-------
o a
= O I-.O O O
o ca a o o o
.* -a o u-i o
o 5 "** o* —* *3
•** o ^ <^i t-» «o
u b.
•3'fl ""I jrj:oi-H
-------
adverse conditions, wet weather, steep slope or both,conventional
harvesting would be used 50% of the time. Otherwise 7070 is to be harvest-
ed with the new equipment and 30% (steep slopes and gullies) by con-
ventional means. The BOD values are very rough estimates. We really
have no clear idea what the levels can be with all systems operational.
265
-------
ACKNOWLEDGEMENTS
This report is not the work of any one or two authors. It represents the
collective effort of several engineers most notably Charles Hart and
Clarence Montgomery and Virgil Hendricks of C. Brewer and Company,
Limited, Engineering Department for harvester development; Lane S.
Thompson', Dr. James Kumagai and James Honke, Consultants from Sunn, Low,
Tom and Kara, Inc. on water treatment; Melvin Tanaka of W. A. Hirai &
Associates, Inc. for dry cleaner and juice washer development and
finally, William Blockley and Richard Webb of Hilo Coast Processing
Company for power plant development.
Hilo Coast Processing Company is particularly grateful for the
financial assistance made possible by the Environmental Protection
Agency. Ken Dostal of the Pacif/ic Northwest Water Laboratory together
with Russel Freeman, Charles Seeley and other EPA personnel from Region
IX have been extremely helpful in their advice and encouragement on this
project.
266
-------
REFERENCES
1. Caswell, C. A., (1972) "Notes on Dilution as an Effective Pollution
Control Technique." Industrial Water Engineering p. 10-11
2. Engineering Science, Inc. & Sunn, Low, Tom & Kara, Inc., (1971)
"Water Quality Program for Oahu with Special Emphasis on Waste Disposal."
Department of Public Works, City and County of Honolulu (pages VIII-18
to VIII-25)
3. Environmental Protection Agency, Region IX, San Francisco, California,
(1971) "Hawaii Sugar Industry Waste Study." (pages 27-32)
4. Grigg, Richard W. (1973) "Some Ecological Effects of Discharged Sugar
Mill Waste on Marine Life Along the Hamakua Coast, Hawaii." Water
Resources Research Center, University of Hawaii No. 2.;:
5. Kennedy Engineers (1967) "Report on Hawaiian Sugar Factory Waste
Receiving Water Study." Prepared for the Hawaiian Sugar Planters'
Association.
6. Payne, John H. (1968) "Sugar Cane Factory Analytical Control."
Elsevier Publishing Company, pp 190.
7- Sunn, Low, Tom & Hara, Inc. (Environmental Consultants - Honolulu, HI)
(1972) "Evaluation of Process Objectives and Pilot Plant Investigation
of Tube Settler Clarification and Vacuum Filter Sludge Dewatering."
Prepared for C. Brewer and Company, Limited and Hilo Coast Processing
Company.
8. Sunn, Low, Tom & Hara, Inc. (Environmental Consultants, Honolulu, HI)
(1973) "Waste Water Management Alternatives and Functional Design of
Recommended Wastewater Treatment Facilities at Pepeekeo." Prepared
for Hilo Coast Processing Company.
9. EPA Proposal #8-801221 "Ecostatic Cane Processing System - Prototype Phase,
1972
10. EPA Proposal #802420 "Ecostatic Cane Processing System - Pilot Phase,
1971
267
-------
PRACTICAL APPLICATION OF A
BIOLOGICAL/PHYSICAL/CHEMICAL TREATMENT SYSTEM
TO MEAT PACKING WASTEWATER
by
Gilbert F. Hill,* Glenn W. Dunkelberger, Jr.*
INTRODUCTION
The meat packing industry has received considerable attention in the
area of pollution control. There are many varied treatment systems
employed by the industry, but by far the most utilized mode of treatment
has been biological in nature. Activated sludge, aerobic and anaerobic
lagoons, trickling filters, rotating contactors, as well as the channel
aeration process have been satisfactorily utilized. Air flotation,
using coagulating agents, as well as the common "catch basin" process
represent the major processes in the area of physical and chemical
treatment.
We at Gilbert Associates, Inc. have had the opportunity to work with
the Roberts Packing Company as consulting engineers for the operation
of their unique waste treatment system. As system consultants, we
have observed and evaluated Roberts' biological, physical, and chemical
unit process oriented waste treatment system. It is felt that by
examining this approach to waste treatment, the advantage in the
utilization of a combination of treatment modes (i.e. biological/
physical/chemical) can be realized.
* Supervising Engineer and Industrial Waste Engineer respectively
Gilbert Associates, Inc. - Reading, Pennsylvania
268
-------
The Roberts Packing Company is engaged in the manufacture and sale of
pork and pork products such as ham, bacon, frankfurters, bologna and
scrapple. In the past Roberts slaughtered an average of 750 hogs per
day for two days a week, and processed pork products five days a week.
Presently, slaughtering is not performed at the plant, and the plant
devotes five days a week to the processing of 50,000 pounds of pork
products per day. The major sources of wastewater are: 1. Carcass
washdown; 2. Scalding wastes; 3. Screened dehairing wastes;
A. Cooling waste; 5. Smoke house wastes; 6. Meat cooking and general
clean-up wastes.
WASTEWATER TREATMENT
Wastewater treatment consists of 4 unit operations which are presented
in Figure 1 - Waste treatment flow diagram. 1) Flotation of insoluble
grease in catch basins. 2) Chemical treatment using ferrous sulfate
and chlorinated lime. 3) Primary - rapid filtration through leelite
sand filters. 4) Secondary - slow filtration through biological
leelite sand filters. The raw waste biochemical oxygen demand
concentration ranges from 2400 mg/1 to 1500 mg/1 on the average,
corresponding with average suspended solids concentrations of 1400 mg/1
to 1000 mg/1 on kill and non-kill days, respectively. The first
treatment process, separation of floatable greases, is basically a
physical unit operation.
Grease Removal
The catch basins are rectangular basins which provide an average of
1.5 hours retention time. This retention time, in addition to adequate
surface area, allows most of the floatable material to collect on the
269
-------
o: ac — z —
IT
O
<
Q
§
U_
H
Z
LU
Ld
CC
UJ
H
LJ
cr
o
270
-------
surface of the basins. All material with specific gravities less than
water do not float to the surface since the retention time may not be
of sufficient length to allow slow rising materials to reach the
surface. Also, some lighter than water material may be characterized
by having surface charges rendering these particles hydrophilic in
nature. A definite advantage in removing the floatables as a first
step in treatment is that it is sold as a renderable material. One
hundred gallons of material is daily skimmed from the catch basins
and placed in barrels. The size of the plant does not warrant
mechanizing this operation. The waste flow leaves the catch basins
and enters one of three 20,000 gallon batch operated chemical treatment
tanks.
Chemical Precipitation
When a tank is filled, the content of the tank is mixed using diffused
air. Chemical dosages typically used are: 100# lime, 100// ferrous
sulfate, and 25# of chlorinated lime. Following chemical addition, the
tank is mixed for a minimum of 10 minutes, and allowed to quiescently
settle for approximately 3 hours. By use of a series of discharge
ports located at various depths in the tank, the treated wastewater
is directed to the next treatment step. The sludge resulting from the
chemical treatment and accumulated at the bottom of the tank is
discharged by gravity to a tank truck for land disposal. The actual
chemical dosages, mixing time, and settling time are varied by the
waste treatment plant operator. The system is manually operated and
the experienced operator adjusts process variables according to the
varying waste loads encountered during operation. Factors such as
color and general appearance are used in determining the chemical
271
-------
treatment requirements. Using the above mentioned method of chemical
treatment, this unit has shown biochemcial oxygen demand reductions of
50% on an average. Suspended solids are removed to levels averaging
95%. Total phosphate reductions of up to 95% have been found for the
chemical treatment step as well as the other mentioned reductions.
Typical non-kill day chemical treatment effluent is characterized as
follows: 750 mg/1 biochemical oxygen demand, 50 mg/1 suspended solids,
and 20 mg/1 total PC^. A significant chemical factor which creates
this reduction is the process of coagulation. The calcium and iron
ions and their associated charged molecules reduce the surface potential
of the particles rendering them susceptible to gravitational forces.
Precipitants of the coagulating ions also tend to encircle, or enmesh,
particles contained in the wastewater resulting in the combination of
the particle and coagulating ion group being able to settle by gravity.
Although the exact means of reduction of biochemical oxygen demand,
suspended solids and total PO^ has not been totally established, the
above postulations are rational explanations. After chemical
treatment, the supernatant from the 20,000 gallon tanks is further
treated by rapid sand filtration on primary filters.
Primary Filtration
The primary filters are constructed of leelite sand with an underdrain
collection system. The filters function to reduce the suspended solids
and any solids associated biochemical oxygen demand present in the
waste flow. A set of four filters is used alternately providing for
time to dewater and clean each filter as required. The chief function
of these filters is to remove carry-over precipitant and suspended
solids from the chemical treatment step. When wet sludge from the
272
-------
chemical precipitation tanks is trucked for disposal, the four filters
provided for sludge dewatering are used for supernatant filtration.
Any possibility of biological growth in these filters is eliminated by
a slight chlorine residual in the flow, as well as the hydraulic
loading rates utilized. The filters are flooded, which prevents oxygen
penetration from the atmosphere. Also, the relatively short detention
time of the flow in the filters results in creating unfavorable
conditions for biological growth. The effluent from these filters,
which constitutes influent to the next unit process, typically is
characterized by the following values: 500 mg/1 biochemical oxygen
demand and 20 mg/1 suspended solids.
Secondary Filtration
The final unit in the system is that of biological filtration. These
filters are of leelite sand construction with an underdrain system.
Unlike the filters used for physical removal of solids, the biofilters
are designed to allow the slow drainage of flow through the sand media.
A relatively large surface area, and a multi-point influent system
provide for the low hydraulic loading rate. Due to this low loading
rate, oxygen from the atmosphere is permitted to come in contact with
the filter media. Also, the detention time of an increment of flow,
relative to the sand media is comparitively long. The factors of
oxygen availability and detention time promote biological growth on and
in the filters with average biochemical oxygen demand removals of 90%.
The exact biota involved in the secondary filters is not known. It
would seem logical to assume the culture would be similar to that
found on trickling filters. The total system consistently produces
273
-------
effluent reflecting over-all reductions of: 95% biochemical oxygen
demand, 95% suspended solids, 95% total phosphate.
MERITS OF MULTI-MODE TREATMENT
The system utilized at Roberts has been presented to show the
applicability of combining several modes of treatment into a workable
system. The merits of a multi-mode waste treatment system for Roberts
Packing starts with the use of the physical separation and recovery of
grease from the flow in the catch basin units. The ultimate sludge
disposal problem is partially reduced through disposal of the recovered
material to a rendering plant. This also has a secondary but inviting
advantage of providing some revenue. The chemical treatment step has
several merits, depending on one's point of view.
By reducing the organic strength of the waste, any biological units
following the chemical treatment need not be sized as large as if they
.were designed to treat the raw waste. Chemical treatment also has the
advantage of requiring only a relatively short time for reduction of the
waste load. Correspondingly, land space can be less for chemical
treatment, than for biological treatment. As in the case at Roberts,
chemical addition feasibly cannot generally remove the total waste load
present.
With significantly reduced waste loads, biological treatment functions
to further remove pollutants to satisfactory levels. Although the
system at Roberts' has produced excellent results, each waste treatment
problem must be investigated with an open mind in order to provide the
most efficient and economical system.
274
-------
It is hoped that this brief presentation has indicated the merits of
using biological/physical/chemical treatment modes. With the ever
increasing demand for "clean" water, the task of the waste treatment
system designer is to investigate all available methods of treatment.
It is felt that in too many cases, industrial waste treatment systems
have been designed with the assumption that biological treatment is
the only feasible mode. The use of biological treatment is not the
issue, but the advantage in using physical and chemical processes in
connection with biological units is the key point. Although the system
in use at Roberts is almost 20 years old, it's ability to meet the
present water quality criteria dramatically indicates the advantages
of a multi-mode waste treatment system.
275
-------
SMALL MEAT-PACKERS WASTES TREATMENT SYSTEMS
by
Jack L. Witherow*
INTRODUCTION
The technology reported herein will be helpful to the meat-packing industry,
especially the smaller plants, in control and treatment of their wastewaters.
The number of establishments processing red meats is about 14,000 of which
some 10,000 are estimated to be small plants. A small plant is defined by an
annual liveweight kill of less than 25,000,000 pounds. Wastewaters discharged
to receiving waters need treatment to meet effluent criteria. Many plants dis-
charge to a municipal treatment system; but, sewer charges and pretreatment
regulations require treatment of these discharges also.
The treatment systems investigated were picked to meet requirements that are
common in the meat-packing industry. These include: (1) reduction of
oxygen demanding material, suspended solids and grease for discharge to
a municipal sewer; (2) equivalent secondary treatment for discharge to a
surface water; (3) reduction of nitrogen, especially in the ammonia form,
and phosphorus. Discharge limitations on nitrogen and phosphorus are
becoming common and are expected to be placed on most discharges in the
future.
Waste treatment systems for small meat-packers should include the following
constraints:
1. The process and operation should be as foolproof as possible.
2. Mechanical equipment should be minimized and designed to prevent
undetected failure.
3. Treatment should be easily monitored and meet effluent limits.
4. Design should allow simple construction to reduce cost.
The unit processes demonstrated were designed to reduce and simplify the
operation of the treatment system. Small packers do not have personnel
trained in the operation of treatment plants. Simple operation is even more
important than minimal costs for construction; hov/ever, a design which
allows plant personnel to undertake construction can reduce costs.
*Chiof, Agricultural Wastes Section, Treatment and Control Research Program,
Robert S . Kerr Environmental Research Laboratory, National Environmental
Research Center-Corvaliis, Office of Research and Monitoring, U.S. Environ-
mental Protection Agency.
276
-------
The facilities used in the development said demonstration project described
herein (12060 GPP) are located at the W. E. Reeves Packinghouse on the out-
skirts of Ada, Oklahoma, about three miles from the Robert S. Kerr Environ-
mental Research Laboratory. The packing company's need to obtain better
waste treatment and control facilities and the Research Laboratory's need for
a waste source and pilot plant test facilities resulted in a cooperative researcl-
effort. Because of limited manpower at the Research Laboratory, East Central
State College in Ada, Oklahoma, joined this cooperative project, supplying
faculty and students to do the chemical analyses.
The W. E. Reeves Packinghouse produces some 30 items including cut and
uncut beef and pork and its own brand of fresh sausage, bacon, weiners,
cold cuts, chili, and other meat items . Meat products sold represent about
60 percent of liveweight killed (LWK) . Smoked and spiced products are 15
percent of the LWK and processed meats are 25 percent of the LWK. Sales
are in the surrounding area mainly to retail groceries and restaurants.
The plant processes 500 to 700 cattle per month and 600 to 800 hogs per month,
or about 10 million pounds of live weight annually. The plant is located west of
the city on 64 acres of rolling land. An unnamed creek flows north through
the property. The prevailing v/inds are from the south. North of the plant
are cattle ranches with the nearest residence 1 1/2 miles distant. South and
southwest of the plant the nearest residences are 1/4 mile distant. Besides
the processing plant, cattle pens, storage areas for machinery and materials,
and parking areas are located on the grounds.
OBJECTIVES
The objectives consist of developing and demonstrating treatment systems
selected to meet present and future needs of the meat industry, especially
the small meat-packers. The treatment systems are combinations of the
following biological processes: anaerobic lagoon, transitional lagoon,
stabilization lagoon, aerated lagoon, and spray-runoff irrigation.
The detailed project objectives were grouped into a two-phase investigation.
In the first phase which is reported in this paper there were two objectives.
The first objective was to demonstrate the anaerobic-aerobic lagoons system
to meet the requirement of the small meat-packer for discharge to a municipal
sewer and to a stream. This system was selected to demonstrate its simplicity
of operation and minimum capital and maintenance cost with high removal
efficiencies. The treatment system consisting of an anaerobic lagoon, a
transitional lagoon, and a stabilization lagoon was designed to obtain greater
than 95 percent BOD removal producing an effluent of less than 50 mg/1. The
cost of operation, maintenance and construction was documented. The need
for sludge recirculation in the anaerobic lagoon was evaluated since removal
of the recirculation pump would result in a system without a moving part,
thereby greatly reducing operating requirements. The three lagoons were
evaluated separately as one or two lagoons were expected to meet require-
ments for discharge to a municipal system. The second objective was to
develop and demonstrate the spray runoff irrigation process to meet require-
ments for 80 percent removal of nitrogen and phosphorus. This process
system was demonstrated in series with the anaerobic lagoon.
277
-------
In the second phase there are also to be two objectives; one of which is to
continue evaluation of the spray runoff irrigation process using both effluent
from the aerated lagoon and raw wastewater for nitrogen and phosphorus
removal. The other objective is to develop and demonstrate the economic
and technical advantage of an all aerobic lagoon treatment system. This is
critical where hydrogen sulfide odors will create a nuisance or where low
ammonia limits are imposed. The anaerobic lagoon is to be converted to
an aerated lagoon. Operation will be on a batch basis with discharge
occurring after settling conditions are applied. Operation of the mechanical
parts of the system is to be automated to meet the small meat-packer's needs.
The second and third aerobic lagoon will be evaluated separately to demon-
strate the different levels of removals obtainable. The aerated lagoon is
expected to meet requirements for discharge to a municipal system. The
two or three lagoon treatment systems are expected to meet requirements
for discharge to surface waters.
DESIGN
The design procedure is described in detail for the small meat-packer and
is divided into preliminary design and detailed design. Preliminary design
includes measure of the wastewater, selection of suitable treatment systems,
sizing of the unit process, and review by the regulatory authorities. Detail
design includes the preparation of plan, specification and modifications
during construction.
Preliminary Design
The W. E. Reeves Packinghouse wastewaters come from the slaughtering area,
the meat processing areas, the lavatory, the hide storage cellar, and the
holding pens. The major waste load is from slaughtering which is a one-shift
operation, Monday through Friday. Meat processing is on a 5 1/2 day basis.
The hide cellar is emptied and flushed once a month and the holding pens are
dry cleaned and then flushed on Saturday.
Wastewater flows and concentrations were both measured. Eig;ht hourly samples
were taken and composited during slaughtering/processing on May 19, 1970,
and on June 9, 1970. A grab sample was taken on June 19, 1970. The samples
were analyzed according to Standard Methods. The data are tabulated in Table 1
Table 1. Wastewater Chemical Anaylses for Preliminary Design
Item May 19. 1970 June 9. 1970 June 19, 1970
BOD 2680 1352 1165
Grease 1823 434
TKN - 108.5 110
NHi-N - 15.5 10
NO2-N - 0.18
N03-N - 0.24
Total P - 31.4
278
-------
The BOD and grease data exhibits the variation normally found in slaughter-
house wastes which are reported as 650 to 2200 rng/1 and 200 to 1000 mg/1,
respectively (2) . A weighted average BOD concentration of 2000 mg/1 was
selected for design purpose. The temperature of the wastewater was 25° to
28° C. There is sufficient nitrogen and phosphorus for biological treatment.
To measure flow, a Parshall flume with a 3-in. throat was installed with a
flow meter. The flow on killing days and Saturday is tabulated in Table 2.
A flow of 15,000 gallon/day was used for design purposes.
Table 2. Wastewater Flow Analyses for Preliminary Design
Date Flow (gallon) Operating Period (hrs)
6/18/70 Thursday 19,152 8
6/19/70 Friday 15,072 8
6/20/70 Saturday 2,495 3
6/22/70 Monday 14,040 9
6/23/70 Tuesday 15,498 9
6/24/70 Wednesday 14,274 10
Total 1 week 80,531 gallons 47 hours
A tour of the packinghouse land revealed several potential sites for a treatment
system. The sites adjacent to the plant were used for holding and feed pens,
and storage of materials and equipment. The site selected was in a pasture
and solid waste disposal area 300 feet west of the plant. This site permitted
a gravity flow system eliminating the necessity for pump maintenance and
operation. The disadvantages were land slope and a conglomerated rock layer
immediately under the surface. The site had sufficient land available for selection
of an anaerobic-aerobic lagoon system. The trade off of land value for the costs
of concrete and steel in more compacted systems was possible, and the lagoons
could be constructed by plant personnel to reduce cost.
The anaerobic-aerobic lagoon system has obtained greater than 90 percent
first stage BOD reduction with highest removals during the critical hot summer.
Outside of the desired minimum capital and operating costs, the system is simple
to operate and shows visible treatment results; mechanical equipment can be
held to a minimum to prevent failures; and the treatment processes can with-
stand the typical shock loading of the meat-packing industry.
The anaerobic process is especially suited to this concentrated hot waste.
Schroaffer (3) demonstrated 90 percent BOD removal at very high loading of
0.25 Ib/cu ft/day at 30°C and at 0 .10 Ib/cu ft/day at 25°C in a constant tempera-
ture reactor. More recent developments have shown the suitability of the
anaerobic lagoon (4) (5) (6). State regulatory agencies in Illinois, Iowa,
Nebraska, Tennessee, Pennsylvania, and Minnesota accept design loadings
279
-------
of 15 Ib BOD/1000 cu ft of anaerobic ponds allowing 60 percent BOD removal.
Using a sludge recirculation system, Hester (7) obtained an average of 80 per-
cent removal with loading of 9.6 to 12 lb/1000 cu ft/day and sludge recirculation
ratio of 2 to 1. After the first year's operation, BOD removals continually
exceeded 90 percent.
The anaerobic lagoon has given high removal efficiency with and without
sludge recirculation. The benefits of sludge recirculation have not been
established (4) (8) . Elimination of sludge recirculation could result in a
reduction of costs and simplifying operation, an especially desirable factor
for small meat-packers. In some cases, a sulfate concentration of over 200
mg/1 in the water supply has resulted in objectionable hydrogen sulfide odor
production in the anaerobic pond. Additionally, the anaerobic pond reduces
the protein (Kjeldahl nitrogen) to ammonia which is also toxic to fish.
Following the anaerobic pond, a variety of aerobic processes have been
utilized (8) . A two-stage aerobic lagoon process was selected. For the
small plant, the aerobic lagoon offers the advantage of simple operation.
The one- and two-stage aerobic lagoon systems have been successfully
applied (4) (6) (7) both with and without mechanical aeration of the first
stage. The first stage aerobic lagoon is considered a transition pond and
the second a stabilization pond. Successful operation was achieved with
organic loadings up to 130 Ib of BOD/day/acre on one stage (4) and 113 and
56 Ib BOD/day/acre for 1st and 2nd stages, respectively (7) . A design
factor developed by Coerver (6) for small packers is based on the number
of beef cattle killed multiplied by three plus the number of hogs killed; pond
design is then based on this "equivalent" number of hogs killed. The design
loading in Louisiana is 800 hogs/week/acre ft in the anaerobic pond and 690
hogs/week/acre of surface area in two aerobic ponds in series. With a waste
load of 2.5 Ib BODs/hog and a 5-day per week killing operation, this is
equivalent to 9 Ib BOD5/day/1000 cu ft on the anaerobic pond. Assuming
an 80% removal in the anaerobic pond, the equivalent loading on the aerobic
lagoons would be 70 Ib BODs/day/acre.
The anaerobic-aerobic lagoon system selected will not meet the future needs
for reduction of nitrogen and phosphorus . To meet future needs, the spray
runoff irrigation system was selected in combination with the lagoon system.
Spray runoff systems have been used successfully for a variety of wastewaters
including those from paper mills, canneries, and municipalities (9)(10)(11) .
Spray runoff systems are being used successfully under both intermittent
application (9) and continuous application (10). A recent study showed that
spray runoff treatment of a cannery wastewater reduced the BOD by 99 per-
cent, total nitrogen by 91 percent, and total phosphorus by 88 percent (12) .
After process selection, a preliminary design and layout sketch of the
anaerobic-aerobic lagoon system was prepared and submitted to the Oklahoma
Water Resources Board for their review prior to detailed design and construc-
tion.
Detailed Design
To determine exact location of the ponds, a detailed topography survey of the
site was made which included depth of soil. The limited soil at the site was
280
-------
mainly composed of decayed paunch contents and hair and was unsuitable
for dike construction. A suitable clay soil that was being stripped to obtain
underlying sand was purchased from a quarry at about a half mile hauling
distance from the site. The conglomerate rock at the site was from three
inches to two feet under the surface. Dike height and the underlying rock
were the controlling factors in location. Fortunately, one of two potential
locations for the deep anaerobic pond was in a draw which would allow
construction of a pond with eight to ten feet water depth without rock
excavation. To maintain a minimum of three feet depth in the stabilization
and transitional ponds for weed control required rock removal. The ponds
were drawn on the topography map at several elevations to calculate minimum
cost of rock cut and dike fill. As a result, the ponds were located as far up
the slope as possible without eliminating a gravity flow system. The maxi-
mum amount of rock cut was 1.5 feet and maximum centerline height of the
dike was 13 feet. A layout of the treatment system drawn to scale is shown
in Figure 1.
The 550 feet of 6-inch sewer line was located to minimize rock excavation and
to go around an existing barn. The pipe was sloped at 0.9 ft/100 ft.
Vitrified clay pipe was used, except under the roadway where steel pipe was
used. A manhole was located where the plant sewers intersected and at each
change in pipe direction to permit cleanout and inspection. An extra manhole
was located on the raw waste line to house sampling and flow recording equip-
ment. In each manhole the outlet invert was set 0.1 feet lower than the inlet
invert. A difference of 0.5 feet was set between the outlet in manhole No. 5
and the water level in the anaerobic pond. This energy drop was to prevent
plugging of the 6-inch pond inlet pipe. The end section of this inlet pipe was set
on a small pad of concrete to prevent scarring of the bottom and slippage of the
pipe down the steep slope of the anaerobic pond dikes. The insert in Figure 1
of the manhole and piping layout gives details of piping arrangements.
The detail of manhole No. 5 is shown in Figure 2. Manholes No .1,2,3 and
6 were similarly constructed. The square shape and other details were
designed to simplify construction. Manhole No. 5 is the structure controlling
bypass of the anaerobic pond. By inserting a wooden gate, flow can be
diverted to manhole No. 6. At manhole No. 6, a similar gate arrangement
allows diversion of flow to either the transitional pond or to the receiving
stream. This bypass arrangement was used after the anaerobic pond was
completed and prior to completion of the other two ponds to obtain treatment
in part of the system prior to completion of the entire system.
The outlet pipe was located two feet below the surface of the anaerobic pond
to prevent the scum blanket from blocking the pipe inlet. The pipe entered
manhole No. 6 one foot below the water level to eliminate scrubbing of gases
which occur at an overflow weir. The water level in the pond was controlled
by the elevation of the outlets in manhole No. 6.
The 6-inch inlet pipe to the transitional pond was extended to discharge to
the deepest portion of the pond. This deep discharge was designed to reduce
odor emission and to aid in forming an anaerobic zone under the aerobic zone.
The transitional and stabilization ponds were connected by a steel pipe. This
281
-------
282
-------
^6"Ctay Pipe
To Pond
V
6"Cloy Pipe
(TO Pond
\ s
) O
s
Floor Poured Seperately To Grade-
FIGURE 2 - INLET a BYPASS MANHOLE
2 Channel Iron Driven
Into Ground Concrete
Poured Around
283
-------
pipe was located at one foot below the water surface, at the furthest poinf
from the transitional pond inlet to prevent plugging by floating material
and to reduce short circuiting.
The final effluent manhole was located at the furthest distance from the inlet of
the pond to prevent short circuiting. Details of the outlet structure are shown
in Figure 3. This concrete structure was designed with a submerged inlet and
a variable weir elevation to reduce discharge of floating materials and permit
controlled discharges. Such control is helpful when the discharge is to an
intermittent stream or when use of the water for irrigation is p] anned. The
length of the structure was designed to allow dry access from the bank and to
provide room for flow measuring and sampling equipment. As depicted in
Figure 3, a large plywood box was constructed and installed over the final
effluent manhole to protect the composite sampler, flow recorder, and the
sample storage refrigerator.
An intake structure, pipeline, and pump were included in the anaerobic pond
design. A bar screen with 1-inch openings was placed over the intake structure
in the bottom of the pond. The intake line was sloped to give a positive
pressure on the pump. This line also serves as a drain for the anaerobic
pond. The pump discharge line went to manhole No. 5 where the recirculated
sludge was mixed with the raw waste. The mixing of sludge and raw waste
and the further mixing of the lagoon content by the increased influent flow
v/ere to increase biological activity and improve removal efficiencies.
The selection of a pump was based on volume of flow desired, type of material
to be pumped, and price. A recirculation ratio between 1: 1 and 2: 1 was
considered adequate. Based on the design of 15,000 gallons in a 12-hour
operating period, a sludge pump capable of delivering 15,000 to 30,000
gallons/day was desired. Five manufacturers of pumps were contacted and
requested to submit recommendations and prices for a sludge pump for pack-
inghouse wastes of a nonclog design that could pass solids up to 3/8 inch
diameter. The small delivery volume of 20 gpm limited the selection of pumps.
Two manufacturers recommended air-operated pumps. The desire to minimize
equipment maintenance and the necessity for an air compressor and tank to
operate these pumps eliminated further consideration. Tv/o manufacturers
recommended nearly identical self-priming centrifugal pumps designed for
solids handling with 1 1/2 inch ports, and one manufacturer recommended a
screw pump. The unit selected was a Model 11 1/2 A-Gormari Rupp pump
with a 1750 RPM 0.5 H.P motor for $350.
The most influential factors in pond design were Ib of oxygen, demand and
minimum water depth. Topography, construction methods, and present
structures controlled other features of design.
The anaerobic pond was designed at. a loading of 15 Ib BOD 5/1000 cu ft with
a 9 ft water depth. The pond was designed as inverted truncated pyramid
with lengths at the bottom, water line, and centerline of dike of 20, 65, and
88 feet, respectively. The side slope was 2.5 to 1. During construction,
water depth was increased to 10 ft without rock excavation, and the as-built
284
-------
2 Angle Iron Bolted
To Walls of Manhole
•
1
*
s '
-»
— *
^
—
_
«•
...
....
4"
B/
'
1
i
x'
a
x- 1/4 Plote Steel -y
Variable Height
V Notch Weir
-Mode of 8 Gage ^
Sheet Metal n f* *"' ~ " '"
Screwed Ta 3/4 ^- — '
Marine Plywood
^-Formed Wit
8'-0"
-6"Dischorge Pipe
._ __ . _
Concrete — -
h 3/4 "Plywood
__ .
4"
-. _ —
F-
II
V~Ext. Plywood Top
Wood Box Constructed of 2'\ 4"Studs -^]|
And 1/4"Ext. Plywood Siding To
Inlarge Work Area In Manhole And
Weir Height Con Be To Protect Equipment
• Varied 2 it. By Changing
Height of Plywood
II
LID
12
1/4 Plate Steel Floor To Support
Sampling Equipment
^-6" Discharge Pipe
'Dike
FIGURES-FINAL EFFLUENT MANHOLE
285
-------
anaerobic pond has a volume of 18,500 cu ft. The tops of all dikes were
sloped to the outside to prevent rainfall runoff from entering the pond. A
six-foot high chain link fence was put around the pond to prevent animals
or individuals from entering this deep pond.
The organic loading of the transitional and stabilization ponds; can be designed
on a combined basis or separately. In either case, the removal efficiency
of the previous unit must be estimated. The anaerobic pond was assumed to
have an 80% removal efficiency and the combined transitional and stabilization
ponds were designed at 50 Ib BOD5/day/acre with 1/3 of the area in the
transitional pond. The combined design loading was selected because of
success with a similar design used in Louisiana (6) . A minimum water depth
of three feet was used to prevent weed growth and accompanying mosquito
problems. The east and west dikes of the transitional and stabilization ponds
followed the land contours. A common dike was used between the anaerobic
pond and aerobic pond to save material. The surface areas at 2, 3, and 4
feet minimum water depths are 0.97, 1.06, and 1.15 acres. This is the range
of depths that can be obtained with the variable height outlet weir. The
transitional pond has 30 percent of these areas. The volume of the transitional
pond and stabilization pond at minimum water depth of three feet are 407,000
and 1,144,000 gallons, respectively.
The spray runoff irrigation plots were designed at 0.1 acres each. The plots
were designed at pilot scale to limit water use and the effect, of this diversion
on the other treatment processes. The plots require a smooth surface having
2 to 6 percent slope. On the available site, fill was needed to obtain a 6 per-
cent slope. The site had 3 to 12 inches of soil over a conglomerate rock and
soil was added to the plot until the minimum soil depth was 1,2 inches; this
raised the height of fill at the toe to about four feet. The soil was the same
clay loam that was used in the pond dikes. A ditch was placed on the upper
ends of the plots to divert rainfall runoff. The total area prepared was 100 ft x
115 ft, which was divided with 8-inch aluminum garden stripping into three
33 ft x 115 ft plots. Additional stripping was buried to a depth of four inches
and placed around each plot to prevent wastewater surface flow from exiting
except at the outlet structure. The aluminum stripping was connected to a
concrete outlet structure and discharge pipe. Water meters were attached
to the pipe for purposes of flow measurements; however, the available ten
feet of head was insufficient to operate the meters. The flow measuring
system was redesigned using a calibrated tipping bucket and counter
arrangement.
The revolving irrigation gun normally used to spray wastes could not be used
on these small plots. Instead, a revolving boom with a nozzle attached to one
end was installed. The radius of the spray pattern was adjxisted to remain
within the 33-foot width. This arrangement allowed an even distribution of
flow across the plot. Nozzles had a 1/8 inch opening and produced a fan-type
spray.
The piping and valve arrangement was designed to allow wastewater to be
taken from any one of the three pond effluents to be put on the plots. The
motor-operated valves and pumps were actuated by automatic timers. The
286
-------
pumps were small impeller pumps designed for constant flow. The flow per
unit of time for each plot was measured by catching the nozzle discharge in
a container. Hydraulic loading was varied by the length of spray application.
Ordinary household electric clocks were attached to the timers to integrate
the amount of time wastewater was applied on each plot. Hand valves and
pressure gauges were also installed to control the rate of flow.
The plots were sprigged with native bermuda grass which was chosen because
of its ability to make a deep mat to provide a surface for bacteria growth.
Since beef cattle and horses were placed in the surrounding pasture, an electric
fence was installed around three plots to protect the grass and the smoothly
sloped surface.
CONSTRUCTION
To determine construction costs, three competitive bids were obtained. Detailed
drawings, specifications, contract documents and bid proposal were prepared
for bidding purposes. Mr. W. E. Reeves, owner of the packinghouse, submitted
the low bid of $21,400 which was less than the engineering estimate.
The use of packinghouse personnel resulted in minor delays in construction
but minimized cash outlays . Construction of facilities shown in Figure 1 was
mainly accomplished by three maintenance personnel at the packinghouse
under the direction of the owner. Two others aided in operating dump trucks,
front-end loader, and bulldozers during the earth moving phases of construction.
Other part-time manpower consisted of a survey party and a supervisory engi-
neer. No other manpower was required except that used by the electric company
to relocate a power pole and to install service to the project.
The major equipment used on construction of the facilities consisted of two
bulldozers (a D8 and a D6), one 16-yard Euclid earthmover, three dump trucks
(1-12 yard and 2-6 yard), one backhoe, one front-end loader, one pickup
truck, two air compressors, and a 1/2 sack concrete mixer. The owner pur-
chased the Euclid earthmover and a D8 bulldozer for the construction. He
leased air compressors and bulldozers when his were inoperable. The other
equipment was already the property of the owner.
The major materials purchased were soil (a silty clay loam) , vitrified clay
sewer pipe, steel pipe for drains, cement, gravel and sand for concrete, form
lumber, dynamite, an underground electrical cable, a sludge recirculation
pump, a Parshall flume, and flow sampling and recording devices.
Construction was begun in December of 1970 and required four months to
complete the pipelines, manholes, and three ponds . The anaerobic pond and
sewer were completed first and waste turned into the pond on February 1, 1971.
The transitional and stabilization ponds were completed next and received
waste on April 15, 1971. The fence around the anaerobic pond, pilot irriga-
tion plots, and auxiliary equipment were then installed. The last construction
item was sprigging of the dikes with bermuda grass which was delayed until
just prior to the 1972 growing season.
287
-------
For small-packers who are considering construction of a treatment system, the
detailed sequence of events was: (1) Move in the equipment, clear the site,
and stockpile the organic topsoil for later use; (2) Excavate site for the
anaerobic pond and installation of pond drain; (3) Construct dike on anaerobic
pond; (4) Construct sewer pipeline and manholes; (5) Construct inlet and
outlet structures to anaerobic pond; (6) Construct intake structures and
housing for pumps; (7) Purchase pumping equipment; (8) Install pumping
equipment and power source; (9) Excavate site for aerobic ponds (removal
of rock by blasting was necessary) and install pond drains; (10) Construct
aerobic pond dikes; (11) Construct inlet and outlet structures in aerobic
ponds; (12) Install flow sampling and measuring devices and power source;
(13) Clean up area and shape dikes and establish grass cover; (14) Install
stock-tight fences and warning signs; and, (15) Shape the access road to the
treatment system.
EVALUATION OF TREATMENT PROCESSES
General Procedure
Sampling is the most crucial part of any evaluation and considerable effort was
made to obtain the best samples possible within the limitation of personnel and
funds. Samples were taken on a weekly basis of the influent and effluent
streams to each treatment process. Automatic composited samples were taken
on all streams except the three effluents from the spray runoff irrigation plots.
Experience with this process on other investigations has shown that grab
samples of the effluent are satisfactory .
The automatic composite sampler used on the raw waste stream was a Model
HG-4 by Sanford Products Corp which contains a dip-type mechanism. The
automatic composite samplers used on the effluent streams from the anaerobic,
transitional and stabilization ponds were Porta-Positer Samplers, Model U,
by Nappe Corporation which contained an impeller pump and a sample
splitting valve.
The samplers were connected to a time clock which activated each sampler
during the normal slaughtering and processing period of the day. The
samplers were set to take a sample three times per hour from 1p.m. to 5 p .m.
on Wednesdays and from 7 a.m. to noon on Thursdays wheji wastewater flow
occurred. Samples were composited in a plastic container located in a refrig-
erator kept at 4° C.
The Biochemical Oxygen Demand (BOD) and Suspended Solids (TSS) analyses
were initiated the same day the sample was collected since these two tests are
sensitive to sample storage. Samples were stored at 4° C, and other analyses
done during the week were Total Organic Carbon (TOC) , Total Phosphate
(T-P), Total Kjeldahl Nitrogen (TKN), Nitrate (NO3-N), Nitrites (NO2-N),
Ammonia (NH3-N), Total Solids (TS), Total Volatile Solids (TVS), and
Chemical Oxygen Demand (COD). Temperatures of the waste streams were
taken when the sample was collected. Occasionally, analyses were run to
determine oil and grease, chloride and total alkalinity. Total Kjeldahl Nitrogen
was analyzed according to Technicon Industrial Methods 30-69A. All other
288
-------
analyses were made in accord with FWPCA Methods for Chemical Analyses
of Water and Wastes, November, 1969. Duplicate samples and unknown
reference samples were run occasionally to determine accuracy and precision
of the analytical results .
Anaerobic Pond
Raw waste was turned into the anaerobic pond in February 1971. Sampling of
the influent and effluent was begun on March 11, 1971. Composite samples
were first taken on the influent on May 6 and on the effluent on June 10, when
the automatic sampler arrived from the manufacturer.
The collected data was placed on computer cards to enable machine tabula-
tion and printout. Programs were prepared to produce machine plotted graphs
showing concentration versus time for both the influent and effluent and percent
removal versus time. Plotting of BOD 5 and TSS removals (Figure 4) showed
stable conditions were obtained by July 15, 1972, 120 days after sampling was
initiated. Thus, some five months or ten displacement periods were necessary
to obtain stable conditions in the anaerobic pond. Concentration of BOD 5
in the raw waste continued to be highly variable throughout the study period
but the anaerobic effluent dropped from levels over 2000 mg/1 to values around
100 mg/1 after July 15, 1971.
The evaluation period for the anaerobic period was nine months beginning
July 15, 1971 and ending on April 20, 1972. During this period, the organic
loading averaged 12 Ib BOD5/1000 ft3 and the detention averaged 11 days.
The significant changes in the anaerobic pond were in concentration of BOD,
COD, TS, TVS, TSS, NH3-N, and TOC with limited change noted in NO2~N,
NOs-N, TKN, T-P, and Temperature. A table of the common statistical values
of the analytical data is in Appendix A. Percent Removal of Oxygen Demand
and Solids are shown in Table 3.
Table 3. Removal Efficiencies in Anaerobic Pond
Oxygen Demand Solids
Item: BOD^ COD TOG fSS TVS TS
% Removal: 92 87 80 84 77 43
The consistence of the effluent (Anaerobic Effluent) concentration and variability
of the influent (Raw Waste) concentration for BOD5, COD, TSS and NHs-N can
be seen in Figure 5. These frequency vs. concentration graphs display the
reliability of the anaerobic pond for treatment of a meat-packing waste.
289
-------
100
80
« 60
ui
oc
bl
U.
£ 401
ui
20|
-20h
-401
OOh
"0 50 IOO 150 200 250 300 350 400 450 500
DAYS INTO STUDY BEGINNING 037 II / 1971
FIGURE 4 - ANAEROBIC POND REMOVALS
290
-------
8
s
g s
« s
O IQ O O O O
in W (NJ o cr> N uj
I/Bui N- CHN
8 £
-"o
O
8I
O
I
O ">
*~ UJ
g
8
?
j> j> A <^ A c!> A' 'o
<0*CVJOCB<0*M,-.
S 5 ^
O
All
1
OD
O
H
<
CC
Ul
o
o
o
CO
>-
o
2
LJ
15
O
3
All
O
Q.
8 1
o
m
o
ui o:
UJ
I
m
o
<
2
<
in
cr
13
CD
008
I /6UJ QOO
291
-------
The most common parameters used in determining municipal sewer rates for
meat-packers are BOD, TSS and Oil and Grease. Figure 5 shows the BOD and
TSS will be below 200 mg/1 except on rare occasion. Oil and grease analyses
made on the effluent show the concentration is well below the 100 mg/1 level
used by municipalities. The high percent removal and consistency of effluent
concentration of anaerobic pond results in an effluent which would meet
common limitations for discharge to a municipal treatment plant.
Two limitations of the process are the reduction of sulfate to hydrogen sulfite
and the reduction of organic nitrogen to ammonia. The sulfaite comes from the
water supply while the organic nitrogen comes from the protein lost in the
meat processing operation.
Discharge of an effluent with high hydrogen sulfide concentrations to a munici-
pal system will result in damage to concrete sewers and structures unless
precautionary devices are installed. Hydrogen sulfide is responsible for the
smell of rotten eggs and even a low concentration has an offensive odor, re-
sulting in nuisance complaints. At several locations with high sulfate concen-
trations in the water supply, the process has been discontinued because of
hydrogen sulfide odors. At the study site, the sulfate concentration in the
water supply was 4 mg/1 and a hydrogen sulfide odor could not be detected.
Other septic odors could only be detected within 50 feet of the anaerobic pond
in the downwind direction.
Ammonia is toxic to fish and several states have restricted its concentration in
receiving waters. The increase in ammonia (NHs-N) is displayed in Figure 5,
which shows that most of the effluent concentrations were between 65 rng/1 and
85 mg/1. The conversion of organic nitrogen to ammonia increases the concen-
tration of ammonia threefold through the anaerobic pond.
