AN EVALUATION OF THE COST
OF POINT SOURCE NITROGEN
LIMITS OF TREATMENT
IMPLEMENTATION IN THE
CHESAPEAKE BAY WATERSHED
March 2001
Virginia Tech
forthe
Chesapeake Bay Program
Clifford W. Randall, Environmental Engineering, Virginia Tech,
Blacksburg, VA
R. Copithorn and T. Young, Stearns & Wheler, LLC, Bowie, MD
-------
AN EVALUATION OF THE COST OF POINT SOURCE NITROGEN LIMITS
OF TREATMENT IMPLEMENTATION IN THE CHESAPEAKE BAY
WATERSHED
Clifford W. Randall, Environmental Engineering, Virginia Tech, Blacksburg, VA
R. Copithorn and T. Young, Stearns & Wheler, LLC, Bowie, MD
The purpose of this project was to perform a cost evaluation of implementing nitrogen
limits of treatment (LOT) technology at wastewater treatment plants (WWTPs) in the
Chesapeake Bay Watershed. LOT technology was defined as technology that would
produce a 12 month average effluent total nitrogen (TN) concentration of 3 mg/L from
each of the WWTPs. Most of this effort was a follow up to the evaluation of 51 WWTPs
performed under a previous project entitled, "Evaluation of Wastewater Treatment Plants
for BNR Retrofits using Advances in Technology". This project was performed by
Virginia Tech at the request of the Point Source Workgroup of the Nutrient Removal
Subcommittee of the Implementation Committee of the Chesapeake Bay Program from
1996-1999, and it was funded by Bay Program Funds administered through the USEPA
Region III Office. All 51 of those WWTPs were evaluated for this report, plus, a few
additional WWTPs were included, notably the Blue Plains WWTP located at
Washington, D.C., the largest WWTP in the Watershed. Altogether, 60 WWTPs were
evaluated for this report.
An Excel spreadsheet model was developed and used for determination of the LOT
upgrade costs for each of the 60 WWTPs. The summary page printouts for all 60 of the
WWTPs are included in Appendix A of this- report.
The WWTPs included in the 1999 report were evaluated for BNR upgrades that would
reduce the effluent TN discharges to less than 8 mg/L on a yearly average. •
Recommendations were made for upgrades that would accomplish this, and a 20 year
present worth cost evaluation was performed for each suggested upgrade option,
including multiple options for individual WWTPs. When multiple options were
provided, a preferred option was suggested for that specific WWTP. Lists of the
estimated costs for each of the preferred options are included with this report in Appendix
B. "During the evaluation* of this project and report, the LOT evaluations were performed
as if the 51 WWTPs ha'd implemented the preferred BNR upgrade recommended in the
1999 report. However, it was known that many of the plants had not implemented the
upgrades. Therefore, the cost of the upgrade for 3 rag/L TN recommended in this report
was combined with the cost of the upgrade recommended in the 1999 report to achieve 8
mg/L TN, unless the authors had specific information that the previously recommended
upgrade, or an equivalent upgrade, was being or had been made to that specific WWTP.
The capital costs and cost per pound additional N removal numbers for each of the plants
included in the 1999 report are included in Appendix C of this report.
i
The separate and combined capital costs and the separate and combined cost
additional pound of nitrogen (N) removed are listed in Table I of this report.
per
report. The
-------
operation and maintenance costs, and.the total 20-year present worth costs for each of the
WWTPs are listed on the summary pages for each WWTP, included in Appendix A.
Table 1 estimatesihat LOT could be implemented at these 60 WWTPs for an average
additional cost beyond 8 mg/L BNR of $2.58 per additional pound of N removed.
Excluding the Blue Plains WWTP, the cost would be $2.98 per pound.
It was known that upgrades were either underway or completed at seven! of the WWTPs.
These can be identified in Table 1 because the cost and nitrogen removal information is
omitted for them under the 8 mg/L heading. Also, cost and nitrogen removal information
is not listed for the nine WWTPs included in this evaluation that were not part of the g
mg/L evaluation and report. These nine plants are:
• Lewisburg, PA
• LockHaven,PA. I
• Bowie, MD
• Easton, MD
• Havre de Grace, MD
• Princess Anne (Fairmount), MD
• Western Branch, MD
• Blue Plains, Washington, D.C.
• Tyson Foods, Temperanceville, VA
Table I also includes the cost of implementing 8 mg/L TN technology at the 51 plants,
and combines it with the cost of implementing LOT technology at the 59 WWTPs of this
report, not including the Blue Plains WWTP. Then, the cost per pound additional N
removeitbecomes $2.40 per pound. This number is not precisely accurate, however,
because it includes flows for some of the S mg/L upgrades that are different from the
flows used for the same WWTPS when detennining the costs of the LOT upgrades.
However, it is reasonably representative, and does represent the cost of upgrading
WWTPs that currently are achieving average effluent TN concentrations greater than S
mg/L Note, however, that the cost per pound of N removed will be higher if the LOT
upgrade is made after the WWTPs are already achieving annual average TN effluent
concentration of <8 mg /L. This information is included in Table 2.
Note that the total capital cost for LOT implementation at the 60 WWTPs is estimated to
be $430 milLion. This includes the Blue Plains WWTP. The total 20 year present worth
cost for LOT upgrading of all 60 WWTPs, assuming that the 51 WWTPs have already
been upgraded to 8 mg /I., is estimated ‘to be $498.21 million (see Table 2).
The approach to the LOT cost estimations are summarized in the individual sheets for the
WWTPs included in Appendix A. The design flow, rather than the current flow was used
for all LOT estimates so that the full potential (or nitrogen removal as well as the full cost
would be included in the evaluation. The Blue Plains WWTP sheet is included as the
next page for illustration purposes. If the current average effluent TN was known
precisely, it was included with the flow so that an automatic calculation of the additional
nitrogen reduction LOT would accomplish would be calculated on a daily basis, and then
I
-------
summed for a year and for the 20 year amortization period. Note that when the Blue.
Plains costs were evaluated, it was known that the current WWTP as modified for BNR
can average an effluent TN concentration of 5.0 mg/L. Therefore, LOT will reduce the
effluent TN by only 2.0 mgIL. The known average effluent TN for the Bowie, MD
WWTP is only 4 mg/L, and LOT will reduce it by only 1.0 rng/L. By contrast. the current
Scranton, PA WWTP effluent TN averages 9.2 mgJL while the Rocco Farm Foods,
Edinburg, VA WWTP will average 12 mgIL TN after the BNR modification currently
being implemented is in place. It was assumed that LOT implementation would be
sufficient to reduce all of these effluents to an annual average of 3.0 mgIL.
It was further assumed that LOT implementation would not be possible at any WWTP
that was not nitrifying ammonia to less than mg/L ammonia-nitrogen. Therefore, if the
WWTP was not currently achieving an annual average effluent ammonia-nitrogen
concentration of less than 1.0 mg/L, it was assumed that LOT implementation cost would
include the cost of upgrading the WWTP to improve nitrification to that level.
Fortunately, most of the plants are already capable of achieving this level of nitrification,
so the number of plants that needed system or operational modifications was small. For
most of those not achieving complete nitrification, it is possible to increase the MCRT
(sludge age) and accomplish this change without additional capital costs. That is, for
most of the WWTPs in this category, the secondary settling basins were adequate for the
increased solids loadings that would result from increasing the MCRT.
Nearly all of the plants required some modification to reduce the nitrate nitrogen to the
1.0 mgIL effluent concentration required necessary to achieve an annual effluent TN
concentration of <3 mglL. The typical plant effluent contains 1-1.5 mg/L non-
biodegradable soluble organic nitrogen. This cannot be removed biologically, chemically
or by settling. Removal would require either activated carbon adsorption or reverse
osmosis type membrane separation, and this would greatly increase the cost over thc
nutrient removal technologies assumed for this evaluation. Therefore, the nitrate
nitrogen cannot significantly exceed 1.0 mgfL, and the ammonia-nitrogen must be less
than 1.0 mg/L, and preferably less than 0.5 mgI ! .., i(the LOlconcentration of 3.0 mgI!.. is
to be met.
The most common method recommended for upgrading the plants from 8 mg/L TN BNR
to LOT was the addition of denitrification filters with methanol addition. Few other
technologies are capable of LOT achievement, but it can be accomplished with
Bardenpho or modified Bardenpho treatment trains. The latter is being implemented at
the Fairmount WWTP, Princess Anne. MD, and the former is in place at the Parkway
WWTP operated by the Washington Suburban SaniLary Commission. However, the
operators have to want to operate to achieve the 3.0 mgFL TN goal. and the WWTPs
possibly will have to have effluent sand filters to achieve the goat.
The modification cost for the Blue Plains WWTP is for modi1 ying the existing deep bed
emuent filters to denitnfication filters and the installation of a methanol feed system for
them. The total capital cost is estimated to be $3 1.69 million, and the M&O cost increase
is estimated to be $1 .676 million per year. This results in a 20 year present worth cost of
-------
$56.82 million for LOT implementation at Blue Plains. However, it would reduce the
nitroge n discharge by 6,170 pounds per day, or more than 45 million pounds over a 20
year period, for a cost per pound of additional nitrogen removed of$ 1.26 per pound.
Additional information that was used to estimate the LOT implementation costs are given
in Table 2. This table lists the WWTPs by state, and provides summary data for each
state. Please note that this table is only for the èalculation of LOT costs, assuming that
the 51 WWTPs of the previous report had upgraded to 8 mgJL TN or less using the
technology recommended in the previous report. Exceptions to the 8 mgIL TN were the
two industrial WWTPs plus Scranton and some of the newly included WWTPs that were
not part of the 51 WWTP report.
The last page of Table 2 also includes a summary of the cost of LOT implementation for
the WWTPs categorized by size. i.e., design influent flow. Again, the costs here are
representative of upgrading WWTPs to LOT after they have already been upgraded to S
mg/L effluent TN. The summary on the last page estimates that the cost would be $2.58
per additional pound N removed forthe 60 plants incluØed in this report. If Blue Plains is
not included, the cost is $2.98 per pound. Mote that the cost per additional pound N
removed increases as the design flow p1 the WWTP decreases. The cost per pound N
removed was estimated to be 31.234 per pound for design flows greater than 50 MOD,
¶2.786 per pound N for flows between 15 and 50 MOD, increasing up to 54.108 per
pound N for WWTPS with design flows less than 1.0 MOD.
DISCUSSION OF RESULTS AND THEIR IMPLEMENTATION
It is recommended that the WWTPs be classified accqrding to their design flows rather
than their current flows for LOT implementation purposes. It is unlikely that there will
be a significant difference in the capital costs of the upgrades because all of the WWTP
owners will insist that the plant capacities not be downgraded. This means that sufficient
modifications will have to be made so that LOT can be achieved when the WWTPs reach
design flow. Consequently, the actual amount of N removal Lot implementation will
achieve will increase with time, but ultimately will approximate the removals calculated
using design flows. Thus, this approach would appear to be a more representative
approach over the coming 20 years than assuming current flows. If desired, a flow
escalation factor could be applied to the current flows, assuming they will reach design
flow in 20 years, to get a more accurate estimate of the amount of N that will be removed.
In this regards, it should be noted that some of the WWFPS included in this report are
already at design flow.
A logical approach would be to first try to classify all of the WWTPs in the Bay
Watershed in accordance with whether or not they are capable of BNR to S mgfL or less
at present. Following this classification, they should be classified in accordance with the
likely LOT technology.that would have to be applied to achieve an avenge effluent TN
concentration of 3 mg/L. For most of the WWTPs capable of BNR to 8 mg/L or less this,
the applicable LOT technology will be the implementation of effluent denitrification
filters, or the modification of existing effluent filters to denitrification filters. For
4
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example. of the WWTPs discharging to the James River and located in the Hampton
Roads area. several ofthemare BNR facilities capable of effluent TN concentrations less
than 8 mgIL. This includes the two Chesterfield County WWTPs, the Henrico County
WWTP, the HRSD-VIP WWTP, the HItSD-NaflSemOnd WWTP and the HRSDYork
River WWTP. Others, such as the Richmond 1 the HRSD Wiilian1SbUrg and the HRSD-
James River WWTPs could be easily upgraded for BNR. Some of the plants, such as
Henrico County, already have effluent filters that could be converted to denite filters, but
most of them would have to be retrofitted with effluent denite filters with methanol
addition. Along the Potomac River, all of the WWTPs that have to meet an effluent total
phosphorus (TP) concentration of 0.18 mg/L already have deep bed effluent filters. All
of these filters need to be converted to denite filters, which is somewhat less expensive
than the installation of denite filters where none currently exist. The point is that this
information is readily available for most of the large plants and they could be quickly
classified.
After the WWTPs have been classified in accordance with design flow and probable type
of LOT upgrade. the results of this report could be used to determine the typical costs of
upgrading for that classification. Then the cost of upgrading all of the WWTPs in that
classification could be quickly determined. Using this approach, a reasonably accurate
estimate of the costs of upgrading all of the WWTPs in the Bay Watershed could be
made.
JAMES RIVER WWTPs
There are several large plants along the James River of Virginia that have not been
included in any way in the preceding parts of this report. Seven of the largest James
River WWTPs arc listed in the following table. I was personally involved with the
development of BNR designs for all of them except the Richmond WWTP, and I
included it because it is the largest discharging to the River. Because I am aware that five
of these WWTPs have already implemented BNR and the sixth is under construction
(1-lopewell) , I decided to perform an economic evaluation of what it would cost to
upgrade all seven of the WWTPs for LOT. All of the I3NR upgrades implemented or
being implemented are capable of discharging yearly average TN concentrations of 6
rng/L. Therefore, the additional N removal calculations were based on the reduction
from 6 to 3 ing/L. To the best of my knowledge, BNR. treatment has not been
implemented at the Richmond WWTPI but it is possible that plans for modification are
underway.
Table 3.The Estimated Cost of TN
Des. increased Increased
WWTP Flow Cap. Cost M&O Cost
mgd 5, mill. 5. thou/year
l.948.4
Incr. 20 -yr Ad’l 20 yr. Cost/lb
Pres’t Worth TN Rem. ad’l TN
S. millions Ibs, millions rem...Sflb
75.42
39.566’ 1.91
Richmond
50
46.2
—
54.52
9.125
5.97
Hopewell
50
2.s:L_
—
796.7
8.02
41.48
7.3
1.10
Henrico
40
4.06
—
73
S.68_
HRSD-VIP
40
— 30.39
7393
—
5
-------
HRSD-Nan
30
2326
556.9
31.61
5.475
5.77
Proctor’s
Creek
20
16.16
377.6
21.82
.
3.65
5.98
Falling Ck.
10
9.05
195.2
11.98
1.825
6.56
TOTALS 240 171.69 5,049.7 244.85 74.241 3.30
The table shows that upgrading most of the WWTPs that already have BNR upgrades
will be relatively expensive as determined by the cost per additional pound of nitrogen
that will be removed. Thai is because all of these WWTPS are capable of producing an
annual average effluent concentration of 6 mg/I , or less as currently constructed or
planned. The exception is the Henrico WWTP because it already has effluent filters, and
the cost will be for modi&ing them rather than constructing them. The cost per
additional pound of removal at the Richmond WWTP is low because it was assumed that
this WWTP is currently discharging a TN concentration of 16 mg/L. The actual
concentration was not known when this estimate was made.
The summaiy work sheets for the James River WWTPs are included in Appendix A of
this report.
6
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TABLE 1. THE COST OF IMPLEMENTiNG UM1 S OF TREATMENT NITROGEN REMOVAL IN THE CHESAPEAKE SAY WATERSHED
Total
9.56
12.763
6.347
24.09
5.19
25.448
24.167
11 659
3.63
4 59
16.135
1.3
12 079
10.24
15949
15.006
25 453
1286
236.46
8mg!L
0.51
042
2.69
324
0.08
2
0.19
1.19
076
033
1.12
1.68
1.36
2.58
o 18
042
0.91
Pennsylvania
Design Flow
BNR Capital Costs, MIllIonS
$ per lb N
Removed
bOOs lb N Removed
Tot. Nrem
Total $ per
WWTPs
mgd
SmgIL. 3mg!L
3nigIL
OniglL 3nigIL
l000lbs
lbNRem.
PJtoona East
9
1.23 8.33
4.15
3165 2740
5925
2.19
Altoona West
13.5
1.233 11.53
4.82
3880 3288
7168
2.44
Chambersburg
6.8
6.347 0
0.48
2841 414
3255
2.41
Greater Hazleton
8.9
7.84 16.25
8.19
3860 2701
55
5.28
Hanover
4 5
0.06 5 13
8 19
3046 803
3849
1 77
Hamsburg
30
25.448 0
0.47
. 27635 1826
29461
1.9
Lancaster City
29.7
1.077 23.08
3.66
9230 9052
18282
1.9
Lebanon
8
4.039 7.62
4 35
4652 2435
7087
3.4
Lewisburg
Lock Haven
24
3.75
- 3.63
- 4.59
1.31
2.42
- 4904
390
4904
390
1.31
2.42
Scranton
16
2.815 13.32
3.2
4464 6059
10523
2.16
UAJA. St. College
8
078 0.52
0.78
3330 1825
5155
0.49
Susq.Lanc. Area
12
1.619 10.46
4.01
2288 3650
5938
2.9
Throop
7
3.32 6.92
4.46
1982 2117
4099
3.12
Wm’portCentral
72
6.339 961
1.86
6600
6716
13316
1.61
Wrn’port West
4.5
5.246 9.76
9.01
.
3200 1387
4587
4.52
Wyoming Valley
32
0.763 24.69
3.65
5575 9709
15284
2.38
VorlcCity
TOTALS
26
227.25
1.78 11.08
69.94 166.52
229
3,41
5806 7884
91514 63486.4
13690
155060.4
1.5
2.28
Maryland
DesIgn Flow
BNR Capital Costs, MillionS
$ per lb N
Removed
lOGOs lb Ad’l N Rem.
Tot Nrem
Total $ per
WWTPS
mgd
8 mg!L 3 mgIL Total
8 mglL
3 mg!L
8 mglt. 3 rnglL
1000 lbs
lb N Rem.
.Bowie
22
- 0.52 052
-
808
- 73
73
8.08
Brunswick
07
0.39 2.65 304
0.5
14.2
530 219
749
4.51
Chestertown
09
1.35 0.1 1.45
5.92
0.38
247 292
539
2.92
Crisfield
1 2
1.949 2.78 4.729
495
916
379 365
744
7.06
Easton
2
- 5.7 5.7
-
9.81
- 730
730
9.81
Elkton
27
. 1.97 0 1.97
187
OM
1452 803
2255
1.37
Federaisburg
0.75
0.75 2.65 34
334
5.16
507 657
1164
4.37
Georges Creek
0 63
0.6 2.65 3.25
3.55
10 82
457 292
749
6 38
HavredeC3race
19
- 3.3 33
-
7.16
- 584
584
7.16
Indian Head
05
0.49 0.52 1 01
2.9
3.ii
219 219
438
3.01
Mattawoman
15
- 0 0
-
0
- 0
0
0.00
Princess Anne
1.26
- 2.61 2.81
-
2.68
- 383.25 383.25
2.66
WestemBranch
1663
- 0 0
-
048
- 5037
5037
0.48
Winebrenner
06
0.6 0 06
3.77
0.45
411 511
922
193
TOTALS
46.97
8.1 23.68 31.78
1.31
2.91
4202 10165.25
14367.25
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8 mgIL.
0.09
0.03
0
0.05
0
0
0.15
0.57
0097
30
2
0.325
3
3
‘05
2
4
16
1.2
18
4.85
67
2
4.5
6.25
2
I
15
1.2
0.975
14
I
4
I
1
193.2
3 mglL
6.01
3.36
0.52
1 06
1 06
0.54
3.36
4.79
13.32
0
3.8
5.39
12.76
3.36
5.13
6.39
3.36
0.52
12.59
2.78
2.65
0.52
2.65
0
052
265
99.09
NEW YORK
Design Flow
BNR Capital Costs, Millions
$ per lb N Removed
l000s lb Ad’l N Rem.
Tot. Nrem
Total
WWTPs
Btnghampton
mgd
25
8 mgIL 3 mgIL Total
- 19.72 19.72
$ mgIL 3 mglL-
- 3.7
8 mgIL 3 rnglL
- 7610
1000 lbs
7610
per
lb N Rem.
3.7
Endicott Village
8
6.656 0 6656
3.35 0.47
3292 2435
5727
2 13
TOTALS
33
6.656 19.72 26.38
3.35 2.92
3292 10045
13337
3.32
VIRGINIA
Design Flow
BNR Capital Costs, Millions
$ per lb N Removed
l000s lb Ad’l N Rem.
Tot. Nrem
Total $
ww’rps
.
-
8 mgIL 3 mg!L
8 mg lL 3 rnglL
1000 lbs
per
lb N Rem.
Arlington
- 1 21
- 9125 0
9125.0
121
Colonial Beach
-0.065 8.22
431 511.0
Dah lgren
-012 808
218 73.0
2910
4.06
1.94
DaleServices#1
- 245
- 5840
5840
Dale S.,jvices #8
- 2.45
- 584.0
245
DupoinWboro
-0.11 0.9i
3,184 1387.0
45710
2 45
Fisheraville
- 8.22
260 511 0
771.0
020
8.22
Front Royal
0.02 5.12
1023 1241.0
2264.0
282
Harrssonburg
- 6.13
- 2920 0
2920.0
Merck, Elkton
0 047
- 2847.0
2847.0
0 47
H.L Mooney
- 1.25
- 5475.0
5475.0
1
Leesburg
- 6.06
- 116&0
1168.0
Lower Potomac
- 1.17
20367.0
Luray
0 822
- 511.0
511.0
117
Middle RiverNer,
0.3 11 03
420 584.0
822
Opequon
0.16 4.59
5328 1898.0
1004.0
634
Parkins M I I I
-0.79 p276
200 1219
7226.0
321.
1.32
Purceilville
- 3 ,06
- 219 0
99
Rivanna River
- 4.75
- 3650 0
219.0
3 06
Rocco, Edinburg
- 5.36
8140 657 0
3650.0
4 75
Strasburg
-0.14 21.58
4366 1460
8797.0
5 36
Stuarts Draft
2.36 4 52
484
4512.0
056
Tyson, Temper.
- 2.46
630.0
2 86
Waynesboro
1.27 0.48
3548 1241.0
1533.0
2.46
Wilderness
- 2.5
- 292 0
292
47890
1 07
Woodatock
‘ -0.22 11.03
292 0
2 5
TOTALS
0.48 2.49
292.0
27894 58084
584 0
85977.9
5 41
2.51
Design Flow
mgd
500.42
BNR Capital Costs, MillionS
8 mgIL 3 mgIL Total
89.369 309.01 398.382
GRAND TOTALS
$ per lb N Removed
8 mgIL 3 mgIL
0.94 2.98
bOOs lb Ad’i N Rem.
8 mgIL 3 mgiL
126962 141780.56
lot. Nrem
1000 lbs
268742.56
Total $ per
lb N Rem.
Total
6.01
3.45
0.55
1.06
1.06
054
3.36
4.84
13.32
0
3.8
5.39
12.76
3.36
5.28
6.96
3.457
0.52
12.59
2.76
2.77
0.52
2.65
3.5
0.52
2.72
103.77
0 12
3.5
0.07
4.68
Blue Plains, DC 370
- 31.69 31.69 1.26
45041 45041 1.26
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• TABLE 2. WORKSHEET FOR DETERMINATION OF COST OF LOT UPGRADES FOR CHESAp 1(r BAY WAT D I n WWTPs
PLANT
Design
Flow
MCD
BNR
Conrug.
Reco-
mend.
Mod.
SRT
Days
Design
Temp
Effluent
NH 1 -N
mgfL
MLSS
75% VS
mg/L
Nitrate
Recycle
BNR
EU.
N0 1 -N
Add’IN
R •m.
LhsId
Capital
Cost
S Mu
Ann.
O&M
S K
20 yr.
Aniort.
$ Mu
Sper
Add lb
N rem.
PEN
NSYLVA
NIA
Altoona
East
9.0
MLE
Denite
Fillers
15
I2
0.8
2550
3Q
(13Q)
6.5
75 3
8.33
212.4
11.52
4.15
Altoona
West
13.5
MLE
Denite
Filters
14
12
0.9
3524
3Q
(1 .5Q)
5.5
450.4
11.53
286.9
15.83
4 82
Chamber
sburg
6.8
TF-
DeniteF
Addl
Math.
-
10
‘
<1.0
•
-
Remove
I mg/L
56.7
0
14
0.21
0.48
(;rca,cr
Iladeton
8.9
BAF-
Denit F
Add
BAF
-
10
cl.0
3500
-
6.5
370
.
16.25
390.4
22.11
.
8.19
Hanover
43
.
OD
Denite
Filters
20
10
.
<1.0
5000
>50Q
4.5
110
5.13
96.5
6.58
8 19
Harris-
burg
30
Unox
Add’I
Meth.
-
10
<1.0
3600
3Q
Remove
I nig/L
2502
0
56.4
0.85
047
La,icaster
. !
297
•
MLE
Denite
Filter
15
10
<1.0
N/a
2Q
6.5
1240
23.08
663.5
33.03
3.65
Lebanon
8.0
IF-AS
Denite
Fitters
15
- tO
<1.0
4000
2Q
6.5
333.6
7.62
190.3
10.47
4.35
Lewis-
berg
24
A2/Ow
Denite
Filters
25
12
<1.0.
4750
2Q
1.5
490.4
3.63
69.7
4.68
- 1.31
Lock
Haven
3.75
•
A2/O
Denite
Filters
25
12
<1.0
4500
3Q
13.5
390
4.59
153.6
.
6.89
242
Scranton
16
•
MLE
Denite
Filters
IS
10
.
1.2
2300
3Q
7.7
83(1
1332
404
19.37
3.20
UAJAI St.
1 l g __
6 0
MLE w
Filters
>SRT,
Meth.
15
12
3 2
3000
2.5Q
65
25u
032
60 6
1.43
0.78
Sus’hann
Lanc area
12.0
MLE
Denite
Filters
15
.
10
<1.0
3600
l.5Q
6.5
500
1046
279
14.64
4.01
Throop.
Lack area
70
MLE
>SRT
IS
12
2.4
2300
2Q
6.5
290
920
6.92
168.2
9.44
4.46
Wm’pnrt
Central
72
MLE-
Cony.
N-DN
BAF
12.5
Ii)
16.7
4000
2.SQ
0’
961
193.5
12.51
1.86
Wm’port
West.
4 5
MLE
N-DN
BAF
15
10
1.6
4500
3 Q
6.5
190
9.76
l82.4
12.50
?.0l
W omiag
Valley
32
Schreib-
MLE
Denite
Filters
12
8
<1.0
2750
IQ
6.5
1330
24.69
716.9
______
35.44
.
3.65
York City
26
MLE
Borden
-pho
15
10
0.5
3600
-
IQ
6.5
1080
11.08
465.4
18.06
2.29
TOTALS 227.3 9461.6 166.52 4603.7 235.56 3.41
()current maximum recycle rate eIncc,mpI e nitrification
-------
PLANT
Design
Flow
MGD
BNR
Conrig.
Keco- SRT
mend. Days
Mod.
Design
Temp
C
Elf
NH 4 4 -N
mg
MLSS
75%VS
mg/L
Nitrite
Recyde
B1%IR
FIT.
NO,-N
Add’I N
Rem.
Ibsld
Capital
Cost
S Mu
Ann.
O&M
S IC
20 yr.
Aniort.
S per
AdcI.lb
MARYLA
ND
$ MU
N rem.
Bowie
2.2
A210
CD
Denite
Filters
15
12
0.2
.
4000
>50Q
15
10
0.52
49
0.59
8.08
Bruns-
0.7
Cyclic
Denite
11.2
12
<1.0
3500
30
6.5
30
265
304
3.11
wick
aeration
Filters
14.20
Chester-
0.9
. Biolac
improve
-
8
3.0
-
-
6.5
40
0.1
0.8
town
lagoons
lagoons
0.38
Crisfield
Easion
1.2
2.0
Step
A2/O
Over-
land I I.
Denite
Filters
N-deN
IJAF
-
13
.
5
0.1
3.4
3000
-
2Q
-
-
6.5
1.9
TN 9.1
50
100
2.78
5.7
39.7
97.1
3.38
7.16
926
9.81
Eihton —
2.7
BAF-
DeniteF
Add
Meth.
-
10
<1.0
-
6.5
110
0
25.4
038
0.47
Federals-
0.75
TF-Den.
Addi
-
12
0.2
-
-
3
90
2.65
492
Butt
Filters
Meth.
3.39
5.16
Georges
0.63
2 Step-
Denite
15
9
<1.0
2700
3Q
8
40
2.65
34
3.16
Creek
MLEs
lilters
-
10.82
Ha rede
1.9
MLE w
-
Dcniie
15
10
<1.0
3000
2Q
.6.5
80
3 30
589
Grace
RBCs
Filters
4.18
7.16
Indian
0.5
A2/O
DeniteF
7.2
14
0.5
3000
3Q(I.5)
85
30
0.52
Head
ifters
.
100
0.68
3.11
Matta-
15
Barden-
Add’l
20
12
<1.0
3000
>S OQ
1.0
0
0
— -
0
Woman
Pria. An.-
.
1.26
pho OD
5-Stage
Meth.
Constru
-
- 12
<1.0
3000
1-3 Q
16
160
.
2.81
0
0
Somerset
Barden.
ction
TN 18
21.6
3.13
2.68
County
phoM
.
Western
16.63
MLE w
.Add’l
10
12
<1.0
3000
3Q
65
690
Branch
DeniteF
Meth.
2.41
0.48
Wine-
0.6
RBC-
Denite
-
12
0.6
-
-
14.5
70
brenner
DeN F
Filters
0
15.5
023
0.45
TOTALS
46.97
NEW YORK
- 1500
23.68
5487
31.91
2.91 -
Bingham
pton
25
MLE-
BAF
DeniiF
.Meth
-
10
<1.0
3000
IQ
6.5
1042.5
19.72
561.8
- 28 15
.7O
Endicott
8.0
-
IF-SC
Denitc
-
10
<1.0
-
-
6.5
333.6
c !Y
Filters
0
76.1
0.47
TOTALS
33.0
1376.1
19.72
Arlington
.
30
Step
Addi
10
.
12
<1.0
VIRGIN
4000
0 — 6.5
.
1250
637.9
- 29.29
—
2.92
Colonial
MLE
Meth.
6.01
336.2
11.05
1.21
2
Alt. Ac;
Denite
IS
12
03
3000
none
5.5
70
-
—
Beach
•_______
•Atrn ic
Filters
55.U
4.2
8.22
-------
PLANT
Design
Flow
BNR
Conrug.
Reco.
mend
SRT
Days
Design -
Temp
EtC. .
NH -N
MLSS
75%vs
Nitrate
Recycle
DNR
£11.
N0 3 -N
Add’IN
Rein.
Lbsld
Capital
Cost
S Mu
Ann. I
O&M
S K
20 yr.
Amort.
Mu
Sper
Add.lb
N rem.
Dahlgrcn
MCD
0.325
Orbal 3
rings
Mod.
EQ&
Mcd i
>30
C
12
mWL
0.9
mgIL
9000
>50Q
4.5
10
0.52
1.06
49
248
0.59
1.43
8.08
2.45
DakSer-
3
MLE
Denite
15
12
<1.0
5300
4Q
4.5
vices UI
pH Ad.
Filters
.
I 06
248
143
2.45
D leSer-
3
M1.E
Denite
iS
12
<1.0
5300
4Q
4.5
80
vices #8
pH Ad.
Filters
.
1400
SQ
47
190
0.54
49.2
1.26
0.91
DuPont
0.5
Barden-
Consir
15
20
<1.0
W’boro
Fishers-
2
pho w
Meth.
A2/O-
ucilon
Denite
15
12
<1.0
3000
3Q
5.5
.
70
3.36
55.9
4.2
8.22
vilk
MLE
Filters
170
4.79
104.4
6.36
5.12
Front
4.0
Alt Ano
Denite
IS
12
0.3
3000
none
6.5
Ro al
-Mr
Filters
.
3000
. 4Q
4.5
400
13.32
304.4
17.89
6 13
harrison-
16
A2/O w
Denite
12
12
<1.0
burg
Fermen.
Filters
3.8
202 8
684
1.25
ILL.
18
Step
Add’l
19
12
<1.0
2200
0
6.5
Mooney
MLE
Mcdi.
5.39
112.5
7.08
6.06
Leesburg
4.85
A2/O
Denite
Filters
12
12
<1.0
3500
3Q
0
5.5
6.5
2790
12.76
744.9
23.93
1.17
Lower
67
Step
Denite
8.3
12
<1.0
2700
.
Potomac
MLE
Filters
—
70
3.36
55 9
4.2
8.22
L.uray
2.0
OD
Denite
Filters
40
12
<1.0
4300
>50Q
—
5
390
0
90.2
1.35
0.47
Merck,
1.2
Bardcn-
Defile
10
25
<1.0
4100
4Q
Elkion
pho —
Filters
3
80
5.13
873
6.44
11.03
MIddle
4.5
- OD
Add
25
12
<1.0
5000
>50Q
RiverlVer
Meth
155
8.71
4.59
Opequon
6.25
Step
Denite
12
12
0.4
3000
3Q
6.5
260
6.39
Wla’chest
A210
Filters
167
3 36
446
4.03
27.6
Parkins
2.0
Bio-De-
Denite
20
12
<1.0
3000
> S OQ
25
Mill
Purcell-
1.0
nitro. 1
ft Fillers
Step
Filters
Add
15
— 10
.
<1.0
3000
3Q
4.5
30
0.52
9.8
0.67
3.06 —
ville
MLE-F
Meth.
12.59
3159
17.33
4.75
Rivanna,
15
A2/O-
Denite
15
11
0.5
3000
2Q
5.0
500 •
Cbar’vl lle
MLE
Filters
2.78
496
352
5.36
Rocco
1.2
A2/O-
Denite
53
10
<1.0
4000
1 OQ
10
90
Foods,
Sch’ber
Filters
Ed.
2.65
33.6
3.15
1.58
Strasburg 0.975 OD Denite 25 12 <1.0 4000 > S OQ 4.5 20
i__Filters
-------
PLANT
Design
l low
MCD
BNR
Config.
Reco-
mend
Mod.
SRI’
Days
Design
Temp
C
U I.
NH -N
mg/L
MLSS
75%vs
mg/L
Nitrate
Rec3cIe
BNR
Eff
NO -N
Adcl’l N
Rem.
Lbs/ti
Capital
Cost
S MU
Ann.
O&M
20 yr.
Amorl.
$ per
Add.lb
S marts
Dr i1t
3.4
OD
Add
Meth.
25
12
<1.0
5000
>50Q
3.5 .
20
052
9]
- S Mu
0.66
N rem.
4.52
Tyson
Foods
1.0
MLE
Denite
Filters
50
14
0.3
4000
4Q
28
210
2.65
745
377
2.46
Waynes-
boro City
40
TF-
RBC.
Filters
Add
Meth.
.
12
1.2
.
-
-
6.5
170
0
394
0.59
0.48
Wilder- —
!i!
3.0
Orbal4
Ring_
Add
Meth.
<1.0
>500
40
0.52
141
073
2.50
\uod-
slink
rA -—
TOTALS
1.0 .
OD
Deni le
l ilt i
•
•
0.5
3200
>50Q
40
2.65
379
3 22
11.03
193 ,2
7956.7
99.09
3037.6
144.63
2.49
GRAND
TOTALS
500.42
. ..
20294.4
309.01
8827.9
443.39
2.98
Blue
Plnins, .
DC
370
3 stage
BNR w
eff. Flit,
Conv’t
to deN
filters
-
12
.
<1.0
.
- 1
______
None
3.5
6716
31.69
16757
56.82
1.26
Rcvised
TOTALS
870.42
.
26466
340.7
10,504
.
498.21
2.58
TOTALS BY SIZE CATEGORY
>50 mgd
437.0
#of plants ‘=2
8961.6
8D.75
9(1.4
— 1)8.1
ifl2.3
-
15 .5oingd
269.3
-.
# f plant, 11
9362.7
44.45
127.61
2420.6
1.234
-
5-J!rn d
<1 mgd
92.7
65.6
5.9
#oIplants — ii -
oFplants —27
of plants ‘=9
4139.6
3477.1
522.8
77.6
78.7
12.3
2026.4
1571.5
2.786
3.577
4.030
Total Plants 6O
-------
APPENDIX A
SUMMARY SHEETS FOR COST
ESTIMATIONS FOR THE 60 WWTPS
PLUS 7 WWTPS IN THE JAMES RIVER
BASIN OF VIRGINIA
7
-------
PROJECT: ImplementIng p3 mgIl. Annual Average TO W Nitrogen Until
PREPARED FOR: USEPA. Chesapeake Bay Office
PREPARED BY: Virginia Tech w Ith Steams & Whaler. LLC
DATE: March 24.2001
FACILITY: Bk. PIaInIWWTP
LOCATION: Wa hlnot0n DO
RATED FLOW: 370.9 ingd PE COD l i la mgfl.
CURRENT EFFLUENT TN. 5.0 mg I. PE TKN rnglL
EFFLUENT TN GOAL: 30 mgI.
NITROGEN REDUCTION: Sl iD bald
2252 1000 Itislyr
45041 1000 Ibst2O-yeers
CURRENT PROCESS (CHECK ALL THAT APPLY): : MLE Existing Aerated Volume (MO). I’Ua
— BEPR (P210. VIP. etc Existing Momc Volume (MG) P ile
— Bardenpho Current t&SS at Winter ADF N b
— Oxidation Ditcti
— Lagoon (Blolac etc)
— C dIeal Aeration
S SR
— High-Rate Biolilter
El1’uent Filtration
A Othet BNR Stistem with Methanol Adddlon
CURRENT EFFLUENT AMMONL4t4: c1.0 mg I. Fiom Report
From Model (at ADF aS Sd. 15 d MCRt it C wider conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA c I i mgiL
No modifications requited New MLSS
I . Ra Ise MCRTIMLSS In existing tanks (check cisritier capacity) W1
[ Construct additional aerated volume Flow (mgd) ________
[ Cànstiud additional dslflers Flow (mgd): -
a Use existing anoat vdtalle as aerobIc (corsiluct sepia denli fpcãty)
41 Use aerated system for BOO removal only (construct separate nltldenit facilgy)
Add Intluent Sow equalization lank
..Otec l:1 \i ,‘ .
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 LI:
No modifIcations required
1. Add downstream teNt Mlervnth methanol
;A Add downstream NSt tiOe &ofllter and DeNt rifler with methanol
Add methanol to existing SNR prcceee
Add dowytatrealil anoic lank welt niethanot feed
Add effluent filtration
0 0w ’- Convert efluu* filters to den lt titers and add more methinol there
CAPITAL COST: Equipment and Structures (from Page 2) $15.600.000
Elec tncal and InstrumentatIon 12% $1 872.000
Yard Piping and Site Work: t5% $2340000
SubtotaL $ 10110000
Contractor OII&P 15% 129 72.000
Engmeenng and Corstr Mgmt 15% 12.972.000
Sittotat $25750000
ContIngency. 30% $5943000
Total Capital Cot $31 A10 C00
CapItal Cost perth 20-Yr. N removal $0.70
OPERATIONS COST: Additional Ikgsapis ( 1 1 cm Page 2). 0 HP
Electrical Power CoaL 00S 3 1kW 30 $l ear
Nitrate Reduction using Methanol t0 mgfL
Methan ol Requued 2110 galsld
Methanol Cost. 0.75 SIgal 1759.200 $lyear
Separate stage Ammonia Reduction 0.0 mgIL
Caustic Soda a 25% cone. 0 galsld
Caustic Soda Cost 060 $lgal $0 $lyesr
Equipment Maintenance Cost 5251 500 $lyear
Denitnficatlon Sludge Production wtMethanol 5390 Ibsid
Sludge Disposal Coat 400 1/ton 5649 000 5/year
Total Annual OW Cost • 51.675 200 Ityesr
Effective Annual Interest Rate alter Inflation 291%
20-Year Present Worth o r OW Costs 325. 130.000
TOTAL 20-YEAR PRESENT WORTh COST. 155.020.000
Total Cost per lb 20-Yr. N removal 11.25
Okse Plains. DC xis Page I o12
-------
SUMMARY COST SHEETS FOR THE
18 PENNSYLVANIA WWTPS
7
-------
.‘ROJECT Implenientinga3 mglL Annual Average Total Nitrogen Lintit —
PREPARED FOR: USEPA. Chesapeake Bay Office
PREPARED BY: Virginia Tech with Steams 1 Whiter. (SC
DATE March 13,2001
FACILITY Altoona East WWTP —
LOCATION. Aileona, PA PE C0005 77 mg!L
RATED FLOW 9 omga PECOO 213 mgii
CURRENT EFFLUENT TN fl,_, mg#t. PE TKN 15 mglL
EFFLUENT TN GOAL. 30 . mg/t
NITROGEN REDUCTION: 300 ibsld
‘30 1000 lbs /yr
2 nd 1000 Ibs/20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): 1 PALE Existing Aerated Volume (MG) 227
: BEPR . ic. , Existing Anoxic Volume (MG); 0,75
— Baroenptio Cwrent MLSS at Winter ADF. 2200
— Oxidation DiWi
— Lagoon (BIotaC.etc)
Cydicai Aeration
SBR
I High-Rate &ofilter
— Effluent Filtration
Other ____________________________________________
CURRENT EFFLUENT AMMONIA-N: . 10 mge’(. From Report
- . From Model (at ADE and load. 15 d MCRT. 12’ C winier conditions)
PROPOSED MODIFIOAUONS TO GET AMMONIA c LU mglL:
X Nbmodirca (ions required . New MLSS
Raise MCRTMLSS in existing tanks (check clarifier capedty) 3000
Construct additional aerated volume Flow (rngd) 0
Conatruci additionsJdarlllecs Flow (mgd) 0
Use edsling anoxic volume as aerobic (corislruci separate denit fadlity)
- Use aerated system for BOO removal only (construct separate ntldenut facility)
Add inluent flow equalization tank
Other _____________
PROPOSED MODIPICA11ON5 TO GET NITRATE c 1.0 mgIL:
No modifications required
A do#mstraam OeNil fitter with methanol
• downstream Nfttlflcetlon Ulofluler and DeNit fitter with methanol
S. msthanolbexisltngBNRproCesa -
• dawwbeam angSt tank with methanol feed
elitisM fiwatlon
- - rc ’ • ‘ :je’ • •
CAPITAL COST: Equipment and Stxvctureajftom Page 2) 54.100.000
ElechiS and InstrumentatIon 12% $492,000
- Yard Piping and Site Work 15% 5615.000
SifloS_I $5,210,000
Cflactor OH&P - 15% 5752.000
Engh earlng and Constr. Mgmt 15% 575200
&ibtotst 86.770.000
Contingency 30% 51.563.000
Total Capital Coat $8,330,500
Capital Coat per lb. 2 0 -Yr N removal 13.00
OPERA ONS COST: Additional Horsepower (from Page 2) 1 50 HP
Electital Power Cost OAtS 5 1KW 556 900 $Iyear
Nitrate Reduction using Methanol so mgfl.
Methanol RequIred 170 ga lsM
Methanol Cost. 075 $Igal 54000 $I ear
Separate Stage Ammonia ReductIon 60 iIlgIL
CatistlcSoda @25% WnC Ogatsld
Caustic Soda Cost 0.60 $1951 SO Slysar
Equipment Maintenance Cost $07,700 $Iyear
Denltnt’icaiton Sludge Production wiMetttanol 540 t iM
Sti i dge Disposal Cost • 400 fln 831.400 SWaf
Toed Annuat OSM Cost 1212400 $ ear
Eltedive Annual Interest Rate alter Inflation 2.91%
20-Year Present fl (3574 Cafl 13,110.000
TOTAL 20-YEAR PRESENT WORTH COST: $11,520,000
Total Costpert 20-Yr. N removal. $4.15
Altoona East xis Page 1 of 2
-------
R JECT. knplemeedng a3 mgit. Aiwiusl Average Total Niftogen Umi
PREPARED FOR: USEPA, Clissapaka Bay Cities
PREPARED DY: VirgIala tech with Staans& WIISIN. tIC
DATE: March 19. 2001
FAC 1UTY : AJo055 West WW1P
LOCATION: 15. PA
RATED FLOW: itS mgd PE COD NM mgfl.
