&EPA
United States
Environmental Protection
Agency
Industrial Environmental Research
Laboratory
Cincinnati OH 45268
EPA-600/2-78-129
June 1978
Research and Development
Effects of Liquid
Detergent Plant
Effluent on the
Rotating Biological
Contactor
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RESEARCH REPORTING SERIES
Research reports of the Office of Research and Development, U.S. Environmental
Protection Agency, have been grouped into nine series. These nine broad cate-
gories were established to facilitate further development and application of en-
vironmental technology. Elimination of traditional grouping was consciously
planned to foster technology transfer and a maximum interface in related fields.
The nine series are:
1. Environmental Health Effects Research
2. Environmental Protection Technology
3. Ecological Research
4. Environmental Monitoring
5. Socioeconomic Environmental Studies
6. Scientific and Technical Assessment Reports (STAR)
7. Interagency Energy-Environment Research and Development
8. "Special" Reports
9. Miscellaneous Reports
This report has been assigned to the ENVIRONMENTAL PROTECTION TECH-
NOLOGY series. This series describes research performed to develop and dem-
onstrate instrumentation, equipment, and methodology to repair or prevent en-
vironmental degradation from point and non-point sources of pollution. This work
provides the new or improved technology required for the control and treatment
of pollution sources to meet environmental quality standards.
This document is available to the public through the National Technical Informa-
tion Service, Springfield, Virginia 22161.
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EPA-600/2-78-129
June 1978
EFFECTS OF LIQUID DETERGENT PLANT EFFLUENT
ON THE ROTATING BIOLOGICAL CONTACTOR
by
Frederick T. Lense
Stanley E. Mlleski
Charles W. Ellis
Texize Chemicals Company
Division of Morton-Norwich Products, Inc.
Greenville, South Carolina 29602
Grant No. S-803890213
Project Officer
Ronald J. Turner
Industrial Pollution Control Division
Industrial Environmental Research Laboratory
Cincinnati, Ohio 45268
INDUSTRIAL ENVIRONMENTAL RESEARCH LABORATORY
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
CINCINNATI, OHIO 45268
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DISCLAIMER
This report has been reviewed by the Industrial Environmental Research
Laboratory - Cincinnati, U.S. Environmental Protection Agency, and approved
for publication. Approval does not signify that the contents necessarily
reflect the views and policies of the U.S. Environmental Protection Agency,
nor does mention of trade names or commercial products constitute endorsement
or recommendation for use.
ii
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FOREWORD
When energy and material resources are extracted, processed, converted,
and used, the related pollutional Impacts on our environment and even on our
health often require that new and increasingly more efficient pollution con-
trol methods be used. The Industrial Environmental Research Laboratory-
Cincinnati (lERL-Ci) assists in developing and demonstrating new and improved
methodologies that will meet these needs both efficiently and economically.
This report concerns itself with the "Effects of Liquid Detergent Plant
Effluent on the Rotating Biological Contactor" and the possible presence of
toxic chemicals in a plant's liquid waste. Results of the study will prove
of interest to those persons who may find a need for on-site primary and
secondary treatment of plant effluent but have insufficient available land to
construct an aerated lagoon system or other conventional treatment facility.
The reader's attention will be focused on the efficiency of the rotating bio-
logical contactor as compared to an aerated lagoon system and problems that
may be encountered in design and operation of this newly developed technique.
Additional information on the results of the report may be obtained by con-
tacting:
David 6. Stephan
Director
Industrial Environmental Research Laboratory
Cincinnati
iii
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ABSTRACT
A pilot-scale investigation to determine the efficiency of the rotating
biological contactor (RBC) on raw wastewater from a liquid detergent manufac-
turing plant has been undertaken. Efficiency of the RBC was compared with a
presently operating, extended aeration lagoon system, each receiving identi-
cal waste.
Selected parameters were chosen for measurement, including chemical
oxygen demand (COD), biochemical oxygen demand (BOD), methylene blue active
substance (MBAS), and dissolved oxygen (DO). The effects of temperature,
loading, and sudden changes in concentration of MBAS were monitored for
effects on the biomass adhering to the disc. In some cases, studies were
also conducted to determine the efficiency of each of the three operating
stages.
Even under the best operating conditions, the RBC performance was
essentially equivalent to that of the (operating) extended aeration lagoon.
At other times, especially when the temperature dropped to 15°C or below, the
RBC was inefficient compared to extended aeration. The temperature of the
air above the discs needed to be kept approximately the same as that of the
wastewater feed to avoid inhibiting bacterial growth on the discs. Further-
more, the biomass was found to be highly sensitive to sudden changes in MBAS
concentration and development of foam. Within hours after contact with an
increase in MBAS or excessive foaming, the mass would be stripped from the
disc, rendering degradation efficiency nearly zero.
A second phase of the study was to determine qualitatively and quanti-
tatively the presence of toxic inorganic and organic compounds in the raw
and treated waste.
No toxic inorganics or organics were found in liquid detergent manufac-
turing waste except zinc, which was traced to the municipal water supply as
received by the company. The quantity of zinc present appeared to have
little or no effect on the biological system, however, and the concentration
remained consistent between the influent and effluent streams.
This report was submitted in fulfillment of Grant No. S-803892013 by
Texize Chemicals Company under the partial sponsorship of the U.S. Environ-
mental Protection Agency. This report covers the period August 13, 1975 to
June 30, 1977, and work was completed as of June 30, 1977.
iv
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CONTENTS
Foreword iii
Abstract iv
Figures vi
Tables vii
Abbreviations and Symbols viii
Metric Conversion Chart ix
Acknowledgment x
1. Introduction 1
2. Conclusions 3
3. Recommendations 5
4. Experimental Procedures and Discussion 6
References 32
Appendices
A. Rotating Biological Contactor Pilot Study,
Analytical Methods 33
B. Detailed Data for Analysis of Toxic Substances 34
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FIGURES
Number Page
1 Rotating Biological Contactor, Side View 9
2 Rotating Biological Contactor, Influent End View 10
3 Rotating Biological Contactor, Biomass on Disc 12
4 Foam Generation by the Rotating Biological Contactor 22
5 General Inorganic Analysis for Background Characteristics
of Waste Treatment System 26
6 Inorganic Analysis of Waste for Toxic Substances at Time
Period One 27
7 Inorganic Analysis of Waste for Toxic Substances at Time
Period Two 28
vi
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TABLES
Number Page
1 Characteristics of Wastewater in Equalization Lagoon ....... 11
2 Seven-Day Reduction of BOD, COD, and MBAS ............ 13
3 RBC Effluent and Extended Aeration Effluent Comparisons ..... 13
4 Percent Waste Reduction Achieved by the RBC System and
Extended Aeration ....................... 14
5 Effect of Increasing Flow on Effluent Quality Under
Ambient Conditions ....................... 15
6 Degradation of Wastewater at Low Temperature ........... 16
7 Biomass, Time, and Waste Reduction Relationship ......... 17
8 Percentage Efficiency of each RBC Stage ............. 18
9 Effect of Increasing Surface Area in First Stage ......... 19
10 Clarification of Effluent Streams ................ 20
11 Alum Test . . .......................... 21
12 Typical Atomic Absorption Analysis of Treated Wastewater
for Inorganic Ions ..................... . . 25
13 Water Analysis by Atomic Absorption for Zinc ........... 29
14 letectable Limits for Organic Compounds with Flame
lonization Detector on Barber Coleman (Drawing
Number A4070) Gas Chroma tograph ................ 30
vii
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LIST OF ABBREVIATIONS AND SYMBOLS
ABBREVIATIONS
°C -- Degrees centigrade.
BOD Biochemical oxygen demand without time limits designated.
Measured in milligrams per liter.
BOD5 Biochemical oxygen demand measured in 5 days. Measured in
milligrams per liter.
COD -- Chemical oxygen demand. Measured in milligrams per liter.
DO Dissolved oxygen. Measured in milligrams per liter.
EPA U.S. Environmental Protection Agency.
Eff Effluent.
gpm Gallons per minute.
Hp Horsepower.
Inf Influent.
1/min -- Liters per minute.
MBAS Methylene blue active substance. Used to quantitatively
determine sulfated and sulfonated products. Units are
milligrams per liter.
mg Milligrams.
mg/1 Milligrams per liter.
pH The measurement of acidity or alkalinity. pH 0-7 represents
acidity, pH 7 is neutral, and pH 7-14 represents alkalinity.
ppm -- Parts per million.
Mg/1 -- Micrograms per liter.
R£C Rotating biological contactor.
rpm -- Revolutions per minute.
SVI -- Sludge volume index.
viii
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METRIC CONVERSION CHART
Multiply
Inches
Feet
Square feet
Cubic feet
Pounds
Gallons
Gallons /minute
Feet/second
By
2.54
0.3048
0.0929
0.0283
0.454
3.79
5.458
0.305
To Get
Centimeters
Meters
Square meters
Cubic meters
Kilograms
Liters
Cubic meters /day
Meters /second
ix
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ACKNOWLEDGMENTS
The authors desire hereby to acknowledge their indebtedness to the many
persons and organizations for their advice and efforts towards making this
paper a contribution to the field of methods of wastewater treatment.
Especially we wish to commend the following for their guidance in
developing the proposed plan of study: Mr. Fred Ellerbusch, former Project
Officer who monitored the project until February 1977, Colin A, Houston &
Associates, Inc., Mamaroneck, New York 10543.
Acknowledgment is also made of the use of published papers and text-
books as a source of material and/or test methods used to develop data noted
in this study.
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SECTION 1
INTRODUCTION
The research described in this report consists of two distinct phases:
Evaluation of the rotating biological contactor (RBC)
as a means of treating liquid detergent plant wastes,
and
Analysis of raw wastes and biologically treated wastes
to determine the presence and treatability of selected
chemicals or chemical families designated by the U.S.
Environmental Protection Agency (EPA).
ROTATING BIOLOGICAL CONTACTOR PILOT STUDY
The RBC concept of treating waste streams biologically has been known
for many years, but it was not until strong, lightweight plastics became
available that significant interest in the technique began to develop. The
treatment technique is to grow biologically active masses on a series of discs
that slowly rotate, alternately exposing the biomass to the wastewater stream
and the air above it. In early models, the discs were made of metal and were
heavy, cumbersome, and subject to corrosion. Recent models have discs fabri-
cated of polyethylene or polystyrene. Many investigators have found advan-
tages for the RBC over activated sludge or other conventional treatment
systems based on specialized circumstances. General advantages for the RBC
system are described as follows.
Space
Biomass is concentrated on disc surfaces rather than dispersed
throughout the wastewater.
Efficiency of Oxygen Transfer
Power requirements to achieve oxygen transfer are significantly lower
than systems requiring aeration of the waste stream as the biomasrs absorbs
oxygen from the air.
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Acclimatization
Because the biomass is fixed on the disc surfaces rather than flushed
through the system, it can become acclimated to a greater variety of waste
streams, resulting in greater efficiency overall.
Ease of Operation
Food-to-mass ratios need not be controlled as in activated sludge
systems. The system requires little expertise and minimum testing for smooth
operation in routine installations.
In addition, the KBC unit can be installed in existing facilities such
as clarifiers to upgrade marginal plant performance at minimum cost.
The Texize Chemicals Company is primarily interested in the RBC concept
because of the space requirements and the simplicity of operation. Requests
for information revealed that there was virtually none available on the oper-
ation of an RBC unit on the raw waste stream from a liquid detergent plant.
To provide meaningful data, a pilot RBC unit was operated on the Texize waste-
water stream and its performance compared to that obtained with the extended
aeration lagoon system currently in operation.