Several times during the study, the raw waste and anaerobic pond effluents
were analyzed for oil and grease, chlorides arid bicarbonate alkalinity to
determine magnitude and change in concentrations.
The oil and grease concentrations in the raw waste and effluent averaged
514 mg/1 and 16 mg/1, respectively, which shows limited loss in the packing-
house and high reduction in the anaerobic pond. A grease cover did not
form on the anaerobic pond which indicates the grease was being digested in
the pond. Some consideration was given to pouring grease on the surface of
the lagoon and covering with straw to form a cover to reduce heat loss. This
was not done and temperature reduction through the pond was as high as 60
percent during part of the winter dropping to values around 10° C. Only minor
changes in removal efficiencies were noted during this period. In a colder
climate there are greater advantages for a cover to reduce heat loss and main-
tain biological activities (13) .
Chloride concentration in the raw waste averaged 1500 mg/1. A packinghouse
normally adds 1,000 mg/1 of chloride in use of the water. The chloride levels
were determined in addition to the total solids to evaluate the potential damage
to soil and crops by spray irrigation.
292
-------
The alkalinity was determined as a check on volatile acids in the anaerobic
pond. Alkalinity concentrations in the raw waste and effluent averaged 300
mg/1 and 700 mg/1, respectively. Only bicarbonate alkalinity was present.
McCarthy (14) has shown that the 85 percent of the volatile acid alkalinity is
measured by titration of bicarbonate alkalinity. The volatile acids are capable
of exhibiting alkalinity because at neutral pH values the acids are ionized and
are in the form of acetates, propionates, etc. When titrating with acid,
the hydrogen ions react with the salt ion registering as alkalinity. The magni-
tude of alkalinity in the effluent and the change through the pond show the
volatile acids production was in control and that methane fermentation was not
exhibited.
Sludge Recirculation
The sludge recirculating pump was installed and started into operation in
March 1971; however, clogging was a continual problem. Clogging was
mainly caused by hair jamming in the piping from the 1 1/2 discharge port.
The flow delivered to manhole No. 5 by pump and motor was measured at
40 gpm. Several hours of maintenance were needed weekly and occasionally
daily to unclog the pump .
After the anaerobic pond had stabilized and removal had reached high levels,
the pump was not operated for two months (July and August) . The pump was
then turned on and operated most weeks in September and October. A
concerted effort to maintain sludge recirculation was successful for two
months (November and December) . In January, February, and part of March,
pump operations were unsuccessful four out of ten weeks. Recirculation
efforts were abandoned in March because of maintenance requirements.
Temperature, BOD5, COD, TVS, TSS and NH3 data on the anaerobic effluent
were grouped according to operation or non-operation periods of the recircu-
lating pump. Hypothesis tests for difference of mean concentrations showed
a significant difference at a probability (p) of 0.90 in all parameters except
NH3 between the two periods. The removal efficiencies, during the pump-off
period (July-August) and the pump-on period (November-December) ,
are shown in Table 4 for the significantly different parameters.
Table 4. Removal Efficiencies for Sludge Recirculation
COD TVS TSS
Recirculating Pump Off 85 83 69 83
Recirculating Pump On 95 87 78 89
293
-------
The anaerobic pond produced a poorer effluent without recirculation even
under more favorable summer temperatures than with recirculation during
fall weather conditions. The mixing and recirculation resulted in a greater
removal efficiency and should be considered for medium or large packing-
houses. However, for the small plants the recirculation pump is impractical
because of the amount of required maintenance.
Transitional Pond
The layout of the transitional pond can be seen in Figure 1 and the area,
volume, and inlet and outlet details are described in the design section. The
liquid depth varies from 7 1/2 feet at the inlet to 3 feet at the outlet.
The discharge from the anaerobic pond was turned into the transitional (second)
pond on April 15, 1971. In May, over half the volume and 90 percent of the
surface area of the transitional pond was being used. The pond was filled
by September 1971. Though data collection was begun early, evaluation of
the process is based on data collected from September through April, a 6.5
month period. During this period, the pond maintained a light gray to green
color with dissolved oxygen near saturation on the surface arid at the outlet;
thus, the transition from an anaerobic to aerobic system was accomplished.
The pond overturned once during the period of warming air temperatures and
the color changed to a darker gray on the surface; however, pirior to collection
of the weekly sample, conditions returned to normal. On one occasion the
outlet pipe was plugged by soil which had eroded into the inlet. An extension
of the pipe to move the inlet a foot from the dike prevented reoccurrence.
The organic loading averaged 52 Ib BOD s/acre/day for the five operating days
per week. The displacement period (theoretical detention time) was 32 days.
The significant changes in the transitional pond were in concentrations of
BOD 5, COD and TSS. A table of the common statistical values of the analytical
data is shown in Appendix A. The percent removal of oxygen demand, solids
and nitrogen is shown in Table 5. There was little change noted in the T-P,
NO2-N, NO3-N, and total TS .
Table 5. Removal Efficiencies in Transitional Pond
Oxygen Demand Solids Nitrogen
BOD_5 COD TVS TSS TKN NH.,-N
Removal % 53 32 15 25 16 13
294
-------
Comparison plotting of concentration data and removal efficiencies versus time
provided little information even though several time lags between influent
and effluent were used. The large variability in differential concentrations
and removal efficiencies, based on individual values, was due to the limited
sampling and large detention period. More meaningful displays of influent
and effluent concentration are shown in Figure 6. These curves show the
frequency of concentration and the change in concentration through the
process. The process is most dependable in reducing the oxygen demand
as measured by BOD5 or COD. The TSS and NH3-N curves show definite
removal but of limited magnitude. The magnitude of effluent concentrations
is what can be expected from the many meat-packing lagoon treatment
systems which are similar in design.
Stabilization Pond
The area, volume, layout and details of design of the pond are described in
the design section. The liquid depth ranges from 7 1/2 to 3 feet. With a mini-
mum water depth of three feet, the displacement period (theoretical detention
time) is 90 days. This can be increased or decreased 18 days by changing
the outlet weir level one foot. The stabilization pond began receiving waste
in late May 1971 and first discharged in September 1971. The pond color is
light green due to algae and on several occasions, the wind has formed an
algae mat along the shoreline. The baffle on outlet structure prevented these
mats from being discharged. The pond has been aerobic and contains numerous
frogs and turtles. Water from the pond has been used on three occasions to
irrigate surrounding bermuda pasture. These grasses were later harvested
by putting 17 head of cattle on the pasture.
The evaluation of the process was based on data collected from September
through April, a 6.5 month period. The organic loading averaged 8.5
pounds per acre per day for the five operating days a week. The significant
changes in the stabilization pond were in the concentrations of NHs-N and TKN
which were 73 and 66 percent, respectively. There was no change in BOD5
concentration but COD increased by 20 percent. The concentration of TVS
did not change, but TSS increased 25 percent. Cumulative frequency verus
concentration graphs are displayed in Figure 7 for BOD, COD, NHs-N and
TSS. The decrease in ammonia (Figure 7) is not accounted for by an increase
by a nitrate or nitrite. A summary of standard statistical parameters on the
analytical data collected is presented in Appendix A.
The stabilization pond was of minor benefit in treatment. The production of
algae in the pond apparently increased the COD and the total suspended
solids . Outside of ammonia reduction, the major benefit of the pond was
one of water storage for use during the irrigation season. At maximum
water level, there is 1,670,000 gallons' storage capacity which would allow
no discharge during the non-growing season. By careful management of
the storage volume the annual wastewater flow of 10.5 acre feet could be
pumped to irrigate part of the 20 acres in the surrounding pasture during
the 224-day growing season.
295
-------
|/6ui 003
296
-------
LU
/ 6iu SSI
- C
HN
o
o
(O
o
o
(M
8
-8
All
l/Ouj
297
-------
Spray Runoff Irrigation Plots
Wastewater was applied to the soil plots in mid-September after the bermuda
grass had covered the surface of the plots. Anaerobic pond effluent was used
on the three plots. The pumps and valves were set to provide equal flow per
hour to each plot. The schedule for application was 5 1/2 days, Monday through
Saturday noon. To insure an effluent flow, application was only during the
plant operation period.
Though the pumping and distribution system copies a similar pilot installation
being used for domestic waste, the first two months of operations showed
several deficiencies. The 1/8 inch nozzles would plug with grease and flow
would be stopped until the next daily inspection. The integrating clocks
indicated up to 20 percent variability in the application cycle between weeks.
Finally, the neoprene impellers in the pumps would, after several days of
operation, take a set and deliver less flow. These equipment problems,
common to small-scale test facilities, resulted in undesirable variations in
the waste application. A new application system was designed and equip-
ment ordered; however, it was more beneficial to accept the variability in
the installed system and continue the six months' study, using anaerobic
effluent. Process evaluation was based on a period beginning on October 7,
1971 and ending on April 20, 1972. Application was stopped for a three-week
period in February, because maintaining the small-scale equipment against
freezing conditions was not warranted. The common statistical parameters
on the data collected are in Appendix A. The data showed the three plots
receivsd nearly identical loadings and could be considered replications.
Previous experience with full-scale spray runoff irrigation systems in this
area have shown that the runoff consists of 49 percent of the water applied (15) .
The loss in flow is attributed to infiltration, evaporation, and evapotranspiration.
Twenty measurements of the cumulative weekly flow were collected on the
influent, but due to the time loss in changing the effluent measuring device,
only ten measurements of the cumulative weekly effluent flow were collected.
The mean values in gallons per acre per day are shown in Table 6. Average
runoff from the three plots was 56 percent, which compares favorably with
the previous experience.
Table 6. Application and Runoff—Spray Irrigation Plots
Item North Plot Center Plot South Plot
Input (gal./acre/day) 8832 7579 8169
Runoff (gal./acre/day) 5177 4070 4408
Runoff (%) 59 54 54
298
-------
The hydraulic loading on the three plots averaged 8200 gallons per acre per
day. The significant changes on the plots were in concentrations of BOD5,
COD, TSS, NHs-N, and TKN. The percent removals of.oxygen demand,
nitrogen, and phosphorus concentrations are shown in Table 7. The change
of phosphorus concentration was considerably less than the goal of 80 percent.
A different operational scheme will be incorporated in subsequent investiga-
tion to increase phosphorus removal. Figure 8 shows the frequency of
occurrence versus concentrations and the change in concentrations through
the process for BOD5, COD, TSS, and NH3-N. The three effluent curves are
shown on each figure along with the common influent curve.
Table 7. Concentration Reduction in Spray Irrigation Runoff (%)
Plots
North
Center
South
Oxygen
BOD
74
76
66
Demand
COD
57
54
50
Solids
TSS
65
75
70
Nitrogen Phosphorus
NH,-N
J
72
79
67
TKN
72
77
59
T-P
17
21
14
Removal efficiencies based only on concentrations are misleading in spray
runoff irrigation systems because 44 percent of the wastewater applied was
lost. Removal of the pollutants by spray runoff irrigation process needs to
be expressed in terms of pounds in the point source discharge. The loadings
and discharge of pollutants on the north, center, and south plots were nearly
identical leadings and may be considered replications. The small variation
in discharge values between plots could be expected from the curves shown
in Figure 8. Overall discharge, loading and removal values for the three plots
are present in Table 8. The anaerobic lagoon removed 80 percent of the organic
carbon and the waste applied to the irrigation plot was lower in carbon than
the carbon: nitrogen: phosphorus ratio of 100: 20: 1, considered ideal for bacterial
cell production.
299
-------
aco
300
-------
Table 8. Loading, Discharge and Removals — Spray Irrigation Plots
Items Loading Discharge Removal
(Ib/acre/day) (Ib/acre/day) ~
BODC 4.6 0.8 83
b
COD 16.9 5.1 70
TOG 5.4 0.8 85
NH3-N 4.9 0.8 84
P 1.1 0.4 64
COSTS
The total capital cost for construction of the three lagoons, pipelines and other
appurtenances, including recirculating sludge facilities, was $21,400. Construc-
tion bids were received with prices on 28 specific items from three contractors.
Eliminating the items necessary to recirculate sludge would have reduced the
construction cost to $20,000. Land costs are not included because of the wids
variance between locations. The cost per gallon of capacity is shown in
Table 9.
Amortization of the capital expenditures are at 7 percent for 20 years. The
shorter replacement period for the recirculating pump was accounted for in
the annual repair parts for the pump which amounted to 20 percent of the cost
of installing the recirculating sludge system. Annual operating and mainte-
nance salaries were based on the owner's estimate of 8 to 10 man hours per
week expended during the second year v/hen the investigation was inactive.
These costs included four mowings during the growing season and daily
inspection and occasional repair of the system. The electric power costs were
determined by the meter readings when the pump was in operation and adjusted
to an annual basis. Eleven hundred kilowatt hours per month of power was
used by the pump .
The monitoring costs were based on the suggested limits in the effluent guid-
ance and the monthly analyses requested by the state. The cost of monitoring
a discharge is dependent upon analyses performed, number of samples, and
the means of samples collected. The least expensive valid means of monitoring
a discharge for a small packer, if acceptable to the control agency, would be:
(1) a collection of an automatic composited sample of a day's flow and a grab
sample in a special sterile container; (2) shipment of the two samples in an
iced container for analyses of BOD 5, SS, oil and grease, and fecal coliforms
within 24 hours of collection by a contract laboratory; (3) analyses by the
301
-------
packer of pH and settleable solids on a grab sample; and, (4) measurement
of the sampled discharge by a totalizing flow meter. Such monitoring would
cost about $100 for each set of data.
The total treatment costs per Ib of BOD5 and COD applied are shown in
Table 9.
Table 9 • Treatment Costs for Anaerobic-Aerobic Ponds
Items
Total Capital Costs
Construction Cost
(at 17,800 gpd)
Amortized Capital Cost
(7% - 20 years)
Annual Repair Parts
Annual Operating and
Maintenance Salary
Annual Electric Power Cost
Annual Monitoring Cost
Total Annual Costs
Treatment Costs
(50,440 Ib BOD ./year)
(81,500 Ib COD/year)
With V/ithout
Recirculating Sludge Recirculating Sludge
$21,400 $20,000
$1.20/gpd Capacity $1.12/gpd Capacity
$ 2,020
280
1,200
360
1,200
$ 5,060
$ 1,888
960
1,200
4,048
$0.10/lb BOD Applied $0.08/lb BOD,. Applied
$0.06/lb COD Applied $0.05/lb COD Applied
The estimated monitoring costs were $0.024 per Ib of BOD5 applied or 30 per-
cent of the annual treatment cost without recirculating sludge. However, proposed
EPA guidelines for state programs only require self-monitoring of discharges
that average over 50,000 gallons per day. If these guidelines are adopted,
many small meat-packers will not be faced with monitoring costs and the total
cost for the system without sludge recirculation would be $0.056 per Ib BOD5
applied.
302
-------
DISCUSSIONS
Treatment System Selection
The objectives of this project were to develop and demonstrate treatment sys-
tems to meet the needs of the meat industry, especially the small meat-packer.
In this first phase of the investigation, two objectives were numerically quanti-
fied. These were: (1) demonstrate an anaerobic-aerobic lagoon system
obtaining greater than 95 percent BOD removal producing an effluent of less
than 50 mg/1, and (2) to develop and demonstrate a spray runoff irrigation
system removing 80 percent of the nitrogen and phosphorus in the wastewater.
Other objectives involving an all aerobic system with an aerated lagoon and
spray runoff irrigation are to be studied in the second phase of this project.
The combination of treatment processes evaluated in Phase I gives four treat-
ment systems. The performance of these four systems, in terms of removal
efficiencies and effluent concentrations of oxygen demand, solids, nitrogen
and phosphorus, are presented in Table 10. The removal efficiencies for the
anaerobic pond with spray runoff irrigation are based on pounds which
recognizes the water volume loss due to evaporation and infiltration. The
total land requirements in Table 10 are those needed for the dikes and all
appurtenances to handle the total flow in each system.
303
-------
Table 10. Performance of Treatment Systems
Anaerobic
Pond
Items
BOD,. Removal (%)
BOD? Effl. (mg/1)
CODRemoval
COD Effl. (mg/1)
TSS Removal (%)
TSS Effl. (mg/1)
TVS Removal (%)
TVS Effl. (mg/1)
NH--N Removal (%)
NH^-N Effl. (mg/1)
TKN Removal (%)
TKN Effl. (mg/1)
PO.-P Removal
PO^-P Effl. (mg/1)
Total Land
Requirement (Acre)
92
102
87
273
84
94
77
309
252
74
2
97
-18
13
Anaerobic and
Transitional
Ponds
96
47
92
182
71
81
262
-204
64
18
81
-18
13
Anaerobic and
Transitional
and Stabili-
zation Ponds
96
44
90
217
85
88
81
252
14
18
72
28
8
9
Anaerobic
Pond and
Spray Runoff
Irrigation*
99
28
97
126
97
28
89
254
47
20
84
29
44
11
.5 1.1 2,5 3.3
*Removals based on a 44% water loss due to evaporation and infiltration.
Though the anaerobic pond accounted for most of the removal of oxygen demand,
it did not, by itself, meet the BOD 5 objective of 50 mg/1; ho\vever, in combina-
tion with the transitional pond or with the transitional and stabilization pond
this objective was obtained. The combined anaerobic and transitional ponds
meet this objective with minimum land requirement and capital cost. The stabili-
zation pond did not reduce the oxygen demand and increased the suspended
solids. Its value is limited to removal of nitrogen, especially ammonia nitrogen
and to storage and controlled release of the effluent.
In regard to the second objective of 80 percent removal of phosphorus and
nitrogen, the anaerobic-transitional-stabilization ponds and the anaerobic
pond-spray runoff irrigation systems accomplished 72 and 84 percent nitrogen
removal, respectively. None of the systems accomplished the desired phos-
phorus removal. In the second phase of this project, application of wastewaters
to the irrigation plots will be altered to duplicate schemes resulting in phos-
phorus removal from other food processing wastewaters.
304
-------
After the project had been designed and the treatment systems constructed and
operational, effluent guideline development was initiated by the U.S. Environ-
mental Protection Agency and the Oklahoma Water Resources Board. The
possible federal effluent limitations are discussed under the section "National
Effluent Limitations ." The Oklahoma Water Resources Board established
guidelines for effluent quality for discharge into intermittent streams which
are defined in terms of maximum effluent concentrations in mg/1. The state
limitations (Technical Release 1002) that are relevant to meat-packing waste-
waters are 2.5 mg/1 NH3-N, l.Omg/lP, 40 mg/1 BOD5, 45mg/lTSS, 15 mg/1
oil and grease, and a requirement that the effluent shall not cause the DO to
be depressed below 4 mg/1 in the receiving water.
Because of the limitations of NH3~N and PO^-P, none of the four systems meet
these effluent discharge guidelines. The anaerobic pond with spray runoff
irrigation meets the other limitations. This system with different application
techniques on the spray runoff irrigation may be able to meet the ammonia
and phosphorus limits. In the Phase II studies, the aerated pond as an extended
aeration process has the potential of meeting the ammonia and phosphorus
limits as other extended aeration plants treating meat-packing wastes have
obtained these limits. To obtain these NH3~N or P limits by either spray run-
off irrigation or extended aeration requires considerable monitoring and
operation experience which is not likely to be available to small meat-packers.
The cost of such operation and monitoring would make additional capital
expenditures more economical for the small packer.
At this small packinghouse, the available pasture makes practical land disposal
to eliminate the discharge and the cost for monitoring or operating an extensive
treatment system for NH3~N or P removal. The stabilization pond will allow
storage of the wastewaters during the non-growing season. During the grow-
ing season, the wastewaters could be beneficially used to irrigate the adjacent
pasture. Irrigation could be scheduled to meet plant requirements and prevent
runoff. Besides the available storage, spray irrigation facilities would be
required. These additional irrigation facilities were designed to apply 10.5
acre feet in 200 days on part of the 20-acre pasture. The estimated annual
cost, including depreciation, power, repair and taxes, would be $600. This
cost (half of that required for monitoring) may make land disposal more
economical than discharge to the receiving -water. However, these are the
added on costs to already available storage facilities and land area. At this
small packinghouse, the annual cost for storage facilities and irrigation
facilities would be equivalent to the cost of monitoring a discharge. The
uncertainty and big cost for other packers is the cost of land which can only
be determined on an individual plant basis .
National Effluent Limitations
National effluent limitations are proposed to be based on units of pollutants per
unit of product. In the meat industry, both raw wastewaters and treated dis-
charges are often described in lb/1000 Ib of LWK. During the study period,
the W. E. Reeves Packinghouse's annual live weight kill was 10,700,000 pounds.
305
-------
The average kill for the five killing days per week was 40,989 lb LWK/day
with cattle plus calves averaging 33,133 lb, and hogs, 7,858 lb. This is
equivalent to 36 head of beef and 36 head of hogs per day. On days that
samples were collected, the average LWK was 40,850 pounds.
Four previous surveys of the meat industry have defined raw wastewater
characteristics in terms of Live Weight Killed (16) . In small plants and new
plants such information is a common basis for design. A comparison of
characteristics of raw wastewaters (Table 11) from the W. E. Reeves Packing-
house and recent survey data (1) from 11 slaughterhouses and 52 packinghouses
shows the Reeves plant to agree more closely with a typical slaughterhouse
than a packinghouse. The slaughterhouses and packinghouses in the survey
were medium and large size plants and all practiced inedible rendering. The
Reeves plant does produce lard, hams, bacon, sausage, weiners, lunchmeat,
chili, etc., like most packinghouses. The reduced waste load may be attribut-
able to the fact that there is no inedible rendering, and the blood and paunch
contents are not disposed of in the sewer system.
Table 11. Comparison of Raw V7astewater Load/1000 lb LWK
(Mean Values)
Parameter Reeves Packinghouse Slaughterhouses Packinghouses
Flow (gal) 435. 695. 1046.
BOD, (lb) 4.49 5.8 12.1
D
TSS (lb) 2.16 4.7 8.7
Grease (lb) 1.85 2.5 6.0
TKN (lb) 0.36 0.27 0.97
Cf (lb) 5.40 12.8 4.70
P (lb) 0.04 0.04 0.17
A comparison of BOD 5 and suspended solids on each process effluent with
effluent limitations under consideration in July 1972 for slaughterhouses
and packinghouses is in Table 12. These interim limits may be the basis for
approval of discharge permits for large and medium meat-packers until
national effluent limitations are established.
306
-------
Table 12. Comparison of Treated "Wastewater and Potential Discharge Limits
BOD5 TSS
Treatment Systems (#/1000#LWK) (#/1000#LWK)
Anaerobic Effluent 0.37 0.33
Transition Effluent 0.17 0.25
Stabilization Effluent 0.16 0.32
Irrigation Runoff* 0.06 0.06
Potential Effluent Limits "A"
Slaughterhouses 0.17 0.23
Packinghouses 0.26 0.35
Potential Effluent Limits "B"
Slaughterhouses 0.30 0.47
Packinghouses 0.61 0.87
*Based on 44% water loss due to evaporation and infiltration.
Potential effluent limits "B" represent the possible minimum acceptable effluent
levels for the meat processing industry. Potential effluent limits "A" may be
applicable for new plants installing pollution abatement equipment and existing
plants now beginning abatement programs. The anaerobic pond in combination
with the transitional or the irrigation plot meets the potential limitations in
Table 12 for a packinghouse discharge. There are also potential limitations
on settleable solids of 0.1 ml/1, on oil and grease 15 mg/1, on pH of between
6.0 and 8.5 and on fecal coliform counts of 1000/100 ml. The limited number
of analyses made on these parameters indicated the discharges can meet the
potential interim guidelines except in the case of fecal coliforms. Some fecal
coliform counts in stabilization pond discharges meet the limit but not all.
Disinfection may be necessary to meet this limitation.
307
-------
Other parameters being considered before approval of a discharge permit are:
toxic materials, ammonia, phosphate, dissolved solids, color and turbidity.
Of these, ammonia is the most significant in the meat-paclcing wastewaters.
Ammonia has also been included in the list of toxic materials; and numerical
limitations are expected to be set nationwide. Several states have already
established effluent limits on NH3~N of 2.0 to 2.5 mg/1. The average con-
centration in the effluent from the anaerobic pond, transitional pond,
stabilization pond, and soil plots were 74, 64, 18, 20 mg/1, respectively.
The magnitude s of these values in relation to state limits are such that different
or additional treatment processes will be needed. Similar nationwide ammonia
limits on effluent discharges will result in a major change in meat-packing
waste treatment systems.
Receiving Streams
Wastewater from the W. E. Reeves Packinghouse is discharged into an unnamed
stream six-tenths of a mile above its confluence with Sandy Creek. Below the
point of discharge, this small stream meanders through two pastures and is
used for stock watering. Sandy Creek is an intermittent stream discharging
to the South Canadian River 12 miles below this confluence. Three miles above
the mouth of Sandy Creek two mgd of treated municipal effluent are discharged
via a tributary. Several sand and gravel pits and numerous oil and gas wells
are located in the pasture lands bordering Sandy Creek. The creek is used
for stock watering and municipal and industrial waste discharges.
After a period of three weeks with no precipitation, stream flow measurements
were made on June 21, 1972. Flow in the unnamed creek below the discharge
was 200 gpm and the flow in Sandy Creek below the confluence with the un-
named creek was 2,000 gpm. Later in the summer, on July 31, 1972, the
unnamed creek had a flow of 140 gpm, but there was no flow in Sandy Creek.
The flow in the unnamed creek is continuous because of a cooling water dis-
charged from a local industry.
Four stream surveys were made from the point of the discharge on the unnamed
stream to its confluence with Sandy Creek and from that confluence to one mile
downstream on Sandy Creek. One summer and one winter survey were con-
ducted prior to and following the initiation of the treatment, system. These
surveys were conducted to determine limnological changes in the streams due
to treatment. Observations were made at eight stations on the unnamed creek
and at four stations on Sandy Creek.
On June 10, 1970, the first stream survey was made. The unnamed stream is
characterized by a rock bottom with sand and gravel deposits. Six orders of
macroinvertebrates including damselfly and mayfly nymphs were collected
above the packinghouse waste discharge. Green algae scums were sparsely
attached to the rock and the dissolved oxygen (DO) concentration was at
saturation. Downstream from the discharge the more sensitive nymphal
insects were nonexistent. Sewage bacteria and sludge worms increased with
increasing distance from the discharge. DO concentrations were below satura-
tion with lowest concentration of 4 mg/1 occurring in an eddy pool one-quarter
of a mile below the discharge. Water temperatures varied from 25° to 26° C
and DO from 4 to 8 mg/1.
308
-------
Sandy Creek, above the confluence with the unnamed stream, was typified by
clear water and clean gravel and sand without sludge banks. DO concentra-
tions were at saturation. The shifting sand bottom is not conducive to biotic
colonization, so these forms were not available for observation; but minnows
and other fishes were observed.
Below the confluence with the unnamed stream, water in Sandy Creek was
slightly milky and the gravel was blackened with organic sludge deposits.
Between a quarter to a half a mile downstream from the confluence, waters in
Sandy Creek were again clear and the gravel and sand were clean. Water
temperatures in Sandy Creek varied from 27° to 30° C. DO concentrations
varied from 6.8 to 12.3 mg/1, dropping from 8.0 mg/1 100 feet above the
confluence to 6.8 mg/1 100 feet below the confluence. Minnows were
observed all along Sandy Creek.
A second survey was made on January 12, 1971, the increased winter flows had
altered the depositional characteristics of Sandy Creek but not those of the
unnamed stream. At least 12 varieties of macroinvertebrates inhabited the
small stream above the packinghouse discharge. These included dragonfly,
midge, and blackfly larvae and the large population of first or second instar
mayfly nymphs. The population below the wastewater discharge consisted
primarily of a few red midge larvae and numbers of sludge worms. These
organisms were found primarily in grain, cereal and animal scrap deposits on
the lee side or bottom of the stream. Slimes of sewage bacteria were dense
50 to 100 feet below the discharge. Cladophora, which was sparse above the
discharge, was dense 100 feet to 400 feet below the discharge. The color of
the water and foam, which formed below the riffles, ranged from a bright
claret near the discharge to a straw yellow at the confluence with Sandy
Creek. Odors from the wastes were detectable 800 feet below the discharge.
In the unnamed stream, the water temperature was 6° C and the DO ranged
from 10.2 to 12.5 mg/1. The water temperature in Sandy Creek was 3° C and
the DO ranged from 12 .6 to 13 .0 mg/1.
After the treatment facilities had been constructed, the third survey was made
on July 8, 1971. The amount of silt and algae scum in the unnamed stream
indicated there had not been a recent rainfall sufficient to scour the rocky
bottom. There was little variation in the community structure of the biota in
the stream in the vicinity of the discharge. In one eddy pool, about 50 feet
downstream from the discharge, there was enough remaining organic material
to cause significant variation in the benthic community. Sandy Creek had low
flow and a silt covered bottom indicating a lengthy period of time since the last
scouring flows. Bottom conditions did not show any change below the conflu-
ence of the unnamed stream. In the unnamed stream and in Sandy Creek,
temperatures ranged from 25° to 26° C and dissolved oxygen ranged from 7.5 to
7.8 mg/1. Abundant minnow populations were observed at all stations.
The fourth survey was made on January 24, 1972, following a period v/hen flows
in the unnamed creek had been insufficient to scour the silt and biota from the
substrate. A broad generic range of benthos was observed in the stream, with
309
-------
relatively few individuals representing each genera. In addition to the diverse
macroinvertebrate population, there was a large amount of attached cladophora.
A profuse algae population was present in the treated discharge from the
packinghouse. The algal community was diverse with flagellated green species
being the most abundant. The water temperature was 8.5° C and the DO was
6 mg/1 in the unnamed creek.
The flow in Sandy Creek was above normal. Due to the unstable and shifting
bottom, macroinvertebrate organisms were not present. The water temperature
ranged from 7° to 7.5° C and the DO ranged from 11.5 to 12 .2 mg/1.
Samples were collected for microbiological analyses on January 21, 1971, when
untreated wastev/aters were being discharged; and on June 21, 1972, when
treated effluent was being discharged. The results are shown in Table 13. A
reduction of 1 to 3 orders of magnitude in these organisms wa.s measured. The
largest change was in the number of organisms in the wastewater discharge.
Table 13. Microbiological Survey of Discharge and Receiving Stream
Fecal Coliforms
Per 100 ml
Fecal Streptococci
Per 100 ml
Station
25 ft above discharge
Wastewater discharge
50 ft below discharge
1/2 mile below discharge
Before
4
6
1
6
.0 x
.2 x
.6 x
.0 x
10 3
10 5
10"
10 3
2
1
1
3
After
.0 x
.1 x
.1 x
.0 x
103
10 2
10 3
102
3
9
1
2
Before
.3 x lO4
.5 x 106
.1 x 106
.2 x 10s
After
2.
1.
4.
2.
5 x
9 x
2 x
0 x
10 3
10 3
10 3
10 3
As a result of the installation and operation of the treatment facilities at the
W. E. Reeves Packinghouse, pollution was abated in a 0.6 mile reach of the
unnamed stream and a 0.5 mile reach of Sandy Creek. Physical evidence of
this was the elimination of excessive oxygen demand, disagreeable odors, and
unsightly sludge banks, water color, and foam. Biological evidence included
increased biotic diversity and the reduction in fecal coliforms and fecal
streptococci.
310
-------
ACKNOWLEDGMENT
This research project was the cooperative study by East Central State College,
W. E. Reeves Packinghouse, and the Robert S. Kerr Environmental Research
Laboratory. The project was supported in part by the Environmental Protection
Agency under Project No. 12060 GPP.
Mr. Phil Wright and Mrs. Susan Stinnett, instructors in the Environmental
Science Department, East Central State College, were responsible for the
analytical chemistry undertaken by themselves and work-study students.
Mr. W. E. Reeves, owner of the packinghouse, along with plant maintenance
and operating employees constructed the treatment system and performed the
maintenance and operation.
Mr. R. Douglas Kreis, aquatic biologist, surveyed the receiving streams and
reviewed that section of the report. Mr. S. C. Yin, microbiologist, made the
coliform counts. Mr. Jim Kingery, mathematical statistician, developed the
printout and plotting programs. Mr. Michael Cook, chemistry technician,
did the special chemical analyses. Mr. Tom Redman, Mr. Montie Fraser, and
Mr. Lowell Penrod, engineering technicians, did the surveying, drafting,
inspection of the construction and maintenance of the monitoring equipment.
Mrs. Josephine Leonard typed and assembled the manuscript. These individ-
uals are on the Robert S. Kerr Environmental Research Laboratory staff.
This report has been reviewed by the Office of Research and Monitoring,
Environmental Protection Agency, and approved for publication. Approval
does not signify that the contents necessarily reflect the views and policies
of the Environmental Protection Agency, nor does mention of trade names or
commercial products constitute endorsement or recommendation for use.
311
-------
LITERATURE CITED
1. PILNEY, J. P., ERICKSON, E. E., and HALVORSON, H. O., "Results of
Industrial Waste Study," The National Provisioner, Vol. 166, No. 8,
pp. 27-52.
2. Anonymous, "An Industrial Waste Guide to the Meat Industry," U.S.
Public Health Service Publication No. 386, 1965 .
3. SCHROEFFER, G. J., and ZIEMKE, N. R., "Development of the Anaerobic
Control Process," Sew. andlnd. Wastes, 31, No. 2.
4. SOLLO, F. W., "Pond Treatment of Meat Packing Plant Wastes," 15th
Industrial Waste Conference, Purdue University, 1961.
5. ROLLAG, DWAYNE A., and DORNBUSH, JAMES N., "Anaerobic Stabiliza-
tion Ponds Treatment of Meat Packing Waste," 21st Industrial Waste
Conference, Purdue University, 1966.
6. COEVER, F. , "Anaerobic and Aerobic Pond for Packinghouse Waste
Treatment in Louisiana," 19th Industrial Waste Conference, Purdue
University, 1964.
7. HESTER, B. L. , and McCLURGE, P. T., "Operation of a Packing Plant
Waste Treatment Plant, Cherokee, Iowa," 25th Industrial Waste Confer-
ence . Purdue University, 1970.
8. STEFFEN, A. J., "Waste Disposal in the Meat Industry, A Comprehensive
Review," Meat Industry Research Conference, Univ. of Chicago, 1969.
9. BLOODGOOD, D. E., VOGEL, J. K., and LUGAR, J. J., "Spray Irriga-
tion of Paper Mill Wastes," Proceedings, 15th Oklahoma Industrial
Wastes Conference, Oklahoma State University, Stillwater, Oklahoma,
November 17-18, 1964.
10. PARMELEE, D. M., and GILDE, L. C., "Natural Land Filtration Treat-
ment System," Campbell Soup Co., Paris, Texas. Presented at Texas
A&M Univ., Water for Texas Conference, 1966 (Mimeographed) .
11. KARDOS, L. T. , "Waste Water Renovation by the Land—A Living Filter,"
American Association for the Advancement of Science, Publication No. 85,
pp. 241-250, 1967.
12. LAW, J. P. , THOMAS, R. E., and MYERS, L. H., "Nutrient Removal
from Cannery Wastes by Spray Irrigation of Grassland," Water Pollution
Control Research Series 16080, U.S. Dept. of Interior, FV7PCA,
November 1969.
13. McCARTY, P. L., "Kinetics of Waste Assimilation in Anaerobic Treat-
ment." In Developments in Industrial Microbiology, American Inst; of
Biological Sciences, Washington, D.C., Vol. 7, p. 144 (1966) .
312
-------
14. McCARTY, P. L., "Anaerobic Waste Treatment Fundamentals—Part Two
Chemistry and Microbiology," Public Works, 95, 123, October 1964.
15. BENDIXEN, T. W., HILL, R. D., DuBYNE, F. T., and ROBECK, G. G.,
"Cannery Waste Treatment by Spray Irrigation-Runoff," JWPCF, Vol. 41,
No. 3, Part 1, pp. 385-391 (1969).
16. WITHEROW, J. L., YIN, S. C., and FARMER, D. M., "National Meat-
Packing Waste Management Research and Development Program,"
Environmental Protection Technology Series EPA-R2-73-178, December
1972.
313
-------
Appendix A
COMMON STATISTICS ON DATA BASE
RAW WASTEWATER - 71/06/17 to 72/04/20
Parameter
Tenp
BOD 5
COD
TS
TVS
TSS
NHs-N
N02-N
N03-N
TKK
P
TOG
Hogs
Beef
TOTAL
Cent
mg/1
Hlg/1
mg/1
mg/1
mg/1
mg/1
Eg /I
mg/1
mg/1
mg/1
mg/1
#LHK/day
#LWK/day
#LWK/day
No.
38
40
35
37
37
36
33
16
15
35
32
22
37
37
37
Mean
Median
23.1315
24.0000
1247.8000
988.5000
2159.9600
1691.0000
3404.7567
3397.0000
1350.0000
1112.0000
600.8611
494.0000
20.9939
14.0000
0.3150
0.1650
3.1986
0.5000
99.3428
92.5000
11.3665
10.7600
500.3636
480.0000
8000.
32850.
40850.
Stan Dev
Range
3.3705
13.0000
802.4431
3072.0000
1497.8731
6679.3000
1184.5759
5114.0000
888.5936
3741.0000
590.1532
2968.0000
19.6946
67.0000
0.3090
1.0500
9.3872
36.9400
52.3144
233.0000
5.7244
26.6000
281.1258
1048.0000
163.
4300
778.
17750.
772.
21050.
tfaxiiruir.
Beg Date
27.0000
71/06/17
3337.0000
71/06/17
7170.0000
71/06/17
6371.0000
71/06/17
4161.0000
71/06/17
3012.0000
71/06/17
68.0000
71/06/17
1.1000
71/09/16
37.0000
71/09/16
260.0000
71/06/17
28.8000
71/06/17
1160.0000
71/06/17
9350.
71/06/17
39950.
71/06/17
50650.
71/06/17
Minimum
End Date
14.0000
72/04/20
265.0000
72/04/20
490.7000
72/04/20
1257.0000
72/04/13
420.0000
72/04/13
44.0000
72/04/13
1.0000
72/04/20
0.0500
72/04/13
0.0600
72/04/13
27.0000
72/04/20
2.2000
72/04/20
112.0000
72/04/13
4050.
72/04/20
22200.
72/04/20
29600.
72/04/20
314
-------
ANAEROBIC EFFLUENT - 71/07/15 to 72/04/20
Parameter
Temp Cent
BOD5 mg/1
COD rag/1
TS mg/1
TVS mg/1
TSS mg/1
NH3-N mg/1
N02-N mg/1
N03-N mg/1
TKN mg/1
P mg/1
TOC nig/I
TRANSITIONAL EFFLUENT -
Temp Cent
BOD5 mg/1
COD mg/1
TS
TVS
TSS
mg/1
mg/1
mg/1
NH3-N mg/1
N02-N mg/1
N03-N mg/1
TKN mg/1
P mg/1
TOC mg/1
No.
38
39
34
36
36
36
32
17
16
35
33
21
,
IT -
30
32
26
29
29
29
24
16
17
28
26
19
Mean
Median
16.8421
16.5000
102.1576
76.1000
273.6764
281.7500
1949.5555
1869.5000
309.0833
300.0000
93.9722
86.0000
73.9187
75.0000
0.6200
0.2500
0.6093
0.1350
96.7514
96.0000
13.3836
13.9200
120.0714
80.0000
71/09/02 to
11.4666
11.5000
47.5131
33.0000
182.4538
185.1500
1921.1034
1795.0000
262.5172
266.0000
70.5517
56.0000
64.0541
65.0000
0.2731
0.1000
0.2447
0.1000
81.3035
82.2500
13.3350
13.9000
78.3947
72.5000
Stan Dev
Range
6.5120
22.0000
64.6678
341.0000
88.8779
407.2000
290.0615
954.0000
110.6013
426.0000
43.3342
206.0000
21.7526
112.0000
0.8315
2.3000
1.0531
3.3000
13.2890
55.0000
4.2269
19.0000
78.3945
381.0000
72/04/20
6.5323
23.0000
42.6526
237.0000
50.7603
182.9000
247.5356
780.0000
94.1763
432.0000
51.4389
192,0000
16.5635
70.0000
0.3935
1.6000
0.3998
1.7100
12.2143
57.0000
3.5752
16.8000
42.8798
205.0000
Ffiyteum
Bef, Date
26.0000
71/07/15
370.0000
71/07/15
484.3000
71/07/15
2482.0000
71/07/15
543.0000
71/07/15
226.0000
71/07/15
121.2000
71/07/15
2.3000
71/09/16
3.3000
71/09/16
125.0000
71/07/15
21.6000
71/07/15
405.0000
71/07/29
23.0000
71/09/02
247.0000
71/09/02
265.5000
71/09/16
2392.0000
71/09/02
527.0000
71/09/02
200.0000
71/09/02
92.5000
71/09/02
1.6000
71/09/16
1.7100
71/09/16
103.0000
71/09/02
20.0000
71/09/02
235.0000
71/09/16
Kiniiruir.
End Date
4.0000
72/04/20
29.0000
72/04/20
77.1000
72/04/20
1528.0000
72/04/13
117.0000
72/04/13
20.0000
72/04/13
9.2000
72/04/20
0.0000
72/04/13
0.0000
72/04/13
70.0000
72/04/20
2.6000
72/04/20
25.0000
72/04/13
0.0000
72/04/20
10.0000
72/04/20
82.6000
72/04/20
1612.0000
72/04/13
95.0000
72/04/13
8.0000
72/04/13
22.5000
72/04/20
0.0000
72/04/13
0.0000
72/04/13
46.0000
72/04/20
3.2000
72/04/20
30.0000
72/04/13
315
-------
STABILIZATION EFFLUENT - 71/09/02 to 72/04/20
Parameter
Temp
BOD 5
COD
TS
TVS
TSS
NH3-N
N02-N
N03-N
TKN
P
TOG
NORTH
Temp
BOB 5
COD
TS
TVS
TSS
NH3-N
N02-N
N03-N
TKN
P
TOC
Cent
mg/1
Hg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
IRRIGATION
Cent
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
ng/1
mg/1
mg/1
ag/1
No.
