Superfund Treatability Clearinghouse Advanced Electric Reactor (aer) For The Treatment Of Dioxin-contaminated Soils


                                  EPA/540/2-89/028
    SUPERFUND TREATABILITY
          CLEARINGHOUSE
            Document Reference:
J. M. Huber Corp. "Advanced Electric Reactor (AER) for the Treatment of Dioxin-
         Contaminated Soils." 14pp. February 1984.
           EPA LIBRARY NUMBER:

         Superfund Treatability Clearinghouse - EXPD

-------
                SUPERFUND TREATABILITY CLEARINGHOUSE ABSTRACT


 Treatment Process:       Thermal  Treatment - Pyrolysis

 Media:                   Soil/Sandy

 Document  Reference:      J.  M.  Huber  Corp.  "Advanced Electric Reactor (AER)
                         for the  Treatment of Dioxin-Contaminated Soils."
                         14  pp.   February 1984.

 Document  Type:           Memo

 Contact:                 James  Boyd
                         J.M. Huber Corporation
                         P.O. Box 2831
                         Borgen,  TX   79007
                         806-274-6331

 Site Name:               J.M Huber Corp. - Borgen, TX (Non-NPL)

 Location  of Test:        Borgen,  TX

 BACKGROUND;  This newsletter reports  on the Huber Technology Groups (HTG)
 high temperature advanced hazardous waste treatment technology capable of
 very high destruction and removal efficiencies of various hazardous wastes.
 This newsletter addresses the  destruction of PCBs in an EPA certification
 test of the HTG Advanced Electric Reactor.
 OPERATIONAL INFORMATION;  The  Advanced Electric Reactor of HTG is a high
 temperature electrically heated  low gas flow reactor, capable of attaining
 temperatures of 4,000°F  to  4,500°F under low flow conditions, which allows
 for relatively long residence  times;  i.e., 5 seconds.  For comparison
 purposes, a rotary kiln  has  only a one to two second residence time.  Soils
 can also  be treated and  after  removal of contaminants they can be land-
 filled.   The reactor can be  connected  to off-the-shelf stack gas cleaning
 equipment to ensure high removal of all pollutants.  The reactor vessel
 uses nitrogen gas.  Oxygen  is  absent  from the combustion process thus
 preventing the formation of  unwanted oxygen containing by-products, such as
 dioxin and furans.  The  system is mobile and was used in a PCB destruction
 test witnessed by the U.S. EPA and Texas Air Board.  There is no discussion
 of the analytical techniques used to measure PCBs.  No QA/QC discussion is
 included.
 PERFORMANCE;  The results of a trial burn run of the HTG Advanced Electri-
 cal Reactor in removing  PCBs are shown on Table 1.  Initial concentration
 of Arochlor 1260 was 3000 ppm.   The Destruction Efficiencies were 99.9999%
 in all but one of the tests.   Solid phase soil PCB concentrations were well
 below the 50 ppm level after treatment.  No HC1, C1-, dioxins or furans
were observed at the stack.  Only trace NO  and particulate levels were
observed.  Chlorine removal  efficiency in the scrubber and carbon beds were
greater than 99.999*.  An accompanying document indicated that the reactor
 technique could also destroy dioxin contaminated material to below current
detection levels.   However,  there were no detailed results of dioxin tests
reported  in the newsletter.
3/89-49                                              Document Number:  EXPD
  NOTE:  Quality assurance of data maya not be appropriate for all uses.

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 CONTAMINANTS;

 Analytical  data is  provided  in  the  treatability  study  report.  The
 breakdown of  the contaminants by  treatability group  is:

 Treatability Group              CAS  Number        Contaminants

 W02-Dioxins/Furans/PCBs         11096-82-5        PCB-1260
Note:  This  is  a  partial  listing  of data.  Refer  to  the document  for more
       information.
3/89-49                                              Document Number:  EXPO

  NOTE:  Quality assurance of data aaya not be appropriate for all uses.

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                                                   TABLE 1
                                 SUMMARY OF RESULTS:  EPA CERTIFICATION TEST
Run
#
1
2
3
4
Date
9/27/83
9/28/83
9/29/83
9/29/83
Feed
#/Min
15.1
15.7
15.7
15.8
R. Temp.
<°F>
4100
4100
4100
4100
Total N2
(scfm)
147.2
147.2
147.2
147.2
% Gas- Phase
Cyclone (DE)
99.99992
99.99992
99.99960
99.99995
Control
Stack (ORE)
99.9999950
99.9999994
99.9999980
99.9999940
Solid Phase PCBs, PPM
Treated Feed
0.0005
<0.0005
0.0006
0.0010
3/89-49
                                                                    Document Number:   EXPD
NOTE:  Quality assurance of data may not be appropriate for all uses.

-------
                     J. M.Huber  ^^^^^^.^^^^    ENviRONMEimL-Qtwtnr
                                P.O. Box 2831               DATE  RECEIVED

                            Borge, Texas 79007             FEB21198-
(806)27.4-6331                                                          **      '
     3-8«58                     February 14, 1984             „ .   4
                                                        — topics to _ .
  Mr.  Robert J. Schreiber, Jr.                           - ^Je  jjfnt
  Director, Division of Environmental Quality            - wrcuiaie
  Missouri Department of Natural Resources
  P.O.  Box 1368  1915 Southridge Drive
  Jefferson City, Missouri 65102

  Dear Mr. Schreiber:

  Dr.   Schofielci and I want to thank you for the recent opportunity  in  Kansas
  City  to provide you with a presentation on the J.   M.  Huber Corporation's
  Advanced  Electric  Reactor (AER) for the treatment of  dioxin-contaminated
  soils.  Your thoughtful and constructive comments  were appreciated and  very
  helpful to us.

  Of  special interest was your suggestion that J. M. Huber consider a  dioxin
  demonstration in Southwest Missouri, possibly at the Syntex site  in Verona,
  Missouri.  We have contacted Syntex and will jointly explore such  a  possi-
  bility in a meeting scheduled for February 23.  We will keep you advised of
  our  progress.

  Of course,  we remain very interested in ultimately applying our technology
  to  the dioxin problems in Eastern Missouri -and would appreciate your  sug-
  gestions  and assistance in developing a demonstration test for the AER on
  the type of soils and contamination levels in that area.   We would like to
  visit  the  sites in Eastern Missouri to evaluate  the applicability of  the
  AER  to the specific sites and would be most appreciative  if you could help
  arrange such a visit.

  Finally,  we  are pleased that you accepted our invitation for you and  your
  staff  to visit to our Borger,  Texas test facility for a detailed examin-
  ation of the AER 12 inch pilot plant. I  will contact your secretary to  work
  out a convenient date for the visit.  As you suggested,   I will also  try to
  arrange a simultaneous visit for the EPA staff and Syntex.

  Again,  please  accept  our personal thanks for your  assistance.   We  look
  forward  to future opportunities to assist you with the dioxin problems  in
  Missouri.
 Sincerely yours,
          r- J^
    n P. DeKany        (j
   rketing Manager
 Environmental Activities

-------
                                                             ENVIRONMENTAL QUALITY
                                                             DATE  RECEIVED

                    J.M.Huber Corporation          FEB2H98-;
                               P. O. Box 2831              	Copies to_
                           Borger. Texas 79007
(6O6) E7A-633I
TELEX.73-8453
February 10,  1984
Mr. Robert Schreiber
Missouri Dept.  of Natural Resources
Div. of Environmental Quality
P.O.  Box  1368
Jefferson City, MO   65102

Dear Mr. Schjunber: AOQD

The J^uber  Technology  G_roup  (HTC)  has  developed a  high-temperature,
advanced  hazardous waste treatment technology capable of extremely high
destruction and removal  efficiencies  in the treatment  of these wastes.

To  inform  responsible  professionals,  we periodically  issue  newsletters
summarizing the status  of  this technology and  progress  toward  its full-scale
operation.  Outlined in this  newsletter are several major points concerning
recent equipment and  process design improvements  and the results  of our
recent EPA/TSCA Certification Tests using PCB.

The Huber Technology  Group Advanced EElectric Reactor (AER)  detoxification
process has five inherent advantages over most competing technologies:

(I)   Extremely high operating temperatures.

(2)   A very low gas-phase flow rate.

(3)   The ability to  process contaminated soils as well as gases and liquids.

(4)   An absence of oxygen in the process gases.

(5)   Mobility.

The first  advantage cited  of the extremely  high operating temperature  is
obvious—high  destruction efficiency.  The AER operates at   4000°-4500°F vs.
less than 3000°F for rotary kiln incinerators.

The second advantage above  is more  subtle.   The AER is heated with elec-
trical  power...not  by  combustion and  therefore  does^ not  generate  large
quantities  of gaseous combustion by-products to be vented to the atmosphere.
The advantage  of this low gas flow rate is two-fold but  may not be obvious.

First,  the  very low gas flow rate  (i.e., approximately  500 scfm in a ISO
tons/day commercial-scale plant)  permits very  high gas-phase residence times
at a reasonable capital  cost.   For example, a five-second residence time at

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 The Advanced Electric Reactor Newsletter                              Page 2


 2500°F  would require an insulated cylindrical vessel 12'  long  with  a 5' inside
 diameter.  This high temperature residence  time  is provided  in the  insulated
 post-reactor vessel  shown on  the  accompanying  process  flow  sheet.   For
 comparison  purposes, a rotary kiln  incinerator typically  has  only  a one-  to
 two-second  residence time and  requires much larger equipment.

 Another advantage of a very  low gas flow rate is that it  permits the use  of
 economical,  small-scale equipment to more intensively clean the gases.  As  the
 gases exit the insulated residence vessel, they pass through  a water-jacketed
 vessel for cooling  and then pass through a  cyclone  and baghouse filter  to
 remove  particulates,  a caustic  scrubber to  remove  chlorine and HCI, and  an
 activated carbon bed to remove  any  residual traces of the organic feed and
 decomposition by-products.  With this type of small scale, off-the-shelf stack
 gas  treatment equipment,  we can achieve gas-phase DREs  as  close to absolute
 destruction  and removal as  a  given  application requires.  An additional ad-
 vantage  of the activated carbon beds is that  they provide a safety backup for
 removing hazardous  organics  from  the process gas stream in the  unlikely
 event that a  problem results  in  hazardous material reaching  the stack gas
 treatment equipment.

 The third cited advantage,  the demonstrated ability to treat commercial  quan-
 tities of contaminated soils, is unique.   With the  Huber Advanced  Electric
 Reactor  process, the melted soil  particles never touch the hot reactor interior
 walls due to the patented  fluid-wall effect.   After treatment,  the soil particles
 are  cooled below  their melting point  prior to  collection  thus producing a
 free-flowing,  nonhazardous, granular material ideal for landfill.

 The major significance of  the  fourth  cited advantage  (the  absence  of oxygen)
 is that  oxygen  containing  by-products such  as  dioxms  and  furans cannot
 theoretically be formed even  in  trace  amounts.   Tests  have  verified this
 prediction.

 All of the above advantages are  even more significant when the fact that the
 AER detoxification  system will  be available in a transportable modular form.
 Being able to move the unit for  on-site treatment of waste adds a dimension
 of attractiveness not available  with most  other  fixed  base processes.  Being
 able to  move the unit to the waste  instead of vice versa avoid many environ-
 mental and economic  problems.

 Because  of these and many  other features, the technology is  uniquely suited
 for  the  treatment of  extremely  hazardous   materials such   as  dioxin-
 contaminated soils  or liquid dioxin  concentrates such  as  still  bottoms.  The
 Office of Technology Assessment, the technological support arm of  Congress,
 has  recognired the AER process  as one of the most promising for soils  treat-
 ment and has recommended  its evaluation as  a potential method to detoxify
 500,000 tons of dioxin soils in Missouri.   (See  the enclosed OTA  preliminary
 response report excerpts.)

 An EPA  Certification Test for destroying PCBs in soils was conducted under
 TSCA regulations  at  our Borger  facility on September 27, 28, and  29.   The
 test  was witnessed by  representatives of the  U.S.  EPA Region VI,  the  Texas
 Department  of Water  Resources, and  the  Texas Air Control Board.   (See  the
attached summary  of  results table.) Briefly,  the results of these tests were:

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The Advanced  Electric  Reactor  Newsletter                              Page  3


(I)   Typical Destruction  Efficiencies (DE) of 99.9999%.

(2)  Typical Destruction  and Removal Efficiencies  (ORE) of 99.9999981.

(3)  Solid-phase (i.e., treated  dirt) PCB concentrations  of  0.0005  to O.OOl
     ppm PCB  (down from 3000 ppm PCB  in the  feed and far below the 50
     ppm required  by EPA under TSCA regulation).

(4)  No  HCI,  CL,  volatile chlorinated  hydrocarbons,  dioxins, or furans were
     observed af the stack.

(5)  Only trace amounts  of particulates and NOx were observed.

An  additional  point of consideration  is that  the quantity of PCB in all four of
the DRE and three out  of the four DE samples  were below their corresponding
analytical "blank"  values, thus  it is  not certain that  PCBs were even  present
in any of the process exit gas  samples.  All of these  results  far exceeded the
EPA/TSCA requirements;  however,  we do not believe  they reflect  the  ultimate
potential of this technology.

The certification test results were submitted to EPA Region VI on  October 31,
1983.   EPA certification is expected during the first quarter of 1984.

We  believe the Huber Advanced Electric Reactor process has  a major  role to
play in the treatment of hazardous  wastes.  We  will  inform  you  as other
progress is  made.

Should you  have any questions concerning  our work, please  call  me at our
Borger,  Texas,  office (806)  274-6331.

Regards,
       \
W. R.  Schofield, Ph.D.
Manager, Marketing  & Product Development

pv

Enclosures

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                                                CAUSTIC
                                               SCRUBBER
STACK
                                 Process Flow Diagram
                                                                             J. M. Hubar Corporation

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                      J. M. Hub«r Corporation

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SUMMARY OF RESUI EPA CERTIFICATION TEST
RADIAN CORPORA. JN - CERTIFIED RESULTS
FOR J. M. HUBER CORPORATION, RORGER, TEXAS
Run
Date
Feed
R. Temp. Total N2 % Gas-Phase Control ' Solid Phase PCBs, PPM'
(°F) (scfm) Cyclone (DE) Stack (DRE) Treated Feed
9/27/83 15.5
4100
147.2
99.99992
99.9999950
0.0005
9/28/83 15.7
4100
147.2
99.99992
99.9999994
< 0.0005
9/29/83 15.7
4100
147.2
99.99960
99.9999980
0.0006
9/29/83
15.8
4100
147.2
99.99995
99.9999940
0.0010
Notes:
Initial concentration of PCBs equals 3000 ppm Aroclor 1260 on a locally available sandy
material (by weight method). The DE and DRE results shown above will change slightly if
the less accurate analyzed feed concentrations are used instead.
Destruction and Removal Efficiency (DRE) required by EPA/TSCA for gas phase i? 99.9999%.
No requirements exist for Destruction Efficiency (DE). Maximum solid phase PCB
concentration allowed by EPA/TSCA for non-hazardous materials is 50 ppm. The detection
limits DLs, for DE and DRE are 99.99999946 and 99.99999976, respectively. DL for "treated
dirt" and "baghouse catch" materials are 0.0005 ppm and 0.001 ppm, respectively.
All four stack samples and three of four cyclone samples were below the concentration of
their corresponding blank. Thus the actual presence of PCBs in both locations is not
certain even though the instrument DLs were significantly below the "observed"
concentrations.
No chlorine (at a DL of 0.009 ppm) or halogenated ^Products of Incomplete Combustion (PICs)
at a DL of 0.001-0.020 ppmv were detected at the stack. Chlorine removal efficiency in
the scrubber and carbon beds was greater than 99.999%. No dioxins or furans were detected.
Trace quantities (far below emission limits) of NOx and particulates were detected at the
stack.
No PCBs were detected in the industrial hygiene monitors which were placed at the locations
most likely to have PCBs present in the ambient air (i.e., near the top of the reactor and
the discharge bin) during each test day.
These results were taken from the Radian Trial Burn Report. Additional information is
available upon' written request to W. R. Schofield, P.O. Box 2831, Borger, Texas,
79008-2831.
10/24/83

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                                       EPA/540/2-89/027
     SUPERFUNDTREATABILITY
            CLEARINGHOUSE
              Document Reference:
 Acurex Corp., Environmental Systems Divisions, Combustion Research Facility.
 "CRF Test Burn of PCB-Contaminated Wastes from the BROS Superfund Site."
Approximately 300 pp. Prepared for U.S. EPA Office of Research and Development.
                    March 1987.
             EPA LIBRARY NUMBER:

           Superfund Treatabiiity Clearinghouse - E)

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                SUPERFUND TREATABILITT CLEARINGHOUSE ABSTRACT
Treatment Process:

Media:

Document Reference:
Document Type:

Contact:
Site Name:
Location of Test:
Thermal - Rotary Kiln

Soil/Clayey

Acurex Corp., Environmental Systems Divisions,
Combustion Research Facility.   "CRF Test Burn of
PCB-Contaminated Wastes from the BROS Superfund
Site."  Approximately 300 pp.   Prepared for U.S.
EPA Office of Research and Development.  March
1987.

EPA ORD Report

Donald Lynch
U.S. EPA - Region II
26 Federal Plaza
New York, NY  10278
212-264-8216

BROS Superfund Site (NPL)

Jefferson, AR
BACKGROUND;  This report provides results of test burns at the EPA Combus-
tion Research Facility on waste from Bridgeport Rental and Oil Service
(BROS) Superfund site, NJ.  The purpose of the study was to:  (1) determine
if waste could be incinerated safely; (2) comply with the Toxic Substances
Control Act (TSCA) regulations governing PCB-contaminated waste; and (3)
determine if residuals could be classified as non-hazardous.
OPERATIONAL INFORMATION;  Rotary kiln was cocurrent propane fired and had a
maximum design capacity of 900°C (1650°F) with a gaseous residence time of
1.7 seconds for 10* excess 02 in flue gas.  Containerized solvents were fed
in 1.5 gallon fiber packs using a ram feeder.  Liquids and sludge were fed
using a progressive cavity pump through a water-cooled lance.  Air pollu-
tion control (APC) equipment included a venturi scrubber/quench with a 30
inch. W.D. pressure drop followed by a packed tower scrubber.  A backup dry
air pollution control system was utilized to ensure ultimate emissions
would be within the  applicable regulatory limits.  Scrubber system
blowdown was directed to a chemical sewer, if non-hazardous, or stored in
tanks for management at a RCRA facility, if hazardous.  Waste included:
lagoon surface oil, lagoon sludge, and soil.  Average composition:  210-600
ppm PCB, low to 38* water, 23.2-10,000 BUT/lb.  The soil was a clay mud
containing rocks, grass, roots, and twigs.
    Twelve tests were performed during 7/21/88 through 9/4/88 (test time
was five weeks).  Tests involved variation of:  waste feed, kiln tempera-
ture, excess 0™, rotation time (solid retention time).  The report provides
specific information on unit design (schematic diagram included) and
provides test data.  Sampling and analysis and QA information is also
provided.
3/89-48                                                 Document Number:   EXPC

    NOTE:  Quality assurance of data may not be appropriate for all uses.

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 PERFORMANCE;   Table 1 summarizes the PCB emission results.   The test  failed
 to meet-the TSCA regulations for 99.9999 percent  destruction efficiency
 (DE)  at  the stack gas effluent  as measured  after  the  scrubber discharge
 flue  gas.   DE results ranged from 99.992 to 99.9998.   On  average DEs  were
 highest  for surface oil and lowest for the  soil sludge mixtures.   Data
 indicated  no  clear correlation  between key  process parameters and DE.
 Analysis  indicates that a gas residence time of 2.0 seconds  in the after-
 burner and a  temperature of 1200°C would be required  for  this unit to
 achieve TSCA  requirements.   This is twice the residence time achieved in
 this  test.
    Scrubber  blowdown PCB content was below detection levels (<1  ug/L).
 Kiln  ash was  below detection level for PCBs except for ash from surface oil
 which tested  at  2.55 ug/g.   Particulate and HCL emissions were within
 regulatory limits.   Metal concentrations in leachate  samples from ash were
 below the  EP  toxicity limit.
CONTAMINANTS;

Analytical  data  is  provided  in  the  treatability
breakdown of  contaminants  by treatability group
Treatability Group

W04-Halogenated Aliphatic
     Solvents
W07-Heterocyclics and  Simple
     Aromatics
WlO-Non-Volatile Metals
Wll-Volatile Metals
W13-0ther Organics
CAS Number

75-35-4
78-87-5
56-23-5
79-01-6
75-34-3

71-43-2
108-88-3
71-43-2

7440-39-3
7440-47-3

7439-92-1
7440-38-2

110-54-3
study report.  The
is:

 Contaminants

 1,1-Dichloroethene
 1,2-Dichloropropane
 Carbon Tetrachloride
 Trichloroethene
 1,1-Dichloroethane

 Benzene
 Toluene
 Benzene

 Barium
 Chromium

 Lead
 Arsenic

 Hexane
Note:  This is a partial listing of data.
       information.
            Refer to the document for more
3/89-48                                                 Document Number:  EXPC
    NOTE:  Quality assurance of data may not be appropriate for all uses.

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                                                  TABLE 1
                                     PCB EMISSION RATE AND DE SUMMARY
Feed
(Arochlor 1254)


Waste Type
Lagoon surface
oil

Soil


Sludge


Soil plus
sludge


Test
No.
1
2
3
1
2
3
1
2
3
1
2
3

Concentration
(rag/kg)
282
296
280
67.3
167
95.4
250
250
250
78.6
120
170

Rate
(mg/s)
1.38
1.68
1.85
0.834
2.02
1.20
2.77
2.46
2.27
0.913
1.39
2.04
Emission (Arochlor 1254)
at scrubber discharge

Concentration
(ng/dscm)
207
212
180
32
39
52
9
42
82
49
73
109

Rate
(ug/s)
0.097
0.12
0.060
0.0093
0.011
0.021
0.0039
0.019
0.037
0.021
0.031
0.041

DE
(percent)
99.9930
99.9929
99.9968
99.9989
99.9995
99.9983
99.99986
99.99923
99.9984
99.9977
99.9978
99.9980
Weighted
average DE
(percent)
99.9944


99.9990


99.9992


99.979


3/89-48
                              Document Number:  EXPC



atziir nnt ho annrnnriate for all US6S.

-------
                                             March  1987
   CRF TEST BURN OF PCB-CONTAMINATED WASTES
         FROM THE BROS SUPERFUND SITE
                      by

     Johannes W. Lee, Robert W. Ross, II,
   Carlo Castaldini, and Larry R. Waterland
              Acurex Corporation
        Environmental Systems Division
         Combustion Research Facility
          Jefferson, Arkansas  72079
          EPA Contract No. 68-03-3267
              EPA Project Officer

               Robert Mournighan
Hazardous Waste Engineering Research Laboratory
         Combustion Research Facility
          Jefferson, Arkansas  72079
     U.S. ENVIRONMENTAL PROTECTION AGENCY
      OFFICE OF RESEARCH AND DEVELOPMENT
            WASHINGTON D.C. 20460

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                                 CONTENTS
Figures	       v
Tables  	       v

  1.  Introduction  	       1
  2.  Facility Description and Operation  	       3
      2.1  Facility Description 	       3
      2.2  Waste Characteristics  	      10
      2.3  Facility Operation 	      17
  3.  Sampling and Analysis Protocols 	      24
      3.1  Sampling Location and Methods  	      24
      3.2  Analysis Protocols 	      26
  4.  Test Results	      33
      4.1  PCB Destruction	      33
      4.2  Volatile Organic Emissions 	      41
      4.3  Particulate and HC1 Emissions	      41
      4.4  Trace Element Emissions  	      51
  5.  Quality Assurance and Quality Control 	      55
      5.1  Measurement of Q-jn	      55
      5.2  Measurement of Qout	      56
      5.3  Volatile Organic Spike Recoveries  	      57

References	•	      60
Appendicies

  A.  Sampling Locations and Methods  	     A-l
  B.  Sample Recovery and Analysis Methods  	     B-l
  C.  Waste Feed Data	     C-l
  D.  Sampling Data	     0-1
  E.  Analytical Reports  	     E-l
                                    iii

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                                  FIGURES

Number                                                                   Page
   1   Rotary kiln incinerator system  	      4
   2   Rotary kiln and afterburner detail   	      6
   3   Kiln temperature and residue time as  a  function  of  heat
       input	      8
   4   Afterburner temperature as  a function of  total heat input  ...      9
   5   Sampling Protocol  	     25
   6   PCB DEs	     35
   7   PCB DE as a function of excess 02	     37
   8   PCB DE as a function of gas flowrate	     38
   9   PCB DE as a function of mean temperature	     39
  10   PCB DE versus  mean temperature/gas  flowrate	     40
                                     iv

-------
TABLES
Number
1
2
3
4
5
6
7
8
9
10

11
12

13

14

15



Summary Analysis Data for the BROS Soil 	





Analysis Performed for Kiln PCB Test Burn of BROS Wastes . . .

Volatile Organic Compounds Routinely Analyzed by GC/EDC at
the CRF 	

Volatile Organic Constituent Concentrations for the BROS

Volatile Organic Constituent Concentrations for the BROS

Volatile Organic Constituent Concentrations for the BROS
Soil /Sludge Tests 	
Volatile Organic Constituent Concentrations for the BROS

Page
5
10
11
13
16
18
20
27
28

31
34

42

43

44

45

-------
                             TABLES (concluded)

Number                                                                   Page
  16   Volatile Organic Feed and Emission Rates   	     46
  17   Volatile Organic Feed and Emission Rates   	     47
  18   Volatile Organic Feed and Emission Rates   	     48
  19   Volatile Organic Feed and Emission Rates   	     49
  20   Particulate Emissions 	     50
  21   HC1  Emissions	     52
  22   Trace Element Emissions 	     53
  23   EP Leachate Concentrations  	     54
  24   Volatile Organic Constituent Spike Sample Recovery  	     58
  25   Volatile Organic Constituent Spike Recovery in VOST Samples . .     59
                                     vi

-------
SECTION 1
INTRODUCTION

One of the primary functions of the Combustion Research Facility (CRF)
is to support Environmental Protection Agency (EPA) Regional Offlees 1n r
evaluations of the potential for "Incineration as a disposal optldrf for wastes
r
generated through remedial action taken at Superfund sites. One priority^
site in Region II Is the Bridgeport Rental and Oil Services (BROS) Superfund
site in Bridgeport, New Jersey. This site has high priority in the Region's .
Remedial Action Program (1). Several hazardous wastes will be generated
through remedial actions at this site. Among these are PCB-contamlnated
lagoon surface oil, lagoon sludge and.contaminated soil.. Region II requested
test burns of these wastes plus a mixture of the soil and sludge at the CRF
to support evaluations of thermal treatment options for decontamination of
soil and destruction of incinerable wastes.
C
This report presents results of a 5-week test burn program conducted at
the CRF during July 21 to September 4, 1986. The rottry Mln Incineration
system was used for these tests. The primary objectives of the program were
C
as follows:
• Detturtne If luith BROS-generated waste can be safely Incinerated in
kv .-•»» "*
compliance with the Toxic Substance Control Act (TSCA) regulations
governing Incineration of PCB-contaminated wastes.

-------
     •   Determine if residual  streams  generated fcom the incineration
         proc«sScC4ft be classified  as non-toxic, awLnoncontaminated
         fadMtating final  disposal into.$h«, land.  ,
     •   Measons volatile products  of Incomplete combustion and compare with
         those observed during  a  TSCA trial burn also conducted at the CRF
The third objective calls for a comparison of organic emission measured
during this program with those  observed during a TSCA trial burn in which
PCB-contaminated sorbent was incinerated in the rotary kiln.  The results of
the TSCA trial burn are presented in greater detail in the trial burn report
submitted to the EPA for permit issuance (2).

-------
                                  SECTION 2
                     FACILITY DESCRIPTION AND OPERATION

     The test burn program was performed using the rotary  kiln  incinerator
system at the CRF 1j> Jefferson, Arkansas.  Figure 1  is  a simplified  schematic
of the system.  Design and operating characteristics of the CRF kiln,
afterburner, and air pollution control  devices (APCDs)  are presented in
Table 1.
2.1  FACILITY DESCRIPTION
     Figure 2 illustrates a three-dimensional layout of the primary  and
secondary thermal chambers (kiln and afterburner).  As  noted, the kiln has
1.2m (4 ft) wide diameter and is 2.4m (8 ft)  long.  The rotational  speed can
be set in the 0.1 to 0.5 rpm range.  Propane  is fired through one or two
530 kW (1.8 x 106 Btu/hr) capacity burners positioned for  either cocurrent  or
countercurrent operation.  However, the current kiln-to-afterburner  flue duct
arrangement limits operation to cocurrent firing of propane using the front
burner.  The kiln has ^««x1 mum design operating temperature of 900°C
                      i 1-31?   - -•                                         '
(1.650°F) with a corresponding minimum residence time of  1.7 sec for a ^
nominal 10 percent excels*Oj? 1n the flue gas.
     The afterburner has a 0.9m (3 ft) inner  diameter and is 3.1m (10 ft)
long.  This chamber can also be fired with propane at up  to 530 kW (1.8  x
    Btu/hr) heat Input.  Maximum design temperature for the afterburner  is

-------
Propane
   Transfer
   duct


Propane -*
             Burner
             No. 2
                                      Venturl
                                      Inlet duct
Cyclone    Packed
separator  tower
          scrubber
                                                    PIMP
                         Blowdown
                         tank
                         No. 2
                                                                                                                  Sanitary
                                                                                                                  sewer

                                                                                                                  Chemical
                                                                                                                  sewer
                               Figure 1.   Rotary kiln  incinerator  system.

