United States
Environmental Protection
Agency
Office Of Water
(WH-595)
EPA 430/09-91-005
May 1991
Assessment Of Single-Stage
Trickling Filter Nitrification
Printed on Recycled Paper
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United States Environmental Protection Agency
Office of Municipal Pollution Control
: Washington, B.C.
ASSESSMENT OF SINGLE-STAGE
TRICKLING FILTER NITRIFICATION
May 1991
r *
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ACKNOWLEDGEMENT
This report ..was prepared by HydroQual, Inc. in fulfillment of
Contract 68-08-0023. It was prepared by O. Karl Scheible and Ashok
Gupta of HydfoQual, Inc. Wendy Bell, OMPC, Washington, B.C. was
the Environmental Protection Agency Project Officer. The
assistance provided by the plant operators and owners, as
summarized in the report, is acknowledged with appreciation.
NOTICE
This document has been reviewed in accordance with U.S.
Environmental Protection Agency policy and approved for
publication. Mention of trade names or commercial products does
not constitute endorsement or recommendation for use.
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: CONTENTS
Section Page
FIGURES . ii
TABLES '. iii
1 INTRODUCTION 1- 1
2 CONCLUSIONS 2-1
3 RECOMMENDATIONS 3 - 1
4 . NITRIFICATION IN TRICKLING FILTERS 4- 1
INTRODUCTION 4- 1
SINGLE-STAGE NITRIFICATION 4- 2
SEPARATE STAGE NITRIFICATION 4- 4
TRICKLING FILTER/SOLIDS CONTACT (TF/SC) PROCESS 4-12
5' STATUS OF TRICKLING FILTER NITRIFICATION APPLICATIONS 5-1
: INTRODUCTION . • . . 5- 1
SUMMARY OF TRICKLING FILTER PLANTS 5- 1
6 EVALUATION OF SELECTED PLANT PERFORMANCE DATA 6- 1
INTRODUCTION 6- 1
ASSESSMENT OF SELECTED TRICKLING FILTER PLANTS 6- 1
Palm Springs. California 6- 1
Amberst. Ohio 6- 5
Chemung County. New York 6- 6
Wauconda. Illinois 6 - 7
Ashland. Ohio 6- 8
Bremen. Indiana 6- 9
Allentown. Pennsylvania 6-10
Cibolo Creek. Texas . . . 6-11
ASSESSMENT OF SYSTEM PERFORMANCE CHARACTERISTICS 6-12
7 REFERENCES 7 - 1
APPENDIX A: SUMMARY DESCRIPTION OF NITRIFYING TRICKLING FILTER
PLANTS
APPENDIX B: PERFORMANCE AND OPERATING DATA FOR SELECTED PLANTS
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FIGURES : . -
Figure Page
4-1 EPA PROCESS DESIGN CURVES, BASED ON MIDLAND, MI STUDY. . .. 4- 6
4-2 EPA PROCESS DESIGN CURVES, BASED ON LIMA, OH STUDY. . . 4-7
4-3 DESIGN CURVES INCORPORATING APPLIED HYDRAULIC AND AMMONIA LOADS
AT TEMPERATURES GREATER THAN 14°C 4- 8
4-4 DESIGN CURVES INCORPORATING APPLIED HYDRAULIC AND AMMONIA LOADS
AT TEMPERATURES BETWEEN 10 AND 14°C .... 4- 8
4-5 ALTERNATIVE CONFIGURATIONS OF THE TRICKLING FILTER/SOLIDS
CONTACT PROCESS •••••" 4-10
6-1 RATIO OF NH3-N REMOVED TO BODs REMOVED AS A FUNCTION OF THE BOD
REMOVAL RATE . ... 6-14
6-2 EFFLUENT NH3-N LEVELS COMPARED TO EQUIVALENT BODs EFFLUENT
LEVELS , . . . 6-15
6-3 EFFLUENT BODs CONCENTRATION AS A FUNCTION OF THE MEDIA AREA BOD
LOADING . 6-16
6-4 EFFLUENT BODs CONCENTRATION AS A FUNCTION OF THE VOLUMETRIC BOD
LOADING . . . . 6-17
6-5 EFFLUENT AMMONIA-NITROGEN CONCENTRATION AS A FUNCTION OF BOD
MEDIA SURFACE LOADING 6-18
6-6 EFFLUENT AMMONIA-NITROGEN CONCENTRATION AS A FUNCTION OF BOD
VOLUMETRIC LOADING . . 6-19
6-7 EFFLUENT AMMONIA LEVELS AS A FUNCTION OF HYDRAULIC LOADING 6-21
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TABLES
Table
4-1 PERFORMANCE DATA SHOWING THE EFFECT OF RECIRCULATION ON NH4+-N
REMOVAL IN A ROCK FILTER . .'. . 4- 3
4-2 AMMONIA REMOVAL DATA ON SEPARATE STAGE ROCK TRICKLING FILTERS., 4-10
4-3 DESIGN DATA FOR FULL-SCALE TF/SC FACILITIES (FROM MATASCI, et.
al., 1988) . 4-14
4-4 PERFORMANCE DATA FROM FOUR FULL-SCALE TF/SC FACILITIES. (FROM
MATASCI, et. al. , 1988) 4-14
5-1 SUMMARY OF PLANT OPERATIONS 5-2
5-2 SUMMARY OF DESCRIPTION OF TRICKLING FILTERS PRACTICING
NITRIFICATION 5-33
6-1 SUMMARY OF PERFORMANCE DATA FOR SELECTED TRICKLING FILER
PLANTS 6- 2
ill
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SECTION 1.
INTRODUCTION
As par-t rof-«itsr- program of - providing technical .assistance' to local
governments in the area of municipal wastewater treatment, the Office of
Municipal Pollution Control (OMPC) evaluates specific technologies and reports
on their capabilities and limitations. This report is part of a larger effort
to compare different wastewater technologies that can achieve nitrification.
OMPC plans to look at oxidation ditches and sequencing batch reactors to
compare their ammonia-removal efficiencies and costs with those of trickling
filters and conventional activated sludge processes.
Many municipalities may have ammonia limits added to their permits in the
near future. For the large number of facilities that include trickling filters
in their treatment train, modifications to the filters would frequently be the
most cost-effective solution to this additional treatment need.
This report evaluates the use of trickling filters for nitrification of
municipal wastewater. This study originally focused on single-stage trickling
filters, a biological process application wherein carbon oxidation and
nitrification are accomplished within the same unit without separation of the
bioinass used to accomplish these operations. Multiple-stage systems were added
to the study due to the limited number of single-stage facilities. The
multiple-stage systems evaluated in this report all had performance data that
were measured after the first stage so they could be compared to single-stage
sys terns.
Information was compiled from the EPA, Regional and State offices,
literature, and wastewater treatment plant personnel. The data were collected
from full-scale treatment facilities and used to evaluate process performance
and aid in understanding the effect of various operating parameters.
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Page 2-1
SECTION 2.
• • CONCLUSIONS
The extent to which single-stage trickling filter nitrification is
practiced is very limited. Ten single-stage plants were identified, with six
of these utilizing the solids-contact process in conjunction with the trickling
filter. Several other plants use separate two-stage processes for
carbonaceous/nitrogenous BOD removal. They have either two-stage trickling
filters with intermediate clarifiers or a trickling filter. in series with an
activated sludge process.
\
The evaluated plants were generally meeting their permit requirements,
including ammonia-nitrogen limits when applied. Several plants exhibit some
increase in effluent ammonia and BOD levels during cold weather months,
although the differences are relatively small and there is no direct
correlation apparent with temperature. Both plastic media and rock filters are
represented by the plants. There are no apparent differences in performance
related to the medium; the reactor sizings are different because of the various
specific area characteristics of the media.
Nitrification requires relatively low organic loadings. These can be
expressed on a volumetric or medium surface area loadings basis, and are
generally set to yield effluent BODs levels less than 10 to 15 mg/L. Operating
at these levels will assure an environment in which the autotrophic nitrifying
bacteria can compete with the faster growing heterotrophic bacteria responsible
for carbonaceous BOD removal. Loadings that are less than 10 Ibs BOD/1,000
ft3-d or 0.3 Ibs BOD/1,000 ft2-d will allow for nitrification and yield
effluent ammonia-nitrogen levels less than 4 mg/L. These loadings, based on a
review of combined data from 10 selected plants, compare favorably with the
organic loading guidelines suggested by the USEPA for proper design and
operation of single-stage trickling filters (1975 Process Design Manual for
Nitrogen Control).
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• , Page 2-2
Recirculation is beneficial to the process performance of trickling
filters. There was no clear indication of optimum rates from the selected
plant data. Ratios of recycle to raw wastewater flow in the order of one to
three would appear to be adequate operational criteria to achieve this
performance.
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Page 3-1
SECTION 3.
RECOMMENDATIONS
Several process configurations are available to accomplish nitrification
with trickling filters. The predominant application utilizes a two-stage
arrangement with intermediate clarification. This offers greater stability and
will likely yield a more highly polished effluent than a single-stage process.
The single-stage operation, however, can offer a more cost-effective approach,
requiring less tankage and unit operations. This presumes that loadings would
be similar to those required for two-stage operation.
This report indicates that the application of the single-stage trickling
filter nitrification process is very limited, and, as such, there are limited
data from which to evaluate performance and process design. It is recommended
that further study be made of the process in direct comparison to a two-stage
configuration. This would best be accomplished in the field* preferably at an
existing full scale facility, with side by side treatment trains. It should
focus on organic loadings (surface and volumetric), hydraulic loadings and
recirculation rates. Encompassing two seasons would allow for an assessment of
temperature effects. The resulting data would enhance OMPC's planned report on
the nitrification costs and capabilities of different technologies.
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Page 4-1
SECTION 4.
NITRIFICATION IN TRICKLING FILTERS
INTRODUCTION
Today, ammonia-nitrogen removal is a major concern for many wastewater
treatment facilities because of the U.S. Environmental Protection Agency's
approach to implementing more stringent water quality based ammonia limits.
This has resulted in an increased interest to find cost effective technologies
for ammonia removal.
Ammonia is biologically converted to nitrite and nitrate in a two-step
nitrification process. It is first oxidized to nitrite (N02) by nitrosomonas
bacteria and then to nitrate (N03) by nitrobacter bacteria, both of which are
autotrophic:
NH4+ + 1.5 02- - N02- + 2H+ + H20 (1)
N02- + 0.5 02 -»• N03" (2)
Nitrification can be accomplished by both suspended and fixed growth
processes as long as a sufficient amount of oxygen is available to nitrifiers
and enough alkalinity is present in the wastewater. Oxidation of high soluble
BOD concentrations in the liquid phase by heterotrophic bacteria deplete oxygen
availability, and the nitrifiers are unable to compete with the relatively
faster growing heterotrophs. Nitrification begins only when soluble BOD
concentrations in the liquid phase are low enough for nitrifiers to compete
with heterotrophs,
A number of wastewater treatment plants in the United States are practicing
nitrification with trickling filters because of the stability, ease of
operation and cost effectiveness of the treatment process. The trickling
filter is an aerobic fixed film reactor which uses a solid surface medium to
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• Page 4-2
support biological film growth. Media traditionally consist of rocks, slag, or
synthetic materials. Rock and slag trickling filters generally have four to
ten feet of media depth. Plastic inedia trickling filters are normally
constructed much deeper (15 to 25 feet) because of the lighter weight and
better ventilation capabilities of the packing. Recent advances in the
development of plastic media with different structural configurations have made
this technology more efficient and cost effective. Various types of trickling
filter configurations in use for achieving nitrification are discussed in this
section.
SINGLE-STAGE NITRIFICATION '.'.'•
Little information is available for the process in which carbon oxidation
and nitrification are accomplished in a single trickling filter unit.
Stenquist et al., (1974) studied the process in a plastic media trickling
filter, the results of which suggested that organic loading is the limiting
factor. Organic loadings less than 25 Ibs BODs/day/l,000 cubic feet (0.40
kg/day/m3) were found to favor a high degree of nitrification in plastic media
filters. !''..-.
The EPA Process Design Manual for Nitrogen Control (1975) recommends an
organic loading of 10 to 12 Ib BODs/day/l,000 cubic feet (0.16 to 0.19
kg/m3/day) to attain 75 percent nitrification in single-stage rock media
filters. Higher allowable organic loadings for plastic media filters, as
reported by Stenquist (1974), is attributed to the greater specific surface
area of plastic media and better oxygen supply. Rock filters generally have
poor ventilation when water and air temperatures are close.
I ' -
The minimum hydraulic loading rate for plastic, media trickling filters is
in the range of 0.5 to 1.0 gpm/ft2 (0.020 to 0.041 m3/m2-minute) to ensure
uniform wetting of the medium. A recirculation ratio of 1:1 was consistently
found to improve ammonia removals in a rock media trickling filter at Salford,
England (USEPA, 1975). The data from this study are presented in Table 4-1.
As shown, lower effluent ammonia levels were achieved with recirculation over a
range of loadings between 22.5 and 3.2 Ibs BODs/l.OOO ft3-d; the greater effect
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EFFECT OF RECIRCULATION ON NITRIFICATION IN ROCK TRICKLING FILTERS
AT SALFORD, ENGLAND '
BOD*
load"
b/1000 c-j ft/day
(kg/rr.2/day>
22.6
(0.36)
16.3
(0.26)
11.8
(0.19)
9.2
(0.15)
7.7
(0.12)
5.9
(0.095)
4.6
(0.074)
3.2
(0.051)
Influent
BOD5.
mg/1
266
235
191
239
165
192
199
206
Influer.:
KK^-N
m'g/1
33.9
31 .3
32.0
43.9
40.5
. Effluent
NH^-K,
mg/1
without
recirculatior.
