United States
 Environmental Protection
 Agency
Air and Energy Engineering
Research Laboratory
Research Triangle Park NC 27711
 Research and Development
EPA/600/S7-85/031a Sept. 1985
 Project  Summary
An  Evaluation  of  Full-Scale
Fabric  Filters  on  Utility
Boilers:  SPS  Harrington
Station  Unit  3

John W. Richardson, John D. McKenna, and John C. Mycock
  The objective of this program was to
 evaluate and characterize the perfor-
 mance of full-scale fabric filter units in-
 stalled on 100 MW or larger coal-fired
 power plants. This document reports
 results of total mass and fractional size
 particulate emission tests at South-
 western Public Service's Harrington
 Station Unit 3 from July 8 to July 11,
 1981. Three outlet and one inlet mass
 and fractional size emission tests were
 performed. Due to the absence of inlet
 ports, inlet testing was done by bypass-
 ing the baghouse and testing at the
 outlet ports of the fabric filter. The fab-
 ric filter is a shake/deflate unit with 32
 compartments. Each compartment has
 204 bags, 30 ft 6 in.* long and 11.5 in. in
 diameter. Design air/cloth ratio is 2.8.
 Average outlet concentration was 0.007
 lb/106 Btu. Inlet loading was 2.0 lb/106
 Btu, giving a 99.65% collection effi-
 ciency. Particle sizing tests indicated
 that the mass geometric mean diame-
 ter for the three outlet tests ranged
from 7.2 to 13 /jm with an inlet mass
diameter of 60 /urn.
  This Project Summary was devel-
oped by EPA's Air and Energy Engi-
neering Research Laboratory, Research
 Triangle Park, NC, to announce key
findings of the research project that is
fully documented in a separate report
of the same title (see Project Report
ordering information at back).
*Readers more familiar with the metric system may
 use the conversion factors at the end of this
 Summary,
Introduction
  EPA funded a program  in 1980 to
evaluate and characterize the perfor-
mance of full-scale fabric filter units in-
stalled on 100 MW or larger coal-fired
power plants. The program required
particulate total mass and fractional size
efficiency testing and collection of per-
formance, operation, maintenance, and
problem information. Southwestern
Public Service's Harrington Station
Unit 3 was selected as one of the sites to
be tested.
  Four outlet particulate total mass
tests and one inlet particulate total mass
test were performed. Run 1 was voided
because an incorrect stack moisture
content was assumed which resulted in
the wrong size sampling nozzle being
used. Runs 2, 3,  and 5 (outlet tests) are
considered  valid. Run 4 was the inlet
particulate test which was conducted by
bypassing the baghouse and testing at
the stack outlet  ports. These data are
summarized in Table 1.
  Sampling was conducted at four
ports spaced equidistant around a
20.8ft diameter stack. Three traverse
points were assigned to each port, re-
sulting in a 12-point traverse particulate
test.

Process and Control Device
Description
  SPS's Harrington Station Unit 3 con-
sists of a tangentially fired, Combustion
Engineering steam generator, capable
of producing 2,682,393 Ib steam/hr at

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Table 1.
Data Summary
(Southwestern Public Service, Harrington, Unit 3)
                                        OUTLET EMISSION DATA
                                                                                                     July 8-11, 1981
                                                                             Orsat
 Run
  &
 Date
    Paniculate Emissions
Ib/W6 Btu
Ib/hr
gr/acf
   MW
Production
% Opacity
 Flow
 acfm
dscfm
Temp.
  °F
CO2
 %
02
%
                                                                           CO
Baghouse
Differential
 Pressure
 in. H2O
  Stack
  Gas
Moisture, %
   1
7/8/81
   2
7/9/81
   3
7/9/81
   5
7/10/81
 •Void-
  0.009       35.91   0.0024
  0.009
  0.003
 34.55   0.0022
 11.7-    0.0008
                   340.5
                     5.5
           349.7
             5.5
           349.4
             5.6
                      1712460
                       944245
             1737950
              911922
             1707690
              938412
                       323.2
          323.2
          322.6
                                                                       11.6
                                                                       11.6
                                                                       11.6
                                                                     6.5    0.0
                                                                     6.5    fl.t?1 •
                                                                     6.5    0.0
                              East BH:
                                6.98
                              West BH:
                                6.26

                              East BH:
                                8.1
                              West BH:
                                6.7

                              East BH:
                                7.1
                              West BH:
                                6.6
                                                                                                           10.6
                                                                                                           10.2
                                               aINLET EMISSION DATA

Run
&
Date

4
7/9/81


Paniculate Emissions

Ib/W6 Btu Ib/hr gr/acf

2.0 7958.5 0.5167


MW
Production
% Opacity

349.3
98.1

Orsat
Flow
acfm Temp. CO2 O2 CO
dscfm °F % % %

1777280 -..„ 11.6 6.5 0.0
947257 34t°

Baghouse
Differential
Pressure
in. H2O
East BH:
5.4
West BH:
4.9

Stack
Gas
Moisture, %

10.7

"Tests conducted by bypassing the baghouse.