CURRENT EFFLUENT TN TO mgIL FE TICK. NM u1 WL
EFFLUENT TN GOAt: 30 mgIL
NITROGEN REDUCTION 450 bald
154 1000 lbs /V T
3205 1000 lbs/20-yeWs
CURRENT PROCESS (CHECK ALL ThAT APPt.YI: I MLE Easting Aerated Volume (MG) tile
BEPR (A210 VIP. tic) Exust’nQ Anoxic Volume (MG ). Pile
Baideiipflo Curreni MLSS at We ller AOF 3524
O etcn Ditch
Lagoon (Biolec. etc.)
Cyolcal Aeration
SBR
Ilcil-Rate tho shler
Ej lluent Filtration
OU t ec
CURRENT EFFLUENT AMMONIA-N. 09 vig iL X From Ripen
Frent Model (atAOf and load, is d MCRT. 12°C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.Om$.
No moecetlons required New MLSS
Raise MCRT/MLSS In erAting tanks (thedr denSer apaatlil ‘ N /a
Cenebuot eddltional aerated volume Flaw (mgd) 0 1
nstjtfleddMonal daiWa/a Flow (mgd) p ’
Use eslathig anSo volume as aerobIc (construct sepefala denl l facility)
- Use aerated epstein for SOD removal only (construct separate nitidenit (acilty)
Add lalluent 1 1 0w equall7ation tank
Ot#r
PROPOSED MODIFICATIONS TO GET NITRATE’ tO mgiL:
[ JNo modifications requited
X Add downstream Oe M filler with methanol
Add downleam N*ilSCsbon Biolilter and DeNul Slier with methanol
Add methanol so existing BNR process
Add domistreanl anadc tank with methanol feed
Mdel IuentflIflhiOhl
Othw •
CAPITAL COST! Equipment and Stn4ures ((rein Page 2) 13.080,000
- E’cctnab aid lastumentedOn 12% 1082.000
Yard Pçeig and Site Watt 15% 5852,000
Subtotal. 1 7 2 10.000
Contractor OH8P. 15% 81,082.000
Engineesing aniCorustf. Mgnt 15% 51,082,000
Subtotal. 59,310.000
Con t ingencY 30% 12,103.000
Total CapItal Cost 111,530,000
Capital Cost per lb 20-Yr N removal $3.61
OPERATIONS COST: Additional Horsepower ((rein Page 2) 270 HP
Electrical Power CosL 005 3 1kW 188.200 1/year
Nitram Radian using Methaid . 4.0 ingiL
Methanol RequIred: 210 gals/d
Methanol Cost. 075 1/gab 101 500 1/year
Separate Stage Ammonia Reduction 0.0 inglL
CauellcSodaO2 S%CO1C OgaIs/d
CauszicSodaCosl 000 S/gal SOS/yea
Equipment MaIntenance Cost 193 P00 1/year
Denutruficauon Sludge Production w/Methanoi 050 bald
Sluege Disposal Cost. 400 S/ton 147 500 5/year
Total Annual Gild Cost $208 900 1/year
Elteclive Annual Interest Rate after Inflation. 2.91%
20-Year Present Watt 0/OW Coslr $4,300,000
TOTAL 20-YEAR PRESENT WORTH COST: $15,830,000
Total Cost per lb 20-Yr N removal 14 - 12
Aitoona West x Is Page 1 ol 2
-------
PROJECT: knpleinandng a3 meJL Annual Average Total NNragen Link
PREPARED FOR: USEPA, Clieuapeaka Say Office —
PREPARED BY. VIrg In ia tech with Stearns &Whelet. tiC
DATE: Marce l 1 9 2001
FACIl iTY Altoona West WWTP
LOCATION: Mount PA
RA IEOFLOW : 135 rngd PECOO N/a mg/L
CURRENT EFFLUENT TN 7Tmgit. . FE 1KM. Mis nvj/L
EFFLUENT TN GOAL. 30 mgit
NITROGEN REDUCTION. 450 Ibsld
184 1000 lbs/yr
3285 1Q00 lbs/20-yeers
CURRENT PROCESS (CHECK ALL THAT APPLY): A MLE Existing Aerated Volume (MG) N /a
— BEPR (AZ10 VIP sic: Exisang Ano int Volume (MG). N/a
— Barden pho Curren MISS a l Winter AOF 3524
— Ox idation Ott ’
— Lagoon (BuolaC, etc. I
Cydical An liliOn
U N
— High-Rate BlellIter
— Effluent P a tton
)ther. _____________________________________________________________
CURRENT EFFLUENT AMMONIA-N: Qj_jnglL X’ From Report
From Model (atADE and load. I5dMCRt 1?Cwlnter00ndidons}
PROPOSED MODIFICATIONS TO GET AMMONIA’1.0 mgIL
X No modilloubofls required New MISS
RaIse MCRT*LSS In existing tanks (check clfler capacity) t Ue
Consmioladditwls aerated volume Flow (nigd) 0
COflwlflat aIC1aflI Iet5 Flew (mgd). 0
Use SsMg aieec volume as aerobc ( iiavua separate denit faciliM
Use aerated system to ’ SOD removal only (construct separate nitidenit facility)
iniluent IowequaiuZallOI1 taik
Other:
PROPOSED MODIFICATIONS TO GET NITRATE’ 1.0 w igiL:
No moolfications —
Add doerstream DeNt Ilber w’Ifi methanol
Mel dowlutreani Nitililcation Biofilter end DeNt Otter tint methanol
Add m.Ui. l1 sa exrsting BNR procass
Add downaealI nec tank with methanol teed
D eter
CAPITAL COST: Equipmeiitand Structisres (from Page 2): 55.080.000
Eleancal and b,svtanentatiott t2% 8852.000
Yard PipIng end Site Work: 15% 3112.000
Subtotal ’ 37.210. 600
Contractor OHIP; 15% 51.052.000
Engineering and Comfr. Mgmt 15% 11.052.000
Subtotal. 39.370.000
Contingency 30% 52.183.000
Total Capital Cost 311,530.0 0 1
Capital COSt pert. 20-Yr. N removal 5331
OPERATIONS COST: Additional Horsepoiner (from Page 2): 270 HP
Electrical Power Cost 005 3 5W 368.200 S/year
Nitrate Redu©On using MeflnOt 4.0 mgI.
Methanol Required. 210 gaWd
Methanol Cost. . 075 S/gal $57 500 S/year
Separale Stage Ammonia ReductiOn 0.0 mgI.
Cabsiuc Seal © 25% comiC 0 gals/d
casic sodaCoat 080 S /gal 505/yew
Equ.øment Maintenance Cost 193 700 S/year
Denrinfrcation SISge Production wiMethanol 650 lbWd
Sludge Disposal Cost 400 IS bn 347.500 S/year
Tol.aI Annual OW Cost $288 900 s/yes’
Elfectr.e Annual interest Rate after titlatlomv 291%
flYca ’ Present Worto of OW Cost 14 .300.000
TOTAL. 2*-YEAR PRESENT WORTH COST: $15J30.000
tcx Cnt per lb .Yr N removal. $4.82
Altoona West xis Page i of 2
-------
PROJECT: implementIng u3 mgIL Annual Average Thai Nkregen LImIt
PREPARED FOR: USEPA. Chesapeake Bay Office
PREPARED QY. vtrglnla Tea with Stearna & Whsisr. LLC
DATE: March15. 2Q01
FACILITY: Chamberflum WWW .
LOCATION aiamtembwo. PA
RATED FLOW pj,mo o PECOD l i lA mg i.
CURRENT EFFLUENT TN: 40 rngtt. PE TTh WA mg i.
EFPLUENTNGOAL - 30 mgIL
NITROGEN REDUCTiON: 60 lbs / t i
n i000ibW
438 1000 lbsIZOjtn
CURRENT PROCESS gCHECK ALL TI IAT APPLY): liE ExatIng Aerated Vok Ine (MG) HIS
BEPR (A210. VIP. etc.) Eadating Anox’c Votiuine (MG)- l Ife
8ardenpllo Current MLSS t Winter ADF. t
Oxidation 04 t h
Lagoon (Odec. etc.)
— Aeration
SBR
— Higlt.Rate Slofihter
Effluent Fihrabpn
Other _______
CURRENT EFFLUENT AMMOMA.N c i 0 mg’L X From Repoti
Frent Model (at AOF a i d load. l Id MCRT, it C winter cono dons)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.0 mgt
X WennS adofiareaufld NOW MLSS
Raise MCRTIMLSS hi existing tanks (check denier capacity) ______
CenatruttadeitienOl eersled volume Flow (ungdy g
ij fltJ ai atdaders . Flow (.ngd). 0
usee anoscvdrle us sereolc(wtabuct separate daM facility)
Usa waled systemic: WC amoval only (construct separete ntt/denit faotdy)
ktfluentlbv equa..ZationWtk
Om .
PROPOSED MODIFICATIONS TO GET NITRATE c tO
dosnebeath DeNIt titer With methanol
doomeleam Nitnflcabon eIc Wter and 00+111 fIl m with methanol
memanol to Sating BNR proosas
Add d 1 ,aiavetl mISC tank t methad teed
im attesetadon
Othr nW MethadMd
CAPITAL COST: Equipment aid Structures (from Page 2). 50
tlectncal and tnatrumefltahlon 12%
Yard Piping ano Site Work 15% 50
SxbtOtal 50
Contractor O I I S P (5% $0
Efl 9 nemIngsMCOitstrMg m t* 15% . $0
Subtotal. SO
ContIngencY 30% 50
Total CaØal Cost $0
Capital Cost per ID nY c N removal: Soi l
OPERATIONS COST: Add l eoS Horsepower (from Page 2) 0 lIP
EleSoal Power Cost 0.05 5 1kW 50 S1 ’ear
NIVIW RudISOIt edsig Methanot
Mnfleqtiwed: SOgalaId
Methanol Cost 0.7$ $ al $5200 $IVear
Segetale Stage Mnmoria ReSSeit Otnt ?L
CaustIc Soda 025% a 0 gaWd
taus lic Soda Coat 0.60 slgal $0 Vyear
Eaulprneftt Maintenena Cost SO 5I ar
Dettwtficsbon Skidge Produti sMethand. 10 t iM
Slidge Oispoeal Cost 400 Win $5000 Slyesr
Total Annual 0114 Cost $14 000 Slflar
EffectS Annuatlntereet Rate after kiftation 2it%
20.Year Present Worth of 0114 Costs. 1210.000
TOTAL 20-YEAR PRESENT WORT14 COST: 5210.000
Total Cost pet lb 20.Yt N lenioval 10.46
Chambersburg wwrp xi i Page I 012
-------
PROJECT implementIng .3 mgtL Annual Average Total Nitrogen Utnit
PREPARED FOR: USEPA. Chosapeake Bay OffIce
PREPARED BY: Virginia Tech with Staanis & Whaler, LI-C
DATE: March 10 .2001
FACILITY- Greater Hszleton WWTP
LOCATION: Mansion PA
RATED FLOW- L b ,ngd PS COO 100 mg4.
CURRENT EFFLUENT TN- IT”mglL PE TKN 25 mvL
EFFLUENT TN GOAL: 30 mgil
NITROGEN REDUCTiON 370 tbsIG
‘35 1000 tastyr
2701 ‘000 Ibsr2O-years
CURRENT PROCESS (CHECK ALL THAT APPLY : X MLE E X1SI1IIQ Aerated Volume 1MG) 0.5
— SEPR (*310 VIP. etc.) Existing Anoxic Volume (MG) 0.21
— Bardenpho CurrentMLSS at Winter AD?: 3500
Oxetatlon 01 1th
Ugoon(Bdec.et}
- Cydical Aeration
S ER
X ttgb.Rate Bioffler
:
Olher. _____________________________________________________________
CURRENT EFFLUENT AMMONiA-N: 3.2 mgfL Fro m Report
FromModel(etADFafldlOad. 1SdMCRT, 12’Cwinterccndltions)
PROPOSED MODIFICATIONS TD GET AMMONIA’ 1.0 mgi: - -
T]No modiflallone requited - New MLSS
Ti f laise MCRTAILSS in exising tanks (cltedc dariler capacity) ti le
T]Conemid addidonel aerated volume Flow tmgd) 0
]ConsUuct addidoS clartlers Flow (mgd) 0
}tIse existing anoxlc volume as aerobic (construct separate aertt taclity)
]vse aerated system for SOD removal only (constuct separate nilldenat lacilily)
Add inluele low equalizetlon tardi
JOther - Abandon activated sludge process and use biofilter focal low
PROPOSED MODIFICATIONS TO GET NITRATE’ 1.0 mglL
No modilcfloifl raquired
- downsteafn DeNit filter with methanol For all LI mgd
downeflailt PliIrItIcabOn BloltIter arid DeNlI Otter witf t methanol
meltatol to existing BISR procas
domwflam smt tank with methanol feed
- effluent lil ve lon
X OUter Add dow i sSam Mat¼tvSC Slofliter b3 41 mod flow
CAPITAL COST: Equlplnelttal’ld 5tfuclures ( 1 1 0 1w Page a $7990000 Adjusted for Special ConditIon
Eledriost and Inetruineitteti c i t 12% 1950.000
Yard PipIng end SI t s Wodi tait 11.109.000
Sublelat $ 10,150,000
ContresOH$P. 15% 11.523.000
Enjneukig end Consi li nIt 15% 51.523.000
Sublotet 113.200.000
C n gen y 30% 13.045,000
Total Caped Cost $ le,250000
Capital Cost per i 20-Yr. N removat $602
OPERATIONS COST- AdditIonal Horsepower from Page 2) 530 tIP
Electilcal Power Cost. 005 51kW 1173.200 $4ear
Nitrate Reduction ucing Methanol’ LLmfl
Methanol Recited 170 galsld
Methanol Cost - 075 S /gal $46 500 5 /year
Separate Stage Amman ’s Reduction 0.0 mglL
Caustc soca @25% cart 0 galsld
Caustic Soda Cost 060 5/gal 50 S/year
EqtxpmentMi lntefla n CO5t $132000 S/year
Denltilllcalion Sludge Prothictien wftMthand 530 tbsld
Sludge Otepesal Coat 400 Men 536 700 s/year
Total Annual O&M Cost $390400 S/year
Elective Annual Interest Rate slIer mOabOn 291%
20-Yew Present Worth of 0111 Co St $SftGOo 000
TOTAL 20-YEAR PRESENT WORTH COST:
Total Cost per lb 20-Yr N uemovai $1.19
Greeter Ilaztelon, PA xis Page 1 of 2
-------
P R OJECT: tmpiemeithnG a 3 mgIL Annual Aveisga T otal NI ngel i UmIt
PREPARED FOR: USEPA, CheUpUKe Biy Office —
PREPARED BY: Virg Inia Tech wIth S horn. & Whale ’. (SC
DATE: March 11,2001
FAClirr i: HanoYs , A,e. V WTP
LOCATION: i4iiovM PA FE BOOS 135 mgil
RATED FLOW: 45 mgd RE COO NIn __ mgiL
CURRENT EFFLUENT TN: eOnigR. PE TXN - 30 rngtt.
EFFLUENT TN GOAL: 30 ingIl.
NITROGEN REDUCTION. 110 hId
40 i000lbsIyr
503 1000 Ib 20.yesrS
CURRENT PROCESS ICHECIC AU. THAT APPLY): talE Essling Aerated Volume (MG) 4.29 _
BEPR (A210. ViP. etc.) Enflnq Anoxic Volume (MG) N h
— Bardenpho Current MLSS at Winter ADP NI .
X OrldatmnDilth
La900A (SWIne. do)
Cydcal Miabon
SBR
IIlgn.Rate ScIli w
EMu 5M FOirstol
Othr
CURRENT EFFLUENT AMMQNIA4d o5jnglt. X From Re nt
From Model (at AbE — load. IS d MCRT. it C winiet condubons)
PROPOSED MODIFiCATIONS TO GET AMMONIA’ 1.0 mgiL:
Lx Nomodte$OllINflec New ML SS
L. RS kaT&tSS IA exising tanks (0W dinfler capaoW) 3000
L ddItIOMteemted ,dttlm5 FIcdvlmgd) 0
L CanstiCeddib0Ahit 1l ’5 Flowtnlgd) 0
[ Use eseting pnewc .ofl’• as aerob Ic l A$lflfl neparats deAd laohIy)
L_ Use aerated tjstem S r €CC removal only (CCASDUCI separate nitIdenit fanruty)
L. Add Inflsstt flow eSJailYStcn taut
çolher:
PROPOSED MODIFICATIONS TO GET NITRATE’ .0 ing lL:
No ngdj5 flfl5 NQ
Add dwnteifl DeNit MWMII flteflS
Add dewi60ecn MbIkáon eloIlfter and DeNut Mv wit methanol
Add inothedol tes*tg 5118 l0C 5i
#Ød — sa at wit methanol feed’
g suit a
OIlier . 4
CAPITAL COST: £qspmentsat S iatturoa (from Pigs 2) 12 .530.00 0
ElectS end i nsUtaTlentetlOn. 12% 1304.000
Yard PipIng end SINOIIC 15% 5310.000
Subtend. P.2 10 . 000
Coi*totOH IP 15% 5462.000
EjneerIc and CoSt. Mgmt 15% 3412.000
Subtotal. 54170 .000
ConlngencY 30% 5953 ®
Total CapS Cost $1130000
Capita) Coal per lb. 20-Yr. 21 re liant $4.35
OPERAtiONS COST. Additional Horsepower (from Page 2’ 90 HP
Elechnoat Power Cost 0.05 5 /sW 525.400 llyeer
NUte Reduction using Methano l, 2.0 mg I).
Maths Reqwed. 50 gaS
Methanol Cost. 075 Sips! 513.700 Slyear
Separate Stage AromaS Reduatlon 0.0 mg I.
Caustic Soda i 25% onnc 0 gaS
Caustic Soda Coat. 060 SIps! SO $Iyeai
Equipment Maintenance Cost 141.700 Slyest
cation Sludge Productuoli SMethonot 100 ted
Sludge Obpo° ’ Cost. 400 Men 511.700 upset
Total Annual OW Coot 1 .500 S lpear
EffeoS MniS Interest Rate Stidaboit 2.91 %
20.YsarPfeSantWOlV lotOtMC05bt . $110.000
TOTAL 20-YEAR pRg3ENT WORTH COST: 55. 550.000
Total Cost pert. 20-Yr. N renioval. $5.10
over ala Page I of 2
-------
PROJECT: Impiemetitkig 13 nglLMnvai Avwqe Total NItrogen Limit
PREPARED FOR: USEPAI Chee.peekn Bay 0 ( 1 1c c —
PREPARED BY: Virginia Tech with Steann £ Whaler, LI-C
DATE: March 10 ,2001
FACIUTY: Greater HaSten WWTP
LOCATION: HaS t en, PA - -
RATED FLOW: 09 rngd PC COD 190 mgIL
CURRENT EFFLUENT TN: 50 mgit. PC TKN 25 mqvL.
EFFLUENT TN GOAt: 30 mgsL
NITROGEN REDUCtION 310 Ibs ld
135 1000 lbsIyt
2101 1000 1b3t20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): X PaLE Existing Aerated Volume 1Mm - 05
— SEPR (*2 10. ViP. elc) Exlsling Anoasc Volume IMG). 021
— r t’pt’o Current MLSS in WWitar AOF 3500
— Oxidflon Ott ’
— Lagoon (Biolac. et)
— Cydleal AeraSon
5 5 1 1 ‘
Z PlWh-Rate Boifter
— Elkient Filtration
Other ______________
CURRENT EFFLUENT AMMONiA-N: 32 niglL From Report
X From Model (aIADF and bad. 15 d MCRT. 12’ C winier cn’ticnsj
PROPOSED MODIFICATIONS TO GET AMMONIA c 1.0 mglL
Raise ICRTIMLSS Si existing tanks (check clanfler capacky) We
Coriseum additional aerated volume Flow lnlgd)’ 0
ConewU o l additional datt eers Flow (mgd) 0
I—— . NewMLSS
Use emeeng anotdc ve in as eerv4 tc (construct separate Oem tacibty)
Use aerareo system S BOO removal only (constnicl separate ntldanul laciliM
Add mfiuers low equdS i on tank
X Other Abandotiatated uludae arocess and use bioteer Ia all low
PROPOSED MODIFICATIONS TO GET NITRATE dO mgt
No moddications required
X Add downs team DeNit Mlerpltti methanol For all i s mgd
üd dowitetrearm NItitleslIon BloMer and DeNit titer wit’ methanol
Ado methanol b eiddkig SNR process
Add 4omispeam anwic tank with mflWd teed
titi anation. __
Other • UI A U.I1I AnSdMSlo $ktsW3,41 m cd how
CAPITAL COST: Equcnti and Slncxes (tam Page 2): i,eeo,ooo Adjusted for Special Condition
Electrical add lnstnensltaheli: 12% 599.000
Yard Pth’g and site V*rt 15% P.159.000
SitexaL 510.150.000
Conea c torOH iP - 15% 11.523.000
Engineering and Gonst. Mgn* 15% 11,523.000
St i stetat . $13200000
Conbngercr 30% 13,045000
Total Capidd Cast 515,250,005
Cepital Cost par is 20-Yr. N removt $602
OPERATIONS COST: Addition s Horsepower (from Page 2). 530 HP
EIecttal Power Cost 0.05 5 1kW 11 13.200 $4r,ar
Mi nis Reduction using Methanol SO nigh.
Methanol Required 110 gIst
Methanol Cost 075 $lgsl 340 509 $Iyear
Separate Stege Minionia Reduction 0.0 night
Cart Soda 025% conc. 0 g lsid
Caustin Soda Cost 060 519a1 $0 Sifter
Equipmel Maintenance Cost $132000 $lyear
OenItrltIcslhon Sudge PreSid lon wiMethanot 530 mild
Sludge Disposal Cost 400 Mon $35,700 Sbear
Tol l Anniad OVA Cost 139t400 $lyear
EltecIwe Annual kilsiesiRS alter SiulalIon 2 , 11%
20 -Year Present Worm c i OUt Costs $S$U 005
TOTAL 20-YEAR PRESENT WORTh COST: 522,110000
Total Cost oar lb 20-Yr N removal 11.19
Greater Mactalon PA ida Page 1 o12
-------
PROJECT Imp lement Ing a3 m t. Annual Average Total NItrogen LImIt
PREPARED FOR: USEPA, Chesapeake eay 0 1 1 1c c —
PREPARED BY: VtrgkiIi Tech with Stearns & Whiter, LLC
DATE: March 19, 2001
FACILITY: Harnlaburq WWTP
LOCATIOW iiiñiibürq. PA
RATED FLOW: 300 mqd PE COO 1419 molt
CURRENT EFFLUENT TN: rrmg’t PE TKN 10 mgsL
EFFLUENT TN GOAL: 30 mglI.
NITROGEN REDUCTION: 250 lbsld
91 100010$/yr
1925 1000 Ibsl2O-years
CURRENT PROCESS (CHECK ALL THAT APPLY)’ - MLE Existing Aerated Volume (MG) We
BEPR 1A2 . l1P it t ) Existirio Anoxic Vclis’ne (MG) l i la
— Bwdenpho Current MI.SS at Winier AOF. N/ a
- OxIdation Ditch
- Lagoon(Blolac.elc)
- CydrcalAefatlon
_SBR
- High-Rate Bloftlter
X Effluent Fllbetion
Other UNOX Process. Aerob lc-Anoxic SAFe -
CURRENT EFF WENT AMMONIA-Il. c i a mgIl. X From Raped
From Modal (atADF and bad. 15 d MCRT it C winter cannons)
PROPOSED MODIFICATIONS TO GET AMMONIA ‘ C 1.0 mgiL:
X No mSflca9 1s rested New MISS
Ra ise MCRTIMLSS a’ existing tanks (check clarifier capacity) _______
Construct addItional aerated volume Flow trngd) 0
Construct additional danfiers Flow ungd) 0
Use existing aroxic ‘are as aerob i c (construct aaparste dent facility)
Use aerated system BOO removal only (constwcl separate nit /del l lacibty)
mfluent sow equ i tintOn tank
PROPOSED MODIFICA 1 1ONS TO GET NITRATE C 1.0 mgt
No modfficsdon requited
And downetewn Val e t tIter with methanol
Add downtewn Nltil$catloll 8 1 0 5 11ev and DeNIt filter t Ci methanol
Add methanol ioeit*ig BNR process
Add downtiMe awE tank with methanol feed
Add aertflau
Ode Anti Methanol
CAPITALCOST: Equlpfnenta sstruclulee(frQn lPate 2 ) 50
Electrical and instrumentatIon 12% 20
Yard PIgIng arid Site Work 15% 10
Subtotal. SO
CctlUic$3r 0 1 4W 15% 10
Emoineefing aid Conet Mo Int 15% 50
Subtotal 30
C i tngency 30% 30
Total Capital Cast $ 0
Capital Coal per lb 20-Yr N removal ga_go
OPERATIONS COST Additional Horsepower (Trcm Page 2) 0 HP
(tactical Power Cost 005 5 1kW SO S/year
Narate RedidiOn using Methanol. 1.1 mgit.
Methanol Required 110 gals/d
Methanol Cast 075 3/gal 530 100 S /year
Separate Stage Ammonia Redudon 0.0 mgit.
Caustic Soda 025% cone. 0 gats/d
Caustic Soda 000 1/gal $0 S/year
Equipment Maintenance Cost $0 $4 &
DeriMici boll Sludge Production WOtaIlOF 300 taM
Sludge DSposal Cost 400 flit 320.300 S/year
T ;ai Annual 05/4 Cost 356 400 5/yes
U’acvve Mnuaf Interest Rate after betatlort 2.91%
20-Year Presenl V rth or 0514 çoeta $a So .00 0
TOTAL 20.YEAR PRESENT WORTH COST: $150,000
Tn C.nl per lb. 20-Yr N removal $0.47
ham burg xis Page i of 2
-------
rnoJ gCT: Iznptem.ntlng 13 iapáLAifl e d A n i ta ’ ToU I NltroganLknlt
PREPARED FOR U$WA. Chesapeake ay OffIce
PREPARED BY: VItgIifl Tack with Steams £ WheW . LLC
DATE: M 5rC111t2001
FACILITY: L anc a s ter WWTP
LOCATION: Ianastet PA
RATED FLOW: aL.mgd PE COO N /a mgIL
CURRENT EFFLUENT TN: tOmg/L N TKN fl nqL
EFFLUENT TN GOAL: 30 mgIL
NITROGEN REDUCTION: 1240 Ib&d
453 1000 lbs/yr
9052 1000 10a120-years
CURRENT PROCESS (CHECK ALL THAI APPLY):
a.
t URRENT EFFLUENT AMMONIA-N: 0.5 mg/I X From Report
From Model (at AM and toad. l Id MCRT it C winIer condulions)
PROPOSED MODIFICATIONS TO GET AMMONIA cli ing iL:
X Q Jp1—-iequked Now MISS
Raise MCRT4&SS In tasting UnIts (chedi dardler capacity) N/a
Comthd M* 1 iai .emtad yohana Row (mgd) 0
Consktd L IW gaitlers Fl (mgq). 0
Use eela*ig niunlo as aerobt(cOnSttfl saparale eng facIlity)
Use aerSO system for 800 removal only (constnd separate nuVdenul facility)
Add I nsist flow
Other
pgØPQSED MODIFICATIONS TO GET NITRATE’ .0 niglL
No moalaSons —
Add doustewll DeNIt ntter *1111 methsM
Add dowisflan N ltatcabon 6 1 0 6 1 * and Dad rater Wtfi methanol
Add matWcIWe1flhl ONRorocasa
Add dowUSs aMmo Ufl I t wel l methaid feed
Ado SkinS BWabon.
Ode
CAPITAL COST.
•
Eqwpment and Structures (froth P a ge 2)
Elecoal and Inatnunenlat IOlE 12%
SEe Woit 15%
311.350000
11.302 000
51.703.000
Yard Piping and
Sutlo t at.
15%
$14420000
52102.000
COnIK*OrOH&P.
Env...aafllg and Cons. Mgnt 15%
Su t aclal:
30%
52.1 03400
910.7*000
54.3*000
Coitngettc y
Coat
$23059060
Toed Capital
20-Yr. N temo w i.
$3.56
Capital Cost per
OPERATIONS COST:
Additional Horsepower (from Pap 2) 590 HP
Elecbal Power Cost - 0.05 S/LW $160600 Siyear
NItrate Redicon uaai Methanot L I nfl
MathaM RequIred 500 g uaM
Methand CoaL - 0.75 $ al 3153.300 $/ ear
Separate Stage Amnttla Radian: 00 refi
Caustic Soda @7 3% co . 0 gaU/d
Caustic Soda Cost. 060 S/gel so s r s
Equip ment Maintena nce Coal 51 .7590 S /year
Dewodication Sludge PmditXlt eEtw’OI 1160 taM
Sludge Dlspoaal COal 400 5/bi 51*900 S/year
T1a1 ANwal 0514 Coal $562500 3/year
iffedive Annual Interest Rata after Inflation. 211%
20-Yes Present Worth of 0654 Cost . 51950 .000
TOTAL 20-YEAR PRESENT WORTH COST:
T,lal Coal per lb 20-Yr. N removal
533.0 3 0 100
1345
x
MLE
OEPR £A2 , V IP. ott)
BardS
Oudalfoil OI i
Lagoon (Betas, elc I
Cyclical IUOi%
SBR
High-Rate Biofillar
EtikienI Fiuatmn
Quiet _______
Existing Aerated Volume (MG) N/a
E ,dstino Anoxic Volume (MO) N/a
Current 141.5$ at Winter ADF N/a
Lancaster PA £15
Page I of 2
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?ROJECT ImplementIng a 3 mglL Annual Average Total Nitrogen Limit
PREPARED FOR- USEPA. Chesapeake a office
PREPARED BY Virginia Tech with Stearns & Whaler. LLC
DATE. March 19, 2001
FACIU1’Y: Qiambenburc WVIIP
LOCATION : Otambeiburg. PA
RATEDFLOW 6 f lmgd PECOD N /A mg/I.
CURRENT EFFLUENT TN- 40 mg/I. PETKN N/A mg/I.
EFFLUENT TN 00AL mglL
NiTROGEN REDUCTIDN- 80 lbs/d
22 1000 lbs/yr
438 1Q00 Ibs/2Ojwers
MLE _______
OEPR (A2I0. VIP elc) _______
Bardenpho _________
Oxidation Ditch
Lagoon (DiSC. ate)
CØlcal Aeration
S DR
High-Rale Biofluier
Effluent Fmta lon
Other -
CURRENT EFFLUENT AMMONIA-N ci 0 mgIL X From Report
From Modal (al AOF and load 15 d MCRT it C winter condlllons)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mgt: -
X No modificatIons required New MLSS
Rae MCRTIftILSS ut eabng tanks (check clanrier capacity) N/a
- Construnt addftional aerated volume Flow (mgd) 0
Construct additional Cla n S era Flow (mgd). L- 0
Use erdaljng anoxlc volume as aerobic (construct separate denit Facility)
Use aerated sØem for SOD removal My (constnfl separate nit/dartS tacitly)
ittuent Ilow equalization tank
Other -
PROPOSED MODIFICATIONS TO GET NiTRATE c IS atglL:
Nomod.P.S4 reqdred
MS downstream Detlit lifter with methanol
MS doenietiesm NiWlration StaRter and DeNt fitter with methanol
Add methanotteedathig BNR process
Add doanstipern moxie lank at methanol feed
effluent MrS
X Other Increase Methanol AdditIon -
CAPITAL COST:
Fcpilpmerit and Struttifls (Worn Page 2)
50
Electrical and lnstnimenlallon 12%
$0
Yard Piping ant Site Work 15%
50
Subtotal.
SO
Coitactor 01 1W 15%
10
Engineering and Constr sdgird ‘5%
50
Subtotal
SO
Contingency 30%
50
Total Capital Cost
Capita l Cost per lb 20-Yr N removal
$0
$0.00
•
OPERATIONS COST
Additional Horsepower fRom Page 2)
Eleotrlcel Power Cost 0.05 1 1KW
Nitrate ReduSon using Methanol
Methanol Requited.
Methanol Coat. 0.15 5/gal
Separate Stage Ammonia Reduction:
Caustic Soda t 25% cario
Caustic Soda Cost 080 5/gal
Equipment Maintenance Coat
Oenatslllcabon Sludge Production wi%Iethanoi
Sludge Disposal Cost 400 Mon
Total Annual O&M Cost
Eftective Annual Interest Rate alter Inflation
20-Year Preeent Worth at O&M Coals
TOTAL 20-YEAR PRESENT WORTH COST:
5210300
Total Cosi pet lb 20-Yr N remavai
toes
CURRENT PROCESS (CHECK ALL THAT APPLY):
Eilsllng Aerated Volume (MG) N/a
Existing Anode Volume (MG) N/a
Current MLSS at Winter M W- N/a
x
0 HP
SOS / year
10 mg/I.
30
$8200 S/year
- _ QQingIt .
o gdeld
SOS/ year
$0 5/year
80 ibs/d
55800 5 /year
514 000 S/year
2.01%
5210080
Chambersburg WWTP its
Page I ol 2
-------
P R OJECT; implement Ing s3 mgsL Annual Average Total Nitrogen LImit
PREPARED FOR. U5 A. Chesapeake Say Office
PREPARED DY: VirgIale Tech with stearns & While!. t iC
DATE: March 15. 2001
FACILITY: UMAWWTP
LOCATION: Cotteoe. PA
RATED FLOW: SO nigd PE COD 334 mgit
CURRENT EFFLUENT TW 60 mg!L PE TKN 30 mgIL
EFFLUENT TN GOAL. 30m9 ’t.
NITROGEN REDUCTION 250 10510
91 t000Ibslyf
1625 ‘000 Ib3120-ytfl’
CURRENT PROCESS (CHECK AU. THAT APPLY ): MLE ExIsting Aerated Volume (MG) 255
BEPR (MID. v I P. tic) Exisung As ia tic Volume (MG) 0.46
Baidanoho CitrenlMLS$ at V*iterADF: 2680 .
OxIdation O Ct
Lagoon (Slolac sic)
CydóI Anton
SSR
Hlgliaate StiuIter
Effluent Filtraton
OThe r
CURRENT EFFLUENT AMMONIMI: 1.6 mgIL From Report
X From Modal (atADF and load. 15 d MCRt It C wiatdz conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.0 mgiL:
No modd S’5 required New MLSS
X Raise MCRTM.SS ki existing tanks (cheek dat ospaaty) 3650
constudadddioS aerated volume F aa (ingdy 0
ConslitC adedonal dpelers Flow (mgo) 0
Ue existilo ro tc votume as aerobic (construct segarate derill facility)
Use te S s systen i for SOD removal only (construct separate nilldenit facilIty)
tank
Otter
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mgIL:
No iec iens required
Add ertnaain Del hi altar with memanot
Add doisnstrealtl Mvut tlon Siofter and DePOt titter teet rrathanol
mesunol ta esellng DNR process
Add doflulS afloilo lank wil l methanol feed
• Add SSsdflOn
Otter weeeson tsS s tocresle coat eaSe zone
CAPITAL COST Equ irnent and SIructies (from Page 2): 1250 000
Ewemud end lnstjwnsnladoft 12% 530000
- Yard Piping and 5lta Watti. 15% 530.000
Subtetat 5320.000
cotta OH&P, 15% 546.000
Engineering and Ccnst. MgnU. 15% 8 4 6.000
Sch lo s S. 5420.000
CentingwlCY 30% SDe.
Total Cwdal Cost 5520.000
cepa Cost per lb. 20 .Yr N removal. $0.26
OPERATIONS COST. AdddcnaIHOlsePOumr(M’l Page 2) 0 HP
Eleclrai Power Cost. 005 SAW 50 $Iyear
tetate Reduction using 5.0 IngIL
Methanol Required 110 guild
Methanol Cost * 7 5 SlgaI 530.500 Slyer
Seøar.te Siege Ammonia Reducton 0 OmglL
Caus lcSod SOZ S%W IC Ogasfl
Causic Soda Cost 060 SIgal 50 Slyear
Equipment Maintenance Coal. 54.200 Sl ear
DefiultutatIOn Sludge Production aflhuiOl. 360 lb M
Sludge Disposal Cost 400 SM ’ 125.300 SNeer
Total Annual OSM Cost 560.600 Slyest
Elteekve Annual Interest Rate alter kdaott 2.91%
20.YeN Present Waith of OW ce eieeoo
TOTAL 20.YEAR PRESENT WORTH COST; 51 .430.000
Total Cost pert 20-Yr N removal $0.75
UAJA Slate Cosege PA its Page i of 2
-------
PROJECT. p.p nfl 83 mglL Annual Average Total Nltngen limit
PREPARED FOR: USEPA. Chesapeake Bay 0 18c c
PREPARED BY: VI lgInla Tech with Stearns £ Wheler. LLC
DATE: March 11,2001
FACILITY: Samewn wwr
LOCATION: . Swenton. PA
RATED FLOW: S.. mgd Pt COD. no mg ,L
CURRENT EFFLUENT TN: 1.2 mg/I. PE TKN 20 mgrL
EFFLUENT TN GOAL; 30 mgit.
NITROGEN REDUCTION: 830 lbs/i
303 t000 lbs/yr
8051 1000 lbs/20.years
URRENT PROCESS (CHECK AU. ThAT APPLY): X Ni l Exlatbig Aerated Volume (MO) 4.51
— BEPR (A210. VIP. etc I Existing Anouc Volume (MG) I 9U
ateenp aio Current MLSS at Winter ADF. 2750
Oxidation Ditch
Lagoon (BJolac etc I
Cyclical Aeration
SBR
Nign-Rale Biot’Itet
Ettluefli Filtration
Other _________________________________________________________________
CURRENT EFFLUENT ANMOMA4I: 12 nigh. it From Report
From Model (aIAL)F and load. 15 d MCRT. I 2 ’ C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1.0 mg/I.:
No moddlcatuais requked New MLSS
I Raise MCRT&tSS In Sating tanks Cot clarifier capacity) 3000
Con addlOonel aerated volume Flow (mgd) 0
— Ccnsni jdSonl clalSlere Flow (mgi) 0
Us. e,Srktg aswix vorume as aerobic (constiuct separate den / I facility)
Us. aerated Sin b SOD removal only (construct separate Slfdenit facility)
— &jeiil eqtmIIzaoon tank
:0
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 mglL
r io &uo ar.mei
[ Add & nttean VaUlt lIter vat methanol
E Add goemawan NobAcatlon So/Nor end DePot l iter wtth methanol
C Add methanol te nttlng SNR process
E l Add dowitatreani anorac lank vat methanol feed
C Mdemuentltle*bon
LO
CAPITAL COST: Equipment and Structurea (Iron Page 2) $8550 000
ElectrIcal slid .iijrflfl Ofl 12% $788000
Yard Piping and Ste Work t5% $183 XC
Sot i totat . $0320000
C MWa .OH&P 15% 11.245000
CnwaartngandConalr. Mgrnt 15% 81.241.000
$10 820.000
Coltigenw 30% 82.496.000
TcWCapltl Cost $13,220,000
CapItal Cat per lb. 20- f t N removaL $3.20
OPERATIONS COST Addi8oS Horaeponorffitan Page 2). 320 HP.
Eleoical Power Cost 005 5 1k W 5104.800 5/peat
NItrate Rethadon using Meelanot
Melt Reqxlred. 3 0 —
Methanol Cost 015 S/gal 8104.000 51$ar
Sepeate Stage Ammonia Reduflon 0.0 mo/I.
CsnecSo daO2 S%COnc 0 gals/it
CaSIo Soda Cost 080 S/gal $0 $lpeet
EquIpment Malrlenance Cost $108200 S/gear
DeiWIIIc&lon Sludge ProditlonwlMelhsiot 1180 lbs/it
Sksdge Olaposel Coat 400 S/ton 188.800 S/year
Toll Annual OW Cost $403200 3/beer
EIIewve Annuel lalerest Rate alter Inflation 2 9 1%
20-Year Present Worth of OW Coals. 55,050.000
TOTAL 20 -YEAR PRESENT WORTH COST: 519370.000
TolalCostperlb 20-Yr N removal $3.20
Scsanton xl; Page I of 2
-------
PROJECT: Implementing IS mglLMnsiei Average Total Nitrogen Umit
PREPARED FOR USEPA. C hesapeake Bay 01 1 ) 0 0 —
PRE PARED BY. VIrgin ia Tech with Sterns & Wheler. tiC
DATE: Marc h 19.2001
FACILITY: ggk haven WWTP
LOCATION: LXII Haven PA
RATED FLOW: flmg d P5 COO 300 n g’L
CURRENTEFFL1JENTTN: 155 rngrt PETKN 20 “1911
EFFLUENT TN GOAL 3.0 mgsl.
NITROGEN REDUCTIOW 390 ibs/d
142 1000 lbs/yr
2847 1000 Ibs/2Oqews
CURRENT PROCESS (ChECK AU. THAT APPLY): — IdLE isZitgMra Volwne (MG) t.344
BEPR (Afl ViP. etc.) EalsangAnoc Vo lwne (MG ). 0
Bardento Current MISS ii WInter ADE 2500
O3odabOfl 0l i
tagoonolac.eIC)
— SO
Son
H hameeae
Effluent P 800 80 1%
i other Conventional pavated Sludge
CURRENT EFFLUENT AMMONIAN: 9.5 mg/I. From Report
From Model (at N W end load. IS d UCRT. ItC wirnef conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA 41.0 mg/L:
No moddtsexns re4lsred New MLSS
Raise MCRtIMLSS ii eisa Wig tanks (check c larifier caoaotyj 4500
Conflud editlonal Stated volume Flow Inigdi 0
Constnid addtional clanfuers Flew (nigo 0
Use existing a l a mo volume as aerobic (consinC separate dank facility)
Use aerated astern hot ODD removal only (cons Duct separate nit/drill taoiUty)
Add influentltow equalization tank
Other. Baffles. Mixem end nItrate rec de
PROPOSED MODIFICATIONS TO GET NITRATE cit zng/L:
NomodlIcetlOns —
Add dewnseewn DeNII Id ler with methanol
Add dowtlSam NtbttSticn Cia/liter and DeNit Bier w ith methanol
netisnsleestlilg GM piocess
Add d flu act tank with nemanfls
Add ethuuW
OPe _______________________________________
CAPITAL COST: Eqwprnerit end $tnnuree (horn Page 2? 12260 . 000
EICctncaI end Insownenteilon: 12% 5771.000
Yard Piping end S e . Work: 15% 5330000
Subtotal. 52.870.000
ConIra rOH&P. 15% 5431.000
Eogineemg and Caner. Mgmt 15% 1431.000
Subtotal 13730.000
Contingency 30% 5561.000
Total Capital Cost $4590000
CapnatCostoarlb 20-Yr Nienioval . $1.61
OPERATIONS COST. Additional Horsepower (from Page 2) 80 HP
Electncal Power Cost 005 5/kW $26 tOO 5/year
Niliate Reduction ning Methanol. 12.5 rngtL
Melhanol Reqwred 180 gMe/d
Methanol Coat. 0.75 1/gal $49300 5/year
Secarate Stage Ammonia Redtflhon. 0.0 mg/I.
Caustic Soda © 25% conc 0 gels/d
caustic Soda Cost. 060 s/gal 50 S/year
Equipn%entMakitenanx Cost 137.300 S/year
Denitr4.aitwl Sludge Production wMethsid. 560 NM
Sludge Disxaal Cost 400 3/tn $40,900 5/Wear
Total Annual OIMCosL 1153.000 5/year
ENective Annual Interest Rate S Inflation. 2.9 1%
20-Year Present Worth of O&M Cost 12.300 .000
TOTAL 20-YEAR PRESENT WORTH COST: 35,590.000
Total Cost per lb 20-Yr. N removt $2.42
LoCk Haven PA i rs Page 1 of 2
-------
PROJECT: im plementIng a 3 mgIt. Mnusl Avenge Total Nitrogen Umi
PREPARED FOR: USEPA. Chenpefle Bay Office
PREPARED BY: Virginia Tech with Steams & Wheler (SC
DATE: Much 10 , 2001
FAC IL itY: USAWWTP
LOCAT iON L a n tin PA
RATED FLOW: j ,,,mgd Current Eft TN PE COO. 150 mc l i.
BNR EFFLUENT TN: 80 mglL 275 FE TICH 35 mgiL
EFFLUENT TN GOAL: 30 sngfL
NITROGEN REDUCTION 100 want Total N Rent 4904 tbslij
by Denite FIlters 31 1000 lbs/yr 119 k/yr
730 1000 lbst2Oyeas 3.580 Sf20-yr .