19.7
16.9
9.7
I2.S<"
11.4
1
40.7
38.3
36.6
5.7
2.8
0.7
with
recirculatior.
13.6
11.8
4.6
2.2
4.9 ;•
2.8
0.9
0.4
Percent
nitrification
without
recirculatior.
«2
46
70
72
72
86
93
93
with
recirculatior.
60
62
85
95
8e
93
• 96
99
Media was blast slag, 8 ft (2.4 re) deep. With recirculation a 1:1 r»tio was employed.
(1) original table had 125 mg/L; this was assumed to be a typo and
changed to 12.5.
TABLE 4-1. PERFORMANCE DATA SHOWING THE EFFECT OF RECIRCULATION ON
NH4 +-N REMOVAL IN A ROCK FILTER
(FROM USEPA NITROGEN CONTROL MANUAL, 1975).
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Page 4-4 '
on removals was apparent at higher loadings. The EPA Design Manual recommends
provision for recirculation for better ammonia removals.
Parker and Richards (1986) investigated single-stage nitrification in
trickling filters by comparing the data from two pilot studies. Results show
that nitrification begins only when soluble BODs concentrations are less than
20 mg/L. Hence, nitrifiers become established in the biofilm only in the lower
portion of the tower, where the soluble BODs concentrations are low enough for
nitrifiers to compete against heterotrophs. Parker and Richards also reported
that cross-flow plastic media were the most efficient for achieving
nitrification in a single-stage system. Process interactions:, like the return
of untreated digester supernatant to the headworks, increase the soluble BODs
concentrations and will affect the single-stage nitrification process. Such
return streams must be considered in design and operation. According to Parker
and Richards (1986), favorable operating conditions required to achieve
carbonaceous BOD removal and nitrification in a single-stage: trickling filter
are low organic loadings, high residence times, sufficient oxygen availability
and consistency in hydraulic, organic and ammonia loadings.
SEPARATE STAGE NITRIFICATION
Most of the wastewater treatment facilities using trickling filters for
nitrification are configured as two-stage systems, with intermediate
clarification. In the first stage, the removal of carbonaceous BODs is
accomplished, followed by the second stage where nitrification is achieved.
An early study of nitrification in trickling filters was conducted by
Duddles et al.f (1974),' which, indicated the feasibility of using a plastic
medium trickling filter for nitrification. In separate stage nitrification,
the rate of nitrification was found to be directly related to the surface area
of the media, rather than the media volume. Plastic media have high specific
surface areas (27 to 68 square feet/cubic ft.), as compared to rock or slag
media (13 to 20 square feet/cubic ft.) resulting in smaller volume
requirements, and reducing the cost for space, structure, and distributor arms.
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• Page 4-5
The USEPA's Process Design Manual for Nitrogen Control (1975) gives design
curves for nitrification in plastic media trickling filters (Figures 4-1 and
4-2), showing that the efficiency of nitrification is directly related to the
surface loading. Figures 4-1 and 4-2 present an empirical relationship between
the desired eff luent ,,NH3-N concentration and the required surface area of
media. The curves also demonstrate the temperature dependency ' of the
nitrification process, indicating lower surface area requirements at higher
temperatures. These curves are based on data collected in pilot scale studies
in Midland, Michigan (Figure 4-1) and Lima, Ohio (Figure 4-2), where primary
treatment and secondary treatment for carbonaceous BOD removal was followed by
plastic media (corrugated vertical type) trickling filtration. Figure 4-2
shows surface reaction rates for Lima, Ohio data compared with the trend lines
developed from the Midland, Michigan data.
Gullicks and Cleasby (1986) suggested that there were deficiencies in the
EPA trickling filter nitrification design procedure, and that the design curves
are applicable only to municipal wastewater and the conditions under which the
data were generated. The accuracy of the EPA design curves was questioned and
they suggested that the effects of the hydraulic loading rate and influent
NH3-N concentration to the tower are not adequately addressed.
Gullicks and Cleasby (1986) proposed new design curves (Figures 4-3 and
4-4) which incorporate the effects of four critical design parameters: the
hydraulic loading rate, the influent NH4+-N concentration, the recycle rate,
and the wastewater temperature. Their empirical approach is based on a flux-
limited fixed film process theory, which suggests that: (1) when wastewater
temperature increases, the mass transfer rate should increase due to the
increase in the * film diffusivities and biomass activity, and (2) when the
hydraulic loading rate or the influent ammonia -nitrogen
concentration increases, the mass transfer rate should increase because the
concentration gradient from the liquid phase to the biofilm is increased. The
proposed design curves (Figures 4-3 and 4-4) apply only to nitrification of
municipal secondary effluent that has been settled before application to the
trickling filter towers. The curves are based on 6.55 m of vertical-type
plastic media with a specific surface area of 88.6 m2/m3. Gullicks and Cleasby
recommended
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SURFACE AREA REQUIREMENTS FOR NITRIFICATION -
MIDLAND MICHIGAN
tt
tu
N
X
o
if
CD
I
2
ct
JU
tc
3
CO
I2,OOO
IO.OOO
8,000
6,000
4,000
2,000
©
\ SF/lb/day = 0.2 m2/ kg/day
Influent Data (meon)
BOD5 l5-20mg/l
SS 15-20 mg/l
Organic N 1-4 mg/l
NH^-N 8-18 mg/l
BOD5/TKN •« l.t
7 to II C
1-3 to 19 C
©
©
Key :
El T = 7 to 11C
© T * 13 to 19 C
1.0 2.0 3.0 4.0 5.O
EFFLUENT AMMON1A-N, mg/l
6.0
FIGURE 4-1. EPA PROCESS DESIGN CURVES, BASED ON MIDLAND, MI STUDY
(FROM USEPA NITROGEN CONTROL MANUAL, 1975).
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SURFACE AREA REQUIREMENTS FOR NITRIFICATION -
LIMA, OHIO
I2,OOO
10,000
X
o
a:
i&
8,000
Q
*
s
o
Ul
(fc
lu
0:
6,000
4,000
o
2 2,000
Influent Doto (mean)
BOD5 = 7.0 mg/l
SS =20.5
Organic N= 3.6 mg/l
NH^-N =16.1
BOD5/TKN =0.36
©
Midland, Data
m 13 to I9G
18 to 22 C
©-—
14
*Data point ignored
in trend line
Key-Lima, Ohio Data
© T« 18 to 22C
Q T=10C
i
1.0 2.0 3.0 4.0
EFFLUENT AMMONIA - N , mg/l
5.0
6.0
FIGURE 4-2. EPA PROCESS DESIGN CURVES, BASED ON LIMA, OH STUDY
(FROM USEPA NITROGEN CONTROL MANUAL, 1975).
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FIGURE 4-3.
25
20
15
— 10
0.75 x 10"
-3
«io
1.25 x ID"' kg N/d-irZ
-3
C.25
_L
^ ' C.G 0.5 1.0 1.5 .
"* APPLIED HYDRAULIC LOAD, L/s-m2 OF CROSS SECTION ! .
. (INCLUDING RECYCLE) :
Predicted NH/-N removal kg/d • m2 of media surface, versus
applied hydraulic load and applied NH/-N for nitrification of municipal
secondary cUrifier eflluenl (BOD5 < 30 mg/L and SS < 30 mg/L),
wasiewater temperatures > 14"C and 6.55 m of vertical plmstk medu
(specific surface = 88.6 m'/m')- i
DESIGN CURVES INCORPORATING APPLIED HYDRAULIC ,AND AMMONIA
LOADS AT TEMPERATURES GREATER THAN 14°C \-
(FROM GULLICKS AND CLEASBY, 1986)
FIGURE 4-4.
APPLIED HYDRAULIC LOAD, L/s-m' OF CROSS SECTION
(INCLUDING RECYCLE)
Predicted NH/-N removal, kg/d • •' rf «edia ivface, vers«s
••plied bydra«Iic load aad applied NH,*-N far •HrificatJo* of »«ucipal
iccoadao^ darifier efflMM (BOD, < 30 «f/L Md SS < 30 mg/U
wmstew«ter teapermttres IO-M"C, «ai 6J5 • «f mtie«l fteftic medto
(•pecific Hriace - 88.6 •*/•*).
DESIGN CURVES INCORPORATING APPLIED HYDRAULIC AND AMMONIA LOADS
AT TEMPERATURES BETWEEN' 10 AND 14°C
1 (FROM GULLICKS AND CLEASBY, 1986).
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Page 4-9
that these curves should be used with caution at wastewater temperatures less
than 10°C and hydraulic loading rates greater than 1.36 L/s-m2 (7 gpm/ft2) of
tower cross-section.
The principal difference between the design curves proposed by Gullicks and
Cleasby and the EPA design curves is that the required media surface area is
dictated by the loading criteria (concentration and hydraulic load) in Figures
4-3 and 4-4, whereas in the EPA curves (Figures 4-1 and 4-2) it is dictated by
the effluent quality.
Table 4-2 presents ammonia removal data for rock media separate stage
trickling filters (USEPA, 1975) . These data show that the nitrification rates
are 15 to 50 percent of those found with plastic media filters, when expressed
on a volumetric loading basis. These lower rates are attributed to the lower
specific surface area and shallower depths of rock media filters when compared
to those using plastic media.
Gujer and Boiler (1986) proposed a theoretical nitrification model for
tertiary trickling filtration. This model emphasizes residual ammonia
concentration, recirculation rates, arrangement of filters in series,
alkalinity, residual nitrite concentration and temperature. Basic design
information was collected during a 20 month long pilot study. Sampling was
conducted with depth, allowing an estimate of actual nitrification rates at
various levels within the trickling filters as a function of the respective
ammonia concentration. T>e peak nitrification rate declined significantly with
depth, apparently due to the patchy development of the biofilm at lower depths.
This was caused by the absence of a continuous supply of ammonia to these lower
regions of the filter. The study also showed significant temperature
dependency.
Boiler and Gujer (1986) reported that plastic media trickling filters
following conventional mechanical-biological wastewater treatment were suited
for nitrification when ammonia load fluctuations were not too high. Low solids
production enabled direct discharge without the need for additional
clarification. Specific media surface areas in the range of 150 to 200 m2/m3,
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NITRIFICATION IN SEPARATE STAGE ROCK TRICKLING FILTERS
Facility location
Johonneibjry, S.A.
(full-icale:
Northampton,
England
(pilot-scale-
Depth ,
ft
(ml
12
(3.7!
12
(3.7)
9
(2.7;
6
(1.8
Madia
2-3 in.
(5.1 to 7.£ err.)
roc*
1 . 5 in .
(3 . 6 cir.)
rock
i in .
(2 . 5 cr.;
rock
1.5 in.
(3 . 1 cr.:
rock
Influent
BOD,
mg/1
26
32
23
BO
KH<-N,
mg/1
23.9
25.2
22
33 '
Effluent
BOD ,
mg/i
14
13
10
NK4 -K
mg/1
e.3
4.4
9.1
i
10
11.2
P»rc*r.t
ramovtd
65
83
59
66
Ammonia - K
oxidized
lb/10QJ5 cu ft'/day
Oca/inVday)
3.5
(O.OS5)
2.2
(0.035)
2.4
(0.038)
1.0
(o . o.i 6;
TABLE 4-2. AMMONIA REMOVAL DATA ON SEPARATE STAGE ROCK TRICKLING FILTERS
(FROM USEPA NITROGEN CONTROL MANUAL, 1975).
•USTE SLUDGE
' RETURN SLUDGE
TRICKLING FILTER
SECONDARY
CLARIflER ,IOCCULATO,
«I«ED LIQUOR ^ _/ CtHTER MLL
WASTE SLUDGE •
RETURN SlUOGt
AERATION TANK
B -<>™
. TREATED
CFFLUENT
URN SLUDGE
TRICKLING ftLTER
SECONDARY
AERATED SOLIDS M,,ED CLARIFIER f
CONTACT TAN. IIOOO, , ujHTtJ ^
WASTE SLUDGE
. TREATED
EfFLUENT
RETURN SLUDGE
AERATION TANK
RETURN SLUDGE
Variations of the TF/SC pntceu.
FIGURE 4-5. ALTERNATIVE CONFIGURATIONS OF THE TRICKLING FILTER/SOLIDS
CONTACT PROCESS (FROM MATASCI, et. al., 1986)
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; * . • Page 4-11
hydraulic loads higher than 2 m^/m^/h, and ammonia loads of approximately 0.4
g/m^/d were favorable conditions for full nitrification (< 2 mg/L NH3-N) under
winter conditions (water temperature, 10°C).
Parker et al., (1989) investigated the use of biofilm-control mechanisms to
f
enhance reaction rates in separate stage nitrifying trickling filters. These
included use of cross flow plastic media with higher oxygen transfer
characteristics and provisions for flooding and backwashing to control predator
organisms. The backwashing was also used to control the biofilm inventory,
eliminating excessive sloughing and the need for subsequent clarification. The
study showed a significant improvement in the reaction rates in tertiary
nitrifying trickling filters; regular flooding and backwashing were successful
in preventing the suppression of nitrification typically caused by filter, fly
larvae and other predators. Parker (1989) also concluded that properly
designed and operated nitrifying trickling filters are reliable, and yield
significant cost savings when compared to competitive nitrification
technologies.
