United States
Environmental Protection
Agency
Water Engineering
Research Laboratory
Cincinnati OH 45268
Research and Development
EPA/600/S2-86/004 Mar. 1986
4>EPA Project Summary
Evaluation of Activated
Carbon for Enhanced COD
Removal from Pharmaceutical
Wastewater
Richard Osantowski and Richard Wullschleger
Two activated carbon technologies
were evaluated for pharmaceutical
wastewater treatment: powdered acti-
vated carbon (PAC) added to an acti-
vated sludge system (PACT®) and
granular activated carbon (GAC) treat-
ment of pharmaceutical plant second-
ary effluent. The lack of information on
applicable removal technologies for
total chemical oygen demand (TCOD)
prevented promulgation of best avail-
able technology economically achiev-
able (BAT) limitations and new source
performance standards (NSPS) for
TCOD for pharmaceutical manufactur-
ing plants in 1983 (EPA/440/1-83/
084). The purpose of this study was,
therefore, to evaluate the ability of
these technologies to achieve con-
sistent reductions in the effluent TCOD
of pharmaceutical wastewaters.
Pharmaceutical wastewaters from a
manufacturing plant that produces
fermentation products (Subcategory A)
and chemical synthesis products (Sub-
category C) were treated in trailer-
mounted pilot plants. The biological
treatment train consisted of three
activated sludge systems operated in
parallel. PAC was added to two of the
units in selected dosages. The third unit
was used as a control. The physical-
chemical treatment train consisted of
chemical coagulation with alum and
anionic polymer, pH adjustment with
caustic (when needed), clarification,
multi-media filtration, and GAC ad-
sorption.
The PAC-enhanced biological treat-
ment train reduced effluent TCOD well
below the level required by best practi-
cable control technology currently
available (BPT). PAC also improved the
settling rate of the mixed liquor sus-
pended solids over that of the control.
However, a viscous floating mass of
mixed liquor solids developed in the
PAC units (but not in the control) and
resulted in premature termination of
the study. The GAC physical-chemical
treatment train also reduced pharma-
ceutical plant effluent TCOD below the
average BPT level.
This Project Summary was devel-
oped by the EPA's Water Engineering
Research Laboratory, Cincinnati, OH,
to announce key findings of the re-
search project that is fully documented
in two separate volumes of the same
title (see Project Report ordering infor-
mation at back).
Introduction
In November 1982, the U.S. Environ-
mental Protection Agency (EPA) pro-
posed effluent limitations and standards
(EPA/440/1-82/084) for the pharma-
ceutical manufacturing point source
category. Some of the proposed regula-
tions limited the discharge of TCOD, a
nonconventional pollutant, from existing
and new pharmaceutical manufacturing
facilities. However, because of a lack of
information on applicable TCOD removal
technologies, limitations and standards
for TCOD were not promulgated along
with the other regulations on October 27,
1983.
In April 1984, EPA decided to conduct
pilot-scale performance evaluations of
-------
activated carbon treatment technologies
using actual pharmaceutical waste-
waters. The purpose of these studies was
to evaluate the ability of these technolo-
gies to achieve consistent reductions in
the effluent TCOD of pharmaceutical
wastewater.
At a Subcategory A and C pharma-
ceutical manufacturing plant that used
secondary treatment and reported high
TCOD concentrations in their discharge
monitoring report, two technologies
were evaluated:
1. PAC addition to the activated-
sludge aeration basin, and
2. GAC treatment of the secondary
effluuent.
Quality Assurance/Quality
Control Methods
Sample analyses were conducted on-
site in a field laboratory and in a base
laboratory in another state. All samples
were collected by the pilot plant op-
erators using prelabeled containers.
