U.S. Environmental Protection Agency
Office of Wastewater Enforcement and Compliance
Washington, D.C.
Evaluation of Oxidation Ditches
for Nutrient Removal
September, 1992
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NOTICE
Mention of trade names or commercial products does not constitute an endorsement by
EPA. Omission of certain products from this document does not reflect a position of
EPA regarding product effectiveness or applicability.
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CONTENTS
Section
OXIDATION DITCH FACT SHEET
Page
FIGURES . ........................................ ,M .-
....................... J-J-x
TABLES ............................................... . ................. iv
EXECUTIVE SUMMARY . . .................................................. ^
BACKGROUND AND OBJECTIVES .......................... .......... 1
FINDINGS AND CONCLUSIONS. . .................... '.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'. 2
.
1 THEORY OF NITRIFICATION, DENITRIFICATION AND
PHOSPHORUS REMOVAL .......................................... 1_ i
NITRIFICATION ................................. '.'.'.'.'.'.'.'."' I- 1
DENITRIFICATION .................................. '.'.'.'.'.'.'.'. 1- 2
PHOSPHORUS REMOVAL .......................... '...'.'.'.'.'.'.'.'.'.'. 1- 3
2 DESCRIPTION OF THE OXIDATION DITCH ............................ 2- 1
INTRODUCTION ........................ . ........ '.'.'.'.'.'.'.'.'.'.'.'. 2- 1
DESIGN VARIATIONS .......................... '.'.'.'.'.I'.'.'.'.'.'.'.'. 2- 3
Eimco ......... .... .................. .............. 2 - 3
Envirex ............................................. 2- 7
Innova-Tech ..................... .................... 2-10
Lakeside ............................................ 2-12
3 PERFORMANCE DATA ............................... 3. l
INTRODUCTION. ... ................... ...... ................ 3. 1
SITE OBSERVATIONS .................... '.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'. 3- 6
Thurmont, Maryland .................................. 3. 7
Fredrick, Maryland .................................. 3_10
Patuxent Water Reclamation Facility,
Crofton, Maryland ................................. 3.^4
OTHER PLANTS PROVIDING DATA ........................ ...... 3-15
Cedarburg, Wisconsin ................................ 3-15
Dousman, Wisconsin .................................. 3-17
Dupage County, Illinois ............................. 3_18
Hanover , Pennsylvania ............................... 3-19
Huntsville, Texas - Parker Creek Plant .............. 3-20
Huntsville, Texas - South Plant ..................... 3-21
Kemmerer, Wyoming ................................... 3-22
Lake Geneva, Wisconsin .............................. 3-22
Lyons, Wisconsin .............................. ....... 3-23
Morgan City, Louisiana .................. . ........... 3-24
Mount Clemens , Michigan ............................. 3.25
Rehoboth Beach, Delaware ............................ 3-25
Wanaque , New Jersey ................................. 3-26
Gwinnette County, Georgia ............... . ........... 3-27
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CONTENTS
Section
4
OXIDATION DITCH COSTS
CAPITAL COSTS
OPERATION AND MAINTENANCE COSTS.
REFERENCES.
APPENDIX A
Monthly Average Tables and Chronological Plots for Wastewater
Treatment Plants Providing Data
Gedarburg, WI
Dousman, WI
DuPage County, IL (Knollwood Plant)
Hanover, PA
Huntsville, TX (Parker Creek and South Plant)
Kemmerer, WY
Lake Geneva, WI
Lyons, WI
Morgan City, LA
Mt. Clemens, MI
Rehoboth Beach, DE
Wanaque, NJ
Yellow River/Sweetwater Creek Water Reclamation Facility,
Gwinnette County, GA
4- 1
4- 1
4- 3
5- 1
ii
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FIGURES
Figure page
* FS-1 FLOW DIAGRAM FS-4
FS-2 CONSTRUCTION AND OPERATING COSTS AND ELECTRICAL ENERGY FS-6
1A . TYPICAL CHANNEL CONFIGURATIONS FOR SINGLE CHANNEL
OXIDATION DITCH 2- 2
IB TYPICAL SCHEMATIC OF A MULTIPLE CONCENTRIC CHANNEL
OXIDATION DITCH 2- 2
2 BASIC CARROUSEL SYSTEM AND MODIFICATIONS FOR NUTRIENT REMOVAL 2-5
3 TYPICAL THREE CHANNEL ORBAL OXIDATION DITCH AND MODIFICATION
FOR NUTRIENT REMOVAL 2- 8
4 TYPICAL BARRIER OXIDATION DITCH AND DRAFT TUBE 2-11
5 TYPICAL LAKESIDE OXIDATION DITCH AND MODIFICATION FOR
NUTRIENT REMOVAL 2-14
6 CHRONOLOGICAL PLOTS OF MONTHLY AVERAGE DATA -
THURMONT, MARYLAND - JANUARY THROUGH JULY 1991 3-9
7 CHRONOLOGICAL PLOTS OF MONTHLY AVERAGE DATA -
FREDERICK, MARYLAND - JANUARY 1990 THROUGH JULY 1991 3-12
8 CHRONOLOGICAL PLOTS OF MONTHLY AVERAGE DATA -
FREDERICK, MARYLAND - JANUARY 1990 THROUGH JULY 1991 3-13
9 CHRONOLOGICAL PLOTS OF MONTHLY AVERAGE DATA - PATUXENT WATER
RECLAMATION FACILITY, CROFTON, MARYLAND - JULY 1990 THROUGH
JULY 1991 3_16
10 CAPITAL COSTS. 4. 2
11 OPERATING AND UTILITY COSTS 4. 5
ill
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Table
1
2 .
3
4
5
6
TABLES
OXIDATION DITCH SUPPLIERS CONTACTED
PERMIT LIMITS FOR PLANTS THAT PROVIDED DATA.
DESIGN BASIS FOR OXIDATION DITCH PLANTS
PERFORMANCE DATA
CAPITAL COSTS
OPERATING COSTS
Page
2- 4
3- 2
3- 4
3- 5
4- 1
4- 4
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EXECUTIVE SUMMARY
BACKGROUND AND OBJECTIVES
The U.S. Environmental Protection Agency (EPA) has encouraged the evolution
of better and more efficient wastewater treatment techniques by supporting the
application of new technologies. The Office of Wastewater Enforcement and
Compliance (OWEC) evaluates specific technologies to determine performance
capabilities and the ability of the technology to meet specific treatment
needs. This report focuses on the use of oxidation ditches for nitrification,
denitrification and phosphorus removal.
The oxidation ditch is an extended aeration, continuous flow, activated
sludge treatment process. Oxidation ditches were first used in the 1950s as an
easily operated and low cost method to treat wastewater in small towns in the
Netherlands. Oxidation ditches were first installed in the United States in
the early 1960s.(1) Since then, the number of oxidation ditches has increased
to 550 in 1975 and to more than 1800 in 1991.
Oxidation ditches were usually not designed for nitrification or
denitrification. Design parameters used, however, often ensured that
nitrification occurred. Current concern over nutrient discharges to natural
water systems has led to interest in upgrading existing oxidation ditches and
modifying the oxidation ditch system design to incorporate biological nutrient
removal.
The objective of this study was to identify oxidation ditch plants that
were achieving nutrient removal, and to obtain typical design parameters and
costs. To accomplish this, oxidation ditch manufacturers were contacted to
identify plants designed for nutrient removal. In addition, other oxidation
ditch plants were contacted to obtain information on performance of plants not
specifically designed for nutrient removal. References describing this process
and providing operational data were also utilized as informational sources.
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Page 2
This report reviews the theory of nitrification, denitrification and
biological phosphorus removal and describes the design and operation of
oxidation ditchesfor nutrient removal. Performance data on nutrient removal
from plants contacted are presented and discussed. Capital cost data obtained
are presented and analyzed with plant design flows. Operation and maintenance
costs were also obtained. The results of the study were summarized in EPA
format "Fact Sheet." The following presents the Findings and Conclusions of
the study and the fact sheet.
FINDINGS AND CONCLUSIONS
Oxidation ditches are typically designed with a nominal hydraulic detention
time of greater than 10 hours at average design flows. At typical mixed liquor
solids levels, mean cell residence time is adequate for nitrification,
especially in warm weather, if enough oxygen is supplied.
Data were collected from 17 oxidation ditch municipal wastewater treatment
plants in the United States. The average design flow for these plants ranged
from 0.1 to 12.0 mgd. Design hydraulic detention times at average design flows
ranged from 10 to 34 hours. Design mean cell residence time (sludge age) was
available for 8 of the plants and ranged from 12 to 48 days. Design organic
loadings of 13 oxidation ditches, where the information was available, ranged
from 5.8 to 39.2 Ibs BOD/day/1000 cubic feet.
Twelve of the plants contacted were designed for nitrification and five
plants were designed for denitrification. Two of the plants were designed for
biological phosphorus removal.
The average flow at the 17 plants ranged from 30 to 116 percent of the
design flow. The average effluent BOD ranged from 1.9 to 10.5 mg/1 and
removals ranged from 90 to 99 percent. All but one plant measured effluent
ammonia nitrogen (NH3-N). Influent NH3-N was measured at 14 of the plants.
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Page 3
* The average influent ammonia concentration, during all seasons where data were
available, ranged from 12.0 to 23.5 mg/1. The average effluent NH3-N
« concentration ranged from 0.05 to 2.7 mg/1. The average removal of NH3-N
ranged from 86 to 99 percent.
Four plants measured influent and effluent TKN and nitrate (N03-N)
concentrations. Of these four plants, two were designed for denitrification.
The removal of total nitrogen was 87 percent at one plant. At the second
plant, operated for denitrification during the summer, the total nitrogen
removal was 88 percent.
Influent and effluent phosphorus were measured at six plants and effluent
phosphorus was measured at one plant. Five of the plants were not designed for
biological phosphorus removal and chemicals were added. At one plant, designed
for biological phosphorus removal, the average influent phosphorus was reduced
from 2.5 mg/1 in the influent to 0.55 mg/1 in the effluent. At the other plant
designed for enhanced biological phosphorus removal, chemicals were added to
meet the permit limit of 1 mg/1.
The oxidation ditch performance data showed that nitrification occurred in
typical oxidation ditch designs. Most of the NH3-N data collected were from
the summer months, during which time permit limits were generally met. Limited
data showed that nitrification also occurred during winter months. An average
total nitrogen removal of 88 percent was achieved in the two plants designed
for denitrification when operated in this mode.
Modifications to the basic oxidation ditch design can be made to achieve
nitrogen and phosphorus removal. The key to obtaining nitrogen removal is the
proper control of dissolved oxygen levels in different sections of the
oxidation ditch, and the maintenance of adequate mass of bacteria under aerobic
9,
and anoxic conditions. To meet more stringent total nitrogen effluent limits a
separate anoxic channel or basin outside the ditch channels may be added.
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Page 4
Holding mixed liquor under anaerobic conditions is required for enhanced
biological phosphorus removal. This can be accomplished in either a non-
aerated channel or by adding an anaerobic basin before the aerobic oxidation
ditch channel.
The total capital costs, based on the information received from 10 plants
averaged $4.89/gpd design capacity. The capital costs ranged from $1.61 to
$9.99/gpd. These costs were for the entire plant and included engineering,
construction supervision and contingencies but did not include land costs.
Overall operating costs ranged from $0.08 to $1.00/gpd based on the average
flow of eight plants for which data were available. Utility costs ranged from
$0.04 to $0.16/gpd based on the average flow for seven plants for which data
were available.
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Page FS-1
OXIDATION DITCH FACT SHEET
Description - An oxidation ditch is an activated sludge biological treatment
process; commonly operated in the extended aeration mode. Typical oxidation
ditch treatment systems consist of single channel or concentric, multichannel
configurations.
Some form of preliminary treatment such as bar screens, comminutors, or grit
removal normally precede the oxidation ditch. Primary settling prior to an
oxidation ditch is sometimes practiced, however it is not common. Flow to the
oxidation ditch is mixed with return sludge from a secondary clarifier and
aerated. The aerators may be brush rotors, disc aerators, surface aerators,
draft tube aerators, or fine bubble diffusers. The aerators provide mixing and
circulation in the ditch, as well as oxygen transfer. A high degree of
nitrification occurs in the ditch due to operation in the extended aeration
mode. Oxidation ditches are typically designed with a nominal hydraulic
detention time at average design flow of greater than 10 hours and a mean cell
residence time (sludge age) ranging from 10 to 50 days. Oxidation ditch
effluent is usually settled in a separate secondary clarifier, however,
intrachannel clarifiers are also used.
Common Modifications - Ditches may be constructed of various materials,
including concrete, gunite, asphalt, or impervious membranes. Concrete is the
most commonly used. The single channel oxidation ditch may be found in a
variety of shapes including ovals, horseshoes, or ells, whichever best fits the
site. The concentric multichannel ditches may be circular or oval in shape.
The addition of an intrachannel clarifier may be incorporated into the ditch
design.
An oxidation ditch may be operated with an anoxic zone in the channel to
achieve partial denitrification. An anoxic tank upstream of the ditch may be
added along with recycle to that tank from the anoxic zone in the channel to
achieve higher levels of denitrification. A anaerobic tank may be added prior
to the ditch for enhanced biological phosphorus removal.
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Page FS-2
Technology Status r There are over 1800 municipal oxidation ditch installations
in the United States. The overall process is fully demonstrated as a secondary
treatment process. Nitrification has been shown to occur when ditches are
operated in the extended aeration mode .
Typical Equipment/No, of Manufacturers - Oxidation ditch equipment (aerators)/6
major suppliers
Applications - Oxidation ditch technology is applicable in any situation where
activated sludge treatment (conventional or extended aeration) is appropriate.
Limitations - Oxidation ditches offer an added measure of reliability and
performance over other biological processes but are subject to some of the same
limitations that other activated sludge treatment processes face.
Performance - The average performance of 16 oxidation ditch plants is
summarized below:
Effluent (rng/1)
Percent Removal
BOD
Suspended Solids
Winter
5.5
6.5
0.88
Summer
4.4
5.3
0.45
Annual Avg
4.9
5.9
0.68
Winter
98
96
95
Summer
98
98
97
Annual Avg
98
97
96
Note: Winter November through April, Summer May through October
Chemicals Required - None; metal salts can be added for enhanced phosphorus
removal .
Residuals Generated - Primary sludge if primary clarifiers precede oxidation
ditch. Secondary sludge is generated at quantities similar to other activated
sludge processes .
Design Criteria - (Extended Aeration Mode)
BOD Loading - 5 to 20 lbs/1,000 ft3 of aerated volume/day
Sludge Age - 10 to 50 days
Oxidation Ditch Hydraulic Detention Time - 10 to 35 hours
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Page FS-3
Unit Process Reliability - The following table indicates the percent of time
the monthly average effluent concentration of the given pollutants was less
than the concentration given in the first column. This table was developed
from data for 16 oxidation ditch plants.
Percent of time Effluent concentration in mg/1 Less than
Concentration Suspended Solids BOD
(mg/1) Winter Summer
0.2 0 0
0.5 0 0
1.0 2 1
2.0 7 13
5.0 49 67
10.0 82 90
20.0 97 96
Environmental Impact - Solid waste, odor and air pollution impacts are similar
to those encountered with standard activated sludge processes.
Toxics Management - The same potential for sludge contamination, upsets, and
pass through of toxic pollutants exists for oxidation ditch plants as for
standard activated sludge processes.