-------
       TABLE  1.  DESIGN CHARACTERISTICS OF THE CRF ROTARY KILN SYSTEM
Characteristics of the Kiln Main Chamber

  Length                 2.44m (8 ft)
  Diameter               1.22m [4 ft)
                               3
  Chamber volume         2.88 m3 (IQQ ft3)
  Rotation               Clockwise or counterclockwise 0.1 to 1.5 rpm
  Construction           0.63 cm (0.25 in.) thick cold rolled steel
  Refractory             12.7 cm (5 in.) thick high alumina castable
                         refractory, variable depth to produce
                         a frustroconical effect for moving inerts
  Solids retention time  1 hour (at 0.5 rpm)
  Burner                 Iron Fireman, Model C-120-6-SMG rated at 530 kW
                         (1.8 MMBtu/hr)
  Primary fuel           Propane
  Feed system            Liquids:  Front face, water-cooled lance
                         with positive displacement pump
                         Semi liquids:  Front face, water-cooled lance
                         with Moyno pump
                         Solids: Metered twin auger screw feeder
  Temperature            900°C (1,650°F) maximum operating

Characteristics of the Afterburner Chamber

  Length                 3.05m (10 ft)
  Diameter               0.91m (3 ft)
  Chamber volume         2.096 m3 (74 ft3)
  Construction           0.63 cm (0.25 in.) thick cold rolled steel
  Refractory             15.24 cm (6 in.) thick high alumina castable
                         refractory
  Retention time         Depends on temperature and excess air
  Burner                 Iron Fireman, Model C-120-6-SMG rated at 530 kW
                         (1.8 MMBtu/hr)
  Primary fuel           Propane
  Temperature            1,200°C (2,200°F) maximum operating

Characteristics of the Air Pollution Control Systems

  System capacity        Inlet gas flow of 106.8 m3/min (3,773 acfm) at
                         1,200°C (2,200°F), at 101 kPa (14.7 psig)

  Pressure drop          Venturi  7.5 kPa (30 1n. WC)
                         Packed tower 1.0 kPa (4 In. WC)
  Liquid flow            VentuH  77.2L/min (20.4 gpm) at 69 kPa (10  psig),
                         Packed tower 116L/min (30.6 gpm) at 69 kPa
                         (10 psig)
  pH control              Feedback  control by NaOH solution addition

-------
Burner No. Z
    Burner No. 1
                                                          Waste feed
                                 Afterburner
                                 10'  x 3'  ID
                                                                          1^-
                                                                          2
              Figure 2.  Rotary kiln and afterburner detail

-------
        (i2»200*Fy.  At a maximum heat  input  of about 1.1 MW (3.6 x
106 Btu/hr) to both chambers the resulting bulk gas residence time in the
afterburner'is approximately 1.4 sec.   Figures 3 and 4 illustrate the
approximate relationships between heat input, gas temperature, and residence
time for the two thermal chambers.
     The kiln waste feed can accommodate  liquids, slurries and sludges, bulk
solids, and containerized solids.  Liquids and sludges can be fed using a
progressive cavity pump through  a water-cooled lance.  Containerized solids
are fed in 5.8L (1.5 gal) fiber  packs  using  a ram feeder.  For
noncontainerized solids, a twin  auger  screw  feeder  can also be used.  During
these tests, the soil was containerized in fiber packs and fed into the kiln
using the ram feeder.  Nominal  retention  time of solids  in the kiln is 1 hour
for a rotational speed of 0.5 rpm.   Kiln  ash is collected in the ash bin.
     The primary particulate and HC1 emission control system reflects what
might be considered typical equipment  for a  commercial or industrial
incinerator.  The venturi scrubber/quench is designed to operate at 7.5 kPa
(30 in. W.C.) pressure drop.  From the venturi, combustion gases flow through
a wetted elbow to a packed tower scrubber.   Slowdown from the scrubber system
can be directed to the National  Center for Toxicological Research  (NCTR)
chemical sewer if the blowdown is determined to be  nonhazardous.   If residual
streams are determined to be hazardous they  can be  stored in several tanks  at
the site and ultimately disposed of in RCRA-approved hazardous waste sites.
     In addltfttfcto the wet control system,  a backup dry air pollution
control systJTift utilized to ensure that ultimate  emissions to  the
atmosphere will remain within applicable regulatory limits.  This  dry  control

-------
00
                  1,700
                  1,600
                  1,500
               ex
               §
               ^  1,300
                  1,200   _
                  1.100
U.S.  EPA CRF
Rotary Kiln System

 Typical  lOr
"excess oxygen at
 exit
                            500
   J	1	1	1	I	I	I	I	I	
                             1,000                       1,500

                                   K1ln heat Input (lOOOx Btu/hr)
                                                                                                                    3
                                                                                                                3.0
                                                                                                                2.5
                                                                                       2.2
                                                                                                                1.5
                                                                                                                1.0
                                                                                                                    01
                                                                                                                    •o
                                                                                                                    O>

                                                                                                                    c
   0.5
2.000
                       Figure  3.   Kiln temperature  and  residence  time as a function of  heat  Input.

-------
VO
       4-

       Ol


       t
            2.400
            2.300
       ?•     2.200
       •=     2.100
•i




I


£    2.000
             1.900
             1.800
             U.S. EPA CRF

             Rotary Kiln System




               Typical 6 to  8 percent

            — excess oxyqen at exit
                         I     I      I     I      I	I	I	I	I	I	1	1	1
                                        3.000                        3,500




                                        Total heat Input  (KBtu/hr)  (kiln + afterburner)
                                                                                       4.000
                                                                                                               .

                                                                                                              2
                                                                                                            3.0
                                                                                                            2.5
                                                                                                                 u

                                                                                                                 01
                                                                                                            1.5   <"
                                                                                                                 1_

                                                                                                                 £
                                                                                                            1.0
                                                                                                     0.5
                         Figure 4.   Afterburner temperature as  a function  of total  heat  input.

-------
system consists of a carbon bed  absorption unit for *«por phase .organfc*
compound reooval and a high efficiency  particulate (HEPA) filter f^c;;.
particulate removal.
2.2  WASTE CHARACTERISTICS
     Four waste materials  from the  BROS site were tested in the rotary  kiln
system at the CRF.  These  waste  materials consisted of PCB-contaminated
(1) lagoon surface oil, (2) soils from  Area 1  of the BROS site, (3) lagoon
sludge, and (4) a mixture  of soil and lagoon sludge.  Tables 2 through  4
summarize data on the concentration of  several hazardous constituents and
other properties of the Area 1 soil, lagoon surface oil, and lagoon sludge
determined prior to this test program (3).
     The soil can be characterized  as clumped  clay mud containing  rocks,
grass, roots, and twigs.  The data  in Table 2  show that  the contaminated
soil contains an average of about 660 ppm PCBs based on  an average of
19 analyses.  The physical appearance of the  lagoon surface oil  reveals a

            TABLE 2.  SUMMARY ANALYSIS  DATA FOR  THE BROS SOIL3
Parameter
Organic sulfur, percent
Sulfide, mg/kg
PCBs, mg/kg
PCB-1254|
PCB-12481
PCB-126&I
Range
0.16-1.65
<2-51
<16-1.010 *
< 0.8- 590 '
-------
    TABLE 3.  CHARACTERIZATION OF THE BROS  LAGOON  SURFACE OIL3

Ignitability
Flashpoint (°F)
Oxidizer (mg/kg)
Organic sulfur
(percent)
Sulfide (Mg/kg)
Heating value (MJ/kg,
(Btu/lb))
Ash (percent)
Moisture (percent)
Specific gravity
Total PCBs (mg/kg)
PCB-1254
PCB-1248
PCB-1260
Volatile organic
priority pollutants
(mg/kg)c:
Toluene
Total xylenes
Ethyl benzene
Range
109-150
<25
0.08-0.80
19-82
8.8-35.5
(3,800-15,300)
0.18-2.1
17-48
0.86-0.95
120-310 /
100^150
140-280

1.7-20
Average^
135
<25
0.33
44
23.2
(10,000)
0.87
38
0.91
240
115
200
7.5
9.7
2.7
Number of
Median analysis
135
<25
0.34
43
23.0
(9,900)
0.84
42
0.92
270
130
190
8.0
11
2.5
56
56
56
11
56
56
11
56
11
11
11
11
11
11
                                                          (continued)
Reference 3.
bLess than detection limit assumed to be 0 for  averaging
 purposes.
cBenzene and t-1,2 dichloroethene were found  at quantifiable
 amounts 1n one sample each.   No other volatile organic priority
 pollutants were detected in  any sample at a  detection limit  of
 1 mg/kg.
dNo other semi volatile organic priority pollutants  were detected
 in any sample at a detection limit of 10 mg/L.
eThe average for all samples  was less than the  detection  limit of
 10 mg/L; therefore, the average was assumed  to be  the detection
 limit.
                                 11
-------
                       TABLE  3.   (concluded)
                            Range
Average''  Median
Number of
analysis
Semi volatile organic
priority pollutants
(mg/L)d:
Acenaphthene
1,2,4-trichlorobenzene
Fluoranthene
Naphthalene
Bis(Z-ehtylhexyl)
phthalate
Butyl benzyl phthalate
Di-n-butyl phthalate
Di-n-octyl phthalate
Benzo(a)anthracene
Benzo(a)pyrene
Benzo(b)fluoranthene
Chrysene
Acenaphthylene
Anthracene
Fluorene
Phenanthrene
Pyrene
<10-21
<10-32
21-110
48-210
120-520

79-420
<10-49
13-96
<10-31
<10-15
<10-31
<10-80
<10-72
<10-32
<10-88
110-460
26- 92
10e
106
54
110
330

240
19
55
10d
10d
14
33
33
13
42
250
50
10
<10
53
97
370

220
24
52
<10
<10
15
42
27
15
39
240
49
11
11
11
11
11

11
11
11
11
11
11
11
11
11
11
11
11
Reference 3.
bLess than detection limit assumed to be 0 for averaging
 purposes.
cBenzene and t-1,2 dichloroethene were found at quantifiable
 amounts in one sample each.   No other volatile organic priority
 pollutants were detected in  any sample at a detection limit of
 1 mg/kg.
dNo other semi volatile organic priority pollutants were detected
 in any sample at a detection limit of 10 mg/L.
eThe average for all samples  was less than the detection  limit of
 10 mg/L; therefore, the average was assumed to be the detection
 limit.
                                 12
-------
      TABLE 4.  CHARACTERIZATION OF THE BROS LAGOON  SLUDGE3
                     Parameter
Value
Heating value, MJ/kg (Btu/lb)                          16.7  (7200)

Ash content, percent                                   2

Moisture content, percent                              13

Specific Gravity                                       1.31

PCB content, mg/kg dryb
  PCB-1248                                             140
  PCB-1260                                             72

Volatile organic priority pollutants0, mg/kg dry
  1,1,1-trichloroethane                                0.23
  t-l,2-dicloroethylene                                0.11
  Ethylbenzene                                         0.74
  Toluene                                              1.7

Other volatile organics0", mg/kg
  Acetone                                              0.75
  2-butanone                                           1.2
  4-methyl-2-pentanone                                 0.11
  Total xylenes                                        2.7

                                                       (continuedT
Reference 3.
bPCBs-1242, 1254, 1221, 1232 and 1016 were also analyzed  for and
 not found at a detection limit of 9 mg/kg dry.
CA11 other volatile organic priority pollutants not detected at a
 detection limit of 0.1 mg/kg dry.
^Carbon disulfide, vinyl acetate, 2-hexanone, and styrene were
 also analyzed for and not found at a detection limit of  0.1 mg/kg
 dry.
eAll other semi volatile organic priority pollutants not detected
 at  a detection limit of 20 mg/kg dry.
^Benzyl alcohol, 2-methyl phenol, 4-methyl phenol» benzoic acid,
 4-chloroanlline, 2,4,5-trichlorophenol, 2-nitroanillne,
 3-nitroaniline, 2-dibenzofuran, and 4-nitroaniline were  also
 analyzed for and not found at a detection limit of 40 mg/kg dry.
                                13
-------
                      TABLE 4.   (concluded)
                     Parameter                           Value
Semivolatile organic priority pollutants6, mg/kg dry
  Fluoranthene                                        33
  Naphthalene                                         180
  Bis (2-ethylhexyl)phthalate                         130
  Butyl  benzyl phthalate                              130
  Chrysene                                            21
  Acenaphthylene                                      21
  Fluorene                                            37
  Phenanthrene                                        170
  Pyrene                                              52

Other Semivolatile organics^, mg/kg dry
  2-Methyl naphthalene                                240

EP toxicity leachate concentration, mg/L
  Arsenic                                             <0.5
  Barium                                              <5.0
  Calcium                                             <0.1
  Chromium                                            <0.5
  Lead                                                2.86
  Mercury                                             <0.02
  Selenium                                            <0.5
  Silver                                              <0.5
  Endrin                                              <0.0001
  Lindane                                             <0.00005
  Methoxychlor                                        <0.0005
  Toxaphene                                           <0.0025
  2,4-D                                               <0.005
  Si 1 vex                                              <0.0005
aReference 2.
bPCBs-1242, 1254, 1221, 1232 and 1016 were also analyzed for and
 not found at a detection limit of 9 mg/kg dry.
CA11 other volatile organic priority pollutants not detected at a
 detection limit of 0.1 mg/kg dry.
dCarbon disulfide, vinyl acetate, 2-hexanone, and styrene were
 also analyzed for and not found at a detection limit of 0.1 mg/kg
 dry.
eAll other Semivolatile organic priority pollutants not detected
 at a detection limit of 20 mg/kg dry.
fBenzyl alcohol, 2-methyl phenol, 4-methyl phenol, benzoic acid,
 4-chloroaniline, 2,4,5-trichlorophenol, 2-nitroaniline,
 3-nitroaniline, 2-dibenzofuran, and 4-nitroaniline were also
 analyzed for and not found at a detection limit of 40 mg/kg dry.
                                14
-------
 dark  brown  syrup  substance  containing some debris.  Data in Table 3 for
 flash point,  oxidizer, organic sulfur, heating value, ash content, and
 specific  gravity  of lagoon  surface oil are based on 56 analyses of
 54  composite  samples.  Data for moisture content and organic priority
 pollutant content are based on 11 analyses of 10 oil composites.  These data
 show  that surface oil contains an average of about 550 ppm total PCBs.  In
 addition, several semivolatile organic compounds are also present at average
 concentrations exceeding 100 ppm.  These are naphthalene (120 ppm by weight
 in  the oil),  phenanthrene (270 ppm) and two phthalates, bis(2-ethylhexyl)
 phthalate (360 ppm) and butyl benzyl phthalate (260 ppm).  Proximate analysis
 of  the oil  reveals 38 percent water content, 0.87 percent ash, 0.92 specific
 gravity and a gross heating value of 23 MJ/kg (10,000 Btu/lb).
      The lagoon sludge appears as a black gel in much water.  The sludge
 contains several kinds of debris including grass, roots, and twigs.  The data
 in Table 2-4 show that the BROS lagoon sludge contains an average of 210 ppm
 PCBs  and other semivolatile organics also found in the lagoon surface oil.
 In addition, the metal and pesticides concentrations in an EP toxicity
 leachate of the lagoon sludge fall below values which would cause the sludge
to be considered characeristic EP toxic.   The heating value of the sludge has
been  reported at 16.7 MJ/kg (7200 Btu/lb) with 13 percent moisture, 2 percent
ash, and a specific gravity of 1.3.
     Waste analyses were performed on each of the waste materials tested at
the CRF.  Table 5 summarizes the result of these analyses.  Waste heating
values ranged from zero for the soil to 10.1 MJ/kg (4,350 Btu/lb) for the
lagoon sludge which contained significant quantities of water.  The average
total  PCBs for the soil  and lagoon surface oil were measured at only 110 and
                                     15
-------
TABLE  5.  BROS WASTE CHARACTERIZATION —  COMPOSITION
Ultimate
analysis
(I by weight as fed)
C
H
0
N
S
Cl
Total
High heating Value
MJ/Kg (Btu/lb)
Total PCBs
(mg/kg as Arochlor
1254)
Metals (mg/kg):
Arsenic, As
Barium, Ba
Cadmium, Cd
Chromium, Cr
Lead, Pb
Mercury, Hg
Selenium, Se
Silver. Ag
EP toxldty leachate
Arsenic. As
Barium, Ba
Cadmium, Cd
Chromium, Cr
Lead. Pb
Mercury, Hg
Selenium, Se
Silver. Ag
Area 1
soil
11.4
4.6
25.0
0.1
0.4
0.44
41.94

0
67.3-167
(110)«


<1
744
<1
55
756
<1
<1
<5
(mg/L):
<0.1
0.12
<0.1
<0.1
0.46
<0.1
<0.1
<0.1
Lagoon
surface
- oil
54.4
10.9
29.9
0.1
0.7
0.1
96.1
8.62
(3,716)
270-300
(286)b


2
1.035
<10
46
2.888
<1
<1
<10

<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
Lagoon
sludge
1.0
11.1
81.8
1.0
1.0
0.01
95.91
10.0
(4,348)

250


<1
23
<5
12
46
<1
<1
<5

0.19
<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
<0.1
Soil and
lagoon
sludge
13.1
4.7
32.2
0.4
0.01
0.06
50.86
2.43
(1.048)
78.6-170
(123)"


11
823
4
65
1,034
<1
<1
<5

0.1
0.30
<0.1
<0.1
0.12
<0.1
<0.1
<0.1
     a - Average value of 9 analyses on  3 composite samples
     b - Average value of 3 analyses on  1 composite sample
                              16
-------
286 ppm by weight, respectively, compared to concentrations  of  about  660  and
550 ppm from the preliminary analyses (see Table 2).   The  PCB concentration
for the sludge was comparable to that from the preliminary analysis.  The
mixture of soil and sludge resulted in a total PCB concentration  of 123 ppm
from an average of three analyses on one composite sample.  Barium, chromium,
and lead were the principal metals detected in these  wastes.  Highest
concentrations of these elements were measured primarily in  the lagoon
surface oil.
2.3  FACILITY OPERATION
     Tables 6 and 7 summarize the operation of the rotary  kiln  incinerator
and air pollution control systems.  A total of 12 tests were performed  (three
tests for each of the four waste feeds).
     For the first series of three tests, the lagoon  surface oil  was  fed  into
the kiln using the progressive cavity pump at an average rate of 18 to
24 kg/hr (39 to 53 Ib/hr).  Average kiln and afterburner temperatures were
varied from about 680 to 8908C (1,250° to 1,640°F), respectively, to
determine the impact of thermal environments on PCB ORE.  Excess 02,  measured
at the afterburner exit, was maintained relatively constant  between  5.6 and
6.5 percent.  Following completion of the surface oil tests, three tests  were
conducted with the contaminated soil which was fed into the  kiln in  5.7L
(1.5 gal) fiberpacks using the ram feeder.  The average feedrate of  the  soil
during each test was maintained relatively constant for the  test series  at
about 45 kg/hr (100 Ib/hr).  Lowest kiln temperature, about  700°C (1,290°F)
was investigated during the second soil test.  Afterburner temperature  was
maintained relatively constant at about 1,130°C (2,060°F)  for each test.
Average excess 02 at the afterburner exit was varied  from 6.7 to 8 percent.

                                     17
-------
                             TABLE  6.   ROTARY  KILN INCINERATOR OPERATING CONDITIONS
00


Test
date
7-21-86



7-28-86



7-29-86



8-4-86



8-5-86



8-7-86



8-12-86





Test
duration
11:00 -
17:20


10:15 -
16:15


10:00 -
19:15


12:10 -
17:16


10:35 -
15:20


9:45 -
14:00


9:38 -
14:39




Test
material
BROS
surface
oil

BROS
turf *ce
oil

BROS
surf tc«
oil

BROS
sot)


BROS
soil


BROS
soil


BROS
soil *
sludge



Feed
method
Progres.
cavity
PU"P

Progres.
civUy
PIMP

Progres.
cavity
pump

Flberpack
by
ran
feeder
Ftberpack
»y
ran
feeder
Flberpack
by

feeder
Flberpack
by
ran
feeder
Test
•aterlal
feedrate
kg/hr
(Ib/hr)
17.6
4.7 - 22.7
(38.8)
(10.4 - 50.0)
20.4
16.3 - 23.6
(44.9)
(36.0 - 52.0}
23.8
21.3 - 30.4
(52.5)
(47.0 - 67.0)
44.6
20.8 - 84.4
l»8.2)
(45.9 -186.0)
43.6
20.8 - 54.4
(96.1)
(45.9 -120.0)
45.3
40.8 - 47.6

\yt.i)
(90.0 -105.0)
41.8
39.3 - 52.3
(92.1)
(86.6 -115.2)
Kiln
rotation
speed
rpm

0.51
0.51 - 0.51


0.51
0.51 - 0.51


0.51
0.51 - 0.51


0.19
0.19 - 0.54


0.19
0.19 - 0.19


0.19



0.19
0.19 - 0.19

Kiln
propane
heat
release
kU
(103 Btu/hr)
294
193 - 382
(1005)
657 - 1305)
323
293 - 332
(1101)
(999 - 1133)
342
323 - 426
(1167)
(1103 - 1453)
489
473 - 576
(1669)
(1616 - 1966)
256
253 - 269
(874)
(864 - 917)
484
423 - 629
f lft*9l
\ IB9t|
(1443 - 2146)
278
270 - 286
(948)
(923 - 975)
Afterburner
propane
heat
release
kU
(103 Btu/hr)
655
642 - 676
(2234)
(2191 • 2306)
763
749 - 783
(2603)
(2555 - 2671)
493
383 - 634
(1682)
(1308 - 2163)
369
363 - 379
(1260)
(1238 - 1294)
446
436 - 511
(1523)
(1489 - 1744)
415
370 - 455
I KID
(1264 - 1552)
510
482 - 533
(1740)
(1645 • 1819)
Kiln
chamber
temperature
•c
CF)
679
635 - 705
(1255)
(1175 - 1301)
678
658 - 694
(1252)
(1217 - 1282)
891
799 - 953
(1636)
(1471 - 1748)
924
893 - 969
(1696)
(1639 - 1776)
697
664 - 724
(1287)
(1228 - 1336)
890
854 - 936
(1614)
(1569 - 1717)
718
643 - 909
(1324)
(1189 - 1668)
Afterburner
chamber
temperature
•c
CF)
1136
1127 - 1155
(2076)
(2060 - 2111)
1211
1206 - 1234
(2211)
(2203 - 2254)
1133
1082 - 1170
(2072)
(1980 - 2138)
1129
1121 - 1143
(2064)
(2050 - 2089)
1126
1121 - 1149
(2058)
(2049 - 2100)
1122
1121 - 1123
(?(K1)
(2049 - 2054)
1122
1121 - 1123
(2052)
(2049 - 2054)
Kiln
exit
oxygen
* (dry)

12.6
1.6 - 13.1


10.4
10.1 • 10.5


10.3
6.1 - 11.8


8.2
6.4 - 9.4


10.3
7.5 - 12.9


8.8



13.14
10.5 • 14.1

Afterburner
exit
oxygen
* Ury)

5.6
5.1 - 5.8


6.0
4.4 • 8.1


6.5
3.0 - 12.8


8.0
4.9 - 16.6


7.2
4.8 - 10.9


6.7



8.5
6.5 - 9.0

-------
TABLE 6.  (concluded)


Test
d*te
8-13-86


8-14-86



8-28-86
9-3-86
9-4-86


Test
duration
*:40 -
14*41


9:55 -
14-51


9:30 -
14:50
9:30 -
14:45
9:1S -
14:20


Test
MterU)
BROS
soil »
sludge

BROS
soil »
sludge

BROS
sludge
BROS
sludge
BROS
sludge


Feed
method
Flberpack
by
ram
feeder
Flberpack
by
ram
feeder
Progres.
cavity
PIMP
Progres .
cavity
PIMP
Progres .
cavity
PIMP
Test
•aterlal
feedrate
kg/hr
(Ib/hr)
41.6
38.4 - 44. 5
(91. 8)
(84.6 - 98.2)
43.3
24.7 - 95.9
(95.4)
(S4.4 -211. 5)
39.9
16.3 -100.4
(87.9)
(36.0 -221.2)
35.5
11.6 - 94.3
(78.2)
(2S.S -208.0)
32.7
21.8 - 49.0
(72.1)
(48.0 -108.0)
Kiln
rotation
speed
rpm
0.
0.19 - 0.


0.
0.36 - 0.

0.
0.36 - 0.
0.
0.36 - 0.
0.
0.36 - 0.




19
19


36
36

36
36
36
36
36
36
Kiln
propane
heat
release
kU
(103 Btu/hr)
470
421 - 576
(1604)
(1436 - 1965)
427
384 - 500
(1456)
(1309 - 1705)
334
331 - 353
(1140)
(1131 - 1206)
619
599 - 642
(2112)
(2044 - 2192)
422
384 - 469
(1439)
(1310 - 1602)
Afterburner
propane
heat
release
kU
(103 Btu/hr)
410
386 - 460
(1400)
(1317 - 1571)
430
395 - 443
(1468)
(1347 - 1511)
474
469 - 510
(1618)
(1600 - 1740)
407
384 - 445
(1389)
(1310 - 1520)
657
642 - 670
(2241)
(2191 - 2285)
Kiln
chanter
temperature
°C
(°F)
897
872 - 929
(1647)
(1602 - 1705)
894
859 - 936
(1642)
(1579 - 1716)
656
647 - 671
(1212)
(1196 - 1240)
881
864 - 899
(1618)
(1587 - 1651)
656
646 - 672
(1212)
(1194 - 1242)
Afterburner
chamber
temperature
"C
CF)
1122
1121 - 1124
(2052)
(2049 - 2056)
1122
1120 - 1123
(2051)
(2048 - 2054)
1116
1106 - 1120
(2040)
(2022 - 2048)
1122
1120 - 1123
(2051)
(2048 - 2054)
1213
1210 - 1213
(2215)
(2210 - 2216
Ktln Afterburner
exit exit
oxygen oxygen
t (dry) I (dry)
7.5
NA 5.1 - 13.1


9.8 6.8
8 - 11.3 5.3 - 7.9

10.1
NA 8.5 - 11.0
NA 6.2
5.2 - 7.2
6.2
NA 4.9 - 6.8
-------
TABLE 7.  AIR  POLLUTION CONTROL  SYSTEM OPERATING CONDITIONS
Test
date
7-21-86



7-28-86



7-29-86



8-4-86



8-5-86



8-7-86



8-12-86



8-13-86



Test
duration
11:00 -
17:20


10:15 -
16:15


10:00 -
19:15


12:10 -
17:16


10:30 -
15:20


9:45 -
14:00


9:38 -
14:39


9:40 -
14:41


Test
material
BROS
surface
oil

BROS
surface
oil

BROS
surface
oil

BROS
soil


BROS
soil


BROS
soil


BROS
soil +
sludge

BROS
soil +
sludge

Venturl
scrubber
liquor
rate
L/«ln
(9f»)
68
68-68
(18)
(18-18)
68
68-68
(18)
(18-18)
68
68-68
(18)
(18-18)
64
64-64
(17)
(17-17)
64
64-64
(17)
(17-17)
64
64-64
(17)
(17-17)
64
64-64
(17)
(17-17)
64
64-64
(17)
(17-17)
Venturl
scrubber
gas
AP
kPa
("we)
6.8
4.5- 10.0
(27.3)
(18.0-40.0)
5.4-
5.5-4.5
(21.6)
(22.0-18.0)
5.8
5.0-8.7
(23.3)
(20.0-35.0)
2.7
2.7-2.7
(11.0)
(11.0-11.0)
2.1
2.0-2.2
(8.4)
(8.0-9.0)
4.7
5.7-3.5
(18.9)
(23.0-14.0)
9.0
7.0-9.7
(36.1)
(28.0-39.0)
8.8
9.7-7.7
(35.2)
(39.0-31.0)
Packed
column
liquor
rate
L/«in
(9PH)
114
114-114
(30)
(30-30)
114
114-114
(30)
(30-30)
114
114-114
(30)
(30-30)
114
114-114
(30)
(30-30)
114
110-114
(30)
29-30
106
106-106
(28)
(28-28)
110
110-110
(29)

114
114-114
(30)
(30-30)
Scrubber
liquor
pH

8.2
2.5-8.2


8.1
8.0-8.2


8.2
8.2-8.2


8.2
8.2-8.2


8.2
8.2-8.2


7.2
6.0-7.8


7.3
7.0-7.5


7.0
6.2-8.0

Scrubbing
liquor
temperature
•c
cn
73
71-75
(164)
(159-167)
73
71-74
(163)
(160-166)
74
72-75
(165)
(161-167)
75
74-77
(167)
(165-170)
76
74-77
(168)
(166-170)
74
71-76
(165)
(159-168)
73
72-74
(163)
(162-165)
73
70-74
(164)
(158-166)
Makeup
water
rate
L/«1n
<9P*}
22.6
13.2-28.0
(6.0)
(3.5-7.4)
26.3
19.9-34.9
(6.9)
(5.2-9.2)
21.9
16.0-28.0
(S.B)
(4.2-7.4)
20.6
9.8-29.9
(5.5)
(2.6-7.9)
20.9
12.5-30.7
(5.5)
3.3-8.1
21.5
6.8-30.8
(5.7)
(1.8-8.1)
20.6
7.9-28.6
(5.5)
(2.1-7.5)
20.5
6.5-29.0
(5.4)
(1.7-7.7)
Slowdown
•ater
rate
L/«in
(9P*)
9.5
9.1-11.7
(2.5)
(2.4-3.1)
12.1
12.1-12.1
(3.2)
(3.2-3.2)
12.5
11.7-15.1
(3.3)
(3.1-4.0)
13.2
13.2-13.2
(3.5)
(3.5-3.5)
13.6
13.6-13.6
(3.6)
(3.3-3.6)
12.5
12.5-12.5
(3.3)
(3.3-3.3)
12.5
12.5-12.5
(3.3)
(3.3-3.3)
12.5
12.5-12.5
(3.3)
(3.3-3.3)
                                                             (continued)
                               20
-------
TABLE 7.  (concluded)


Tett
-------
Kiln rotational speed of 0.19 rpm corresponds  to  about 2.5 hr solid retention
time.
     The mixture of soil and lagoon sludge  was also fed into the kiln with
fiberpacks at an average feedrate of about  42  kg/hr (93 Ib/hr).  Two kiln
rotational speeds were investigated, namely 0.19  rpm  for the first two tests
and 0.36 rpm for the third test;  the latter corresponding to about 1.4 hr
solid retention time.  The lowest kiln  temperature investigated during these
tests was 718°C (1,320°F).  Kiln  design temperature of about 895°C (1,650°F)
was utilized during the other two tests. The  afterburner temperature was
maintained constant throughout this series  of  tests at 1,120°C  (2,050°F).
Afterburner exit 03 ranged from 6.8 to  8.5  percent on the average for each
test.
     Sludge only tests were performed with  two temperature settings for  each
of the kiln and afterburner chambers.  The  lowest temperature combination of
656°C (1,210°F) for the kiln and  1,116°C (2,040°F) for the afterburner was
investigated during the first test.  Higher kiln  and  afterburner
temperatures to about 880°C (1,620°F) and 1,210°C (2,210°F)  for the kiln and
afterburner, respectively, were alternatively  tested  during  the remaining two
tests.  Lowest temperature settings were tested with  the highest excess  02
(10 percent) at the afterburner exit.  The  average excess Og for the  other
tests was held constant at 6.2 percent.  The sludge was pumped  to the kiln
which rotated at 0.36 rpm.
     Table 7 summarizes the operational settings  of the major components of
the wet air pollution control system.  For  the most part the scrubbing  liquor
flowrate, pressure drops, and pH levels were held relatively constant
throughout the test program with the exception of the venturi scrubber

                                     22
-------
pressure drop which showed a range of average settings  between  2.1  kPa
(8.4 in. W.C.) during tests with contaminated soil  and  9.7  kPa  (39  in.  W.C.)
during tests with lagoon sludge.
                                     23
-------
                                  SECTION 3
                       SAMPLING AND ANALYSIS PROTOCOLS