CURRENT PROCESS (CHECK ALL THAT APPLY). — M.E Exisisnq Aetated Volume (MG) 0.324/0434
X BEPR (A24) VIP etc) Existing Anoxic Volume (MO) 0.222 101 11
Beidenono Curreni MISS . 1 Winter AOF 1500
— OxIdahQn Ditch
- Lagoon (BioiaC. etc 1
Cyclical Aeration
S OR
High-Rate BIofltW
Emuent Filfltion
Other _____________________________________________________
CURRENT EFFLUENT AMMONtA-N: 1 5 rngfL From Report
X PromModeI(atAOFendbad. 25dMCRT, i °c M l u
PROPOSED MODIFICATiONS TO GET AMMONIA c 1.0.mgit.:
1No It Iona requIred New MLSS
KJRCISe MCRT&ILSS ii Sating tanks (check dat capacity) 4750
JConsnd SM.ad aerated volume Flow (mgit 0
LICawtn additional dariflers I _______
T]L’ea ecethig S it -n as aerotac ccnstruct separate dene facility)
Ti Use aerated system I cr SC travel only (construct separen Jde t facility)
JASA inlhient flaw eqtioiizztcn lalik
JOthe c
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 nigt:
DHo modifiS re4uired
X Add downiveam G Nd rdter with metiwnol
dd a,fllstreaIflhIlWlOflon Brother and DaR n lifter eMit methanol
M o mee larci ta eenng BNR piooan
Add dowrsiinm act tank with methanol Feed
patda aaaeon
APITAL COST: Equipment aid Sindures (Iroril Page 2): 91.790.000
Electrical aid ritatiort . 12% 5215.000
Ya rd Piping anti Ste Wodc 15% 1209.000
Subtotal 12.270.000
ConvacterOH iP. 15% 1341.000
Engineering and Constt Mgnt - 15% 5341.000
Sutitetal. 12.950.000
Contingency 30% 1 60 1.000
Total Capital Cost $3430400
Capes Cost per lb. 20-Yr. N removal. $1.02
DPERATIOMS COST: Additional lioreepaver (from Page 2) 50 HP
Ejeceal Power Coat tO O lAW 516.300 $4cear
Mora ls Reduction useig MedianS 50 mgit.
Megiariol RequIred. gaivd
Me thanol Cost 0.75 Sfgal 5 13.100 $I ear
Secarate Stage Anvuonta Reduckon 00 tolL
Caasirc Soda e 25% cent 0 gale /ti
Caustic Soda Cost 0605 1g M 50$/year
,Eo -ement Maintenance Cost 529500 S/ leer
Deninttion Sludge Produdron wlMethanol ‘40 IbsM
Skiege Disposal Cast 400 1/ten 510.200 s/leer
Toist Annual OSM Cost 560 700 S /year
Elf carve Annual Interest Rate a 1 W Inflation 2 9I%
20-Year Fteaei* Worth of O&M Catty 11050.000
TOTAL 20-YEAR PRESENT WORTH COST: $4600000
Iota Cost per lb. 20-Pt N removal $1.31
1e msbwg PAds Page 1 o(2
-------
PROJECT: Implemetttflg .3 mgd. MooS Avenge TOW * 1 109 5 0 UmIt
PREPARED FOR: USEPA. Clienpealls flay Office
PREPARED BY; VirginS Tech with Steams & Whaler. LI.C
DATE: March 1 1,2001
FAOUTY: L.banOil WWTP
LOCATIOPI : Lebanon. PA —
RATED FLOW: 3.L...mQd PE COO. 175 _ mWL
CURRENT EFFLUENT TN: fl•mgll. - PE TKN. 27 IOWL
EFFLUENT TN GOAL: 3.0 mgIL
NITROGEN REDUCTION: 330 Ifrsld
120 1000 i sIyr
2409 1000 1b120-ysare -
CURRENT PROCESS (CHECK AU. THAT APPLY):
1.0mg
flNomodihcnons reqilS New MLSS
]RaIUIMCRTIMLSS hi t im Ing MIIKS (check dat aP SC IY) N I .
TIConflufl 1 l” S aei*isd votumo Flow (mgd) ________
daSlem fl 0
JUse *a th tO minom Voltrele a aerobIc (untnflSIpamS denit f Eisty)
I]Us. asuaS system for 800 removal only (consimfit separate MIdenIt laaIdy)
TlMd fl$flIpP
PROPOSCO MODIFICATIONS TO GET NrTRATE 1.0 nigik:
No moddloslions —
MddomtsflWn DeNit lifter with methanol
Add datCa am Nkrlllcabon B Snd DO methanol
m uSed te Srig SHE M09U
M I dgreeeam anmec in with methanol feed
Add etiaS
Other
Equipment C M Structures (from Page 2)
Electrical and lnstruineiaabon 12%
Yard Piping end Site Wont: 15%
53.760.000
5450.000
5563.000
Subtotal.
$4j60.000
Contractor 0*4W 15%
014.000
Engineer i ng nd Const. Mgnit 15%
5714.000
Subtota L
ContIngency. 30%
36 ,100.000
11.425.000
Total CapS Cost
$TS S Qi000
Cap i tal Cost per lb 20-Yr N reinovat
$3.11
I SO lIP
AdditIonal Morsepoa (from Page 2):
Eiedtl P r Cost 0.05 flW
HI nts Red’t usIng Methatd.
Methanol Reqused:
MethaS Cost 075 SIgal
Separate Stage Ammonia Redu at
$52300 5 ur
.__SLmWt
160 pill
$41100 siyear
0.0 mglL
Caustic Soda 25% own
0 plaId
Caustic Soda CoaL 010 5 al
Equipment Maintenance Colt:
Oenulntlcabofl Sludge Pdionwdltlhaiiol
Sludge Oieposal Cost 400 SMi
10 Ilyear
551 900 SIti’ear
400 Ib Id
- 55.090 Slyear
TotatAieiiial OEM Coat
fl003 0 5Iysa(
Effective Annual Interest Rate 1l I ntlabon
201%
20-Year Present Worth ot OEM Cats
12. 1 * 0 00
x
MLE
BEPR (MID, VIP. elc.l
Bardenpite
OxidatIon ClIck
Lagoon IBlooa. etc I
C tcS Aeration
SBR
High-Rate BoWler
Effkient Filtration
ow __
Etastuig Aerated Volume (MG) Wa
Existing Amnc Volume (MG) We
CusTeid MISS at WInter AOF NIa
PROPOSED MODIFICATIONS TO GET AMMONIA
____ From Report
CURRENT EFFLUENT AMMONIA-N: 05 mWl. AOF arid load. 15 d MCRT. itt winter conditions)
CAPITAL COST:
)PERATIONS COST:
TOTAL 20-YEAR PRESENT WORTH COST:
Total Cost at lb 20-Yr N removaL
510.470,000
“is
Lebanon its
Page 1 of 2
-------
PROJECT: ImplementIng e3 mgIL$wwal Average Total Nttrogeà UnIt
PREPARED FOR: USEPA Chesapeake Say OSlo.
PREPARED BY; Vhglnla Tech wIth Steams S Wheler, LLC
DATE: Merch It, 2001
FACILITY ’ UAJA WWTP
LOCA UON: State College. PA
RATEDFLOW. . 80 rngd PECOD 334 mg/i
CURRENT EFFLUENT TN. irmgR. PC TKN 38 mg/i.
EFFLUENT TN GOAL. 30 mg/I.
NITROGEN REDUCTION: 250 Ibeld
91 I000Ibstyr
1825 1000 Ib5/2Q.years
CURRENT PROCESS (CHECK AlL ThAT APPLY): IC MLE Exnstmg Aerated Volume (MG). 255
HEPR (AM. VIP. ot t) Erciating Mo4c Volume (MO) 0.46
Bsdenpho Current MLSS at Winter ADF 2650
— O tIon Dith
— Lagoon (SIclac. etc.)
— CyciealAeration
38R
— Hlgtiaate S’otilter
I C Eflttmntfltpation
: v
CURRENT EFFLUENT AMMONIA -N: 1. 8 mgi. From Repert
IC From Model (at ADF and load, 15 d MCRT. 12°C w inter nd ’bons)
PROPOSED MODIFICATiONS TO GET AMMONIA C tO mØt
Nornodlicatlona required New MLSS
IC Rnke MCRTRSILSS I i eidslbig tanks (check clarifier capaddy) 3 650
Conafrum additional sated volume Flow (mgd). r
COestndaddIIIoneI olallIlers Flow (mgd) 0
Lisa existing anoxc volume as aerobc (raistruct separate daM fadirty)
Use aerated swm (or SOD removal only ( c inaVuct Separate niIJdent tacihiy)
Add Mituent 110w eQualization tank
Other ____________
PROPOSED MODIFICATIONS TO GET NITRATE C 1. sngt
Nomoditleatione required
Mdtmiatream OeNlt 1111w wIth methanol
ASdaaesteain NItrIlloalion 8b$Iterand DePil lilterwith methanol
ASniSia’igl te Sating StIR gm as
downstream anoido tank we methanol teed
Add emuent on , -
x omer i I iL1 bal r attoXIc $ -
CAPITAL COST: EquIpment and Spucturaa ( toni Page 2): 5250.000
Eledr tcal end kietu I 4 : 12% $30,000
Yard Piping and Site Wodc 18% 130.000
$ubtot.t $320000
Contrador CH aP. t5% $45000
Engineering and Cons. Pignit 16% 148.000
Subtotal. $420000
Contingency 30% $96,000
Total Capital Coat $620,00Q
Capital Coat per lb 20-Yr N removal 10.2$
DPERATIONS COST. Additional Horsepower (from Page 2) 0 lIP
ElectrIcal Power Coat’ 0.05 $IKW $0 $lyear
Nirate Reduction usIng Methanol’ to infl
Methanol RequIred 110 gola n
Methanol Cost 015 S/gal $30100 S/year
Separate Stage AmmonsReduclion 0.0 mg/I.
Caustic Soda 025% oonc 0 gale/ti
Caustic Soda Ccii 060 S/gal $0 S w
Equipment Maintenance Cast $4200 S/year
Derdtrtllcatlon Sludge Produflon veMelhanal 300 lbs$d
Sludge DIsposal Cost’ 400 1/ton 525.300 1 /year
Total Annual 0511 Cast: $50400 5/year
Eltaotive Annual Inleresl Rate altar Inflation 2 91%
20-Year Present Woith ot 0511 Coats $916,000
TOTAL 20-YEAR PRESENT WORN COST: $1,430,000
Total Cost per lb 20-Yr. N ro M . $0 _ T B
11AM. Slate College PA Pagp I or i
-------
PROJECT - Implement In g a3 mglt. Annual Awirage Total Nitrogen Limit — -
PREPARED FOR: USEPA. Cheaapflke Sly Office
PREPARED BY: Virginia Tech with Stearns 6 Whaler. LLC
DATE: March 19, 2001
FACILITY: Lock Haven VMTP -
LOCAT iON tôc* Haven, PA
RATED FLOW: Se rngd PE COD 300 mglt.
CURRENT EFFLUENT TN: Trrmg ’t PE TKN 26 ing lt.
EFFLUENT TN GOAL: 16’mgit.
NiTROGEN REDUCTION 390 Ths/d
142 1000 lbalyt
2847 1000 lbs/20-yeare
CURRENT PROCESS (CHECK ALL THAT APPLY): : MLE Existing Aerated Voliane (MG): 1.344
BEPR (A2& vip, a ExistIng Anoxic Volume (MG). - 0
Eatdenpho Qirrent MLSS at Winter .41W 2500
— Oxidation Ot t
— Lagoon (Blolac. elc.)
Cynical Aetetlon
• SBR
— HighRate 5 1 0MW
Effluent Flikabon
I Othat ,venttcnal Activated Slidee
CURRENT EFFLUENT AMMONLA.N. 95 tnglL X From Repent
From Model (aLADF end load. 15 d MCRT. 12’ C winter ctnddions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.0 sflglL
No ntodiflceXne reqwed New MLSS
AJRarse MCRTIMLSS pi. existing tan ks (check darufler capacity) 4500
J}Consltuct additional aerated volume Fta (mgd) 0
•JConstnict additional danteca Flow (modI ’ 0
_JUu exiatteg n e c f lume as aerobic (xnsttuct separate dent VacUity)
,JUs. aerated system lot BOO removal only (constiuct separate nAldenst fadttty)
intIuieiUoW etssPSt tl0n tank
!JOIhet. Add Baffles. Macre and nitrate reci
PROPOSED MODIFICATiONS TO GET NITRATE C 1$ mglt
Nomodthedicns required
X Add dow, nt DN I I (tiler with nteflnd
r. Add N lli lilcetuon $lnllIter and DeNd filter with methanol
Add iSaao1tee lQ BNR pseass
Add dewn*um anode WSteIth meNnol feed
Other d,t..S.3 *Pt :‘ •%J fl.L•.rI i i _ t ”t• . _ ” • ,
CAPITAL COST: Equipment end Structurea Øvnn Page 2) $2,260,000
Eloctrrai and iitatturnentallon- 12% $271,000
Yard Piping and Site West 16% 1359.000
St totai $2,870,000
Contractor OH&P: 15% $431000
Engineering end Conair. Mgmt. 16% $411,000
S i ttotat $3,130,000
Contingency ’ 30% 5661.000
Total Capital Coal $4,690,000
Capital Cost per lb 20-Yr N removal $1.61
OPERATIONS COST: Addilional Horsepower (Iron rage 21 80 VIP
Electtloal Power Coat 005 $iicW $26 tOO 5? cear
Nitrate Reduction using MethanOl 12.6 mgit
Methanol RequIted 180 galed
Methanol Cost 0.15 5S $49,300 $Mer
Separate Stage Ammonia ReductlwV 0.0 rnglk
Caustic Soda @25% co lic 0 g515fl
Caustic Soda CoaL 060 $Igel $0 $i ieer
Equipment Maintenance Cost. $37,300 $lysar
Denititfication Sludge Produmon w4UeOsed. 560 lbsld
Sludge Dispolal Cost: 400 SIlan $40 .900 $1 ear
Total Annual OW Coat $153,800 $4ear
Effective Annual InWeat Rate aiter laltatlon: 2.91%
20Year Present Worth of M Coat $2,300,000
TOTAL 20.YEAR PRESENT WORTH COST: 16,890,100
Total Coal part. 20 .Yr N removal $2.42
Lockltavvn.PPixI S paget Of 2
-------
PROJECT: ImplementIng 53 inqlt. AntHill Average Total Nihugen Lknlt -
PREPARED FOR: USEPA , Chesapeake flay Office
PREPARED BY: Virginia Tech with Stearns & wneie . tic
DATE: March 10, 2001
FACILITY: USA WWTP
LOCATION: lamburo. PA
RATED FLOW: 24 in Current Elf TN PE COO 450 ‘riglL
BNR EFFLUENT 7N 8.0 ing/L 215 PE TKN. 35 - mgIL
EFFLUENT TN GOAL. 15 mg/L
NITROGEN REDUCTION TOO lba/d Total N Rain 4904 Ibeld
byDen lteFl lters 37 i00 0Wyr 179k / yr
730 1000 te12S’ eara 3580 k/20-yr i
CURRENT PROCESS (CHECK ALL THAT APPLY): : M I E Ex ’sti ’ AeaI Volume (MG)’ 0 32410 434
X SEPR (A210 VIP at) Ex.atingAnoacVolumelMG) 0222 1 0 ,111
— Saitenpho Current MLSS at VWder AOF 4500
— Oxidation D Ich
Lagoon (Biolac, etc I
— Cyclical Aeration
SM
High-Rate BlotIller
— Emuent FiltratIon
, ,jOther.
URRENT EFFLUENT AMMONIA-N: 1.8 mg/L From Ripen
3C Front Model (atADF and load. 25 it MCRT. 12a C winier conditionsj
‘ROPOSEO MODIFICATIONS TO GET AMMONIA <1.0 mg L
rlwomodircateons requIred New MLSS
X Raise MCRT/P.ILSS in ealatlig lanka (diedi danfler capacsty} 4t$o
COItSIrUd additIonal aerated volume Flow (mgd) 0
Construd addsnsl dantiers Flow (rngd) - - 0
Use existing snoxic vthnt as aerobic (cnnstxuct separate dent facility)
Use aerated Mtem for 000 removal only (construct separate nilldend facility)
Add intluent low equalization lank
Other, ___________________________________________
PROPOSED MODIFICATiONS TO GET NITRATE <10 nig/L:
E]No modiSoatiorta required
X Add downstream DeNIt liter with methanol
Add downstream N.tdflcation Siofilter and DeNrt filter with methanol
Add methanol te existIng SUB process
Add downstream afloat tank with methanol feed
Add effluent Ebation
Ot(ia ___________________________________________
APITAL COST: Equipment and Structures (from Page 7) 51 ,790.000
Electicel and nstumenta@on 12% 5215,000
Yard Piping and Ste Wodi 15% 8269,000
Subtotal 32.270,000
ContradotOfl&P’ 15% 5341.000
Engineenng end Conatr 1 1gM 15% 5341.000
Subtotal- 52.950,000
Contingency 30% 5681 , 000
Total Capital Cost 13, 130.800
Capital Cost per lb 2*-Yr. N removal’ $102
OPERATIONS COST: Additional Horsepower (from Page 2) 50 HP
Electrical Power Cost 0.05 5/kW 516.300 Slyer
Nitrate Redudilon using MethanOl LU . mgit.
Methanol RequIred. 50 ga la /tI
Methanol Cost 075 stgai $13 700 5/year
Separale Stage Ammonia Reduction ‘ 0.0 nigiL
Caustic Soda 25% cat ogaIs d
Csusiic Soda Coat - 060 Slgal SO S/year
Eqijipnient Mainlenance Cost 529.500 S /year
Denitrification Sludge Production w/Melhanol 140 lbs/it
Sludge Disposal Cost 400 3/ton $10200 S/year
Total Annual 0811 Coat $61700 S /year
Effective Annual Interest Rate after inflation 2 91%
20-Year Present Worth of 0811 Costa $1050000
TOTAL 20-YEAR PRESENT WORTH COST: - $4,150,000
Total Coal perth 20-Yr Nremoval 51.31
LewiabflPAxis PagetoV2
-------
PROJECT: ImplementIng aS mp h. Annual Average Total NItrogen Limit
PREPARED FOR: USEPA, Chesapeake nay Office
PREPARED BY: Virginia Tech with Stearns A Whaler, Lit
DATE. March 19,2001
FACILITY: Lebanon WWTP
LOCATION: Lebmion. PA
RATED FLOW: t oingd PECOD 175 virgiL
CURRENT EFFLUENT TN- tO ff lL PE TKN. 27 rag /I
EFFLUENT TN GOAL: 50 rng/L
NITROGEN REDUC 1 1ON: 350 tan
120 1000 lbs / yr
2409 1000 ibe/20-years
CURRENT PROCESS ICHECK ALL THAT APPLY): X MLE Existing Aerated Volume (MG). N s a
B€PR (Alt o. VIP. etc.) Existing Anoxuc Volume (MC ) Pile
— Bardenpho CurrenIMLSSalWunterADF N / a
— OxldaIuon Ditch
Lagoon (Bolac. ot)
CsclicaI Aeration
SUR
Hugh-Rate Brother
EfflueM Fltrflon
Other ______________________________________________________
CURRENT EFFLUENT AMMONIA-N. 05 vi rg /L X From Report
From Model (al ADF end bed. 15 d MQRT. ‘2 C wInter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.0 rapt:
X No ,noorti 5ons required New MLSS
Raise MCRTSMLSS f r i etdetlng tenka (check clarifier capacity) N /a
construct ad6eonal aerated vchpvue Flow (ned) ‘ ,O
Coititruttadd lb on l denim Flow (m od) -
Uae Britetbtg wioxt volume a, esubic (construct seperele dealt facility)
the eeratad eyslnn for SOD ranoval only (construct separate nit/dealt facility)
jntgowequalraatmntark
omer- r ..‘,.‘ - . “ e ”
PROPO5ED MOO IFICATIONS TO GET NITRATE C 1.0 mgiL:
[ JNO modittitelions required
H Add downateem DeW4IIbaSI rTethanob
Add downstream Nlrtblcelrcn Bioster aid DeNII tiller with methanol
Add methanol in erdaing 5NR wocoss
Add downstream anode tenkrdth methanol feed
Add eflbuergElballon
0 0 w _____________
CAPITAL COST Equipment sAd Structures (from Pea 2). 53.750 000
Eledrcal end Insumenta Iron 12% 5450 000
Yerd Piping end Site Work 15% 1503.000
Subtotal. $t76t000
Conuaotor 08SF 15% 1714000
Engineering and Consti. Mgfl 15% 1714.000
SubtOtat $5190000
Ccnbngeflcy. 30% 11.421.000
Total Capital Coa $7,621,000
Capital Cost per lb 20-Yr. N removal: $3.10
OPERATIONS COST: Additional Horsepower (from Page 2) 150 PIP
Electiloal P r Cost 0.05 SAW 152.300 5/year
Niketa Rethieben using MethanoL U rapt
Methanol Required: 150 psleld
Mepianol Cost: 0.16 $ el 541.100 5/year
Separate Stage Anunonra Reduction 0.0 niojL
Caustic Soda @25% colic 0 gele/d
Caustic Soda Cost 0.00 5/get 50 1/year
Equipment Melntenasice Cost 561.000 1/pear
Denrtrlllcebon Sludge Production wReIethanol. U0 ba/d
Sludge Disposal Cost. 490 Stir 135.000 1/year
Total Annual OeM Cost $100 300 S/year
(lieclive Annual Interest Rate elter Inflation 201%
20-Year Present Worth of OSM Coats $2,150,600
TOTAL 20-YEAR PRESENT WORTH COST: $ 10,470 . 000
Total Cost per lb 20 -Yr N removal $4.36
Lebanon tis Page b r 2
-------
PROJECT: Implementing .3 mgft. Annual Avenge Total Nitrogen Limit
PREPARED FOR: USEPA. Chesapeake Bay C i Rce
PREPARED BY: Virginia Tech with Steams & Whaler, tic
DATE: March 19.2001
FACiUTY Laac.s .( .WWIP
LOCATiON: LarSster. PA
RATED FLOW: 29.7 mgd PE COD Pita mglt.
CURRENT EFFLUENT TN. 1rmgit. PE TKN 22 mglt.
EFFLUENT TN GOAL; 3.0 mg/L
NiTROGEN REDUCTiON: 1240 Weld
453 1000 Ibe4v
9052 1000 lbsl20-yuara
CURRENT PROCESS (CHECK ALL THAT APPLY) X MLE Existing Aerated Volume (MG) Pile
— BEPR (A2z’O, ViP. Sc) Existing Anoxic Volume (MG) — N/a
Bardenptio Currer* MLSS ci Winier ADF N/a
Oxidation Ditch
Lagoon (Biolac dc I
Cyclical Aeralcn
S IR
High-Rate Rdillec
Effluent Filration
Other ____________________________________________________________
CURRENT EFFLUENT AMMONIA-N: 05 n’igll. X From Report
FrcmModet(atADF and load t5 d MCRT. 12°C winter conditions)
PROPOSED MODiF ICATiONS TO GET AMMONIA C t O fliglL:
X No modlficflone requIred New MISS
Raise MCRTIMLSS in existing tanks (check clanfler capadly) Pile
Construct addilioAai aerated volume Fiow (mgd) 0
Construolsddit lonaidadfleis Flow (mqd) 0
Use existing anoxic votaite as aerotac (construct separate denit Fac ulty)
Use aerated s o 1sm to , BOO removal oriy (construct separate nit/dent taSty)
Md Influent flow equaiizexn lank
ROPOSEO MOD1FICATIONS TO GET NITRATE C 10 mglL:
No modifucaixins required
X Add downstream CeNit filter with niethanoi
Add doerisbeam N*tboalmn si attttcr and DeNit filter with methanol
Add methanol be4sbng BNR procasa
Add downstreafnanoudt tank with methanol teed
Add effluent Iuiratlon
Other _________________________________________
CAPITAL COST Equipment arid Structures (tram Page 2) 511.350.000
Eiectncel alid Instrumentation 12% 11.352.000
Yard Piping and Site rk’ 15% 11,703000
Si tal 914 420.000
CU,4,CI.AiI OH&P. 15% 12,1 53000
Englneej lng and Ccnsv Mgmt 15% *2.163.000
Subtotat 11 1.750 ,000
Contngency, 30% *4.325.000
Total Capital Cost. $23,010,000
Capital Cost per lb. 20-Yr N removal: $2.55
OPERATIONS COST: Additional Horsepower (rroãi Page 2): 500 HP
EieeeIcsi P r Coat 005 lAW $102100 $ eer
Nitrate Reduction using Watielinr tO ingtL
Methanol Required: 550 plaId
Methanol Coal. 075 lIgal $153,300 $lyear
Separate Stage AmmonIa Redittion 00 net.
Caustic Soda 25% oonc * getsld
Caustic Soda Cost 05* Sleat 1* Siyaar
Equipment Maintenance Cost 9187 500 SIb /ear
Denstflcauon Sludge Production SMathanol flSO Weld
Slu d geDisposal Cost 400 Silon 1129.900 $fyear
TotaiMnuet O W Cost 1553 500 $Iyear
Eltecawe Annual retest Rate fler Inflation 291%
20-Yes Present Woinli of 0611 Costa 99,350000
TOTAL 20-YEAR PRESENT WORTH COST: $33030000
Total Cost pert 20-t I I removal $3.95
Lancaster. PA Page 1 of 2
-------
PROJECT: Implenienthlg• a nip. Aivntal AvenGe Total Nitrogen Limit
PREPARED FOR : USEPA, Cheaapealie say Office
PREPARED BY: VIr Irda Tech with Stearns & WheW LLC
pATE: March19 2001
FACIUTY: Hanistitse WWTP
LOCATION: I4emsbura. PA
RATED FLOW. 30.0 mgd PE COD NIe mg /I
CURRENT EFFLUENT TN: 40 mg /k PE TKN 16 mg/ I
EFFLUENT TN GOAL: 30 mg/I
NITROGEN REDUCTION: 250 thaN
01 i000balyr
1025 1000 tsl2O-yeers
CURRENT PROCESS (CHECK ALL THAT APPLY): — MLE Existing Aerated Volume (MG) N/a
— BEPR (A210. VIP. eta) Existing A/ lottie Volume (MG) N/s
Bardencho CurTail MISS at Winter ADF. N/s
Oxidation Oldi
LagoOn (Bidac. etc.)
C S Mm
S an
High-Rate mott ler
X Effluent Fifration
J Other. UNOX Pve00a AercboAnctdo OAFs
CURRENT EFFLUENT AMMONIA-N; d . C mgIt. From Repoit
From Model (eIADF enit load. 15 d MCRT. 1 3°C winter condltbas)
PROPOSED MODIFICATIONS TO GET AIIONIA <1.0 mgIL
X No niodificaliosle required - New MLSS
Raise MCRTIMLSS in etating tanks (cited’ clarifier capacity) Wa
Construct addttatal aerated volume Flow (rngd). a
Construct additional danflers Flow (mgd): 0
e existing anOsc volume as aerobic (construct separate donit facility)
Use aerated system t BUD removal only (construct separate nnldenit facility )
,nfluertt flow equaizatlon tank
oi l ier. -
PROPOSED MODIFICATIONS TO GET NITRATE C t O mg /I. _____
No medikSwla required
• Add downanam DeNit filter with methanol
Add dossadeam Nidlatloil Olofilter end DeNit filter with mee anol
Add methami be ttitfi BNR proase
• Mddownsem wiSe Wnkvâth met*d feed
‘Mdemantaa..
K Other MdMeIwd :. ?. - • .: •
CAPITAL COST: Equipment and Stases (from Page 2): 50
Electrical end ISMTIenSOII 12% $0
Yard Piping 55 15% $0
Subtota l. $0
Convatr CHiP. 15% 50
Engineethig end CflIr Mgmt 15% 50
Subtotat $0
Contingency 30% 50
Total Capital Cost. $0
Capital Coat t 20-Yr N removal $000
OPERAT(ONS COST: Additional Horsepower (from Page 21 0 HP
Electrical Poser Cost 001 58kW 50 S /year
Nitrate Ped ’ uslrigMettlaflol 1.0 mg/I.
Methanol Re Sed. ito gale/d
Methanol Cost 075 $10 530 .1 00 S/year
Separate Stage Ammonia fledudion 0.0 mg/I.
Caustic Soda 025% 0 gale n t
Caustic Soda Cost 050 S iQat $0 s/yew
Equipment MSttenanoe Coat $0 styear
Denitntlcatloflaidge Production witaeuwitct 300 lbs/d
Sludge Disposal Coat 400 SMt 5263005MW
Total Asvwal OSM Cost 550.400 S/yen
Effective Arstud kiterest Rate after litton. 2 5t%
20-Year Present Wore ’ at OSM Cost $$10 X0
TOTAL 20-YEAR PRESENT WORTH COST: $550000
Total Cast pert 20-Yr N removal . $047
Hatrisburg xix ce 1 of 2
-------
i 3 ROJECT. Implementing as mglLA.tnuel Avenge Total Ilbagen Umi
PREPARED FOR. USEPA. Chesapeake Say Office
PREPARED BY. Virginia Tech with Steams & Whaler, LLC
DATE; March19, 2001
FACILITY: Hano v er Ate. WWTP
LOCATION: Hanover. PA PE BOOS 135 mglt.
RATEOFLOW. 45 41100 PEG® Ni ’s mglL
CLIRRENTEFFLLIENTTN 12.__nlalL PETICN 30 rngll
EFFLUENT TN GOAL. 30 nigll.
MITROGEN REDUCTION 110 ma /d
40 1000 lbalyr
803 1000 Ibs’20-years.
CURRENT PROCESS (CHECK ALL THAT APPLY): : Existing Aerated Volume (MG) 4.28
BEPR (A2’O, VIP. et) Existing Anoxic Volume (MG). N /a
— Bsrdenpho Current MISS at Wirier AOF N/a
X Ondation Ditch
— Lagoon(Oiolat.etc)
Cydlcal Aeration
SM
High .Rate Blofilter
Effluent Filtration
Other ________________________________________
CURRENT EFFLUENT AMMONIA4I: 03 n /L K From Report
From Modal (at ADE and load. 15 d MCRT. 12 ’ C winter ndIbona)
PROPOSED MODIFICATIONS TO GET AMMONIA d o mglL:
K IND modifications required New MISS
JRaiae MCRTIMLSS In existing larks (diedt clarifier capaoty) thoo
T]Constnn additIonal aerated volume Flow (mgd) 0
JConsntt additional ctanflera Flow (mgd) C -
111.1st existIng anozic volume as obc (construct seperale danil laciliM
1] Use aerated system ior SOD removal only (construct separate nwdenlt facility)
IIJAdd irdluent 110* equalIzation IonIc
PROPOSED MODIFICATIONS TO GET NITRATE 41.0 mglL
E]No meddicatlons required
[ KlAdddewnstream DeNit filter with methanol
Add downstream Nititflcation Biofifter and OeN1I Alter wIth methanol
Add methanol to exIsting StIR preasa
Add downstream anedc tank with methanol feed
eflluaftt r4.tlon
— i ’ , s
CAPITAL COST; Equipment and Sliuctwee (Item Page 2) 52 ,550.000
Eledncal and Ins t rumentatlOft 12% $304000
Yard P pmg eno Site 15% 1380.000
Subtota l 55.210.000
CentradorOet&P. 15% 1482.000
Engineerng and Conair Mgr,r 15% 5482.000
Subtotst 54.110.000
ContIngency 30% 5953.000
Total Capital Cost $5,130,000
Capital Cost per lb 20.Yr N removal $6.39
OPERAT 1ONS COSTS Additional Horsepower (from Page 2) - 90 HP
Electrical Power Cost. 0.05 SAW 520.400 5/war
Nitrate Reduction usIng Methanol 30 mglI.
Methanol RequIred SO gatsfd
Methanol Cost 075 5/gal 513.700 S /year
Separate Stage Ammonia Reduction 0.0 mgi.
Caustic Soda @25% cAnc 0 gals/if
Caustic Soda Cost 0.00 S/gal 50 5/year
EQuipment Maintenance Colt 541.700 S /year
Denititficallon Sludge Production wiMathanol 180 bald
Sludge Disposal Coal 400 Mon 111.700 S/year
Total Atvtiret OVA Coat 595.500 5/year
Eftective Annual Interest Ralealtar Inflation 2 91%
20Yesr Present Worth of 0114 Coats. $1,450,000
TOTAL 20-YEAR PRESENT WORTH COST: $8,580,000
Total Cost per lb 20-Yr N removal 51.19
Hanovef als Pageto l2
-------
PROJECT: Wnptelnetttlflgt 3mg/ I Annual Avusags Total NItrogen Umit
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY: Virginia Tech wIth Steams & Whslsr. t.LC
DATE: March 10,2001
FACILITY: Greats ’ I(ntstoo %WI1P
LOCATION: j on . PA
RATED FLOW: t9n ’gd PE COD 180_n ’ S
CURREIITEFFLUENTN. 80 mg/I PETKN’ 25_mg /I
EFFLUENT TN GOAL: 30 mg/I
NITROGEN REDUCTOIC 370 lba/d
135 1000 lbs /yr
2701 1000 lbsl2O-years
taLE
BEPR (M I D. VP. sic)
Bwdenpho
Oxidatioll atti
lagoon (SlSn dc)
Cydical Abration
SSR
Hugh-Rate Siotiller
Effluent Filtration
Other
CURRENT EFFLUENT AMMONIA-N: 32 mgII. From Repel
- - X Front Model (atPOF and load. 15 d MCRT. it C winter uxdtlona)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.0 mgit
No modIficallona requwed New MISS
Raise MCRTIMLSS Ut dstlfl9 tank; (check clarifier capacity) ______
Confltjdadthbonat aerated volume Flow (mgd) 0
Conseua ibonal derlI lera Flow (mgd). C
Use ensbn anoicle volume as aerobic (cons truct separate denlt fa tuIty)
Use aerated system (or SOD re-noval only (construct separate natldenit laoluty)
Add inhluent soar equalization rank
K Other Abandon adivatad sludoe stoats and use holtiter ( or all flow
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 nigh:
[ ]N. niocificabona required
K Add downstream DeNd Mar with methanol For all 0 mgd
Add downstream tlltdfatiedt Blofilter and OeNit sitar weli methanol
Add mqthanol te eMsiitg StIR P006 55
- Add donflum ano,sc t at with methanol feed
Add Sflrsd MUISOn - -
X Other Add dda,sj .,nMS&AetvtIC Slo llter totS 41 sd4
CAPITAL COST:
Equuptvwll cad Structures (hum Page 2)
InstnhhlentatlOlr 1215
51,990 ,000
5959,000
BeWucal
Site Woik: 15%
51.1*000
Yard PIping
SubtotaL I
15%
Skl.tSO.000
$1,523,000
Contractor 0K W
EngmeenngandConfl Mgit 15%
Si*total.
30%
$1523000
113.200 ,000
$3,04L000
Conlinganc$
$16,250,000
Total Capital
20-Yr N removal:
$02
•
Capital Cat pert.
530 HP
OPERATIONS COSt
Adduluonal Horsepower (from Page 2):
Electrical P r Coat 005 5 1 KW $173200 S/year
Nitrite Reduction using Methanol 5.0 mg/I
MaIMS Required - 170 gala/d
Meiftenol Cost 075 Seal 146.500 S /year
Separate Stage Ammonia Reduction 00 mg /I
Caustic Soda 25% conc 0 galald
Caustic Sods Coal 060 Seat $0 $&ear
Equipment Maintenance Coat - 1132.000 S/year
Oen’tflfoebon Sludge Production witasthat. 530 bald
Sludge Disposal Coat 400 SM ’s - 1*700 5/year
Total Annual 001 Coat 1390.400 5/year
EffectuaeAnitual Interest Rate slier Inflation. 191%
20-Year Present Worth of OW Coat $5,990,000
TOTAl. 20YEAR PRESENT WORTH COST:
Total Cost pert. 20-Yr N renioval.
$22,110,000
I L l S
CURRENT PROCESS (CHECK ALL THAT APPLY): I
x
Existing Aerated Volume (MG) 03
ExIstIng Artoxic Volume (MG) 021
Current MISS at Winter ADF. 3500
Adjusted for Special Condition
Greater Kaztoton PA xIs
Page 1 of 2
-------
PROJECT imgtementmg a S mfl Annual Avenge Total Nitrogen Limit
PREPARED FOR: USEPA. Cheeapeeke Bay Office
PREPARED BY: Virginia Tech with steams 8. Whaler, LLC
DATE: March 19 . 2001
FACILITY: Susquehanna WWTP
LOCATION: I.anceaterArea. PA
RATED FLOW: 12.0 mgd PE COD 220 mgIL
CURRENT EFFLUENT TN: 0.0 mg/I. PE flCN . 24 ing/L
EFF WENT TN GOALt Tömg i t.
NiTROGEN REDUCTION 500 theM
103 l000ibs.’yr
3050 1000 lbe/20.yeart.
CURRENT PROCESS (CHECK ALL ThAT APPLY): MLE EsJebng Aerated Volume (MG). i s
— SEPR (A210. VIP. etc.) Exlsdng Anoxic Volume (MG) 0 044
— Baadenptio Current MISS at Winter ADF 3600
— Oxidation Ditch
- Lagoon (Biolac. etc.)
C1,vlteai Aeration
S M
: HTgh.I te
— Effluent Filtration
Other ____________________________________________
CURRENT EFFLUENT AMMONIA.N: cj,0 mg/I. X From Repoil
From Model (at ADF and load. 15 d MCRT. 12°C winter conditions)
PROPOSED MOCIFICAT1ONS TO GET AMMONIA C 1.0 ,nglL
fliomod lticationa required New MISS
IIIRaIae MCRTIMI.SS In eatIng tanks (check clarifier capacity) N/a
Tlcons lruct additional aerated volume Flow (mgd) 0 ’
Jconstnid additonal dermflers F low (mgd) 0
TiLls . .xldng anoxic volume as aerotlo (construct separate dent facuuty)
T]Uae aerated ayshelt lot BOO removal onlirfooneiruol separate n lt/denit factiuty)
lAdd hdluent 1 10w equstzatma tart
]omer ‘ - “ .
PROPOSED MODIFICATIONS TO GET NITRATE ‘c i .0 mg/Lt
No moditcations —
downstream VoMit 2u with methanol
- downstream Nietficeffon Buofilier and OeM / I filter with methanol
Md methanol to . 4.4 .. , StIR procesa
Add downstream anoic fank with methanol feed
Add effluent fllirallOn
Oilier ______________________________________
CAPITAL COST Equipment and Stnrctrres (from Page 2). S t 150.000
Electrical and tnstiunentatron 12% 5615 000
YardPlpungandSftcWoffi 15% 5773.000
Sublotat. . St 540.000
Contractor OHIP 15% 5901.000
EngineerIng and GonaD Mgmt 15% 3001 000
Subtotal 38.500.000
Contingency 30% 31,002.000
Total Capital cost 510.460000
Capital Cost per lb. 20.Yv N removaI $2.57
OPERATIONS COST: Additional Horsepower (from Page 2) 240 HP
Electncal Power Coat 0 ,05 5/kW 578400 $Iyaar
N/Irate Reduction using Methanol. to nigiL
Methanol Requlred 230 gab/d
Methanol Coat. 075 S/gal 503.000 S/year
Separate Slage Mimonus ReductIoff 00 mg I.
Caustic Soda @25 ’ cone 0 gala l s
Caustic Soda Cost 000 S/gal 50 $4ear
Equipment Maintenance Cot $85000 S/yet
Denutrifloatlon Sludge Production wSAethrd 720 loaM
Sludge Disposal Cost 400 S/ton 552.000 S/yet
Totat Annual OSM Cost 5278 000 S/year
Effective Annual Iniereat Rate after Inflation: 201%
20 Year Present Worth or ow Costs: $4,180,000
TOTAL 20 -YEAR PRESENT WORTH COST: 514340,090
Total Cost per 10 20 Yr N removal $4.01
Susqueflanna xi i Page I oi 2
-------
PROJECT: lmplemsntlng .3 rag iL Annual Average Total Nibogen UlIti
PREPARED FOR: USEP& Cheespeeke Bay Office
PREPARED BY: VirginS Tech with Stearns $ Whaler. LLC
DATE: March 19.2001
FACIUTY: Droop WWTP
LOCATION: LSC Ina REM. PA
RATED FLOW: 7.0 ingd PE COD 100 mgIL
CURRENT EFFLUENT TN: to mglL PE TKN:_ _rngIL
EFFLUENT TN GOAL 3Ounq1L
NITROGEN REDUCTION: 290 tbsld
106 t000Ib$i
2117 1000 Ibaf 20 jeers
CURRENT PROCESS (CHECK ALL. THAT APPLY): R MLE Exising Aerated Volume (MG). 2.025
BEPR (A2JO VIP. etc) Existing Anojoc Volume (MG) 0115
Oardenpflo Current MLSS at Winier AOF 2300
Oxidaicn Ditch
Lagoon (BiOlac. eta)
Cyclical Aeration
SOR
FbnJi.Rate Biofiller
Eliluerd Filtration
Other _________________________________________________________
CURRENT EFFLUENT AMMONIA-N: 24 mgfl. From Reporl
X FromModsl(atADF endload. IS d MCRT. it Cwinter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1.0 mglL
E]Nomodilcallons reqtired New MISS
X Raise MCRTIMLSS In exIst I ng tank; (dteck daniter capacity) _______
add Wonal laratad volume Flow (mgd) O
Conatud addltlomcladllers Flow (mgd) ______
the ezathig anosc volume as aerobic (construct separate dent taSty)
Use arMed system for DOD removal only (construct separate nivdend teciI4)4
Add kifluerd tow epualatlon tank
Other ___________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE dO mglL:
No modIfications —
A Add dowiwiream D e ll OIler md i methanol
Add doensheeni Nitdleattn BioSiter arid DeNit filter with methanol
Add methanol to existing BNR procose
Add ootnstraam anoxic tank Ct methanol teed
Add aliluent lIl vatiolt
Othr _________
CAPITAL COST: . Equloment end Stnictirea (from Pegs 2): 13.400.000.
Electrical end thstnattentaWn 12% 1401000
- YaitPiplngandSiteWad c 15% *510.000
SubtotaL 64 . 220000
Contrast OH&P. 15% 1646000
Engineering andConW Ifont 15% 1545000
Subtotat 33.020.000
Contingency 30% 11201000
Total Capital GoaL 16.9*000
Capital Coat per lb. 20-Yr. N removal $3.27
OPERATIONS COST: Mdkional Horsepower (train Page 2 140 HP
Electrical Power Gist 0.03 1 1KW 145700 $dyaer
Nitrate A iCon using aiethant 5.0 molt.
Methanol RequIred 130 —
MetItand Coal 075 Slgal 535.600 Miser
Separate Stage Anvnonls Reduction 0.0 ut’iglt.
CeuaDcSOda©25%cOl ’c Ogale ld
CeuaticSedaCosi 060 llgal $O s lyear
Equçnant Maintenance Coat 556.200 Slyest
Dendrtllcatsi Sludge Produdion wiMeihanol 420 lbsld
Sludge Disposal Cost 400 Mon 530700 Slyear
YotaSA ,mual OSM Cost $158200 $lyesr
Effe&ie Mutual Interest Rate after Inflation. fl1%
20-Year Present Worth of OSM Coats $2.420000
TOTAL 20-YEAR PRESENT WORTH COST: 11.440.000
Total Coat per lb 20-Yr. N removal- $4.46
Throop. Lacliawanna. PA ala Page 1 of 2
-------
PROJECT: Implementing a a mgIL Annual Average Total NItrogen Limit — .
PREPARED FOR: USEPA. Chae.paake Bay Office
PREPARED DY Virginia Tech with Steama & Whaler. LLC
DATE: Msmh 19, 2001
FACILITY: 5usquehanna WWT !
LOCATION: La rea, PA
RATED FLOW: 12.0 mgd PE COO’ 220 iTIgIL
CURRENT EFFLUENT TN: Trmg/L PE TKN 24 ngIt.