ANALYSIS AND TREATABILITY OF RAW WASTES FOR TOXIC CHEMICALS
The analytical phase of the study arose from the EPA need to character-
ize the waste from a liquid detergent manufacturing plant with regard to its
toxic constituents. The study consisted of a survey to determine the possible
presence of specific toxic chemicals that could possibly be present in the raw
wastewater stream and the treated wastewater from a liquid detergent manufac-
turing plant. Qualitative and quantitative analyses were conducted on the
untreated and treated streams to confirm the presence or absence of the
materials thought to be present. In addition, data were collected on the fate
of those chemicals found to be present and their effects on biological action.
The study was conducted using analytical techniques specified or approved by
EPA when feasible.
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SECTION 2
CONCLUSIONS
ROTATING BIOLOGICAL CONTACTOR PILOT STUDY
Data obtained in a pilot study on the performance of the RBC on a
liquid detergent plant effluent indicate that satisfactory performance can be
obtained only when operating under optimal conditions. Under the best condi-
tions, degradation of wastes was approximately equivalent to that obtained in
the extended aeration lagoon system currently being operated, but was con-
siderably inferior at other times.
High levels of surfactant, measured as methylene blue active substance
(MBAS), in the waste stream were found to have an inhibitory or toxic effect
on the biomass affixed to the rotating discs. In addition, die-offs of bio-
mass occurred when they were subjected to rapid decreases in wastewater
temperature. Degradation levels achieved when waste stream temperatures were
below 20°C were also considered unsatisfactory.
Though problems were encountered in obtaining satisfactory levels of
improvement in wastewater characteristics, the RBC concept is still consid-
ered viable where special problems must be overcome. The system requires
relatively little space, and operation is simple and virtually maintenance
free. Where space is limited and waste streams are relatively small, it may
be possible to overcome the system deficiencies when operating at tempera-
tures below 20°C by preheating the waste stream before pumping it to the RBC
unit. MBAS concentrations could be maintained at acceptable levels by re-
cycling RBC effluent into the influent stream. Studies should be made to
determine the feasibility of such control where space is a problem and/or
a»relatively small waste stream must be treated.
ANALYSIS AND TREATABILITY OF RAW WASTES FOR TOXIC CHEMICALS
Samples of raw, untreated plant effluent, effluent after secondary
treatment, and effluent from the RBC were submitted to atomic absorption
analysis for detection and measurement of inorganics appearing on the list of
toxic substances. In addition, samples taken from identical locations were
submitted to gas chromatographic analysis for organic compounds appearing on
the list.
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Zinc was present in all samples in measurable quantities (0.25 mg/1).
The source of zinc was traced to incoming municipal water. Its concentration
did not interfere with biological activity, however.
All other inorganics appearing on the toxic list were detectable but
below minimum measurable limits.
Of the 18 organic compounds subjected to gas chromatographic analysis,
all proved to be below the minimum detectable limits.
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SECTION 3
RECOMMENDATIONS
Though the information and conclusions reported here are based on a
2-year study of the RBC, the operating phase was limited in scope to an
actual operating year of only four calendar seasons. If duplicate seasons
data were available for comparison, some deviations would possibly occur as
a result of climate and raw influent stock variations. The concept of the
RBC appears sound for certain uses and should not be discarded based upon a
1-year test.
The RBC should be operated long enough to gain an overall view of the
effects of climatic conditions. Data for several summers, winters, springs,
and autumns should be compared.
The influent temperature should be maintained at 23°C to 25°C during
times of low temperature to determine the RBC's effectiveness under control-
led temperature conditions.
The above two suggestions should be conducted at an operating facility
where there is a problem of space, (land area) . The outfall from the plant
should have comparable waste, both qualitatively and quantitatively, to cor-
relate results obtained in this study.
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SECTION 4
EXPERIMENTAL PROCEDURES AND DISCUSSION
BACKGROUND
The Mauldin, South Carolina Plant of Texize Chemicals Company, Division
of Morton-Norwich Products, Inc., manufactures liquid detergent products for
use in the home. Currently, the product line includes hard surface cleaners,
light duty dishwashing liquids, laundry softeners, laundry soil and stain
remover and a disinfectant containing pine oil. In addition, alkyl benzene is
sulfonated and alcohol ethoxylates are sulfated by a AIR/S03 batch process to
produce anionic surfactants for use in formulating the products eventually
distributed to the consumer.
The major raw material types used in formulating Texize products include
nonionic surfactants, anionic surfactants and coupling agents, quaternary
ammonium compounds, pine oil, caustic soda, sodium silicates, and various
oxygenated solvents.
The waste treatment system at Mauldin has evolved over the years from a
series of holding ponds and grease pits to an extended aeration lagoon system
which is highly efficient in BOD and MBAS reduction. The waste streams dis-
charged to the lagoons include product and raw material losses through spil-
lage and washouts, and sanitary wastes from approximately 500 employees.
There are no by-products waste streams generated at this site. The various
components of the waste treatment system are described as follows:
Equalization Chamber
All waste streams from the plant enter a concrete box with a nominal
4 to 6 hour residence time. The waste streams are mixed using an 8 rpm paddle
blade mixer. The pH of the mixed waste in the chamber is monitored but not
controlled. pH can vary from approximately 2 to 12 depending on activities in
the Plant. The equalization chamber functions to "smooth out" waste flow into
the lagoon system and prevent "slugs" of concentrated waste from possibly
flowing through the system.
Equalization Lagoon
The equalization lagoon has a capacity of approximately 4,000,000 liters
(1 million gallons) and a nominal retention time of 40 days. The equalization
lagoon has two high speed 5 hp surface aerators which are there to provide
complete mixing and prevent anaerobic decomposition, with the associated
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odors, from occurring on the lagoon bottom. In addition to providing mixing
to the lagoon, oxygen is introduced and biological degradation does occur.
The dissolved oxygen content of the lagoon effluent is normally zero.
Grease Trap
Effluent from the equalization lagoon flows through a grease trap and
weir into the aerated lagoon. Separated oils and other floatable materials
are removed from the waste stream. pH of the stream and volume flow are
automatically monitored.
Extended Aerated Lagoon
The aerated lagoon has a capacity of approximately 6,000,000 liters
(1.5 million gallons) and a nominal retention time of 60 days. The lagoon
has a maximum depth of approximately 2 meters (6 feet). Aeration of the
lagoon is accomplished through the use of four 10 hp floating aerators. The
lagoon is completely mixed. Dissolved oxygen levels are normally in the
range of 2 to 6 mg/liter (2-6 ppm). During the summer months a heavy
growth of green algae develops. Because the manufacturing plant only
operates 5 days/week, flow through the lagoons is negligible on weekends with
the result that biological activity is severely reduced on the weekends. To
correct this situation, wastewater is pumped from the aerated lagoon back
into the equalization lagoon on weekends at the rate of approximately 400
1/min (100 gal/min) . This in turn creates a flow from the equalization
lagoon back to the aerated lagoon. Increases in efficiency have been
dramatic since this change. Normal results are reductions in BOD of 90+
percent, COD of 85+ percent and MBAS of 95+ percent.
The major problems with the current system are foam generation during
cool, high humidity periods, and the large amount of valuable land space
required by the lagoons. Foam is objectionable because it can be blown by
wind out of the lagoon. To date no effective defoamer has been found which
would reduce the problem. When foam buildup occurs aerators are turned off
until foam subsides. The land occupied by the lagoons at the present time is
directly adjacent to the manufacturing plant and warehouse. Further expan-
sion of these facilities is not possible unless the treatment system is moved.
Discharge from the treatment system is into the Western Carolina
Regional Sewer Authority system. No clarification or disinfection steps are
taken to reduce suspended solids or fecal coliform.
ROTATING BIOLOGICAL CONTACTOR PILOT STUDY
Initial interest was generated at Texize Chemicals Company by a paper.
"Application of the Bio-disc System for Industrial Wastewater Treatment",
presented at the Tenth Annual Seminar on Air and Water Pollution Control at
Clemson University by Larry G. Blackwell.
The paper cited characteristics such as improved refractory and oil
waste removals, gentle mixing action, and smaller space requirements which
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had appeal to Texize as possibly being an answer to some of the shortcomings
in the operating treatment system. Excessive foam generation and the use of
valuable land space are viewed as the two main problems in the current system,
and improved reductions in COD and oil and grease would be desirable.
Objectives of the Project
A project was proposed to operate a pilot RBC unit on the effluent from
a liquid detergent manufacturing plant. The major objectives of the project
were to answer the following questions:
Are waste streams from a liquid detergent manufacturing
process amenable to treatment by the RBC to the same, lesser,
or greater extent than extended aeration?
Are the more refractory organic materials present in a
liquid detergent manufacturing process effluent more adequately
treated in a RBC system due to development of harder to maintain
bacterial strains?
Are RBC systems more adaptable to varying waste loads
than activated sludge or extended aeration lagoon systems?
Are RBC systems more efficient than the extended aeration
lagoon system at lower operating temperatures (waste stream
temperatures from 5°C to 15°C)?
Approach
The project proposed was to install and operate a pilot RBC unit for
approximately 8 months. During that time major emphasis would be placed on
evaluating the following variables:
Determination of optimum loadings range.
Determination of maximum loadings.
Determination of the effect of rapid changes in loadings
on quality of effluent.
Determination of the effect of temperature on performance.
Determination of whether acclimated bacterial growths could
be developed to degrade the more resistant organic constituents
in the waste stream.
The major parameters for determining performance were BOD5 reduction, COD
reduction, and MBAS reduction. Measurements of other parameters would in-
clude oil and grease reduction, settleable and suspended solids of effluent,
nitrogen concentration in effluent, and phosphorus concentration in effluent.
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Description of Pilot Installation
The pilot RBC operation consists of the RBC unit itself, a variable
capacity pump to provide constant feed to the unit, and a building to house
the unit providing protection from the elements (Figure 1).
ROTATING BIOLOGICAL CONTACTOR
Side View
Figure 1. Rotating Biological Contactor, Side View
The RBC unit is a commercially available unit of conventional design.
The rotating discs are 1.2 meters in diameter and fabricated of flat poly-
ethylene. The discs are grouped to give four stage operation with 10 discs
in each stage. The stages are separated by baffle plates so arranged that
flow c>f wastewater occurs along the outside edges of the unit (Figure 2).
Total surface area available for biological growth is approximately 11.69
square meters per stage, and 46.76 square meters for the unit overall. The
discs are suspended in a carbon steel tank with a total liquid capacity of
approximately 660 liters (175 gallons). The discs are powered by a 1/3 hp
totally enclosed motor. Speed of rotation is controlled by the size of the
wheels on the belt drive. The discs were operated at 2 speeds during the
course of the project, either 8 rpm or 10 rpm.
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ROTATING BIOLOGICAL CONTACTOR
Influent End View
Figure 2. Rotating Biological Contactor, Influent End View
Feed to the RBC unit of wastewater was accomplished by means of a
variable capacity centrifugal pump. The pump was so designed that flows
could be regulated over the range of 0 - 30 liters/per minute. The intake
line was in every case below the surface of the wastewater to avoid floating
matter and provided with a screen to prevent suspended matter from fouling
the pump. Wastewater feed to the RBC was to the end of the unit.
The RBC unit and the pump were both housed in an insulated metal build-
ing to protect them from the weather. The building was completely closed so
that the RBC unit was operated in the dark. Provision was made to heat the
building during winter months to prevent the equipment from freezing and to
ventilate it during the summer to prevent temperatures from getting too high,
Experimental Conditions and Results
Initial Startup--
The RBC unit was put into operation on August 13, 1975.