     In order to achieve the objectives of the test burn, an extensive
sampling and analysis (S&A) program was executed.  This section summarizes
the S&A protocols and methods used.  More detail on actual equipment  and
procedures can be found in Appendices A and B of this report.
3.1  SAMPLING LOCATION AND METHODS
     Figure 5 illustrates the sample locations and test methods.   Waste,
propane, and combustion air feedrates to the kiln were monitored  using
process monitoring equipment available at the facility.  Waste  feedrate was
monitored by recording the cumulative weight of waste feed to the kiln  over
the duration of each test.  The rate of feed was then obtained  by the slope
of the cumulative weight versus time graphs presented in Appendix C.
     Incineration residuals were accounted for in the protocol  by taking
samples of the kiln ash from the ash bin following the conclusion of  each
test.  When solid waste feeds (soil and soil plus lagoon sludge)  were
incinerated, multiple kiln ash samples were taken for analysis  of organics
and metals.  Composite scrubber blowdown samples were also collected
throughout the duration of each test.
     Continuously monitored (CM) gaseous emissions were  limited to
measurements for D£ and C02 concentrations at four locations  in the
incinerator system namely at the exits of the kiln,  afterburner,  wet  APCD

                                     24
-------
-^
Kiln





After
burner




Venturl
scrubber



Packed
toner





Carbon
bed



HEPA
filter

ro
                                                                   Parameter



Sailing Waste Waste Fuel Air Kiln Scrubber
point feedrate feed feedrate feedrate ash blowdown
1 X X X X
2 X
3
4
5 X
6
7
MM5
(partlculate.
PCBs. and
CH's Volume semi volatile
(02, CO?) 'low organic*)


X
X
X
X X X
X X


VOST
(volatile Method 5
organlcs) (Paniculate)




X
X
X
        T:   Temperature
        P:   Pressure
       RH:   Relative Humidity
                                             Figure  5.   Sampling protocol,
-------
system and the stack.  Details of the 02  and  C02 traces at each of these
locations are shown in Appendix D.   Measurements for participate, PCBs, and
semi volatile organics in the gas stream were  made using the modified EPA
Method 5 (MM5) at the packed tower scrubber outlet  (downstream of the wet
particulate and acid gas control system).  Measurements for volatile products
of incomplete combustion (PICs) were performed  at the afterburner and packed
tower scrubber exit locations using the standard EPA Volatile Organic
Sampling Train (VOST).  Particulate and HC1 emissions measurements were also
made at the stack to measure compliance with  the operating permit at the
CRF.
3.2  ANALYSIS PROTOCOLS
     Table 8 summarizes the total number  of samples collected and analyses
performed on each sample.  The analytical  protocols are summarized in
Table 9.  The laboratory analyses procedures  included:
     •   Analyzing all waste feed samples, the  composite  kiln ash samples,
         all blowdown water samples, and  all  MM5 train samples  for PCBs.
     •   Analyzing one composite waste feed sample, the composite kiln  ash
         sample, all scrubber blowdown samples  taken upstream of the  carbon
         bed, and all MM5 train samples for the semivolatlle organic
         priority pollutants.
     •   Analyzing one composite waste feed sample, the composite kiln  ash
         sample, and all scrubber blowdown samples  taken  upstream of  the
         carbon bed for 21 volatile organic compounds  visible to the  Electron
         Capture Detector (ECD) and routinely determined  at the CRF  (see
         Table 10.
                                     26
-------
                        TABLE 8.   ANALYSIS PERFORMED FOR KILN PCB TEST BURN OF  BROS  WASTES
ro
Method
Composite
Composite
grab

Composite
grab
Composite

Composite

VOST

EPA MS


MMS

Location
Feed
material
Kiln ash

Blowdown
mixture
Blowdown
liquid
61 owdown
solids
Scrubber
flue
Afterburner
flue
Stack

Scrubber
flue
Analysis
PCB
Volatile organic
Trace elements
EP toxlclty
Characterization
PCB
Volatile organic
Trace elements
EP toxlclty
Volatile organic
PCB
EP toxlclty

Trace elements

Volatile organic

Partlculate load
HC1
Partlculatc load
HCI
PCB

Surface oil
7-21 7-28 7-29
3
(-
1
2
1

1

3

("


1

3

1
2
1

1

3

1
1


1

3
--)
1
2
1

1

3

--)


1

Soil
8-4 8-S
1
1
1
1
2
1

1

3

1-
(--
( —
1

1
1
1
1
1
1
1
1
1
1
2
1

1

3

1
1
1
1
1

8-7
1
1
I
1
2
1

1

3

--)
— )
— )
1

Soil and sludge
8-12 8-13 8-14
1
1
1
1
2
1

1

3

("
(--
(--
1



1
2
1

1

3

1
1
1
1
1

1
1
1
1
2
1

1

3

")
--)
--)
1

SI udge
8-29 9-3 9-4
(-- 1
(-- 1
(-- 1
(-- 1
1 1
2 2
1 1

")
--)
--)
1
2
1

No solids

3 3

(-- 1
(-- 1
(-- 1
(-- 1
1 1


3

--)
..)
--)
I

-------
                                                        TABLE 9.   ANALYSIS MATRIX SUMMARY
Sample
                                            Location
                                                                                           Analysis
Sampling
procedure
                                   Parameter
                                                                          Method
                              Frequency
ro
00
Soil

Lagoon
surface oil

Lagoon
sludge oil

Soil plus
1agoon
sludge
                                        Kiln Inlet
                   Composite   PCBs
                   sample
Extraction by Method 3550,    All  tests
GC/EDC by Method 8080a
                                                                       Ultimate analysis
                                                                       (C.H.O.N.S.CI)
                                                    A003b
                                                                       8 EP toxlclty trace   Digestion by Method 3030.
                                                                       elements0
                                                                       EP toxlclty
                                                    AA by 7000 series methods'
                                                    Aqueous extraction by
                                                    Method 1310. AA analysis
                                                    by 7000 series methods8
                             1  composite


                             1  composite




                             1  composite
21 ECD volatile
organic*
Semi volatile
organic priority
pollutants
Purge and trap GC/ECD by
Method 8010*
Extraction by Method 3550,
GC/MS by Method 8270*
1 composite
1 composite
                         Kiln ash
Kiln ash pit
                               Composite   PCBs
                               sample
Extraction by Method 3550.    1  composite
GC/ECD by Method B080a
                                                                       8 EP toxlclty trace   Digestion by Method 3010.    1 composite
                                                                       elements0             AA by  7000 series methods8
                         'Reference 4.
                         Reference 5.
                         cAs. Ba.  Cd. Cr, Pb. Hg. Se. Ag.
                         ^Reference 6.
                         'Reference 7.
                         'Filters  desstcated to constant weight and weighed prior to extraction.
                         ^Reference 8.
                                                                                 (continued)
-------
                                                          TABLE 9.    (continued)
                                                                                    Analysis
Sample
Kiln ash
(continued)
Sampling
Location procedure

Parameter
EP toxlclty
Method
Aqueous extraction by
Method 1310. AA analysis
by 7000 series methods'
Frequency
1 composite
                                                                21 ECO volatile
                                                                organlcs

                                                                Semi volatile
                                                                organic priority
                                                                pollutants
                                                     Purge  and trap GC/ECD by      1 composite
                                                     Method 8010*

                                                     Extraction by Method 3550.    1 composite
                                                     GC/MS  by Method 8270*
ro
to
                  Scrubber
                  blowdown
Slowdown
discharge
upstream of
carbon bed
                                  Downsteam of
                                  carbon  bed
Composite   8 EP toxlclty trace
sample      elements0 In both
            solids and filtrate
                               PCBs


                               21 ECO volatile
                               organlcs

                               Semi volatile
                               organic priority
                               pollutants

                   Composite   PCBs
                   sample
AA by 7000 series method.
solids digestion by
Method 3010a
                                                                                                                   All tests
                                                                                      Extraction by Method 3510,   All tests
                                                                                      GC/ECD by Method 8080*

                                                                                      Purge and trap GC/ECD by     All tests
                                                                                      Method 8010*

                                                                                      Analysis of above extract    All tests
                                                                                      by Method 8270*
                                  Extraction by Method 3510.   All  tests
                                  GC/ECD by Method 8080*
                  •Reference 4.
                  ^Reference 5.
                  cAs. Ba. Cd.  Cr.  Pb.  Hg.  Se.  Ag.
                  ^Reference 6.
                  'Reference 7.
                  'Filters dessicated to constant weight  and weighed  prior  to extraction.
                  9Reference 8.
                                                                                                                   (continued)
-------
                                                 TABLE  9.   (concluded)
co
o

Sample
Flue gas
particulate,
PCB. and
other
semi volatile
organlcs
Flue gas
volatile
organlcs
Stack gas
participate

Location
Downstream of
scrubber system,
upstream of
carbon bed/HEPA
filter
Downstream of
scrubber,
upstream of
carbon bed/HEPA
filter
Stack downsteam
of carbon bed/
HEPA filter

Sampling
procedure
Modified
Method 5d
Volatile
organic
sampling
train
(VOST)9
Method 5

Parameter
Particulate load
PCBs
Semi volatile
organic priority
pollutants
21 ECD volatile
organics
Particulate load
Analysis
Method
Method 5e»f
Soxhlet extraction of
train components by
Method 3540. combination.
concentration, and GC/EDC
analysis by Method 8080*
Analysis of above extract
by Method 8270'
Thermal desorptlon.
purge and trap GC/ECD
by Method 8010
Method 5«

Frequency
All tests
All tests
All tests
All tests
All tests
              'Reference 4.
              bReference 5.
              cAs. Ba. Cd. Cr.  Pb, Hg. Se. Ag.
              ^Reference 6.
              Reference 7.
              fFilters desslcated to constant weight and weighed prior  to extraction.
              9Reference 8.
-------
              TABLE  10.  VOLATILE ORGANIC COMPOUNDS ROUTINELY
                         ANALYZED BY GC/EOC AT THE CRF
               Methylene chloride        Trichloroethylene
               1,1-dichloroethylene      Benzene
               1,1-dichloroethane        1,1,2-trichloroethane
               t-l,2-dichloroethylene    Hexane
               Chloroform                Bromoform
               1,2-di chloroethane        Tetrachloroethylene
                                         plus Tetrachloroethane
               1,1,1-trichloroethane     Isooctane
               Carbon tetrachloride      Toluene +  Heptane
               Bromochloromethane        Chlorobenzene
               1,2-dichloropropane       Octane
               t-1,3-dichloropropylene
     •   Analyzing one composite sludge sample, the  composite  kiln  ash

         sample, and all scrubber blowdown  samples taken  upstream of  the

         water treatment carbon bed  for the  8  EP toxicity trace  metals.

     •   Subjecting one composite sample of  each waste  feed  and  a composite

         kiln ash sample to EP toxicity extraction  (Method 1310,

         Reference 4) and trace element analysis

     •   Subjecting one composite waste feed sample  to  ultimate  analysis

     •   Analyzing all VOST samples  for the  21  volatile organic

         compounds visible to the ECD  and routinely  determined at the

         CRF (see Table 10)

       Ultimate analyses (C, H, 0, N,  S, and Cl) were  in  accordance with

approved ASTM methods as documented  in Reference 5.  Waste feed  and kiln  ash

were sonication extracted in accordance with Method  3550.  Scrubber blowdown

were extracted 1n accordance with Method 3510.  All  resultant  extracts  were

be concentrated and analyzed for PCBs  via direct injection GC/ECD  by

Method 8080, and for the semi volatile  organic  priority  pollutants  by
                                      31
-------
Method 8270 except those for scrubber blowdown taken  downstream  of  the  carbon
bed which were only analyzed for PCBs.
       One composite waste feed sample, the composite kiln  ash sample,  and
all scrubber blowdown samples taken upstream of the carbon  bed were analyzed
for the volatile chlorinated organics by purge and  trap  6C/ECD in accordance
with Method 8010.
       Trace element analyses were performed by atomic absorption in
accordance with the 7000 series methods.  Appropriate acid  digestion of solid
samples were performed as needed by Method 3010.  EP  toxicity extraction and
extract analyses were performed for one composite surface oil and  lagoon
sludge and for individual test samples of soil and  soil  plus sludge.  (See
Table 5). Composite kiln ash samples were also subjected to EP toxicity
analyses.
       MM5 train samples (filter catch, sorbent resin, condensate,  and
impinger solutions) were Soxhlet extracted in accordance with Method 3540.
Resulting extracts were analyzed for PCBs via direct  injection GC/ECD by
Method 8080 and for the semivolatile organic priority pollutants by
Method 8270.  VOST traps were analyzed for halogenated volatile  organics by
thermal desorption, purge and trap (Method 5030) GC/ECD  in accordance with
Method 8010.
                                     32
-------
                                  TABLE  11.   PCB  EMISSION RATE AND DE SUMMARY
CO
Waste type
Lagoon surface
oil
Soil
Sludge
Soil plus
sludge
Test
no.
1
2
3
1
2
3
1
2
3
1
2
3
Feed (Arochlor
Concentration
(mg/kg)
282
296
280
67.3
167
95.4
250
250
250
78.6
120
170
1254)
Rate
(mg/s)
1.38
1.68
1.85
0.834
2.02
1.20
2.77
2.46
2.27
0.913
1.39
2.04
Emission (Arochlor 1254)
at scrubber discharge
Concentration
(ng/dscm)
207
212
180
32
39
52
9
42
82
49
73
109
Rate
(pg/s)
0.097
0.12
0.060
0.0093
0.011
0.021
0.0039
0.019
0.037
0.021
0.031
0.041
OE
(percent)
99.9930
99.9929
99.9968
99.9989
99.9995
99.9983
99.99986
99.99923
99.9984
99.9977
99.9978
99.9980
Weighted
average DE
(percent)
99.9944
99.9990
99.9992
99.9979
-------
                                  SECTION 4
                                TEST RESULTS

     This section summarizes emission  results and PCB destruction efficiency.
Details on sampling and analytical reports can be found  in Appendices  D
and E, respectively.
4.1  PCB DESTRUCTION
     Table 11 summarizes PCB emissions  (as Arochlor  1254) and  DE  for  each  of
the 12 tests performed.  On the average PCB emissions were highest  for the
lagoon surface oil and lowest for the  soil and sludge waste  streams when
incinerated individually rather than in combination.  DE calculations
indicate that a PCB destruction in the  99.992 to 99.9998 was  achieved  during
these tests as measured in the scrubber system discharge flue  gas.  Thus
destruction performance measured at this location failed to  meet  the
requirements under TSCA regulations for 99.9999 percent  efficiency.   As
reflected by the relative emission rate for each waste  feedstock, the lowest
DE values were recorded for the lagoon  surface oil  (mass weighted average  for
the three tests at 99.9944 percent) and highest for  the  sludge (mass  weighted
average for the three tests at 99.9992  percent).  Figure 6  illustrates the
relative levels of DEs achieved.  In this figure the ordlnate (or y-axis)
represents the number of nines 1n destruction efficiency, thus a value of
four signifies 99.99 percent DE.
                                      33
-------
                                  PCB DE SUMMARY
  99.9999
   99.999-
    99.99-7
c
-------
     Figures  7 through  9  illustrate attempts at correlating  key  process
parameters  (excess Og at  the  afterburner exit, gas  flowrate,  and mean
temperature)  with DE.   In  general, no definitive trends  are  evident  from
these graphs.  Gas flowrate shows the greatest effect  on  DE  with decreasing
PCB destruction as gas  flowrate  is increased.  Gas  flowrate  was  increased
during tests  tests primarily  by  increasing the amount  of  excess  air  as
evidenced by  increased  02  concentrations at the afterburner  exit.  Some of
this excess air was the result of air infiltration  through the kiln  seals
thus directly affecting the gas  residence time in the  afterburner  chamber.
Also note that the highest DE volume was recorded when the average oxygen
concentration at the afterburner exit was 10 percent,  the highest  setting
during these tests.  This  data point would suggest  that  very high  excess  air
levels are also conducive  to  high levels of PCB destruction.
     When the mean gas  temperature; defined as the  arithmetic average  of  the
kiln and after burner temperatures, is normalized by the  actual  gas  flow  rate
(essentially  inverse residence time) a more visible trend is observed  as
shown in Figure 10.  If the high DE at high excess  Q£  data point  is
disregarded, extrapolation of these data would suggest that  at a mean
temperature of 960°C (1,760°F) a gas flowrate of 1.18  m^/sec would be
required for 99.9999  percent ORE.  This gas flowrate  corresponds  to gas
residence time in the afterburner of about 2.0 sec  at  a  temperature  of
1,200°C (2,200°F).  This  is about twice the actual  residence time  achieved
during these tests.
     Scrubber blowdown  and kiln  ash were also analyzed for PCB content.
Concentrations in the blowdown were below detection (<1  ug/L) for  eacn test
sample.  In the kiln ash  the  concentration was also below detection

                                     36
-------
8 -
5.0 -
5.8 -
5.7 -
5.6 -
5.5 -
5.4 -
5.3 -
-5 "-
£ 5.1 -
f 5"
§ 4.9 -
1 4.S -
4.7 -
4.6 -
4J -
4.4 -
4.2 -
4.1 -
i

a





D

a
a

° 0
a

0

a a

J 7 9 1
                   EXCESS 02 (PERCENT}
Figure 7.   PCB DE as a function of excess
                       37
-------
  6
5.9 -

3.7 -
5.6 -
5 J -
3.4 -

*2 -
3.1 -
  5 -
4,9 -
43 -
4.7 -
4.6 -
4.5 -
4.4 -

4.2 -
4.1 -
  4
1.2     1.4     1.6     1.8      2     Z2
                 GAS FUOWRATE (ACM/SEC)
2.4
2.6
                                                                     2J
      Figure  8.   PCB DE  as a function of  gas flowrate.
                                   38
-------







^
o

C£


1








5 .8 -
5.7 -
5.6 -
5.5 -
5.4 -
33 -
5.2 -

5.1 -
5 -

4.9 -
4.8 -
4.7 -

4,6 -
4J -
4.4 -
4.2 -

a





a


a

a

0 a
o
D n

a


a a
1.6
1.64
1.68
1.72
1.76
1.8
1.84
1.88
  Figure 9.  PCB  DE as a function of mean temperature.
                              39
-------
   99.9999-
   99.999-1
    99.99 -
S     9.9
OJ
CL
       99 _
       90 -
          6.5
                       PCB DE vs. temp/flowrate  (F/ACM/SEC)
9.7
   Linear regression
   Coefficient = 0.82
  0.9
(Thousands)
1.1
1.3
         Figure 10.  PCB DE  versus mean  temperature/gas  flowrate
                                    40
-------
 (<0.4 ug/g)  for all  samples  except  for the composite ash from the surface oil
 test which  revealed  a  concentration of 2.55 ug/g.
 4.2   VOLATILE  ORGANIC  EMISSIONS
      Tables  12 through  15 summarize the measured concentrations of volatile
 organics  in  the kiln feed material and in each of the three discharge
 streams,  namely the  kiln ash, scrubber blowdown, and flue gas.  Most of the
 volatile  organics were  detected in the lagoon surface oil in concentration
 ranging from about 3 to 68 ppm by weight.  The kiln ash and scrubber blowdown
 streams were found to be mostly devoid of volatile organics with the
 exception of methylene  chloride in the scrubber blowdown.  Flue gas
 concentrations  of individual compounds ranged from as low as 0.5 ug/dscm to
 1,730 wg/dscm.   Highest concentrations were generally reported for methylene
 chloride.
     Tables  16  through  19 list corresponding mass flowrates in ug/sec for the
 volatile organic compounds.  Typically, emission rates of benzene, methylene
 chloride, bromoform, and tetrachloroethylene were higher than those
 accountable  by  the waste being incinerated.  Except for bromoform, these are
 common PICs.  Highest total emissions were recorded for the surface oil test
 due primarily to highest average emissions for benzene and methylene
 chloride.
 4.3  PARTICIPATE AND HCl EMISSIONS
     Table 20 summarizes particulate matter concentration at each flue gas
 location tested.  Not surprisingly, the highest emissions were measured
during soil  and soil  plus sludge tests.  However, scrubber discharge
concentrations were well below the hazardous waste Incinerator regulatory
limit of 180 mg/dscm for all  tests.

                                     41
-------
                           TABLE 12.   VOLATILE ORGANIC  CONSTITUENT CONCENTRATIONS FOR  THE  BROS
                                        LAGOON  SURFACE OIL TESTS3
ro
Scrubber blowdown
concentration


Compound
Methyl ene chloride
,1-dichloroethylene
,1-dtchloroethane
-1,2-dlchloroethylene
Ihloroform
, 2-d 1 ch I oroethane
,1,1-trlchloroethane
Carbon tetrachlorlde
Bromodi ch 1 oromethane
1,2-dichloropropane
t-l,3-d1chloropropylene
Trichloroethylene
Benzene
1,1,2-trichloroethane
Hexane
Bromoform
Tetrachloroethylene +
tetrachloroethane
Tnluftnp
1 u 1 UVTIIC
Chlorobenzene
1 ,3-dlchlorobenzene
1 ,2-dichlorobenzene
1 , 4 -di Chlorobenzene
Internal standard
recovery (X)
Isooctane
Octane

Feed material
concentration
(mg/kg)
NO
4.7
NO
7.1
27
16
3.3
68
NO
4.0
NO
21
3.7
NO
23
NO
NO

44
^^
NO
NO
NO
NO


_-
--

Kiln ash
concentration
(*g/kg)
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO

NO
nv
NO
NO
NO
NO


--
--
Average virtual stack
flue aas concentration
(mg/L) (ng/d$cm)b
Test 1
7-21
22.000C
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO

NO
NO
NO
NO
NO


--
--
Test 2
7-28
45
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO

NO
NO
NO
NO
NO


--
--
Test 3
7-29
1,080C
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO

NO
NO
NO
NO
NO


—
- •
Test 1
7-21
NO
NO
NO
NO
NO
4.7-5.6
NO
6.2
NO
NO
NO
NO
1,730C
NO
NO
NO
3.6

1.7-2.6
NO
NO
NO
NO


404-1,560
5-38
Test 2
7-28
240°
NO
NO
NO
3.2
6.2
NO
76C
1.7-2.4
NO
NO
NO
0.6-0.8
NO
5.4
0.63-0.96
1.9-2.3

2.9-3.3
NO
NO
NO
NO


134-694
72-108
Test 3
7-29
26
NO
NO
NO
4.8
31C
NO
35C
NO
NO
NO
NO
NO
NO
6.4
NO
7.5

9.9
NO
NO
NO
NO


114-189
161-185
                 aND denotes not detected
                  -- denotes not applicable
                 ^Average over three trap pairs  analyzed.  When range Is cited, analyte not detected  In one or more trap
                  pairs, low values correspond to  nondetects  assumed to be zero.  High values correspond to nondetects
                  assumed to be In detection limit.
                 cAnalyzed value above  calibration range.
-------
         TABLE  13.   VOLATILE ORGANIC CONSTITUENT CONCENTRATIONS  FOR  THE  BROS
                       SOIL TESTS3
                                                      Scrubber btowdown
                                                        concentration
                                                            (n»g/L)
   Average virtual  stack
  flue gas concentration
        (ug/dscm)b
Feed material
concentration
Compound (ng/kg)
Hethylene chloride
,1-dlchloroethylene
,1-dlchloroethane
-1.2-dlchloroethylene
;h)oroform
,2-dichloroethane
,1.1-trlchloroethane
Carbon tetrachlorlde
BroModlchloromethane
1.2-dlchloropropane
t-l,3-d1ch1oropropylene
Trichloroethylene
Benzene
1.1,2-trlchloroethane
Hexane
Bromoform
Tetrachloroethylene *
tetrachloroethane
Toluene
Chlorobenzene
1,3-dtchlorobenzene
1.2-dt Chlorobenzene
1 ,4-dlchlorobenzene
ND
ND
ND
ND
ND
ND
NO
NO
ND
ND
ND
ND
ND
ND
ND
ND
ND

ND
ND
ND
ND
ND
Kiln ash
concentration
(mg/kg)
ND
4.7
ND
ND
ND
29
ND
20
ND
ND
ND
ND
ND
ND
ND
ND
ND

ND
ND
ND
NO
ND
Test 1
8-4
53
ND
ND
ND
NO
ND
ND
ND
ND
ND
NO
NO
ND
ND
ND
ND
NO

NO
ND
ND
ND
NO
Test 2
8-5
16
ND
ND
ND
NO
ND
NO
ND
ND
ND
NO
ND
ND
ND
ND
ND
NO

ND
ND
ND
ND
ND
Test 3
8-7
34
ND
NO
ND
ND
ND
NO
ND
ND
ND
ND
NO
ND
ND
ND
ND
ND

ND
ND
ND
ND
ND
Test 1
8-4
38
0.61-0.72
NO
NO
2.4
ND
4.6-5.0
7.8
ND
ND
ND
ND
0.82-1.0
ND
2.8-3.0
1.9-2.6
11

9.0
ND
ND
ND
ND
Test 2
8-5
14
NO
NO
ND
2.4
ND
ND
4.4
ND
ND
NO
ND
1.4
NO
1.8
3.9-4.2
7.4

6.9
ND
ND
ND
ND
Test 3
8-7
39^
2.4
ND
ND
4.7
14.5-15.6
4.8-5.0
17C
ND
ND
ND
NO
0.7-1.0
ND
0.62-0.87
1.2-1.4
17

12
ND
ND
ND
ND
Internal  standard
  recovery  (X)
  Isooctane

  Octane
66. 99.
  602
81-106
 64-138   69-172

106-114   50-116
•ND denotes not detected
 — denotes not applicable
bAverage over three trap pairs analyzed.  When range  Is cited, analyte  not detected In one or more trap
 pairs,  low values correspond to nondetects assumed to be zero.  High values correspond to nondetects
 assumed to be In detection  limit.
cAnalyzed  value above calibration range.
-------
          TABLE 14.   VOLATILE ORGANIC  CONSTITUENT CONCENTRATIONS FOR THE  BROS
                       SOIL/SLUDGE  TESTS9



Scrubber blowdown
concentration
(ntg/L)
Feed material Kiln ash
concentration concentration Test 1
Compound
Methylene chloride
1,1-dlchtoroethylene
1,1-dichloroethane
t-l,2-d1chloroethylene
Chloroform
1 ,2-dlchloroethane
1.1.1-trlchloroethane
Carbon tetrachlorlde
Bromodl chl oromethane
1 ,2-dlchloropropane
t - 1 , 3-d 1 ch 1 oropropy 1 ene
Trlchloroethylene
Benzene
1 .1 ,Z-tr1chloroethane
Hexane
Bromoform
Tetrachloroethylene +
tetrachloroethane
Toluene
Chlorobeiuene
1 ,3-dlchlorobenzene
1.2-dichlorobenzene
1 , 4 -d 1 ch 1 orobenzene
Internal standard
recovery (*)
Isooctane
Octane
(«9/kg)
NO
15
NO
NO
ND
59
NO
57
ND
ND
ND
5.0
ND
ND
ND
ND
ND

5.1
ND
ND
ND
ND


--
--
(«g/kg)
ND
ND
ND
ND
ND
ND
17
ND
ND
ND
ND
ND
ND
ND
NO
ND
ND

ND
ND
NO
ND
ND


—
--
8-12
53
ND
ND
ND
ND
ND
11
ND
ND
ND
ND
ND
ND
ND
ND
NO
ND

NO
ND
ND
NO
ND


—
--
Test 2
8-13
44
ND
NO
ND
ND
NO
ND
ND
ND
ND
ND
ND
ND
NO
ND
ND
ND

ND
ND
NO
NO
NO


..
--
Test 3
8-14
ND
ND
NO
ND
ND
ND
ND
NO
ND
ND
ND
ND
ND
ND
ND
ND
ND

ND
ND
ND
NO
ND


..
--
Average virtual stack
flue gas concentration
(ng/dsan)b
Test 1
8-12
45C
ND
ND
ND
3.2
ND
0.47-0.82
18C
ND
ND
ND
ND
1.4
ND
4.8-5.0
1.7-2.0
2.0-2.3

4.6
ND
ND
NO
ND


52-75
54-112
Test 2
8-13
230°
ND
ND
ND
5.3
ND
ND
18C
NO
NO
ND
ND
1.2
ND
9.6C
2.5-2.8
3.2

3.4
ND
ND
NO
NO


48-62
76-90
Test 3
8-14
18
ND
ND
ND
3.2
ND
ND
14C
ND
ND
ND
ND
2.0
ND
1.0
1.1-1.6
6.6

5.2
NO
ND
ND
ND


62-67
99-112
aND denotes not detected
 -- denotes not applicable
bAverage over three trap pairs analyzed.   When range Is cited, analyte not detected In one or more trap
 pairs, low values correspond to nondetects assumed to be zero.  High values correspond to nondetects
 assumed to be In detection limit.
cAnalyzed value above calibration range.
-------
                           TABLE  15.
tn
VOLATILE ORGANIC  CONSTITUENT  CONCENTRATIONS  FOR  THE  BROS
SLUDGE  TESTS3
                                                                        Scrubber blowdown
                                                                          concentration
                                                                              (mg/L)
                                                      Average virtual stack
                                                      flue gas concentration
                                                            (ng/dscm)b
Feed material Kiln ash
concentration concentration Test 1 Test 2 Test 3 Test 1
COMpound (mg/kg) (*g/kg) 8-28 9-3 9-4
Hethylene chloride
1,1-dichloroethylene
1,1-dichloroethane
t-l,2-dichloroethylene
Chloroform
1,2-dichloroethane
1.1.1-trichloroethane
Carbon tetrachloride
Bromod i chl oromethane
1 ,2-di chl oropropane
t-l,3-dichloropropylene
Trichloroethylene
Benzene
1 .1 ,2-trichloroethane
Hexane
Bromoform
Tetrachloroethylene +
tetrachloroe thane
Toluene
Chlorobenzene
I ,3-dichlorobenzene
1,2-dichlorobenzene
1 ,4-dichlorobenzene
Internal standard
recovery (X)
Isooctane
Octane
NO
ND
ND
ND
ND
14
ND
63
ND
25
ND
12
2.1
ND
6.0
ND
16

4.7
ND
ND
ND
ND


__
—
53
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND

ND
NO
NO
NO
ND


-.
--
131
NO
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
NO
ND
ND

ND
NO
ND
ND
ND


..
--
538C
ND
NO
ND
NO
ND
NO
ND
NO
ND
NO
NO
ND
ND
ND
ND
ND

ND
ND
ND
NO
NO


—
__ — —
Test 2
9-3
11
ND
ND
ND
5.8
ND
ND
5.1
ND
1.4
ND
3.5
8.4
NO
9.3
ND
8.8

5.1
ND
ND
ND
ND


64-146
106-122
Test 3
9-4
28
ND
4.3
ND
9.2
ND
ND
ND
ND
0.70-0.90
ND
2.1
6.5
ND
2.2
ND
ND

2.9
ND
ND
ND
ND


102-161
100-102
                   'NO denotes not detected
                    -- denotes not applicable
                   bAverage over three trap  pairs analyzed.   When range is cited, analyte not  detected in one or more trap
                    pairs.   Low values correspond to nondetects  assumed to be zero.  High values correspond to nondetects
                    assumed to be in detection  limit.
                   cAnalyzed value above calibration range.
-------
TABLE 16.  VOLATILE ORGANIC FEED AND EMISSION RATES (LAGOON SURFACE OIL)