Winter
0
0
0
5
57
92
99
Summer
0
0 '
2
12
64
93
100
Winter
33
58
79
92
98
99
100
Summer
48
76
91
95
100
100
100
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OXIDATION DITCH
SCREENED AND
DEGRITTED
WASTEWATER
AERATOR I
ROTOR — *
RETURN SLUDGE
FINAL
CLARIFIER
EFFLUENT
EXCESS
SLUDGE
Figure FS-1. Flow Diagram
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Page FS-5
ENERGY NOTES - Assumptions:
Energy Requirements Based on:
Water Quality Influent (mg/1) Effluent (mg/1)
BOD 200 20
TKN 35 1
Design Assumptions -
Oxygen transfer efficiency — 2.5 Ib 02/bhp/hr
Nitrification occurs
Operating Parameters -
Oxygen requirement 1.5 Ib 02/lb BOD removed
4.57 Ib 02/lb TKN oxidized
Type of Energy Required - Electrical
COSTS - July 1991 dollars; ENR Index 4854. Assumptions: Construction costs are
for the entire plant but do not include land, or engineering. O&M costs
include all costs incurred in operating the plant (labor, utilities,
maintenance materials, etc)
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Figure FS-2. Construction and Operating Costs and Electrical Energy
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Page FS-7
References
Ettlilch, William F. , A Comparison of Oxidation Ditch Plants to Competing
Processes for Secondary and Advanced Treatment of Municipal Wastes., U.S.
Environmental Protection Agency, Municipal Environmental Research Laboratory,
Office of Research and Development, Cincinnati, Ohio, EPA-600/2-78-051, March
1978.
Innovative and Alternative Technology Assessment Manual, Office of Water
Program Operations, Washington, D.C. and Office of Research and Development,
Cincinnati, Ohio, U.S. Environmental Protection Agency, February 1980.
Preliminary Draft Evaluation of Oxidation Ditches For Nutrient Removal,
Prepared by HydroQual, Inc., September 1991.
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Page 1-1
SECTION 1.
THEORY OF NITRIFICATION, DENITRIFICATION AND PHOSPHORUS REMOVAL
The following sections describe the biological processes that occur
naturally in the environment and which can be encouraged to take place for
wastewater treatment.
NITRIFICATION
Nitrification is the biological oxidation of ammonia (NH4+) to nitrite
(N02~) and then to the nitrate (N03_) form. The two major species of
microorganisms responsible for the biological oxidation of nitrogen compounds
are the autotrophic bacteria Nitrosomonas and Nitrobacter. Nitrosomonas
oxidizes ammonia to nitrite. Nitrobacter completes the nitrification process
by oxidizing nitrite to nitrate.
The overall nitrification of ammonia can be expressed by the following
reaction:
NH4+ + 202 ---> N03" + 2H+ + H20
Temperature, pH, and dissolved oxygen concentration are important
parameters in nitrification kinetics. The rate of nitrification in an
activated sludge system decreases with decreasing temperature. The optimum
temperature is between 25 and 35°G. The optimum pH for nitrification is in the
range of 7.5 to 9.0. Below pH 7.0 and above pH 9.8 the nitrification rate is
y less than 50 percent of the optimum. Alkalinity is destroyed by the oxidation
of ammonia, thereby reducing the pH. A ratio of 7.14 mg alkalinity is
destroyed per mg of ammonia nitrogen oxidized. Aeration partially strips the
carbon dioxide from the wastewater thereby reducing alkalinity reduction;
however, enough alkalinity must remain in the wastewater so as not to depress
the pH. Maximum nitrification rates occur at dissolved oxygen concentrations
greater than 2 mg/1. The nitrification process consumes 4.57 Ibs of oxygen per
pound of ammonia nitrogen converted to nitrate.C2)
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Page 1-2
The nitrification rate is also dependent on the fraction of nitrifying
bacteria present in the system. A principal means of increasing the
nitrification rate is to increase the fraction of nitrifiers. This can be
accomplished by increasing the aeration basin mixed liquor suspended solids
(HLSS) concentration. Lowering the ratio between the 5-day BOD and the total
Kjeldahl nitrogen concentration (BODs/TKN) by nitrifying in a separate second
stage aeration system also increases the percentage of nitrifiers. This
increase in nitrifiers increases the nitrification rate.(2) This approach,
however, has not been found to be a cost effective design for normal municipal
wastewater. ,
DENITRIFICATION
Biological, anoxic denitrification is a process in which nitrate is reduced
to nitrogen gas by microorganisms in the absence of dissolved oxygen.
Denitrification can occur provided a sufficient source of nitrate and organic
carbon are present. The denitrification process can be expressed by the
following reaction:
NOs" + organic carbon > N2(gas) + CC>2
The denitrification process occurs in two steps. The first step involves
the reduction of nitrate to nitrite. In the second step nitrite is reduced to
produce nitrogen gas. Many species of facultative heterotrophic bacteria,
including Psuedomonas, Micrococcus, Archromobacter, and Bacillus can convert
nitrate to nitrogen gas. Nitrate replaces oxygen in the respiratory processes
of the organisms capable of denitrification under anoxic conditions,(2)
Environmental factors including temperature, pH, and dissolved oxygen
concentration have an effect on the rate of denitrification. Denitrification
occurs at temperatures in the range of 10 to 30°C. The rate of denitrification
is reduced below pH 6.0 and above pH 9.0. The optimum pH is in the range of
6.5 to 8.0. A dissolved oxygen concentration greater than 1 mg/1 inhibits
denitrification.
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Page 1-3
PHOSPHORUS REMOVAL
Phosphorus in wastewater may be present as orthophosphate, polyphosphate,
or organic phosphorus. Orthophosphate is the more easily removed of the three
types .of phosphorus. Polyphosphates are converted to orthophosphate by
hydrolysis and organic phosphorus is converted to orthophosphate through
bacterial decomposition.(3)
Conventional, secondary biological treatment systems accomplish partial
phosphorus removal by using phosphorus for biomass synthesis during BOD
removal. A typical phosphorus content of microbial solids is 1.5 to 2 percent
based on dry weight. Wasting excess biological solids with 1.5 to 2 percent
phosphorus content results in a total phosphorus removal of 10 to 30 percent.
The percent phosphorus removal is dependent on the BOD to phosphorus ratio, the
system sludge age, sludge handling techniques and sidestrearn return flows.(3)
Additional biological phosphorus removal will occur if wastewater is
subjected to both anaerobic and aerobic conditions. When an anaerobic stage
(absence of DO and oxidized nitrogen) precedes an aerobic stage, fermentation
products are produced from the BOD in the wastewater by the action of
facultative organisms. The phosphorus storing microorganisms can assimilate
the fermentation products under anaerobic conditions. Since many competing
microorganisms cannot function in this manner, the phosphorus storing
microorganisms have a distinct advantage over other organisms in the activated
sludge system. Thus, the anaerobic phase results in the development of
phosphorus storing microorganisms.(3)
The stored substrate products are depleted in the aerobic phase and soluble
phosphorus taken up by the microorganisms in quantities in excess of what is
needed to function. This "luxury uptake" of phosphorus is maximized at
dissolved oxygen concentrations greater than 2 mg/1. At lower DO
concentrations the excess phosphorus will be released from the microorganisms.
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Page 1-4
For biological phosphorus removal to occur, an anaerobic stage is required
for the production of the fermentation products. If nitrification is
occurring, a denitrification step must occur before enhanced biological
phosphorus removal. If nitrite or nitrate are present, the system is anoxic
rather than anaerobic.
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Page 2-1
SECTION 2.
DESCRIPTION OF THE OXIDATION DITCH
INTRODUCTION
The original oxidation ditch designs used in the Netherlands were earthen
ditches in a race track configuration. The modern design trend for oxidation
ditches in the United States is concrete construction in a race track
configuration. There are several configurations and modes of operation used.
The most commonly used configuration is the single channel design, but the
multiple concentric channel design is also used quite frequently.
Oxidation ditch plants generally have pretreatment before the raw sewage
enters the ditch. Pretreatment is generally bar screens, comminutors, and a
grit chamber. Primary settling prior to an oxidation ditch is sometimes
included, however, it is not common. Flow to the oxidation ditch is mixed with
return sludge from a secondary clarifier and is mechanically aerated. The
mechanical aerators may be brush rotors, disc aerators, surface aerators, draft
tube aerators, or fine bubble diffusers, depending on the design. The liquid
in the ditch typically completes a circuit every 5 to 20 minutes depending on
the channel length, flow and velocity. Effluent from the oxidation ditch flows
to secondary clarifiers for settling before discharge.
The single channel oxidation ditch may. be found in a variety of shapes
including ovals, horseshoes or ells, whichever best fits a site. The various
cdnfigurations are illustrated on Figure 1A. The concentric multichannel
design is illustrated on Figure IB. The number of concentric rings ranges from
two to five. Oxidation ditches are typically followed by a separate final
clarifier, however, one modification incorporates a clarifier in the oxidation
ditch channel.
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CIRCULAR
OVAL
ELL
HORSESHOE
Figure 1 A. Single Channel Oxidation Ditch - Typical
Channel Configurations
(Ref. 1)
TRANSFER PORTS
(between channels)
O
(Ref. 1)
Figure 1B. Multiple Concentric Channel Oxidation Ditch - Typical
Schematic
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Page 2-3
DESIGN VARIATIONS
There are many variations on the original oxidation ditch design that
incorporated brush aerators followed by a separate secondary clarifier. These
variations include different types of aeration equipment such as disc aerators,
draft tube .aerators, and surface aerators and the use of intrachannel
clarifiers. Three oxidation ditch suppliers that represent the major design
variations were contacted. Oxidation ditches similar in design to those
marketed by the three manufacturers contacted are marketed by several other
companies.
Table 1 presents the most commonly used configurations, and the aerator and
clarifier type commonly used by the manufacturers contacted. Also presented
in Table 1 are the modifications to each design for nutrient removal. The
following paragraphs describe the specific designs of the manufacturers
contacted.
Eimco
Oxidation ditches supplied by Eimco are referred to as the Eimco
"Carrousel" Oxidation Ditch System. A schematic of a typical Carrousel system
is presented in Figure 2. Information received from Eimco in June 1991
indicated that a total of 169 Carrousel systems were in operation in the United
States. The design flows of these plants range from 0.1 to 25.6 mgd. Eimco's
literature states that Carrousel plants can treat raw domestic wastewater to
advanced secondary standards without primary clarifiers or effluent fliters.(4)
Eimco traditionally has marketed the Carrousel system in wastewater treatment
applications where the effluent permit requirements were 30:30 or 20:20 as mg/1
of BODs:mg/l of TSS. Eimco has also marketed the Carrousel system for
~ applications in which partial or total nitrification is required. Carrousel
Systems have been designed to meet permit limits of 10:15:1 as mg/1 BOD5:mg/l
-" TSS:mg/1 NH3-N.(4)
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TABLE 1. OXIDATION DITCH SUPPLIERS CONTACTED
Manufacturer
Eimco
Envirex
Innova-Tech
Lakeside
Typical
Configuration Aeration Method
Racetrack Mechanical
(Carrousel) Surface Aerators
Concentric Channel Disk
(Orbal)
Racetrack Draft Tube
(Barrier
Oxidation Ditch)
Racetrack Brush Rotor
(Closed Loop
Reactor)
Clarifier
Most
Commonly Used
External
External
External
External
Nutrient
Removal
Design
System
Bardenpho
SIM-PRE
Anoxic zone
Anaerobic
basins
Modified
Ludzach-
Ettinger
Process
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-TO SECONDARY
CLARIFICATION
BASIC CARROUSEL SYSTEM
Q ».
-TO SECONDARY
CLARIFICATION
MODIFICATION OF BASIC CARROUSEL SYSTEM
FOR PARTIAL DENITRIFICATION - ANOXIC ZONE
IN CHANNEL
db-~0
1-4Q
-»-TO SECONDARY
CLARIFICATION
MODIFICATION OF BASIC CARROUSEL SYSTEM
FOR DENITRIFICATION -ANOXIC ZONE IN CHANNEL
AND UPSTREAM ANOXIC TANK
cb
MODIFICATION OF BASIC CARROUSEL SYSTEM
_ FOR DENITRIFICATION - ANOXIC ZONE IN CHANNEL
TO SECONDARY AND UPSTREAM AND DOWNSTREAM ANOXIC TANKS
(BARDENPHO PROCESS)
1-4Q
i
!
*
-O
d)
1-40
MODIFICATION OF BASIC CARROUSEL SYSTEM
FOR DENITRIFICATION AND PHOSPHORUS REMOVAL
- ANOXIC ZONE IN CHANNEL - UPSTREAM
FERMENTATION TANK AND UPSTREAM AND
DOWNSTREAM ANOXIC TANKS
(MODIFIED BARDENPHO PROCESS)
(Ref. 5)
Figure 2. Basic Carrousel System and Modifications for Nutrient Removal
-------
Page 2-6
Host of the Carrousel systems in the United States are designed to be
operated in the extended aeration mode that implies a solids retention time
(SRT) of 20 to 30 days. The long SRT's enable the system to absorb shock
hydraulic loadings, toxic shocks, and diurnal fluctuations in both quality and
quantity of incoming wastewater. These long SRT's are conducive to complete
nitrification
Aeration in the Carrousel system is provided by low speed surface aerators
mounted at turns in the racetrack configuration. Plug flow exists in the
channels between the aerators. Flow velocity is maintained in the channels by
the pumping action of the aerators. This pumping action is achieved by lining
up the partition walls with the aerators so the aerators pump mixed liquor from
the upstream channel into the aeration zone. In the aeration zone the mixed
liquor is completely mixed and forced into the downstream channel.
The aerators in the Carrousel oxidation ditch system are typically designed
for 0.4 HP per 1000 cubic feet. The power draw of the aerator can be changed
by lowering or raising a variable height overflow weir located on the outside
wall of the basin. This weir controls the water level in the basin and
therefore the impeller submergence. The power drawn and oxygen transferred
increases with increasing impeller submergence. According to the
manufacturer's information, aerator horsepower can be varied from 100 percent
to 25 percent of installed capacity without loss of adequate mixing for solids
suspension and oxygenation.(4)
Modifications may be made to the Carrousel system to achieve
denitrification. To achieve partial denitrification in addition to BOD removal
and nitrification, an anoxic zone is added in the channel upstream of the
aerators. The anoxic zone in the basin channels is created by controlling the
amount of air produced by the aerators. This modification is shown in Figure
2. A DO of approximately 2 mg/1 in the aerobic zone decreases in the channel
and approaches zero in the anoxic zone.
-------
Page 2-7
To meet a total nitrogen effluent requirement of less than 10 mg/1, a
Carrousel system with a separate upstream anoxic tank for denitrification can
be added to the design. A schematic of this modification is shown in Figure 2.
The denite tank is an uncovered tank with submerged turbine mixing equipment.
This anoxic tank is used in addition to the anoxic zone in the channel. Up to
400 percent of the influent flowrate is recycled to the denite tank from the
Carrousel basin at a point near the downstream end of the anoxic zone.
A second anoxic stage may be added to the above design for further
denitrification. This second anoxic stage, which follows the oxidation ditch,
is used to reduce the remaining nitrates to a level of 1 mg/1 or less. This
stage is followed by a reaeration stage to strip the nitrogen gas. This four
stage system is referred to as the Bardenpho Process. (6) A schematic of this
modification is presented in Figure 2.
A fifth stage may be added to the Bardenpho Process if biological
phosphorus removal is required. This fifth stage is referred to as a
fermentation stage and usually consists of two cells in series. Each cell is
typically a concrete tank equipped with submerged turbine mixers.
Concentrated sludge from the secondary clarifiers is returned to this stage.
This creates an anaerobic environment where the bacteria are stressed causing
phosphorus within the cells to be released. When exposed to an aerobic
environment, the uptake of phosphorus is greater than if the organisms were not
previously exposed to a stressed environment. A schematic of this process
known as Modified Bardenpho Process(6) is presented in Figure 2.
Envirex
Oxidation ditches supplied by Envirex are called "Orbal" systems. The
Orbal system is typically a three channel looped reactor system, although two
channels may be used in very small flow systems (less than 0.2 mgd). (7) A
typical three channel orbal aeration basin is shown in Figure 3. An
installation list received from Envirex in May 1991 indicated there were 171
Orbal systems treating municipal waste in the United States.(7)
-------
. SIM-PRE INTERNAL
RECYCLE CHANNEL
(FOR NITROGEN REMOVAL)
RETURN SLUDGE
INFLUENT-
EFFLUENT TO
CLARIREH
(Ref. 7)
Figure 3. Typical Three Channel Orbal Oxidation Ditch
With Modification For Nutrient Removal
-------
Page 2-9
Most of the Orbal systems in the United States are designed to be operated
in the extended aeration mode. Solids retention times in these systems range
from 20 to 38 days. The long SRT's are conducive to complete nitrification.