Okey and Albertson (1989) analyzed data from five pilot tertiary treatment
facilities to study the kinetics of ammonia nitrogen oxidation under varying
operating conditions. The study concluded that more than one kinetic regime
existed in the nitrifying tower, corresponding to ammonia concentration. A
zero order region existed when the ammonia nitrogen concentration was high and
the system was oxygen limited. A first order regime for ammonia nitrogen
oxidation occurred at low ammonia nitrogen concentrations. At loading rates
gresiter than 1.2 gNH3-N/m2-d the units periodically exhibited an oxygen
deficient condition. The study recommended the use of forced ventilation for
plants that are required to produce an effluent with less than 3 mg/L ammonia
nitrogen. •
Okey and Albertson (1989) also studied temperature effects on ammonia
nitrogen oxidation in nitrifying trickling filters. They indicate that changes
in the nitrification reaction rates with temperature are controlled by
diffusivity and external concentration and not by basic changes in the rate at
-------
Page 4-12 •
•which the cell processes the substrates; this suggests that using Arrhenius-
type temperature corrections for reaction rates may not be appropriate.
TRICKLING FILTER/SOLIDS CONTACT (TF/SC) PROCESS
The TF/SC process was first developed in the late 1970s to enhance the BODs
and suspended solids removal efficiency of an existing trickling filter
facility at the City of Corvallis (Norris et al. , 1982). It has since been
widely applied, particularly for upgrading existing trickling filters.
The TF/SC process is biological/physical in nature and typically includes a
trickling filter, an aerobic solids contact tank, flocculation and secondary
clarification. Biological solids are continuously extracted from the secondary
clarifier and returned to the aerated solids contact tank for contact with
trickling filter effluent. Matasci et al., (1986) listed three different modes
of operation for the TF/SC process (Figure 4-5).
Mode 1: The secondary clarifier sludge is returned to an aerated contact
tank to mix with the trickling filter effluent. 'This mode is
favored to enhance removal of soluble BOD and particulates.
Mode 2: The return sludge is first aerated before mixing with the TF
effluent. Settling is improved; yielding lower effluent solids.
Mode 3: Both procedures are implemented. This mode is normally required
when improved soluble BOD and particulate removals are required.
In a typical TF/SC process, most of the soluble BOD removal takes place in
the' trickling filter. The trickling filter effluent is mixed with the return
sludge from the secondary clarifier in order to improve particulate BOD removal
and SS reduction via enhanced flocculation. The solids contact tank is
normally designed for less than one hour contact time; typical design values
for solids retention time in the solids contact tank are less; than two days.
-------
Page 4-13
Field investigations were conducted by USEPA in 1984 at Oconto Falls,
Wisconsin; Tolleson, Arizona; Medford, Oregon; Chilton, Wisconsin and Morro
Bay, California (USEPA, 1988). Tables 4-3 and 4-4 give information about
design parameters and monthly performance data, respectively, for the Tolleson,
Oconto Falls, -Corvallis and Medford facilities. Tolleson had ' two stage
trickling filtration with intermediary clarification. Corvallis and Oconto
Falls had single stage filtration. Medford was originally an activated sludge
plant that was converted to a TF/AS plant, with the flexibility to operate in
the TF/SC mode. The performance of the Medford facility is difficult to
compare with the other TF/SC plants as it has plastic media (compared to rock
media at Corvallis, Oconto Falls and Tolleson), high organic loadings (115
lb/1,00.0 ft3 - d) and the longest solids contact time (39 minutes). Within the
narrow range of organic loadings studied at the different TF/SC plants, organic
loading was not found to affect final effluent quality significantly. Matasci
et al., (1986) emphasized the need for reliable primary treatment; an increase
in the primary effluent suspended solids was found to correlate well with an
increase in final effluent suspended solids.
Keeping the secondary solids and return sludge in an aerobic condition
appears to be an important factor in the successful operation of the TF/SC
process. A minimum solids contact time of 12 minutes is required for reliable
performance. Although the solids contact tank is primarily designed to
increase solids flocculation and capture, it is also found to remove additional
soluble BOD from the trickling filter effluent if longer aeration contact time
is provided. At the Medford facility, a 75 percent reduction in the trickling
filter effluent soluble BOD was accomplished at a solids contact time of 39
minutes. . .
The TF/SC process can operate over a broad range of MLSS concentration
without affecting effluent quality. .Other major advantages noted for the TF/SC
process are relatively low capital costs, an ability to withstand high organic
loadings, production of a very dense sludge, and high quality effluent. Solids
retention time in the solids contact tank is less than 2 days. Although the
minimum required solids retention time for nitrifying bacteria is a function of
temperature, dissolved oxygen and pH (USEPA, 1975), typical minimum. SRTs
-------
Design data for operating TF/SC faciictieB.
Design flow. m3/s (mgd)
Average dry weather flow
Peak wet weather flow
Design toadng. 1000 kg/d (1000 fo/day)
BOO
SS
Pnmary overflow rate, m3/m* • d (gpd/sq ft)
Tnckkng fitter
Modatype
BOO toeing. g/m3 • d (b/day/1000 cu n)
TF/SC mode
Return sludge aerabon trne (33% return rate).
mrxjles
Aerated solids contact time (total flow
indudng recycle), minutes
FloccUator center wen
Percent of danfier area
Detention bme (totaf flow including recycle).
minutes
Secondary darifier
Overflow rate based on total cteriter area.
rrrYrrr*-d (gpd/sq ft)
Sidewater depth, m (ft)
Sludge removal system
We* location
Tottraon
0.36 (8.3)
0.78(17.7)
10.9(240)
9.80(21.6)
40 (970)
Plastic/rock
880/150(55/9.1)
1
—
9
13
oc
25
18(440)
4.9 (16)
Suction header
Inboard
Oconto F«ll»
0.017(0.38)
0.033(0.75)
0.30 (0.67)
0.36 (0,79)
15 (370)
Rock
560(35)
1 "
-• .8 , -
. 16
38
12(300)
4.6 (15)
Suction tube
Inboard
CorviiNl*
043(9.7)
1.23 (.28.0)
4.94 (10.9)
5.22(11.5)
40(980)
Rock
380(24)
3
9
2
12
~ •
25
•
19 (470)
5.5 (18)
Suction (lube
Inboard
Modford
.0 79 (18,0)
2.63(60,0)
15.9(350)
12.7(28.0)
42 (1030)
Plastic
1840(115)
1
- ..
5
e
*j
20 (480)
4.6(15)
Suction header- 1
Suction lube-3
Inboard
• Contact time at existing flow of 0.39 m'/s (8.8 mgd) plus 33% return rate is 39 minutes.
TABLE 4-3. DESIGN DATA FOR FULL-SCALE TF/SC FACILITIES
(FROM MATASCI, et. al., 1988)
Monthly average performance at operating TF/SC facilities.
TolleftOn
April 1983-March 1C84
Oconto FaM»
April 1 BBS-March 1M4
CorvaHi*
April IMS-March 1984
April 1984- July 1M4
Parameter
Influent flow
Average m'/s
(mgd)
Influent characteristics
BOO. mgA.
SS.mgA-
Temperature. *C
Pnmary effluent
BOD. mgA-
SS.mgA.
TF effluent
BOD.mgA-
SS. mgA.
Return sludge SS. gA-
MLSS.mgA.
Secondary effluent
BOO. mgA.
Carbonaceous BOO. mgA-
SS. mgA-
High
0.29
(6,7)
350
300
—
373
400
42.5'
45.9"
—
1620
15
• —
20
Low
0.22
(5.0)
222
192
— •
107
57
104'
9.9"
—
551
4
—
4
Average
0.27
(61)
277
224
—
173
121
22.8*
23.6'
—
1040
7
—
9
Miflfh
0.020
(046)
179
151
19
—
- —
—
• —
_
—
32
—
.23
Low
0.012
(0.28)
119
100
8
— -
—
_
—
—
—
14
6
Average
0.016
(0.36)
146
118
13
—
—
— .
—
•
21
13
High
078
(17.9)
188
191
22
114
82
39
72
17.2
4960
9
7
13
Low
0.25
(5.6)
48
112
13
35
56
22
54
5.4
1560
5 '
4
7
Average
046
(10.5)
106
154
17
70
66
30
59
11.3
3130
7
5
9
High
0.43
(9.9)
173
159
22
90
38
61
89
1870
23
11
g
Low
0.36
(8.2)
142
119
16
76
29
51
39
1480
14
6
6
Average
0.39
(8-9)
157
138
19
81
34
66
71
1620
19
8
8
' Intermediate darifier effluent
TABLE 4-4.
PERFORMANCE DATA FROM FOUR FULL-SCALE TF/SC FACILITIES.
(FROM MATASCI, et. al., 1988)
-------
Page 4-15
reported in the literature for nitrifying bacteria are over two days. Hence,
it is likely that minimal nitrification enhancement is being accomplished in
the solids contact tank. Matasci et al. , (1986) have also mentioned in their
study that solids contact tanks are not designed for nitrification. . Thus the
trickling filters themselves, even if operating in a TF/SC system will still
accomplish the major fraction of soluble BODs reduction and nitrification.
-------
-------
Page 5-1
; SECTION 5.
STATUS OF TRICKLING FILTER NITRIFICATION APPLICATIONS
INTRODUCTION
A survey was conducted to identify the extent to which trickling filters
are used at municipal facilities in the United States to accomplish
nitrification. This was not meant to be an exhaustive search, but of
sufficient coverage to assess the state-of the-art, and to determine the
availability of performance data.
[ i .
"Information was obtained from several sources. This included a computer
search, using the USEPA Permit Compliance System (PCS); however, only two
trickling filter plants were identified that were required to practice
nitrification. Other sources included USEPA regional and/or State offices;
consultants/engineering firms having expertise in this area; and treatment
plarits cited in the literature. The design and performance data for the plants
were obtained directly from the facility operators.
SUMMARY OF TRICKLING FILTER PLANTS
Twenty-seven trickling filter plants that are accomplishing some degree of
nitrification were identified. Each is described in Appendix A. Seven are
located in Ohio; four in Indiana; three each in California, Pennsylvania and
Texas, and one each in Alabama, Colorado, Illinois, Iowa, Nevada, New Jersey
and New York.
.The types of plants are summarized in Table 5-1. A total of ten plants are
practicing single-stage nitrification. Of these, six have the solids contact
modification to enhance particulate BOD removal. Seventeen plants have
separate stage nitrification, six of which use an activated sludge or
stabilization pond in conjunction with the trickling filter.
-------
Page 5-2
TABLE 5-1. SUMMARY OF PLANT OPERATIONS
Mode of Operation
Single-stage nitrifying
trickling filter
Single-stage trickling
filter with solids contact
modification
Separate-stage trickling
filter (with intermediate
clarification)
Trickling filter in series
with activated sludge process
(two-stage)
Number of
. Plants
P1ant Location
11
.Palm Springs, California; Amherst,
Ohio: Chemung County,; New York; New
Providence, New Jersey
i
Wauconda, Illinois; Ashland, Ohio;
Buckeye Lake, Ohio; Wauseon, Ohio;
East Montogomery County, Ohio;
Pickerington, Ohio j
Bremen, Indiana; Kendallville, Indiana;
Rochester, Indiana; Allentown,
Pennsylvania; Reading, Pennsylvania;
Cibolo Creek, Texas (three plants);
Ozark, Alabama; Boulder, Colorado;
Laport, Indiana
Cedar Rapids, Iowa; Stockton,
California; Sunnyvale, California;
Reno, Nevada; Youngstown, Ohio;
Landsdale, Pennsylvania
Relevant information regarding the plant configuration, wastewater
characteristics and current performance are summarized in Table 5-2. Design
flows range as high as 42.0 mgd with most plants between 50 a.nd 100 percent of
their design capacity. The majority of plants use plastic media. Twelve are
exclusively plastic, while there is one slag media plant (Palni Springs) and two
rock media plants. The rest have combinations of rock and plastic media
filters. Depths of the rock filters range between 4 and 10 feet. The plastic
media filters are generally deep, typically between 20 and 40' feet. Shallower
filters with plastic media are typically retrofits of old rock filters.
Trickling filters are generally designed with'effluent recycle capabilities
to maintain stable hydraulic loadings during normal diurnal variations. The
Wauconda and Amherst plants do not practice recirculatipn, while a
recirculation ratio of 1:1 is maintained at Palm Springs, Bremen and New
Providence. A high ratio of 6:1 is used at Ozark to control solids buildup.
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• , Page 5-7
j
Recirculation rates at the Cibolo Creek plants range between 2.4 and 6.0. At
several plants, although recirculation is practiced, measurements are not taken
of the recycle rate, and estimates of the recirculation ratio cannot be made.
None of the -plants are experiencing problems with meeting permit
requirements for BODs, suspended solids, and ammonia removal (if required),
particularly during warmer temperature seasons. Problems have been noted at
LaPorte, Bremen, and Ashland with ammonia removal during cold temperature
periods.
Performance data availability was limited. Several plants practicing
separate stage nitrification had no intermediate data, while others were only
recently started and had a small data base. Ten plants were identified that
had sufficient data to evaluate their performance. These included five plants
with separate stage nitrification, for which the first stage performance data
were available. As assessment of the facilities' performance data is presented
in the next section.