Average emission rate (pg/sec)
Waste feed
Into kiln Test 1
Compound (pg/sec) 7-21
Methylene chloride
1 , l-d1 chloroethy 1 ene
1,1-dlchloroethane
t-l,2-d1chloroethylene
Chloroform
1,2-dlchloroethane
1,1,1-trlchloroethane
Carbon tetrachlorlde
Bromodl chl oromethane
l,2-d1chloropropane
t-l,3-d1chloropropylene
TMchloroethylene
Benzene
1,1,2-trlchloroethane
Hexane
Bromoform
Tetrachloroethylene +
tetrachloroethane
Toluene
ND
27
ND
41
150
92
19
390
ND
23
ND
120
21
ND
132
ND
ND

250
ND
ND
ND
ND
ND
2.2- 2.6
ND
2.9
ND
ND
ND
ND
813
ND
ND
ND
1.7

0.80-1.2
Test 2
7-28
140
ND
ND
ND
1.8
3.6
ND
44
1.0- 1.4
ND
ND
ND
0.34-0.47
ND
3.1
0.36-0.55
1.1- 1.3

1.7- 1.9
Test 3 Average all
7-29 tests
8.7
ND
ND
ND
1.6
10
ND
12
ND
ND
ND
ND
ND
ND
2.2
ND
2.5

3.3
49
ND
ND
ND
1
2
ND
20
0
ND
ND
ND
270
ND
1
0
1

2




.1
.3


.4





.8
.15
.8

.0
-------
TABLE 17.  VOLATILE ORGANIC FEED AND EMISSION RATES (SOIL)
Average emission rate (ug/sec)


Compound
Methyl ene chloride
1 , l-d1 chloroethyl ene
1,1-dichloroethane
t-1 ,2-d1 chl oroethyl ene
Chloroform
1,2-dichloroethane
1,1,1-trichloroethane
Carbon tetrachloride
Bromodichloromethane
1 ,2-dichloropropane
t-l,3-dichloropropylene
Tri chl oroethyl ene
Benzene
1,1,2-trichloroethane
Hexane
Bromoform
Tetrachl oroethyl ene +
tetrachloroethane
Toluene
Waste feed
into kiln
(ug/sec)
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND

ND

Test 1
8-41
11
0.18-0.21
ND
ND
0.7
ND
1.3-1.5
2.3
ND
ND
ND
ND
0.24-0.29
ND
0.81-0.87
0.55-0.75
3.2

2.6

Test 2
8-5
3.9
ND
ND
ND
0.70
ND
ND
1.3
ND
ND
ND
ND
0.41
ND
0.52
1.1-1.2
2.1

1.9


Test 3 Average all
8-7
16
1.0
ND
ND
1.9
5.8-6.3
1.9-2.0
6.9
ND
ND
ND
ND
0.28-0.40
ND
0.25-0.35
0.48-0.46
6.9

4.8
tests
10
0.40
ND
ND
1.1
2.0
1.1
3.5
ND
ND
ND
ND
0.37
ND
0.55
0.80
4.1

3.1
-------
                 TABLE 18.  VOLATILE ORGANIC FEED AND EMISSION RATES (SOIL PLUS SLUDGE)
00


Compound
Methylene chloride
I,l-d1chloroethylene
1,1-dlchloroethane
t-l,2-d1chloroethylene
Chloroform
1,2-dlchloroethane
1,1,1-trlchloroethane
Carbon tetrachloride
Bromodl chl oromethane
l,2-d1chloropropane
t-l,3-dichloropropylene
Tri chl oroethy 1 ene
Benzene
1 ,1 ,2-trlchloroethane
Hexane
Bromoform
Tetrachloroethylene +
tetrachloroethane
Toluene

Waste feed
into kiln
(ug/sec)
ND
180
ND
ND
ND
690
ND
670
ND
ND
ND
12
ND
ND
ND
ND
ND

60
Average emission rate (pg/sec)
Test 1
8-12
19
ND
ND
ND
1.4
ND
0.20-0.35
7.7
ND
ND
ND
ND
0.60
ND
2.1
0.73-0.85
0.85-0.98

2.0
Test 2
8-13
99
ND
ND
ND
2.3
ND
ND
7.7
ND
ND
ND
ND
0.51
ND
4.1
1.1-1.2
1.4

0.60
Test 3
8-14
6.7
ND
ND
ND
1.2
ND
ND
5.2
ND
ND
ND
ND
0.74
ND
0.37
0.41-0.60
2.5

1.9
Average all
tests
42
ND
ND
ND
1.6
ND
0.09
6.9
ND
ND
ND
ND
0.62
ND
2.2
0.83
1.6

1.5
-------
TABLE 19.  VOLATILE ORGANIC FEED AND EMISSION RATES (SLUDGE)


Compound
Methyl ene chloride
1 , 1-di chl oroethyl ene
1,1-dichloroethane
t-l,2-di chl oroethyl ene
Chloroform
1,2-di chl oroethane
1 ,1 , 1-tri chl oroethane
Carbon tetrachloride
Bromodi chl oromethane
1,2-di chl oropropane
t-l,3-dichloropropylene
Tri chl oroethyl ene
Benzene
1 ,1 ,2-tri chl oroethane
Hexane
Bromoform
Tetrachl oroethyl ene +
tetrachl oroethane
Toluene

Waste feed
into kiln
(ug/sec)
ND
ND
ND
ND
ND
140
ND
630
ND
250
ND
120
21
ND
60
ND
160

47
Average emission
Test 1 Test 2
8-28 9-3
4.9
ND
ND
ND
2.6
ND
ND
2.3
ND
0.63
ND
1.6
3.8
ND
4.2
ND
3.9

2.3
rate (ug/sec)
Test 3
9-4
13
ND
2.0
ND
4.2
ND
ND
ND
ND
0.32-0.41
ND
0.95
3.0
ND
1.0
ND
ND

1.3

Average all
tests
9.0
ND
1.0
ND
3.4
ND
ND
1.2
ND
0.50
ND
1.3
3.4
ND
2.6
ND
2.0

1.8
                             49
-------
                   TABLE 20.   PARTICULATE  EMISSIONS
       Test
Afterburner
exit participate
(•g/dscm)
Scrubber discharge
participate
(mg/dscm)
Stack
partlculate
(mg/dscm)
          Corrected            Corrected            Corrected
Measured  to 71  02   Measured  to 71 (>2a  Measured   to  71  02
Lagoon surface oil

  Test 1              19.7       17.9       0.5       0.5
  Test 2              8.9        8.3      <0.3       <0.3
  Test 3              13.6       13.1      <0.2       <0.2

Soil

  Test 1             259        279        11.9       12.8
  Test 2              47.6       48.3      16.7       16.9
  Test 3              52.2       51.1       9.9       9.7
                                           15.7
                                           11.5
                                           21.3
                                                                        18.5
                                                                        13.7
                                                                        26.1
  Test 1              24.8       31.9       6.2        8.0      12.2       12.7
  Test 2              33.0       31.2       7.4        7.0       9.7       12.5
  Test 3              19.3       18.3       6.0        4.7      38.1       45.7

Soil plus sludge
Test 1
Test 2
Test 3
14.1
216C
98.4
15.8
224
97.0
8.3
9.3
126
9.3
9.6
124
30.0
134
146
39.6
166C
182C
•02 not measured In the  scrubber discharge; correction assumes scrubber  discharge
 02 1s the same as  afterburner exit D£.
bNot measured for these  tests.
cData suspect due to unusually high proportion of partlculate catch  1n the  probe
 rinse.
                                       50
-------
     HC1 emissions, summarized in Table 21, indicate afterburner  exit
concentrations in the range of about 5 to 31 mg/dscm for all  tests.  The
corresponding mass emission rates at this location  of 0.007 to  0.0034  kg/hr
(0.015 to 0.075 Ib/hr) are also well below the hazardous waste  incinerator
regulatory limit of 1.8 kg/hr (4.0 Ib/hr).  Stack emission  rates  measured
downstream of the scrubber were all  below detection limits.
4.4  TRACE ELEMENT EMISSIONS
     Waste feed and discharge streams from the incinerator were analyzed for
arsenic, barium, cadmium, chromium,  lead, mercury,  selenium,  and  silver.
Metals analyses of leachates were also performed to determine whether  these
would be considered EP toxic hazardous wastes.  Only barium,  chromium, and
lead were consistently found in each of the samples analyzed.  Trace amounts
of arsenic and cadmium were detected in selected samples.
     Table 22 summarizes the concentrations of most common  trace  elements.
Lead showed the highest concentrations in the waste feeds with  nearly
3,000 ppm detected in the lagoon surface oil.  The higher concentration of
lead in the scrubber blowdown solids compared with the kiln  ash,  during the
soil and soil plus sludge tests, clearly shows that lead partitions  to the
flue gas particulate rather than in  the kiln ash and 1s eventually caught  in
the scrubber.  Both chromium and barium showed nearly equal  concentrations  in
the two discharge streams.
     Table 23 summarizes barium, chromium, and lead concentrations in
each of the leachate samples.  All measured levels were less  than 1  mg/L,
well below the respective EP toxicity limits.
                                     51
-------
                       TABLE 21.  HC1 EMISSIONS
       Test
                    Afterburner exit HC1
                                                Stack HC1
                              ppm                    ppm
                    mg/dscm   dry  Kg/hra  mg/dscm   dry  kg/hr
                                                                  Feed Cl
                                                                  content
Lagoon surface oil

  Test 1              9.6     6.3   0.015
  Test 2             12.6     8.3   0.024
  Test 3             17.3    11.4   0.020

Soil

  Test 1             30.9    20.4   0.016
  Test 2             16.8    11.1   0.016
  Test 3             17.8    11.6   0.024

Sludge

  Test 1             <4.9    <3.2  <0.007
  Test 2              7.2     4.8   0.011
  Test 3              5.7     3.8   0.009

Soil plus sludge
<9.6   <6.4  <0.010
<8.1   <5.3  <0.007
<8.1   <5.3  <0.009
<9.8   <6.5  <0.013
<9.7   <6.4  <0.012
<8.3   <5.4  <0.013
                                                                   0.10
                                                                   0.04
                                                                   0.009
Test
Test
Test
1
2
3
17
23
20
.8
.2
.8
11.7
15.3
13.7
0
0
0
.026
.034
.026 -
<9.3
<9.5
clO.l
<6.1
<6.3
<6.7
<0
<0
<0
.010
.012
.011
0.06


aFlue gas flowrate not measured at afterburner exit; scrubber discharge
 flowrate assumed for mass flow calculation.
^Method 5 train not run at the stack for this test.
                                   52
-------
             TABLE 22.  TRACE ELEMENT EMISSIONS
                                     Concentration (ppm)a
       Test/sample
Arsenic    Barium  Chromium    Lead
Lagoon surface oil

  Composite feed                2      1,040       46      2,890
  Composite kiln ash           <2        120    1,090      2,160

Soil

  Composite feed               <1        740       55        760
  Average kiln ashb            <2        550      130        910
  Average blowdown solids0    <60        980      100      2,400

Sludge

  Composite feed               <1         23       12         46
  Composite kiln ash           <2        680      110        800

Soil plus sludge
Composite feed
Average
Average

kiln asM>
blowdown
solidsb
11
<2
24
820
740
820
65
87
73
1,030
450
5,010
aNo mercury, selenium, nor silver was found in any sample; no
 cadmium was found in any sample except the composite soil
 plus sludge at 4 ppm and the blowdown solids from soil plus
 sludge, Test 3, at 49 ppm.
^Average over three tests.
cAverage over Tests 2 and 3; Test 1 blowdown contained no solids,
                              53
-------
          TABLE 23.  EP LEACHATE CONCENTRATIONS
                            Leachate concentration
                                   (mg/l)a
        Test/sample            Barium  Chromium     Lead
EP Toxicity Limit              100       5.0         5.0
Lagoon surface oil
Composite feed
Composite kiln ash
Average blowdown liquidb
Soil
Composite feed
Average kiln ash°
Average blowdown liquidb
oi33 
-------
                                 SECTION 5
                    QUALITY ASSURANCE AND QUALITY CONTROL

     The quality assurance and quality control efforts performed during these
tests aimed at demonstrating that the rotary kiln incinerator system could
achieve a destruction efficiency of at least 99.9999 percent for
polychlorinated biphenyls (PCBs).
     The parameters germane to DE determination were the amounts of PCB
entering (Qjn) and leaving (Qout) tne incinerator system.  Hence the QA/QC
effort focused on the measurements of the parameters that affect the incoming
and outgoing POHC.  These QC activities will be discussed below.
5.1  MEASUREMENT OF QIN
     The feed rate of Arochlor 1254 depended on the feed rate of the waste
material and the concentration of Arochlor 1254 in the individual waste.
     The lagoon surface oil  and the sludge were contained in a stirred tank
which sat on the platform of a weigh scale.  The weigh scale had been
calibrated with known weights.  The tank was connected to the pump by
flexible hoses.  The readout of the weigh scale was located in the control
room.  At nominal 15-minute intervals, the weight registered on the weigh
scale and the corresponding clock time were recorded.  The weigh scale was
accurate to 0.5 Ibs.  The time was recorded to within 15 seconds.  Hence the
feed rate of this waste material was determined by dividing the weight loss
                                     55
-------
by the elapsed time between weight  readings  and  is a highly reliable
measurement.
     The PCB-contaminated soil  and  the  mixture of soil plus lagoon sludge was
contained in preweighed 5.7L (1.5 gal)  fiberpacks.  The  rate of feed was
determined by the cummulative weight  or number of fiberpacks fed into the
kiln using the ram feed system over the duration of each test.
     The concentrations of the PCB  in the  waste  was determined by standard
EPA methods as discussed in Section 3 and  Appendix B and were found to be
100 to 250 ppm by weight for the four waste  materials  used.  Again, the
accuracy of these analyses is commensurate with  the method capability.
5.2  MEASUREMENT OF QQUT
     The amount of PCB leaving the  incinerator was dependent on the flue  gas
flow rate and the the PCB concentration in the flue gas.
     Stack velocity measurement with  a  calibrated pitot  probe during Method  5
sampling activities provided the data to calculate flue  gas  flow rate.
Strict adherence to the specified procedure  ensured that the data quality
would conform to the method specifications.
     Concentrations of the POHC in  the  various  sampling  locations were
determined by following standard accepted methodologies  as  described  earlier.
For this test series, the analytical  system, namely the  GC/ECD,  was
calibrated with a blank at the beginning of  each test  day.   After  every four
injections, a calibration standard sample was injected to  verify that the
system was functioning and responding properly.
     An additional procedure was followed in an  attempt  to detect  and prevent
cross-contamination of samples taken  from the same  location on  successive
days.  Following the probe sample recovery procedure,  the  probe was rinsed

                                     56
-------
with a solvent which was then collected and subjected  to  analysis to verify
absence of contaminants.
5.3  VOLATILE ORGANIC SPIKE RECOVERIES
     Spike and recovery studies for volatile organics  were  performed on  feed
materials, kiln ash, and scrubber blowdown.  Internal  standards  of  octane and
isooctane were also included in these analyses.   Results  of these studies are
presented in Table 24.  Internal standard recoveries were in the range of 89
to 107 percent for all spiked samples.  With the exception  of
1,2-dichloroethane, carbon tetrachloride and bromoform, which had recoveries
of approximately 145 percent, all recoveries from the  spiked feed material
were between 93 and 108 percent.  Kiln ash spike recoveries were in the  89  to
112 percent range, with the exception of carbon  tetrachloride, which had a
recovery of 140 percent.  Recoveries from spiked scrubber blowdown  were  all
between 84 and 116 percent with the exception of methylene  chloride which had
recoveries of 104 to 213 percent.
     Recoveries from VOST trap internal standards were presented in Table 25.
Recoveries were between 50 and 185 percent for octane  and between 48 and
602 percent for isooctane with the exception of of the first series of tests
which had relatively poor recoveries between 5 and 1,560  percent.   Recent
evaluation of VOST trap isooctane recoveries from many test series  has shown
that relatively poor and irreproducible recoveries for this compound are
common.  In future, isooctane will no longer be used as an  internal standard
for VOST analyses.
                                     57
-------
TABLE 24.  VOLATILE ORGANIC CONSTITUENT SPIKE SAMPLE  RECOVERY
                    Spiked
                     feed
                   material
Spiked
 kiln
  ash
      Spiked
scrubber blowdown
  concentration
   (% recovery)
concentration
Compound (% recovery)
Methylene chloride
1,1-dichloroethylene
1,1-dichloroethane
t-l,2-dichloroethylene
Chloroform
1,2-dichloroethane
1,1,1-trichloroethane
Carbon tetrachloride
Bromodichloromethane
1,2-dichloropropane
t-l,3-dichloropropylene
Trichloroethylene
Benzene
1,1,2-trichloroethane
Hexane
Bromoform
Tetrachloroethylene +
tetrachloroethane
Toluene
Chlorobenzene
1,3-dichlorobenzene
1,2-di Chlorobenzene
1,4-di Chlorobenzene
Internal standard
Isooctane
Octane
94
106
99
96
94
147
93
144
98
95
94
106
97
95
108
145
105

100
97
96
95
99

102
107
concentration
(% recovery) 7-28
90
108
94
84
86
112
88
140
95
89
89
89
93
90
86
108
90

89
89
90
90
90

85
88
125
84
104
89
91
92
91
96
92
91
93
87
93
92
87
86
93

91
92
91
91
91

89
93
8-5
104
96
105
98
96
99
98
96
96
98
98
98
98
97
98
96
98

98
98
98
98
98

99
100
8-13
143
93
102
92
94
91
94
96
95
94
95
94
97
86
90
90
92

94
94
94
95
95

92
94
9-3
213
109
114
111
116
113
114
74
116
114
113
113
113
114
106
115
112

111
112
110
111
110

107
106
                             58
-------
TABLE 25.  VOLATILE ORGANIC CONSTITUENT SPIKE
           RECOVERY IN VOST SAMPLES3
                    Percent Recovery
        Test date  Isooctane  Octane
7-21
7-28
7-29
8-4
8-5
8-7
8-12
8-13
8-14
9-3
9-4
404-1,560
134-684
114-189
66-602
64-138
69-172
52-75
48-62
62-67
64-146
102-161
5-38
72-108
161-185
81-106
106-114
50-116
54-112
76-90
99-112
106-122
100-102
        alnternal standards used were
         Isooctane and octane.
                     59
-------
                                 REFERENCES
1.  Memo from W.J. Librizzi, Director, Emergency and Remedial response
    Division to W.A. Cowley, Acting Director, Hazardous Waste Engineering
    Research Laboratory, "Request for Technical  Assistance Utilizing the EPA
    Combustion Research Facility (CRF) for the Bridgeport Rental and Oil
    Services (BROS) Superfund Site," February 11, 1986.

2.  Lee, J., R. W. Ross, II, and L. R. Waterland, "PCB Trial Burn Report for
    the U.S. EPA Combustion Research Facility Rotary Kiln Incinerator
    System," Acurex Draft Report under EPA Contract 68-03-3267, March 1987.

3.  Personal Communication, J. Pearson, Ecology and Environment, Inc.,
    Buffalo, New York, March 1986.

4.  "Test Methods for Evaluating Solid Wastes: Physical Chemical Methods,"
    EPA SW-846, 2nd ed., July 1982

5.  Harris, J. C., et al., "Sampling and Analyzing Methods for  Hazardous
    Waste Incineration," EPA-600/8-84-002, February 1984

6.  Schlickenreider, L. M., et al., "Modified Method 5 Train and Source
    Assessment Sampling System Operators Manual," EPA-600/8-85-003,  February
    1985.

7.  40 CFR Part 60, Appendix A

8.  Hansen, E.M., "Protocol for Collection and Analysis  of  Volatile  POHC
    Using VOST," EPA-600/8-84-007, March 1984.
                                      60
-------
                                 APPENDIX A
                       SAMPLING LOCATIONS AND METHODS

     Figure A-l lists the sampling methods and sample locations.   Gas  samples
were taken at the stack, the afterburner chamber exit, and  the  carbon  bed
inlet.  The stack samples were required to satisfy permit requirements;  the
afterburner exit and carbon bed inlet samples were taken to provide
information on the PCB destruction efficiency and PIC emissions prior  to flue
gas scrubbing.
     The CRF staff performed monitoring of the flue gas for C02 and 03 with
continuous emission analyzers (CEAs) throughout the test period.   Og and COg
were monitored simultaneously at the kiln exit, stack, afterburner exit, and
scrubber outlet locations.  Volatile organic species were sampled with VOST.
A standard M5 sampling strain extracted samples for HC1 and particulate
concentration determinations.  Semi volatile organic compounds were sampled
with the MM5 sampling train.
     The following sections describe the various test methods,  equipment, and
procedures used.  Appendix D provides a summary of the sampling data for
VOST, M5, and MM5, and continuously recorded emissions.
A.I  CONTINUOUS EMISSION MONITORING
     Table A-l lists the CEAs, their operation principles and their
analytical range sensitivities.
                                     A-l
-------
-V
1
Kiln
!



After
burner



i
VentuH
scrubber

t

Packed
toH«r

i


1
Carbon
b«d



HEPA
H1t«r

ro
                                                                    Para«eter



Sailing Waste Waste Fuel Air Kiln Scrubber
point feedrate feed feedrate feedrate ash blowdown
1 X X X X
2 X
3
4
5 X
6
7
MH5
(parttculate.
PCBs, and VOST
CN's Volume senlvolattle (volatile Method 5
(Oj, COj) flow oryanlcs) organlcs) (Partlcu)ate)


X
X
X X
XXX X
XX X
         T:  Temperature
         P:  Pressure
         RH:  Relative Hunldlty
                                           Figure  A-l.   Sampling protocol
-------
TABLE A-l.  CONTINUOUS GAS ANALYZERS
Instrument
Bendix 304
02 analyzer
Species
measured
02
Principle
of
detection
Zirconium oxide
detector
Instrument
concentration
range
0-25 percent
0-10 percent
Known
interferences

High combustibles
Lead, antimony,
arsenic
Bendix 8903
       analyzer
Infrared Systems
CO/C02 analyzer

Theta Sensors
02 analyzer
CO/COg


CO/C02


02
        NDIR


        NDIR


        Fuel cell
C02 0-10 percent  None
CO  0-1000 ppm

C02 0-20 percent  None
CO  0-2000 ppm

0-5 percent       None
0-15 percent
0-25 percent
                 A-3
-------
     Samples of combustion products were drawn continuously  from  the
afterburner exit and the stack.  After passing through  the sample
conditioning system which removes the moisture and particulates,  the
combustion products were analzyed for 03 and C02.   Figures A-2  and  A-3  show
the sample conditioning system details for the afterburner chamber  and  the
stack, respectively.
     From the afterburner chamber, gas laden with  moisture and  particulates
was withdrawn through a 61 cm (24 in.) long, 6.4 mm (1/4  in.) diameter
uncooled SS316 tubing.  The gas passed through a Graham glass condenser coil
and was cooled by 7°C (45°F) water.  The condensate was trapped and retained
in a 500-ml glass impinger.  The cleaner dried gas sample then  passed through
a glass fiber particulate filter and was pumped to the  gas analyzers.
     From the stack, the gas was withdrawn through a 61 cm (24  in.) long,
9.5 mm (3/8 in.) diameter uncooled SS 316 tubing.   Since  the stack  gas  was
saturated with water at about 71°C (160°F), it was passed through a water
drop-out glass jar to remove the condensate.  Particulates were then  removed
by a glass fiber filter.  The sample was further dried  by a  30.5  cm (12 in.)
Graham glass condenser chilled by 7°C (45°F) water.  The  condensate was
collected in a 500-ml glass container.  The clean  dry gas was then  pumped to
the 03, CO, and C02 analyzers.
A.2  VOLATILE ORGANIC SAMPLING TRAIN
     The VOST was designed to collect trace volatile organic compounds  in
combustion product streams (7).  The equipment used during these  tests  is
shown in Figure A-4.  Essentially, the train consisted  of:
     •    An unheated probe.  A 5.1 cm (2 in.) long glasswool plug at  the
         probe tip acted as a soot trap.  The afterburner probe was Hastelloy

                                     A-4
-------
   Primary
  Combustion
   Chamber
  Afterburner
24" x  1/4" 00
Hastelloy C-276 probe
                                          Partlculate filter
                                          (polycarbonate)
7 ft x  1/4" 00
polyethylene
transfer  tubinr
                          24"  x  1/4" 00
                          polyethylene tubinq
                      36" x 1/4"  00
                      SS transfer
                      tubinq
                         12" Graham
                         condenser
                         (glass)
To spray quench
            500 ml condensate.
            catch  (glass)
                                                     50 ft x 1/4" OD
                                                     polyethylene tubinq
                                                                  Pump
                                                                                                              oo
                                                                                     Vent to
                                                                                   Incinerator
           Figure  A-2.   Continuous  gas  analysis  system for the  afterburner exit.
-------
                              Mater droplet
                              removal vessel

                                 (glass)
2V x 3/8" 00
316 SS probe
ne
\
*.
i
tubing
1

i
ran
(P<
n

36" x 1/4" 00
polyethylene
tubing
                                                    Participate filter
                                                       polycarbonate )
500 ml
catch
       20  ft x 1/4" 00
       polyethylene
       tubing
                                                                 condensate
                                                                (glass)
'.i
5
                                                                                          12" Graham
                                                                                          condenser
                                                                                          (glass)
                                           50 ft x  1/1" 00
                                           polyethylene tubinq
                                                                                Pump and
                                                                                delivery system
                                                                                                                Vent  to
                                                                                                                incinerator
                         Figure A-3.   Continuous  gas analysis system  for  the  stack.
-------
             Afterburner
               28" i 3/8"
               Haslet toy C-276
               probe wttn • 2"
               glass wool plug

                            316
                                  I	,
9" PVC      /
condenser—'
                                                       316 SS two-way
                                                       ball  valve
                                                              15"  x  1/4" aluminum
                                                              tube.  Teflon lined
26" x 1/4"
316 SS
transfer
line
       1/4"  316 SS
       fitting with"
       thermocouple
                             	I
                                 ISO ml
                                 condensate
                                 catch (glass)
Water out
                           later In

                           316 SS tube fitting
                           with thermocouple
                           5" 316 SS cartridge
                           with 1.6 qns lenax
                            316 SS fitting
                           5" « 1/4" Teflon
                           tubing (sealed to
                           glass vessel with a
                           Teflon ring seal)
r
                                                                        32" x 1/4"
                                                                        Teflon tubing
                                                                     116 SS
                                                                     fitting
                                                              :316 SS  fitting

                                                              15" x 1/4" aluminum tube.
                                                              Teflon  lined


                                                              9" PVC  condenser
• Uater out


•Hater in

 3H SS fitting
                                   . 5"  316 SS cartridge
                                    with  1.6 gms Tenax
                                    316  SS  fitting

                                    5" x 1/4" Teflon tubing
                                    (sealed to glass vessel
                                    tilth a  Teflon ring seal)
                                                           50 ml asniratlon bottle
                                                          '(glass) with sIHca gel
                                  Figure  A-4.    VOST sampling  train.
-------
         C-76, 71 cm (28 in.) long and 9.5 mm (3/8  in.)  diameter.  The stack
         probe was 316 SS, 61 cm (24 in.)  long and  6.4 mm  (1/4 in.)
         diameter.
     •   A piece of 6.4 mm (1/4 in.) diameter SS  316  interconnecting tubing.
     •   A primary sample gas moisture condenser  consisting of a 38 cm (15
         in.) long and 6.4 mm (1/4 in.)  diameter  teflon-lined aluminum tubing
         encased in a water-cooled 22.9  cm (9 in.)  long  PVC shell.
     •   A 12.7 cm (5 in.) long SS 316 primary resin  cartridge containing
         1.6g Tenax.
     •   A glass condensate catch reservoir.
     •   A piece of 81 cm (32 in.) long  and 6.4 cm  (1/4  in.) diameter Teflon
         tubing.
     •   A secondary  gas moisture condenser similar to the primary
         condenser.
     •   A secondary  resin cartridge, similar to  the  primary resin
         cartridge.
     •   A 50 ml silica gel desiccator.
     The VOST methodology in use at the  CRF was designed for sampling
organics with boiling points between 40°C  (104°F  to 252°F).  Three duplicate
VOST samples were collected daily on each  test day.  They  were taken at
approximetely 90-minute intervals in order to cover the  typical 4- to 5-  hour
tests.  The VOST samples were taken for  20 minutes  at a  1  liter/minute.
Nominally,  20 liters  of gas passed through the Tenax  resin traps.
Approximately 50 ng per sample train is  sufficient  for quantification of  most
volatile compounds.
                                     A-8
-------
A.3  EPA M5 SAMPLING
                                                                        •
     The EPA M5 train was used to sample  participates, stack gas moisture,
and HC1 (4).  Figure A-5 shows the sampling  train which consisted of the
following:
     •   A heated glass-lined probe
     •   A heated particulate filter
     •   Two impingers containing 0.1 N sodium  acetate (for collecting HC1)
     •   One empty impinger
     •   One impinger containing 200g silica gel
M5 sampling in compliance with federal  regulations  (40 CFR 60,  Reference 6)
was performed at the stack and at the afterburner exit.
A.4  EPA MM5 SAMPLING
     The MM5 sampling train was used to extract semi volatile organic
compounds from combustion product streams (5).   During these tests, samples
were collected over a 4 to 5 hour test period from  the afterburner  chamber
exit and the stack.  The sampling trains for the afterburner chamber  and the
stack locations differed slightly to account for the sample gas temperature
and moisture differences.  Figure A-6 illustrates the train used for  the
scrubber outlet sample location.
     The MM5 train consisted of the following components:
     •   A 1.2 m (4 ft) long glass-lined, heated probe/pitot tube assembly
         with a 9.5 mm (3/8 In.) 00 SS 316 nozzle
     •   A heated filter 1n a 121°C (250°F)  oven
     •   A 30 cm (12 1n.) long and 9.5 mm (3/8 in.) diameter  00 teflon
         interconnecting tubing
     •   A water-cooled glass capsule containing 30g XAD-2