EFFLUENT TN GOAL: mgIL
NITROGEN REDIJCflOpi: 500 Ibsld
183 l000IbsIyr
3650 1000 1bs120-years
CURRENT PROCESS (CHECK ALL THAT APPLY): X MIE EJdate’$ Aerated Volume (MG). 1.9
BEPR ( M m. VP, ate) Existing Anojoc Volume (MG) 0944
Bardenpho Currant MISS au Winter ADF seod
Diddaton Ditch
lagoon (Blulac. sic)
Cydcal Aeration
SBR
Higli-Rate8idUtar
Effluent Filtration
Other ___________________________________________
CURRENT EFFLUENT AMMONIA-N ci 0 mgit X From Report
From Model (at ADF and load IS I MCRT. it C winier conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA <1.0 mglL:
(liMo inoddicatlons required New MISS
Raise MCRTIMLSS In eidsting tanks (check clarIfier capaciM Wa
Constn MdiSa aerated voltane Flow (mgd) 0
Conwuct adddlonl daffilers Flow (rngd) - 0
Use existing afloat volume as aerobic (construct separate daM facdity)
- Use aerated syatern for DOD removal oily (conatiud separate nitldend ledlity)
- Add trifluent boa equalization tank
• 01St. ! • -
PROPOSED MODIFICATIONS TO GET NITRATE c I a mglL:
‘.- No modificatons required
X Add downstream Detit tuier wi megiatiol
downturn NItiIOca3on Bluffer and DaNit liter wit methanol
methanol te exlateq StIR proowa
Add doan teum anSa * with methanol feed
Add effluent ton
Other . -
CAPITAL COST. Equipmanu and Stuctires (from Page 21 35 150.000
Electrical and Instrumentation 12% s&ieooo
Yes Piping and Site Work. 15% 3773.000
Subtotal 55.340 000
ContractorOH&P - 15% 5901.000
Engineenrg and Conav Mgint 15% $08i 000
ubtotaL 36300.000
Contingency 30% 31.962.000
Total Capllal Cost SI OAG O, 000
Capital Cost per lb 20-Yr N removnt 2fl
OPERATIONS COST: Additional lioztepowr 1 1mm Page 2) 240 HP
Electrical Power Cost. 005 3 1kW $76400 ter
Nitrate Reduction using Methanol SO mfl
Methanol RequIred 230 plaId
PMths,d Coat. 0.75 $Igal 363 000 Slyest
Separate Stage AmmonIa Reduction. 00 InwL
Caustic Soda @25% conc 0 galS
Caustic Soda Cost. 000 algal $0 &%ear
Equipment Maintenance COIL 385.000 VS’ear
Danitrlllcatlon Sludge Production wiMethanol. 720 maId
Sludge DIsposal Coat- 400 Mon $52600 $lyear
Total Annual 0814 Cost 3279000 $IWar
Effective Annual Interest Rate after MUtation 291%
20-Year Present Worth of O W Cost 34 . 1 10 .000
TOTAL 20-YEAR PRESENT WORTH COST- 314 ,640.000
Total Cost per l b 20-Yr N removal u_e l
Susquehanna xis Page 1 o12
-------
PROJECT. Inuplamentlnge $ mgt Annual Average Total Nivogen UmIt
PREPARED FOR: USEPA. Chesapeake Say Office
PREPARED BY: Virginia Tech with Steams $ Whaler, LLC
DATE: March 19, 2001
FACILITY:’ WillIam eport Central WWTP
LOCATION: W! ns polt PA .
RATIO FLOW: fl_ rngd PE COD. 268 ungIL
CURRENT EFFLUENT TN: 184 mnJi. PE TKN 32 rnglL
EFFLUENT TN GOAL: i7 rtgtL
NIThOGEN REDUCTION: 920 ibsfd
338 i000lbs1 t
6718 1000 lbs/20-yeara
URRENT PROCESS (CHECK ALL ThAT APPLY): I SALE Existing Aerated Vdunie (MC). 1.061
— BEPR flit, VIP, etc) Eidsturug Anoxac Volume (MG) 0J225
— Bardsnp lto CusrentMtSSatWunterADF 1318
Oxidation Dil l ’
— Legoon(BioIac. 810)
Cyclical Aeration
SBR
— Hugh-Rate BluSter
Eflk ent Filtration
:00 -
CURRENT EFFLUENT AMMONIA-N. 16.7 mg/I. X From Report
From Model (aIADf and load. 15 d MCRT 17’ C writer wtOul’ons)
PROPOSED MODIFICATIONS TO GET AMMONIA cl.O niglL:
No modifications requited New MLSS
X Reuse MCRTIMLSS in eirueling tanks (checic clarifier capacity) 4000
Construct addilicnal aerated voluMe Flow (mgd) 0
X Construct additional de n Im . Flow (mgd) 2.8$
use easing anosuc volUme as aerobic (cQns(rud separate dens lacilky)
(isa petaled system fat-BOO removal only (construct separate nltldenut Facility)
Add Sent ltoweoualuaarion ranuc
PROPOSED MODIFICATIONS TO GET NITRATE c 1.OnuglL:
No mcdlficatlons requirad
Add downstream DaNk liter vddt methanol
- Add downstream Nftuicadon liG hter and DeN t l ute, with meliald
Add methanol to . aa cag MR pmoaea
- dddowv*esnanostctaric at nwthanol Seed
-: Add ellusctflltSurn
— Other - r ’ l fl “ ‘iT” ” ‘ “i - - -
CAPITAL COST: Equipment and Structures (from Page 2) $4,730,000
- Electrical end InstrumentatIon: 12% $588,000
Ysud Piping end Site WaIt 15% 5710.000
stoioooo
Contractor 01-ISP 15% 5902000
Engineering arid Consti Mgml 15% $902000
Subtotal $1,810,000
Coritingency 30% 51.803.000
Total Capital Coat $1,110,000
- Capital Cost per lb 20-Yr N removal $1.43
OPERATIONS COST: Addubonai Horsepower (rrOm Page 2) 140 HP
Bectral Power Coal ods 5 1kW 545.700 sipm,’
Nitrate Reduction using Methant 50 nugIL
Methallol RequIred 140 galafd
Methanol Cost 075 $Igai 5*300 $4ear
Sepdrata Stage Ammonia Raductuoti tO mg I.
Cm. Soda 25% mc. 0 gaWd
raisu . Soda Coat. 0 80,$Igal 50 tlyear
Equipment Maintenance Coat. 578,100 $/ wer
Uwtllztllcatlon Sludge Pnducaons isnt 430 taM
Shape Disposal Cost 400 Mon P1400 84w
Total Annual 08W Cost 5193.300 $4’ear
Effective Mnuat interest Rate after ht8ation: 291%
20-Yew Present Worth of OUt Cost $2,100,000
TOTAL 20-YEAR PRESENT WORN COST: - 5 1Z 8 $8,000
Total Coat per it 20-Yr N removal $188
‘ Mtpon Centrai ris Page 1 of 2
-------
PROJtCT: lmplemsnthig a3 .iglL Annual Average Total NIflgofl LImIt
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY: VIrginia tech with Steams & Wtteler, LLC
DATE: March 19, 2001
FACil ITY. W llltans port West WWTP
LOCATION: W llliemepod , PA
RATED FLOW: 4J mga FE COD $00 mgfl.
CURRENT EFFLUENT TN: 8.0 mg I. PE TKN $7 niglt.
EFFLUENT TN GOAL: 3On lgIL
NITROGEN REDUCTION: 100 ts/d
50
1367 1000 ibsl2O-years,
MLE _________
BEPR (A210. V IP. etc.) _______
Badenpho _____
O xidation Ditch
Lagoon (OtOlaC etC)
Cyclical Aeration
StiR
High-Rate eiordlei
Effluent Fdtration
Other ___________________________________
CURRENT EFFLUENT AMMONIA-N ’ 26 mg /I From Repoit
X From Model (aIADF and load. 15 d MCRT. if C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1 . 0 mgIL:
rnNo modlficaXns required New
Construct additional aerated volume Flow (mgd)’ 0 ’
Construct adthbonal darlilers now (mgd)’ “0
Fe MCRT/MLSS ki exisling tanks (check denSer capselty) ______
Use existing a’o ac volume as aerobic (construct separate donut lacthty)
X Us. aerated system kr BOO removal only (construct separate nit&Ienst tastIly)
Add mfluent flow wpddketucn tank
owefl ‘ “ “ ‘ .
PROPOSED MODIFICATIONS TO GET Nrl’RATE c l.a mglL
No modIfications requIred
Add downstream Bes et litter with methanol
Add downstream Ndrlflcabcn Biotliter and DeNut filter with methanol
Add methanol to ettig BNR process
A o l downstream sicec lank with methanol feed
Add effluent aaeo .
Other ______________________________________________
CAPITAL COST. Equipment and Structures thorn Page?) 54,000 001)
Electrical end Instrumentation 12% 1576,000
Yard Piping and Site Worn, 15% 3720.000
Subtotet 56,100,000
15% 5015,000
15% 1915.000
Sub tote r. $7,930,000
Cont lngency 30% 51830,000
Toial Capital Cost $9,780,000
Caplial Cost per lb. 20-Yr. N removt $704
Additional Horsepower (from Page 2): 1 0 NP
Electrical P Cost 005 1 /kW , 558.800 $4rear
NIPS Redirotsi using Methanol “S
Methanol RequIred. 90 gale a t
Methanol Cost 0.75 1/gal 524.600 SNeer
Separate Stage Ammonia Reduction. 0.0 mgIL
Caustic Soda @25% cont 0 gaJs
Caustic Soda Cost- 060 a lgal SO S /pear
EquIpment Maintenance Cost’ $79,300 S/pear
Denrtnflontlcn Sludge Production wiMethapol 270 taM
Sludge Disposal Coal. 100 5/ton 5t9 700 3/pear
Total Annual O&M Cost $182,400 3/peat
Effective Annual Interest Rate after Inflation 291%
20 Year Present Worth of 0tH Costs’ 52 .740,000
TOTAL 20-TEAR PRESENT WORTH COST $12 ,500,000
Total Cost per lb 20-Yr N removal 59.01
CURRENT PROCESS (CHECK ALL THAT APPLY): )C
Existing Aerated Volume (MG) 0.09
Existing Anordc Volume (MG). — 0.33
Ctnent MISS at Winter ADF: 4500
OPERATIONS COST:
Wulliemaport West PA xIs
Page 1012
-------
, ROJECT: - bn lemeSng a $ snfl Ma cal Average Total Ntbvgen tIre s
PREPARED FOR: USEPA, Chesapeela Ray Office
PREPARED BY: Vlrghila Tech wIth Stearns & Whaler, tIC
DATE: March19, 2001
FACILITY: W yomIn g VeiNy WWTP
LOCATION: Lineme D i v. PA PE 8006. 200 mgsl.
RATED FLOW. 32.0 mgd PE COO: NM rngIL
CURRENT EFFLUENT TN: jQ_mgiL PETKN _ 27 mg/L
EFFLUENT U I GOAL: 30 mgiL
NITROGEN REOUCTIOPF 1330 lbsld
485 1000 tbslyr
9709 1000 lbslZOjeets
CURRENT PROCESS (CHECK ALL THAT APPLY): 3 MLE Existing Aerated Volume (MG). 1.34
BEPR (A210. VIP. etc.) Exsbng Anoxic Volume (MG) 0.334
Oardenpho Current MISS at Winter ADF 3000
OxIdaIb Ditch
— Lagoon (Blotac sic)
X Cydical Aarstson
5 8 k
HIgh-Rala Sict)tter
— Effluent F htration
A Otber Sdirelber Process
CURRENT CF FLUENT AMMONIA-N: d. C mgA. X From Repast
From Model (at ADF and load. IS d MCRT, 12°C winter ccnditlcna)
PROPOSED MODIFICATIONS TO GET ANMONIA C 1.0 mgIL:
X Nontodtheabonsreqtdmd New MLSS
• Raise MCRTMLSS hi existIng tanks (check øadfNr capacity) P ta
C0t15M101 sddttlooal seited vcttaue Flow (mgd) 0
Coiletnct eddiSonat c*tlstn now (mgd) 0
Use existtng anoix volume as eetebc (const%fl separate daM Iaakty)
Use aerated system for GOD temoval only (consbvd separate niI/donlt tecitity
titant flow eqcm mn tart
Other ‘ 1 ”
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 reg aL:
No modiflcebats —
downstream OeNlt Met with methanol
downalreamjlitdfleation BóSIer and DeNit flier with methanol
Add methanol to Siting 5*1 5 process
Da d domistreeru angeIctanli *15 methanol teed
efluent filbation
Other , _____________
CAPITAL COST: Equipment end Stnflns (from Page 2) 312.150.000
Electncal and flislrumoitla bon. - 12% *1.4*000
Yard Piping end S i te W0& 15% 11. 123.000
Subtotal. *15.430 ,000
Connr lorOPtSP . 15% *2.313.900
Engu’ieemig and Cons Mgmt 18% $2,315,000
Subtotal 320,000,000
ConIlngenW 30% 14.629.000
Total Capital Coat: 124 5 10 ,800
Cap ital Cost pert. 20-fl N removal $2.04
OPERATIONS COST: Mdittensl Ilomepower (from Page 2). 040 HP
Eleattal Power Cost 005 3 1kW 3209.100 Slyest
NItrate Reduction Mg Mathanot tO mgt
Methanol Reqsred 610 gSM
Methanol Cost: 0.75 $ aI $167000 34’ear
Separate Stage Animattls Reduction: 0.0 W-
Caustlo Soda © 25%wic. . 0 galsM
CaustcSodaCost 060$lgaI $0$lyeas
Equipment Maintenance Cost. 1200.680 St’year
Oendrdlcalton Sudge Production u i ttlethanol, 1920 bId
Sludge Disaoeal Cost’ 400 siton $140200 5I ear
Total Annual OW Cost P16 ,900 Slyeer
Effective Annual interest Rate altar Intlabon 2 1 1%
20-Year Present Welt of OW Costs $10,T60,000
TOTAL 20-YEAR PRESENT WORTH COST: *35.40,000
Total Cost pee lb 20-Yt N removal $3.65
wyoming Valley x Is Page I of 2
-------
PROJECT: Implementing aS mgIL Annual Average Total NItrogen LImit
PREPARED FOR USEPA. Chesapeake Bay Office
PREPARED BY Virginia Tech with 5tearna A Wheler. tic
DATE: March 19, 2001
FACILITY. York WWTP
LOCATION: Yak. PA
RATED PLOW. 260 mgd. Pt COD 200 rng’L
CURRENT EFFLUENT TN 80 mglL PE TKN 16 mglt
EFFLUENT TN GOAL 30 mglL
NITROGEN REDUCTION. 1080 Ibald
394 1000 lbsIyi
7804 1000 Ibs/20-yflra
CURRENT PROCESS (CHECK ALL THAT APPLY): I MLE Existing Aerated Volume (MG) 901
BEPR (A210. VIP. etc) Ex lsling Anoxic Volume (MC). 2.05
Current MLSS at Winter ADF 3600
OxidatIon Ditch
Lagoon (Blolac. etc)
ydicni Aeration
SM
HIgh-Rate BluSher
Oawir -
CURRENT EFFLUENT AMMONIA.N Os mg/L X Fiom Reposi
From Model (al AUF ari d load 15 d MCRT. 12’ C winIer nonditions)
PROPOSED MODIFICATIONS TO GET AMMONiA c tO sng/L
X Nolnodlilcetbnsreqtdred New MLSS
Raise MCRTIMLSS In existlig tanks (check clatter capacity) N ra
Consirud additional aerated solume row (mgdj 0
Corwtruct additional darters Flow (mgd) 0
Use costing anoxc volume as aerobic lconslrua separate den lt tacllity)
l isa aeraled system tot 600 removal only (construct separate niti’denit tacitly)
Add ,rfkient flow equabzation tank
Other. ____________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 mgi.:
No modifications required
Add downsteam OeNst fitter vath methanol
Add downstream Nitnitcatson BloMer and DeNit Mer with methanol
Add rne(liatel to existing BNR process
X Add downturn anoido lank with methanol lead
Add effluerditralon
OUr. . ;‘ç -. ‘.w r:.. “7 ;
APITAI. COST: Equipment and Stucteres ( tan Page 2) 55.4 60.000
Electrical and tnatrumeritatlon 12% $654600
Yard Piping and Sit. Wolk: 15% $018000
Subtotal. 56.920.000
Contractor OH&P 15% 11.039.000
Engineering and Conair. Mgmt. 15% 01.039 000
Subtotal 19.000.000
Contingency. 30% $2,076,000
Tctal Capital Cost $t1,080.000
Capital Cost perth 20.Yr N removal $141
OPERATIONS COST Additional Horsepower (from Page 2) 390 HP
Electrical Power Coal 005 SSiW 1127.400 S/yea’
flhtrale Reductmn using Methanol. 5.0 nlg/L
Methanol Required. 490 gais/d
Methanol Cost 075 Slgal 5134.100 S/year
Separate SIege Ammonia Reduction 0.0 mgi.
Caustic Soda @25% conc. 0 galsld
Caustic Soda Cost. 0005190 $0 S/year
Equipment Maintenance Cost $90000 S/year
Danitritiostion Sludge Produdion w ltaaihanol 1560 lbsld
Sludge Disposal Cost. 400 Mon $ 113.000 S/year
Total Annuel OSM Cost 5455.400 S/year
Effective Annual Viterest Rate sitar InflatIon. 291%
20-Year Present Worth or OW Costr 15,980 000
TOTAL 20-YEAR PRESENT WORTH COST: 510,050.000
total Coat per lb. 20-Yr N removal $2.29
York PA xrs Page I or2
-------
SUMMARY COST SHEETS FOR THE
14 MARYLAND WWTPS
8
-------
PROJECT: ImplementIng a 3 mgtL Annual Average Total Nitrogen Umit
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY: Virginia Tech with Steams & Whe Iar, LLC
DATE: March19. 2001
FACILITY: BOwIe TP
LOCATION: Bowls. MI )
RATED FLOW 22 PE COD Wa mg/I.
CURRENT EFFLUENT TN. g IL PC TKN — We rngiL
EFFLUENT TN GOAL: 30 mg /I.
NITROGEN REDUCTION: 10 tald
4 l000lbs/yr
73 1000 Ibs/20.yeers
CURRENT PROCESS (CHECK ALL ThAT APPLY): — MLE Eiaating Aerated Volume (MG). His
X 8EPR (fl/ a. VIP sIc) EsistinoMo’ncVthne(MG) H is
— Bardenpito Current MLSS at Winter ADF- 4000
X OXidation Ditch
Lagoon (Blolac, etc)
Cyclical Aeration
- S M
high-Rate StaRter
— Effluenl Filtration
X OI lier Anaerobic Basin followed by 2-stage Bnjsh Aerator Oxidsllon Ditches —
CURRENT EFFLUENT AMMONIA-N 02 nrg/L X From Repori
From Model (at ADF and load. 15 d MCRT ‘2’ C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1 .C mg/L.
RIN G mOdIJICeUOIIs required New MLSS
•TIRaI5eMCRT6MLSS In existing tanks (chedcdarlllercapaclly) N /a
JConstnctaddit lonalaera ledvclunie Flow (mgd). 0 -
JCcnstruct additional clanliers Flow (mgd) 0
Juse eioatlng anotdc vokatie as aerobic (construct separate denut faaluty)
]Use aerated system for BOO re’noval only (construct sepamie nuWenit facililyj
.I]Add Inhluent flow equalization Ionic
jOther I tT
PROPOSED MODIFtCATIONS TO GET NITRATE c 1.0 mg4.:
No modlllcallons required
• Add downstream DeNIt lItter with methanol
,afr m NIilhSeatcn Biofllterand Deflitfilterwith methanol
- methanol i n existing BNR process
• Add dOenstreaTi anoxieteflic with methanol teed
effluent filtration
Oilier ____________________________________
CAPITAL COST: Equipment and Structures (from Page 2) 5250000
Eledrcal and kuslrumentslron 12% 530.000
YsrdPçingsndSiteWork 15% 138000
Subto l al $320 000
Contractor QH$P 15% 548,000
Engineering and Cons Mgrlit 15% 545.000
Subtotal - 3420 000
Cc rdi igsncy 30% 596,000
Total Capital cost $520,000
CapdalCostpert 20-YiN rantoval 57.12
OPERATIONS COST. - Additional Hoqsapower (from Page 2)- 0 HP
Electncsl PC Coat 0.05 3 /KW 50 5/year
Nitrate Reduction uaa’g Iotefliano& 0.0 L
- Methanol Reqsrad. 0 plaId
Methaici Cost .0 15 3/gal $0 3/yew
Sepfla Singe Ammonia ReductIon 0.0 mg/k
CausticSods o26% conc 0 gals/ri
Causes Soda Cost 060 S/gal $0 3/year
Eqwpmenl Matiulenana Cost 34.200 S/Star
Denitrdlcabon Sludge Prediction w/Methanot t o Ibald
Sludge Disposal Cast 400 3/ton 51001/yew
Total Anisial O&M Cost 54.900 1/yen
Eftecive Anrsjal interest Rate alter Inflation 291%
20 Ye ar Present Worth of O&M Costs 510.000
TOTAL 20.YEAR PRESENT WORTH COST: ssse.ooo
Total Cost pert 20.Yr N removal $505
Bowia.MOxIs Page 1 of 2
-------
PROJECT: - - - - Impletnen dag aS mgiL Annual Averegs Total Nltregen Uinft
PREPARED POt IJSEPA. Chaaapeake Bay Office
PREPARED BY Virginia Tech with 5teama & Whaler. U.C
DATE; MsrcN l l,2001
FACILITY: Bruna e deic WWTP
LOCATION: flnaw,âdc. MD
RATED FLOW: 07 mgd P t COO 250 mgIL.
CURRENT EFFLUENT TN mglL PE TKN 34 mplL
EFFLUENT TN GOAL: 3.0 m Il.
NITROGEN REDUC 1 1ON: 30 lbald
11 1OC0Iba/ e
219 1000 1bs120-yeara
CURRENT PROCESS (CHECK ALL THAT APPLY) MLE E4sUng Aerated Volume (MC) 0.234
— BEPR (*210. VIP. at) Exisbng Anoac Volume (MG) _______
— Sardenpflo Current MLS$ at Winter ADE 5500
— Oxidation D’d CØucallyAera lod
— Lagoon (6 . 01st. alt)
I CyClIcal Aeralcn
S OR
— High.Rate BoSiter
— Effluent F.lflh.on
0 m w ______________
:URRENTEFFLUENTAMMONIAJI. C l 0 mgIL X Frosnflepwt
From Model (aIADF and bad. 15 d MCRT. 12’ C wintet conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C VP mgIU
X No mod lScatlens requfred New MLSS
— RaIse MCRTIMLSS i i Sating la st. (d uCt daitSer capacity) ______
r Constnfl aR&uS nested chime p ( ) ._.
: Consfiud adi*fl daitliera Flow ( mgd):’ 0
— Use eidsllng iliac v tam U aerobIc (con inG esparate dm11 fadhily)
— Use aerated system W BOO removal only (construct saparaie ndldenlt facility)
dkanl . S 5S i t enk -
PROPOSED MODIFICATIONS TO GET NITRATE dO
No modification reqiired
Add downstream Deli Slflth meIha oI
IJfraafl NItilIlcattost BloOlter and OeNuI Otter wil l methanol
Add methend to u , * l ENS pccass
Add dowiustreahl anciac lank with methanol feed
Add effluent Sb n
Othst ____________
CAPITAL COST Equipment and Sbucluruti (from Page 2) 31.300000
Dectricat stud Inalrutnentatlon 12% $158000
YardPip.ngandSlfeWonk. 15% 3195.000
Subtotal *1.650000
Conagor Ol-I&P. 15% 3248.000
Engineenrig and Consti Mgml 16% 3248.000
SW.otaF 12.150.000
Contingency 30% 5496.000
Total Capöl cost 12 ,550 .000
Capitol Cost per lb 20 -Yr N removal. $12.10
OPERATIONS COST: Additional Horsepownr (from Pag ; 2) 10 HP
Electitcal P Cost 005 MiW 53.300 $I)ear
Nitrate RSUoda1 usIng Methanol, tO ing iL
Methanol Requked 10 galS
Methanol Cost 075 Imat 52.700 $I t&
Separate Slage Ammonip Reduction’ 0.O v i rg iL
Caustic Soda @25% cairo. 0 gslstd
Caustic Soda Cost 060 Imal $0 Sitter
Equipment Maintenance Cost 521.500 Slysar
OenMllcatlon Shidge Production wiMeihad. 40 ibaid
Sludge Olapoeal Coat ‘400 IRon 52.900 Slyear
Total Annual OSM Coe l 330 400 Slyear
Effective Annual lniereat Rate atlas Inflation, 291%
20-Vea l Present WOe. ol OSM Costs 1460.000
TOTAL 20:YEAR PRESENT WORTH COST: $3.1 10 .000
Total Coil perth 20 .Yr Nre,novat $1420
Brunawck, MD xli Page 1 012
-------
PROJECT: ImplementIng a3 mgiL Annual Avenge Total Nitrogen Limit -a
PREPARED FOR USEPA, Chesapeake oay Office
PREPAREO BY VIrginIa Tech with Steams £ Whaler, UC
DATE: March 10, 2001
FACILITY: Chestertown 1 TP
LOCATIOW Kant Cowitv. MO
RATEDELOW: 09 mgd PECOD. N/a mg/I
CURRENT EFFLUENT TN. 80 mg/I. PE TKN N/a mgd.
EFFLUENT TN GOAL: 30 nfl
NITROGEN REDUCTION 40 meM
15 I000lbs/yr
292 1000 Ibef2D.yeers
CURRENT PROCESS (CHECK ALl. THAT APPLY): MLE Existing Aeraled Volume (MG). N/a
BEPR (A2/O. VIP. etc.) Existing Anoidc Volume (MG): N/a
Sarder pho Cwrenl M1.SS at Wnte’ ADF N/a ’
Oxidation Ditoti
— lagoon (BloIao. etc.)
X Cyclical Aeration
SBR
— HLgh•Rata Biofilta
IC Effluent FIltration
Other _________________________________
CURRENT EFFLUENT AMMONIA -N: 30 mg/I X From Report
From Model (at ADF and load, 15 d MCRT 12” C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mg/I.:
[ Jet modifications required New MISS
Raise MCRTIMLSS in existing lanka (check clarifier capacity) N /a
Construct additional aerated volume flow (rngo) 0
Conatruct adthtional darillera Flow (mgd) 0
Use existing anoxt volume as aerobic (construct separate d c/st raolity)
Use aerated sy i tor BOO removal only (construct separate niUderut facility)
Add influent flow equaltatlon fank
X Other SrM lagoon operation w/llow pattern and diffuser chances
PROPOSED MODIFICATiONS TO GET NITRATE c 1.0 mgt
No modlficallena requtred
Add downatreemoeNltmerwivimethanol
Add downstream Ni$lficflon Slolhlter and DeNil filter with methanol
Add methanol bstiulg SNR aosaa
Add downetteam enoido tart with methanol feed
Add effluent fittedon -
X Other: MtnorcoemeonMdi0000Wkiooon
CAPITAL COST. Equipment and Structures (from Page 2) 550.000
El& 1 1 1 4 aid instrumentation 12% $8,000
YardPrpaigsid Site Woric. 15% *8.000
Subtotat 580.000
Contractor QIIP: 16% 39.000
EngmeerinpandConslr Mgml’ 16% $9000
Subtotal $80000
Contingency 30% 118,000
Total Capital Coal 5100.000
Capital Cost pert 20 -Yr N removal 50.34
OPERATIONS COST: Additional Ftorsepower (from Page 2). 0 HP
Elec fr PowerCost 005 liliW 50 s/yeas
NItrate Radian using Methanol. 0.0 ing/L
Methanol RequIred 0 gala/d
Methanol Cost 076 S/get $0 S/year
Separate Stage A mmonia Reduction 01 mg/I.
Caustic Sods @25% onc 0 gate /ti
.CauslicSodaCost 060$/gal $0$/yeer
Equipment Maintenance Cost $800 5/year
DaMlficabon Sludge Production wiMethanot 0 lbs/ti
Sludge Disposal Cost 400 S/ton so s/year
Total Annual O&MCost. $800 s/year
Effective Annual flare d Rate after Inflation. 1 9 1%
20.Year Present Worth of OW Costs $10000
TOTAL 20 -YEAR PRESENT WORTH COST: $110,000
Total Cost pert. 20.Yr N removal $0.38
Cheslerlown MD xis Page 1 of 2
-------
PROJECT: Impleun enl lng a3 mg i . Annual Average Total Nttgen Limit
PREPARED FOR: USEPA. Ctieeepealra Bay Office
PREPARED BY: VirgInia Tech with Steams & Whiter, Lit
DATE: Martltlt200t
FACILITY CrfofletdWWTP
LOCATION: çnsos. VA
RATED FLOW: 1 2 mgd PE COO 345 angst.
CURRENT EFFLUENT TN. mgIL PE TKN 25 nig/t.
EFFLUENT TN GOAl.: 30 mg /I
NITROGEN REDUCTION. SO lbeld
15 1000 ItisSyr
365 1000 Ibsl2O-yeara
CURRENT PROCESS (CHECK ALL THAT APPLY): : MLE Existing Aerated Volisne (MO ). 0.340
X BEPR (A210. VIP. etc.) Exiting Anoxuc Vdtn (MG). 0.157
— Bardenpito Current MISS at Winter AOF 3700 -
Oxidation Did ’
Lagoon (Blolac. ate)
CtclcaI Aeration
SBR
High-Rate BloMer
Effluent Ffltmtton
Other ‘ “‘
CURRENT EFFLUENT AMMONIAJ1 - 05 mg/ I. X From Repolt
From Model (at ADF and load. 154 MCRT. 120 C winter condiSons)
PROPOSED MODIFICATiONS TO GET AMMONIA <1.0 mg/L:
X No medications requIred New MLSS
Raise MCRTIMLSS in existing tanks (Check daRner capaccy) His
Constiuct adlsonal ,ersted volume Flow (mgd) 0
Constnact eddilonel danGers Flow (mgd) 0
Use exIsting enoxuc volume as aerobic (onnatruct separate derat facility)
Use aerated system for Bob removal only (construct separate nitldenlt tacukty)
Add Influesdltw equalIzation tars
Other _____________
PROPOSED MODILCAUONS TO GET NITRATE <1.0 mg/I:
I — required
Add downstream DeNit Sitar with melianol
Add down*eenl Ntlficstlon Odhar and DeNit tI ler with methenol
t Add n,dI..u4be,dsgBNRP IOn*
‘Add downateam sneldO tank wal l methanol feed
Add eMueMUbaOOn
Other ..
CAPITAL COST: Equipment and Stiuttirea ctoin Page 2): 51.37 0.000
Electncal and kistnamentatiorv 12% ‘5164.000
Yard Piping end Site Work: 15% 5200.000
Subtotal: 11.740.000
Con lradtorON&P 15% 5201,000
£ngeieerlng and Contr. Mgeit 15% 1261.000
Subtotal: $2,260 ,000
Contingency 30% 5522.000
Total Ceptat Cost 5Z7 1 0 X0
Capital Cost per lb 20.Yr N removal. . 17.62
OPERATIONS COST: Adffillor’aI Horsepower (from Peg, 2) 20 HP
Elq@tnc.sl Power Cost 005 5/kW 30.500 S/year
Nitrate Reduthon using Methanol 5.0 angst
Methanol Required. 20 galwd
Methanol Cost 0.75 5/Oat 55.500 S/flU
Separate Stage Arninorna aW 0.0 angSt
Caustic Soda @25% oorc 0 p
Caustic Soda Cost 0.60 5/get 505/bear
Equipment IMuntenance Cost $21600 5/year
Denrtntucatlon Sludge Production wtMthanol. io me/d
Sludge Disposal Coat 400 5/tn 55,100 5/year
Total Annual OW Cost 139.700 5/year
Effective Annual interest Rate alter Meta L 2 9lY.
20-Year Present Worth of 6aM Coat 1600.000
TOTAL 30-YEAR PRESENT WORTH COST: 13350.000
Total Cost pert. 20-Yr N removal - 15.26
Crietleti NO iris Page 1 of 2
-------
PROJECT: Implementing a 3 mgIl. Annual Avenge Total Nitrogen Limit
PREPARED FOR: USEPA. Chesapeake Bay Office
PREPARED BY: Virginia Tech with Steams £ WhSs, LLC
DATE: March 19, 2001
FACILITY: Eaton WWTP
LOCATION: Easton, MD
RATED FLOW: 2.0 mgd PE COO 220 mg I.
CURRENt EFFLUENT TN: iTThng/L PE TKN 3D mglL
EFFLUENT TN GOAL: to mg / I.
NITROGEN REDUCTION: ¶00 held
37 l000lbsJyr
130 1000 5 ./20-years
CURRENT PROCESS (CHECK AU. THAT APPLY): MLE E s Aerated Volume (MG) N /a
BEPR (A210. VIP. etc Existing Anoxic Volume (MG) N/a
— 5ardenpho Current MLSS at Winter ADP N/a
- Ox Idation Cildi
.! Lagoon (Biclac etc)
— CyclicatAecalion
SSR
— High-Hale SoliNg
— Effluent Fivatot
X Other Overland Flow of Lagoon Effluent
URRENT EFFLUENT AMMONIA-N ’ L4 mgll. X From Report
From Model (at ADF and load. IS O MCRT. 12°C winter conditiona l
PROPOSED MODIFICATIONS TO GET AMMONIA C 10 mg/I.:
Dtlo modifications lequired New I{SS
Rain MCRTSMLSS S Sstlng tanks (check clarifier capacity) “ Wa
c c addluomal aerated volume FIow(rngd)’
- Construct additional dafflers Flow 410 ” 4
Use existing anon volume as aerobic (construct separate denft fadhiM
Use aerated system MOOD removal only (construct separate ntt/derwt facility)
Add lntuenl Sow aqrslintion tank
. SionS.P •n..rr!r n/r .
PROPOSED MODIFICATIONS TO GET NITRATE tO mgIL:
No modth ns —
Add downstmam Oe M filer with methanol
X Add downstream Nitrdlcailon Sb/liter and DeNil filter with methanol
- Add methard to existing BNR procosa
Add downe*eamanoelc tank with methanol teed
Add eliluent tItration
Other . 1 -
CAPITAL COST Equipment and Structures (from Page 2) $Z600.000
Eleetnoal and Instrumentation 12% 5330,000
Yard P ip/ng and Sule Work 15% 1420.000
S it lolal 33550,000
Contractor 011 W tflt $534,000
Engrneenng and Ccnstr. Mgnft 1554 $534,000
Si slolai. $4,830,000
Contingency: 30% 51.068.000
Total Capital Cost $6.T00,000
Capital Cost per lb. 20-Yr N removal PSI
DPERATIONS COST Additional Horsepower (from Page 2): 80 HP
Electrical Power Cost 0055 1 kW 526,100 5&ear
Nitrate Reduction isng Methanol. 8. 1 mg/I.
Methanol Reqiired 80 gals/d
Methanol Cost 075 5/gal 513.700 $Fyew
Separate Stage Mwnonla Reduction 0.0 mg/I.
Caustic Soda @ 25% conc 0 ga wd
Caustic Soda CoaL 080 3/gal 50 5?yec
Equipment Maintenance Cost $48,300 5/year
Derutritcatlom Sludge Production wiMethanol 150 than
Sludge Disposal Cost 400 S/Ion 511.000 s /year
Total Aruwal 0tH Cost $97100 5/year
Effective Annuat Iniereal Rate after Inflation 2Jt%
20 Year Present Worth of OW Costs $1,450,000
TOTAL 20-YEAR PRESENT WORTH COST: 11,160.000
Total Coal per lb 20-Yr N removal 59.81
fission. MD xis Page sot 2
-------
PROJECT: ImplementIng a 3 4. Mmvi i Average TOW Nitrogen Unit
PREPARED FOR: USEPA. Chesapeake Bay O hio ,
PREPARED BY: Virginia Tech with Steams & Whaler, U C
DATE: MIrth 10 .2001
FACIUfl’ Eiitten w wTP
LOCATION Cent Corn Y MD
RATED FLOW: 27 mgd Pt COD 344 ing!L
CURRENTEFFLUENTTh: ITmgit. PENN 2$ mg!L
EFFLUENT TN GOAL 30 rnglL
NITROGEN REDUCTION: 110 held
40 l000IbeIvr
803 1000 Ibs/20.years
CURRENT PROCESS (CHECK ALt. ThAT APPLY):
CURRENT EFFLUENT AMMON1A.N: c l.0 mglL X From Raped
•. FromM000I(atADF and load. 15dMCR(. ItCwrnWonndrtKXls)
Equipment and Stnduras (from Page 2).
Electrical and msbianentaxn
Ya rd PIpIng end 5* 5 Watt
Subtotal
Contractor OHSP.
Engineering addtarsr Mgnt
Subtotal
Contingency.
Total Capital Cost
Capital Costperl, XYr. N renwa t
Additional ltorseporsr (from Page 2):
Electrical Power Cist 005 5 1kW
Nitrate Re I r i wing Methad
Methanol Res ket
Methanol Coat 015 $lgaI -
Separate Stage Ammonia Redudiow
Caustic Soda @25% wit
Caustic Soda Cast 060 $Igal
Equipment Maintenance Cost
Oenitrtfcation Sludge Production waMethanot
Sb4ge Diagonal Cost 400 Mon
Total Annual OSM Cost
Elective Annual btweet Rare altec Inlation
20.Y r Present Worth atO&M Costs
$0
12% $0
15% $0
$0
15% 50
15% So
$0
30% $0
$0
$0.00
0 HP
$0 $lyear
5.0 mg I.
flOgelsld
513.100 SI ster
0.0 nç&
0
Soa4ear
160 Ibsld
511.700 $Iyear
$25 400 $4’ear
5380.000
TOTAL 20.YEAR PRESENT WORTH COST:
Total Cost pert 20.Yr Nienioval
5380.000
$0.41
x
MLE
BEN (AVO, VIP. eic I
Bardenpho
Oxidation Ouch
Lagoon (BIOlaC aic)
Cyclical Aeration
SBR
Hlgh.Rale Biotiller
Effluent FIltration
Ouier
Ewebng Aerated volume (MG) Wa
Existing Anoinc Volume (MG) NSa
Cuntrd MLSS at Wa iler ADF. - —
PROPOSED MODIFICA11ONS TO GET AMMONIA (1.0 nigit:
No . 1 etIIflcdOns reqtAred New MLSS
$4Ralse MCRT*ILSS 1 , existing tanks (check danfiw capacity) tN/a
.floons’jifl additional aerated volurca flow ( mgd):’ 0fl ”
‘aconstnn addtonal dariflets flow ( nigd). flX
IJIJIO c hQ aioit voiwie a aerobic (COtlStnfl separate dent hadlity)
sfled system tar BOO removal ordy(wnsuuct separate ndfdentt lacllity)
J JMd telkaestflow.quahta uon tank
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 rnglL: I
r —
Add down*eam DeNd filler with methanol
Add dosatatreani Nitnllcatton Blobiter and DeNIt Alter with niethend
Add memsnolto nidating ERR process
Add dmwratreanl ancteq tank wt methanol teed
Md emueni Mtration
x ov wti more metuaree 10 elUetIno Deite risers
CAPITAL COST:
OPERATIONS COST:
Elkton MD xis
Page 1012
-------
PROJECT: ImplementIng e3 mg/LMnuet Avenge T e dS N i trogen Unit
PREPARED FOR: USEPA, Chesapeake Say 011155
PREPARED BY: Virginia Tech whit Steame & Whaler, LLC
DATE: Mar c h 9,200 1
FACIL iTY: Federalshurg WWTP
LOCATION: Caroline Coidy. MO
RATED FLOW: 0 75 mgd PE COO - 332 mg/I.
CURRENT EFFLUENT TN: s_mgi. PE T1Q( 20 rug/I.
EFFLUENT ‘TN GOAL: 30 mg/I.
NITROGEN REDUCTION: 90 ba/d
33 l000Ibe/yr
657 1000 lbs/2ojeera
CURRENT PROCESS (CHECK ALL THAT APPLY): MLE Existing Aerated Volume (MG) N/a
SEPR (A2 . VIP. etc.) Exishng Moxic Volume (MG). N/a
Cirant P/L35 at Whiter ADF N/a
Oxidation Dtth
Ijgoon(Olotac. sic)
C dS Psabon
S n
HIgh.Rate PsofiW
— EflIuentFIItiatlon
X Other Trick ling Filter wilh efiluenl Gltrotion
CURRENT EFFLUENT MIMOPJIMI: 05 mgi. 2 tsem Repast
‘ . Front Model (at ADF and load, 15 d MCRT. it C winter wndsliona)
PROPOSED MOOIF1CATIONS TO GET AMMONIA d.c mg/L:
wiraan .od&a lw ass
jjpetee MCRTMLSS in . ...s&1Q I Sa (check daitfier rapaaM N/a
.ElConatnfl.JSSa.J aerated dsne Flow (mgd). 0
EJccnstndaddl0onal dslflen Flow (mQd). 0
flue. esJe& 4 anwdcvolunie a aerobic (oanstnjd separate devil ladilty)
E]tiae aerated sytii lbr BOO removal only (conetnict separate nWdwuft tedfllty)
flAdd Irsilueti low equallzellon thrift
JOthat 4 -
PROPOSED MODIFICATIONS TO GET NITRATE ‘ C 1.0 mgfL:
[ liNe moUatiorw requtrad
‘2 Md dcrMsebaam DeNit liter with methanol
drstsawn NitrIlloalon Bbtilter end OeNit filler with methanol
M i methanol te..s g StIR pvo s
Add das..die...i enoix test wIth methanol reed
• eGueSSThGoa
Other t.i
CAPITAL COST: Equipment and Stnsotwss (from Page2V $1300E00
Electrical and Inetnrenletbt 12% 116&000
Yard Piping and Ste Woik 15% 1195.000
SubtotaL $1650000
Covet 0 1 1W: 15% $246000
EngInaesb and Coast Mgnt 15% 12*000
Stbto A 12.150.000
Cositingency 30% 5495,000
Total CapItal Coat 12.550.000
Capital Coal pert. 20.Yr. N mnvvt $4.03
OPERATIONS COST: Addikonal power (from Page * 20 HP
Electrical P r Cost 005 lAW $6,500 I/year
Nitrate aw SngLiellwnd ItO mgi.
Methanol Requ let 40 gisld
Methanol Coat 0.7$ 5/gal 111.000 Meal
Separate Siege AmmonIa Reductlost 00 mg/i.
CaustIc SodsØ 25% coic 0 gale/d
CaustIc Soda CoaL 0.60 SIgN $0 V ear
Equipment Metniepance cost 121.500 1/year
Denslrltlcalon Sludge PicdudwnwlMethenot 140 bald
Sludge 0l... —l Cost 400 $bai $10200 $4eer
Total Anmal OW Cost $49200 5/hear
Effective AmmusI Interest Rate after InflatIon 221%
20.Year Present Woith of 051.1 Cost $740,000
TOTAL 20-YEAR PRESENT WORTH COST: $3.3 10fl
Total Cod pert. 20-Yr. N mmovat $5.15
Federelaburgi Page 1 ol 2
-------
PROJECT: ImplementIng s 3 nig lL Annual Avenge Tota l Nitrogen UrnS —
PREPAREO FOR; USEPA. csnapeate Bay Office
PREPARED DY: Virginia Tech with Steams S Whaler. LW
DATE: March 19, 2001
FACILITY Geo.’yes Cree k YWVTP
LOCATION: Mleohaiw County. t iC
RATED FLOW; 0.5 mgd PE COD 195 mgIL
CURRENT EFFLUENT TN’ jjj_mg!L PETKN: fl mgit.
EFFLUENT TN GOAL tO mgIL
NITROGEN REDUCTION. 40 lbsid
15 1000 Ibslyr
292 1000 IbsI2O.yesrs
CURRENT PROCESS (CHECK AL l. THAT APPLY): X IdLE Existing Aerated Volunie (MCI) 0.4959
OEPR (A210. VIP S W ) Eiastkig Anoinc Volume (MG) 0.212A
Bardenpho Currenl ML5S at Winter M W. 2700
Oxidation Ditch
— Lagoon (Biolac. SW)
Cyclical Aeration
5CR -
: H h .Rn
— E lit isM Filtration
X Other O,ddslion Ditch niodiléd to two step-feed PLC Units
CURRENT EFFLUENT AMMONIA-N: 05 mgIL X From R oit
From Model (stAG ? sniSload. 15 d MCRT. 12°C Writer corldLtions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1. 0 mgIL _____
!‘ No n iod ons reqSred New MLSS
*j RSe MCRTIMLSS hi eidslitlg tanks (diedc ctarWe capacity)
Con*tfl sddI&4 aerated dtane Flow (mgi) o”i .