Analyses for TCOD, soluble chemical
oxygen demand (SCOD), total biochemi-
cal oxygen demand (TBOD), nitrogen-
inhibited biochemical oxygen demand
(NIBOD), nitrogen-inhibited soluble bio-
chemical oxygen demand (NISBOD),
chloride, total suspended solids (TSS),
and volatile suspended solids (VSS) were
performed at the onsite laboratory. All
other analyses were performed at the
base laboratory. The base laboratory also
provided computer support to the field
and base laboratories for analytical
scheduling, sample labeling, chain of
custody, and other quality assurance/
quality control (QA/QC) functions.
All samples were refrigerated after
collection and were iced during shipment
to the base laboratory. Samples that were
analyzed onsite were analyzed the same
day they were collected, and no addi-
tional chemical preservation methods
were required. Samples sent to the base
laboratory for phosphate, nitrogen, and
total organic carbon (TOC) analyses were
preserved with sulfuric acid addition to
pH2.
TCOD and SCOD analyses were per-
formed by the Hach* colorimetric method
(Federal Register, Vol. 45, No. 78, April
21, 1980). All other analyses for the
conventional parameters were per-
formed according to the procedures de-
scribed \r\Methods for Chemical Analysis
of Water and Wastes (EPA/600/4-79/
020, U.S. Environmental Protection
'Mention of trade names or commercial products
does not constitute endorsement or recommendation
for use.
2
Agency, Cincinnati, Ohio, 1979). At least
10 percent of all samples were analyzed
in replicate for all conventional para-
meters. At least 5 percent of all samples
were spiked with appropriate reagents
for analysis of all conventional para-
meters except TSS and VSS. Blanks and
reference samples were analyzed for
each analytical run or sample lot.
QA/QC objectives for precision were
to have a maximum of 20 percent dif-
ference between replicates for TBOD,
NIBOD, NISBOD, and VSS. A maximum
of 15 percent difference between repli-
cates was sought for all other conven-
tional parameters. Accuracy objectives
were ± 20 percent spiked sample re-
covery for TBOD, NIBOD, and NISBOD,
and ±15 percent spiked sample recovery
for other parameters.
Of 652 replicate samples, 618 (94.8
percent) were within the precision per-
cent difference criteria. Of 322 spiked
samples, 303 (94.1 percent) were within
the percent recovery objectives.
In all, 3,732 analyses were performed,
with 1.5 percent of the analytical results
deleted for QA/QC reasons. The project
had a 98.1 percent completion rate.
Biological Study
From September to December 1984,
an 83-day study was conducted using
one biological pilot plant as the control
and two biological pilot plants as the
experimental (PAC-fed) systems. The
three activated sludge units were op-
erated in parallel.
System Operation
Raw pharmaceutical wastewater was
collected just before it entered the full-
scale aeration basins and was used as
the feed to the pilot plants. This flow
consisted of neutralized and equalized
pharmaceutical waste combined with a
nominal amount (=* 6 percent) of mac-
erated, chlorinated sanitary waste.
The two experimental activated sludge
systems were identified as biological
treatment system nos. 1 and 2 (BTS-1
and BTS-2). Each system consisted of an
aeration tank (5,940 L in BTS-1 and
5,560 L in BTS-2) and a 2,840 L circular
center feed clarifier. Each aeration tank
had three aeration cells in series, and the
air flow to each cell was controlled in-
dependently. Pumps were used to supply
wastewater, return sludge, and add
chemicals to each system. PAC slurry
was pumped to the first cell of the ex-
perimental systems, and sodium hydrox-
ide was pumped to all three systems as
needed to maintain an adequate pr
range.
The control pilot plant (BTS-3) con
sisted of an aeration tank with three
aeration cells in series (total volume o
180 L) and a 47-L secondary clarifier
Peristaltic pumps were used to fee<
wastewater to the system, to recirculat<
settled sludge, and to waste sludge. Th<
raw wastewater was pumped to a mixei
equalization tank that served as the feei
reservoir for each of the three pile
plants.