                                     A-9
-------
                                        Filter oven
       3/8" 316ss nozzle
I
(—•
o
                        1.2m (4 ft) 1"     Glass
                        glass-lined probe  connector

            types
            pttot
            tube
                       1/4" pilot
                       tube lines
r
             s$*
                                                   2.5 cm filter
                                                   assembly
                                                                          Glass connectors
                                                                                             Dial
                                                                                          thermometer
     Sampling console
                          Imolnqer kith 200 ml
                          0.10 sodium acetate
                                                                 D
                                                               •o   o-
                                           Impl
    Implnger with
    silica gel
oer
                                            empty
                                       Figure  A-5.  Method  5 sampling train.
-------
                                               19
                                                Lf)
                                                <
                                                OJ
                                                01
SSSS
    A-ll
-------
     •   A 4-liter glass  condensate  catch  reservoir
     •   A desiccator.
     Prior to assembly, the glassware  and  all tube fittings upstream of the
condensate catch were sonicated  in a 1:1 solutin of methylene chloride in
methanol.  Subsequently,  they were rinsed  with  100 ml of clean solution which
was then extracted and analyzed  by 6C/FID  to ensure that the fittings and
glassware were clean.  Following assembly  and prior to sample collection, the
trains were leak-tested.   All connections  upstream of the second condensate
catch were Teflon-to-glass joints or SS 316 tube fittings.  After the
sampling was completed,  the trains were again leak-tested.
     During the sampling period, the sample temperatures downstream  of the
probe, at the filter and downstream  of the resin capsule were monitored  and
controlled at about 121,  121 and 20°C  (250, 250 and 68°F),  respectively.  The
samples were withdrawn at approximately 0.02 m3/min  (0.75  ft3/min) for 4 to
5 hours.  At this rate,  about 5.4 dscm (200 dcsf) was  passed through the
train.  Upon test completion, the probe, interconnecting tubings,  filter, and
resin capsule were disassembled, sealed with  aluminum  foil, and  immediately
transported to the CRF analytical laboratory  for  sample  recovery.   All the
train components' internal surfaces  exposed to  the  gas were brushed  and
rinsed with a 1:1 solution of methylene chloride  in methanol.   The individual
rinse solutions, the particulate filters,  the condensate,  and  the XAD-2  resin
were then subjected to a series of analysis procedures which are discussed  in
Appendix B.
                                     A-12
-------
                                 APPENDIX  B
                    SAMPLE RECOVERY  AND ANALYSIS METHODS

     The samples collected by the CRF sampling team were  recovered and
analyzed onsite.  This appendix describes  the sample  recovery procedures and
the analysis methods followed by the CRF analytical laboratory.
B.I  SAMPLE RECOVERY
B.I.I  VOST Samples
     No special  sample recovery procedure  was needed  except  for  capping the
resin traps to prevent contamination and storing them on  ice prior to
analysis.  The traps were immediately delivered to the onsite analytical
laboratory where desorption and analysis were performed on the  same  day.
B.I.2  EPA MS Samples
     The CRF sampling staff recovered the  samples  from the EPA  M5 sampling
train, following procedures in accordance  with those  described  in
Reference 6.  The following discussion is  a  brief  description of the recovery
activities.
     After sampling a post-test checks were  completed, the probe was
disassembled from the train.  The outside  of the  sampling nozzle and the  ball
joint were wiped clean.  The particulate filter  holder was  removed  from the
train and the glass joints were wiped clean.  The subsequent recovery
procedure collected the following samples:
                                     B-l
-------
     •    The  outside surfaces of the probe, nozzle, and filter holder were
         wiped  clean to prevent inadvertent collection of dust and
         particulate.
     •    The  filter and the particulate cake were carefully removed from the
         filter holder and placed in a labeled petri dish.  The inside
         surface of the front half of the filter holder was brushed with
         clean, dry nylon bristles.  The particulate removed with the
         brushing was added to the filter in the petri dish.
     •    The  inside surfaces of the probe, nozzle, and filter holder front
         half were rinsed with an acetone solution repeatedly until no
         visible particulates were washed out.  The wash was collected in a
         clean, sealed amber glass container.
     •    The  silica gel was weighed directly in the impinger before and  after
         the  sampling to note the moisture trapped.  The silica  gel was  then
         regenerated.
     •    The  condensate catch in the  impingers was weighed  and the condensate
         color was noted.
     The samples were then  delivered  to  the  onsite analytical  laboratory for
chemical analysis. These  analyses  are discussed  in  Section 5.2.
B.I.3  EPA MM5 Samples
     The CRF analytical  laboratory  staff recovered the samples from  the MM5
sampling train in accordance with  procedures outlined in Reference 5.  A
brief description of  the procedures is  given below.
     The sample recovery took place immediately  following the conclusion of
each test as follows:
                                     B-2
-------
Tne  filter  and  the  participate  cake,  in  their  unmodified  state, were
carefully removed from  the  filter  holder  with  forceps  and
transferred  Into a  desiccator for  drying  overnight  prior  to  weighing
and  subsequent  Soxhlet  extraction.
The  1:1 methanol/methylene  chloride solution containing the
particulates washed  from the inside of the  probe  and the  probe
nozzle and the  front-half of the filter  holder—the outside
surfaces of  these components were  wiped  free of particulates.  The
inside surfaces were brushed with  clean  nylon  bristles and rinsed
with the above  solution repeatedly.   The  wash  was  volume-reduced  in
a Kuderna-Danish apparatus, dried, and combined with the  extracts  of
other train  components.
The  XAD-2 resin in  its  capsule  was quantitatively  transferred to  a
Soxhlet in which extraction began  immediately.
The  fluid volume and pH of  the  condensate collected in the
condensate knock-out vessel were measured and  recorded.   The fluid
was  transferred to  a separator  funnel for liquid-liquid extraction
on the next  day.
The  1:1 methanol/methylene  chloride solution collected from  washing
the  train components between the fiber filter  and  the  first  wet
impinger was collected  by repeatedly  brushing  and  rinsing the
various components,  combined with  the above probe  washes.
The  silica gel  1n the fourth impinger was transfered to a clean,
sealed container.
                            B-3
-------
     •   The unused portion of the 1:1 methanol/methylene chloride  wash
         solution to be used as blank was transferred into a  clean, sealed
         glass bottle.
B.2  ANALYSIS METHODS
     The samples from the recovery efforts were subjected to  analysis  to
determine the amounts of Arochlor 1254, and other organic constituents
trapped in the resins and sample extracts.  The following describes briefly
the analytical procedures employed at the CRF laboratory.
B.2.1  VOST  Samples
     Analysis of the VOST samples was performed in accordance with  purge  and
trap method (7).  The Tenax-GC resin traps were thermally desorbed  for 15
minutes at 180°C with organic-free nitrogen gas at a flowrate of 40 ml/min,
bubbled through 5 ml of organic-free water, and trapped on an analytical
absorbent trap.  After the 15-minute desorption, the analytical  absorbent
trap was rapidly heated to 180°C with the carrier gas flow reversed so that
the effluent flow from the analytical trap was directed into  the GC.  The
volatile volatile were separated by temperature programmed gas chromatograpy
and detected by a electron capture detector.
     The list of organic compounds sought with this analytical method is
given in Table B-l.  The primary focus of the tests was to determine the  DEs
of Arochlor 1254, which is analyzed with MM5 samples as described in
Section B.2.3.
B.2.2  EPA H5 Samples
     The rinse materials collected in the recovery procedure  were combined
and the entire aliquot was measured volumetrically to the nearest 1 ml and
quantitatively transferred to a tare-weighed beaker.  The sample was

                                     B-4
-------
evaporated to dryness on a steam table in a 140°C  (289°F) oven for 1 hour.
After it had cooled in a desiccator, the sample was weighed to the nearest
0.1 mg.  A. 200-ml aliquot of unused acetone was processed in the same manner
to account for blank weight gain.
     The filter paper was transferred to a petri dish and dried in a 140°C
(289°F) oven for 2.5 hours and weighed to the nearest 0.4 mg.  An unused
filter was processed in the same manner to act as  blank.
     The solution in the two impingers was measured volumetrically and
transferred to the CRF laboratory for chloride analysis  by specific ion
electrode.  The silica gel and the impinger were weighed to the
nearest 0.5g.
B.2.3  EPA MM5 Samples
     The samples derived from this sampling method were  analyzed for PCBs  and
other semivolatile chlorinated organic compounds in accordance with
Method 8080 which used gas chromatography/electron capture detection
(GC/ECD).  Samples were first extracted via separatory funnel  liquid-liquid
extraction (Method 3510), sonication (Method  3550), or Soxhlet extraction
(Method 3540) as appropriate.
B.3  OTHER SAMPLES
     In addition to the samples discussed earlier, samples of  the waste  feed,
kiln ash, and blowdown water were collected and analyzed in the CRF
laboratory.  All PCB analyses were performed  using direct  injection  GC/ECD by
Method 8080 following extraction in accordance with Methods 3540,  3550,
or 3510.  Analyses for semivolatile priority  pollutants  were  performed by
Method 8270.  Trace element analyses were performed by  atomic  absorption in
accordance with the 7000 series methods.  Appropriate add digestion  of  solid

                                     B-5
-------
samples was accomplished as needed by Method 3010.   EP extractions of
individual waste material and kiln ash were also performed with trace element
analyses by 7000 series methods.
                                     B-6
-------
  APPENDIX C



WASTE FEED DATA
      C-l
-------
        BROS SURFACE OIL TEST  7-21-86
m
o
LJ
 •

3


O
      10
                        CRF ROTARY KILN
T

12
   14

TIME (HOUR)
-------
m
o
LJ
U
        BROS SURFACE  OIL  TEST 7-28-86

                       CRF ROTARY KILN
      10
      14


TIME (HOUR)
 i

16
-------
CD
O
Ul
D
O
        BROS  SURFACE  OIL TEST  7-29-86
   340
      10
                       CRF ROTARY KILN
 14

TIME (HOUR)
16
 i

18
-------
    500
   400 -
tfl
CD
Q
LJ
 •

2


CJ
   300 -
   200 -
    100 -
              BROS SOIL TEST 8-4-86
                         CRF ROTARY KILN
                          TIME (HOUR)
-------
V)
CO
Q
Ld
o
    500
       10.5
                BROS SOIL TEST  8-5-86
                            CRF ROTARY KILN
1 1.5
12.5        13.5

  TIME (HOUR)
14.5
15.5
-------
m
v-/

Q
ID
O
       9.5
               BROS  SOIL TEST  8-7-86
                           CRF ROTARY KILN
10.5
1 1.5

TIME (HOUR)
12.5
13.5
-------
          BROS  SOIL/SLUDGE    TEST  8-12-86
(ft
CD
o
ui
 •
2


o
    500
                          CRF ROTARY KILN
                            TIME (HOUR)
-------
CO
O
UJ
O
    500
          BROS  SOIL/SLUDGE     TEST 8-13-86
                          CRF ROTARY KILN
                           TIME (HOUR)
-------
m
o
LJ
D
u
    500
          BROS  SOIL/SLUDGE    TEST  8-14-86
                         CRF ROTARY KILN
                           TIME (HOUR)
-------
             BROS  SLUDGE     TEST  8-28-86
CD
Q
Ld
                         CRF ROTARY KILN
                          TIME (HOUR)
-------
                BROS  SLUDGE     TEST  9-3-86
m
Q
LJ
O
    400
    350 -
    300 -H
    250 -
    200 -
    150 -
    100 -
     50 -
                             CRF ROTARY KILN
                               TIME (HOUR)
-------
CD
O
LJ
2
D
O
    400
    350 -
                BROS  SLUDGE    TEST  9-4-86
                            CRF ROTARY KILN
                              TIME (HOUR)
-------
 APPENDIX D



SAMPLING DATA
    D-l
-------
                                         Table.   Gas Concentntion on July 21,  1986
Tine
Start Stop
1115 113S
1135 1155
1155 1215
1215 1235
1235 1266
1255 1315
1315 1336
1335 1355
1355 1415
1415 1435
1435 1455
1455 1515
1515 1535
1535 1555
1555 1615
1615 1635
1635 1655
1655 1715
1715 1735
1735 1755
1755 1815

TIME
Start Stop
1115 1135
1136 1166
1155 1216
1215 1236
1235 1255
1255 1315
1315 1335
1335 1355
1355 1415
1415 1435
1435 1455
1455 1616
1515 1536
1635 1565
1555 1615
1616 1635
1635 1655
1655 1715
1715 1735
1735 1755
1 1755 1815
AFTERBURNER EXIT
Oxyg«n
Concentration
(* Dry as a*as'd)
Mift Max Mean
4.3 6.3 5.3
NA NA NA
HA NA NA
4.5 6.5 6.5
5.0 6.0 5.5
NA NA NA
NA NA NA
NA NA NA
NA NA NA
6.5 6.0 5.8
5.5 6.0 5.6
NA NA NA
NA NA NA
NA NA NA
6. 5 6.0 6.8
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(* Dry as Mes'd)
Hin Max Mean
7.4
7.8
6.5
NA
7.6
8.0
8.4
NA
7.8
8.0
8.0
8.2
NA
3.2
3.2
8.1
0.4
0.0 1
NA 1
.6
.3
.4
A
.2
.7
.4
1A
.4
.5
.5
.4
«A
.3
.4
.3
.5
J.O 1
«A 1
.0
.6
.0
tA
.4
.5
.4
.4
-------
                                        Table.
                                                   Gas Concentration on July 28, 1986

TIME



Start Stop
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
ijnn U9n
I*»UU 19 fV
1420 1440
1440 1SOO
1SOO 1620
1S20 1S40
1540 1600
1600 1620
1620 1640
1640 1700
1TOO 1714
AFTERBURNER EXIT
Oxygen
Concentration
| Carbon Dioxide | Carbon Monixide
j Concentration | Concentration
(t Dry as Mas'd) |(k Dry as Mas'd) |(* Dry as Mas'd)


Min Max Mei
4.0
3.8
NA
NA
.
.

,
•
.6
.0
A
«A
.8
.0
.0
.0
.0
NA IIA tu
NA NA Ml
1 1
in) Min Max Mean) Min Max Hean
4| NA NA NA | NA NA NA
4| NA NA NA | NA NA NA
k 4.2 4.3 4.3| NA NA NA
1 4.0 4.4 4.2J NA NA NA
.S| NA NA NA | NA NA NA
8| NA NA NA | NA NA NA
9| NA NA NA j NA NA NA
9| NA NA NA | NA NA NA
• j NA NA NA j NA NA NA
I 3.7 4.0 3*9| NA NA NA
t 3.7 3.9 3.8J NA NA NA
NA NA NA 3.7 3.9 3.8| NA NA NA
NA NA HI
5.8 6.3 6
4.S 6.8 6
6.0 6.0 6
6.0 6.0 6
6.0 10.3 •
7.3 7.3 7
NA NA HI
I

^ 3.7 3.9 3.8| NA NA NA
OJ NA NA NA | NA NA NA
6 j NA NA NA j NA NA NA
OJ NA NA NA j NA NA NA
OJ NA NA NA | NA NA NA
1| NA NA NA I NA NA NA
3 NA NA NA | NA NA NA
k NA NA NA | NA NA NA
1
'
CARBON BED INLET

Oxygen
Concentration
Carbon Dioxide
Concentration
(* Dry as Mas'd) |(k Dry M Mas'd)

Hin
7.
9.
NA
NA



•
kta\
NA
NA
U4
HM
NA
NA

Max Mei
10.6
10.0
NA
NA
9.6
10.0
10.0
9.8
9.6

n| Min Max Mean
1| NA NA NA
6| NA NA NA
3.7 4.4 4.1
j 4.0 4.4 4.2
8 j NA NA NA
• | NA NA NA
9 1 NA NA NA
6| NA NA NA
6| NA NA NA
Carbon Monoxide
Concentration
(\ Dry as Mas'd)

Mm Max Hean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
•J 41 ti A k.1 *
NA NA C.S *.T t.C| NA NA NA
UA UA ft ft at t ft ft 1 UA UA UA
HA IvH V • 9 •*• V • 0 | liM MA NM
NA NA 6.5 C.7 6.6J NA NA NA
NA NA 6.5 7.4 7.0| NA NA NA
.8 6.
.5 6.
.0 6.
.0 6.
.0 10.
7.3 7.
NA

NA N>

0| NA NA NA NA NA NA
6| NA NA NA NA NA NA
1| NA NA NA NA NA NA
OJ NA NA NA NA NA NA
1| NA NA NA NA NA NA
3| NA NA NA NA NA NA
k NA NA NA NA NA NA


TIME



Start Stop
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
1500 1520
1520 1540
1540 1600
1600 1620
1620 1640
1640 1700
1700 1714
KILN EXIT
-
Oxygen
Concentration
Carbon Dioxide
Concentration
Carbon Monixide
Concentration
(» Dry as Mas'd) | (* Dry as Mas'd) | (* Dry as Mas'd)



Min Max Mean] Min Max H«an| Hin Max Mean
NA NA NA
NA NA NA
.2 9.6 8.9
NA NA NA
.6 10.0 9.8| NA NA NA
0.0 14.3 7.1| A NA NA
14.0 14.5 14.3J NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
.3 .5 9.4| NA NA NA
.2 .5 9.4| NA NA NA
.1 .5 ».3| NA NA NA
.1 .3 9.2| NA NA NA
.1 .3 9.2| NA NA NA
0.0 14.8 7.4| NA NA NA
14.5 15.0 14.6J NA NA NA
14.8 15.0 14.9| NA NA NA
14.5 15.0 14.8
NA NA NA
15.0 15.0 1S.O| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
.9 9.3 .1
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
.5 10.0 .31 NA NA NA
.0 .1 .1) NA NA NA
.1 .2 .2| NA NA NA
.4 .1 .6| NA NA NA
.9 .5 .2 | NA NA NA
.3 .6 .4
NA NA NA
STACK
Oxygen
Concentration
(» Dry as Mas'd)

Min Max Hean
NA NA NA
NA NA NA
10.0 10.3 10.1
10.3 10.3 10.3
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide j Carbon Monoxide
Concentration j Concentration
(1 Dry as Mas'd) |(* Dry as Mas'd)
1
Min Hax Mean| Hin Max Mean
.5 6.5 7.5| NA NA NA
.8 7.4 7.1| NA NA NA
NA NA NA | NA NA NA
.8 7.1 7.0| NA NA NA
.0 7.2 7.1| NA NA NA
.9 7.2 7.1| NA NA NA
.8 7.1 7.0| NA NA NA
.8 7.1 7.0| NA NA NA
.8 7.1 6.5| NA NA NA
10.3 10.5 10.4| NA NA NA | NA NA NA
10.5 10.5 10. 5| NA NA NA j NA NA NA
10.5 10.5 10. 5| NA NA NA j NA NA NA
10.5 10.5 10. 5| NA NA NA j NA NA NA
10.0 10.5 10.3) .6 7.2 6.9| NA NA NA
NA NA NA .3 8.3 7.3| NA NA NA
NA NA NA .8 6.9 6.9| NA NA NA
NA NA NA .6 7.1 7.0| NA NA NA
NA NA NA .6 7.1 5.9J NA NA NA
NA NA NA .6 6.3 5.5| NA NA NA
NA NA NA .2 6.3 6.3| NA NA NA
NA NA NA .2 6.3 6.3| NA NA NA
1 1
NA - Data not taken
-------
                                         Table.    Gas Concentration on July 29.  1966

TIME



Start Stop
950 1010
1010 1030
1030 10SO
1050 1110
1110 1130
1130 1160
1150 1210
1210 1230
1230 1250
1250 1310
1310 1330
1330 1350
1350 1410
1410 1430
1430 1450
1450 1510
1510 1630
1530 1550
1550 1610
1610 1630
1630 1650
1650 1710
"1710 1730
1730 1750
1750 1810
i • 1 ft i Bin
IO'U IDJw
1830 1850
1850 1900

AFTERBURNER EXIT
Oxygen Carbon Dioxide Carbon Monoxide
Concentration Concentration Concentration
(* Dry as Mas'd) (*

Dry as Mas'd) (X Dry as Mes'd)

Nin Max Mean Min Max Mean Min Max Mean
3.5 6.0 4.8|
4.0 5. 4.8|
4.6 9. 7.0)
5.0 9. 7.3|
S.O 19. 12. 4|
20.0 20. 20.3|
6.0 20.5 12.8|
1.5 4.5 3.0| 1
1.5 10.5 6.0|
7.S 13.5 10.5J
3.6 7.5 6.«|
3.0 6.0 4.8
4.6 6.8 S.1J
.3 10.0 9.7| NA NA NA
.1 10.0 9.6| NA NA NA
.1 8.2 7.7| NA NA NA
.3 10.0 9.7| NA NA NA
.0 9.7 4.9J NA NA NA
.0 2.6 1.3| NA NA NA
.0 10.0 e.OJ NA NA NA
.0 10.0 10. 0| NA NA NA
.5 10.0 7.3J NA NA NA
.0 9.2 8.1J NA NA NA
.7 10.0 9.4J NA NA NA
.2 10.0 9.6| NA NA NA
.3 10.0 9.7| NA NA NA
NA NA NA | NA NA NA | NA NA NA
NA NA NA j NA NA NA | NA NA NA
NA NA NA | 1
M NA NA | NA NA NA
NA NA NA | NA NA NA | NA NA NA
S.S 8. 5 6.5|
5.3 S.S S.4|
5.3 5.3 5.3|
5.0 .3 5.6|
6.0 .5 .3)
6.0 .0 .01
6.0 .0 .0|
6.0 .0 .0!
6ft ft ft 1
. U • U * U I
6.0 .0 .0|
NA NA NA |
1
.2 .3 .3| NA NA NA
.2 .3 .3| NA NA NA
.4 .5 .5] NA NA NA
.8 .7 .6| NA NA NA
.2 .7 .3| NA NA NA
CARBON BED INLET
- . -

Oxygen | Carbon Dioxide | Carbon Monoxide
Concentration | Concentration | Concentration
(ft Dry as Mas'd)j(* Dry as «eas'd)|(ft Dry as Mas'd)

Min


i !
e

1 .
.
.

7.
6.
7.
1 1
Max Mean) M1n Max Mean) M1n Max Mean
10.0 9.3| 6.8 7.9 7.4| NA NA NA
10.3 9.3| 6.1 7.6 6.3| NA NA NA
12.3 11.1| S.I T.7 6.4| NA NA NA
16.8 12. OJ 3.1 7.5 6.3| NA NA NA
21.6 15.11 0.2 7.4 3.8| 12.3 5.5 8.3
21.5 19.9| 0.2 7.9 4.1| NA NA NA
18.0 12.3| 7.3 .5 8.4| NA NA NA
6.3 6.9J •* •* • •*! NA NA NA
16.6 12.1) .1 .4 4.6| NA NA NA
12.6 10.1| .6 .S 7.5J NA HA NA
9.6 8.1) .9 .7 7.8| NA NA NA
9.0 6.4| .0 .0 7.5J NA NA NA
8.0 9.0 8.5| .5 7.6 7.1| NA NA NA
NA
NA
NA
NA
NA NA | NA NA NA I NA NA NA
NA NA | NA NA NA | NA NA NA
NA NA j NA NA NA | NA NA NA
NA NA j NA NA NA j NA NA NA
.5 .8 .6| .2 .3 9.31 NA NA NA
.S .6 .S| .2 .S 9.4| NA NA NA
.5 .5 .5| .4 .6 9.5| NA *A n.
.5 .5 .0| .5 .7 y.»| KM i» ,—
.0 .0 .0| .8 .7 9.3| NA NA NA
.2 .3 .3| NA NA NA j .0 .0 .0| .2 .3 9.3| NA NA NA
.2 .3 .3| NA NA NA
.0 .0 .U| ...
.2 .3 .3| NA NA NA .0 .0 ,U| .* .» »..., i.~ *- ,.„
.3 .4 .4| NA NA NA .0 .0 .0| .3 .4 9.4| NA NA NA
.3 .4 .4| NA NA NA .0 .0 .0| .3 .4 9.4| NA NA NA

I I

TIME


Start Stop
950 1010
1010 1030
1030 1050
1050 1110
1110 1130
1130 1t60
1150 1210
1210 1230
1230 1250
1250 1310
1310 1330
1330 1350
1350 1410
1410 1430
1430 1450
1450 1510
1510 1530
1630 1SSO
1S50 1610
1110 1630
1630 I860
1660 1710
1710 1730
1730 17SO
1760 1610
1610 1630
1630 1680
I860 1900
KILN EXIT
Oxygen
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA M NA
NA HA NA
NA M NA
Carbon Dioxide
Concentration
(\ Dry M Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
MA NA NA
NA MA NA
NA NA MA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(ft Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
MA NA NA
NA NA NA
MA NA NA
MA MA MA
NA NA NA
NA NA NA
NA NA MA
NA NA NA
NA NA NA
NA MA MA
NA MA NA
0.0 It.* 8.1| 6.5 6.5 6.0J NA NA NA
11.0 «.» 11.61 S.6 6.4 5.0) NA NA NA
11.3 12.3 11.8) 6.6 6.3 6.0J NA NA NA
11.} 12.3 11.8| (.7 6.3 6.0| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA HA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
MA NA NA
NA NA NA
NA NA NA
NA NA MA
NA NA NA
NA NA NA
NA MA MA
NA MA NA
NA NA NA
NA NA NA
NA NA MA
NA NA NA
NA NA NA
NA NA MA
STACK
- - _
Oxygen
Concentration
(ft Dry •• seas' d)
Min Max Mean
NA NA NA
NA NA MA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA MA
NA MA NA
MA NA MA
NA NA NA
NA NA MA
NA NA NA
NA MA NA
Carbon 01 ox id*
Concentration
(ft Dry as Mas'd)
Min Max Mean
MA NA NA
NA NA NA
MA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA MA
NA NA NA
NA NA NA
NA NA NA
MA MA NA
Carbon Monoxide
Concentration
(ft Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA MA NA
NA MA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA MA NA
NA MA NA
NA MA NA
NA NA NA
9.5 10.0 9.8| 6.5 T.O 6.6| NA NA NA
t.S 6.8 9.6| 6.T 7.0 6.9| NA NA NA
9.6 9.8 9.«| 6.6 7.3 7.0) NA NA NA
9.6 9.6 t.8| 7.1 7.S 7.3) NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
MA NA NA
NA NA NA
NA NA NA
NA MA NA
NA NA NA NA NA NA
MA NA NA NA NA NA
NA NA NA NA NA NA
NA MA NA MA NA NA
NA NA NA NA NA NA
NA NA NA NA NA NA
NA NA MA NA NA NA
NA MA MA NA NA NA
NA NA NA NA NA NA
NA NA NA NA NA NA
NA NA MA | NA NA NA
NA - Data not taken
-------
                                             On Concentration on August  4,  1986

TINE



Start Stop
910 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
1500 1S20
1520 1540
1540 1600
1600 1620
1620 1640
1640 1700
• MMfk If 911
17QO 1720
1720 1740

AFTERBURNER EXIT
Oxygen | Carbon Dioxide Carbon Monoxide
Concentration j Concentration Concentration
(k Dry as Mas'd) |(k Dry as Mas'd) |(k Dry a* Mas'd)
1
Min Nax Mean) Min
.
Max Nean| Hin Hex Hean
NA NA NA | 0.0 0.0 0.0| NA NA NA
6.3 20. a 14.5| 0.0 .3 3.2| NA NA NA
8.0 21.0 14.5| 0.0 .7 4.9) NA NA NA
12.3 21.0 16.6| 0.0 .1
4.S 11. S 8.0| .2 1 .0
8.0 15.8 11.9| .4 .5
6.8 14.0 10.4| .1
.9
S.O 7. .3| .7 10.0
4.5 S. .0| 1 .0 10.0 ^
3.5 6. .9| .7 10.0
6.0 7. .3| .0 10.0
3.0 7. .3| .
NA' NA NA |
NA NA NA | NA
NA NA NA j NA
3.5 10.0 .8| 7.
3.8 6.8 .3|
4.0 6.5 .3|
4.0 T.O .it
5.0 7.3 .1|
6.0 7.3 .1|
4.0 7.3 5.6|
NA NA NA | NA
NA NA NA | NA
MA MA MA 1 MA
NA NA NA ( NA
NA NA NA | NA
1
10.0
to.o
NA
NA
10.0
10.0
10.0
10.0
10.0
10.0
10.0
.1) NA NA NA
.6| NA NA NA
.0| NA NA NA
.0| NA NA NA
.4) NA NA NA
.0| NA NA NA
.9) NA NA NA
.5| NA NA NA
.5| NA NA NA
.9| NA NA NA
A NA NA NA
U | NA NA NA
.8| NA NA NA
.7| NA NA NA
.81 NA NA NA
.7| NA NA NA
.7| NA NA NA
.8| NA NA NA
.8 NA NA NA
NA NA NA NA NA
NA NA NA NA NA
MIA MA MA MA MA
NA NA JVA NA NA
NA NA NA NA NA

CARBON BED INLET
Oxygen
Concentration
(\ Dry as Mas'd)

Carbon Dioxide
Concentration
Carbon Monoxide
Concentration
(k Dry as Mas'd)j(k Dry as Mas'd)


N1n Max Hean | Mln Max Meanj Min Max Mean
NA NA NA
6.6 . 8.1
NA HA NA
S.5 11.0 8.3) E.2 . 7.3| NA NA NA
6.6 8.5 7.6| 6.0 . 7.3| NA NA NA
7.0 9.8 8.4| (.3 . .2| NA NA NA
6.0 15.0 11.5) 2.4 . .1
12.3 6.5 8.3
10.3 13.5 1t.9| 3.7 . .3| NA NA NA
8.5 11.5 10.0| 6.2 . .3| NA NA NA
7.5 9.3 .4| 6.6 . .2| NA NA NA
7.3 7.5 .4| 7.6 . .9| NA NA NA
6.5 9.0 .8| 7.2 . .0| NA NA NA
7.0 9.3 .11 (.5 .1 7.3| NA NA NA
6.3 6.6 .8| 6.9 .9 7.9| NA NA NA
7.5 9.0 .3| 6.5 .3 7.4| NA NA NA
7.0 9.0 .0) 6.8 .5 7.7| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
7.5 .3 7.9| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
7.0 9.0 6.0| 6.8 6.7 7.8| NA NA NA
7.3 8.0 7.6| 7.1 8.7 7.9| NA NA NA
7.8 8.3 8.0| 7.1 6.3 7.7| NA NA NA




TIME


Start Stop
910 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
1500 1620
1620 1640
1540 1600
1600 1620
1620 1640
tjEjn iTfln
I0*V 1 7UU
1700 1720
1720 1740
KILN EXIT
_.__.__ . .
Oxygen
Concentration
(* Dry aa Mas'd)
Hin Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
3.0 9.8 6.4
6.3 10.8 8.6
6.5 11.3 6.9
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(k Dry as Mas'd)
_
Hin Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(k Dry as Mas'd)
M1n Hax Hean
NA NA NA
NA NA NA
NA HA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA HA
NA NA NA
NA NA NA
NA NA NA
7.6 10.0 8.8J NA NA NA
6.9 10.0 6.5) NA NA NA
6.4 10.0 8.2| NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
4.5 9.0 6.6| 6.5 10.0 9.3| NA NA NA
6.0 10.8 9.4| 7.4 10.0 8.7
6.5 10.8 8.6| 7.6 10.0 6.6
1-
| IM nH I«M
NA NA NA
NA NA NA
I
STACK
Oxygen
Concentration
(* Dry as Mas'd)
H1n Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(k Dry as Mas'd)
Mln Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(k Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
.3 8.7 7.5| NA NA NA
.5 10.0 9.3| .2 7.6 6.9| NA NA NA
.3 9.8 9.0) .3 7.8 T.lj NA NA NA
.8 9.8 9.3) .5 7.5 7.0| NA NA NA
.8 10.0 9.4| .0 7.6 6.6| NA NA NA
.3 9.3 8.6| .5 7.8 7.2) NA NA NA
NA NA NA
fcfA MA UA
NA NA NA
NA NA NA
NA NA NA NA NA NA
MftIA ftIA ftfA UA NA
MA HA HA HA n*
| NA NA NA NA NA NA
NANANAJNANANANANAN/