The initial charge to the unit was made up of 50 percent wastewater
from the equalization lagoon, and 50 percent wastewater from the extended
aeration lagoon. The extended aeration lagoon had a significant population
of bacteria which were acclimated to the type waste to be fed to the system.
10
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The initial feed to the system was from the equalization lagoon. Feed
was taken from the lagoon rather than from the equalization chamber for the
major part of the study. There were two reasons for this:
pH in the equalization chamber varied from 2.0 to 12.0
whereas in the equalization lagoon it varied between 6.5 and
8.5 requiring no control.
In the equalization chamber, concentrated slugs of waste-
water would wash through periodically as a result of spills
and washouts. Wastewater in the equalization lagoon was more
typical of the average wastewater being discharged. In addi-
tion it had the advantage of being more consistent enabling
data taken at different times to be more easily compared.
The intake to the pump was placed inside a screened box below the sur-
face of the lagoon. The screen prevented insoluble material from fouling the
pump. The subsurface intake prevented intake of floating materials which
would not be typical of the waste stream.
The initial feed rate was approximately 1.9 liters (0.5 gal) per min-
ute. Detention time in the unit was approximately 6 hours (1.5 hours/stage).
The BOD5 loading on the unit (average concentration 250 - 300 mg/1) was
0.0146 to 0.0175 kg per square meter per day. This rate was selected as an
estimate of approximately 50 percent of the maximum loading for the unit.
Rotational speed of the discs during startup was 10 revolutions per
minute.
For approximately 6 weeks before the beginning of the RBC pilot opera-
tion, samples of the wastewater from the equalization lagoon were obtained
and analyzed to characterize the nature of the waste feed to the unit (Table
1). The values in Table 1 are typical of those obtained during the period.
TABLE 1. TYPICAL CHARACTERISTICS OF WASTEWATER IN EQUALIZATION LAGOON
Parameter
Concentration
in Wastewater
Parameter
Concentration
in Wastewater
Temperature °C
pH
BOD5, mg/1
COD, mg/1
Suspended Solids, mg/1
MBAS, mg/1
Dissolved Oxygen, mg/1
Oil and Grease, mg/1
Kjeldahl Nitrogen, mg/1
27
6.8 - 7.9
200
1000
97
2.8
0
22
32
Aluminum, Mg/1
Cadmium, «g/l
Chromium, Mg/1
Copper, Mg/1
Iron, Mg/1
Lead, t\g/l
Mercury, ug/1
Nickel, Mg/1
Phosphorus , mg/1
Zinc, Mg/1
600
70
30
40
4800
100
0.6
50
1.2
20
11
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Operation at "Standard" Conditions
Initial startup conditions were selected on the basis of providing
"base case" data on the performance of the RBC unit. Within 2 days growth of
a slime on the discs became noticeable. Bacterial accumulation on the discs
could be observed in the first stage in 4 to 6 days. Growth continued to
accumulate on all four stages until it was an estimated one-fourth inch thick
(Figure 3).
ROTATING BIOLOGICAL CONTACTOR
Bio-Mass or Disc
Figure 3. Rotating Biological Contactor, Biomass on Disc
At that point sloughing began to occur on large areas of the discs, beginning
in the first stage and successively progressing through the fourth stage.
A significant reduction in BOD5, COD and MBAS was being obtained after
7 days of operation (Table 2).
Because neither the effluent from the RBC unit, nor the aerated lagoon
were being clarified to remove suspended solids, samples tested for BOD5 were
filtered to remove suspended solids. This was done to provide a better basis
for comparing data.
L2
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TABLE 2. SEVEN-DAY REDUCTION OF BOD. COD. AND MBAS
Parameter
BODs, mg/1
COD, mg/1
MBAS, mg/1
Influent
150*
630
3.5
Effluent
30*
473
0.86
Percent Reduction
80
25
75
*BOD5 determined on filtered samples.
The RBC was operated under the initial conditions for approximately 5
weeks. Slight improvement in effluent quality occurred for the first 3
weeks, then appeared to level off. At that time effluent from the RBC was
approximately equivalent to effluent from the extended aeration lagoon in
characteristics (Table 3). Average waste reductions achieved for each of
the major parameters of interest for the period 9/2/75 to 9/18/75 are shown
in Table 4.
TABLE 3. RBC EFFLUENT AND EXTENDED AERATION EFFLUENT COMPARISONS
Parameter Influent
PH 7.5 - 8.2
BOD5, mg/1 80 - 290
COD, mg/1 675 - 1300
MBAS-, mg/1 2.3 - 6.8
Suspended Solids, mg/1
RBC Effluent
7.4 - 7.5
25 - 40
340 - 650
0.15 - 0.40
40 - 80
Aerated
Lagoon
Effluent
--
25 - 50
220 - 470
0.15 - 0.35
30-90
13
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TABLE 4. PERCENT WASTE REDUCTION ACHIEVED BY THE RBC SYSTEM
AND EXTENDED AERATION
Percent Reduction Achieved
Parameter RBC Effluent Aerated Lagoons Effluent
mg/1 mg/1
BOD5 83 78
COD 46 65
MBAS 96 96
The next phase of the experimental program was to determine the maximum
feed rate at which satisfactory results would be obtained.
The RBC unit was run at "standard" conditions on several occasions
during the course of the project. All data obtained when running the RBC
under these conditions are compiled in Appendix, Table A-l to provide easy
comparison of results. The performance of the RBC was not as good at any
time as was found with the September-October, 1975 experiments. For example,
all startups after failure of the system required longer times, the degree of
degradation obtained was not as complete, and the length of time until fail-
ure of the system was shorter.
Operation at Increased Loading
With the results obtained at "standard" conditions as a target, opera-
tion at increased feed rates was conducted to determine if possible the
maximum loadings under which the RBC unit would give comparable results
(Table A-2).
With the advent of a period of cold weather and rain in mid-September,
1975, a failure of the RBC system occurred. All bacterial growth on the
discs died and sloughed from the discs. The same die-off was experienced in
the aerated lagoon system. Die-off appeared to be associated with a rapid
drop in wastewater temperature from 24°C to 19°C in 2 days. The temperature
continued to drop to a low of 17°C before warming slightly by the end of the
month. Attempts to reestablish growth on the discs were unsuccessful until
the RBC was flushed and recharged with a 50/50 mixture of materials from the
equalization lagoon and the extended aeration lagoons as in the initial
startup.
14
-------
After recharging the unit, slime began to develop on the discs but at a
considerably slower rate than when the experiment was begun. This was
(attributed to lower wastewater feed temperatures (approximately 20°C versus
27°C) . After 3 weeks it was felt that effluent quality from the KBC unit was
approaching the quality obtained before the failure of the unit.
The flow rate of the wastewater feed was then increased from 1.9
liters/minute to 2.85 liters/minute (0.75 gpm). Dentention time in the unit
was reduced to 4 hours (1 hour per stage). The increase in feed rate did not
materially affect the quality of the effluent measured by BOD5, COD, or MBAS.
After operating approximately 2 weeks at wastewater feed rates of 2.85
liters/minute, the feed rate was increased to 3.8 liters/minute (1.0 gal/
rain). Thus increase in feed rate did not appear to seriously affect quality
of the effluent when measured by BODs, COD, or MBAS. However, data are
difficult to interpret in this case because the waste concentrations in the
wastewater feed were considerably lower than earlier when feed rates were
lower. The net effect was that although the hydraulic rates were increased
and residence times shortened, the waste load measured as contaminant/square
foot of disc/day did not increase. The wastewater feed rates were increased
to 7.8 liters/minute in early December, however, by this time wastewater feed
temperatures had dropped to below 15°C and data were not representative of
what might have occurred during warmer weather and could not provide a valid
comparison to quality at lower feed rates.
Table 5 shows typical data obtained with changing wastewater feed
rates.
TABLE 5. EFFECT OF INCREASING FLOW ON EFFLUENT QUALITY
UNDER AMBIENT CONDITIONS
Date
10/15/75
10/23/75
ll/4'/75
11/11/75
11/20/75
12/16/75
Flow (1/Min]
1.9
2.85
2.85
3.8
3.8
7.6
>
Parameter
BODS (me /I)
Inf. Eff.
150
150
77
135
77
157
43
20
20
20
6
34
COD (me/I)
Inf. Eff.
1090
1300
800
940
825
1370
560
570
400
300
330
680
MBAS
Inf.
8.8
4.9
3.1
0.6
0.2
7.6
(me/I)
Eff.
1.3
0.9
0.6
0.2
0.1
4.5
Further studies at feed rates above 1.9 liters/minute were not con-
ducted since it was not possible to obtain consistent performance of the RBC
at that low feed rate thus to yield meaningful data.
15
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Operation at Different Feed Temperatures
A major factor in RBC performance on liquid detergent plant waste
streams is the temperature of the wastewater feed. As noted earlier in the
report, a rapid drop in temperature from 24°C to 19°C in mid-September, 1975
resulted in a die-off of the biomass on the discs and the concurrent failure
of the unit. A similar drop occurred in late November, 1975, which resulted
in severely decreased biological activity. Further, it was not possible to
generate or maintain a heavy growth of biomass on the discs until wastewater
temperatures increased to above 20°C. Although bacteria were present in the
system, no significant degradation of waste occurred even at wastewater feed
rates of 0.95 I/minute (0.25 gpm) which was the lowest rate at which our
equipment would operate (Table A-3). However, when waste flow to the unit
was stopped and the discs were allowed to continue to rotate, degradation did
occur as shown in Table 6.
TABLE 6. DEGRADATION OF WASTEWATER AT LOW TEMPERATURES
Test 1
Test 2
Parameter
BOD5, mg/1
COD, mg/1
MBAS, mg/1
Temperature °C
Influent
12/30/75
50
1125
8.2
8
Effluent
12/30/75
(1.81
1/min.)
26
893
7.8
11
1/6/75
(no flow)
8
580
0.2
10
Influent
1/15/76
114
1850
18
8
Effluent
1/15/76
(0.95
1/min.)
50
1500
8.7
11
1/27/76
(3.8
1/min.)
11
420
0.55
10
These tests clearly indicate that the waste streams were amenable to
biological action and that biological activity was occurring; however at a
very low rate.
The rate of degradation which occurred under "no flow" conditions was
observed during July 1975 and September 1975 when wastewater temperatures
were above 20°C. Based on the earlier ekperiences where failure of the
system occurred when MBAS levels were high, it was of interest to see whether
a high MBAS waste could be degraded if residence times were longer as in a
"no flow" situation. A trial run was made in July 1976 (Table 7) where there
16
-------
was little or no biomass on the discs. Over a period of 96 hours, MBAS
levels dropped from 33 mg/1 to 5.8 mg/1. A second trial was conducted in
early September 1976 (Table 7), when approximately 50 percent of the discs
were covered with biomass. In this case, the MBAS concentration in the unit
decreased from 8.1 mg/1 to 2.0 mg/1 in 48 hours. At the same time, the COD
dropped from approximately 1500 mg/1 to 1000 mg/1. A third run was made in
September 1976 (Table 7), when approximately 80 percent of the discs were
covered with biomass. MBAS concentrations in the unit decreased from 0.60
mg/1 to 0.16 mg/1.
It would appear that a "batch" type operation has some feasibility with
high MBAS wastes particularly where daily flows are not too high.
TABLE 7. BATCH TEST; BIOMASS. TIME, AND WASTE REDUCTION RELATIONSHIP
Parameter
Date:
Biomass Coverage
Initial
After 2 hours
After 6 hours
After 24 hours
After 30 hours
After 48 hours
After 96 hours
Removal Efficiency
7/2/76
0%
33
--
--
5.8
827.
