by the treatment process (Table 4-8). Phosphorus levels after the contact tanks were slightly
higher than those in source water (i.e., 57.3 vs. 44.7 |o,g/L [on average]), probably due to the presence of
trace quantities in the pretreatment chemicals. Phosphorus levels decreased significantly to <17.0 ng/L
(on average) after the pressure filters, indicating removal via coagulation/filtration. Turbidity also
decreased slightly with treatment (i.e., from 3.1 to <1.3 NTU on average).
4.5.2 Backwash Water and Solids Sampling. Treated water was used for backwash. Table 4-11
presents analytical results from 11 backwash wastewater sampling events starting from November 30,
2006, through October 10, 2007. Results for the November 30, 2006, sampling event are not included in
the table because these samples were collected from an incorrect sampling tap.
pH, TDS, and total suspended solids (TSS) values ranged from 7.9 to 8.1 (averaged 8.0), from 324 to
1,040 mg/L (averaged 370 mg/L), and from 125 to 685 mg/L (averaged 336 mg/L), respectively. The
average pH value of backwash wastewater (i.e., 8.0) was somewhat lower than that across the treatment
train (i.e., 8.3). Concentrations of total arsenic, iron, and manganese ranged from 371 to 2,203 |og/L
(averaged 1,229 (ig/L), 27.5 to 188 mg/L (averaged 107 mg/L), and 151 to 955 |o,g/L (averaged 551
(ig/L), respectively. Over 99% of these metals were present in the partculate form.
Assuming that 724 gal (Table 4-5) of backwash wastewater would be generated from each vessel during
each backwash event and that 336 mg/L of TSS would be produced, approximately 920 g of solids were
generated from each filtration vessel during each backwash and were discharged into and accumulated in
the recycle tank. Based on the average particulate metal data in Table 4-11, approximately 3.4 g of
44
-------
Table 4-11. Backwash Wastewater Sampling Results
Sampling Event
No.
1
2
3
4
5
6
7
8
9
10
11
Date
11/30/2006(a)
01/03/07
02/07/07
03/07/07
04/05/07
05/09/07
06/14/07
07/11/07
08/08/07
09/05/07
10/10/07
BW1
Backwash Tank A
31
CL
s.u.
in
Q
\—
mg/L
"&
\—
mg/L
I
CO
<
M9/L
As (soluble)
M9/L
As (particulate)
M9/L
CD
§
CD
M9/L
Fe (soluble)
M9/L
I
£=
^
M9/L
Mn (soluble)
M9/L
BW2
Backwash Vessel Tank B
m
o
S.U.
in
Q
mg/L
%
\—
mg/L
I
CO
<
M9/L
As (soluble)
M9/L
As (particulate)
M9/L
ro
§
CD
M9/L
Fe (soluble)
M9/L
S3
a
c=
^
M9/L
Mn (soluble)
M9/L
BW3
Backwash Tank C
m
o
S.U.
if>
Q
mg/L
%
\—
mg/L
I
CO
<
M9/L
As (soluble)
M9/L
As (particulate)
M9/L
ro
§
CD
LL
M9/L
Fe (soluble)
M9/L
I
c=
S
M9/L
Mn (soluble)
M9/L
Samples were collected from the wrong sample taps during the first sample collection on 1 1 /30/06; data was not reported.
8.0
8.1
8.1
8.0
7.9
7.9
8.0
8.1
8.0
8.0
328
332
344
344
352
358
356
354
360
356
190
266
410
265
155
335
420
195
390
205
800
1,108
1,656
765
769
1,559
1,997
876
1,039
716
9.6
6.7
7.6
5.7
6.9
6.3
6.3
7.0
3.4
3.0
790
1,101
1,648
759
762
1,553
1,990
869
1,036
713
73,404
90,169
135,760
62,605
54,835
121,064
187,504
64,893
131,939
76,129
<25
85.3
<25
29.0
<25
<25
<25
<25
<25
<25
364
398
592
320
316
616
955
364
686
392
0.2
0.5
<0.1
1.4
0.2
<0.1
0.2
<0.1
<0.1
0.2
8.0
8.0
8.1
8.0
7.9
7.9
8.0
8.1
8.0
8.0
324
338
348
336
354
342
352
324
370
358
430
450
635
685
215
195
330
125
420
190
1,462
1,518
2,049
1,679
750
627
1,309
371
761
618
15.2
5.9
7.7
5.7
6.4
5.7
6.6
7.1
3.9
3.3
1,447
1,512
2,041
1,674
744
621
1,302
364
757
615
130,280
117,655
165,859
135,388
62,365
51,888
113,355
27,492
114,914
83,641
78.1
37.2
<25
<25
<25
<25
<25
<25
<25
<25
621
545
800
708
375
274
611
151
595
449
0.4
0.3
<0.1
0.3
<0.1
<0.1
<0.1
<0.1
0.1
<0.1
8.0
8.0
8.0
8.0
7.9
8.0
8.1
8.1
8.0
8.0
326
334
354
346
362
1,040
362
334
360
358
285
515
590
565
240
255
320
250
220
345
1,247
2,061
2,203
1,848
1,021
1,347
1,495
1,434
601
1,191
15.6
6.8
8.1
6.2
6.3
6.2
6.8
7.0
5.5
2.9
1,231
2,054
2,195
1,842
1,015
1,341
1,488
1,427
596
1,188
124,876
151,885
171,373
148,509
84,375
83,132
131,067
108,815
64,245
140,627
76.8
69.0
<25
30.6
<25
<25
<25
<25
<25
<25
584
745
829
735
500
439
706
601
327
929
0.3
0.5
<0.1
1.1
<0.1
0.1
0.1
<0.1
<0.1
0.1
(a) November 2006 results omitted since samples collected from an incorrect tap.
-------
arsenic (i.e. 0.4% by weight), 293 g of iron (i.e. 31.8 % by weight), and 1.5 g of manganese (i.e. 0.2 % by
weight) were generated from each vessel during each backwash event.
Solids loadings to the recycle tank also were monitored through collection of backwash solids (Section
3.3.5). Table 4-12 presents analytical results of the solid samples collected in May and October 2007.
Arsenic, iron, and manganese levels in the solids averaged 3.4 mg/g (or 0.34% by weight), 324 mg/g (or
32.4% by weight), and 2.0 mg/g (or 0.2 % by weight), respectively. These amounts matched very well
with those derived from the backwash wastewater metal analysis (i.e. 0.4%, 31.8%, and 0.2%,
respectively).
Table 4-12. Backwash Solids Sampling Results
Date: Location
05/09/07: Vessel A
05/09/07: Vessel B
05/09/07: Vessel C
10/10/07: Vessel A
10/10/07: Vessel B
10/10/07: Vessel C
Mg
mg/g
4.8
5.4
4.5
4.5
4.2
3.9
Si
ug/g
681
558
372
126
244
393
P
mg/g
5.1
4.5
6.4
6.2
5.3
6.0
Ca
mg/g
19.8
24.1
23.3
17.4
14.1
15.2
Fe
mg/g
245
311
344
343
303
400
Mn
mg/g
1.7
2.0
2.1
2.0
1.9
2.3
As
mg/g
3.2
3.6
4.5
3.2
2.8
3.3
Ba
ug/g
45.9
43.5
37.7
24.6
31.6
20.6
4.5.3 Distribution System Water Sampling. Table 4-13 summarizes results of the distribution
system sampling. The stagnation times for the samples ranged from 6.0 to 18.0 hr and averaged 9.5 hr,
which is 58% longer than the 6-hr minimum stagnation time required by LCR.
There was no change in pH values before and after system startup. pH values before startup ranged from
7.6 to 8.3 and averaged 8.0; pH values after system startup ranged from 7.7 to 8.1 and averaged 8.0.
Alkalinity levels stayed essentially unchanged, with concentrations ranging from 304 to 326 mg/L (as
CaCO3) before startup and from 301 to 332 mg/L (as CaCO3) after startup.
Arsenic concentrations in the baseline samples were similar among the three LCR locations, ranging from
24.8 to 47.0 (ig/L and averaging 34.4 (ig/L. These concentrations were consistent with those in source
water (i.e., 27.2 to 43.3 (ig/L and averaged 34.4 (ig/L) as shown in Table 4-7. After system startup,
arsenic concentrations decreased significantly to an average of 8.5 ug/L. Arsenic levels in the distribution
system were slightly higher than those in treatment system effluent (i.e., 8.3 ug/L [on average] in Table 4-
7), indicating some resuspension and redissolution of arsenic in the distribution system. Figure 4-22
illustrates the effect of the treatment system on As, Fe, and Mn concentrations in the distribution system.
Iron concentrations in the baseline samples were low, ranging from <25 to 47.0 ug/L and averaging 26.9
ug/L. These concentrations were consistent with those in source water (i.e., ranging from <25 to 62.5
ug/L and averaging 26.1 ug/L in Table 4-7). After system startup, the average iron concentration
increased slightly to 38.1 ug/L, which was consistent with the average iron concentration of 43.7 ug/L in
system effluent (Table 4-7). The slight increase in iron levels was likely due to instances of iron
breakthrough from the pressure filters. For the most part, iron concentrations in the distribution system
mirrored those in treatment system effluent (Figure 4-22).
Total manganese concentrations in the distribution system averaged 1.7 and 0.5 ug/L before and after
system startup. Total manganese levels in the distribution system were consistent with those measured in
system effluent (i.e., 0.3 ug/L [on average] at TT location).
46
-------
Table 4-13. Distribution System Sampling Results
Sampling
Event
No.
BL1
BL2
BL3
BL4
1
2
3
4
5
6
7
8
9
10
11
DS1
24 E. Sewell St.
LCR
1st draw
Stagnation Time
Date | hrs
04/13/05
05/11/05
06/15/05
07/13/05
11/08/06
12/20/07
01/17/07
02/14/07
03/14/07
04/11/07
05/09/07
06/14/07
07/19/07
08/15/07
09/12/07
7.5
6.0
18.0
7.5
9.0
8.0
10.0
7.4
7.6
9.0
8.0
7.9
8.0
8.0
6.3
X
Q.
s.u.
8.3
7.8
8.2
7.9
7.8
7.7
7.9
8.0
8.0
8.0
8.0
8.0
8.1
8.0
8.1
Alkalinity
in
-------
Arsenic in Treated Water and Distribution System
O2/O8/O5 O5/O9/O5 O8/O7/O5 11/O5/O5 O2/O3/O6 O5/O4/O6 O8/O2/O6 1O/31/O6 O1/29/O7 O4/29/O7 O7/28/O7 1O/26/O7
Iron in Treated Water and Distribution System
02/08/05 05/09/05 O8/O7/O5 11/O5/O5 O2/O3/O6 O5/O4/O6 O8/O2/O6 1O/31/O6 O1/29/O7 O4/29/O7 O7/28/O7 1O/26/O7
Manganese in Treated Water and Distribution System
02/08/05 05/09/05 O8/O7/O5 11 /O5/O5 O2/O3/O6 O5/O4/O6 O8/O2/O6 10/31 /O6 01/29/O7 O4/29/O7 O7/28/O7 10/26/O7
-DS1
-DS2
-DS3
Treated Water
Figure 4-22. Effects of Treatment System on Arsenic, Iron, and Manganese in Distribution System
48
-------
Lead and copper concentrations within the distribution system decreased slightly from baseline levels.
Baseline lead concentrations ranged from 1.2 to 7.7 (ig/L and averaged 2.4 (ig/L; baseline copper
concentrations ranged from 33.9 to 162 (ig/L and averaged 85.6 (ig/L. After system startup, lead levels
decreased slightly to 1.6 (ig/L (on average) with no samples exceeding the action level of 15 (ig/L.
Copper concentrations decreased to 44.0 (ig/L with no samples exceeding the 1,300 (ig/L action level.
4.6
System Cost
The system cost was evaluated based on the capital cost per gpm (or gpd) of design capacity and the
O&M cost per 1,000 gal of water treated. Capital cost of the C/F system included cost for equipment, site
engineering, and system installation, shakedown, and startup. O&M cost included cost for chemicals,
electricity, and labor. Cost associated with the building, including the recycle system, sanitary sewer
connections, and water system telemetry, was not included in the capital cost because it was not included
in the scope of this demonstration project and was funded separately by the Town of Felton.
4.6.1 Capital Cost. The capital investment for the Macrolite® Arsenic Removal System was $334,297
(Table 4-14). The equipment cost was $201,292 (or 60% of the total capital investment), which included
cost for an iron addition system, two contact tanks, three pressure vessels, 75 ft3 of Macrolite®,
instrumentation and controls, miscellaneous materials and supplies, labor, and system warranty. The
system warranty cost covered the cost for repair and replacement of defective system components and
installation workmanship for 12 months after system startup.
Table 4-14. Capital Investment for Kinetico's C/F System
Description
Quantity
Cost
% of Capital
Investment Cost
Equipment
Welded stainless steel frame
Fiberglass pressure vessel
Fiberglass contact tank
Wedge wire distributors
Macrolite® media (75 ft3)
Process valves and piping
Air scour system
Chemical feed equipment
Instrumentation and controls
Turbidimeter
Additional sample taps/totalizer/meters
Shipping
Labor
Equipment Total
1
3
2
3
1
1
1
1
1
1
-
1
1
-
$12,500
$24,426
$16,284
$9,909
$18,750
$26,278
$6,300
$6,402
$18,723
$6,612
$1,700
$2,600
$50,808
$201,292
-
-
-
-
-
-
-
-
-
-
-
-
-
60%
Engineering
Labor 1 1
Engineering Total | -
$44,520
$44,520
-
13%
Installation, Shakedown, and Startup
Labor
Subcontractor
Travel
Installation, Shakedown, and Startup
Total Capital Investment
1
1
1
-
-
$15,400
$68,300
$4,785
$88,485
334,297
-
-
-
27%
100%
49
-------
The site engineering cost covered the cost for preparing the required permit application submittal
(including a process design report, a general arrangement drawing, P&IDs, electrical diagrams,
interconnecting piping layouts, tank fill details, and a schematic of the PLC panel) and obtaining the
required permit approval from DHSS. The engineering cost of $44,520 was 13% of the total capital
investment. The installation, shakedown, and startup cost covered the labor and materials required to
unload, install, and test the system for proper operation. All installation activities were performed by the
vendor's subcontractor, and startup and shakedown activities were performed by the vendor with the
operator's assistance. The installation, startup, and shakedown cost of $88,485 was 27% of the total
capital investment.
The total capital cost of $334,297 was normalized to $891/gpm ($0.62/gpd) of design capacity using the
system's rated capacity of 375 gpm (or 540,000 gpd). The total capital cost also was converted to an
annualized cost of $31,554 gal/yr using a capital recovery factor (CRF) of 0.09439 based on a 7% interest
rate and a 20-yr return period. Assuming that the system operated 24 hr/day, 7 day/week at the design
flowrate of 375 gpm to produce 197,100,000 gal/yr, the unit capital cost would be $0.16/1,000 gal.
During the 13-month demonstration study, the system produced 43,446,110 gal of water (Table 4-5),
corresponding to 38,211,600 gal/year, so the unit capital cost increased to $0.83/1,000 gal.
A38ftx 18ft building with a ceiling height of 14 ft was constructed by the Town of Felton to house the
treatment system (Section 4.3.2). In addition to the building, a recycle system was installed and included
al6ftx6ftx 10ft concrete recycle tank, recycle system controller, booster pumps, and associated
piping (Section 4.2). Not included in the capital cost, the total cost of the building, recycle system, and
supporting utilities was approximately $240,000.
4.6.2 O&M Cost. O&M costs included chemical use, electricity consumption, and labor for a
combined unit cost of $0.30/1,000 gal (Table 4-15). No cost was incurred for repairs because the system
was under warranty. Since chlorination already existed prior to the demonstration study, incremental
chemical cost for iron addition was $0.05/1,000 gal. Electrical power consumption was calculated based
on the difference between the average monthly cost from electric bills before and after building
construction and system startup. The difference in cost was approximately $150/month or $0.045/1,000
gal of water treated. The routine, non-demonstration related labor activities consumed approximately 45
min/day (Section 4.4.5.3). Based on this time commitment and a labor rate of $30/hr, the labor cost was
$0.21/1,000 gal of water treated.
Table 4-15. O&M Cost for Kinetico's C/F System
Category
Volume processed (1,000 gal)
Value
43,446
Remarks
From 09/14/06 through 11/03/07
Chemical Usage
37-42% FeCl3 unit cost ($/lb)
FeCl3 consumption (lb/1,000 gal)
Chemical cost ($/l,000 gal)
$0.99
0.049
$0.05
Supplied in 12 180-lb drums, including
cost for drum deposit and freight
-
-
Electricity Consumption
Electricity cost ($/month)
Electricity cost ($/l,000 gal)
$150.00
$0.045
Average incremental consumption
including building heating and lighting
-
Labor
Labor (hr/week)
Labor cost ($/l,000 gal)
Total O&M cost ($/l,000 gal)
5.25
$0.21
$0.30
45 min/day, 7 day/week
Labor rate = $30/hr
Including FeCl3 usage
50
-------
5.0 REFERENCES
Battelle. 2004. Quality Assurance Project Plan for Evaluation of Arsenic Removal Technology.
Prepared under Contract No. 68-C-00-185, Task Order No. 0029, for U.S. Environmental
Protection Agency, National Risk Management Research Laboratory, Cincinnati, OH.
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.