The targeted aeration basin hydrauli
retention times (HRT's) and solids re
tention times (SRT's) were 3 and 10 days
respectively, for all systems. Thesi
values were similar to those used in th
full-scale plant before the start of th
pilot plant tests. Solids were wasted fror
the third cell of each aeration basin t
allow a more positive contrrsttest perioc
208 and 827 mg/L of PAC were added t
the influents of BTS-1 and BTS-2, re
spectively, and in the second test perioc
496 and 1,520 mg/L of PAC were adde
to BTS-1 and BTS-2, respectively.
Daily composite samples were take
from the raw feed wastewater and fror
the three clarifier effluents using autc
matic sampling equipment, and from th
wasted mixed liquor obtained from th
waste solids holding tanks.
Test Phases
The planned pilot plant operation wa
scheduled for a series of five phases a
described below:
Phase 1 — Start-up
The three biological pilot plants wer
operated for 10 days after being seede
with mixed liquor from the full-seal
aeration basins. The objective of th
phase was to determine whether th
effluents were comparable for each <
the three pilot plants.
Phase 2 — Acclimation
Following Phase 1, PAC addition to th
influents was initiated for BTS-1 ar
BTS-2 at rates of 208 mg/L and 82
mg/L, respectively. Single doses of PA
(as a 10-percent slurry) were added
each aeration cell of BTS-1 and BTS
each day for the first 10 days to reach th
calculated equilibrium PAC concentr
tion, and the operation of all three uni
was continued for an additional 13 day
Phase 3 — Intensive Test Perio
Pilot plant operation continued for 1
days with Phase 2 operational cone
tions, but the frequency of sampling ai
analysis was increased.
-------
Phase 4 — Transition and
Acclimation
PAC feed to the influent of BTS-1 and
BTS-2 was increased to 496 and 1,520
mg/L, respectively. Single doses of PAC
(as a 10-percent slurry) were again added
to each aeration cell of BTS-1 and BTS-2
for each of the first 10 days to reach the
calculated equilibrium PAC concentra-
tions. Operation was planned to continue
until steady state conditions were
achieved based on effluent SCOD mea-
surements. Following equilibrium attain-
ment, a second 2-week intensive sam-
pling period (Phase 5) was to be con-
ducted; but as discussed below, Phase 5
was not initiated.
Operational Problems
During Phase 3, the pH began to de-
crease significantly in all three systems.
Samples collected for nitrogen analyses
confirmed that nitrification was occuring
in the three systems and the addition of
caustic was initiated to maintain the
mixed liquor pH near 7. BTS-1 and BTS-2
also showed evidence of significant
denitification in the clarifiers, which
caused some of the sludge to float. The
sludge recycle rates for these systems
were increased in an attempt to maintain
amall sludge inventories in the clarifiers
and thereby minimize the floating sludge
in the experimental clarifiers.
Near the end of Phase 4, a viscous
floating layer of mixed liquor suspended
solids (VFMLS) formed on the surface of
the clarifiers and the aeration basins of
the two PAC-fed systems. This layer re-
sulted in significant reductions in the
mixed liquor suspended solids (MLSS) in
the aeration basins of BTS-1 and BTS-2.
The VFMLS developed first in BTS-1 and
about 10 days later in BTS-2. The
phenomenon did not occur in BTS-3, the
control system. As a result of this
problem, the Phase 5 intensive test
period was cancelled. However, data
generated during Phase 4, just before the
onset of the viscous layers, were used to
evaluate the effects of the 496 and 1,520
mg/L PAC feed rates to BTS-1 and
BTS-2, respectively. Also, during Phase 4
(prior to the VFMLS formation), the aera-
tion basin effluent line plugged and the
MLSS overflowed the aeration basin of
BTS-2; this resulted in a significant loss
of both volatile MLSS (MLVSS)and PAC.
As a result, the data presented later for
the 1,520 mg/L PAC system were col-
lected when the system was not in
equilibrium, at least as far as the MLSS
concentration was concerned.