33
33
26
31
31
30
27
14
16
28
26
-19
RUNOFF
16
28
24
26
26
2V
19
15
12
22
21
16
Mean
Median
10.7878
12.0000
44.5687
38.0000
217.6730
214.4500
1998.8064
1917.0000
252.7419
240.0000
88.1000
96.0000
17.6740
18.5000
1.7764
0.5600
4.6650
4.3000
27.7857
22.5000
9.1350
9.0400
70.4736
70.0000
- 71/10/07 to
10.3750
10.5000
26.8460
22.5000
117.3499
119.5000
1886.2692
1871.5000
245.3076
268.0000
32.8076
28.0000
20.4105
18.0000
2.8999
1.3000
9.9325
10.7000
26.1590
24.5000
11.0514
11.5600
55.4687
52.5000
Stan Dev
Range
6.2S36
21.0000
30.7925
132.7000
63.0127
327.6000
249.3075
1139.0000
91.1332
301.0000
27.3475
107 . 0000
10.6033
35.0000
3.0625
10.0000
3.5168
10.9000
13,6796
43.0000
2.7552
14.2200
24.1600
76.0000
72/04/20
2.9183
9.0000
17,3059
88.0000
38.5902
141,4000
306.0431
1273.0000
93.9168
319.0000
25,1300
100.0000
7.2446
24.5000
2.9814
8.1500
6.8374
23.3800
8,0332
31.0000
3.5141
15.8000
33.6894
115.0000
Maximum
Beg Date
21. ,0000
71/09/02
144,0000
71/09/02
401. ,9000
71/09/16
. 2450.0000
71/09/02
402.0000
71/09/02
135.0000
71/09/02
38.5000
71/09/02
10.0000
71/10/14
11.0000
71/09/16
51.0000
71/09/02
15.2000
71/09/02
115.0000
71/09/16
15.0000
72/02/17
99.0000
71/10/14
195.0000
71/10/21
2338.0000
71/10/07
400.0000
71/10/07
104.0000
71/10/07
36.5000
71/10/14
8.2000
71/10/14
24.0000
71/10/14
42.0000
71/10/07
16.8000
71/10/07
125.0000
71/10/07
Mininiun
End Date
0.0000
72/04/20
11.3000
72/04/20
74.3000
72/04/20
1311.0000
72/04/13
101.0000
72/04/13
28.0000
72/04/13
3.5000
72/04/20
0.0000
72/04/13
0.1000
72/04/13
8.0000
72/04/20
0.9800
72/04/20
39.0000
72/04/13
6.0000
72/04/20
11.0000
72/04/20
53.6000
72/04/20
1065.0000
72/04/20
81.0000
72/04/20
-4.0000
72/04/20
12.0000
72/04/20
0.0500
72/04/13
0.6200
72/04/13
11.0000
72/04/20
1.0000
72/04/20
10.0000
72/04/13
316
-------
CENTER IRRIGATION RUNOFF - 71/10/07 to 72/04/20
Parameter
Temp
BOD 5
COD
TS
TVS
TSS
NH3-N
N02-N
.:o3-N
TKN
P
TOC
SOUTH
Temp
BOD 5
COD
TS
TVS
TSS
NH3-N
N02-N
N03-N
TKN
P
TOC
Cent
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
IRRIGATION
Cent
mg/1
ffig/1
mg/1
nig/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
No.
7
21
17
18
18
18
14
11
7
18
16
/ll
RUNOFF.
7
19
19
18
18
18
16
14
11
19
17
14
Mean
Median
9.7142
10.0000
24.4904
21.0000
126.2411
117.2000
1914.1666
1880.0000
269.5555
277.0000
23.2777
22.0000
15.1785
16.2500
3.0136
2.6000
15.1928
12.9000
21.6111
22.0000
10.4850
10.7200
58.1818
65.0000
- 71/10/07 to
11.2857
12.0000
34.4247
26.2500
135.8894
141.4000
1966.6111
1967.5000
247.6111
269.0000
•28.0111
22.0000
24.6062
21.5000
2.6178
1.8000
12.5218
10.6000
39.2368
37.5000
11.4700
12.0000
56.8214
57.5000
Stan Dev
Range
2.5634
7.0000
16.0034
69.0000
49.2342
158.8000
370.6000
1554.0000
100.7701
409.0000
14.2738
36.0000
7.0126
22.5000
2.3039
5.7000
8.3876
24.6500
8.6476
31.5000
4.0444
17.7000
34.0787
100.0000
72/04/20
2.7516
8.0000
24.5849
108.0000
50.1131
174.8000
318.3406
1152.0000
89.2103
302.0000
21.9314
71.2000
14.1788
48.5000
2.2287
5.5500
6.5774
22.5000
20.9970
94.2000
3.9475
16.4800
36.8571
130.0000
Maximum
Beg Date
13.0000
72/02/17
72.0000
71/10/07
212.4000
71/10/21
2638.0000
71/10/07
427.0000
71/10/07
40.0000
71/10/07
25.5000
71/10/14
6.0000
71/10/14
28.6500
71/10/14
37.5000
71/10/07
18.9000
71/10/07
110.0000
71/10/07
15.0000
72/02/17
119.0000
71/10/14
230.1000
71/10/07
2487.0000
71/10/07
365.0000
71/10/07
75.2000
71/10/07
51.0000
71/10/07
5.6000
71/10/14
24.9000
71/10/14
97.0000
71/10/07
19.6800
71/10/07
140.0000
71/10/07
Minimum
End Date
6.0000
72/04/20
3.0000
72/04/20
53.6000
72/04/20
1084.0000
72/03/30
18.0000
72/03/30
4.0000
72/03/30
3.0000
72/04/20
0.3000
72/01/20
4.0000
72/01/20
6.0000
72/04/20
1.2000
72/04/20
10.0000
72/02/17
7.0000
72/04/20
11.0000
72/04/20
55.3000
72/04/20
1335.0000
72/04/13
63.0000
72/04/13
4.0000
72/04/13
2.5000
72/04/20
0.0500
72/04/13
2.4000
72/04/13
2.8000
72/04/20
3.2000
72/04/20
10.0000
72/04/13
317
-------
LAND DISPOSAL OF POTATO STARCH
PROCESSING WASTE WATER IN THE NETHERLANDS***
by
Dr. F.A.M. de Haan* and P. J. Zwerman**
INTRODUCTION
In this paper the results of a study about the possibilities for land dis-
posal of starch processing water are discussed. Land disposal of process
water, combined with agricultural use of the nutrient elements of this
waste water, has to be subjected to a number of stipulations of which the
most important one is: the amount of water that can be purified by the
soil. Important is the utilization of the nutrient elements in the
growing plant as is the effect of land disposal on farm economics. The
technical elaboration of water distribution together with all the above
aspects were studied by a special working group. The results of these
studies have been described in a report (1). Here the presentation of
data is confined to the first topic, viz. the purification by the soil.
Results of related studies on other topics will be briefly described in
the discussion.
The northeastern portion of The Netherlands is included in. the so called
Veen Colonies, with a total area of approximately 70,000 hetctars. The
soil is made up of sandy subsoil and of the previous organic soil, covered
with low grade organic matter not suitable for the preparation of fuel (2).
With the latest methods of land preparation being utilized approximately
35,000 hectars are annually utilized for the production of starch potatoes,
The starch from these potatoes is produced in some 13 factories, spread
over the area. This results in a tremendous quantity of waste water that
is released on open cannels and water ways, and in this mariner is led off
to the Eems Dollard estuary and Lake IJssel. This method of disposal of
waste from the starch industry was utilized since the second half of the
previous century. The pollution of surface waters and the excessive
stink, as a consequence of the rotting of proteins in the waste water,
will no longer be tolerated.
*Senior Scientific Officer of the Laboratory of Soils and Fertilizers
of the State Agricultural University and also Guest Scientist and Co-
worker at the Institute for Land and Water Management Research.
**Professor of Soil Conservation, Cornell University and Fullbright
Grantee of The Netherlands in Environmental Science 1972-1973;
cooperatively appointed with the State Agricultural University at
Wageningen, The Netherlands.
***Agronomy Paper No. 1008.
318
-------
The potato starch industry is a typical seasonal processing industry.
All potatoes are processed during the period from the middle of August to
the middle of December. After arrival at the factory the potatoes are
washed and transported by means of water to the actual site of extraction
of starch. This results in the first kind of waste water, viz. the wash
and transport water. It contributes scarcely 5% to the total waste
burden. Especially, at the refinery procedure of the starch, large
quantities of water are used. The present average production of proc-
essing water amounts to approximately 8 m3 per ton of potatoes. However,
the tendency exists to arrive at a limitation of water utilization by
application of washing against the stream.
The total capacity of the 13 factories is 1,160 tons of potatoes per hour
and the average duration of working hours for a campaign is 2,200 hours;
thus about 20 1/2 million cubic meters of process water is produced
annually. This coincides on the base of biochemical oxygen demand with
a waste burden of almost 21 million human equivalents.
REVIEW OF LITERATURE
Recently various studies have been performed to evaluate the best solution
for this waste water problem. Thus a proposal was made to lead all the
waste water to the Eems Bollard estuary by means of an underground pipe-
line (3). This has led to numerous discussions; biologists fear for an
excess of the self purification capacity of the water in this estuary (4).
A technological solution of the problem by making byproducts from the
water in the form of proteins, although possible from a technical point
of view (5), is excessively high in costs.
MATERIALS AND METHODS
The effect of land disposal on purification of the process water was
studied by a comparison of the composition of the waste water and of the
leachate from soils which had been flooded or sprinkler irrigated with a
known amount of process water. To this purpose samples of the upper
layer of the groundwater were collected by means of piezometers, with a
filter at the bottom. In all samples chemical and biochemical oxygen
demand was measured, as well as the concentration of a number of compo-
nents, viz. N-total, NH, in inorganic form, NH, in organic form, NOo,
NO^, total phosphate as PO^, and K. Analyses have been performed
according to the standard procedures applied for the examination of water
and waste water (6, 7).
The soils used in the experiments were of average composition for that
part of the country. A distinction was made between sandy soils, con-
sisting of medium fine sand with a top layer of about 30 cm with an
organic matter content of 5%, and soils with a relatively large amount of
peat in the profile. All experiments were performed in the field, both
on "new" soils as well as on flood fields which were used for about 40
years for land disposal of process water.
Since the limit of the purification capacity of the soil had to be deter-
mined in a short time period, this study should be looked upon more or less
as a pilot study. The mechanism of purification as well as the water
319
-------
transport in the soil is now being investigated in the laboratory by means
of column studies and analogous water transport models.
An indication of the influence of land disposal on the soil composition
was obtained at a separate site, viz. a flood field of town sewage of
which soil samples were collected during a time period of 10 years (8).
Phosphate contents of these samples were measured according to the
ammonium lactate extraction procedure, whereas potassium contents are ex-
pressed as tag K20 per 100 gram of dry soil.
EXPERIMENTAL RESULTS AND DISCUSSION OF THESE RESULTS
The average composition of Dutch potato starch process water, at a waste
water production rate of 8 m3 per ton of potatoes, is presented in Table
1. These are the mean values of a large number of sampling dates.
Process water production rates, and consequently the composition of the
waste water, may slightly differ from one factory to another, depending
on the refinery procedure applied.
Table 1. Average Composition of Potato Starch Process Water, in mg/1.
COD BOD5 N-tot. NH4 inorg. NH4 org.
N00 NO. PO, K
8,400 3,900 420 110 310 - 5 190 580
The very high oxygen demand values must be attributed to the presence of
organic matter in the waste water. This organic material mainly consists
of proteins. Nitrogen almost completely occurs as ammonium, with 3/4 in
the organic form. In fresh process water nitrite was found not to be
present at detectable concentration, whereas the nitrate content is very
low. The phosphates consist for the major part of orthophosphates. Also
small quantities of easily hydrolyzable polyphosphates were found. The
high potassium content of the process water limits agricultural use. The
water has to be disposed of in a potato growing area. High potassium
availability in soil decreases starch content of potatoes.
Flooding of the land offers a means of disposal of large quantities of
waste water. In the experiments amounts as high as 500 mm were added to
both sandy and peaty soils. The effect on the composition of the upper
groundwater layer is given in Table 2. For comparison data for untreated
soil are also represented.
320
-------
Table 2. Composition, in mg/1, of the Upper 50 cm Layer of Groundwater
on Sandy and Peaty Soils After Addition of 500 mm Processing
Water, in Comparison to Untreated Soil.
Soil
Sand
Peat
Untreated
COD
320
680
56
BOD
34
6
2
N-tot.
18
36
2.3
NH4
inorg.
13
25
1.0
NH4
org.
5
11
1.3
NO
1.
1.
0.
2
6
0
2
N03
61
25
17
P04
1.1
47
0.3
K
197
251
15
It is shown that disposal of process water at this level results in an in-
crease of all components in the groundwater as compared to the untreated
soil. However, the degree of purification, expressed as a percentage
removal from the waste water (cf. Table 1) is extremely high. Only
potassium is removed to a minor degree which is in accordance with the
limited adsorption capacity of the soils under consideration.
A remarkable difference exists between the sandy soil and the peaty soil.
Due to precipitation as Fe- and Al-phosphates, phosphate removal is almost
complete in sand, whereas on the peaty soil about 75% removal only is
obtained. This percent may still be reasonably high in comparison to
normal biological waste water treatment. The remaining phosphate concen-
tration, however, is considered as much too high with respect to eutro-
phication (9) . Whether or not eutrophi-cation will be induced by these
phosphates depends on the reactions which may occur before the groundwater
reaches the open water. Also nitrate may contribute to eutrophication,
especially on the sandy soil, whereas a consequence of better aeration
conditions for biological decomposition of the organic matter, nitrate
concentrations of the groundwater are high as compared to the peaty soil.
These nitrates may easily be transported to the open water, unless
denitrification takes place.
The influence on the composition of deep groundwater was also studied.
For this purpose samples were taken at a depth of 60 meters under the
flood fields which have been used for 40 years for land disposal of proc-
essing water. The results are presented in Table 3. The soil at these
plots is sandy over the entire depth of 60 meters.
321
-------
Table 3. Composition of Groundwater, in mg/1, at a Depth of 60 meters
Beneath Flood Fields, Which Have Been Flooded During 40 Years
With a Yearly Amount of 500 mm Potato Starch Waste Water.
COD
60
N-tot
1.0
NH, inorg.
0.9
NH4 org.
0.1
P°4
0.8
At this depth there seems to be no influence of land, disposal on the
ground water composition.
In the first days after addition of these large amounts a temporary in-
crease of oxygen demand in the upper groundwater was found. Sometimes
this was up to a BOD^ of 1,000 mg/1. In a separate experiment the effect
of partial additions was studied. For this purpose an amount of 420 mm
was applied at once, and also in 3 portions of 140 mm with time intervals
of 3 weeks. Only part of the 140 mm could be stored in the profile. It
was found here that 140 mm were completely purified; between the second
and third applications a sharp increase of oxygen demand was measured.
Application by means of sprinkling irrigation is advantageous in that the
addition can be controlled much more accurately than with flooding. This
is of special importance as the process water production will decrease in
the future. A proportional increase of the waste water concentration will
then result, which requires an accurate distribution system with respect
to plant nutrition.
An amount of 40 mm was applied by sprinkling on a sandy soil (10). This
quantity was sufficiently small not to exceed the unsaturated soil water
storage capacity. The course of COD, BODi- and N-total as a function of
time is presented in Figure 1. Application was performed at the end of
September. At the end of December and in March heavy rainfall occurred,
which at that time still caused a small leaching of organic matter. After
leaching the composition of the groundwater gradually improves again.
Unfortunately data of soil analyses from plots of soils flooded for many
years with processing water are not available.
Provided that adequate applications are choosen, land disposal of proc-
essing water will meet purification requirements for such a time period.
Yearly additions of 400-500 mm result in a temporary high oxygen demand
of groundwater. It is suggested that application must not exceed 100-
500 mm per year. This amount must preferably be disposed of in portions
of 40-50 mm. So one maintains optimal aeration conditions for biological
decomposition of the organic material.
322
-------
GENERAL DISCUSSION
As a consequence of the tremendous amount of process water land disposal
must, from an economic point of view, be combined with agricultural use
of the nutrient elements in crop growing. In addition to the resulting
economic advantage, this induces a recycling which should be preferred
from an environmental point of view. Moreover this recycling enlarges
the purification capacity of the soil. To suit the application to the
plant nutrient requirements, the working coefficient of the different
nutrient elements of process water for different crops was determined
in separate experiments (11). With the use of these values, and the
relation between fertilization and crop yields the savings of expenses
for fertilizers were calculated for all rates of application. On the
other hand, yield depressions as a consequence of non-optimal meeting of
nutrient requirements and application rates must also be taken into
account. Moreover the farmers experience disadvantages as the water is
disposed of in fall when there is no need for extra water and the dis-
posal may force delay of farm operations. All these and related factors
were taken into account in a computerized model study (12). This study
showed results in a farm economic advantage of about 100 Dutch guilders
per hectar per year at an application rate of 100 mm. This application
is the average value for the entire farm. An optimalization was performed
with respect to different crops of the most common crop rotation schedules
for this area. So if the crop growing area is covered for 50% by potatoes;
as actually is the case in this area, the other crops as grains and sugar-
beets will receive 150 mm, since potatoes allow an application of 50 mm
only.
In a case study for one of the factories a plan for disposal of all the
process water of this factory in a continuous program during the campaign
was worked out for flooding as well as for sprinkling irrigation.
Flooding turned out to be almost twice as expensive as sprinkling irri-
gation. High costs for flooding are mainly due to the required land
levelling and drainage systems. As was pointed out before purification of
the water is also best served by sprinkling irrigation. Yearly costs for
application by sprinkling at a rate of 100 mm were found to be 380
guilders per hectar. Thus leaving net expenses for land disposal of about
280 guilders per hectar. It may be reasoned that the farmers pay their
economic advantage back to the land disposal system. This is true be-
cause they contribute to the pollution by growing these starch potatoes,
whereas at the same time the farmers are in general the cooperative owners
of the factories.
For a "standard" factory with a capacity of 100 tons of potatoes per hour,
a yearly working period of 2,200 hours and a waste water production of 8
m3 per ton, land disposal will lead to yearly expenses of about half a
million guilders. Such a factory produces a waste burden comparable to
1.8 million human equivalents. Costs for land disposal are thus about
0.3 guilders per human equivalence, as compared to about 10 guilders for
biological treatment of the waste water. This number has a limited value
only since data were derived for one specific factory only. However,
eiTen if the extrapolation to other situations would increase the costs by
a factor of two, land disposal still remains a relatively inexpensive and
good solution of this specific industrial waste water problem.
323
-------
SUMMARY
Possibilities for and implications of land disposal of potato starch proc-
essing water are discussed. In a series of experiments the purification
by soil was studied from the composition of the upper groundwater after
different additions of process water. Removal of oxygen demand from the
waste water as well as of different components was found to be complete
on sandy soils, except for potassium,if application does not exceed 100-
500 mm. At higher doses a temporary high increase of oxygen demand of
groundwater was measured. Peaty soils turned out to be less effective in
purification, especially with respect to oxygen demand and phosphate
removal. Aeration conditions in the soil should be maintained at optimum
for biological decomposition of the organic matter. In this respect the
waste water must preferably be applied by means of sprinkling irrigation,
at doses not exceeding 40-50 mm. In this way land disposal may be an
effective method for process water treatment during a time period of at
least 30-40 years. Due to the small adsorption capacity of the soils
studied and the high potassium content of the waste water, a considerable
part of the potassium applied will be leached. Land disposal in combina-
tion with agricultural use of the plant nutrients leads to a relatively
inexpensive way of potato starch waste water treatment.
References
1. WERKGROEP TNO onderzoek irrigatie afvalwater aardappelmeelindustrie.
Landbouwkundig gebruik van aardappelmeelafvalwater (On the agricul-
tural use of potato starch waste water). I.C.W., P.O. Box 35,
Wageningen (1972).
2. EDELMAN, C. H. Soils of The Netherlands. N. H. Publ. Company,
Amsterdam (1950).
3. EGGINK, H. J. Het estuarium als ontvangend water van grote
hoeveelheden afvalstoffen (The estuary as receiving water of waste
products). Mededel. R.I.Z.A. 2, The Hague (1965).
4. HALLENGA, K. and H. D. COSTER. Groninger persleicling is economisch
niet aantrekkelijk (Pipeline to Estuary is non-economic). Nat. en
Techniek, 33, 1 (1971).
5. PETERS, H. Zuivering van afvalwater; enige mogelijkheden voor de
agrarische Industrie (Purification of waste water; possibilities
for agricultural industry). Nat. en Techniek, 32:488 (1970).
6. STANDARD METHODS for the Examination of Water and Waste; latest ed.;
Am. Public Health Assn. Inc., New York, N.Y.
7. DEUTSCHE EINHEITS VERFAHREN zur Wasser-, Abwasser- und
Schlammuntersuchung, latest ed. Weinheim, Verlag Chemie.
8. HAAN, F.A.M. DE. Resultaten van belasting van de bodem met grote
hoeveelheden afvalstoffen (Results on use of soil for disposal of
waste products). Nota 657, I.C.W., P.O. Box 35, Wageningen (1972).
324
-------
9. MENKENS, Ch. H. Fertilizers and the quality of surface water.
Stikstof 15. Central Nitrogen Sales Organization Ltd. 360
Thorbeckelaan, The Hague (1972).
10. HAAN, F.A.M. DE and J. BEUVING. Zuivering van proceswater uit de
aardappelmeelindustrie door beregening op landbouwground (Purifi-
cation of potato starch waste water after sprinkling irrigation).
Nota 693. I.C.W. P. 0. Box 35, Wageningen (1972).
11. RIEM VIS, F. Maximaal toelaatbare hoevellheden vruchtwater van
aardappelmeelfabrieken op landbouwgronden uit een oogpunt van
mineralenvoorziening (Fertilization of agricultural crops by
nutrients from potato starch process water). Report 71-100.
Institute for Soil Fertility, Haaren (1971).
12. HOOGEVEEN, G. J. Bedrijfseconomische gevolgen van het gebruik van
afvalwater van de aardappelmeelindustrie op het veenkoloniale
landbouwbedrijf (Farm economic consequences of land disposal of
potato starch process water). Cultuurtechnische Dienst, Utrecht
(1972).
325
-------
PRETREATMi'.NT OF COMBINED MUNICIPAL
AND POTATO PROCESSING WASTES
by
Guilford 0. Possum*
This paper presents a progress report on research being conducted on the
aerated and anaerobic pretreatment of combined municipal and potato pro-
cessing wastes at Grand Forks, North Dakota. Data is presented for only
the first year of operation dating from 1 January to 31 December, 1972.
It discusses some of the physical and chemical parameters, but excludes
the data gathered on bacteria, algae and other organisms which will be
available from others at a later time.
ACKNOWLEDGMENT
This study was supported in part by funds received under Grant No. 11060-
DJB from the Federal Water Pollution Control Administration of the U.S.
Department of the Interior to the City of Grand Forks, and in part from
funds supplied by the City of Grand Forks, North Dakota.
INTRODUCTION
The City of Grand Forks. North Dakota, is located in the Red River Valley
at the junction of the Red River of the North and the Red Lake River.
It is situated in the heart of a rich agricultural area whose principal
products are small grains, potatoes and suaar beets-. - The city has a
pcpul.?t5<"»n of spproxinateiy /:0_,000 r.nd *rh? principal industries are the
potato or grain processing types. All sewage, domestic and industrial,
is sent through the city system for final treatment and disposal, some
on-site pretreatment being done by the potato processors.
The use of conventional lagoons or stabilization ponds for sewage treat-
ment has become very common in North Dakota because large areas of
relatively inexpensive land are usually available. These "conventional"
ponds are normally operated in a depth range of from 3 to 5 feet and
the raw sewage enters these ponds without pretreatment. Stabilization
occurs from the natural action of aerobic organisms receiving oxygen from
wave action or from photosynthesis from algae present. In most cases
the effluent is discharged to surface streams when the necessary degree
of treatment has been obtained to meet the water quality standards for
the receiving stream. Design criteria for these ponds has normally been
an organic loading of 20 pounds of BOD per acre per day (all useage of
BOD in this paper refers to the standard 5-day 20° Centigrade value).
Ice cover and cold temperatures slow down the biological action during
the winter months so that hydraulic considerations become important
in that a storage period of 6 months or more may be necessary before
the effluent reaches satisfactory quality for discharge.
* Professor of Civil Engineering, University of North Dakota
326
-------
In 1962 such a stabilization pond system was put into operation at
Grand Forks. The system consisted of two primary and two secondary
cells with a combined water surface of approximately 585 acres. At
that time, it appeared that this system would meet the needs of Grand
Forks for quite some time as no serious problems were anticipated for
a population equivalent approaching 100,000. During the 1960's,
however, there was a dramatic increase in the use of processed potatoes
and by 1967 expansion of the potato processing industry at Grand Forks
had occurred to the point where it was apparent that it was going to be
necessary to make modifications in the waste disposal system. The BOD
loading on the ponds had reached about 12,000 pounds per day and this
was expected to increase to about 25,000 pounds per day with the
annexation of a large industrial area.
To meet the situation, the City of Grand Forks in 1968 applied for and
received a Research and Development Grant from the Federal Water
Pollution Control Administration (FWPCA), Department of the Interior.
The project was entitled "Controlled Treatment of Combined Potato
Processing-Municipal Wastes by Anaerobic Fermentation, Aerobic
Stabilization Process". The stated objectives were, in part, to demon-
strate, develop, and evaluate joint treatment of potato processing -
municipal wastes by use of stabilization pond pretreatment methods con-
sisting of anaerobic treatment, aeration treatment, and anaerobic-aerated
combination treatment. A research period of 18 months was involved
but contractual and construction obstacles delayed the project until 1
January 1972, for beginning collection of operating data.
PRETREATMENT FACILITIES
Surveys of the waste being produced by the potato industries indicated
that a daily loading of about 33,000 pounds of BOD could be expected
from this source. At the same time the other municipal sewage was ex-
pected to give a loading of about 11,000 pounds per day for a total of
44,000 pounds of BOD per day. A recently passed industrial waste or-
dinance, however, was expected to reduce the industrial waste load to
about one-half of the organic loading with no appreciable change in the
expected hydraulic loading of between 4 and 4.5 million gallons per day.
Considering all these factors, it was decided to design the pretreatment
facilities on the basis of 25,000 pounds of BOD being applied per day
with a flow rate of 4.2 mgd.
Experience with the existing stabilization ponds indicated that no
serious problems were to be expected if the loading were kept to a
maximum of 12,500 pounds per day during the cold weather season. This
amounts to a gross loading of about 21.4 pounds per acre per day, or
about 40.4 pounds per acre per day on the primary cells alone. To re-
duce the incoming load to a value of 12,500 pounds per day the pretreat-
ment cells would have to reduce the BOD by at least 50%.
Available data on the raw sewage indicated that it should arrive at the
treatment site with a temperature between 10 and 15 degrees Centigrade
during the coldest weather. Since it was not planned to cover the cells,
the operating temperature was estimated to be between 5 and 10°C in mid-
winter in the aerated cells. Calculations indicated that at this tem-
327
-------
perature a detention time of 4 days would probably give a BOD reduc-
tion very near the required 50%. On the basis of these projections
the prctreatment cells were designed as shown in Figure 1, each cell
being about 320 feet square at the water line, 15 feet maximum depth,
with a volume of 8.6 million gallons. Two of them were designed to be
unmixed anaerobic cells, and the other two were each equipped with 4
aerating and mixing units. Thus, if all the sewage is to pass through
aerated cells, the detention time in the aeration units is about 4 days.
As an additional factor of safety against greater loadings than anti-
cipated, or other unforeseen conditions, no BOD reduction was assigned
to the anaerobic units. The cells are so arranged that portions may be
operated anaerobically, aerated, or in series.
Each of the 8 aeration-mixing units is platform-mounted and the impeller
is driven by a 60 hp electric motor. Compressed air from the compressor
building is piped in and released below the impeller which is submerged
within a couple of feet of the bottom of the cell. The air is supplied
by 5 rotary air compressors, each driven by a 75 hp electric motor. The
air is piped separately to each of the two aerated cells and at each
mixer a valve is used to further regulate air flow. The original speci-
fications required that the aeration equipment for each cell be capable
of transferring 440 pounds of oxygen per hour to pure water at 20°C, 760
mm Hg pressure, and zero dissolved oxygen. A central meter house and
distribution box allows control of the flow to each of the four cells.
The raw sewage flow is metered by one totalizing and recording magnetic
meter at the central meter house. The effluent from the cells is metered
by either one or two meters depending on the flow pattern being used.
PROCEDURE
During the first 12 months of operation, three different flow patterns
were used concurrently. These patterns were begun about 1 January, 1972,
and were operated without change until 31 December, 1972. Part of the
data collected from these three patterns is the basis of this report.
The patterns were as follows: (a).One-fourth of the raw sewage was
sent to the north anaerobic cell (NAN) from where it was metered out
through the north effluent meter directly to the east primary cell of
the large ponds. (b). One-fourth of the raw sewage was sent directly
to the north aerated cell (NA). It then went through the south effluent
meter and on to the west primary cell of the large lagoons; (c) . One-
half of the raw sewage went to the south anaerobic cell (SAN) and then
to the south aerated cell (SA). It then joined the effluent from NA
and proceeded through the south effluent meter to the west primary.
Thus, one-fourth of the flow received anaerobic treatment only before
going to one of the primary ponds of the system. The rest of the flow
went through the aeration process and then was sent to the other primary
pond. The two aerated cells were kept fully mixed at all times by
operating all 8 mixers continuously. The number of air compressors on
line was anywhere from one to five depending on the demand for oxygen.
It was attempted to maintain not less than one irig/1 of dissolved oxygen
in the effluent from the aerated cells.
Sampling was conducted on a weekly basis with composites being collected
for approximately a 24-hour period on the raw sewage and the effluents
328
-------
8- 52
3 < O
O «>
3- Q.' w
P 6
«-- in o
c s- o
O 1
-------
from each of the four cells. From January through June the composites
were generally collected between Wednesday morning and Thursday morning.
From July through December the pattern was changed to collect composites
from Tuesday morning until Wednesday morning. Grab samples were also
taken for analysis of bacteria, algae, and other plankton and micro-
organisms. Also, occasional grab samples were collected from the four
large stabilization ponds.
On several occasions samples were collected on a daily basis, again using
the compositers, for more accurate determinations of the BOD reductions
being obtained. Daily samples for 7 consecutive days at a time were
collected in January, April, May, June, November and December. After
the first three of these weekly series it was found that it was not
necessary to collect the cell effluents daily. Thereafter, only the
raw sewage was composited daily and the cell effluents composited
weekly. The flow meter readings were taken at the beginning and end of
each sampling period. In addition, personnel from the. City of Grand
Forks recorded daily meter readings for influent, effluents, and air
flow from the compressors.
The raw sewage compositer had its own refrigeration system which kept the
sample near 5°C during collection. Samples from the other compositers
were kept cool by collecting in styrofoam containers which were packed
with ice. Immediately after collection the samples were transported to
the laboratory for storage until the analyses were completed. All the
analyses discussed here were conducted according to Standard Methods(2).
In the laboratory the samples were analyzed for pH, alkalinity, total
hardness, total solids, total suspended solids, orthophosphatc, t^tal
phosphate, organic nitrogen, ammonia nitrogen, nitrite nitrogen, nitrate
nitrogen, COD, and BOD. Field measurements were taken for temperature
and dissolved oxygen. In mid-September the tests for the nitrogens,
phosphates, total hardness and total solids were discontinued except on
a monthly basis. In mid-October tests for volatile suspended solids
and soluble BOD were added to the weekly analyses.
After the final sample of 1972 was collected on 27 December, the flow
pattern of the pretreatment cells was altered so that all of the influent
would flow in series through south anaerobic, north anaerobic, north
aerated and south aerated in that order. The effluent leaving the south
aerated is then distributed between the east and west primary ponds.
Similar data will continue to be collected under the nesw flow pattern
until 30 June, 1973.
DISCUSSION
Temperature
Temperature variations of the raw sewage, the south anaerobic and the
south aerated cell are shown in Figure 2. The aerated cell had temper-
atures somewhat lower than the 5 to 10°C that had been predicted for
about 3 months out of the year during which time it averaged about
1.5°C. From mid-April until mid-November the aerated cell had higher
temperature than the anaerobic cell; the anaerobic cell was warmer than
330
-------
w
cs
0)
M
60
(Do) 9Jn|DJ9dUJ91
331
-------
the raw sewage only between mid-June and the first of September.
During January and February the south anaerobic seldom had ice cover, and
when it occurred it was a very thin film for only a day or two at a
time on part of the pond. The aerated cell was never frozen as such,
but had a heavy layer of foam which helped to insulate the surface.
Conditions in the north anaerobic and north aerated were quite similar
except the anaerobic cell did cover completely with thin ice for several
days at a time. The foam blanket was less dense on this aerated cell
and also darker in color than that on the south aerated cell.
Figure 3 plots the pH data for the south anaerobic and aerated cells as
well as for the raw sewage. Considerable variations is evident in the
raw sewage which shows values of pH as low as 6.0 and a.s high as 7.7.
One daily reading in April, not plotted, actually gave a pH reading of
5.7. Generally, the low values can be correlated with potato processing
operations. The largest potato processor in waste contribution operated
an on-site treatment process involving a clarifier and aerated ponds.
Problems arose with this system in early spring and finally it became
inoperative until the processing ended in mid-June. This period of low
pH is very evident on the graph. When processing resumed in September
the system was put back in operation but was only partially effective
until the middle of November, again clearly shown on the plot.
When the pretreatment cells were first put into operation the pH fell
gradually for about 6 weeks in both the anaerobic and aerated cell.
TiieittalLer , at> cue effective organisms became established, the pK
rose gradually for about one month after which no dramatic variations
occurred. During the potato processing season the anaerobic cell had a
higher pH than the raw sewage, and the aerobic cell had a still higher
value. When the processors were not operating the two reversed positions
with the anaerobic cell having the highest value. This was not as
evident for the two north cells, but it did occur for about a one-month
stretch in August.
Nitrogen
The total nitrogen concentration in the raw sewage, and in each cell
effluent, is shown as monthly averages in Table 1. Similar data is
presented for ammonia nitrogen in Table 2.
The north aerated cell showed very little reduction in total nitrogen
at any time of the year, and in about 40% of the individual readings
taken an actual increase was noted. The two anaerobic cells gave very
nearly identical reductions, generally around 20%. Further treatment
by aeration did not further remove nitrogen as is indicated by the
series-operated south aerated cell. Actually, total nitrogen increased
slightly in the south aerated cell in all months except July, August,
and September.
Ammonia nitrogen increased in both anaerobic cells in all cases, but
was reduced considerably in both aerated cells. The final concentration
of ammonia nitrogen was very nearly the same whether the aerated cell
332
-------
u
O
LU
Q
O
Z
O
O
Q_
LJ
CO
ID
>-
LU
2
CVJ
3
60
•H
o:
CL
a:
<
CO
00
333
-------
Table 1. Toial_Nrtro£en (m^/lasM) By Monthly Average.
Month
Jan.
Feb.
Mar.
Apr.
May
June
July
Aug.
Sept.
Oct.
Nov.
Dec.
Average
Raw
68.4
89. 3
80.3
52.8
57.4
49.4
34.2
33.1
35.6
46.0
47.2
56.4
54.2
NAN
52.1
50.7
52.9
43.3
50.6
45.4
35.2
32.9
36.2
39.0
40.8
42.0
43.4
NA
64.0
76.0
78.9
63.3
57.0
50.0
24.5
24.1
27.4
49.2
52.4
62.6
52.5
SAN
48.5
48.7
52.3
42.3
49.4
43.8
33.9
31.8
35.6
39.0
39.2
40.4
42.1
SA
54.8
50.6
52.3
45.0
49.8
45.4
31.9
22.9
30.8
39.6
40.8
42.8
42.2
334
-------
Table 2. Ammonia Nitrogen (rcg/1 as N) By Monthly Average
Month
Jan.
Feb.
Mar.
Apr.
May
June
July
Aug.
Sept.
Oct.
Nov.
Dec.
Average
Raw
25.5
25.5
20.6
22.9
27.9
23.1
23.6
22.9
23.1
23.0
25.6
23.2
23.9
NAN
29.8
29.6
25.8
27.2
37.9
34.4
28.7
27.1
29.9
27.4
31.2
30.5
30.0
NA
16.1
16.3
10.8
7.8
7.4
11.4
13.1
11.1
20.4
7.1
12.0
19.1
12.7
SAN
29.5
27.4
25.5
27.1
37.1
33.1
28.0
26.2
27.6
29.2
31.6
29.5
29.3
SA
17.9
15.7
10.1
9.3
10.6
11.6
iy.5
13.3
13.1
9.3
18.0
18.3
13.9
335
-------
was preceded by an anaerobic cell or not. Based on the raw sewage, the
aerated cells decreased ammonia content by about 50%. The relative
concentration of ammonia nitrogen in the south anaerobic and south
aerated cells is shown in Figure 4. The relative differences are quite
consistent except during the. period when the on-site treatment facilities
were not operating properly for the large potato processor.
Phosphate
Tables 3 and 4 show the monthly averages of the phosphate (PO,)
concentration as total phosphate and orthophosphate, respectively. Both
tables indicate that the pretreatment system was ineffective in the
removal of phosphates. At times the anaerobic cells showed some decrease
in total phosphate because of sedimentation of solids, but at times when
influent phosphate was low there was an increase in these cells. The
orthophosphates increased in the anaerobic cells and then decreased
again in the aerated cell for series operation. Overall reduction was
negligible, however. A recent study of aerated lagoons at Winnipeg,
Manitoba, indicated total nitrogen reductions of about 12%, and about
20% reduction of total phosphate^). However, detention times in these
cases were 20 to 30 days. A study by others of treatment of pea process-
ing wastes indicated no significant reduction of nutrients by an aerated
lagoon(^).
Suspended Solids
Figure 5 compares the total suspended solids in the north anaerobic
and north aerated cells with the raw sewage. The two siouth cells
cro chcwn in a similar iuaiiaci: c.u Tigi^e C. Du^'lug Lue firsi; louir iucatlis
of the year the suspended solids in the-incoming sewage; were very erratic
from week to week. The lowest value during this period occurred on 2
March when a reading of 185 mg/1 was obtained. One week later,' on 9
March, the highest reading of 1175 mg/1 was recorded. Both anaerobic
cells were effective as settling basins in that the effluent suspended
solids were seldom greater than 125 mg/1 and for 70% of the time in the
south anaerobic the readings were below 100 mg/1. There was also very
little variation from week to week. Generally, the anaerobic cells
reduced the suspended solids by about 85%.
The north aerated cell receiving raw sewage directly was also quite
erratic in concentration of total suspended solids. As would be expected,
the formation of biological floe caused an increase to occur. Because
of the detention time and mixing in the aerated cell, relative values
of raw sewage and effluent for a particular day vary greatly; however,
when all readings are averaged, the north aerated shows an increase of
about 15% in suspended solids over the raw sewage.
The south aerated cell had the benefit of the sedimentation in the
south anaerobic and consequently the variations in suspended solids
were less extreme. The bio-mass produced in the south aerated, however,
caused an increase of approximately 3% times of the suspended solids
entering the cell. In absolute values the south aerated had only about
40% as much suspended solids as the north aerated cell and 50% as much
as the raw sewage.
336
-------
o
"
Q)
O
C
w.
O)
o o
CO CO
X O
_L
O
in
O
ro
(l/6ai)
o o
C\J _
DIUOUJLUV
o
LJ
Q
O
O
O
Q_
LJ
CO
=> CJ
~5 fv_
UJ &
cn
Q.
a:
CD
UJ
u.
O
-(
3
CO
•H
337
-------
, Table 3. Total Phosphate (mR/1 as PO,) By Monthly Averap.c
Month
Jan
Feb.
Mar.
Apr.
May
June
July
Aug.
Sept.
Oct.
Nov.
Dec.
Average
Raw
68
77
90
67
71
78
32
33
37
35
48
58
58
NAN
59
54
58
77
84
80
48
39
39
54
63
57
59
NA
64
63
89
84
82
78
43
37
35
34
64
68
62
SAN
58
53
60
78
83
79
41
37
39
53
58
56
58
SA
60
53
58
78
83
82
45
38
39
54
63
59
59
338
-------
Table 4. Orthophosphate (mg/1 as PO/.) By Monthly Average
Month
Jan.
Feb.
Mar.
Apr.
May
June
July
Aug.
Sept.
Oct.
Nov.
Dec.
Average
-Raw
46
46
46
54
61
62
28
30
31
34
37
32
42
NAN
48
48
50
68
77
65
43
37
38
46
49
4V
51
NA
37
33
36
54
57
45
37
31
31
30
32
35
38
SAN
47
46
52
69
74
60
39
36
38
48
50
46
50
SA
41
37
40
58
63
53
41
34
35
39
42
40
44
339
-------
O
CO
Q
M
n
w
Q
CM
en
H
O
H
3
00
•H
(l/6uj) spi|o$ papusdsng
340
-------
,
,
1
>
j
( Q_
LJ
CO
(D
4 ID
^^
5
.-£
LJ CD
•z. —
33
H
»— >
t— '
O
CO
!
CO
Q
!— 1
i-4
O
co
Q
Q
fe;
W
cc
CL
cr
<
CD
LJ
U.
1
O
o
CM
1
O
m
o
i
o
o
(T)
1
O
m
N.
i
o
o
CO
1
o
in
-------
Readings on volatile suspended solids were not started until October
when some of the other data collection was partially discontinued. The
data available indicates that the raw sewage suspended solids were 74%
volatile; for the north aerated the figure was 78%, south aerated 89%
and both anaerobic cells 91%. It must be noted that these figures are
all based on data obtained while the potato processing industries were in
operation. It is evident, however, that the aerobic cells gave a poor
quality effluent as far as suspended solids are concerned. Similar
statements have been made by others on treatment of potato processing
wastes'-').
COD
The variations in COD are shown on Figure 7 for the raw sewage and the
two north cells, and in a similar manner for the raw sewage and the two
south cells on Figure 8. The erraticness of the raw sewage suspended
solids for the first few months previously discussed is repeated for
COD. During this time COD readings as high as 2700 mg/1 were obtained
and the low reading was 690 mg/1.
Reduction of COD was nearly equal for both anaerobic ponds as well
as the north aerated pond, and was about 40%. Of these three cells, the
south anaerobic had the highest reduction of about 42%, while the north
aerated was lowest at about 36%. However, during the summer months when
no potato processing wastes were being received the COD reduction in
the north anaerobic cell fell below 25% while the reduction in the
north aerated rose above 50%.
The anaeroblo-?erobic series gave a COD reduction overall of h3% based
on the raw sewage, while the reduction in the areated cell was practi-
cally the same as the 36% obtained in the north aerated cell. These
figures show no significant change during the summer months.
BOD
The BOD relationships for the first year of operation are presented in
Figure 9 for the two north cells and the raw sewage, and in Figure 10
for the south cells and raw sewage.
The erratic values that were noted for suspended solids and COD of the
raw sewage are repeated, as expected, for BOD. Six tests were run
during the year where each test involved continuous sampling for a
period of seven consecutive days. The reductions obtained during these
tests are given in Table 5. Also included are preliminary figures on
the total reduction obtained during 1972. During the year an inflow
of 1,666 million gallons was recorded, averaging 4.55 million gallons
per day. The total influent BOD was calculated at 8.36 million pounds
for an average daily load of 22,840 pounds.
The yearly reductions for each of the cells is somewhat higher than
had been predicted in the design. Reductions of about 30% were obtained
in the two anaerobic cells. The south cell was quite consistent, but
reductions in the north cell fell off sharply at year's end. The reason
for this is unknown at the present time. The south anaerobic gave 4.5%
342
-------
I
o
o
v:
c
-------
C\J —
003
344
-------
o
UJ
Q
O
2
O
O
Q.
UJ
CO
~~) -> •
r^ OJ
^ ^
UJ CT>
2!
ID
o:
Q.
1
O
O
PQ
CTi
a)
CD
UJ
U_
a
o
CD
o
o
o
o
C\J
o
o
o
o
o
CD
o
o
CD
O
O
O
o
OJ
345
-------
o
Ld
Q
o
o
Q.
UJ
CO
O
Lu
=>
o:
Q.
tr
m
UJ
1
o
o
to
1
o
o
^fr
i
o
o
C\J
1
o
o
o
1
o
o
00
1
o
o
CD
1^
o
o
*•
|C
o
o
CJ
o
CO
I
O
O
rH
0)
00
•H
346
-------
Table 5. BOD Reduction (%)
Period
1972
1/15-1/21/72
4/21-4/27/72
5/9-5/15/72
6/6-6/12/72
11/16-11/22/72
12/12-12/18/72
All of 1972*
NAN
30.4
36.0
25.9
28.8
19.4
13.3
28.1
NA
53.9
61.3
58.5
77.0
31.6
34.7
57.9
SAN
32.0
42.3
26.1
21.0
28.5
30.4
32.6
SA
63.1
59.6
64.2
82.7
70.2
59.8
64.0
SAN-SA
Series
74.9
76.7
73.5
86.0
78.7
72.0
75.7
ALL CELLS
58.5
63.0
57.6
69.4
50.3
46.1
59.3
more reduction during the year than the north cell and this can probably
be attributed to higher temperature during cold weather in the south cell.