MBAS (me/I")
9/1/76
50%
8.1
7.6
6.9
4.0
3.4
2.0
75%
9/13/76
80%
0.60
0.32
0.23
0.18
0.16
73%
COD (me /I)
9/1/76
50%
--
1485
--
--
1100
1020
--
75%
During the period from early November, 1975 to late January, 1976, the
temperature in the building in which the RBC unit was housed was kept at a
minimum of 15°C in accordance with the originally proposed program. However,
from late November on, no appreciable growth was generated on the rotating
discs under a variety of wastewater feed rates and conditions. It was then
thought that growth on the discs might be inhibited through "shocking" the
bacteria by exposing them 'to significantly different temperatures in the
water and the air. The temperature in the building was adjusted to keep it
in the range of 8°C to 10°C, more nearly the temperature of the wastewater in
the unit. After approximately 10 days with a wastewater feed rate of 1.9
I/minute a significant reduction in COD and MBAS occurred. It appears that
it would be necessary to keep the temperature of the air above the discs at
approximately the same temperature as the wastewater feed to keep from
inhibiting bacterial growth on the discs. However, although the biomass
exists, the reduced rate of activity at the lower temperatures occurring
17
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during the winter months would make the usefulness of the KBC system minimal.
The problem of low wastewater temperatures can be overcome in situations
where wastewater flows are relatively small as they are at the Texize
Chemicals Company. Capital investments and operating costs to install heat
exchangers making use of waste steam as a heating mechanism would not be
prohibitive. If other factors would favor the adoption of an RBC system then
heating the waste stream should be considered as a means of overcoming the
shortcomings encountered in operating at low wastewater temperatures.
Relative Degradation in the Various Stages of the RBC
A number of times during the study, all four stages of the RBC unit were
sampled to determine the degree of degradation that was taking place in each
stage (Table A-4). Invariably it was found that the great majority of BODs,
COD and MBAS reduction occurred in the first stage. At the same time,
virtually no change in concentrations occurred between the third and fourth
stages (Table 8). No additional reduction in COD concentration was obtained
as a result of the second stage treatment. These findings can be illustrated
using analytical data obtained during sampling of the several stages.
TABLE 8. PERCENTAGE EFFICIENCY OF EACH RBC STAGE
Parameter
BOD5 me/I COD me/I MBAS mg/1
Influent
First Stage
Second Stage
Third Stage
Fourth Stage
180
90
-
70
40
1280
1040
480
480
480
5.0
2.0
1.1
0.85
0.40
Because so much of the degradation was occurring in the first stage an
experiment was conducted in which the baffle plate between the first and
second stage was removed, effectively doubling the surface area of the discs
in the first stage. The RBC unit would then operate as a three stage unit
with the first stage having 23.4 square meters of disc surface and the second
and third stages 11.7 square meters each. It was considered that possibly a
greater total degradation would be achieved in this manner. As the data
shown in Table 9 indicate no significant advantage in overall waste reduction
was obtained.
18
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TABLE 9. EFFECT OF INCREASING SURFACE AREA IN FIRST STAGE
Before Removing Baffle
Parameter
Sample Date
Influent
First Stage
Second Stage
Third Stage
Fourth Stage
MBAS
7/23/76
mg/1
5.4
3.0
3.0
2.8
2.6
COD
7/23/76
mg/1
1240
1150
990
990
990
After Removing Baffle
MBAS
7/26/76
mg/1
2.8
1.4
1.2
1.2
-
8/5/76
mg/1
13.0
7.8
-
7.2
-
COD
7/26/76
mb/1
1100
700
-
700
-
8/5/76
mg/1
1240
1070
1030
1030
-
Although this experiment did not indicate any advantage in increasing
the surface area of the first stage, the experiment was run at a time when
the RBC unit was not operating at optimum. It would be of interest to repeat
the experiment when the unit was operating better. It may be found that
there is no real advantage in having stages.
Amenability of RBC Effluent to Clarification
Of interest in this study was whether any significant difference
existed between RBC effluent and aerated lagoon effluent with respect to
attempts at clarification. Accordingly laboratory jar tests were run to
compare the quality of the supernatent liquid from the two sources after
treatment with alum.
A stock solution of alum was prepared with the proper amount to give
the desired dosage and added to slowly stirred samples of wastewater. After
addition of alum was completed, the sample was mixed vigorously for one
minute, then at a more moderate speed for 15 minutes to allow the floe to
form. Mixing was then discontinued and the sample allowed to stand for 60
minutes while the floe settled. The sludge volume index (SVI) was determined
after 30 minutes of settling. After 60 minutes the supernatent liquid was
sampled and analyzed for the various parameters.
There was no significant difference in the effluent's response to
clarification attempts. Trials were run in February and August of 1976
(Table 10).
19
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TABLE 10. CLARIFICATION OF EFFLUENT STREAMS
Effluent Source
Date
Dosage
Parame ter
BODs, mg/1
COD, mg/1
MBAS, mg/1
TSS, mg/1
SVI (30 min)
RBC
2/76 8/76
300 me/1 1000 me/1
Before After Before After
140 60
1800 400
2.8 1.1 26 3.4
44 28 72 24
86 145
Aerated Lagoon
2/76 8/76
300 me/1 1000 me/1
Before After Before After
121 7
630 130
0.9 0.5 0.3 0.3
108 28 44 12
90 120
Although a much higher concentration of alum was required in the
studies conducted during August, in both experiments Total Suspended Solids
of the clarified effluent were in the acceptable range. A factor of interest
is the significant reductions of both MBAS and COD obtained during clarifica-
tion. If suitable disposition of the sludge could be arranged, an attractive
treatment route could be the clarification of the raw waste before biological
treatment.
During the latter part of the research study, the possibility of using
the RBC unit as a polishing step after secondary treatment was investigated.
Additional reduction in MBAS and COD concentrations was achieved in doing
this; however, clarification of the two effluents resulted in similar final
effluent concentrations (Table 11). Thus use of the RBC as a polishing step
did not benefit final effluent after clarification.
The results of a comprehensive study conducted on the aerated lagoon
effluent by AWARE, Nashville, Tennessee, can be compared to current results
by referring to the report issued which is included as part of this report as
Appendix Table A-5.
20
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TABLE 11. ALUM TEST
PH
mg/1
10/27/76
MBAS
mg/1
COD
mg/1
Flow to RBC from
#2
Extended Aerated Lagoon
(Initial 10/27)
(750 mg)
Rotating Biological Contactor
7.4
5.3
0.94
0.51
598
341
(Initial 10/27)
(750 mg)
7.6
5.5
0.58
0.52
488
323
3.785 1/min
Incidence of Foaming in the RBC Unit
One of the major problems which occurs in the present aerated lagoon
treatment system is the generation of foam when temperatures are below 20°C
and humidity is high. If at'the same time the wind was blowing, it would be
necessary to shut down the aerators to keep foam from blowing out of the
lagoon. Because of the relatively slow speed at which the RBC discs were
rotating it was felt that significant foam would not be generated in the
system. Alternatively if foam was generated it would be easier to cope with
in the relatively small area occupied by the RBC units.
Contrary to expectations, small amounts of foam were generated in the
first stage of the RBC even at relatively low concentrations of MBAS (less
than 10 mg/1) and warm temperatures (above 20°C) . This did not appear
deleterious to the functioning of the unit. However, during the winter
months when the wastewater feed temperatures were below 15°C and MBAS levels
in the wastewater were above 5.0 mg/1 copious amounts of foam were generated
in all four stages of the unit (Figure 4). Foam would spill out of the unit
tank onto the floor and adhere to and completely cover the rotating discs.
During these periods it would take only a short time for the biomass to be
completely stripped from the discs.
If the other conditions are met for satisfactory performance of the RBC
(wastewater temperatures above 20°C and MBAS less than 10 mg/1) it is not
believed that foam would be a significant problem with the RBC unit.
21
-------
Figure 4. Foam Generation by the Rotating Biological Contactor
Characterization of Bacteria in the System
There were no significant differences in types of bacteria growing in
the two treatment systems. Bacteria found were gram negative rods typical of
those associated with organic degradation. In one sampling a small popula-
tion of mold similar to a yeast was identified. The mold represented less
than 1 percent of the total growth found in any one sample.
Operation and Maintenance of the KBC Unit
A prime advantage claimed for the RBC unit is the simplicity of opera-
tion and low maintenance requirements. Based on the experience obtained in
this study it would appear the claim is well founded. Mechanically very
little problem was encountered with any of the equipment. The only problem
encountered was that the polyvinyl chloride baffle plates fractured where
they were attached to the sidewall of the unit. Additional clamps were
placed on the plates and the unit functioned very well. The manufacturer has
indicated that later models of this unit have been strengthened in this area.
The unit required no operators care. After the initial charge was made
on startup the only operator time involved was to check the feed rate to the
22
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unit, record the wastewater temperature, and collect samples for testing.
Review of Operational Data by Colin A. Houston & Associates, Inc.
Upon completion of data collection and evaluation, a draft report con-
cerning the operation of the KBC was presented to Colin A. Houston &
Associates, Inc." for review and comments on the conclusions reached by the
Texize Chemicals Company personnel. In private correspondence dated January
12, 1978, with the Effluent Guidelines Division (WH-552) of the United States
Environmental Protection Agency, comments were made and are extracted below.
"All in all, it would appear that the RBC is not applicable
to the successful treatment of wastewater containing high con-
centrations of surfactants unless at least all the following
things are done.
(a) The unit is preceeded by a large equalization tank
in which the wastewater is mixed thoroughly to pre-
vent step changes in feed composition.
(b) The temperature of the feed is adjusted to and con-
trolled in a narrow range.
(c) The feed is diluted to maintain a uniformly low con-
centration of detergent measured as MBAS - this could
be done by recirculating the effluent from the unit.
(d) The effluent from the RBC is subjected to coagula-
tion and settling treatment to remove suspended solids.
Unfortunately, if all the foregoing are done then the advantages
of using the RBC equipment are largely negated and alternative
methods are more attractive."
ANALYSIS AND TREATABILITY OF RAW WASTES FOR TOXIC CHEMICALS
Obiectives
Upon completion of the operational phase of the RBC study a program was
planned in order to determine the presence of toxic materials that may appear
in effluent from a liquid detergent plant. Ions and compounds of interest
were published in "Toxic Materials News", April 15, 1976, a copy which was
forwarded to these laboratories by the EPA Project Officer.
In that the existing waste treatment facility is an earthen aerated
lagoon system the plan called for qualitative and quantitative determinations
of all inorganics appearing on the list, it being conceivable that leaching
of these elements from the earth may have been possible. Further considera-
tion was given to the fact that some of the inorganics could have possibly
been used by a raw material manufacturer as a catalyst, the catalyst then
23
-------
only partially removed would possibly be shipped in the raw material creating
problems of which the detergent f emulator may be unaware.
A decision was made in the case of organic compounds appearing on the
list of toxic materials that only those compounds that could be considered as
a likely candidate in effluent from a liquid detergent plant would be deter-
mined both qualitatively and quantitatively. The presence of many of the
compounds appearing on the list are candidates only to very specific types of
chemical industry and any likelyhood that such compounds could or would
appear in a detergent plant even as a raw material contaminant would be
remote. Certain of the listed compounds are used as laboratory reagents,
e.g., chloroform and could conceivably be detected in the waste treatment
basin should careless handling of reagents occur in the laboratories. None
of the listed organics are either maintained in the Company's raw material
inventory or have ever been knowingly used in a manufacturing process within
the last 8 to 10 years. Further, the synthesis procedures of raw materials
used in detergent manufacturing do not lend themselves to the use of these
organics even as a medium for reactions.