Clark, J.W., W. Viessman, and M.J. Hammer. 1977. Water Supply and Pollution Control. IEP, aDun-
Donnelley Publisher, New York, NY.
Edwards, M., S. Patel, L. McNeill, H. Chen, M. Frey, A.D. Eaton, R.C. Antweiler, and H.E. Taylor.
1998. "Considerations in As Analysis and Speciation." J. AWWA, 90(3): 103-113.
EPA. 2003. Minor Clarification of the National Primary Drinking Water Regulation for Arsenic.
Federal Register, 40 CFRPart 141.
EPA. 2002. Lead and Copper Monitoring and Reporting Guidance for Public Water Systems.
EPA/816/R-02/009. U.S. Environmental Protection Agency, Office of Water, Washington, D.C.
EPA. 2001. National Primary Drinking Water Regulations: Arsenic and Clarifications to Compliance
and New Source Contaminants Monitoring. Federal Register, 40 CFR Parts 9, 141, and 142.
Ghurye, G.L. and D.A. Clifford. 2001. Laboratory Study on the Oxidation of Arsenic III to Arsenic V.
EPA/600/R-01/021. U.S. Environmental Protection Agency, National Risk Management
Research Laboratory, Cincinnati, OH.
Kinetico. 2005. The Village ofPentwater, MI: Installation Manual; Suppliers Literature; and Operation
and Maintenance Manual, Macrolite FM-260-AS Arsenic Removal System. Newbury, OH.
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.
51
-------
APPENDIX A
OPERATIONAL DATA
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet
Start-up Date: October 12, 2006
Week
No.
1
2
3
4
5
6
7
Day of
Week
R
F
Sa
Su
M
T
W
Thur
F
Sa
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
Date
09/14/06
09/15/06
09/16/06
09/17/06
09/18/06
09/19/06
09/20/06
09/21/06
09/22/06
09/23/06
09/24/06
09/25/06
09/26/06
09/27/06
09/28/06
09/29/06
09/30/06
10/01/06
10/02/06
10/03/06
10/04/06
10/05/06
10/06/06
10/07/06
10/08/06
10/09/06
10/10/06'"
10/11/06
10/12/06'"
10/13/06
10/14/06
10/15/06
10/16/06
10/17/06
10/18/06
10/19/06
10/20/06
10/21/06
10/22/06
10/23/06
10/24/06
10/25/06
10/26/06
10/27/06
10/28/06
10/29/06
Time
8:00
8:00
5:30
10:10
8:20
7:45
7:45
8:20
9:00
16:20
20:12
7:15
8:00
8:00
7:55
7:10
6:30
7:00
7:55
8:10
5:15
7:40
8:00
12:35
20:00
16:25
7:45
8:00
8:00
8:45
16:00
12:55
15:00
13:50
10:05
10:10
12:05
11:00
11:45
11:50
12:00
9:45
8:00
9:15
12:20
19:45
Cumulative Hrsin Service
TA
hr
72.1
77.1
84.8
87.6
95.0
00.6
06.9
13.8
17.7
29.5
36.7
36.7
42.8
47.3
53.5
60.8
66.8
73.7
82.8
90.1
93.6
200.7
207.6
213.7
223.8
228.4
234.6
241.0
244.6
250.5
261.3
262.5
269.7
276.1
281.9
286.5
294.9
299.3
306.1
312.5
318.9
326.2
330.7
337.0
344.5
358.7
TB
hr
79.3
79.3
91.4
97.1
104.4
109.6
115.9
122.8
126.3
138.1
145.3
145.3
151.4
163.7
166.0
170.2
176.1
183.0
192.0
199.3
202.8
209.8
216.7
222.8
232.8
237.5
243.6
250.1
253.7
259.7
270.5
271.7
278.9
285.3
291.1
295.8
304.1
308.5
315.3
321.6
328.0
335.3
339.7
346.0
353.5
367.7
TC
hr
111
77.7
89.8
95.5
102.8
108.0
114.3
121.2
124.7
136.5
143.7
143.7
149.8
155.1
161.4
168.6
174.5
181.4
190.4
197.7
201.2
208.2
215.1
221.2
231.2
235.9
242.0
248.5
252.1
258.1
192.3
193.5
200.6
207.2
212.9
217.5
225.8
230.3
237.1
243.5
249.9
257.1
261.5
267.8
275.2
289.5
Avg Run
Time
hr
NA
1.7
10.6
4.7
7.3
5.3
6.3
6.9
3.6
11.8
7.2
0.0
6.1
7.4
4.9
6.2
5.9
6.9
9.0
7.3
3.5
7.0
6.9
6.1
10.0
4.7
6.1
6.5
3.6
6.0
10.8
1.2
7.2
6.5
5.8
4.6
8.3
4.4
6.8
6.4
6.4
7.3
4.4
6.3
7.5
14.2
Hour
Meter
hr
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Run
Time
hr
NA
1.7
10.6
4.7
7.3
5.3
6.3
6.9
3.6
11.8
7.2
0.0
6.1
7.4
4.9
6.2
5.9
6.9
9.0
7.3
3.5
7.0
6.9
6.1
10.0
4.7
6.1
6.5
3.6
6.0
10.8
1.2
7.2
6.5
5.8
4.6
8.3
4.4
6.8
6.4
6.4
7.3
4.4
6.3
7.5
14.2
Chlorine
Chlorine
Tank
Level
gal
36
32
27
24
19
15
12
23
21
12
25
25
21
18
14
9
25
19
13
8
6
35
30
25
17
14
10
6
36
33
26
25
21
18
14
11
8
37
33
29
25
21
19
15
28
20
Cl
dosage
mg/L
5.3
4.0
5.1
5.1
3.5
4.4
4.1
5.2
4.6
NA
5.0
4.1
4.7
5.2
NA
6.4
4.8
5.3
4.5
4.2
5.5
6.0
5.7
4.5
5.3
4.6
4.3
4.9
4.5
6.2
4.4
3.4
4.9
4.8
3.1
3.7
4.5
4.6
4.5
4.2
3.2
4.6
4.2
4.1
Totalizer to
Totalizer
kgal
24,022.8
24,105.1
24,215.2
24,302.9
24,417.5
24,509.2
24,609.8
24,715.8
24,773.5
24,975.0
25,076.3
25,076.3
25,170.7
25,256.5
25,357.3
25,469.0
25,559.5
25,669.4
25,817.0
25,927.5
25,979.8
26,092.1
26,199.1
26,296.6
26,462.0
26,540.0
26,628.1
26,729.0
26,810.0
26,882.1
27,066.0
27,085.0
27,191.4
27,293.5
27,388.3
27,461.5
27,573.2
27,668.5
27,772.7
27,874.6
27,978.0
28,090.2
28,162.4
28,263.6
28,375.8
28,607.4
Avg Flow
Rate
gpm
NA
NA
173
309
260
287
266
256
265
285
234
NA
258
194
341
299
254
265
272
252
249
266
258
266
275
279
239
260
375
201
284
264
247
263
274
263
223
358
255
267
269
257
271
268
250
271
Pressure Filtration
Influent
psg
81
82
85
80
86
63
66
68
NA
NA
NA
NA
NA
62
86
90
82
69
88
86
82
81
78
NA
81
81
67
67
86
83
85
82
85
78
79
82
78
78
83
77
78
84
78
80
83
87
Outlet TA
pag
72
71
69
74
71
57
59
60
NA
NA
NA
NA
NA
NA
72
70
71
65
73
67
71
70
73
NA
72
69
NA
NA
NA
71
70
70
68
71
71
71
72
70
71
72
70
72
72
70
70
71
Outlet TB
pag
71
70
68
70
67
56
58
59
NA
NA
NA
NA
NA
56
71
68
69
65
71
65
70
68
72
NA
71
68
NA
NA
NA
70
69
69
67
70
70
69
70
68
69
70
69
69
70
68
69
69
Outlet TC
pag
71
70
68
70
68
57
60
55
NA
NA
NA
NA
NA
NA
71
68
65
60
61
73
65
72
67
NA
71
68
NA
NA
NA
69
70
69
68
71
70
70
71
69
70
71
69
71
71
68
69
69
Effluent
pag
56
62
60
60
60
58
58
58
NA
NA
NA
NA
NA
55
62
61
58
56
60
59
59
56
55
NA
60
58
NA
NA
NA
57
59
57
55
57
57
56
55
54
57
56
57
55
57
56
55
59
Flow/Totalizer to
Flow
Rate
gpm
293
270
265
295
258
268
270
285
295
249
0.0
0.0
0.0
0.0
274
254
278
0.0
252
261
271
302
300
0.0
292
277
0.0
0.0
0.0
293
261
295
270
308
289
304
302
290
295
309
294
296
304
281
296
258
Totalizer
kgal
921.8
1,002.6
1,106.6
1,193.6
1,302.0
1,391.0
1,488.9
1,589.2
1,644.7
1,825.8
1,937.5
1,937.5
2,027.4
2,108.9
2,207.2
2,312.9
2,401.5
2,500.0
2,639.2
2,744.0
2,798.8
2,906.7
3,009.6
3,103.9
3,258.0
3,328.5
3,416.8
3,514.1
3,571.3
3,664.3
3,835.6
3,854.2
3,957.7
4,056.0
4,148.0
4,217.1
4,324.6
4,415.2
4,516.4
4,614.0
4,715.3
4,821.4
4,890.9
4,989.7
5,098.7
5,319.2
Avg Flow
Rate
gpm
NA
NA
163
306
246
278
259
242
255
256
259
NA
246
184
NA
283
249
238
257
239
261
256
249
257
256
252
240
251
265
260
264
258
241
253
266
249
215
341
248
256
264
243
261
261
244
258
:erric Chloride
Fed,
Tank
Level
gal
40
35
29
23
16
10
3
31
27
15
7
7
31
26
19
12
5
34
24
16
13
5
35
30
21
17
14
8
32
28
18
16
11
6
36
33
28
23
18
12
6
36
32
27
21
10
Fe
Dosage
mgIL
NA
1.8
1.6
2.0
1.8
2.0
2.1
2.0
2.1
1.8
2.4
NA
1.9
1.7
2.1
1.9
2.3
1.6
2.0
2.2
1.7
2.1
1.7
1.5
1.6
1.5
1.0
1.8
1.1
1.7
1.6
3.2
1.4
1.5
1.6
1.2
1.3
1.6
1.4
1.8
1.7
1.3
1.7
1.5
1.6
1.4
Backwash
Tank
A
No.
5
5
5
6
6
7
7
7
8
8
9
9
9
10
10
10
11
11
12
12
13
13
14
14
15
15
15
15
16
16
17
17
17
18
18
18
19
19
19
20
20
20
21
21
21
22
Tank
B
No.
5
5
5
6
6
7
7
7
8
8
9
9
9
10
10
10
11
11
12
12
13
13
14
14
15
15
15
15
16
16
17
17
17
18
18
18
19
19
19
20
20
20
21
21
21
22
Tank
C
No.
5
5
5
6
6
7
7
7
8
8
9
9
9
10
10
10
10
10
10
11
11
12
12
12
13
13
13
14
14
14
15
15
15
16
16
16
17
17
17
18
18
18
19
19
19
20
Total
kgal
10.1
10.1
10.1
12.8
12.8
16.6
16.6
16.6
18.7
18.7
21.2
21.2
21.2
23.0
23.0
23.0
24.1
24.1
25.4
26.0
27.2
27.2
28.9
28.9
30.6
30.6
30.6
31.2
32.3
32.3
34.1
34.1
34.1
36.0
36.0
36.0
38.2
38.2
38.2
40.7
40.7
40.7
43.0
43.0
43.0
45.0
Since Last BW
Run Time
Tank A
hr
0.0
5.1
12.2
2.8
10.2
0.6
6.9
13.8
0.0
11.8
6.4
6.4
11.7
0.1
6.3
13.6
5.9
12.9
5.5
12.8
0.0
7.1
0.0
6.1
3.2
7.8
14.0
20.4
3.6
9.6
10.4
11.6
18.8
1.5
7.3
11.9
1.2
5.7
12.5
0.0
6.4
13.7
0.0
6.3
13.8
9.8
TankB
hr
0.1
5.1
12.2
5.7
13.0
1.3
7.6
14.5
0.3
12.2
6.4
6.4
12.5
0.5
6.8
14.0
5.9
12.8
5.9
13.1
0.3
7.3
0.0
6.1
3.2
7.8
14.0
20.4
3.6
9.7
0.0
11.2
18.4
2.0
7.7
12.4
1.9
6.4
13.2
0.7
7.1
14.4
0.7
7.0
14.5
10.5
TankC
hr
0.0
5.1
12.1
5.7
13.0
1.0
7.2
14.1
0.0
11.9
6.4
6.4
12.5
0.8
7.1
14.4
20.6
27.6
37.1
3.2
7.1
0.0
6.9
13.0
3.5
8.1
14.3
6.5
10.1
16.2
9.6
10.8
17.9
1.3
7.0
11.6
1.5
6.0
12.8
0.3
6.7
13.9
0.3
6.6
14.0
10.1
Standby Time
Tank A
hr
NA
33.4
46.5
12.2
26.5
6.2
21.9
41.5
17.1
37.5
9.3
19.1
37.7
14.3
32.1
47.9
17.4
34.4
15.0
31.9
17.3
36.2
5.2
27.6
0.3
16.0
25.1
43.0
14.7
33.3
19.9
34.5
57.8
16.5
30.8
50.1
17.2
35.4
53.2
17.3
34.9
49.2
16.2
35.4
55.8
17.5
TankB
hr
NA
37.0
40.1
21.8
36.1
6.2
23.9
41.5
17.4
37.8
9.9
19.7
38.3
14.3
32.0
47.8
17.1
34.1
15.0
31.9
17.2
36.2
4.8
27.3
0.0
15.7
24.8
42.7
14.4
33.1
19.9
39.5
57.8
16.5
30.7
50.1
17.2
35.4
53.2
17.3
34.9
49.2
16.2
35.4
55.8
17.5
TankC
hr
NA
38.8
46.9
21.5
35.8
6.2
23.9
41.5
17.4
37.8
9.6
19.4
38.0
14.3
32.0
47.8
65.3
82.3
97.4
16.9
34.2
4.8
22.1
44.5
16.8
32.5
41.6
11.1
31.2
49.8
19.9
39.5
57.8
16.5
30.7
50.1
17.2
35.5
53.2
17.2
34.8
49.1
16.2
35.4
55.8
17.5
Actual Run Time
Between BW
Tank A
hr
12.2
15.2
17.7
12.6
16.1
13.7
16.5
16.3
14.0
13.0
20.4
10.0
23.7
19.1
18.9
18.2
21.3
TankB
hr
12.1
16.9
17.7
24.3
14.0
15.9
16.3
14.2
12.9
20.4
20.5
22.8
18.8
18.8
18.1
18.2
TankC
hr
12.1
17.2
17.6
12.7
17.C
14.1
19.5
14.3
17.2
23.2
18.4
18.£
18.C
18.2
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet (Continued)
Start-up Date: October 12, 2006
Week
No.