Design BOD loadings in these systems range from 12.5 to 20 Ibs BOD/day/1000
cubic feet. For treatment plants with flows greater than 2 mgd, the extended
aeration system design is used only when nitrification is required.
Aeration in the Orbal system is provided by 4.5 foot diameter plastic
aeration disks. Triangular nodules on the surface of the molded plastic disk
provide mixing and aeration. The nodules have a base face and an apex face and
can be run with either entering the mixed liquor first... This reversing of
direction is accomplished by reversing the drive rotation of the disks.
According to manufacturer's literature the base face provides one third more
oxygen than the apex side. The disks have an immersion operating range of from
21 to 9 inches, allowing for adjustment of oxygen delivered and power drawn
with influent variations. This adjustment ranges from 50 to 100 percent of
that at maximum immersion of the disks. Velocity in the ditch is maintained by
the rotation of the disks.
Manufacturer's information indicates that the Orbal system needs only one
horsepower per 100,000 to 200*,000 gallons for efficient mixing. (8) Typical
rotational speed for the disks is 43 rpm but may be adjusted upwards to 55 rpm
to supply additional oxygen. Manufacturer's literature also states that
nitrogen and phosphorus removal rates of 80 percent and ammonia effluent levels
below 1 mg/1 can be achieved with a standard extended aeration Orbal system.(8)
Regulatory agencies in some states may require dual aeration basins. When
this is required the Orbal system is designed with individual dewaterable
channels and influent and return sludge lines to all three channels. In this
design the first channel has 50 percent of the total basin volume.
In the standard three channel extended air Orbal system, the wastewater
flow normally enters the outer channel. Oxygen delivery rates in the first
channel are higher than in the other two channels. The aerated zones in the
first channel provides oxygen for nitrification. The actual oxygen demand in
-------
Page 2-10
the first channel exceeds the oxygen supplied and an oxygen deficit condition
is established. Despite the oxygen deficit, most ammonia is nitrified in the
first channel. Denitrification occurs as the nitrates pass through zones of
zero dissolved oxygen in the channel. The second channel works with the first
channel for further nitrification and denitrification. The third innermost
channel is used for further reduction of BOD and any necessary final reduction'
of ammonia.
Modifications may be made to the standard Orbal system to achieve nitrogen
removals greater than 80 percent. The modification, called the SIM-PRE
process, include an internal recirculation loop where residual nitrates from
the third channel are recycled to the first channel. This recycle rate is
usually four times the influent flow. The process uses the simultaneous
nitrification-denitrification available with the standard Orbal system plus the
recirculation of residual nitrates to achieve additional biological
denitrification.
An additional modification also may be made to the Orbal system for
biological phosphorus removal. To enhance biological phosphorus removal, the
system is designed with an oxygen deficit. This creates anaerobic conditions
resulting in phosphorus being released from the solids. In the inner channels
where aerobic conditions exist, the solids take up more phosphorus than they
originally contained, thus increasing the biological phosphorus removal.
Innova-Tech
Oxidation ditches supplied by Innova-Tech are known as "Total Barrier
Oxidation Ditch" systems. A typical Total Barrier Oxidation Ditch is shown in
Figure 4. A variety of ditch designs and configurations are available
depending on system requirements and available land. Information received from
Innova-Tech in June 1991 indicated that a total of 57 systems were installed in
the United States, 36 of which were at municipal plants. The design flows
ranged from 0.04 to 7.0 mgd.
-------
TOTAL BARRIER OXIDATION DITCH
VA'STEWATER
INFLUENT
-TOTAL BARRIER
WALL
NITRIFICATION
OCCURS
DRAFT TUBE
AERATORS
BLOWER
BLDG-
•DENITRIFICATION
OCCURS
DRAFT TUBE a AERATOR DRIVE
pANTI VORTEX
INTAKE BAFFLES
TOTAL BARRIER WALL
AIR SUPPLY TO
CONTACT DIFFUSER
DUCT
CONTACT DUCT
DIFFUSER ACCESS
DUCT
(Optional) REMOVAL CONTACT
DUCT DIFFUSERS
HORIZONTAL OR VERTICAL
AERATOR DRIVE
>AIR SUPPLY FROM BLOWER
TO AIR SPARGE
ANOXIC
ZONE
DRAFT TUBE
AIR SPARGE
DEEP OXYGEN
CONTACT DUCTS
(Ret. 10)
Figure 4. Total Barrier Oxidation Ditch and Draft Tube
-------
Page 2-12
Once design parameters are established by the design engineer, Innova-tech
recommends the wastewater treatment process design and system to meet the
required treatment needs.
The Total Barrier Oxidation Ditch differs from traditional oxidation ditch
systems in that a vertical barrier wall is installed across the entire cross
section of the ditch channel. The wall prevents backmixing and forces all the
flow into the draft tube turbine aerators. Compressed air is introduced to the
turbine assembly through a sparge ring located beneath the turbine blades.
Aerated mixed liquor is discharged below the water surface on the downstream
side of the barrier wall through a J-tube extension of the basic draft tube.
The turbine part of the draft tube turbine aerator provides enough energy to
circulate liquid through the ditch, while blowers deliver air to the draft tube
turbine aerators for aeration. The use of separate devices for aeration and
mixing allows for independent control of channel velocity and oxygen transfer
rate. Manufacturer's information indicates that, except in very large plants,
no more than two aerators are required and they are placed side by side at one
location. Oxygen transfer efficiencies of 4.0 to 5.0 Ibs 02/bhp/hr at standard
test conditions are claimed by the manufacturer.(9)
The Barrier Oxidation Ditch may be operated with an anoxic zone in the
channel to promote denitrification as long as the channel is long enough for
both aerobic and anoxic zones. If biological phosphorus removal is required,
the Barrier Oxidation Ditch may be modified by adding an anaerobic tank prior
to the oxidation ditch. In this system there is an internal recycle from the
anoxic zone of the ditch to the anaerobic tank. Sludge from the secondary
clarifier is returned to the anoxic zone of the oxidation ditch to prevent
nitrates (thereby oxygen) from being introduced to the anaerobic tank.
Lakeside
Lakeside furnished the first oxidation ditch plant in the United States in
1963. Oxidation ditches supplied by Lakeside are called the "Closed Loop
Reactor Process" (CLR). The CLR process consists of a single channel reactor
-------
Page 2-13
with a single feed point for raw sewage and return sludge. A typical Lakeside
oxidation ditch is presented in Figure 5. Information received from Lakeside
in August 1991 indicated there are approximately 1500 operating Lakeside
oxidation ditches.
Lakeside literature states that the CLR process can provide effective
secondary biological treatment with BODs and suspended solids reductions of 92
to 99 percent.(10) Manufacturer's literature states that the CLR process can
achieve 95 to 99 percent nitrification and high levels of denitrification
simultaneously without major modifications. (H) According to manufacturers
information, single reactor designs can be utilized to achieve a total nitrogen
level of approximately 10 mg/1 depending upon mixed liquor temperature. In
warm climates lower total nitrogen concentrations may be achieved.
The CLR process operates in the extended aeration mode with a long
detention time (18 to 32 hours), a well conditioned sludge, and high MLSS
concentrations (3000 to 9000 mg/1). Hydraulic and organic surges have no
significant effect on the process efficiency according to manufacturer's
information. These operating conditions promote nitrification.
Aeration in the CLR process is provided by horizontal bladed rotor
aerators. The rotors are low speed mechanical surface aerators that rotate in
a plane horizontal to the liquid surface. Three rotor types, Cage, Mini-Magna,
and Magna are available.(10) xhe Cage and Mini-Magna rotors have a speed range
of from 60 to 90 rpm and a minimum design immersion of six inches. The Magna
rotor has a speed range of from 50 to 72 rpm and a minimum design immersion of
eight inches. The oxygenation capacity of the rotor may be varied by changing
the immersion and rotational speed. The velocity in the ditch varies with
rotor length, rotor speed, rotor immersion, ditch configuration, ditch depth,
ditch liner and rotor baffles. Typically a velocity of at least 1 fps is
required to maintain MLSS in suspension.
-------
RETURN
SLUDGE
INFLUENT
ROTOR
''/,.
FLOW
"HIGH DO
TYPICAL LAKESIDE OXIDATION DITCH
EFFLUENT
RawWsstewater/
Return Sludge
Blending Tank
I
ANOXIC
BASIN
FLOW
— »
DO*i(M.5mfl/L^/
£
ROTOR
AEROBIC
BASIN
FLOW
^,
DO»2.0mg/L
Recycle
EFFLUENT
MODIFICATION FOR NUTRIENT REMOVAL (Ref. 11)
(Modified Ludzack-Ettinger Process)
Figure 5. Lakeside Oxidation Ditch and Modification for
Nutrient Removal
-------
Page 2-15
A modification may be made to the CLR process to meet stringent nitrogen
effluent limits (less than 5 mg/1) and to enhance phosphorus removal. This
modification is the Modified Ludzack-Ettinger (MLE) process. A schematic of
this process is presented in Figure 5. This process consists of two separate
^aeration basins, the first anoxic and the second aerobic. The basins operate
in series with the mixed liquor being recycled from the aerobic reactor to the
anoxic reactor. Manufacturer's literature states that 83 percent nitrogen
removal can be expected at a mixed liquor recycle ratio of 4 and a return
sludge ratio of one.
-------
-------
Page 3-1
SECTION 3.
PERFORMANCE DATA
INTRODUCTION
Treatment plants with oxidation ditches and nutrient removal data were
identified by EPA personnel and the ditch manufacturers. The effluent permit
limits and type of oxidation ditch for the plants that provided data are
presented in Table 2.
Eight of the 17 plants have effluent ammonia permit limits. These limits
ranged from 0.5 to 3.0 mg/1 during the summer months. One plant, Lake Geneva,
Wisconsin, that discharges to seepage cells has a year round total nitrogen
limit of 10 mg/1. The Crofton, Maryland plant has a seasonal total nitrogen
limit of 10 mg/1. Thurmont, Maryland, Fredrick, Maryland, and Wanaque, New
Jersey have a Total Kjeldahl nitrogen limit during the summer months. The
Yellow River/Sweetwater Creek Water Reclamation Facility has a nitrate limit of
6.0 mg/1 year round. Six of the plants have effluent phosphorus limits that
range from 0.5 to 2.0 ing/1.
Design information for the 17 plants is presented in Table 3. All design
information was not available for each of the plants. The average design flow
for the plants ranged from 0.1 to 12 mgd. The design hydraulic retention time
at the average design flow ranged from 10 to 34 hours. The design mean cell
retention time, available for eight of the plants, ranged from 12 to 48 days.
The design MLSS concentration, available for 12 of the plants, ranged from 1500
to 8000 mg/1. Design BOD loadings of 13 plants which provided information
ranged from 5.8 to 39.2 Ibs BOD/day/1000 cubic feet.
The performance data for the 17 plants are summarized in Table 4. The
average flow ranged from 30 to 116 percent of design. Actual hydraulic
detention times ranged from 10.7 to 57 hours. The average effluent BOD ranged
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-------
TABLE 3. DESIGN BASIS FOR OXIDATION DITCH PLANTS
Dupage County
Illinois
Cedarburg Dousman (Knollwood
Wisconsin Wisconsin
Design Flow (mgd)
Aerator Type
Influent BOD (mg/1)
Influent NH3-N (mg/1)
Influent Total P (mg/1)
Design Nitrification?
Design Denitrification?
Design Biological F Removal?
Design BOD Load (Ib/1000ft3/day)
Design MLSS (mg/1)
Design Hydraulic Detention Time (hrs)
Design SRT (days)
Design Flow (mgd)
Aerator Type
Influent BOD (mg/1)
Influent NH3-N (mg/1)
Influent Total P (mg/1)
Design Nitrification?
Design Denitrification?
Design Biological P Removal?
Design BOD Load {Ib/1000ft3/day}
Design MLSS (mg/1)
Design Hydraulic Detention Time (hrs)
Design SRT (days)
2.75
disc
200
20
5
Yes
No
Yes
12.2
8000
24
30
Huntsville
Texas
(South Plant)
1.60
disc
0.3S
disc
200
Yes
No
No
12.0
3000
24
48
Kemmerer
Wyoming
1.45
surface
180
No
No
No
3750
30
Plant)
8.3
draft tube
215
25
Yes
No
No
15.9
3500
20
Lake Geneva
Wisconsin
1.74
disc
153
18
3.2
Yes
Yes
No
15.0
4000-5000
15
22
Frederick
Maryland
7.0
fine bubble
Yes
No
No
2500
12.5
Lyons
Wisconsin
0.10
brush
271
Yes
No
No
13.0
31.5
Hanover
Huntsville
Texas
Pennsvlvani a (Parker Creek)
3.65
brush
153)
draft tube
100
Yes
No
No
29.0
Thurmont
Maryland
1.0
brush
75(a)
36 (TKN)
No
No
No
11.1
4000-4500
10.
Yellow River/
Wanaque Sweetwater Creek
Hew Jersey
0.7
surface
250
25
10-12
Yes
No
No
12.7
5000
29.5
Georgia
12.0
disc
250
25
10
Yes
Yes
No
3500
11.4
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Page 3-6
from 1.9 to 10.5 mg/1 with removals ranging from 90 to 99 percent. The average
BOD loading ranged from 2.5 to 15.8 Ibs BOD/day/1000 cubic feet. Nine of the
ten plants where both design and actual loadings were available were below
design. The load to one plant exceeded the design BOD loading.
Nitrate, total nitrogen, and phosphorus data were limited. Effluent
phosphorus data were available for seven plants. Chemicals were added at five
of the plants for higher phosphorus removals. These plants typically achieved
effluent phosphorus levels less than 1 mg/1. The monthly average data for each
plant is presented in Appendix A. Chronological plots of the data are also
presented in Appendix A.
Effluent ammonia data indicates that nitrification was occurring at all the
plants. TKN and N03-N data from two plants designed for denitrification
indicated that denitrification was occurring when operated in a mode to promote
denitrification. The Patuxent Water Reclamation Facility in Crofton, Maryland
was designed for denitrification, however, during the winter it is not operated
to promote denitrification.
SITE OBSERVATIONS
Three of the 17 plants that provided data were selected for site visits to
obtain detailed information on operations and performance. The three plants
selected monitor ammonia, nitrate and phosphorus. The three plants visited
represented three types of aeration equipment - brush rotor, fine bubble
diffuser and draft tube aerator. One plant (Thurmont) was designed for only
BOD removal. One plant (Fredrick) was designed for nitrification and the third
plant (Patuxent Water Reclamation Facility) was designed for nitrification and
denitrification.
The following discussion summarizes the observations made at the plants.
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Page 3-7
Thurmont. Maryland
The Thurmont, Maryland wastewater treatment plant was designed for an
average daily flow of 1 mgd, and a peak flow of 4 mgd. The plant was designed
to treat an influent BOD of 210 mg/1, an influent TSS of 230 mg/1 and a TKN of
36 mg/1.
The current treatment plant is an upgrade of a trickling filter plant. The
oxidation ditch was completed in 1983. The influent flow passes through a grit
chamber, comminutor and bar screens prior to primary clarifiers. The plant has
three primary clarifiers, however, only two were in service. The primary
clarifier effluent flows either directly to the oxidation ditch or to the
trickling filter before the oxidation ditch. Flow cannot be split between the
trickling filter and the oxidation ditch. The trickling filter was used in
addition to the oxidation ditch from mid May until August 19, 1991. The
oxidation ditch effluent is settled in two secondary clarifiers operated in
parallel. The clarified effluent is polished by sand filters and disinfected
using ultraviolet light. The effluent is discharged to Hunting Creek, a Class
III trout stream.