On this basis, in agreement with the project officer a total of 16
compounds were chosen for analysis, those being 16 that could possibly either
be shipped as contaminants or find their way into the treatment system
through an improper discard from a laboratory. Inorganics and organics
chosen for the study were
1.
2.
3.
4.
5.
6.
7.
8.
9.
10.
11.
12.
13.
Inorganics
Antimony
Arsenic
Beryllium
Cadmium
Chromium
Copper
Lead
Mercury
Nickel
Selenium
Silver
Thallium
Zinc
Organics
14. Benzene 22.
15. Carbon Tetrachloride 23.
16. Chlorinated benzene 24.
17. Chlorinated ethane 25.
18. Chlorinated phenol 26.
19. Chloroform 27.
20. 2-Chlorophenol 28.
21. Dichlorobenzene 29.
Organics
Dichloroethylene
2,4-dimethylphenol
Ethylbenzene
Pentachloropheno1
Phenol
Tetrachloroethylene
Toluene
Trichloroe thylene
24
-------
The plan for study required that raw plant effluent be sampled and
analyzed for each element and compound. Should the analysis indicate that
any of the toxic materials be identified in an accurately measurable quantity
then production records would be consulted to determine products manufactured
during the analysis period. From these records raw materials used could be
established. Each raw material involved then would be checked for contamina-
tion. In addition samples of waste obtained from sumps leading from an
operating department would be analyzed in order to establish the source of
the unwanted material. Additionally, the fate of each identified and
measured compound or element would be determined.
Analysis for Inorganic Ions
On November 3, 1976, a complete inorganic characterization of effluent
took place to not only include those elements appearing on the toxic list but
also to include others that could possibly influence biological action in
either the RBC or the extended aeration system. The results of the atomic
absorption analysis indicated all elements classed as toxic were detectable
with very few in the measurable range. There appeared to be no element in
the system classed as toxic or non-toxic in a concentration that may inter-
fere with biological oxidation (Table 12).
TABLE 12. TYPICAL ATOMIC ABSORPTION ANALYSIS OF
TREATED WASTEWATER FOR INORGANIC IONS
Element
Maximum Concentration
Element
Maximum Concentration
Aluminum
Antimony
Arsenic
Barium
Beryllium
Boron
Cadmium
Calcium
Chromium
Copper
<500
< 0.02
0.001
< 100
< 0.006
< 50
< 2
2.73
< 20
< 10
Mg/1
mg/1
mg/1
Mg/1
mg/1
mg/1
Mg/1
mg/1
MS/1
Mg/1
Iron
Lead
Magnesium
Mercury
Nickel
Potassium
Selenium
Silver
Sodium
Thallium
Zinc
2.35
50
1.45
< 0.001
< 20
13.8
< 0.001
< 0.01
410
< -0.06
70
mg/1
Hg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
Mg/1
25
-------
On April 14, 1977 and July 1, 1977, analysis was again completed for
elements listed as toxic. At this time samples were analyzed to include raw
untreated waste (which served as influent to both the BBC and the extended
aeration system), effluent from the RBC, and effluent colleeted'from the
secondary treatment lagoon. In all but one case it was found the elements
were detectable but generally below accurate quantitative measurement. The
exception was zinc. In each case this element was definitely present
(Figures 5, 6, and 7_).
Metal
METALS ANALYSIS REPORT
Units Concentration
Aluminum
Antimony
Arsenic
Barium
Beryllium
Boron
Cadmium
Calcium
Chromium
Copper
Iron
Lead
Magnesium
Mercury
Nickel
Potassium
Selenium
Silver
Sodium
Thallium
Zinc
Mg/1
mg/1
mg/1
Mg/1
mg/1
mg/1
Mg/1
mg/1
Mg/1
Mg/1
mg/1
Mg/1
mg/1
mg/1
Mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
Mg/1
< 500
< 0.02
0.001
< 100
< 0.006
<50
<^
2.73
< 20
<10
2.35
50
1.45
< 0.001
<20
13.8
< 0.001
<0.01
410
£0.06
70
Figure 5. General inorganic analysis for background characteristics
of waste treatment system.
26
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WATER ANALYSIS DATA
Parameter
Cadmium
Chromium
Copper
Lead
Nickel
Silver
Zinc
Antimony
Arsenic
Beryllium
Mercury
Selenium
Thallium
Units
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
Primary
Treatment
Lagoon
<0.002
<0.02
<0.05
<0.1
<0.05
<0.1
0.25
<0.2
< 0.001
< 0.005
< 0.001
< 0.001
<0.05
Aeration
Lagoon
<0.002
<0.02
< 0.05
<0.1
<0.05
<0.1
0.20
< 0.2
< 0.001
< 0.005
< 0.001
<0.001
<0.05
RBC
Effluent
<0.002
<0.02
<0.05
<0.1
<0.05
<0.1
0.25
<0.2
< 0.001
< 0.005
< 0.001
< 0.001
< 0.05
Figure 6. Inorganic analysis of waste for toxic substances April 14, 1977
27
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WATER ANALYSIS DATA
Primary
Parameter
Antimony
Arsenic
Beryllium
Cadmium
Chromium
Copper
Lead
Mercury
Nickel
Selenium
* Silver
Thallium
Zinc
Units
mg/i
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
Treatment
Lagoon
<0.02
<0.001
< 0.007
< 0.002
<0.05
<0.04
<0.05
<0.001
<0.02
<0.001
0.80
<0.07
0.095
Aeration
Lagoon
<0.02
^0.001
< 0.005
<0.002
<0.02
<0.01
<0.05
<0.001
0.03
<0.001
2.11
< 0.05
< 0.047
RBC Tap
Effluent Water
<0.02
<0.001
< 0.007
< 0.002
<0.05
0.08
<0.05
<0.001
0.04
< 0.001
1.32
<0.07
0.115 0.02
Figure 7. Inorganic analysis of waste for toxic substances July 1, 1977,
*Results declared invalid due to an erratic atomic adsorption lamp.
28
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Upon examination of samples for the purpose of locating the zinc source
it was found that incoming water from the municipal supply contained a
measurable quantity of this ion. It was later confirmed that a trace
quantity of zinc salts is added to the municipal water for the purpose of
corrosion control. This being the primary source of the metal, no further
effort was expended in the identity of other sources as the quantity added
exceeded the quantity found in the wastewater (Table 13).
TABLE 13. WATER ANALYSIS BY ATOMIC ABSORPTION FOR ZINC
Date
11/3/76
4/14/77
7/1/77
Raw Plant
Effluent
0.025 rag /I
0.95 mg/1
Sample Source and
Aerated Treatment
Effluent
70 Ug/1
0.20 mg/1
0.47 mg/1
Cone en tra t i on
RBC
Effluent
0.25 mg/1
0.115 mg/1
Municipal
Supply
0.20 mg/1
Analysis for Organic Compounds
Analysis for organic compounds were performed with a commercial gas
chromatograph equipped with a flame ionization detector. The gas of choice
was helium. Purchased pre-packed columns as indicated in the Standard
Methods for the Examination of Water and Wastewater, APHA-AWWA-WPCF or
American Society for Testing Materials D-3328-74 were obtained for use to
minimize the possibility of void spaces or improper packing.
Detector signals were fed to a data interface connected with a Spectra-
Physics SP-4000 central processing unit capable of data reduction using
internal standards methods. The actual trace was produced on a printer-
plotter followed by calculated datfa from the central processing unit.
Solutions of analytical grade standards were prepared in distilled
water for each chemical with which the study was concerned up to the limit of
solubility for the chemical. In some cases it proved difficult to obtain
good solubility above 10 mg/1 at room temperature. Prepared known concentra-
tion standards were then used to determine the detector sensitivity, reten-
tion time, plus the minimum qualitative and quantitative limits of the
instrument. The detectable limits of the organic compounds for analysis can
be found in Table 14.
29
-------
TABLE 14. DETECTABLE LIMITS FOR ORGANIC COMPOUNDS WITH FLAME
IONIZATION DETECTOR ON BARBER COLEMAN
(DRAWING NO. A4070') GAS CHROMATOGRAPH
Minimum
Compound Qualitative Limit
me/1
Benzene
Carbon tetrachloride
Chlorinated benzene
Chlorinated ethane
Chlorinated phenol (2,4-di)
Chloroform
2-Chlorophenol
Dichlorobenzene
Dichloroethylene
2,4-Dimethylphenol
Ethyl benzene
Pentachloro phenol
Phenol
Tetrachloroethylene
Toluene
Trichloroethylene
0.25
0.5
0.8
0.8
0.1
0.06
0.10
0.8
0.5
1.0
1.2
3.0
0.2
1.5
0.6
0.8
Minimum
Quantitative Limit
mg/1
0.57
0.83
1.7
1.42
0.20
0.17
0.20
1.7
1.09
1.92
1.82
4.43
0.44
3.16
1.14
1.25
30
-------
Upon completion of the determination of detector response samples of
raw plant effluent, RBC effluent, and aerated lagoon effluent were injected
under the same parameters of temperature and flow rates as were the prepared
analytical standards. In all cases there was no detectable quantity of
materials found (Tables B-4 and B-5) .
In order to confirm the absence of these organic compounds of interest
preparations were made using analytical grade chemicals and raw wastewater
taken from the manufacturing plants effluent. Sufficient numbers of these
preparations were made to confirm that probable detection would have been
possible should the organic compounds of interest have been present.
As was suggested in the discussion of the plan of analysis it was
unlikely that the chemicals listed as toxic would be found in a liquid
detergent plants effluent unless there had been mishandling within a labora-
tory. On the basis of inability to detect the compounds it is assumed raw
materials are free of any contamination of chemicals for which this analysis
was designed and that laboratories are following safety disposal procedures.
In addition these analyses suggest that in the process of biological degrada-
tion of waste there is no formation of toxic organic chemicals appearing on
the list of toxic substances as by-products due to either oxidation in an
aerobic system or fermentation during an anaerobic state.
Organic analyses to include instrument calibration may be found in
Appendices Figures B-l thru B-7 inclusive and Tables B-4, B-5 and B-6.
31
-------
REFERENCES
1. Application of Jthe Bio-disc System for Industrial Wastewater Treatment,
L. G. Blackwell, Tenth Annual Seminar on Air and Wastewater Control,
Clemson University, 1974.
2. Standard Methods for the Examination of Water and Wastewater, 14th
Edition, American Public Health Association, New York, 1976.
3. Methods for Chemical Analysis of Water and Wastes, EPA, 1971.
4. Toxic Materials News, April 15, 1976.
5. Gas-Liquid Chromatography, Stephen Dal Nogare and Richard S. Juvet, Jr.,
Interscience Publishers, 1962.
6. Gas Chromatograph Instruction Manual, Barber Coleman Company for Drawing
A-4070.
7. SP-4000 Microprocessor Instruction Manual, Spectra Physics, Inc., 1977.
8. American Society for Testing Materials, Methods D-3328-74 aT and
D-3257-73, USA.
9. Letter, Colin A. Houston & Associates, Inc., Mamaroneck, New York, 10543
to Effluent Guidelines Division (WH-552) U.S. Environmental Protection
Agency, Washington, D.C., dated January 12, 1978.
32
-------
APPENDICES
APPENDIX A. ROTATING BIOLOGICAL CONTACTOR PILOT STUDY, ANALYTICAL METHODS
Routine grab sample laboratory determinations during the RBC pilot
operation study were carried out by the procedures described in:
American Public Health Association, American Waterworks
Association, and Water Pollution Control Federation, "Standard
Methods for the Examination of Water and Wastewater", 14th
Edition, American Public Health Association, Inc., New York,
1976.