NA • Data not taken
-------
                                              Gas  Concentration on August S,  1986

TIME



Start Stop
920 9*0
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
1SOO 150S
1505 1530

AFTERBURNER EXIT
Oxygen | Carbon Dioxide | Carbon Monoxide
Concentration j Concentration | Concentration
(* Dry as B*as'd)j(t Dry as Beai'djiu Dry as swas'd)
1 1
Min Hax Me«n| Hin Max Mean| Min Max Mean
4.0 14.5 9.3|
7.3 10.0 B.6|














.5 13.5 9.0|
.5 9.0 7.8|
.0 8.5 T.3|
.5 a. a 7.6)
A NA NA |
A NA NA |
.a is.o io.9|
.a 7.8 6.8|
.8 .0 6.9|
.0 .5 4.8|
.5 .0 6.3|
.3 .0 5.1|
.5 .a S.6|
.S .3 7.4|
NA HA NA |
NA NA NA |
.6 8. 7 6.7| NA NA NA
.4 9.5 7.0| NA HA NA
.1 10.0 7.6J NA NA NA
.9 10.0
.0 10.0
.2 10.0
.1 10.0
«A NA
.4 10.0
.4 10.0
.3 10.0
.1 10.0
.1 10.0
.3 10.0
.a 10.0
.3 10.0
.2 10.0
.3 10.0
.0) NA NA NA
,5| NA NA NA
. 1| NA NA NA
,6| NA NA NA
A | NA NA NA
.2| NA NA NA
.7| NA NA NA
.7| NA NA NA
.6| NA NA NA
.6| NA NA NA
.7| NA NA NA
.4| NA NA NA
.7| NA NA NA
.6| NA NA NA
.7| NA NA NA
NA NA NA | NA NA NA | NA NA NA
1 I
CARSON BED INLET
Oxygen
Concentration
Carbon Dioxide | Carbon Monoxide
Concentration I Concentration
(* Dry as Ma*'d)|(* Dry as Mas'd>j(% Dry as acas'd)

Min Hax Mean
.8 14.5 11.6
1
Min Max Mean| Min Max M*«n
3.6 7.0 6.31 NA NA NA
.3 13.0 11.1| 4.4 C.a S.6| NA NA NA
.5 13.5 10.0J 4.2 8.3 6.3J NA NA NA
.s 10.0 a.ai a.o 9.9 T.OI NA NA NA
.0 9.5 8.8| 6.4 7.7 7.1) NA NA NA
.0 9.5 8.8J 6.3 7.7 7.0J NA NA NA
NA NA NA
NA NA NA
HA NA NA
NA NA NA
NA NA NA
6.3 7.1 6.7f NA NA NA
NA NA NA j NA NA NA
NA NA NA I NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
7.5 18.3 12.9| 7.3 .3 7.8) NA NA NA
7.0 8.0 7. SI 7.2 .S 7.9| NA NA NA
7.0 7.8 7.J! 7.4 .5 8.0| NA NA NA
6.8 7.8 7.3, 7.4 .3 7.9| NA NA NA
6.5 8.0 7.3| 7.3 .5 7.9| NA NA NA
6.5 7.5 T.0| 7.4 .6 8.0| NA NA NA
NA NA NA
NA NA NA

7.4 .5 8. Of NA NA NA
7.2 7.6 7.4J NA NA NA
1
TIME
Start Step
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
1500 1505
1505 1530
KILN EXIT
Oxygen
Concentration
(* Dry as awas'd)
Min Max Mean
HA NA NA
HA NA NA
HA NA NA
HA NA NA
HA NA HA
HA HA NA
3.5 17.5 10.5
10.0 IS. a 12.9
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA HA
6.5 8.5 7.6
NA MA NA
Carbon Dioxide
Concentration
(X Dry as ewas'd)
Carbon Monoxide
Concentration
(X Dry as awas'd)
Hin Max Mean| Min Max Mean
NA NA NA
NA NA HA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
4.1 5.6 4.9
1.1 7.9 4.5
4.5 5.3 4.9
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
HA NA NA
S.I 7.1 6.1
(.0 a. 2 s.a
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA HA NA
NA NA NA
NA NA HA
HA HA HA
HA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
HA NA NA
NA NA NA
STACK
-
Oxygen
Concentration
(* Dry a* Mas'd)
Min Max Mean
NA NA NA
HA NA NA
HA NA NA
HA NA NA
HA NA NA
HA NA HA
.3 12.0 .8
.0 9.8 .4
.3 9.5 .9
Carbon Dioxide
Concentration
(X Dry as Mas'd)
Carbon Monoxide
Concentration
(X Dry as awas'd)
Min Max Mean) Min Hax Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
.0 8. 3 6.7
.2 7.0 6.S
.2 7.7 7.0
.5 10.0 .3| .0 7.5 6.8
HA NA NA .7 7.9 7.3
HA HA NA | NA NA NA
NA HA NA j NA NA NA
NA NA NA | NA NA NA
8.5 10.0 9.3) NA NA NA
8. 3 9.8 9.0J NA NA NA
a. a 10.0 9.3| NA NA NA
8. 8 10.0 9.4| HA NA HA
1
NA NA NA
NA NA NA
HA NA NA
NA NA NA
NA NA NA
NA NA • NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
HA - Data not taken
-------
                                             Oas  Concentration on August 7,  1986
TIME
Start Stop
•45 100S
1005 1025
1025 1046
1045 1105
1105 1125
1125 1145
1145 1206
1205 1225
1225 1245
1245 1305
1905 1325
1325 1345
1345 1405
1405 1425
AFTERBURNER EXIT
Oxygen
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA HA NA
NA NA MA
NA NA NA
MA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA MA
7.8 10.0 8.9
1.8 8.8 6.3
6.0 7.0 6.0
Carbon Dioxide
Concentration
(* Dry as Mas'd)
M1n Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
7.4 9.2 8.3
8.2 10.0 9.1
9.3 10.0 9.7
Carbon Monoxide
Concentration
(t Dry as Mas'd)
Hin Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
CARBON BED INLET
Oxygen
Concentration
(t Dry as Mas'd)
Mln Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA MA
NA NA NA
NA NA NA
NA NA MA
NA HA NA
Carbon Dioxide
Concentration
(* Dry as Mas'd)
Hin Max Mean
6.5 7.4 7.0
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA M NA
NA NA NA
NA NA NA

8.0 9.3 8.6| 6.4 7.4 6.9
1
Carbon Monoxide
Concentration
(* Dry as Mis'd)
Mln Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
1
1 TIME
Start Stop
945 1005
1005 1025
1025 1045
1045 1105
1105 1125
1125 1145
1145 1205
1205 1225
1225 1245
1245 1305
1305 1325
1325 1345
1345 1405
1405 1425
KILN EXIT
Oxygen | Carbon Dioxide | Carbon Monoxide
Concentration j Concentration | Concentration
(1 Dry as Mas'd) |(* Dry as Mas'd) | (* Dry as Mas'd)
1 1
Min Max Mean) M1n Max Mean| Min Max Mean
1

.0 9.3 7.1| 7.0 9.6 8.3| NA NA NA
.5 9.8 8. 6 1 8.8 10.0 8.4| NA NA NA
.0 10.3 9.1| 7.2 10*0 8.6) NA NA NA
.5 10.0 B.8| 7.1 8.6 7.9| NA NA NA
.3 9.5 7.9| 7.0 9.1 8.1| NA NA NA
.8 12.0 10. 9| 6.9 10.0 8.5| NA NA NA
.3 11.3 10.3) 6.1 8.1 7.1| NA NA NA
.5 11.5 10.5] 6.6 6.3 7.5| NA NA NA
«A NA NA | 6.3 7.9 7.1| NA NA NA
HA NA NA | 6.8 8.S 7.6| NA NA NA
«A NA NA | NA NA NA | NA NA NA
1 1
STACK
Oxygen | Carbon Dioxide | caroon nonoxiae
Concentration | concentration | borivvnti BUOII
(* Dry as Mas'd) |(* Dry as Mas'd) j(* Dry as Mas'd)
1 1
M
•
1
n Max Mean) Min Max Mean| H-in Max Mean
F.8 10.8
.6 9.5
.0 14.3 1
.0 9.5
.6 9.5
.5 9.3
.0 11.0
.5 1C. 3
.8 10.0
.8 10.0
.5 9.5
MA NA 1
MA NA 1
*A NA
•31
• 0|
.61
.8|
•1|
-•I
•*l
•«l
•'1
•«l
.0!
«A |
«A |
«A j 1
1
•
«A
7.
7.
7.
7.
7.
7.
7.
7.
7.
7.
7.
7.
1 7.
NA
7.1| NA NA NA
6.5| NA NA NA
7.0| NA NA NA
6.9J NA NA NA
7.0 j NA NA NA
6.8J NA NA NA
6.9J NA NA NA
6.3| NA NA NA
6.6| NA NA NA
2 6.7| NA NA NA
9 6.6J NA NA NA
0 6.6| NA NA NA
) 6.7J NA NA NA
NA j NA NA NA
1
NA - Data not taken
-------
                                             Ois Coneentrltlon  on  August  12,  1966
TINE
Start Stop
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
AFTERBURNER EXIT
Oxygen | Carbon Dioxide Carbon Monoxide
Concentration j Concentration j Concentration
(* Dry as Mas'd) |(« Dry as Mas'd) |(* Dry as Mas'd)
- - 1
Hin Max Mean
Hin Max Mean) Min Max Mean
3.5 9.S 6.5| 6.2 9.2 T.T
6.0 6.6 6.9| T.O 9.9 6.S
6.3 9.5 7.9| 6.9 10.0 6.5
NA NA NA 7.0 9.T 6.4
NA NA NA NA NA NA
NA NA NA NA NA NA
NA NA NA NA NA NA
NA NA NA NA NA NA
7.0 11.0 .0| 7.4 9.8 .6
.5 10.3 .4| T.1 10.0 .6
.S 10.6 .6| 6.6 10.0 .4
.5 10. S .S| 6.9 tO.O .5
.0 10.5 .6| 7.0 10.0 .5
.S 10.3 .4| 7.1 10.0 .6
.3 10.5 .4| 7.0 10.0 .5
I
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
CARBON BED INLET
Oxygen
Concentration
(« Dry as Mas'd)
Min Max Mean
Carbon Dioxide | Carbon Monoxide
Concentration j Concentration
(* Dry as Mas'd) |(* Dry as Mas'd)
I
Min Max Heanj Min Max Mean
10.0 11.6 10. 9| .6 6.3 S.1| NA NA NA
9.3 11.0 10.1| .0 7.1 6.1| NA NA NA
9.5 11.0 10. 3| .5 7.3 6.4| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
.6 10.6 9.6
.0 11.0 10.0
.0 11.0 10.0
.0 11.0 10.0
.3 10.6 9.5
.0 9.5 6.6
.6 10.3 9.5
.5 7.2 6.9| "A NA NA
NA NA NA I NA NA NA
NA NA NA j NA NA NA
NA NA NA | NA NA NA
NA NA NA 1 NA NA NA
6.3 6.5 .4| NA NA NA
5.5 7.6 .7| NA NA NA
5.4 7.5 .5| NA NA NA
6.5 7.5 .S| NA NA NA
6.5 6.1 .8 | NA NA NA
5.6 7.6 .6| NA NA NA
6.2 6.2 7.2J NA NA NA
I
I

TIME


Start Stop
920 940
•40 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440

KILN EXIT
Oxygen
Concentration
(\ Dry as Mas'd)
Carbon Dioxide
Concentration
(* Dry as Mas'd)
Carbon Monoxide
Concentration
(* Dry as Mas'd)
Min Max Mean| Min Max Mean| Min Max Mean
NA NA NA
NA NA NA
NA NA NA | NA NA NA
NA NA NA
NA NA NA
NA NA NA | NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
6.3 14.8 10.5| .3 .6 4.5| NA NA NA
12.3 14.8 13.5| .6 .1 4.9| NA NA NA
12.0 15.0 13.5| .4 .5 6.0) NA NA NA
13.0 15.3 14. 1| .5 .0 4.8J NA NA NA
13.0 16.3 14.1] .4 .S 4.6| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA

.7 .2 S.0| NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA

NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA


STACK
Oxygen | Carbon Dioxide
Concentration | Concentration
(ft Dry as Mas'd) j(% Dry as Mas'd)
Carbon Monoxide
Concentration
(\ Dry as Mas'd)
Min Max Mean) Min Max Mean| Min Max Mean
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA j NA NA NA
NA NA NA | 6.2 7.0 .6
NA NA NA
NA NA NA
NA NA NA
NA NA NA
9.5 11.5 10.5) 5.4 7.2 -3| NA NA NA
9.3 11.3 10. 3| 6.5 7.4 .5) NA NA NA
9.8 11. S 10.8| 5.5 7.0 .3| NA NA NA
9.5 12.3 10. 9| 4.3 7.3 .8| NA NA NA
10.0 11.8 10.9) 4.9 6.9 .9| NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA | NA NA NA
NA NA NA j NA NA NA
NA NA NA | NA NA NA
1
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA

NA - Data not taken
-------
                                            Gis Concentration on August 13,  19S6
TIME
Start Stop
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
AFTERBURNER EXIT
Oxygtn | Carbon Dioxide I Carbon Nonoxide
Concentration j Concentration j Concentration
(* Dry es Mas'd) | (ft Dry as Mas'd) |(* Dry as Mas'd)
1 1
Min Max Mean) Min Max Mean) Nin Max Mean

1.0 7.3
J.5 7.8
.5 .0
.5 .3
.0 .0
.0 .0
.0 .3
.0 .3
.3 10.0
.0 9.9
.5 19.8 1
.0 9.5
.0 10.0
.5 10.0
.0 9.5
.8 10.0 '
.5 10.3 1
• 11
•1|
•31
••1
.0)
.5|
• 1|
• •I
•1|
.»!
.11
• •I
•0|
.31
r.8|
1.9\
l.4|
1
.!
*.
1.
r.
7.
i.i
r.
5 10.0
I 10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
) 10.0
1 10.0
.31 HA MA NA
.21 NA NA MA
.3| NA NA NA
.4) NA NA NA
.2| HA NA NA
.3| NA NA NA
.21 NA NA NA
.9| NA NA NA
.0| NA NA NA
,0| NA NA NA
.2| NA NA NA
.1) NA NA NA
,8| NA NA NA
.8| NA NA NA
.9| NA NA NA
.0| NA NA NA
.7| NA NA NA
1
CARBON BED INLET
Oxygen | Carbon Dioxide | Carbon Honxide
Concentration j Concentration j Concentration
(t Dry as Mas'd) j(* Dry as Mas'd) j(t Dry as Mas'd)
1 1
Min Max Meenj Min Max Mean) Min Max Mem

.(
•
•
•
•
.
.1
».

10. .0) i
10. .6| !
10. .5|
10. .9|
9. .5|
9. .6|
10. .9|

10.5 10.0!
10.0 9.3|
9 11.5 10. 3|
) 10.5 9.8|
) 11.3 10.3J
1
t.S .0 .3) NA NA NA
1.4 .4 .4| NA NA NA
.6 .1 .4| NA NA NA
.6 .3 .0| NA NA NA
.5 .3 .9| NA NA NA
.0 .8 .9| NA NA NA
.1 7.1 .3| NA NA NA

.3 7.2 6.3| NA NA NA
.2 7.0 6.1| NA NA NA
.3 7.0 6.2| NA NA NA
.1 6.8 6.0) "A NA NA
.7 6.7 S.7| NA NA NA
1
TIME
Start Stop
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1600
KILN EXIT
Oxygen
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(t Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
1
STACK |
1
Oxygen
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide Carbon Monxtdc |
Concentration j Concentration |
(* Dry as Mas'd) | (X Dry as Mas'd)!
1 1
Mm Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Min Max Hem1
NA NA NA |
NA NA NA |
NA NA NA |
NA NA NA |
NA NA NA |
NA NA NA |
5.0 8.3 6.7)
6.2 7.0 6.6|
3.0 7.7 7.0|
6.5 7.6 7.1|
6.0 7.5 6.81
NA NA NA |
NA NA NA |
NA NA NA |
NA NA NA |
NA NA NA |
1
NA - Data not taken
-------
                                            Gas Concentration  on  August  14,  1986
1
1
TIHE



Stirt Stop
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1SOO


AFTERBURNER EXIT
Oxyg«n | Carbon Dioxide I Carbon Monoxide
Conctntrltlon j Concentration j Concentration
(* Dry as •«as1d)|(* Dry as Mas'd)|(k Dry as Mas'd)
1 1
Min Max Mean| Hin Max Mtan| Min Max Htan
4.5 6.0 S.3|
4.0 7. 5 5.8|
5.0 8.0 6.5|
6.0 0.0 7.0J
4.8 7.S .1|
6.0 8.0 .S|
5.5 7.5 .5|
6.0 9.0 .S|
6.5 8.8 .6|
6.0 8.5 .3|
5.8 8.8 .3|
5.5 8.3 .91
7.0 8.0 7.9|
NA NA NA |
.1 10.0
.0 10.0
.0 10.0
.0 10.0
10.0
10.0
10.0
10.0
10.0
10.0
10.0
.2 10.0
.7 10.0
.1 10.0
.6| NA NA NA
.5| NA NA NA
.S| NA NA NA
.51 NA NA NA
.9| NA NA NA
.7| NA NA NA
.6| NA NA NA
. 3| NA NA NA
.4) NA NA NA
.5 j NA NA NA
,7| NA NA NA
.6| NA NA NA
,4| NA NA NA
.6| NA NA NA
NA NA NA j NA NA NA | NA NA NA
NA NA NAJKA NA MAJNA NA NA
1 1

CARBON BED INLET
Oxygen | Carbon Dioxide | Carbon Monoxide
Concentration j Concentration j Concentration
(* Dry as Mas'd) I (t Dry as Mas'd) |(* Dry as ntas'd)
1 1
Min Max Mean) Min Max Mean) Min Max Mean
8.0 10.0
7.8
8.3
7.8
7.3
7.6
7.8
6.3
7.6
7.8
8.3
.3
.3
.3
.8
.6
.3
.3
.0
.3
.8
• 0|
• 5|
• •I
•3|
•0|
.11
•S|
• »l
•3|
.51
•0|
NA NA NA |
.2 .1 6.7| NA NA NA
.6 .4 7.5J NA NA NA
.6 .4 7.5| NA NA NA
.7 .9 7.3J NA NA NA
.0 .5 7.8J NA NA NA
.2 .6 7.9J NA NA NA
.5 7.9 7.2) NA NA NA
.7 7.9 7.3| NA NA NA
.6 8.5 7.6| NA NA NA
.0 8.3 7.7) NA NA NA
.7 7.7 7.2| NA NA NA
.7 7.4 7.1) NA NA NA
NA NA NA | NA NA NA | NA NA NA
NA NA NA j NA NA NA | NA NA NA
1 1

TIME



Start Stop
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
KILN EXIT
Oxygen
Concentration
(* Dry as Mas'd)

Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Carbon Monoxidt
Concentration f Concentration
(t Dry as Mas'd) |(* Dry as teas'd)
1
Min Max Mean| Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA j NA NA NA
NA NA NA | NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
MA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
4.0 12.0 8.0| 5.4 7.4 6.4| NA NA NA
9.5 13.0 11.31 6.7 6.5 7.6| NA NA NA
6.6 11.6 10. 1| 7.1 9.S 6.3| NA NA NA
1 1
STACK
Oxygen | Carbon Dioxidt
Concentration
Concentration
(% Dry a* Mas'd) |(* Dry as Mas'd)


Min mx Meant Min Max M««n
NA NA NA
NA MA NA
NA DA NA
NA MA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA «A NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA HA
NA NA NA
Carbon Monoxide
Concentration
(t Dry as Mas'd)

Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
8.3 W.O 9.1| 6.7 7.9 7.3| NA NA NA
6.5 S.S 9.0) 6.1 7.4 6.8| NA NA NA

1
NA - Data not taken
-------
                                            CM Concentration on August 28,  1986
TIME
Start Stop
900 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1445
AFTERBURNER EXIT
Oxygen | Carbon Dioxide | Carbon Monoxide
Concentration j Concentration j Concentration
(* Dry a* Mas'd) j(* Dry as Mas'd) j(t Dry as Mes'd)
1 1
Min
10.1

TIHE
Start Stop
900 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1t20 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1445
Max Mean| Min Max Mean) M1n Max Mean
12.0 10.9| 7.2 10.0
11. B 10. 5| .3 10.0
11.0 10.4| .9 10.0
11.3 10.4| .1 10.0
10. 10.3| .• 10.0
10. 10. OJ .7 9.9
10. 10.0| .7 10.0
11. 10.3| .3 10.0
11. 10.3| .1 10.0
10. 9.9| .1 10.0
10. 9.9J .5 10.0
10. 10.2| .7 10.0
10.3 9.8| .5 9.8
10.0 9.4| .3 10.0
10.8 9.8 .4 10.0
11.0 10. 3| .3 10.0
) 10.8 10.4| .9 10.0
1

••1
.1|
•2|
•1|
•*l
•3|
•
-------
                                            On Concentration on September 3, 1986

TIKE


Start Stop
900 920
920 940
9«0 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1940 1400
1400 1420
1420 1440
1440 1500
1500 1520

AFTERBURNER EXIT
Oxygen Carbon Dioxide | Carbon Monoxide
Concentration Concentration j Concentration
(t Dry as Mas'd) (« Dry as Mas'd) |(* Dry as awes'd)
1
Min Max Mean Min Max Mean) Mm Max M«an
4. a T.a
4.5 6.3
4.5 6.0
4.3 6.5
5.0 6. a
5.3 7.3
S.3 7.3
4.8 7.3
5.3 7.3
5.0 7.0
4.8 6.
5.0 6.
5.3 7.
4.3 7.
.3|
•4|
,3|
•4|
• 9|
.31
•3|
.0|
•31
.0|
.6|
• 91
.3|
• 0|
6.8 8. 7.0|
6.0 8. 7.1J
6.3 6. 9.3|
6.0 6.5 7.3|
.4 10.0
.9 10.0
.1 10.0
.1 10.0
.1 10.0
.9 10.0
.0 10.0
.0 10.0
.9 10.0
.0 10.0
.1 10.0
.9 10.0
.9 10.0
.7 10.0
.7 10.0
.8 10.0
.0 10.0
.1 10.0
.7| NA NA NA
. 1| NA NA NA
.2| NA NA NA
.1| NA NA NA
.4| NA NA NA
.3| NA NA NA
.4| NA NA NA
.2| NA NA NA
.1| NA NA NA
.1) NA NA NA
.3| NA NA NA
.4| NA NA NA
.2| NA NA NA
.1| NA NA NA
,Z| NA NA NA
.2| NA NA NA
.2| NA NA NA
.5 j NA NA NA
6.3 9.0 7.1| NA NA NA | NA NA NA
1 1
CARBON BED INLET
Oxygen
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA . NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(t Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(t Dry as Bets' d)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
10.0 .4| .0 6.7 .4| NA NA NA
10.0 .4| .1 7.4 .B| NA NA NA
10.0 .4) .1 7.4 .B| NA NA NA
10.0 .5) .2 7.3 .8| NA NA NA
10.8 .8| .1 6.3 .2| NA NA NA
7. 10.8 .3| NA NA NA
1
NA NA NA

1

TIME


Start Stop
900 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
1440 1500
1500 1620
1
KILN EXIT
Oxygen
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA HA NA
Carbon Dioxide
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA HA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA HA NA
NA NA HA
NA NA HA
NA NA NA
NA HA NA
NA NA NA
NA NA NA
NA NA NA

Carbon Monoxide
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
HA NA NA
HA NA NA
NA NA NA
HA HA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
HA NA HA
HA NA HA
HA HA NA
NA NA NA
NA NA NA
NA HA NA

Oxygen
Concentration
(* Dry as Mas'd)



STACK
Carbon
Dioxide
Concentration
(* Dry as Mas'd)
Min Max Me*n| Min Max Mean














.5 12.3 10.9
.
.
.
.
.
.
.
.
.
.
.
.
13.
10.
10.
10.
10.
10.
10.
10.
10.
10.
10.
10.
.0 10.
11.6


10.0)
10. 0|
10.0|
10.11
10

•••1
10.11
9.9

10.01
9.9|
9.4)
9.9|
NA NA HA
HA NA NA
NA NA NA
NA NA NA
NA HA NA
.7
.3
,1
•
•
.0
.0
.0
.T
.0
Carbon Monoxide
Concentration
(* Dry as Mas'd)
Min Max Mean
.6 5.8! "A NA NA
.9 S.6J NA NA NA
.0
.1
.0
.9
.9
.2
.9
.0
.0 7.0
.1 7.0
.0 7.0
.8 7.7
.6 1 NA NA NA
.6| NA NA NA
.6
NA NA NA
.5) NA NA NA
.5| NA NA NA
.6| NA NA NA
.8| NA NA NA
.S| NA NA NA
.S| NA NA NA
.6| NA NA NA
.5) NA NA NA
.6
HA NA NA
NA NA NA
NA NA NA
NA 1
HA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA - Data not taken
-------
                                            Gas Concentration on September t, 1986

TIME



Start Stop
900 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
AFTERBURNER EXIT
Oxygen | Carbon Dioxide I Carbon Monoxide
Concentration j Concentration j Concentration
(* Dry as •«ai'd)|(* Dry as s*as'd)|(t Dry as aeas'd)
1 1
Hin Max Nean| Hin Max Mean| Min Hex Mean
4.5 5.3 4.9| 7.4 10.0 9.7| NA NA NA
5.3 .5 5.9| 9.3 10.0 10. 0| NA NA NA
5.3 .3 S.8| 10.0 10.0 10. Of NA NA NA












.5 .3 5.9|
.8 .3
.8 .5
.5 .8
.0 7.3
.3 7.3
.3 7.3
.5 7.3
.3 7.0
.3 7.0
.0 6.8
.0 6.5
5.8 6.5
S.8 6.5
•0|
.11
•1|
•«l
.8|
••1
•«l
• 6|
.21
• 4|
• 31
• 11
•1|
1
10.0 10.0| NA NA NA
10.0 10.0| NA NA NA
10.0 10.0J NA NA NA
10.0 10.0| NA NA NA
10.0 .8| NA NA NA
.7 10.0 .9| NA NA NA
.6 10.0 .8| NA NA NA
.7 10.0 .9| NA NA NA
.7 10.0 .9| NA NA NA
.7 10.0 .9| NA NA NA
.9 10.0 10.0| NA NA NA
.9 10.0 10.0| NA NA NA
.4 10.0 10.0| NA NA NA
.4 10.0 10.0| NA NA NA
1
CARBON BED INLET
Oxygen
Concentration
(t Dry as aeas'd)

Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(X Dry as >eas'd)

Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA MA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(I Dry as neas'd)

Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
8.S 9.0 8.8| 6.7 7.3 7.0| NA NA NA
8.8 9.0 8.9| 7.1 7.3 7.2| NA NA NA
8.5 9.0 8.8| 1-0 7.3 7.2| NA NA NA
1 1
TIME
Start Stop
900 920
920 940
940 1000
1000 1020
1020 1040
1040 1100
1100 1120
1120 1140
1140 1200
1200 1220
1220 1240
1240 1300
1300 1320
1320 1340
1340 1400
1400 1420
1420 1440
KILN EXIT
Oxygen
Concentration
(t Dry as twas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Dioxide
Concentration
(t Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA HA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
Carbon Monoxide
Concentration
(* Dry as Mas'd)
Min Max Mean
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
NA NA NA
1
STACK |
1
Oxygen | Carbon Dioxide I Carbon Monoxide !
Concentration j Concentration | Concentration 1
(t Dry as •ees'dJK* Dry as swas'dHt* Dry as neas'd);
1 1 I
Min Max Mean) Min Max Mean) Min Max Mean;
1
1
.5
.0
.3
.3
.0
.0
.3 1
.3
.8
.5
.3
.8
«A 1
«A 1
«A 1
.8
.5
.5
.4
.5
.5
.3
.8
.8
.5
.4
.3
«A
«A
«A
.1!
• 31
.41
•4|
.3|
•3|
.81
•5|
•31
• *l
• 5|
.0|
KA j
HA |
KA |
1
.5 7.5 7.0| NA NA NA ;
7.2 7.1 j NA NA NA |
7.1 7.0| NA NA NA |
7.1 7.0| NA NA NA |
7.1 7.0| NA NA NA |
7.3 7.1J NA NA NA |
.7 7.2 7.0| NA NA NA |
.1 7.1 .6| NA NA ' NA |
.7 7.1 .9| NA NA NA j
.6 7.0 .8| NA NA NA |
.7 6.9 .81 NA NA NA ;
.7 7.0 .9| NA NA NA |
KA NA NA | NA NA NA |
HA NA NA | NA NA NA |
WA NA NA | NA NA NA f
1 !
NA - Data not taken
-------
                E-DUCT 02  7-21-86
              KILN  O2  7-21-86
    so
    I*

    17
    It
    It
•   I*
X   M
U   IX
ft
O   II
    to
20
It
I* •
17 -
ia •
it •
to
 t -
 t -
 7 •
 t -
                                              ItM
                      nut 1*00 cLcex-nwc
                       •  at COHC B
                      J«oo cv.ocx-nuc
                      oa COHC m
                 STACK O2  7-21-85
        AFTERBURNER O2  7-21-66
    xo
    It -

    17
    It -
    I* •

    13
    IX
    It
    to •
     t •

     7
     t
XO
It •
II -
17
It
It -
14
13
IX
II
10
 t •

 7
 t
      IIM
                                        IMS
                                                                             I15t
                                                                                            IStt
                       TMK X*OO O.OCH-HMC
                        O OX COMC S
                   TIWC X*00 CIOCK-TIMC
                    •  OX COX B
-------
           E-DUCT C02  7-21-86
            KILN  C02  7-21-85
It


to


 t
 X


 I .
It


to •


 t -
                                                5£
                                                8
 J.