9
10
11
12
13
14
15
16
17
Day of
Week
T
W
F
Su
M
T
R
F
Sa
Su
T
W
R
F
Sa
M
T
R
F
Sa
Su
T
W
R
F
Sa
M
T
W
R
Sa
Su
T
W
R
Su
M
T
W
R
F
Sa
Su
M
T
R
F
Sa
Su
M
T
W
R
F
Sa
Su
Date
0/31/06
1/01/06
1/3/06(c)
1/05/06
1/06/06
1/07/06
1/09/06
1/10/06
1/11/06
1/12/06
1/14/06
1/15/06
1/16/06
1/17/06
1/18/06
1/20/06
1/21/06
1/23/06
1/24/06
1/25/06
1/26/06
1/28/06
1/29/06
1/30/06
2/01/06
2/02/06
2/04/06
2/05/06
2/06/06
2/07/06
2/09/06
2/10/06
2/12/06
2/13/06
2/14/06
2/15/06
2/17/06
2/18/06
2/19/06
2/20/06
2/21/06
2/22/06
2/23/06
2/24/06
2/25/06
2/26/06
2/28/06
2/29/06
2/30/06
2/31/06
1/01/07
1/02/07
1/03/07
/04/07(d)
1/05/07
/06/07(e)
1/07/07
Time
14:55
9:25
10:10
12:30
13:30
16:00
7:30
12:00
10:30
10:30
13:00
13:00
9:15
11:35
11:00
11:15
NM
17:00
17:00
12:00
14:10
13:45
10:25
8:10
13:50
10:40
14:15
11:25
8:00
13:30
NM
14:45
15:00
10:20
11:35
15:15
8:55
8:15
11:30
15:00
10:40
8:00
10:15
10:00
10:30
18:45
16:00
8:50
8:15
9:15
16:20
11:00
Cumulative Mrs in Service
hr
366.2
370.5
380.9
393.6
398.7
405.1
414.6
420.5
427.7
432.4
445.0
451.3
461.4
467.6
479.0
484.8
NM
503.8
509.0
514.1
524.8
531.6
535.8
540.6
546.3
557.8
564.7
570.8
575.2
589.6
NM
606.9
621.5
633.4
646.4
650.4
656.1
661.4
670.7
678.3
684.4
696.3
701.0
716.8
728.7
733.9
740.0
746.0
751.6
hr
371.8
379.0
387.5
402.1
407.2
413.6
422.9
428.8
436.0
440.7
453.3
459.4
469.5
475.7
487.0
492.8
NM
511.4
521.7
532.4
539.3
543.4
548.2
553.9
564.4
571.8
577.7
582.1
596.2
NM
612.1
621.5
633.0
646.0
649.1
654.8
660.6
669.4
676.4
683.0
692.6
697.2
712.6
725.0
730.2
736.3
742.5
747.9
hr
297.0
301.3
311.8
324.5
329.7
336.1
345.6
351.5
358.7
363.4
376.0
382.0
392.1
398.3
409.7
415.5
NM
434.2
444.6
455.3
462.1
466.3
471.1
476.8
488.1
495.0
501.2
505.7
519.8
NM
537.1
550.7
562.3
575.4
579.1
584.8
590.6
599.5
607.0
613.1
624.2
628.9
644.3
656.7
661.9
668.0
674.3
680.1
Avg Run
Time
hr
4.5
5.3
5.7
5.7
5.1
6.4
4.9
5.9
7.2
4.7
6.8
6.1
5.7
6.2
3.1
5.8
NA
12.0
5.2
6.8
6.8
4.2
4.8
5.7
3.9
7.1
6.1
4.4
8.2
NA
6.0
4.2
5.8
6.9
3.6
5.7
5.6
9.0
2.6
6.3
4.9
4.7
9.2
3.8
5.2
6.1
6.3
5.6
Hour
Meter
hr
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
Run
Time
hr
4.5
5.3
5.7
5.7
5.1
6.4
4.9
5.9
7.2
4.7
6.8
6.1
5.7
6.2
3.1
5.8
NA
12.0
5.2
6.8
6.8
4.2
4.8
5.7
3.9
7.1
6.1
4.4
8.2
NA
6.0
4.2
5.8
6.1
6.9
3.6
5.7
5.6
9.0
2.6
6.3
4.9
4.7
6.3
9.2
3.8
5.2
6.1
6.3
5.6
Chlorine
Chlorine
Tank
gal
16
30
25
18
16
12
8
38
35
32
25
16
13
8
5
NM
27
21
16
12
10
7
38
33
29
25
2
1
NM
36
26
23
20
18
14
11
40
34
30
22
20
17
7
4
34
31
28
Cl
mg/L
4.4
5.1
2.4
3.7
2.8
4.7
3.0
6.1
3.2
4.6
3.3
3.9
3.6
2 3
3.8
NA
4.3
4.2
3.3
4.5
3.2
4.2
2.6
3.5
4.3
4.8
3.3
3.6
NA
3.6
4.5
5.2
3.8
3.4
3.3
3.9
5.2
3.7
3.4
5.1
4.8
5.9
3.1
3.6
4.0
4.1
3.6
3.5
3.8
Totalizer to
Totalizer
kgal
28,720.2
28,789.4
28,958.2
29,158.0
29,241.2
29,341.4
29,491.0
29,587.9
29,699.2
29,776.4
29,975.7
30,150.6
30,241.7
30,338.3
30 522 3
30,614.5
NM
30,911.1
31,078.7
31,248.7
31,353.0
31,425.3
31,508.8
31,600.2
31,777.8
31,886.0
31,984.4
32,056.4
32,282.0
NM
32,551.6
32,629.0
32,774.0
32,959.0
33,061.0
33,167.2
33,226.9
33,317.2
33,411.1
33,549.0
33,672.6
33,770.4
33,953.5
34,029.1
34,127.0
34,275.0
34,468.6
34,553.6
34,652.5
34,753.3
34,845.3
Avg Flow
Rate
gpm
291
219
293
280
270
261
271
274
258
274
259
285
266
260
268
265
NA
265
273
262
254
289
290
267
285
255
270
271
268
NA
270
346
267
267
277
257
276
264
278
255
291
260
274
270
259
267
283
260
259
272
270
269
274
Pressure Filtration
psig
77
77
80
80
81
81
76
84
85
78
85
81
84
80
88
80
81
NM
84
77
79
86
85
86
79
87
77
81
78
79
82
NM
79
79
79
84
79
84
85
87
79
84
89
79
80
79
80
90
84
79
84
83
79
79
84
78
psig
72
70
70
71
70
70
70
69
71
72
68
72
71
69
71
70
71
NM
72
72
72
68
71
72
71
69
69
69
73
70
71
NM
73
70
69
69
71
69
71
68
71
69
69
72
70
72
69
69
65
71
73
71
70
69
73
70
psig
71
69
68
70
68
68
68
67
68
71
67
70
69
68
67
68
69
NM
70
71
70
68
69
70
70
67
68
68
72
69
70
NM
73
72
69
69
70
67
68
66
71
68
67
70
68
71
68
67
71
67
69
67
70
69
64
71
psig
71
70
68
70
68
68
69
68
71
71
67
71
70
68
69
68
69
NM
70
71
70
67
70
71
71
68
69
69
72
69
70
NM
69
73
69
69
71
67
69
67
70
68
66
71
69
72
68
68
72
68
70
68
71
69
72
69
psig
57
57
55
58
57
57
55
57
57
56
55
58
57
56
57
57
57
NM
56
56
57
56
56
57
56
57
56
56
57
55
58
NM
57
57
56
56
56
56
56
56
57
57
56
56
57
56
57
58
55
57
55
56
55
56
56
Flow/Totalizer to
Flow
Rate
gpm
312
295
290
295
280
282
298
266
295
310
267
285
287
280
280
305
NM
301
312
295
266
295
304
306
260
293
285
310
298
295
NM
306
302
285
290
309
275
295
265
300
270
307
285
310
290
255
265
296
282
287
278
292
Totalizer
kgal
5,427.1
5,495.4
5,655.6
5,849.4
5,928.0
6,022.8
6,167.6
6,260.8
6,366.2
6,440.7
6,632.8
6,800.3
6,887.1
6,978.5
7,158.4
7,245.4
NM
7,530.0
7,609.9
7,692.8
7,854.4
7,953.2
8,025.0
8,107.7
8,194.5
8,366.0
8,468.8
8,562.7
8,634.1
8,854.1
NM
9,109.5
9,186.3
9,260.9
9,324.2
9,506.4
9,600.3
9,705.8
9,758.2
9,844.5
9,936.3
0,186.8
0,280.1
0,456.2
0,530.2
0,623.7
0,766.6
0,895.3
0,951.2
1,129.2
1,221.4
1,311.6
Avg Flow
Rate
gpm
291
216
280
278
255
247
268
263
244
264
247
274
254
246
260
250
NA
254
258
250
241
287
287
254
282
243
258
268
264
NA
265
343
270
252
270
255
255
243
252
272
289
248
284
264
247
258
246
248
264
246
:erric Chloride
FeCI3
Tank
gal
5
36
28
16
11
5
31
25
19
15
4
30
25
19
8
4
NM
28
24
18
8
3
34
29
24
13
6
37
32
19
NM
4
14
9
5
30
25
18
15
10
4
24
18
7
3
34
26
18
14
3
33
Fe
Dosage
mg/L
.1
.7
.5
.9
.8
.8
.5
.9
.6
.6
.4
.6
.6
.9
.8
.3
NA
.4
.1
.0
.4
.7
.8
.6
.8
.9
.5
.1
.8
NA
.8
.5
.9
.8
.5
.7
.9
.0
.8
.9
.6
.2
.8
.8
.5
Backwash
Tank
No.
23
23
23
24
24
24
25
25
25
26
26
27
27
27
28
28
NM
30
30
30
30
31
32
32
33
33
34
34
35
NM
36
36
36
36
37
38
38
39
39
40
40
40
42
43
Tank
No.
23
23
24
24
24
25
25
25
26
26
27
27
27
28
28
NM
30
30
30
30
31
32
32
33
33
34
34
35
NM
36
36
36
36
37
37
37
38
38
39
39
40
40
40
42
42
Tank
No.
21
21
21
22
22
22
23
23
23
24
24
25
25
25
26
26
NM
28
28
28
28
29
30
30
31
31
32
32
33
NM
35
36
36
36
37
37
38
38
39
39
40
40
40
41
42
43
kcfal
—
4 .
4 .
9.
. 9.
9.
1.
1.
1.
53.
53.5
56.3
56.3
56.3
58.3
58.3
NM
62.2
62.2
62.2
62.2
64.4
66.2
66.2
68.2
68.2
71.0
71.0
73.1
NM
5.5
6.1
6.1
6.1
8.0
8.0
80.0
80.0
82.4
82.4
84.8
84.8
84.8
86.2
89.0
89.8
Since Last BW
F
hr
0.0
4.2
14.7
2.8
7.9
14.3
0.7
6.6
13.8
0.5
13.1
4.6
10.3
16.5
5.8
11.6
NM
0.0
5.1
15.8
22.6
2.8
3.4
9.1
4.1
11.0
0.3
4.7
3.3
NM
0.0
5.6
10.4
14.6
2.2
8.3
19.2
0.7
6.5
2.8
8.9
0.9
5.6
7.8
0.0
un Tim
hr
0.0
4.2
14.7
3.1
8.2
14.6
1.4
7.3
14.5
1.2
13.8
5.3
11.0
17.2
6.5
12.3
NM
0.6
5.8
16.5
23.4
3.5
2.8
8.5
4.1
11.0
1.0
5.4
3.6
NM
0.0
0.4
9.4
2.9
9.0
15.9
19.0
0.4
6.2
3.5
9.6
1.6
6.2
3.9
6.9
13.1
hr
0.0
4.2
14.8
3.5
8.7
15.1
1.0
6.9
14.1
0.8
13.4
4.9
10.3
16.5
6.2
12.0
NM
0.3
5.5
16.2
23.0
3.2
2.0
7.7
4.0
10.9
0.7
5.2
3.2
NM
6.5
0.0
4.2
8.4
2.3
8.4
15.3
19.0
1.1
6.9
3.1
9.2
1.2
5.9
12.2
3.5
6.3
0.0
St
hr
16.2
30.4
68.3
18.3
37.3
58.0
14.8
34.8
52.7
18.7
55.8
33.6
51.1
70.1
36.0
55.0
NM
18.3
32.1
69.5
87.9
16.1
16.3
37.5
35.2
55.9
14.6
30.6
18.1
NM
9.7
35.0
53.3
68.7
18.6
32.9
56.9
69.6
17.0
37.4
58.1
30.8
50.8
15.3
35.6
56.0
75.1
36.6
20.8
ndbyTi
hr
16.8
31.0
68.4
18.3
37.3
58.0
14.8
34.8
52.7
18.7
55.7
33.6
51.1
70.2
36.0
54.9
NM
18.3
32.0
69.3
87.7
16.1
16.4
39.4
35.9
56.6
14.6
30.6
18.3
NM
10.0
23.8
42.1
57.3
18.6
32.9
56.9
69.6
17.0
37.4
58.1
30.8
50.7
15.3
35.6
56.0
19.2
36.6
57.3
ne
hr
16.5
30.7
68.6
18.3
37.4
58.1
14.8
34.8
52.7
18.7
55.8
15.3
34.0
51.5
70.5
36.0
54.9
NM
18.3
32.0
69.3
87.7
16.1
16.3
37.6
35.5
56.2
14.6
30.6
18.4
NM
15.9
18.5
36.8
52.2
19.0
33.3
57.3
70.0
17.0
37.3
58.0
30.9
50.8
15.3
35.6
56.0
19.2
39.6
55.7
36.6
20.5
Actual Run Time
Between BW
hr
—
— f^
18.0
19.2
22.2
18.6
24.0
4.2
16.5
16. E
24.2
20.1
22.1
753.8
hr
—
_^J
18.0
19.0
22.0
18.6
24.0
5.5
15.4
15.9
24.3
19.0
17.7
20.7
17.0
hr
—
_2±Q
18. C
19.2
21.7
18.7
16. S
24. C
6.C
15. C
16.4
11.7
23.6
20.2
17.8
20.S
12.6
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet (Continued)
Start-up Date: October 12, 2006
Week
18
19
20
21
22
23
24
25
Day of
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
M
W
R
F
Sa
M
T
W
R
F
Su
M
T
R
F
Sa
Su
M
W
R
F
Sa
Su
M
T
W
R
F
Sa
M
T
W
F
Sa
M
T
W
F
Sa
Su
01/09/07
01/10/07
01/11/07
01/12/07
01/13/07
01/14/07
01/15/07
01/16/07
01/17/07(f)
01/18/07
01/19/07
01/20/07
01/21/07
01/22/07
01/24/07
01/25/07
01/26/07
01/27/07
01/29/07
01/30/07
01/31/07
02/01/07
02/02/07
02/04/07
02/05/07
02/06/07
02/08/07
02/09/07
02/10/07
02/11/07
02/12/07
02/14/07
02/15/07
02/16/07
02/17/07
02/18/07
02/19/07
02/20/07
02/21/07
02/22/07
02/23/07
02/24/07
02/26/07
02/27/07
02/28/07
03/02/07
03/03/07
03/05/07
03/06/07
03/07/07
03/09/07(9)
03/10/07
03/11/07
15:00
11:20
10:00
13:15
16:30
18:10
16:50
:00
45
00
30
40
:00
30
40
40
i :40
:15
:35
:40
40
45
:30
:50
:15
:00
:10
:00
:30
:30
:00
45
30
:00
00
:20
00
i :15
00
:00
:00
30
30
40
:40
:40
:00
:50
30
:40
Cumulative Mrs in Service
TA
763.4
769.4
774.5
781.2
787.4
794.7
799.8
805.0
809.5
813.3
818.6
824.4
830.6
838.4
846.8
851.9
857.7
863.5
882.0
887.4
892.7
898.1
912.0
922.1
933.5
939.5
946.1
952.8
959.6
970.3
975.1
981.0
993.6
998.2
,004.8
,011.1
,015.9
,022.0
,028.4
,041.0
,063.9
,077.0
,086.1
,091.6
,104.1
,115.2
,125.8
,131.4
,138.2
TB
759.1
764.9
770.0
776.4
782.6
789.6
791.6
799.8
804.3
808.1
813.3
818.7
824.9
829.1
841.1
845.9
851.8
857.5
875.4
880.8
886.0
905.0
914.8
926.2
932.2
938.3
945.0
951.7
962.3
966.7
972.7
984.9
989.5
996.1
,002.0
,006.7
,012.9
,019.4
,031.7
,054.6
,067.4
,076.2
,082.1
,093.9
, 05.0
, 15.6
, 21.1
, 27.6
TC
690.7
696.6
698.9
705.1
711.9
719.0
724.0
729.2
737.5
742.8
748.2
754.5
758.7
770.8
781.8
787.5
805.4
810.6
815.8
835.1
845.3
856.5
862.5
868.8
875.8
882.5
893.2
897.6
903.2
915.9
920.5
927.1
937.8
943.9
950.0
962.6
985.5
998.3
,007.1
,012.6
,024.8
,035.6
,046.0
,051.2
Avg Run
Time
6.0
5.9
4.2
6.4
6.4
7.1
4.0
6.2
3.8
5.3
5.5
6.2
5.4
6.6
4.9
6.0
5.7
5.1
5.3
5.2
8.6
5.6
5.8
6.0
6.3
6.8
6.0
4.5
5.8
7.1
4.6
6.6
4.8
6.1
6.3
5.9
22.9
12.9
5.7
5.6
12.2
5.4
6.4
5.4
Hour
Meter
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
4.4
11.6
Run
Time
6.0
5.9
4.2
6.4
6.4
7.1
4.0
6.2
3.8
5.3
5.5
6.2
5.4
6.6
4.9
6.0
5.7
5.1
5.3
5.2
8.6
5.6
5.8
6.0
6.3
6.8
6.0
4.5
5.8
7.1
4.6
6.6
4.8
6.1
6.3
5.9
22.9
12.9
5.7
5.6
12.2
5.4
4.4
7.2
6.0
Chlorine
Chlorine
Tank
Level
21
18
15
12
25
20
17
14
10
8
38
35
33
26
23
20
34
24
21
18
9
36
30
27
23
19
11
9
22
15
13
10
37
34
30
24
12
38
34
30
24
18
13
11
Cl
4.7
3.5
4.5
3.4
3.6
5.1
4.5
4.0
3.7
2.6
3.8
3.5
3.1
3.1
3.6
3.6
4.1
4.0
3.9
3.3
3.8
3.6
3.5
4.7
4.0
3.6
3.1
3.5
4.1
3.0
3.3
2.9
3.5
4.4
3.5
3.8
2.2
2.5
5.1
3.5
3.8
3.5
2.5
Totalizer to
Totalizer
35,027.1
35,126.8
35,204.4
35,306.7
35,404.5
35,520.0
35,598.6
35,685.6
35,824.7
36,006.3
36,106.6
36,181.5
36,378.2
36,459.8
36,558.4
36,655.2
36,955.6
37,042.7
37,132.4
37,455.0
7,619.5
7,813.3
7,913.6
38,012.5
38,128.4
38,415.1
38,491.6
38,591.9
38,796.5
38,874.0
38,980.1
39,161.1
39,263.0
39,369.0
39,576.4
39,948.0
40,158.2
40,310.7
40,403.2
40,605.5
40,790.5
40,962.7
41,055.7
Avg Flow
Rate
276
282
310
265
255
270
325
234
278
277
268
231
281
278
275
281
278
272
286
273
275
282
279
260
284
275
269
281
287
271
281
268
285
277
279
280
270
272
276
274
277
286
383
215
Pressure Filtration
Influent
psig
86
79
81
79
80
81
81
81
82
79
80
79
81
81
81
84
8
8
8
82
80
80
78
80
80
78
82
79
81
81
84
80
82
80
78
83
80
84
77
78
81
80
81
80
81
85
83
79
Outlet TA
psig
67
70
70
73
71
65
69
70
70
70
69
71
71
66
71
72
70
72
70
71
67
72
68
69
73
69
70
73
72
69
71
72
70
71
70
68
69
69
69
69
69
71
70
71
68
72
67
69
70
Outlet TB
psig
67
70
70
67
66
70
69
69
70
66
72
69
70
67
69
69
69
70
71
68
69
72
71
70
68
67
68
70
68
69
71
68
66
71
70
69
70
71
69
68
69
62
70
71
72
70
67
66
70
Outlet TC
psig
67
70
70
67
66
70
69
69
71
68
69
72
70
71
70
65
66
70
71
68
70
72
69
68
69
71
69
68
66
67
70
72
69
67
69
70
70
66
69
67
61
69
70
68
69
66
74
67
73
69
Effluent
psig
55
56
56
55
55
56
55
57
57
56
57
56
56
56
56
56
56
56
55
55
56
56
57
56
55
56
56
56
54
57
56
56
56
56
57
56
56
56
55
56
55
51
56
56
56
56
56
56
56
56
56
Flow/Totalizer to
Flow
Rate
gpm
270
295
282
305
287
275
285
273
306
280
306
290
305
276
278
276
270
290
303
291
305
308
290
308
287
287
295
288
290
276
290
295
297
290
273
287
290
288
280
280
290
275
280
302
293
285
273
295
287
290
290
Totalizer
kgal
1,484.5
1,580.3
1,652.6
1,749.4
1,844.1
1,956.7
2,030.4
2,114.6
2,186.0
2,335.1
2,422.5
2,518.9
2,780.4
2,859.0
2,954.0
3,047.1
3,256.2
3,335.5
3,420.5
3,507.2
3,595.9
3,815.6
3,884.8
3,974.3
4,159.3
4,255.3
4,355.7
4,463.1
4,569.9
4,739.1
4,813.1
4,908.5
5,106.8
5,181.8
5,282.7
5,378.4
5,456.5
5,556.1
5,658.6
5,858.8
6,212.4
6,415.6
6,564.2
6,653.7
6,850.4
7,029.7
7,195.8
7,286.9
7,397.5
Avg Flow
Rate
gpm
265
271
289
251
247
263
305
226
264
276
263
258
272
267
265
271
NA
259
266
276
272
265
262
265
273
267
264
263
264
259
272
272
260
272
255
264
273
271
270
271
257
263
271
265
269
277
254
279
275
:erric Chloride
FeCI3
Tank
Level
gal
17
11
6
36
30
24
20
14
8
30
24
16
31
25
18
32
17
10
4
34
27
10
5
34
19
12
31
24
4
39
25
19
10
3
44
36
29
14
1
35
24
17
31
17
3
31
23
Fe
Dosage
1.8
1.8
1.9
1.2
1.8
1.6
1.5
2.0
2.0
2.4
2.2
2.1
2.2
2.3
2.5
2.1
2.0
2.3
2.3
2.1
1.9
2.1
2.1
2.3
2.5
2.3
2.1
2.3
2.5
1.8
2.4
2.0
2.1
1.0
1.7
2.2
2.3
2.3
2.4
2.3
2.1
Backwash
Tank
43
44
44
45
45
45
45
48
48
50
51
52
53
54
54
55
56
57
58
58
60
61
62
64
64
66
67
67
67
68
69
70
71
72
73
75
76
79
80
81
82
Tank
43
44
44
45
45
46
46
50
53
54
55
57
58
58
59
60
62
63
64
66
67
69
71
72
75
76
76
77
78
79
80
82
83
85
88
88
93
94
96
98
Tank
43
44
44
44
44
45
45
49
50
52
52
53
55
56
56
57
58
60
60
61
63
64
65
67
68
70
71
1
3
4
6
7
8
80
83
84
86
89
90
92
93
90.