The methods used were:
Biochemical Oxygen Demandp. 543
Chemical Oxygen Demandp. 550
Oil and Greasep. 518
pHp. '460
Suspended Solidsp. 94
Total Solids--p. 91
Total Kjeldahl Nitrogenp. 437
Environmental Protection Agency, National Environmental
Research Center, Analytical Quality Control, "Methods for Chemical
Analysis of Water and Wastes", 1971.
Method used:
Ammonia--p. 134
33
-------
APPENDIX B. DETAILED DATA FOR ANALYSIS OF TOXIC SUBSTANCES
Specific tests for the detection and measurement of toxic substances
were performed on grab samples by atomic absorption spectrophotometry and/or
gas chromatographic techniques. Methods for determination of these para-
meters may be found in:
American Public Health Association, American Waterworks
Association, and Water Pollution Control Federation, "Standard
Methods for the Examination of Water and Wastewater", 14th
Edition, American Public Health Association, Inc., New York,
1976.
American Society for Testing Materials, Methods ASTM
D-3328-74 aT and ASTM D-3257-73.
Inorganic Analysis by Atomic Absorption Spectrophotometry
was performed by R. S. Noonan of South Carolina, Inc.
34
-------
TABLE A-l. DATA OBTAINED DURING OPERATION AT FEED RATE OF 1^9 LITERS/MIN. (STANDARD)
to
Ui
Parameter
Sample
Date
A. Initial
Startup
8/13/75
8/20/75
8/22/75
8/26/75
8/28/75
9/2/75
9/4/75
9/9/75
9/11/75
9/16/75
B. Second
Trial
9/29/75
9/30/75
10/1/75
10/2/75
10/3/75
10/6/75
10/7/75
10/9/75
. 10/10/75
10/14/75
10/15/75
10/16/75
10/21/75
10/22/75
Temo.
Inf.
_
27
27
28
28
25
25
25
24
19
.
20
-
20
-
-
19
19
23
21
22
22
20
-
°C
Eff.
_
24
24
25
25
23
23
23
22
17
.
19
-
19
-
-
21
18
21
22
22
22
19
-
oH
Inf.
-
7.2
8.1
7.8
7.6
8.0
7.9
8.2
7.8
7.6
_
7.1
6.9
6.9
6.8
6.9
7.0
7.8
7.2
7.2
7.4
7.5
7.3
7.1
Eff.
-
7.3
7.5
7.1
7'.3
7.5
7.5
7.5
7.5
7.5
.
7.4
7.0
7.0
7.0
7.0
7.1
7.5
7.5
7.3
7.4
7.4
7.5
7.2
BODs*
Inf.
_
150
340
-
300
250
290
150
180
80
.
150
-
150
-
-
140
-
-
150
-
150
270
-
- me /I
Eff.
_
30
30
-
30
30
30
30
40
20
50
-
60
-
-
100
-
-
40
-
40
35
-
COD -
Inf.
630
1090
1280
1090
850
1010
960
1280
730
1140
-
1330
_
-
1320
1620
-
1090
-
1700
1050
-
me/1
Eff.
473
470
480
580
580
650
550
480
340
1090
-
1160
_
-
1290
1050
-
560
-
730
820
-
WBAS
Inf.
_
3.5
6.2
16.9
17.9
4.6
6.7
2.3
5.0
1.0
4.8
4.0
6.1
6.0
5.8
6.5
18.6
24.8
8.8
8.3
9.4
6.5
7.3
me /I
Eff.
0.86
0.50
0.40
0.23
0.15
0.42
0.15
0.37
0.13
4.2
3.7
2.5
4.2
4.7
6.0
9.1
13.8
1.3
2.0
2.0
4.0
3.6
-------
TABLE A-l, DATA OBTAINED DURING OPERATION AT FEED RATE OF 1.9 LITERS/MIN. (STANDARD)
LO
Sample
Date
C. Third
Trial
12/15/75
12/15/75
12/16/75
12/17/75
12/29/75
12/30/75
D. Fourth
Trial
1/28/76
1/29/76
1/30/76
2/2/76
2/3/76
2/4/76
2/5/76
2/6/76
2/9/76
2/10/76
2/11/76
2/12/76
2/16/76
2/17/76
Terno.
Inf.
-.
11
13
11
10
8
7
8
8
7
8
8
-
9
11
11
13
12
°C
ML.
15
16
13
12
10
10
9
9
8
9
9
-
10
13
11
14
12
oH
Inf.
7.2
7.2
7.2
8.7
7.2
7.2
7.1
7.0
7.2
6.8
6.9
7.0
6.8
8.0
7.1
-
BOD=j* - mp/1
Eff. Inf. Eff.
-
7.2
7.2 160 34
7.2
7.5
50 26
7.2 110 50
7.3
7.2
7.3
7.3
7.0
7.0
7.1
6.9
7.4
7.2
7.3
COD -
Inf.
1370
1120
1180
_
1510
_
1660
2030
2180
*
1810
tns/1
Eff.
680
890
1180
mm
1410
1620
_
1930
2010
w
1500
MBAS
Inf.
7 fi
/ O
7.6
10.0
10.0
8.2
5.65
7 g
/ \J
5.3
11 8
J. JL \J
11.2
8 2
W fc»
20.0
15.0
16.8
3.0
- ms/1
Eff.
3a
. o
4.5
5.5
10.0
7.8
2.8
^ 1
J . JL
6 0
W V/
3.0
3 8
J \J
3.6
4 3
~ «^
8 0
U * \S
7.7
9.0
4.0
6.5
-------
TABLE A-l. DATA OBTAINED DURING OPERATION AT FEED RATE OF 1.9 LITERS/MIN. (STANDARD!
Sample
Date
E. Fifth
Trial
2/26/76
2/27/76
3/1/76
3/2/76
3/3/76
3/4/76
3/8/76
3/10/76
3/11/76
3/12/76
3/16/76
3/18/76
3/19/76
3/22/76
3/23/76
3/24/76
F. Sixth
Trial
3/26/76
3/29/76
3/30/76
4/1/76
4/5/76
4/6/76
4/8/76
Temp.
Inf.
-
-
15
17
18
18
14
12
15
-
-
12
12
14
14
-
_
16
17
-
18
17
16
°C
Eff.
-
-
15
17
18
18
14
12
15
-
-
12
12
14
14
-
_
16
17
-
15
17
15
oH
Inf.
-
-
-
6.1
7.4
7.0
7.2
6.9
6.8
-
8.0
6.5
6.4
6.8
9.3
7.7
_
6.8
6.8
6.4
7.0
7.2
7.1
Parameter
BODs* - me/1
Eff. Inf. Eff.
-
-
-
6.5
7:6
7.2
7.2
7.1
7.1
\
7.5
6.9
6.9 '
7.1
7.8
7.5
- _
7.0
7.0
7.1
6.9
7.4
7.2
COD - me /I MBAS
Inf. Eff. - Inf.
1.6
1.9
1.3
1.6
_ _
1350 980 4.2
2.0
1070 920 4.0
_ _
3.6
1.8
2250 1960 16.0
18.2
36.0
-
-
_
28
22
2670 2350 20
9.4
12.3
12
- me/1
Eff.
3.0
2.8
1.1
1.5
-
4.2
3.0
4.7
-
3.6
3.2
40.0
45.0
45.0
-
-
_
30
24
19.5
9.4
9.0
-
-------
00
Sample
Date
G. Seventh
Trial
4/23/76
4/26/76
4/28/76
5/4/76
5/5/76
5/6/76
H. Eighth
Trial
5/14/76
5/17/76
5/18/76
5/19/76
5/20/76
I. Ninth
Trial
7/16/76
7/19/76
7/20/76
7/21/76
7/23/76
7/26/76
7/27/76
7/29/76
Terno.
Inf.
-
17
-
20
19
22
-
17
19
_
24
25
-
26
-
25
27
°
-------
w
\O
Sample
Date
A. Feed Rate at
2.85 1/min.
10/22/75
10/27/75
10/28/75
10/30/75
11/3/75
11/4/75
11/6/75
B. Feed Rate at
3.8 1 /min .
11/6/75
11/10/75
11/11/75
11/13/75
11/14/75
11/17/75
11/18/75
11/20/75
11/25/75
11/26/75
12/1/75
12/2/75
12/3/75
Terno.
Inf.
18
-
16
17
16
18
19
.
20
19
15
10
12
12
15
9
7
-
9
10
°C
Eff.
19
-
18
19
18
20
22
.
22
20
16
13
15
14
17
11
10
-
10
13
oH
Inf.
7.1
7.0
6.5
7.0
7.0
7.0
7.0
.
6.9
6.9
6.9
-
7.0
7.2
8.0
7.2
7.2
7.5
7.5
7.7
Eff.
7.2
7.2
7.0
7.2
7.5
7.5
7.2
7.1
7.1
7.1
-
7.2
7.5
7.3
7.3
7.3
7.6
7.6
7.8
^^K^H^mMpMMV^^^H
BODs*
Inf.
150
-
-
-
-
75
75
_
-
135
70
-
-
30
80
30
-
-
36
-
- me/1
Eff.
20
-
-
-
-
20
15
_
-
20
30
-
-
20
10
10
-
-
15
-
COD -
Inf.
1300
-
1360
1800
-
790
960
-
-
940
690
-
-
620
820
490
-
-
-
-
me/1
Eff,.
570
-
670
800
. -
400
400
-
-
300
300
-
-
290
330
490
-
-
-
-
MBAS -
Inf.
4.9
4.6
4.4
7.0
4.8
3.1
4.2
-
0.88
0.60
0.60
0.84
0.13
0.08
0.23
0.21
0.20
0.10
1.39
1.00
me /I
Eff.
0.92
0.82
0.88
2.0
0.62
0.58
0.88
-
0.64
0.21
0.38
0.45
0.16
0.01
0.01
0.21
0.18
0.09
0.09
0.18
-------
TABLE A-2. DATA OBTAINED AT FEED RATES GREATER THAN 1.9 LITERS/MIN. (STANDARD}
Sample
Date
C. Feed Rate
76 1/min.
12/3/75
12/4/75
12/5/75
12/9/75
12/10/75
12/11/75
Tetno.
Inf.
at
10
11
9
9
9
°c
Eff.
M
12
14
10
11
11
oH
Inf.
7.0
7.1
6.8
-
7.2
Eff.
7.5
7.5
7.1
-
7.3
BOD
-------
TABLE A-3. DATA OBI
SD AT FEED RATES LESS THAN 1.9 LITERS/Mil
Sample
Date
Temp. °C
Inf. Eff.
PH
Inf.
BODs* - tng/1
Inf. Eff.
COD - me/1
Inf.
Eff.
MBAS - me/1
Inf.
Eff.
A. Feed Rates of
0.9 1/min.
Initial Startup
1/12/76
1/13/76
1/14/76
1/15/76
B. Second Trial
4/8/76
4/9/76
4/13/76
4/15/76
4/19/76
4/21/76
C. Third Trial
5/6/76
5/7/76
5/10/76
5/11/76
5/12/76
5/14/76
H
9
9
8
16
18
21
-
20
.
-
20
20
21
21
13
13
11
14
16
21
21
21
20
20
21
21
7.5
7.1
7.0
7.3
7.0
7.0
9.9
10.0
9.6
8.9
8.4
7.1
7.2
7.1
7.5
7.2
7.2
8.6
8.4
8.4
7.6
8.4
75
115
30
50
1660
1850
990
1500
1070
1060
900
480
340
1610
1050
15.4
16.4
17.8
8.7
7.9
8.2
4.4
4.0
26.1
17.4
6.0
12.0
9.4
4.5
5.5
8.7
7.2
4.5
2.2
1.4
1.2
4.0
0.28
0.10
0.12
0.15
-------
N)
Sample
Date
D. Fourth Trial
5/21/76
5/24/76
5/26/76
5/27/76
6/1/76
6/2/76
6/3/76
6/4/76
6/9/76
6/10/76
6/11/76
6/14/76
6/16/76
6/21/76
6/22/76
6/23/76
6/25/76
6/30/76
7/2/76
E. Fifth Trial
9/3/76
9/7/76
9/9/76
9/10/76
9/17/76
Temp.