Test Results
Feedwater Quality
TSS averaged 639 mg/L for 83
samples. The raw waste TCOD was quite
variable, ranging from 2,260 to 12,000
mg/L, and it averaged 7,030 mg/L. The
average TBOD concentration was 2,830
mg/L, with a range from 1,700 to 4,400
mg/L. Nitrogen and phosphate were
present in adequate amounts in the raw
wastewater (BOD:N and BOD:P ratios
were less than 20 and 100, respectively).
Pilot Systems
During Phase 1, the effluent SCOD
from BTS-1 and BTS-2 averaged 754and
770 mg/L, respectively, whereas the
effluent from BTS-3 averaged 849 mg/L.
This variation did not result from design
differences between the pilot plants but
from an initial problem created by the use
of a different (colder) air supply for aera-
tion of BTS-3. Once this fact was recog-
nized, heaters were installed in the aera-
tion basin of BTS-3 to raise the tempera-
ture to that of the other two systems. The
average Phase 2 temperatures of 31°,
32°, and 30°C for BTS-1, BTS-2, and
BTS-3, respectively, demonstrated that
this problem was corrected.
Table 1 summarizes the average op-
erating parameters and effluent quality
during Phases 3 and the latter part of
Phase 4. Average HRT's ranged from 3.0
to 3.1 days, and average SRT's ranged
from 9.4 to 10.0 days. During Phase 3,
average aeration basin temperatures
ranged from 31.5° to 32.5°C, and during
Phase 4, they ranged from 27° to 28°C
and from 24° to 27°C for the two interim
test periods, respectively. Average MLSS
for the control system (BTS-3) during the
three time periods ranged from 4,770 to
4,790 mg/L. For the experimental
systems (BTS-1 and 2), the average
MLSS concentrations ranged from 5,850
to 8,830 mg/L as the PAC addition to the
influent was increased from 208 to 1,520
mg/L.
The addition of PAC resulted in some
improvement in sludge settleability;
however, the MLSS settling rate re-
mained at very low levels (from 0.01 to
0.05 cm/min). The effect of the PAC on
the average effluent SCOD concentra-
tions is also shown in Table 1. During
Phase 3, PAC feed rates of 208 and 827
mg/L resulted in effluent SCOD'sof 459
and 265 mg/L, respectively, compared
with 825 mg/L for the control. During
Phase 4, a PAC feed of 496 mg/L re-
sulted in an effluent SCOD of 314 mg/L
compared with 670 mg/L for the control.
A PAC feed of 1,520 mg/L to BTS-2 in
Phase 4 produced an effluent with 194
mg/L of SCOD, and the control effluent
contained in 583 mg/L. As discussed
earlier, the MLSS in BTS-2 during Phase
4 was not in equilibrium. If it had been,
the effluent SCOD would probably have
been less than the reported 194 mg/L.
Physical-Chemical Study
Concurrent with the biological study,
final effluent from the full-scale treat-
ment system was treated in trailer-
mounted pilot plants. The physical-
chemical treatment train consisted of
chemical coagulation with alum and
anionic polymer; pH adjustment with
caustic (when needed); clarification;
multi-media filtration; and GAC adsorp-
tion. The TSS removal technologies were
used for pretreatment of the wastewater
before carbon adsorption because of the
high TSS concentrations (an average of
341 mg/L and a range of 65 to 1,560
mg/L. Pretreatment for TSS removal was
necessary, but optimizing this pretreat-
ment was not an objective of this study.
Initially, an attempt was made to op-
erate the carbon columns in the down-
flow mode. However, a combination of
rapidly changing chemical demand of the
feed water plus poor performance of the
multi-media filter created a large carry-
over of TSS to the carbon column system.
As a result, the carbon columns had to be
backwashed several times during this
run. A review of the first run's results
determined that design deficiencies in
the backwash system of the carbon
columns were causing the bed to be
mixed during this procedure, so the re-
sults were not representative. Design
changes were implemented, and a sec-
ond run was initiated in the upflow mode.
Feed Wastewater Characteristics
Table 2 summarizes the pilot plant
feed wastewater characteristics during
the entire study as determined from 24-
hr composite sample analyses.