91.
92.
92.
93.
93.
98.5
99.8
02.0
02.9
04.2
06.5
07.8
07.8
09.
0.
2.
3.
4.
16.
18.0
19.8
22.5
23.3
26.4
27.7
27.7
28.6
29.9
31.2
33.0
34.7
36.0
38.2
41.7
42.6
45.1
48.2
49.5
51.7
53.5
Since Last BW
10.1
0.0
6.2
13.5
18.6
7.2
1.6
8.5
2.8
0.7
3.1
0.1
5.4
2.2
0.8
8.8
1.7
7.5
3.8
0.0
3.4
6.1
8.0
1.4
8.0
2.3
2.6
2.2
13.7
5.3
1.3
0.1
2.2
8.1
3.9
3.9
13.3
9.0
0.0
6.2
2.9
7.9
0.3
1.3
1.7
2.5
1.0
2.8
0.3
5.7
2.7
1.4
1.6
1.4
3.3
3.2
1.6
2.1
1.6
6.1
1.2
3.8
0.2
6.8
2.6
0.4
3.7
1.3
16.2
4.1
0.0
5.9
3.2
7.3
2.9
2.2
16.4
6.9
13.7
19.9
3.2
8.2
0.0
1.4
7.6
4.2
2.5
0.1
5.3
2.4
1.1
1.6
6.2
3.6
2.6
0.8
0.0
7.0
2.5
7.3
2.6
9.2
3.6
1.1
0.0
3.1
18.2
4.7
0.8
0.9
3.0
0.0
6.5
0.3
3.1
St
70.5
32.1
15.5
41.3
59.9
77
37.9
35.1
19.0
18.8
15
17.6
35.3
17.2
18.3
16.4
NA
18.5
15.6
33.7
17.6
16.8
17.3
35.3
35.9
18.9
35.2
53.9
17.6
20.3
12.9
0.0
13.1
18.5
17.2
18.8
15.8
35.4
18.4
16.7
ndbyTi
55.7
32.0
15.7
41.6
18.6
35.7
14.8
19.4
18.5
19.0
18.8
15
17.9
35.6
17.2
18.3
16.4
NA
18.5
15.6
18.1
17.6
16.8
34.6
18.0
17.1
18.8
35.1
18.7
20.3
12.9
0.0
13.1
18.5
17.2
18.8
15.6
35.5
18.3
16.7
76.2
31.7
47.4
73.1
18.6
35.7
14.8
19.3
18.5
37.6
18.8
15
17.9
35.6
17.1
18.3
35.9
NA
18.5
15.6
18.1
35.7
16.8
34.6
18.0
35.5
18.8
35.1
18.7
17.6
20.3
12.9
0.0
13.1
8.5
7.2
8.8
5.4
5.5
8.4
6.8
Actu
Be
18.4
16.8
19.8
19.6
11.5
7.9
8.3
8.5
6.8
5.9
7.8
9.8
9.9
10.1
8.8
11.2
16.8
6.3
11.4
6.7
7.9
7.8
5.8
4.7
9.8
6.8
7.0
al Run 1
tween E
15.2
15.4
10.3
12.4
9.4
7.1
5.1
7.2
4.7
7.5
8.2
6.7
6.2
3.9
4.2
7.6
5.8
7.5
6.4
6.4
9.3
8.8
4.0
6.6
8.2
10.1
6.9
6.3
6.1
8.0
5.3
4.6
6.5
5.7
tw
17.7
23.8
10.0
7.7
9.5
7.2
9.1
7.6
7.4
8.1
6.8
6.2
8.1
4.0
7.8
7.1
9.2
7.2
9.9
6.7
6.8
9.3
11.5
7.8
5.4
5.3
3.S
4.0
5.5
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet (Continued)
Week
27
29
31
32
Day of
M
T
W
R
Su
M
T
W
F
Sa
Su
M
T
W
R
F
Sa
M
T
W
F
Sa
Su
M
T
W
R
F
Sa
Su
T
W
R
F
Sa
Su
M
T
W
F
Sa
Su
03/13/07
03/14/07
03/15/07
03/16/07
03/18/07
03/19/07
03/20/07
03/21/07
03/23/07
03/24/07
03/25/07
03/26/07
03/27/07
03/28/07
03/29/07
03/30/07
03/31/07
04/02/07
04/03/07
04/04/07
04/06/07
04/07/07
04/08/07
04/09/07
04/10/07
04/11/07
04/12/07
04/13/07
04/14/07
04/15/07
04/17/07
04/18/07
04/19/07
04/20/07
04/21/07
04/22/07
04/23/07
04/24/07
04/25/07
04/27/07
04/28/07
04/29/07
9:30
9:00
8:20
9:15
13:00
11:00
9:15
8:20
10:10
10:10
8:00
8:00
8:00
8:00
8:00
10:00
<:30
<:00
1 :00
1 :30
1 :30
1 :00
1 :00
1 :30
<:45
1 :30
- :00
1 :55
1 :15
8:30
8:30
8:00
8:15
8:10
15:00
8:40
8:30
7:40
8:00
8:00
8:20
Cumulative Mrs in Service
TA
, 49.4
, 60.8
, 66.8
, 80.1
, 85.8
, 96.2
,206.9
,219.7
,225.4
789.7
,236.5
,242.1
,248.9
,254.3
,266.4
,275.2
,279.6
,292.7
,296.5
,301.9
,307.1
, 16.1
, 20.3
, 25.4
,335.9
,34 .0
,35 .5
,35 .8
,36 .6
,36! .3
,380.8
,382.1
,388.5
,394.4
,405.8
,411.7
TB
,138.7
,149.8
,155.9
,168.7
,174.4
,184.2
,195.1
,207.6
,213.0
,218.2
,223.7
,229.3
,236.1
,241.1
,252.3
,258.E
,266.2
,279.1
,282.8
,287.6
,292.7
,296.3
,301.1
,304.9
,309.7
,319.2
,328.7
,334.7
,339.9
,345.C
,350.4
,360.9
,361.9
,367.6
,373.5
,383.8
,389.5
TC
,068.8
,080.3
,086.3
,098.8
, 04.5
, 14.5
, 25.4
, 37.9
, 43.3
, 48.5
, 54.0
, 59.6
, 66.1
, 71.6
, 83.0
, 89.5
, 95.9
, 09.8
, 12.3
, 18.7
,223.8
,227.4
,232.6
,236.8
,242.2
,252.7
,262.4
,268.5
,274.1
,279.5
,285.5
,296.9
,298.1
,304.5
,310.4
,321.5
,327.5
Avg Run
Time
5.5
6.3
6.6
5.7
5.0
5.4
5.4
5.5
-141.8
152.6
5.6
6.7
5.3
6.3
7.3
6.1
7.9
3.3
5.5
5.1
5.0
4.1
5.1
5.8
5.1
6.2
5.4
5.4
5.7
11.1
6.2
5.9
4.7
5.9
Hour
Meter
23.6
35.8
42.3
56.0
62.1
73.3
85.0
98.6
104.8
110.4
116.6
122.6
129.8
135.6
148.6
156.1
163.0
177.0
180.8
186.7
192.3
196.6
202.2
206.8
212.7
224.1
235.0
241.5
247.5
253.8
260.3
272.8
281.3
287.9
300.0
306.8
Run
6.0
6.6
6.5
7.0
6.1
5.6
5.8
6.0
6.2
5.6
6.2
6.0
7.2
5.8
—
7
6
7
3
5
5
5.
4
6
5
6
6
6
12
7
6
5.3
6.8
Chlorine
Chlorine
Tank
Level
5
35
29
26
17
14
11
9
18
11
8
6
3
32
28
26
21
19
17
28
26
24
22
16
13
18
12
9
39
37
34
27
27
24
20
13
43
Cl
dosage
4.9
3.3
3.5
4.3
3.7
4.1
2.7
3.9
3.8
3.6
2.8
3.6
3.7
4.2
2.6
3.3
2.0
2.2
2.8
3.9
2.6
2.7
4.1
4.9
3.9
4.7
4.1
3.5
3.7
2.4
3.5
9.1
3.3
4.7
4.4
3.4
Totalizer to
Totalizer
,259.0
,354.7
. ,440.7
,545.9
,646.1
,860.3
,954.7
,041.4
,127.1
2,309.5
2,521.9
2,619.5
2,704.4
2,800.8
. 2,895.2
3,008.1
3,099.0
. 3,298.8
43,415.6
43,522.4
43,740.8
43,800.2
43,890.3
43,977.0
44,043.1
44,129.3
44,200.7
44,291.7
44,470.2
44,639.6
44,739.8
44,833.8
44,929.6
. 5,028.9
5,222.5
5,243.1
5,351.0
5,451.8
5,637.1
5,740.9
5,847.8
Avg Flow
Rate
NA
266
256
266
257
261
258
258
255
261
258
262
253
259
262
261
261
255
260
258
262
261
255
258
256
257
259
257
261
261
262
257
261
253
255
258
245
253
255
254
254
244
Pressure Filtration
Influent
82
80
79
82
84
82
79
84
80
82
81
80
78
82
81
81
81
83
82
80
78
80
81
81
81
81
81
81
82
80
80
80
81
83
80
83
79
84
79
81
83
82
81
Outlet TA
72
72
71
73
76
68
72
69
69
74
74
69
72
69
71
73
70
68
70
70
71
70
68
69
67
71
71
75
73
72
68
65
72
70
75
71
69
69
74
67
70
71
Outlet TB
71
68
72
70
67
67
69
67
72
69
69
71
71
71
70
65
68
71
72
68
70
68
74
70
70
69
69
68
66
71
69
71
66
70
67
73
69
72
69
69
70
70
Outlet TC
67
73
68
66
66
70
72
74
69
67
68
70
66
68
64
74
66
68
69
70
70
74
70
68
70
72
71
67
74
70
68
74
68
72
58
73
69
70
67
69
69
74
Effluent
56
56
55
56
56
56
56
56
56
55
56
56
55
55
56
56
56
55
56
55
57
56
56
56
56
56
56
56
55
56
56
56
55
56
56
56
55
55
55
55
55
56
Flow/Totalizer to
Flow
Rate
296
305
292
290
275
308
283
304
295
300
304
295
295
273
295
277
293
297
294
290
304
302
283
290
302
297
293
300
307
285
302
280
305
295
305
295
305
295
290
300
300
Totalizer
17,487.6
17,577.8
7,763.0
7,859.7
8,066.9
8,157.6
8,242.5
8,327.1
8,505.0
8,619.8
8,805.4
8,889.6
8,984.7
9,076.1
9,185.5
9,273.6
9,470.6
9,585.4
9,690.1
9,894.4
9,950.4
20,039.9
20,125.0
20,189.2
20,274.9
20,345.5
20,435.8
20,513.1
20,611.8
20,779.6
20,967.5
21,062.2
21,160.7
21,357.5
21,373.8
21,481.0
2 ,581.2
2 ,765.9
2 ,869.3
2 ,975.4
Avg Flow
Rate
273
269
267
267
265
277
278
266
287
-10
10
272
272
277
282
263
288
259
280
270
276
284
289
295
293
285
282
288
290
288
295
233
290
283
285
294
284
:erric Chloride
FeCI3
Tank
Level
8
31
24
7
9
38
17
8
35
28
20
13
3
38
22
13
5
31
26
18
11
27
21
14
7
29
15
36
29
21
8
39
31
24
8
35
27
Fe
Dosage
2.2
2.3
2.1
2.2
2.5
2.1
2.3
2.1
2.5
2.5
2.2
2.7
2.3
2.5
2.3
2.2
2.4
2.5
2.7
2.4
2.4
2.5
2.3
2.7
2.1
2.4
1.3
2.2
2.4
2.0
1.5
2.2
2.1
2.6
2.3
2.2
Backwash
Tank
A
84
86
87
88
89
90
94
96
97
98
99
00
01
03
05
06
09
09
10
11
13
14
16
17
18
20
22
23
25
28
28
30
32
34
36
39
Tank
B
100
103
104
106
109
114
118
119
121
122
123
125
12S
132
133
134
134
137
138
142
144
147
149
152
156
159
162
165
172
172
176
178
183
186
190
Tank
C
96
99
03
12
13
15
16
18
19
23
26
27
28
29
30
31
34
35
36
38
39
42
44
46
47
51
51
53
55
58
60
64
Total
156.5
160.9
166.2
176.9
178.2
180.5
181.8
183.6
185.3
189.8
193.3
194.7
196.8
197.2
199.5
200.8
204.8
206.
209.
2 1.
2 3.
2 7.
2 8,
223.
225. i
232.
232.
235.
238.