Hiib cenjpeL'aLure (inference iioet> not e.R.ist during the summer when the
north anaerobic was about one-half degree higher than the south cell.
During this time equal or better reductions were obtained in the north
cell which was receiving only one-half as much load as the south cell.
The south aerated cell showed the beneficial effect of being preceded
by an anaerobic cell in that the BOD reduction was 6% greater than
that in the north aerated while the detention time was only one-half
as long. When the two south cells are considered as a unit, thereby
making the detention time the same as for the north aerated cell, the
BOD reduction is about 18% above that in the north aerated cell. A
good share of this increase is, of course, due to the sedimentation
occurring in the anaerobic cell. The eventual effect of accumulating
sludge in this cell has not been determined at this time.
During the two 7-day runs made during November and December, soluble
BOD values were also determined. The north anaerobic cell gave very
inconsistent data for these two runs in that one of them indicated an
increase in soluble BOD of 21%, and the other an increase of 40%. The
south anaerobic values agreed closely with each other, showing an aver-
age increase of 17%. In the two aerated cells the results were very
nearly identical with a reduction of 90% in soluble BOD observed in the
* Preliminary figures
347
-------
north cell and 87% in the south cell.
The average ratio of BOD for COD for the year was 0.55 for the raw
sewage, 0.68 for each of the anaerobic cells, and 0.39 for each aerated
cell. These values are nearly identical with values reported by others
for secondary treatment of potato processing wastes'5),
In order for aerobic biological treatment to proceed satisfactorily
a certain level of inorganic nutrients must be maintained. Commonly
quoted minimum figures are a BOD : N : P ratio of 100 : 5 : 1.
In this study the ratio for the raw sewage averaged 100 : 9.9 : 4.0,
and for the south anaerobic cells the values were 100 : 10.6 : 5.5.
Therefore, it would appear that the nutrient level preceding each
aerated cell was entirely adequate.
Since the anaerobic cells were not mixed a sludge builcl-up is occurring
in both of these cells. On September 8, 1972, a study was made of the
sludge depth in the south anaerobic cell as this cell had been receiv-
ing one-half of the total flow. By withdrawing samples at varying
depths it was found that a sludge layer about 4 ft. dee:p existed as
the center of the cell. At the side opposite the inlet, the depth was
only about 2 ft. Eventually it is possible that sludge will have to
be withdrawn from the anaerobic cells. The necessity or frequency of
this has not as yet been determined.
The treatment provided by the system used during this p>eriod had a very
beneficial effect on the large stabilization ponds. During the summer
of 1971 it was mid-June before the secondary ponds met water quality
standard of a ROD of ?5 mg/1, or .less. The primary lagpor.s remained
above this level until well into July and some odor problems occurred.
In the summer of 1972, the large ponds made an early recovery with no
odors of any significance. This was a great improvement when it is
considered that the pretreatment cells did not become operative until
the first of January, while potato processing began in September.
While the pretreatment cells were effective in reducing the odor problem
from the main ponds, there was odor emitted from the two uncovered
anaerobic cells. Normally, this did not present any problems because
of the distant location of the cells from the city. However, if weather
and wind conditions were right, an occasional detection of odor occurred
within the city.
Generally, the research project operated quite smoothly during 1972 al-
though some nuisance problems occurred. The magnetic flow meters did
not give valid readings until the first week in February so the flow for
the first month had to be taken from pumping records at the master lift
station. At the end of the year the effluent meter which measured all
the flow except from the north anaerobic cell was again inoperative.
The most serious interference with the research occurred between 13
May and 19 June. The largest potato processing plant experienced
operating difficulties with its waste treatment process and greatly
exceeded the organic loading that had been anticipated from them. The
7-day tests taken in April, May and June all gave an average BOD load-
ing of about 35,000 pounds per day, with individual days in excess of
348
-------
50,000 pounds. With the arrival of warmer weather the biological
activity increased to the point where it was impossible to maintain an
aerobic condition of the effluent from the two aerated cells. Between
13 May and 19 June the dissolved oxygen content of the effluent leaving
the aerated cells was less than 0.25 mg/1, and for most of the period
was 0, even with all compressors in operation. When potato processing
ceased in mid-June the problem was overcome immediately and did not
reoccur again during the year.
During the severe weather of January and February there was some ice
build-up on the mixer platforms and shafts. No interruptions of mixer
operation occurred, however. All the compositing samplers were housed
in insulated shacks equipped with electric heaters but occasionally a
stoppage with ice would occur in the sampling line and a grab sample
would have to be taken. Fortunately, these situations took place only
infrequently. Because of the discharge method the sampler housed over
the effluent manhole from the north anaerobic cell was subject to severe
corrosion from escaping gases. This sampler could not be left in place
except while it was operating which was somewhat inconvenient. Also,
electrical connections and contracts would corrode and as a result the
sampler would occasionally fail to function.
City personnel responsible for maintenance of the equipment had consider-
able difficulty with circuit breakers and circuit board vibrations.
None of these occurred at such a time that the research project v/as
adversely affected, however.
SUMMARY
This progress report presents data from the first full year of operation
of pretreatment cells preceding conventional stabilization ponds at
Grand Forks, North Dakota. The waste handled was a combined municipal-
industrial waste with main industrial contribution coming from potato
processing industries. Data was gathered on anaerobic operation, aerated
operation, and anaerobic-aerated series operation for the calendar year
of 1972. Composite samples were collected at weekly intervals, with
occasional runs of daily sampling for a full week at a time. Although
this project is still active and the collection of data continues,
the following observations are made on the first year's data:
1. Combined wastes from potato processing and municipal
sources contain ample nutrients for successful pre-
treatment by either aerated or anaerobic-aerated
processes.
2. BOD reductions of 50 to 70% can be obtained at
temperatures of 5°C, or less, with detention times
of from 4 to 7 days in the aerated cells.
3. Aerated or anaerobic-aerated pretreatment produces
a poor quality effluent for nitrogen,phosphorous,and
suspended solids. Further treatment is necessary to
meet surface water quality standards.
349
-------
4. Periodic removals of sludge may be required from
anaerobic pretreatment cells which are not
completely mixod. The frequency of such removal is
indefinite from the period covered in this report.
5. Winter operation at temperatures of -30°F present no
particular problem with diffused aeration and submerged
impellers.
6. Anaerobic cells need not be covered or mixed for
effective cold weather operation ahead of aerated
cells. During warm weather, however, an odor problem
may develop.
7. Considerably better pretreatment is obtainable from
an anaerobic-aerated series than from aerated treatment
alone.
350
-------
LITERATURE CITED
1. ALSAGER, MELVIN 1). An Approach to Total Management of Potato
Processing Wastes. Presented at 27th Annual Industrial Waste
Conference, Purdue University, Lafayette, Indiana, May, 1972.
2. American Public Health Association, American Water Works
Association, and Water Pollution Control Federation. Standard
Methods for the Examination of Water and Westewater, 13th edition,
1971, APHA.
3. BURNS, G. E., GIRLING, R. M., PICK, A. R., and VAN ES, D. W.
Evaluation of Aerated Lagoons in Metropolitan Winnipeg. The
Metropolitan Corporation of Greater Winnipeg, Waterworks and
Waste Disposal Division, March, 1970.
4. DOSTAL, KENNETH A. Aerated Lagoon Treatment of Food Processing
Wastes. Water Quality Office, Environmental Protection Agency,
Washington, D. C., March, 1968.
5. DOSTAL, KENNETH A. Secondary Treatment of Potato Processing
Wastes. Water Quality Office, Environmental Protection Agency,
Washington, D. C., July, 1969.
351
-------
ACTIVATED SLUDGE - BIO-DISC TREATMENT OF DISTILLERY WASTE***
BY JOHN L. THOMAS* AND DAVID A. SANBORN**
INTRODUCTION
Waste treatment facilities at the Pekln, Illinois, distillery of
The American Distilling Company began operation on September 27, 1971.
Since that time, facilities have not only provided treatment for plant
process wastes, but have also served as a demonstration project with the
assistance of an Environmental Protection Agency (EPA) grant.
The objectives of the studies made were to determine the performance,
economics, and the design parameters for treating distillery Wciste. Parti-
cular emphasis has been placed on the comparison of the activated sludge
and the Bio-Disc (Rotating Biological Contacter) processes.
PRODUCTION PROCESSES
The distillery utilizes processes such as mashing, cooking, fermenting,
and distilling. Approximately 12,500 bushels of grain per day are used as
the raw material. The initial process step consists of mixing ground grain
with water and cooking to produce a mash. The starch content of this mash
is then converted to sugar by a malt. The malted mash is fermented
and the sugar content is converted to alcohol. Alcohol is recovered
from the mash in a primary distillation column. Distillate from this
first column is again distilled in a pot still to refine the product.
Mash remaining after distillation is centrifuged and dried to produce
a high protein feed.
Process wastewater contains non-recoverable grain particles and
byproducts such as organic acids, aldehydes, esters, and alcohols. Normal
process wastes are increased in flow and strength by the cleaning of grain
mixers, cookers, converters, mash coolers, fermenters, stills, centrifuges,
and evaporators.
* Associate Chief Sanitary Engineer, Stanley Consultants.
** Chemist and Treatment Plant Supervisor, The American Distilling Company.
*** This investigation was supported by funds from the Environmental Protection
Agency under Project 12060FL.
352
-------
WATER AND WASTE SYSTEMS
Water is supplied to the distillery from three sources. A well water
system provides process and some cooling water. A river supply is used for
other cooling applications. City water is used primarily for domestic and
fire protection purposes.
Wastewater discharges include the following:
1. Storm drainage and other uncontaminated waters.
2. Process and sanitary waste.
3. Slightly contaminated wastewater discharging from barometric
condensers.
A survey of waste facilities made in 19&7 identified 27 sewers front,
the distillery discharging a mixture of these wastes to the river.
Starting in May, 19&7, a systematic program was initiated to identify
and isolate process wastewaters. During the summary of 19&9. a sewer
separation program was completed in which all high strength process w*stft~
waters were routed to a pumping station which directed this flow to, the "
river. Later, this pumping station was utilized for discharging the '
wastewater to the treatment plant. High volume flows from the barometric
condensers which contain relatively low concentrations of BOD were also
isolated and combined in a separate trunk sewer for direct discharge to
the river.
After completion of the sewer separation project, the process waste-
's "'
water stream was continually monitored to establish wastewater character-
istics and flow variations. These data were to serve as a basis for
treatment plant design.
In the initial assessment of the treatment requirements, it was
planned to treat the process waste stream and then mix this treated water
with the high volume flows from the barometric condensers. This mixture
would yield a total waste flow to the river having a BOD_ content of less
than 30 mg/1. Subsequent modification of regulatory agency standards
required change to this approach. These revised regulations prohibited ,<
the blending of cooling water with waste. Also, the goal for effluent
quality was revised to permit only 20 mg/1 of BODc.
353
-------
Sampling, gaging, and testing prior to treatment plant design In-
dicated that flow, BOD, and suspended solids varied quite widely on both
a daily and hourly basis. These variations are a function of production
process and operations being performed. An operation such as mashing
may occur two, three, or four days per week. Distilling may be performed
on other days. Some days, both of these processes are used. Equipment
cleaning also affects the total load by imposing periodic additions to the
normal process loads. Fermenter washing and pot still cleanout are typical
of such operations.
A complete analysis of hourly waste strength variation was not made.
However, limited hourly tests of BOD,, indicate a variance from less than
200 mg/1 to over 10,000 mg/1. It was projected that daily loads would
exceed a level of 3,200 pounds of BOD,, about 20 percent of the time.
The pH of the waste is Increased periodically by the presence of
alkaline cleaning chemicals. Data indicated that pH of the processed
waste flow may vary from a low of 2 to as high as 13. Large flows of
waste bearing condensate during periods of evaporator operation signifi-
cantly increase the total process waste temperature. Temperature of the
waste varied from 50 F to over 150 F.
Concentrations of nitrogen and phosphorous were low enough to
indicate the need for the addition of these nutrients for satisfactory
biological treatment.
Variation of these waste parameters directly influenced the design
philosophy for the treatment facility.
After the waste treatment plant was placed in operation, collection
of raw waste data continued. These data are described later herein along
with treatment plant operating characteristics.
LABORATORY STUDY
In 1968, laboratory studies were Initiated to determine factors
affecting treatment plant performance. These studies indicated that the
waste was amenable to biological treatment and that the activated sludge
process was an effective treatment for distillery wastewaters. It was
also determined that consideration must be given to pH, temperature, and
nutrients. In the aeration basin, pH must be maintained within the range
of 5.0 to 9-0, temperature must be maintained at less than 100 F and some
supplemental nutrient addition would be required.
354
-------
PLANT ARRANGEMENT
Because of the relatively low level of suspended solids anticipated,
primary sedimentation of the waste was not included as a unit operation
in the treatment plant design. However, a grit chamber was included as
an initial step to remove heavy particulate matter.
The selection of the configuration and size of biological treatment
equipment was based on several considerations:
1. The Bio Disc was included to evaluate its performance for treating
distillery waste.
2. An equalization basin was incorporated to minimize the effect of
waste load variation. This was required particularly for the
Bio Disc because of its plug-flow characteristics.
3. One aeration basin for the activated sludge process was sized to
be capable of treating approximately the same flow as the Bio Disc.
4. Facilities were arranged to maintain a relatively constant flow
through the Bio Disc and the companion aeration basin to minimize
the effect of flow variation on equipment performance.
The plant configuration selected included four biological treatment
lines. The Bio Disc was sized to treat one-fourth of the plant waste while
each of three activated sludge lines were sized to treat one-third of the
plant waste. It was planned that the Bio Disc and one activated sludge
line would each treat equal flows during many phases of the test period.
Any additional flow would be delivered to other two aeration basins.
The Bio Disc was designed as a six stage unit with an intermediate
settling tank after the third stage. The manufacturer designed a system
to provide 90 percent reduction of BOD and suspended solids at an average
flow rate of 120,000 gpd and a BOD loading of 800 pounds per day. These
waste characteristics result in an organic loading of 17.8 pounds of BOD,.
per 1,000 square feet of biological surface. To minimize the effect of the
continuing variations in wastewater flow, pH, temperature, and strength an
equalization basin preceding the Bio Disc was designed with a detention
time of eight hours at a flow of 132,000 gpd.
355
-------
' The activated sludge aeration basin was designed for solids retention
time of approximately 30 days at average flow rates. This resulted in a
33~Hour hydraulic detention period at an average flow of 177,000 gpd and
an average organic loading of 33 pounds BOD per 1,000 cubic feet per day.
The objective was to achieve some measure of aerobic digestion and provide
sufficient aeration volume to dampen out the effect of large hourly varia-
\ *
tJons' in wastewater flow, temperature, pH, and strength.
PROfiESS FLOW PATTERN
Figure 1 is a plant flow schematic which illustrates the relationships
of the various unit operations in the treatment plant.
Untreated waste is collected in the process sewer system and routed to
th» lh*in pump station. The flow is pumped through a grit chamber where
large particulate matter is removed and required supplemental nutrients
(nitrogen and phosphorus) are added.
The next unit in the flow sequence is an, equalization basin and flow
splitter which is designed to serve two functions:
1. Provide adequate volume for buffering peaks in temperature and pH
for that portion of waste flowing to the Bio Disc unit.
2. Provide a means for dividing total waste flow to the four process
treatment 1ines.
In the basic parallel flow sequence, a constant 25 percent of the plant
design waste flow (133,000 gpd) was directed to the Bio Disc unit and another
25 percent was routed to Aeration Basin No. 3. The balance of the waste
flow was treated in Aeration Basins 1 and 2.
The Bio Disc unit consists of a series of closely spaced discs mounted
on a horizontal shaft. Discs are submerged in the wastewater to just below
the. shaft level in a tank with the bottom formed in a cylindrical shape
slightly larger than the discs. Rotation of the shaft alternately exposes
disc" surface area to the wastewater and to the atmosphere. The discs thus
serve both as media for growth of a biological slime and as an aeration
device. Intermediate settling is provided between stages of the Bio Disc.
Sludge removed at this point is normally discharged to Aeration Basin No. 2
for further stabilization.
356
-------
Treatment Plant Schematic
NUTRIENTS
i
SPLITTER
BOX
AERATION
BASINS
CLARIFIERS
1
NO
^
NO
PUMPS
r
. 1
r
. I
-i r
i
NO.
1
NO.
r
2
r
2
r
A
v__^
nr
*TJ
\ ^
F
N
NO. 3
^ '
NO. 3
EFFLUENT
T
CHLORINE
ALTERNATE
FLOW
METERING
SLUDGE
TANKS
. TO SLUDGE LAGOON
RETURN
SLUDGE
t t
SLUDGE
BASINS
NO. 1 Of
1
357
Figure 1
-------
The Bio Disc unit is housed in 16 feet by 6k feet concrete block
buiIding.
Three identically sized aeration basins operating as complete mix
activated sludge units are provided for contact between the active micro-
organisms and the waste materials. A separate final clarifier is provided
for each aeration basin. Sufficient underflow from the final clarifiers
is returned to the aeration basins for maintaining the desired mixed liquor
suspended solids content. The remaining sludge is wasted. It is possible
to return the sludge from Final Clarifier No. 3 to Aeration Basin No. 3
independent of the operation of other basins.
A separate final clarifier is also provided for the Bio-Disc flow
stream. Sludge from this unit is normally routed to Aeration Basins 1 and 2
for stabi1ization.
Effluent from all four final clarifiers is combined in a single sewer
leading to a chlorine contact chamber.
Excess sludge, not needed for return to the aeration basins, is pumped
onto an abandoned ash disposal area. Sludge was not thickened prior to
disposal.
METERING, SAMPLING. AND TESTING
Flows were measured at the following points:
Po j nt Description
A Total Plant Influent
B Clarifier No. 3 Effluent (Activated Sludge)
C Clarifier No. k Effluent (Bio Disc)
D Return Sludge to Aeration Basin No. 3
E Return Sludge to Aeration Basin Nos. 1 and 2
F Waste Sludge
G Total Plant Effluent
358
-------
Twenty-four hour composite samples were routinely collected from
Points A, B, C, and G for a complete analysis. Solids and COD tests were
made daily while BOD, nitrogen, and phosphate tests were made twice weekly.
All samples were analyzed at the American Distilling Company laboratory.
All analyses were conducted in accordance with procedures described in the
13th edition of Standard Methods.
OPERATIONAL PROCEDURES
In order to achieve the stated objectives of the research project,
the study period was divided into stages of different operational patterns.
During the total period of the study from the beginning on September 27,
1971, to the completion on December 2k, 1972, 12 operational stages were
evaluated. The original operational plan was modified considerably as
the results from each stage were obtained.
Table 1 summarizes the operational conditions for each stage. A
brief description of each stage is presented below.
Stage 1 - The purpose of this stage was to establish an acclimated
population of biological organisms for both the activated sludge and Bio
Disc Processes. It was also to provide an opportunity to determine and
correct any mechanical operational problems.
Operational problems with the stationary aerators, septic conditions
in the equalization basin, and apparent overloading of the Bio Disc unit
extended this stage until February 6, 1972, for a total period of 19 weeks.
Initially, flow to both the Bio Disc and Aeration Basin No. 3 were routed
through the Equalization Basin. This operating pattern was selected on
the basis that both test lines should receive waste of the same quality.
At the start of this stage, flow to the Bio Disc and Aeration Basin
No. 3 was to be 133,000 gpd (25 percent of the plant design flow) each.
Because of inadequate treatment by the Bio Disc, flows were reduced to this
unit in November to about 50,000 gpd. In January, in order to reduce the
effect of sudden peaks in raw wastewater temperature and pH, only flow to
the Bio Disc was routed through the Equalization Basin.
359
-------
LA oo cn oo
CM! vo oo r^ PA
— 1 CM — CM
— 1 CM LA -3" 1^-
•—( r-. vo P~ CM
Ol -3- LA CM OO
— 1 vO LA CA CM
•—
o -a* o vo
CT\| CA •"" -3" PA
•— »— •—
col o • — vo i —
cn r-- oo CM
co i~~| LA LA cn o
2 -3" -3" LA —
or:
LU
1—
<; \o| LA OO CM LA
Q. .a- -a- r-. —
eg
1— LA| LA LA o oo
c£.
— LU
Q.
LU O .
_l -3- LA Cn LA LA
OQ _i -a- -a- vo CM
^ ^
1— 3
o
< <| LA LA •— -3-
CA| -3- -a* VD CA
(~\
z
t-\
LU CA| o cn oo o
"^ vo vo r""* LA
Z
a. .
oj I o f^ -3~ **^
\o ^D r*^' -cj"
—• | 1 p- LA LA
i LA f-
cnl
4-1 1 a. LU
co cn C3
a
0 — u .c
— c co 0) cn 2 Q
O C ^ > ~ O l±l
CO -OJ*J
0 U. 1-
— CJ
03 <
LA —
VO O
CM CM
CM LA
CM —
LA O
oo r*»
•— *—
o oo
CA —
•— 1—
O OO
cn !*••
LA O
-a- LA
o cn
oo r**1*
CA OO
CA -3"
*«- •—
CA -a-
CA —
r— t—
CA CA
CA CM
•— i—
CA vO
CA LA
^— *—
CA LA
CA CA
*— t—
CA CM
rA CT\
Q.
cn
o
•• ID 4J <:
3—0
O Q- <
LL.
cn CM
r-- oo
CM
CM VO
CM OO
CM
VO LA
cn cn
»—
— vO
vO OO
^~
CM CA
cn CA
CA rA
vO CA
O f*^
LA CM
w—
PA LA
O PA
r—
LA PA
LA PA
*—
t^ cn
-^" vO
^~
LA O
r^s. CD
r~- r—
CM CM
vo r^
^«-
OA ^~
oo • —
C"
cn 2
— O
O
O
o
•3-
o
o
o
-3"
O
O
O
-a-
o
o
LA
-a-
o
o
LA
-a-
o
o
o
-a-
o
o
IJ-I
-a-
o
0
ILA
-a-
o
0
LA
IPO,
O
o
ILA,
IPO,
O
0
LA
«M
O
U^i
ir^
• —
,
i
r—
^- 'T3
cn a>
E c
c
- CO
CO .—
CO Q-
1
3:
LA
OO
CM
CA
LA
CM
O
-3"
O
vD
OO
-a-
o
-a-
CM
-3-
O
O
CM
-a-
o
vO
cn
CA
O'
vO
vO
CA
O
O
CA
-3-
LA
r—
VO
CA
O
O
CM
CM
O
O
_3*
CM
0
r^
vO
• —
i
4-"
-------
Stage 2 - This stage extended from February 7 to February 20, for a
period of two weeks. The plan was to hold the average flow to the Bio
Disc at 60,000 gpd (11 percent of total plant design flow) and the flow
to Aeration Basin No. 3 to 133,000 gpd. Actual flow to the Bio Disc
averaged 63,000 gpd while flow to Aeration Basin No. 3 averaged 135,000 gpd.
Scheduled MLSS concentration in the aeration basin was 1,250 mg/1, but rapid
bio-mass growth resulted in an average MLSS of 1,670 mg/1 during this stage.
Stage 3 - Stage 3 extended from February 21 to March 12 for a period of
three weeks, and was divided into two phases. The first week, the average
flow to the Bio Disc was 69,000 gpd, but BOD removal was so poor that flows
to the Bio Disc were reduced to 45,000 gpd during the last two weeks
(Stage 3A).
The scheduled average flow to Aeration Basin No. 3 was again 133,000 gpd
but actually averaged 156,000 gpd for the first week and 123,000 gpd during
the last two weeks. The target MLSS level was 2,500 mg/I. Actual MLSS
concentrations averaged 2,400 mg/1 for the first week and 2,200 mg/1 for
the last two weeks.
Stage 4 - The goal of Stage 4, which began on March 13 and ended on
April 2 for a total of three weeks, was to hold the flow to Aeration Basin
No. 3 at 133,000 gpd and the MLSS concentration at 3,500 mg/1. Flows to
the Bio Disc were scheduled at 45,000 gpd.
The actual average flow to the Bio Disc was 49,000 gpd. Aeration
Basin No. 3 received an average flow of 114,000 gpd and MLSS concentrations
averaged 3,615 mg/1.
The septicity of the wastewater influent to the Bio Disc from the
Equalization Basin was considered to be a contributing factor in the
continuing low BOD removal rates. Therefore, work was initiated on the
design and installation of an aeration system for the Equalization Basin.
Stage 5 ~ This stage began on April 3 and ended on April 16 for a
total period of two weeks. The scheduled flow to the Bio Disc was 45,000 gpd
which was the actual average flow for the period. Scheduled flow to Aeration
Basin No. 3 was 133,000 gpd with MLSS concentrations at 4,500 mg/1. Actual
average flow and MLSS were 103,000 gpd and 4,294 mg/1, respectively.
361
-------
It was initially anticipated that after Stage 5, a MLSS level would
be selected at which optimum BOD removals occurred. Since BOD removals
were excellent at all studies MLSS concentrations, there was no apparent
optimal level. Therefore, it was decided to maintain a MLSS concentration
in the 3,500 to k,500 mg/1 range for future stages. It was felt that this
level would provide average protection against moderate shock loads. Flows
to the Bio Disc would be continued at 45,000 gpd until the aeration system
was installed in the equalization basin.
Stage 6 - This stage lasted four weeks, from April 17 to May 14, until
septic conditions were reduced in the Equalization Basin. The schedule was
to operate Aeration Basin No. 3 at an average flow of 80,000 gpd (15 per-
cent of total plant design flow) and the Bio Disc at 45,000 gpd.
Actual flow to Aeration Basin No. 3 averaged 79,000 gpd and MLSS
averaged 3,360 mg/1. Actual flow to the Bio Disc averaged 48,000 gpd.
On May 11, the Equalization Basin aeration system was put Into
operation. By May 15, septic conditions in the Basin had been substantially
reduced, although no measurable DO was present In the effluent.
In order that the activated sludge and Bio Disc operations be comparable,
it was decided In the next stage to again route all flow to Aeration Basin
No. 3 through the Equalization Basin. In order to not overload the Bio Disc,
about 100,000 gpd of raw wastewater would be routed to the Equalization Basin.
About half of the flow would go to each process.
Stage 7 ~ This stage began on May 15 and ended on June 18 for a period
of five weeks. Flows to Aeration Basin No. 3 averaged 50,000 gpd and MLSS
concentrations averaged 4,000 mg/1. The Bio Disc received an average flow
of 1*5,000 gpd.
Stage 8 - In this stage, it was decided to increase the flows to each
of the processes to 90,000 gpd, and again route the total flow of 180,000 gpd
through the Equalization Basin. MLSS concentrations in Aeration Basin No. 3
was scheduled for 4,000 mg/1.
This stage began on June 19 and ended on July 16 when the distillery
began its annual shutdown for vacations and maintenance. During this
four-week period, the average flow to Aeration Basin No. 3 averaged 78,000 gpd
and MLSS concentrations averaged 4,200 mg/1. The Bio Disc received an average
flow of 71,000 gpd.
362
-------
At the end of this stage, ft was concluded that the activated sludge
process should receive hydraulic loads of progressively greater magnitude
in the stages following the annual distillery shutdown period. Since the
activated sludge process showed no recognizable sensitivity to sudden
changes in influent pH and temperature, it was decided to route only the
Bio Disc influent through the Equalization Basin in future stages.
Stage 9 - This stage began September 11 and ended on October 1 for a
period of three weeks. Scheduled flows to both test lines were 130,000 gp).
The average flow to Aeration Tank No. 3 was 118,000 gpd and the average ML3S
concentration was 4,237 mg/1. Flow to the Bio Disc averaged 114,000 gpd.
Stage 10 - This stage began on October 30 and ended on November 26,
for a period of four weeks. Scheduled flow to Aeration Basin No. 3 was
185,000 gpd. Actual flow averaged 170,000 gpd and MLSS averaged 4,860 mg/1.
Scheduled flow to the Bio Disc was 64,000 gpd. The actual flow averaged
55,000 gpd. Effluent from the Bio Disc final settling tank during the fir-,t
week of this stage was so poor that it was returned to Aeration Basin Nos. 1
and 2. After the first week, the Bio Disc effluent quality improved
considerably and this practice was stopped. During the last week of this
phase, the first stage of the Bio Disc was inoperable because of mechanical
problems.
Stage 11 - This stage began on October 30 and ended on November 26 for
a length of four weeks. Average flow to Aeration Basin No. 3 was scheduled
for 212,000 gpd but actually averaged 195,000 gpd. MLSS averaged 4,025 mg/1.
Average Bio Disc flow was scheduled for 72,000 gpd but actually averaged
65,000 gpd. Effluent from Final Settling Tank No. 4 was returned to Aeration
Basin Nos. 1 and 2 during one week because of poor quality.
Stage 12 - This stage was the last four weeks of the project, from
November 27 to December 24. During this period, the Bio Disc and activated
sludge processes were operated in series. Flow from the Equalization Basin
went first through the Bio Disc and then directly to Aeration Basin No. 3.
Mixed liquor from Aeration Basin No. 3 was proportioned between Clarifier
Nos. 3 and 4 to achieve equal surface settling rates in each unit.
363
-------
Necessary piping changes were made during the first week of the stage.
Flows during the last three weeks averaged 22^,000 gpd, while MLSS in
Aeration Basin No. 3 averaged 3,285 mg/1.
START-UP ADJUSTMENTS AND OPERATIONAL PROBLEMS
After plant operation began in late September, 1971, Stage 1 operating
procedures were followed through February 6. During this period, a biological
mass capable of treating the distillery wastewaters developed and necessary
modifications to some of the equipment was begun.
Nutrient Addition - As previously indicated, nitrogen and phosphorous
were to be added to the wastewater to provide necessary nutrients for biological
growth. Nitrogen and phosphorous were to be added equal to 5 percent and
1 percent of the BOD,., respectively. Anhydrous ammonia injected as a water
solution was added to provide nitrogen and phosphorous was added as triple
superphosphate.
Both nutrient supply systems developed problems with plugging of
supply piping. This was solved in the phosphate system by:
1. Mixer modification in the supply tank to provide better dispersion
of the poorly soluble triple superphosphate.
2. Screening of the phosphate suspension.
3. Use of supplemental carriage water to dilute the phosphate
suspension.
The nitrogen system originally relied upon untreated well water as a
carrier of the ammonia nitrogen to the wet well. The high pH of the ammonia
solution resulted in precipitation of calcium and possibly some magnesium
present in the well water. Scale formations completely plugged the ejector
in only a few hours. This problem was minimized by substituting mixed liquor
from Aeration Basin No. 2 for the well water as the carriage liquid.
Due to operational problems as well as some initial analytical errors,
nutrients were often below requirements during the first several months of
operation. By the time Stage 2 began on February k, the phosphate problems
had been corrected, although a satisfactory nitrogen delivery system was not
completed until Stage A in late March.
364
-------
Grit Removal - The amount of participate material in the waste far
surpassed original design estimates. So much so, that a chute to transport
the materials to the ground replaced the original reception barrel. Also,
some freezing of the solids in the grit chute was experienced.
Mechanical Aerators - The pier-mounted mechanical aerators underwent
numerous mechanical modifications. The initial units exhibited excessive
vibrations that resulted in mechanical failure. In November, the mechanical
aerators were replaced by temporary floating units while repairs were made
to the mechanical units. While the pier-mounted aerators were all operating
again by February 4, in-place modifications were not complete until April.
Low DO levels were frequently experienced in Aeration Basin No. 3-
DO levels often dropped to 0 mg/1.
Flow Rates - It was difficult to control flow rates to Aeration Basin
No. 3, because of the constant-speed raw wastewater pumps and the problems
encountered in attempting to manually adjust the flow with an on-off pumping
cycle serving a continually varying wet well influent flow.
Equalizat ion Bas in - The longer detention periods of waste in the
Equalization Basin due to lower flow rates through the Bio Disc resulted
in septic conditions. This led to the installation of an aeration system
in the Basin that was put into operation on May 11.
Bio Pisc - The Bio Disc experienced numerous mechanical failures,
particularly in the intermediate settl ing tank.
Final Settling Tanks - Several days of icing were experienced during
the coldest weather, but in general the final clarifiers were free of
mechanical problems.
Sludge Disposal - The waste activated and Bio Disc sludge did not dewater
satisfactorily in the sludge disposal area. Ponds of water were nearly always
present. Periods of very high SVI's were experienced with the MLSS. Possible
reasons for these two conditions are explained later in the report.
SYSTEM LOAD
The wide variation in wastewater flow, strength, pH, and temperature
resulted in wide variations in loadings to Treatment Line Nos. 3 and ^
during the various operational stages as shown in Table 1.
365
-------
Results shown based on a five-day operational week from Monday through
Friday. Weekend flows and wastewater characteristics have not been sub-
jected to a detailed study. However, loads during weekends are generally
considerably lower than weekday loads.
In an attempt to develop a technique for prediction of BOD loadings
from distillery operations a relationship between BOD,, and bushels of
grain mashed was investigated. Grain is not mashed every day and other
plant production processes in use vary from day to day. However, a one
week period represents a normal recurring cycle and it was believed
reasonable that a relationship between bushels of grain mashed weekly and
weekly total pounds of BOD,, could be developed. Data is shown on Figure 2.
Two curves are also shown. The equations of these curves are as
fol 1 ows :
Curve A: BOD- = 0.256 B
where
Curve B: BOD = 7,982 + 0.177 B
BOD = Total weekly raw wastewater BOD,., Ib.
B = Grain mashed weekly, bushels.
The equation for Curve A is derived from the design basis of 3,200 Ib
of BOD;, produced from a daily grain mash of 12,500 bushels.
The equation for Curve B is obtained from a linear regression analysis
to determine the line of best fit. A correlation coefficient of 0.^3
indicates a poor fit of the curve to the data.
It was concluded that weekly loadings of BOD,, cannot be accurately
predicted from bushels of grain mashed.
Figure 3 shows the frequency of daily BODj. loadings. The data analyzed
the daily BOD- load was less than the design load of 3,200 pounds, 76 percent
of the time.
BOD :COD RELATIONSHIP
Nutrients were added to the wastewater in the weight ratio of BOD :
Nitrogen: Phosphorous of 100:5:1. In order to adjust the nutrient feed
to BOD levels an immediate analysis for BOD is desirable. Since the BODj.
366
-------
35
30
25
CO
o
o
Q-
o
CO
co 20
LO
Q
O
00
15
CO
•<
Q£
>-
10
Relation Of Raw Waste BODs
To Grain Mashed
Q
0
0
o
o
o
10 20 30 40
GRAIN MASHED WEEKLY, THOUSANDS OF BUSHELS
50
367
Figure 2
-------
BOD5 Load Frequency
Treatment Plant Influent
PERCENT OF THE TIME BOD5 IS EQUAL TO OR LESS THAN VALUE
368
Figure 3
-------
test takes five days for completion results cannot be used to adjust
nutrient feed rates to correspond to variations in BOD,..
At some wastewater treatment plants, the hourly and daily fluctuations
in BOD are minimal or exhibit a rather predictable pattern. At this plant
the BOD,, loadings are not only highly variable, but do not show any
predictable pattern. Without reliable information as to likely BODj. loads
for a given day or hour, the plant operator has had to set nutrient feed
rates at arbitrarily high levels, so that enough nitrogen and phosphorus
will be available during periods of high loads. This has led to unnecessarily
high BOD_:N:P ratios during days of low loads.
The standard COD test takes about three hours for completion and,
therefore, could be of considerable more value in adjusting nutrient feed
rates if a relationship between BOD,, and COD is established. In addition,
there are automatic COD analyzers on the market that can give COD analyses
in a matter of minutes.
Therefore, a correlation between influent BODj. and COD was sought.
The relationship developed is shown in Figure ^.
ACTIVATED SLUDGE PERFORMANCE
Waste loads to the activated sludge process varied widely from day
to day and hour to hour on a daily basis. Variance on a daily basis was from
*»0 to over 7,000 pounds of BOD . The response of the system to such variations
in load has generally been good. Effluent BOD was normally measured only on
Tuesday's and Thursday's so removal percentages were available twice per
week on this basis. However, COD values were determined daily on composite
samples. Average BOD removals shown on Table 2 were well in excess of
90 percent. In an assessment of all the data, only five or six values were
less than this level.
During several stages of the study, varying quantities of the flow to
Aeration Basin No. 3 have passed through the Equalization Basin. As expected,
such equalization had no apparent effect in treatment performance.
The response of the activated sludge system to large shock loads was
demonstrated on two occasions. Early in March, a BOD,, load of 3,000 pounds
369
-------
5-
•<
UJ 0£
O LU
>- O.
X
O CO
o
_l Z
•< 3
O O
— O-
a: o
O
O 00
— Q
CO LU
COD And Corresponding BOD5
Treatment Line No 3 Influent
1 O
1 5
1 ">
q
fi
1
n
t
)
•^
5^
5L
^
O
<£,
1
TV.
&
fe
<7
<
c
rf
n
TI
^
3
,/
>
•«
Tl
!>
P|
fl
0
(J
^
"SJ
X
1
B
a
<
'•!"
S
3
q
.t
J
fe'
9
(j
U)
^4
|T)
Pf
;;
"
(
\
1
f)
f!)
\
I
I
$
c
4
a
r
)
a
J&
p
>
n
^
A
ft
.d
9
(
(!)
ffi
la)
t
1
u
4
I
^
/
T
2
C
f*l
gf
'<
fil
fj
12
^
d
ft
^
^
(i
i>
S
i
j''
5
S
0
/*
/
®
p
9
V
/
<
'
*}<•
s
y
w
8
^/
.<
^
,x|
9
i
^i
1
i1
2
>^
<;
s
ffl
c,
u3
/I
•>
ff)
^
2
CHEMICAL OXYGEN DEMAND, HUNDREDS OF POUNDS PER DAY
370
Figure 4
-------
in o
rf\ •—
— VO
r~
-3- in _
— O CM •— — in
vO — -a- CM
en
oo
vO O fl
on o on
CM 01 m
CM in
CM \O
CM CM
CM in OO — -3" —
•— CM •— CM -3" CT\
VO
O1
oo o on
-3- oo o
CM CM l-»
o ir\
VO CM
en on — un in CM
CM CM •— -3- CO
vD
on
c»> o vo
o -a- co
-a- vo on
o
on
o CM
co on
vO On
in o vo
•S' oo —
-a- tn on
in o O
on c on
CM on co r-
•— CM •— on
— O -3-
CM O Q
— OO O
LA O -3"
• -3- —
CM OO •*
ir\
i*» on o
CM -3"
\0 l*« O
CM o vo m
in — on
in o r-.
IA on -a-
m en r-s
in o vo
*- \o oo
CN — -3-
CM O CO fr\ *— vO
-3- CM ...
m m -3- r-»
co — on
I- ml
CM O
00 O —
in o CM
m t*\ o
o o r~
oo — oo
t** r~~ CM on co ^r vo
CM ro m ...
r~- -a- o vo
•3" ro on
in o on
CM CM 4-
-a- ro on
— o oo
— O —
-a- o o
co oo CM o o vo r—
— o m ...
— — co co ro
CM — m on
ce <
O f>
oe
ui
o.
S
en
on
o o m
on CM m
CM vo -3-
— o oo
•— o on
M — r»
-3- cn r~
— mm
•a- oo vo
-3- 06 ff\ o h-. on
CM — ...
oo r^ on r-»
CM ~ on
o — •— CM o vo oo
CM CM CM ... .
on o on CM
CM ft CM on
mom on o —
Soo r-- o en —
o r- m — on
o on *—
r- oo -3-
-3- in
8.
ID
I f1
o
co
i1
O
4-1
to
X
ID
o in co
— oo <">
on CM
NO
en
ID
i .? §»
o
CO
^ I 6
u- o
in
CM
^~
in
ro
|
O
—1
X
re
•o
•^
j*
4-(
j:
O)
1
o on
OO CM
CO -3-
CO P-
r~. ej
vO CM
£
ID
j: i.
o> a)
•- >
x <
—
vO
on
on
m
en
n
<
>
§
UJ
ce
in
a
UJ
o
s
UJ
>
<
B
I
4J
O
• ID
4)
- J=
t.W
<5 2
VI
VI
5."
I/I 0)
O VI
E c
8 —
u
i. in
O 0
jr i
1 O
-3- ~
CM m
-K
* *
371
-------
entered Aeration Basin No. 3. On that day, no BOD sample was taken. COD
of the waste was reduced nearly 95 percent from 2,730 to 1^9 mg/1 . BOD,.
samples taken the following day indicated reduction from 935 to 108 mg/1.
This is 88 percent removal. Only 30 mg/1 of effluent BODr was soluble. In
mid-July, Aeration Basin No. 3 received a load of approximately 7,000 pounds
of BOD_ on one day. BOD_ determinations were not made on that day, but
COD was reduced 99 percent from 9,635 to 129 mg/1. The following day when
BOD^ tests were made, reduction was 97 percent from 1,650 to 65 mg/1. On
the basis of these and other experiences with less severe shock loading,
it is concluded that the activated sludge process as designed has the
ability to withstand such peak loadings without upset and still provide
removal for large quantities of BODj.
One of the major concerns of the research project was to determine
the range MLSS concentrations which resulted in optimum BOD,, removal. It
is concluded from the present data that good removals can be obtained at
any level of MLSS between 2,*»00 to *»,500 mg/1.
A related operating factor studied was the F/M ratio expressed as
pounds of influent BODj. per pound of MLVSS under aeration. Although
there is a lack of data at the higher F/M values, removals rate appear
generally satisfactory at all levels from 0.01 to 0.65.
Dissolved oxygen levels in Aeration Basin No. 3 often drop to
essentially zero. This would naturally be expected on those days with
high loadings. However, it is quite possible that some o'F this problem
may be associated with aerator performance and that actual alpha and beta
factors are lower than that used for design purposes. Nevertheless, such
oxygen deficiencies did not appear to seriously lower removal efficiencies.
Sludge settl eabi 1 ity and drainability have not been good. The sludge-
volume index has frequently exceeded 200 ml/g. Since many of the F/M
ratios were low, this could account for a part of this problem. Most
polyelectrolytes and metal coagulants tested to date have not been effective
in providing clarification of the effluent. However, further work is
proceeding along these lines with some promise being shown.
372
-------
BIO-DISC PERFORMANCE
Early in Stage 1, it became apparent that the Bio Disc would not be
able to treat its design flow of 120,000 gpd without some modifications
of the treatment process. Data on performance are shown on Table 3.
It was believed that two factors were the prime cause of poor performance.
The first was the wide fluctuation in raw waste temperature and pH. These
variations were not being adequately minimized by the Equalization Basin.
The second factor was that the flow rate was apparently higher than Bio Disc
capacity. It was determined that the answer to both of these problems
was to reduce the volume of flow through the Equalization Basin to the Bio
Disc. In Stages 3 to 6, all flow to the Bio Disc was routed through the
Equalization Basin. Detention time was approximately doubled. This improved
temperature and pH control, but led to septic conditions in the Equalization
Basin. The septic condition of the waste flowing to the Bio Disc was believed
to be reducing normal biological activity. By Stage 7, an aeration system
had been introduced for the Equalization Basin. After several days, the
septic conditions were eliminated. However, little or no dissolved oxygen
was present in the Equalization Basin discharge. Successive attempts in
later stages to increase Bio Disc hydraulic loading resulted in poor
removal performance. This indicates that the Bio Disc capacity is quite
sensitive to hydraulic loading.