2500 psig, 1005°F superheat, and 1005°F
reheat.
  Pulverized Western coal with average
parameters of 8475 Btu/lb, 0.3% sulfur,
and 5.5% ash is burned.
  Paniculate emissions are controlled
by a Wheelabrator-Frye, Inc., baghouse
designed to operate at a flue gas flow of
1,650,000  acfm at  313°F, with a mini-
mum design efficiency of 98.6%. Design
air/cloth ratio is 2.81  gross, 2.90 with
one  compartment  down, and 3.0 with
two compartments down.
  There are two baghouse systems at
Harrington Unit 3,  east and west, each
with its own operating control  system
and bypass dampers for start-up, emer-
gency operation, and shutdown. This
shake/deflate cleaning system consists
of 6528 bags: 32  compartments with
204 bags  per compartment.

Testing  Methodology,
Sampling Equipment, and
Procedures
  Particulate emission tests were con-
                              ducted according to U.S. EPA Reference
                              Method  5 procedures in conjunction
                              with Methods 1, 2, 3, and 4.  Each test
                              included a 12-point traverse with  a 10-
                              minute sampling  duration  for  each
                              point.
                               Assembly and use of the  impactor
                              train followed state-of-the-art protocol
                              and general Method  5 sampling  train
                              procedures.  Special  precaution was
                              taken to avoid rough handling of loaded
                              impactors, overloading of the  impactor,
                              and in the performance of hot leak tests.
                               The particulate sampling equipment
                              used is referred to as the "EPA Method
                              5 Particulate Sampling Train," designed
                              and developed by EPA.
                               The apparatus consisted of a stainless
                              steel sampling nozzle, a Method 5 filter
                              holder containing an 87 mm Schleicher
                              and Scherell #1-HV high-purity glass fil-
                              ter, a series of  four Greenburg-Smith
                              impingers, a check valve, a leakless vac-
                              uum pump, a dry gas  meter, and a cali-
                              brated orifice. The  impingers and con-
                              necting tubes were made of Pyrex  glass
                              and were connected with glass  ball-
                                                        and-socket joints. The probe was Type
                                                        316 stainless steel.
                                                          Using the type "S" pitot tube, a veloc-
                                                        ity traverse was performed along each
                                                        traverse axis during each particulate
                                                        run. The velocity pressure at each sam-
                                                        pling point was measured using an in-
                                                        clined manometer.
                                                          Prior to, and at the conclusion of, each
                                                        run, the complete  sampling train, in-
                                                        cluding probe and  nozzle, was leak-
                                                        tested by plugging  the  nozzle with a
                                                        rubber stopper and applying a vacuum
                                                        of 15 in. Hg to the system.
                                                          At the completion of  each test the
                                                        sampling nozzle, the inside of the probe,
                                                        the inside of the thimble holder, and the
                                                        front-half of the glass fiber filter  holder
                                                        were washed with acetone. The wash-
                                                        ings were collected and stored.
                                                          Tests to determine carbon dioxide,
                                                        oxygen, and carbon monoxide were
                                                        conducted using an Orsat analysis ac-
                                                        cording to EPA Method 3.

                                                        Discussion of Results
                                                          During this test series,  there were no