-------
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Page 6-1
SECTION 6.
EVALUATION OF SELECTED PLANT PERFORMANCE DATA
INTRODUCTION
Of the twenty-seven facilities that were identified as trickling filter
plants accomplishing nitrification, ten were selected for further evaluation.
These had sufficient data for analysis, which were made available by the
individual plant operators:
1. Palm Springs, California
2. Amherst, Ohio
3. Chemung County, New York
4. Wauconda, Illinois
5. Ashland, Ohio
6. Bremen, Indiana
7. Allentown, Pennsylvania
8-10. Cibolo Creek, Texas (three parallel plants)
Each is described in Appendix A. Summaries of the performance data are
provided in Appendix B. These data have been further reduced and summarized in
Table 6-1. Please note that the figures presented in Table 6-1 and Appendix B
may not always match with the figures presented in Table 5-2 and Appendix A
because different sampling locations and different sets of data may have been
used. The following discussions present an assessment of the plants, and then
evaluate in general the use of trickling filters for nitrification.
ASSESSMENT OF SELECTED TRICKLING FILTER PLANTS
Palm Springs. California
The Palm Springs, California wastewater treatment plant utilizes a single-
stage slag media trickling filter system. The facility is comprised of bar
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screening, an aerated grit chamber, primary clarification, four 140 foot
diameter, 9.5 feet deep trickling filters, secondary clarification, sludge
thickening and anaerobic digestion. The secondary effluent is disposed either
to percolation ponds for groundwater recharge or to tertiary treatment for
irrigation use.
The BOD to the trickling filters was estimated to average 101 mg/L in 1989
(see Table B-l for summary of monthly performance data), with an average
/.
ammonia concentration of 20 mg/L. Note that these reflect an assumed 35
percent BOD5 removal through the primary clarifiers. The flow was 7.73 mgd,
approximately 70 percent of its design capacity. Temperatures are moderate
year-round, ranging between 23 to 28°C in 1989.
The secondary plant is required to meet an effluent BOD or 30 mg/L or less
(30-day mean), but does not have an ammonia limit. The monthly average
effluent BODs ranged between 3.4 and 15 mg/L, with a mean of 7.4 mg/L. Ammonia
nitrogen ranged between 0.27 and 10.6 mg/L, with an annual mean of 2.61 mg/L.
The loadings to the plant are consistent with nitrification design; the BOD and
ammonia loadings are 11.1 and 2.15 -lbs/1,000 ft3-d, respectively, on a
volumetric basis, and 0.55: and 0.107 lbs/1,000 ft2-d, respectively, on a media
surface area basis. The hydraulic loading rate is relatively low at 125
gpd/ft^ of filter surface .area. The plant maintains a recirculation ratio of
1:1.
Overall the Palm Springs secondary filter generates a consistent quality
effluent, accomplishing high levels of ammonia removal. Although not required
to nitrify, the loadings imposed on the system are consistent with those
generally imposed for ammonia removal.
Amherst. Ohio
The Amherst, Ohio treatment plant is comprised of screening, grit removal,
primary clarification, trickling filtration, secondary clarification and
chlorine disinfection. There are two trickling filters placed in series
without intermediate clarification. As such, the units are considered
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;Page 6-6
equivalent to a single-stage system. The filters are each 40 feet wide, 90
feet long and 17 feet deep, with plastic cross-flow media .
Currently, the plant is operating at an average flow of approximately 2 mgd
(1.856 mgd-winter, 2.12 mgd summer); equivalent to its design capacity.' The
plant is required to meet an effluent ammonia-nitrogen limit of 6 mg/L in the
winter and 3 mg/L during the summer months. The BOD limit year-round is 10
mg/L. The BOD and NH3-N levels to the trickling filters are estimated for 1989
to have averaged approximately 65 and 14 mg/L, respectively. (See Table B-3;
note that a 35 percent removal was assumed for BODs through the primary
clarifiers.) Temperatures for October through May ranged between 8 and 15°C,
while the summer month temperatures ranged between 17 and 20°C.
The Amherst plant has consistently met .ammonia removal requirements at
loadings generally associated with nitrification design practices. Lower
temperatures will cause lower removal rates. The average effluent ammonia
concentration at temperatures greater than 17°C was 1.7 mg NHs'-N/Ly while this
increased to 3.0 mg/L at temperatures between 8 and 15°C. BODs in the effluent
averaged approximately 7.5 mg/L. Loadings were relatively low. The BOD and
ammonia loadings were 7.29 to 8.96 Ibs BOD/1,000 ft3-d and 1.7 Ibs NH3-N/1.000
ft^-d, respectively. When expressed on a media surface area basis, these were
0.242 to 0.3 Ibs BODs/1,000 ft2-d and 0.05 Ibs NH3-N/1.000 ft2-d, respectively.
Hydraulic loadings were 517 to 589 gpd per ft2 of filter area.
Chemung County. New York
The Chemung County wastewater treatment plant is in its first year of
operation. Operating data (See Table B-2) are for the months November 1989
through April 1990, with a temperature range of 11 to 16°C. The treatment
works include comminution, screening, grit removal, primary clarification,
trickling filtration, secondary clarification, post aeration_and disinfection.
There are two trickling filters in series without intermediate clarification
(as such, they are considered a single-stage system). They have rock media,
are 135 feet in diameter, and are 6 feet deep.
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Page 6-7
The average flow to the plant was 5.8 mgd. The monthly average BODs to the
trickling filters ranged between 42 and 88 mg/L and the ammonia-nitrogen ranged
between 6.5 and 13.0 mg/L. The plant is required to meet an effluent BOD5 for
25 mg/L; there is no ammonia requirement. Loadings to the plant's trickling
filters are somewhat higher than the preceding plants. The BOD5 loading was
13.7 lbs/1,000 ft3-d and 0.676 lbs/1,000 ft2-d; the ammonia loading was 3.17
lbs/1,000 ft3-d and 0.159 lbs/1,000 ft2-d. The average hydraulic loading was
approximately 407 gpd/ft2 of filter area. The plant is meeting its BOD limit,
with monthly averages ranging between 8 and 14 mg/L (mean of 10^8 mg/L). The
equivalent effluent ammonia levels ranged between 3.0 and 7.3 mg/L, with a mean
of 5.4 mg/L. ,
Wauconda. Illinois
The Wauconda wastewater treatment plant consists of aerated grit removal,
comminution, primary clarification, trickling filtration, aerated solids
contact/flocculation, sand filters and chlorine disinfection. The single-stage
trickling filter plant has two plastic media, 50 feet diameter, 28 feet deep,
filters in parallel. The media surface area is 30 ft2/ft3.
The average flow to the plant (See Tables B-4A and B-4B for 1987 and 1988
performance data) has been approximately 0 . 7 mgd, or 50 percent of its design
capa.city. Cold month temperatures ranged between 11 and 16°C, with a range of
17 to 21 °C during the warmer months. The BODs in the primary effluent (monthly
averages) ranged between 76 and 188 mg/L, with a mean of approximately 115
mg/L. The ammonia-nitrogen levels ranged between 12.4 and 17.6 mg/L. The
plant is required to meet an effluent ammonia-nitrogen limit of 4 mg/L in the
winter and 1.4 mg/L in the summer. The BODs limit is 10 mg/L year-round.
loadings were approximately 12 lbs/1,000 ft3-d and 0.4 lbs/1,000
ft2-d; equivalent ammonia-nitrogen loadings were 1.6 N/1,000 ft3-d and Ov04 Ibs
N/1,000 ft2-d. The hydraulic loading had a mean level of approximately 355
gpd/ft2. Overall the plant is generating a high quality effluent, consistent
with the relatively low loadings to the plant . The mean effluent ammonia was
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• . Page 6-8
0.67 mg/L at temperatures greater than 17°C, and 1.26 mg/L at temperatures less
than 16°C.
Ashland. Ohio
The Ashland, Ohio facility has an average design flow of: 5.0 mgd, and is
currently averaging approximately 3.0 mgd. It is a single-stage trickling
filter plant with a solids-contact modification. Unit operations consist of
screening, preaeration, grit removal, primary clarification, two biotowers in
parallel, a solids contact tank, final clarification and UV disinfection. The
plant is required to meet an ammonia-nitrogen limit of 2 mg/L;in the summer and
11 mg/L in the winter. A BOD limit of 10 mg/L is imposed year-round. Both
biotowers have plastic cross-flow media. Each is 80 feet in diameter and 30
feet deep. The media surface area is 30 ft2/ft3. Recirculation is practiced,
but the rates are not measured.
The BODs of the trickling filter influent .(See Table B-5; the BODs levels
reflect a. 35 percent removal through the primary system) ranged between 70 and
123 mg/L, with the higher levels during the warmer temperature months (17, to.
22°C). The mean flow for the colder months (13 to 16°C) was higher (3.3 mgd)
than that of the warmer months (2.7 mgd). Ammonia levels were similar in
variability, ranging between 8.5 and 20 mg N/L on a monthly average basis.
Loadings were very consistent for the one year period. The BOD and ammonia
loadings were 7.6 and 1.1 lbs/1,000 ft3-d, respectively, on a volumetric basis
and 0.253 and 0.285 lbs/1,000 ft2-d on a surface area basis. The hydraulic
loadings averaged 267 gpd/ft2 during the warmer months and 327 gpd/ft2 during
the colder months.
The plant is meeting its effluent requirements. The BOI>5 in the effluent
(including the solids-contact process) was less than 10 mg/L. The effluent
ammonia-nitrogen levels are somewhat anomolous (See Table B-5) with high levels
in the October through December period (average 8.6 mg N/L), and 4.6 mg/L in
January. Levels were consistently lower in the April through September period
preceding this and February and March afterward. Overall, one would expect
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Page 6-9
lower levels of ammonia throughout the year, given the lower loading to the
system.
Bremen. Indiana
The Bremen, Indiana wastewater treatment plant is a two-stage trickling
filter process. Unit operations consist of screening and comminution, grit
removal, primary clarification, two parallel biotowers, intermediate
clarification, a second-stage rock media filter, secondary clarification, sand
filtration and chlorine disinfection. The first-stage biotowers are each 35.3
feet in diameter, and 32 feet deep, with plastic media (34 ft^/ft^) . The
second-stage rock filter is 60 feet in diameter and 6 feet deep. Recirculation
is , practiced in the first stage (0.8:1). There is no recirculation in the
second stage.
Data are available for all of 1989; these can be found (monthly averages)
in Table Br6. A temperature range of 10 to 14°C was observed November through
May, while it ranged from 17 to 19°C during the remaining months. Primary
effluent BODs was low, ranging between 24 and 60 mg/L, with a mean of.
approximately 42 mg/L. The ammonia-nitrogen averaged approximately 9.8 mg/L
for the year. The plant effluent permit includes limits of 10 mg/L BOD5, and 6
and 9 mg/L NH3-N for summer and winter conditions, respectively. The design
flow is 1.3 mgd; the current flow is averaging 1.1 mgd.
Loadings to the first-stage are relatively low, because of the lower
incoming concentrations. The BOD load is approximately 6 lbs/1,000 ft^-d and
0.17 lbs/1,000 ft2-d; equivalent ammonia-nitrogen loadings are 1.4 lbs/1,000
ft3-d and 0.04 lbs/1,000 ft2-d. The hydraulic loading is approximately 552
gpd/ft2 of reactor area. The effluent BODs and NH3-N levels were 10.6 and 1.12
.mg/L, respectively, during the warmer months. These increase to 2.72 and 15.2
mg/L during the colder months.
Loadings to the second-stage rock filter were not greatly different than
the first stage loading due to differences in volume and media surface area
(See Table 6-1). Further reductions were accomplished during the summer months
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Page 6-10
when the BODs and NH3-N averaged 3.1 and 0.8 mg/L; these increased to 5.2 and
2.1 mg/L during the colder months. In all, the plant was consistently in
compliance with its discharge permit requirements for BODs and ammonia.
Allentown. Pennsylvania
The Allentown plant is a two-stage trickling filter plant designed for an
average flow of 40 mgd. The facility is required to meet effluent ammonia-
nitrogen limits of 3 and 9 mg/L during warm and cold temperature periods,
respectively. The effluent BODs limit is 30 mg/L. Data are available for 1989
(Table B-7) including intermediate ammonia-nitrogen and BODs concentrations.
The unit operations include screening, grit removal, primary clarification,
trickling filters (first stage), intermediate clarification, trickling filters
(second stage), clarification and chlorine disinfection. The first stage has
four plastic media trickling filters in parallel, each 100 feet in diameter and
32 feet deep. The second stage is a single large rock filter, 8 feet deep and
covering an area of approximately 8 acres. Normally 2 of the first-stage
filters and 75 of the -second stage filter are in service. Recycle is practiced
only on the second stage, with a target ratio of 0.2:1.
The current average flow to the plant is approximately 32.87 mgd. The
warmer months temperature ranged between 17 and 19 °C; the cold temperature
averaged 11 to 16°C. The first-stage influent (primary effluent) averages
monthly BODs and NH3-N levels between 100 and 137 mg/L, and 8.5 to 16.1 mg/L,
respectively.
First-stage loadings are high, more typical of roughing filters. The BODs
loading averaged 66.36 lbs/1,000 ft3-d and 2.21 lbs/1,000 ft:2-d for the year.