CONCLUSIONS
Based on the studies made, the following conclusions are reached:
1. Flow and strength of waste from a distillery can vary quite
widely. For satisfactory characterization, a well-planned gaging
and sampling program is required.
2. Design philosophy must recognize the variable nature of the waste
by providing waste equalization capacity. This requirement can
be met by separate equalization tanks or by added detention
periods in such plant components as aeration basins. The Bio
Disc or any plug-flow or short detention process will require
separate equalization facilities.
373
-------
o
in
VH
O
1
o
m
i
g
<
c^
UJ
o
2:
^£
z
ce
o
li-
ce
UJ
0.
—
o
cn
oo
i-.
NO
cn
CM
CO
-3-
CM
00
O
-3-
0
cn
NO
^
CM
. —
in
in
oo
in
OO
in
in
-3-
in
CM
-3-
<
cn
O
NO
m
o
cn
CM
CM
un
o
^
m
NO
^—
^—
0
o
CO
•«
—
0
CM
ro
•
CM
O
CO
CM
»
~—
O
CM
NO
O
OO
o
o
p^.
-3-
•
' —
-C
cn
:n
cn
m
cn
o
r^.
NO
cn
CM
cn
f-
""~
-3-
0
O
— *
^
-3-
p^.
,
CM
O
•»
—
cn
^j-
cn
ro
cn
p^.
m
m
-3-
m
p«^
l"~
cn
co
m
-
10
-o
•^
J3
^~
4~t
r~
cn
• _>
*
-3" CM
-3- -3-
r*** PO
LT\ O
LA CM
r--. PO
LA —
O""\ OO
LA OO
*
~~
o —
-3- O
— CM
K f.
NO —
O OO
CM r^
I^- CO
in -3-
cr\ cn
NO CM
o r^
co tn
in ro
o oo
in cn
O CO
~
^_
NO r-~
m o->
-=r CM
i — co
-3- NO
CO CM
CO f-^
in CM
NO -3"
o cn
NO OO
-3- CM
•>
1 —
01
ID
l_
>
<
NO
-3-
OO
cn
CO
CO
CM
CO
CO
_
_
f^
co
-3-
NO
CM
CO
V—
r—
-3-
co
CM
i —
O
_l
>v
ID
~-«
-0
4J
t~
cn
•_
^
co
COi
0
in
r-^
"
~~
in,
-a-'
0
r~^
in
cn,
LA
O
p^
p-
. —
CO
. —
P^
NO
• —
-3-
NO
LA
OO
C^i
r~
O)
•X-
co
m
-3-
O
oo
^
NO
oo
CM
in
_.j_
cn
CM
NO
oo
o
-3-
r—
O
CM
NO
_
<
CO
-3"
O
o
-3-
+-
O
V
.
cn
-3-
o
.
NO
r--
CO
,
r—
m
CM
r-.
LO
in
o
p^
.
m
m
o
.
o
-3-
m
.
CO
+-
o
V
1
1
*e
r.
m
0
0
m
»
LU
(-
<
^
—i
>
O
LU
ce
-3"
co
CO
.
fv^
cn
-3"
CM
NO
NO
,
in
CO
NO
cn
^
.
-3-
cn
p-~
,_
oo
m
p^
co
CO
.
-3-
cn
o
0
-3-
00
oo
NO
CM
cn
-C
cn
I
r~
CO
-3"
co
CO
1
CO
0
co
NO
, —
cn
.
NO
OO
co
J-
ps.
p-~
.
CM
00
J-
m
o
•
o
-3-
, —
.
m
, —
.
o
r^
<
4-t
C
-------
3. The activated sludge process is an effective means of reducing
BOD of distillery waste to a low level. Normally removals in
excess of 90 percent can be accomplished. Wide fluctuations in
temperature, pH, and loading do not affect performance.
k. Some further study of aeration equipment application is desirable
for this facility to maximize performance.
5. Additional work is required toward production of a better settling
and more drainable sludge. Recent use of polyelectrolytes has
shown some promise.
6. Bio Disc performance is not as satisfactory as that anticipated.
This is undoubtedly due to wide variation in waste characteristics.
Pre-settling and long equalization periods may prove advantageous.
It should be emphasized that smaller space requirements, lower
power consumption, and other similar advantages of the Bio Disc
indicate that this process with adequate pre-treatment modifi-
cations may still hold promise for economical treatment.
375
-------
LOADING CHARACTERISTICS AFFECTING THE PERFORMANCE
OF A
LABORATORY DAIRY WASTE WAT3R TREATMENT SYSTEM
by
Dr. James V. Chambers*, and Dr. W. James Harper**
INTRODUCTION
As a result of much early work with dilute skimmilk as the
model of dairy waste water, most people have come to accept
milk wastes as "completely compatible with municipal wastes"
and "easy to treat by biological means". These views have
held in spite of continuous problems encountered over the
years by dairy plants which operated their own treatment
facilities. Two factors that were ignored in much of the
early work on dairy wastes was the effect of loading of or-
ganic solids above 1000 ppm BOD and the presence of materials
other than skimmilk in the waste water which might affect the
performance of the biological treatment system. Harder,
et al.(H) reported dairy food nlant waste waters with BODt
strengths in excess of 3000 prim as being rather common. They
also found surfactants in these waste waters at concentrations
that would be expected to affect the oxygen diffusion charac-
istics of the treatment system and which might change the
microbiological character of the waste water arid subsequent
performance of biological treatment systems.
* showed that the microflora in the activated
sludge system of dairy waste water treatment was slow to adapt
to this waste and that the composition of the waste water could
affect the types of microflora which developed. He also showed
that the different microflora differed in their metabolic char-
acteristics which would be expected to affect BOD and COD re-
duction.
The purpose of this investigation was to investigate the effect
of relatively high BOD loading and the presence of various sur-
factants, at concentrations reported in dairy waste waters on
the microflora, performance and some selected characteristics
of a laboratory dairy waste treatment system.
*Der>artment of Animal and Food Sciences, University of
Wisconsin, River Falls, Wisconsin.
**Department of Food Science and Nutrition, The Ohio State
University, Columbus, Ohio.
376
-------
PBOCSDURES
The Dairy Activated Sludge Laboratory Model
A single stage, closed continuous extended aerated homogeneous-
spatial system was used for this study (Figure 1). The system
was adapted to a commercial fermentor assembly (Fermentation
Design,'incorporated, Bench Model SA5F1), which possessed con-
trols for agitation, temperature, and air flow rate and pres-
sure. In addition to the fermentor assembly, pH and dissolved
oxygen probes and recorders were utilized for continuous moni-
toring of these parameters during the operation of the system.
Activated sludge was obtained from a dairy waste water treat-
ment operation located in New Bremen, Ohio; immediately frozen
in dry ice; freeze dried in a Virtis 10-145 MR Freeze-Dry
Mobile unit at a vacuum of 20-50 microns and a temperature of
-50 to -?0°C until used. A 1.0 g aliquot of the freeze dried
sludge was used to inoculate the substrate. Approximately 8
hours were required under the defined growth conditions before
growth was initiated.
Commercially pasteurized skimmilk obtained from The Ohio State
University Dairy Plant served as the primary source of the
model waste water effluent. The skimmilk was diluted with
distilled water to yield the desired total solids, heat treat-
ed at 121°C for 7 minutes and immediately cooled to room tem-
perature prior to introduction into the treatment system.
The following operating conditions were maintained for all ex-
periments :
Agitation - 160 rpm
Temperature - 23 + IOQ
Air Flow Rate - 2.0 to 4.0 I/minute
Air Pressure - 6.0 to 11.0 p.s.l.
Substrate and Effluent Flow Rate - 79.8 ml/hour
Dilution Factor - 0.053 (equivalent to 18.8 hours of
retention in the system)
Return Sludge - 9 times the substrate flow rate/hour
Fixed Volume in Aeration Tank - 1500 ml.
Material from the sedimentation vessel was collected con-
tinuously in a flask, held at 3-4°C. The pooled material was
centrifuged at 9000 x G for 20 minutes. The resulting super-
natant served as the effluent to be tested, and the sedlmented
pellet represented the biomass.
377
-------
1
UJ
u
l
CD '
c
0
0)
s
0)
+3
V.
>>
K
*>
c
0)
3
.p
OS
o >»
^ ^
•P -H
as co
B TJ
0)
£ ^
o o
CO
-------
The biomass pellet was washed twice with distilled water,
with centrifugation between washing?. The washed pellets
were stored at -20°C until further use of these cells was
required.
A 10 ml aliquot of the reaction vessel mixture (mixed liquor)
was obtained from the outlet leading to the settling vessel.
This was performed only during the establishment of "steady-
state" conditions.
Analytical Procedures
The analysis for Biological Oxygen Demand (BOD), Chemical
Oxidation Demand (COD), total, volatile, and fixed suspended
solids, and the Sludge Volume Index were carried out accord-
ing to the procedure outlined in Standard Methods for "the
Examination of Water and Waste Water, 13th Edition, 19?1(20'.
Dry weight determinations were carried out according to the
procedure outlined in Manual of Microbiological Methods(o).
The Lowry procedure'^5) was used for determining protein con-
centrations of the cellular extract^
Microscopic film slide examinations were made from the out-
going effluent still in the settling vessel prior to collec-
tion, settling and centrifugation. A gram stain was perform-
ed on the film smear and examined for general shifts in micro-
flora based on morphological characteristics. This was per-
formed routinely throughout the course of the investigation.
Pipes(18) Atlas for Activated Sludge Systems was used as a
reference.
To disaggregate the cells from adsorbed protein and other
material 2.0 g of the biomass was suspended in a 20 ml 0.1 M
ohosphate buffer at pH 7.4. This suspension was allowed to
stand at ambient temperature for 30 minutes.. An addition of
0.4 ml of 2N NaOH adjusted the solution pH to 10.5. The cells
were centrifuged out at 4000 x G for 20 minutes. The super-
natant was discarded. The cells were resuspended in 10 ml of
a 0.1M phosphate buffer pH 7.0. Determination of cell mass
weight as a percent of total biomass was determined.
Through consultation, the following mathematical relationships
were used to derive experimental K^a oxygen capture and total
and endogenous respiration rates. T?he values for the follow-
ing equations were obtained from the D.O. record (Figure 2).
The mathematical relationships were:
For K^a with cells:
Assumption: Oxygen transfer rate is influenced by "C".
slope "A"
KLa = (dc/dt)o '
("C» - C0)
379
-------
rH
O
JD
Ol
JC
(O
<5
s
CD
C.
O
cr/
c:
o
(O
Ol
Q
o
en
c
M-
C
O
•f—
4->
fO
J-
3
-)->
(O
I/)
•fj
(O
c
o
•r~
4->
C
$
•o
c:
o
•f"p
4->
(O
i_
4-»
C
• 4->
O
rc
t_
4->
C
0)
u
c
o
u
•
o
.
ca
•o
0)
Jt
l/>
r~-
^t
ns
+J
tn
li
_
O
t—
•r^
C
•r-
A
O
•F—
4->
0)
0
o
u
•
o
B
Q
c
(U
Ol
c
(O
.C
o
II
u
01
4->
C
QJ
C
•^
4-»
C
Ol
CD
c
(O
t-
o
II
*
4-*
<
UJ
380
-------
For KTa without cells:
LI
Assumption: (Cs - "C") is plotted on semi-log
•oaner and slope passes through 1.0
log cycle.
K a = 2.3/^t Note -«&t is from slotted graph or C2
k computed slope.
HESULTS
Effect of 30D Loading;
A skimmilk-water mixture as the substrate to yield organic
load levels of 1000, 2000, and 3000 mg/1 BOD^ was used to
determine the effect of organic load on the characteristics
and performance of the treatment system. Each experimental
condition under evaluation was allowed to achieve ooerational
equilibrium and "steady-state" prior to initiation of the ex-
periment. Primary indicators of "steady-state" were the sub-
strate flow rate, pH level, dissolved oxygen concentration,
and the mixed liquor biomass dry weight. Following achieve-
ment of "steady-state" the system was operated for 3-^ days
with daily renewal of the BOD loading substrate. All exoeri-
rnents were run sequentially, with no shut down of .the fer-
mentation system.
Determinations were made to determine the effect of BOD load-
ing on microflora and selected performance characteristics.
Microflora
The microflora were identified by gram stain and moroho-
logical characteristics. No attempt was made to classify the
microflora biochemically. Table 1 summarizes the microfloral
Doxmlation shifts at the respective BOD load conditions indi-
cated and are expressed in percentage of the stained morpho-
logy of the microorganisms. Shifts occurred in the gram posi-
tive rod and gram negative rod populations with changing load
levels and these changes were apparent within 24 hours after
changing the BOD load. As the BOD load increased from 1000
ppm to 3000 ppm the gram positive rods increased from 11.9$ to
48.1$ and the gram negative rods decreased from 86.8$ to
50.7$ of the biomass microfloral population.
Performance Characteristics
Performance data for the sludge system at the three BOD
level? are presented in Table 2. As the BOD load level in-
creased, the biomass concentration also increased, with the
greatept increase occuring between 2000 and 3000 ppm BOD in
the waste water. At the same time the cell mass,-as percent
of the biomass, did not change consistently with an increase
in BOD load, although the percentage of cell mass was higher
at both 2000 and 3000 ppm BOD loading than at 1000 ppm BOD
loading.
381
-------
Table 1. Microfloral Population Distribution in the
Biomass for Different 30D Loading Levels.
(expressed as percentage of total)
Field BOD Loading, mg/1
Distribution 1000 2000 3000
Gran Fos. Rods:
Pleomorphic type 11.9 10.6 48.1
Gram Neg. Kods:
Single type 72.0 82.9 46.1
Diploid type 14.8 5.6 4.6
Yeast -0- 0.2 0.5
Filamentous Forms:
Bacteria 1.3
Fungus 0.1
382
-------
U-l
o
CO
0
•H
It
10
•H •
h X
,
f)
•o
(0 C
0)
0) 6
0 4J
C fO
i i
& -p
o
MH 0)
0) 'G
ex a
•H
c w
o
bO CJ
C P
•H m
•d ^>
O "-P
H O
to
Q
o >>
CQ M
O
\^J If
O <0
(-4
P O
O ,Q
i^ H
<{-(
i-4 n3
•
CM
0)
H
•a
H
co
rH
V
9>
Cii
d
T>
(0
O
H
^
0
fp
tiO
c
•H
*j
b
H
^
O
k
O
M-i
*O
0)
c
•H
m
4-j
r- 1
o
01
^3
H
rti
e
0,
(X
o
o
o
co
e
a,
o
0
0
CN
e
04
O
o
o
rH
C
0
'S
c
•H
*
a
0)
2
a>
to
9>
bo
C
fO
r.
CO CO CN CM 1 • co iDiDenotu*)
^ • • • • t • •
m r> o rHoHocNd-
to CN H t^ in
CD H |
0 0 & & •***
co co o cnoHoaoo
CO CN CO 00
o
in
o o CM t*- o
O CM (D CM t^ rH • H
CD • • •••O •
CO CO O CO CN rH 1 CO
d" CN 1 1 CO
III II
II C~ 1
O O CO CO .3-
o CM if) coojoo r*
I/) • • • • • • •
CO CO O J-CTtrHO P-
co H r>-
.
if} H
O -3" 3r CM UD ^^
co co ^ co ^o ^ O o m
o> • • ••••••
H CN O OOlrHoCOCT)
CM H CD CO
f^
o c^ ID in :_o
CO IjD d1 J" O * O
rH • • » « • •
CM CM O rH O rH O
CN CM H
III 1 1 1 0
1 1 1
O rH CO f- CN 1 1
C- (D d- (O CN CO ID
co • • * • • o m
H CM O aiOOrHO* 00
H H
to
W <">•
to
O ^t £4 *"***
'H O J3 C3
>> 1 ^ A -^ >>
(0 £ *H ^*s <^p ft) n3
JiQ ^>j O ^»* *O CiO (0 4-* rH rH
ergo «J-H «> (0(0
•HTJOC >(B MM C &3 > >
'O "^^ O O ^ Wo) O ^ O O
rB SO o) *H R n3 fl *«H 0 E
in ePi "^ZJ'1^ a>i3
O -H O 0)
-------
The sludge age and "BOD removed oer g biomass (dry vrt.)" values
observed are within the normal operational parameters exoected
for this type of system. The "BOD removed oer g biomasp" in-
dicates the daily rate at which the substrate (30D) is being
removed from the waste water. At the 1000 BOD load level, the
daily BOD removal rate was observed to be at 0.4^- which in-
creased to 0.60 as the BOD load level was increased to 2000
mg/1. In contrast, the 3000 BOD level exhibited a 50^ de-
crease in the BOD removal rate as compared to the 2000 mg/1
level. KLa decreased from 0.065 at 1000 mg/1 EOD loading to
0.0^-6 at 3000 mg/1 loading. The efficiency of BOD reduction
decreased from 9Q% at 1000 opm. BOD to about ?3$ at 3000 opm
BOD in the raw waste water and COD decreased from 89 to 62%.
The percentage cell mass of the biomass was shown to increase
two fold as the BOD load level was increased from 1000 to
2000 mg/1. As the BOD load was further increased to 3000
mg/1, the percentage cell mass of the biomass decreased by
GOD was determined on the substrate and waste water effluent
from the model waste treatment system to reflect the total
oxidizable organic material present. The COD removal effi-
ciencies were then ascertained from these data to indicate
the removal rate of the biodegradable organic material. The
COD removal rates under the three different BOD loading level:
are presented in Table 3- ?°r the BOD load levels investigat-
ed the COD removal efficiencies decreased as the loading con-
centrations increased. As the BOD loading concentration was
increased to 2000 mg/1 and 3000 mg/1 BOD the average decrease
in removal efficiency decreased by 10# and 30^, respectively.
The "ing COD removed/g cell, min" data shows the highest re-
moval rate at the 1000 BOD load level with a decreasing COD
removal rate observed as the BOD load levels were increased
to 2000 and 3000. The "nig COD removed per g biomass" rate?;
did not reflect the same basic trend as the "mg COD removed
per g cell, min". The correlation coefficient for the three
BOD load levels as compared with the "mg COD renaoved/g cell
mass, min" was a correlation of 0.9989.
Effect of Surfactants
After acclimating the treatment system to a 3000 t>arts/
million BOD loading level, experiments were initiated using
various surfactants. These included an anionic detergent,
alkylaryl sulfonate (AAS); a nonionic detergent, nonyl-
phenoxypoly (ethyleneoxy) ethanol (NPPS); and a caticnic
detergent, alkyldimethyl benzyl ammonium chloride (3AC).
These were used in concentrations ranging from 13 to 52
mg/1 which was within the range reported in dairy food plant
waste waters.
In initial experiments the anionic detergent (AAS) was used
first at a level of 13 mg/1 and subsequently at 52 mg/1.
Subsequently, the system was restored in the absence of any
384
-------
3
•H
1
•H
Ai
n) to
b fc
O O
H | i| |
10 O
> -M
O 81
e >>
« 00
•H
(3 C«
O (U
o 3
^J
m n)
0 g
4) H
•P
T3
S3
c~(
W
to
C *w
•H Q)
-o <->
(|^ H
o o
4J n)
4) O
S3
*
CO
0>
H
H
to
p"l
o
^J
§
2
n>
to
•H
O
H
H
0
(M
^
*
01
0)
3
H
fO
J>
CJ
2
0)
<
bO
"O C
2(0
CO
o
r^
t>o o>
{3 U
bo
^c
0) **H
^ te
n
0) V)
(ft
O c
O 0
a -H
A
s
H
•N.
a y
cj o
££
(iQ dj
e S
0)
S H
•N.
H bO
'H
Q 9>
O ?•
S
in
U) O
f3 ^?
•H H 05
1 >e
O Q) Oj
hj 1*4 C^4
in at
CO to «-i
CM H H
0) * CN
j- to co
o o o
to en
en o en
H CO CO
in f-
in CM H
O H CM
OT H CM
CO CO tO
000
000
000
H CM CO
385
-------
surfactant before going on to the next exoerinent. The or-
ganic load from the skimmilk was maintained at a 30D level of
3000 mg/1.
The percentage population for the control before and after
and the two levels of AAS are shown in Table 4. Shifts vrere
observed for the gram positive uleomorohic rods from 43 to
9l/£ as the concentration of AAS was increased to 52 mg/1 with
a total loss of gram negative rods at the 52 mg/1 level of AAS.
On removal of the AAS the recovery of the microflora was slow
and incomplete. The data in Table 4 for the controlled re-
stored system, at 3000 mg/1 BOD, was obtained after two weeks
with no AAS in the system. There was a very plight recovery
of gram negative rods, a decrease in the gram oositive pleo-
morphic types but a marked subsequent increase in the yeast.
At this point an attempt was made to reinoculate the system
with the freeze dried sludge used initially. For about three
days after addition the performance of the system showed mark-
ed improvement but the microflora was unable to sustain itself
and returned eventually to the population indicated in Table 4
for the restored control. Performance and COD rate removal
data are shown in Table 5 as averages of the three days
analyses. The biomass concentration increased from about 8
to 25 grams/liter with the addition of 13 mg/liter of AA" and
to about 38 grams/liter in the presence of 52 mg/liter of AAS.
Elimination of the AAS did not affect the biomass concentra-
tion. The increase in biomass concentration was reflected by
a similar increase in sludge age which also remained unchanged
unon removal of the AAS from the system. The cell mass per-
cent of the total biomass increased from 26.9 to 33•9 and
46.1$ in the presence of 13 and 52 mg/1 of AAS respectively.
In the restored control this is increased further to 53»3/»»
The effect of AAS on KLa was similar to that reported in the
literature. Thirteen mg/liter of AAS had no effect on the
efficiency of BOD or COD removal whereas 52 parts per million
reduced the performance efficiency. Removal of AAS from the
system allowed full recovery in terms of performance as
measured by BOD and COD removal. However, there was a marked
effect on the rate of removal COD/gram of cell mass changing
from a value of 1.2 to 0.34 in the presence of 13 mg/1 and
0.1 in the presence of 52 mg/1. Restoration of the system
by removal of the AAS did not restore the efficiency of COD
removal per unit of cell mass. Overall the results indicate
that the presence of 13 mg/1 of AAS, while having little ef-
fect on the efficiency had a marked effect on some of the
microbiological characteristics of the system and markedly re-
duced the rate of COD removal per gram of cell mass. The
higher concentration of AAS did affect the efficiency and
further reduced the rate of removal per unit cell mass.
These changes could not be reversed by the removal of the
AAS over a two-week period of time.
The next series of experiments were conducted witn a nonionic
detergent (NPPS) at 13, 26, and 39 mg/1. The effect of this
surfactant on the microflora of the system is shown in Table 6.
386
-------
Table 4. Microfloral Population Distribution in the Biomass
for a BOD Loading of 3000 mg/1 in the Presence of
Alkylaryl Sulfonata (expressed as Percentage of Total)
Experimental Conditions
Field
Distribution
Gram Pos . Rods :
Pleomorphic Type
Gram Neg. Rods:
Single Type
Diploid Type
Yeast
Filamentous Forms:
Bacteria
Fungus
Control
Before
48.1
46.1
4.6
0.5
0.5
0.2
13 mg/1
AAS
47.5
31.8
6.9
10.0
1.9
1.9
52 mg/1
AAS
91.8
-0-
-0-
4.9
3.3
-0-
Control
Res tore d/jL
66.4
7.2
-0-
24.4
1.0
1.0
/!_ Data taken 2 weeks after removal of surfactant (AAS) from
the skimmilk
387
-------
Table 5. Effect of Anionic Detergent (AAS) on the Performance
and Rate of Biological Oxidation of Skimmilk (3000 mg/1 BODg)
Average values for the following
Parameter
Biomass concen-
tration g/1
Retention time
(hrs)
Sludge age
Cell mass as %
of biomass
KLa
% BOD removal
% COD removal
Cell mass g/1
mg COD remove d/min
Initial
Control
8.1
20
2.3
26.9
0.046
73.7
62.5
2.1
3.9
13 mg/1 AAS
25.5
20.3
5.4
33.9
0.15
73.1
65.4
12.9
4.6
52 mg/1 AAS
37.6
20
10.3
46.1
0.08
65.1
49.2
26.2
2.9
Restored
Control
37.7
19.6
10.5
53.3
0.06
74.9
67.7
30.4
4.5
mg COD removed/g
biomass, min .32
m£ COD reinoved/g
cell mass, min 1.19
.12
0.34
.11
0.11
.08
0.14
388
-------
Table 6. Bioraass Microfloral Population Distribution, as
Percentage, for a BOD Loading of 3000 mg/1 in the
Presence of I-ionylphenoxypoly (ethyleneoxy) Ethanol.
Field
Experimental Conditions
Distribution Initial13 mg/126 mg/139 mg/lRestored
Control NPPE NPPE NPPE Control
Gram Pos. Rods:
Pleomorphic
type 66.4
Gram Meg. Rods:
Single type 7.2
Yeast 2H.4
Filamentous
Forms:
Bacteria 1.0
Fungus 1.0
88.7 85.1 81.2 90.1
5.8 8.7 -0- -0-
3.9 5.2 18.8 5.0
1.6 0.7 -0- 4.3
-0- .3 OUTGROWTH 0.6
389
-------
The surfactant affected the initial decrease in yeast and an
increase in the gram positive pleomorr>hic rods. At the
highest concentration (39 rag/1) all gram negative rod? were
eliminated and concentration of yeasts increased at the ex-
pense of the gram positive rods. Elimination of NPPE from
the system was followed by a decrease in the yeasts and an
increase in the gram positive rode and in the filamentous
forms as fungi.
The effect on performance and rate of COD removal is
shown in Table 7. This surfactant had a different effect on
the performance and characteristics of the system. The
efficiency of BOD and COD removal were partly effected even
at 13 mg/1 with very little further effect on increasing the
surfactant concentration. At the same time the rate of COD
removal per unit cell increased with increasing concentra-
tions of ^urfactant. In contrast the percent of cell mass
of the total biomass was markedly decreased by the surfactant,
although the total biomasc concentration showed relatively
little change. Attempts to restore the system were generally
unsuccessful with inability to show recovery of BOD and COD
removal efficiency or influence in rate of COD removal. This
is also in contrast to the K^a which was markedly increased
by the surfactant but returned to normal in the absence of
the ^urfactant in the system.
Because of failure to return the oerformance efficiency system
to anything like normal the results with the cationic deter-
gent are extremely difficult to interpret. This surfactant
increased the filamentous forms of the microorganisms; in-
creased the Kj-a from .06 for normal operation to .76, .38 to
.66 for 13, 26, 39 mg/1 of cationic surfactant (BAG), respec*
tively, though the K^a returned to normal when the BAG ras re-
moved. COD removal was essentially unaffected, remaining
about kr$% for all levels of surfactant but upon removal drown-
ed to JQfa. The mg COD removed/gram of cell .was .57, .75» and
.7^ for 13, 26, and 39 rag/1, resoectively, with a percentage
cell mass of biomaps of 9.8, 7.0, and 8.2 for these levels,
respectively. After removal of BAG the cell mass percent of
biomass was 11$ but the milligram of COD removed per gram was
0.28. Further experiments are needed in this area to more
fully understand the potential effect of the cationic sur-
factant.
DISCUSSION
BOD Load Factors
The biological oxidation process involves several factors
which influence the removal of organic material from waste-
water and effect microbial metabolism.
A laboratory extended aeration activated sludge system was
maintained for the purpose of investigating the bio-oxidation
process. This system demonstrated an initial BOD removal
390
-------
Table 7. Effect of
Rate of a
a Non-Ionic Surfactant (^PPE) on the Performance and
Biological Oxidation of Skimmilk (3000 mg/1 BOD5).
Average values for the following
Parameter
Biomass concentra-
tion in g/1
Foetention time
(hrs.)
Sludge age
Cell mass as %
of biomass
KLa
% BOD removal
% COD removal
Cell mass, g/1
mg COD removed/min
Initial
Control
37.7
19.6
10.5
53.3
0.06
74.9
67.7
30.4
4.5
13 mg/1
34.8
19.9
11.8
39.9
0.36
59.1
45.1
13.8
3.3
26 mg/1
36.6
19.0
10.3
13.8
0.39
55.5
45.0
5.0
2.8
39 mg/1
40.5
19.8
10.7
9.0
0.55
51.0
43.9
3.7
2.9
Restored
Control
29.0
20
6.6
12.3
0.06
50.0
43.6
3.6
2.4
mg COD removed/g
biomass, min 0.08 0.06 0.05 0.05
mg COD removed/g
cell, min. 0.14 0.16 0.38 0.54
0.06
0.46
391
-------
efficiency at 89.5fj for the 1000 mg/1 BOD loading phase of
this study. This BOD removal efficiency is in agreement
with reoorted literature values for this tyoe system. As the
BOD loading was increased, the BOD removal efficiency decreas-
ed to a low of 65.1$ for the 52 mg/1 AA5 trial.
A performance factor which is closely associated with BOD re-
moval efficiency is that of sludge age. Sludge age is defined
as follows:
Volume of Aeration tank x Biomass dry weight
Sludge Age = TdXl
Daily Flow Rate x COD removed - (dt'T
During the course of the experimentation, the sludge age in-
creased to approximately 10 days old. The most efficient BOD
removal occurred with a sludge age of less than 2 days for
this type activated sludge system.
Another performance factor which indicates the activated
sludge's BOD removal capacity is the system's retention time.
Usually the BOD removal capacity correlates with the reten-
tion time and provides a convenient check on the system's r>er-
formance, assuming all other performance factors are within
the normal operational parameters. This correlation (r = 0.15
to 0.30) did not exist for this activated sludge system. TWO
oossible reasons for this lack of correlation would be the
continually shifting microfloral population distribution and
changing cellular growth rates.
Another performance parameter of significance was the daily
BOD removal rate per biomass (dry wt.) which is defined as
BOD removed, mg/biomass dry weight, g. At the start of this
study, the BOD removal rate was 0.45 which increased to 0.60
for the 2000 mg/1 BOD loading level, and then declined to an
average rate of 0.335 for the 3000 mg/1 BOD-load.
The most critical factor of any waste treatment system is the
microflora distribution of the activated sludge. The type of
microflora present effects the removal rate of the wastewater
substrate and stabilization of the final effluent.
It was observed that the gram negative bacteria were the pre-
dominating microflora throughout the course of the three BOD
load levels. However, as the BOD load level was increased
from 1000 to 2000 mg/1, a shift downward in the gram negative
bacteria and an increase in the gram oositive pleomorohic
bacteria was noted. This trend continued as the BOD load
level was increased to 3000 mg/1. Correlated with these
shifts were decreasing BOD and COD removal capabilities of
the waste treatment system which could be attributed to the
decline of the gram negative bacteria in the activated sludge
system. Adaiase^l) suggested one possible explanation for the
loss of the gram negative rods. He suggested that the in-
ability of the gram negative rods to store polysaccharid.es
392
-------
places these tyoe "bacteria at a disadvantage.
organisms that can store nolysaccharides can then use this
material for a source of cellular energy when all the exogen-
ous substrate (i.e. lactore) has "been removed from the system.
The second possible explanation would be catabolite repression
stimulated by high concentrations of glucose or galactose
(4) derived from the lactose.
"3xr>erlmental evidence also showed a decrease in the COD ^e-
moval capability and a shift in the grain positive nleomorphic
rod population as the BOD load levels were increased to 2000
and 3000 mg/1 levels. These type bacteria appeared to be
less effective in the removal of COD. Additionally, increased
bioinass weights and percentages of biomass cells were observ-
ed without improved BOD or COD removal rates. Possibly, the
presence of high carbohydrate and protein concentrations have
disturbed the substrate transport mechanisms along with a
suppression of the mass transfer coefficient.
The Surfactant Factors
The early work of Hoover, Forge-?, and their associates
on diluted skimmilk laid the foundation of our current under-
standing of the fundamentals of biological oxidation of dairy
food t)lant wastes. This investigation is aimed to extend the
findings of these and other earlier investigators with par-
ticular attention to the effect of higher 30D^ levels and the
contribution of selected surfactants found in dairy food plant
waste waters on biological oxidation.
The effect of BOD load on activated sludge systems has been
given much consideration, but little attention has been given
to dairy wastes in excess of 2000 oom EOD^. Increasing BOD
loading In activated sludge treatment systems ha<= long been
recognized to affect sludge characteristics and the perform-
ance of the system. However, the effect of high BOD loading
on substrate removal rate has been considered to be minimal
for dairy food plant wastes. Kornegay and Andrews(1^) reported
that substrate removal rate at>o^oached a constant value as sub-
strate loading level increased.
Before discussing the details of the specific findings in this
investigation, attention should be directed to two innovations
that apoear to have merit in laboratory waste treatment stud-
ies: the use of freeze dried dairy activated sludge as a
"^•tarter" and the development of a method to separate cells
from aggregated debris in the biomass.
The use of freeze dried sludge from a well operating activated
sludge system to establish a normal microflora for a dairy acti
vated sludge system worked well, and this concent has potential
value in dairy waste treatment. Although the concept to use
the freeze dried sludge as a "starter" to re-establish the nor-
mal desired mixed flora to an ut>set system did not work under
the conditions of the^e experiments, limited field work has
suggested that the addition of "starters" to commercial
393
-------
activated sludge treatment systems improved performance and
its efficiency which makes this approach worthy of further in-
vestigation.
For biochemical studies on the cells of the activated sludge
system, the results of which are to be reported in a sub-
sequent paper, it was necessary to develoo a orocedure to
separate the microbial cells from the associated colloids and
debris in the biomass. The nethod reported in this pat>er also
o^ovided a means of determining the proportion of the total
biomass that was composed of microbial cells. Microscooic ex-
amination revealed almost complete separation of cells and non-
cellular matter. This provided a means for following changes
in the microbial cell biomaes ratio and to calculate removal
of substrate both on a total biomass and on a microbial cell
basis. This permits pome estimation of the relative role of
physical-chemical aggregation of eiaulsoids and colloids and
the microbial cell population.
Increasing the BOD loading had an immediate effect on the per-
formance and characteristics of the waste treatment system.
The changes were apparent in the first 2^ hours after a change
in loading and persisted during the three consecutive days of
operation at the same level. The most significant changes
were the loss of gram negative microorganisms in the micro-
flora, the increase in biomass (sludge) concentration, the de-
crease in BOD and COD removal percentages, increase in cell
mass, increase in the percent of cells in the biomass and the
decrease in the rate of COD removal per unit weight of micro-
bial cells. Of less significance were the change in sludge
age, K-ra and rate of COD removal uer unit of biomass. In
terms of overall rate of substrate removal, the values did
approach a maxima as suggested by Kornegay and Andrews(1^-).
Although full interpretation of the findings is difficult, the
loss of performance efficiency as a function of increased BOD
loading would appear to be related primarily to the reduction
of substrate removal efficiency per unit mass of microbial
cells which is a-sociated with the change in the microflora.
The loss of efficiency of the rate of removal of COD per unit
cell mass is a first order reaction in respect to BOD loading
level. This loss, in percentage, is greater than the IOPS of
performance efficiency. This at>r>arent discrepancy can be
accounted for in the increase in percentage of cells in the
biomass at both 2000 and 3000 mg/1 BOD as compared to the
control at 1000 mg/1.
The effect of an increase in the BOD load on the character-
istics and performance of the activated sludge system was
greater between 2000 and 3000 mg/1 BOD, than it was between
1000 and 2000 mg/1. There was a 2-1/2 fold increase in the
biomass concentration and a loss of microbial cells in the
biomass at 3000 mg/1 as compared to the 2000 mg/1 level.
Based on these data, levels of BOD loading above 2000 mg/1
should be avoided in all cases. This can be achieved through
394
-------
"better in-plant control and the installation of engineering
system?? designed to reduce BOD loads (H).
Harrier, et al.' ^' reported data for surfactant concentra-
tion? in dairy food slant waste waters ranging from about
12 to 60 mg/1 and exore^sed concern of the effect of these
materials on dairy food r>lant waste treatment. The data ob-
tained in this investigation confirm this concern and extend
the knowledge of the effect of surfactants on an activated
sludge system beyond that of pevious investlgators(-0»l6,17).
In addition they provide specific information on the role of
surfactants on the biological oxidation of dairy wastes at
high BOD loading levels. Manganelli'16) studied anionic and
nonionic and cationic surfactants at levels between 5 and 100
mg and found that a cationic detergent concentration from 10
to 100 rag tended to suppress.sewage oxidation and oxygen
utilization. Sdwards et al.'-^' gave attention to the effect
of surfactants on the interaction with "oroteins and the tend-
ency to increase foaming characteristics. McClelland'*•?',
studying two different anionio surface active agents, showed
that the surfactents tended to concentrate in air-water and
biomass-water interfaces. The results suggested that the ab-
corbed anionic surfactant interferred with the production and
availability of extra cellular hydrolytic enzymes and act as
a barrier between the substrate molecule and its respective
enzyme site. Kost of the«e worker? have attributed the effects
of surfactive agents primarily on decreasing the efficiency of
aeration and to some effect on the activity of certain bio-
logical units.
Our studies on the anionic surfactant had the expected effect
on the oxygen diffusion rate. The new Information from the
results of this investigation were the effects on the micro-
flora, sludge age, percentage cells in the biomass and the
rate of COD removal per gram of cell. Although the efficiency
as measured by BOD and COD removal were uneffected at the 13
mg/1 level of the anionic surfactant, sludge age was doubled,
the percent of cells biomass increased and the rate of COD re-
moval oer unit of cells was decreased by about 70$. The high-
er level of anionic surfactant did materially reduce the effic-
iency of the system and totally eliminated gram negative or-
ganisms from the treatment system. Thi^ was accompanied by a
five-fold increase in sludge age as compared to the control
and a 90$ reduction in the rate of COD removal per unit of cell
mass. The fact that the percentage of cells in the total bio-
ma --p almost doubled as compared with control provided some off
setting influence on the overall apoarent performance. A sec-
ondary effect of considerable importance was, whereas the over-
all sludge mass increased about five-fold the cell mass in-
creased ten-fold. This suggests that the anionic surfactant
used in the experiments markedly reduced the physical-chemical
aggregation of colloidal material to the biomass.
The results obtained upon the removal of the anionic surfactant
from the system are not easy to explain. The K^a value returned
395
-------
to nearly normal and the percentage of 30D and COD removal
vyere slightly higher than the Initial control,, The rate of
COD removal per unit cells, however, remained about 1/10 that
of control and the cells total biomass Increased to 82$. There
was only a Flight recovery of grain negative organisms in the
system.
The non-ionic detergent, while having a marked effect on BOD
and COD removal efficiency at 13 mg/1 level, had quite & dif-
ferent effect on other characteristics of the treatment system
which we~e also different than those obtained with the anionic
detergent. Increasing levels of the surfactant had basically
no effect on the BOD and COD removal percentages. In contrast
to the anionic surfactant the sludge age was unaffected as
compared to the control, and concentration of the biomass was
not significantly affected by the surfactant. However, there
was a Deduction in the cells present in the biomass, with
about 1/5 as many cells in the system containing 39 mg/1 of
non-ionic detergent as compared to control. The rate of COD
removal per g cells, however, was actually improved by the
presence of the surfactant. These results might be inter-
preted to indicate a tendency for the surfactant to interact
with colloidal and emulsoid material and to further the inter-
action of these materials to the total biomass. This was in
p~oite of a decrease in sludge age, a marked decrease in the
biomasp concentration and an improvement of the rate of COD
removal per unit cells. However, the system performance did
not recover during a two-week period after removal of the sur-
factant. The reasons are not understood at this time.
Subsequent application of cationic surfactant to the system
completed the essential destruction of the system as a viable
waste treatment unit. It appeared that the various surfact-
ants had an additive effect and that the microflora wa? so
altered that recovery was not possible.
There is need for continued investigation^ of the fundament-
als of dairy waste treatment systems for the development of
methods to either eliminate surfactants or to improve the per-
formance of the systems in the presence of surfactants that
would be ^resent in current dairy food plant wastes.
SUMMARY
This investigation showed that high BOD loading (3000 mg/1) •
was unsatisfactory from the standpoint of the utilization of
a laboratory activated sludge system. Increased BOD loading
from 1000 to 3000 mg/1 altered the microflora very rapidly,
reduced the efficiency of BOD, COD removal, and decreased the
rate of COD removal per unit weight of microbial cells. Al-
terations were effected als.o in respect to K^a, t>ercentage of
microbial cells in the sludge and a slight increase in sludge
age.
396
-------
Anionic and non-ionic surfactant concentration found in dairy
food plant wastes did influence the characteristic t>erformance
of the system but not necessarily in the same manner. The an-
ionic detergent resulted in an increase in cells in the bio-
mass, s. decrease in the rate of COD removal r>er unit microbial
cell mass, and a decrease in performance efficiency at high
levels of surfactant. The non-ionic surfactant had a dele-
terious effect on performance at 13 mg/1 but increasing con-
centrations had no further effect on performance efficiency.
However, there was a tendency for a BOD increase in the per-
centage of microbial cells in the biomas^ as non-ionic sur-
factant concentration increased and a co-comitant increase in
the rate of COD removal per unit of weight of cells.
From these experiments it would apoear that anionic detergents
are superior to either non-ionic or cationic since removal of
the surfactant permits recovery of the performance character-
istics of the system and the concentrations required to create
and influence are higher with the anionic than with the other
surfactants.
397
-------
LITERATURE CITED
1. ADAM'vS, A. D. Bacteriological studies on dairy
activated sludge, Meded. Landb Hojesch. Wageningen, 66:
(6)1-79 (196?)
2. ADAMSE, A. D. Pe^xxmse of dairy waste activated sludge to
experimental conditions affecting oH and dissolved oxygen
concentration. Wat. Res., 2:708-713 (1968)
3. AI3A, S., and TODA, K. The effect of surface active agent
on oxygen absorption in bubble aeration. J. Gen. Appl.
Kicrobiol 9:^13 (1963)
4. ANDERSON, R. L. and WOOD, W. A. Carbohydrate Metabolism in
Microorganisms in "Annual Review of Microbiology" ed. by
Clifton, C. S., Raffel, S., and Starr, M. P. Publ. Annual
Reviews, Inc., Palo Alto, Calif. Vol. 23:539.578 (1969)
5. BLAISDSLL, J. L. Personal communication, re: calculations
for laboratory extended aeration dairy activated sludge
system, August 19 and 20 (1972)
6. DSMOSS, R. D., and BARD, R. C. Physiological and biochemical
techniques in "Manual of Microbiological Methods by the
Society of American Bacteriologist". Edited by H. J. Conn,
Publ. McGraw-Hill Book Co., Inc., New York. Chap. 8, p. 172
(1957)
7. ECKENFELDSR, W. W., Jr. Aeration and mass transfer in
Industrial Hater Pollution Control." Publ. by McGraw-Hill,
New York. 62-86;153-1?? (1966)
8. ECK2NP3LDSR, W. W., Jr., and 3ARNHART, E. L. The effect of
organic substances on the transfer of oxygen from air
bubbles in water. A. I. Ch. E. Jour. 7:631 (I9ol)
9. ECKSNFELDBR, VI. U., Jr., and WSSTON, R. P. "Kinetics of
Biological Oxidation." InJBiological Treatment of Sewage
and Industrial V.'astes. Vol. I, ed. by Eckenf elder, W. W.,
Jr., and McCabe, B. J., Reinhold Publishing Corp., New
York. (1956)
10. EDWARDS, G. P., KSSAVULU, V., SMITH, S., AND LULLA, K. B.
Frothing of detergents in the presence of carbohydrates,
fats, and proteins. J. Wat. Poll. Cont. Fed. 33:737-7^7.