-------
 deviations from normal operating con-
 ditions for Unit 3 that could be deter-
 mined from the control room, baghouse
 control room data, or conferences with
 the boiler operators. Control room data
 monitored during the test period com-
 pared closely with previous data. Emis-
 sion  rates in  pounds per  million  Btu
 were calculated using average F factors
 derived from  coal analysis  performed
 on SPS coal.  Outlet  paniculate emis-
 sions at Harrington  Unit 3 averaged
 0.007 lb/106  Btu (27.39  Ib/hr) for the
 three outlet tests. The single inlet emis-
 sion test,  performed by bypassing the
 baghouse, resulted in an emission rate
 of 2.0 lb/106 Btu (7958.5 Ib/hr). Emission
 rates for outlet Runs 2 and 3 were very
 close: 0;009 lb/106 Btu (35.9 Ib/hr), and
 0.009 lb/106  Btu (34.6 Ib/hr), respec-
 tively. Outlet Run 5 resulted in an unex-
 pected low emission rate of 0.003 lb/106
 Btu (11.7 Ib/hr). The inlet run performed
 at the outlet stack ports also resulted in
 a  lower emission rate than expected
 when compared to previous test results
 conducted at Unit 3.
  Cascade impactor sampling was per-
 formed under the supervision of  Re-
 search Triangle Institute, July 8 and 9,
 1981. Three outlet and one inlet  im-
 pactor tests were performed. Emission
 rates for the impactor and  Method  5
 tests are compared in Table 2.
  After comparing previous ash analy-
 ses with the analysis made on the ash
 generated during this test series, it was
 concluded that little difference existed
 between the typical coal burned and the
 coal burned during this testing project.
 The coal burned at Southwestern Public
 Service Co. is a western coal, high in
 calcium and silica, mined from the Pow-
 der River Basin near Gillette, Wyoming.
  Bag analyses were performed on four
 bags (two  used and two new). The tests
 performed included permeability, ten-
 sile strength, MIT flex, and Mullen burst.
  Overall,  the bag analyses indicated  a
 greater  percentage loss of strength in
terms of MIT flex, Mullen burst, and ten-
 sile strength than previous tests. The
cleaning procedures differed between
the two testing laboratories but, in gen-
eral, indicated  approximately the same
permeability improvement after clean-
ing.
Table 2.    Gram Loading from Method 5 and Impactor Tests (SPS-Harrington Unit 3)

                               July 8-11, 1981
Run & Date
      Impactor Loading Rates
             gr/acf
Method 5 Paniculate Loading
          gr/acf
Outlet
7/8/81
Outlet
7/8/81
Outlet
7/9/81
Outlet
7/10/81
alnlet
7/9/81
1 0.0004
2 —
3 0.0007
5 0.0015
4 1.06
VOID
0.0024
0.0022
0.0008
0.5167
"Test performed by bypassing the baghouse.

Metric Conversions
  This Summary includes certain non-
metric units for the  reader's conve-
nience. Those more familiar with  the
metric system may use the following
conversion factors.
Nonmetric
Times    Yields Metric
Btu
°F
ft
ft3
gr
in.
in.2
Ib
1.055
5/9 (°F-32)
30.48
28.32
0.065
2.54
6.45
0.454
kJ
°C
cm
1
9
cm
cm2
kg

-------
      J. Richardson, J. McKenna, andJ. Mycock are with ETS, Inc.. Roanoke. VA 24018.
      Dale L. Harmon is the EPA Project Officer fsee below).
      The complete report, entitled "An Evaluation of Full-scale Fabric Filters on Utility
       Boilers: SPS Harrington Station Unit 3," (Order No. PB 85-235 513/AS; Cost:
       $16.00, subject to change! will be available only from:
             National Technical Information Service
             5285 Port Royal Road
             Springfield, VA 22161
             Telephone: 703-487-4650
      The EPA Project Officer can be contacted at:
             Air and Energy Engineering Research Laboratory
             U.S. Environmental Protection Agency
             Research Triangle Park, NC 27711
United States
Environmental Protection
Agency
Center for Environmental Research
Information
Cincinnati OH 45268
Official Business
Penalty for Private Use $300
EPA/600/S7-85/031a
          0CQ0329    PS

          U S  ENVIR  PROTECTION  AGENCY
          REGION 5  LIBRARY
          230  S  DEARBORN  STREET
          CHICAGO               IL    «Q*G4