The plant's effluent permit limits are a 30 day average BOD of 30 mg/1 and
a 30 day average TSS of 30 mg/1. From May through October the effluent TKN
limit is a 30 day average of 3 mg/1. The plant is also required to monitor
NH3-N, NOs-N and phosphorus and report the results although there are no permit
limits for these parameters.
The state of Maryland is in the first phase of a biological nutrient
removal program in which Thurmont is participating. As part of a study, which
started in October 1990, existing treatment plant operations are being
evaluated and nutrient levels monitored. Treatment plants with operations that
could be upgraded for nutrient removal without extensive modifications were
included in the study.
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Page 3-8
The oxidation ditch is a Lakeside ditch with two brush rotor aerators with
BL maximum immersion of 7.5 inches. The ditch was designed for a 10 hour
hydraulic detention time at the design flow of 1 mgd. The ditch was designed
for an organic loading of 4.6 Ibs BOD/day/1000 cubic ft. The manufacturer's
recommended MLSS concentration was 4000 to 4500 mg/1. The secondary clarifier
was designed for a 5.4 hour detention time at the average design flow of 1 mgd
and an overflow rate of 300 gpd/ft2.
The oxidation ditch is operated at a MLSS concentration of approximately
1800 mg/1 in summer and approximately 3000 mg/1 in winter. The return sludge
concentration in the summer is 6000 mg/1 and 8000 mg/1 in winter. Operation of
the ditch at the higher solids concentrations specified in the design was tried
but was not successful. The plant superintendent felt that the secondary
clarifiers did not have the capacity to handle a higher solids concentration.
The ditch was operated at an SET .of 5 to 10 days.
During the period of January 1991 to July 1991 the plant operated at an
average flow of 0.64 mgd or 64 percent of design. For the period of May
through July the trickling filter was in use. Chronological plots of BOD, TSS,
and TKN are presented in Figure 6. The plant consistently met the effluent BOD
and TSS permit limits of 30 mg/1.
Final effluent TKN concentrations measured during May, June, and July 1991
were 2.1, 1.8, and 1.4 mg/1, respectively. Partial nitrification may have
occurred in the trickling filter, however this was not measured. Final
effluent N03-N was measured several times during the period April through July
and ranged from 2.2 to 8.0 mg/1.
The plant superintendent was generally satisfied with the oxidation ditch,
however he feels the aeration system is too small, especially for summer
operation. A problem has been experienced with a "wave" developing .in the
ditch if both rotors are set at 72 rpm. This "wave" randomly occurs and
neither the operator or the ditch supplier had an explanation as to the cause.
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Thurmont, Maryland
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Page 3-10
To prevent the "wave" one rotor is sometimes operated at 54 rpm. Approximately
eight weeks prior to the site visit both rotors were set at 72 rpm, and no
"wave" developed during that time.
A problem has been experienced with filamentous bacteria due to a low F/M
ratio in the ditch during the summer. Chlorine has been added to control the
filamentous bacteria in the past, however since the plant discharges to a class
III trout stream chlorine can no longer be used. Hydrogen peroxide was
recommended by the state, however its use killed the biomass. At the time of
the site visit the plant was still recovering and trying to control the
filamentous bacteria. Operations to denitrify had been abandoned.
Fredrick. Maryland
The Fredrick, Maryland wastewater treatment plant was designed for an
average daily flow of 7.0 mgd and a peak hourly flow of 16.2 mgd. The influent
design BOD, TSS and TKN concentrations were not available.
The treatment plant went on line in February 1988. The influent flow
passes through a bar screen and grit chamber prior to four primary clarifiers.
The primary clarifier effluent flows to three oxidation ditches that operate in
parallel. Each oxidation ditch has an intrachannel clarifier. The clarifier
effluent solids are removed by sand filters and the effluent disinfected using
chlorine. The effluent is discharged to the Monocacy River.
The plant has an effluent 30 day average BOD limit of 8.7 mg/1 from May
through October, and 26 mg/1 from November through April. The 30 day average
TSS concentration limit is 26 mg/1. From May through October a 30 day average
TKN concentration of 2.6 mg/1 must be met. The current permit has no total
nitrogen or total phosphorus limit, however, the plant must monitor and report
N02-N and N03-N and total phosphorus two times per month. The flow to the
Monocacy River cannot exceed 8 mgd on the basis of a 12 month moving average.
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Page 3-11
Each oxidation ditch/clarifier basin has a total volume of 1.55 million
gallons. The volume of each clarifier is 0.34 million gallons and the aeration
channel volume is 1.21 million gallons. The design hydraulic detention time in
the aeration portion of the basin is 12.5 hours at average design flow.
Aeration in the oxidation ditch is supplied by fine bubble, submerged
diffusers. The intrachannel clarifier was designed for a 3.5 hour detention
time and a surface loading rate of 606 gpd/ft2 at the average design flow.
The oxidation ditches are being run at a MLSS concentration of between 2000
and 2500 mg/1 and an F/M of between 0.13 and 0.15. The design MLSS
concentration was not available. The ditch is operated at an SRT of between 19
and 21 days.
Figures 7 and 8 present Chronological plots summarizing the monthly average
flow, BOD, TSS, TKN, NH3-N, N02+N03-N, and total phosphorus for 1990 and May
through July 1991. During that period, the plant operated at an average
influent flow of 8.1 mgd, which was above the average design flow of 7.0 mgd.
The average hydraulic detention time for the period was 10.7 hours. During the
same period the oxidation ditch influent BODs averaged 102 mg/1. This converts
to an organic loading of approximately 14 Ibs BOD/day/1000 cubic feet. Based on
the data for the period approximately 30 percent of the raw BODs is removed in
.the primary tanks. Approximately 90 percent of the BODs entering the oxidation
ditch was removed before discharge to the Monocacy River. The TKN removals
indicated that nitrification occurred during the entire period. The average
removal of TKN was approximately 87 percent. The average removal of ammonia
was approximately 91 percent. The plant is not being operated in a mode to
promote denitrification. Approximately 25 percent of the phosphorus in the
influent is removed during treatment.
As part of Maryland's biological nutrient removal program, an investigation
was made to determine if any inexpensive modifications to the oxidation ditch
could be made to achieve denitrification. It was determined that because of
the clarifier in the ditch there was insufficient space to set up an anoxic
zone.
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Page 3-14
The assistant superintendent noted that although the three oxidation
ditches are designed the same, they each have their own "quirks". This has
made operation of the ditches somewhat difficult since the same adjustments and
operating conditions do not produce the same results in each ditch. It has
taken considerable time and effort to get the plant to the current level of
operation.
Patuxent Water Reclamation Facility. Crofton. Maryland
The Patuxent Water Reclamation Facility in Crofton, Maryland was designed
for an average daily flow of 6 mgd and a peak flow of 13 mgd. The plant was
designed to treat an influent BOD5 of 250 mg/1, an influent TSS of 200 mg/1, an
influent TKN of 25 mg/1, and an influent total phosphorus of 10 mg/1.
The treatment plant began operation in April 1988. • The influent flow
passes through bar screens and a grit chamber before entering two oxidation
ditches operated in parallel. The oxidation ditch effluent flows to three
secondary clarifiers operated in parallel. The clarified effluent is filtered
as a polishing step. The filtered effluent is chlorinated and dechlorinated
and discharged via cascade aeration tanks to the Little Patuxent River.
The plant's effluent permit limits require a 30 day average BODs of 20 mg/1
from April through October and 30 mg/1 from November through March. The 30 day
average TSS limit is 30 mg/1. From April through October a 30 day average
total nitrogen limit of 10 mg/1 must be met. The plant has no total nitrogen
limit during the remainder of the year, however total nitrogen is reported.
The plant must meet a total phosphorus limit of 1 mg/1 year round. Ferric
^chloride is added for phosphorus removal.
Each of the two total barrier oxidation ditches provided by Innova-Tech has
a volume of 3.4 million gallons. The design hydraulic detention time of each
is approximately 27 hours at the average daily flow. Aeration in the oxidation
ditches is supplied by positive displacement blowers providing air to the draft
tube aeration spargers. Each secondary clarifier has a volume of 1.1 million
gallons resulting in a detention time of approximately 12 hours at design flow.
The clarifier overflow rate is 177 gpd/ft2 at average design flow.
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Page 3-15
The oxidation ditch is being operated at a MLSS concentration of
. approximately 1450 mg/1 and a mixed liquor volatile suspended solids (MLVSS)
concentration of approximately 1000 mg/1. The ditches are being operated at an
, SRT of approximately 15 days. During the period July 1990 through July 1991
the plant operated at an average influent flow of 3.5 mgd, or approximately 58
percent of design. The average hydraulic detention time during the period was
approximately 46.6 hours. During the same period the influent BOD was between
150 and 200 mg/1. The BOD removal was greater than 95 percent during the
period. The BOD loading during the period was 6.5 Ibs BOD/day/1000 cubic feet
which was below the design loading of 13.8 Ibs BOD/day/1000 cubic feet.
Chronological plots of the monthly average flow, NHs-N, total nitrogen, and
phosphorus are present in Figure 9. The oxidation ditches were operated to
achieve nitrification and denitrification in the summer. The long channel
length (1230 feet) allows room for an anoxic zone. Nitrification and
denitrification were occurring in the oxidation ditches from April through
October during the time a total nitrogen permit limit had to be met. The
average total nitrogen removal during the summer months was 89 percent. During
the winter months only one oxidation ditch is used and the ditch is not
operated to achieve nitrification and denitrification. The ditches were not
designed for biological phosphorus removal.
The plant superintendent was generally satisfied with the operation and
performance of the oxidation ditches. Some problems were experienced with the
gear boxes for the draft tube mixers, however that problem has been resolved.
OTHER PLANTS PROVIDING DATA
Cedarburg. Wisconsin
The oxidation ditch at the Cedarburg, Wisconsin wastewater treatment plant
is a three channel Envirex Orbal system designed to treat an average flow of
2.75 mgc and a peak flow of 8.0 mgd. The total volume of the ditch is
approximately 2.8 million gallons. The first channel has a capacity of 42
percent of the total volume, the second channel 33 percent, and the third
channel 25 percent
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Patuxent Water Reclamation Facility
Crofton, Maryland
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Page 3-17
The design detention time for the oxidation ditch at average design flow is
24 hours. The average flow for the period January 1989 to April 1991 was 54
percent of the design flow, and the average detention time was approximately 45
hours.
The plant was designed for a BOD loading of 12.2 Ibs BOD/day/1000 cubic
feet. During the period where data were available the average BOD loading was
5.5 Ibs BOD/day/1000 cubic feet. BOD removals during the period averaged 98
percent.
The plant effluent must meet permit limits of 2 mg/1 NH3-N during the
summer and 4 mg/1 during the winter. The monthly average effluent ammonia
concentration during the period of record (1/89 to 4/91) met the permitted
limits. Ammonia removals averaged 99 percent for the period of record.
Influent and effluent total Kjeldahl nitrogen were measured once per month from
August 1989 to April 1991. The influent concentration ranged from 10 to 90
mg/1 and the effluent ranged from 0.6 to 4 mg/1. The average TKN removal was
95 percent. Nitrate was not routinely measured.
The plant effluent is required to meet an effluent phosphorus limit of 1.0
mg/1. Ferrous sulfate is added for phosphorus removal. The monthly effluent
phosphorus concentration exceeded the permit limit in three of the 28 months
that data were available.
Dousman. Wisconsin
The oxidation ditch at the Dousman, Wisconsin wastewater treatment plant,
in operation since 1982, is a three channel Envirex Orbal system designed to
-treat an average flow of 0.35 mgd and a peak flow of 0.88 mgd. The total
volume of the ditch is approximately 0.37 million gallons.
The design detention time for the oxidation ditch at average design flow is
24 hours. The average flow for the period January 1989 to December 1990 was 60
percent of design. The average detention time during that period was
approximately 43 hours.
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Page 3-18
The plant was designed for a BOD loading of 11.7 Ibs BOD/day/1000 cubic
feet. During the period when data were available the average BOD loading was
6.4 lbs/day/1000 cubic feet. BOD removals during the period averaged 97
percent.
The plant effluent must meet permit limits of 2 mg/1 NHs-N during the
summer and 4 mg/1 during the winter. The monthly average effluent ammonia
concentration during the period of record (1/89 to 4/91) met the permitted
limits. Influent ammonia concentration is not measured. TKN and nitrate are
not measured.
The plant does not have an effluent phosphorus limit in its permit,
therefore effluent phosphorus is not measured.
Dupape County. Illinois
The Dupage County, Illinois, Knollwood Treatment Plant has three Innova-
Tech total barrier oxidation ditches with draft tube aerators. The plant was
designed to treat an average wastewater flow of 8.3 mgd and a peak flow of 24.7
mgd. The total volume of each ditch is 2.33 million gallons.
The design detention time for each oxidation ditch at average flow is 20
hours. At the average flow for the period January 1989 to May 1991, which was
96 percent of design, the detention time averaged approximately 21 hours.
The plant was designed for a BOD loading of 15.9 Ibs BOD/day/1000 cubic
feet. During the period when data were available the average BOD loading was
12.8 Ibs BOD/day/1000 cubic feet. BOD removals during the period averaged 97
percent.
The oxidation ditch was designed for a MLSS concentration of 3500 mg/1 and
a. MLVSS concentration of 2500 mg/1. During the period January 1989 to May 1991
the overall average MLSS concentration was 2820 mg/1.
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Page 3-19
The plant effluent must meet permit limits of 1.5 mg/1 NH3-N during summer
* and 4 mg/1 during the winter. The monthly average effluent ammonia
concentration during the period of record (1/89 to 5/91) met permit limits
? except in August and September 1990. During those months repairs were being
made to the aeration system. The overall average effluent NH3-N concentration
in the both the summer and winter was 0.57 mg/1. The summer average excludes
the two months (August and September 1990) when repairs were made to the
aerators. The average ammonia removal was 95 percent in the both the summer
and winter. TKN and nitrate are not routinely measured.
The plant does not have an effluent phosphorus limit and does not measure
phosphorus.
Hanover. Pennsylvania
The Hanover, Pennsylvania wastewater treatment plant has two oxidation
ditches supplied with Passavant brush rotors. The plant was designed to treat
an average flow of 3.65 mgd and a peak dry weather flow of 5.58 mgd. The
volume of each ditch is approximately 1.43 million gallons. Approximately 30
percent of the plant flow is industrial.
The design detention time for each oxidation ditch at average flow is
approximately 19 hours. The average flow for the period January 1989 to May
1991 was 105 percent of capacity. The detention time during that period was
approximately 18 hours.
The oxidation ditch was designed for a MLSS concentration of 4000 mg/1 and
a MLVSS concentration of .2835 mg/1. During the period January 1989 to April
1991 the overall average MLSS concentration was 2932 mg/1.
The design BOD loading to the oxidation ditch was 12.1 Ibs BOD/day/1000
cubic feet. The average loading for the period of record (1/89 to 5/91),
assuming a 30 percent BOD removal in the primary settling tanks, was 14.6 Ibs
BOD/day'/lOOO cubic feet. The BOD removal in the oxidation ditch averaged 98
percent.
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Page 3-20
The plant effluent must meet permit limits of 1.5 mg/1 NH3-N during the
summer and 4.5 mg/1 during the rest of the year. The monthly average effluent
ammonia concentration during the period of record (1/89 to 5/91) met the permit
limit for 21 of the 28 months. Three of the months during which permit limits
were exceeded were summer months. The ammonia removal during the summer was 94
percent and 86 percent during the rest of the year. TKN and nitrate were not
routinely measured.
The plant must meet an effluent phosphorus limit of 2.0 mg/1. Ferrous
sulfate is added for phosphorus removal. The effluent concentration met the
phosphorus limit in 27 of the 28 months. The average phosphorus removal was 82
percent.
Huntsville. Texas - Parker Creek Plant
The Parker Creek wastewater treatment plant has two Envirex Orbal oxidation
ditches. The plant was designed to treat an average dry weather flow of 2.75
ngd and an average wet weather flow of 4.15 mgd. The volume of each ditch is
approximately 0.723 mgd. There are three aeration channels surrounded by an
outside basin that is used as an aerobic sludge digester. The first channel
has a capacity of approximately 52 percent of the total volume, the second
channel approximately 31 percent, and the third channel approximately 17
percent.