..9 Con*id Wtzitalda$flers Flow (mgi) Ot
- . Use eSsing enoidcvoline as aerobIc (construct separate dent ladhity)
— Use aerated system for SOD removal only (construct separate nitAlend facility)
L. Addlnfiuenttlowequalflhlontank
‘Other ____________________________
PROPOSED MODIFICATIONS TO GET NITRATE <1.0 mglL
No ,noddlcathoflt required
X downstream DeNil Alter with methanol
Add downstream Nutnicslion BluRter end OeNit lifter with methanol
Add medr iaS to eiusing BNR process
Add downstream enoioc tank with methanol feed
Add efltuent Nation
Other _____________________________________________________________
CAPITAL COST: Equipment and Structures from Page 2) 51.300.000
Electrical and lnsvumentadon 12% 1150.000
- YardPipngsndSlteWort 15% 1195.000
Subtetat 51.650.000
Contractor 0 1 1W. 15% 1240.000
EngIneering and Constr. Mgmt 15% 3240.000
Subtotal. 52,150,000
Contingency: 30% 5495,000
Total Capital Cost 12.9 50. 0 0 0
CapItal Cost perle 20-Yr. N removat $9.96
OPERATIONS COST Additional Horsepower (from Page 2P 1 0 HP
Elechicel Power Cost. 005 54kw $3,300 9 /year
NlIrate Redisitonusing Methanol
Melanol Requlre& 30 gets/ i
Methanol Cost: 075 5/gal 50.500 Skew
Separate Stage Ariwnonla Reduction 0.0 inglL
CausticSods @25%conc 0 gsls/d
Cerstie Soda Cost 060 5/ al . 50 9/year
Equipment Maintenance Cost. 521,500 5/year
Denitr t ilcation Sludge Production wIMeIhenQl S Q l sJ d
Sludge Disposal Cost 400 5/ton $&700 5/year
Total Annual 090.1 Coal 531 000 9/ye a r
Efleauve AnngØl interes l Rile alter k ul lalion 291%
20-Year Present Worth of OW Costs 5510 .000
TOTAL 20 -YEAR PRESENT WORTH COST: 53.1 10,000
Total Cost per lb 20-Yr. N removal 5 10J2
Georges Creek. MD its Page 1 01 2
-------
PROJECT: - Splementlng a3 unejk Annual Avenge Total Iffirogan Ufl p
PREPARED FOR. USEPA, Cheaapeaka Say 0 ( 1 1c c
PREPARED BY: VIrgInia Tech with Steams £ hSer, LLC
DATE: Maidi 19,2001
rAC IuTy: Dttent
LOCATiON: ueabam. VA
RATED FLOW O s nio FE COD. 487 mg/I.
CURRENT EPFLUENT TN. iiF’mglL PE TKN’ os mg/I
EFFLUENT TN GOAL: 3Onig/L
NITROGEN REDUCTION 190 lbs/it
69 t000lbs/yr
1387 1000 lbs/20.years
CURRENT PROCESS (CHECK ALL THAT APPLY):: MLE Existing Aerated Volume (MG) 0.76
— BEPR (A2/0, VIP. et) Existing Anoxic Volume (MG). - N/a
I 6arder ho Current MISS at WlnterAOF 7140
Oxidation Ouch
: geen (BSac, ‘sic)
I CØicai Aeration
SBR
hugh-Rate Biolllter
— E h fluent Filtration
Other _____________
CURRENT EFFLUENT AMMONIA-N: c1.0 mg/I. X From Report
From Model (atADF and load, 15 if MCRT, 1211 C winter conditions)
PROPOSED MODIPICA nOPIS TO GET AMMONIA C 1.0 mg/L
No mcdII bis requIred New MLSS
RS MCRTALSS hi eidath’ug tanks (chadidanfier capacity) •, - t ile
.‘ Connuct I S I S ants wtme Flow (myd) Z’th
‘“- Constiud addl nS darlters Flow (mgi ‘ tO ’
Use eidsdng anatdc vatutne as aerobc (eanstiud separate dent factuty)
Use aerated s tn for SOD removal a/Wy (constauct separate n itMenit facil ity)
mtuetdtlowecpiaflzation tank
Other- -
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mg/U
- No modtflcatlcns —
• Add downstream DeNit Met with methanol
Add downstream N ltt ltcation Siohlfter and DeNut filter with methanol
Add methanol ho existing BNR proass
downstream anoidc tank with methanol feed -
effluent 5&a
OUr ____________
CAPITAL COST: Equipment and Structures (from Page 2)’ $250000
Electrical and Instrumentation 12% 5*000
Yard Puging end Site woilr 15% *35,000
SutMal : 5320 000
Contractor CHAP. 16% $46,000
EngineerIng a i d Constr Mgnil 16% $48,000
$420000
CuuM cnq 30% SS6.0Q0
Total Capital Cost $520,000
Capital Cost per ID. 20-Yr N removat. $0.37
OPERATIONS COST: Additional h-lorseporeer flrom Page 2). 0 lIP -
ElectrIcal Power Cost. 0.05 5 1kW *0 $ ieav
Nitrate ReductIon using Methanol 46.0 mg/I.
Methanol Required. . $0 gats/d
Methanol Cost 075 Sfgal 524.600 S/year
Separate Stage Ammonia Redudlert 0,0 mg/I
Causec Soda 025% conc. 0 gats/d
Cetabc Soda Cost 060 $&sl $0 5/year
Equipment Maintenance Coat 54200 5/year
Denutrthcation Sludge Production wi’Methanor 250 teat
Sbxfge Disposal Cost 400 S/Ion 520400$/year
Total Annual O W Cost 549200 $I ew
Effective Annual Interest Rate alter Inflation 291%
20-Yew Present Worth of CAM Coals’ $7401600
TOTAL 20-YEAR PRESENt WCRTHCOST: 51 260 , 000
Total Cost per lb 20-Yr N removal $ 0_ Il
OuPont Waynesboro xis Page 1 of 2
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PROJECT: Iniplemenl lng a 3 m. M ACSI Ave rage Total Nitogail Unit
PREPARED FOR: USEPA. Chesapeske Bay ORb.
PREPARED BY: Virginia Tech with Steams & Whaler, LLC -
DArE: March 10,2001
FACILITY: Dale ServIces 10 WWTP
LOCATION; Dale CItv VA
RATED FLOW: jjngd PE COD Nla mg /I.
CURRENT EFFLUENT TN: j.mgIL PE TKN N /a mg/t.
EFFLUENT TN GOAL: 30 rug/I.
NITROGEN REDUCTION: 60 lbs/d
29 1000 l bs/yr
564 1000 l sl20-yeara
CURRENT PROCESS (CHECK AU. THAT APPLY); Ethshng Aerated Volume (MG) N/a
— SEPR (Atm. V iP. etc.) Exisluig Moiac Volume (MG). N/a
— BarderO Current PALES 51 WInterADF. 5300
Osldat mn Dti
n(Blcte ;etcl
CydIcSAerflOn
-SBR
High-Rate BloOftsr
— EBuerd Fwration
Cthsc oH aofuelnad to boreese nSflcatton rate
CURRENT EFFLUENT AMMONIA-N: ‘ 1.0 IUgIL X From Report
From Model (at ADF and toad, 15 d MCRT. 1? C wsiler conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 1.0 mglt:
I ineditlawne required NavM I .SS
Raise MCRT/MLSS In existing tanks (check clarifier capacity) We
Cons Inst additional aerated volume Flow (mgd) 0
Constn#addltIOnsIdaItlIel5- Fbv(mgd) 0
Use e iaslung snout volume as eembc (coostrud separate OeM tacfluty)
Use aerated system brOOD removal odly (construct sdparate ndldend facility)
Add Intivent lime equatixabort tank
Other _______________
PROPOSED MODIFICATiONS TO GET NITRATE <
UJNO modil lcalioris required
o isveam DeNit litter with methanol
dgensflam litMosbon Blolbltsr end DeNit Filter with methanol
melkaS to . dfl StIR process
M donflstIeallI 5006k tank with methanol teed
‘etantliration___
Other - .%%s,USq.flJr. r” 7 !
CAPITAL COST. Equpuent and Structires (from Page 2)- $520,000
Electrical and ninaerltation: - 12% $02,000
YardPipingandSlteWdrlc 15% - 176.000
Subtotal $050000
Contractor ON&P. 10% 196,000
Enflisering and Ccitt. Mgmt 15% S*
Subtotal . $560000
Contingency 30% 1195.000
Told Capital Cost. 11060,000
Capital Cost per lb 20-Yr N removaL $182
OPERATIONS COST: Additional ljoaepower (from Page 2) 0 HP
Electrical P’ower Cost 005 VkW 50 S/peer
Nblrsle Redintion ucing Msthanol - 30 mg/b.
Methanol Required 30 gatsld
Methanol Coal 0.75 1/951 15200 5/pear
Separate Stage Ammonia Reductioft 0.0 mg/i.
Caustic Soda 025% xnC 0 gsls/d
CausticSodaCos l. 060 S/gal 50$/peer
Equipment Malntensnct Cost 55.500 S/yew
Denitnfieatlon Sludge Production w/MelhsnOl 110 teAl
Sludge Disposal Coal. 400 1/ton 88.000 1/year
Total Annual 0511 Cosr 124.800 S/yeN
Effective Annual l etorsst Rate after irdletioft 291%
20-Year Present Worth of O OM Coats; 8370.000
TOTAL 20-YEAR PRESENT WORTH COST: 11.430.000
Total Cost pert. 20-Yr N removal $2.45
OaIe Services #8 cls Page 1 ol 2
-------
PROJECT ImplementIng •J mg& Annual Avenge Total Nitrogen UntIl — .
PREPARED FOR: USEPA. Chesapeake Bay Office
PREPARED BY: VirgInIa Tech with Steams & Whaler. U-C
DATE March 18, 2001
FACILITY: Dale SdMcn #1 WWTP -
LOCAT iON: Da le City , ‘ 1 k
RATED FLOW: 3. Omgd PE COft M rnglL
CURRENT EFFLUENT TN: t0rng/L Pt TKN i _ inglt
EFFLUENT TN GOAL: 30 rng/L
NITROGEN REDUCTiON 80 Ibsld
29 1000 lbs/yr
504 1000 lbs/20j’eais
CURRENT PROCESS (CHECK ALL THAT APPLY): A I tt Es l e vng Aerate Volume (MG) Nla
— BEPE $240. VIP,’etj ExIstIng Anoxic Voliawe (MG) NFa -
Bsrdenpho Curent MLSS ai Winter MF 5300
— Oxidation DItch
— Lagoon (Blolac. etc.)
— Cyctical Aeration
SBR
— High-Rate S ha tNer
— Efilu e n IFlI f ratlon
X Other pit adjus i to increase nit rate
CURRENT EFFLUENT AMMONIA-N. CI A) mg /I X From RepO lt
FtomModel(3IADF and load, 15dMCRt 12’Cwinterconditlons)
PROPOSED MODIFICATIONS TO GET AMMOMAC 1.0 mgiL:
kiNo . .,oddtaUons requked New MISS
• RaIaeMCRTIALSS In SatIng tanks (chSc daitfier capaaty) . T’k!e
• eddibonal aetated volume Flow (rngi c .i4 e ti
‘Conslnn addtllonal daililan r (mgd): - . .a. -. -
Use eidetlnQ atteSt volume as aerd& (constu c t separate daM bal’ty)
- - Use aerated jyatem for BOO removal ontg fconstnsct separate SVdenIl facility)
- ‘Add Influent flow eficallzaton tank
- z: ; ’ j ‘v-c. r: .’ ’ ‘•‘-.t.. .‘ ‘
PROPOSED MODIFICATIONS TO GET NITRATE 41.0 mgL
- No medifloatlena requfrad’
t doenaeaam UeNft lifter with methanol
Add domietsani Nltdllcation Owliftar end DaN1 filter with methanol
• Add methanol at exIsting BNR process
Add downefresm ancinc tank with methanol lead
Add e l i lue S oft
Quiet Me dean bed fifteti to denlte lifters
CAPITAL COST. Equipment and Ividurea (from Page 2) 1520.000
Electrical and lgweuJinenthIioit 12% 562.000
Yard Piping and Ste Wodi: 15% 178.000
Subtotal $060000
Conlrador CH aP. 15% 109.000
EnglnaanrgandConalr MgM 15% 189.000
Sublolat 5000.000
Contingency: 30% 5198,000
Total Capital Cat $1,000,090
- Capital Cost pert 20-Yr. N removal $1.82
OPERATIONS COST: AddItional Heneposer (from Page 2)! 0 HP
EleeSed Pewe 0.06 1 1kW 0 1 /year
Nate Redixitlon uskig Mdthanot • • $0 ItI QA
Methanol Reqitat 3OgaIsid
Methanol Coat 075 Slgal 18.200 1/year
Separate Stage Aeanonla Reduction. 00 rng/L
CauabcSoda 25% o onc Ogalald
CaustIc Soda Cost 080 1 al SO 1 /year
Equipment Maw itenance tost 50.600 8 / year
Danltrllication Sludge Prodicuon wft4ethanol 110 Ibs/d
Sludge Disposal Oat 400 1/ton $8,000 S/yer
T o tal Annual O&M Cost 124.800 5/year
Etlecave Annual Sweat Rate after Inflation 291%
20-Year PresentWettI ctO&MCda4t $370,000
TOTAL 20-YEAR PRESENT WORTH COST: $1,430,000
Total Coil per le 20-Yr N removal 12.45
Dale Services ci xis Page 1 of 2
-------
‘ROJECT: lrnplemmdli%0a3 I,IQLAAI%UUI A n n , ’ Total Nitrogen Link
‘REPARED FOR. USEPA, Chesapeake Bay Office
‘REPARED BY: Virgin Ia Tech will’ Sterna & Wheler , I-tO
DATE: Marc h 19, 2001
FftCIL 1TY: Qahioren WWTP
LOCATION DaNoren. VA
RATED FLOW: 0.3 ingd PE coo N/a mg / I .
CURRENT EFFLUENT TN: jQ_,rng/L PE TICN _ J!a mwL
EFFLUENT TN GOAL. 30 mg/t.
NITROGEN REDUCTION ID lbs/it
4 1000 lbs/yr
73 1000 Ibs/20 yelf5
CURRENT PROCESS (CHECK ALL THAT APPLY): ULE Existing Aerated Volume (MG) N /a
BEPR (A2!0. VIP. eicj Existing Anoxuc Volume (MG) N /a
Bwdenphe Current MISS at Winter ADF 2100
OxidatIon 0 1 1th
Lagoon ( ala/ac. etc.)
Cydical Anton
SER
Hlgh-RateBditer
Sltluent Filtration
Oth€ - is. caantnc rti
CURRENT EFFLUENT AMMoNIA-N: ‘ 1.0 ing/L. K From Report
From Modal(at AD! and tad. 15 d MCRT. 12°C vnnterooJldihOns)
PROPOSED MODIFICATIONS TO GET AMMONIA’ mg/L:
No moddtcatens required New MISS
Raise MCRTIMLSS in existing (ants (flck cleriller capacity) N/s
toristruct adaltianal aerated volume Flow (mgd) 0
Construct eStibonal dar llters Flow (mgd) fl
Use existing anoiac volume as aerobic (construct separate d m11 ladIdy)
Use aerated system lar BOD removal o4’ (construct separate rut/dent facility)
Md Irilluent (Ow equalization tank
Other
PROPOSED MODIFICATIONS TO GET NITRATE’ 1.0 mg/k:
No modifications required
downstream DeNit lIter with methanol
downattam NSfltceIiatI 8 1 0 1 1 W sod DeNlI litter with methanol
methanol to SatIng BNR procass
dowiwnem nSc nk with methanol teed
Md effluard lIbatIon __
r ’ rin flr. 4 r . -
CAPITAL COST: Equipment and Stnielires ((reni Page 2): *250.000
Eledneal — lnstiums,ilatIoW 12% 930.000
Yard Piping and Ste Wet 15% $31000
Subtotal. . 3320.000
Contractor OH&P 15% $48000
Engineering and Censtr Mgint 15% 08000
Subtotat *420.000
ContingencY 30% 390.000
Total Capital Cost 1520,000
Capital Cost per lb 20-Yr N removal. 31.12
OPERATIONS COSTS AddIIlcnal hlorsepove t im . ” Pegs 21 0 HP
Eteancal P nr Cost D.Q5 5 1kW 50 5/year
Nitrate Reduction using Methanol S Omg /L
Meffiarial RequIred 0 pla/d
Methanol Cost 0 75 5/gal 50 5/yeer
Separate Stage Animona Reduction 0.0 mg/t
Caustic Soda § 25%conC 0 galald
Caustic Soda Cost 060 S/gal $0 $4 ea
Equipment Maintenance Cost *4.200 S /year
Denikifloatian Sludge Production w&teflflot. 10 lbs/it
Sludge Disposa l Cost 400 S/ton $100 S/year
Total Annual 041.1 Cost $4,900 5/year
Effective Anal Interest Rate after Inflation 2.91%
20-Year Present Worth c i 06W Costa. $70000
TOTAL 20-YEAR PRESENT WORTH COST: $510000
Total Coat per lb 20-Yr N rental $6.08
Dehlgren VASIS Page
-------
PROJECT implementing a 3 mg/L Annual Anrage Total Nl uogen Limit — .
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY Virginia Tech with Steams & Wheler, LLC
DATE: March 19 . 2001
FACILITY ColonIal SUCh WWTP
LOCATION Colonial Beach. VA
RATED FLOW 20mgt PE COO N/a z ag / i .
CURRENT EFFLUENT TN fl_mg/ I PE TICK - N/a mg/I.
EFFLUENT TN GOAL: 30 mg/I
NITROGEN REDLjCT1ON: 70 ibsfl
20 t000ibs/yr
511 1000 ibs/20-yeazi
CURRENT PROCESS (CHECK ALL THAT APPLY): MLE Existing Aerated Volume (MG) N /a -
— BEPR (1 2I0. ViP. etc.) Existing Moxie VokaTle (MG) N /a
— Bardenpli& Current M ISS at Wnier AQP N/a
— Oaddahon Ditch
- Lagoon(Blola&etcj
A CyclicelMvstioa
SM
— High-Rate Rhidifter
— Effluent FiltratIon
O tter ____________________________
CURRENT EFFLUENT AMMONIA-U: 05 mg/I. X From Report
From Model (at ADF and load. 15 d MCRT. 12’ C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA <1.0 mg/I:
[ ]No modifications required New MISS
Raise MCRTL’MLSS In existing lanka (check clarifier caperity) N/a
Construct additional aerated volume Flow (mgd) 0
Ccnstnict additional dariflers Flow (mgd) 0
Use existing anosuc votiine as aerobic (construct separate denit racihty)
- Use aerated system lur BOO removal only (construct separate nit/dead faolify)
Add lifluent Sow equalization tank
Other ____________
PROPOSED MODIFICATIONS TO GET NITRATE c i a mglL
The modifications —
Add downsbeem De l hI lifter with methanol
‘ downstream NiV on 6 101 1 1W and DeNit lifter wit h methanol
r- Add meihanolto . 4SflO BNR pit 5$
. Add d nsflam enoidcisS S matsnof teed
- £
CAPITAL COST- Equipment and Slrudures (tram Page 2) 51.650.000
Electrical and kiafnanenlabon. 12% 3190.000
- ‘fad Piping and Site Work 15% 3248.000
Stttotal 32100.000
Contractor OH&P 15% 3315000
Engineenng and Constr Mgmt t5% 3315.000
Subfotai $2130000
Conlirigency 30% 5530 000
Total Capital Coal $3360000
Capital Cost per lb 20-Yr N removal. $1.58
OPERATIONS COST Additional Noreaponor (from Page 2). 40 PIP
Electrical Power Cost 005 $ikW $ 13.1 00 3/year
NItrate Reductionusing Methanol 4 O fTIg/L
Methanol RequIred 30 gaia/d
Methanol Cost 075 $ af 30.200 1/pear
Separate Slage Ammonia Reduction 0.0 mg/I
Caustic Soda 25% co lic. 0 gaWd
Caustic Soda Coat. 0.60 5/gal 30 S/pear
Equipment Maintenance Cost $21,300 8/peer
Denltrffication Sludge Production SMethanoP 100 ibe/d
Sludge Disposal Coal 400 IRon $7300 S/pea-
Total Annual 0811 Cost $55900 3/yew
Effective Anmiel Merest Rate alter Inflation. 2.91%
20-Yw Present Worth uf 0811 Costa $8401000
TOTAL 20-YEAR PRESENT WORTh COST: $4,200,000
TotaiCostperib 20-Yr N removal $3.22
Colonial Beach VA ls Page tof 2
-------
PROJECT. ImplementIng .3 mgit. Annual Avenge Total Nitrogen Limit
PREPARED FOR. USEPA. Cheespeelte Bay OffIce
PREPARED BY. VIrginia Tech with Stearns & Whaler, LLC
DATE: March 16, 2001
FACILITY: Arl ington WWTP
LOCATION: Nlngtn. VA
RATED FLOW: 30.0 nigd PE COD — 300 mgIL
CURRENT EFFLUENT TN: IOniglt. PE 104 — 27 ITIQ/L
EFFLUENTTNGOAL 30 regIt.
NITROGEN REDUCTiON: 1250 lbsld
456 l000Ibslyr
9125 1000 IbsI2O-yeara - -
MLE __________
BEPR (fib, VIP. elc)
BaSon
Oxldflon INth
Lagoon (Blolac, etc.)
CyvJIcaI Aeration
SBR
High-Rate BioMer
(fluent FUpatlori
Othec Step-Feed MLE, no nitrate iec de. Deep Bed Fillers
CURRENT EFFLUENT AMMONIA-N: ‘ do rngi’L X From ROpM
From Model (at ADF and load, 15 d MCRT ¶2 °C winier conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C 10 ntglL:
pfe pio iflcj j oj remaed Now MLSS
Raise MCRTIMLSS in existing tanks (thetA dafl ter pfl ) ______
Consind stiditlgnal aerated clume p y ( ngd) . -
Conatuct additional danliera Flow (mgd) ‘ _
Use existing anoino volu me as aerobic (conshud separate d m11 jollity)
- Use sealed system for BOO removal only (coast-trot separate nltldenil facility)
- Add li* srd low egueliatiOn Ionic
Other t ’ ’ 1 SV 1 ’ 4” ‘ -
PROPOSED MODIFICATIONS TO GET NITRATE’1.0 mgt
Q]No rF ,., -’ia required
i’ AS doetsteaniOeflk 611ev with i iethanoI
AS dontium Nitifloston Biofdtet and DeNil filter wtth methanol
X AS methanol ba Q BNR process
AS dossiatissin eriordoteot aS methanol feed
X Other itaWdJi’ 8IffiueniEIlera fo denlSSerI .
CAPITAL COST:
Equipment end Stnflurea (from Page 2)’
62,950,000
Electlcal end lrabujmentailon: 12%
$354000
Yard Piping and Stie Wodr 15%
$443,000
Subtotal.
53.750000
Cowers OHIP. 15%
$563,000
Engneenng end Consir. Mgmt’ 15%
Subtotal
Contingency 30%
Total Capital Coat -
Capital Cost per lb 20-Yr N removal
$563,000
14.080.000
51.125.000
$5,010,000
$0.66
OPERATIONS COST:
Ad ltJgnaI Horsepower (from Page 2).
Elena) Power Cost 0.03 5 1kW
Minis Redudion using Methanot
MeSsed Required -
Ma nna) Cost 0.75 lIgal
Seporate Stage Ammonia RedIIdIOtt
Causac Soda (0 25% cant
Caustic Soda Coet 060 $IgaI
Equipment MaIntenance Cost
Oend*afion Sludge Produdion wiMeIhanoL
Sludge Disposal Cost 400 $ftn
Total Annual 0651 CoaL
Eltedive Annual Interest Rate after tii tion
20-Yea, Present Woilh of OSM Coete
0 HP
50 $IYear
SO .mgi.
510 gala/d
5156.000 $4 ear
0.0 mglI,
0 gelsM
$0 ltpear
$46600 Slyest
1800 thud
$131 .400 Slyest
$336200 Slyest
29 1%
$5,040,000
TOTAL 20-YEAR PRESENT WORTH COST: 511.05 1.000
TotalCoetperib 20-Ye Nremovat $1.21
CURRENT PROCESS (CHECK ALL ThAT APPLY):
x
EidsSg Aefaled Volume (MG). - i. 6 (
Existing A.noxic Volume (MG). 0.76
Current MLSS at Winter ADF: . 3000 _
Arlington VA xis
Pag e I 012
-------
SUMMARY COST SHEETS FOR THE
26 VIRGINIA WWTPS
I0
-------
rrwat ii.
PREPARED FOR:
PREPARED BY:
DATE:
FACIUTY:
LOCA 1 1ON:
RATED FLOW,
CURRENT EFFLUENT TN:
EFFLUENT TN GOAL:
NITROGEN REDUC11ON
Equipment and Struclures (from Page 2 1.
ElectrICal and tnstrurnanlatlon.
Yard Piping and Site Wo&
Subtotal:
Contractor OH&P’
Engmeedng and Constr. Mgmt.
S stotal.
Conbngenw
Total Capilal Cost
Capital Cost per lb 20-Yr N removal’
Additional Horsepower (Iron Page 2)
Electrical Power Cost 005 54 kW
Nrtrate ReducUon using Methanol.
Methanol Required
Methanol Cost 075 SSgal
Separate stage Ammonia Reduction
Caustic Soda @ 25% conc
Caustic Soda Coil 0 5 1*
Equipment Maintenance Cost
Deniirthcalion Sludge Production w lMettianol
Sludge pisposal Cost 400 Mon
Total Annual OW Cost
EIfeci’ve Annual Interest Rate altar Inflation
20-Year Present wortn of 0614 Costa
PECOD 100 mgIt.
PE TKN. ___22.__molL
$0
12% $0
15% $0
$0
16% $0
15% -$0
$0
30% $0
$0
$000
o HP
$0 $4,ear
td ingR.
— teD gals’d
$41,100 54,ear
00 mglt.
0 gale(d
S OS —
$0 fl4eer
4fl0 tbs/d
536.000 $4ear
$76,100 $lyear
291%
$1 ,140,000
$1,140,000
$0.47
tntplemendng a 3 nq - Annual Avenge Total Nlngen un It
USEPA, Chesapeake say Office
VirginIa Tech wIth Stearns & Whaler, LLC
March11, 2001
EnifixU WiMP
- NY
flmgd
eornglL
30 mgIt.
330 bud
120 t00 0 Ibslyr
2409 1000 lbsl2O-yeara
CURRENT PROCESS (CHECK ALL THAT APPLY): — MLE Existng Aerated Volume (MO) 1.82
— BEPR (AVO. tAP. etc.) ExIsting Anoxic Volume (MG)- 0.78
— Bardenpho Current MLSS at WiriierADF.. 2700
Oxidation Dttth
Lagoon (Biolac. etc)
— Cyclical Aeratio n
SBR
High-Rate Bloltltervnth Sclida Contact Activated Sludge
Eitluent Filiratoit -
X Other DeititeFiters’ ,
CURRENT EFFLUENT AMMONiA-N: cl i rng/L U’Fron% Report
L jFromModel(atAoFandload. I5dMCRT, 12°Cwinteroondilions)
PROPOSED MODIFICATIONS TO GET AMMONIA
-------
PROJECT: ImplementIng a3 mg ’ S - Annual Average Total Nitrogen Limit —
PREPARED FOR: USEPA. Cheaapeafte Say Office
PREPARED SY: Virginia tacit with Stearns & Wheler, tiC
DATE: . Msrch l l,2001
FACILITY: B Ing hamton-Johnson CItflWVTP
LOCAt iON: Binghamton. NV
RATED FLOW: 25.0 i gd PC COD 240 mg/L
CURRENT EFFLUENT TM: ir’riIg!L PE TKN- 10 mglL
EFFLUENT TN GOAL: 30 rngft.
NITROGEN REDUCTION: 1040 lbs/d
380 1Q00 lbs/yr
7592 1000 lbs/fl years
CURRENT PROCESS (CHECK ALL ThAT APPLY I: X MLC Existing Aerated Volume (MG) _ 1 62
BEPR (AZ /U. VIP etc) Existing Anoxic Volume (MG) 076
Rerdenpho Current MiSS at Winier ADF 2700
Oxrdalion Oitch
Lagoon(B’olac, ott)
Cydical Aeration
SBR
High-Rate Biofilter
— EINIIaIt Filiratlon
X Other Nit-Dealt BAF5 for 125 mod
CURRENT EFFLUENT AMMONIA-N. 05 mg/I X From Report
From Modal (atADF and load. l Id MCRT. 12’ C winter condItIons)
PROPOSED MODIFICAtiONS TO dET AMMONIA c 10 rngILr
IC Mo t5rSLi required New MISS
Raise MCRTDtSS hi eidadng tanks (check ctanller capacity) - N /a
CenSid . &a ,,& aratedSwne Flow (m):____
Corist’at StUUo ” S ifiers Flow (rngd) . .. 0 ‘
Use eioslsig aneruc volume as aerobic (construct separate dealt facility)
Use aerated system lbr POD removal only (construct separaie nilldenit tacitity)
Add Influent flow equalization tank
Other. ____________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 mg&:
No modirucatioris required
X Adddownsfream DePth Alter vS methanol
Add downatearn NIt lItIcation IsoMer and GeN e filler with rrwlhawi
Add medianS to existing ENR ri ms
Add doensteam anoidc tank with methanol feed
dd etlluent l Ibation
Other ________________________________________
CAPITAL COST: Equipment and Structures (from Page 2) 1 1 700.000
Electrical and tnatnsineiilation 12% 11.104.000
Yard Pijig and Site Work: 15% 11.455.000
Subtotal . 112.320.000
Contractor Ol-i&P 15% $1541000
Engineering and Constr Mgni 15% 11.141000
Subtotal 816020.000
Cn_ndngency 30% 83.Ige.000
Total Capital Cost $19,720,100
Capital Cost perth 20-Yr N removal: $210
OPERATIONS COST: Addulional Horsepower (from Page?) 500 HP
E leeb icalPowerC eat 005 5 1kW 1163.400 5/year
Nitrate ReductIon using Metianot 50 mg/I
rathanot RequIred. 470 gatasid
Methanol Cost 0.75 1/gal 1128 7(10 1/year
Separate Stage Ammorva Reduction 00 mg/I.
Caustic Soda C 23% conc 0 gassEd
Caustic Soda Cost 060 S/gal 50 1/year
Equipment Maintenance Cost 1160.200 S/year
Denilrtficatiofl Sludge Produclon w!Methanot 1500 Ibs ld
Sludge Osposal Coil 400 5/ton 1109.500 $‘year
Total Annual 0dM Cost 5581.800 1/year
Effective Annual Interest Rate alter Inflation 2 . 11%
20-Year Present Worth of O W Costa 18.430.000
TOTAL 20-YEAR PRESENT WORTH COST: $2 0 ,150,e0
Total Cost per lb 20-Yr N removal $3. it
BinghamptOn NY xis Page 1 012
-------
SUMMARY COST SHEETS FOR THE
2 NEW YORK WWTPS
9
-------
PROJECT: lptemsnthig.3 malLAnnual Awing. Total N1Dt 11 ,. . LImit
PREPARED FOR: USEPA. Chesapeake Bay Office
PREPARED BY: Virginia Tack with Steams & Whaler, LLC
DATE: Match 11, 2001
FACILITY: Winebrenner WWTP
LOCATION: Wash.. . *., County. MD
RATED FLOW: 0.6 mgd PE COD ’ 355 m 1I.
CURRENT EFFLUENT TN ijrrng/L PE TXN 22 ingii
EFFLUENT TN GOAL. 3 OnI9 IL
NITROGEN REDUCTION 70 lbWd
20 1000 lbslyr
- 511 I000lbe/20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): MLE Existing Aerated Volume (MG) Nla —
BEPR (A VIP. et) Existing Anoxic Volume (MG) PUs
Ganteng lie Current MISS at Winter ADF His
Oxidation Ditch
— Lagoon (Blolac. etc)
- 4tlcalMratlon
- 558
High-Rste BlaMer
Efihieffi Fflteban - - -
‘X Other RBC5 tooned S Denim Filters
CURRENT EFFLUENT AMMONIA-N: 0.6 mglL X From Repoil
(at F and load, 15 dMCRT 12°C winter conditions)
PROPOSED MOD 1FICATIONS TO GET AMMONIA C 1.0 mglL:
X tie Inodsak... qulred New MLSS
Raise MCRTAMLSS In Siting larks (cbeck clarifier capacity; Nje
anstn na d dSw i S aerated volume Flow (mgd) 0
Conatnactadntmnatc larl ilcrs F (nigd) 0
Use eiushtç anedc volume as aerobic (construct separate denit facility)
Use aerated system fec BOO removal only (construct separate nitldentt facility)
Add Inlluent llow equalization lank
Other ___________________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE C 1 0 mglL:
ONo modifbatlons requIred
Add downstream DeNit lllterwulh methanol
• Add downstream NifrIlictelon Blolliter and DeNil liter with methanol
• c Add methanol to ng BNR process
1 Add damjneam enoidc lank wIth methanol feed
• • AS eiiflmaa
X Other adJ0àS mot W t oam I ntte Filler ••
CAPITAL COST: Equipment and Stuctures (born Page 2): 10
Electncal and tes tnunentatlon. 12% 10
- Yard Plpmg and Site Woitc 15% $0
Subtotal $0
• Contractor OH&P 15% 50
Engineemig and Censir Mgml 15% $0
Sublotit $0
Contingency 30% $0
Total Capital Cost $0
Capital Cost per lb. 20-Yr. N removal $0.00
OPERATIONS COST Additional Horsepower ((coin Page 2) 0 HP
Electncal Potiwir Cost 005 5 1kW $0 $4ear
Mtrate Redut*on uskig Methanol 13.5 mglL
Methanol Reqtared 30 gsleld
Methanol Cost 075 legal 56.200 Wear
Separate StageAmmonla Reduction 0.0 mgIL
Caustic Seda 25% oonc 0 Qalsld
Caustic Soda Cost 000 SegS $0 $ war
EquIpment MaIntenance Cost . $0 $Iyear
Denltrthcatcn Sludge Production 100 bald
Sludge DIsposal Cost 400 ISa 17.300 $ rev
Total Annual 0671 Cost 115,500 Slyer
EffectiveAnnud Werast ((ale slIer kullationc 201%
20-Year Present Worth of OW Costs $230,600
TOTAL 20-YEAR PRESENT WORTH COST:
Total Cost pert. 20-Yr. N removal. $045
Wmebrenner MD xis Page 1 ol 2
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PROJECT: Iinplernentkig c i ingfl Annual Average Total NIIIOQIn Limit
PREPARED FOR: USEPA, Clteeape.ke Bay Office
PREPARED BY Virginia Tech with Stearns &Wheiet, US
DATE: Mardi 10.2001
FACiLITY: Western Btartcb TP
LOCATION: Weelikiaten Sububan Sander ? Commission MD
RATED FLOW: i6.6 PE COO ’ NIa mg!L
CURRENT EFFLUENT N: frmgit. PE TKN Pita sngfL
EFFLUENT TN GOAL: TThng i L
MITROGEN REDUCTION: 600 lbeld
252 1000 lbalyr
0037 1000 lbsI2O-yeara
URRENT PROCESS (CHECK AU. THAT APPLY): X MLE Exislrng Aaraled Volume (MG) Us
— OEM ( nIL ViP. etc.) ExisUngAnooric Volume (MG) Mt .
— Bardeiwho Current MLSS at Winter ADF. 2000
— OxIdation Ditch
— Lagoon (Biolac. dc)
Cyclical Aeration
SEP
: High-Rate Bother
X Effluent Fdlration
i Other Demt. Filters
CURRENT EFFLUENT AMMONIA-N: c l.0 _ “g IL X Fr Report
From Model (. IADF and load. 15 d MCRT 120 C winier wndrt.one)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mgIL:
R No mo jtaoonsrequred New MISS
Raft. MCRTIMLSS te existIng tanks (check clantlercapedly) M1e
Conatud additional aerated volume Flow (rnpd): -
Conairud additional claiMers Flow (ingd)._______
Use e’detng enoico volume a erobc (cansinid separate drlt tedlhly}
Use sead system for BOO removal only (onnatrud separate n4 enht lacibly)
Add kifluent itowequaliSon tenS
. t ‘i’ : ‘ . - 4 e’ Firr iJ-.
PROPOSED MODIFICATIONS TO GET NITRATE <10 ing lL:
: No modifications requied
Add d0*’Ilafl&fl DeNIt liter wIll IllatheM
dovelabealli Nitnflcáon Blotiltar end DeNit titter with methanol
Add methanol tuSslIng BNR Focea
Add demiabeem anoioc tank wIth methenol teed
Add ethiont a .
X Other Add additonel meptanol m pleko dante lIter
CAPITAL COST: Equupmenl end SIruaweS (from Page 2) 50
Electncal and lnebumantatOn 1 7% $0
Yerd Piping and Site P /ak 15% 50
Subtotal $0
Contractor OHIP ¶5% 50
Engineering and Coin Mgint 15% 50
Subtotat $0
Contingency 30Y. $0
Total Capital Cost $0
Capital Coet per lb 20-Yr N removal $0.00
OPERATiONS COST: Addilionel ktorsepow (horn Page 2) 0 HP
Eleostoal Power Cost 005 SAW $0 $IØar
NlflIe RediCon uSg Mathand. tO mgIt
Metitancl Reflet 320 geIe
Methanol Co t 07$ SIgal 507.600 S w
Sep rate Stage Ammonia Reduction 0.0 rngtt
Caustic Soda 025% at 0 gala/d
Caustic Soda Coal. 060 5/gal 50 5/year
Eametit Malntenanra Cot $0 S/year
Oenitrdicebon ca1ge Production wiMethatiol 1000 tatd
Sludge DIsposal Cost 400 5/Ion P3.000 S/year
Total Annual CaM Cost 5160500 siyear
EffectIve Annual Interest Pale alter Inflation 201%
20-Year Present Woitli or DIM Costs $2410000
TOTAL 20-YEAR PRESENT WORTH COST $2,410,000
Total Coal per lb 21)-Yr N removal. $0.45
Western Branch WWTP Is Page 1 of 2
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PROJECT ’ lntploinantlng fl .nqlL Amnual Average Total Nitrogen Limit
PREPARED FOR’ USEPA Chesapeake Bay Office
PREPARED av. Virginia Tech with Steams 1. Whaler. LLC
DATE: March 11, 2001
FACILITY: Pilnoesa Anne temP
LOCATION’ SomaraM County, MO
RATED FLOW: 1.3 — . PE COD 260 mg/I
CURRENT EFFLUENT TN: l iT m&l. PE TICN: 26 mg /I
EFFLUENTTNGOAL’ 30 ntgft,
NITROGEN REDUCTION: 160 Itato
56 l000Ibs4ir
use 1000 Iba120-years
URRENT PROCESS (CHECK ALL THAT APPLYI MLE Etosting Msated Volume (MO)’ N I .
BEPR (A2V, VIP, etc.) EXISt lug Anoxlc Volume (MG) PlIa
Baroenpno . Current MISS St WinWADE 3000
Oxidation Ditch
Lagoon (Blotac, tic)
Cyclical Aeration
SBR
High-Rate Biollitef
— Ernuent Filtration -
X Other thr&tr Conventional Activated Sludge
CURRENT EFFLUENT AMMONIAJI: €1.0 mgIL From Roped
LJFrom Model (atADf and mad. l Cd MCRt 12’ C winter condSons)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1.0 m g /k
fl No modifications raqutred New MISS
C Raise MCRTIItSS Eu esdating tanks (check clarifier capaoly) NJa
C Constiuctadmonal.eratedvctume Flow (mgd). 0
C Qonavuel addItional darifleis Flow (mgd) 0
L Use existing anoicle volume as aerobic (construct separate dend Iecllity}
Use aereled system for SOD removal only (construct separate nat/GeniI fadhity)
Add kultuent flow equalization lank
Other _________
PROPOSED MODIFICATiONS TO GET NITRATE ‘ C 1.0 mgil :
No modtllostlona required
Add downstream DeNit filter with methanol
Add downStream NItrIlISlon Buolilter and DeNit nlt with methanol
Add methanol ta eSthg SNR process
Add uabsonu anoudc lank with methanol Med
Add effluent fllnbotu
otter £ttSdil&darcrio baa ii i%bCv be constructed
CAP1TAL COST: Equlpsifl and Structures (from Page 2): St.30t230
Electrical and Instiumentatloir 12% $157,000
- ‘Yard P%aEtg and Site Work. 15% 5156,000
Subtotal $1M62722
Contractor CHAP’ 15% $24%000
Enganeetwig and Constr Mgmt 15% 5246,000
Subtotal s2.laLs3a
Contingency: 30% 5543.000
Total Capital Cost $2,510,000
Capita l Cost per lb 20-Yr N remoyal. $241
DPERATIONS COST Additional Itorse000er (from Page 2) 0 HP
Electns Power Cost 005 $#kW So S /year
Nitrite Reduction using Methan Ol 0.0 mg/I
Methanol Required 0 galald
Methanol Cost 075 $Fgal $0 U ear
Separate Stage A mmonia Reduction 0.0 mghi.
Caustic Soda @25% conc 0 pla/d
Caustic Soda Coal 060 5/gal $0 S/year
EquIpment Starr llenance Coat $21600 Slyest
Denutrificat i on Sludge Production wittethanot 0 lbatd
Sludge Disposal Cost 400 S/tcfl $0 5/year
Total AnnuatO&MCoat 521.000 5/year
Etleclive Adniat Interest Rate alter mutton. 2.91%
20-Year Present Worth of OEM Costs $320000
rOTAt. 20-YEAR PRESENT WORTH COST: , $3,130,000 -
Total Cost per lb. 20-Yell removt $tS l
Pnnceas Anne, MOa ts Page 1 ot 2
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, ‘ROJEC I: iMØemsnInge3 mWL AniuM Avenge TOW NIVSII L im it —
PREPARED FOR: USEPA. Chesapeake Bay OMce
PREPARED BY: VIrgInia Tech wIth Steams & Whiter. LAS
DATE: March 5,2001
FAC ILiTY: M,ttswomsutWflP.... .
.OCAUON: Clndes County. MD
RATED FLOW: 150 mgd PE COO. 104 mglt.
CURRENT EFFLUENT TN: ITm&L • PE 11(14: 20 mgn.
EFFLUENT iN GOAL: TiThnpi. ‘The ti. currently — upgraded
NITROGEN REDUCTION. 0 tsld to a Bardenio with the abi lily to add
0 l000ibalyr mSso3TN w iDbeact1lefl e
0 1000 tW2Ojsars
CURRENT PROCESS (CHECK Mt. THAT APPLY): — ItE Existing Mated Volume (MG): N b
: BEPR . VP. etc.) Existing Mo lt Volume (MG). Nba
(Undar Design - March 2001) X Baidenptm Currant PASS at Winter ADF. His
- O,ddaIielDIIcI%
- Lagoon (Biolac. sic)
- CyclicaiAeration
SBR
- High-Rate BsofiIIer
Effluent F uIrotlon
CURRENT EFFLUENT AMMO44IMi: Cs mg i. X From RepS
From Modal (at ADF and Iqed. 15 d MCRT. 12° C winier conolhions)
PROPOSED MODIFICATIONS TO GET AMMONIA ‘tO mglL:
C X No modifloatlone NqtSrad New M I SS
LI Raise MCRTIP&SS i n soiling tanks (thick deiffiercapedly) — His
LI isav additional aerated volume flow (mod): 0
LI tonstnfladddlonat dettilers Flow (mgd) 0
LI Jae . .Jetiuig sto Ic volume as iambic (conatrud separate datA tacit ly)
LI Use aerated system for BOO removal only (constiud separate al f lenit facility)
ntnowaqueIm6on t a *
PROPOSED MODIFICATIONS TO GET NITRATE’ IS
Ho nodmcalaona reqi*ed
Add dseam OeNlt titer with methanol
Add dansteem Ninleallon BioSIter and DNI I 6 1 1w with ntetiaS
P 44 methend to ealahing BNR procaee
Pdddowiflm anoflk with methanol teed
Add etIueMRntion
Om i c
CAPITAL COST: EqiApment aid Sbtauas (lam Page 2): $0
EIeScel and kietnenentallon: 12% $0
YaM P ilng aid Sit. WaIt: 15% $0
SubtotaL $0
Con n1wOH&P 15% 10
and Con*. Mgmt 15% $0
Subtotal: $0
Contingency 30% $0
Total Capital Cost $0
Capital Cod per B 20-Yr. N removaL WIV M 1
OPERATIONS COST: Additional Horseposer (from Page 2). 0 HP
EIeais P r Cost 0.05 1 1kW 10 $lyear
t4*a i eReduollOiualI10MelS 0 - 00 mgi.