Pretreatment Results
The pilot-scale clarifier and filter
were run continuously throughout the
testing program. The feed rate to the pilot
clarifier was 17 to 23 L/min (4.5 to 6.0
gpm). This was equivalent to an overflow
rate of 9 to 13 m3/day-m2 (230 to 305
gal/day-ft2). Chemical treatment before
clarification consisted of alum, anionic
polyelectrolyte, and caustic addition (as
needed for pH control). Chemical feed
concentrations were based on onsite jar
testing. Required alum and polymer
3
-------
Table 1. Operating Parameters and Average Effluent Quality During Phase 3 and the Latter Part of Phase 4
Phase 3 Latter Part of Phase 4
Pay 34-47
Day 62-65
Day 71-76
Operating Parameter
BTS-1
BTS-2
BTS-3
BTS-1*
BTS-3
BTS-2"
BTS-:
Operational data:
Feed flow, L/min
PAC flow, L/min
RS flow, L/min^
Waste ML flow,
PAC dosage, mg/L
F/M, g COD/g MLSS-day**
HRT, days
SRT, days
Mixed liquor data:
Temperature, °C
pH (range)
DO, mg/Lft
TSS. mg/L
Effluent data:
TCOD. mg/L
SCOD, mg/L
TOO. mg/L
NIBOD. mg/L
NISBOD, mg/L
TSS, mg/L
VSS. mg/L
Removals:
A verage feed TCOD, mg/L
TCOD removal, %
1.34
0.018
3.01
0.420
208
3.1
9.5
32.5
4.1-7.5
3.3
5850
585
459
158
16
<6
85
60
8120
92.8
1.26
0.018
408
0.367
827
ND
3.1
10.0
32
4.5-7.7
3 4
7690
532
265
110
15
<5
190
158
8120
93.4
0.044
0
0.163
0.013
0
0.64
3.0
9.4
31.5
6.0-8.7
4.3
4790
1070
825
290
27
<8
143
109
8120
86.8
1.38
0.031
3.80
0.419
496
ND
3.0
9.7
27
6.0-7.2
3.6
7000
454
314
115
NA
NA
59
50
7420
93.9
0.045
0
0.092
0.013
0
0.69
3.0
9.8
28
6.6-8.1
5.0
4770
770
670
NA
NA
44
46
7420
89.6
1.27
0.032
6.37
0.374
1520
ND
3.0
10.0
24
6.7-7.5
3.4
8830
334
194
NA
12
3
108
76
6810
95.1
0.04'
C
0.09'
o.oi:
(
0.7i
3.C
9.t
2.
6.1-7.'
4.i
4781
68!
58:
to
It
9i
7(
681 (
89..
* Data for periods just before onset of VFMLS on surfaces of aeration basins and secondary clarifiers
t Return sludge
ft Mixed liquor
** Food to microorganism ratio
t Not determined
ji Dissolved oxygen
§ Not analyzed
dosages ranged from 200 to 1,340 mg/L
and from 0.2 to 3.0 mg/L, respectively.
About 0.8 m3 (200 gal) of sludge was
produced for every 3.8 m3 (1000 gal) of
wastewater treated based on 30-min
settling tests.
Following chemical treatment and
clarification, the pharmaceutical plant
effluent was filtered using a downflow
granular multi-media filter with an effec-
tive filtering area of 0.1 m2 (1.0 ft2). The
filtration rate during the study ranged
from 100 to 120 L/min-m2 (2.5 to 3.0
gpm/ft2). Filter media consisted of two
grades of garnet sand (15 cm each)
covered by silica sand (38 cm) and a top
layer of anthracite coal (51 cm). Table 3
summarizes the pretreatment efficiency.
All analyses except temperature (grab)
were performed on 24-hr composite
samples. At the end of the study, exami-
nation of the multi-media filter revealed
that 41 cm (16 in.) of media had been lost
and that some intermixing of the media
had occurred. The conclusion was that
this situation was created by a design
deficiency in the filter backwash system,
and therefore, the filter removals were
not representative.