242.7
245.8
250.9
Since Last BW
1.7
0.0
1.3
1.0
1.6
2.7
1.E
1.5
0.8
3.2
1.3
2.7
7.5
11.3
2.8
1.6
1.9
0.1
0.3
1.3
3.7
9.2
1.5
0.2
0.6
1.6
0.6
0.1
2.9
,un Tim
2.9
3.8
0.9
0.3
1.3
1.1
1.4
3.4
0.4
1.0
0.4
2.4
7.0
10.7
0.1
1.3
1.5
0.4
0.7
1.0
2.2
0.7
0.8
0.9
0.1
1.0
0.1
1.4
0.0
4.7
1.8
0.6
2.0
1.9
2.3
0.1
1.3
1.6
0.9
2.0
6.5
0.0
2.0
1.0
1.2
2.9
0.1
1.7
2.6
0.1
0.4
2.3
0.3
1.3
0.3
2.0
2.1
St
9.0
8.1
7.2
5.7
7.9
7.4
7.4
8.2
8.0
6.9
5.7
5.2
2.9
3.4
6.1
7.6
7.4
8.0
9.9
6.8
7.5
6.0
8.5
7.3
0.0
6.2
6.8
6.3
8.6
ndbyTi
9.0
8.1
0.4
7.2
5.7
7.8
7.4
7.4
8.2
8.0
6.9
5.7
5.2
2.9
3.4
6.1
7.6
7.4
8.0
9.9
6.9
7.5
8.5
8.5
7.4
0.0
6.2
6.8
6.3
8.6
18.9
18.1
20.4
17.2
15.7
17.8
17.5
17.5
18.2
18.0
16. S
15.7
15.2
12.8
20.5
16.1
17.6
17.4
18. C
19.8
16.8
17.5
18.5
18.5
17.4
0.0
16.1
16.9
16.3
18.6
Actu
Be
6.2
6.4
11.6
4.5
-436.3
445.7
6.5
7.1
6.1
4.8
—
3.0
13.9
4.0
5.9
3.9
4.4
4.9
4.1
3.5
al Run 1
tween E
5.3
8.9
5.3
4.8
5.4
tw
4.0
3.8
5.6
10.4
3.4
5.3
9.C
4.4
3.6
4.2
4.C
3.7
4.5
6.2
8.6
4.4
4.1
4.2
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet (Continued)
Start-up Date: October 12, 2006
Week
34
35
37
38
39
40
41
42
Day of
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
T
W
F
Su
T
W
R
F
Sa
Su
M
T
W
R
F
Su
M
T
W
R
F
Sa
M
T
W
R
F
Sa
Su
M
T
W
R
F
Su
M
T
W
R
F
Sa
04/30/07
05/01/07
05/02/07
05/03/07
05/04/07(h)
05/05/07
05/06/07
05/07/07
05/08/07
05/09/07
05/10/07
05/11/07
05/12/07
05/13/07
05/15/07
05/16/07
05/18/07
05/20/07
05/22/07
05/23/07
05/24/07
05/25/07
05/26/07
05/27/07
05/28/07
05/29/07
05/30/07
05/31/07
06/01/07
06/03/07
06/04/07
06/05/07
06/06/07
06/07/07
06/08/07
06/09/07
06/11/07
06/13/07
06/14/07
06/15/07
06/16/07
06/17/07
06/18/07
06/19/07
06/20/07
06/21/07
06/22/07
06/24/07
06/25/07
06/26/07
06/27/07
06/28/07
06/29/07
06/30/07
07/01/07
8:00
8:00
8:00
8:45
11:00
10:20
9:00
8:45
8:20
8:00
8:00
9:30
8:30
8:00
9:15
10:00
11:00
14:00
10:00
9:15
9:00
8:30
9:15
9:45
8:00
8:00
8:00
15:00
16:00
15:35
12:40
8:00
8:00
8:00
NM
35
:25
:00
:45
:30
50
:20
:45
i :40
40
20
:35
:55
:20
:30
:00
8:45
9:30
Cumulative Mrs in Service
TA
,430.2
,436.7
,443.4
,452.5
,460.0
,467.2
,473.6
,480.7
,488.2
,501.9
,509.3
,517.9
,530.3
,538.9
,553.6
,566.3
,582.8
,588.8
,594.9
,602.7
,610.7
,620.0
,629.2
,637.6
,645.2
,659.6
,668.2
,687.5
,693.6
,699.6
,704.5
,711.0
,719.0
NM
,745.7
,752.5
,759.2
,766.1
,771.2
,779.0
,786.1
,795.5
,805.5
,811.8
,818.3
,824.4
,842.5
,853.8
,860.5
,867.7
,874.8
,889.6
,895. S
,905.2
TB
,406.4
,412.6
,418.1
,426.3
,433.5
,441.1
,447.3
,454.4
,461.6
,475.7
,482.8
,491.6
,504.1
,512.3
,526.8
,539.6
,556.0
,562.0
,567.7
,583.5
,592.7
,601.9
,618.0
,632.0
,640.7
,660.4
,666.6
,672.3
,677.2
,683.8
,691.8
NM
,718.4
,725.3
,732.0
,738.6
,742.0
,751.3
,758.3
,767. E
,777.5
,784.3
,790.5
,796.9
,814.E
,826.2
,832.6
,840.3
,847.1
,862.3
,868.7
,877.6
TC
,344.9
,351.4
,357.7
,366.2
,373.7
,380.9
,387.1
,394.5
,401.7
,415.9
,423.0
,431.7
44.2
52.5
67.4
80.1
,496.6
,502.6
,508.4
,524.6
,533.6
,542.9
,558.8
,573.2
,581.9
,601.3
,607.5
,613.6
,618.5
,625.1
,633.1
NM
,659.9
,666.4
,673.4
,679.9
,685.1
,692.5
,699.9
,709.3
,719.0
,738.2
,755.9
,767.4
,774.1
,781.4
,786.2
,803.5
,809.9
,818.9
Avg Run
Time
4.7
6.4
6.2
8.6
7.4
7.3
6.3
7.2
6.3
7.7
7.2
8.7
6.1
8.4
7.8
7.0
10.1
6.0
5.9
7.8
8.1
9.2
9.2
7.5
14.3
8.7
6.2
5.9
4.9
6.6
8.0
NA
8.0
6.7
6.8
6.7
4.6
8.2
7.2
9.4
9.8
6.2
9.8
11.4
6.6
7.4
6.2
15.8
6.4
9.1
Hour
Meter
327.0
333.4
340.0
350.1
357.6
365.3
371.8
379.4
393.8
401.6
409.1
418.2
431.2
439.8
455.2
468.5
485.5
491.6
497.7
506.0
514.4
523.8
533.6
550.2
565.1
574.2
601.0
607.1
612.5
619.1
627.6
NM
655.5
662.3
669.4
676.4
682.0
689.8
697.3
707.2
717.3
737.3
756.0
767.7
774.6
782.3
789.5
805.2
811.9
821.2
Run
Time
5.5
6.4
6.6
10.1
7.5
7.7
6.5
7.6
6.9
7.8
7.5
9.1
5.7
8.6
8.1
7.5
10.2
6.1
6.1
8.3
8.4
9.4
9.8
7.6
14.9
9.1
6.6
6.1
5.4
6.6
8.5
NA
8.4
6.8
7.1
7.0
5.6
7.8
7.5
9.9
10.1
6.5
10.3
11.7
6.9
7.7
7.2
15.7
6.7
9.3
Chlorine
Chlorine
Tank
Level
34
30
26
21
18
15
8
32
28
25
2
1
1
1
1
1
1
38
34
28
23
14
7
35
22
19
16
12
6
NM
18
15
12
8
20
16
13
9
5
10
15
9
38
34
29
15
Cl
3.0
4.7
4.2
4.2
2.9
2.9
4.0
4.9
3.3
3.8
3.0
3.3
3.5
3.5
4.6
3.9
3.6
4.9
4.8
2.7
3.6
4.7
3.9
4.5
3.5
4.1
4.6
3.6
4.2
4.4
5.4
5.4
3.3
3.2
4.3
4.0
3.8
3.0
3.0
3.0
3.3
4.6
3.6
3.8
5.5
6.8
3.6
6.8
5.6
4.0
Totalizer to
Totalizer
46,045.0
46,145.4
46,257.4
46,397.8
46,518.1
46,640.0
46,742.6
46,861.0
46,980.5
47,088.6
47,213.0
47,330.1
4 ,473.5
4 ,677.4
4 ,812.8
48,054.2
48,264.6
48,534.5
48,629.8
48,726.6
48,854.8
8,986.2
9,135.5
. 9,286.5
. 9,546.4
9,779.3
9,920.9
50,236.6
50,339.1
50,436.5
50,520.3
50,626.1
50,757.1
NA
51,193.1
51,301.2
51,412.0
51,522.1
51,610.6
51,732.7
51,849.9
52,004.0
52,162.3
52,268.6
52,474.1
52,766.5
52,949.9
53,056.8
53,126.1
53,289.2
53,531.6
53,636.5
53,783.0
Avg Flow
Rate
241
261
283
232
267
264
263
260
266
261
266
260
263
296
262
262
264
268
260
264
257
261
265
257
239
287
261
259
261
259
266
259
267
257
NA
258
265
260
262
263
261
260
259
261
257
264
259
260
261
258
150
378
257
261
263
Pressure Filtration
Influent
psig
83
78
84
75
83
80
79
79
81
77
84
84
78
81
84
81
81
80
82
78
80
81
83
80
78
82
81
82
80
81
84
77
84
80
82
81
81
81
78
81
80
77
83
80
81
79
81
81
82
80
83
81
81
83
Outlet TA
psig
69
67
71
68
69
68
70
67
69
65
69
68
66
68
72
68
67
66
68
75
68
69
74
67
69
70
75
68
67
71
73
70
68
69
72
NA
72
70
71
68
64
66
70
69
66
69
68
68
68
70
68
71
65
73
74
66
Outlet TB
psig
71
73
68
67
69
69
68
67
70
71
68
66
68
68
66
70
73
69
69
68
68
67
70
71
72
72
71
72
68
66
67
69
68
67
66
NA
69
68
68
72
68
70
72
70
73
66
72
65
68
68
73
66
68
65
68
66
Outlet TC
psig
68
69
72
72
69
67
69
71
64
68
68
67
70
71
73
76
69
69
70
68
68
72
68
68
71
68
67
70
68
73
73
67
69
70
70
NA
65
71
65
72
69
74
67
67
69
73
70
69
73
72
68
72
74
69
70
71
Effluent
psig
56
56
56
57
55
56
56
55
55
56
55
55
55
56
56
56
56
56
56
56
55
55
54
55
55
55
56
55
56
55
56
56
56
56
56
NA
56
55
56
56
56
56
56
55
56
55
56
55
56
56
56
55
55
55
56
56
Flow/Totalizer to
Flow
Rate
gpm
275
290
300
285
297
280
290
285
282
276
285
270
268
290
275
272
297
280
280
295
290
298
285
290
302
300
290
298
285
300
310
270
285
292
297
NA
292
300
275
300
290
293
302
290
288
298
302
283
290
292
294
295
295
268
Totalizer
kgal
22,093.6
22,171.8
22,272.0
22,383.0
22,521.3
22,634.6
22,750.1
22,845.8
22,957.3
23,171.2
23,288.6
23,398.7
23,533.6
23,728.1
23,857.4
24,087.7
24,287.3
24,542.1
24,633.1
24,726.5
24,849.1
24,974.1
25,118.8
25,262.4
25,396.7
25,511.0
25,734.1
25,871.0
26,172.5
26,271.2
26,364.9
26,445.7
26,545.1
26,670.6
NA
27,088.7
27,190.3
2 ,297.3
2 ,402.0
2 ,488.1
2 ,604.2
2 ,716.2
27,864.4
28,015.3
28,117.3
28,216.8
28,314.6
28,594.2
28,769.5
28,871.3
29,325.5
29,567.2
Avg Flow
Rate
gpm
294
279
261
300
268
255
263
255
258
268
254
255
258
261
258
259
266
257
253
265
262
256
263
259
263
254
261
263
255
267
263
275
252
262
NA
263
251
262
262
314
237
261
262
257
262
258
262
261
256
257
246
259
:erric Chloride
FeCI3
Tank
Level
pal
17
11
3
38
30
22
14
5
32
16
7
34
24
9
34
17
31
20
16
9
36
28
17
6
32
24
6
33
10
39
32
26
18
8
NM
15
6
34
26
20
11
38
27
16
8
36
29
8
24
15
15
20
Fe
Dosage
2.3
2.4
2.1
1.7
2.0
2.0
2.6
2.0
2.2
2.1
2.1
2.2
2.1
2.0
NA
1.3
2.2
2.1
1.8
2.2
2.2
2.1
1.8
2.3
1.9
1.8
2.2
2.1
2.3
2.3
NA
2.1
2.5
2.2
2.2
2.0
2.2
2.1
2.1
2.3
2.6
2.1
2.2
2.0
2.5
2.2
2.5
Backwash
Tank
42
44
45
45
46
46
47
49
50
51
51
52
53
54
55
55
56
57
57
59
60
60
61
64
64
65
65
66
NA
68
68
9
9
0
2
3
3
4
5
6
6
9
80
Tank
198
203
207
208
208
209
210
212
214
215
216
218
219
220
220
221
222
223
224
226
227
228
229
231
232
233
233
234
NA
237
237
238
239
240
241
244
244
245
245
247
248
249
251
253
Tank
1 7
1 7
1 8
1 9
1 9
181
183
184
185
186
187
188
188
189
190
190
191
193
194
195
196
199
199
200
200
201
NA
203
204
204
205
206
207
209
210
210
211
213
214
214
217
218
269.6
270.1
271.0
271.8
272.7
275.6
277.7
278.9
279.8
281.5
282.8
284.0
284.0
285.3
286.6
287.4
288.2
290.7
292.8
294.1
298.0
299.2
299.2
300.4
NA
303.3
303.7
304.6
305.4
306.7
307.5
3 0.4
3 1.2
3 1.7
3 2.5
3 4.6
3 5.8
3 6.2
3 9.6
321.7
Since Last BW
2.5
10.0
3.6
10.0
3.5
7.7
15.1
6.6
4.1
12.7
11.9
9.9
14.9
0.1
6.1
3.2
0.0
9.3
1.7
9.8
6.4
2.2
8.7
0.0
NA
7.7
8.5
1.0
7.9
4.5
12.0
4.2
10.7
3.0
8.7
6.2
12.9
0.0
1.8
0.4
8.0
4.5
1.5
8.0
5.5
4.5
8.0
6.2
0.0
3.7
10.2
16.2
3.9
4.6
4.2
3.9
0.2
1.9
4.1
1.9
8.5
6.9
NA
5.2
12.1
5.0
1.8
4.1
1.5
8.3
2.0
8.4
5.5
8.3
2.7
10.0
5.5
8.0
2.1
9.6
6.0
1.1
8.5
8.4
3.8
0.6
2.7
1.1
4.5
5.9
12.4
18.4
3.6
0.9
9.3
7.5
3.9
4.3
7.6
1.5
8.1
3.1
NA
10.1
4.2
11.2
4.2
3.6
5.5
0.0
6.6
1.9
0.7
2.2
8.9
4.6
3.3
4.1
St
9.2
6.2
7.4
6.2
2.6
0.1
5.6
6.4
4.2
3.3
5.8
0.7
4.2
1.2
5.1
5.3
0.7
3.5
1.1
9.2
5.6
3.1
5.5
NA
4.3
2.9
8.5
5.6
9.1
3.8
NM
NM
NM
NM
NM
NM
15.4
31.1
9.0
16.1
31.2
ndbyTi
19.2
17.0
34.3
16.2
16.1
32.7
17.5
15.6
33.2
17.9
16.7
17.3
30.7
452.0
17.1
15.1
15.3
15.4
13.5
11.2
12.4
15.6
33.2
15.5
NA
14.3
32.9
18.5
17.1
19.2
14.8
NM
NM
NM
NM
NM
NM
15.4
2.9
9.0
16.1
15.1
19.2
36.2
17.3
31.9
16.1
32.7
17.5
15.6
16.3
17.8
16.7
17.2
30.7
45.2
17.1
15.1
30.3
15.4
13.5
11.3
11.2
29.3
15.6
33.1
15.5
NA
28. S
18.7
37.3
17.1
19.2
14.7
NM
NM
NM
NM
NM
NM
15.5
9.1
9.0
16.1
15.1
Actu
Be
6.0
14.0
17.1
—
15.6
14.7
11.5
20.8
10.7
11.2
11.4
8.9
11.7
8.6
9.1
16.7
NA
14.2
8.5
14.1
13.8
13.8
15.9
26.1
6.1
12.4
al Run 1
tween E
8.9
9.7
8.3
9.6
9.8
8.9
10.0
10.7
9.9
18.0
7.1
8.4
9.5
11.9
4.1
15.8
7.8
11.1
12.5
6.7
7.1
9.6
NA
—
13.8
9.8
1.1
10.0
9.8
8.9
12.5
10.9
8.6
12.0
9.4
10.9
6.4
8.5
tw
4.6
10.9
11.1
10.9
9.6
11. S
9.9
10.0
20.6
10.5
10.8
11.9
9.6
4.8
16.5
8.1
10.6
5.6
11. C
13. C
NA
12.4
13.5
5.E
10.6
11.3
11. S
10. S
8.S
10. C
14.8
12.7
7.7
8.2
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet (Continued)
Start-up Date: October 12, 2006
Week
No.