(1961)
11. HARPER, W. J. and BLAISDSLL, J. L. Dairy Food Plant Wastes
and Waste Treatment Practices, A "State-of-the-Art" study
for the Water Quality Office of The Environmental Protec-
tion Agency, Wat. Poll. Con. Res. Series 12060 -EGU 03/71.
(1971)
12. HOOVER, S. R., JASEWICZ, L., AND PORGSS, N. Endogenous
respiration and stability of aerated dairy .waste sludge.
Proc. 7th Ind. Waste Conf., Purdue Univ., 541-548. (1952)
398
-------
13. HOOVER, S. R., FORGED, N., AMD JA^SWICZ, L. An ir.terore-
tation of the BOD test In terms of endogenous resoira-
tion of bacteria. Sewage Ind. Wastes 25:(10)1163-1173-
(1953)
14. KORNEGAY, B. H. and ANDREWS, J. F. Kinetics of Fixed-
Film Biological Reactors, J. Wat. Poll. Cont. Fed. 40,
Part 2:P.460-R468. (1968)
15. LOWRY, 0. H., ROSSN3ROUGH, N. J,, FARR, A. L., and
RANDALL, R. J. Protein Measurements with Folin Phenol
Reagent. J. Biol. Chem. 193:265-32?. (195D
16. MANGANELLI, R. Detergents and Sewage Treatment. Sewage
Ind. Wastes 24:1057-1068. (1952)
17. MCCLELLAND, NINA I. The effect of surface active agents
in substrate utilization in an experimental activated
sludge system. The University of Michigan, Ph.D.,
1968 Dissertation, University Microfilms, Inc., Ann
Arbor, Michigan. (1968)
18. PIPES, W. 0. An atlas of activated sludge tynes. F.eoort
on Grant No. WP-00588-04, FWPCA USDI, Civil Sngrng. Dept,
Northwestern University, Evanston, 111. (1968)
19. PORG3S, N., JAS3WICZ, L., and HOOVER, S. R. Biochemical
oxidation of dairy wastes. VII. Purification, oxida-
tion, synthesis and storage. Proc. 10th Ind. Waste
Conf., Purdue Univ. 135-146. (1955)
20. Standard Methods for the Examination of Water and Waste-
water publ. by U.S.P.H.A. (1965)
21. STEWART, M. J. Activated sludge process variations: the
complete spectrum. Water Sew. Works III:(4)153-158s
(5)246-249; (6)295-297. (1964)
399
-------
CHARACTERIZATION AND TREATMENT OF FISH PROCESSING
PLANT EFFLUENTS IN CANADA
by
M.J. Riddle and K. Shikaze"
SECTION I
INTRODUCTION
Canada's position as a major fish processing nation can be judged from the
1970 Fisheries Statistics. During that year, approximately 1.5 million
metric tons of fish (live weight) were landed in Canada with a landed
value in excess of $200 million. Canada exported some 380,000 metric tons
of processed fish with a value of $247.4 million. This makes Canada the
second largest fish exporting country in the world behind Japan.
Table 1 below summarizes the landings in volume and value for 1970 for
both Atlantic and Pacific Regions as well as freshwater fish. It should
be noted that the Atlantic region processes 85% of the fish catch by
volume, however this only represents 65% of the total landed value and
70% of the total marketed value of all fish landed in Canada.
Table 1. Volume and Value of Seawater and Freshwater Fish Caught in Canada
(1970 Annual Statistics Review of Canadian Fisheries)
Landings. Landed Value Marketed Value
(Ibs x 10b) ($ x 105) ($ x 10 )
Atlantic 2375.1 131.6 290.0
Pacific 238.5 60.2 110.0
Sea Fisheries
Total 2613.6 191.9 400.0
Freshwater
Fisheries 120.0 15.6 22.0
Canada Total 2733.6 207.5 422.0
^Respectively Program Engineer and Program Coordinator, Food and
Allied Industries Division, Water Pollution Control Directorate,
Environmental Protection Service, Department of Environment, Ottawa,
Canada.
400
-------
Table 2 below summarizes the volumes and landed value of the 10 major
fish species landed in Canada. It should be noted from table 2 that the
herring catch represents approximately 40% of the total volume landed but
the landed value of herring represents approximately 16% of the total
landed value of the 10 major fish species. In comparison salmon landings
account for approximately 6% of the total volume landed with a landed value
of approximately 25%. During the 1971-72 fishing seasons the herring catch
declined markedly and as a result the use of herring for fish meal
production has been discouraged.
Table 2. Volume and Landed Value of Ten Major Species
(1970 Annual Statistics Review of Canadian Fisheries)
No.
1
2
3
4
5
6
7
8
9
10
Species
Herring
Cod
Small Flatfish
Redfish
Salmon
Haddock
Lobster
Mackerel
Halibut
Turbot
Canada - Total of 10 Major Species
Volume Landed
(Ibs x 10 )
1,064,400
494,836
311,180
243,855
159,490
49,477
36,584
34,613
32,981
26,097
2,733,600
Landed Value
($ x 10-*)
13,539
23,180
15,486
8,056
48,030
5,296
29,661
1,253
12,179
1,092
207,500
In 1970 the Canadian fishing industry supported a commercial fleet of
39,350 boats with a value of $267 million. The industry employs some
53,000 fishermen of which 41,700 work in the Atlantic provinces of
Nova Scotia, New Brunswick, Prince Edward Island, Quebec and Newfoundland.
Table 3, below, summarizes the number of fish processing plants and
persons employed in these plants by province for 1969. It should be noted
from this table that, although there are some 450 processing plants in
Canada, the number of persons employed in these plants is approximately
19,000, giving an average of approximately 30 persons per processing plant.
Plant processing capacity ranges in size from 60 million pounds of raw
fish processed per year to approximately 100,000 Ibs. of raw fish processed
a year. The largest plants employ in excess of 300 persons where as the
smallest operations are usually run by a single family.
Across Canada the industry provides necessary employment for a large
number of small communities. These communities, most of which are
scattered along both coastlines are dependent to a significant degree, if
not wholly, on the fishing industry for their livelihood. The industry also
plays a significant role in the lives of both Indian and Eskimo native
peoples both as a source of food and a means of commercial livelihood.
401
-------
Table 3. Number of Fish Processing Plants and Persons Employed in these
Plants by Province
(1969 Dominion Bureau of Statistics, "Fish Products Industry")
Province Number of Fish Number of Persons
Processing Plants Employed
Nova Scotia 136 5,177
New Brunswick 92 3,219
Prince Edward Island 23 597
Quebec 46 1,414
Newfoundland 71 5,104
Ontario § Prairie Provinces 35 923
British Columbia 57 2,725
Canada - Total 460 19,159
Current methods of processing fish require the use of considerable
quantities of water for: cleaning the fish, transporting the waste
material, plant clean-up, and use in deodorizers. The discharge of
this waste water directly into adjacent lakes and rivers solved the
disposal problem of the fish processors for many years. In recent
years the expansion and consolidation of the fish processing industry
and the improvement of the by-product recovery techniques has made it
economical to remove the large solid material from the waste water by
screening. The screenings were processed and the resulting fishmeal
was sold as animal feed, but the remaining waste waters still have
been discharged to receiving waters.
As a result of the discharge of this waste water, and the inefficient
operation of offal screening devices, serious pollution problems have
occurred around fish processing plants. This has been aggravated by
the congregation of a number of plants around harbour areas. These
plants then discharge their waste material into the harbour which is
not subjected to the tidal flushing action required to sufficiently
dilute these waste and thus prevent pollution problems!.
The fishing industry relying on a renewable resource is often affected
by pollution. However, it is difficult for the Canadian fishing
industry to lay the blame at other industrial polluters when it is also
contributing to this pollution. It therefore seems reasonable to
expect the fishing industry to take an exemplary position with respect
to water pollution control. However, one of the major problems has been
the lack of information on waste characteristics and type of treatment
that could be effectively employed. In order to aid the industry in its
fight against water pollution, the Canada Department of the Environment
has undertaken a number of studies to characterize and to determine the
treatability of the effluents from various processing plants. These
402
-------
studies will be discussed in this paper. Firstly, however, it is
necessary to outline the major processing techniques employed in this
industry as well as to review the literature to obtain an indication of
the present level of knowledge in the characterization and treatment
of these wastes.
SECTION II
PROCESS DESCRIPTIONS
The processes which characterize the fish processing industry in Canada
can be divided into the following five major groups:
Groundfish processing
Herring processing
Salmon processing
Shellfish processing
Fishmeal processing
Each group has a unique production process and consequently unique
effluent characteristics. Variations in processing procedures are found
from plant to plant, but the major features of each type of production
are quite consistent and are discussed below.
2.1 GroundfishProcessing:
Cod, halibut, ocean perch (redfish), sole and flounder are the species
of fish referred to as groundfish. With the exception of halibut the
remaining species are processed in somewhat the same manner.
2.1.1 Cod, Redfish, Sole and Flounder:
The fish are either stored whole in the ship or are eviserated prior to
storage, the viscera and blood being washed overboard. At the wharf,
unloading is usually accomplished by pitching the fish into a basket that
has been lowered into the hold. The fish are then weighed, washed and
iced in tote boxes. In some larger plants, mechanized unloading methods
are used to minimize manual handling.
Most groundfish require no pretreatment prior to filleting, but the
scales must be removed from redfish before they can be filleted. The
descaling of redfish is accomplished in a revolving cylindrical screen
which removes the scales by the abrasive action of the fish rubbing
against themselves.
In small plants, the fish are processed by hand. The fillets are cut on
a wooden board next to a sink, washed and immediately iced in boxes for
distribution.
Most plants processing fillets use mechanized equipment. First, the
fish are washed in large wash tanks or by water sprays in large rotating
tumblers. Next the fish pass to filleting machines or hand filleting
403
-------
tables. Filleting machines only operate on certain fish sizes and shapes,
but considerably reduce labor costs and increase yields, over hand-
filleting. The skin is removed from fillet by hand or machine. The
solid wastes from filleting and skinning operations are usually rendered
for pet food or animal meal. Figure 1 outlines a typical groundfish
filleting operation.
The skinned fillets are transported by conveyor belt through a washing
tank and, in some cases, a brining tank. After inspection the fillets
are packed into containers by hand or frozen and then packed. Steaks are
produced from the eviscerated fish by cuts made at right angles to the
backbone. These steaks are marketed frozen or fresh. Fillets are
marketed frozen (fresh or breaded), chilled or fresh.
2.1.2 Halibut:
After being landed on the vessel, the halibut are dressed by removing the
viscera and cutting away the gills. The halibut are then packed in ice
in the hold. Halibut are ordinarily processed in relatively small plants.
The fishermen usually behead the fish before sale to the processor.
If the fish are not processed immediately, they are re-iced in the fish
plant. The majority of halibut are filleted and marketed frozen,
however, some are frozen whole or sold fresh.
Prior to whole freezing, a continuous belt washer sprays the fish. The
fish are frozen with a glaze protection at approximately -20 F.
Halibut are cut in fletches (boneless and skinless pieces produced from
fresh fish). This process divides the halibut into four or more trimmed
meaty protions weighing from 5 to 20 pounds. The fletches are frozen
and either glazed or packaged in moisture proof wrapping. Other forms
of fresh or frozen halibut include packaged fillets, steaks, and
breaded fillets.
2.2 Pelagic and Estuarial:
The most important pelagic and estuarial species are salmon and herring.
2.2.1 Salmon:
The five main species of salmon are spring, sockeye, coho, pink and chum.
The major portion of the catch (approximately 80%) is canned.
Spring, coho, and some sockeye salmon are caught using a trolling technique
whereas the remaining species of salmon are netted. Troll caught salmon
are gutted at sea and subsequently stored in ice. Following unloading
a small portion are usually sold fresh while the balance is frozen and
glazed for sale in this form or as steaks cut from the frozen fish.
Net caught fish are usually taken close to the canneries and are often
held for short periods in the boats without refrigeration. Canning
operations are conducted for the most part employing standard cannery
equipment in a conventional manner. The principal exception is the use
404
-------
PROCESS
WASTES
DISPOSAL
WATER
SUPPLY
<
RAW
PRODUCT
I
RECEIVE
i
DESCALE
i
GRADE
i
ICE
i
WASH
i
FILLET [
i
SKIN
i
TRIMMING 1
i
WASH
i
FREEZE
1
WASH DOWN
I
! RNISHED
PRODUCT
SOLIDS
SOLIDS
SOLIDS, SLIME, WATER
SOLIDS, OFFAL, WATER
SOLIDS, SKINS, WATER
SOLIDS, WATER
WATER
SOLIDS, WATER
RENDERING
TREATMENT
_L
RECEIVING
WATER
FIGURE I. GROUNDFISH FILLETING
405
-------
of the "iron chink". The iron chink performs several functions in one
operation by mechanically removing heads, fins, and viscera. During all
the steps a strong stream of water continuously washes the blood away.
The remaining canning operations are somewhat standard, as shown in
figure 2. The fish are washed, inspected and cut into can-length portions
and the cans are filled mechanically. Finally, the cans are automatically
sealed under vacuum and then retorted.
2.2.2 Herring Processing:
Herring is processed into a number of products, including fish oil, fish
meal, herring fillets, marinated herring, and for the herring roe.
This section describes only the operations which process herring for
human consumption - herring filleting, marinated herring and herring roe.
2.2.2.1 Herring Filleting:
As with the groundfish processing plants herring are trucked to the plant
and stored in holding bins, there being packed in ice. Herring are
delivered to the plant round (head, tails, fins and viscera intact) and,
in the filleting operation, have the heads, tails, fins and viscera
removed by automatic machines. After filleting they are prepared for
consumer marketing.
Wastes from herring filleting originate from the fluming of the round
herring to the splitting machines, and from the water used in the machines
themselves. Offal is removed prior to final discharge of the waste water
for further processing in the fish meal operation.
2.2.2.2 Marinated Herring:
In the production of marinated herring, round herring is trucked to the
processing plant and stored in iced or refrigerated bins. From the
storage bins the herring are either flumed or conveyed to a hand or
machine splitting operation where removal of head, tails, fins and
viscera takes place. The resulting split fillets are then stored in
barrels or vats in a solution of brine and acetic acid for a period of
5 to 9 days. After this period the solution is dumped and the fillets
are introduced to a second solution of brine and acetic acid and
stored at low temperature for a period of two weeks. While in this
stored solution the fillets are called bismarcks. Following this two-
week storage period the bismarcks are dumped, skinned, and repacked in
barrels ready for distribution. The process is illustrated in Figure 3.
Wastes are produced during the splitting operation, clean-up, and acetic
acid brine dumps. The offal is transported to fish meal plants for
further processing.
With both the herring filleting and marinated herring processing, the
waste is extremely colored, due mainly to the loss of blood during the
splitting operation. The coloration does not dissipate readily upon
discharge to the receiving waters.
406
-------
PROCESS
WASTES
DISPOSAL
RAW
PRODUCT
STORE
J.
EVISCERATE
BEHEAD
SLIME
_L
PACK
_L
WEIGH
PATCH
SEAM
_L
RETORT
I
COOL
BLOOD,SLIME
VISCERA, WATER
HE ADS, WATER
BLOOD, FINS,
SLIME, WATER
MEAT
MEAT
MEAT
WATER
WATER
SOLIDS, WATER
\
/
V
RENDERING
TREATMENT
RECEIVING
WATER
Figure 2 . Salmon Canning
407
-------
PROCESS
WASTES
DISPOSAL
VESSEL
UNLOADING
STORAGE PRIOR
TO PROCESSING
MACHINE
FILLETING
ACETIC ACID
BRINE
TREATMENT
SKINNING
PACKED
STORAGE PRIOR
TO SHIPMENT
SLIME.WATER^-
BLOOD.HEAD, V
VISCERA, FINS,
TAIL,WATER. '
ACET(C ACIDv
BRINE >
SOLIDS '
[SOLIDS, SKIN ,WATER)-
Rgure 3. Process Row Diagram
Marinated Herring Plant
408
-------
2.2.2.3 Herring Roe:
There has recently been a marked increase in the herring roe industry.
The herring are brined prior to process for removal of the roe. The
roe are salted, packaged and refrigerated prior to shipment. Following
roe removal the remaining herring flesh is sent for reduction to fish
meal or to pet food production.
2.3 Shellfish Processing:
Lobster is the major species of shellfish caught and processed in Canada.
Lobster are caught in large traps and must be kept alive until processed.
Approximately 65 percent of the lobsters are marketed in their shells
either alive or cooked. The remaining 35 percent are cooked and shucked.
Lobsters are steam cooked in retorts for 20 to 30 minutes and are water
cooled after cooking to facilitate handling. If the lobsters are to be
butchered their backs are removed and the remaining viscera are washed
free. The cooking, cooling and washing waters contain considerable
quantities of solids and organic pollutants.
Small numbers of cooked lobsters and meat are frozen for later marketing.
Low storage temperatures and quick turnovers are necessary for the
maintenance of high quality. Little lobster meat is canned because of
the rapid degradation of texture and flavour quality of the canned product.
2.4 Fish Meal Production:
In the processing of most species of fish for food purposes from 30 to 80
percent of the raw material is waste. Efforts are made by most plants to
recover all edible portions, and the recent introduction of deboning
machines promises greater utilization in the future. Still, much of the
fish poses a disposal problem and one practice has been to produce a
protein concentrate for poultry feed. Oil may also be recovered from oily
species.
The waste material, termed offal, is normally conveyed wet or dry to the
fish meal plant and stored in pits until enough is accumulated to warrant
operation. Solids recovered by screening of off-loading and processing
water are also sent to the fish meal plant. During storage some liquid
is drained or pressed from the offal. This stream called bloodwater, is
not large in volume but is very strong in terms of organic content. Some
plants attempt to recover this, but most discharge the stream with the
plant effluent.
The general flow for fish meal production is shown in Figure 4. The offal
is hashed by machine if large pieces are present, and then cooked in
direct or indirect continuous steam cookers for up to 10 minutes. Non-
oily offal may be added directly to driers, while oily species are
pressed to expel most of the water and oil prior to entering the drier.
In the latter case the press liquor undergoes a fine solids separation
using vibrating screens or decanting centrifuge followed by oil separation
in nozzle centrifuges. The oil is further clarified in polishing
409
-------
STEAM
WATER DISCHARGE
WATER TO
I COOKER]—[CENTRIFUGE!—^DISCHARGE
1 "WATER GAS TO ATMOSPHERE
WATER TO
•-DISCHARGE
BAGGING
OR STORAGE
IT
UJ
£
o
a
CO
TO STORAGE
•*WATER TO DISHARGE
EVAPORATION
CONDENSER WATER TO DISCHARGE
SOLUBLES TO MARKET
STICKWATER
DISCHARGE
Figure 4. Flow Diagram for Fish Meal Production
410
-------
centrifuges before sale as either an edible oil or animal oil. The
aqueous phase may still contain up to five or six percent organic solids
and is termed stickwater. At one time this was discarded, but now many
plants employ multiple effect evaporators to concentrate these solids.
The resultant product is termed condensed fish solubles and contains from
30 to 50 percent solids. It is marketed as a poultry or animal feed, a
specialty fertilizer, or is recycled back to the driers for incorporation
in the meal. The condenser water used in the evaporators does pick up
volatile solids and gases, the extent depending on the degree of freshness
of the offal and the manner of operation of the evaporators.
The fish meal driers are usually rotary kilns, with heat being supplied
by direct flame heating of the air, or by indirect heating using steam.
The solids are dried to between 5 to 10 percent moisture content, ground
to pass 10 mesh screens and sold in either 100 Ib. bags or in bulk.
The steam and odors generated during the drying of the meal can be very
obnoxious and most plants employ some sort of direct water scrubbing to
these vapours prior to release. Large volumes of water are employed for
this, and the scrubber effluents will contain a significant quantity of
organic material.
Many fish processing plants in Canada combine a number of the above-
mentioned operations. For instance, many plants on the West Coast have
the capability of processing both groundfish and salmon. These
operations might also be linked to a fish meal plant. The resulting
wastes from the fish processing plant are usually flumed together and
discharged as one effluent, after removal of the offal.
SECTION III
LITERATURE REVIEW
3.1 Characterization Studies:
Fish processing wastes vary considerably in pollutional strength. This
variation is due in part to:
1. Species of fish being processed
2. The age of fish being processed
3. The processing techniques
4. Plant size
5. Water usage
The characterization of wastes from various types of fish plants has been
the subject of a number of studies. Table 4 summarizes the characteristics
of effluents from fish processing plants as reported in 8 different
studies and reports. It should be noted that the BODj. values are all in
the same order of magnitude, however, greater fluctuations occur in the
suspended and total solids values. These fluctuations are due to
those factors listed above.
411
-------
Table 4. Characteristics of Effluents from Fish Processing Plants as
Reported in the Literature
Author
(Fish Processed)
Washington State Pollution
Control Commission (1969)
(Species of fish not specified)
Limprich (1966)
(Herring, Red Perch, Fish Meal)
Soderquist et al_ (1970)
(Bottom fish processing)
Matusky et_ al^ (1956)
(Wastewater)
Chun et al (1968)
( Tuna fish processing)
Soderquist et_ al (1970)
Salmon processing
Sardine packing
Stanley Associates (1972)
Halibut
Sole
Salmon
Shaffner (1970)
Ocean Perch
BOD,
Cms/1)
2700-3400
Suspended
Solids
(mg/1.)
2200-3020
Total
Solids
(mg/1)
2198-21,820
2658
192-1726
1000
895
397-3082
100-2200
64-150
160-195
390-1900
— —
300
425
1091
40-1824
100-2100
66-110
34-85
665-760
—
--
--
17,900
88-3422
--
390-540
330-1395
412
-------
Table 5 summarizes the characteristics of effluents from fish meal
plants as reported in the literature. The major effluents of concern
are bloodwater and stickwater, which although very high in BOD,, and
suspended solids are relatively small in volume. This compares to
deodorizer water which has a low value of BOD^ and suspended solids but
large volumes of this effluent are produced in fish meal production.
The total effluent characteristics as shown in table 5 indicate the result
of diluting the high strength low volume v/astes, such as bloodwater and
stickwater, with the low strength high volume wastes, such as deodorizer
water. The results given in table 5 for the different effluents are all
of the same order of magnitude. Variations in the results for the total
effluents are due to differences in the relative volumes of each type
of waste discharged by the fish meal plant. For instance, some plants
recover all stickwater while other plants discharge it with their
plant effluents.
5.2 Treatability Studies:
The difficulties in the treatment of wastes from fish processing plants
are attributable to high flows, medium to high BOD- and suspended
solids and high grease and protein levels. The short and variable
processing season, high peak loadings and rapid biodegradability of the
wastes also cause treatment problems.
3.2.1 Physical Treatment:
With the possible exception of the work by F.G. Claggett of the Fisheries
Research Board of Canada, which will be discussed later, little work on
the physical or biological treatability of fish processing wastes has
been undertaken.
A study by the New Brunswick Water Authority (1970) indicated the
effectiveness of screening wastes from groundfish processing plants.
Using both 10 and 40 mesh screens BOD,, removals up to 60 percent were
reported, however, the median removal value was 33 percent for both
screens. Further, the 40 mesh screen provided approximately 25 percent
removal of BOD5 for deodorizer water and for the total effluent from fish
meal plants.
Shaffner (1970) concluded that passing the wastewater from groundfish
plants over 20 mesh screens would remove approximately 20 percent of the
BOD,, and 16 percent of the suspended solids.
Flotation has been examined as another method of suspended solids removal
from fish processing plant effluents. Davis and McKinney (1970) used
chemical flocculation and flotation to remove oil and solids from herring
pumpwater. It was reported that the organic matter was concentrated from
0.4 percent to a 1.0 percent sludge by pressurized air flotation of a
recycled portion of the clarified effluent. Davis and McKinney concluded
that, while flotation could recover at least half of the solids remaining
in screened pumpwater, it was uneconomic because of its complex operation
and the creation of a sludge handling problem.
413
-------
Table 5. Characteristics of Effluents from Fish Meal Plants as
Reported in the Literature
BOD Suspended Solids
(mg/1) (mg/1)
Matusky ejt al ("956)
Stickwater 110,000 125,000
Deodoriser we? e-r 800 2,000
Canadian Plart and Process
Bng. (1970)
Stidcwater 25,000-72,000 6..500-47.000
BJDOdwater 35,000-90,000 40,000-55,000
Tots.! Ijffluenf 18,000-42,500 8,638-23,910
Shaffner (1970)
Stickwater 34,000 15,270-53,880
Deodorizer water 490 390
Total Effluent 4,400 4,300
Delaney (1971)
Deodorizer water 47
Total Effluent 3,180 1.020
Sha.winigan bng. Co, Ltd, (1968)
Stickwater 38,000 63,010
Total Effluert 257 33,500
Stanley Associates (1972)
Stickwater 69,000-83,000 10,000-15,000
414
-------
5.2.2 Biological Treatment:
Soderquist et_ ad_ (1970) reported that the carbon:nitrogen ratio of fish
processing wastewater indicated that biological treatment should be
successful. The biochemical oxidation rate was found to be similar to
sewage, however, nitrification began sooner and was more significant.
Soderquist et^ al_ (1970) further reported that a number of authors had
found that oil and grease interfered with the oxygen transfer in an
activated sludge system. In Soderquist's opinion pretreatment to remove
high solids, grease and oil content is a necessity if biological treatment
is to be successful.
Matusky et^ aJ_ (1965) stated that fish solids and oil digested readily
and the resultant sludge dewatered easily. The digester loading rates
varied from 0.1 to 0.36 pounds volatile solids per cubic foot per day.
A review of the literature indicates the current knowledge and process
technology involved in the characterization and treatment of wastes from
various types of fish plants. It is obvious that if the Canadian fish
processing industry is to adequately respond to the need for pollution
control better effluent characterization and treatability data must be
made available to this industry. Thus the Department of Environment has
embarked on a number of projects to collect this data.
SECTION IV
ENVIRONMENT CANADA STUDIES
The studies undertaken by Environment Canada are as shown in table 6.
The majority of these studies were carried out during the summer of
1971 or 1972. The exception is study #5, the characterization and
treatability of the wastes from a groundfish and salmon processing
plant, this study is still continuing and should be complete by mid-
1974. The results from these studies will be presented in two parts,
the first part being the characterization results and the second part
the results of the treatability studies.
4.1 Characterization Studies:
4.1.1 Groundfish:
The groundfish operations involve the processing of halibut, cod, redfish,
sole and flounder. Two basic types of processing are used:
a) dry line operations which use a system of conveyors to move the raw
product and mechanically operated filleting tables. In the majority
of cases offal is removed from the filleting area by fluming.
b) wet line operations characterized by the use of water to flume the
raw product and the offal.
In general dry line operations are used in the larger operations whereas
the smaller plants rely on wet transport of raw product and offal. In
the majority of cases fish are washed in tanks or spray conveyors
immediately prior to processing.
415
-------
cd
*"O
g
03
U
P
C
6
C
o
f-i
•H
w
X
Xt
C
4)
rt
P
0
r*
-3
in
C
CD
3
rH
tH
CH
OJ
X
"O
3
P
CO
4-1
O
0)
p
cd
Q
bO
cs
•H
in
in
CD
O
O
CX
rj
in
•H
[T ,
li_J
af °
• H l/l
in
0)
u
O
CL,
"w
•H
U-,
4-1
O
in
(U
T3
3
P
co
O
X
f-l
cd
g
•j
CO
0
£
+"*
C
CD
3
i— i
14-4
4-1
O
CD
PH
£
X
3
P
vO CO
CD <4-l
rH O
Xl
cd p£
H 0
•H
P
cd
o
o
rH
O>
rH
„
f-l
0>
€
g
3
co
in
3
cf
•H
C
•8
a>
00
C
• H
P
CD
i— (
rH
•H
-o
in
in
ID
o
f-i
O,
P
rH
CD
6
co
«£T
r^
O
fH
0>
a.
' •"O
C
SK,
*n3
3
CO
cd
X
p
•H
rH
•H
•8
p
o3
4J
*£E . ^
O ^H
t-J PQ
•
r^
O">
rH
^
J»(
£
•P O -H
Cd rH +J
C rH CD
•H -H rH
rt -H
2 PU
C
O
•H
CU 4J
e u
•H 3
rH "O
X! O
C/D M
rX
r^ •»
W XI rH
•H in cd
OO 4-1 -H CD
C -O 4-i S
•H C rH
H 3 rH X
fn o D in
CD fn Xl -H
X O CO tt,
£*
0
•H
p
cd
N
•H
fH
CD
p
u
cd
(H
ri
u
u
o
55
^J S^
in o
cd -H
-------
4.1.1.1 Dry Line Processing:
Tables 7 to 10 give the BODj., suspended solids and ether soluble oil
loadings in the effluent from the processing of halibut, grey cod, ling
cod, sole and redfish. The results are given in both concentrations,
means and ranges, and in pounds of parameter per 1000 pounds of raw
product, again in both means and ranges.
Examination of tables 7 to 10 indicates the wide variability in effluent
BOD5 and suspended solids loadings. This variability in loadings not
only existed in effluents from the processing of different species in
one plant but also in the effluents from processing of the same species
in plants of differing size. Table 11 below summarizes the BOD- effluent
loadings for the processing of sole, grey cod and ling cod - the species
processed in the three different sized plants studied (study f2).
Table 11. Summary of BOD- Loadings from Groundfish Processing Plants
b Study #2
Plant Sizj; Sole Grey Cod Ling Cod
Lbs of Raw Product/Day Lbs BODr/1000 Lbs Raw Fish
6,000 1.4 8.1 6.3
10,000 2.7 2.2 4.1
15,000 0.7 0.9 6.0
Average 1.6 3.7 5.5
Table 12 summarizes the total effluent values for the dry line processing
of groundfish. The results indicate the range of BOD- loadings for this
type of groundfish processing varied from 1.3 pounds of BOD,, to 7.9
pounds of BODp per 1000 pounds of raw product.
Further examination of table 12 indicates the variability of suspended
solids loading of 0.98 to 2.4 pounds per 1000 pounds of raw product and
of 0.13 to 1.0 pounds per 1000 pounds of raw product for ether soluble
oil (study #2 and #3).
The variability of tie effluent in terms of BOD_, suspended solids and
ether soluble oil loadings is considerable due to differences in water
usage, age of fish processed, amount of fish processed as well as the
processing techniques. A review of tables 7 to 12 indicates that there
is no relationship between effluent loadings and plant size.
4.1.1.2 Wet Line Processing:
Table 13 summarizes the total effluent loadings for the wet line process-
ing of groundfish from studies #3 and #4. The BOD effluent loadings
417
-------
O VI
1— 1
•H
O
,
-o
3
•P
i
r^
I/)
V
rH
H,
,^
CO
!H
0>
JS
(JJ
O -H
O
4-1 C X
crj ^
3 *
rH
/— N
r-l ^ oo ./->
00 CX
B rt ^
^
CM
1
00
d
LO
CM
LO
0>
CM
CM
l/>
tO
LO
to
• /"•>
O CM
I
tO
tO
CM
LO
• /">
to to
I •
i—I r-H
. V..S
O
to
r-l
O (--,
fH O»
rt 00
to
Q
e
o
^1
u.
p
C
3
rH
^M
MH
U
o
0
o
I— 1
*v»^
J3
LO
a
•
O
C
o
u
V) 0)
(•H C | X
rt ^— '
s otf
• <— \
Tt \O
1
tO CM
• v_ y
Cu ^H
O I— N
»-> CM CM
rH 0)
~>» 00 ./-^
00 C X
S rt v_/
s— ^ ON
Tt 00
1 CM
LO ^
«?}•
rH
<^^
0
I
1 Tf
^^
/— \
«^f
1 O
1 CM
v_^
,
rH
1
rt
•
O
Tl-
rH
rH
1
O
•s
H
a>
LO
II
./—\
Ix
418
-------
10
X)
x: O
rH - -
•H
O
0>
^H
•9
^H
o
U3
t .
H
*S
\ S as
«M
• /•"•!
m t^.
i •
t rH
0 ^
TO
Xl H 0
H-I
r^
* ^-^
• ^^^ ^«- « ^
O rH . bo .<-%
3^ § &
^ OS
i^» ^^
CM .
CM rH
1 VO
O v-'
•
^t
\o
• r~\
C3 CM
!• •
IH O
O '-'
o
CM /— >
• r*»
m •
m >o
1 rH
•* »— '
•a
o
4-1
O
W
•H
O
O
O
rt
a,
w
oo
s
to
O vi
O -H
O
Ix
•8
u
o
to)
(U
•H
^
vO
•
O
10
o>
in
CM
r^ oo
in
s
00
in
O ^-^
O f>
rS O^
I CM
V)
CM
m in
rH tf)
i •*
ro «-^
in
s
o
•
o
o»
I
in
o
CM
I/J
O>
f*
CM
O
O
O
r
419
-------
CM
O tfl
O -H
O
X
+J
tu
O r-l
c --.
O 00
u S
> — '
0)
oo
e
OS
< — \
X
V — /
i in
I O
I
O
0
O,
0)
C
•H
X
Q
S
o
£H
4-i
•P
C
0)
1— 1
4-4
4-1
o t/> • ^^
O -H LO LO
O 4-1 bO .^— . 1 •
•-i ex \o to
-^ S « >-^ • ^-^
w rt oJ i-i
5
•
co
1^-
C/3 • / — i rH I — \
O rH 00
u e cij N — ' • 'i'
v-' Oi tO CM
t^ ^— '
rH
W
rH I***-
^=j • <~^
O I/) <1> CM IO
O -H bO ./-^ rH .
0 4^ Pi X 1 ^>
rH Cj v— ' CM < — '
^*^ 2c Qi •
t/> rt CM
LO J
o
s
O /—s
• r- x LO rH
CT> O i-4 0) O •
Pi ^ DO ./— \ r-H O
0) O (30 C 1 X 1 O
•— 1 U vg, OS ' — ' i-H LO
r\ o«J t — ^ v — '
H ^
/ — » T3
>> O
rt cj
tJ
0) •>*. W
NX! c
•H t/> -H
CO -H i-J O
4-1 O
4J O
c s ••
C(J cd t/) \O
rH M 0)
Cu -H
in o
Xi
rH 00
' ^^
0 ^
to
o
o
o
•t
o
rH
" t — \
CNI 00
1
OCl rH
.i V /
O
i— 1
,i
rH /-^\
CNI Lrt
r-l
1 LO
vo cn
.1 ^ — /
r-l
^J'
O
1— 1 / — v
i-l O
1
r-l VO
.1 V — /
r-l
\Cl /"-N
Tt- O
LO O
1 to
^' ^— '
LTl
O
O
o
>»»
LTl
r-l
c
rt
0)
420
-------
t/J
,0
0
rH
•H
O
,
|
CO
1
CD
O
CO
4-1
O
w
c
•H
(/)
t/)
CD
0
o
ex,
CD
c
•H
*J
rT
a
s
o
rH
4->
C
CD
•3
i— i
4-1
4-4
PJ
CO
rH
,=!
+J
CU
o
o
rH
"t/T
3
•
O
o
CJ
(/)
,0
o
o
o
1— 1
*^^
I/)
f-^
^J
•
.
CO
•
o
R
O
u
5
o
o
o
r-l
**»^
i"i
uo
o a
l_3
in CD
• H bO ,/-N
4H C X
co ^
at
rH
^ CD
rH 00 .<— .
-*. g x
60 3 ^
xE ^
C*
« 0
• H bO ,i-\
(ii j^ 1 S^
aJ ^
2 a:
nJ
f-^
-H t>0 /-^
Co ^— ^
s ex:
rt
rH
^?
CM
1
CM
O
vO
O
^
**?
to
o^
rH
1
CM
0
00
oi
vO
CM
1
rH
•
CM
0>
00
*H^
1
to
,
o
f-^
to
•
V- J
f—^
^H^
•
C7>
O
Xv/
/ \
oo
•
o
V 1
r^
00
•
1-
CM
rH
v— '
r— \
•
i— 1
>._»/
rH
rt ^->
1 vO
rH
O rH
O
rj-
•
\O «^^v
CM LO
10 rH
1 CM
o ^
to
CM
•
to ^.
1 ^t
VO rH
. ' — '
O
00
o
o^ / — \
1 CM
00 to
rH IO
rH >— '
XO
• / — N
t^ r^
i
IO CM
. ^— -
rH
«t
O ^^
1 rH
CM •
o o
• s_^
o
\o
• *^~N
to o*
1 O
tO rH
• \—i
0
l/>
•
rH /—,
1 v£>
O O
• *— '
O
OO
IO
^* /^*N
rH LO
1
\o co
• f-
CM •— '
IO
rH
• r~\
•H r-
1
•* o
. >— '
0
1— 1
•s
8-
0
§
u
r~-\
rH
>
> — '
CD
bO
s
&.
,d
H
o
m
i
oo
to
rH
CM
1
O
o
CM
rH
to
o
to
rH
OO
rH
00
> — /
C
rt
CD
N -C
•H I/)
CO -H
4H
•M
S *
co nt
rH rH
Ok
t/)
3
>— <
rH
O
CO
o
o
o
CD
•H
O
p.
CO
•v
VO
O
o
o
o
rH
o
o
o
LO
rH
421
-------
M
•H
(/I
O
o
•H
M-l
(1)
c
I
C
rQ
rH
rC
O trt
rH O -H
•H o m
O <-i
"*v S
O •!-*
O M-l
rH
"*"^s S
u) cd
rQ rH
,-J
vj
•
C/i • / — \
U rH
C ^s.
o bo
U B
V 1
rQ
rH
O 01
O -H
O M-l
rH
\ s
01 cd
LO J
§
• t — x
O rH
C \
o tso
u 6
\ — i
/ — x
X
X x
•H Wl
tO -H
MH
4->
rH S
0,
O
j^
v — /
CD
bO .f^
C \X
erj ^->
C£
0
bO ./-x
C |X
rt v- •<
oJ
tu
bo ,^->
C |X
cd x_/
pi
a,
bO ^-x
C | X
cd x — ^
o^
co
bO r~^
C X
s ~
!-(
X
to
1
to
•
o
LO
t*^
rH
1
Ol
0
0
O
*v
xO
CM 1
t — x
O
rH
V_^
i — \
00
.
\Q
LO
V- J
f — \
xrf
•
CM
\ /
f~-^
LO
•
vD
CM
CM
* — /
f — \
r-~
.
LO
v— ^
; — v
LO
•
rH
LO
' '
rH
•
^f
1
rH
O
0
•*t
vC
CM
LO
1
^t
O
LO
•
LO
1
rH
•
O
vO
O
O
rH
1
CO
*»
vO
t~^
I
CM
CM
•
0
t^
^>
LO
rH
1
0
(0
o
0
o
n
o
rH
/— \
LO
^
o
X /
t — \
to
•
to
V J
r — x
vO
•
rH
x — t
r— \
<^
LO
CM
, v
t^^
.
CM
v — '
/^>
0
r— t
rH
Tf
x — '
•t
•
O
1
CM
O
O
\o
to
T^
1
10
to
d
UO
to
1
^-
o
o
oo
.
to
rH
1
•
rH
O
rH
rH
1
^~
•
O
xO
^>
LO
t--
(N
o
o
o
A
IO
r-l
/— -\
to
i-H
O
^—^
/— N
^O
.
^^
rH
\^_ /
oo
en
o
,— ^
tn
•
^j*
NO
**-/
t — i
tO
i— i
v^»
s~ %
o^
*
f— t
o
f-H
V~—'
CD **^
o o
LO O
o •—'
I O
I •
O
to
CN
i
CN
IO LO
CM IO
I rH
O >—'
to
LO O
I O>
O IN
O
ui
rH LO
1 LO
o -=t
O v-^
LO
LO
I
o
to
00 r-^
to 01
I t~-
OO CN
c o
CIS N
o
o
o
•*
o
o
to
nl
0)
f
to|
422
-------
M
C
•H
in
o
o
5^
a,
xl
10
•H
e
o
-P
G
to
XI
x:
O to
O -H
rH O <4-l
•H rH
O ^3
1/1 Oj
.
•P O bO
W US
\ ^
tn
Xi
r~H
Xi
o to
O -rH
O M-l
rH
•-x^ |2
to oj
Xi 5n
CO
CO • r~^
O rH
G "--
O W>
0)
bO v— ,
G 1 X
ni < — '
QJ
0)
00 ./-%
G X
oJ ^
Qi
0>
bO ./->
G X
rt •>-',
OJ
(U i
bo ./-^
P? I.X
1 f — ^
i to
f-H
N—'
O
o
Lf) /^->1
rH O
1 O
0 O>
o ^
CS
/ — s
1 O
1
f^
* — /
IO
CTl O>
CJ &
00
00 •<*
I O
to
o
o
r-4 tO
I 1—I
O LO
CM
I CM
O rH
tO ' — '
o
10
10 /-x
rH rt
1 (N
o •<*
UJ
id
o
H
nJ
H
LO
O
o
CO
to
X>
o vi a>
O -H bC
O UH (3
ui
X)
IO
o /—>
CM \O
rH tO
I i—I
CM rH
O >—'
O
i oo
I O
I
to
rt
a>
N
•H
co
•p
G
rt
rH
a,
x:
l/l
•H
3
crj
5H
to
Xi
1 — '
5-4
X
G C
a>
G rH -rH
3 a. co
o
o
o
n
o
LO
CM
o
o
o
S
o
o
o
•k
o
(N
423
-------
vary from 15.0 to 20.2 pounds per 1000 pounds of raw product whereas the
suspended solids loadings vary from a low of 7.0 pounds to a high of 34.0
pounds per 1000 pounds of raw product. As with dry line processing
these effluent loadings vary widely.
Comparison between the effluent loadings from dry a.nd wet line
processing of groundfish (tables 12 and 13) indicates that wet line
processing produces an effluent in excess of three times the dry line
effluent loadings. These increased loadings are due to:
a) increased BOD^, suspended solids and oil concentrations in the
wet line effluents.
b) water consumption figures (table 14) indicate that wet line
processing requires 2 to 3 times the water required for dry line
processing.
This variation in the effluent loadings from dry and wet line groundfish
processing supports the theory that the longer water is in contact with
fish solids the higher the BOD5, suspended solids and oil concentrations
in the effluent. In wet line processing, water is in contact with the
fish for considerably longer periods than in dry line processing. Study
#1, carried out on freshwater fish processing, also supports this theory.
A major step toward reducing the pollution from groundfish processing
plants would be the widescale adoption of dry transporting techniques as
opposed to the presently more commonly used fluming methods characteristic
of wet line processing.
4.1.2 Pelagic and Estuarial:
4.1.2.1. Salmon:
Spring, coho and some chum and pink salmon are usually glazed and sold
whole, while the majority of the remaining salmon catch is canned. The
wastes from the canning operation include butchering water, viscera,
wash water, retort water and cooling water.'
Table 15 shows the values of total effluent from salmon canning and
glazing operations as determined from study #2. The results indicate
that BOD5 loadings of about 25 pounds per 1000 pounds of raw fish can be
expected form salmon canning using either iron chink or hand processing
techniques. The suspended solids in the effluent will vary from about
15 to 25 pounds per 1000 Ibs of raw fish.