The design detention time for each oxidation ditch at average dry weather
flow is approximately 12.6 hours. At the average flow for the period January
1989 to April 1991, which was 87 percent of the design flow, the average ,
detention time was approximately 14.5 hours.
The plant was designed for a BOD loading of approximately 39 Ibs
BOD/day/1000 cubic feet of aeration volume. Influent BOD data were not
available, however influent COD data were received. Based on an estimated
BOD/COD ratio of 0.6, the average BOD loading was 15.8 Ibs BOD/day/1000 cubic
feet.
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Page 3-21
The plant's discharge permit does not have an NH3-N limit, however influent
and effluent ammonia are monitored. The monthly average effluent NH3-N
concentration during the period of record (January 1989 to April 1991) was less
, than 1.0 mg/1 in 27 of the 28 months. The average ammonia removal was 97
percent. TKN and nitrate are not routinely measured. Data in manufacturer's
literature indicated that five samples were collected in June 1983 for effluent
nitrate measurements. The average of these samples was 3.6 mg/1. The influent
ammonia during that period averaged 24.7 mg/1 and the ammonia removal was 95.5
percent. These data indicate denitrification occurred.
The plant is not required to meet an effluent phosphorus limit and does not
measure phosphorus.
Huntsville. Texas - South Plant-
The oxidation ditch at the South Plant in Huntsville, Texas is an Envirex
Orbal system. The plant was designed to treat an average flow of 1.6 mgd
The volume and configuration of each channel of the oxidation ditch were not
available.
The design BOD loading was not available. The plant consistently met the
permit BOD limit of 20 mg/1 during the period of record. The plant effluent
permit does not have an NH3-N limit, however influent and effluent ammonia is
monitored. The monthly average effluent NH3-N concentration was less than 1
mg/1 each month for the period of record (January 1989 to April 1991). The
average ammonia removal was 99 percent. TKN and nitrate are not routinely
measured.
The plant is not required to meet an effluent phosphorus limit and does not
measure phosphorus.
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Page 3-22
Kemraerer. Wyoming
The oxidation ditch at the Kemmerer, Wyoming wastewater treatment plant, in
operation since 1981, is an Eimco Carrousel system. The plant was designed to
treat an average flow of 1.5 mgd. The total volume of the ditch is 1.43
million gallons.
The design detention time for the oxidation ditch at the average design
flow is approximately 23 hours. The average flow for the period January 1990
to June 1991 was 30 percent of the design flow. The detention time during that
period was approximately 76 hours.
The design BOD loading was not available. The BOD loading to the plant
during the period of record was 3.7 Ibs BOD/day/1000 cubic feet. BOD removals
during the period averaged 98 percent.
The plant effluent must meet an NHs-N permit limit of 3.8 mg/1 during the
summer. There is no ammonia limit in the winter. The monthly average effluent
ammonia concentration for the summer months during the period of record (1/90
to 6/91) met the permit limits. The average removal of ammonia was 98 percent.
TKN and nitrate are not routinely measured. ;
The plant does not have an effluent phosphorus limit and does not measure
phosphorus .
Lake Geneva. Wisconsin
The oxidation ditch at the Lake Geneva, Wisconsin wastewater treatment
plant is a three channel Envirex Orbal system using the SIM-PRE mode. This
mode of operation promotes denitrification. The plant is designed to treat an
average flow of 1.74 mgd and a peak flow of 4.64 mgd. The total volume of the
ditch is approximately 1.1 million gallons. During the period December 1989 to
May 1991 the internal MLSS recycle rate from the third to the first channel
ranged from 1.0 to 5.5 mgd. This system recycles nitrified mixed liquor from
the third channel to the first channel for denitrification.
-------
Page 3-23
s The design detention time for the oxidation ditch at average flow is
approximately 15 hours. The average flow for the period January 1989 to May
^ 1991 was 63 percent of design, and the average detention time was approximately
24 hours.
The oxidation ditch was designed for a MLSS concentration of 4000 to 5000
mg/1. During the period of record (1/89 to 4/91) the average MLSS
concentration was 5805 mg/1. The MLVSS concentration averaged 4108 mg/1 during
the same period.
The design BOD load to the oxidation ditch at average flow was 15.0 Ibs
BOD/day/1000 cubic feet. The average loading for the period of record (1/89 to
5/91) was approximately 14 Ibs BOD/day/1000 cubic feet.
The plant effluent is discharged to seepage cells for groundwater recharge
and must meet a total nitrogen permit limit of 10 mg/1 year round. Effluent
TKN and nitrate are measured daily. The effluent total nitrogen concentration
was less than the permit limit in each of the 29 months (1/89 to 5/91) where
data were available. The influent TKN and NH3-N are measured less frequently
than the effluent. The average removal of total nitrogen was 87 percent.
The plant does not have a phosphorus limit in its permit and does not
measure phosphorus.
Lyons. Wisconsin
The oxidation ditch at the Sanitary Sewer District No. 2 plant in Lyons,
Wisconsin is a Lakeside oxidation ditch. The ditch is designed to treat an
average flow of 0.1 mgd. The total volume of the ditch is approximately 0.13
million gallons.
-*
The design detention time for the oxidation ditch at average design flow is
31.5 hours. The average flow for the period January 1989 through May 1991 was
74 percent of design. The average detention time during that period was
approximately 42.5 hours.
-------
Page 3-24
The plant was designed for a BOD loading of approximately 13 Ibs
BOD/day/1000 cubic feet. During the period that data were available the
average BOD loading was 8.2 Ibs BOD/day/1000 cubic feet. BOD removals during
the period averaged 97 percent.
The plant must meet a permit limit of weekly average NHs-N concentration of
3.0 ffig/1 from April through October, and 6.0 mg/1 during the rest of the year.
The effluent NHs-N concentration met the permitted limit during the period of
record (1/89 -5/91) . Influent ammonia was not measured. TKN and nitrate were
not measured.
The plant does not have a phosphorus limit in its permit and does not
measure phosphorus.
jflorgan City. Louisiana
The three oxidation ditches at the Morgan City, Louisiana wastewater
treatment plant are Eimco Carrousel oxidation ditches with an iriterchannel
clarifier. The system is designed to treat an average daily flow of 3.0 mgd.
The total volume of each ditch is 1 million gallons, including the clarifier.
The volume of the ditch taken up by the clarifier was not available. The
average flow during the period January through December 1990 was approximately
4 mgd which is approximately 133 percent of design.
The plant effluent must meet a monthly average BOD permit limit of 30 mg/1.
During the period of record (1/89 to 12/90) the monthly average concentrations
were below the permit limit every month.
The plant does not have an NHs-N or total nitrogen limit in its permit,
however, influent and effluent ammonia are measured several time a month.
During the period of record the influent NHs-N concentration averaged 19.2 mg/1
and the effluent concentration averaged 0.35 mg/1. The average ammonia removal
was 98 percent. TKN, nitrate, and phosphorus were not measured.
-------
Page 3-25
Mount Clemens. Michigan
The oxidation ditch at the Mount Clemens, Michigan wastewater treatment
plant is a three channel Envirex Orbal system. The oxidation ditch is designed
to treat an average flow of 6.0 mgd. The total volume of the ditch is
approximately 8.5 million gallons. The first channel has a capacity of 59
percent of the total volume, the second channel 26 percent, and the third
channel 15 percent.
The design detention time for the oxidation ditch at average flow is 34
hours. The average flow for the period January 1990 through June 1991 was 65
percent of design and the average detention time was approximately 57 hours.
The plant was designed for an average BOD loading of approximately 5.8 Ibs
BOD/day/1000 cubic feet. Influent and effluent carbonaceous BOD (CBOD) are
reported by the plant. During the period when data were available the average
CBOD loading was 2.5 Ibs CBOD/day/1000 cubic feet. CBOD removal during the
period averaged 98 percent.
The plant effluent must meet permit limits of 0.5 mg/1 NH3-N from May
through September and 7.0 mg/1 NH3-N from October through November. The plant
has no effluent NH3-N limit during the rest of the year. The plant
consistently met the permit limits for NH3-N. The average ammonia removal was
98 percent. Ammonia was not measured during months when effluent limits did
not have to be met.
The plant effluent must meet a phosphorus limit of 1.0 mg/1 year round.
Chemicals were not added during the period of record, however, the plant does
have a ferric chloride feed system. The average effluent phosphorus
concentration reported was 0.55 mg/1. The average phosphorus removal was 78
percent.
Rehoboch Beach. Delaware
The two oxidation ditches at the Rehoboth Beach, Delaware wastewater
treatment plant are Innova-tech oxidation ditches with draft tube aerators.
-------
Page 3-26
Rehoboth Beach is a summer resort and the treatment plant was designed for an
average summer flow of 3.4 mgd and an average winter flow of 1.0 mgd. The
total volume of each ditch is approximately 2 million gallons at average flow.
The design detention time for each oxidation ditch at average summer flow
is approximately 29 hours. The average summer flow for 1989 and 1990 was
approximately 1.4 mgd or 41 percent of design. The average winter flow for
1989, 1990, and the first three months of 1991 averaged approximately 0.68 mgd
or 68 percent of design.
The plant effluent must meet a monthly average BOD permit'limit of 19 mg/1.
During the period January 1989 to April 1991 the plant effluent was within
permit limits. The plant also must meet a monthly average total nitrogen limit
of 3 mg/1 from April through September. The effluent TKN concentration ranged
from 0.47 to 7.98 mg/1 during the summer months of 1989 and 1990. An average
TKN reduction of 89 percent was achieved during the summer months. The
effluent N03-N concentration ranged from 0.13 to 18.5 mg/1 during the same
period. An average 54 percent reduction in total nitrogen was reported for the
summer period. The monthly average effluent total nitrogen concentration was
greater than the 3 mg/1 plant limit during all the summer months.
The plant does not have an effluent phosphorus limit in its permit and does
not routinely measure phosphorus.
Hanaque. New Jersey
The two oxidation ditches which operate in parallel, at the Wanaque Valley
Regional Sewage Authority wastewater treatment plant in Wanaque, New Jersey are
Eimco Carrousel oxidation ditches. The plant was designed to treat an average
daily flow of 0.7 mgd. The total volume of each ditch is approximately 0.43
million gallons.
The design detention time for each oxidation ditch at average design flow
is approximately 29.5 hours. The average flow for the period November 1989 to
February 1991 was 104 percent of design. The average detention time during
that period was approximately 28 hours.
-------
Page 3-27
The plant was designed for a BOD loading of 12.7 Ibs BOD/day/1000 cubic
feet. During the period of record the average BOD loading was 8.2 Ibs
BOD/day/1000 cubic feet. BOD removals during the period averaged 98 percent
and the effluent consistently met the 8 mg/1 permit limit.
The plant must meet an effluent permit limit of 2.2 mg/1 TKN from May
through October. The monthly average effluent TKN concentration during the
period of record (November 1989 to February 1991) met the permit limit every
month. The average TKN removal was 97 percent both in the summer and during
the rest of the year. Influent and effluent NH3-N are also measured. The
average NH3-N removal in the summer was 99 percent and 98 percent during the
rest of the year.
The plant must meet an effluent phosphorus limit of 1.0 mg/1 year round.
Alum is added for phosphorus removal. The average removal of phosphorus was 83
percent.
Gwinnette County. Georgia
The four parallel oxidation ditches at the Yellow River/Sweetwatef Creek
Reclamation Facility in Gwinnette County, Georgia, are three channel Envirex
Orbal oxidation ditches. A plant expansion was completed in June 1989 to treat
an average design flow of 12 mgd. The volume of each ditch is approximately
1.4 million gallons. Three of the four oxidation ditches are currently in use.
An internal recycle from the third channel to the first channel is used to
promote denitrification.
The design detention time for each oxidation ditch at the average design
flow was approximately 11.4 hours. The average flow for the period January
1989 through December 1990 was 47 percent of design and the average detention
time was approximately 18.5 hours.
The plant was constructed with four primary clarifiers, however, they were
not in use during the period of record. The plant must meet a monthly average
effluent BOD concentration of 5.0 mg/1. During the period of record the plant
consistently met this limit.
-------
Page 3-28
The plant must meet permit limits of 1 mg/1 NH3-N and 6.0 mg/1 N03-N. The
monthly average NH3-N concentrations were less than 1.0 mg/1 for each of the 24
nonths of record. The average NH3-N removal was 98 percent. N03-N data were
available for the period April 1990 through June 1991. The monthly average
N03-N concentration was less than 5.0 mg/1 for each of the 15 months.
The plant must meet an effluent phosphorus limit of 0.5 mg/1. Alum was
added for phosphorus removal. The average phosphorus removal was 99 percent.
-------
Page 4-1
SECTION 4.
OXIDATION DITCH COSTS
CAPITAL COSTS
<
Construction costs were available for ten plants. The construction costs
are for the entire plant but do not include land costs. Capital costs were
estimated from construction costs by adding 15 percent for engineering and
construction supervision and 15 percent for contingencies. All capital costs
were adjusted to July 1991 costs using the ENR construction cost index 4854.
The adjusted capital costs for the ten plants, their design flow, and costs per
gallon per day are presented in -Table 5. The costs ranged from $1.61 to
$9.99/gpd. The costs for the two plants designed for denitrification, Lake
Geneva, Wisconsin, and Patuxent Water Reclamation Facility in Crofton, Maryland
were $8.44 and $6.28/gpd, respectively. These costs are in the same range as
the eight plants not designed for denitrification. Figure 10 presents the
adjusted capital costs for the ten plants.
TABLE 5. CAPITAL COSTS
Facilitv
Cedarburg, WI
Dousman , WI
Dupage County, IL
(Knollwood Plant)
Hanover , PA
Huntsville, TX
(Parker Creek)
Huntsville, TX
(South Plant
Lake Geneva, WIa
Morgan City, LA
Patuxent, MDa
Rehoboth Beach, DE
aDesigned for denitrification
Adjusted
Capital Costs
Julv 1991 (SI
8,238,588
3,464,424
34,526,123
14,321,834
6,911,766
2,574,969
14,691,967
10.284,377
37,702,014
22,914,934
Design
Flow
(mgd)
2.75
0.35
8.3
3.65
2.75
1.6
1.74
4.50
6.0
3.4
$/gpd
2.99
9.99
4.16
3.92
2.51
1.61
8.44
2.29
6.28
6.74
-------
100-
I I I I I I 111 I I I I I I 111
"X DESIGNED FOR DENITHIFICATION
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en
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100
DESIGN FLOW (mgd)
Figure 10. Capital Costs
-------
Page 4-3
OPERATION AND MAINTENANCE COSTS
Overall operating costs for eight plants were available. These costs
include all costs to operate the wastewater treatment plants in the year
indicated. Utility costs, which includes electricity, telephone, and gas for
the entire wastewater treatment plant were available for seven plants. The
costs for two plants are the projected 1991 budget. The design flow, average
flow during the period of record, year, the operating costs, utility costs, and
costs per gallon per day at the average flow are presented in Table 6. The
operating costs per gallon per day ranged from $0.14 to $1.00/gpd. The utility
costs per gallon per day at the average flow ranged from $0.04 to $0.16/gpd.
It should be noted that operating and utility costs vary with plant location
within the United States. The relationship between actual plant flow and
overall operating costs and utility costs are presented in Figure 11.
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-------
-------
Page 5-1
SECTION 5.
REFERENCES
1. Ettlich, William F. , A Comparison of Oxidation Ditch Plants to Competing
Processes for Secondary and Advanced Treatment of Municipal Wastes, EPA-
600/2-78-051, U.S. EPA, Wastewater Research Division, Municipal
Environmental Research Laboratory, Cincinnati, Ohio, March 1978.
2. Process Design Manual for Nitrogen Control. U.S. Environmental Protection
Agency, October 1975.