 2 •


 I
          I ISO
                                                      II2O
                                                                    1310
                 YIWC J»oo ctocr-tiMt
                 a  eea COHC »
                 tiwt Jjoo cioeit-nwc
                 o  eoa COMC B
II


ie
           STACK C02 7-21-86
       AFTERBURNER  CO2  7-21-86
                IJIO
                                                      IO«0
                                                               n»e
                 TIMt I
-------
            E-DUCT 02  7-28-86
                                                                   KILN  O2 7-28-85
 10-
 It •
 I* •
 17 .
 I* .
 IJ -
 IX •
 II -
 to .
                                                     SO
                                                     It
                                                     I*
                                                     17
                                                     IJ
                                                     12 •
                                                     II
                                                     IO
                                                      t •
  10X0
                                             1*40
                  TlUt 1*00 CIOCK-T1UC
                  e  ox CONC •
                                                                       tint 2*00 nocK-nuc
                                                                        •  02 cox •
            STACK O2 7-28-86
                                                             AFTERBURNER 02 7-28-86
20 •
It •
I* •
17 •
It -
!• •
II •
IO •
 t •
                                                     20
                                                     It
                                                     1*
                                                     17
                                                     14
                                                     It
                                                     12 •
                                                     II
                                                     10
                                                      t •
                                                       1020
                                                                  IJO
                 nut 2*00 o.ocK-nwt
                  •  02 COX •
                                                                             IMO
                                                                       Tluf 2«OO ClOC
                                                                        o  02 cox I
-------
           E-DUCT CO2 7-28-86
     KILN  C02  7-28-86
         1120
                M20
                       t*«0
                 TIUC 24OO CVOCK-TIUC
                  O  COX COMC •
          1IMC 2
-------
            E-DUCT 02  7-29-86
     KILN  O2  7-29-86
       10SO
              1130
                    1ISO
                          1990
                                       1710    I«IO
                                                                      14 JO
                                                                                      14M
                  T1UC J400 CIOCK-TIUC
                   o  02 CONC •
         TlUf 14OO CLOCX-TIUC
          O  02 COMC »
             STACK  O2  7-29-86
AFTERBURNER O2  7-29-86
It •
la •
17 •
i* •
it •
14 •
13 -
11 -
1 1
 1410
                                I4SO
                                               1S10
                                                        •so
                                                              toso
                                                                    115O
                                                                          issa
                                                                                 13M
                  TtMC 1400 ClOCK-TIMC
                   •  OX COMC •
          nut i4oo etocK-Tiuc
           a  oa CONC •
-------
           E-DUCT C02  7-29-86
10 •

 I -
 7 -
 4 •


 3


 2

 1
       1100
              1200
                    1300
                          1400
                                1*00
                                      1700
                   Tiyt 2*00 CLOCK-T1WC
                   O  COX COMC B
                                                        • -1
            KILN C02  7-29-S6
                                                                                        1500
                    ?400 ClOCK-TlMt
                    CO2 COMC •
             STACK C02 7-29-86
 11

 10 -

 t •
  1420
                                 ISOO
                                                  I

                                                1920
                   Tint 2400 CU5CK-TIUI
                   0  CO2 CONC B
      AFTERBURNER  C02 7-29-86
1000   1100    120O   1JOO
                                                                                               17ZO
                 TIUW 34OO CLOCK-Tlut
                 O   CO2 CONC B
-------
             E-DUCT 02 8-4-86
     KILN  O2  8-4-86
                                              1700
                                                                                                    1700
                  nuc 24oo CLOCK-
                    a  02 COMC m
        TIUC 24OO CIOCK-TIWC
         O  O2 CONC •
               STACK O2  8-4-86
AFTERBURNER  02  8-4-86
21
20
It

17
It
15

13
12
II
10
 3 -
 2 •
 1400
         1*10
                          1500
                   TIUC 2400 CIOCX-TIWC
                    e  02 CONC •
                                          114O
                                                              •20
                                                                      1020
                                                                              1120
                                                                                       1220
         TIUC 2400 CIOCK-TIUC
          O   O2 COMC •
-------
           E-DUCT  CO2  8-4-86
             KILN  CO2  8-4-86
                                                     II
                                                     10
                                                      t
                                                 u
                                                 8
                                                 u
* -
                                                      2 •
                                                      I -
                       1200
                              1100
                                      It ZO
                                                      I JOS
                                                              1110
                                                                     114O
                                                                             1*20
                                                                                    1»40
                                                                                            I TOO
                                                                                                   1720
                 TIUC J4OO ClOCK-TIUf
                 O  CO2 COMC •
                 TlUt 24OO CLOCK-TIWC
                 O   CO2 COMC •
            STACK  CO2  8-4-86
        AFTERBURNER CO2  8-4-86
1.
2 •
1 -
                                                  w
                                                  ••
                                                  8
 114*
       1*00
             I42O    I**O   I»OO    1*20
                 TIMC 2«00 CLOCK-TIMt
                 O  CO2 COMC E
                                                       »«0     IO4O     tt«O     11*0     1*20
                  TlUt 1*00 CLOCK-T1UC
                  O   CO2 CONC •
                                                                                               ISZO
-------
             E-DUCT  02  8-5-86
      KILN  O2 8-5-86
                                                         1120
                  TIUC 3*OO CIOCK-TIUC
                   O  O2 CONG B
         TIUC 2400 ciocK-Tiuc
          e  02 CONC m
              STACK 02  8-5-86
AFTERBURNER 02  8-5-86
2t
20 -
I*

17 -
1* -

14 -
IJ •
t2 -
IO
 t
 7 •

 9 -
 4 -
 J •
 2 •
 1120
                        120O
                  •nut 2400
                   O  O2 CONC •
                                    tuo
                                               12*0
                                                         92O
                                                                   1020
                                                                              I20O
                                                                                         tJOO
         •nut 2400 CLOCK--nut
          o  02 CONC m
-------
           E-DUCT C02 8-5-86
     KILN  CO2  8-5-86
                                                     11
                                                     to -
                                                     t -
                                                     • -
                                                     7 -
                                                     4 .

                                                     J

                                                     1
                                                     1 -
                    11X0
                 nut 2*00 CIOCK-TIUC
                  O  CO2 CONC •
                                                      1125
                                                                            1200
         TIME 2400 CV.OCK-TIUC
         O   CO2 CONC •
                                                                                       1509
            STACK CO2 8-5-86
AFTERBURNER CO2 8-5-86
11
10-
 t •
 3 -
 * -
 1 .
 0-
 1125
          114O
                   120O
                            1220
                                     124O
                                             1300
                 T1WC 2«00 CLOCK-T1MC
                  O   COJ CONC •
          TlUt 1*00 CLOCK-TIWC
          a  coz COMC •
-------
             E-DUCT 02 8-7-86
                    KILN  O2 8-7-86
21
20
1*
II
17
1*
It
14
13
12
11
1O
                         1349
                   •nut 1*00 CLOCK-TIVC
                    o  at COMC •
                                                1*05
                       TIME 2400 CIOCK-T1UC
                        O  02 CONC m
               STACK  O2  8-7-86
              AFTERBURNER  O2  8-7-86
21
JO -
It
18
17 -
I* •
IB •
14 -
13
12 -
II -
IO -
    SI
    20
    If
    17
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    It
    14
5   "
8   "
0   11
g   te
  •4S
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                              M*»
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                                                          132S
                   TMt 24OO ClOCK-TMC
                    O  02 CONC •
                                                                                 134*
                       TIMC 24oo eiocK-nuc
                        O  02 COMC •
-------
11 •


10-
 7 i ,
 4 •


 1 •


 2 •


 1 -
           E-DUCT CO2 8-7-86
              KILN CO2  8-7-86
11

10

 *
 k •

 4

 J
 I •

 0
                13JS
                                                       • 23
                                                                  1O20        1120
                                                                                         1220
                  T1UC 2«OO ClOCK-TIMC
                  O  C02 COMC •
                  TIUC 24OO ClOCK-TIMC
                  O  CO2 COMC •
            STACK CO2  8-7-86
        AFTERBURNER  CO2  8-7-86
10 -
                                                      3 -


                                                      2 •


                                                      1 -
         1OOO
                I04O
                        112O
                               1200
                                       1240
                                              1320
                  TIMt 24OO CLOCie-T>Ul
                  O  CO2 COMC •
                                                                              134O
                  TIUC 2400 CLOCX-TIUC
                  O   C02 COMC •
-------
            E-DUCT  O2  8-12-86
                   KILN  02 8-12-86
o
M
O
21 •
20 •
It •
1* •
17 •
1* •
I* •
14 •
13 •
12 •
11 •
IO •
U
8
 •20
                    1220
                             1300
                  TlUC 2400 ClOCK-TIMC
                   O  O2 CONC •
                                                                                   lltO
                       nut I tea
                        o  02 COHC m
             STACK  O2  8-12-86
             AFTERBURNER  O2  8-12-86
tt
20 •
I* •
1* •
17 •
1* •
Ik •
14 •
13 •
12 •
11 •
IO •
    21
    20
    It
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    17
    !•
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    14
    13 •
    IS •
    11 •
    10
 1040
                         11*0
                      1400 CLOCK-TIUC
                       O2 CONC •
                                     1140
                                                             •20
                                                                               122O
                                                                                        13OO
                       T1MC 2400 ClOCK-TIMC
                        O  02 CONC M
-------
          E-DUCT CO2 8-12-86
            KILN C02  8-12-86
                                                  it
                                                  to
                                                   §-

                                                   4
                                                   2 •
                                                   1
            102O
                       124O
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                   C02 COMC •
                                   1)40
                                                   o-
                                                   1C JO
                                                            1100      1120
                                                                                     I2OO
                                                                                             I22O
                TlUt 2400 CIOCX-T1WC
                o  coi CONC H
           STACK C02  8-12-86
       AFTERBURNER  CO2  8-12-86
11
10 -
 t -
 4 .

 J •

 2 •

 1 -
11

IO

t •

t

7 •
 1040
                  I12O
                          114O
                                   1200
                                           1220
                                                    120
                 TlUt 240O CLOCK-TIWC
                 O  CO2 COMC •
            1020         1140
                TlUt >4OO (TLOCK-TlUt
                 a   eat COMC •
                                                                                       1340
-------
E-DUCT  02  8-13-86
              I22O
      nut j«oo CLOCK-TIUC
       e 02 CONC m
                                                 AFTERBURNER 02  8-13-86
                                                   1020
                                                           1120
                                                                   1220
                                                                           1320
                                                          nut 1*00 CIOCK-TIMC
                                                           O  O2 CONC B
-------
             E-DUCT C02  8-13-86
U

8
11 •

IO •

 t •




 7

 4 •




 4 -


 J -


 2 •

 I -
     t*o
            1020
                   I HO
                           122O
                                  I MO
                                         1420
                   TIWC 2«OO CLOCK-HUC
                   O  C01 COMC •
                                                           AFTERBURNER C02  8-13-86
                                                     10

                                                     t

                                                     §•

                                                     7 •
                                                             10ZO    11ZO    122O

                                                                    TIMt 24OO CXOCK-TIUt
                                                                    a  CO2 COMC •
-------
             E-DUCT O2 8-14-86
                                                                           'KILN  O2 8-14-86
2O
It
ia
17
i*
is
14
13
12
II
10
 t
 4 -
 3 -
 2 '
  t40
          1010
                                   I MO
                                           1300
                                                    11*0
                                                             It -
                                                             18
                                                             17 -
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                                    E-DUCT O2  8-28-86
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                                          TIUC 2400 CtOCK-tluC
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                                    E-DUCT  O2  9-03-86
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                              E-DUCT CO2  9-03-86
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-------
                          Bros Surface Oil

      Schedule of Vost, Method 5, And Modified Method 5 Sampling

             Combustion Research Facility Sampling Times
DATE
1986
7/21
7/28
7/29
STACK
MS
NO
NO
NO
E-OUCT
VOST
1203-1233
1410-1430
1610-1630
1111-1132
1330-1350
1530-1550
1407-1427
1610-1630
1805-1825
MM5
1203-1722
1114-1622
1405-1916
AFTERBURNER
MS
1157-1307
1119-1245
1415-1623
 * - 2400 Clock Time
NO - No Data
-------
                             Bros Soil



    * Schedule of  Vost,  Method 5,  And Modified Method 5 Sampling



            Combustion Research Facility Sampling Times
DATE
1986
8/04
8/05
8/07
STACK
	
MS
1324-1432
-
1105-1217
1000-1106
E-DUCT
____________ _
VOST
1328-1348
1500-1528
1630-1650
1111-1137
1318-1338
1410-1430
1000-1022
1135-1156
1330-1350
MM5
1324-1735
1100-1528
1000-1410
AFTERBURNER
	
MS
1320-1420
1105-1214
1000-1100
* - 2400 Clock Time
-------
                       Bros  Soil And  Sludge



    * Schedule of Vost, Method  5, And  Modified Method 5 Sampling



            Combustion Research Facility Sampling Times
DATE
1986
8/12
8/13
8/14
STACK
MS
1002-1108
1000-1108
1015-1121
E-DUCT
VOST
1001-1027
1138-1158
1200-1320
1001-1021
1136-1201
1330-1350
1015-1040
1206-1237
1330-1356
MM5
1004-1441
1001-1439
1015-1453
AFTERBURNER
MS
1006-1135
1000-1116
1015-1126
* - 2400 Clock Time
-------
                             Bros Sludge

       Schedule Of Vost,  Method 5,  And Modified Method 5 Sampling

             Combustion Research Facility Sampling Times
DATE
1986
8/28
9/03
9/04
STACK
MS
945-1055
940-1042
930-1032
E-DUCT
VOST
NO
940-1000
1200-1220
1330-1449
930-950
1120-1140
1330-1350
MM5
951-1455
940-1446
930-1429
AFTERBURNER
MS
955-1120
951-1108
937-1044
 * - 2400 Clock Time
ND - No Data
-------
Table
             BROS SOIL




Stack Method 5 Sampler Operating Conditions
DATE
1966
8/04
8/05
8/07
SAMPLE FLOW RATE
L/MIN
(ASCFM)
	
16.3
(0.57)
13.6
(0.48)
16.7
(0.59)
OSL/MIN
(DSCFM)
15.1
(0.53)
12.5
(0.44)
14.5
(0.51)
DRY GAS METER
TEMPERATURE
INLET
*C CF)
AVE
MIN-MAX
45.6
31.1-50
(114.0)
(88-122)
44.9
32.8-48.9
(112.8)
(91-120)
49.1
31.7-55
(120.3)
(89-131)
OUTLET
*C CF)
AVE
MIN-MAX
35.2
29.4-39.4
(95.4)
(85-103)
35.4
30-38.9
(95.8)
(86-102)
37.2
30-42.2
(99.1)
(86-108)
FILTER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
_______________
	
131.9
130.6-133.3
(269.5)
(267-272)
120.2
95.6-131.7
(248.3)
(204-269)
119.4
105-134.5
(247.0)
(221-274)
DESSICANT
IMPINGER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
25.3
24.5-26.1
(77.5)
(76-79)
28.5
27.8-29.5
(83.3)
(82-85)
31.1
30.6-31.7
(88.0)
(87-89)
ISOKINECITY
PERCENT
	
108.4
108.0
99.7
-------
Table
        BROS SOIL AND SLUDGE




Stack Method 5 Sampler Operating Conditions
DATE
1986
8/12
8/13
8/14
SAMPLE FLOW RATE
_ •» v _
L/MIN
(ASCFM)
16.4
(0.58)
17.7
(0.63)
15.9
(0.56)
DSL/MIN
(DSCFM)
15.3
(0.54)
16.3
(0.50)
14.5
(0.51)
SAMPLE TEMPERATURE
INLET
*C CF)
AVE
MIN-MAX
—
40.5
30.6-47.2
(104.9)
(87-117)
40.6
29.5-47.2
(105.1)
(85-117)
43.5
32.2-48.9
(110.3)
(90-120)
OUTLET
*C CF)
AVE
MIN-MAX
33.8
28.9-37.2
(92.8)
(84-99)
33.9
26.7-39.5
(93)
(80-103)
36.5
30.6-41.7
(97.6)
(87-107)
FILTER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
____ 	 _ 	 	
	
121.8
113.3-127.2
(251.3)
(236-261)
125.6
123.9-127.2
(258.1)
(255-261)
121.2
118.9-122.8
(250.1)
(246-253)
DESSICANT
IMPINGER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
18.6
17.2-20
(65.4)
(63-68)
.
18.7
17.2-20
(65.6)
(63-68)
20.2
19.5-21.7
(68.3)
(67-71)
I SDK I NEC I TY
PERCENT
92.7
92.3
99.1
-------
Table
           BROS SLUDGE




Stack Method 5 Sampler Operating Conditions
DATE
1986
8/28
9/03
9/04
SAMPLE FLOW RATE
L/HIN
(ASCFM)
16.7
(0.59)
19.0
(0.67)
21.6
(0.76)
DSL/MI N
(DSCFM)
15.8
(0.56)
17.6
(0.62)
20.0
(0.71)
DRY GAS METER
TEMPERATURE
INLET
*C (*F)
AVE
MIN-MAX
	
37.1
23.9-45.1
(98.8)
(75-106)
44.2
28.3-50
(111.6)
(83-122)
44.9
27.8-50
(112.8)
(82-122)
OUTLET
*C CF)
AVE
MIN-MAX
	
31.9
21.1-31.1
(89.5)
(70-88)
31.7
26.1-35.6
(89.0)
(79-96)
32.7
25.6-36.1
(90.8)
(78-97)
FILTER
TEMPERATURE
•c
(°F)
AVE
MIN-MAX
117.8
112.8-122.2
(244.0)
(235-252)
125.3
120.6-127.2
(257.5)
(249-261)
128.3
127.2-130
(263.0)
(261-266)
DESSICANT
IMPINGER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
18
16.1-20
(64.3)
(61-68)
18.3
17.8-18.9
(64.9)
(64-66)
18.7
17.8-20
(65.6)
(64-68)
ISOKINECITY
PERCENT
98.2
98.4
96.6
-------
Table
      BROS SURFACE OIL




E-Ouct MM5 Sampler Operating Conditions
DATE

1986

TIME
START
7/21



7/28



7/29


SAMPLE FLOW RATE

	
L/MIN

(ASCFM)

22.9
(0.81)


20.6
(0.73)


11.8
(0.42)

DSL/MIN

(DSCFM)

20.5
(0.72)


18.2
(0.64)


10.5
(0.37)

SAMPLE TEMPERATURE

	
INLET
•C (»F)
AVE
MIN-MAX
101.9
93.3-114.4
(215.5)
(200-238)
101.7
93.3-114.4
(215.1)
(200-238)
119.3
110.0-126.7
(247.6)
(230-260)
OUTLET
•C (*F)
AVE
MIN-MAX
119.7
98.9-127.8
(247.4)
(218-262)
103.1
90.0-132.2
(217.6)
(194-270)
126.2
98.9-128.9
(259.2)
(210-264)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
46.1
32.8-53.9
(115.0)
(91-129)
50.7
38.9-56.1
(123.3)
(102-133)
7.2
6.1-9.4
(45.0)
(43-49)
PRESSURE
mm Hg

Hn Hg)
AVE
MIN-MAX
401.3
381.0-431.8
(15.8)
(15-17)
243.9
203.2-330.2
(9.6)
(8-13)
396.3
254.0-431.8
(15.6)
(10-17)
-------
                   BROS  SOIL
Table  .   E-Duct MM5 Sampler Operating Condition
OATF
1986
TIME
START
8/04
8/05
8/07
SAMPLE Fl
L/MIN
(ASCFM)
9.7
(0.34)
8.0
(0.28)
15.3
(0.54)
.OW RATE
DSL/MIN
(DSCFM)
9.0
(0.32)
7.4
(0.26)
13.4
(0.48)
PROBE
OUTLET
TEMPERATURE
•c
CF)
AVE
MIN-MAX
106.9
88.9-118.9
(224.5)
(192-246)
106.7
87.8-121.1
(224.0)
(190-250)
107.0
93.3-132.2
(224.6)
(200-270)
FILTER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
125.2
107.8-133.3
(257.3)
(226-272)
108.7
76.7-126.7
(227.6)
(170-260)
119.5
112.2-126.7
(247.0)
(234-260)
RESIN
TEMPERATURE
•c
CF)
AVE
MIN-MAX
8.7
7.2-9.4
(47.6)
(45-49)
8.6
7.2-9.4
(47.5)
(45-49)
7.8
1.7-10.0
(46.0)
(35-50)
DRY GAS METER
OUTLET
TEMPERATURE
•c
CF)
AVE
MIN-MAX
42.1
30.0-45.6
(107.8)
(86-114)
41.5
31.1-46.1
(106.7)
(88-115)
44.3
32.2-48.3
(111.7)
(90-119)
-------
Table
    BROS SOIL AND SLUDGE



E-Duct MM5 Sampler Operating Conditions
DATE
1986
START
TINE
8/12
8/13
8/14
SAMPLE FL
L/MIN
(ASCFM)
15.3
(0.54
15/8
(0.56)
14.6
(0.52)
.OW RATE
DSL/MIN
(DSCFM)
13.8
(0.49)
14.2
(0.56)
13.0
(0.46)
PROBE |
OUTLET
TEMPERATURE
•c
CF)
AVE.
MIN-MAX
103.9
97.8-115.6
(219.1)
(208-240)
104.3
93.3-121.1
(219.7)
(200-250)
101.7
87.8-117.8
(215.1)
(190-244)
FILTER
TEMPERATURE
•c
(•F)
AVE.
MIN-MAX
119.1
95.6-136.7
(246.3)
(204-278)
123.6
98.9-134.4
(254.4)
(210-274)
123.6
110.0-132.2
(254.4)
(230-270)
RESIN |
TEMPERATURE
•c
CF)
AVE.
MIN-MAX
8.9
6.7-10.0
(48.1)
(44-50)
8.5
5.0-9.5
(47.3)
(41-49)
8.5
3.3-9.4
(47.3)
(38-49)
DRY GAS METER
OUTLET
TEMPERATURE
•c
CF)
AVE.
MIN-MAX
39.4
28.9-58.3
(102.9)
(84.137)
41.5
27.2-47.2
(106.6)
(81-117)
46.1
33.3-51.1
(115.0)
(92-124)
-------
Table
         BROS SOIL



E-Duct MM5 Sampler Operating Conditions
DATE
1986
START
TIME
8/28
9/03
9/04
SAMPLE FLOW RATE
L/MIN
(ASCFM)
17.2
(0.61)
17.3
(0.61)
17.8
(0.63)
DSL/MIN
(OSCFM)
16.0
(0.57)
15.7
(0.55)
16.1
(0.57)
PROBE
OUTLET
TEMPERATURE
•c
CF)
AVE.
MIN-MAX
103.3
91.1-121.1
(218.0)
(196-250)
125.9
121.1-137.8
(258.6)
(250-280)
115.6
87.8-143.3
(240.0)
(190-290)
FILTER
TEMPERATURE
•c
CF)
AVE.
MIN-MAX
100.8
78.9-101.1
(213.4)
(174-214)
131.7
76.7-137.8
(269.0)
(170-280)
134.9
115.6-137.8
(274.9)
(240-280)
RESIN |
TEMPERATURE
°C
CF)
AVE.
MIN-MAX
8.3
4.4-11.1
(47.0)
(40-52)
8.9
-1.7-12.1
(48.1)
(29-54)
8.2
3.3-10.0
(46.7)
(38-50)
DRY GAS METER
OUTLET
TEMPERATURE
•c
CF)
AVE.
MIN-MAX
34.7
27.2-37.8
(94.4)
(81-100)
42.7
27.8-48.9
(108.9)
(82-120)
40.7
27.2-47.2
(105.3)
(81-117)
-------
Table
      BROS SOIL AND SLUDGE




E-Duct Vest Sampler Operating Conditions
DATE

1986

TIME
START

8/12
(1000)


8/12
(1138)


8/12
(1300)

SAMPLE FLOW RATE

___________________
L/MIN

(ASCFM)


1.05
(0.037)


1.35
(0.048)


1.05
(0.037)

DSL/MIN

(DSCFM)
	

1.06
(0.038)


1.33
(0.047)


1.05
(0.037)

SAMPLE TEMPERATURE

—____—_-—____—_________
INLET
*C CF)
AVE
MIN-MAX
42.8
36.1-47.8
(109)
(97-118)
45.4
33.3-50.6
(113.8)
(92-123)
48.8
37.2-51.7
(119.8)
(99-125)
OUTLET
*C CF)
AVE
MIN-MAX
11.3
11.1-11.7
(52.4)
(52-53)
16.6
13.3-25.6
(61.8)
(56-78)
20.0
19.4-22.2
(68)
(67-72)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
	
29.3
29.9-30.0
(84.8)
(84-86)
33.3
33.3-33.3
(92)
(92-92)
33.9
33.9-33.9
(93)
(93-93)
PRESSURE
mm Hg

(in Hg)
AVE
MIN-MAX
177.8
177.8-177.8
(7.0)
(7.0-7.0)
279.4
254.0-330.2
(11.0)
(10-13)
254
254-254
(10)
(10-10)
-------
Table
      BROS SOIL AND SLUDGE



E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

8/13
(1001)


8/13
(1136)


8/13
(1330)

SAMPLE FLOW RATE


L/MIN

(ASCFM)


1.0
(0.035)


1.16
(0.041)


1.10
(0.039)

OSL/MIN

(DSCFM)


1.0
(0.035)


1.13
(0.04)


1.07
(0.038)

SAMPLE TEMPERATURE


INLET
•C CF)
AVE
MIN-MAX
52.8
32.2-61.7
(127)
(90-143)
33.9
33.9-33.9
i S3)
(93-93)
52.2
42.2-58.9
(126)
(108-138)
OUTLET
•C CF)
AVE
MIN-MAX
16.7
16.1-17.8
(62)
(61-64)
18.9
16.7-22.2
(66)
(62-72)
21.0
20.6-21.1
(69.8)
(69-70)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
27.9
27.2-28.9
(82.3)
(81-84)
33.9
33.9-33.9
(93)
(93-93)
37.0
36.7-37.2
(98.6)
(98-99)
PRESSURE
mm Hg

(In Hg)
AVE
MIN-MAX
184.2
177.8-203.2
(7.25)
(7-8)
482.6
482.6-482.6
(19)
(19-19)
264.2
254-279.4
(10.4)
(10-11)
-------
Table
      BROS SOIL AND SLUDGE




E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

8/14
(1015)


8/14
(1206)


8/14
(1330)

SAMPLE FLOW RATE


L/MIN

(ASCFM)


1.0
(0.035)


0.90
(0.032)


1.0
(0.035)

DSL/MIN

(DSCFM)


0.98
(0.035)


0.87
(0.031)


0.96
(0.034)

SAMPLE TEMPERATURE


INLET
*C CF)
AVE
MIN-MAX
41.2
36.1-51.7
(106.2)
(97-125)
37.2
37.2-37.2
(99)
(99-99)
41.0
39.4-43.3
(105.8)
(103-110)
OUTLET
•C (*F)
AVE
MIN-MAX
20.0
18.3-23.3
(68)
(65-74)
19.8
15.6-26.1
(67.6)
(60-79)
21.1
20.0-22.8
(70.0)
(68-73)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
33.8
33.3-35.6
(92.8)
(92-96)
38.9
38.9-38.9
(102)
(102-102)
40.0
40.0-40.0
(104)
(104-104)
PRESSURE
mm Hg

(In Hg)
AVE
MIN-MAX
477.5
457.2-482.6
(18.8)
(18-19)
502.9
482.6-508.0
(19.8)
(19-20)
508
508-508
(20)
(20-20)
-------
                    BROS SOIL




Table  .   E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

6/04
(1328)


8/04
(1500)


8/04
(1630)

SAMPLE FLOW RATE


L/MIN

(ASCFM)

	
0.97
(0.034)


0.73
(0.026)


1.03
(0.036)

DSL/MIN

(DSCFM)

	
0.97
(0.034)


0.72
(0.026)


1.03
(0.036)

SAMPLE TEMPERATURE


INLET
•C CF)
AVE
MIN-MAX
61.9
59.4-65.0
(143.5)
(139-149)
50.3
42.2-55.6
(122.6)
(108-132)
63.6
61.7-65.0
(146.5)
(143-149)
OUTLET
•C CF)
AVE
MIN-MAX
13.8
3.9-17.8
(56.8)
(39-64)
19.3
16.7-23.9
(66.8)
(62-75)
18.9
17.2-22.2
(66)
(63-72)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
35.0
35.0-35.0
(95)
(95-95)
35.1
33.9-35.6
(95.2)
(93-96)
33.3
32.8-35.0
(92.0)
(91-95)
PRESSURE
mm Hg

(in Hg)
AVE
MIN-MAX
157.5
152.4-177.8
(6.2)
(6-7)
411.5
330.2-431.8
(16.2)
(13-17)
241.3
228.6-279.4
(9.5)
(9-11)
-------
Table
            BROS SOIL



E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

8/05
(1111)


8/05
(1318)


8/05
(1410)

SAMPLE FLOW RATE


L/MIN

(ASCFM)

	
0.98
(0.035)


1.01
(0.036)


1.03
(0.036)

DSL/MIM

(DSCFM)


0.97
(0.034)


0.99
(0.035)


1.0
(0.035)

SAMPLE TEMPERATURE


INLET
•C CF)
AVE
MIN-MAX
48.1
42.8-51.7
(118.6)
(109-125)
61.1
51.7-66.7
(142)
(125-152)
69.4
65.6-70.0
(156.4)
(150-158)
OUTLET
'C CF)
AVE
MIN-MAX
20.6
17.8-26.1
(69)
(64-79)
21.2
18.9-26.7
(70.2)
(66-80)
19.8
17.8-23.9
(67.6)
(64-75)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
34.6
33.9-35.6
(94.2)
(93-96)
37.9
33.9-38.9
(100.2)
(93-102)
39.4
39.4-39.4
(103)
(103-103)
PRESSURE
iron Hg

(*n Hg)
AVE
MIN-MAX
^
411.5
381.0-431.8
(16.2)
(15-17)
208.3
203.2-228.6
(8.2)
(8-9)
162.6
152.4-177.8
(6.4)
(6-7)
-------
Table
           BROS SOIL



E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

8/07
(1000)


8/07
(1135)


8/07
(1330)

SAMPLE FLOW RATE

L/MIN

(ASCFM)


0.87
(0.031)


1.03
(0.036)


0.87
(0.031)

DSL/MIN

(DSCFM)


0.84
(0.030)


0.99
(0.035)


0.82
(0.029)

SAMPLE TEMPERATURE

INLET
•C (»F)
AVE
MIN-MAX
50.6
48.9-51.2
(122)
(120-125)
37.0
36.1-37.2
(98.6)
(97-99)
37.8
37.8-37.8
(100)
(100-100)
OUTLET
•C CF)
AVE
MIN-MAX
19.3
18.9-20.0
(66.8)
(66-68)
23.3
21.7-26.7
(74.0)
(71-80)
19.6
17.8-26.7
(67.2)
(64-80)
METER
TFMPFRATIIRF
•c
CF)
AVE
MIN-MAX
31.7
31.7-31.7
(89)
(89-89)
37.2
37.2-37.2
(99)
(99-99)
38.9
38.9-38.9
(102)
(102-102)
PRESSURE
nwn HQ

(in Hg)
AVE
MIN-MAX
299.7
254.0-330.2
(11.8)
(10-13)
431.8
431.8-431.8
(17)
(17-17)
436.9
431.8-457.2
(17.2)
(17-18)
-------
Table
        BROS SURFACE OIL



E-Ouct Vost Sampler Operating Conditions
DATE

1986

TIME
START


7/21
(1203)


7/21
(1410)


7/21
(1610)
-
SAMPLE FLOW RATE

___________________
_____ 	 _ 	 	 	 ___
L/MIN

(ASCFM)



0.76
(0.027)


1.01
(0.036)


0.85
(0.030)
DSL/MIN

(DSCFM)