Water use figures from study #2 indicate that salmon canning requires
between 0.9 to 8 gallons per pound of salmon canned. The processing of
spring salmon (glazing and storage) requires approximately 1.5 gallons
per pound of product.
Frequently, water used in the unloading of salmon at the plant dock
is discharged direct to the harbour. Following unloading, the ships
holds are washed, this wash water also enters the harbour directly.
Table 15 gives the effluent load associated with the hydraulic pumping
424
-------
-a
e
•H
•a
C
rt
C
O
X! -H
(/) rH
•H
O
i
a> i a>
c c
xt -H xi -H
in rH (/) rH
•H -H
TJ rH 13 rH
O
rH
CJ
O
rH
CJ
•d
(D
C
0)
e
XI
tn
§S
O
cj
xl
tn
•H
§*
O
CJ
I 0)
XI -H
T3
rt
OJ
rH
X)
SI
•H
t/)
rt
X
rt
xl
tn
§
rH
O
o
o
•\
&
X
rt
•d
N
I
-a
2
o
o
o
cT
o
to
X
rt
-d
tn
§
rH
in
XI
O
O
o
o
(N
tn
rH
in
O
o
o
o
oo
X
-d
X!
rt
in
Xi
O
o
o
CN
it
t
•P
CO
to
*
X
"3
X
-d
4J
en
425
-------
i-H
• H
o
fll
w
1—4
,0
3
r~4
o
(/)
t-l
a>
A i
&
00
c
•H
W
!/>
1)
O
0
£
q
0
6
c-l
$
S
S
IH
to
4->
pH
3
in
0)
oi
4->
C
S
r~
o t^-
CM 00 ^O
^ VO N
i-l CM
(0 r-l M
w °° ij
Mh rxt
• O» *
iH CM CN .
00
•o >J
Processing an
Plant Capacit
S1 S 5 -S
_ . F K. tj ^ Tl
CJ -H M X H 2?* M
i £ .•€ .-S S
,5^c3r->tn -aS..^
c5?^8^3c355|g
•H fn -H P* cC _ P^ _,
BON 0. S 0 U 0 C
.s^ ^§ s -a g s | a
fcj rn C CJ •> 'H O " 'H iH
^^1"^^^^-^
/•—•^
bO
f-J
•H
I
(Hydraulic pi
r-l O» VO
00 -«t CM
i • •
O O O
^- to
oo m IH
• • •
C>1 iH «H
£
-------
method of unloading salmon. Table lb indicates that the wastes from the
unloading operations vary somewhat but should be considered as part of
the plants effluent and should, therefore, be treated in the plants
effluent treatment systems.
4.1.2_. 2 Herring:
There has recently been a marked increase in the volume of herring being
processed for human consumption because of the general decline in the
total herring catch and restrictions on the use of herring for fish meal.
The major waste sources associated with the variety of herring processing
techniques include pumpout water, brine used in roe recovery processing,
acetic acid-brine dumps used in the marinating process, and water used
during the filleting processes. The majority of wastes are screened
prior to discharge, however pumpwater used in the unloading process is
usually discharged direct to the harbour.
Table 16 gives the effluent characteristics for food herring production
as reported from studies 3 and 5. The total plant effluent from
marinated herring does not include the acetic acid-brine dumps. The
results shown indicate the high strength of the effluents generated by
food herring production. The high BOD,, and suspended solids in the
pumpout water indicates clearly the necessity of treating these wastes
in the plants effluent treatment system rather than allowing direct
discharge to the harbour.
4.1.3 Shellfish:
4.1.3.1 Lobsters:
Lobsters are processed solely in the Atlantic region. The main waste
source occurs from the butchering operations with its associated wash
water. The effluent loadings vary from 20 to 30 pounds of BOD per 1000
pounds of raw product with a suspended solids loading of from 4 to 7
pounds per 1000 pounds of raw product. Water usage averages about
2500 Imp. Gallons per 1000 pounds of raw product.
4.1.3.2 Crab:
Crab are processed on both the Atlantic and Pacific coasts, the largest
volume being on the Pacific coast. As in lobster processing, the
largest waste loads originate in the butchering area. BOD5 effluent
loadings vary from 20 to 60 pounds per 1000 pounds of raw product, with
a suspended solids effluent load of between 10 and 30 pounds per 1000
pounds of raw product. Water consumption averages about 6,500 Imp.
gallons per 1000 pounds of raw product.
The data given for both the lobster and crab effluent loadings was
obtained from study #3.
427
-------
IT,
Xl
r-4 r*
01 (U
rH
•H
0
X
4->
UP
0 -H bO i
0 4H C 1
o cd
rH S OS
-•^ cd
in !H
Xi
• ^^ (l)
O rH 60 .
c •— c 1
O bO cd
u5«
in
XI
bO
c
.H
in
in
in
*H
rH
(1)
<-)
O
OS
'M
cd
C^-HI
U
4->
aj
^H
4-1
4-1
OJ
rH 43
ul — '
l' — '
Ix
v^
,/ — >
1 X
*v— /
I O
o
O ^—v
o o
to o
I CN
O r-l
O ^
M-l
o tu
U» at
r-l
GOO,
• H r-l
rH Cd
r< +->
4) O
I tO
I 00
o
o /-%
o o
LO O
i tn
o CM
o ^
00
i in
i oo
o
o
\O /™N
rt O
I rH
00 <*
o to
LD
i i—i
I CM
O
o
o
I 00
O oo
a *->
I O
I O
LO
O
to
in
If)
i in
1 $5
bO 3
C rH
!H U
(U
as *->
c
T3 Cd
fl) rH
cd
00
in
CM
C
•H
Cd OH
* 60
•p e
3 -H
O
H
c
3
Cd C rH
+J cd 4-i
O rH 4-1
t- CU W
O
tl
+-)
to
428
-------
4.1.4 Freshwater Fish Processing:
There is in Canada a sizeable freshwater fish processing industry. Study
#1 was carried out at a plant which processes approximately 30 million
pounds of perch and smelt per year. This plant fillets perch whereas
smelts are eviserated. The combined effluent loadings from this plant
are given in table 17. The sampling of the individual perch and smelt
effluents as well as the combined effluent indicated the dampening effect
of mixing the two component flows as the combined effluent is stronger,
but less variable on a day to day basis, than its individual component
parts.
During the study, water use in the plant was examined and found to be
relatively constant at about 295,000 Imp. gallons per day, irrespective
of the volume of fish processed. This is shown diagramatically on figure
5. A number of other studies also indicated that the rate of water
usage was relatively constant regardless of the quantity of fish being
processed.
Table 17. Combined Perch and Smelt Wastewater Characteristics (Study#l)
BOD5 S.S.
Cone. Lbs/1000 Ibs Cone. Lbs/1000 Ibs
_(mg/lj_ raw fish (mg/1) raw fish
Mean 3044 4.5 1397 2.3
Standard ±1413 ±2.0 ±724 ±1.3
Deviation
Coefficient of 46.3% 45.4% 51.8% 58.7%
Variation
Number of 40 29 40 29
Samples
4.1.5 Fish Meal Production:
The processing of fish meal can lead to the discharge of high strength
wastes. A review of table 18 indicates the advisability of limiting the
direct discharge of bloodwater and stickwater to receiving waters. Many
plants do in fact recover both their bloodwater and stickwater, producing
fish meal, condensed solubles and oil from these waste products. Such
recovery practices should be encouraged in those plants which presently
discharge their waste direct to the receiving water.
429
-------
o
i 0
+•>
^^
>•>
J3
TJ
O ©
TJ ©
>
TJ
/A
^ x
>>
frt
vu
TJ
O
£
**-*
O x*x
^*x
(0 x
0 J
" 3
S *s
Q)
_3
/n (0
vl ;•'
0) > >
3 TJ
15 c
•^ /1\
> 2 x,
>0
'S ®
(0 ^
Q §
X ©
X
i 1 1
©
X
x x
X _
( X
X
X
©0
^
©
X
c x
© —
X
,x
—
X
f
X
X
II
1
(N
00
T""
(D
r >
Q
^v
Tf w
- m £
-J rt
^ Q
o
T~ ^
«, x <»
2 z °-
T~ t-
Q ?
1- w
O m
OD S
S 2
0 Q.
2 4
ff\
00 I iC
2 «
j °
CD < i:
h «
0 -s
i_ «
n en
-*.
£
430
-------
Table 18. Average Effluent Characteristics from Fishmeal Processing
Waste Stream
Non-Oily Bloodwater
Oily Bloodwater
Deodorizer Water
Condenser Water
Stickwater
Groundfish
Herring
Perch and Smelt
Pumpout Water
BOD
O
(mg/1)
120,000
80,000
20
10
120,000
70,000
160,000
34,000
SS
(mg/1)
--
15,000
100
80
10,000
30,000
66,000
8,000
Ether Soluble Oil
(mg/1)
3,000
--
--
__
300
5,000
1,200
500
Many of the studies reported previously indicate that the results
obtained from BOD-, suspended solids and oil analyses varied widely.
This is due to:
1. Inherent sampling and analysis problems.
2. Variable characteristics of the fish such as age, sex, and season of
the year.
3. Variations in the catch handling and storage techniques employed by
the fishermen as well as the time required to transport the fish to
the plant.
4. Variations of off-loading, storage and processing techniques employed
by the plants.
Reliable results from fish plant effluents studies can only be obtained
from a thorough sampling program. In most cases such a sampling program
can only be carried out on the total effluent.
431
-------
4.2 Treatability Studies:
4.2.1 Physical Treatment:
4.2.1.1 Screening:
In the course of pilot plant studies on the treatment of fish processing
wastes, the Vancouver Laboratory of the Fisheries Research Board of
Canada (Study #5) established that tangential screens equivalent to 40
mesh screens could successfully screen salmon canning wastewater and
herring pumpout water. A diagram of such a screen is shown in figure 6.
A design flow-rate of 50 IGPM per foot of cross-section could be maintained
with periodic high pressure spraying of the screen surface to prevent
clogging.
In a subsequent demonstration unit designed by the Fisheries Research
Board staff, two 6 foot 45 degree tangential screens were used in
parallel to handle a flow of 650 IGPM of salmon canning wastewater. The
screen sizes were equivalent to 18 and 25 mesh respectively and
subsequent visual examination revealed that the 25 mesh screen was subject
to less plugging. With the addition of high pressure sprays working on
a time clock of 10 seconds on every three minutes, the screens have
operated satisfactorily and effectively on water from salmon canning,
groundfish filleting, salmon unloading, herring unloading and herring roe
recovery. These screens are preceded in line by a 4 mesh rotary screen,
and typical recovery rates are given in table 19.
Table 19. Solids Removal by Tangential Screens (Study #5)
Wastewater
Source
Flow Rate
(Gals/ft, of
cross section)
Insoluble
Solids
Removal %
Dry Solids
Recovery
lib/hour}^
Salmon Canning 56 43 280
Groundfish 66 10 24
Herring pump water
plus process water 28 50 1500
During study #1 the effect on smelt and perch processing effluents of
20 mesh tangential screens, similar to that shown on figure 6, was
examined. The percent suspended solids removals are shown in table 20,
Further tests of 25 mesh tangential screens are to be carried out on
groundfish filleting effluents and pumpout water. These tests should
be complete by August 1973.
432
-------
Oversize
Tangential
Screen
Figure 6. DSM Tangential Screen
433
-------
Table 20. Suspended Solids Removal by Tangential Screens
(Average and standard deviation of the S.S. Concentrations)
Wastewater Before After Percent
Source Screening Screening Removal
(mg/1) (mg/1)
Smelt Processing
Line 1 2362±380 16211261 31.4
Line 2 3434±483 24731332 28.0
Perch Processing 1107+191 825+156 25.5
4.2.1.2 Flotation for Protein and Oil Recovery:
Based on the pilot plant studies of the Fisheries Research Board of
Canada, a demonstration protein and oil recovery system has been
installed at a Steveston fish processing plant as a joint venture of
the Fisheries Association of British Columbia, B.C. Packers, Ltd.,
and the Industrial Development Branch of the Fisheries Service,
Department of the Environment. The unit was designed by Fisheries
Research Board staff, and the operation of the unit has been monitored
for two years. A flow diagram, of the unit is shown in figure 7.
The unit consists basically of two 6-foot tangential screens of 18 and
25 mesh respectively, operating in parallel, followed by a dissolved
air flotation cell. In this unit the screened water is pressurized
to 45 psig, air is injected at 2 percent by volume, and retention
time under pressure is supplied to allow the air to enter solution.
As the pressure is released by passage through a throttling valve the
water enters a baffled tank. The dissolved air is released under the
reduced pressure in the form of minute bubbles which attach themselves
to the solid or oil particles present. These rise rapidly to the surface
and are skimmed off for recovery of protein and oil. The clarified liquid
is withdrawn by stand-pipe from the bottom of the tank.
The use of chemical additives has been found necessary for proper clarifi-
cation, for emulsion breaking, colloid destabilization, protein precipita-
tion and flocculation. Two chemical combinations have been found to be
effective for treating wastewater generated in fish processing. The one
utilizes a caustic-alum combination and the incoming water is dosed with
sodium hydroxide to raise the pH to about 9.2. Enough aluminum sulphate
is then added to lower the pH to about 5.4 The other utilizes alum-polymer
combination and enough aluminum sulphate is added to lower the pH to about
5.4 and an anionic polyelectrolyte is added to assist the proper
flocculation. Both systems are equally effective but the latter has been
favored slightly due to lower chemical costs, ease in solids recovery and
lesser sensitivity to operating parameters. The clarification achieved
434
-------
H
o
<
Q.
Q
HI
h-
a?
3
O)
U.
435
-------
is shown in table 21.
Table 21. Degree of Removal of Various Characteristics by Air Flotation
(Study #5)
Water Source Insoluble Soluble Protein BOD,. Oil
Solids Solids _
Salmon 92% 28% 61% 84% 90%
Herring 74% 44% -- 72% 85%
Groundfish 86% 14% -- 77%
Stickwater 95% 60% -- -- 95%
The solids which are skimmed from the flotation cell represent about 3
percent of the total flow treated. The solids content averages about 5
percent. Recovery is affected by raising the temperature of the stream
to about 200 degrees F. to denature the protein followed by removal
of the solids and oil by centrifuging. The solids are added to the driers
for recovery as fishmeal. Analyses of the recovered solids is given in
table 22.
Table 22. Analysis of Solids Recovered by Air Flotation (Study #5)
Protein
Oil
Ash
Moisture
65.0%
9.4%
12.6%
10 . 1%
The effluent from a flotation cell has a biochemical oxygen demand (BODr)
of 100 to 500 mg/1 as opposed to screened wastewater which ranges from
200 to 3500 mg/1. The BOD- remaining is essentially soluble, is readily
dispersed in the receiving water, and is easily assimilated by bacteria.
In addition, this effluent is fully saturated with oxyger due to the use
of dissolved air flotation.
436
-------
Experiments in the demonstration unit indicated that better than 85% of
the solids in stickwater can be recovered during air flotation by mixing
9 parts of clarified effluent with 1 part of stickwater prior to treatment
(i.e. operating at 90 percent recycle). The resultant BOD^ is still very
high, averaging over 5000 mg/1, but this does offer a partial solution to
the problem of handling salty stickwater. Yet to be established is the
value of the recovered solids as an animal feed ingredient, and these
experiments are planned for the near future.
Other chemical combinations are possible with the dissolved air
flotation process. One currently under test in the Scandinavian countries
involves the precipitation of protein by pH adjustment using sulphuric
acid followed by reaction of the protein with a derivative for ligno-
sulphonic acid, a pulp mill waste product.
The economics of dissolved air flotation treatment have not been fully
established, but based on interim results obtained on salmon canning
wastewater, the value of the recovered solids sold as fishmeal should
offset the direct operating costs but not the capital investment.
4.2.2 Biological Treatment:
Several problems exist in attempting to design biological treatment
systems for fish processing plants. Superimposed on the seasonal nature
of the industry are discontinuous operating periods within the seasons.
For example, many processing plants operate only one or two days a week
in all except the busiest part of the fishing period. Such operations
make almost any biological treatment system except lagoons impossible to
use. This type of discontinuous flow would tend to upset the operation
of all but the largest of joint municipal-industrial treatment plants.
Study #1 examined the treatability of combined perch and smelt wastewater
using laboratory scale continuous flow biological reactors. By varying
the detention time and sludge age in the continuous reactors, it was
found that a sludge age in excess of 3 days is required for optimum
removal of BOD , both filtered and unfiltered. Figure 8 summarizes the
results for the continuous reactors, giving mean percent removals with
standard deviations for each sludge age tested.
Examination of figure 8 indicate that increasing sludge age above 3 days
with or without sludge recycle did not markedly effect the percent removal
of filtered or unfiltered BOD^. The removal of filtered BOD was approx-
imately 80 percent for each sludge age tested, whereas the removal
dropped to approximately 45 percent for unfiltered BOD,.. Maximum BOD
removals could be achieved by either a short detention time reactor
(7.5 hours) with sludge recycle and a 3 day sludge age or a larger
detention time reactor (5 days) with no sludge recycle.
The Fisheries Research Board of Canada's Vancouver Laboratory (Study #5)
have been experimenting with the use of a rotating biological contactor
(RBC) pilot plant as a high rate biological treatment system for
reducing the BOD load after air flotation. This system involves passing
wastewater through a compartmented trough in which styrofoam discs are
slowly rotating. A biological growth develops on the disc and is
437
-------
o<
_
UJ -
00
CD CD
UJ
QO
T~
CJ
O
03
(ID
CO
LU
CD
<
UJ
0
Q
D
_l
CO
CM
0
00
0
(D
0
(N
in
Q
O
CD
w
0)
-P Q)
O -M
<« !2
Q) (0
3
O
3
C.
03
d)
i_
D
O)
_LN3OJd3d
438
-------
alternately exposed to the wastewater and air. Some of the biomass is
constantly sloughed off the disc and is carried through the unit to a
clarifier. Not only is the system stable to hydraulic surges, but
continues to operate effectively under low flow or recycle conditions.
Preliminary results indicate that, under normal conditions, a BOD
removal of 4.5 pounds per 1000 square feet of disc surface per day is
easily attainable on a salmon canning plant effluent previously treated
by air flotation, resulting in an effluent of about 50 mg/1 of BOD^.
In addition to previously mentioned advantages, the capital costs of this
type of system is competitive with other high rate systems, whereas the
operating costs are considerably lower.
4.2.3 Cost of Treatment Systems:
The capital costs associated with the installation of fine screening and
air flotation can be estimated fairly readily from the data obtained in
the installation of the demonstration unit at Steveston (Study #5).
These are in the order of $2,500 and $10,000 per 100 Imp. gallons per
minute respectively. Estimation of the cost of biological treatment by
aerobic lagoons is more difficult because the largest portion of the
total cost is in land aquisition. Roughly one acre of land per 100 Imp.
gallons per minute is required if the water is from a groundfish plant
or has been previously treated by screening and air flotation to about
five acres per 100 Imp. gallons per minute for untreated wastes. Thus
near metropolitan areas the cost could range from $40,000 to $200,000
per 100 Imp. gallons per minute to achieve proper secondary treatment,
based on a price of $30,000 per acre. A further problem of lagoons would
be the availability of suitable land in close proximity to many fish
processing plants.
Table 23. Cost Estimate to Achieve Various BOD,. Levels
(100 IGPM of Flow)
Waste
Salmon
Herring
Groundfish
BODC
3000 5
$2500
$2500
__
Level (mg/1)
500
$12,500
$12,500
—
100
$52,500
$52,500
$12,500
439
-------
SECTION V
CONCLUSION
The five studies undertaken by Environment Canada have provided the fish
processing industry with characterization and treatability data on their
effluents.
Although there is a good deal of variation in the effluent loadings
determined for each type of effluent, characterization results are
summarized in table 24.
Table 24. Summary of Characterization Data (Averages)
Fish Processed
1. Groundfish Filleting
a) Dry Line
b) Wet Line
2. Salmon Processing
3. Herring
a) Filleting
b) Marinated
4. Shellfish
a) Lobster
b) Crab
5. Freshwater Fish
a) Combined Perch
and Smelt
BOD5
Lbs/1000 Ibs
raw product
4.5
18.0
28.2
22.0
215.0
25.0
40.0
4.5
Suspended Solids
Lbs/1000 Ibs raw product
1.5
15.0
19.7
21.0
85.0
5.5
20.0
2.3
The major waste streams are associated with the processing of salmon,
herring and shellfish. However, all major effluents associated with fish
processing are of sufficient strength to require some type of treatment.
In the majority of cases the removal of solids is adequate treatment to
protect the receiving environment as this will prevent a build up of
sludge around the effluent outfall with its consequent effect on dissolved
oxygen. Following screening the effluent should be discharged through
an outfall which allows sufficient tidal flushing action to dilute the
remaining effluent and thus minimize pollution problems.
440
-------
Bloodwater, stickwater and pumpout water arc the effluents of highest
strength associated with fishmeal production. Bloodwater and stickwater
should be recovered and pumpwater should be fine screened prior to
discharge to the receiving environment.
As stated previously fine screening will in most cases provide adequate
effluent treatment provided this is coupled with a well designed outfall.
In cases where the provision of this level of primary treatment produces
an effluent which still creates pollution problems, then either flotation
or biological treatment must be considered. In general most fish
processing plants do not have easy access to land on which lagoons of
adequate size can be built. This problem, coupled with the high cost of
less land intensive methods of biological treatment, would lead to the
use of flotation as an economical and practical method of secondary
treatment. Further, flotation provides some economic return in the form
of recovered sludge which can be recycled back to the fishmeal plant.
Acknowledgements
The authors wish to express their thanks to F.G. Claggett, Fisheries
Research Board of Canada for his valuable contributions to this paper.
441
-------
REFERENCES
1. BRODERSEN, K.TV, "Characterization of Fish Processing Plant Effluents
A Study of the Waste Characteristics of Fish Processing Plants
Located in the Maritime Region", Report prepared by Department of
Environment, Government of Canada, October (1971).
2. Canadian Plant and Process Engineering Limited, "Fish Processing
Wastes, A Study of Harbour Pollution Resulting from Fish Processing
in Shippegan, Lameque, and Caraquet, New Brunswick", for the New
Brunswick Water Authority, February (1970).
3. CHUN, M.J. £t £l_, "A Characterization of Tuna Packing Waste",
Proceedings 23rd Industrial Waste Conference, Purdue University,
786-805 (1968).
4. CLAGGETT, F.G., "Clarification of Wastewater Other Than Stickwater
from British Columbia Fishing Plants", Fisheries Research Board of
Canada, Vancouver, British Columbia, Technical Report No. 14 (1968).
5. CLAGGETT, F.G. and J. WONG, "Salmon Canning Wastewater Clarification,
Part I: Flotation by Total Flow Pressurization", Vancouver,
Fisheries Research Board of Canada, British Columbia, Circular No. 38,
January (1968).
6. CLAGGETT, F.G. and J. WONG, "Salmon Canning Wastewater Clarification,
'.'art II: A Comparison of Various Arrangements for Flotation and
Some Observations Concerning Sedimentation and Herring Pump Water
Clarification", Fisheries Research Board of Canada, Vancouver,
British Columbia, Circular No. 42, February (1969).
7. CLAGGETT, F.G., "A Proposed Demonstration Plant for Treating Fish
Processing Plant Wastewater", Fisheries Research Board of Canada,
Vancouver, British Columbia, Technical Report No. 197, (1970).
8. DELANEY, J.A. AND ASSOCIATES, "Georgetown Seafoods Limited, Georgetown,
Prince Edward Island, Study of Waste Treatment", for Department of
Regional Economic Expansion, Ottawa, November (1970).
9. ENVIRONMENT CANADA, "Annual Statistical Review of Canadian Fisheries",
2: 1954-1969, Economic Branch, Fisheries Service,, Ottawa (1971).
10. ENVIRONMENT CANADA1 "Study of the Effluent Characteristics from Fish
Processing Plants in British Columbia", Unpublished Report,
Environmental Protection Service, Pacific Regional Office, Vancouver
(1971).
11. ENVIRONMENT CANADA, "Study of Effluent Characteristics from Ground-
fish Processing Plants in the Maritime Region", Unpublished Report,
Environmental Protection Service, Atlantic Regional Office, Halifax,
(1972).
442
-------
12. LIMPRICH, H. (Problems Arising from Wastewaters from the Fish Industry)
IWL Forum, 66: 36 (1966).
13. MATUSKY, F.E. et_ al_, "Preliminary Process Design and Treatability
Studies of Fish Processing Wastes", Proceedings 20th Industrial Waste
Conference, Purdue University, 60-74, (1965).
14. NUNNALLEE, D. and B. MAR, "A Quantitative Compilation of Industrial
and Commercial Wastes in the State of Washington", Washington
State Water Pollution Control Commission, Olympia, Washington (1969).
15. RIDDLE, M.J., "Characterization and Treatability Study of the
Effluent from a Fish Processing Plant", M. Eng. Thesis, McMaster
University, Hamilton, Ontario.
16. SHAFFNER, J., "The Various Methods of Reducing the Waste Material
Being Discharged from the Fish Processing Plants In Lameque,
Shippegan and Caraquet, New Brunswick", Report submitted to New
Brunswick Water Authority (1970).
17. SHAWINIGAN ENGINEERING COMPANY LTD., AND JAMES F. MAC LAREN, LTD.,
"Water Resources Study of the Province of Newfoundland and Labrador",
for Atlantic Development Board, Appendices, _8_, September (1968).
18. SODERQUIST, M.R., et_ aJ_, "Current Practice in Seafoods Processing
Waste Treatment", Department of Food Science and Technology, Oregon
State University, Corvallis, Oregon, Report prepared for the
Environmental Protection Agency, Water Quality Office, Washington,
April (1970).
19. STANLEY ASSOCIATES ENGINEERING LTD., "Fish Processing Plants: Liquid
Waste and Receiving Water Study", Project for the Fisheries
Association of British Columbia, January (1971).
443
-------
BIOLOGICAL TREATMENT OF EGG PROCESSING
WASTEWATER
by
N. Ross Bulley*, F.W. Soper**, and L.M. Staley*
INTRODUCTION
Many problems exist in treating and disposing of food pro-
cessing wastewater. The egg grading and processing industry
is an example where basic information is unavailable for
designing biological treatment systems for wastewater.
This report is based on a study carried out to establish
basic biological oxidation characteristics of egg processing
wastewater. The laboratory studies were one part of an
overall study undertaken to assist a local company-"" which
was experiencing wastewater problems.
The plant originally stored their effluent in an anaerobic
lagoon, and then followed with spray irrigation onto pasture.
After complaints from neighbour's of obnoxious odors, the
company installed two concrete lined aerobic lagoons witn
surface aerators. The effluent from the lagoons was spray-
irrigated during dry weather, or stored in a third earthem
lagoon until spray-irrigation was possible. The syste.~ still
produced odors periodically and in view of a pending plant
expansion, the company found that they needed more basic
information before being able to decide on a solution to
their problem. Initially information was required on the
flow rate and pollution parameters of the raw waste, the
capabilities of the lagoons for odor control and BOD reduction
during both winter and summer conditions,and the possible land
requirements for final effluent disposal.
WASTE SOURCES AA?D CHARACTERISTICS
The company grades and washes about 325 cases of eggs per
day (30 dozen eggs per case), and processes about 600 cases
per day producing about 16,000 Ibs of liquid egg material.
* Dept. of Agricultural Engineering, University of British
Columbia, Vancouver, B.C.
** Pollution Control Branch, Water Resources Services,
Victoria, B.C.
*** Brookside Farms Ltd., Mt. Lehman Rd., R.R. #3,
Abbotsford, B.C.
444
-------
The combined operation produces a maximum of 12,000 Imp. gallons
ol effluent per day, having a BODr of about 6,000 ppm, with a
total solids content of about 7,000 ppm. The eggshells are
collected separately, augerec into a truck and disposed of in
a landfill operation. Otner characteristics of the wastewater
are shown in Table 1.
Table 1. Typical Egg Grading and Processing Wastewater
Characteristics
Analysis
BOD5
COD
T.S.
Kjeldahl-N
NH4 -M
N03 -N
PO ~ -P
Mg/1
6300
9780
6950
537
48
2
144
Three other characteristics of the waste should be noted and
are a function of plant procedure. During the cleaning of
the eggs a chlorine spray (100 ppm) is used in the processing
operation to control Salmonella. This cleaning water is used
continuously and is collected with other cleanup water con-
taining disinfectants and discharges into the lagoon for
treatment. Also at the end of an 8 hr shift, the egg washer
wastewater (pH 10) is dumped (150 gal) and arrives at the lagoon
in a slug load.
These procedures tend to produce conditions which could upset
any active biological system in the lagoons.
BASIS OF DESIGN
The basic system at Brookside uses two aerated lagoons in
series. Lagoon 1 has a four day and lagoon 2 an eight day
detention time when treating wastewater at the maximum plant
flow rate of 12,000 Imp. gal/day. The two 5 HP surface aerators
give complete mixing characteristics with no detectable settling
of solids. There is also complete oxygen dispersion throughout
the lagoons.
445
-------
LaLcratcrv Model Design
Data obtained through bench scale systems can be informative
but extremely hazardous to use in designing full scale treat-
ment facilities. However, realizing this limitation, a model
system was developed to simulate the particular aerated lagoon
treatment system at Brookside and which would also give the
more basic information required to design other systems.
Two complete model systems were constructed to be run in
parallel. The replicated experiments were felt to be required
due to the unpredictability of the biological system and would
give duplicate results for better interpretation of any
possible upsets.
The construction of the two stage aerated basin system was
from one-quarter inch plexiglass (Fig. 1). The main body of
the model consists of a rectangular volume, with a divider
partition with fixed overflow to provide the division between
the two stages. The bottom corners were provided with one
inch corner deflectors to minimize solids settling in the
corner extremities. Five liter and ten liter volumes were
fixed by the overflow of the first stage into the second stage
and by the final overflow respectively. Air was introduced
into each basin by diffuser stones connected to plexiglass
pipes and the flow rate controlled by needle valves. Small
variable speed laboratory mixers gave complete mixing and
dispersal of oxygen in each tank with no solids settling. A
lid was placed over the top of each system to minimize odor
during start up.
BATCH TREATMENT STUDIES
Batch treatment studies were used to determine basic informa-
tion on the characteristics and treatability of the waste-
water during aerobic stabilization. Two complete batch runs
were carried out, yielding four sets of data. The two models
were filled with 5 liters of egg processing wastewater on
the "A" side (5 liter basin) and aerated for 7 days. Daily
analyses was carried out on sample aliquots for BOD,.*, COD""
and TOC***.
Dissolved oxygen, pH and temperature were monitored. Dissol-
ved oxygen was controlled within a desirable range by varying
air flow rates. Stirring rates were maintained at sufficient
rates for complete mixing. Table 2 indicates the operating
parameters.
* BODc ~ Biochemical Oxygen Demand
** COD - Chemical Oxygen Demand
a** TOC - Total Organic Carbon, difference between total
carbon and inorganic carbon as analysed with
"Beckman Total Organic Carbon Analyser",
Model 915.
446
-------
Fig. 1. Laboratory Model of Two Stage Aerobic Treatment
System
447
-------
Table 2. Operating Parameters for Batch Treatment Studies
Parameters lst Batch Treatment 2nd Batch Treatment
D.O. 2-6 ppm (controlled) 2-6 ppm (controlled)
pH 7.6-8.9 (uncontrolled) 7.2-8.8 (uncontrolled)
Temp. 26°C Model 1 25°C Model 1
23°C Model 2 25°C Model 2
The pK in the first batch run was initially pH = 8.9 and
during the stabilization period, the pK fluctuated between
this upper limit and a lower of pH 7.6. In the second batch
run, the pH was neutralized at the onset from pH 8.8 to
pH 7.5 and fluctuated during the experiment between 7.2 and
8.8. Hence, the pH varied considerably but the system
indicated some buffering capacity and remained within a pH
range in which there would be minimal cell inhibition.
Results of Batch Studies
In order to facilitate planned research, an attempt was made
to correlate the parameters of BOD^, COD and TOC during
aerobic stabilization. It was found that BODg correlated
well with COD as indicated in equation [1],
BOD, = 0.8H COD - 910 [1]
o
r2 = .938
r = correlation coefficient
BOD5 and COD are mg/fc
As expected the BOD,, to COD ratio was not constant but
decreased dur
equation [1].
decreased during the aerobic stabilization as indicated by
The correlation between COD and TOC is represented by the
following:
COD = 3.1 TOC + 42 [2]
r2 = .987
COD and TOC are mg/t
Typical stabilization curves during the batch treatments are
shown in Fig. 2. If their decay rate follows the first order
rate equation then:
448
-------
CO
o
to
0
U
-------
_ , q
dt K c L3J
where c = concentration
k = rate constant
t = time
Rearranging and integrating gives the familiar equation
c = CQ e~kt [4]
c
It was found that a semi log plot of — vs time for the BOD^
data produced a straight line indicating that the kinetics of
the overall treatment process could be represented by a first
order rate equation. The rate constants(k) are given in
Table 3. The mean removal rate was 0.43/days.
Table 3 BODs Removal Rate Constants Batch Treatment
Batch Test 1
Model 1 k = 0.43/day 26°C
Model 2 k = 0.36/day 23°C
Batch Test 2
Model 1 k = 0.41/day 25°C
Model 2 k = 0.53/day 25°C
Mean removal rate constant k = 0.43/day
m
Qualitative Observations
Color; The color of wastewater undergoing biological
oxidation changed considerably during the stabilization
period as follows:
Day Color BOD. (mg/Jl)
5
1 greyish white
2 greyish brown
3 brown
4 orange brown
5 greenish brown
It was noted that the color was very indicative and could be
qualitatively related to the wastewater strength, in that
the analytical results could be predicted very closely by
examining color during the batch treatment of this waste-
water.
450
-------
Turbidity
The turbidity of the wastewater decreased considerably during
the stabilization period. This is indicative of the solids
hydrolysis taking place during stabilization.
Odor
During the initial stabilization, the wastewater exhibited
extremely noxious odors even though the system was completely
aerobic. This odorous condition decreased during the stabi-
lization period to almost no odor after four or five days.
The stabilized wastewater had an "earthy" odor, typical of
stabilized aerobic systems. The original odors were most
likely a result of organic sulfur groups and proteinaceous
materials, resulting in mercaptan and amine odors respectively.
Biological growths were evident on the basin walls within 24
hours after aeration and large floes developed during this
initial period. Oxygen transfer into these wall growths and
floes might not be adequate to maintain aerobic conditions
leading to anaerobic conditions at their centers which could
be responsible for the odors.
CONTINUOUS TREATMENT STUDIES
To determine the treatability of the wastewater under con-
ditions which were more representative of the plant operation
continuous treatment studies were carried out at 24°C and 5°C.
The processing v/astewater was stored in a 5°C cold room and
brought into the laboratory as required where it was con-
tinually mixed on a magnetic stirrer to prevent solids
settling. The model systems were continuously fed from this
reservoir using a ministaltic pump. The discharge from the
pump was split by a "Y" fitting, and discharged into the
5 Jl basins (1250 ml/day) above the liquid surface. The flow
to each basin was regulated by clamps. This continuously
mixed first stage then overflowed into the second stage,
basin B, maintaining a four day detention time in basin A.
Basin B, kept at a lower liquid level by means of the final
overflow, maintained an eight day detention time.
The liquid system was stabilized under constant continuous
feeding for at least two weeks after which COD analysis was
carried out each day on each basin of each model. When the
COD analysis showed little or no change for three successive
days, each basin of each model underwent full analysis.
Results of Continuous Treatment Studies
The analysis for the raw waste and for the effluent from each
of the two aerobic basins in series after equilibration had
been reached are shown in Table 4 for^experiments 1 and 2.
The results indicate that the waste will undergo a high
degree of treatment in these two stage aerobic systems. The
451
-------
TABLE 4
Analysis
1st Conti
BOD5
COD
T.S.
Kieldahl
-11
N03-N
2nd Conti
BOD5
COD
T.S.
Kieldahl
-N
NH4-N
Organic
-N '
N03-N
PO — P
u
Feed
TUOUS Rl
8,300
11,000
7,900
508
0.45
1UOUS P.I
7 ,000
8,670
6,280
555
76
479
1.75
265
Basin 1A Basin IB
mjy/1
in
4,900
6 ,780
4 ,140
438
0.60
in
2,700
3,650
3,210
468
165
303
6.5
90
640
2 ,180
3,260
174
27.5
550
1,580
2 ,800
162
17
145
188
80
Fil-
tered
Basin
13-
150
390
Basin 2A Basin 2B
mg/1
5,300
6,300
4 ,640
428
0.50
2 ,780
2 ,940
3,100
456
185
272
1.3
120
920
2 ,980
3,380
202
0.41
450
1,840
2 ,330
151
3
148
148
150
Fil-
tered
Basin
2B
100
320
452
-------
percentage reduction in BODr, COD, T.S. and Kjeldahl-N in each
of the experiments at room temperature and at 5°C is summarized
in Tables 5 and 6.
BOD Removal Rate K
The following formula can be derived and has been used to
describe BOD removal efficiencies in a completely mixed
lagoon which has reached a stabilized equilibrium (1).
Le _ 1
Lo 1+K t
or
„ % removal
[5]
_
" (100 - % removal) t
where Le = effluent BOD
Lo = influent BOD
t = time in days
K = BOD removal rate coefficient.
Using this equation, the BOD removal rate coefficients
(uncorrected for temperatures) were calculated for each
basin (Table 7).
During run No.l (Table 5) it can be seen that a very low
removal rate in Basin A was experienced in both models. This
would indicate that possibly a high pH , due to the caustic in
the feed or a high chlorine concentration, were affecting the
breakdown rate. This problem appears to have disappeared in
basin B resulting in a high degree of treatment. In study 2
a high rate of breakdown occurred in basin A and was followed
by an even higher rate in basin B. The lower rate in basin
A could again be due to the same problems as in run No.l, or
it could be due to hydrolysis and liquification of solids in
basin A being followed by breakdown and cell assimilation in
basin B.
The overall removal rates for the two basins in series was
still quite consistent even though removal rates within each
basin of the system varied. The average removal rate for
basin B is 0.65/day.
The reduced removal rates at the low temperature were to be
expected but even at 5°C, 78% BOD removal was achieved. This
gave an average BOD removal rate of 0.2 /day.
The temperature effect on the removal rate can be expressed
as :
K _ K Q (T-20) r
KT - K20oc B L
where G = temperature correction coefficient
T = temperature °C.
453
r - -,
L J
-------
u
o
d-
CM
H.
2:
H
<
W
Pi
H
CO
:D
o
o
o
o
~z.
W
M
O
W
I
W
K
CO
o
M
EH
:D
s
C9
<
rH
rH
O
0)
bC
m
p
CO
T3
C
O
0
£
0)
tO
o ^
0) «
[. | .;;
CQ
E CM
0
fc 0
P t ±j
oN°
V^
CM
CO
6 CM
O
k 0
fj-i -P
^^
T-1 » j
p £
CO 0)
CD ro r— O
co r~ LO CD
ro ro c — co
CO LO CM LO
tu I CD CM CM CD
p , <
W E CM
?-. 0
•H
m 3- 3- rH
j- a> ro ro
CD t~- CD r-
j~ r^ LO r^
oo ro CM CD
O CD CD OO
CD CO LO rH
5-i O ! i
4-'
1 r~( _
, 1 X
r-f O cs
r-« 1 C) ^-
( - "-
: 1
, \
k
o
tf*
o
I 03 I CM
1 £ rH ! CD
i o !
tj O '
i iJ-i -P
o
CO
CD
LO
CD
CD
O
C4
0-,
CM CM LO
CD CO LO
a>
(0
t i
CO
T3
C
o
o
G)
CO
a)
b2
-.
O
•z^
-p
(fl
3
0)
-p
6 E
- I
d
(X
LO
Q ^5
O O
CQ O
00
H
O
be k:
• 6 E E
^5 V_X **** N^.r'
"Z.
Lf) .
2 O Q to
3 O O
Pi CO O H
ftf
•u
rH
a)
oo cn
CD cn
I! II
C
o
•H
q
o
•H
•P -P
0 O
Q) d)
P t
o Q
o o
CQ CQ
o\° OP
i i i>
C C
0) 0)
3 3
0) Q)
T3 T3
(0 0)
fc f.
O (D
•P -P
rH tH
•H -H
O O
•P -p
(U QJ
Q) Q)
iH rH
rH rH
fK rrj
d)
-------
u
o
LO
H
H
CO
•X3 CM
C X>
O E CM
0 O
0 f-i O
CO PH -P
bi c\° !
S j ffl T3 ^
W ! -P 1 P-t p.< -P ]
^0 Q
O 'Pi T3 x"> '
3 ! rH C! =t.°
S W ' H fl> ^
M & 1 t P~
H < f-i CO
2 H ' CJ 6 r-i
o ' 2; > ! o
O ' M O !-, O
0 i PH 4-'
o w
PH jo, !
^_l
CJ
t— p.
u
M
C_)
M
[. ,
(D /^^
fci dP
* i ^
CO
1 *^,
-V r-l
/-* po I
0 ' R rH !
u o '
P4 Q> ' f-i O
j CO PH -P
S
-------
TABLE 7 BOD REMOVAL RATES FOR CONTINUOUS TREATMENT
Model 1 Model 2
Basin 1A Basin IB Basin 2A Basin 2B
Study 1
(24°C)
Study 2
(24°C)
Study 3
(5°C)
0.17 0.84
0.39 0.49
0.14 0.61
0.37 0.65
0.18 0.21
0.31 0.11
456
-------
Using this equation and the removal rates determined at 2>+0C
(K24 = 0.65/day) and 5°C (K5 = 0.2/day) a value for 9 was
calculated to be 1.07.
Eckenfelder ( 2 ) gives the following general values for 9 for
biological treatment processes:
Process 9
Aerobic lagoon 1.035
Aerobic-facultative
lagoon 1.07-1.08
Hence the calculated value is close to the typical values
found for this type of treatment. Since the experiments were
carried out at only two temperatures the value of 9 is only
an approximation but since the temperatures used are at the
extremes of the possible temperatures which might be experien-
ced in practice, there should be no sudden unforeseen reduction
in 9 with lower temperatures. This can occur when 9 values
are used in designing systems for operation at temperatures
lower than those used in the experimental determinations of K.
In basin A COD removal followed BOD removal (Table 5) as was
expected but in basin B COD removal was not as great as BOD
removal. This reduction in COD removal was also to be
expected as the oxidizable materials in the wastewater are
being converted to more stable forms which still exert an
appreciable COD but a lower BOD.
It is of interest to follow the change in the forms of
nitrogen in the basins (Table 4) at room temperature. In the
raw waste 86% of the nitrogen is in the organic fraction,
with the balance being in the form of NHij-N. In basin A at
equilibrium about 20% of the organic nitrogen had been con-
verted to NH^-N with a very slight increase in N03~N. In The
second basin B, both organic and NH^-H have decreased in
concentration being converted to NOo-N. A mass balance on
nitrogen indicates that about 40% of the total nitrogen has
been lost from the system presumably given off mainly as
NH3 to the atmosphere.
Qualitative Results for Continuous Treatment
Nutrient requirements: To ensure that adequate nitrogen
and phosphorous were available and low concentrations would
not be responsible for inhibited growth of cells, the BOD5 to
N and P ratios were calculated for the wastewater. Typical
ratios were:
BOD5 to N 13 to 1
BOD5 to P 26 to 1
Since ratios of BODs to N of about 32 to 1 and BODs to P of
150 to 1 ( 3 ) have been shown to be adequate in most cases,
457
-------
there appears to be an abundance'of nutrients in the waste-
water to support bacterial growth.