3. Process Design Manual for Phosphorus Removal. EPA/625/1-87/001, U.S.
Environmental Protection Agency, Center for Environmental Research
Information, Water Engineering Research Laboratory, Cincinnati, Ohio, 1978.
4. Eimco Process Equipment Company, Eimco Carrousel Biological Oxidation
System, Excellence in Biological Treatment, 1986.
5. Riser, Fredrick M. , Nutrient Removal from Wastewater Using the Carrousel
Oxidation Ditch System with the Modified Bardenpho Process, Presented at
the New Jersey Water Pollution Control Association Meeting, May 1990.
6. Eimco Process Equipment Company, Bardenpho Process Biological Nutrient
Removal System, 1984.
7. Envirex, Orbal Aeration System Product Book for Envirex Field Force Offices
and Representatives, August 1989.
8. Envirex, The Orbal System for Flexible Efficient Biological Treatment,
1988.
-------
Page 5-2
9. Innova-tech, Inc., The Total Barrier Oxidation Ditch System. Equipment
information received June 1991.
10. Berk, William L. , Things You Should Know About the Lakeside Oxidation
Ditch, Lakeside Equipment Corporation, RAD-603, November 1984.
11. Lakeside Equipment Corporation, Equipment information and design
information.
-------
APPENDIX A
Monthly Average Tables and Chronological Plots for Wastewater
Treatment Plants Providing Data
Cedarburg, WI
Dousman, WI
DuPage County, IL (Knollwood Plant)
Hanover, PA
Huntsville, TX (Parker Creek and South Plant)
Kemmerer, WY
Lake Geneva, WI
Lyons, WI
Morgan City, LA
Mt. Clemens, MI
Rehoboth Beach, DE
Wanaque, NJ
Yellow River/Sweetwater Creek Water Reclamation Facility,
Gwmnette County, GA
-------
-------
Cedarburg, Wisconsin UUTP - Monthly Average Data.
Date
• QQ
lo9
289
389
^489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
Flow
1.141
1.072
1.277
1.174
1.146
1.467
1.381
1.643
1.578
1.178
1.144
1.034
1.333
1.291
1.898
1.772
2.425
1.708
1.407
1.392
1.393
1.320
1.412
1.663
1.385
1.442
1.948
2.621
Influent Effluent
BOO BOD
(mg/L) (mg/L)
196.4
215.9
165.3
158.3
186.8
143.5
152.2
129.1
144.6
186.7
217.9
227.7
188.2
186.5
162.4
141.7
111.3
133.1
148.6
181.1
177.7
181.1
158.0
152.8
188.7
168.1
133.8
93.9
5.53
5.46
7.00
5.67
6.14
4.60
3.77
2.77
3.20
3.10
3.33
3.39
4.10
3.86
3.74
5.41
2.77
2.65
2.62
2.32
2.57
2.26
2.15
2.03
3.29
2.48
2.74
3.55
Influent Effluent
TSS TSS
(mg/L) (mg/L)
168.9
165.8
146.9
153.4
159.1
136.5
151.6
124.8
130.9
157.5
167.9
176.2
188.2
134.3
122.3
122.3
108.7
125.7
147.6
181.0
166.7
181.4
143.8
127.8
156.8
147.1
117.4
89.8
4.10
3.54
4.68
4.03
4.61
3.03
2.87
2.45
4.67
3.71'
3.60
2.68
2.97
2.43
2.71
2.38
2.58
3.03
2.35
3.13
3.50
3.35
2.27
1.97
3.39
2.93
2.39
2.67
Influent Effluent Influent Effluent
P" PH TKN TKN
(mg/L) (rog/L)
2.5
1
0.6
1.1
1.1
1
0.9
0.94
1.2
1.1
1.3
1.6
0.99
0.67
0.97
1.1
0.72
1.5
0.96
Influent
NH3-H
(mg/L)
25.80
18.05
19.33
15.10
13.62
13.53
15.50
9.58
.10.17
14.00
18.20
20.40
17.96
16.62
12.87
11.60
7.85
11.92
13.86
16.10
16.92
17.48
17.10
15.23
16.77
15.08
11.72
8.05
Effluent
NH3-N
(mg/L)
0.127
0.034
0.331
0.043
0.032
0.035
0.031
0.031
0.030
0.030
0.030
0.112
0.030
0.030
0.030
0.034
0.030
0.031
0.030
0.030
0.038
0.033
0.031
0.036
0.030
0.031
0.030
0.031
Effluent
Total P
(mg/L)
0.602
0.643
0.589
0.765
0.654
0.728
0.698
0.554
0.913
2.520
1.100
0.415
0.560
0.547
0.994
0.620
0.699
0.824
0.574
1.032
0.530
0.813
0.236
0.311
0.502
0.373
0.393
0.649
Hydraulic
Sludge Detention
Age Time
(Days) (Days)
293 "
59.5
60.2
63.1
55.4
53.8
55.3
29.1
34.9
36.6
34.8
36.3
30.4
30.1
30.8
30.4
30.1
21.9
21.8
20.6
18.5
21.0
18.5
16.8
18.7
19.8
17.7
14.4
2.5
2.6
2.2
2.4
2.5
1.92 '
2.04
1.7
1.8
2.4
2.5
2.7
2.1
2.2
1.5
1.6
2.1
1.6
2
2
2
2.1
2
1.7
2
1.95
1.4
.1.1
-------
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Cedarburg. Wisconsin
o.oo
JFMAMJJASONDJFMAMJJASONDdFMA
300
200
100
_A influent
o Effluent
Effluent BOD Limit - 10.0 mg/L
iTi lAl I KJ)l I lAl I lAl I lAl I lilil I lAl I llI till I lAl I lAl I idil I lilil I idil I Irlil I ijil I Ifil Mff114
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100
Effluent TSS Limit - 15.0 mg/L
7. ill • iii i ill i ill i ill i ili i ili i ilt i ill i iL i ill i ill i iii i ili i ili i ill i ill i ill i ill i ili i ill i ill i ili i ill i ill i ili 11.
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
O)
I
CD
X
100
Cedarburg, Wisconsin
so
60
Hi 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 Mill
_ ' ' ' ' ..... 'Mo'nthiy AVerWes1 ! '
-A Influent
-o Effluent
O) .
20
1 1 1
|m|iii|ui[nT[TiL
n 1111111 M 111111111111111 i^fmij-iiLij ill j tL i iJ>i i i/li i ill i ill i i/ii' 'li i i-l-i 11-^1' 'ii i ill 11Jj iiii i ill i iJsi i ill IT
JFMAMJJASONDJFMAMJJASONDJFMA
100
80
60
40
Summer Effluent NH3-N Limit - 2.0
Winter Effluent NH3-N Limit - 4.0 mg/fc-
JFMAMJJASONDJFMAMJJASONDJFMA
5.00
(0
C £_.-^
CD O _J
r-l D. D)
s- tn e
M- O
UJr:
Q.
JJI|lll|lll|lll|lll|lll|lll|lll|lll|lll|lll|lll|lll|lll|lll|!ll|lli|lll|lll|lll|lll|lll|lll|lll|l||||||||ll
Effluent Phosphorus Limit =1.0 mg/k-
4.00
3.00
'~' 2.00
1.00
n nnrnilllllllllllllllilinlllllllllllllllllllllllllllllllllllllllllllllllllllllllllllll
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
9.00
Cedarburg. Wisconsin
-A Influent
o Effluent
8.00
(0
X
Q.
7.00
6.00
Mo'nthi
Effluent pH Limit is between 6.0 and 9.0-
JFHAMJJASONDJFMAMJJASONDJFMA
100
80 _
CD
03
D)
(U
O>
T3
03
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
Dousman, Wisconsin WWTP - Monthly Average Data.
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
Flow Influent Effluent Effluent Effluent
HGO BOO BOD TSS NH3-H
0.192
0.196
0.204
0.194
0.188
0.18
0.181
0.205
0.239
0.188
0.206
0.201
0.206
0.203
0.205
0.21
0.262
0.24
0.216
0.231
0.221
0.211
0.223
0.21
179
178
207
198
156
172
195
196
199
245
196
202
205
184
173
147
155
173
184
171
183
171
155
178
6
7
6
6
6
5
6
6
6
6
6
6
7
6
6
6
6
6
6
5
6
6
6
6
<4
5
<4
<4
<4
<4
<4
<4
<4
<4
<4
<4
5
4
4
4
4
4
3
2
2
3
2
3
2.56
1.3
0.5
0.61
0.56
0.8
0.89
0.7
0.71
"0.55
0.75
1.51
1.56
1.4
1.16
1.32
0.94
0.35
0.29
0.22
0.5
1.18
1.22
1.52
1.91
2.05
1.86
0.91
-------
Q
CD
3:
o
l-i
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01
Q
O
CD
D>
CO
CO
0.30
0.20.
0.10
0.00
rm
Dousman. Wisconsin
lljiil|iil|lll|
Mo'nthly Aver
- Q o o-
JFMAMJJASONDJFMAMJJASONDJFMA
300
200 _
Influent
o Effluent
Summer Effluent BOD Limit - 10.0 mg/L
Winter Effluent BOD Limit - 20.0 mg/C
100 _
JFMAMJJASONDJFMAMJJASONDJFMA
10.0
8.0
6.0
4.
2.0
0.0
-e—e—o o—e—e—e—e-
Summer Effluent TSS Limit » 10.0 mg/tr
Winter Effluent TSS Limit - 20.0 mg/C
Q o o
JFMAMJJASONDJFMAMJJASONDJFMA
3.00
O)
CO
2.00
1.00
o.ooEi
Summer Effluent NH3-N Limit - 2.0 mg/C
Winter Effluent NH3-N Limit =4.0 mg/C
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
DuPage County, Illinois WWTP - Monthly Average Data
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
591
Flow
(MOD)
5.860
4.449
7.083
5.705
5.504
7.157
6.832
6.850
7.566
5.954
6.264
4.885
7.556
8.348
9.672
8.152
12.145
9.271
10.235
9.392
7.972
9.856
9.438
9.001
7.519
8.257
11.108
11.179
9.469
Influent
BOO
(mg/L)
158.0
204.8
142.5
257.0
224.7
196.9
241.3
180.0
113.6
156.6
170.8
253.4
214.9
142.2
238.7
203.5
187.3
236.9
279.0
271.4
224.9
181.3
165.7
155.1
262.7
100.8
156.3
80.5
95.1
Effluent
BOO
(tng/D
7.3
2.6
3.7
5.3
7.7
11.5
3.9
1.6
1.4
2.9
2.3
2.4
4.6
3.2
3.8
2.3
7.1
2.3
3
5.9
7
16
10.6
2.4
2
2.7
11.1
6.4
5.3
Influent
TSS
(rag/L>
163.4
185.9
138.7
362.1
267.8
339.8
480.3
386.8
157.8
307.8
241.9
254.0
379.3
187.4
465.6
303.2
318.1
202.7
280.7
419.5
339.8
304.9
231.5
143.1
450.2
112.0
282.3
113.9
137.2
Effluent
TSS
(mg/L)
12.3
2.4
3.9
3.8
5.1
29.3
9.3
3.3
3.7
• 5.3
5.2
3.6
9.2
5.3
6.4
4.3
16.2
2.1
4.6
8.1
4.3
53.9
39.5
3.4
3.3
4.6
61.9
40
30.2
Influent
pH
(mg/L)
7.9
7.9
7.9
7.8
7.7
7.8
7.8
8.0
7.9
7.9
7.9
7.9
7.7
7.5
7.5
7.4
7.5
7.5
7.5
7.4
7.4
7.5
7.6
7.6
7.5
7.6
7.7
7.7
7.6
Effluent
PH
(mg/L)
7.9
8.0
7.9
7.9
7.9
7.9
7.8
8.0
8.0
7.8
8.0
8.1
7.7
7.5
7.5
7.4
7.4
7.6
7.5
7.6
7.5
7.7
7.7
7.5
7.5
7.4
7.5
7.5
7.5
Influent
NH3-N
(mg/L)
13.5
16.4
10.1
13.2
14.5
13.7
13.7
10.9
9.7
16.3
12.9
16.4
12.0
10.9
8.8
11.3
8.1
12.1
11.4
12.7
16.0
14.0
12.7
11.2
13.1
11.4
8.9
8.6
9.2
Effluent
NH3-N
(mg/L)
0.7
0.2
<0.1
0.3
0.7
0.6
0.4
<0.1
0.2
2.6
<0.2
0.6
1.5
0.4
1.3
0.3
0.2
0.3
0.4
3.4
3.9
0.3
0.6
0.3
0.8
0.5
0.2
0.4
0.5
Mean HLSS
of the 3
Reactors
(mg/L)
2398
2544
2906
2917
2711
2343
2407
2863
2943
2839
2529
2430
2824
2832
2502
3411
2879
3118
3136
3624
3657
3366
3058
2495
2353
2880
2715
2452
2671
Note: High TSS in October, November 1990, March, April and May 1991 are
due to heavy rains.
Aeration system repairs in August and September 1990.
-------
O)
2
m
x
Q.
100
DuPage County. Illinois
_A influent
o Effluent
80
60
40
20
onthly Averages
Summer Effluent NH3-N Limit =2.0 mg/L
Winter Effluent NH3-N Limit - 4.0 mg/C
'idiii^mliidndiMJjM^iii^if^
OFMAMJJASONDJFMAMJJASONDJFMAM
10.0
9.0
7.0
6.0
a Influent
•o Effluent
Effluent pH Limit is between 6.5 and 9.0
JFMAMJJASONDJFMAMJJASOND. JFMAM
January 1989 through May 1991
-------
15.0
DuPage County. Illinois
en
a
o
m
O>
en
en
O.Oi
JFMAMJJASONDJFMAMJJASONDJFMAM
300
200 _
Eftflu^it BOD Limit a 80.0 mg/L
100 _
JFMAMJJASONDJFMAMJJASONDJFMAM
500
400 _
300 _
Effluent TSS Limit * 85.0
200 _
100 _
JFMAMJJASONDJFMAMJJASONDJFMAM
January 1989 through May 1991
-------
Hanover, Pennsylvania WWTP - Monthly Average Data.