Inf.
_
20
22
-
21
24
24
24
25
24
23
22
24
24
23
23
22
25
24
21
°C
Eff.
19
22
-
21
23
23
24
25
23
24
21
23
24
22
23
«
22
25
24
21
oH
Inf.
tm
8.0
7.9
7.8
-
7.6
7.6
7.7
7.8
7.7
7.7
8.1
7.8
7.6
7.8
-
*»
-
7.5
7.6
7.4
BODs* - me /I
Eff. Inf. Eff.
.
8.2
8.4
450 375
8.0
_
7.8
7.9
7.9
7.8
7.9
7.8
8.1
8.0
7.9
8.0
: : :
.
_ _ _
7.6 275 180
7.7 -
7.6
^^iHIMHi^^BM
COD -
Inf.
-
2100
1240
2030
1540
_
1160
1120
950
-
me/1
Eff.
1570
1640
730
780
780
1010
1100
960
475
-
MBAS -
Inf.
28.8
33 6
J *J \J
22.4
13 2
JL.J *-
15 0
JL.J * \J
11.3
12.6
20 0
fctW \J
16.3
2? 0
££ \J
8 S
O . -7
10.0
8 1
\J J.
5 3
J
-------
TABLE A-4. DATA OBTAINED BY SAMPLING INDIVIDUAL STAGES OF THE RBC
OJ
Date
1. 8/18/75
2. 8/26/75
3. 9/8/75
4. 9/11/75
5. 9/25/75
6. 10/1/75
7. 10/10/75
8. 10/16/75
Temp. °C Feed Rate
Source Inf. Liters/Mln,
Influent to Stage I 27 1.9
Stage I
Stage IV (Effluent)
Stage I 25 1.9
Stage IV (Effluent)
Stage I - 1.9
Stage IV (Effluent)
Influent to Stage I 24 1.9
Stage I
Stage II
Stage III
Stage IV (Effluent)
Stage I 17 1.9
Stage IV (Effluent)
Influent to Stage I - 1.9
Stage I
Stage IV (Effluent)
Influent to Stage I 23 1.9
Stage I
Stage IV (Effluent)
Influent to Stage I 22 1.9
Stage I
Stage II
Stage III
Stage IV (Effluent)
BOD5*
mg/1
-
-
_
-
_
-
180
90
-
70
40
-
-
-
-
-
-
150
-
-
-
40
COD
rog/1
-
-
_
-
_
-
1280
1040
480
480
480
-
-
-
-
-
-
-
1700
-
-
-
730
MBAS
mg/1
_
-
-
_
-
_
-
5.0
2.0
1.1
0.85
0.37
-
4.0
-
3.7
24.8
-
13.8
9.4
4.5
3.8
2.5
2.0
Dissolved
Oxygen, mg/1
0
3.7
4.1
1.0
1.8
1.5
1.8
_
-
-
-
-
0.2
0.2
.0
1.0
0.5
0
0.7
1.2
_
-
-
-
-
-------
Date
9. 10/20/75
10. 10/29/75
11. 11/6/75
12. 11/13/75
13. 11/20/75
14. 12/5/75
15. 2/9/76
Temp. °C Feed Rate
Source Inf. Liters /Mi".
Influent to Stage I 16 1.9
Stage I
Stage IV (Effluent)
Stage I - 2.85
Stage IV (Effluent)
Influent to Stage I 19 2.85
Stage I
Stage IV (Effluent)
Influent to Stage I 15 3.8
Stage I
Stage IV (Effluent)
Influent to Stage I 15 3.8
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 11 7.6
Stage I
Stage IV (Effluent)
Influent to Stage I - 1.9
Stage I
Stage IV (Effluent)
me/1
.,
-
-
*
-
80
-
15
70
-
30
80
35
25
10
10
_
-
-
_
-
-
COD
me /I
-
-
_
-
960
-
400
690
-
300
820
665
330
400
330
_
-
-
«.
-
-
MBAS
me/1
-
-
-
4.2
-
0.88
0.60
-
0.38
0.23
0.06
0.01
0.01
0.01
_
-
-
20
-
8.0
Dissolved
Oxvsen. me /I
0.0
0.6
2.1
0
1.9
0
0.2
2.4
0
0.1
1.9
w
-
-
-
-
0
4.65
4.70
0
7.9
8.0
-------
BY SAMPLING INDIVIDUAL STAGES OF THE RBC
Date
16. 3/4/76
17. 3/10/76
18. 3/11/76
19. 3/18/76
20. 4/13/76
21. 4/19/76
Temp. °C
Source Inf.
Influent to Stage I 18
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 13
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 15
Stage I
Stage IV (Effluent)
Influent to Stage I 12
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 18
Stage I
Stage IV (Effluent)
Influent to Stage I
Stage I
Stage IV (Effluent)
Feed Rate BODs* COD
Liters/Min. me/1 mg/1
1.9 - 1350
1200
980
980
980
1.9 - 1070
910
- -
- -
910
1.9
- «"
" m
1.9 - 2250
2100
2000
2000
1950
0.95 - 1070
900
900
0.95
-
-
MBAS Dissolved
me/1 Oxveen, me /I
4.2
4.2
4.2
4.2
4.2
4.0
4.8
5.0
4.7
4.7
0
3.1
4.2
16 0
3.4
- -
4.6
40
7.9
4.5
4.5
4.4
2.1
1.4
-------
Date
22. It/21/76
23. 4/28/76
24. 5/6/76
25. 5/12/76
26. 5/L4/76
Temp. °C
Source Inf.
Influent to Stage I 20
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 17
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 19
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 21
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 21
Stage I
Stage IV (Effluent)
Feed Rate BODs* COD
Liters/Min. mg/1 mg/1
0.95 - 1060
650
480
480
480
1.9 - 1680
890
810
810
810
1.9 - 1930
1050
1050
1050
1050
0.95 - 1610
1150
1050
1050
1050
0.95
- -
-
MBAS Dissolved
mg/1 Oxveen. ma- /I
^MMMMB «
4.0
2.0
1.2
1.2
1.2
2.1
-
_
1.8
15.2
-
-
_
5.0
12
0.7
0.18
0.12
0.12
9.4
-
0.15
_
_
_
-
-
-
-
-
H
-
-
-
-
_
-
-
-
-
0
0
2.6
-------
Date
27. 5/19/76
28. 6/18/76
29. 7/2/76
30. 7/23/76
31 7/26/76
32. 7/27/76
Temp. °C Feed Rate
Source Inf. Liters/Mint
Influent to Stage I 17 1.9
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I - 0.95
Stage I
Stage IV (Effluent)
Influent to Stage I 23 0.95
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 26 1.9
Stage I
Stage II
Stage III
Stage IV (Effluent)
Influent to Stage I 1.9
Stages I & II (Combined)**
Stage III
Stage IV (Effluent)
Influent to Stage I 25 1.9
Stages I & II (Combined)
Stage III
Stage IV (Effluent)
BOD5* COD
mg/1 mg/1
370 1440
840
840
840
300 840
-
-
-
-
-
-
- -
1240
1150
990
990
990
1100
700
-
700
_
-
-
-
MB AS
mg/1
12.6
9.9
-
-
7.5
-
-
-
33
-
-
-
16
5.4
3.0
3.0
2.8
2.6
2.8
1.4
1.2
1.2
2.9
1.8
1.3
1.3
Dissolved
Oxveen, tng/1
0
1.0
-
-
2.8
0
2.5
3.3
0
0.3
0.5
1.7
2.0
0
0.5
1.3
2.0
2.4
-
-
-
-
0
0.1
0.2
0.5
-------
TABLE A-4. DATA OBTAINED BY SAMPLING INDIVIDUAL STAGES OF THE RBC
oo
33. 7/29/76
34. 8/4/76
35. 8/5/76
36. 8/12/76
Temp. °C
S_qurce Inf.
Influent to Stage I 27
Stages I & II (Combined)
Stage III
Stage IV (Effluent)
Influent to Stage I 24
Stages I & II (Combined)
Stage III
Stage IV (Effluent)
Influent to Stage I 25
Stages I & II (Combined)
Stage III
Stage IV (Effluent)
Influent to Stage I 25
Stages I & II (Combined)
Stage III
Stage IV (Effluent)
Feed Rate BOD5* COD
Liters/Min. me/1 me/1
1.9 900 1700
830
830
375 830
1.9
-
-
1240
1070
1030
1030
1.9
-
-
MBAS Dissolved
me; /I p^ypep, pR/1
7.8
1.9
1.4
1.3
8.1
7.0
6.5
6.0
13
7.8
-
7.2
10 0
1.7
2.8
9.4 3.3
*A11 BOD5 samples filtered before testing. BODs measured is soluble 6005.
**Baffle plate between first and second stages removed doubling surface area in the first stage making
three stages.
-------
TABLE A-5. DATA OBTAINED ON SUSPENDED SOLIDS, NITROGEN, PHOSPHORUS,
AND OIL & GREASE UNDER VARIOUS OPERATING CONDITIONS
p-
VD
Sample
Date
8/20/75
8/22/75
8/26/75
8/28/75
9/2/75
9/4/75
9/9/75
9/16/75
9/23/75
9/25/75
9/30/75
10/7/75
10/14/75
10/16/75
10/21/75
10/23/75
10/28/75
10/30/75
11/4/75
11/6/75
11/11/75
11/13/75
11/18/75
11/20/75
11/25/75
12/2/75
Wastewater Feed
Rate,
1/min. Temp. °C
1.9
1.9
1.9
1.9
1.9
1.9
1.9
1.9
3.8
3.8
1.9
1.9
1.9
1.9
1.9
2.85
2.85
2.85
2.85
2.85
3.8
3.8
3.8
3.8
3.8
3.8
27
27
28
28
25
25
25
19
23
17
20
19
21
22
20
18
16
17
18
19
19
15
12
15
9
9
Total Suspended
Solids, ma/1
Inf.
104
84
32
28
76
108
136
88
44
30
_
-
32
76
36
68
36
56
36
72
120
116
124
156
100
84
Eff.
104
116
160
40
72
80
60
52
48
32
_
-
48
48
44
56
36
48
80
68
60
40
40
60
92
132
Nitrogen, mg/1
Inf. Eff.
-
-
-
-
-
-
-
-
-
-
-
-
-
41.2
_
40.0
-
-
-
14.6
-
7.8
-
4.2
8.7
-
-
-
-
-
-
-
-
-
-
-
21.6
-
24.6
_
38.4
-
-
-
12.0
-
6.0
-
0.84
6.5
Phosphorus, me/1
Inf. Eff.
1.44
-
-
3.08
-
-
-
6.63
3.00
3.01
2.05
5.10
5.10
4.00
_
6.93
-
5.75
-
4.50
-
3.93
-
3.20
3.20
1.40
-
-
2.78
-
-
-
5.75
3.00
-
2.50
2.50
2.70
2.70
3.00
-
4.50
-
5.50
-
2.63
-
3.38
-
2.80
3.20
Oil & Grease, me/1
Inf.
-
-
14.1
-
48.7
-
-
6.1
-
-
34.5
16.1
16.1
16.2
-
21.8
-
-
-
22.0
-
14.7
-
21.8
5.9
Eff.