Memenot Required. 0 galeld
Meland Cost 0.75 ligel $0 $Mer
Sepia Stage Ammonia Reductloit • 00 mglt.
Ca# .rSoda 25% n ot iC. Ogaleld
Soda co ’ 050 VgaI 10$lyaer
Equipment Maintenance Cost $0 SlYsar
Doltifflatlon Skidge Production wlMollwnOl. 0 Bald
Sludge Disposal Coat. 400 Iltoit 101Mw
Total Annual 0614 Cost $0 1 MW
Effective Annual lowest Rate alter InflatiOn: 251%
20-Year Present WorSt ot O&M Cost $0
TOTAL 20-YEAR PRESENT WORTH COST: $0
Total Coet pert. 20-Yr P4 removal 50IVIOI
Maltawomen xis Page 1012
-------
PROJECT: Implementing s3 mfl Annual Average Total Nitrogen Llintt
PREPARED FOR’ USEPA, Chesapeake a Office
PREPARED BY: Vtngtnla Tech with Steenis & Whaler , (SC
DATE. MarthlLZGO l
FACILITY’ tanj9ead WWTP
LOCATION: Iitsi Heed,. MO
RATED FLOW: 0.5 mod FE COO 430 mgi !.
CURRENT EFFLUENT TN: 106 mglL PE TKW 20 mgIL
EFFLUENT TN GOAL: ‘iEn igii.
NITROGEN REDUCTION: 30 Ibeld
11 l000Ibsiyc
219 1000 bsl2O-ye&rs
CURRENT PROCESS (CHECK ALL THAT APPLY). X MLE Extsting Aerated Volume (MG) _ j 037
BEPR (P.210 YIP eke) Einting Anoxic Volume (MG) 0 259
: B en o Current MLSS at Winter ADF 2000
Ox,Cauon I)tch
Lagoon (Blolac. etci
Cydicol Aeration
SBR
Itloli-Rate Blofilter
Effluent Fitration
Other :
CURRENT EFFLUENT AMMONIA-N: 05 nigh. X From Repod
Prom ModdI (atADF and load. IS d MCRT. U ’ C vinter coiiddlone)
PROPOSED MODIFICATIONS TO GET AMMONIA (10 mfl:
x plj n%oaJk stnita requited New MLSS
Raise MCRTIMLSS Vi Snag tanks (check dan t e capacity) - . Nip
- Construct additional aerated volume Flow (mgd) 0
Construct SdtOoneI dedilera Plow (mgd) 0
Lisa eiastlng anodoacAmme aa aerobic (ccnstruct separate dent faolily)
Use aerated system for BOO removal only (construct separate nltfdenltfaclhty)
- Addedluentnoweqtsntbintsnk
Other ________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE c 1 0 mnçIL:
E l No modifications mequied
F1As d neteamfl DeNt filter with methanol
Add downstream Neitficabon BlollIter and DeNt filter with methanol
Add methanol 10 etdating BSR process
AØd downstream ailoste tank with methanot feed
Add efltuent NIlatlan
Other. ______________________________________
CAPITAL COST: E ulpment and Stnnurea (from Page 2)’ 1250,000
Electrical and lnstnmeiltifjofl 12% $30,000
Yard Piping and Site 15% $36000
Subtotal. $320000
COntJadOI’OH SP 15% 148.000
Engineering and Ccnatr Mgmt. ¶6% 148.000
Subtotal’ 1420.000
Contingency 30% 196.000
Total Capital Coat $520,000
Capital Cost per lb 20-Yr N removal. $2.31
OPERATIONS COST: Addltonal Horsepower (from Page 2): 0 HP
Electrical Power Cost 005 1 1kw 1084ev
NItrate Reduction using Methanol’ 7J night.
Methanol Required’ 10 gals ld
Methanol Cost: 075 ll9at 12,700 $Iyear
Separate Stage Ammnonw’Reduction 0.0 mglt.
Caustic Soda 025% conc 0 galsld
Caustic Soda Coat 060 $ al $0 $IØar
Equipment Maintenance Cost $4,200 $iyear
Donitnttqat,on Sludge Production wlMelhanol SO bald
Sludge Disposal Cost 400 $Aon $3,700 1 /year
TotatAnnmal OW Cost. $10,000 1/year
Effective Annual Interest Rate altar Inflation. 291%
20-Year Present Worth otOSM Costs. $160,000
TOTAL 20-YEAR PRESENT WORTH COST’ 1660.000
Total Cost per lb 20-Yr. N removal 13.11
IndlanHead MDids Page 1d2
-------
PROJECT: Implementing a3 rogIL Annual Avenge Total Nitrogen LimIt
PREPARED FOR- USEPA. Chesapeake Bay Office
PREPARED BY. VirgInIa TacIt with Stesms & Wheler, LLC
DATE March 19,2001
FACILITY Havre de Grace WWTP
LOCATION: Ilsvre de Grace. MD
RATEO FLOW: T iThngd PE COO N /a mgit
CURRENT EFFLUENT TN: TWmg/L PE TKN N/a mgat
EFFLUENT TN GOAL: 30 mg/I
NITROGEN RECUCTION 80 lbs/d
29 I000 lbs/yr
584 1000 Ibs!20.years
CURRENT PROCESS (CHECK ALL THAT APPLTh :i taLE ExistIng Aeratad Volume (MG)- N/a
BEPA (A2/0, VIP. etc.) Existing Anoxic Volume (MG) N/a
— Bardenplio Cinnt MISS at Wider M W N/a
Oxidation Ditch
Lagoon (Boat elc)
Cyclical AeratIon
SOR
High-Rats Biolliter
Effluent Filtration
i Other MLE with Recycle ( toni RBCs in SeW before Clarifier
CURRENT EFFLUENT AMMONIA-N: ci 0 mg/I X tori Report
m9 Ond 15dMCRT, 12°C wintercondlbonc)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.OØg/L:
K No modifications required New MISS
Raise MCRT/MISS in existing tanks (check clarifier capaBly) ff 1 5
Conatnd additional aerated volume Flow triad)- 0
Gonstaict sJditnnal das hers Flow (mgd) 0 -
L Isa existing anoidt vckmie as aerobic (constnfl separate denit faclity)
Use aerated system for BOD removal onty (construct separate ni/deibt facility)
Iniuen1flowequallaatlon tank
-Other __________
PROPOSED MODIFICATIONS TO GET PWRATEC I A mg/L
. No moddicabene —
And dSwitem DeNIt Eter win methanol
And dowsitesm NItrlfl n Biolllter and OeNtt hitervath nietlwiol
‘. methanol bexiehig SNR process
* And dowmteeit siioidc unit with momanol feed
r- Add sflfuerdhlbsbcn
otter “ c--’ -
CAPITAL COST: Equipment end Structures (from Pegs 2) 11.620,000
Electncal and inslngnesdatlen: 12% $194,000
- Yard P mg and SIte Wait. 15% 1243,000
Subtota l $2060000
Contractor OH&P. 15% 5309.000
Engureenng and Constr Mgml 15% 1309.000
Subtotal $2 580 000
Contingency 30% $518 000
Total Capital Cost $3,300,900
Caoilsl Cost per lb 20-Yr N removal 15.65
OPERATIONS COST: Additional Horsepower (kern Page 2) 40 HP
Electiicsl Power CosI 0.05 $/IiW $13100 1/year
Nitrate Reduction using Methenot 50 mg I.
Methanol Requwet 40 gaIs
Methanol Cost. 075 1/gal $11,000 S/yea
Separate Stage AmmonIa ReductIon - 0.0 mglt.
Caustic Soda © 25% ooric 0 gawd
Cauex Soda Cost 010 1/gal $0 S/year
£Qulpmett Maintenance Cost 120,800 1/year
Oemtnllcation Sludge Predumalon witaabiand 110 lba/d
Sludge Disposal cost 400 S/tn 51.000 S/year
Total Annual 0511 Cost 558.900 S/year
Effective Annual Interest Rate Merin ltabon 291%
20-Year Present Worth of 0111 Costa. $880,000
TOTAL 20-YEAR PRESENT WORTH COST: 14. 180,000
Total Cost per lb 20-Yr N removal $7.11
I4svre de Grace MO ifs Page 1 of 2
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PROJECT: Implementing .3 mg /I Annual Average Total Nitrogen Limit
PREPARED FOR: US EPA, Chesapeake Bay Office
PREPARED BY. Virginia Tech with Steams S Whaler, LLC
DATE: Merctt 19, 2001
FACILITY: Rucco Femi Food. WWTP
LOCA1 ON: Edinbum. VA
RATED FLOW. j _ nigd PE COO: Wa mg/I
CURRENT EFFLUENT TN: .j&LmglL . PE TEN __ Wa fig/I.
EFFLUENT TN GOAL: 30 mg/I
NITROGEN REDUCflON: 90 1MM
33 1O00t5
65? 1000 ts/20-yee.s
CURRENT PROCESS (CHECK ALL THAT APPLY): PaE Existing Aerated Vokime (MG) - Eta
X BEPR (A2m. VIP. etc) Existing Anoxic Vohane (MG)’ N/a
— earrp ia Currant MLSS at Winter ADF’ 4000
— OxIdation Ortoli
— Lagoon (Belie. etc.)
— CptttaiAetatttt
— S ER
— High-Rate Biotsiter
— Effluent Fitsaton
31 Other P.210 with Integral Schresber Process
CURRENT EFFLUENT AMMONIA-N CI 0 mglL X From Report
From ittadel (atADF and load IS d MCRT 12’ C winter conditions)
PROPOSED MODEICATIONS TO GET AMMONIA 41.0 sf1911:
‘Xkto modtatlona required New MLSS
jjtcalse MCRTIMISS In existing tanks (chedt danfler capacity) ‘ N /a
-i!Constin additional aerated vo l ta ire flow (mgd)
iJConstsuct add Wonal danhiem Flow (mgd):_______
]IIn eSing aiwdovolwne as aerobic (corratsucl separate da n a taSty)
Juae aerated system tar BOO removal only (oonslnfl separate nltMerdt facility)
IASJ inlluerd flow equa&atson tank
Joeser - - ‘ - -I -
PROPOSED MODIFICATIONS TO GET NiTRATE ‘1.0 mg /I:
? mcj4PV-S.s required
Md doenstietan OeNlt lifter with methanol
Add doellite N1jflc 5on Biofilter end DeNit Sitar with methanol
M d methan9ite eloa*19 ONE prooess
.‘r Add do ..aa. . aitSO tank with inetlianol/aed
Add effluent Station
Othr _________________________________________________________
APITAI. COST: Eq u ipment and Sin aires (from Page 2) 51.370.000
Electrical end kishurnentaton 12% 1164,000
- Yard Piping and StWosk. 16% 1206.000
Subtotal 31 740.000
Conactor 0MW. 15% 5261.000
Engineering aid Conslr Mgmt 15% 5261.000
Subtotal 12.260.000
Contingency. 30% 5522.000
Total Capital Cot $L7$0.00 0
Capital Coat per ro 20-Yr N removat $4.23
DPERATIONS COST- Additional Horsepower (from Page 2): 20 HP
Electrical Power Cost 005 flW 56.500 1/year
Nitrate Reducedn uelig l4ethSiol. 9.0 rust
Methanol Requ tet 40 galS
Methanol Cot 0.75 5/gal $1 t,000 1/year
Separate Stage Ammon Ra*icoott 0.0 mgt
Caustic Soda C 25% cost. 0 gawd
Caustic Soda Cost 0603/gal 101/year
Equipment MaSanance Cost $22,600 1/year
Denitsiflostlon Sludge Production waMatfianol. 130 IteM
Sludge DegaS Coat 400 Mon 19.500 1/year
Total Annual OVA t ’ 549.600 5/year
Ellective Annual test Rate after kifiSon 2 91%
20-Year Present Wwth of O&M Costa $140,000
TOTAL 20.YEAR PRESENT WORTH COST: 53.520.009
Total Cost pert. 20.Yr N removal $5.36
RoccoFoods, VA ‘ c lx Page 1012
I
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PRO CT. Implementlnge3 nfl Aiii%ttal Average YSI Nitrogen Umit
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY: VIrginS Tech edit Stearns & Whaler, LLC
bA l i: March 19 .2001
FACILITY. Mona Creek WWTP
LOCATION: Wvenna frajtiorty, cttarióttesviitt VA
RATED FLOW 15.0 mgd PE COD NM mglt.
CURRENT EFFLUENT TN: YWmgit PE TKN NM mglt.
EFFLUENT TN GOAL: 30 mgsl.
NITROGEN REDUCTION: 500 lb M
183 l000lbslyr
3850 1000 Ibs/20-seaa
CURRENT PROCESS (CHECK ALL THAT APPLY): I DALE ExIsting Mated Wurne (110)- N M
X BEPR (AVO. VIP. tic) Existing Ano oc Volume (110). NM
— Berdenpho Current MLSS at Waiter AOF 3000
— oaidauun Ditch
— Lagoon(BIOIaC.etc)
— CyciicslMralioi l
SSR
: Hiphaaw
— ElIluent Flitatiori
X Other A210 that also canOe canted es en MLE -
CURRENT EFFLUENT AMMONIA-N: 0.5 mg / I. From Report
From Modal (MACF and load, 15 d MCRT. 12’ C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0mg/I-:
X No ,a qd New MLSS
Raise MCRTIMLSS in tasting tanks (c/tack c/wilier capacity) N /s
Construct additional aers led volume F (mgd) - 0
Construct additional danliers Flow (mgd) 0
I /se erisling anoxic voltithe as aerobic (construct separate tie facility)
Use aerated system for GOD removaf only (construct separate nit/dend facility)
Add ‘ifluent SOW equakzatlon tan*
Other ______________________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE ( 1.0 mg&
£J$o mcdmcellons requIred
X Add downstream DeN it litter with methanol
Add doteistreem Nitillicatlon Blofilter and DeNit otter with methanol
Add meUWIel teeidstlngBNR process
Mddswnsveam enctdc tank with methanol feed
Add effluent l O n don
, . - s -
CAPITAL COST. Equipment and Stnctu’n (from Page 2). 55.200.090
Electncal end Instrumerfltloft 12% $744000
Yard Piping end Site Work: 15% 5930.000
- Subtotal. 57.870,000
ContractorOH&P: 15% 51,101,000
EngIneering end Consv. Mgmt 15% 51,181.000
Subtotal - 510,230.000
Contingency 30% 52.381,000
Tolal Capital Cost 8h2.893,000
Capital Cost per lb. 20-Yr N removal $3.45
OPERATIONS COST. Additional Horsepower (from Page 2) 300 FtP
Electucal Power Cost 005 5 /trW 598 000 5/year
Nitrate Reduction usM Methanol 4.0 mg/I.
M achanoI Required. 230 galaM
Methanol Cost 075 S/get 103 000 S/year
Separate Stage Ammono Reduction 0.0 mg/I.
Caustic Soda 025% 00110.
Caustic Soda Cost 060 S/gal 10 5/year
Equipment Maintenance Cost $102,300 5 /year
Derilkification Sludge Piodi.Clon *4lelhanol 720 Ibsld
Sludge Disposal Cost. 400 S/ton 552.800 SPyear
Total Annual OSM Cost $315,900 5/year
Effective Annual Interest Rate alter InflatIon- 2.91%
20-Year Present Wodit dO&M Coslr 54 74 (3 000
TOTAL 20-YEAR PRESENT WORTH COST. 517,330.000
- Total Cost per lb 20-Yr N removal $4.76
Rivannax ls page lof2
-------
PROJECT: implementing a 3 mgit. Mnual Average Total Nitrogen U hf
PREPARED FOR: USEPA, Chesepeake Bay Office
PREPARED BY. VVgInla Tech with Stearns A Whiter, LLC
DATE: Mar di 19,2001
FACILiTY: Pu IfvItle WWTP
LOCATiON: VA
RATED FLOW. tomgd . PE COO. Nil niglL
CURRENT EFFLUENT N: jQ_mgfl. PE 1104 Ma inglL
EFFLUENT TN GOAL: 3.0 mg I.
NITROGEN REDUCTION- 30 bsfd
ti 1000 Ibslyr
210 1000 Ihsi2O-yews
CURRENT PROCESS (CHECK ALL THAT APPLY) tItLE Existing Aerated Volume (MG) N/a
OEPR (A210 VIP. etcp Existing Ancaic Volume (MG)- vita
Bardanptio Current 111.55 at Wvitet AOF 3000
Oxidation Ditch
— Lsgoon(Biotac et)
— CyclicalAeratzon
SBR
— High-Rate B’of’lter
Effluent Fittiation
X Other St*p Feed MIX with Effluent Filters
CURRENT EFFLUENT AMMONIA-N: C l 0 molt. X From Pepc’t -
From Mod& (at AOF and load. 15 d MCRT. 12’ C winter onMtions)
PROPOSED MODIFiCATIONS TO GET AMMONIA c 1,0 ntglt.:
ffK]No modifications required New MISS
F MCP17MLSS f ri existing tanks (thedi dazdlercepaohy)
‘Cqnemnedtituoost aerated volume Flow (mgd): ..o1 ’
Ccnsnol addItional daittlara Flow (mgd) 0
“Use Siting anndc vokatie as aercbt ( nstiuct s4flatdentt facilIty)
Use aerated systs’ri for BOD removal only (construct separate nit/denli facility)
J’ Add influent flow equalization tan l
t ; Other: -r - ‘ -
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 m 1t 4 :
No modifications required
- - Add downstream DeNd fitter with methanol
AØd Øownstream NhtttflcatIon Biotilter and CeNit fitter veth methanol
Add methanol to existing BNR proceee
- Add dowintmam anoido tank *4th methanol toed
Add ettluant ffltra n
Othir -
CAPITAL COST: Equipment and Structures (tront Page ?) $25t000
Eleattoal and lnst,umentahuon 12% 530.000
Yard PipIng and Site Work. 15% 130.000
Sittotal: 1320,000
CwtactixOH&P 15% 345.000
- Engviaait g and Constt MgrnL 15% $45,000
Sutfiotat 1420 .000
Contingency- 30% 398000
Total CapItal Cost. $630,000
Capital Cost pert 20-Yr. N rtinovai’ $2.3?
OPERATiONS COST: Additional Horsepower (from Page 2) 0 HP
Electrical Power Cost 005 SiliW $0 $lyear
Nitrate Reduction usaig Methanol: $0 mglt,
Methanol Required - 10 gould
Pilt—n.A Cost 0 15 ligal $2,700 $Iyear
Separate Stage Anunonla Reduction’ 00 n-igfi.
Cats Soda 025% conc 0 gals/d
Caustic Soda Cost. 0 ,60 $igai $0 $lyear
Equipment Maintenance Cost 54.200 Slyear
Deidrdtcation Sludge Production wlMelhanol 40 mild
Sludge Disposal Cost 400 S/Ion $2,900 llyear
TctalAnnu i tO&MCosl $9000 S/yest
Etfective Annual interest Rale after inflation 291%
20 Year Preserd Worth of O&M Costs $150,000
TOTAL 20-YEAR PRESENT WORTH COST:
Total Cost per * 20-Yr N removal’ $3.06
Purceihaite VA ils Page lor2
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PROJECT : lnplementlng .3 nfl Annual Average Total Nitrogen Unit
PREPARED FOR USEPA, C hesapeake Say Office
PREPARED BY: Virgin t a Tech with Stearns & Whaler. US
DATE: March 19.2001
FACILITY: Parktns 160
LOCATION Fiedendc CounW.W!. _
RATED FLOW: 2.0 .ngd FE COO N i’s mglL
CURRENT EFFLUENT TN: WThngii. PE TICN N!Lmg/L
EFFLUENT TN GOAL. TUmgit
NITROGEN REDUCTION. 20 bud
7 1000 Ibalyr
146 1000 1bw20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): : Eidsting Aerated %ftbjine (MG). We
— SEPR (Alit. VIP. it) Existing Mono Vobjina (MG) - PUs
— Bardenptio . CUITBnIMLSSSIWIAteVADF 3000
K OxidatonDdoh
: (Bdac. ito)
Cydtcal Aeration
SOft
Hch RateBcf Iter
Effluent Filtration
K Other SkidwitohO OxidatIon pllthcon squretlOn
CURRENT EFFLUENT AMMONIMI; c i a mg I. X from Report
From Model (at AUF and load. lSd MCRT, it C winter cundutlons)
PROPOSED MODIFICATIONS TO GET AMMONIA’ iAnsglL:
X NO modificatiOns required New MISS
Raise MCRTJMLSS in existing tanks (check clarifier capacity) P ile
Coits lruct additional seated icluine Fba (mgd) 0
Cons lruct additional ctauifuen Plow (rngdi 0
Use netaig anoauc volune as aerobic (constru separate dent facubty)
Use aereled system for SOD removal only ( o anslruct separate nlt/denll fadlity)
Add unfluerd flow equatSdon lank
Other - -
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 nglt.
No nodultCa ne reqused
Add dowasteant DeNfl filter with methanol
Add domedman NutrifIcalton StoNIer and DoNut filter with methanol
Add meda lS fo Sating BNR prooess
Add aflwnwiStitSM with nethand bed
‘Add eflks* Station
Other:
CAPITAL COST: EquIpment arid Structuras ((rain Page 2) $1650000
Electrical and instrumentatIon. 12% $165000
Yard Piping arid Site Work. 15% 1240.000
Sub l otat 12.100. 1700
Contras 011SF 15% 1315.000
Engineering and Constt Mgnt 15% 1315.900
Subtot al 13.730.000
ContingenCy 30% 1630.000
Total Capital Cost 13.360.000
Capital Cast per lb 20.Yr N removal $23.01
OPERATIONS COST. Additional Horsepower (from Page 2) 4Q HP
Elecircal Power Cost 00$ 1 1 KW 113.100 Slyest
Nitrate Reduction using Methanol. 1.0 nfl
Methanol Required 10 gals ld
Methanol Cost 075 1 $37 $ly
Separate Stage Ammonia Reduction 0.0 ng&
Caustic 5oda 25% Cant 0 gslsld
Caustic Soda Cost 060 Ilgal 10 $4uear
Eourptnefl Maintenance Cost 127.300 lfrear
Denumficatuon Sludge Production wiMethanol 20 held
Sludge Olsoosat Cost 400 11101% 11.500 Ilyser
Total Mnuat O&M Cog 144.600 $4ear
Lifectue Arviusi interest Rife after inflation 291%
20-Year Present Wad? ’ of O&M Costs 1 070,000
TOTAL 20.YEAR PRESENT WORTH COST. 14.030000
Tota’ Cost per lb 20-Yr N removal 127.30
Parkms Mull VA sis Page I of 2
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?ROJECT: implementing *3 mgIL Mnuat Avenge Total Nitrogen USI —
PREPARED FOR. USEPA, Chesapeake Bay OffIce
PREPARED BY Virginia Tech with Steen ’s & WhS LLC
DATE: Mirth 19,2001
FACILITY. Opequon WWTP’
.OCATIO N: Frederick Coat’. V
RATED FLOW 6 $mgd PE COD: - ‘ 14 1 * mglL
CURRENT EFFLUENT TN: 0.0 mgit PE TKN’ 14 1 * mgtL
EFFLUENT TN GOAL: 3 OmglL
NITROGEN REDUCTiON: 260 Ibeld
95 1000 lbs /yr
1890 1000 Ibsl2O’y.ara
CURRENT PROCESS (CHECK ALL THAT APPLY): MLE Existing Aerated Volume (MG). Pr/a
! BEPR(A210.VIP.etc) £xistlngAnolcicVolume(MG) N I ,
-. Bsrdenpno . Current MLSS at WinIer ADF 3000
— Oxidation Ditch
— Lagoon (Siolac dc)
— Cydital Aeraticn
SBR
High-Rate Siofittec
— Effluent Filtration
X Other Step.MedA2 l system
CURRENT EFFLUENTAMMONIA.N: 04 mgIL X From Report
Fran Model (atADFandtad. ISdMCRT. 12°Cwinterconditions)
PROPOSED MOD1flCATIONS TO GET AMMONIA 41.0 infl:
( ]No modlL tan required New MLSS
b Rs ise MCRTIMIJSS bi editing tanks (check c larIfier capacity T NIa ”
Construct additional volume F (mgd). . -
Construct additionS dar ien Flow (mgd) :
o Use Siting sno ut wine Ia aerobic (construct separate dm11 tacility)
• Use aerated sysloun bBQO removal only (construct separate nivdfl facility)
bifluent flow eqwkntion tart
‘-Other ‘ -rfl -
)ROPOSED MODIFICATiONS TO GET NITRATE C 1.0 mgtt
No modifications required
Add downstream 0e148 filer with methanol
Add downstream Nitrl&alloui Biolilter and DeNit litter with methanol
• Mc methanol to e tng BNR proossa
M e downstream aisle tank with methanol teed
Add effluent Iteration
Other ________________________________________
CAPITAL COST; Equipment and Structures (from Page 2). 13 .140 .000
Electncal and Instrumentation 12% 5377.000
- Yard Piping end Site WOrt 16% $471000
Subtotal 53990.000
Contractor OH S? 16% 5599.000
Engineering and Const Mgnlt 15% 1599000
Subtotal 56.190.000
Contingency 30% 51,197.000
Total Capital CoiL 5 5.390. 000
Capital Cost porte. 20-Yr N removal $3.37
OPERATIONS COST: Additional Horsepower (from Page 2) 130 HP
Electrical Power Coat 005 5 1kW 542,500 S / year
Nitrate Reduction usIng Methanol 50 mqri.
Methanol Requwed. 120 gataS
Methanol Cost 075 5/gal 132.900 5 / year
Separate Stage Ammonia Reduction: 0.0 mglL
CsusucSoda 2S%0OnC . Ogsisid
Caustic Soda Cost 0.60 5/gal 50 5/year
Equipment Maintenance Cost 381 900 S /year
Denutrufication Sludge Production w lMettianol’ 300 b/d
Sk idgeOlaposatC os l 400 5/ton 127 700 Slyest
Total Annual ow coat. $155,000 slyest
Elfeclive Annual Inlerest Rate after Inflation 291%
20.Year Present Worth of OW Costs *2.320.000
TOTAL 20.YEAR PRESENT WORTH COST; $5,710,900
Total Cost per lb 20.Yr N removal. $4.59
Opeauon. VA s!s Pege 10 (2
-------
PROJECT. Impleinentlnga 3 raft Annual Avenge Totel mgen Unit
PREPARED FOR: USEPA. Chesapeake Bay 0 1 8 1c c
PREPARED BY: Virginia Tech with Steams & Wheler LLC
DATE: March 19, 2001
FACIUTY: Middle RIver-Verona WWTP
LOCATiON: Aimusta County. VA
RATED FLOW: 43 mgd FE COD N b rngIL
CURRENT EFFLUENT TN: SOrriglL FE TKN 14 /a . - rngit
EFFLUENT TN GOAL: 30 mgIL
NITROGEN REDUCTION- 90 lbs/C
29 I000lba/yr
584 1000 IbsI20. ar5
MLE _________
OEM (*2/0. ViP. etc l _______
OardenphO
Qiadation Ditch
lagoon (Bidac. etc
Cyclical Aeration
5 8 K
High-Rate Glofilter
Effluent FIltration
Ovier Bruth Aerator Oxtiation Dutch
CURRENT EFFLUENT AMMONIA.N: cl.0 ‘ng/L X From Recoil
From Model (at ADF andlood. 15 dMCRT 12° Cwuntar conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA 4 1.0 ingiL:
Nonloduficaticns required New MLSS
Raise MCRTaMLSS in exating tanks (check clanrier capacity) N/a
Conatruct pddutionat aerated volume Flow (mgd). 0
Conatnict additional Sitters Flow (mgd) 0
Use wdsting anoxic voluise as aerobic (construct separate dank fadhlty)
Use aerated a tem forBOD removal only (construct separate nlvdenut teSty)
Md killuent fl equaluz.aadn tank
Oth - -
PROPOSED MODIFICATIONS TO GET NITRATEd 1.0 ingbL:
IflNo modlficatlona required
F detenstrea’n DeNit 1I with mevtanol
Md downeteem Nubtitcabin Bcfuhter and DeNit filter edli methanol
Md methanol ki eristirçBNR proasa
Add dasistream anSe flwth methanol feed
.7 PeMdflIh*tion
1 4 .
Mdutlonal Horsepower (from Page 2)
ElectrIS Power Coat 005 9kW
Nitrate Reduction usog Methanol ________
Methanol Requires
Metheno lCoat. 015 S/gal
Separate Stage Ammonia Reduction ________
Caustic Soda p25% corto
CaustE Soda Cost 060 1/gel
EqSpment Maintenance Cost
Denltdllcetloui Sludge Production wiMethanol
Sludge Diaposal Coat 400 3/tOn
Total Annual O&M Cost
Effective Annual Interest Rate after Inflation
20-Veer Present Worth of O&M Costs.
CURRENT PROCESS (CHECK ALl. THAT APPLY):
x
K
Existing Aerated Volume (MG) His
Existing Moxie Volume (MG). N/a
Currenl MLSS at Winter ADF’ 5000
CAPITA!. COST:
OPERATIONS COST.
Equipment and Structures (from Page 2)
Electrical and Inatnimentatuon
Yard Piping and Site Work
Subtotal
Contractor OH&P:
Enpneenng end Constr Mgint
Subtotal
Contingency
Total GaaS Cost
Capital Cost per lb 20-Yr N removal
12.530.000
12% 5304.000
15% 5380.000
13.210000
13% 1482000
15% 5482.000
54 170000
10% 1063.000
35,130.000
8878
90 HP
529.400 5/tear
20 lug/ I.
- SOgats/d
51.200 S/year
to mg /h.
0 gale / C
10 S/year
541200 S/tear
110 maId
a000 5
581.300 S/year
2 91%
11 10,000
1 1.4 4 8 ,000
511.03
TOTAL 20-YEAR PRESENT WORTH COST.
Total Cost per lb 20-Yr N OIal
Prbddle River-Verona VA iris
Page 1 or 2
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PROJECT: tmplamenthiga3 ung& Annual Average Total Nitrogen UntiL —
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY Vkglnla Tech with Stearns & Whaler, LLC
DATE: VSrvh 18,2001
FACILITY: mc. VA
LOCATION: FItS. VA
RATED FLOW: 12 mgd PE CCI) 5071 tnglL
CURRENT EFFLUENT iN: tFmgii. PE TKN 98 mgIL
EFFLUENT TN GOAL:
TROGEN REDUCTION 390 tbski
142 1000 lbs/yr
2841 1000 1 0 5/20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): — MLE ExislungAeraled Volume (MG) 4.0715
BEPR (AWO VIP etc.) Existing Anoinc Volume (MG)- o.nir
K Bardeapho Current MISS at Winter ADE M11
Oxidation 04th
:
Cyclical Aeratmn
SBR
: H h-RaffiSIQfIIIOr
— Effluent Filrflon
Other. ________________________________________
CURRENT EFFLUENT AMMONIA-N: < 1.0 mg/I K From Report
From Model (S AD! and load, 15 d MCRT, 12° C winter conditions)
R0POSED NODIFICA 1-lOrtS TO OCT AMMONIA c 1.0 rag/I: -
I$ Itinodilcoflons teqtired- New MLSS
I Raise MCRT/MLSS li i tdsting tesdcs (dfl cterrapa 4y)
IT! Construct additional aerated volume Flow ( mgd):- ç ,. - ,
C Constnictadditleneldestlters Flow (ingd). -b
C Use ex 5uig ama-dc v ste as aerobic (construct separate dealt laclitty)
[ if Use aerated intern for 900 removal only (conalnict separate nIt/denit taSty)
[ f i l l Add Inftiet*llow equatntion tank
Lamer
PROPOSED MODIFICATIONS TO GET NITRATE ‘1.0 mg/I;
No inodit lcations requIred
Adddowistream DeNIt fitter with methanol
A downstream Nitriflcatlon SloA ne , and DoN ’t filter with methanol
mamaS to axisllng SNR procoss
Add downstream snoxlc tank w,tttaielhsnol feed
A S aMuses aeration
X Other Add mote methanol
CAPITAL COST: Equipment and Stnflwes (hem Page 2)r 80
Electrical aid tnsbumentabort 12% 50
YaidPçlngand sltaWc$t 15% 50
Subtotal
Contractor Ot t &P. 15% $0
Engineering and Constr. Mgmt 15% $0
Stfltat $0
Contingency: 30% 80
Tota l Capital Cost $0
Capital Coat pa l O 20-Yr N removal $000
OPERATIONS COST: Adthttonal Horsepower(froin Page 2): 0 HP
Electitcal Power Cost 005 1 5kW $0 Ilyear
Nwate Reduction using Methanol StY mg/I
MedianS Required. 100 gate/el
Methend Cost. 015 Vga 349i00 vyear
Separate Stage Ammonia Reduction 00 angSt.
Caustic Soda 25% nc. 0 galsld
Caustic Soda Coat 060 S lgal 50$/year
Equipmeni Maintenance Cost SO S/year
Denitnlication Sludge Production w*tlhanOl 560 We ld
Sludge Disposal Cost- 400 elton 340900 S/year
Total Annual 0&M Cost 590 200 Slyest
Effective Annual Interesi Rate aster Inflation 2 91%
20-Year Present Worth of O W Costs $1,350,000 -
TOTAL 20-YEAR PRESENT WORTH COST: - $1, 150,000
T Cost per tO 20-Yr N removal $947
MerckVAxls Page lof 2
-------
PROJECT: impleinetdjng a n f l Annul Average Total Nitrogen (knIt
PREPARED FOR. USEPA, Cheiepa.ka eay Office
PREPARED BY: Virginia Tech with Steams & Whdec LLC
DATE: March10,, 2001
FACLITY: LuryYAWTP —
LOCATION: janv PA
RATED FLOW: 2. Omgd P t COO. HIs mglL
CURRENT EFFLUENT TNt fl•,mgIL PE TXN K u mg lt.
EFFLUENT TM GOAL: 30 mg /I.
NITROGEN REDUCTION: 70 Ibs I S
20 t000 lbs/yr
511 1000 Ibs/20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): : MLE Aerated Volume (MG) 196
- BEPR (*210, VIP Sic) Eaisiirig Anoxic Volume (MG) Wa
— Sardenpho Current MLSS at Winier AQF 5500
IC Oindat’on Ouch
- Lagoon (B’olac etc I
IC Cyclical Aeration
SBR
High-Rate Sioliltor
Etiluent Fitratcn
— Other
CURRENT EFFLUENT AMMONIA-N: ‘ (1,0 mg/L X Fran Repoit
From Model (at ADF and load. 15 d IdCRT 12’ C Ster conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA <1.0 u ligILt
inoddlcfln rsqwred New MISS
r I . Raise MCRTIMLSS In eidstng tanks (check clardiercapacuty ) 7? N/a
19’ Conseud additional aerated volume Flow (mgd). ‘.0
Constun addulIonel dan / l ois Flow (mgd). o
Use eidsdng anoxto volume as aerobic (oonslruct separate dent facIlIty)
• . Use aerated system for BOO removal only (construct separate nitlden;t (acuity)
Add stAt ism 110* equalaaXfl tank
Other _______________________________________
PROPOSED MODIFICATIONS TO GET NiTRATE < 1.0 mgIL:
No modifIcations required
IC Add dosealftam DeNit liner otth methanol
domisliwani NulnfóluoA Sdllter SM DeNit r lter with methanol
niemaid to etueVstd BNR process
Add downstream anoxic tfl sell’ methanol teed
effitisnl ttlon.
CAPITAL COST. Eqtiprrant and Structures ((rum Page 2) 51,650.000
Electrical and Instrumenta dOn 12% $t98000
Yard Piping and Site Wait: 15% 1248.000
Sut4c(a l. 12,100,000
Contractor 0 M W: 15% 1315.000
En selti 1g end ConeIr. Mgnt 15% 1315.000
Subtotat 52.730,000
Conlingency 30% 1630.000
Total Capltel Cost. $3,380,065
Capital Cost per lb 20-Yr. N removal $0.56
OPERATIONS COST: Mottlcnal Horsepower ((runt Page?) 40 HP
ElathIs Power Coat. 0.05 5 1kW $1 3.100 Slyear
Nitrate P ’ttlNl using Methanol. 4.0 mg/I.
Methanol RequIted. 30 galafo
Methanol Coat. 075 S/gal 58.200 S/year
Separate Stage Ammonia Reduotiow 0,0 mgit
Caustic Soda 25% conc 0 gala
Caustic Soda Cost 060 s/gal 505/year
Eqtspment Maintenance Cost 527.300 5/year
Denitriricalion Sludge Production wIMethanol 100 thud
Sludge Disposal Cost 400 Men 57.200 5/year
Total Annual OSM Cost. $55000 5/year
Effeciuva Annual lisest Rate alter In f tation 91%
20-Year Present Worth ol OW Costa *640.000
TOTAL 20-YR PRESENT WORTH COST 54,200,000
Total Cost per lb 20’Yr N removal $6.52
Luray.VA Ida Page 1 at 2
-------
PROJECT: ki,,Iamanting a3 mglL Annual AYSI19 Tota l Nlwget umit — .
PREPARED FOR: USEPA, Cheaspuke Say Office
PREPARED BY: Vl,!Inla Tech with Steams & Wheler, LLC
DATE: March 1 6 . 2001
FACILITY: . Nesnen M. Cole WwyPjfermerly Lower Potomac)
LOCA 1 1ON: Featax ( otflv. ! JA
RATED PLOW’ €70 mgd PE COD 300 mgiL
CURRENT EFFLUENT Ut PE TKN. 23 mgiL
EFFLUENT TN GOAL: ilmg/i.
NITROGEN REDUCTION: 2790 bed
1011 l000lba/yr
20367 1000 lbS2Oqears
MLE’
BEP,R ( f l / U. VIP. s ic)
Sardenpho
OxiØeI’On Ditch
LS OOA(BdaC.a)
Cyclical Aeration
SBR
High-Rate Bdilter
Effluent Flitnaflon
Other Step M’WMLE no nuawi rwyuv
CURRENT EFFLUENT AMMONiA- Id- c1.0 sip/I. From Repast
- - ‘iti From Model (etAOF end load, 15 d MCRT, I?C winter condlbons)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mg/L
j’ JNo modilicetlons required New MISS
j]Rilse MCRT&ILES in ensllng lank a (check derSer capadty) ______
‘3!!]Conatwct edtlonal aerated volume Flew (mgd) 0
. ]CnJfllfiJolalflUonS d.rlflers Flew (mgd)’ -0
!]tisa exiebng snostcvotime as aerotic (construct separate dents faotsty)
IJse eerated system for BOO removal only (construct separate nlVdenit raS hly)
I]Add InItuent now equelisation tank
_JOther
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mg1L:
No modifications required
AØd downstreem DoN ’t Oltec with methanol
Add downs treem Nitilitabon Biofilter and OeN’t liter with methanol
Add methanol to e iethig BNR process
Add downstream m ac tank with methanol feed
Y.. Add affluent liltalOn
• Other Conweit S&,ep Sd SMIKecs todenite liters ‘. . . -
CAPITAL COST:
Equipment end Structures (from Page 2)’
Eledocal and instrumerilallon: 12%
Yant Piping and See Work 15%
Subtolal
Contractor OHIP. 16%
Engineering and Casteir. Mgnit 15%
Subtotal -
Contingency: 30%
Total Capital Cost
Capital Cost perth. 20 -Yr N removal
$6,210,000
5754,000
5942.000
17 . 600,000
11.1 57,000
11,197.000
$10370000
$2,394,000
$12760000
$0.53
OPERATIONS COST-
Additional Horsepower (from Page : 0 HP
Electrical Power Cost 005 SAW 10 s4eer
Nitrate Reduction usIng Methanol 50 mg/I.
Methanol Required — 1270 gals/if
PswJan 015 S/gal 1347 700 S/year
Seperate Stage Ammonia Reduction 00 mg/I.
Caustic Soda @25% flC 0 galeld
Caustic Soda Cost 060 S/gal 50 3/year
Equipment Maintenance Cost 1103,100 3 /year
DenilrisCatiorl Sludge Production SMethenOl 4020 tiltS
Sludge Disposal Cost. - 400 S/ton 5293,500 5/year
TotalAnntiel OE M Cost 1744.600 5/year
Effective Annual ititereet Rate after In lalion 2 . 61%
20-Year Present Wor m of OEM Costs $11,170,000
TOTAL 20.YEAR PRES
ENT
WORTH COST;
Total Cost pert. 20-Yr. N removaL
5 *930,000
$1.17
CURRENT PROCESS (CHECK ALL THAT APPLY)’ !
ExIsting Aereled Volume (MG) 1t05
Existing Anoxic Volume (MG). 7.3
Current MLSS at Winter ADF 2700
Fairfax County VA xis
Page tot 2
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PROJECT: lmpl.menthtg aS mg i. Annual Average Total NItrogen LimIt
PREPARED FOR. USEPA, Chesapeake Say OffIce
PREPARED BY: Virginia Tact wIth Steams & Whaler. LLC
DATE: March 19,2001
FACILITY: LeesburqWWTP
LOCATIO N: Leesbum. VA
RATEDFLOW: 49 mgd PECOD NSa mgiL
CURRENT EFFLUENT UI: iTThngIL PE TKN NSa mgiL
EFFLUENT UI GOAL: 30 mgIL
NITROGEN REDUCTION: ISO lbs/U
58 l000ibs/yT
1158 I000lbs/zoyaars
CURRENT PROCESS (CHECK ALL THAT APPLY): x PALE Existing Aerated Volume (MG). N/a
X SEPR (flfl. VIP. etc) Eaostflg Moxie Volume Q) N/s
- Ba.detw*o Cunent MLSS at Waiter ADE. 5500
- Oxidation DItch
— Lagoon (Blolac. etc.)
- CyclIcal Aeration
S M
— High-Rate Biotilter
- Effluent Filtration
X Other An M V that can alto be operated as an PALE
CURRENT EFFLUENT AMMONIA-N: < 10 mg/I. [ jjFfom Report
LJffroin Model (at ADF aid toad 15 d MCRT 121 C waiter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mg/I.
flNo modifications required New MLSS
] Raise MCRTIMLSS biuiatng tanks (check ctarther capacity) N/ I
:Jconsvuci addItIonal aerated volume Flow (mgd] 0
JConstsuctadddionatdaarmts Flow (mod) 0
I]Use eiaebrtg anoie@ volume as aerobic (construct separate dernt facility)
JUse aerated sysleni icc SOD removal only (construct separate nltldenlt facttsly)
JAdd influent flow aqualizatioll lank
JOther
PROPO tO MODIFICATIONS TO GET NITRATE ‘1.0 mgi.:
- NomodIflcatzonere*ed
doentaveanl DeNIt filter ath methanol
dovmatreani leltrifleflon Sloltlter end DeNit filter with methanol
i - i methanol beitiseng StIR process
tcuesesul attic lank with methanol feed
efl tte i tfi l tia lien -
- omer . - i, , -p
CAPITAL COST: EquIpment as Structures (from Page 2). 32.650.000
Electrical and InstrumentatIon. 12% 5319.000
Yard Plplng aid SIte Worti. 15% $390,000
Subtotat 53 .310.000
Contractor 011SF 15% 5506,000
Engmeeilng end Cena t r. Mgmt 15% 3500.000
Sittotal $4300000
Cenlingency. 30% $t.Ott 000
Total Capital Coal 55,350,000
Capital Cost per lb 20-Yt N removal $4.61
OPERATIONS COST: Additional Horsepower (from Page 2) 100 HP
Electrical Power Cost. 0.05 SAW $32,700 5/year
Nitrate Reduction using Methanol 4.0 mg /I
Methqnol Required. 70 gatani
MevtatdCost 0753/gal 51 9 300$ / year
Separate Stage Ammonia Reduction 00 mg/I. -
CaustioSodeO2 f l%ccnC Ogets/d
- Caustic Soda Cost 0.60 S/gal SOS/year
[ qiapment Maintenance Coat $43800 S/year
Dettilcetlen Sludge Production w/Metltaiol 230 meld
Sludge Oleposal CoaL 400 S/tn 515,000 siyear
Total Annual O&M Cost $112500 S/ year
Effective Annual Internal Rate alter inflatIon 2.91%
20Yea Present Worth of OW Costs $1 90.000
TOTAL 20-YEAR PRESENT WORTh COST: 5 7 . 0 8 0. 000
T Cost ear lb 20-Yr N removal $6.06
Leesbuig VA ala Page I of 2
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PROJECT: Implementhtg a3 mgll,Mnual Average Total NItiege li UntIl —
PREPARED FOR: USEPA, Chesapeake Bay 0 611c c
PREPARED BY: Virginia Tacit with Stea a & Wittier. LLC
DATE; March 16, 2001
FACILITY. ILL Moorw V TP
LOCATION: Prince W IllIam CbtauIv. VA
RATED FLOW: Ito m PE COD: ITS mg / I.