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
Influent Effluent Influent Effluent Influent Effluent Influent Effluent
Flow BOO BOD fSS TSS NH4N NH4N TP TP
(HCO) Cog/L) (mg/L) (mg/L) (mg/L) (mg/L) (ing/L) (mg/L) (mg/L)
2.950
2.777
3.491
3.877
7.029
5.036
4.727
4.406
4.256
5.020
5.306
3.395
3.816
3.634
3.095
3.412
3.900
3.206
3.107
3.246
2.537
3.604
3.047
3.855
4.639
3.075
3.369
3.153
287.6
330.0
294.9
281.1
181.9
231.5
217.1
265.5
284.0
277.8
220.9
337.3
251.1
250.0
250.0
258.0
224.0
231.0
248.0
240.0
307.0
255.0
255.0
208.0
147.0
184.0
191.0
223.0
5.0
5.9
7.0
3.8
15.0
3.9
6.0
5.3
5.3
3.3
5.9
7.5
11.7
6.5
6.2
5.8
12.1
5.4
3.9
6.3
4.0
7.5
3.0
8.6
13.5
2.2
2.0
2.9
171.6
178.0
150.5
205.0
152.8
209.3
217.0
338.4
304.5
370.7
333.4
329.0
274.9
250.0
248.0
237.0
243.0
227.0
247.0
238.0
274.0
273.0
252.0
175.0
148.0
236.0
214.0
272.0
3.3
4.7
5.0
3.3
14.0
2.9
7.2
3.5
3.3
2.3
5.0
2.7
6.0
2.9
2.9
1.5
4.6
1.7
4.0
2.7
2.5
5.3
1.4
3.3
10.4
1.0
1.6
1.3
20.2
23.2
16.5
18.8
10.5
14.1
16.5
19.9
24.7 ,
19.9
19.4
25.8
16.1
15.3
19.4
17.7
13.1
16.4
20.4
14.6
20.8
14.6
17.2
12.7
8.9
13.7
11.7
12.5
2.2
8.7
2.4
1.8
4.7
0.5
0.4
0.7
0.9
0.6
1.9
1.5
1.3
0.8
1.1
0.5
1.3
1.0 '
0.9
2.4
2.0
1.6
0.8
5.7
13.1
1.0
1.1
0.2
7.2
8.1
7.4
9.4
5.2
8.5
7.3
9.6
9.4
8.5
7.5
10.5
7.0
7.0
8.3
7.6
7.8
6.8
7.5
7.1
8.4
6.8
7.0
5.3
4.7
8.0
8.0
8.3
1.9
1.9
2.1
0.9
1.2
1.3
1.3
0.9
1.2
0.8
0.7
0.8
0.7
1.1
1.5
1.5
1.1
1.5
2.0
1.5
2.0
1.9
0.9
1.2
1.4
1.9
1.5
1.3
HLSS
(mg/L)
3171
2495
2497
3065
2726
2179
2769
2229
3159
4043
4028
3458
3117
2669
2382
-------
O
(S3
0)
E
a
o
m
•O)
E
10.0
8.0
6.0
4.0
2.0
Hanover. Pennsylvania
o.olllllllllllllllllilililililililil, l.l.l.l.l.hhhl.hhl.l.lil
JFMAMJJASONDJFMAMJJASONDJFMAMJJASONDJFM
500
400
300
200
100
-A influent
-o Effluent
I'lUiI'MI'MMI'I'I'MMM
I'l'I'IM'MI'I'lUJJ'I'J'lU'l'J'J'I'I'J'J'I'i
Effluent'BOD'Limit'-'l2.0 mg/l
^hMuUU^AMU.t^^^44^j
JFMAMJJASONDJFMAMJJASON DJFMAMJJASONDJFMA
400
-U'lM'I'MI'I'MHIH'MHMM
300
200
100 _
I'l'I'I'I'I'I'lU'l'I'I'IMiliJiJililijiiiiii
A EfflUerit'TSS'Limit'-'30.0 Ag/
QlTl 1111 111 111 I h 11 I 11
JFMAMJJASONDJFMAMJJASONDJFMA fTj J A S 0 N D J F M A
January 1988 through April 1991
-------
\
O)
X
O)
£
CO tfi
•p a
o c.
H o
jr
o.
en
o
30.0
25.0-
20.0 _
15.0
10.0 _
Hanover. Pennsylvania
Mill UNI |IJMI Mill l|l|l
1 Monthly1 Averages '
Effluent NH3-N Limit (Summer) -1.5 mg/tr
Effluent NH3-N Limit (Winter) =4.5 mg/t
UM'MlM'I'lMMMM
FMAMJJASONDJFM-AMJJASONDJFMAMJJASONDJFMA
20.0
15.0
10.0
5.0
O.i
Effluent Phosphorus Limit = 2.0 mg/L
hlii.I.Itl.ill iTihhliTiliTi
JFMAMJJASONDJFMAMJJASONDJFMAMJJASONDJFMA
January 1988 through April 1991
-------
CD
Q
O
CJ
25.0
Huntsville. Texas - Parker Creek Plant
111 111 111 111 111 111 MI 111 MI 111 111 111 111 111 m m 111 111 111 111 111 111 111 111 111 11 Mill
- i ' i ' i i ' « i 'Mo'ntniy AWages1 ' ' ' ' ' ' ' ' ' -
_A Influent
o Effluent
20.0
15.0
10.0
5.0
JFMAMJJASONOJFMAMJJASONDJFMA
500
400 _
300 _
fh~ O O G> ^^^"«r ^^ ^
niTiiiTiiiTiiiliiiliitTniliiiliiilnil
200 _
100 _
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
HuntsvUle, Texas - Monthly Average Data
Parker Creek UWTP
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
Flow
HGO
3.500
2.500
2.470
2.170
2.200
2.200
1.900
2.120
2.360
2.370
2.210
2.140
1.800
1.940
1.820
1.840
2.280
1.590
1.820
2.060
2.580
3.260
2.470
2.800
4.130
2.740
2.490
2.850
EFF
BOO
-------
25.0
Huntsville. Texas - South Plant
O)
a
o
o
20.0_
15.0 _
O)
23 10.o_
II! Ill III III MM III III III III III III III III
1 ' 'Mo'ntfilvl AVeiWes1 ' '
_ A influent
o Effluent
JFMAMJJASONDJFMAMJJASONDJFMA
500
400
11111111111111111111111111111111111111111111111111111111111111111111II1111111111111111111111111111111111111
300
200
100
11 m i HI i in 111 n 1111 iTi i ill i iTi i ill
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through .April 1991
-------
6.00
5.00
~ 4.00
Q
CD
Huntsville, Texas - South Plant
3:
o
D)
E
O
O
CD
C
03
=J
CO
•4J
(U
«*-
«4-
Hl
3.00
2.00
Monthi
JFMAMJJASONDJFMAMJJASONDJFM
50.0
30.0
20.0
10.0
Effldent BOD Limit = 10.0 mfl/l_
JFMAMJJASONDJFMAMJJASONDJFMA
50.0
TJTJTT
40.0
30.0
20.0
10.0-
Eident TSs imit - iS. md/l_
o.otmilLL
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
Huntsville, Texas - Monthly Average Data
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
Flow
30 Day 3
HGO (
0.950
0.950
0.820
0.860
0.810
1.000
0.940
0.880
.060
.000
.030
.140
.180
.110
.030
.030
0.950
0.900
0.930
0.940
1.040
0.980
0.940
0.980
1.190
1.110
0.940
1.100
BOO
0 Day
mg/L)
2.6
1.8
2.7
2.9
3.3
2.2
2.3
7.6
2.1
2.2
1.9
2.4
4.3
3.4
3.2
2.0
3.2
4.9
2.2
1.9
2.6
2.5
2.0
3.2
3.7
2.5
1.7
2.7
South UUTP
Raw
COO
234.8
253.2
237.4
299
286.4
201.8
227.9
258.2
268.2
262.5
284.2
421
273.2
220.8
237.2
248.58
256.7
214.3
208.9
315.6
274.7
320
276
343.8
331.2
277.6
334.3
333.7
Final
COO
-------
3:
o
r-i
0.
O)
£
Q
O
CQ
4J
C
-------
a
CD
o
c—I
u_
en
a
o
m
o>
CO
CO
i.oo
0.80
0.6C
0.40
0.20
C3)
Kemmeren. Wyoming
Mot
nln'^"^^'''"''"'"'!'"!'"!!!!!
o o
I I I I I I IM 11i i IiM I , ,, I M . I.., I , , , I,,, ,.. , , 1,, , ,, , . . . . .
JFMAMJJASONDJFM
A M J
300
A Influent
o Effluent
200
100
111 '" I 'J!' I'' M 1111111111II111111
Effluent! BOo'Limi't = 30.0 U/
ig/C
500
I I M I I I |
Effluent TSS'Limi't
A M J J A
MAMJJAS°NDJFMAMJ
January 1990 through June 1991
-------
Kenroerer, Wyoming UWTP - Monthly Average Data
INF EFF INF EFF INF EFF
Date Flow BOO BOO TSS TSS NH3-N NH3-N
(HGO) (mg/L) (mg/L) (mg/L) (mg/L) (mg/L> (mg/L>
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
591
691
0.567
0.560
0.502
0.463
0.446
0.445
0.413
0.402
0.412
0.355
0.418
0.467
0.499
0.574
0.392
0.389
0.417
176
168
203
163
183
202
188
187
199
198
200
259
192
179
161
179
178
158
4.18
5.10
3.58
3.83
4.19
3.11
3.67
1.99
2.12
1.94
2.23
3.89
7.39
8.42
4.15
3.39
2.80
2.20
258
203
354
262
223
242
238
339
296
343
288
326
293
223
243
259
433
334
6.80
8.00
4.25
6.70
6.80
5,30
9.10
4.40
5.00
4.60
3.80
5.70
5.20
6.60
3.60
4.40
3.50
3.10
16.05
15.51
16.89
18.57
18.82
19.38
15.24
17.68
19.41
17.86
20.75
16.38
17.22
15.74
15.08
18.29
16.61
15.14
0.414
0.376
0.102
0.065
0.132
0.078
0.121
' 0.084
0.073
0.072
0.075
0.517
1.073
0.794
0.333
0.092
0.094
0.075
-------
3.00
a
CD
2
o
a.oo
i.oo
en
a
o
CQ
O)
E
CO
CO
o.ooi
Lake Geneva. Wisconsin
-------
Lake Geneva, Wisconsin UUTP - Monthly Average Data
Influent Effluent Influent Effluent Influent Effluent Influent Effluent Influent Effluent Influent Effluent
OHe FtOW iOO BOO TSS TSS TKN TKN NH3 NH3 TN TN N03 N03 HLSS
(mg/L) (mg/L) (mg/L) (mg/L) (mg/L)
169
289
349
<89
SS9
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
591
0.75
0.75
0.80
0.76
0.79
0.80
0.77
1.10
1.09
1.25
1.04
1.02
1.05
1.10
1.35
1.20
1.56
1.38
1.36
1.38
1.23
1.13
1.10
1.12
1.08
1.12
1.26
1.46
1.36
251.2
253.7
233.3
249.5
257.1
257.5
245.9
268.1
233.3
182.1
226.7
251.5
234.0
213.7
179.1
195.7
172.8
193.9
210.9
225.7
207.5
219.6
240.6
221.2
226.8
231.8
209.0
187.9
212.9
6.7
6.0
6.0
3.5
3.8
4.5
3.6
3.0
3.6
4.2
5.3
5.3
5.1
4.8
3.2
3.7
3.7
3.6
2.9
3.8
2.6
3.0
6.4
6.1
6.1
7.3
5.3
14.1
4.2
199.5
187.6
189.8
211.3
230.5
211.4
203.5
236.0
184.0
149.4
188.7
204.0
194.8
175.7
148.1
166.3
153.4
173.7
192.8
181.6
170.1
182.0
205.2
173.2
179.3
194.8
167.4
149.6
171.1
8.1
9.1
8.6
5.6
6.5
7.1
4.6
5.1
5.3
6.6
6.7
6.1
5.1
4.8
4.4
4.1
3.5
3.5
2.7
3.5
3.6
4.9
10.1
10.9
12.1
11.6
6.6
6.7
4.9
33.1
34.7
34.6
30.4
30.3
32.1
30.8
32.4
28.7
25.8
27.1
31.3
33.9
28.7
21.7
26.1
19.8
25.3
25.8
29.2
28.7
27.8
27.2
31.5
26.5
24.2
23.2
23.1
24.5
2.0
2.0
1.8 19.5
1.4
1.4
1.7
1.5
1.3
1.6
1.8
2.1
1.6
2.6 22.0
.9 20.9
.6 7.9
.3
.3
.3
.1
1.4
1.2 17.5
1.2 16.8
1.7 29.8
1.7
1.6 20.0
1.7
1.3 18.2
2.9 13.5
1.7
62.5
35.0
0.4 34.6
33.4
30.3
32.3
30.8
34.1
29.8
27.1
28.9
33.3
2.4 36.0
0.1 31.4
0.3 23.5
28.1
21.9
26.5
26.4
29.4
0.1 30.4
0.2 29.7
1.1 29.6
34.3
0.1 29.4
26.8
0.1 25.9
4.3 25.2
26.3
4.2
3.9
3.7
3.6
3.7
3.5
3.9
3.6
4-0
3.6
4.2
4.9
4.9
4.0
4.1
2.8
3.4
3.8
3.5
3.5
2.9
3.5
4.1
3.9
3.9
4.6
3.8
4.6
4.8
29.4
0.3
3.0
0.2
1.7
1.1
1.3
1.8
2.0
2.1
2.7
1.8
2.0
2.1
1.3
0.6
0.2
1.7
1.8
2.4
2.8
2.9
2.6
2.7
2.1
1.8
2.3
1.9
1.8
2.2
2.2
1.8
2.4
2.3
2.4
1.9
2.2
3.4
2.3
2.1
2.5
1.5
2.1
2.5
2.3
2.1
1.8
2.3
2.3
2.3
2.3
2.9
2.4
1.7
3.2
600
656
625
562
518
538
546
524
544
583
618
588
549
546
513
502
499
503
538
577
633
621
652
642
697
666
636
614
528
-------
CD
c
o>
CD
-P
O
cn
O)
E
I
on
x
CD
O
z
80.0
Lake Geneva. Wisconsin
11111II111111II11111II1111111II1111111111! 11M1111111II111111 It | II11II111 u 11 ll 111111 u 11II111111 ii 11U.
Effluent Total Nitrogen Limit - 10.0 mg/C
n ri>i i rf>i I KPi I ri>i I KPi I m I TO I m i ffl i
0.
JFMAMJJASONDJFMAMJJASONDJFMAM
•HI III III lit III III III llt|MI|lll|IM|MI|lll|HI|1ll|IU]lll|lll|IM|lll|IU|lll|lll|MI|lll|IM|in|l(+l
- A influent
-o Effluent
JFMAMJJASONDJFMAMJJASONDJFMAM
30.0
20.0 _
10.0
0.0
111111111M11111111111 ill I li
JFMAMJJASONDJFMAMJJASONDOFMAM
0.0
JFMAMJJASONDJFMAMJJASONDJFMAM
January 1989 through May 1991
-------
Lyons, Wisconsin WUTP - Monthly Average Data
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
591
Flow Influent Effluent Influent Effluent Effluent
HGO BOO BOD TSS TSS NH3-N
CLbs/d) (mg/L) (rog/L)
0.0576
0.0519
0.062
0.0622
0.067
0.0652
0.0676
0.0734
0.0736
0.0575
0.0567
0.056
0.0576
0.0663
0.1012
0.0916
0.1154
0.0923
0.0809
0.0777
0.0667
0.0649
0.069
0.0786
0.0723
0.0689
0.0866
0.1025
0.0885
247
269
258
266
267
278
274
260
218
253
249
262
278
247
191
174
144
182
231
227
247
269
237
226
256
234
206
139
188
8
7
15
10
9
7
10
10
5
6
6
10
12
7
7
10
9
7
5
3
4
3
4
4
5
6
6
5
3
119
110
124
119
115
134
139
140
127
129
141
139
134
136
105
99
81
114
140
122
138
152
154
125
120
140
124
118
130
9
13
16
14
14
9
23
29
• 17
15
8
12
14
9
7
11
10
12
10
6
4
4
6
5
6
6
8
7
5
1.9
2.05
0.45
0.23
0.43
0.51
2
0.2
0.14
0.17
0.22
4
0.91
1.1
0.71
0.3
0.32
0.25
0.12
0.06
0.43
0.18
0.14
0.45
0.39
0.16
0.06
0.7
0.12
Hote: Plant reports influent NH3-N ranges from 10 - 40 mg/L.
-------
0.20
^ 0.15_
a
CD
2:
~~" o.ioC
a
o
tn
_J
O)
CD
O3
Lyons. Wisconsin
n nnnilllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllllnillIT
0.095
JFMAMJJASONDJFMAMJJASONDJFMAM
400
300
200
100
Influent
Io Effluent
urnimi ill ill ill ill in HI in MI in MI lu.