Equivalent ammonia-nitrogen loadings were 6.7 lbs/1,000 ft^-d and 0.22
lbs/1,000 ft2-d.' The hydraulic loading averaged 2,093 gpd/ft2 of reactor area.
The effluent BODs averaged 50 mg/L at the warmer temperatures and 73.1 mg/L
during the colder period. Ammonia-nitrogen levels in the first stage effluent
were 10.0 and 11.4 mg/L for these periods, respectively.
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- ' - ' Page 6-11
The second-stage loadings at Allentown were more in line with those shown
for the preceding plants, consistent with design loadings for nitrifying
plants. The BODs loading averaged 8.5 lbs/1,000 ft3-d and 0.44 lbs/1,000 ft2-d
for the year. The average ammonia-nitrogen loads for the year were 1.4
lbs/1,000 ft3-d and 0.07 lbs/1,000 ft2-d. The hydraulic loading averaged 12:6
gpd/ft2 of reactor area. The average monthly effluent BODs was consistent
through the year, ranging between 6 and 18, with an average 12.3 mg/L. The
ammonia-nitrogen averaged 4.7 during the higher temperature months and 5.9
during the colder temperature months.
Cibolo Creek. Texas
Cibolo Creek operates three parallel treatment plants. All ,are two-stage
trickling filter systems required to meet a BODs limit of 10 mg/L. Ammonia
limits are 6 mg N/L if the flow (total of three plants) is less than 4 mgd, and
4 mg; N/L at flows greater than 6 mgd. The design flow is 6.2 mgd, which is
split to the three plants (A, 29 percent; B, 16 percent; C, 55 percent). The
current average total flow is approximately 2.2 mgd (0.64 mgd to A; 0.35 mgd to
B; 1.23 mgd to C). Temperatures are moderate year-round, ranging between 20
and 27°C.
Unit operations at the three plants consist of primary clarification, first
stage trickling filter, intermediate clarification, second stage trickling
filter, secondary clarification, sand filter and chlorine disinfection.
The data available from the plants are summarized in Tables B-8, B-9 and B-
10. These are from 12 sampling events encompassing a total period of 18 months
(May 1988 through November 1989). The average BODs levels in the primary
clarifier effluent ranged between 67 and 86 mg/L; average ammonia-nitrogen
levels ranged between 17 and 21 mg/L.
All of the trickling filters reactors utilize plastic media. The first-
stage filters for Plants A and B are 8 feet and 7 feet deep, respectively, and
55 feet in diameter. The medium surface area for both is 32 ft2/ft3. The
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: , Page 6-12
second stages are each 7 feet deep, 55 feet in diameter and use media with a
surface area of 64 ft2/ft3. The first-stage of Plant C is 82 feet in diameter
and 16 feet deep, while the second-stage has a diameter of 82 feet and a depth
of 12 feet. The packing in both units is comprised of alternative layers of
vertical (27 ft2/ft3) and cross-flow (48 ft2/ft3) plastic media.
Loadings to each plant differ to a degree. First-stage average BODs
loadings ranged from 10.5 lbs/1,000 ft3-d on Plant C to 22.4 lbs/1,000 ft3-d
for Plant A. Similarly the average ammonia-nitrogen loadings ranged from 2.5
lbs/1,000 ft3-d for Plant C to 5.8 lbs/1,000 ft3-d for Plant A. The ranges
were similar when expressed on a surface loading basis (See Table 6.-1).
Average hydraulic loadings were from 147 gpd/ft2 to 271 gpd/ft2 of reactor
area. Effluent BODs and NHs-N level were consistent with the loadings. The
BODs was 16.9 and 18.6 mgd for Plants C and B, respectively, and 25.6 mg/L for
the higher loaded Plant A. Similarly the first stage effluent NH3-N was 5.6
and 5.7 mg/L for Plants C and B, respectively, and 10.5 for Plant A.
Second-stage loadings for BODs and NH3-N to the three plants showed the
same variation as discussed for the first stage; ranging from low to Plant C
and highest to Plant A. On a volumetric basis, the average BOD loading to C
was 2.7 lbs/1,000 ft3-d, increasing in B and A to 4.2 lbs/1,000 ft3-d and 8.2
lbs/1,000 ft3-d, respectively. Comparable ammonia-nitrogen loadings were 0.93,
1.3 and 3.4 lbs/1,000 ft3-d to Plants C, B and A, respectively. Again the
average effluent BODs and NH3-N levels reflect these loadings. The average
effluent BOD was 3.6, 5.8 and 6.6 mg/L for Plants C, B and. A, respectively.
The average effluent NH3-N levels were 0.5, 0.52 and 2.8 mg/L, respectively.
ASSESSMENT OF SYSTEM PERFORMANCE CHARACTERISTICS . ;
The data that were received from various plants, as presented in Table 6-1
and Appendix B, were reviewed as a whole, assessing the general operational
characteristics for accomplishing nitrification. These analyses must
necessarily be of a general nature, given the limits of the data and the narrow
range of operating conditions experienced by the individual plants.
-------
Page 6-13
Figure 6-1 presents the ratio of the ammonia-nitrogen removal to the
removal as a function of the BOD removal rate. These are averages for the same
periods delineated in Table 6-1. As would be expected, the ratio decreases
with increasing BOD removal rates, shifting to a process dominated by
carbonaceous BOD removal with ammonia -nitrogen removal limited to that required
for cell growth. If a nitrogen requirement for active systems is assumed to be
0.8 to 0.12, then the Allentown first stage, Bremen first stage and Ashland
p.lants are considered carbonaceous removal processes with marginal ammonia
removal activity outside that needed for cell growth, . The remaining units
show higher ratios (in particular the second- stage units for Bremen, Cibolo
Creek and Amherst) , indicating nitrification activity. The transitional BOD
removal rate appears to be in the range of 0.2 to 0.4 Ibs BODs/d- 1,000 ft2.
The effluent ammonia-nitrogen concentrations are compared to the equivalent
period effluent BODs levels accomplished by the systems on Figure 6-2. This
suggests that ammonia levels less than 2 to 4 mg/L NH3-N will be reached when
the effluent BOD5 concentration is at levels less than 15 mg/L and preferably
less than 10 mg/L
Figures 6-3 and 6-4 present the average effluent BOD concentration as a
function of the BOD loadings to the trickling filters . These loadings are
expressed on the basis of the media surface area (Figure 6-3) and the reactor
volume (Figure 6-4). In both cases there is considerable scatter.
Additionally, there is no apparent significant difference due to temperature
effects. The da.-a on Figure 6-3 suggest that surface area loadings should be
less than approximately 0.3 Ibs BOD/1,000 ft2-d for effective BOD removal.
Equivalent BOD volumetric loadings are less that 10 lbs/1,000 ft^-d to
accomplish effluent BODs levels less than 10 to 15 mg/L.
A similar analysis is shown on Figures 6-5 and 6-6. Figure 6-5 presents
the effluent ammonia -nitrogen concentration as a function of the media surface
area BOD loadings. The variability is somewhat high, but the data indicate a
surface area loading less than 0.25 to 0.30 lbs/1,000 ft2-d is needed in order
to yield effluent ammonia levels less than 2 to 4 mg/L. When the BOD loading
is expressed on a volumetric basis (Figure 6-6), the variability is reduced.
-------
0.03
O.04 O.OG 008 O.I
02. Q3 O.4 0.6 0.8 1.0
2.0
BOD- Removal Rate (IbsVd-1000ft2)
5
LEGEND ••
O
A
O
V
O
X
(l3-l6ee)
PALM SPRINGS
WAUCONDA (l7-2l°c)
ASHLAND (17-22° c) _
(!7-20°c) O (8-l5°c)
(I7-I8°C) V (I0-I40e)
(I7-I9°C)
CIBOLO CREEK- A (20-:
CIBOLO CREEK- B (20-27°c)
CIBOLO CREEK- C ( 20- 27°c)
CHEMUNG COUNTY ( Il-I6°c)
AMHERST
BREMEN
ALLENTOWN
FIGURE 6-1.
RATIO OF NH3-N REMOVED TO BOD REMOVED AS A FUNCTION OF THE BOD REMOVAL RATE
-------
C i i i i
— ' o o 6 —
CM CM » -
< CD U
••• ^— w rj
UJ Ul 111 o
Q£ fiC O-
^_ U U U
o
o q q
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o u u *> u
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w
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w
w
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O
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ED
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-------
Effluent
BOD5
(mg/L)
Q25 0.5 0.75
BOD Loading (Ibs./d-1000 ft2 media area)
1.0
LEGEND *
o
A
a
O
x
PALM SPRINGS
WAUCONDA (!7-2lec)
ASHLAND
AMHERST
BREMEN
• (Il-I6°e)
(17-22° e) A (l3-l6°e)
(!7-20ee) • (8-l5°c)
(I0-I4°c)
(Il-I6ee)
(I7-I80C)
ALLENTOWN (17- I9°e)
CIBOLO CREEK- A (20-27ec)
CIBOLO CREEK- B (20-27ec)
CIBOLO CREEK- C ( 20- 27°c)
CHEMUNG COUNTY ( Il-I6°e)
FIGURE 6-3.
EFFLUENT BOD5 CONCENTRATION AS A FUNCTION OF THE MEDIA AREA BOD LOADING
-------
10
CM
•* Nr
CM i ~
•s
O
10
O
o
o
.
• • , H
x x * Z
111 til UJ o
W III in o
5 « «
C
C
6
X CIBOLO
* CIBOLO
t CIBOLO
4 CHEMU
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o e e
o
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+• O O O DO
O
M
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o
o
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H
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H
O
U
§
o
H'
H
W
O
&
O
o
PQ
H-
E5
W
-------
12.5-
Effluent
NH3-N
(mg/L) 7.5.
O Q25 0.5 0.75
BOD Loading (Ibs./d-1000 ft2 media area)
LEGEND'
1.0
+ PALM SPRINGS
O WAUCONDA (l7-2l°c)
(17-22° c)
(I7-20°C>
A ASHLAND
O AMHERST
V BREMEN
O ALLENTOWN
X CIBOLO CREEK-A (20-27°c)
•K CIBOLO CREEK- B (20- 27°c)
t CIBOLO CREEK- C ( 20-27°c)
• CHEMUNG COUNTY ( Il-I6°c)
A (!3-l6°c)
IB (8-l5°e)
€1
FIGURE 6-5.
EFFLUENT AMMONIA-NITROGEN CONCENTRATION AS A FUNCTION OF BOD MEDIA
SURFACE LOADING
-------
IO
o
o
o
•
o
0
o o o *rj
° * 9 o
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i i i i
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m
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' i i '
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e
§5
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Ul g
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•i- O <3 D D>O
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s
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pq
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H
O
&
Fn
S
O
M
EH
-------
• Page 6-20
This also shows that the BOD loadings need to be less than 10 lbs/1,000 ft3 for
effective ammonia removal. .
These loadings conform to those suggested by the USEPA Process Manual for
i
Nitrogen Control (1975), which -recommends an organic loading of 10' to 12 Ibs
BODs/1,000 ft3-d for nitrification in a single-stage trickling filter. On an
areal basis, the USEPA design loadings are O-.l to 0.3 lbs/1,000 ft2-d,
depending on temperature and effluent targets (see Figures 4-1 and 4-2). These
compare favorably to the loadings suggested on Figure 6-5.
The effect jf hydraulic loading is shown on Figure 6-7, which^presents the
effluent ammonia level as a function of the hydraulic loading (gallons per day
per ft2 of reactor cross-sectional, area), including recycle. Most plants
practice recycle; and it is recommended by the EPA (1975) at a rate of
approximately 100 percent Q for adequate media wetting.
The Wauconda plant is the lowest hydraulically loaded plant and does not
practice recycle. Amherst does not recycle, but has a relatively high
hydraulic loading of 500 to 600 gpd/ft2. Ammonia levels in this case range
between 1.5 and 3.5 mg/L, with applied ammonia levels similar to Wauconda. The
i
Cib'olo Creek plants all practice recirculation at relatively high rates, with
the lowest ammonia levels accomplished through the second stage. Hydraulic
loadings in these plants range from 1,000 to 1,600 gpd/ft2.
Overall, recirculation is beneficial to trickling filter performance
lowering the applied concentrations, assuring uniform surface wetting
(particularly in the lower depths) and helping to control filter flies and
predators. These is no clear indication of optimum rates from the data in
Figure 6-7, although ratios in the order of 1 to 3 would appear to be adequate.
A review of the plant data on the basis of hydraulic loading and applied
ammonia-nitrogen concentrations do not compare favorably with the design
figures proposed by Gullicks and Cleasby (1986) (Figures 4-3 and 4-4). The
removals (Ibs NH3-N/1.000 ft2-d) observed at the plants are typically 20 to 50
percent of the teinovals that would be suggested from Figures 4-3 and 4-4, for
similar conditions In all cases, the applied hydraulic loadings were at the
-------
8
!
[
b
^o
< t—
H 2
CO <
«• >
z —
1/5 U.
a 5
^i 2
cr
UJ
.< 0
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o:
^ (+5>\ •- ° 4+
I—
O
Z
© . , . T
^ O 0 O -
3 CM M W ~
o ' • ** "— ~ ~
.£ < CD 0 >.