GAC Results
Four columns were operated in series
in the upflow mode. Each of the four
columns had an effective area of 0.1 m2
(1.0ft2). Insufficient time was available to
select an optimum carbon. Calgon's
Filtrasorb 300 was chosen because of its
successful application on similar waste
streams. Virgin carbon was used in each
of the four columns.
Clarified and filtered pharmaceutical
plant final effluent was pumped through
the activated carbon columns. Each of
the four GAC columns was loaded with
1.3 m (4.3 ft) of carbon. The system was
operated at a hydraulic flow rate of 37
L/min-m2 (0.9 gpm/ft2), which resulted
in an empty bed contact time (EBCT)of 35
min per column, or 140 min total.
Grab samples were collected once per
day from five locations around the
activated carbon columns during the
GAC run. These included the influent anc
effluent from each column. The sample:
were analyzed for SCOD.
This GAC run was conducted over 42
days of operation. During this period
199,830 L (52,795 gal) of pretreatec
pharmaceutical plant effluent was treatec
by the GAC columns. Each day during the
study, the time and cumulative flow
totalizer readings were recorded at the
time of sampling. This information was
used to prepare SCOD breakthrough
curves.
Breakthrough is defined as the pro
cessing time (or volume) after which the
impurity concentration in any of the
carbon column effluents is no longei
acceptable. From each curve, the time
and volume processed to reach an SCOC
breakthrough of 300, 400, and 500 mg/1
were calculated.
The carbon usage rate in kg/1,000 I
(lb/1,000 gal) can be determined b]
-------
dividing the weight of carbon in each
column by the volume processed to
breakthrough. Pilot study results showed
that the carbon use to maintain an
effluent SCOD concentration of 300
mg/L or less decreased from 3.1 to 2.1
kg/1,000 L (26 to 18 lb/1,000 gal) as the
EBCT was increased from 35 to 140 min,
respectively. For a 400 mg/L or less
SCOD effluent, the carbon use ranged
from 2.6 to 1.7 kg/1,000 L (22 to 14
lb/1,000 gal), and for a 500-mg/Lor less
effluent SCOD, the. carbon use ranged
from 1.9 to 1.2 kg/1,000 L (16 to 10 Ib/
1,000 gal) as the EBCT was increased
from 35 to 140 min.
Daily 24-hr composite samples were
also collected of the GAC influent and
final effluent and analyzed for TSS,
TBOD, TCOD, and SCOD. Table 4 sum-
marizes the removal efficiencies for each
of these parameters. Note that the
averages in Table 4 are for the entire run
and not for some specific effluent SCOD
concentration.
Identification of Specific
Organic Compounds
To identify the specific organic con-
stituents in the pharmaceutical plant
effluent, a series of mass spectral and
infrared studies was carried out by
several laboratories. A composite sample
of biologically treated pharmaceutical
plant final effluent was collected on
March 14, 1984, and submitted to three
independent laboratories for gas chro-
matography/mass spectrometry (GC/
MS) low-resolution analysis. Approxi-
mately 17 peaks were observed by each
of the laboratories.
An extract of a composite sample
made from the control pilot plant effluent
collected from October 17 to 21, 1984,
resulted in a chromatogram with approxi-
mately 9 of the 17 major peaks having
mass spectra similar to those determined
from the March 14 sample.
A major component in the gas chro-
matogram of the biologically treated
effluent from the pilot plant control was
tentatively identified as 2-butyl-4-amino-
5-pyrimidyl-carbinol by a combination of
high-resolution GC/MS, low-resolution
GC/MS, gas chromatography/Fourier
transform infrared spectrophotometry,
and chemical information concerning the
manufacturing processes at this plant.
The concentration of this component was
approximately 4 mg/L. Dimethylphenol
was also identified as a minor component.