1 ' kffWnt'BOD L'imlt A 30.01
md/b-
JFMAMJJASONDJFMAMJJASONDJFMAM
200
150 _
100_
JFMAHJJASONDJFMAMJJASONDJFMAM
4.00
I
cn
C D)
UJ
3.00
2.00
1.00
jj MI HIIIIIII Mill] n ii mil M 11111111111 mini i ii ii HI n nil 1111111111 MI ill iiii in it mi n ii n MM i] n MI
-' ' ' ' ' ' ' ' ' ' A ' Effluent Nk3JN liimit '(sJmmdr)'- 3.01 md/
Effluent NH3-N Limit (Winter) - 6.0 mg/lr
ill
lid
JFMAMJJASONDJFMAMJJASONDJFMAM
January 1989 through May 1991
-------
Morgan City, Louisiana UUTP - Monthly Average Data
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
Flow
(HGO)
3.283
2.221
3.254
2.906
3.793
6.143
6.061
4.890
5.373
2.987
4.636
4.680
5.660
6.220
5.020
3.120
2.850
2.48
2.48
3.38
3.98
2.54
2.71
4.32
EFF
BOOS
(mg/L)
4.053
3.933
7.786
4.991
7.521
6.269
8.666
14.810
16.530
15.150
6.285
4.307
6.330
9.640
3.970
3.610
4.040
4.220
4.320
2.990
4.100
3.190
3.560
4.290
EFF
TSS
(mg/L}
3.545
2.476
6.759
4.260
4.138
5.460
4.161
6.195
4.570
4.220
4.663
8.520
5.320
6.440
3.850
3.840
3.160
3.320
4.130
1.810
4.010
2.440
2.590
4.460
INF
NH3
(mg/L)
19.52
17.57
15.68
16.27
15.91
16.78
10.66
10.43
19.57
17.40
11.23
18.45
16.48
18.15
21.53
22.34
23.72
23.38
23.27
22.03
18.51
33.10
26.63
23.90
EFF
NH3
(mg/L)
0.24
0.40
0.19
0.19
0.24
.0.57
0.34
0.55
0.26
0.28
0.34
0.35
0.09
0.75
0.18
0.17
0.17
0.18
0.14
0.17
0.35
0.11
0.15
1.88
-------
a
CD
2
o
a
o
m
QJ Dl
Z3 E
UJ
CD
Cfl
(D D)
ZJ E
UJ
cn
10.0
e.o_
6.0 _
4.0_
2.0_
Morgan City. Louisiana
O.Oi
JFMAMJJASONDJFMAMJJA
S 0 N D
50.0
40.0
30.0
20.0
10.0
O.Oi
Effluent BOD Limit - 30 mg/br
JFMAMJJASONDJFMAMJJASOND
50.0
40.0
30.0
20.0
10.0
0.0
Effluent TSS Limit = 30 mg/f
iiiliiiPm?mrm?mlmTMi?i^
i
JFMAMJJASONDJFMAMJJA
S 0 N D
50.0
dl I lil I ill I ill I dl I ill I iL I ill I ill I ill l ill l ill i 4, i ii|, 11
JFMAMJJASONDJFMAMJJA S. OND
January 1989 through December 1990
-------
Mount Clemens, Michigan UWTP Monthly Averge Data
Date
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
591
691
Influent Influent Influent Influent Influent Effluent Effluent Effluent Effluent Effluent
Flow CBOO TSS TP NH3-M pH TSS NH3-N TP pH CBOO
(MOD) (mg/t) (mg/L) (mg/L) (mg/L) (mg/L) (mg/L) (mg/L) (mg/L)
-------
D)
i
en
en
D
c_
o
.c
CL
CO
en
to
4J
o
H-
CO
X
CL
35.0
Mount Clemens. Michigan
n nhl I I I I I linlnili
•JFMAMJJASOND
F M A M d
5.00
-Effluent Phosphorus Limit =1.0 mg/L
4.00
3.00
2.00
1.00
I I I I I I I I ML
12.
11.0
10.0
9.0
B.O _
I"1!"1!"1!111!"1!1"!"1!"1!111!"1!111!111!111!111!111!11
Effluent pH Range = 6.0 to 9.
T
0-J
4.oD_
H I H I I I ih i i I i i i I i i
FMAMJJASONDJF
M A K J
January 1990 through June 1991
-------
a
CD
3:
o
r-i
U-
8.00
Mount Clemens, Michigan
-4 I I I I I I I I I 1 I I 1 I I I I I I I I I I I I I I I I I I I M I I I I I
='•'«'' MohthlV Averages ' ' '
3 I i I I I I I i M I i i i I i i i I M i I i i i I i i i I i i i I i i i I i i i I i M I i i i I i i i I i i i I i i i I i i f-
JrMAMJJASONDJFMAMJ
O)
E
Q
O
m
o
200
150
100
50
j 1111111 M 111111111111111111111111111 n |TITJTI 111 rrpi i fir ry 111111 r
A Influent"
o Effluenr
0 11 1^1 i i dt I I ' J)' I IJ) I I I i|i I I lj) II ijil I Iffil I lij^l I ijil I lf}il I ijil I ijtl I I ij>Jj|JLJiJ_L 14i I I \i
JFMAMJJASONDJFMAMd
300
DJ
cn
tn
200
100;
jll|I I I|IM|III|II I|II I|I I III I I|I I I|I II|I I I|I I I|I I I|I I I|I I I| I I I | I I I
JrMAMJJASONDJFMAMd
January 1990 through June 1991
-------
a
CD
o
I—J
U.
O)
E
O
O
CD
4J
c
(U
LU
CO
Cfl
f-
3.00
Rehoboth Beach, Delaware
2.00_
i.oo_
o.oo
iiilmliiiliiiliiilmliiilmliiiliiiliiiliiilmliii
JFMAMJJASONDJFMAMJJASONDJFMA
40.0
30.0
20.0
10.0
lll|lll|lll|lll|lll|lll|lll|lll|lll III III III III III III III III III III III Illllllllllllll IIIJIII
- I I I I I I I I «« I I I ' • ' 'Efhu^nt'eofa Limit -' ad m
lTi 1111 n 111 MI n 11111111111111111111111 mi ill imi MI 11111111 n
JFMAMJJASONDJFMAMJJASONDJFMA
30.0
,-^ 20.0_
0)
E
10.0_
in mi mi mi mm mi mi mm mi mm mmi mi mi mi mi mi mi mi
11111111111111 'Efnuint'lSS Limit -' 23
liilmlmlmliiiliiilill
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
Rehoboth Beach. Delaware WHIP - Monthly Average Data
Date
189
289
389
489
589
689
789
889
989
1089
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
391
491
001 Effluent Effluent Influent Effluent Influent Effluent Influent Effluent
Flow BOOS TSS Aitroonia Anroonia TKH TKN N03 N03
(KCD)
0.408
0.425
0.569
0.780
1.007
1.300
1.860
2.016
1.398
1.007
0.803
0.684
0.694
0.676
0.705
0.881
0.774
1.763
2.200
1.917
1.295
0.997
0.840
0.599
0.578
0.546
0.607
0.733
13.12
8.25
5.18
2.40
5.90
5.50
5.40
4.70
1.70
1.20
1.40
2.20
4.00
3.40
2.80
4.00
4.00
4.50
5.30
3.10
3.50
2.20
3.00
2.10
3.00
5.10
5.80
6.20
C«g/L)
5.18
5.16
7.93
9.60
8.40
10.00
9.90
9.10
5.70
7.60
14.10
12.00
11.00
10.00
9.40
11.00
3.00
5.00
7.00
13.00
14.30
4.70
8.00
16.50
13.00
10.00
9.90
5.70
(«g/L) (sg/L) (mg/L)
4.180
1.110
0.510
7.30 0.409 24.70
10.75 3.890 23.60
16.54 0.579 28.50
16.41 1.070 30.80
13.54 0.215 26.20
7.65 0,272 22.30
13.87
15.50
26.90
36.80
33.00
34.37
25.40
18.95
14.41
16.30
13.35
16.23
(mg/L)
5.10
5.17
1.45
1.25
5.35
1.28
2.83
1.66
0.80
1.22
1.12
0.47
2:80
7.98
3.54
1.61
1.24
3.84
5.00
4.90
12.00
2.88
(mg/L)
1.67
1.93
0.74
1.75
2.56
4.05
2.51
1.97
0.10
0.15
2.10
4.27
2.95
0.37
2.51
2.94
0.62
1.06
(mg/L)
9.92
13.43
10.33
9.28
8.24
17.60
7.56
4.34
15.47
11.27
11.34
18.49
3.60
0.13
11.48
22.00
12.20
13.30
11.00
9.40
6.35
7.60
Influent Effluent
Total N Total N
(mg/L)
26.30
26.10
27.20
32.10
28.60
26.30
-
16.40
17.30
27.00
36.95
35.00
38.60
28.40
19.33
16.87
19.23
13.95
17.27
(mg/L)
14.83
18.20
11.77
10.70
13.44
17.60
11.68
5.94
16.16
12.50
12.40
18.82
6.39
8.08
14.96
23.60
13.49
17.20
16.10
14.30
18.00
10.30
Minimum
pH
(s.u.ll
7.02
6.60
6.20
6.40
6.40
5.90
6.60
6.70
6.76
6.30
6.40
6.50
6.30
6.40
6.40
6.30
6.30
6.70
6.50
6.50
6.30
6.40
6.10
6.30
6.20
6.10
6.40
6.60
Maximum
oH
r"1
7.17
7.30
7.50
7.10
7.20
7.00
7.70
7.10
7.29
7.10
7.00
7.20
7.20
7.00
7.00
6.90
6.90
7.10
7.00
7.70
6.80
7.10
7.00
6.70
6.90
7.10
8.00
7.20
-------
O)
c
CD
O)
O
(D
-4J
O
40.0
30.0
20.0 _
10.0 _
Rehoboth Beach, Delaware
Effluent Total N/trogen IMmit - 5.0 mg/f
o nhllllllllllll
JFMAMJJASONDJFMAMJJASONDJFMA
D)
50.0
40.OZ
30.0 ~
20.or
10.01
JFMAMJJASONDJFMAMJJASONDJFMA
20.0
O)
fD
•rt
C.
O
15.0
10.0
O.OUl
TTU
JFMAMJJASONDJFMAMJJA
"lIlllllIT
SONDJFMA
30.0
25.0-
•I
I
*0
JFMAMJJASONDJFMAMJJASONDJFMA
January 1989 through April 1991
-------
Uanaque Valley, Neu Jersey WUTP - Monthly Average Data
Dote
1189
1289
190
290
390
490
590
690
790
890
990
1090
1190
1290
191
291
flow
(HCO)
0.75A
0.665
0.719
0.784
0.742
0.769
0.8S9
0.729
0.659
0.763
0.661
0.64
0.655
0.783
0.752
0.705
INF EFF INF EFF IMF EFF INF EFF INF EFF INF EFF Average
BOOS BODS B0020 BOD20 TKN TKN NH3 NH3 TSS TSS Tot P Tot P MUSS
(mg/L) (mg/L) (mg/L) (mg/L) (mg/L) (mg/L) (mg/L) (rag/L) (mg/L)
166.0
154.0
224.0
221.0
220.0
199.0
122.0
134.0
141.0
137.0
115.0
161.0
141.0
116.0
122.0
109.0
3.30
2.50
2.20
3.00
2.70
2.20
2.90
2.00
2.50
2.20
1.90
1.70
1.10
2.00
2.70
5.30
239
243
297
360
324
284
164
178
199
198
160
195
196
167
162
128
8.60
5.00
8.70
9.40
5.90
5.90
5.10
3.70
4.40
3.10
2.90
2.40
2.60
4.00
3.40
5.60
38.0
30.0
48.0
41.4
40.0
35.0
26.0
27.3
24.8
29.3
35.8
40.3
41.0
27.5
25.0
30.0
1.40
1.80
1.90
1.90
0.83
0.56
1.50
0.91
0.84
0.65
0.37
0.47
0.65
1.00
0.90
1.40
23.0
19.0
40.0
18.0
40.0
18.6
18.4
19.9
23.0
20.0
20.8
26.3
26.8
15.8
15.9
17.5
0.46
0.77
0.67
0.51
0.76
0.30
0.14
0.41
0.12
0.14
0.12
0.13
0.15
0.29
0.30
1.19
104
117
188
127
120
76
105
95
121
140
138
132
164
93
125
104
1.80
2.70
3.00
6.50
5.00
5.00
3.70
3.20
1.90
2.20
1.12
2.00
2.90
6.40
7.20
6.30
4.6
2.0
3.6
3.9
5.0
4.1
3.7
4.3
3.9
4.3
4.8
5.5
5.1
3.1
3.2
3.5
1.20
1.10
0.54
0.88
0.84
0.75
0.70
0.84
0.48
0.57
0.66
0.58
0.41
0.44
0.42
0.35
2684
1941
2507
2009
2318
2447
2275
2043
2300
2280
2523
2639
2829
3540
Mote: Began adding chemicals for phosphorus removal in January, 1990
-------
o
o
i-H
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in
d
o
m
en
e
o
cxi
a
o
ca
en
en
2.00
1.50
i.oo
0.50
0.00
Wanaque Valley, New Jersey
JI I I I I I I I I I I I I I I I I I I I I I I I I II I I I I I I I I I I I I I I I | II
11111 Monthly Av'eragfes '
I I I I I I I I L
-i i i I ii i I i i i I i i i I i i i I i i i I i i i I i i i I i i i I i i i I i i i I i i i I i i i I i i i I i i r
NDJFMAMJJASONDJF
400
300 _
200 _
100 _
J I I I I I M I I M I I I I M I I I I M I I I I I I I I I I I I I I I I I I I I L
NDJFMAMJJASONDJF
BOO
J I I I I I I I I I II I I I I I I I I I I I I I I I I I I I I I | I I I | I II | I I I | I I L
600
400
NDJFMAMJJASONDJF
300
200
I I I | II I | I I I | I I I | I I I | I I I [ I I I | II I | I I I | I I I | I I I | II I | I I I | I I l_
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NDJFMAMJJASONDJF
November 1989 through February 1991
-------
BO.O
Wanaque Valley, New Jersey
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Influent
f-o Effluent
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NDJFMAMJJASONDJ
50.0
I I I | I I I | I M | | M | I I I | I I I | I I | | | | | | I I I | I I M
40.0_
30.0_
CD 20.0_
10.0_
NDJFMAMJJASONDJ
20.0
J " | N ' | I ' I | I I I | II I | I I I | I I I | I H | I I I I I I I I I I I I I I I I I I I |
CD
J§ 15.0
(0
3
C.
O
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Q.
CO
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10.0
5.0_
.oTTTTTlTr^rn T111T
-MO I I Id) I M
NDJFMAMJJASONDJF
November 1989 through February 1991
-------
20.
15.0
D)
m
10.0
5.0
O.Ot
Gwinnett County, Georgia
Effluent NH3 Limit = 1.0 mg/L
JFMAMJJAS°NDJFMAMJJASOND
o
D-
50.
•40.0_
^7 30.0_
Effluent P04 Limit - 0.5 mg/l_
20.0_
10.0_
JFMAMJJAS°NDJFMAMJJASOND
January 1989 through December 1990
-------
GU1NHETT COUNTY WATER RECLAMATION DIVISION
IMF EFF INF EFF IMF
A.D.F. BOD BOD TSS TSS NIB
(HOD) (mg/L) (mg/L)
0.300
0.200
0.200
0.140
0.170
0.090
0.390
0.140
0.040
0.430
0.500
0.310
0.520
0.526
0.880
0.050
0.084
0.030
0.600
0.060
0.060
0.063
0.090
0.310
35.3
31.6
22.9
28.7
28.4
48.7
24.3
23.4
20.1
22.0
31.7
10.3
8.4
7.4
8.1
10.5
7.0
8.9
6.8
5.5
5.8
5.4
7.0
6.2
EFF
P04
(mg/L>
0.30
0.20
0.20
0.33
0.36
0.28
0.21
0.31
0.16
0.18
0.11
0.55
0.19
0.18
0.25
0.39
0.38
0.31
0.23
0.14
0.14
0.17
0.13
0.19
EFF AVG
N03 HLSS
(mg/L)
-------
Q
CD
15.0
Gwinnett County. Georgia
10.0 _
5.0 _
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JFMAMJJASONDJFMAMJJASOND
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Effluent BOD Limit - 5.0 mg/L.
-A influent
o Fffluen
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JFMAMJJASONDJFMAMJJASOND
2000
Effluent TSS Limit - 8.0 mg/IT
ll i ill i ill i ill i ill i ill i ill i ill i ill i ill I ill I ill I ill I ill I ill I ill I ill I ill I ill I ill I ill 11.
MAMJJASONDJFMAMJJASOND
January 1989 through December 1990
S. Government Printing Office : 1992 - 312-014/40168
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