43
44
45
46
48
49
SO
52
Day of
Week
M
W
R
F
Su
M
T
R
F
Sa
Su
M
W
R
F
Su
M
T
W
R
F
Sa
Su
T
W
F
Sa
M
T
W
R
F
Sa
M
T
W
R
Sa
Su
M
W
R
F
Su
M
T
W
R
F
Su
M
T
W
R
Sa
Su
T
W
R
F
Su
Date
07/02/07
07/04/07
07/05/07
07/06/07
07/08/07
07/09/07
07 0/07
07 2/07
07 3/07
07 4/07
07 5/07
07 6/07
07 8/07
07 9/07
0 /20/07
0 /22/07
0 /23/07
0 /24/07
0 /25/07
0 /26/07
0 /27/07
0 /28/07
0 /29/07
0 /31/07
08/01/07
08/03/07
08/04/07
08/06/07
08/07/07
08/08/07
08/09/07
08/10/07
08/11/07
08/13/07
08/14/07
08/15/07
08/16/07
08/18/07
08/19/07
08/20/07
08/22/07
08/23/07
08/24/07
08/26/07
08/27/07
08/28/07
08/29/07
09/01/07
09/02/07
09/03/07
09/04/07
09/05/07
09/06/07
09/08/07
09/09/07
09/1 1/07
09/12/07
09/13/07
09/14/07
09/16/07
Time
7:45
9:10
8:30
10:45
7:45
12:00
8:10
11:10
13:45
11:15
9:50
11:15
11:00
7:20
8:15
MM
13:20
15:20
10:05
8:00
8:00
9:30
22:10
12:45
9:05
14:10
11:00
13:20
11:40
9:50
7:45
12:30
16:50
13:55
12:45
1 :20
8 5
: 5
1 0
1 0
1 0
1 :25
1 0
1 0
1 0
1 :50
1 :20
1 5
1 0
1 :55
1 0
i 5
12:50
1 0
1 5
1 5
1 0
1 5
18:10
Cumulative Mrs in Service
hr
1,911.9
1,928.1
1,934.0
1,943.2
1,960.1
1,972.0
1,976.1
1,993.6
2,002.8
2,012.5
2,018.3
2,031.0
2,051.7
2,059.2
2,066.1
MM
2,096.2
2,105.2
2,113.9
2,120.8
2,131.3
2,139.7
2,148.1
2,158.4
2,163.5
2,185.2
2,195.7
2,214.6
2,222.7
2,230.1
2,237.7
2,246.9
2,254.8
2,271.8
2,279.6
2,289.3
2,294.6
2,310.1
2,321.8
2,327.6
2,338.5
2,343.7
2,350.0
2,362.4
2,369.9
2,377.1
2,384.6
2,398.6
2,413.5
2,420.2
2,428.5
2,432.8
2,440.1
2,454.5
2,463.7
2,476.8
2,489.1
2,496.6
2,508.1
hr
1,884.4
1,900.4
1,906.6
1,915.4
1,932.3
1,944.3
1,948.8
1,966.3
1,975.5
1,984.8
1,990.7
2,003.4
2,024.1
2,031.5
2,038.4
MM
2,068.4
2,077.1
2,085.9
2,092.8
2,103.1
2,111.6
2,120.1
2,130.5
2,136.0
2,157.7
2,167.9
2,186.9
2,195.1
2,202.2
2,210.0
2,218.9
2,226.8
2,243.9
2,251.8
2,261.5
2,266.5
2,281.9
2,293.7
2,299.1
2,309.9
2,315.1
2,321.3
2,334.3
2,341.4
2,348.3
2,356.1
2,362.3
2,369.9
2,385.1
2,392.3
2,400.2
2,404.5
2,411.9
2,426.5
2,435.7
2,448.4
2,461.0
2,468.1
2,479.6
hr
,826.0
,841.9
,848.1
,857.0
,874.0
,886.0
,890.5
,907.8
,917.0
,926.4
,932.7
,945.4
,965.8
,973.4
,980.0
MM
2,010.6
2,019.3
2,028.1
2,035.1
2,045.5
2,054.0
2,062.4
2,072.7
2,078.1
2,100.2
2,110.7
2,129.4
2,137.6
2,145.1
2,162.9
2,167.9
2,170.1
2,187.4
2,195.2
2,204.9
2,209.9
2,225.0
2,237.0
2,242.7
2,253.7
2,258.9
2,265.2
2,277.8
2,284.8
2,292.1
2,299.7
2,306.0
2,313.7
2,328.8
2,335.6
2,343.1
2,347.9
2,355.3
2,369.8
2,378.9
2,391.9
2,404.1
2,411.3
2,422.9
Avg Run
Time
hr
6.9
6.6
6.1
9.0
11.3
12.0
4.4
4.0
9.2
9.5
6.0
12.7
10.1
7.5
6.8
MA
22.4
8.8
8.8
6.9
10.4
8.5
8.4
4.8
5.3
12.2
10.4
10.5
8.2
7.3
11.1
7.7
6.0
9.4
7.8
9.7
5.1
8.2
1 .8
.6
.6
.2
.3
.1
.2
.1
.6
.2
.7
1 .1
i.9
.9
. .5
.4
.1
.2
.3
.1
.3
1 .5
Hour
Meter
hr
828.5
845.3
851.6
860.9
878.4
890.9
895.6
914.2
923.4
933.2
939.5
952.6
974.2
982.0
989.0
MM
,020.2
,029.3
,038.5
,046.0
,056.7
,065.5
,074.4
,085.2
,090.8
,113.5
,124.4
,144.2
,152.8
,160.3
,169.0
,178.1
,186.4
,204.5
,212.7
,222.9
,228.3
,244.2
,252.8
,262.6
,274.0
,279.3
,286.0
,299.5
,306.8
,314.1
,322.2
,328.8
,336.8
,352.7
,360.0
,368.3
,373.0
,380.7
,395.7
,405.3
,418.9
,431.8
,439.5
,451.5
Run
Time
hr
7.3
7.0
6.3
9.3
11.6
12.5
4.7
4.5
9.2
9.8
6.3
13.1
10.5
7.8
7.0
NA
23.1
9.1
9.2
7.5
10.7
8.8
8.9
5.0
5.6
12.6
10.9
11.1
8.6
7.5
8.7
9.1
8.3
9.8
8.2
10.2
5.4
8.4
8.6
9.8
5.8
5.3
6.7
6.7
7.3
7.3
8.1
6.6
8.0
15.9
7.3
8.3
4.7
7.7
5.2
9.6
7.6
6.4
7.7
12.0
Chlorine
Chlorine
Tank
gal
16
6
18
11
34
26
23
26
20
30
27
19
6
34
30
MM
6
34
28
24
18
1
1
1
29
20
8
33
27
21
15
24
10
5
12
8
31
27
25
17
13
8
30
23
17
13
38
32
20
15
9
38
32
21
14
4
26
20
11
Cl
dosage
mg/L
4.2
4.3
4.8
5.6
.5
.8
.9
i.8
.9
.8
.6
.6
.0
.7
.7
3.3
4.9
4.1
4.2
4.3
5.1
3.0
5.5
5.5
6.2
4.1
5.3
6.0
5.2
5.0
6.3
6.1
.6
i.O
.7
.6
.4
.6
.8
.7
.7
.7
.2
i.2
.8
.6
.6
.7
.2
.4
.0
.8
.7
.5
.9
.9
.9
.6
Totalizer to
Totalizer
kgal
53,894.2
54,155.9
54,253.7
54,401.2
54,677.0
54,870.5
54,941.6
55,230.5
55,375.1
55,521.
55,620.
55,823.3
56,156.6
56,280.7
56,381.0
NA
56,874.5
57,014.
57,158.
57,272.3
57,439.1
57,575.
57,714.3
57,883.0
57,968.7
58,313.9
58,483.0
58,788. i
58,922.2
59,039,
59,174.7
59,316,
59,446.0
59,727.
59,854.0
60,011.
60,093.9
60,341.
60,534.5
60,625.2
60,803.6
60,886,
60,990.1
6 ,199.1
6 ,313.7
6 ,427.
6 ,551.
6 ,653.9
6 ,779.2
62,026.9
62,139.5
62,270.
62,341.
62,463.;
62,696.7
62,845.8
63,056.8
63,259.0
63,377.5
63,565.9
Avg Flow
Rate
gpm
254
261
259
264
265
258
252
256
262
248
262
259
259
265
239
NA
260
257
260
254
260
25S
259
262
255
254
259
256
258
26C
25S
26C
260
26C
258
257
256
26C
374
154
264
26C
258
256
262
26C
256
258
261
260
257
262
252
265
264
259
261
264
259
256
262
Pressure Filtration
psig
81
NA
80
79
82
78
81
79
82
83
80
82
80
81
83
NA
81
79
82
80
82
82
79
78
79
79
79
79
79
83
77
81
82
81
80
81
80
82
79
81
80
81
78
82
81
83
82
78
79
NA
78
80
79
77
79
81
78
80
79
82
82
psig
71
NA
72
68
67
6S
70
6S
68
67
67
68
71
66
66
NA
74
6E
71
71
65
6E
69
68
71
67
68
6E
70
67
67
65
68
6E
73
74
66
66
71
69
70
67
68
69
70
67
71
69
65
NA
7C
7C
7C
67
73
73
71
68
70
66
69
psig
67
NA
67
69
69
71
66
69
65
70
70
68
68
71
67
NA
70
68
70
67
69
71
69
71
65
68
72
69
69
66
68
71
69
71
70
72
66
68
71
73
68
70
66
66
70
71
71
71
NA
65
70
68
68
68
68
72
69
66
70
69
psig
65
NA
66
68
68
70
64
71
66
75
65
67
73
66
74
NA
69
68
70
67
69
71
69
69
66
68
68
72
73
65
69
72
66
66
68
69
69
73
73
68
69
67
67
71
73
66
68
67
67
NA
70
74
73
68
70
70
68
72
72
73
73
psig
56
NA
54
55
57
56
55
56
55
57
55
56
56
56
55
NA
56
55
57
57
57
58
56
56
55
55
56
55
56
55
55
55
55
55
56
57
55
55
55
56
57
56
56
55
56
55
56
55
55
55
55
57
55
55
57
56
55
55
55
56
57
Flow/Totalizer to
Flow
Rate
gpm
273
NA
304
286
268
29C
282
29E
279
295
275
270
301
272
292
NA
304
29C
295
292
268
28E
312
288
285
290
283
305
302
275
29C
295
297
275
307
302
296
293
301
297
302
28C
286
290
295
285
30C
302
283
NA
285
29E
307
29C
275
298
306
296
297
293
295
Totalizer
kgal
29,674.1
29,923.9
30,017.7
30,159.3
30,423.4
30,607.6
30,674.7
30,953.4
31,090.5
31,229.4
31,325.5
31,519.6
31,839.3
31,956.9
32,059.2
NA
32,524.3
32,659.8
32,796.8
32,907.6
33,066.3
33,199.3
33,329.9
33,492.9
33,574.3
33,905.6
34,068.2
34,362.0
34,490.2
34,601.6
34,732.5
34,868.9
34,993.9
35,263.1
35,383.6
35,535.0
35,613.9
35,851.2
36,037.6
36,124.0
36,294.7
36,373.7
36,473.7
36,673.8
36,783.8
36,892.2
37,011.7
37,110.4
37,230.7
NA
37,577.3
37,701.0
37,769.7
37,888.5
38,111.5
38,254.6
38,457.1
38,555.1
38,651.3
38,764.7
38,944.9
Avg Flow
Rate
gpm
260
266
256
263
262
257
256
273
248
245
267
255
258
261
251
NA
255
257
260
266
254
262
258
266
254
252
261
257
262
253
197
295
347
262
256
26C
258
254
262
256
260
253
266
271
255
253
261
265
259
NA
NA
261
256
26S
26C
260
260
259
264
260
260
:erric Chloride
FeCI3
Tank
qal
11
24
15
5
19
4
41
20
9
35
27
11
29
20
10
NA
9
34
23
14
4
36
26
12
5
23
10
24
13
3
23
12
39
16
6
31
24
5
34
26
12
5
40
27
15
6
39
31
22
25
16
6
36
27
9
34
17
9
39
30
15
Fe
Dosage
mg/L
2.4
2.2
2.8
2.3
2.3
2.1
2.2
2.3
2.1
2.4
2.4
2.4
2.2
3.0
NA
2.2
2.1
2.3
1.8
2.2
2.2
2.7
2.4
2.2
2.3
1.9
2.5
2.6
2.2
2.3
1.8
2.5
2.4
2.3
2.5
2.3
2.0
2.6
2.6
2.5
2.0
1.2
3.1
2.4
2.2
2.3
2.2
2.2
2.4
2.3
2.1
2.2
2.2
2.0
2.3
2.3
2.1
2.3
Backwash
Tank
No.
181
182
183
184
185
186
18E
188
18E
18S
190
192
192
192
NM
195
195
196
197
19E
199
200
201
203
204
206
207
207
20S
20S
2 0
2 2
2 3
2 4
2 4
2 5
2 7
2 7
2 8
2 E
2 9
220
221
221
222
223
223
225
226
226
227
22E
22S
230
231
231
232
232
Tank
No.
254
256
256
258
259
259
262
262
263
264
265
267
268
268
NM
271
272
273
275
276
277
278
278
281
283
285
286
287
290
291
293
294
295
296
297
299
300
301
301
302
303
304
305
306
307
308
10
; 10
11
12
; 13
14
15
17
17
18
19
Tank
No.
219
221
221
223
224
224
227
227
228
228
229
232
232
233
NM
235
236
239
240
241
242
242
243
244
247
248
248
250
251
251
253
254
255
256
25E
26C
260
261
261
262
264
265
265
266
267
268
270
271
272
273
274
275
276
277
278
279
280
hqal
322.6
324.6
325.0
327.1
328.4
328.8
332.1
332.1
333.0
333.9
335.1
338.0
338.5
338.8
NM
342.1
342.9
346.2
347.4
348.6
349.4
350.3
352.9
358.6
362.2
363.0
365.5
366.7
367.9
368.8
370.3
372.8
373.2
3 4.5
3 4.5
3 5.7
3 7.4
3 8.6
3 9.0
382.3
384.8
385.6
386.5
387.7
388.9
390.1
391.3
393.0
393.4
394.6
Since Last BW
hr
3.7
5.7
0.0
12.1
0.3
1.9
11.1
20.8
5.7
6.5
3.3
10.8
17.7
NM
0.0
9.0
12.5
7.0
4.9
5.7
0.9
8.0
3.5
13.0
6.9
4.4
0.0
0.5
5.5
11.2
3.5
9.3
6.4
11.6
2.6
5.1
2.9
10.1
10.6
5.9
1.0
9.3
1.2
5.4
0.5
1.9
2.9
u n Tim
hr
6.3
0.1
6.2
6.5
1.1
10.3
6.0
2.5
5.0
8.6
2.9
9.9
NM
7.2
3.7
1.6
0.5
0.0
1.9
7.4
6.8
5.8
4.6
2.9
3.3
3.2
4.0
0.0
6.9
5.0
2.8
1.7
6.9
1.4
7.4
6.5
4.8
1.0
1.0
8.2
6.0
2.3
4.8
9.2
6.6
0.5
hr
11.2
4.2
10.4
7.2
0.7
9.9
1.7
8.0
10.5
0.4
8.0
2.9
NM
10.7
6.5
6.3
3.6
3.3
3.1
8.5
5.5
0.2
1.8
10.0
8.3
6.6
7.0
2.7
0.1
0.0
5.7
9.0
14.2
4.8
2.0
0.9
8.2
4.9
4.8
2.5
0.0
O.C
4.2
5.2
4.7
8.1
Sfc
hr
13.8
NM
25.8
15.6
14.7
20.3
37.9
49.7
16.3
11.7
11.9
24.4
42.3
NM
12.4
29.4
13.4
16.5
12.7
27.5
14.8
15.3
15.2
13.6
33.8
19.9
11.8
15.0
11.3
27.4
32.5
14.8
32.1
36.3
55.4
17.8
17.7
14.5
33.1
33.8
NM
13.5
25.
18.
19.2
17.
15.1
17.6
35.4
20.9
ndby Ti
hr
13.9
NM
36.8
6.6
21.3
20.3
37.9
11.8
16.3
11.8
11.9
12.5
30.4
NM
12.5
17.0
0.0
0.0
12.7
15.5
30.3
15.3
15.1
13.6
19.6
19.8
11.7
15.0
11.3
16.1
16.9
14.8
17.4
17.2
36.3
17.8
34.5
14.5
18.4
17.2
NM
32.2
11.7
18.1
19.2
34.1
15.1
17.6
35.4
20.9
ne
hr
29.0
NM
36.7
6.7
21.3
20.1
37.7
11.8
28.1
11.7
11.9
24.4
17.9
NM
12.4
17.0
13.3
0.0
12.7
15.6
30.4
15.3
15.2
13.6
27.5
19.5
39.3
11.8
15.0
11.3
16.2
16.8
14.8
32.1
36.3
55.3
17.8
17.8
14.5
33.0
17.2
NM
13.5
11.7
18.1
19.2
34.1
15.1
17.6
17.8
20.9
Actu
Be
hr
11.6
14.0
11.3
6.7
—.
20.9
11.9
13.9
18.6
10.7
13.9
10.5
9.5
9.9
7.3
10.3
11.1
11.2
14.0
10.1
12.2
9.2
9.8
13.8
15.3
9.7
11.6
19.6
11.6
12.4
3.1
7.8
13.5
al Run Time
tweenBW
hr
12.3
—
11.2
15.8
—
13.6
9.4
10.2
9.4
13.1
12.0
20.7
12.2
8.8
9.6
9.6
9.0
7.5
7.9
9.1
9.6
8.2
8.0
8.9
9.0
^^
11.7
7.0
8.0
8.6
8.7
7.4
15.2
10.1
8.0
4.9
10.2
11.8
8.3
9.2
12.1
hr
14
—
12.1
2.0
15.0
—
17.6
10.2
20.8
^^
11.7
9.5
13.3
12.9
9.3
8.3
8.8
11.2
8.7
—r~
9.1
8.7
8.9
10.6
9.5
9.3
9.3
9.5
7.6
15.7
7.7
8.1
8.9
8.4
15.2
9.1
10.0
4.8
3.2
13.5
9.6
9.6
12.0
8.1
-------
Table A-l. US EPA Demonstration Project at Felton, DE - Daily Operational Log Sheet (Continued)
Start-up Date: October 12, 2006
Week
No.