«"-* 1 1 ! K
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o _ uj UJ uj 5
8O> uj ui w o
_ C a K K
=0 ° ° ° o
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o 2-1-15
-> iis|
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.- x *«- •
8 1
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>> 0 0 0 ° 0
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= eci ^ =
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?_ Yvj O «D 9*
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5 •• ^ ^ t t t
O
-------
. ! Page 6-22
' - * ' f '
low end of the'curves (400 to 1,200 gpd/ft2, or 0.2 to 0.6 L/S-m2), or below it
(less than 400 gpd/ft or 0.2 L/S m2).
-------
Page 7-1
I SECTION 7 .
i - -- - i
. i ; ' REFERENCES ,
A Literature Search and ; Critical Analysis of Biological Trickling Filter
Studies, 1971, U.S. Environmental Protection Agency, 17050 DDY 12/71, Vol I &
Boiler, M. and W Guyer. 1986. Nitrification in Tertiary Trickling Filters
Followed by Deep -Bed Filters. Water Research, Vol. 20, No. 11, pp. 1,363-
1,373.
Buddies, A.G. and S.E. Richardson. 1973. Application of Plastic Media
Trickling Filters for Biological Nitrification Systems. Office of Research and
Monitoring, U.S. Environmental Protection Agency, (Washington, D.C.) EPA-
R2-73-199. |
Gujer, W. and M. Boiler. 1986. Design of a Nitrifying Tertiary Trickling
Filter Based on Theoretical Concepts. Water Research, Vol 20, No. 11, pp.
1,353-1,362.
Gullicks, M.A. and J.L. Cleasby. 1986. Design of Trickling Filter
Nitrification Towers. Journal Water Pollution Control Federation, Volume 58,
1 ' - "
Number 1, pp. 60-67.
Hall, J.D. 1986. Nitrification Options Evaluated Using Pilot Filters.
Journal Water Pollution Control, Vol. 85, pp. 431-439.
t <*.
Huang, J.M., Y.C. Wu and A. Molof. 1983. Nitrified Secondary Treatment
Effluent by Plastic-Media Trickling Filter. National Technical Information
Service. AD-P000764/1.
-------
• ; Page 7-2
A :
Jenkins, C.R., G.K. Bissonnette, P.B. Huff and G.W. Gillespie. 1980.
Application of the Aerobic-Media Trickling Filter to Nitrogen Control in
Wastewater Treatment, National Technical Information Service, PB81-118762.
Matasci, R.N., C. Kaempfer and J.A. Heidman. 1986. Full-Scale Studies of the
Trickling Filter/Solid Contact Process. Journal Water Pollution Control
Federation, Volume 58, No. 11, pp. 1,043-1,049.
Matasci, R.N., D.L. Clark, J.A. Heidman, D.S. Parker, B. Petik and D. Richards.
1988. Trickling Filter/Solids Contact Performance With Rock Filters at High
Organic Loadings. Journal Water Pollution Control Federation, Volume 61,
Number 1, pp. 68-76.
Municipal Wastewater Conveyance and Treatment. September 1988. Technological
.Progress and Emerging Issues, USEPA.
Norris, D.P., D.S. Parker, M.L. Daniels and E.L. Owens. 1982. High Quality
Trickling Filter Effluent Without Tertiary Treatment. Journal Water Pollution
Control Federation, Volume 54, Number 7, pp. 1,087-1,098.
Okey, R.W. and O.E. Albertson. 1989. Diffusion's Role in Regulating Rate and
Masking Temperature Effects in Fixed-Film Nitrification. Journal of Water
Pollution Control Federation, Volume 61, Number 4, pp. 500-509.
Okey, R.W. and O.E. Albertson. 1989. Evidence for Oxygen-Limiting Conditions
During Tertiary Fixed-Film Nitrification. Journal Water Pollution Control
Federation, Volume 61, Number 4, pp. 510-519.
Parker, D.S. and T. Richards. 1986. Nitrification in Trickling Filters.
Journal Water Pollution Control Federation, Vol. 58, No. 9, pp. 896-902.
Parker, D.S.', M. Lutz, R. Dahl and Bernkopf. 1989. Enhancing Reaction Rates
in Nitrifying Trickling Filters Through Biofilm Control. Journal Water
Pollution Control Federation, Vol. 61, No. 5, pp. 618-631.
-------
! • Page 7-3
Paulson, C. 1989. (September) 'Nitrification for the 90s. Water/Eng. and
Mgmt.
Pierce, D.M. 1978. Upgrading Trickling Filters, U.S. Environmental Protection
Agency, 430/9-78-004. '• '
Process Design Manual for Nitrogen Control. 1975. U.S. Environmental
Protection Agency - Technology Transfer.
Reed. S.C., C.J. Diener and P.B. Weyrick. 1986. Nitrogen Removal in Cold
Regions Trickling Filter Systems. National Technical Information Service, AD-
A167118/9/XAB. :
Richards T. and D. Reinhart. 1986. Evaluation of Plastic Media in Trickling
Filters. Journal Water Pollution Control Federation, Vol. 58, No. 7, pp.
774-783.
Stenquist, R.J. , D.S. Parker and T.J. Dosh. 1974. Carbon Oxidation-
Nitrification in Synthetici Trickling Filters. Journal Water Pollution Control
f -
Federation, Vol. 46, No. 10, pp. 2,327-2,339.
Trickling Filter/Nitrification - A Regional Assessment. January 1988. U.S.
Environmental Protection Agency, Region V Report.
Upton, J. and D. Cartwright. 1984. Basic Design Criteria and Operating
Experience of a Large Nitrifying Filter. Wat. Pollut. Control, Vol. 83, No. 3,
pp. 340-48.
-------
-------
APPENDIX A
SUMMARY DESCRIPTION OF NITRIFYING
TRICKLING FILTER PLANTS
1. KENDALLVILLE, INDIANA
2. AMHERST, OHIO
3. YOUNGSTOWN, OHIO
4. ALLENTOWN, PENNSYLVANIA
5. ROCHESTER, INDIANA
6. ASHLAND, OHIO
7. PICKERINGTON, OHIO
8. LANDSDALE, PENNSYLVANIA
9. WAUSEON, OHIO
10. BUCKEYE LAKE, OHIO
11. CEDAR RAPIDS, IOWA
12. STOCKTON, CALIFORNIA
13. WAUCONDA, ILLINOIS
14. CIBOLO CREEK, TEXAS
15. PALM SPRINGS, CALIFORNIA
16. BREMEN, INDIANA
17. CHEMUNG COUNTY, NEW YORK
18. READING, PENNSYLVANIA
19. LAPORTE, INDIANA
20. BOULDER, COLORADO
21. SUNNYVALE, CALIFORNIA
22. RENO, NEVADA
23. EAST MONTGOMERY COUNTY, OHIO
24. OZARK, ALABAMA
25. NEW PROVIDENCE, NEW JERSEY
-------
-------
1. KENDALLVILLE, INDIANA !
Contact:
Phone:
Treatment Process:
APPENDIX A ,
Rick McGee
(219) 347-1362 •
Two stage trickling filter - biotower combination.
Wastewater treatment works include comminutors, preaerated grit chambers,
primary clarification, three trickling filters in parallel, secondary
clarification and a biotower.
Comments:
Nitrification is reported to be taking place in the second stage biotower.
Sampling is done on the influent and final effluent. Some data is available for
first stage effluent.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BODs, rog/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling:
6. Trickling Filters I
Number of Units:
Series/P irallel: ;
Diametei of Each Filter, Feet:
Depth of Rock Filter, Feet:
Depth of Plastic Filter, Feet:
2.68
6.0
1.4
2.2
300-400
160-180
7-9
10
5
< 1
15
15
2
Daily, Composite
3 (2 Rock Media,
1 Plastic Media)
Parallel
80
5.5
6.5
-------
Page 2 '
7. Biotower
Number of Units:
Diameter, Feet:
Depth, Feet:
Media Type:
1
80
24
Plastic, Dense Cross Flow
2. AMHERST, OHIO
Contact:
Phone:
Treatment Process:
Danny Damyan
(216) 988-4920
Two trickling filters in series without intermediate
clarifier.
Wastewater treatment works include screen, preaerated grit chamber, primary
clarification, two trickling filters in series, final clarification and
chlorination:
Comments:
Nitrification is reported to be affected during very cold temperatures. Data
is available for influent and effluent ammonia levels. Frequency of sampling is
three times a week.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
2
4
2.03
2.25
100
150
13.68
< 10
6-8
3 (Winter)
1.7 (Summer)
4. Permit Requirements,
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
10
12
3 (Summer,
6 (Winter,
max 7 Day Average)
max 7 Day Average)
-------
Page 3
5. Frequency of Sampling
6. Trickling Filters
Number of Units:
Series/Parallel:
Intermediate Clarifier:
i Size of Each Unit, ft2:
Depth, Feet:
Media Type:
Not known
2
Series
No
40 x 90 (Rectangular)
17
Plastic, Cross Flow
3. YOUNGSTOWN, OHIO
Contact:
Phone:
Treatment Process:
Larry Gurlea
(216) 742-8820
Single-stage trickling filter with activated
sludge process.
Wastewater treatment works include bar screen, two grit chambers, primary
clarification, four trickling filters in parallel,, activated sludge process,
secondary clarification, microscreen, cascade aeration and chlorine contact
tank.
Comments:
Most of the nitrification is reported in the trickling filter. Composite
samples for ammonia are taken daily. Effluent ammonia levels are temperature
dependent.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd/:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BOD5, mg/L: '
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BOD5, mg/L: ,
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
35
90
20-30
60-65
115
250
8-10
3-5
5-10
0.31
12 (summer), 25 (winter)
20 (summer), 30 (winter)
3 (summer), 15 (winter)
-------
Page 4
5. Frequency of Sampling:
6. Trickling Filters
Number of Units:
Series/Parallel:
Diameter of Each Filter, Feet:
Depth of Each Filter, Feet:
Media Type
Once/Day (Composite)
Parallel
100
16
Plastic, Cross Flow
4. ALLENTOWN,-PENNSYLVANIA
Contact:
Phone:
Treatment Process:
Peter Schwenzer
(215) 437-7682
Two - stage trickling filter.
Wastewater treatment works include bar screen aerated grit chamber, 4 primary
settling tanks (usually 3 in operation) , 4 high rate trickling filters in
parallel, intermediate clarification, second stage trickling filters, final
clarification and chlorination.
Comments ;
Data is available for raw influent, primary clarifier effluent, intermediate
clarifier effluent and final effluent. :
Salient Features :
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BODs, in§/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling:
40
32.87
78
261
190
17
12
11
4.7-5.9
30
30
3 (summer), 9 (winter)
I
Once/day, (Composite)
-------
Page 5
6. Trickling Filters •
Number of Stages:
Number of Units in First Stage:
Series/Parallel:
Diameter of Each Unit, Feet:
Depth of Each Unit', Feet:
Media Type:
Number of Units in Second Stage;
i Size of the Unit, Area,
Depth of the Unit, Feet:
Media Type:
Two
4
Parallel
100
32
Plastic, Vertical
1
348492
8
Rock
5. ROCHESTER, INDIANA
Contact:
Phone:
Treatment Process.
Herb Corn
(219) 223-3485
Three - stage trickling filter/biotower combination.
Wastewater treatment works include comminutor, 2 primary clarifiers, 1 first
stage trickling filter, 3 first stage clarifiers, 1 second stage trickling
filter, 2 second stage clarifiers, 1 biotower, final clarifier, and chlorination.
Comments:
Effluent ammonia is consistently less than 1 mg/L.
Salient Features: ;
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
! BOD5, mg,/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
CBODs, mg/L:
Suspended Solids, ing/L:
' Ammonia Nitrogen, mg/L:
1.65
2.48
0.8 to 0.93
1.5
340-1,000
220-380
22
12
21
0.6
25
30
6 (summer), 12 (winter)
-------
Page 6
6. Trickling Filter/biotower:
Number of Stages:
Number of Units in Each Stage:
First Stage:
Type of Unit:
Diameter, Feet:
Depth, Feet:
Media Type:
Second Stage:
Type of Unit:
Diameter, Feet:
Depth, Feet:
Media Type:
Third Stage:
Type of Unit:
Diameter, Feet:
Depth, Feet:
Media Type':
3
1
Trickling Filter
80
6
Rock
Trickling Filter
80
6
Rock
Biotower
80
18
Plastic, 60°C Crossflow,
42
6. ASHLAND, OHIO
Contact:
Phone:
Treatment Process•
Bob Sweinheart
(419) 281-7041
Single - Stage trickling filter with solids contact
process.
Wastewater treatment works include screen, preaeration, grit chamber, primary
clarifier, two biotowers in parallel, solids contact tank, final clarifier and UV
disinfection.
Comments:
Plant data shows very good nitrification efficiency during summer and fall.
Nitrification efficiency is affected during the winter months.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5
10
2.96
4.5
146
185
14.2
-------
Page 7
3. Effluent Characteristics,
BOD5> mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling:
6. Trickling Filters .
Number of Units:
Series/Parallel:
Diameter of Each Filter, Feet:
: Depth of Each Filter, Feet:
Media Type:
6
7
1-2
10
10
2,
11,
30. days avg. (summer)
30 days avg: (winter)
3 times/week (composite)
Parallel
80
30
Plastic, Crossflow
7. PICKERINGTON, OHIO
Contact:
Phone:
Treatment Process:
Jerry Styler
(614) 837-6470
Trickling filter with aeration tank.