CURRENT EFFLUENT TN. ,ftj,,niglL PE TKN. 26 rng/L
EFFLUENT TN GOAL: 30 mg/I.
NITROGEN REDUCTION: 750 (bald
274 1000 lbs/yr
5475 1000 Ibal2O.yeara
CURRENT PROCESS (CHECK ALL THAT APPlY): MLE EidatlngAera led Volume (MG)
— BEPR (A2 V IP tic) Exiting Anoxic Volume (MG) 078
— Bardenpho Current MISS at W uet ADF 2700
— Oxidalion Ditch
Lagoon (Biolac. etc I
Cyclical Aeration
SOR
: HIg/ Rale Sc ORer
— ! Effluent Filtration
X Othec Slip Feed MLE, no nitrate rec ,de
URRENT EFFLUENT AMMONIA -N; 0.5 molt From Report
From Model(atADF and load. t5 dMCRT. it Cwintewidiborts)
PROPOSED MODIFICATIONS TO GET AMMONIA c 0 mglL
S No modleatlona mqilred New MLSS
I RaE. MCRTIMLSS In eiSng tanks (cheth clarfier capacity) ______
1 onabuctadddkSaemSSume FIOW(ITfl :
-. Construct additional ch a Sers Flow (mgd). .
-. Use Sating artoc Volume as aerobic (construct separate dent facility)
Use aerated ayatem for 800 removal only (construct separate nit/den/I facility)
Md kiSuent Ilow equaliz$en tank
WDther I
PROPOSED MODIFICATIONS TO GET NITRATE <10 mg/I.:
No modilloatlona required
Add downstream Della Mar safti nthanol
Add downstream NiolIcatlon Sidfiltar and DeNit filter with methanol
Add methanol 10 exiatitig BIER prooeas
Add downaleam anoxic lank walt memanc Iced
• Add etlkient Avarice
OI ier MSv edulue deep bed eltluetfllters to dflefln
CAPITAL COST: Equipment and Structwee (from Page 2) 81.870.000
Elacrical and kietnanentalion. 12W $224,000
Yard PIping end SIte Woitt. 15% $201,000
Subtotal: $2,360 ,000
Contractor OHAP 15% $357,000
Engineering and Consir. Mgmt 15% $357,000
Subtotal $3,090,000
Contmgenqir 30%- 8714.000
total Capital Cost $3800000
Cepital Coat perth 20.Yr II removal: $0.69
OPERATIONS COST: Addibonal Horsepower (from Page 2) 0 tIP
Electrlcel Power Coat 0.05 81kW $0 8/year
Nitrate ReductIon using Methanol. 6.0 mg/I.
Methanol RequIred 340 gaw
Methanol Coil 075 S/gal $93,100 S/year
Sepertee Stage Ammonia Reductroff 00 mg/I.
Caustic Soda 025% wt 0 o a leld
Caustic Soda Cost 000 S/gal $0 8/year
Ecuipment Manlenanca Coal 530.900 S/year
Denilnflcat.on Sludge Product/on wftdelhanol 1080 lbs/d
Sludge Disposal Cost 400 S/Ion 570.000 S/year
Total Annual OW Cost 5202,000 5/year
Effective Annual Interest Rate afte l Inflation 291%
20.Year present Worth of O W Coats $3,040,000
TOTAL 20-YEAR PRESENT WORTH COST. $M*000
Total Cost pert 20-Yr N removal $1.25
Prince William Cty ida Page 1 or 2
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PROJECT: ImplemeMlnga3 mgiL Annual Anrsge Total Nltrogen LImIt
PREPARED FOR USEPA. Cliesapestie Day OffIce
PREPARED BY VirgInIa Tech wIth Stearns I Whaler, LLC
DATE: March 11,2001
FACILITY Harrisonburi WWTP
LOCATION. iI i ortum, VA
RATED FLOW: 100 mgd PC COO 340 mgill.
CURRENT EFFLUENT TN: 60 mgIL PE TKN 34 m 4.
EFFLUENT TN GOAL. 30 ingll.
NITROGEN REDUCTION: 400 lb5Id
146 1000 lbs /yr
2920 1000 lba/20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): t ALE Exusiltig Aerated Volume (MG) PIta
A BEPR (AltO. VIP, etc.) Exusing Anoxic Volume p,tG) N/a
— Bard e tipl iD Ctvrent MLSS at WInWADF. 3800
— Oxidabon DItch
— Lagoon (Biolac, etc.)
— Cyclical Aeration
SBR
— High-Rate Bioflier
A Elfuerd Filtistiol
om -
CURRENTEFFLUENTAMMONIA.N: 0.5 mgiL K ’ From Repoit
Rem Model (at ADF end load. 150 MCRT. 1 ? C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mgII-:
JNo modrications required New lASS
!JRalse MCRTIMLSS In existing tanks (check darifia capacity) N/a
JConstruct additional aerated volume Flow (41190) 0
JConslmct additional clardlers Flow (rngd) 0
Juse existing music votiatle ae aerobic (construct separate Stilt faclity)
,Jtise metaled system for BOO removal only (constrict separate ndMen’t facitty)
IIlAdd In lluent flow equalizattn tank
JOiiiec -
PROPOSED MODIFICA11ONS TO GET NITRATE ‘1.0 mgiL.
, ,.utScadora required
Note: ExistIng Elf Alters only 30 deep, - Mddoiwtslrealrt DeNK SItar with methanol
Replace with denite fitters donnebuam Mittitcebon Blolitiar end DeNut SlIer with methanol
Add methanol S Setkig8NR process
Add d aeam snoido Sit tdth methanol feed
s Addelfluantl&oWI
05*— ‘ ‘ ;r” t.V- ’ - “
CAPITAL COST: Eqtnpnient and Stnflutes (hem Page 2)’ 56. 550.000
Getsical and Insfiumentfltlon 12% 5180.000
Yard PIpIng and $5 f4fl. 15% 5663.000
Subtotar 58.320.000
ContivctorOH$P. 15% $1.245.000
Engineenng and Consv MgniI 15% 51.248.000
Sjbtotal ’ 310.120 DCC
Conwigency 30% 12.496,000
Total Capital Cost 1 13,320.000
Capital Cost per lb 20-Yr N reniovel 54_ I l
OPERATIONS COST: Additional Horsepower (from Page 2) 320 HP
Eleancat Power Coat 005 SAW 5104 600 $1 cear
Nitiale Reduxbon using Methanol LII mfl
Methanol Required 150 gatsM
Methanol Cost 015 5 al 145.300 Styear
Sepatate Stage Ammonia Redudion. 0.0 mglL
Caustic Sods @25% conc 0 gels/d
Cau Soda Cost 0.80 Smel $0 5/year
Equipment Maintenance Cost 1106.200 S/year
Denllitflcatlcn Sludge Produnlon wLlethanol. 510 Weld
$1 140. Disposal Cost 400 Shun 142.300 Slbear
Total AntICS O8MCost 1304.400 $IflaV
Eftective Annual interest Rate eAs t titaluorr 2 0 1%
20-Yew Present Woith of OSM Cost $4,570,000
TOTAL 20-YEAR PRESENT WORTH COST: $11,010,000
Total Cost per lb 20-Yr N removat 16.13
Hairisonbvrg VA xis Page 1 of 2
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?ROJECT: Implementing a 3mgit. Adnial Avenge Tota l Nitrogen LMØ
PREPARED FOR: USEPA. Chesapeake Bay diflee
PREPARED BY: Vbitnla Tech with Stearns & WhJ.. , LLC
DATE: March 9,2001
FCILITY: Front Royal
LOCATION: Finns a wi. VA
RATED FLOW: 40 mgi PE COO: 206 mgit.
CURRENT EFFLUENT TN: •16 mgiL PE TICH: 21 mglL
EFFLUENT TN GOAL’ 3.0 mg1L
NITROGEN REDUCTION: 110 theM
62 1000 lbs4r
1241 1000 Ibe!20jears
C%MRENT PROCESS (CHECK ALL THAT APPLY): MLE Existing Mrsted Volume (MG): 1J25
BEPR (A2C. W. sic) Existing Moxlc Volume (MO)
Saiden p iio Cuneni ItSS at Winter ADF. We
Oxidation 0
Lagoon (Odac. etc.) tide: Existing plant has 4 aeratIon tanks,
! 4dlcaI Motion Jan1996 report oconiniend 2 addItional
SER lankaOa2 b omgeach
9 dar
Enluetti Filtration
Other ‘
CURRENT EFFLUENT AMMONIA4I: 05 mgi. X From Report
FromModel(atAOFand load, 1SdMCRT. 12’ Cnlntarcondldons)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1.0 mgi.:
flN. modliS — New PtSS
:JRalee MCRVI&SS in Sating tanks (check olarifier capacity) ‘ N M ’
jjConetmdsd l*,.Jaetatad volume Flow (mgd)’ 0 ’
T] o ,atnaSflnSct men flow (mgd): 0
]Uee viflt, o CkNne as aerobic (conatiuct separate denht facilIty)
JJtise aerated s atem BOO removal only (conalnn separate nit ldenlt facility)
IIlAdd inRietti 6Weq tn tank
iJOmer “
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mglL:
No modifications veq,áS
Add ean DeNt WW*Ith methanol
• Add downeflam NtS.tm SleNler and DeNt S l Ier with methanol
- ‘ MdmeUisd b&xisUIig BNR process
Add &.,..S.. . a lait with methanol feed
“ Add elIlueuiSon
othec , aAV t ’
CAPITAL COST ’ Equipment and Siruoturee (from Page 2) 12,350,000
Electrical and Instumentation: 12% 5202.000
Yard P ipingandSite Wart 15%. $353000
- Subtotal: $2190000
Contractor OH&P: 15% $449000
Engineering and Conet. Mgntt. 15% $449,000
SubtotaL’ 1 3 890.000
Contingency - 30% 5697,000
Total Capital Cost. $4,760,000.
Capital Cost pert 20-Yr. N lament $3.06
NOTE A Ma need toinwlenlent re.a. ..anandad tw4ovements (or BNR at desIgn Sow found in the Jan 1996 retion
Coat (2 Addi aeration basin, SE PEflowdistilbuton)
OPERATIONS COST: Additional Horsepower (f 00 Page 2 00 lIP
Electitcal Power Cast 0.05 $&W $26,100 llyear
Nitrate Redection using Methanol. 6.0 malL
Methanol Roquked: 60 galeld
Methanol Cost’ 075 $ al 121,900 $l ear
Separate Stage Ammonia RedudIoft 0.0 mgi.
Caustic SodaS 25% cons. 0 gstsld
CaiatlcSodaCost 060$fgaI $0$4ear
Equfluent MaIntenance Cost $36900 $?yeer
Derillitficatlon Sludge Production wlMeltanot 240 theM
Sludge Disposal Cost’ 400 Vtett $17.500 $ ‘ear
Tow Annual 061.1 Coal’ $104,400 $4ceer
EffectIve Annual Interest Rate alter InflatIon’ 291%
20-Year Present Worth of O&M Costa $1,570,000
TOTAL 20-YEAR PRESENT WORTH COST. $6,360,000
Total Cost perm 20 -Yr N removal’ $512
Fmnlfloyat$ ala Page 1 012
-------
#ROJECT: tmpienwntthj .3 mg I. Mnuat AVerage tcb l NWvgsn Lhntt
PREPARED FOR IJSEPA, Chesapeake Bay 0 17 1c c
PREPARED BY: Virginia Tech with Stunts £ Whets ? LLC
DATE: March 13 2001
FAC IUTY: . FShere tIIe WWIP
LOCATION. Aucusta County. VA
RATED FLOW: 20 mgd - PE COft M Is rng/L
CURRENT EFFLUENT TN iCmgil. PE TKN. M I s rnglL
EFFLUENT Th GOAL: 30 nig lL
NITROGEN REDUCTION: 70 Ibe ld
25 l000ItsIyv
511 1000 Ibs/20-Içsai5
CURRENT PROCESS (CHECK ALL THAT APPLY): X MLE ExistIng Aerated Volume (MG), — H is
X BEPR (flIP VIP. etc.) Existing Most Volume (MG) N /a
— Rardenpilo Curta Il MLSS at winier ADF 3000
— Oxidation Ditch
— Lagoon (Riolac etc p
— Cyclical Aeration
SBR
— )tgn-Rete BoNier
— EIiIuertt.FlltratiOfl
X Other Can be operated as either M V or a E
CURRENT EFFLUENT AMMONIA-N: c I.O rn mg/L [ flFrcm Report
DFrvm Model (atAUF and bad. 15 d MCRT. it C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA ‘C 1.0 mgIU
‘ jNo modificatIons roqidied New MLSS
RaIse MCRTIMLSS In ettig tanks (check ciariler capacity) ______
Consaactaddt l tona lael sdvokJme Fbw(ungd). n lfl
. Conideddion&.t&lIn . FIOw(ni9d) Ttt \t1
• - Use eidatq enwdciiohmieas aerobic (construct separate dentt tasty)
Use waled syetwn tsr 000 removal only (construct separate nitidenut tacitly)
InftuentlIowequaI n tank
OVIer - P • - .4.
PROPOSED MODIFICATIONS TO GET NITRATE <1.0 mglL:
No modilcationa reqiirel
X downstream Oct11 Alter a4Ih methanol
downstream Nifl lcabon Olofittar end DeN 1t MIst with methanol
methanol to SatIng StIR process
downstream anoidebotwWl methanol teed
Md effluent Il ltretion
Other _______________________________
CAPITAL COST: Equipment and Structur es (from Page 2) 51 .550.000
Electncsl and Inatrunientation 12% 1190.000
YerdPtpingand llte Work. ib% 5240.000
Subtotal 12.100.000
Contractor 011W. 15% 5315.000
Enginewing aid Cons Mgmt 15% 5315.000
Subtotal.
Catbngencr . 30% 1530.000
Total Ceflel Cot 53380.000
Cepital Cost per lb. 20-Yr. N removt $8.55
OPERATIONS COST: Additional Horsepower (train Page 2) 40 HP
Electrical PowerCost 005 1 /kW $t3.l0O$ raer
Nfle Reduction using Methanol’ - . 4 0 ingfl.
Methanol Required. SOgaIWd
Methanol Coat 075 $i at 55.200 1/year
Separate Siege Ammonia Reduction. — 0.0 mglt.
Caustic Soda 25% car lo 0 gslsld
Caustic Soda Cost 0 an 5/gal 10 5/year
Equipment Maintanana Cost 537300 5/year
Denirn f lcadon Sludge Production w iMelhanel 100 lbs/a
Sludge Disposal CosI 100 S/inn IT.300 3 /year
Total Annual OW Cost 555.000 1/year
Eltective Asviual Interest Rate alter In aation 291%
20. Year Present Worth of OW Costs 1840.000
TOTAL 20.YEAR PRESENT WORTH COST 14.200.000
Total Coat per lb 20-Yr N removal $5.22
FIst,ersvdle. VA ala Page 1012
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PROJECT: ImplementIng a S inglL Amiual Average Total Nirogen LImit
PREPARED FOR ’ USEPA. Chesapeake Say Office
PREPARED BY: Virginia Tech with Steams & Whaler. LLC
DATE: March 25 2001
FACILITY: Ilenctco County WWTP
LOCATION: Flenitco County. VA
RATED FLOW: 40.0 rngd PE CO mg/I.
CURRENT EFFLUENT TN: 6.0 rng/L PE TKN ing l l
EFFLUENT TN GOAL: 30 mglL
NITROGEN REDUCTION: 1000 Iba
355 l000ibslyr
7300 1000 Ibs/20-years -
Existing Aerated Volume (MG) ______
Ernstmg Anoxto Volume (MGI.______
Cur rent MISS a Anter ADF._______
PALE
BEPR $2/0. VIP. etc.)
Oaitenpho
Oxidation Odd ’
Lagoon (Buolac. etc.)
Cydicat Aeration
SOR
High-Rate Bditer
Eltk,entFdtrabOn
Other Two systems. a modif ad UCI & a modified pure Oc gen
;URRENTEFFILfENTAMMONIA N: c i 0 mgIL FrOn1 Report
FromModel(SIADF andloed. ISi S MCRT. i ?Cwlnler conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 1.0 mg/I.
X Nornoditicatuons requ ired New MLSS
Ratee MCRTIMLSS Ni eidsting tanks (check clarifier capac ity) l i la
Coifluct addilloiwl lad volume Flow (mgd} ‘ .0
Coistud ddlIlnlJslSNS Flow (mgd)’ - Th
use eitebng anoatcvolusneas aerobic (construct separate denit faclity)
Use aerated ey*un for BOO removal only (construct separate nlt /denit fadhum
Add Influent flow equalbadod tank -
Other •- IS” . : ‘ -‘ : -
PROPOSED MOOIFICA11ONS TO GET NITRATE C 1.0 mgfl.
No modifications isqubid
Add downstream DeNit filter wil l niethaS
Add downstream Nitaflon B IOI8S end DoNut lifter with methanol
- Add medwiol to esSIllig StIR process
Add downsfte.m eneidc lett wIth methanol feed
Add
Otlwr •nie.e ol St II ri’ioSenitr ’ncatbn with methanol addSofl
CAPITAL COST:
Equtpment and Structures (1mm Page 2Y
Electrical and Instrwnentelion 12%
15%
12.000.000
*240.000
1300.000
Yard Piping and Site Wa lK
Subtotal
15%
$2.540.000
$38i.000
contractor OPtS ?
15%
*381.000
Engmeenng and Constr Mgmt
su b total
$3 300.000
1162.000
ContIngency 30%
Total Capital Cost
CapItal Cost per lb 20-Yr H removal.
14 .090.000
$0.56
OPERATIONS COST:
Additi onal Housepower ifrom Page 2) 0 HP
ElearIcel Power Cost. 8.0$ 1 1kW 90 1/year
Nitrate Reduction using Methanol. 3.0 .mgIL
Methwol RequIred 460 gstsld
Methanol Cost , 0.75 1/gal 1125.900 S / year
Separate Siege Ammonia Redudloit 00. m g / k
Caustic Sod. © 25% conc. 0 gatsnt
Caustic Soda Cost 0.60 1/gal 10$/year
Equipment Maintenance Cost. 133 000 1/year
OenlInlIcallOn Sludge Productuon SMetrianol 1440 Ibsfd
Sludge Disposal Cost. 400 Mon 1105.100 1/year
Total Annual O&M Cost- . $264000 1/year
Effective Annual Interest Rate alter Inflation 2.91%
20-Year Present Worth of OSM Costs 13 S60.000
TOTAL 20-YEAR PRESENT WORTh COST:
Total Cost per lb 20-Yr N removal
•60 °
$1.10
CURRENT PROCESS (CHECK ALt.. THAT APPLY):
x
A
Henraco County VA xis
Page 1 of 2
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r’ROaCTY Implsmsntclg a 3 m g I. Annual Awtgs NW Nitrogen Um i t —
PREPARED FOR: USEPA. Chesapeake Bay OffIce
)REPARED BY: VIrgInia Tech with Steam . & WhsIfl. LLC
DATE:. March 20,2001
LOCATION: _ _
RATED FLOW: 50.0 mgo PE COD ______mglL
CURRENT EFFLUENT TN: p,mat PE 11(11 _______mglL
EFFLUENT TN GOAL: 30 mglL
NITROGEN REDUCTION: 1250 bald
458 1000 lbs /yr
9125 1000 Ibs/20 jeers
CURRENT PROCESS (CHECK ALL THAT APPLY): MLE ES5t419 Aerated Voliafle ( 1401 .
BEPR 1A240. VIP SIC) Existing Anoxic Volume (MG ) _______
BwdenonO Currant MLSS ci Winier Alit ________
Qxidalioii 0th
Lagoon (BdaC 510.1
Cicliost Anton
SBR
High-Rate BIoltsr
— Effluent Fillialion
X Other second oe dentrdlcalion will ’ methanol sMIlon
CURRENT EFFLUENT AMMONIA-ft c i 0 regiL From Repoll
Fran Model (stAOF end bad. 15 d MCRT. 12’ C winIer conditions)
PROPOSED MODIFICATIONS TO GET AMMOPIA ci i mglL:
[ TINe noJi . ” refled New MLSS
Rates MCRTaSSm edstlng tanks (diSc claiffler capacity) His
- ‘ Constiuct aosnratsd votilme Flow (mgd) 0
COASINOI aidariflsrs Flow (mgd) 0 ’
• Use siitsfl sliolseSUtn e 53 aerObiC (oonstiUcl separate i teM tacility)
- Use eersted systw 1 tsr 800 rsniovaf only (construct separate nltidenit fetiDly)
- Add influsis sew sqiiatlwl)On isnk
Othsr
PROPOSED MODIFICATIONS TO GET NIT*ATE c 1.0 mgI.:
N i meditations —
dowIlsbal% Detsit mIst with methanol
Add downstream pItsIfteatlOn Biofilter and DeNit l Itter with methanol
X Add mesaS te msefl BNR process
Add downslssm anodc tank with methanol feed
X Add emusntNti.WJl
Oth
CAPITAL COST: Equip ment and Slructsxes (tion l Page 2): 520.950.000
Etectrtcal and ICstrumetsbon 12% 53.514.000
Yes Piping end Sits Work - 16% 55,143,000
Sub t a laL *26.810.090
Cortacor OKSP 15% 55,992,000
Enginsenn gS ldCeI I CLM gta 15% *3 .992.000
Sub t etsI: 534.590.000
Contlngency 30% 37,993,000
TotsI Capital Coat. 542570,000
Capital Coat pat 20-Yr. N renlovt $4.67
OPERATIONS COST: Additional Horsepoeer (from Pegs 2)
Etecinlesi Pawa Cost 005 5 1 1W *103.400 Slyest
NS Redudmon ning Methsnot tO mg I .
MeltS Rsqutred 570 galsld
Methanol Coat 075 VgS 5154.000 Slyest
Sepsmte Stage Ammonia Reduction 00 mnojL
CaushcSodaO ZS%C0flC. 0 giSt
CauiCc Soda Cost 050 StgN SO Slyest
EquipmsntPalntenancs Coal 5345.900 Slysar
Denitslttalson Sludge Production wiMethanol ‘900 Weld
Sludge Oiaposel Cost 400 $151 1131.400 Slysar
Total Annual 08 1 4 Cost 5796.700 Slyest
Etfscbve Annual Werest Rals after 291%
7 0 -Year present Worth of 0514 C05W 51 1. 950000
TOTAL 20-YEAR PRESENT WORTH COST: 5S4 52O,OOO
Total Cost per lb 20-Yr N rentoval. - $5.67
Ilopowell Regional. VA id e Page 1 of 2
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PROJECT: implementIng a3 mglt. Annual Avenge Total N itrogen Limit -r
PREPARCO FOR: 1JSEPA. Chesapeake flay Office
PREPARED BY. Virginia Tech with Steerns & Whaler. LLC
DATE: March 25 2001
FACILITY: Richmond WWTP
LOCATION: Rlch .Crit VA
RATED FLOW 50.0 mgd PE COO ______rng!L
CURRENT EFFLUENT TN: 15.0 mg& PE TKEI _______mglL
EFFLUENT TN GOAL- 30 mg /I.
NITROGEN REDUCTION: 5420 ibaId
1970 1000JbS/ r
39566 1000 tbs/20-years
CURRENT PROCESS (CHECK ALL THAT APPLY): MLE Eirbling Aerated Volume (MG) _______
— BEPA (Afl VIP, ate) ExIstIng Anoxic Volume (MG) ’_______
fleØenpho Current MLS$ at Winter ADF- ________
- — Oxidation Ditch
— Lagoon (Biolac. oft)
— CyolicalAeraiion
SBR
— High-Rate Biotilter
— Effluent Filtration
x Other Conventional Activated Slialee
CURRENT EFFLUENT AMMONIA-N- 05 mg/I X From Repe l
From Model (al ADF and tad. t5 d MCRT 12’ C wetter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA ’ i.Oing&:
X No mod’ricatnns required New MLSS
Raise MCRTNLSS in existing tanks (check danfier capacity) His
: c s a aerated volume Flow (mgd). 0
— Construct additional clanflets Flow (mgd) 0 -
l isa exIsIJ’tg amotoc voliatie as aertiac (construct separate daM facility)
Use aerated syitem for BOO removal onfy (construct separate nWdenlt Ieclhty)
#. Add Inlluent row equalization tant
: Other - . • ‘ ; ) ny: •g ’ - .
PROPOSED MODIFICATIONS TO GET NITRATE ‘1.0 mglL:
No htodrflcatlOrts required
X Add downstream DeNt filter with methanol
Add downstream Nititfication Bio S Iter and DeNit filter with methanol
Add mnegianol ta existing BNR process
Add downsveamfl anoitic tent with methanol teed
Add eflIuentfhImIion
X Other. t.bdlfybMtEOirefatlcn
CAPITAL COST. Equipment and 5lpjcftire$ (from Page 2) 122.740.000
Electrical and Instrumentation 12% 12.729.000
YardPipingandS/IeWOmk t5% 53.4)1000
Subtplat us eso.ooo
coattaclor 0KW 15% 54332 000
Enguneenng and ConsV Mgrnt iS% 54.332.000
Subtotal 137.540.000
Contingency 30% 18664.000
Total Capital test ‘ 14 5.2*000
Capital Cost pert. 20-Yr. N removal. $1.17
OPERATIONS COST: Additional Horsepower (from Page 2) 1.000 HP
Electrical Power Coot 0.05 SAW 5326.700 Iiyear
Nitrate Reduction using MethanoL 13.0 mg/ I
Methanol Req uired 2470 gals/d
Methanol Cost 075 ligaI 1676.200 I/year
separate Stage Aninionia ReduCtioi 0.0 mg/ I
Caustic Soda C 25% cons 0 gats/d
- Caustic Soda Coat 0.60 SIgal $0 S /year
Equipment Maintenance Cost 1375.400 S/year
Oenttrtflcation Sludge Production w1( tthanoI’ FUtO 05/4
Sludge Disposal Cost. 400 Mon 1570.100 5/year
Total Annual 0814 Cost 11.948.400 1/year
Elfectlve Annual Werest Rate after Inflation 291%
20-Year Present Worth o 0314 Costs $29220000
TOTAL 20-YEAR PRESENT WORTH COST:
TotalCostert 20-Yr Nreniavat $1.11
Richmond VAxis . Page tof2
-------
SUMMARY COST SHEETS FOR THE 7
JAMES RIVER, VIRGINIA WWTPS
12
-------
?ROJECT: ImplementIng ji rngiL Mnual Amiage Total Nftrogen UmIt -x
PREPARED FOR; USEPA Chesapeake Bay Office
PREPARED BY: Virginia Tech with Steams & Whaler. LLC
DATE: March 19.2001
FACIUTY odstockVVWTP —
LOCATION: V odstodLVA
RATED FLOW ’ 1.0 mgd P S COD $06 mglL
CURRENT EFFLUENT TN. IOmg/L PS TKN 20 mg /I.
EFFLUENT TN GOAL- 30 mg/I
MITROGEN REDUCTION 40 lbsJd
15 t000ibs/yr
292 1000 lbs/20-ysars
LIR RENT PROCESS (CHECK ALL THAT APPLY): MLE Existing Aerated Volume (MG) 1 3
- — BEPR (A2i0. VIP. at) Existing Anoxc Volume (MG) His
— Bardcnpho Current MLSS at Winter ADF 3200
X OxidatIon Ditch
Lagoon (Blolac. etc.) Note. Oxidation Ditches operate Cycli liy
Cyclical Aeration
SBR
Itgh-Rate8iolilter
.‘ ‘ Effluent F ltrallon
- Other r’ Pr: .-.r
CURRENT EFFLUENT AMMONiA-N: 05 mgit. X flcni Repoit
- Froni Model(etADFandload. 15 d MCRT. 12°Cwlnlerconditions)
PROPOSED MODIFICATIONS TO GET AMMONiA c I A mglL:
[ *]No rnodlflcal)onl reqiererl . New MLSS
“ Rae MCRTIMLSS In Sating tanks (check denSer capadty) NFa _
Ccnainact add Itlontit eerated volume Flow (mgd) X IX .
COnstnfl additional clarifies Flow (mgd) 0
Use Sating anoidc volume as aerobic (ccnatnfl separate dead faolity)
Use aeratea system for ROD removal only (constiuct separate nltJdenul facility)
Add rifluenl flow equalization tank
Othot. _______________
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mqS
E IN0 modiltflis —
X Add deanalream DeMt litter with methanol
Add dcwnslieern (Iltilficetion BlaMer end DeNut Mar with methanot
-‘Md methanol te eidelkig BNR ptvoesa
Add downstream artS tat Wth mtariol teed
Add effiueidttion
- ‘ ‘ tr t ; 777
CAPITAL COST: Equipment and SVv sies (hum Page 2): 51,300,000
Electrlcs lendInatnjmentatlon’ 12% 1158000
15% 1105.000
Subieta t ‘ 51650,000
Contractor O f - ISP’ 15% 1248000
EngineerIng and Canatr Mgmt 15% $246,000
Subtotal . fl ISO 000
Contingency . 30% 5495.000
Total CapItal Cost *2.650,000
Capital Cost perth 20-Yr N removal $9.08
OPERATIONS COST- Addutionai Horsepower (from Page 2) 20 HP
Electrical Power Coat 0.05 *4kW $6 500 S/ye W
Nitrate Reduction using Methanol tO mgit.
Methanol Required 20 plaId
Methanol Cost. 015 S/gal 55500 S/year
Separate Stage Ammonia Reduction OJ mg /I.
Caustic Soda 025% oonc. 0 gala/ti
Caustic Soda Cost’ 060 S/gal $0 Mear
Equçvnent Maintenance Cost $21,500 5/year
Denhirli/caton Sludge Production witeethanol 50 IteM
SISge Diapolal Cost. 400 Mo lt $4A00 S/year
Total Anniati 051.4 Cost $31,900 5 / year
Effective Annral kiteresi Rate after Inflaboar 2.91%
20 -Year Present Worth olO$M Costa $5 10,000
TOTAL 20-YEAR PRESENT WORTH COST: $3,220,000
Total Cost per lb 20.Yr N removal’ ‘ $11.03
Woodatock VA ii i S Page iot2
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PROJECT: Impleme n tIng .3 ing/L Annual Average Total NlUvgen UntIl
PREPARED FOR. USEPA. Chesepefle eay Office
PREPARED BY: VIrgInts Tech wIth Steanis 8 Whaler, LLC
DATE: March 19,2001
FACIUTY : WIldqrne jSWWTP
LOCATION: Rudceiiv le.VA
o aow l omgd PE COD 435 mg/i
CURRENT EFFLUENT TN 80mg /I PE TKN. 25 mg/I.
EFFLUENT TN GOAL: 3.0 mg /I
NITROGEN REDUCTION: 40 Ibsld
IS t000Ibs/w
292 1000 Ibs/20-ners
CURRENT PROCESS (CHECK ALL THAT APPLY). MLE ExistIng Aerated Volume (MG) His
— BEPR (A210. VIP. at) Existing Anoxic Volume (MG) NM
— Baiderpho Currenl MISS at Winier ADF N /a
A OxIdation OiIth. 4 Ring Qrbal
— Lagoon (Bidet. otc
— Cydical Aeraluon
SER
— High-Rate Biofilter
Effluent Fillratuon
Oilier ___________________________________________
CURRENT EFFLUENT AMMONIA-N: 05 mgII X Ruin Repoit
rem Model (at ADE and load, 15 d MCRT. 12’ C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA 1.0 mg/ I:
No modlScallons required New MISS
Rules MCRTIMLSS Ineidetng tanks (thud’ clanflrcapac4y) Ni t
“ Ccratnt ed4lbajtal aerated volume Flaw (mgd}: 0 / “
Q ifl t $efl Flow (toga) , 0.W ’
Lies Sating avedo e nm ae aerobic (constiud eeparate denthodity)
• Uae eetahJ syStem I Cr MOD removal only (construct separate nd/den/I fadliM
Add Influant Sew ec 1 ueluzalionfl
Other . C’ ’ .. 1
PROPOSED MODIFICATiONS TO GET NITRATE <1.0 mg/1
No modifIcatIons requked
Add downstream DeNS filter with methanol
Add downstream Nhtriflcaluon Buotller and DeNul rifler with methanol
Add medienel is existing BNR proteus
Add doatisbeam ruozc tunic with methanol feed
Add e e iuent flIbaUon
Other ____________
CAPITAL COST; Equipment and Structures ((torn Page 2) 1250.000
ElectrIcal and lnatruine/utabon. 12% $30000
- Yard Piping and Site Wait 15% 338.000
&ibtotat 1320.000
ConflolorOH8P 16% 148000
Engineering aid ccnstr. Mgml 15% 148.000
Subtotal: $420,000
Contingency 30% 598.000
Total Capital Coat 5520.000
Capital Coal per lb. 20-Yr. N removaL $1.75
OPERATIONS COST. AddItional Horsepower (from Page 2): 0 HP
EleS c aIP rCoat 00$ $/kW S olkear
Nitrate Redicoul using Metitanot 5.0 mg/I.
Methanol Required 20 gals/c
Methanol Cost 0.75 S/gal 35.500 3/year
Separate SlageAmmon le Reduction 0.0 mg/i
Ceusllc Soda 25% cant 0 gelsid
Ceusluc Soda Coal . 050 3/gal $0 S/year
Equipniem Maintenance Coat $4200 s/year
Demtrulcatuon Sludge ProductIon w/Methanol 50 lbs/c
Sludge DIsposal Cost 400 S/ton 34.400 5/bUt
Total An ualO&M Cost sii.ioo 3/year
Effective Annual Interest Rate after Infisluon 291%
20-Yeas Present Worth of O W Costs 1210.000
rOYAL 20-YEAR PRESENT WORTH COST: eno.eoe
Total Cost per lb 20-Yr. N removat $2.50
Wilderness wwrp sic Page 1 of 2
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PROJECT: ImplementIng a3 mgiL Annual Average Total Nitrogen Limit
PREPARED FOR USEPA, Chesapeake Bay Otilce
PREPARED BY: Virginia Tech with Stearns & Whelsr SC
DAtE: Mirth 19, 2001.
rACiun’ • Waynasboro City WWTP
LOCATION: Weynesboto, VA
RATED FLOW: 40 mgd PE COD - - 270 mgIl.
CURRENT EFFLUENT TN’ 60 mg/I. PE TKN 20 mg/I.
EFFLUENT TN GOAL: S OmgIL
NITROGEN REDUCTiON. 170 PbWd
62 1000 ibsfr
1241 1000 Ibst2D years
CURRENT PROCESS (CHECK ALL THAT APPLY): : t i tLE Aersted Volume (MG) 1 -Va
— BEPR (A24 VIP, eta) Existing Anoxic Volume (MG) N b
— Bardenoho Cwreni MLSS at WInter ADF. N I n
— Oxidation OiSi
— Lagoon (Okilac, at)
— CydlcalAe ,alion
SOR
— High-Rate BoNier
— Effluent Fitation
- X Ottiec 1*ltflFltwRBCs, Denite Filters
UPRENT EFFLUENT AMMONIA-N: OS mg/I. X From Report
From Model (at ACF and load, 15 d MCRT, 12’ C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA c 10 mg/I.:
X Non’iodl*cat.ons requited New MLSS
Raise MCRT$itLSS in existing tanks (check defi ler capacity) N/a
Cernuct addlbmal aerated volume FIo (mgd) 0
Constnd adetbenal dariflera Flow (mgd). 0
Use emaing mat ane as aerobic (construct separate denit facility)
Use aerated syste m trSOD removal only (construct seporate nit/dooR facility)
- Add influent Sow aq”nalon tank
Othec _________
PROPOSED MODIFICATIONS TO GET NITRATE ‘ C 1.0 mglL:
N0 niodlfloatlam required
Add downsveam DeNti filter SIti rnetianol
-. And down$Iitam NsóaUcn Bioffiter and DeNII 2cr with methanol
Add metha id i es log BNR procesa
• din, .& & , . S cseI&w4UI mettwiol feed
Add elltue ittaV n
oUte r MdlatiilMethsncl r •. ‘•‘ - - t
CAPITAL COST: Equipment and Struc&ree (from Page a so
Electrical and Instnimentation 12% 30
Yard Piping and Site Work. 15% $0
Subtolat 50
Contractor 01-ftP 15% 50
EngIneering end COIIatI Mgmt. 15% $0 -
Sutilolal $0
Contingency 30% $0
Total Capital Cost $0
Capital Cost perlb 20-Yr Nremoval - $000
OPERATIONS COST: Additit nil Horsepower (from Page 2) 0 HP
Electrical Power Cosi 005 5 1kW $03/year
Nitrate Redudion using Methanol 30 mg/I.
Methanol Reqt*ed- 00 gala/d
Methanol Cost - 075 S/gal 521.900 3/year
Sepnste Stage Ammonia Reductiomr 0 .0 mg/I.
CaustIc Soda @25% pc, 0 gala/d
Caustic Soda Coat 060 S/gal $0 5 /year
Equipment Matntenanos Coal. $0 V ear
Denitrlllcation Sludge Proluclion w lMethanal 240 Ibsbd
Sludge Disposal Cost 400 S /tn 517.300 3 / year
Total Annual 0514 Coat. $39400 3/year
Effective Annual Interest Rate attez b*Sen. 291%
20-Year Present Worth 010W Costs. $590,000
TOTAL 20-YEAR PRESENT WORTH COST: $590,000
Total Cost per lb. 20-Yr N removal. $040
Waynesboro xIs Page lot2
-------
tROJECT: - . - ImplementIng a3 mgII. Annual Avenge Total Nitrogen LISt
PREPARED FOR USEPA, Chnapnke Bay Office
PREPARED BY: VIrgInia Tech with Steam & Whiter LLC
DATE: March 11,2001
FACIL ITY: Tnoáfl$bda( Inc. WWITP
LOCATION: Teflmuas’,anSa:VA
RATED FLOW. 10 — PE COD 345 rnglL
CURRENT EFFLUENT TN: j4j,nlgIL PE TKJt 172 mgIL
EFFLUENT TN GOAL: 30 ntg lL
NITROGEN REDUC 1 1ON: 210 Ita ld
7? 1000 10 3 1w
1533 1000 1beI201’.ara
CURRENT PROCESS (CHECK ALL THAT APPLY): I tItLE Existing Aerated Volume (MO) 4.5
BEPR (fliP, lP. etc) Existing Anoxic Votiane (MG) 4.5 —
: Bar d an Current MLSS at Winter ADF 4000
— Oxidation Deoti
— Lagoon (Biolac. ott)
— Cyclical Aeration
SBR
High-Rate Biofilter
Emuent FiltratIon
A Qthet. OAF nd Aivemetc Lagoon pretreatment
CURRENT EFFLUENT AMMONIA-N: 03 niglL X From Roped
Fmm Model (at AOF and load. t O d MCRt 12°C wInter gonditlona)
PROPOSED MODIFICATIONS TO GET AMMONIA <11 mgIL:
I Plomodlficabonsreflad New MLSS
1 Raise MCRTIMLSS f ri eidatng tanks (check clantler capacity) ft .
Construct adt AW earatad volume Flow (mgd): Ibtt -
f T. additional SS’a Flow (ingd) ‘t ’ -
£1 ties exlstlnganodcv sneas aerobic (construct separate dealt luclitty)
‘ Use aerated system & BOO removal only (construct separate nitldenut facile
Add Pdtuent Sow eQualtzaJlon tank
Other - -
PROPOSED MODIFiCATIONS TO GET NITRATE <1.0 mgIL:
No niodtlIabcns re%ared
Add downstream DeNI I lifter with methanol
Add downstream Nltntlntron SoOner and DeNit filter with rnranol
methanol to exlatwig BNR process
dd dowtiatearn anoxc W A with methanol teed
affluent finreton
Other : . ‘‘fl .
CAPITAL COST: EquIpment and Structures (from Page 2) $1 .300.000
ElectrIcal and h akumentat4On. 12% $15t000
- Yard Piping and SIte Wart 15% 1195.000
Subtotal . $1,050,000
OHSP 15% *248.000
Engineervig and Canatr t mt 15% *248.000
sutitoii $2,150,000
Contingency 30% $4a5,000
Total Capital Coat $2,610,000
Capital Coal per lb. 20-Yr. N removal $1.73
OPERATIONS COST. Add itlonal $oraepower (from Page 2): 20 HP
Electrical Poser Coat 0.05 1 1kW $4,500 $ ar
Nitrate Reduction using Methanol ‘ 25.0 mg/L
Methanol Reqt*ed 90 glald
Methanol Coal. 0.75 $lgal $24,800 $#ysar
Separate Stage Ammonia Reduction. _ a mgll.
Caustic lode S 25% curio. 0 gela/d
CaustIc Sode Coat 060 WOS $0 $Iysar
Equipment Maintenance Coat $21,500 l4ear
Oenitrlfication Sludge ProducliOn wiMelhanol 300 lba/6
Sludge Dlepoul Cost 400 Mon $21 900 SNeer
Total Annual OUt Cost $74 500 $lyear
Effective Annual Interest Rate after Inflation 291%
20-veer Prasant Wwlh of OW Costa $1,120,000
rOTAL 20-YEAR PRESENT WORTH COST: 13.770.000
Total Cost per lb 20-Yr N removal $2.44
TysonFoods.VArrIs Page lot2
-------
PROJECT: Implementi ng as mgit. Annual Average Total Nitrogen Limit
PREPARED FOR: IJSEPA, Chesapeake Bay Office
PREPARED BY: Virginia Tech with Stearns 8. Wheler, LLC
DATE March 15, 2001
FACIUFY. Stuarts Draft WWTP
LOCATION: Atcueta County. VA
RATED FLOW: 1.4mgo PE COO Ni mg/I.
CURRENT EFFLUENT TN. j,LJnglL P6 TKH Nip mgi.
EFFLUENT TN GOAL: 30 mg / I.
NITROGEN REDUCTION 20 IbsId
7 1000 lbs/yr
146 1000 Ibsl2O-years
MLE _______
BEPR (A210, VIP. etc) _______
Baitienpho _________
Oxidation Ditch
Lagoon (Biolac. etcj
C cllcaI Mçation
SBR
High-Rate Slofilter
Effluent Filtration
Other. Bnish Aerator OxIdation D ches
CURRENT EFFLUENT AMMONIA-N ci 0 mg/I. X From Report
From Model (at ADF and load. 15 d MCRT. 12° C winter Conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA mgi.:
J No IltQdWlCatIQnS rc und New ML$S
— Raise MCRTIMLSS in casting tanks (check clarifier capaoty) N/a
Construct addeonal aerated volume Flow (mgd) C
— Construct additional çlpnflen Flow (mgd) 0
— Use existing sioxic volume as aerobic (cenatnici separate denit facility)
— Use aerated system for BOO removal only (constuct separate nitldenit facIlity)
— Add H tIuent flow eqiahzalion tank
Other _____________________________________________________________
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 mgi.:
1 Nomodlflatkxis required
Add downafream DeNIt filter with methanol
Md doematream Fitlisalion 8) 0 1 0 1 st end DeNlI filter with methanol
a methanol to eidaing BNR process
dosi w i veam anonc tank with methanol teed
S-Md effluetit tilVatlon
• • ••
CAPITAL COST:
Eqipment arid Structilles (from Page 2)
Electrical and Instrumentation. 12%
$250,000
530.000
YardP.pingandSdeWork 15%
flOOD
Sublo
5 3 20.000
Contractor OHSP: 15%
545.000
Eng i neering anti Cons V. Mgmt 15%
M .0ciO
Subtotal
5420.000
Contingency 30%
596.000
Total Caplal Coal
,gqg
Capilal Coal par lb 20-Yr N removal
$3.54
DPERATIONS COST
.