Solids settling: Although neither the time nor the
facilities "were available for complete coagulation, floccu-
lation and settling studies, some tests were undertaken on
model effluent settling.
The plant effluent (model feed) did not show any signs of
settling after more than 24 hours. This is probably due to
the colloidal nature of the solids system.
The model effluent, however, showed good settling with a
clear supernatant and a bottom cell sludge blanket.
Additions of aluminum sulphate increased flocculation
considerably resulting in higher settling rates. These
settling characteristics, together with the filtered effluent
BOD^ data of Table 4, indicate that clarification for the
treated effluent could be used as an efficient final stage
in the treatment process increasing the BODr removal from 93% to
98% and COD removal from 80% to 96%.
SUMMARY
Two laboratory wastewater treatment models were developed to
obtain biological oxidation characteristics of an egg grading
and processing plant wastewater discharge into existing
aerated storage lagoons. The laboratory models were operated
in batch and continuous feed mode at temperatures of 5°C and
24°C.
Qualitative observations indicated that wastewater color was
indicative of BODg values changing from greyish white at
4,000 mg/1 BOD5 to greenish brown at 800 mg/1 BODs. Odors
changed from an initial "noxious" to final "earthy" smell
after 4 to 5 days. The very poor clarification characteristics
of the wastewater were greatly improved by the aerobic treat-
ment and would make clarification of the final effluent
practical.
For the two stage continuous aerobic treatment model (4 days
and 8 days detention times in series) 93% BOD& and 80% COD
removals were found at 24°C.
For the batch treatment model the BOD5 mean removal rate
constant k was found to be 0.43/day at 25°.
m
For the continuous treatment model the BODc mean removal rate
constant K was found to be 0.65/day at 24°C and 0.2/day at
5°C. m
A nitrogen balance on the continuous treatment system indicated
a 40% loss in total nitrogen during the 12 day treatment at
24°C.
458
-------
Acknowledrc/ronts
The authors wish to acknowledge the cooperation and the
financial assistance of Brookside Farms Ltd. in conducting
this study.
References
1. Bartsch, E.H. and C.W. Randall. Aerated Lagoons - A
report on the state of the art. J. Water Pollution
Control Federation 43: 699, 1971.
2. Eckenfelder, W.W. In "Water Quality Engineering",
Barnes £ Noble Inc., New York, 1970,
3. Rich, L.G. In "Unit Processes in Sanitary Engineering",
John Wiley Inc., New York, 1963.
459
-------
EVALUATION OF RESEARCH AND DEVELOPMENT NEEDS
FOR THE FOOD PROCESSING INDUSTRY
Franklin J. Agardy, Ph.D. *
Introduction
It might be appropriate to review the background — where we have
been. I see the beginning in September 1967 when the Cost of Clean
Water Series was published by the Federal Water Quality Administration
and suddenly industry, and particularly the food processing industry,
became aware of the fact that somebody else was looking at them. It
is of value to note some of the information in the 1967 publication,
Series No. 3, which addressed the food processing industry. Interest-
ingly, it was projected that by 1972, the waste treatment state-of-the-
art would result in removals of 68 percent of BOD in the wastes, 77
percent of the suspended solids and about 19 percent of the total dis-
solved solids, and it was projected for 1977 that 73 percent of the
BOD, 82 percent of the suspended solids, and 25 percent of the total
dissolved solids would be removed. That was only some six years ago
and now that study reads like a comic book. I happen to have worked
on that study and I made other projections as to what I thought would
be the situation. My colleagues felt that my numbers were extreme and
they were laid to rest.
The next step came about more recently. The now "obsolete"
effluent limitation guidelines published through October of 1972
resulted from an industrial waste studies program sponsored by the
Environmental Protection Agency. Reviewing the food processing
industry, we found that, in addition to information on BOD and
suspended solids, which was available in 1967 from the industry,
the expanded list included pH and COD, and that accomplishment in
a six-year interval is called progress. However, the guidelines
also pointed out some other constituents that the food processing
industry must be concerned with in the way of characterization. This
included color, fecal coliforms, total phosphorous, temperature, TOC
* URS Research Company
San Mateo, California
460
-------
and, interestingly enough, TDS, which was recorded in 1967 but for which
data was missing in 1972. Presently, there is another EPA study under-
way. By the way, I was involved as a consultant to EPA on the study re-
ported in 1972 and URS Research Company is one of two firms working on
the survey being conducted presently. In addition to the parameters
included in the publication of 1972, the following parameters are being
evaluated: total suspended solids, total solids, total coliforms,
phosphate, lead, zinc, mercury, pesticides, PCB's, dissolved oxygen,
alkalinity, nitrogen, nitrates, and oil and grease.
So, in the short space of six years, we have moved from no infor-
mation to a voluminous amount of data that is going to be collected on
the industry and, believe me, treatment will have to be accomplished
because in rather short order, perhaps in October of this year, there
will be limitations on virtually every one of the constituents listed.
There were two other events which, I feel, are historic — two
events which, I feel, will have an even more significant impact upon
the industry than the 1972 Clean Water Act. The first of these was
the 1969 National Environmental Policy Act, a rather innocuous act
referred to as NEPA. This act stimulated many states to pass legisla-
tion concerning environmental quality and industry will soon discover,
if it has not already done so, that not only will new treatment facili-
ties be required to meet effluent requirements but industry will have
to see to it that the treatment facilities meet general environmental
and ecological constraints placed on the industry by the local communi-
ties as well as state and federal governments.
The other action, also a seemingly inno"cuous act, the 1899 Permit
Program, having been resurrected from the dead, lasted about two years
and was laid to rest with the passage of the 1972 Water Quality Act.
In its brief life, it did establish, rather magnificently, the require-
ment for industry to monitor their effluents and to report the results.
The very fact that information filed under the 1899 Act is still sitting
in somebody's office in Washington, and that most industries filed for
461
-------
permits and have not received a response, does not change the situation.
The 1973 Conference
Thus, we have what I call a rather recent history of where the
industry has been and where it is going. Now, let us turn our attention
to this conference and comment on the proceedings. It is notably appro-
priate that the keynote speaker was an attorney. Let this sink in. He
was a lawyer talking to us, not in terms of pollution control, waste
treatment problems, and design parameters, but rather he was talking
law and he quoted a very interesting aspect of the 1972 Water Quality
Act. He said July 1, 1977, the target date. The date was the signifi-
cant element of his presentation and I will return to this point later.
Essentially, he ran up the flag and went back to 1956 when the federal
government became involved in pollution control and he attempted to trace
the legislation to date. He presented, I think, rather conclusively that
with each piece of legislation, the requirements became tougher and
tougher, and while he did not say so directly, he implied that industry
tended to sit back and watch and wait and not respond very actively,
although the flag was there. To those in the industry who are going to
suffer in the next several years, all I can say is that the flag was up
but industry was slow to salute. Now the penalty will be double, a fine
for failure to salute and a permit fee in order to salute. Industry
will have to pay for each "privilege."
Reviewing the technical portion of the conference, we find a num-
ber of papers which fell into four basic categories. While I would like
to go into each category in detail, reviewing selected content, time
really does not permit it. However, I am going to review the substance
of each area.
A large number of papers addressed the subject of problem defini-
tion and here, I think, is an important element because industry has
spent considerable time hassling with problem definitions. Some people
462
-------
assume, and perhaps correctly, that industry is satisfied with this ap-
proach on the assumption that what is ill-defined does not have to be
resolved.
The second set of papers dealt with in-plant modifications and
attempts to reduce water use by industry. This certainly makes economic
sense. It was pointed out by several speakers that when we reduce water
use, we often get reductions of waste loads.
The third set of papers is perhaps more important because they
dealt with by-product recovery and because they did point out, in
several cases, practical applications to by-product recovery and in-
cluded engineering design information necessary to the industry.
The fourth group dealt with treatment processes, and papers in-
cluded treatment of stillage wastes and land disposal. Also, treatment
schemes for distilling wastes, meat packing, starch wastes, and others
were developed. Thus, we do have a collection of papers here that gave
definitive information ranging from pilot scale to actual field install-
ation studies with some design and, appropriately, cost data.
Conference Highlights
As I see it, there were four speakers whose words highlighted this
conference, at least from where I was sitting and viewing the situation
as I have to confront it virtually everyday in my role as a consulting
engineer and a researcher. The first of these has to do with a slide
which Professor Soderquist showed Monday morning. He sort of threw the
slide up and casually commented on it, but it was probably the most sig-
nificant thing in his paper because he showed a relationship between
what he called a social optimum cost versus a private sector (industry)
optimum cost to arrive at pollution control objectives. The social
optimum cost is a constraint posed either by EPA or state agencies and
the social optimum cost is, at present, considerably higher than industry
had budgeted in its private sector optimum cost. So, somewhere along the
463
-------
line, we are going to have to reconcile these two numbers or go broke.
This hypothesis is a significant point which was made casually but
nevertheless should not be overlooked.
The second point was made by a i-ather young, and perhaps somewhat
inexperienced speaker, Mr. Hassett, who talked about cost alternatives
to industry. He tried to develop a strategy of industry pretreatment
versus municipal service charges. Again, I feel this is significant
because there are alternatives which are going to have to be explored
by industry. However, unless sound definitive information regarding
the feasibility of these various alternatives, in terms of cost, is
available, solutions will not be readily forthcoming. Here we had a
speaker who attempted to develop trade-offs. I do not necessarily
agree with the answers he came up with because he appeared to stress
pretreatment and, therefore, biased his presentation, but the point
was significant. He tried to address economic alternatives and is able
to present alternatives to his clients.
The third and most "ideal" solution was presented by Dr. Gallop
Monday evening. Unfortunately, the majority of attendees of this con-
ference were not present at his talk because of the late hour. Pro-
fessor Gallop, of Canada, gave a rather stimulating talk. Really, the
first 10 minutes should have been recorded and reproduced for the pro-
ceedings. Basically, he said that food processing is really a wastewater
business and the commercial product is really a "by-product." The point
he made was that we must begin looking at the industry from a total sys-
tems concept approach. We cannot continue optimizing production while,
and as he so aptly put it, burying the sanitary pipes under the floor
where they cannot even be found. We must view an entire plant as a
"total system" with the waste element being as important as or, in some
cases, more important than the product being put out for commercial sale.
The fourth speaker, whom I would like to single out, was Dick
Stephen-Hassard from Hawaii for he, in fact, demonstrated a total systems
464
-------
concept for the sugarcane industry. In this case, on the Island of
Hawaii, they are reviewing their industry from the field to the furnace,
and he made the point, rather emphatically, that at one of their plants,
the primary function is going to be the generation of power and the
secondary function, or by-product, is going to be sugar processing. I
think this is perhaps the most dramatic illustration of what many of
the companies, which make up the food processing industry, are going
to have to address themselves to. We must credit this approach a total
systems approach. We can no longer develop solutions in terms of a
series of bits and pieces connected up, modified and "accommodated."
It is simply not going to work. What it will accomplish is to put a
lot of companies out of business. I cannot conclude any differently
when I see major automotive manufacturers, who represent the most sig-
nificant contribution to our gross national product, seemingly unable
to convince our government, and particularly Mr. Ruckelshaus, of the
validity of their point regarding pollution control devices. I do not
see the food processing industry exerting any greater leverage. Face
the fact that when the requirements for effluent standards are released,
industry will have to meet them, and we are not going to be able to meet
them piecemeal.
I feel that these four papers dictated a strategy where most other
papers were, what I call, tactical, and I will say more on this subject
later. I commend those speakers because they were talking about solu-
tions, not problems, but hard definitive solutions.
The Future
What kind of direction do we need? Where do we go from here? Let
us review the facts, the status quo, so to speak. It is fact that the
1972 Water Quality Act is law and that there is a definitive time schedule
in the law for implementation of effluent standards and treatment require-
ments. When industry sees the numbers, there will be some cries of an-
guish. However, there is not going to be very much point in arguing. I
465
-------
believe that EPA has tired of excuses. They have asked, too long, for
information that has not been forthcoming from industry,,
It is also a fact that user charges are being developed and are
going to be with us for t* long time. The City of Los Angeles has al-
ready sent out 66,000 copies of their regulations to local industry.
I am of the opinion that many of those industries discharging to munici-
palities face a worse problem than those who have been treating their
wastes and discharging directly to a receiving water.
It is also a fact that citizens now have the right to sue a "pol-
luting" industry. This is in the 1972 Act, but more significantly, the
National Environmental Policy Act and parallel state acts, particularly
in California, give the citizen the right to take an industry to court
on general environmental and ecological grounds. The people are doing
it and they are getting injunctions against industry and they are bring-
ing about temporary closures. This is not the federal government, this
is citizen action, and it is not a federal employee with a degree in
engineering who is making the decision, it is a judge who is interpret-
ing the law and ruling that the citizen has the right to demand environ-
mental equity.
In an excellent paper given at the AIChE Conference in Southern
California last November, Mr. Milton Beychok of Fluor Engineers and
Constructors pointed out that for industries planning new facilities,
the National Environmental Policy Act or various state environmental
quality acts are going to be a much greater deterrent to the development
of new facilities than any guidelines promulgated by EPA. He is emi-
nently correct in the position that most industries do not have the
foggiest idea of what these environmental acts contain. They usually
find out when they are dragged into court, and by then, they are on the
losing side.
466
-------
With these facts behind us, where should this conference go and
what do we have to do in the intervening years between now and July 1
of 1977? I stress a "solution orientation" as opposed to "problem
definition," because I feel that we can no longer afford the luxury
of studying problems; we must develop solutions. I would like to see
the next several conferences aimed at the development of a strategy
for meeting treatment requirements. To achieve this goal, I see a
series of finite objectives to be addressed. The first of these ob-
jectives concerns the development of a handbook or guideline for the
industry on monitoring. Rather than let each plant manager suffer
through the difficulties of developing an extensive monitoring program,
we should prepare guidelines for the industry which would indicate the
type of tests which will have to be run, the monitoring equipment
available, the precise techniques to be used in the analyses, and the
typical costs associated with collecting and analyzing data. I would
also hope that the question of equipment reliability and data reli-
ability could be addressed. I feel that the people who contribute to
this conference do have tho capability to put this information together
and make it available to the industry. I believe this to be a critical
step and something which certainly could be accomplished by next year.
A second objective concerns the consolidation of information which
we presently have across the industry on water reuse and reduction.
Several speakers have discussed this point. Let us collect the infor-
mation together and evaluate it. Let the conference have a panel to
address this issue. Let us also stress the economics of water reuse
and reduction. What will the cost be or possibly the savings gained
by reducing water use 20 percent or 30 percent or 40 percent? Let us
convert this information to dollars and cents.
Another panel should address the area of unit process modification.
Again, a consolidation of all of the information available to this in-
dustry based on prior studies and based on information which is forth-
coming or translatable from other industries should be consolidated and
467
-------
definitive unit process modifications shown and explained. Let me stress
again the need for practical design information coupled with estimates of
cost for these systems.
A fourth objective has to do w.ith the subject of by-product recovery.
This section should address not only the technology of by-product recov-
ery but also the economics of by-product recovery and sale. It is not
sufficient to say that technology allows us to convert a certain type of
waste into a by-product. We must also establish whether or not the market
for the by-product exists, and if it does exist, is it a regional or
national market. We must also determine what the present prices are for
this material and whether or not the by-product recovery scheme is com-
petitive with raw materials. Clearly, an engineering solution in terms
of by-product recovery is insufficient if the production of x-tons of
material suitable, let us say, as a livestock feed supplement cannot be
readily utilized because of price competition or because of a shipping
constraint. In this example, the only thing which has been contributed
by the engineering solution is a solid waste problem which has to be ad-
dressed. I submit that we have qualified people in this industry who are
capable of putting triis information together and who are capable of making
a fair and equitable evaluation of the situation.
Several speakers directed their remarks at land disposal as an al-
ternative to treatment and discharge to receiving waters. This is a
process which has been used for many years by this industry, but recently
a new look at land disposal has emerged particularly as a result of inter-
est shown by the Corps of Engineers and the Environmental Protection
Agency. It does appear that in the face of a zero discharge posture, the
alternative of land disposal becomes very appealing. Ho>wever, we must
address the engineering of land disposal systems in greater detail. We
must also review the significance of the soil mantle as a treatment mode
and we must answer the question of how long the soil mantle can accommodate
wastes. We must also explore how long it might take before we get a break-
through of pollutants to the groundwater table. This is particularly
468
-------
relevant because in today's vernacular the Environmental Protection Agency
is talking about discharges to streams, navigable waters and marine envi-
ronment, etc. However, it is clear that the next logical step is going
to be reviews of effluent discharges to groundwater systems. So, we must
begin looking at land disposal with a greater intensity and recognize
this treatment scheme as a very viable treatment alternative.
I have already discussed the implications of a total systems approach
within the industry. I really cannot say it any better than Professor
Gallop did on Monday evening or show you the potential results any more
dramatically than Dick Stephen-Hassard of Hawaii did. The industry must
open its eyes to this approach, particularly with regard to the development
of new facilities. The present approach of simply adding on elements to
existing facilities in the hope that each increment will satisfy the pre-
sent requirement will ultimately fail to meet 1977 limitations. I would,
therefore, like to see a panel address this question of a systems approach
and at least delineate the steps involved in reviewing a plant in this
concept.
I discussed earlier the significance of pretreatment as opposed to
direct discharge to municipal systems. Needless to say, the strict inter-
pretation of the 1972 Water Quality Act will place a certain pretreatment
requirement on industry regardless of the capability of the municipality
to handle the waste. However, to broaden the subject, I would like to
see the alternatives of pretreatment and municipal treatment coupled with
the consideration of developing regional treatment facilities which might
bring together partially treated waste from a number of industries and
municipalities within a given region. This approach is presently being
tried in Texas where the Gulf Coast Waste Disposal Authority acts as the
centralized waste handling agency for a mix of industries and municipali-
ties. Perhaps some of you are familiar with this operation, but I would
like to give some emphasis to it. There are tremendous advantages to
this approach if properly employed. California passed a law last June
which allows this type of regional agency to be established. The advantage
469
-------
to industry is that the burden for meeting state and federal requirements
falls to the regional agency rather than to each individual contributing
partner. Further, the state can sell bonds to cover the cost of operating
the agency. The industries who are contributory to the centralized fa-
cility are partners in the enterprise and essentially guarantee the bond.
In turn, industry turns over title of its existing facilities to the new
agency and industry is now able to write off the cost as an "operating
cost" rather than a "capital cost." It is only necessary to review the
tax structure to appreciate the significant gain to industry from this
type of approach.
I would further encourage the conference to act as an information
center for interpretation of federal and state laws which apply to the
industry. I would like to see a panel consisting of process engineers,
sanitary engineers, management, regulatory representatives, and environ-
mental lawyers discuss the full spectrum of implications of the various
water quality and environmental laws.
I would like to see a paper, at this conference next year or in
years hence, address an updated review of the cost alternatives to
industry to meet the federal and state requirements. It is significant
to note that the 1972 Water Quality Act does require a cost/benefit
analysis to be made in order to justify pollution control measures for
industry.
Finally, it is obvious that most of the solutions forthcoming to
meet federal and state requirements will create large quantities of
solid wastes. I feel that this subject must also be addressed in greater
detail so that we fully appreciate the implication of an expanded solid
waste handling problem.
Summary
Let me return to the subject of strategy. Industry must face the
ever increasing demand placed on it by the 1972 Water Quality Act and
470
-------
REGISTRATION LIST
ANTHONY ADAMCZYK
New York State Dept. of
Environmental Conservation
Bureau of Industrial Wastes
50 Wolf Road
Albany, NY 12201
FRANKLIN J. AGARDY
URS Research Co.
155 Bovet Road
San Mateo, CA 94080
LOUIS D. ALBRIGHT
University of California
Dept. Agricultural Engineering
Davis, CA 95616
HENRY ALLEN
Gerber Products
460 Buffalo Road
Rochester, NY 14602
JONATHAN ANSLEY
Boutell Co., Inc.
1300 Clinton Ave. S.
Rochester, NY 14620
ROGER ATHERTON
Dept. of Agricultural
Riley-Robb Hall
Cornell University
Ithaca, NY 14850
DALE BAKER
Dept. of Agricultural
Riley-Robb Hall
Cornell University
Ithaca, NY 14850
Engineering
Engineering
R.C. BAKER
Director, Food Science &
Marketing
100 Rice Hall
Cornell University
Ithaca, NY 14850
MARTHA I. BEACH
N-Con Systems Co., Inc.
308 Main St.
New Rochelle, NY 10801
CHARLES BELKNAP
Beech-Nut, Inc.
Canajoharie, NY ,13317
C. REESE BERDANIER, JR.
USDA - SCS
2939 Tallow Lane
Bowie, MD 20715
S. BERNSTEIN
Amber Labs Division
Mil brew, Inc.
330 S. Mill Street
Juneau, WI 53039
WARREN V. BLASLAND, JR.
O'Brien & Gere
1304 Buckley Road
Efex 1181
Syracuse, NY 13201
WILLIAM H. BOUCK
O'Brien & Gere
1304 Buckley Road
Syracuse, NY 13201
WAYNE A. BOUGH
Georgia Experimental Station
Dept. Food Science
Experiment, GA 30212
J.R. BOYDSTON
Chief, Industrial Wastes Branch
Pacific Northwest Environmental
Research Laboratory
200 SW 35th Street
Con/all is, OR 97330
473
-------
DAN BROOKS
National Canners Association
1600 S. Jackson Street
Seattle, WA 98144
LEO BRIAND
NYS Dept. of Environmental Cons.
50 Wolf Road
Albany, NY 12201
WILLARD R. BROSZ
Green Giant Company
Research Center
Food Science Department
LeSueur, MN 56058
N. ROSS BULLEY
University of British Columbia
c/o Dept. of Agricultural Engineering
Vancouver 8, B.C., CANADA
R.F. FURGHARDT
RJR Foods, Inc.
P.O. Box 3037
Winston-Sal em, NC 27102
DONALD CALHOUN
Graduate Student
Cornell University
Riley-Robb Hall
Ithaca, NY 14850
DENNIS J. CANNON
EPA-Technology Transfer
Xerox Building, Rm. 400
Washington, DC 20460
ROY E. CARAWAN
North Carolina University
Food Science Extension
129 Schaub Hall
Raleigh, NC 27607
B.L. CARLILE
North Carolina State University
330 Williams Hall
Raleigh, NC 27607
JAMES V. CHAMBERS
University of Wisconsin
Department of Food Science
River Falls, WI 54022
474
VINOD CHAWLA
Environment Canada
Waste Water Technology Center
P. Box 5050
Burlington, Ontario, CANADA
RICHARD D. CHUMNEY
New Jersey Dept. of Agriculture
P.O. Box 1888
Trenton, NJ 08625
F.G. CLAGGETT
E P Service
1437-54 Street
Delta, British Columbia, CANADA
MAX W. COCHRANE
Environmental Protection Agency
200 SW 35th Street
Con/all is, OR 97330
ARTHUR COPPINGER
Gold Seal Vineyards
Hammondsport, NY
DAVID L. CUMMINGS
Tri-Aid Sciences, Inc.
161 Norris Drive
Rochester, NY 14610
DOMENIC DEFELICE
RD #1 Box 290 B
Geneva, NY 14456
G.H. DHAWAN
Electrohome Limited
809 Wellington Street, N.
Kitchener/Ontario, CANADA
FRANK DEITCH
Libby, McNeil, and Libby
555 W. 115th Street
Worth, IL 60482
NORMAN DONDERO
Cornell University
Department of Food Science
Stocking Hall
Ithaca, NY 14850
KENNETH DOSTAL
Industrial Wastes Branch - EPA
200 SW 35th Street
Corvallis, OR 97330
-------
RICHARD DOUGHERTY
Purdue University
Dept. of Horticulture
West Lafayette, IN 47907
D.L. DOWNING
Dept. of Food Science & Technology
NYS Agricultural Exp. Station
Cornell University
Geneva, NY 14456
GLENN W. DUNKELBERGER
Gilbert Associates, Inc.
525 Lancaster Avenue
Reading, PA 19603
PHILIP B. DWOSKIN
USDA - Econ. Research Service
500 12 Street, S.W.
Washington, D.C.
RUBEN A. ECHANDI
Blue Star Foods, Inc.
1023 Fourth Street
Council Bluffs, 10 51501
T.R. EDGERTON
T.R. Edgerton Company
607 E. 90th Terrace
Kansas City, MO 64131
ROBERT H. EINARSEN
Triangel E By-Products Co., Inc.
P.O. Box 471
Harrisburg, VA 22801
EUGENE E. ERICKSON
North Star Research & Development Inst.
3100 38th Avenue, S.
Minneapolis, MN 55406
WILLIAM F. ESCUDERO
Carnation-Contadina Foods
135 N. Morton Blvd.
Modesto, CA 95354
T.C. EVERSON
Amber Labs. Division
Mil brew, Inc.
330 S. Mill Street
Juneau, WI 53039
ROBERT C. FARO
Dept. Civil Engineering
Syracuse University
Syracuse, NY 13210
JOHN W. FARQUHAR
American Frozen Food Inst.
919 18th Street, N.W.
Washington, DC 20006
GUILDORD 0. FOSSUM
Civil Engineering Dept.
University of North Dakota
Grand Forks, ND 58201
S.L. FREEDMAN
The Carborundum Co.
P.O. Box 337
Niagara Falls, NY 14302
DOUG FRIEND
Friend's Lab. Service
30 Lincoln
Waverly, NY 14892
R.A. GALLOP
Head, Food Science Dept.
University of Manitoba
Winnipeg, Manitoba
R3T 2N2, CANADA
J.R. GEISMAN
Ohio State University
2001 Fyffe Court
Columbus, OH 43201
R.E. "BOB" GERHARD
Mgr., Industrial Sales
George A. Hormel & Company
Env. Pollution Control Division
P.O. Box 800
Austin, MN 55912
LOUIS C. GILDE
Campbell Soup Company
Campbell Place
Camden, NJ 08101
F.S. GIVENS
Niagara-Mohawk Power Corporation
300 Erie Boulevard, West
Syracuse, NY 13202
475
-------
ARYE GOLLAN
Hydronautics Inc.
Pindell School Road
Laurel, MD 20810
MIGUEL A. GONZALEZ
University of Puerto Rico
Agricultural Experiment Station
Food Technology Laboratory
Upsala #256
College Park, Rio Piedras
Puerto Rico
PHILIP R. GOODRICH
Agricultural Engineering Dept.
University of Minnesota
St. Paul, MN 55101
JOHN H. GREEN
US Dept. of Commerce
NOAANMFS
Fishery Products Tech. Laboratory
Regents Drive
College Park, MD 20740
BARBARA GREENOUGH
Lockheed Missiles & Space Co.
D62-40 B151
P.O. Box 504
Sunnyvale, CA 94088
JAY S. GRUMBLING
Box 477
c/o Gentech Services
Morrisville, NY
MAURICE GUERRETTE
NYS Dept. of Agriculture & Markets
Building #8
State Campus
Albany, NY 12226
C. FRED GURNHAM
Gurnham & Associates Inc.
223 W. Jackson Boulevard
Chicago, IL 60606
CALEB HALL
Marion Food Corporation
60 S. Main Street
Marion, NY 14505
Y.D. HANG
Dept. of Food Science & Tech.
NYS Agricultural Experiment Sta.
Food Research Lab.
Cornell University
Geneva, NY 14456
W. JAMES HARPER
Ohio State University
2121 Fyffe Road
Columbus, OH 43210
WILLIAM HART
Sweco, Incorporated
P.O. Box 197
134 Main Street
Acton, MA 01720
Q. DICK STEPHEN-HASSARD
C. Brewer & Co., Ltd.
P.O. Box 1801
Hilo, Hawaii 96720
ALAN F. HASSETT
O'Brien & Gere Engineers, Inc.
P.O. Box 1181
Syracuse, NY 13201
HARRISON L. HATCH
Carnation Co. - Contadina Foods
5045 Wilshire Boulevard
Los Angeles, CA 90036
LAWRENCE L. HEFFNER
Extension Service - USDA
Washington, DC 20250
ELIZABETH HENDERSON
Auburn University
Dorm 8, Room 219
Auburn, Alabama 36830
H.A. HENDERSON
Tennessee Valley Authority
Muscle Shoals, Alabama 35630
WILLIAM E. HEUCKROTH
Ralston Purina Company
835 South 8th Street
St. Louis, MO 63188
476
-------
WALTER HILDEBRANDT
Franklin County Cheese Corporation
Endsburg, VT 05450
GILBERT F. HILL
Gilbert Associates, Inc.
525 Lancaster Avenue
Reading, PA 19603
RICHARD W. KLIPPEL
O'Brien and Gere
1304 Buckley Road
Syracuse, NY 13201
MARSHALL KRAUSE
Silver Floss Foods
Eagle Street
Phelps, NY 14532
VACLAY KRESTA
Department of Fisheries
and Environment
Centennial Building
Fredericton, N.B.
CANADA
JOHN M. KROCHTA
USDA
800 Buchanan Street
Berkeley, CA 94710
GERALD D. KUHN
Pennsylvania State University
Dept. of Horticulture
103 Tyson Building
Univeristy Park, PA 16802
CARL E. LANNING
Eastern Milk Producers Coop.
Kinne Road
Syracuse, NY 13214
DENNIS LARSON
Michigan State Extension Service
Agricultural Engineering Dept.
Michigan State University
East Lansing, MI 48823
PAUL F. LEAVITT
Gerber Priducts Company
445 State Street
Fremont, MI 49412
R.A. LEDFORD
Cornell University
Stocking Hall
Ithaca, NY 14850
C.Y. LEE
NYS Agricultural Experiment Sta.
Food Research Laboratory
Dept. of Food Science and Tech.
Geneva, NY 14456
SERGE LESSARD
Labrecque, Vezina and Assoc.
3300, Cavendish #385
Montreal 261
Quebec, CANADA
R.G. LIGHT
University of Massachusetts
Agricultural Engineering Bldg.
Amherst, MA 01002
GEORGE LINDSAY
Environment Canada - EPA
P.O. Box 2406
Halifax, Nova Scotia
CANADA
JESSE LUNIN
USDA - Soil Scientist
USDA, ARS, NPS, SW&A Room 233A
North Building - ARC-West
Beltsville, MD 20705
DAVID N. LYONS
EPA, Office of Permit Programs
Washington, DC 22306
I.E. MCCARTY
University of Tennessee
Food Technology and Science Dept.
Knoxville, TN
JOHN McCULLOUGH, R.S.
The Great A&P Tea Company NYC
317 Madison Avenue
Hampton .Manor
Rensselaer, NY 12144
477
-------
A.D. MCELROY
Midwest Research Institute
425 Volker Boulevard
Kansas City, MI 64110
KEN R. MCMILLAN
General Foods Ltd.
520 William Street
Cobourge, Ontario
CANADA
PAT McNELIS
Environmental Relations
10 Dougal Lane
East Northport, NY 11731
CHARLES V. McREYNOLDS
Blue Star Foods, Inc.
1023 Fourth Street
Council Bluffs, 10 51501
DONALD MACGREGOR
Tri-Aid Sciences, Inc.
161 Norris Drive
Rochester, NY 14610
RALPH MANNING
Delaware River Basin Commission
P.O. Box 360
Trenton, NJ 08603
JOHN H. MARTIN, JR.
Cornell University
Dept. of Agricultural Engineering
Riley-Robb Hall
Ithaca, NY 14850
ROBERT W. MASON
EPA
26 Federal Plaza
New York, NY 10007
DR. MORRIS G. MAST
Pennsylvania State University
226 Animal Industries Bldg.
University Park, PA 16802
N. DENNIS MEANS
Hershey, Mai one and Associates
2480 Browncroft Boulevard
Rochester, NY 14625
JAMES G. MEENAHAN
Johnson and Anderson, Inc.
Box 1066
2300 Dixie Highway
Pontiac, MI 48056
THOMAS MERRILL
Sheffield Chemical
Norwich, NY 13815
ROBERT MICHEA
Ministry of the Environment
275 Ontario Street
Kingston, Ontario
CANADA
VERLIS MILLER
National Fruit Prod. Co., Inc.
P.O. Box 609
Winchester, VA 22601
A.J. MONTA
Welch Foods, Inc.
2 South Portage Street
Westfield, NY" 14787
STANLEY T. NADOLSKI
John S. MacNeill, Jr., PE-LS
222 Tompkins Street
Cortland, NY 13077
RALPH NITZ
The Heil Company
3000 W. Montana Street
Milwaukee, SI 53201
PAUL 0'BOYLE
Calgon Corp. - Waste Mgmt. Div.
The Inwood Building
Syracuse, NY 13219
HAROLD T. PEDERSON
Foremost Foods Company
Foremost R&D
6363 Clark Street
Dublin, CA 94556
JOHN A. PERELL
Wallerstein Co. (Deerfield, IL)
P.O. Box 55
Ham! in, NY 1446-1
478
-------
PAUL PIECZONKA
City of Lackawanna
18 Cottage Place
Lackawanna, NY 14218
CPT. THADDEUS J. PIECZONKA, JR.
U.S. Army
1st USA Medical Laboratory
Ft. Meade, MD 20755
JACK W. RALLS
National Canners Association
1950 Sixth Street
Berkeley, CA 94710
JAMES REIDY
U.S. EPA
26 Federal PI a.
Room 807
New York, NY 10007
ANDREW C. RICE
Taylor Wine Company, Inc.
Hammondsport, NY 14840
M.J. RIDDLE
Canadian Dept. of Environment
EPA
Ottawa, Ontario K1A OH3
CANADA
ROBERT A. RINDO
0-AT-KA Milk Products Coop., Inc.
Cedar & Ellicott Streets
Batavia, NY 14020
RALPH L. ROBBINS, JR.
Sheffield Chemical
Woods Corners
Norwich, NY 13815
CHRIS ROBERTS
Contadina Foods
P.O. Box 29
Woodland, CA 95695
DAN ROBISON
US EPA Region X
1200 6th Avenue
Seattle, WA 98101
MIKE RUDD
American Pollution Prevention Co.
800 Flour Exchange Building
Minneapolis, MN 55415
PAUL RUSSELL
Harnish & Lookup Associates
615 Mason Street
Newark, NY 14513
WILLIAM M. RYAN
Univ. of California - Davis
P.O. Box 418
Davis, CA 95616
HERBERT H. SALSBURY
Supervisor, Environmental Control
Campbell Soup Company
Napoleon, OH 43545
DAVID A. SANBORN
The American Distilling Co.
South Front Street
Pekin,, IL 61554
JIM SANTROCH
EPA
200 SW 35th Street
Corvallis, OR 97330
JACOB SAVAGE
Stanford Research Institute
333 Ravenswood Avenue
Building 28
Menlo Park, CA 94025
JOHN R. SCHAUB
Economic Res. Service, USDA
Washington, DC 20250
R.K. SCHMIDT
Ecodyne Corporation
Smith & Loveless Division
Kansas City, Kansas
WILLIAM A. SCHMIDT
Campbel1 Soup Company
Campbell Place
Camden, NJ 08101
479
-------
E.D. SCHROEDER
Dept. of Civil Engineering
U. of California
Davis, CA 95616
EDWARD SEGEL
U.S. Brewers Association
1750 K Street, N.W.
Washington, D.C. 20006
R.S. SHALLENBERGER
Dept. of Food Science
and Technology
NYS Agriculture Exp. Station
Geneva, NY 14456
NORMAN I. SHAPIRA
Hydronautics, Inc.
7210 Pindell School Road
Laureli MD 20810
RONALD E. SHARPIN
Metcalf and Eddy
1200 Statler Building
Boston, MA 02116
KIM SHIKAZE
Department of Environment
EPS
Ottawa K1A OH3
Ontario, CANADA
H.H. SHOCKEY
National Fruit Product Co;, Inc.
P.O. Box 609
Winchester, VA 22601
WILLIAM SIDEREWICZ
Cornell University
1093 Warren Road
Ithaca, NY 14850
CLIFFORD B. SMITH
Ralston-Purina Company
835 South 8th
St. Louis, MO 61388
JAMES L. SMITH
Colorado State University
Department of Agr. Engineering
Fort Collins, CO 80521
JAY H. SMITH
USDA-ARS
Snake River Conser.
Rt. 1, Box 186
Kimberly, ID 83341
Res. Center
WILLIAM SONNETT
EPA
Office of Permit Programs
Washington, DC 20460
SOUZANA SOTIRACOPOULOS
Cornell University
Department of Food Science
Stocking Hall
Ithaca, NY 14850
DAVID SPRAGUE
Elmi re Road
Ithaca, NY 14850
ALFRED L. STAFFORD
Virginia Dept. of Agriculture
1444 E. Main Street
Richmond, VA
D.F. SPLITTSTOESSER
NYS Agr. Experiment Station
Dept. of Food Science & Tech.
Food Research Laboratory
Geneva, NY 14456
JACK STAUFFER
Stauffer Chemical Company
Westport, CN 06880
JOHN L. STEIN
Anheuser-Busch, Inc.
Engineering Department - Bldg. 3
721 Pestalozzi Street
St. Louis, MO 63118
RICHARD W. STERNBERG
National Canners Association
1133 - 20th Street, N.W.
Washington, DC 20036
CHARLES STEVENSON
Curtice-Burns, Inc.
P.O. Box 670
Rochester, NY 14602
480
-------
HAROLD STONE
Libby, McNeil! & Libby
555 West 115th Street
Alsip, IL 60482
E. STRUZESKI, JR.
EPA-NFIC
Denver Federal Center
Building 53
Denver, CO 80225
GLENN E. STUCKY
Soil Conservation Service
7600 W. Chester Pike
Upper Darby, PA 19080
DENNIS J. SUGUMELE
NYS Dept. of Environmental Cons.
Box 57
Avon, NY 14414
EMERY C. SWANSON
Swanson & Associates
1710 North Douglas Drive
Minneapolis, MN 55422
NORWOOD K. TALBERT
Agway, Inc.
Box 1333
Syracuse, NY 13201
R.H. TAYLOR
SuCrest-Xtravim
P.O. Box 3251
Station "C"
Hamilton, Ontario
CANADA
A. RAYMOND TERWILLEGAR
419 Riley-Robb Hall
Cornell University
Ithaca, NY 14850
INDU THAKER
Lozier Engineers
752 Garson Avenue
Rochester, NY 14609
HAROLD W. THOMPSON
EPA - PNERL
200 SW 35th Street
Con/all is, OR 97330
JOHN THOMAS
Ross Poultry Ltd.
Worstead, North Wanshare
Norfolk, ENGLAND
JOHN TODD
General Foods Ltd.
Research Department
540 William Street
Coburg, Ontario
CANADA
Eric Turkki
NYS Dept. of Env. Conservation
100 El wood Davis Road
North Syracuse, NY 13212
BERNARD A. TWIGG
University of Maryland
Department of Horticulture
College Park, MD 20740
MIKE VAN DEN BOSCH
Environmental Protection Branch
Dept. of Mines, Resources &
Environmental Management
Box 7, Bldg. 2, 139 Tuxedo Ave.
Winnipeg, Manitoba, CANADA
JOHN VILLAMERE
Environment Canada
1090 W. Pender Street
Vancouver 1, British Columbia
CANADA
R.H. WALTER
NYS Agr. Experiment Station
Dept. of Food Science & Tech.
Food Research Laboratory
Geneva, NY 14456
L.R. WEBBER
Land Resource Sciences
University of Guelph
Guelph, Ontario-
CANADA
PETER R. WENCK
Gerber Products Company
Box 456
Newaygo, MI 49337
481
-------
CARROLL G. WILLS
EPA, National Field Investigation
Center, Denver Fed. Center
Denver, CO
RALPH WILSON
Red Wing Co.
196 Newport Street
Fredonia, NY 14063
WESLEY WINTERBOTTOM
Dept. of Civil & Env. Engr.
Cornell University
Ithaca, NY 14850
JACK L. WITHEROW
EPA - PNERL
200 SW 35th Street
Corvallis, OR 97330
S.K. WOLCOTT, JR.
Seneca Foods Corp.
74 Seneca Street
Dundee, NY 14837
GEORGE WONG-CHONG
Agricultural Engineering Dept.
Cornell University
Riley-Robb Hall
Ithaca, NY 14850
N. HENRY WOODING
Penn State
204 Agr. Engr. Bldg.
University Park, PA 16802
P.Y. YANG
Dept. of Agr. Engr.
Cornell University
Ithaca, NY 14850
R.R. ZALL
Cornell University
Dept. of Food Science
Stocking Hall
Ithaca, NY 14850
TERRY L. ZEH
C-B Foods
360 East Avenue
Rochester, NY 14604
JAMES C. ZOMBRO
National Fruit Products Co., Inc,
P.O. Box 609
Winchester, VA 22601
PAUL ZWERMAN
Agronomy Department
1002 Bradfield
Cornell University
Ithaca, NY 14850
The following are students
at Cornell University:
AYED S. AMRE
GLEN J. ANDERSEN
RICHARD C. BOWER
DONALD B. BUDINOFF
RAYMOND R. BURKE, JR.
MICHAEL F. BURT
ROBERT J. BUTCHER
HECTOR R. COVACEVICH
EARL C. DEAN
MARGARET A. FEATHERS
STEVEN N. HELLER
STEVE C. HON
RICKE A. KRESS
JUAN B. LEON
HERNAN MATEUS-VALDES
ROBERT T. MORRIS
PETER C. MUELLER
ARNULFO S. NAVARRO
OLADIPO D. ONAYEMI
JOHN J. PFISTER
GUILLERMO J. RAMIREZ
FARAHNAZ ROSHANAI
CAMILO ROZO
ARTURO SALINAS-CONTEL
MICHAEL G. SCANLAN
FRANCIS J. SCHWENDE
STEVEN T. UYENO
FIDEL VODOVOZ
CHRISTOPHER E. WILCOX
JOHN T. WILLIAMS
DAVID P. PROWN
482
*U.S. GOVERNMENT PRINTING OFFICE:1974 546-319/379 1-3
-------
SELECTED WATER
RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
i K-'p.nt V)
w
PROCEEDINGS FOURTH NATIONAL SYMPOSIUM ON FOOD
PROCESSING WASTES
Pacific Northwest Environmental Research Laboratory,
National Canners Association and Cornell University
9. Organization
Industrial Wastes Branch
Pacific Northwest Environmental Research Laboratory
Environmental Protection Agency, Corvallis, OR 97330
Environmental Protection Agency report number EPA-660/2-73-031
December 1973
The Proceedings contains copies of 25 of the 27 papers presented
at the Symposium. Subjects included: waste characterization, product
and by-product recovery, process modification, and wastewater treatment
of many different segments of the food processing industry.
The two and one-half day symposium was attended by approximately
225 members of industry, universities, consulting firms and state and
federal agencies. Typical papers include: biological treatment of winery
stillage, meat packing wastewater, potato processing wastes, dairy wastewaters,
distillery wastes and egg processing wastewaters; process modifications
for blanching vegetables; as well as by-product recovery from fish processing
effluents, cheese whey and sauerkraut wastewaters.
*Industrial Wastes, *Food Processing Industry, treatment, By products
By product Recovery, Process Modification, Food Processing Waste Characterization
and Treatment
Send To:
WATIN RESOURCES SCIENTIFIC INFORMATION CENTER
U4. DEPARTMENT OF THE INTERIOR
WASHINGTON. OJC. 10t40
Kenneth A. Postal
EPA. NERC-Corvallis
-------