Wastewater treatment works include screen, grit removal, one trickling
filter, two aeration tanks, two solids contact clarifiers with flocculation zone,
chlorination and dechlorination. ^
Comments:
Samples for ammonia are taken once a month as per permit requirement. Data on
ammonia nitrogen is available for influent and final effluent.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3 . Effluent Characteristics ,
CBODs, mg/L:
Suspended Solids, mg/L:
; Ammonia Nitrogen, mg/L:
0.58
2.03
0.5
1.6
200
200
18
< 2
6
0.11
-------
Page 8 '
4. Permit Requirements,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling:
6. Trickling Filters .
Number of Units':
Depth of Each Filter, Feet:
Media Type:
10
12
1.5 (summer), 4.0 (winter)
Once/Month (Composite)
1
27
Plastic Crossflow (60R)
8. LANDSDALE, PENNSYLVANIA
Contact:
Phone:
Treatment Process:
Dan Shinski
(215) 361-8362
Activated sludge process with '.nitrification tower
and denitrification basin.
Wastewater treatment works include bar screen, comminutor, aerated grit
chamber, equalization basin, activated sludge process, secondary settling, two
trickling filters in parallel, final clarifier, denitrification basin and
chlorination.
Comments;
Most of the nitrification takes place in the first stage activated sludge
process. Cold weather appears to affect nitrification. Composite samples for
ammonia are taken three times a week.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
CBODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
2.5
4.0
2.4
4.0
100
125
15
< 5
< 5
0
22 (winter), 11 (summer)
30
1.9 (summer), 5.7 (winter)
-------
Page 9
5. Frequency cf Sampling:
6. Trickling Filters
: Number of Units:
i Series/Parallel:
Diameter of Each Filter, Feet:
Depth of Each Filter, Feet:
Media Type:
3 Times/Week (Composite)
Parallel
65
20
Plastic, vertical '
9. WAUSEON, OHIO
Contact:
Phone:
Treatment Process:
Leon Smith
(419) 335-3026
Single - stage trickling filter with solids contact
process.
Wastewater treatment works include bar screen, aerate grit channel, two
primary clarifiers, two trickling filters in parallel, two solids contact
aeration channels, two flocculating final clarifiers, chlorination and
dechlorination.
Comments: .
Detention time in the solids contact process is approximately one hour. Most
of the nitrification takes place in the trickling filter. Grab samples for
ammonia nitrogen are taken three times a week.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
: Current Peak Daily Flow, mgd:
,2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
i Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BOD5, mg/L:
I Suspended Solids, mg/L:
i Ammonia Nitrogen, mg/L:
5. Frequency of Sampling:
1.5
0.9
3
150
215
18
< 10
< 15
5
15
17
1.5 (summer), 4.0 (winter)
3 Times/Week (Grab)
-------
Page 10
6. Trickling Filters
Number of Units:
Series/Parallel:
Diameter of Each Filter, Feet:
Depth of Each Filter, Feet:
Media Type:
7. Solids Contact Process
Solid Contact Time, Min.:
Solids Retention Time, Days:
10. BUCKEYE LAKE, OHIO
Parallel
75
14
Plastic, Crossflow
60
< 2
Contact:
Phone:
Treatment Process
Single - Stage trickling filter with solids contact
process.
Was tewater treatment works include comminutor, two primary clarifiers, two
trickling filters in parallel, solid contact tank, air flocculation and two
secondary clarifiers .
Comments : •
Solids contact process incorporated to assist in the settling of suspended
solids. Sampling for ammonia nitrogen is done for the influent and final
effluent.
Salient Features: .
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
1.1
2.6
0.8-0.9
2.6
105
106
40
< 2
5
0.1-0.3
15 (summer), 25 (winter)
20 (summer), 30 (winter)
3 (summer), no requirement
for winter
-------
Page 11 .
5. Frequency of Sampling: - 3 Times/Week'
6. Trickling Filters
Number of Units: 2
Series/Parallel: Parallel
'] Diameter of Each Filter, Feet: 45
Depth of Each Filter, Feet: 42
Media Type: Crossflow Plastic
7. Solids Contact Process
Current Solid Contact Time, Min.: 71
Solids Retention Time, Days: < 2
11. CEDAR RAPIDS, IOWA
Contact: Pat Ball
Phone: (319) 398-5286
Treatment Process: Single - Stage roughing filter with two - stage
activated sludge process.
Wastewater treatment works include primary clarification, four high rate
trickling filters in parallel, two stage activated sludge process, final
clarification and chlorination.
Comments:
Nitrification efficiency of the roughing filter appears to be greatly
affected by organic loading and ambient temperature.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd: 42
Design Peak Daily Flow, mgd: 65
Current Average Daily Flow, mgd: 35
Current Peak Daily Flow, mgd: 46
2'.. .Influent Characteristics,
CBODs, mg/L: 300
Suspended Solids, mg/L: 430
Ammonia Nitrogen, mg/L: 20
3>. Effluent Characteristics,
BODs, mg/L: 5
Suspended Solids, mg/L: 17
Ammonia Nitrogen, mg/L: < 1 0.5
4. Permit Requirements,
BOD5, mg/L: 30
Suspended Solids, mg/L: 30
Ammonia Nitrogen, mg/L: 7.5
-------
Page 12
5. Frequency of Sampling:
6. Trickling Filters
Number of Units:
Series/Parallel:
Diameter of Each Filter, Feet:
Depth of Each Filter, Feet:
Media Type:
Once/Day (Composite)
4
Parallel
140
24 |
Plastic, Vertical;
12. STOCKTON, CALIFORNIA
Contact:
Phone:
Treatment Process:
Tim Anderson
(209) 944-8734
Single - stage roughing filter with oxidation pond.
Wastewater treatment works include primary clarification, 3 trickling filters
and 3 biotowers in parallel, oxidation pond, chlorination and dechlorination
tanks. During summer, effluent from oxidation pond is further treated by DAF
units and dual media filters before chlorination.
Comments;
During winter and fall, oxidation pond effluent is discharged after
chlorination and dechlorination. In summer, effluent from oxidation pond is
further treated by DAF units and dual media filters.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4 . Permit Requirements ,
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
42
64
28
72
300-900
350-500
25
20-30
10
17 ; " -
10 (Secondary Effluent)
30
10
None
-------
Page 13
5. Frequency of Sampling:
6. Trickling Filter/Biotower:
' Total Number of Units:
Series/Parallel: ,
Diameter of each T. Filter, Feet:
Depth of Each.T. Filter, Feet:
Diameter of Each Biotower, Feet:
' Depth of Each Biotower, Feet:
Media Type in Each Biotower:
5 Days/Week
6: 3 Trickling Filter,
3 biotowers
Parallel
150
4
150
22
Plastic, Vertical
13. WAUCONDA, ILLINOIS
Contact:
Phone:
Treatment Process:
Mark Dierker
(312) 526-9612
Single - stage biotower with solids contact process,
Wastewater treatment works include aerated grit tank, comminutor, two primary
clarifiers, two plastic media trickling filters in parallel, aerated solids
contact tank with flocculation chamber, two intermittent sand filters and
chlorination.
Comments:
No problem is reported with nitrification during winter.
Salient Features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Design Peak Daily Flow, mgd:
Current Average Daily Flow, mgd:
Current Peak Daily Flow, mgd:
21. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
A. Permit Requirements,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
1.4
0.7
2.0
163
145
10-15
< 10
< 5
0.05-0.1
10
12
1.4, 30 day average (summer)
4, 30 day average (winter)
-------
Page 14
5. Frequency of Sampling:
6. Trickling Filters
Number of Units:
Series/Parallel:
Diameter of Each Filter, Feet:
Depth of Each Filter, Feet:
3 Times/Week (Composite)
Parallel
50
28
14. CIBOLO CREEK, TEXAS
Contact:
Phone:
Treatment Process:
Roy Bingham
(512) 658-6243
Two - stage high rate trickling filter plant.
Three separate wastewater treatment streams. Each stream consists of one
primary clarifier, one first stage trickling filter, one intermediary clarifier,
one second stage trickling filter, one final clarifier, dual media sand filter
and chlorine contact chamber.
Comments:
Effluent ammonia levels are consistently below 5 mg/L.
Salient Features:
1. Wastewater Flows,mgd:
Design Average Wastewater Flow,
(from 3 plants combined)
Design Peak Wastewater Flow,
(from 3 plants combined)
Current Daily Average Flow
(from 3 plants combined)
Current Daily Maximum Flow
(from 3 plants combined)
Plant A treats 29% of the total flow
Plant B treats 16% of the total flow
Plant C treats 55% of the total flow
2. Influent Characteristics
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics:
CBODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
6.2
16
2.23
3.3
190
180
25
< 5
< 5
< 5
-------
Page 15
4. Permit Requirements:
1 CBODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling:
6. Trickling Filters
a. Plant A
Number of Units:
Series/Parallel:
Intermediary Clarifier:
: Diameter of Each Filter, Feet:
Depth of First Filter, Feet:
Depth of Second Filter, Feet:
Media Type of First Filter:
Media Type of Second Filter:
b. Plant B
Number of Units:
Series/Parallel:
Intermediary Clarifier:
Diameter of Each Filter, Feet:
Depth of Each Filter, Feet:
Media Type of First Filter:
Media Type of Second Filter:
c. Plant C
Number of Units:
Series/Parallel
Intermediary Clarifier:
Diameter of Each Filter, Feet:
Depth of First Filter, Feet:
Depth of Second Filter, Feet:
Media Type of Each Filter:
15. PALM SPRINGS, CALIFORNIA
Contact:
Phone:
Treatment Process:
10
15
6 (If flow is < 4 mgd)
4 (If flow is > 4 mgd)
5 Days/Week (Effluent)
2 Days/Week (Influent)
2
Series
Yes
55
8
7
Plastic, 32 sq. ft./cu. feet
Plastic, 64 sq. ft./cu. feet
2
Series
Yes
55
7
Plastic, 32
sq. ft./cu. feet
Plastic, 64 sq. ft./cu. feet
2
Series
Yes
82
16
12
Plastic, alternate layers of
vertical (27 sq. ft./cu. ft/)
and cross flow (48 sq. ft./cu.
ft)
Andy Fisichelli
(619) 323-8166
Single - stage trickling filter.
The wastewater treatment works consist of bar screen, aerated grit chamber,
primary clarification, four high rate slag media trickling filters in parallel
employing 1:1 recirculation, secondary clarification, sludge thickener, and
-------
Page 16
anaerobic sludge digester. The secondary effluent is either disposed through
percolation ponds for eventual recharge to the natural underlying aquifer or
directed to the tertiary treatment system for irrigation reclamation usage.
Comments: :
Effluent ammonia levels are reported to be less than 1 mg/L. No major problem
reported with the operation of the trickling filters and nitrification.
Salient features:
1. Wastewater Flows,
Design Average Flow, mgd:
Design Peak Flow, mgd:
Current Average Flow, mgd:
Current Peak Flow, mgd:
Daily minimum, mgd:
2. Influent Characteristics:
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics:
4.
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
Permit Requirements:
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling ,(NH3-N)
Influent:
Effluent:
6. Trickling Filters
Number of Units:
Series/Parallel :
Diameter of each, ft. :
Depth of each , f t . :
Volume cf each, cf :
Organic loading # BOD/day/1 , 000 cf:
Hydraulic loading with recirculation,
gpd/sq. ft.
Type of media:
10.9
21.8
7.53
9.71
6.17
153
123
9-15
7
9
0.5
30
30
None
Once/week (Composite)
Once/week (Composite)
4
Parallel
140
9.5
146,167
23.2
354
Slag
-------
Page 17
16. BREMEN, INDIANA
Contact:
Phone:
Treatment Process:
Bill Reed
(219) 988-4920
Two - stage biotower/trickling filter combination.
Wastewater treatment works consist of primary sedimentation, two plastic
media biotowers in parallel, intermediate clarifier, rock media trickling filter,
final clarifier, rapid sand filter and chlorine contact tank. The plant is
required to meet effluent NH3-N limits of 6.0 mg/L in summer and 9.0 mg/L in
winter.
,Comments:
Nitrification is reported in the first stage biotower.
Salient Features:
jl. Wastewater Flows,
Design Average Flow, mgd: 1.3
Current Average Flow, mgd: 1.1
Current Peak, mgd: 2.2
2. Influent Characteristics,
BODs, mg/L 125
Suspended Solids, mg/L: 154
Ammonia Nitrogen, mg/L: 8.8-10.7
3. Effluent Characteristics,
BODs,mg/L: <1°
Suspended Solids, mg/L: <10
Ammonia Nitrogen, mg/L: 1.1-2.7
4. Permit Requirements,
BOD5, mg/L: 10
Suspended Solids, mg/L: 10
Ammonia Nitrogen, mg/L: 6 (summer)
9 (winter)
f- !
5. Frequency of Sampling (NH3-N)
Influent: Daily
Secondary Effluent: Daily
Trickling Filter Effluent: Daily
6. Biotowers
Number of Units: 2
Parallel/Series: . Parallel
Diameter of each, feet: 35.5
Depth of each, feet: 32.0
Hydraulic Loading, gpd/s.f.: 0.77
Organic Loading, Ibs. BOD/1000 cf: 20.0
-------
Page 18
Recirculation Ratio: . ' 0.8:1
Type of media: Plastic
Specific Surface Area of Media: 29-40 sf/cf.