54
55
56
57
58
59
60
Day of
Week
M
T
W
R
F
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Su
M
T
W
R
F
Sa
Date
09/1 7/0701
09/18/07
09/19/07
09/20/07
09/21/07
09/23/07
09/24/07
09/25/07
09/26/07
09/27/07
09/28/07
09/29/07
09/30/07
10/01/07
10/02/07
10/03/07
10/04/07
10/05/07
10/06/07
10/07/07
10/08/07
10/09/07
10/10/07
10/11/07
10/12/07
10/14/07
10/15/07
10/16/07
10/17/07
10/18/07
10/19/07
10/20/07
10/21/07
10/22/07
1 0/23/07
10/24/07
10/25/07
10/26/07
10/27/07
10/28/07
10/29/07
10/30/07
10/31/07
1 1/01/07
1 1/02/07
11/03/07
Time
13:40
11:05
10:45
13:15
16:10
16:20
16:30
13:50
15:10
14:45
14:10
15:25
14:10
15:25
13:55
13:40
15:35
11:30
12:00
15:30
16:10
16:00
12:10
14:00
12:55
13:00
14:20
12:10
12:00
13:25
13:35
14:15
10:40
9:45
14:00
10:35
9:30
10:20
12:45
MM
13:50
11:35
10:30
11:20
11:25
8:45
Cumulative Mrs in Service
TA
hr
2,512.9
2,518.9
2,523.2
2,529.9
2,535.9
2,549.3
2,555.4
2,561.6
2,566.9
2,574.4
2,581.2
2,586.8
2,593.6
2,600.5
2,606.0
2,611.0
2,619.3
2,623.5
2,631 .5
2,639.2
2,646.2
2,653.9
2,659.4
2,663.6
2,671.2
2,682.8
2,687.4
2,695.0
2,700.4
2,706.8
2,712.7
2,718.7
2,725.9
2,729.9
2,737.8
2,745.0
2,749.2
2,755.5
2,761.4
2,767.3
2,774.1
2,780.0
2,784.2
2,791.2
2,796.9
2,804.4
TB
hr
2,484.4
2,490.5
2,494.8
2,501.1
2,507.2
2,520.5
2,527.0
2,533.3
2,538.3
2,545.8
2,552.6
2,558.3
2,565.2
2,572.1
2,577.3
2,583.5
2,590.7
2,594.9
2,603.0
2,610.7
2,617.3
2,624.9
2,630.4
2,634.7
2,642.7
2,653.7
2,658.3
2,665.9
2,671.0
2,677.5
2,683.6
2,689.6
2,696.8
2,700.5
2,708.5
2,715.8
2,720.0
2,726.0
2,731 .9
2,733.0
2,745.1
2,750.8
2,755.0
2,761.8
2,768.0
2,775.5
TC
hr
2,428.1
2,433.9
2,438.6
2,445.0
2,451.0
2,464.2
2,470.7
2,477.0
2,481.9
2,489.4
2,496.2
2,501.9
2,508.7
2,515.7
2,520.8
2,526.7
2,533.9
2,538.5
2,546.6
2,554.0
2,560.7
2,568.7
2,574.2
2,578.5
2,585.8
2,597.8
2,602.1
2,609.7
2,615.1
2,621.6
2,627.7
2,633.7
2,640.6
2,644.7
2,652.6
2,659.8
2,663.8
2,670.2
2,676.2
2,682.2
2,689.0
2,694.9
2,699.5
2,706.2
2,712.3
2,719.5
Avg Run
Time
hr
4.9
6.0
4.4
6.5
6.0
13.3
6.4
6.3
5.1
7.5
6.8
5.7
6.8
6.9
5.3
5.7
7.6
4.3
8.1
7.6
6.8
7.8
5.5
4.3
7.6
11.5
4.5
7.6
5.3
6.5
6.0
6.0
7.1
3.9
7.9
7.2
4.1
6.2
5.9
4.3
8.6
5.8
4.3
6.8
6.0
7.4
Hour
Meter
hr
1,456.8
1,462.9
1,467.7
1,474.4
1,480.9
1,494.8
1,501.4
1,508.1
1,513.5
1,521.4
1,528.2
1,534.4
1,541.6
1,549.C
1,554.6
1.560.G
1,568.4
1,573.0
1,581.5
1,589.6
1,596.7
1,604.7
1,610.7
1,615.4
1,623.1
1,635.6
1,640.2
1,648.3
1,653.8
1,660.6
1,667.1
1,673.6
1,680.8
1,685.C
1,693.3
1,701.0
1,705.2
1,711.7
1,718.1
1,724.5
1,731.7
1,738.2
1,742.G
1,749.9
1,756.1
1,764.0
Run
Time
hr
5.3
6.1
4.8
6.7
6.5
13.9
6.6
6.7
5.4
7.9
6.8
6.2
7.2
7.4
5.6
6.2
7.6
4.6
8.5
8.1
7.1
8.0
6.0
4.7
7.7
12.5
4.7
8.0
5.5
6.8
6.5
6.5
7.2
4.2
8.3
7.7
4.3
6.4
6.4
6.4
7.2
6.5
4.6
7.1
6.2
7.9
Chlorine
Chlorine
Tank
Level
gal
7
35
31
26
21
10
6
34
30
26
22
18
14
9
6
28
23
20
32
27
22
17
14
11
7
30
27
22
18
14
10
38
34
31
26
20
18
14
29
25
20
16
13
8
4
31
Cl
dosage
mg/L
5.8
6.1
6.4
5.6
5.8
6.0
4.6
5.7
5.7
.8
.4
.0
.2
.2
. .1
. .9
.0
.9
. .5
.7
.4
• .6
.9
.8
:.9
.9
. .8
• .8
.5
.4
. .7
. .7
.1
.5
.6
.9
:.e
. .7
.8
.7
.3
. .7
. .9
.3
.9
.8
Totalizer to
Totalizer
kgal
63,647.0
63,743.0
63,815.9
63,920.3
64,021.1
64,237.7
64,339.7
64,443.0
64,526.0
64,649.2
64,756.4
64,850.0
64,961.7
65,075.5
65,162.2
65,258.3
65,375.8
65,447.9
65,579.2
65,704.7
65,813.6
65,940.1
66,031.0
66,104.0
66,224.0
66,416.4
66,489.8
66,612.9
66,697.9
66,804.1
66, 903. C
67,003.1
67,116.5
67,180.4
67,309.2
67,428.5
67,494.2
67, 593. G
67,691.8
67,790.7
67,901.8
68, 002. C
68,073.2
68,183.2
68,279.8
68,400.4
Avg Flow
Rate
gpm
255
262
253
260
258
260
258
257
256
260
263
252
259
256
258
258
258
261
25G
258
256
264
252
259
260
257
260
256
258
260
25=1
257
262
254
259
258
255
259
255
258
257
257
25G
25G
259
254
Pressure Filtration
Influent
psig
80
83
81
82
80
80
82
81
81
79
82
82
82
81
80
78
82
77
MM
80
81
80
80
82
83
80
83
81
82
79
79
80
83
79
82
81
81
82
81
MM
81
84
81
81
81
MM
Outlet TA
pag
72
69
72
67
68
68
73
74
67
68
68
70
71
74
69
69
67
68
MM
7
6
7
7
6
6
7
66
71
68
69
69
74
71
66
68
71
68
67
68
MM
73
69
69
6G
72
MM
Outlet TB
pag
73
6G
69
71
73
73
68
6G
69
7C
67
68
68
71
72
65
67
68
MM
67
69
72
71
67
7C
71
74
6G
72
72
69
7C
69
7C
69
73
6G
72
72
MM
68
69
69
72
68
MM
Outlet TC
pag
69
73
67
68
69
70
68
68
69
70
67
68
68
69
71
71
73
67
MM
73
74
68
69
68
74
66
68
75
68
68
65
68
74
66
67
70
74
69
69
MM
72
74
66
70
67
MM
Effluent
pag
56
57
56
56
56
56
56
57
55
55
56
56
56
56
57
55
55
55
MM
56
55
55
57
55
5G
57
57
57
56
56
56
55
58
55
55
57
57
57
56
MM
57
57
55
56
55
MM
Flow/Totalizer to
Flow
Rate
gpm
312
293
29G
292
307
302
296
30C
296
304
280
296
296
305
31 C
285
292
290
NM
303
307
30C
301
275
29C
282
287
302
295
301
28C
307
295
286
279
300
30C
294
298
MM
306
294
276
295
295
MM
Totalizer
kgal
39,022.3
39,114.4
39,184.4
39,284.6
39,381.5
39,590.6
39,687.9
39,787.7
39,867.8
39,986.6
40,088.9
40,179.8
40,286.6
40,395.7
40,478.2
40,572.1
40,684.1
40,754.1
40,879.9
4 ,000.8
4 ,104.8
4 ,226.3
4 ,314.6
4 ,385.9
4 ,499.9
4 ,685.8
4 ,756.0
4 ,872.9
4 ,954.5
42,056.9
42,153.4
42,248.7
42,357.1
42,418.8
42,542.9
42,657.0
42,719.9
42,814.3
42,909.1
43,004.9
43,111.3
43,206.4
43,275.8
43,380.5
43,472.4
43,588.7
Avg Flow
Rate
gpm
NA
257
262
25G
268
262
NA
266
262
264
251
267
261
262
261
275
247
269
26C
265
NA
261
268
279
249
269
26C
256
257
264
267
265
254
262
261
263
252
252
266
368
207
272
267
255
255
262
=erric Chloride
FeCI3
Tank
Level
qal
8
41
33
21
10
24
13
38
29
16
5
38
26
14
4
29
17
9
40
27
16
3
29
21
9
24
16
3
15
4
38
28
17
10
33
21
14
4
35
25
13
38
30
19
9
34
Fe
Dosage
mg/L
2.6
2.8
3.3
3.4
3.3
2.9
3.2
2.9
3.2
3.2
3.1
2.9
3.2
3.2
3.5
3.1
3.1
3.3
2.3
3.1
3.0
3.1
3.0
3.3
3.0
3.1
3.3
3.2
3.2
3.1
2.7
4.8
2.9
3.3
2.8
3.0
3.2
3.0
2.7
3.0
3.2
2.7
3.4
3.0
3.1
2.5
Backwash
Tank
A
No.
234
234
235
235
236
237
238
239
239
240
240
241
242
243
243
244
244
245
246
247
247
248
249
250
250
252
252
253
253
254
255
256
256
256
257
258
258
258
259
260
261
261
262
262
263
264
Tank
B
No.
321
321
322
323
324
326
326
327
328
329
329
330
331
332
333
333
334
335
336
337
338
339
340
341
342
344
344
345
346
347
348
349
349
350
351
352
352
353
354
355
355
356
357
358
358
359
Tank
C
No.
281
282
282
283
284
286
286
287
288
289
289
290
291
292
293
294
295
295
296
298
299
299
300
301
302
303
304
305
305
306
307
308
309
309
310
311
312
312
313
314
315
316
316
317
317
319
Total
kcjal
397.5
397.9
398.8
399.6
400.8
402.9
403.3
404.5
405.3
406.6
406.6
407.9
409.1
410.4
411.2
412.0
412.8
413.6
414.9
416.5
417.3
418.C
419.4
420.7
421.5
423.7
424.1
425.3
425.7
427.0
428.2
429.6
430.0
430.4
431.6
432.9
433.3
433.7
436.0
436.2
437.1
437.9
438. G
439.6
440.0
441.7
Since Last BW
Run Time
Tank A
hr
2.5
8.5
1.7
8.4
5.3
9.2
3.4
0.2
5.5
5.5
12.3
4.0
2.8
0.0
5.5
2.7
10.2
3.4
1.2
1.6
8.6
6.2
2.2
3.2
10.8
3.5
8.2
3.6
9.0
4.5
2.4
0.0
7.2
11.2
6.6
4.8
9.0
15.3
5.0
4.1
0.6
6.6
3.5
10.5
3.4
2.4
TankB
hr
0.0
6.1
3.7
3.2
0.0
1.0
7.5
4.1
2.C
O.G
7.6
3.0
4.6
4.7
O.C
6.2
6.1
2.0
2.9
5.3
4.G
2.7
0.9
2.7
3.1
1.5
6.1
6.C
3.0
1.1
1.7
2.2
9.4
2.7
4.1
2.4
6.6
2.C
1.6
0.9
8.0
4.2
2.4
1.2
7.4
5.7
TankC
hr
8.5
1.9
6.6
5.6
3.8
4.0
10.5
5.5
3.8
3.6
10.4
4.9
6.0
6.3
2.7
1.1
1.4
6.0
5.0
0.0
0.0
8.0
4.4
1.8
1.0
7.0
3.1
0.0
5.4
5.8
4.2
4.9
4.3
8.4
5.7
5.9
0.0
6.4
3.8
2.9
2.8
1.9
6.4
5.1
11.2
0.0
Standby Time
Tank A
hr
14.2
29.6
19.0
38.6
20.3
34.2
17.5
14.6
34.5
15.7
32.1
19.2
17.6
15.7
32.6
17.4
35.6
15.4
NM
13.7
31.7
16.0
14.2
20.2
35.9
12.8
11.2
15.4
33.8
18.6
17.6
18.2
31.4
50.2
19.4
13.4
32.0
50.3
20.2
NM
13.9
29.5
17.5
35.9
17.5
NM
TankB
hr
14.2
29.6
19.0
19.6
20.3
13.8
31.3
14.6
193.9
15.7
32.0
19.2
17.6
15.7
16.9
34.2
18.2
15.4
NM
13.8
18.C
16.C
14.2
20.2
15.7
12.8
O.C
15.4
18.4
18.6
17.6
18.2
31.4
18.G
19.4
13.3
31.9
18.2
20.2
NM
34.7
15.6
17.5
18.4
36.0
NM
TankC
hr
28.2
1.9
34.3
19.6
20.3
13.8
31.3
14.6
19.9
15.7
32.1
19.2
17.6
15.7
16.9
17.4
18.2
33.6
NM
13.8
18.0
34.0
14.2
20.2
15.7
35.8
6.1
15.4
33.8
18.6
17.6
18.2
13.1
31.9
19.4
13.3
18.6
36.9
20.2
NM
13.9
15.6
33.2
18.4
35.9
NM
Actual Run Time
Between BW
Tank A
hr
11.1
9.1
9.5
11.9
9.4
7.5
13.9
8.0
9.7
7.G
11.0
10.2
7.2
10.1
9.5
3.2
18.9
12.2
10.9
8.0
8.4
12.5
9.0
16.2
6.8
10.3
7.2
12.G
8.5
TankB
hr
6.7
6.7
9.4
12.3
9.7
7.1
8.7
10.3
5.3
6.8
9.9
7.3
8.3
7.2
5.2
7.1
9.7
7.3
2.5
7.6
12.6
7.7
8.1
8.4
5.5
5.5
10.4
6.6
9.0
10.6
6.2
1.8
9.4
6.1
7.9
9.2
TankC
hr
12.4
7.4
7.G
13.C
11.2
e.e
7.7
11.2
5.7
6.7
8.7
7.£
6.E
9.1
12.4
6.7
9.1
6.E
8.1
6.C
8.2
10.7
6.1
7.7
5.2
7.£
10.6
7.C
9.E
s.e
6.E
6.E
6.G
8.C
18.4
(a) Operator began tracking the trigger that activated each backwash.
(b) Battelle personnel onsite for system inspection and operator training.
(c) Increased stroke on FeCIs chemical feed pump from 18 to 25. Target iron concentration of 1.5 mg/L.
(d) Minimum and maximum backwash time decreased from 10 to 5 min and 40 to 15 min, respectively. Turbidity threshold increased from 10 to 20 NTU.
(e) Cumulative hours in service for Tank A reset on its own.
(f) Differential pressure backwash trigger was reduced from 24 to 18 psi; stroke on chemical feed pump from 25 to 32 (target iron concentration of 2.0 mg/L).
(g) Hour meter installed at wellhead.
(h) Recycle system shut-off due to level of solids in recycle tank.
(i) Recycle system back on-line after solids were removed from the tank on May 11, 2007.
(j) Iron addition was switched to manual operation; FeCIS pump settings: stroke = 75 and speed = 50.
-------
APPENDIX B
ANALYTICAL DATA TABLES
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L(a)
mg/L
mg/L
mg/L
ug/L(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a)AsCaCOS. (b) As P.