Additional Horsepower (fro m Page 21
Electrical Power Cost 005 SAW
Nitrate Reduction using Methanol
Methanol R ulred.
Mathand Coal 075 S/gal
Separate Stage Ammonia ReductIon.
Caustic Soda i 25% oonc
Caustic Soda Cost 060 5/gal
Equ ment Maintenance Cost
Dentl’lfation Sludge Production w iMethanet
Sludge DIsposal Cost 400 Mon
Total Annual DIN Cost.
EttettIve Annual Metes: Rate after InflatIon.
20-Year Present Watt of OSM Cost
0 HP
SO $lyew
- ing/L
10 galsM
52700 5/pear
0.0 zngll.
0 gals/d
$0 S/year
$4,200 5/year
SO lba
$2,200 5/year
55.100 5/year
291%
1140 O
TOTAL 20-YEAR PRESENT WORTH COST:
Total Cost per lb 20-Yr N removal $432
CURRENT PROCESS (CHECK ALL THAT APPL’l):
x
‘ C
Eidstlng Aerated Volume (MG) N/a
Existing Anoalo Volume (MO) N/a
Ciarant ktSS at WInter ADF 5000
Sluaita Draft. VA ala
Page 1o12
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PROJECT: ImplementIng a3 mglI. Annual Avssage la S Nitrogen Limit
PREPARED FOR: USEPA, atesapeike Bay Gifts.
PREPARED BY: Virginia Teth with Steams & Whaler, LLC
DATE’ Mirth 19, 2001
FACILITY: Strasbura WWTP
LOCATION: St ate n. VA
RATED FLOW: 1.0 mgd Pt coo. M Is m Olt
CURRENT EFFLUENT TN: 60 mgIL Pt TKN: N h n’tgit.
EFFLUENT TN GOAL: aOmght.
NITROGEN REDUCTION 20 bald
7 l000Ibatyr
146 1000 Ibe/20.years
CURRENT PROCESS (CHECK ALL TRAT APPLY). : MLE Aerated Volume CMG) N/a
— BEPR (A ltO. VIP tic) tasting Ariosc Volume (MG) We
Batdeiiplio Current MLS$ at Winter ADE 4000
:i QaIflabon Ditch
— Lagoon (Bidac etc)
— Cyclical Anton
SBR
high-Rate Blofiter
: Effiue , ItFIIVabon
X Other Brush Aerator Osidation Ditch
CURRENrEFFLUENTAMMONIA-PI cl.0 inglL X Fromifepoit
From Modal (aIADF and load. 15 d MCRt it C ‘te’ ccnditioiis)
PROPOSED MODIFICATiONS TO GET AMMONIA’ i.0 mgiL:
Nem.Sdjonsreqtdred S lew MLSS
— Raise MCRTJMLSS Si existIng tanks (ch ad ’ clanrcer capacity) P01
Constuct eddltionat aerated volume Flow (mgd) 0
Conesad aldttlonal dears Flow (mgd) 0
- - Use eidstlng eaSt volume as aerobic (eenstruct separate dealt facility)
tie. waled system S SOD removal only (oanstruct separate nltldenut facility)
— Add SilkienI flaw equalization tank
_Other _ ‘ r d C ’ ’
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mglL
No modiflCsttoris required
X Add downateam DeNIt Oiler aD methanol
Add downstream Nitnfation Biolilter and 0644 filter aD methanol
methanol to ex lsthig BNR procen
Md dowrtsteem moat lank with metienci feed
Add sl’atthvabcn
• Other ‘ •‘ •• .
CAPITAL COST: Equipment and Structures (from Page 2) - 51.300.000
Bedrical end Inslrumeritation. 12% 5158.000
YerdPlplnqand Site Work: 15% $105000
Subtotal. 11,060000
Contractor OH&P. 15% 5248,000
Digaeers end Constr. Mgmt 15% 5248.000
Subtotal. 52.1*000
Con bngOncy 30% 5498.000
Total Cagitat Cost. 52 .850 .000
Capital Cost per lb. 20-Yr N rentovat $15.15
OPERATiONS COST: AddItional Ptrsepower (from Page 2) 20 HP
Becblcal Power Cost 005 5 1kW 58.500 Sar
NItrate Reduction using Methanol SO mglL
Methanol Required 10 gabld
Methanol Cost 075 5 10a 1 $2,700 Slyest
Separate Stage Ammonia Reducllorr OflmglL
Caust,cSoda@25%cOnc Ogafald
CaustioSodaCost 060$lgal 50$ltear
Equipment Malnleriance Cost 521.500 Slyest
Denitriticallon Sludge Produdion istteethanol 40 theM
Sludge DIsposal CosI 400 $llon 52.900 Slyear
Total Annual OEM Cost 133.500 $lyear
Effective Annual Inlerest Rate alter Irdlatlon 2 gi%
20-Year Preseni Woilh glOW Costa $500,000
TOTAL 20-YEAR PRESENT WORTH COST: - $3,150,000
Total Cost per lb 20-Yr. N removal 511.5$
Strasburg VA hIs Page 1 E 2
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PROJECT. impeernentlng a3 mgIL Annual Average total Nitrogen UmIt
PREPARED FOR USEPA, Chesapeslie Gay OffIce
PREPARED BY Virginia Tech with Steams I Whaler, LLC
DATE: Marvh 28, 2001
FACIUTY: 1MSD-VIP -
LOCATtON : NOrt&. VA
RATED FLOW. 40.0 mgd FE COD: mg / i.
URRENT EFFLUENT TN; 0.0 ngIL Pt TKt1 _______ing lt.
EFFLUENT TN GOAL- 30 171911.
MITROGEN REDUCTION; *000 thald
385 i000IbsIyr
7300 1000 Ibsl2O’yean
CURRENT PROCESS (CHECK ALL ThAT APPLY): : MLE EXIsWI Aeraled Volume (MG) _______
. OEPR (AltO. VIP. qtcj Existing Anoxic Volume (MG) _______
: Swdenpho Ctwrent MLSS at Winter ADF _______
Oxidation Oltoli
Lagoon (Brotac. alt)
— C vbcalAeraIion
SBR
— Hugh-Rate Biotilter
— Effluent Fitration
21 Other The Original V IP Plant, no effluent filtration
CURRENT EFFLUENT AMMONIA -ti: °1 0 mg/I. I ] ] From Report
[ JFrom Model (atADF and load 15 dMCRT 12°C winIer condliOfia)
PROPOSED MODIFICATIONS TO GET AMMONIA c 1.0 n IgiL:
[ No modlfloatlons requited New MLSS
a RSe MCRTIMLSS in eidstkiglanks(theck riazifler capacily) N /a
a Construct eddmonui aerated Sin Flow (mgd) 0
[ Constnact additional dal lfleti Flow (mgd)’ 0
lIE Use Sating anoxic vo lume as aerobic (construct separate dent facility)
[ Use aerated ayst4rn for SOD i ii , ‘ vS ofly (construct separate nit/denit facility)
t5 Add influent Stow equalization tank
E Other ‘ ‘“‘ . I
PROPOSED MODIFICATIONS TO GET NITRATE C 1. 0 g/L
[ flNo niod ltGa0oris requIred
ltlMd downstream DeNli fitter slit methanol
Add downstream NibIficatlon BloMer and DeNrt filer with methanol
AS memsibi to existhig StIR pvas
.. AS downstream enoxic tarE wil l methanol feed
Add effluenUltrallon
• 0 t , - I •
CAPITAL COST: Equipment aid Structures (from Page 2) *14.950.000
Electncal and inatrianentation 12% 11,794.000
Yard Piping and S iteS 15% 12,243000
Subtotal . $19 990.000
Contractor CHIP 15% $ M0.0O0
Engineenuig end Con sir. Mgmt. 15% $2849000
Subtotal 124.090.000
30% $5897000
Total Capital Cost: $30,380,000
Capital Cost per lb. 20 -Yr N removd $4.10
OPERATIONS COST: Addutlotial Horsepower (from Page 2). HP
Electrical P c Cost 0.05 5 1 1W 5381.400 $Iyear
titrate Redtfllon usIng Methanol 3.0 mg / I.
Methanol RequIred: 450 gale/ti
Methanol Coat: 075 $tgal $125900 $l ear
Separate Stage Ammonia Redinion 0.0 . mg/I.
Caustic Soda § 25%conc. 0 galald
Caustic Soda CoaL 0.80 S/gal SO $/ uew
EquIpment Itaintanaftos Cost P16.800 $4ieat
Denutrtfloetlon Sludge Production Sutethanol. 1440 taM
Sludge DIsposal Cost 400 $tlon 0105.190 sMer
Total Annual O&M Cost 5731.300 S4ear
Effect/ve Annual Interest Rate after k u h letlon 291%
20-Yet Present Wotthof O&M Costs. $11,000,000
TOTAL 20-YEAR PRESENT WORTH COST: $41,449 ,000
Total Cost per lb 20-Yr P 1 removal $3.40
HRSD-VIP VA xis Page 1 ol 2
-------
PROJECT: tinpismentlng .3 n IgLAn DUSI Average Teed Nunogen Umit
PREPARED FOR: USEPA, Cheaspeske Bay Office
PREPARED BY: VirgInIa Tech wI lts Stea ms S Wheler . UC
DATE: March 25, 2001
FACILITY: HRSD4 lunsemOnd
LOCATION: Portsnioulh. VA —
RATED FLOW: i O’ mgd PE COD ______mg / I
CURRENT EFFLUENT TN: 80 mg/I. PE 11CN _______rrg/L
EFFLUENT N GOAL’ 30 mgiL
NITROGEN REDUCTION. 750 lbsld
274 ¶000 IbsIyt
5415 1000 tDW2D’yesrS
CURRENT PROCESS (CHECK ALL THAT APPLY)’ : MLE ExIsting Aerated Volume (MG) _______
SEP11 (MID. VIP. etc.) . ExistUig Anoxtc Volume (MG) ________
— BardenphO Cuirent MLSS at Winier ADF _______
— OSSa On D
Lagoon (Slolec, etc.)
Cyclical Atabon
SIR’ -
HIgh-Rate BlaMer
oviec aQjltnnw/oefIkient SfbSu
CURRENT EFFLUENT AMMONIA-N: ‘cLQnig/L From Report
‘1. From MoØel (atADF and load. 15 dMCRT, 12’ C wmtercondillons)
PROPOSED MODIFICATIONS TO GET AMMONIA’ 10 mglI :
pi Ne v MLSS
RaIse MCRTIMLSS lfl ealaling tanks (check dan Cer capacity) ‘ ‘ Nls ‘
ConstJuca additional aerated volume Flow (mgd). 0
• Construct addl f lonal daiffiers F (mgd)’ 0 ’
Use SatIng anonc yekime is aerobic (construct separate debt /acrUty)
• Use seined sØem 1w BOO removal only (construct separate nut!denlt (acuity)
4d bifluent twequabsebon tank
other
PROPOSED MODIFICATIONS TO GET NITRATE c 1.0 tnqlL:
No niodllcalroits required
X Add doenateam Ce/lit Mar wit/ i methanol
Add downstream NhttatIon Sic/liter and Oe114 fIlter with methanol
• Add , Jtwid le uStu BNR procees
£ dit isnaln .ncrec tank wIl i methanol feed
t , emunt a
- ov $.fl ] jv4it fl’dPT 1 ’ . ‘J ’ - It Z , -
CAP/TAL COST: Equipment and Strutres(Itm Page 2): $11,450,000
Electrical end instiumentallon: .12% $1,374,000
YaM P/ping end SIte Worte 15% *1.718000
Subtotal. 114.540,000
Contractor OHS?: 15% *2,151,000
Eng’neetng and Catsir. Mr. 15% $2,181,000
Subtotal. sie,eoo.
Cflngency 30% 14,382.000
Total Capital Cost $23280000
Capital Cost per lb. 20-Yr. N removal, $4.25
OPERATIONS COST: AddItional horsepower ((rem Page2V . 600 HP
ElectrIcal P r Cost 0.05 5 1kW $196,000 S / year
Nitrate Reduction isng Methanol 30 mg/I.
Methanol Required 340 gSst’d
Methanol Cost 075 S/gal 193.100 5 /year
Separate Stage Ammonia Reduthon 0.0 mgot
CausticSoda @25%COflG OgSsfd
Caustic Soda Coal 080 S/gal SO Slyest
Equipment Maintenance Coal 5189,000 5/year
Osnitnllcabon Sludge Production vdMadiard’ 1080 ars/d
Sludge Disposal Coat. 400 S/b ’ $75800 S/year
Total Annual OW Cost., $556,900 5/year
Et(ectwe Annual Interest Raw alter kiflalion 211%
20-Year Present Worth glOW Coats: $5,350,000
TOTAL 20-YEAR PRESINT WORTH COST: $31,110,000
Total Cost per lb 20-Yr N removal. 5577
HASO-Nensemond Page 1 of 2
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P RO J ECT: Iniplenientlng .3 uS MnuStAVflSt foISt NNiogei Limit —
PREPARED FOR: USEPA, Chesapeake Bay Office
PREPARED BY Virginia Tech with Steams & Whaler, tIC
DATE. March 25.2001
FACILITY: Proctor’s Creek WWW
LOCATiON: 9 pterfleld County. VA
RATED FLOW: 20.0 mgd PE COD _______mgiL
CURRENT EFFLUENT TN. 90 mgll. PE TXN _______mgIL
EFFLUENT TN GOAL 30 mgFI.
NITROGEN REDUCTION 500 Ibs!d
183 1Q00 lbslyr
3850 1000 IbsI2 0-years -
CURRENT PROCESS (CHECK ALL THAT APPLY): X MIE Existing Aerated Volume (MG). _______
OEPR (A2I0. VIP dc) Existing Moxic Volume (MG) ________
Ba,denpbo Current MISS at Winier ADF _______
Oxidation Ditch
Lagoon (Blotac. etc )
Cyclical Aerefleri
SER
High-Rate Siolilter
EMuent Filtration
Other:
CURRENT EFFLUENT AMMONIA-N: rIO ingi’I X From Repoft
From Model (at AOF and load. lEd MCRT. i t C winter conditions)
PROPOSED MODIFICATIONS TO GET AMMONIA C tO mglt-
]NO mnodtllcetlons required New MISS
Jkatse MCRTR.tSS in Sating tanks (check clarifier capacity) Nla ’
JConstruct additional aerated volume Flow (mgd) 0
JCcnstnd additional dardleri Flow (nigd). 0
- JUse existing anoxic volume u aerobic (construct separate denit facility)
Juse aerated system for BOO removal ordy (construct separate niusenht racility)
JAal Iniluent flow equalizalion lank
JOther -
PROPOSED MODIFICATIONS TO GET NITRATE C tO mgit.-
No niodificetions requrred
Add downatewn DeNil liter with methanol
Add downabeaifl Nitilftcatior Bl aSter and DeNil Utervettt methanol
- methanol te ealedng BNR pronass
downaheam anotoc (silt with methanol teed
Add eMuent lNrMb .
Other. t 1 - - - b ’ j 4
CAPITAL COST: Equipment end flinwes(flom Page 2)- 57, 960,000
Electrtcal and trietrumentetlon 12% 5954.000
Yard Pipingand S te V h S. 15% $1193000
Stflotat: 510.100.000
Contra c tor 0M W- 15% 11.515.000
Engineering and Constr Mgml. 15% $1 .515.000
Subtotal: $13130000
Contingencr 30% $3030000
Total Caps ICoe l $11,150,000
Capital Cost per lb. 20-Yr N removal $443
OPERATIONS COST Mdltlonat Horsepower (frohi Page 2) 400 HP
Electncal Poertir Cost DOS SAW $130700 Slyear
Nitrate ReductIon using Methanol 30 mnglL
Methanol Required 230 galsld
Methanol Cost 075 1 /gal 163.000 1 /year
Separate Stage Ammonia ReductIon 0.0 inge’L
Causticsoda@25%cO1C 0 0 5 10
Caustic cc t 050 5/gel SO 1/pear
EquipmelttMalnteflaflOe Cost 1131.300 5 /year
Deriitrlfication Sludge P,odi.tbon silMethanol. 720 teld
Sludge Disposal Cost 400 1/ton $52600 5/year
Total Annual 0M4 Cost 537 1.600 5/year
EttecliveAnnral interest Rate after tnflatiow 2 91%
20-Year Pyesent Worth of OSM Costs $5 , 010,000
TOTAL 20-YEAR PRESENT WORTH COST: $21,120,000
Total Cost per lb 20-Yr. N removal $5S$
WWTP_3mgI BNR evaluation Page of 2
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PROJECT: implementing a 3 mglL Annual Avrage Total Nitrogen Limit
PREPARED FOR: USEPA, Chesapeake Say Office
PREPARED DY; Virginia lath with Stearns S Wheler, U -C
DATE: March 25,200 1
FACIUTY: Falling Croak YWTP
LOCATION: Cheelcilcid Coinv. VA
RATED FLOW: 10.0 mgd PE COO ______mglL
CURRENT EFFLUENT TN: 6.0 n4L PE TKN _______sng lL
EFFLUENT TN GOAL: 3.0 mglL
NITROGEN REDUCTiON: 250 16 514
0% 100016
1025 1000 ibsl2O-Iraass
CURRENT PROCESS (CHECK ALL THAT APPLY): X MLE Ealelaig Aerated Volume (MG) _______
SEPR ($210. lP, 5t ) Eidsvng AA0 IOC Volume ( MC) .
: — Current MLSS at Winter APP ______
— Oxlda on 04th
— Lagoon(Siefec.elC)
- CychceiAerabon
SOR
:
Effluent Fdtmtion
Other _________________________________________________________________
CURRENT EFFLUENT AMMONIA-N. cl.0 rrglt X From Report
FromModel(SIADF andload. 151$ MCRT if C *interconoidone$
PROPOSED MODIFICATIONS TO GET AMMONIA 41.0 mgIL:
f]]Nomodillcetione rewired NewMLSS
DRalse MCRT(MLSé I ii exs$dng tanks (check darifiercapaolly) N / l
DConS dSdii0neI aSe d volume Flow mgd) - 0
Use e)ds*q wcido vokn as aerobc (constuct separate denit fealty)
Use aerated s m tar SOD removal aNy (anstruct separate nitldenlt fadIit
CaS d or Se t ’s . Flow (mgd): .0 , .
Add inlisd Sow equelirallon tank
Other i t r1tP ’t: :r . v .
PROPOSED MODIFICATIONS TO GET NITRATE C 1.0 mgllJ
[ JNomoddk3truns reqtired
X Add downsfletn DeNit filter with methanol
oownstesn NllrtOoe100 Slufil tar and DeNit tIller with methanol
Add methanol to Sebng BNR process
Add downeteam anedo tank with methanol feed
Add effluent Svflon
other r
CAPITAL COST: Equipment and Spuctures (from Page 2) $4 450.000
Elecilcal and Inslnan’entatiofl. 12%, 9531000
- Tint pipIng end Slit %tyoit 15% 1008.000
Subtotal 35650000
Contractor OI-I&P 15% 1840.000
Engineering sit Constr Mg 15% 9840 000
Subtotal 17.350.000
Continyency 30% $1,695,000
Total Capital Coal. $9,050,000
Capital Cost per lb 20-Yr N removal. $4.10
OPERATIONS COST. Additional Horsepower (from Page 2) 200 lIP
EleojiosI Power Coat. 0.05 1 1kW 105,300 S/year
NIVate Peduc& i using Methanol 3.0 regit
M aaA ReqtSed 110 galeld
Methanol Cast 0.75 S/gal $30,100 5/yea
Separate Stage Ainmottia Reduolloit - 00 mgIL
Caustc Soth § 25% conc 0 gets/a
Caustic-Soda Cost 0.60 $lgal 10 S/year
Equipment M i lnter.aflee Cost 173500 Sjye ,
Oenitrlficaden Sludge Poduotlon wlMethanol 300 Weld
Sludge Disposal Coat 100 IRon 126.300 S/bear
Total Annual OW Cost $105,200 Slyest
Elfecttve Annual Interest Rate alter ktflebon . 291%
20-Year Present Wait aVOW Cost 12,130,000
TOTAL 20-YEAR PRESENT WORTH COST: $11,180,000
Total Cost perlb 20-Yr N removal. 16.56
Falling Creek VA x is Page 1 01 2
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APPENDIX B
COST INFORMATION FROM THE FINAL
REPORT FOR 8 MGIL EFFLUENT TN
UPGRADES AT 51 WWTPS IN THE
CHESAPEAKE BAY WATERSHED
13
-------
modification costs in this report were based on the “permanent modification” standards- of each
owner if such standards were known.
Pennsylvania WWTPs
The jesuits of the 16 Pennsylvania WWTP evaluations are summarized in Table 7.
Table 7. Pr ’. ”Q”vaflia WWTPS for BNR Removal
Total Capital
Capital
per
WWTP
BNR Design
Flow
Costs
$
Cost(FIoW
SIMGD
Add. N
Removal
Altoona City (E)
—
9.0
.230 x 10’ —
— .233x10 ’
x 106
1.84 x I0’ .
. 0.060 x 10’
- 25.448 x itfT
1.077 x 106 -
— 4.039 x 10’
— 2.815 x 10’
136,667
91,333
$0;5 I
0.42
A ltoonaCity(W1
Chambersburg
Greater Hazleton
Hanover
Harrisburg
Lancaster
Lebanon
13.5 —
4.5 —
89 —
4.5
- 30.0
29.7
8.0
L,4 10,444
880,899
13,333
— 848,250
36,263
504,875
175,938
2:69
3.24
0.08
2.00
0.19
1.19
0.76
ranton
State College
16.0
— 6.0
— 0.780 x l0’’
130,000
0.33
.
(IJAJA)
1.619 x 10’
3.320 x I0 ’_
6.339 x 10’
5.246x 100
0.763 x l0 ’ _
1780x 10’
.
- 134,917
1.12
Susquehanna
(Lancaster Area)
Throop
WLl1iamsport(C1
Will iamsportW)
Wyoming VaIIey_
— 7.0
7.2
4.5
32.0
26.0
474,285
880,417
- 1,165,778 .
23,843
-- 68,462 —
1.68
— 1.36
2.58
0.18
0.42
YorkC ity
69.936 x 10’
— 319,634
80.946
Total/Average
218.8 -
The 16 Pennsylvania WWTPs can be easily classified into two categories based on the capital
costs of the needed modificatiOnS for BNR. Six of the plants, accounting for only 29% of the post
BNR design flows, would account for 79% of the total capital costs. Of the six, the Harrisburg
plant, alone, accounts for 36% of the total projected capital costs. The six plants, their post BNR
design flows, their projected capital costs for BNR, and the BNR modification costs por MGD,
are listed in Table 8. The capital cost per MOD would be nearly $900,000, and the cost per
pound additional N removal projects to $2.09/lb.
Table 8. “° Cost BNR Modification Plants _____________
—
Total Capital
Capital
Cçst per
WWTP
BNR Design
Flow
MGD
43
Costs
$
6.347 x 10’
CostlF low
$/MGD
1.4104 x 10’
Add. N
Removal
$2.69/lb -
Chambersburg
—
—
—
7.84 0 xl 0’
880,899
$3.24/lb
Greater liazieton —
Harrisburg —
— 8.9
30.0
—
— 25.448 x 10’
4.039 x 10’
6.339 x 10 ’_
848,250
504,875
$2.00/lb
$1.19/lb
Lebanon
7.2
880.474
$1.36/lb
W’msport Central
—
5.246 X 10’
- 1.166 * 10°
$2.58/lb
W’mspor( West
.
-
55.26 x 10’
875,737
$2.09/lb
Total/Average
63.1
4
-------
The high capital investment and cost per pound projections suggest that these plants are good
candidates for nutrient trading with non-point source controls or other WWTPs, if such an option
is developed.
In contrast to the six plants listed in Table 8, the 10 other plants account for 155.7 MOD (7 1%) of
the post BNR design flow, but only S 14.676 x 106 (21%) of the projected capital costs, for a
modification cost of only $94,258 per MGI). Also, five of these 10 plants would have a
reduction in annual O&M costs from converting to BNR. The projected average cost per pound
of additional N removal by these 10 plants is only $0.4 1/lb. ft is unlikely that non-point controls
could even remotely approach these costs, and obviously could not promise the same reliability of
N reduction. Clearly, these plants are good candidates for economical BNR modification and
operation.
Maryland and New York WWTPs
The nine Maryland WWTPs jncluded in this draft report are small scale plants, with one
exception, and, consequently, the projected costs per additional pound of nitrogen removed are
very high for most of them. The information is tabulated in Table 9. The two New York plants
are relatively large, but one is a trickling filter (IF) plant, and the other has very severe site
constraints. Consequently, the projected costs for implementing BNR at the two NY plants are
high. Their data aLso are ihcluded in Table 9.
Table 9. Maryland and New York WWTPS Evaluated for BNR Removal
WWTP
BNR Design
flow
MGD
Total Capital
Costs
S
Capital
Cost/Flow
S/MGD
Cost per lb
Add.
N Removal
$0.50/lb N
Brunswick
0.7
390,000
10’
557,143
1.50
10
$5.92/lb N
Chostertown
Crisfield
Elkton
Federalsburg
0.9
1.0
2.7
0.75
l.350x
1.949x 10’
10’
1.525 x l0
10’
x
1.949 x 10’
729,630
2.033 x 10’
10’
SL87/lbN
$3.34/lb N
$3.55/ IbN
Georges Creek
(Alleghany Cty.)
0.6
1.663x
106
.
$2.90F 1b N
Indian Head
0.49
532,000 —
1.085 x
$0.07/lb N
Mattawoman
15
4.250 x 10’
283,333 —
106
$3.77/lb N
Winebrcnner
0.6
1.480x
x
—
10
1.31/lb N
MD Totals/Avg.
22.74
15.109x —
10’
x
522,280
$2.24/lb N
Binghainpton
Endicott
25
8
13.057 x
6.656 x 10’
832,000
$3.35/lb N
N
NY Totals/A .
33
19.713 x 10’
597,364
Only two of the Mazyland WWTPs, Brunswick and Mattawoman, have the potential for low cost
BNR modification. This is because most of the other plants have fixed-film biological processes,
either trickling filters or rotating biological contactors. or are old facilities that need substantial
upgrading before BNR is possible. One, Chestertown, is an aerated lagoon system that cannot
maintain nitrification during the winter months. The cost per pound of additional nitrogen
removed is relatively small for the nine plants collectively, but that is because the Mattawoman
flow dominates the total flow, and it potentially can be modified for BNR very economically.
The seven WWTPs other than Brunswick and Mattawornan account for only 31% of the design
5
-------
BNR flow, but 69% of the projected capital costs. The CoSt per additional pound of Nremoval
for the seven “high cost” plants averages $3.36/lb N, which is substantiallY higher than the
$2.09/lb N average of the high cost Pennsylvania WWTPS. Clearly, it would be economical to
upgrade the Brunswick and Mattawomafl WWTPs for BNR. The other plants do not fall into the
low cost category based on cost per additional pound of potential nitrogen removal, and non-point
pollution reduction trading may be more attractive. However this coSt per pound is still
considerably less than the çstimatcs for some types of non-point source controls. Also, some of
the Maryland plants are in need of upgrades for conventionitl treatTf%eflt. If they are to be
upgraded or expanded, it may be possible to economically include modifications that enable BNR
along with the expansions and upgrades.
Virginia WWTPs
The twenty-four Virginia WWTPs are primarily small plants, as shown by the data llstcd in Tabl 10.
Virainia BNR IIA “ 1 n’t Plants
BNR Design -
Flow
MGD
30
Total Capital Capital Cost per lb Add.
Costs Cost/Flow . N removal
S SIMGD
560,000 18,667 50.605/lb
—
2.0
90,000 - 45,000
-50.065/lb
Beach .
—
— 30,000
92,000
-$0.12/lb
0.325 —
3.0 220 .000
-
73,000
$0.29/lb
Scrvices#l
3.0
220,000
73,000 —
$029/lb
Services#8
2.0
0
-
-$0.1 1/lb
2.0
790,000
—
395,000
$2.20/lb
Royal — 4.0
16 —
— 18
50,000
4.688x 106
490,000
2.980x 106
13,000 -
— 293,000
27,222
614,000
$0.02/lb
$0.54/Lb
50.063/lb
Mooney
— 4.85 —
$0.68/lb
Potomac — 67.0 —
2.0
20.800 x 10°
0
310,448
0
$030/lb
N/A
— 1.2
0
0
—
0
and Co.
4.5
— 150,000 -
— 570,000
— 33,000
— $0.30/lb
6.25
91,000
S0. 16/Lb —
2.0
— 97,000
49,000
-$0.79/lb
Mill
— 1.0
1.3 x 100
— 1.3 x 100
$1.80/lb
1.2 —
4.480 x 10° —
3,733,000
— 80.338/lb
Foods,
0.975 120,000
1.240 x 10°
123,000
886,000
-$0.14/lb
— $2.36/Lb
Draft 1.4
4.0 — 3.500x 10° 875,000
1.0 —- 70,000 70,000
$127/lb
-$0.22/Lb
113.7
42.445 x 10’ —
244,358 $0.48/lb
Total/Average -
6
-------
Four of the Virginia plants are large and collectively wilt be designed to treat 131 MOD by a M A ; which is
75% of the Virginia total The othet 20 WWrPs treat an average flow of only 2.14 MOD and twelve of
them are designed to treat 2 MOD or less. Although the plants are relatively small 1 they should be much
more economical to modify for BNR. removal than the typical Mazyland WWTP. This is because nearly all
of them are activated sludge (AS) process facilities, and several of them are oxidation ditch AS systems.
Oxidation ditches typically are easy to operate for biological nitrogen removal, simply by changing the
operating approach. The primary expense for most of them is the purchase and installation of timer
switches for the aerators. Also, most of the Virginia facilities are not near design flow, and can
be easily modified for BNP. with the existing activated skidge basin volumes and clarifier
capacities. However, the recommended constructive or operative modifications may lead to a
downsizing of the plants’ hydraulic design capacity. Therefore, the resulting BNR process might
have a shorter usefUl service life (as plant flow increases) than a more permanent retrofit designed
to maintain the existing permitted design capacity. The savings accumulated during the interim
years, however, may be sufficient to pay for much of the subsequent expansion. Regardless, the
average cost per additional pound of N removed for the Virginia plants is projected as only
$O.4811b, the lowest of the three states. Even this figure is misleading because most of the
projected capital costs would be expended on six of the WWTPs, and three plants project much
higher costs per additional pound of N removed than the rest. The seven high capital outlay
and/or high N removal cost plants are listed in Table 11.
Table 11. VirginIa High Cost BNR R ind W.raftu Plants _______________
Capital
Cest lb Add.
WWTP
BN1t Design
Flow
MGD_
Total Capital
Costs
S
Coat/Flow
S/MGD
395,000
N removal
.
$2.20/lb
Fishersville
2.0
790,000
10°
293,000
$0.54/lb
Harrisonburg
16
4.688 x
106
614,000
$0.68/lb
Leesburg
4.85
2.980 x
—
310 448
$0.50/lb
Lower Potomac,
Fairfax County
67.0
20.8 x
$0.33 8/lb
Rocco Farm
Foods,Edinburg
1.2
4.480 x l0
10 ’
3,733,000
886,000
—
$2.36/lb
Stuarts Draft
IA
1.240 x
10°
875,000
$1.27/lb
Waynesboro
4.0
3.500 x
-
10’
398,942
—
$0.61/lb
Total/Average
96.45
38.418 x
The seven plants listed above account for only 56% of the total discharge flow, but nearly 91% of
the projected BNR modification capital costs. In spite of the high capital costs, the projected
average cost per additional pound of nitrogen removed is only $0.61/lb. The other 17 Virginia
plants would have.a cost per lb additional N removed of only $027, and six of these plants should
save money over 20 yrsby implementing the recommended BIlE approach. Two of the
evaluated plants. Merck, Inc. and Luray, have no reason to implement liNE because their
wastewaters are nitrogen deficient for biological wastewater treatment, which necessitates
nitrogen addition.
7
-------
Table 1. Summary list of P lait and NPUES Permit Raquiremeots
liavyland
Plant Pennlt Flow SObS ItS NH-N l t d TP 00 p H NOTES
MCD ‘aglL mge’L mg i ! . mg i!. mglI. m gi !.
Brunawidi 0.7 30 30 - - 2 ‘5.0 6.54.5
0.9 30 00 • - - >50 6.5-8.6
CrIsfie ld 1.0 30 30 2 ‘tO 6.5-6.5
Elk Im i 16 30 30 20 - 2 ‘5.0 65-55 TKN
Fedeta lsbu ig 035 30 30 10 2 > 5.0 66-6.5
Georges Creek 06 30 30 2 ‘6.0 6.54.5
Ind Ian Head 0.49 16 30 8 2 ‘6.0 65-8.5 ‘TKN
Mettawornan 15 30 30 . 016 >5.0 65-8.5
Wtneb 1 n. ,ec 0.6 10 10 0.65 - 2 >50 6.5-6.5
TOTAL 21 64
All permits Include a goal of a ysafly averageS mgi ! . ¶74. w Idth go Into sHed once lbs avenge
annual plaid flow exceeds 050 MGD.
Pennsy lvan ia
Plant Pennit Flow SODS ItS - 1 4 1 1 4- I l Th 1? DO pH NOTES
MOO mgit. mgi !. mg i ! . mgi!. mg i ! . mgi!.
I I I I l l I V V
AliSine CtIy(E) 9 20 25 30 2.5 4 P5 6.0-9.0 land Ill: Ma y - O c t II arid IV Nov-A pr.
noon. Clty(W) 9 20 25 30 2.5 4 >5 60-tO I End III: May-0d I I and IV Nov- A pr.
Cti.mbeisburg 4.5 15 25 30 3.5 10 ‘5 60-9.0 lend Ill: M ay-Oct II and IV: Nov-Apr.
Greater 1-faxleton 6.9 25 30 6.0-9.0 tAll Year Round
Hanover 6.5 15 25 30 1.5 4.5 2 ‘5 6.0 .9.0 land I II: May-Oct II and M Plov-Apç / All Year Round
Hadsburg 30 35 30 15 2 >5 to-to landV:AflYearRound:IltMsy.Oc
Laaster Cay 29.7 15 25 30 2.5 7.5 2 >5 6.0-9.0 I and 111: May-Oct I I and M Nov-Ap r- flYaar Round
Lebanon 5 10 20 30 2.5 7.6 2 >5 tO-tO land Ill: May -Oct II end M Plov-Ap V All Year Round
Saanton 20 25 30 3 9 ‘5 6.04.0 I. All Veer Round. ILl: May-Oct.; IV: Nov-Apr.
Stale College 6 10 10 1 varIes 0.13 >5 6.0-9.0 ltJu Nov1V 2.5-5.5 mglL.V:Osathed PMar-Octtfl year Ro,nW
(UAJAJ
Susquehanna 12 25 30 15 2 ‘5 6.0-9.0 land V: All Year Round: UI: May-at
— Are
fliroop 7 25 30 4.5 138 ‘5 6.0-6.0 I: All Year Round: 1W May-Cd: MNov-Apr.
wmwnepoa(C) 7.2 25 30 6.0-96 l:AllYearRcund
W%emapod(W) 4.5 54 54 . 0.0-to l;n’rearRoumt
Wyoming Valley 32 25 30 6.0-00 1: A l Year Round
( g Q )
YottCfty 26 15 20 30 1.7 2.1 2 ‘5 6.0-90 larIdlItMay-OcL;llendMflov.Apr.
TOTAL 216.3
-------
tablet. Ow.ea..y Ustof PlanS
If ew Yett
.
.
Plant
PunnIt flow
MGD
RODS
mgll.
155
mgIL
WH4.N
tnglL
TN
ingA.
TP
mgfl.
DO pit
mglL
Elrqhanton-fl%r ancity
9V ge of £ndlcott
20
8
s
2
30
I I
30
m
11
12.
iv
W2SMGO gsthelimdis S O O4lb. ld),rn.ain-Oct
A1 8 MOD tthe limit S 830 t Jun -Oct
TOTAL
28
-
-
VkgISa
p44 ’4 Punft flow RODS 153 M I f f -N TN 1? DO p 14 NOTES
MOD mgIt. mgIL niII. mgIt. .ngt mgn.
i i to iv
Wtng Sn 30 to 10 1 018 ‘60 80-90 tii vearRound
Colonial ancit 2 21 28 4.83 - - ‘0.5 III. Apr-Sap
Da l d g ian. 0.325 30 30 1.35 . 2 ‘50 80
Dale3acvioaa *1 3 2 3 or ‘P04 -P
OalaSuMcscSS 3 2 3 or •po .p
DuPont V ’naabom • 2 21S 14 0.669 0.801 - - kgld; Al mSnium valuus. Tamp 31 C. III Jun-Dec. IV Jan-May
Fluheav lt. 1.4 24 24 8.14 106 4.0 81-95 lILJun.DaçIVJan.Mey
Fi a ritRoy a l 4 30 30 . 7 13 - - 85-90 llLJun-DaqMJun-May
H tMo OnSy .P i tCSV i aWtiflCty 1 5 10 10 1 015 ‘60 0.0.90 flea n jn4 -
HanIaonti 15 C 9 ’ 1KM; ill. Jun-Dec. lVrJan-Muy.
Leesbwg 4.85 12 20 3 V 2 ‘50 6.5.5.5 1KM fcc May-Oct; IlL May-Oct
LowurPotwnac.FSdsCty. 54 10 10 1 - - 015 ‘60 0.0.9.0 landIll Year i tound
Liaray 2 23.5 30 3 ‘85 6.5-90
MScdI&COJnO..EDI10A 11.50 1567 2684 406 1291’ MonItor ‘45 6.5.9.5 Mvakaesmlglo; IKN:Tow cyattde-29kfl lanip-37C
MlddleRlvat i veione 45+ 25 30 3.1 3.6 ‘40 0.6-9.5 llI;Jun-OctIVJ lo-J-May
Opequon, VW S 0.25 5 10.4 30 048 0.9 71 0.5-9.5 I: Jun-Sn: II. Oct-Mo,: l iE Mey.Jan IV Feb-Apr
paJtfl (fl . 2 74 23 30 11 1.7 - - 7.2 landlltMey-No,:Ilun dMDeo-Apr
PwvulvSIe, New 1 14.5 14.5 1 5 1.5 ‘6.0 0.0-9.0
Puvo.lPfla. Old 0.6 14.6 14.5 - - - ‘-60 6.0-9.0
Ro P m Food., Edbturg 1.2 6 30 - 1.95 654 4J5 I so.r 65-9.5 11 CM For Jun-Dec. Jan44.,: I and lItJun-Oec, land IVJan-M.y
Svaabw 0978 20 30 LY 10.4 MSmunz Ill: Jun-D.c. IV-.JSn-May
StaagftDrslt 1.4 10.5 25 30 4’ 121’ ‘7.1 6.1-9.3 1*4; land Ill:Jun-Dec. ItlndIV an-May
Naynnboro - 4 75 15 30 2 - . - ‘60 landttl-Jun-OctIl:Nov-Muy
‘# cdstofl 1 30 30 - - - - 7.2 6 5-0.5
TOTAL
a lnaidea cooang water.
164.8
‘0
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Table 2. Summary of Projected Nitrogen Removals and Costs
Qcurrent
MOD
Qdeslgn
MOD
Ncurrent
Ibid
Nreduc.
lbl2Oyrs In thousand
Cost
$IIb N
Maryland
0.5
BRUNSWICKWWTP
0325
07.
68
530
CHESTERTOWN WWTP
0.65
0.9
58
247
592
495
CRISFIELD WWTP
0.7
1
91
319
ELKTON WWTP
1 37
2.7
206
1452
1 67
FEDERALSBIJRG WWTP
0355
0.75
54
507
GEORGES CREEK WWTP. ALLEGANY COUNTY
0.626
0.6
107
457
2.9
INDIAN HEAD WWTP
0.314
0.5
43
219
MATTAWOMAN WWTP
7.55
15
869
4913
0.07
WINEBRENNER WWTP, WASHINGTON COUNT\!
03
06
44
411
3.77
MarWand Totals/Average
12.19
22.75
1540
9115
£21
New York
BINGHAMTON-JOHNSON CiTY JOINT SEWAGE TREATMENT PLANT
24.9
25
3011
9965
2.24
VILLAGE OF ENDICOTT WWTP
7 39
8
924
3292
3.35
New York Totals/Average
32.29
3935
13257
242
Pennsy lvanIa
ALTOONA CITY AUTHORITY EASTERLY PLANT
6.67
9
645
3185
0.51
ALTOONA CITY AUTHORITY WESTERLY PLANT .
9.14
13.5
1052
3880
0.42
CHAMBERSBURG WWTP
4 .5
4.5
563
2841
2.69
GREATER HAZLETON JOINT SEWER AUTHORITY WWTP
6.2
8.9
765
3860
3.24
HANOVER AREA REGIONAL WWTP
3.46
3.65
568
3046
-0.08
HARRiSBURG WWTP
24
30
4003
27635
2.00
LANCASTER CITY WWTP . .
23.4
29.7
1971
9230
0.19
LEBANON WWTP
5.7
8
870
4652
.
1.19
SCRANTON SEWER AUTHORITY WWTP
13.8
16
1266
4464
0.76
STATE COLLEGE UAJA WWTP
4.5
6
582
3330
033
SUSQUEHANNA WWTP LANCASTER AREA AUThOR iTY
9.45
12
796
2288
1.12
THROOP WWTP. LACKAWANNA RBSA.
4.5
7
499
1982
1.68
WIWAMSPORT SANITARY AUThORITY CENTRAL PLANT
8.98
7.2
1296’
6600
1.36
W1LLJAMSPORT SANITARY AUTHORITY WEST PLANT
35
4.5
686
3200
2.58
WYOMING VALLEY SANITARY AUThORITY WWTP, LUZERNE CT?.
22.3
32
1213
5575
0.17
YORK CITY SEWER AUTHORITY STP
13.1
26
1289
5806
0.36
Pe nns y l van ia Totals/A VRF8CLC
163.2
18064
91574
0
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Table 2. Summary of Projected Nitrogen Removals and Costs
Qcurrent Qdesign Ncurrent Nreduc.. Cost
MGD MGD Ibid lb!ZOyrs In thQusand $Ilb N_
Virginia
ARLINGTON WWTP 32.4 30 2432 1973 0.605
COLONIAL BEACH WWTP 0.64 2 72 431 -o
DAHLGREN WWTP 0.28 0 325 41 218 -0.12
DALE SERVICES Section 1 WWTP 3 3 300 730 0.29
DALESERV1CESSection BWWTP 2.12 3 210 500 0.29
DUPONT WAYNESUORO WWTP 0.491 2 188 3184 -0.11
FISKERSVILLEWWTP 1.3 2’ 121 260 2.2
FRONT ROYAL WWTP 227 4 284, 1023 0.02
HARRISONBURC WWTP 8 16 1334 8712 0.54
H L.MOONEY WWTP, PRiNCE WILLIAM COUNTY 12.8 18 1858 8820 0.06
LEESBURG WATER POLLU11ON CONTROL FACILITY 286 4.85 382 1580 0.68
LOWER POTOMAC NWTP , FAIRFAX COUNTY 45 54/67 5630 34,094 05
LURAYWWTP 1.5 2 300 NA NA
MERCKANDCO., INC WWTP 0.906 1.2 27 ‘ NA 0
MiDDLE RIVERNERONA WWTP 3.65 4.5# 180 420 0.3
OPEQUON WRF, CITY OF WINCHESTER 5.14 6 25’ ‘857 5328 0.16
PARKINS MILL WWTP 1.09 2 82 200 -0.79
PURCELLVILLE EXIST1NG WWTP 0.315 0.5 63 - -
PURCELLVILLE NEW DESIGN.WWTP - 1 87 720 . 1.8
ROCCO FARM FOODS WWTP 1.1 1.2 1238 8840 0.338
STRASBURG WWTP 0.6 0.975 75 4366 -0.14
STUARTS DRAFT WWTP 0.98 1.4’ 85 484 2.36
WAYNESBORO WWTP 3.63 4 424 3548 1.27
WOODSTOCK WWTP 077 1 77 292 -0.22
V ,yqfr,ia Totals/Average 130 8 164.2 16260 85703
GRAND TOTALS 39799 199649
‘Average daily flows “Design flow less than permit flow #Comblned Effluent NA: Not Applicable
pS
I -
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