7. Trickling Filter . •
Number of Units: 1
Diameter, ft. : 60.0 .
Depth, -ft. : 6.0 . ...
Type of Media: Rock
Design Hydraulic Loading, gpd/cf: 76 @ 900 gpm
17. CHEMUNG COUNTY, NEW YORK
Contact: Dan McGovern
Phone: (607) 733-1837
Treatment Process: Two trickling filters in series without intermediate
clarification. '
Wastewater treatment works consist of comminutor, bar screen, aerated grit
chamber, primary clarification, two rock media trickling filters in series,
secondary clarification, post aeration tank and anaerobic sludge digester.
Comments : Effluent ammonia is temperature dependent. Data on Influent ammonia
is available since October, 1989.
Salient Features
1. Wastewater Flows,
Current Average Flow, mgd: 5.8
Current Peak, mgd: 12 .
2. Influent Characteristics ,
BODs, mg/L: 66-136
Suspended Solids, mg/L: 120-150 ;
Ammonia Nitrogen, mg/L: 6.5-15.6
3. Effluent Characteristics,
BODs, mg/L: 10
Suspended Solids, mg/L: 8-12
Ammonia Nitrogen, mg/L: 5.4
4. Permit Requirements.
BODs, mg/L: . 25
Suspended Solids, mg/L: 30
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling (NH3-N)
Influent: Twice/week (Composite)
Effluent: Twice/week (Composite)
-------
Page 19
Trickling Filters:
Number of Units:
Parallel/Series:
Intermediary Clarifier:
Diameter of Each, ft.:
Depth of Each, ft..:
Hype of Media:
2
Series
No
135.0
6.0
Rock
18. READING, PENNSYLVANIA
Contact:
Phone:
Treatment Process:
Michael Rieber
(215) 223-3485
Three-stage trickling filter.
Wastewater treatment works include primary clarifier, two primary trickling
filters, two secondary trickling filters, secondary clarifier, one tertiary
trickling filter, final clarification, chlorine contact chamber, and anaerobic
sludge digestion.
Comments:
Influent ammonia is not measured. Final effluent ammonia levels are around
3.5 mg/L.
Salient features:
1. Wastewater Flows,
• Current Average Flow, mgd:
Daily Maximum Flow, mgd:
2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Jltrogen, mg/L:
4. Permit Requirements,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
20.0
40.0
400-500
600-700
20
25-30
15-20
3.5
30
30 •
5 (summer)
15 (winter)
-------
Page 20
5. Trickling Filters ' •
Total Number of Units: 5
Number of Primary Trickling Filters: 2; Series
Diameter of Each Primary T. Filter, ft.: 212
Number of Secondary T.Filter: 2; Parallel
Diameter of Each Secondary T. Filter, ft.: 212
Number of Tertiary T. Filter: 1
Diameter of Tertiary T. Filter, ft.: 154
19. LAPORTE, INDIANA
Contact:
Phone:
Treatment Process:
Alex Toth
(219) 362-2354 ;
Two-stage biotower/trickling filter combination.
Wastewater treatment facility includes screening, grit removal, primary
clarification, rotary trickling filter and fixed nozzle trickling filter in
parallel, intermediate clarifier, two biological towers in parallel, final
clarification, anaerobic sludge digestion, chlorination and dechlorination.
Comments; ,
Nitrification process appears to be seriously affected by very low ambient
temperatures. Influent ammonia is not measured.
Salient Features:
1. Wastewater Flows,
Design Average Flow, mgd:
Current Average, mgd:
Current Peak, mgd:
2. Influent Characteristics,
BOD5, mg/L:
Suspended Solids mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BODs, m6/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling
Influent:
Effluent:
7.0
3.0
4.5
100-120
128
20
8
12
2-3
30
30
2 (summer)
4 (winter)
Daily
Daily
-------
Page 21
6. Trickling Filters
Number of Units:
Series/Parallel:
Size of Fixed Nozzle Filter,
Type of Media:
Diameter of Rotary-T. Filter, ft.
Depth of Rotary T. Filter, ft.:
Type of Media:
7. Biotowers
Number of Units:
Series/Parallel:
Diameter of Each, ft.:
Depth of Each, ft.:
Type of Media:
Data Availability for NH3-N
20. BOULDER, COLORADO
Contact:
Phone:
Treatment Process:
2; 1 rotary, 1 fixed
Parallel
2 Sections, each 178 X 125
Limestone, 6 ft. deep
116.0
6.0
Synthetic, Pack-type'
Parallel
70.0
20.0
Synthetic, Pack-type
Ernie Oram
(303) 441-3259
Two-stage trickling
procejss.
filter with solids contact
Wastewater treatment works include bar screen, grit chamber, four primary
clarifiers, four trickling filters in parallel, four solids contact tank, three
secondary clarifiers, one nitrifying biotower, chlorination chamber and
dechlorination unit.
Comments:
At present only one third of the flow is nitrified; Rest is sent to the
chlorination chamber after solids contact tank.
Salient features:
1. Wastewater Flows,
Design Average Daily Flow, mgd:
Current Average Daily Flow, mgd:
2. Influent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BOD5, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
46.0
15.0
15
10
5
-------
Page 22
4. Permit Requirements,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Trickling Filters
Number of Units:
Series/Parallel:
Diameter of Each Filter, Feet;
Depth of Filter, Feet:
Media:
6. Biotower
Number of Units:
Diameter. Feet:.
Depth, Feet:
Media Type:
30
30
13 (summer) 20 (winter)
4
Parallel
48
8
Rock
1
48
16
Plastic
21. SUNNYVALE, CALIFORNIA
Contact:
Phone:
Treatment Process:
22. RENO, NEVADA
Contact:
Phone:
Treatment Process:
Comments:
Jean Willroth
(408) 730-7260
Oxidation pond with trickling filter.
Arthur Molin
(702) 785-2230
Single-stage trickling filter with activated sludge
process
Nitrification appears to be taking place in the activated sludge process.
Data on ammonia nitrogen is available for influent and final effluent only.
23. EAST MONTGOMERY COUNTY, OHIO
Contact:
Phone:
Treatment Process:
Single-stage trickling filter with solids contact
process.
Wastewater treatment works consists of flow equalization, primary
clarification with chemical addition, three trickling filters, an aerated return
sludge and contact channel, and three flocculating vacuum sweep final clarifiers.
-------
Page 23
24. OZARK, ALABAMA
Contact:
Phone:
Treatment Process:
Joe Wainwright
(205) 774-8447
Two-stage trickling filter. Comments : Each stage
has plastic media trickling filters in parallel
mode. First stage has high recycle (6:1 ) to reduce
solids build up.
1. Wastewater Flows,
Design Average Flow, mgd:
Current Average FLow, mgd:
2 . Influent characteristics ,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements
BODs, mg/L:
Suspended Solids, mg/L:
; Ammonia Nitrogen, mg/L:
5. Frequency of Sampling (NH3-N)
Influent:
Effluent:
6. First Stage Biotower:
Number of Units:
Series/Parallel:
Diameter of Each Tower, ft:
Depth of Each Tower, ft:
Recirculation:
Media:
Specific Surface Area of Media:
7. Second Stage Biotower:
Number of Units:
Series/Parallel:
Diameter of Each Tower, Feet:
Depth of Each Tower, Feet:
Recirculation:
Media:
Specific Surface Area of Media:
2
1
100-150
100-150
10-20
10
10
25
25
5
Once/Week
Once/Week
Parallel
48
20
6:1
Plastic,
Serpentine Shape
Corrugation
27 sq. ft/cu. ft.
Parallel
48
20
None
Plastic
45° Corrugation
33 sq. ft./cu. ft.
-------
Page 24
25. NEW PROVIDENCE, NEW JERSEY ! .
Contact: Dan Ranich
Phone: (201) 665-1077
Treatment Process: Two trickling filters
clarifier. "
in series without intermediate
Comments:
First trickling filter has plastic media while second one has rock media.
There is 1:1 recycle from final clarifier to the first .trickling filter.Typical
effluent ammonia levels are between 2 and 4 mg/L.
Salient Features:
1. Wastewater Flows,
Design Peak Flow, mgd:
Current Average Flow, mgd:
Current Peak Flow, mgd:
2. Influent Characteristics,
BOD5, mg/L: ,
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
3. Effluent Characteristics,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
4. Permit Requirements,
BODs, mg/L:
Suspended Solids, mg/L:
Ammonia Nitrogen, mg/L:
5. Frequency of Sampling (NH3-N)
• Influent:
Effluent:
6. Trickling Filter,
Number of Units:
Series/Parallel:
Intermediate clarifier:
Diameter of Plastic Media filter, ft:
Depth of Plastic Media Filter, ft:
Diameter of Rock Media, Filter ft:
Depth of Rock Media Filter, ft:
Recirculation:
6.0
0.8
5.0
160-200
125-175
30
2-4
16 (30 days average)
16 (30 days average)
4 (30 days average)
Once/Week
Once/Week
2 (1 plastic media)
(1 rock media)
Series
None
36
14.5
65
6
1:1
-------
APPENDIX B
PERFORMANCE AND OPERATING DATA FOR SELECTED PLANTS
TABLE B-l.
TABLE B-2.
TABLE B-3.
TABLE B-4A.
TABLE B-4B.
TABLE B-5.
TABLE B-6.
TABLE B-7.
TABLE B-8.
TABLE B-9.
TABLE B-10.
PALM SPRINGS, CALIFORNIA
CHEMUNG COUNTY, NEW YORK
AMHERST,OHIO
WAUCONDA, ILLINOIS 1987
WAUCONDA, ILLINOIS 1988
ASHLAND, OHIO
BREMEN, INDIANA
ALLENTOWN, PENNSYLVANIA
CIBOLO, TEXAS; PLANT A
CIBOLO, TEXAS; PLANT B
CIBOLO, TEXAS; PLANT C
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TABLE B-8. SUMMARY OF CIBOLO CREEfK, PLANT A PERFORMANCE DATA
i Ammonia-Nitrogen
Date
06/07/88
07/14/88
08/16/88
08/23/88
09/08/88
10/27/88
11/29/88
01/03/89
02/14/89
03/09/89
10/31/89
11/16/89
Process
Flow
0.74
0.66
0.67
0.65
0.59
0.65
0.64
0.66
0.63
0.62
0.61
0.60
Primary
Effluent
Cmg/LI
19.0
18.5
20.0
19.3
19.5
21.0
24.0
20.3
19.7
21.5
23.0
19.6
1st Stage
Effluent
fntz/LI
8.3
14.1
11.3
12.6
13.4
14.7
15.1
6.3
7.5
8.4
12.0
2.5
2nd Stage
Effluent
fme/L')
1.6
4.8
2.9
3.1
5.7
6.4
5.2
0.2
0.2
0.6
1.9
1.1
Primary
Effluent
(me/I/)
69
93
79
87
84
84
64
88
97
101
46
55
BODq
1st Stage
Effluent
Cmg/L')
18
28
19
29
37
34
28
26
23.
31
11
23
2nd Stage
Effluent
Cmg/L")
4.9
9.3
7.8
8.0
9.5
7.9
8.0
4.2
3.8
3.5
3.8
5.1
-------
TABLE B-9. SUMMARY OF CIBQLO CREEK, PLANT B PERFORMANCE DATA
Date
08/18/88
09/01/88
09/13/88
09/15/88
01/12/89
02/02/89
03/02/89
10/12/89
11/14/89
Process
Flow
0.36
0.36
0.35
0.34
0.36
0.35
0.34
0.35
0.34
/
Primary
Effluent
(mg/L1)
19.9
18.3
16.0
16.5
20.0
16.2
15.5
18.1
18.2
" VT *
1st Stage
• Effluent
Cme/D
7.0
7.4
6.9
5.3
7.1
1.6
7.1
4.0
4.5
ogen
2nd Stage
Effluent
(me/L1)
1.0
1.0
0.4
0.5
0.9
0.1
0.3 .
0.2
0.2
Primary
Effluent
fme/L')
64
77
55
61
101
66
81
44
55
BOD-;
1st Stage
Effluent
(mc/L)
19
23
16
19
18
17
28
11
16
2nd Stage
Effluent
Cme/L")
4.7
7.7
6.1
5.4
6.4
4.3
4.8
7.0
.4
-------
TABLE B-10. SUMMARY OF CIBOLO CREEK, PLANT C PERFORMANCE DATA
Ammonia -Nitrogen
Date
05/17/88
08/25/88
09/22/88
11/03/88
01/17/89
02/21/89
03/16/89
10/05/89
11/07/89
Process
Flow
1.27
1.30
1.29
1.19
1.19
1.19
1.24
1/22
1.18
Primary
Effluent
(me./L)
18.3
17.9
20.7
16.2
22.2
23.4
22.7
23/2
24.7
1st Stage
Effluent
fmp/L')
1.6
10.2
11.2
8.5
2.3
1.3
1.3
7.5
7.0
2nd Stage
Effluent.
Cmg/L}
0.0
1.1
1.0
0.6
0.3
0.3
0.2
0.6
0.6
Primary
Effluent
fme/L1)
97
92
84
71
104
101
100
67
56
BODs
1st Stage
Effluent
fmg/L} -
9
21
23
17
20
17
17
17
14
2nd Stage
Effluent
(me XL}
1.2
4.9
4.1
3.5
4.1
2.7
2.6
4.1
5.1
-------
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