-------
                     United States
                     Environmental Protection
                     Agency
Air and Energy Engineering
Research Laboratory
Research Triangle Park NC 27711
                     Research and Development
EPA/600/S7-85/030 Nov. 1985
SEPA          Project  Summary
                     Steam  Stripping  of  Fixed-Bed
                     Gasification  Wastewaters
                     F. D. Skinner and B. J. Hayes
                      Laboratory- and bench-scale steam
                     stripping tests were conducted using
                     gas liquor from a fixed-bed coal gasifier
                     at the Department of Energy's Morgan-
                     town Energy Technology Center. The
                     gas  liquor was pretreated by solvent
                     extraction (for phenol removal) and fil-
                     tered prior to stripping. This report pre-
                     sents the results of the wastewater
                     stripping tests  and provides engineer-
                     ing and environmental data for the de-
                     sign of steam  strippers for fixed-bed
                     gasification wastewaters. The labora-
                     tory tests were performed primarily to
                     determine the effect of pH on contami-
                     nant removals. During the bench-scale
                     tests, samples of influent, effluent, and
                     overhead vapor and condensate were
                     analyzed for a number of species of po-
                     tential environmental concern (dis-
                     solved gases, sulfur and nitrogen spe-
                     cies, trace metals, organics, and other
                     water quality parameters). Mass trans-
                     fer coefficients for ammonia, carbon
                     dioxide, and hydrogen suffide stripping
                     were calculated.
                      This Project Summary was devel-
                     oped by EPA's Air and Energy Engineer-
                     ing Research Laboratory, Research Tri-
                     angle  Park, NC, to announce key
                     findings of the research project that is
                     fully documented in a separate report
                     of the same title (see Project Report or-
                     dering information at back).

                     Introduction
                      The raw gas liquor resulting from
                     fixed-bed coal  gasification processes
                     contains  a  number of contaminants,
                     some of which are present in relatively
                     high concentrations. These include tars
                     and  oils,  dissolved organic (especially
                     phenols), dissolved gases (e.g., NH3,
                     HCN, H2S, C02), and both suspended
and dissolved inorganics. Removal of
these contaminants in a multiple step
wastewater treatment system has been
included in many proposed commercial
coal gasification plant designs.
  Steam stripping for the removal (and,
in some cases, recovery) of dissolved
ammonia and acid gases is a treatment
process which is common to most of
these designs. Capital and  operating
costs for steam stripping systems can
account for a significant portion of the
overall cost of wastewater treatment in
coal gasification plants. There is a need,
therefore, to develop design data that
can be used to maximize the cost effec-
tiveness of this process. In addition, the
outlet streams need to be characterized
to evaluate the effects of contaminants
on downstream process performance.
  This report presents the results of
laboratory- and bench-scale stripping
work, using wastewater obtained from
a fixed-bed gasifier at the Department of
Energy's Morgantown Energy Technol-
ogy Center (DOE-METC).

Objectives and  Approach

  The principal  objectives  of the
wastewater stripping study were:
  • To provide data characterizing the
   various stripper outlet streams for
   species of environmental interest
   with respect to potential impacts on
   downstream process performance
   and environmental effects.
  • To develop mass transfer data that
   could be used in the design of  a
   steam stripper for wastewater from
   fixed-bed gasifiers following pre-
   treatment by solvent extraction, fil-
   tration,  and pH adjustment (if
   needed).

-------
  To meet these objectives, two series
of tests were performed. First laboratory-
scale screening tests were conducted to
determine the effect of wastewater pH
on the removal  of dissolved ammonia,
H2S, C02, HCN, and the residual phenol
remaining after pretreatment by solvent
extraction using methyl isobutyl ketone
(MIBK). These tests were conducted by
heating a measured quantity of  pH-
adjusted  wastewater to  95-100°C in a
distillation flask. Gas (air or  nitrogen)
was sparged through the  contents of
the flask, and the ammonia concentra-
tion and pH of the wastewater were
measured over a 270-minute  period.
After each run the contents of the flask
were analyzed for pH, conductivity, total
alkalinity, ammonia, cyanide  (free and
total), phenol,  sulfide, sulfite,  sulfate,
and thiocyanate.
  The  results of the laboratory tests
were used to determine the influent pH
for the second series of tests, performed
using a bench-scale steam stripping ap-
paratus. The stripper was a 0.1 m (4 in.)
diameter stainless steel column packed
with 1.2 m (4 ft) of 0.6 mm (1/4-in.) ce-
ramic Intalox saddles. Solvent-
extracted wastewater was preheated to
90°C in an electric heater and pumped
into the top of the column.  Stripping
steam  entered  below the packing and
flowed countercurrent to the waste-
water. Concentric tube heat exchangers
were  used  to condense and cool  the
overhead vapor and to cool the stripped
effluent. Samples  were obtained peri-
odically during each run  of the various
inlet and outlet  streams for analysis of
the environmental  and performance
parameters of interest. The principal in-
dependent variable  during these tests
was the steam  to wastewater  influent
flow ratio.