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
mg/L
mg/L
mg/L
H9/L
H9/L
H9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
12/14/06
IN
323
-
-
23.8
9.0
0.4
8.1
18.5
0.8
216
-
-
-
-
-
30.4
-
-
-
<25
1.5
AC
323
-
-
-
21.7
9.0
1.5
8.3
18.4
0.5
319
0.7
0.8
-
-
-
30.6
-
-
-
-
1,913
8.8
TA
317
-
-
<10
8.6
1.1
8.2
18.4
0.9
382
0.7
0.8
6.5
-
-
-
74
-
0.2
TB
317
<10
8.7
0.7
8.3
18.3
0.7
465
0.8
0.8
5.6
-
27
-
<0.1
TC
325
<10
8.5
0.3
8.3
18.4
0.5
486
0.7
0.8
-
-
-
5.2
<25
<0.1
1 2/20/06
IN
322
-
48.3
8.9
1.0
8.1
18.1
0.9
234
-
-
-
-
-
38.2
-
<25
1.3
AC
322
-
-
-
48.8
9.3
1.1
8.2
18.4
1.1
582
1.3
1.4
-
-
-
37.9
-
-
-
-
1,453
6.2
TA
316
-
-
-
15.1
8.7
0.7
8.1
18.2
1.3
574
1.3
1.4
10.4
-
-
-
-
124
-
0.6
TB
320
-
16.4
8.8
0.7
8.2
18.4
1.0
606
1.4
1.4
10.2
-
-
93
-
0.5
TC
320
14.3
8.5
0.6
8.3
18.4
0.6
617
1.4
1.4
9.9
98
-
0.5
01/03/07
IN
341
1.3
9
<0.05
40.8
9.6
0.5
8.1
17.9
1.0
277
-
40.4
18.0
22.4
36.2
32.2
4.0
29.7
2.5
32
42
1.4
1.8
AC
339
1.2
10
<0.05
39.7
9.3
1.4
8.1
18.1
1.1
305
0.6
0.7
39.6
18.0
21.6
34.9
10.3
24.6
<0.1
10.2
1,590
<25
6.1
<0.1
TT
327
1.4
9
<0.05
11.3
9.3
0.5
8.2
18.2
0.8
503
0.7
0.7
39.1
17.3
21.8
9.9
7.9
2.0
0.1
7.8
82
<25
0.4
0.4
01/10/07
IN
345
349
-
-
45.1
40.3
9.2
9.3
0.8
0.9
8.1
17.9
1.0
240
30.9
31.1
-
-
-
38
33
-
1.3
1.3
AC
328
339
-
41.0
41.9
9.3
9.1
1.8
1.7
8.3
18.3
0.7
293
0.7
0.8
32.3
31.8
-
1,810
1,811
-
6.8
6.7
TA
341
328
<10
<10
9.1
10.0
1.0
1.1
8.3
18.3
1.1
315
0.8
0.8
-
-
8.1
7.4
36
36
-
0.2
0.2
TB
339
328
-
<10
<10
9.1
8.7
0.9
0.9
8.3
18.2
1.1
325
0.8
0.8
-
-
-
7.2
6.7
-
8
7
<0.1
<0.1
TC
331
331
-
-
-
<10
<10
9.0
9.2
0.6
0.7
8.3
18.1
0.7
514
0.7
0.8
-
-
-
8.9
7.8
-
-
-
-
65
68
0.3
0.3
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
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
mg/L
mg/L
mg/L
H9/L
H9/L
H9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
(a) As CaCOS. (b) As P.
01/17/07='
IN
315
-
-
28.2
9.4
1.6
8.4
18.1
1.4
222
-
-
-
-
-
27.2
-
-
38
1.0
AC
292
-
-
-
50.3
10.1
3.1
8.2
18.1
1.5
251
0.4
0.5
-
-
-
40.2
-
-
-
-
3,438
13.5
TA
310
-
-
-
<10
9.4
0.8
8.1
17.8
2.6
277
0.5
0.5
5.1
-
-
-
-
<25
-
<0.1
TB
299
-
<10
9.1
0.5
8.2
18.0
1.4
287
0.5
0.5
5.5
-
48
-
<0.1
TC
302
<10
8.6
0.4
8.2
18.0
1.2
527
0.8
0.9
-
-
-
4.8
<25
-
<0.1
01/24/07
IN
276
43.3
9.3
1.4
8.3
18.1
1.2
257
-
-
-
-
-
33.5
-
40
2.0
AC
283
-
-
45.3
9.5
1.9
8.3
18.3
0.7
335
0.6
0.7
-
-
-
34.7
-
-
-
1,567
8.8
TA
280
-
-
-
11.4
9.2
1.8
8.3
18.2
0.9
338
0.9
0.9
7.8
-
-
-
-
115
1.0
TB
274
-
-
12.4
9.1
1.7
8.3
18.2
0.8
582
1.3
1.4
8.3
-
-
-
159
-
1.2
TC
270
13.0
9.3
0.7
8.3
18.3
0.6
617
1.0
1.0
7.9
-
162
-
1.3
01/31/07
IN
325
1.0
10
<0.05
109.5
9.1
0.5
8.2
17.5
1.1
259
40.7
15.5
25.2
39.9
38.1
1.8
38.3
<0.1
53
50
2.9
3.0
AC
318
1.4
9
<0.05
120.1
9.1
1.8
8.2
18.2
0.8
458
0.8
1.0
40.0
15.5
24.5
39.8
9.5
30.3
8.6
0.9
1,930
<25
12.4
1.0
TT
323
1.0
10
<0.05
79.0
8.5
0.4
8.2
17.9
1.1
578
0.8
0.8
38.0
15.2
22.8
13.4
13.0
0.4
10.1
3.0
71
<25
1.6
1.6
02/07/07 (d)
IN
335
-
-
-
38.6
8.8
1.0
8.2
15.4
1.3
226
34.1
-
-
-
-
34
-
1.5
AC
325
-
40.5
9.0
3.8
7.8
15.4
1.0
295
0.6
0.7
34.5
-
-
1,553
-
8.0
TA
327
<10
8.5
0.6
7.8
15.4
0.9
326
0.6
0.6
6.1
48
-
0.2
TB
327
<10
8.4
0.8
7.9
15.5
1.4
334
0.6
0.6
-
-
-
7.0
-
69
0.4
TC
330
-
-
<10
8.7
1.4
7.9
15.5
1.5
352
0.6
0.6
-
-
-
6.7
-
-
-
69
0.3
(c) AP reduced from 24 to 18 psi; stroke increased from 25 to 32. Target iron level was 2.0 mg/L. (d) Water quality parameters taken on 02/08/07.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a)AsCaCOS. (b) As P.
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
mg/L
mg/L
mg/L
H9/L
H9/L
H9/L
M9/L
M9/L
M9/L
M9/L
M9/L
M9/L
02/14/07
IN
325
-
-
50.4
9.1
0.7
8.2
17.4
1.1
247
-
-
-
-
-
30.3
-
-
-
43
1.6
AC
315
-
-
-
53.4
9.1
1.7
8.2
17.9
1.3
284
0.5
0.6
-
-
-
30.1
-
-
-
-
1,250
6.8
TA
318
-
-
-
17.1
9.4
1.1
8.3
18.1
0.9
317
0.7
0.7
6.5
-
-
-
<25
-
<0.1
TB
315
-
19.2
9.4
0.6
8.3
18.2
0.7
372
0.5
0.6
6.9
-
42
-
0.3
TC
315
16.5
9.0
1.6
8.3
18.1
0.8
418
0.6
0.6
-
-
-
6.8
60
-
0.3
02/21/07
IN
332
-
74.3
9.6
0.3
8.2
18.0
1.7
242
-
-
-
-
-
38.6
-
36
1.9
AC
327
-
-
-
86.3
9.2
6.0
7.9
18.1
1.2
282
0.6
0.7
-
-
-
42.0
-
-
-
2,617
16.7
TA
322
-
-
-
47.9
8.8
1.7
7.9
18.1
0.9
298
0.6
0.6
13.9
-
-
-
-
289
1.7
TB
322
-
-
48.1
8.8
0.4
8.1
18.1
0.8
313
0.6
0.6
10.3
-
-
101
-
1.0
TC
310
49.3
9.1
0.6
8.0
18.1
1.0
541
0.8
0.8
12.1
217
-
1.5
02/28/07
IN
330
1.5
9
<0.05
52.8
9.9
0.8
8.2
16.7
1.9
479
-
38.2
16.0
22.2
34.5
30.4
4.1
28.6
1.7
33
29
1.5
1.5
AC
325
1.5
9
<0.05
51.5
9.7
2.1
8.2
18.1
1.5
531
0.6
0.6
38.8
16.2
22.6
33.9
4.3
29.5
0.6
3.7
1,871
<25
10.9
<0.1
TT
322
1.4
9
<0.05
16.1
10.3
3.3
8.2
18.1
1.2
500
0.6
0.7
39.0
16.2
22.8
7.4
5.0
2.4
0.6
4.5
148
<25
0.6
<0.1
03/07/07
IN
337
-
-
-
33.6
9.2
0.8
8.1
17.7
1.1
327
33.5
-
-
-
33
-
1.4
AC
320
-
36.1
8.9
2.0
8.4
17.8
1.0
451
0.3
0.4
33.7
-
1,314
-
7.5
TA
317
<10
8.8
2.7
8.4
17.9
0.9
465
0.4
0.5
7.4
140
-
0.6
TB
324
-
<10
9.2
2.9
8.4
17.8
0.8
497
0.5
0.5
-
-
-
6.3
-
77
0.3
TC
317
-
-
<10
8.3
3.2
8.4
17.8
0.8
547
0.5
0.5
-
-
-
6.1
-
-
-
<25
<0.1
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
174a>
-
-
-
-
1 3,646^
10,937C)
-
59.2(c)
48.8(c)
TA
316
316
-
-
-
19.9
17.6
9.4
9.3
1.1
0.7
8.2
17.8
1.4
492
0.4
0.4
8.8
8.2
-
-
-
76
68
0.5
0.4
TB
316
318
-
-
18.5
17.3
9.2
9.3
0.8
0.7
8.6
18.2
0.7
532
0.4
0.4
9.0
8.9
-
39
34
0.3
0.3
TC
318
316
17.4
17.1
9.1
9.4
0.9
0.3
8.6
17.5
0.8
535
0.4
0.4
7.7
7.7
38
37
0.3
0.3
03/28/07
IN
320
1.5
10
<0.05
64.2
8.5
0.5
NA
NA
NA
NA
40.6
16.8
23.8
37.1
32.5
4.5
31.0
1.5
<25
<25
2.1
1.8
AC
312
1.5
11
<0.05
63.8
9.0
0.9
NA
NA
NA
NA
NA
NA
42.6
17.7
24.9
37.7
18.1
19.5
2.2
15.9
788
<25
5.4
0.4
TT
310
1.6
11
<0.05
32.3
8.8
0.8
NA
NA
NA
NA
NA
NA
40.2
16.4
23.9
12.8
10.3
2.5
1.8
8.5
<25
<25
0.6
0.2
04/04/07
IN
319
-
-
-
52.8
8.8
1.1
8.2
18.3
1.1
302
-
33.5
-
-
<25
1.3
AC
307
-
55.9
8.7
2.3
8.1
18.3
0.8
332
0.6
0.6
33.3
1,952
11.3
TA
310
22.5
8.4
0.5
8.2
18.4
0.6
429
0.5
0.6
8.5
<25
<0.1
TB
307
-
18.9
8.3
0.6
8.2
18.4
0.7
440
0.5
0.5
-
-
-
6.6
-
-
-
32
-
0.4
TC
305
-
-
-
20.0
8.7
1.0
8.2
18.8
0.7
411
0.5
0.5
-
-
-
7.0
-
-
-
-
85
-
0.6
(c) Data was questionable; however, were verified through re-analysis.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a)AsCaCOS. (b) As P.
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a) As CaCOS. (b) As P.
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a)AsCaCOS. (b) As P.
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a) As CaCOS. (b) As P.
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a)AsCaCOS. (b) As P.
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
(a)AsCaCOS. (b)AsP.
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
pH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO 3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L(a)
mg/L
mg/L
mg/L
H9'l_(b)
mg/L
NTU
S.U.
-------
Table B-l. Analytical Results from Long Term Sampling, Felton, DE (Continued)
Cd
Sampling Date
Sampling Location
Parameter Unit
Alkalinity
Fluoride
Sulfate
Nitrate (as N)
P (total)
Silica (as SiO2)
Turbidity
PH
Temperature
DO
ORP
Free Chlorine
Total Chlorine
Total Hardness (as CaCO 3)
Ca Hardness (as CaCO3)
Mg Hardness (as CaCO 3)
As (total)
As (soluble)
As (paniculate)
As (III)
As(V)
Fe (total)
Fe (soluble)
Mn (total)
Mn (soluble)
mg/L(a)
mg/L
mg/L
mg/L
ug/L(b)
mg/L
NTU
S.U.
°C
mg/L
mV
mg/L
mg/L
mg/L
mg/L
mg/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
ug/L
(a) As CaCOS. (b) As P.
10/24/07
IN
306
34.3
9.1
3.2
8.3
19.7
1.1
291
30.4
<25
1.4
AC
304
-
31.5
9.1
3.7
8.4
19.1
1.0
518
0.6
0.7
-
-
27.7
-
1,248
7.7
TA
302
-
<10
8.8
5.1
8.3
19.2
1.1
515
0.7
0.7
-
-
5.1
-
-
<25
<0.1
-
TB
296
<10
8.7
4.5
8.4
19.2
1.4
453
0.7
0.7
5.7
<25
<0.1
-
TC
300
<10
9.0
3.6
8.4
19.2
1.0
563
0.8
0.8
-
-
5.2
<25
0.1
-------
APPENDIX C
BACKWASH LOG SHEETS
-------
Table C-l. Backwash Operation (Vessel A)
Sampling Event
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
Date
1 0/1 3/06
11/30/06
01/03/07
02/07/07
03/07/07
04/05/07
05/09/07
06/05/07
06/14/07
07/11/07
08/08/07
09/05/07
1 0/1 0/07
After Filtration "TA" Backwash
Backwash Start
Time
9:18
11:48
12:28
14:11
13:14
11:59
13:57
13:01
11:44
12:12
13:26
11:51
13:20
GAL
32,311
64,414
86,882
115,268
148,208
195,528
275,107
297,955
305,409
330,885
360,213
387727
419,409
NTU
142.3
127.4
199.4
197.1
165.2
123.4
82.2
104.7
112.8
119.0
74.3
102.6
83.1
Backwash End
Time
9:29
12:58
12:38
14:18
13:21
12:05
14:02
13:06
11:49
12:17
13:31
11:56
13:25
GAL
32,944
65,044
87,520
115,730
148,630
195,874
275,552
298,389
305,847
331,300
360,649
388,094
419,849
NTU
5
4.2
4.9
17.3
16.7
14.7
10.5
9.3
14.2
15.1
10.8
15.1
7.7
Backwash
Flowrate
GPM
61.2
64.3
64.4
64.5
65.6
66.1
86.4
85.7
85.6
86.1
84.8
84.5
84.7
Backwash
Duration
Min
10.5
10.1
10.1
7.2
6.4
5.3
5.2
5.2
5.2
5.0
5.2
4.4
5.2
Wastewater
Generated
GAL
633
630
638
462
422
346
445
434
438
415
436
367
440
-------
Table C-l. Backwash Operation (Vessel B)
Sampling Event
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
Date
1 0/1 3/06
11/30/06
01/03/07
02/07/07
03/07/07
04/05/07
05/09/07
06/05/07
06/14/07
07/11/07
08/08/07
09/05/07
10/10/07
After Filtration "TB" Backwash
Backwash Start
Time
9:40
12:30
13:18
14:50
14:02
12:29
13:37
13:20
12:15
12:59
14:00
12:26
13:54
GAL
32,944
65,044
87,520
115,730
148,630
195,874
274,683
298,389
305,847
331,300
360,649
388,094
419,849
NTU
230.2
278.2
394.7
274.2
356.7
321.2
140.1
114.6
87.1
132.1
70.2
129.7
94.8
Backwash End
Time
9:50
3:40
13:33
14:58
14:09
12:37
13:43
13:25
12:20
13:05
14:05
12:32
13:59
GAL
33,508
65,665
88,427
116,199
149,100
196,349
275,107
298,784
306,221
331,720
361,003
388,509
420,235
NTU
9.3
9.2
8
17.8
14.6
14.1
13.8
14.6
14.4
13.6
15.3
12.9
14.6
Backwash
Flowrate
GPM
60.5
63.4
64.8
64.6
66.4
66.4
85.1
83.7
84.1
84.6
83.8
83.4
83.6
Backwash
Duration
Min
10
10
14.6
7.5
7.3
7.4
5.3
4.8
4.7
5.1
4.4
5.1
4.8
Wastewater
Generated
GAL
564
621
907
469
470
475
424
395
374
420
354
415
386
C-2
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Table C-l. Backwash Operation (Vessel C)
Sampling Event
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
Date
1 0/1 3/06
11/30/06
01/03/07
02/07/07
03/07/07
04/05/07
05/09/07
06/05/07
06/14/07
07/11/07
08/08/07
09/05/07
1 0/1 0/07
After nitration "TC" Backwash
Backwash Start
Time
10:08
13:18
13:55
15:22
14:40
13:01
13:14
13:45
12:44
13:43
14:32
13:01
14:46
GAL
33,508
65,665
88,427
116,199
149,100
196,349
273,995
298,784
306,221
331,720
361,003
388,509
420,235
NTU
212.2
219.8
286.8
268.3
251.9
230.3
110.5
116.1
95.8
116.3
105.3
72.3
110.1
Backwash End
Time
10:18
13:27
14:04
15:29
14:46
13:08
13:23
13:50
12:50
13:48
14:37
13:05
14:51
GAL
34,079
66,242
89,008
116,624
149,505
196,766
274,683
299,177
306,655
332,139
361,404
388,860
420,676
NTU
3.5
4
5.5
13.1
11.5
11.1
14.9
12.3
7.1
13.8
14.1
12.9
7.8
Backwash
Flowrate
GPM
61.4
64.5
65.4
65.2
66.8
67.1
86.5
85.7
85.8
86.1
84.6
84.5
84.6
Backwash
Duration
Min
10
9.4
9.3
6.6
6.2
6.5
8.4
4.8
5.2
4.9
4.8
4.3
5.3
Wastewater
Generated
GAL
571
577
581
425
405
417
688
393
444
419
401
351
441
C-3
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