-
-
6.4
-
13.9
-
-
19.2
-
-
21.0
12.7
12.7
19.2
-
47.1
-
-
-
19.1
-
13.0
-
14.4
5.9
-------
TABLE A-5. DATA OBTAINED ON SUSPENDED SOLIDS, NITROGEN, PHOSPHORUS,
AND OIL & GREASE UNDER VARIOUS OPERATING CONDITIONS
Ul
o
Sample
Date
12/4/75
12/9/75
12/11/75
12/16/75
1/6/76
1/13/76
1/20/76
1/26/76
1/29/76
2/3/76
2/10/76
2/17/76
3/4/76
3/10/76
3/18/76
4/13/76
4/21/76
4/28/76
5/6/76
Wastewater Feed
Rate,
1/min. Temo. °C
7.6
7.6
7.6
1.9
No flow 10
0.95
No flow 11
No flow 20
1.9
1.9
1.9
1.9
1.9
1.9
1.9
0.95
0.95
1.9
1.9
10
9
9
13
(in unit)
9
(in unit)
(in unit)
7
7
9
12
18
13
12
18
20
17
19
Total Suspended
Solids, me/1
Inf.
84
44
52
44
-
12
-
-
28
24
36
52
36 (1st
Stage)
52
28
68
88
364
96
Eff.
84
68
32
85
124
112
-
20
32
12
72
60
52
40
20
16
100
132
64
Nitroeen. me /I
Inf.
«.
22.0
17.6
-
38.6
-
-
-
33.0
38.0
26.6
-
24.4
17.9
-
12.6
28.8
22.1
Eff.
_
14.6
16.5
25.8
38.4
-
21.8
-
28.6
25.0
21.6
17.4
17.4
14.0
-
10.9
7.3
11.8
Phosphorus, me/1
Inf. Eff.
3.25
3.38
-
3.25
2.38
-
-
2.50
2.38
-
-
3.38
2.38
3.93
3.93
4.25
3.80
3.50
-
3.25
5.38
4.13
4.50
4.50
_
4.50
4.50
-
-
3.25
2.00
3.40
3.00
4.00
3.00
Oil & Grease, me/1
Inf.
_
'32.6
~
66.4
-
8.6
-
-
-
29.8
4.7
12.9
-
12.7
63.5
7.6
13.7
16.7
24.7
Eff.
«.
31.1
"
66.2
2.1
8.6
-
12.6
-
45.0
42.0
51.0
-
12.0
26.1
1.8
13.0
50.0
42.3
5/12/76
0.95
21
124
48
10.4
6.2 3.75
1.25
34.9
25.2
-------
TABLE A-5. DATA OBTAINED ON SUSPENDED SOLIDS, NITROGEN, PHOSPHORUS,
AND OIL & GREASE UNDER VARIOUS OPERATING CONDITIONS
Total Suspended
Wastewater Feed
Sample
Date
5/19/76
5/27/76
6/3/76
6/10/76
6/16/76
6/23/76
6/30/76
7/21/76
7/29/76
8/5/76
8/10/76
8/17/76
9/19/76
Rate,
1/min.
1.9
0.95
0.95
0.95
0.95
0.95
0.95
1.9
1.9
1.9
1.9
1.9
0.95
Temo. °C
17
_
21
24
24
24
23
_
27
25
24
27
25
Solids,
Inf.
28
88
76
76
124
108
68
92
84
92
92
44
68
me/1
Eff.
92
84
72
24
8.0
60
68
56
72
44
100
72
60
Nitrogen.
Inf.
9.4
22.4
33.0
39.5
27.4
47.6
21.3
68.3
45.9
78.9
66.9
12.0
32.5
mg/1
ML.
5.6
10.4
10.9
8.1
-
6.7
20.4
8.1
6.5
12.3
3.4
4.8
4.8
Phosphorus .
Inf.
-
3.50
3.00
-
4.13
3.00
4.13
3.50
4.13
4.25
4.10
4.10
-
mg/1
Eff.
-
3.75
3.50
-
3.25
2.90
3.40
3.00
4.10
4.00
4.60
3.75
-
Oil &
Grease ,
Inf.
14
14
10
28
29
34
23
20
36
-
69
-
60
.6
.3
.7
.1
.4
.9
.7
.3
.1
.4
.0
mg/1
Eff.
-
35.6
28.1
26.0
-
21.5
13.7
28.4
27.2
-
-
-
17.8
-------
TABLE B-l. ROTATING BIOLOGICAL CONTACTOR EFFLUENT
Element
Antimony Mg/1
Arsenic Mg/1
Beryllium Mg/1
Cadmium Mg/1
Chromium ug/1
Copper Mg/1
Lead Mg/1
Mercury Mg/1
Nickel Mg/1
Selenium Mjg/1
Silver Mg/1
Thallium Mg/1
Zinc Mg/1
4/14/77
<200
< 1
< 5
< 2
< 20
< 50
< 100
< 1
< 50
< 1
< 100
< 50
250
Samole Date
7/1/77
<200
< 1
< 7
< 2
< 50
< 80
< 50
< 1
< 40
< 1
*1.32 ing/1
< 70
115
*Results declared invalid due to erratic atomic absorption lamp.
52
-------
TABLE B-2. RAW PLANT WASTE INORGANIC ANALYSIS FOR TOXIC METALS
Element
Antimony Mg/1
Arsenic Mg/1
Beryllium MS/1
Cadmium Ajg/1
Chromium MS /I
Copper MS/1
Lead Mg/1
Mercury MS/1
Nickel Mg/1
Selenium MS/1
Silver MS/1
Thallium Mg/1
Zinc MS /I
Sample
4/14/77
<200
< 1
< 5
< 2
< 20
< 50
< 100
< 1
< 50
< 1
< 100
< 50
< 250
Date
7/1/77
£200
< 1
< 7
^ 2
< 5
< 40
< 50
< 1
< 20
< 1
*0.8 mg/1
-------
TABLE B-3. EXTENDED AERATED LAGOON EFFLUENT
Element
Antimony Mg/1
Arsenic itg/1
Beryllium *ig/l
Cadmium Hg/1
Chromium Ug/1
Copper i^g/1
Lead Mg/1
Mercury i\g/l
Nickel *ig/l
Selenium Mg/1
Silver «g/l
Thallium Mg/1
Zinc Mg/1
11/3/76
< 20
1
< 6
< 2
< 20
< 10
50
<: i
<20
< 1
-------
TABLE B-4. ORGANIC ANALYSIS ON ROTATING BIOLOGICAL
CONTACTOR EFFLUENT FOR TOXIC SUBSTANCES
Compound
Benzene
Carbon tetrachloride
Chlorinated benzene
Chlorinated ethane
Chlorinated phenol (2, 4-di)
Chloroform
2-Chlorophenol
Dichlorobenzene
Dichloroethylene
2 , 4 -Dime thy 1 ph eno 1
Ethyl benzene
Pentachlorophenol
Phenol
Tetrachloroethylene
Toluene
Trichloroethylene
Results
£0.
-------
TABLE B-5.- ORGANIC ANALYSIS ON RAW PLANT WASTE FOR TOXIC SUBSTANCES
Compound Results of Analysis Dates of
Benzene
Carbon tetrachloride
Chlorinated benzene
Chlorinated ethane
Chlorinated phenol (2 ,4-di)
Chloroform
2-Chlorophenol
Dichlorobenzene
Dichloroethylene
, 2,4-Dimethylphenol
Ethyl benzene
Fentach loropheno 1
Phenol
Te trach loroe thy lene
Toluene
Trichloroethylene
^0.25
< 0.5
<0.8
<0.8
< 0.1
<0.06
<0.10
* 0.8
< 0.5
<1.0
< 1.2
<3.0
< 0.2
<1.5
< 0.6
x 0.8
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
6/16/77
6/20/77
6/17/77
6/20/77
6/20/77
6/15/77
2/2/77
3/28/77
3/28/77
3/28/77
3/24/77
3/22/77
6/20/77
6/20/77
6/17/77
3/20/77
4/27/77
Analysis
6/20/77
6/20/77
6/20/77
4/27/77
6/17/77
4/27/77
4/27/77
4/27/77
4/27/77
6/20/77
3/30/77
5/9/77
56
-------
TABLE B-6. ORGANIC ANALYSIS ON AERATED LAGOON EFFLUENT FOR TOXIC SUBSTANCES
Compound Results of
Benzene
Carbon tetrachloride
Chlorinated benzene
Chlorinated ethane
Chlorinated phenol (2,4-di)
Chloroform
2 -Chloro phenol
Dichlorobenzene
Dichloroethylene
2,4-Dimethylphenol
Ethyl benzene
Fentachloro phenol
Phenol
Tetrachloroethylene
Toluenft
Trichloroe thylene
<0.25
< 0.5
<0.8
< 0.8
< 0.1
< 0.06
^ 0.10
<0.8
<0.5
<1.0
<1.2
<-3.0
< 0.2
<1.5
<0.6
<0.8
Analysis
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
mg/1
Dates of Analysis
6/16/77 6/20/77
6/20/77
6/20/77
6/20/77
6/15/77 6/20/77
4/27/77
3/28/77
4/27/77
4/27/77
4/27/77
4/27/77
4/27/77
6/20/77
6/20/77
6/20/77
4/27/77
57
-------
TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
1. REPORT NO.
EPA-600/2-78-129
3. RECIPIENT'S ACCESSION NO.
4. TITLE AND SUBTITLE
Effects of Liquid Detergent Plant Effluent on the
Rotating Biological Contactor
5. REPORT DATE
June 1978 issuing date
6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)
Frederick T. Lense
Stanley E. Mileski
8. PERFORMING ORGANIZATION REPORT NO.
Charles W. Ellis
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Texize Chemicals Co.
Div. of Morton-Norwich Products, Inc.
P.O. Box 368
Greenville, SC 29602
10. PROGRAM ELEMENT NO.
1BB610
11. CONTRACT/GRANT NO.
S-803892013
12. SPONSORING AGENCY NAME AND ADDRESS
Industrial Environmental Research Lab. -Cincinnati, OH
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, Ohio 45268
13. TYPE OF REPORT AND PERIOD COVERED
Task Final 8/13/75-6/30/77
14. SPONSORING AGENCY CODE
EPA/600/12
15. SUPPLEMENTARY NOTES
IERL-Ci Project Officer for this report is Ronald J. Turner,
513/684-4481
16. ABSTRACT
This report summarizes data on the treatment of wastewaters from a liquid
detergent manufacturing plant by a rotating biological contactor and
presents the findings of an analytical effort to determine the presence or
absence of metals and organic compounds which were among those listed in the
Consent Decree, Train vs NRDC, et al, June 1976. Even under the best operating
conditions, the rotating biological contactor performance was essentially
equivalent to that of the extended aeration lagoon. All metals except zinc
(0.25 mg/1) were below minimum measurable limits. All organic compounds subjected
to analysis by gas chromatograph were below minimum detectable limits.
7.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTIFIERS/OPEN ENDED TERMS
c. COSATI Field/Group
Industrial Wastes
Industrial Waste Treatment
Detergents
Rotating Biological
Contactor
68D
91A
18. DISTRIBUTION STATEMENT
RELEASE TO PUBLIC
19. SECURITY CLASS (ThisReport)
Unclassified
21. NO. OF PAGES
68
20. SECURITY CLASS (Thispage)
Unclassified
22. PRICE
EPA Form 2220-1 (Rev. 4-77) PREVIOUS EDITION is OBSOLETE 53
U.S. GOVERNMENT P8IOTIHG OFFICE; 1978-757-140/1343 Region No. SHI
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