Results and Conclusions
Laboratory-Scale Results
  • Greater than 90% removals of dis-
    solved ammonia and alkalinity (due
    to dissolved C02) were obtained by
    stripping  the  extracted METC
    wastewater  at a pH of 8.6 (existing
    after solvent extraction) and higher.
    Ammonia removal increased from
    about 92% to over 99.9% as the ini-
    tial wastewater pH was raised from
    8.6 to 11.0.  A  decrease in C02 re-
    moval efficiency from over 99 to
    96% was observed when increasing
    pH from 8.6 to 11.0.
  •  Dissolved H20 removals decreased
    from 80 to 50% as the initial pH was
   increased from 8.6 to 11.0. Cyanide
   removals were  between  10 and
   20%; most of the cyanide content of
   this wastewater was present as
   fixed (and therefore non-strippable)
   cyanide at the pHs evaluated. It is
   likely that some of the free cyanide
   initially in the wastewater had been
   converted to fixed cyanide and/or
   thiocyanate, and the removal  may
   be higher for "fresh" wastewater.
  • Removal of the small amount  of
   phenol (total) remaining in the ex-
   tracted wastewater was found to be
   less than 20%. No clear trends were
   observed as the  pH was increased.
   Technical questions remain regard-
   ing phenol stripping for unextracted
   wastewater  or wastewater  having
   phenol  levels closer to those ex-
   pected from commercial  gasifier
   systems.
  • Because of  its buffering capacity
   (due to HC03/C03 alkalinity), the
   wastewater  required a significant
   quantity of lime to raise its pH from
   8.6 to 11.0. In order to go from pH
   8.6 to 9.5,  470 milliequivalents
   (meq)of lime per liter was required:
   to go from pH 8.5 to 11, nearly 1200
   meq of lime per liter was  needed.
   The buffering capacity of the waste-
   water is readily  reduced by steam
   stripping of the dissolved C02.
  • Two-stage stripping would likely be
   required to remove all (or nearly all)
   of the dissolved ammonia and acid
   gas species (expecially H2S and
   HCN) from this wastewater.
  • Stripping the wastewater at a pH of
   8.6 produced significant quantities
   of solids that collected on the sur-
   faces of the equipment and led to
   plugging problems.  Increasing the
   pH to 9.5 or higher by lime addition
   significantly reduced the plugging.
   The solids are likely ammonium
   salts, possibly ammonium  carbon-
   ate or ammonium carbamate; how-
   ever, the solids were not analyzed.

Bench-Scale  Tests:
Environmental
  • Thiocyanate, sulfate, fluoride, and
   chloride are not removed by steam
   stripping. These  contaminants will
   be  found in the stripper  effluent
   stream.
  • Trace elements detected in stripper
   outlet streams appear to be largely
   system contaminants, possibly
   from the column, ceramic packing,
   and the lime added for  pH adjust-
  ment.  It appears that some of the
  volatile trace elements (e.g., ar-
  senic, selenium, and antimony) are
  stripped to some extent. This has
  implications for the potential envi-
  ronmental impacts  of the stripper
  overheads and effluent streams. For
  example, it may be possible to re-
  duce the amounts  of some toxic
  trace elements thafmight otherwise
  concentrate in brines produced by
  downstream evaporators; however,
  this potential was not investigated.
•  Phenols were  the  major organic
  species found in the wastewater. 2,
  4-dimethyl phenol was largely
  stripped and was found principally
  in the overhead condensate. Other
  phenols (e.g., phenol, cresol, and
  other xylenols) were only partially
  stripped and are found in both the
  effluent and overhead condensate.
•  Hydrocarbon analyses of the over-
  head vapor were  hampered by the
  relatively high concentration of
  residual  methyl  isobutyl  ketone
  (MIBK) from the solvent extraction
  process. Toluene and xylene were
  not detected in any  of the samples,
  and benzene  was detected (at
  1.1 ppmv) in only  one  set  of the
  samples collected on charcoal. The
  residual solubility of MIBK in water
  is significant (reportedly about 2%
  by weight). Some  other organics
  may be present in  the MIBK layer
  produced as a result of condensing
  the stripper overhead stream. The
  solvent layer was not analyzed in
  this work.
•  The presence of significant quanti-
  ties of solvent vapor in the stripper
  overhead vapor stream  has poten-
  tial impacts on the downstream pro-
  cesses that may be  used to  remove
  H2S and other acid gas species from
  this stream.The  residual solvent
  concentration  after  extraction/inert
  gas stripping seen  in this study is
  probably not representative of com-
  mercial operations. In a commercial
  extraction system, solvent recovery
  would be more efficient, not only to
  reduce the possibility of problems
  with downstream processes, but
  also to reduce  solvent makeup re-
  quirements.  However,  more effi-
  cient solvent stripping would likely
  produce additional streams contain-
  ing species stripped from the raffi-
  nate (including ammonia and hy-
  drogen sulfide).
•  Carbonyl sulfide was detected in all