Conclusions
Conclusions regarding the biological
pilot study are as follows:
Table 2. Summary of Feed Wastewater Characteristics
Parameter Average
Range
TBOD. mg/L
TSS. mg/L
TCOD. mg/L
SCOD. mg/L
pH, units
Temperature, °C
151 (33)*
341 (8JJ
1410 (57)
830 (551
24 (57)
61-360
65-1560
730-3180
412-1330
7.7-8.6(80)
14-40
*Parenthesis indicate number of observations.
Table 3. Pretreatment Efficiency
Parameter Influent
Effluent
% Removal
TSS. mg/L
TBOD. mg/L
TCOD. mg/L
SCOD, mg/L
pH , units
Temperature, °C
301
158
1360
828
7.7-8.6(67)
14-37 (42)
121
81
877
657
6.4-8. 1 (67)
15-36 (42)
60 (70)*
49 (29)
35 (43)
21 (51)
^Parenthesis indicate number of observations.
Table 4. Average Removal Efficiencies for Activated Carbon
Parameter Influent (mg/L) Effluent (mg/L)
i Removal
TSS
TBOD
TCOD
SCOD
87
121
914
651
75
>85
432
25 1
14 (38)*
<30(14)
53 (42)
61 (42)
1. PAC addition to the activated
sludge process can increase the
SCOD removal from pharmaceuti-
cal manufacturing wastewater.
2. The PAC/activated sludge process
cannot be recommended as a
viable process for this plant's
wastewater until the cause of the
VFMLS is identified and adequate
safeguards against its occurrence
are demonstrated.
The results of the physical-chemical
study are as follows:
1. GAC treatment can reduce the
secondary effluent SCOD to 200 to
400 mg/L.
2. The chemical clarification and
multi-media filtration technologies
provide adequate pretreatment for
operation of the downstream GAC.
3. The combination of biological treat-
ment and GAC can reduce the in-
fluent TCOD from 7,060 mg/L to
an average effluent SCOD of 200 to
400 mg/L.
4. Carbon use is a function of the
effluent SCOD concentration and
the EBCT. A summary of the carbon
use rates determined from the pilot
study is shown in Table 5.
Table 5. Carbon Use. kg/1.000 L
Design Effluent SCOD. mg/L
EBCT, min
300
400
500
35
70
105
140
3.1
2.1
2.8
2.1
2.6
2.1
2.1
1.7
1.9
1.9
1.5
1.2
The full report was submitted in fulfill-
ment of Contract Numbers 68-02-3928
to Rexnord and 68-01-6675 to E.G.
Jordan Company with Rexnord and
Environmental Science and Engineering,
Inc., acting under a subcontract to E.G.
Jordan Company under the sponsorship
of the U.S. Environmental Protection
Agency.
"Parenthesis indicate number of observations
. S. GOVERNMENT PRINTING OFFICE:1986/646-l 16/20789
-------
Richard Osantowski and Richard Wullschleger are with Rexnord, Inc., Milwaukee,
WI43214.
Clyde R. Dempsey is the EPA Project Officer (see below).
The complete report consists of two volumes entitled "Evaluation of Activated
Carbon for Enhanced COD Removal from Pharmaceutical Wastewater:"
"Volumel. Final Report," (Order No. PB86-148 160/AS; Cost $16.95, subject
to change).
"Volume II. Appendices,"(Order No. PB 86-148 178/AS; Cost $28.95, subject
to change).
The above reports will be available only from:
National Technical Information Service
5285 Port Royal Road
Springfield, VA22161
Telephone: 703-487-4650
The EPA Project Officer can be contacted at:
Water Engineering Research Laboratory
U.S. Environmental Protection Agency
Cincinnati, OH 45268
United States
Environmental Protection
Agency
Center for Environmental Research
Information
Cincinnati OH 45268
u.s.ornc!AL MAL
Official Business
Penalty for Private Use S300
EPA/600/S2-86/004
ft
V OH '" -' •' • ^-
'^Kb--\ : Q 3
t * - W -J
• -
0000329 PS
------- |