-------
Table 1.    Component Removal Summary for Bench-Scale Stripping Tests3

                                                                          % Removal
Run Date
9/25
9/27
11/1
11/2
n/5"
Steam/Influent
kg/m3
133 ± 7
298 ± 31
282 ±44
459 ± 49
297 ± 34
Influent
PH
9.03 ± 0.05
9.02 ±0.15
9.14 ± 0.03
9.17 + 0.06
8.45 ± 0.04
NH3
83.6 ± 3.8
94.3 ± 1.5
91.6 ± 4.5
95.0 ± 1.7
31.0 ± 25.6
CO2
93.3 ± 0.5
98.3 ± 0.6
98.6 ± 0.2
99.0 ± 0. 1
8T.6 + 5.1
Sulfide
30.9 ± 17.9
17.7 ±38.7
65. 1 ±9.1
69.4 ± 16.6
-7.6±S1.8
Total
Cyanide
18.9 ± 4.2
23.8 ± 13.6
59.7 ± 3.5
16.6 ±41.1
23.7 ± 21.0
Total
Phenols
-5.2 ± 5.4
44.9 ±9.7
-72.8 ±28.6
4.2 ± 37.8
46.7 ± 12.4
aValues shown are mean ± sample standard deviation. All runs performed using 1.2 m (4 ft) of packing.
bn/5 run performed using effluent collected from previous stripping runs at similar steam/influent ratios.

   overhead vapor samples at concen-
   trations of about 0.04 ppmv in the
   two-pass stripper run and from 1 to
   5 ppmv in the single-pass runs. Car-
   bon disulfide was the only other sul-
   fur species detected (1 to 32 ppmv).

Bench-Scale Tests:
Performance
  • Contaminant removals consistent
   with the results of the laboratory-
   scale tests were found for  ammo-
   nia, C02, and H2S. Data scatter pre-
   cluded the  development  of
   meaningful correlations for HCN
   and phenol (total) removal as a
   function of the steam to influent
   ratio. The component removals are
   summarized in Table 1.
  • Contaminant removals were found
   to increase with increasing steam to
   wastewater ratio up to 250-300 kg
   steam/m3 wastewater. Higher ratios
   produced no statistically significant
   improvement in contaminant re-
   movals. There would appear to be
   little incentive to operate at a steam
   to wastewater ratio  higher  than
   about 250 kg/m3.
  • Overall volumetric mass transfer
   coefficients (KLa)  were calculated
   for steam stripping of NHj, CO2, and
   H2S for the wastewater. For ammo-
   nia, KLa  increased  from 1.8 to 6.6
   hr~1 as the liquid mass velocity in-
   creased from about 550 to 2000 kg/
   m2hr. Over this same range KLa for
   CO2 increased from 2.2 to 4.5 hr1.
   KLa for H2S was found to be approx-
   imately constant at 0.6 hr~1  over
   this range of liquid flow rates.

-------
      F. D. Skinner andB. J. Hayes are with Radian Corporation, Austin, TX 78766.
      William J. Rhodes is the EPA Project Officer (see below).
      The complete report, entitled "Steam Stripping of Fixed-Bed Gasification
        Wastewaters,"(OrderNo. PB85-247450; Cost: $16.95, subject to change) will
        be available only from:
            National Technical Information Service
            5285 Port Royal Road
            Springfield, VA 22161
             Telephone: 703-487-4650
      The EPA Project Officer can be contacted at:
            Air and Energy Engineering Research Laboratory
            U.S. Environmental Protection Agency
            Research Triangle Park, NC 27711
United States
Environmental Protection
Agency"
Center for Environmental Research
Information
Cincinnati OH 45268
Official Business
Penalty for Private Use $300

EPA/600/S7-85/030
        0030329   PS

        U  S  ENVIR  PROTECTION AGENCY
        REGION  5  LIBRARY
        230  $  DEARBORN  STREET
        CHICAGO               li.   60604

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