0.76
(0.027)


0.99
(0.035)


0.84
(0.030)
SAMPLE TEMPERATURE

	
INLET
•C (-F)
AVE
MIN-MAX
38.7
37.8-40
(101.6)
(100-104)
35.6
33.9-36.7
(96.0)
(93-96)
33.3
31.1-34.5
(92.0)
(88-94)
OUTLET
'C CF)
AVE
MIN-MAX


(72.4)
(68-76)


(68.4)
(67-73)
22.2
20-25.6
(72.0)
(68-78)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
35.9
35.6-36.1
(96.6)
(96-97)
38.9
38.3-40
(102)
(101-104)
36.1
36.1-36.1
(97.0)
(97-97)
PRESSURE
mm Hg

(In Hg)
AVE
MIN-MAX
223.5
177.8-279.4
(8.8)
(7-11)
248.9
228.6-254
(9.8)
(9-10)
401.3
381-406.4
(15.8)
(15-16)
-------
Table
        BROS SURFACE OIL



E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START


7/28
(1111)


7/28
(1330)


7/28
(1530)
SAMPLE FLOW RATE

	
L/NIN

(ASCFM)
'


0.94
(0.033)


1.05
(0.037)


1.07
(0.038)
DSL/MI N

(DSCFM)



0.91
(0.032)


1.06
(0.036)


1.04
(0.037)
SAMPLE TEMPERATURE


INLET
•C fF)
AVE
MIN-MAX
61.1
47.8-64.5
(142.0)
(118-148)
62.6
45-67.8
(144.6)
(113-154)


(142.0)
(116-149)
OUTLET
•C («F)
AVE
MIN-MAX


(73)
(72-75)
22.7
21.7-25.6
(72.8)
(71-78)
20.8
20-22.2
(69.4)
(68-72)
METER
TEMPERATURE
•c
CF)
AVE
MIN-MAX
41.2
40.6-41.7
(106.2)
(105-107)
42.9
42.8-43.3
(109.2)
(109-110)
40.5
40-41.1
(104.8)
(104-106)
PRESSURE
mm Hg

(1n Hg)
AVE
MIN-MAX
457.2
457.2-457.2
(18)
(18-18)
223.5
203.2-304.8
(8.8)
(8-12)
299.7
254-330.2
(11.8)
(10-13)
-------
Table
       BROS SURFACE OIL




E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

7/29
(1407)


7/29
(1610)


7/29
(1805)

SAMPLE FLOW RATE

L/MIN

(ASCFM)



0.95
(0.034)


1.03
(0.036)


1.01
(0.036)
DSL/MIN

(DSCFM)



0.92
(0.032)


1.0
(0.035)


0.99
(0.035)
SAMPLE TEMPERATURE
	
INLET
*C CF)
AVE
MIN-MAX
43.1
40-45.6
(109.6)
(104-114)
55.7
40.6-59.4
(132.2)
(105-139)
52.6
40-57.2
(126.6)
(104-135)
OUTLET
'C CF)
AVE
MIN-MAX
21.3
21.1-21.7
(70.4)
(70-71)
21.1
19.4-25.6
(70.0)
(67-78)
21.1
19.4-25.6
(70.0)
(67-78)
METER
TCftJDCD A Tl IDC
TEMPERATURE
•c
CF)
AVE
MIN-MAX
45.6
44.5-50
(114)
(112-122)
41.1
41.1-41.1
(106)
(106-106)
40
40-40
(104)
(104-104)
PRESSURE
mm ng

Hn Hg)
AVE
MIN-MAX
401.3
381-431.8
(15.8)
(15-17)
243.9
203.2-330.2
(9.6)
(8-13)
396.3
254-431.8
(15.6)
(10-17)
-------
Table
E-Duct Vost Sampler Operating Conditions
DATE
1986

TIME
START

9/03
(0940)


9/03
(1200)


9/03
(1330)

SAMPLE FLOW RATE
L/MIN

(ASCFM)


1.05
(0.037)


1.04
(0.037)


0.53
(0.019)

DSL/MIN

(DSCFM)


1.02
(0.036)


0.96
(0.035)


0.51
(0.018)

SAMPLE TEMPERATURE
—_..___ _ _ _
INLET
*C CF)
AVE
MIN-MAX
122.1
115.6-124.5
(251.8)
(240-256)
117.8
107.2-126.7
(244)
(225-260)
117.9
110-126.7
(244.3)
(230-260)
OUTLET
•C CF)
AVE
MIN-MAX
15.6
14.5-16.7
(60)
(58-62)
24.1
21.1-28.3
(76.4)
(70-83)
25.6
22.2-28.9
(78.0)
(72-84)
METER
TCUDCD ATI IDC
1 EMrtRATURc
•c
CF)
AVE
MIN-MAX
27.3
25.6-28.9
(81.2)
(78-84)
36.6
35-38.3
(97.8)
(95-101)
30.1
28.3-39.4
(86.1)
(83-103)
PRESSURE
mm Hg
(1n Hg)
AVE
MIN-MAX
	 	 — 	 	
165.1
165.1-165.1
(6.5)
(6.5-6.5)
332.8
292.1-381.0
(13.1)
(11.5-15.0)
152.4
127.0-355.6
(6.0)
(5-14)
-------
Table
           BROS SOIL




E-Duct Vost Sampler Operating Conditions
DATE

1986

TIME
START

9/04
(0930)


9/04
(1120)


9/04
(1330)

SAMPLE FLOW RATE


L/MIN

(ASCFM)

	
1.0
(0.035)


1.1
(0.039)


1.01
(0.036)

DSL/MIN

(DSCFM)


1.0
(0.035)


1.08
(0.038)


0.98
(0.035)

SAMPLE TEMPERATURE


INLET
*C CF)
AVE
MIN-MAX
_
112.2
98.3-120.0
(234)
(209-248)
117.6
110-123.9
(243.6)
(230-255)
119.4
101.7-137.8
(247)
(215-280)
OUTLET
°C CF)
AVE
MIN-MAX
	 	
17.1
14.4-18.9
(62.8)
(58-66)
17.0
16.1-18.3
(62.6)
(61-65)
19.0
17.8-20.6
(66.2)
(64-69)
METER
TEMPERATURE
•c
(°F)
AVE
MIN-MAX
	 	 	 	
	
25.6
25.0-26.1
(78)
(77-79)
30.1
30.0-30.6
(86.2)
(86-87)
33.1
32.8-33.9
(91.6)
(91-93)
PRESSURE
mm Hg

(in Hg)
AVE
MIN-MAX
127
127-127
(5.0)
(5.0-5.0)
284.5
254-330.2
(11.2)
(10-13)
335.3
330.2-355.6
(13.2)
(13-14)
-------
        Table  - .  Schedule of Vest, Method 5, And Modified Method 5 Sampling
Feed
Material
Surface
Oil
• Soil
Soil
And
Sludge
Mixture
Sludge
I
Date
7-21-86
7-28
7-29
8-04
8-05
8-07
8-12
8-13
8-14
8-28
9-03
9-04
Stack
M5
ND
NO
NO
1324-1432
1105-1217
1000-1106
1002-1108
1000-1108
1015-1121
945-1055
940-1042
930-1032
E-Duct
VOST MM5
1203-1233
1410-1430
1610-1630
1111-1132
1330-1350
1530-1550
1407-1427
1610-1630
1805-1825
1328-1348
1500-1528
1630-1650
1111-1137
1318-1338
1410-1430
1000-1022
1135-1156
1330-1350
1001-1027
1138-1158
1200-1320
1001-1021
1136-1201
1330-1350
1015-1040
1206-1237
1330-1356
NO
940-1000
1200-1220
1330-1449
930-950
1120-1140
1330-1350
1203-1722
1114-1622
1405-1916
1324-1735
1100-1528
1000-1410
1004-1441
1001-1439
1015-1453
951-1455
940-1446
930-1429
Afterburner
M5
1157-1307
1119-1245
1415-1623
1320-1420
1105-1214
1000-1100
1006-1135
1000-1116
1015-1126
955-1120
951-1108
937-1044
*  - 2400 Clock Time
NO - No Data
-------
:lue Gas Flow Rates for Kiln PCB Trial  Eurr a»d  RDS Tests
Location

Surf act Oil 7-21
7-28
7-29
Soil 6-4
8-5
6-7
Soil + Siucce 6-12
6-13
6-14
Siucce 8-26
5-3
9-*
Flue Flow Rat
Scrubber
26.4
£.2
16.9
16.3
15.6
22.6
24.0
24.1
20.9
24.4
24.9
25.5
,e (dscfl/iin)
Stack
tt
H
«
IS. 4
l£.e
£0.6
22.9
24.6
20.4
22.5
25.0
26.6
Flue Flw Ra4
ScrubJer-
932
1137
6«
574
557
7Sc
847
650
737
660
681
899
e (5sc*s)
Stac*
M
H
*ff
66*
e-r«
c • «
725
610
670
7£1
7:2
6fi2
10:7
-------
    APPENDIX E



ANALYTICAL REPORTS
        E-l
-------
 /N ACUREX
r*^ Corporation
    October  10,  1986
    Dr. Larry H. Waterland
    Program  Manager
    US EPA Combustion Research Facility
    c/o NCTR, Building 45
    Jefferson. Arkansas  72079
                    (CRF!
Energy & Environmental Division

     page 1 of 15

     Distribution:
     Johannes Lee
     Jerry Lewis
     Ralph Vocque
    Subject:    VOST Analytical  Results

    Reference:  EPA Contract  68-03-3267
    Dear Dr. Waterland:

          The tables which  follow  summarize  the  results  of  analyses  performed  on
    Volatile Organic Sampling Trains  (VOST)  taken  at  the CRF  between July 8,  1986
    and September 4, 1986.  These  data  are associated with  the  performance of  the
    rotary kiln system during incineration of  the  following:  Askarel +  Auto  Dry;
    BROS surface oil; BROS  soil: BROS soil * sludge and  BROS  sludge.

          Sampling and analysis were  performed  in  general accordance with
    "Protocol For The Collection And Analysis  Of Volatile POHC'S  Using VOST",  EPA-
    600/8-84-007. March  1984.  Variations from  this protocol  are  documented in
    "Proceedings of the  Eleventh Annual  Research Symposium:   Incineration and
    Treatment of Hazardous  Waste".  EPA/600/9-85/028.  September  1985.  pages 252-
    260.
    Sincerely;
    Robert W. Ross,
    Senior Chemist
II
                  NCTR. Building 45. Jefferson. AR 72079  (501) 5*1-0004  FAX. (501) 536-6446
        555 Clyde Avenue. PO Box 7555, Mountain View, CA 94039 (415) 964-3200 Telex 34-6391 TWX. 910-7796593
-------
ABLE 8.   COMPOUNDS ROUTINELY DETERMINED IN VOST  SAMPLES
Compounds
Mtthyl tne Chloride
1,1-01 chloroethylene
1,1-01 ehl orethane
trans-1 ,2-01 ehl oroethylene
Chloroform
1 .2-01 ehl oroethane*
2-butanone
1 ,1 ,l-Tr1 ehl oroethane
Carbon TttrachloHde
Browdl chloromethane
1 ,2-DI ehl oropropane
trans-1 ,3-01 chloropropene
Trlchloroethylene
Benzene
1 ,1 ,2-Tr1 ehl oroethane*
Chi orodl broiaomethane
Hexane
Bronof orti •
Tetrachloroethylene*
1 .1 ,2 ,2-Tetracnl oroethane
1so-octane
Toluene*
Htpane
Chlorobenzene
Octane
1 ,3-01 ehl orobenzene
1 ,2-01 chl orobenzene
1 ,4-01 ehl orobenzene
Abbreviation
H/C
1.1-DCEENE
1.1-DCEANE
t-l,2-DCEENE
Chloroform
1.2-DCEAME
2B
1,1.1-TCEANE
ecu
BOCM
1,2-DCPRANE
t-l,3-OCPRENE
C13-EENE
BZ
1.1.2-TCEAME
CDBM
HEX
Bronofonn
CU-EENE/ANE
1so-octane
To!
Hep
C1-BZ
Octane
1,3-DCBZ
1.2-DCBZ
1.4-OCBZ
        Total of 28 compounds
        * Elute at sane retention t1i
                            41
-------
                      TABLE 3.  VOST ANALYSIS  (Total (jg/Train)

                          JULY 21,  1986 -  BROS SURFACE OIL
COMPOUNDS
M/C
1,1-DCEENE
1 , 1 -OCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1 -TCEANE
ecu
BOCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1, 2 -TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E0721 1203V
-B-
-B-
-B-
-B-
-B-
-B-
-B-
.102
-B-
-B-
-B-
-B-
*68.3
-B-
-B-
-B-
.048
1560%
-B-
-B-
19*
-B-
-B-
-B-
E07211410V
-B-
-B-
-B-
-B-
-B-
-B-
-B-
.046
-B-
-B-
-B-
-B-
*1.96
-B-
-B-
-B-
.061
404*
-B-
-B-
5*
-B-
-B-
-B-
E07211610V
-B-
-B-
-B-
-B-
-B-
.279
-B-
*.224
-B-
-B-
-B-
-B-
*40.9
-B-
-B-
-B-
.101
1215%
.100
-B-
38%
-B-
-B-
-B-
*    Greater than calibration range
-B-  BeloM quantification 1i«it
**   These compounds are internal standards.
The number reported is % Recovery.
-------
                      TABLE  4.  VOST ANALYSIS  (Total UQ/Train)

                         JULY 28, 1986 -  BROS SURFACE OIL
COMPOUNDS
M/C
1,1-DCEENE
1,1-DCEANE
T-1.2-DCEENE
CHLOROFORM
1.2-DCEANE+2B
1,1,1-TCEANE
CC14
BOCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE •*• ANE
ISO-OCTANE**
TOLUENE
C1-BZ
OCTANE**
1,3-DCBZ
1,2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E07281111V
*2.29
-B-
-B-
-B-
.072
.104
-B-
*3.39
.096
-B-
-B-
-B-
.017
-B-
.111
.020
.069
134%
.110
-B-
104%
-B-
-B-
-B-
E07281330V
.634
-B-
-B-
-B-
.061
.216
-B-
*.726
-B-
-B-
-B-
-B-
.020
-B-
.129
.017
.044
192%
.058
-B-
108%
-B-
-B-
-B-
E07281530V
*11.9
-B-
-B-
-B-
.060
.050
-B-
*.311
-B-
-B-
-B-
-B-
-B-
-B-
.082
-B-
-B-
694%
-B-
-B-
72%
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification liait
**   These compounds are internal standards.
The number reported is % Recovery.
-------
TABLE 5.  VOST ANALYSIS (Total jig/Train)




   JULY 29,  1986  -  BROS SURFACE OIL
QUANTIFICATION
COMPOUNDS
M/C
1,1-DCEENE
1,1-DCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-OCEANE+2B
1,1,1-TCEANE
CC14
80CM
1,2-DCPRANE
T-1,3-OCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-OCBZ
1,4-DCBZ
LIMIT E07291407V
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
.561
-B-
-B-
-B-
.183
-B- '
-B-
*.642
.146
.067
-B-
.089
.061
-B-
.026
-B-
*.402
568%
*1.84
.115
508*
*1.60
*1.48
-B-
E07291610V
.291
-B-
-B-
-B-
.077
*.608
-B-
*.579
-B-
-B-
-8-
-B-
-B-
-B-
.011
-B-
.105
114»
.097
-B-
16U
-B-
-B-
-B-
E07291805V
*.739
-B-
-B-
-B-
.207
*1.211
-B-
*.823
-B-
-B-
-B-
-B-
-B-
-B-
*.243
-B-
.193
189*
*.296
-B-
185*
-B-
-B-
-B-
* Greater than calibration range
-B- Below quantification
** These compounds are
liait
internal standards

. The number

reported is

\ Recovery.
-------
                      TABLE 6.  VOST ANALYSIS (Total ug/Train)

                            AUGUST  4,  1986 -  BROS  SOIL
COMPOUNDS
M/C
1,1-DCEENE
1,1-DCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
CC14
BOCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
C1-BZ
OCTANE**
1,3-OCBZ
1 , 2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E08041328V
*1.43
.018
-B-
-B-
.057
-B-
*.269
.189
-B-
-B-
-B-
-B-
-B-
-B-
*.138
-B-
.277
602%
*.278
-B-
81%
-B-
-B-
-B-
E0804 1500V
.380
-B-
-B-
-B-
.033
-B-
-B-
.110
.019
-B-
-B-
.009
.024
-B-
-B-
-B-
.213
66*
.124
-B-
106%
-B-
-B-
-B-
E0804 1630V
.458
-B-
-B-
-B-
.056
-•-
-§-
.171
-B-
-B-
-B-
.009
.026
-B-
.027
.116
.179
99%
.135
-B-
104%
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification limit
**   These compounds are internal standards.
The number reported is * Recovery.
-------
                       TABLE 7.   VOST ANALYSIS (Total ng/Train)

                             AUGUST 5,  1986 - BROS SOIL
COMPOUNDS
M/C
1,1-OCEENE
1 , 1 -OCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
ecu
BOCM
1,2-OCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
C1-BZ
OCTANE**
1,3 -DCS 2
1,2-DCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E08051111V
.196
-B-
-B-
-B-
.055 -
-B-
.003
.064
-B-
.010
-B-
-B-
.020
.020
.029
.088
.068
64*
.096
-B-
114%
-B-
-B-
-B-
E08051318V
.403
-B-
-B-
-B-
.049
-B-
-fl-
.112
-B-
-B-
-B-
-B-
.026
-B-
.059
.141
.175
138%
.124
-B-
106%
-B-
-8-
-B-
E08051410V
.260
-B-
-B-
-B-
.039
-B-
-B-
.084
.015
-B-
-B-
-B-
.038
-B-
.017
-B-
.197
72%
.194
-B-
110%
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification  Halt
**   These compounds are internal standards.
The number reported is % Recovery.
-------
                       TABLE  8.   VOST ANALYSIS  (Total jig/Train)

                             AUGUST 7. 1986 -  BROS SOIL
COMPOUNDS
H/C
1,1-DCEENE
1 , 1 -DCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
CC14
BOCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-DCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E0807 1000V
*.859
.066
-B-
-B-
.094
-B-
.192
*.367
-B-
-B-
-B-
-B-
-B-
-B-
-B-
-B-
.237
93*
.212
-B-
50%
-B-
-B-
-B-
E08071135V
.455
.042
-B-
-B-
.087
*.861
-8-
*.189
-B-
-B-
-B-
-B-
.029
-B-
.015
.033
.250
172*
.179
-B-
114«
-B-
-B-
-B-
E0807 1330V
*.721
.021
-B-
-B-
.070
-B-
.048
*.307
-B-
-B-
-B-
-B-
-B-
-B-
.018
-B-
*.412
69%
.245
-fi-
ll 6\
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification limit
**   These compounds are internal standards.  The number reported is ft Recovery.
-------
                       TABLE 9.   VOST ANALYSIS  (Total yg/Train)

                       AUGUST 12,  1986 -   BROS  SOIL PLUS SLUDGE
COMPOUNDS
M/C
1,1-DCEENE
1,1-OCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
ecu
BDCM
1,2-OCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E08121007V
*1.19
-B-
-B-
-B-
.060 .
-B-
.023
*.521
-8-
-8-
-8-
"*O"*
.023
-8-
-8-
-8-
-B-
75%
.116
-B-
na
-B-
-8-
-8-
E08121138V
.586
-B-
-B-
-B-
.046
-8-
-B-
*.218
-B-
-B-
-8-
-8-
.008
-8-
.115
.055
.035
56*
.072
-B-
103*
-B-
-8-
-8-
£081 21 300V
*.860
-8-
-B-
-B-
.088
-8-
-B-
*.312
-B-
-B-
-8-
-B-
.050-
-B-
.214
.063
.095
52*
.086
-B-
54*
-8-
-8-
-8-
*    Greater than calibration range
-B-  Below quantification liait
**   These compounds are internal standards.
The number reported 1s * Recovery.
-------
                      TABLE 10.  VOST ANALYSIS (Total

                      AUGUST  13,  1986  -  BROS SOIL PLUS SLUDGE
COMPOUNDS
M/C
1,1-DCEENE
1,1-OCEANE
T-1,2-OCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
ecu
BDCM
1,2-DCPRANE
T-1,3-OCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E08131001V
*3.53
-B-
-B-
-B-
.065
-B-
-B-
*.398
-8-
-B-
-B-
-B-
.020
-B-
*.230
.050
.050
62*
.045
-B-
90%
-8-
-B-
-B-
E08131136V
*9.04
-B-
-B-
-B-
.070
-B-
-B-
*.281
-B-
-B-
-B-
-B-
.018
-B-
*.150
-B-
.053
48*
.040
-B-
90*
-B-
-B-
-B-
£081 3 1330V
*2.16
-B-
-B-
-B-
.204
-B-
-B-
*.449
-B-
-B-
-B-
-B-
.038
-B-
*.230
.109
.101
50*
.134
-B-
76*
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification 1i*it
**   These compounds are internal standards.
The number reported is \ Recovery.
-------
                      TABLE 11.  VOST ANALYSIS (Total  jig/Train)

                      AUGUST  14,  1986 -  BROS SOIL PLUS SLUDGE
COMPOUNDS
M/C
1,1-DCEENE
1,1-DCEANE
T-1.2-OCEENE
CHLOROFORM
1.2-DCEANE+2B
1,1,1-TCEANE
ecu
BDCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
C1-BZ
OCTANE**
1.3-DCBZ
1,2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E08141015V
.507
-B-
-B-
-B-
.070
-B-
-B-
*.255
-B-
-B-
-B-
-B-
.024
-B-
.023
-B-
.110
62*
.116
-B-
112»
-B-
-B-
-B-
E08141206V
.332
-B-
-B-
-B-
.050
-B-
-B-
*.247
-8-
-B-
-8-
-B-
.026
-B-
.016
-B-
.132
62%
.082
-B-
99%
-B-
-8-
-8-
E08141330V
.317
-B-
-B-
-B-
.060
-B-
-B-
*.289
-B-
-B-
-B-
-B-
.061
-B-
.017
.047
.130
67*
.094
-B-
ion
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification liait
**   These compounds are internal standards.
The nuafaer reported is % Recovery.
-------
                      TABLE 12.  VOST ANALYSIS (Total  jig/Train)

                           AUGUST 28, 19B6 -  BROS SLUDGE
COMPOUNDS
M/C
1,1-DCEENE
1,1-DCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
CC14
BDCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-DC82
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E0828 1043V
*5.68
-B-
-B-
. -B-
*11.7
-B-
-B-
-B-
*52.3
-B-
-B-
*19.1
-B-
-B-
*3.92
-B-
-B-
5005*
-B-
-B-
7645*
-B-
-B-
-B-
E08281152V
.304
-B-
-B-
-B-
*.520
-B.
-B-
.120
*3.19
.129
-B-
*.377
*4.41
-B-
*.212
-B-
-B-
130*
*1.84
.044
136*
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification  Halt
**   These compounds are Internal standards.
The number reported Is % Recovery.
-------
                      TABLE 13.   VOST ANALYSIS (Total  pg/Train)

                          SEPTEMBER 3, 1986 -  BROS SLUDGE
COMPOUNDS
M/C
1,1-DCEENE
1,1-DCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1 -TCEANE
ecu
BOCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE «• ANE
ISO-OCTANE**
TOLUENE
Cl-BZ
OCTANE**
1,3-DCBZ
1,2-OCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E09030940V
.084
-B-
-B-
-8-
.081
-B-
-B-
.127
-B-
.025
-B-
.051
.113
-B-
.075
-B-
.150
64*
.074
-B-
106*
-fl-
-B-
-B-
E0903 1200V
.367
-B-
-B-
-B-
.086
-B-
-8-
.091
-B-
.042
-B-
.073
*.333
-B-
.092
-B-
.170
88%
.134
-B-
122t
-B-
-B-
-B-
E09031330V
.185
-B-
-B-
-B-
.175
-B-
-B-
.088
-8-
.018
-B-
.082
.053
-B-
*.383
-B-
.204
146*
.097
-B-
114*
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification limit
**   These compounds are internal standards.  The number reported is * Recovery.
-------
                      TABLE 14.   VOST ANALYSIS  (Total ug/Train)

                          SEPTEMBER 4, 1986 -  BROS SLUDGE
COMPOUNDS
M/C
1,1-DCEENE
1,1-OCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE+2B
1,1,1-TCEANE
CC14
BDCM
1,2-DCPRANE
T-1,3-DCPREN
CL3-EENE
BENZENE
1,1,2-TCEANE
HEXANE
BROMOFORM
CL4-EENE + ANE
ISO-OCTANE**
TOLUENE
C1-BZ
OCTANE**
1,3-DCBZ
1,2-DCBZ
1,4-DCBZ
QUANTIFICATION
LIMIT
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E09040930V
.568
-B-
.140
-B-
*.258.
-B-
-B-
-B-
-B-
.026
-8-
.068
.151
-B-
.066
-B-
-B-
16U
.078
-B-
102%
-B-
-B-
-B-
E09041120V
*1.16
-B-
.037
-B-
.156
-B-
-B-
-B-
-B-
-B-
-B-
.041
.041
-B-
.045
-B-
-B-
102%
.038
-B-
100%
-B-
-B-
-B-
E0904 1330V
.059
-B-
.083
-B-
.146
-B-
-B-
-B-
-B-
.016
-B-
.039
.196
-B-
.025
-B-
-B-
134t
.062
-B-
100%
-B-
-B-
-B-
*    Greater than calibration range
-B-  Below quantification liait
**   These compounds are internal standards.
The number reported is \ Recovery.
-------
                       TABLE 2.  ANALYTICAL RESULTS OF VOST SAMPLES ON JULY 28, 198S
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :

M/C
1,1-OCEENE
1,1-DCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-OCEANE +
2-8UTANONE
1,1,1-TCEANE
CCL4
BDCM
1,2-DCPRANE
T-1.3-DCPRENE
CL3-EENE
BENZENE
1,1,2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL «• HEP
CL-BZ
OCTANE
1,3-DCBZ
1,2-DCBZ
1,4-DCBZ




QUANTIFICATION
LIMIT
(MG/ TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.126
0.126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E07281111V
E-DUCT
VOST
19.174

DETECTED /
*2.298 (119.849)
-8-
-B-
0.072 (3.755)
0.104 (5.424)

-B-
*3.398 (177.219)
0.096 (5.007)
-B-
-B-
-B-
0.017 (0.887)

0.111 (5.789)
0.020 (1.043)
0.069 (3.599
134 * **
0.110 (5.737)
104 % **
-B-
-B-
-B-
E07281330V
E-OUCT
VOST
20.311

IMOUNT, JJG/TRAIN (CONC
0.634 (31.215)
-B-
-B-
0.061 (3.003)
0.216 (10.635)

-B-
*0.726 (35.744)
-B-
-B-
-B-
0.020 (0.985)

0.129 (6.351)
0.017 (0.837)
0.044 (2.166)
192 % **
0.058 (2.856)
-B-
108 % **
-B-
-B-
-B-
E07281530V
E-DUCT
VOST
20.889

:ENTRATION, PG/DSCM)
*11.99 (573.986)
-B-
-B-
-B-
0.060 (2.875)
0.050 (2.394)

-B-
*0.311 (14.888)
-B-
-B-
-B-
-B-
-B-

0.082 (3.926)
-B-
694 % **
-B-
-B-
72 % **
-B-
-B-
-B-
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % RECOVERED
-------
                      TABLE  3.   ANALYTICAL RESULTS OF VOST ON JULY 29, 1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :

M/C
1.1-DCEENE
1 , 1 -DCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-DCEANE +
2-BUTANONE
1,1,1-TCEANE
CCL4
BDCM
1,2-DCPRANE
T-1,3-DfcPHENE
CL3-EENE
BENZENE
1,1,2-TCEANE *
CDOM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3»DCBZ
1,2-DCBZ -
1,4-DCBZ


QUANTIFICATION
LIMIT
(MG/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253
0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337
0.0127
0.0211
0.0252
0.0127
0.0254
0.0063
0.0127
0.063
0.063
0.063
E07291407V
E-DUCT
VOST
18.338

E07291610V
E-DUCT
VOST
20.099
f

E07291805V
E-DUCT
. VOST
i '
19.731
1
1
DETECTED AMOUNT, pG/TRAIN (CONCENTRATION, pG/DSCM)
	 ' j i
0.561 (30.592) . 0.291 (14.478)
-8- ' -B-
-B- -B-
0.183 (9.979) ; 0.077 (3.831)
-B- *0.608 (30.250)
-B- -B-
*0.642 35.009) *0.579 (28.807)
0. 146 7.9r>2) -Q-
*0.739 (37.454) i
— R- '
-B-
-B-
0.207 (10.491)
*1.211 (61.376) .
-B- i
*0.823 (41.711) i
-n-
0.067 3.654) -B- -5-
-li- i -R-
0.089 4.853)
0.061 3.326)
-B-
0.026 (1.418)
*0.402 (21.922)
568 * **
*1.842 (100.447)
0.115 (6.271)
508 % **
*1.603 (87.414)
*1.481 (80.761)
-B-
-
-B-
-B-
-B-
0.011 (0.547)
0.105 (5.224)
114 % **
0.097 (4.826)
161 % **
-B-
-B-
-B-
-B- '
-B-
-B-
-B-
*0.243 (12.316)
0.193 (9.782)
189 % **
*0.296 M5.002)
185 % **
-B-
-B-
-B-
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % RECOVERED
-------
                       TABLE 4.
ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST A,  1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :

M/C
1,1-DCEENE
1 , 1 -OCEANE
t-1,2-DCEENE
CHLOROFORM
1,2-DCEANE +
2-BUTANONE
1,1,1-TCEANE
CCL4
BOCM
1,2-OCPRANE
T-1.3-DCPRENE
CL3-EENE
BENZENE
1,1,2-TCEANE *
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
I SO -OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-DCBZ
1,2-DCBZ
1.4-DCBZ





QUANTIFICATION
LIMIT
(pG/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
E0804 1328V
E-DUCT
VOST
19.404

DETECTEI
*1.433 (73.851)
0.018 JO. 0928)
-B-
0.057 (2.938)
-B-

*0.269 (13.863)
0.189 (9.740)
-B-
-B-
-B-
-B-
-B-
-B-

*0.138 (7.112)
-B-
0.277 (14.275)
602 % **
*0.278 (14.327)
-B-
81 % **
0.063 i -B-
0.063 j -B-
0.063 »1 -B-
l
E08041500V
E-DUCT
VOST
20.314

E08041630V
E-DUCt
VOST
20.530

3 AMOUNT, pg/TRAIN (CONCENTRATION, pg/DSCM)
0.380 (18.706)
-B-
-B-
-B-
0.033 (1.625)
-B-

-B-
0.110 (5.415)
0.019 (0.935)
-B-
-B-
0.009 (0.443)
0.024 (1.182)
-B-

-B-
-B-
0.213 (10.485)
66 % **
0.124 (6.104)
106 % **
-B-
-B-
-B-

0.458 (22.309)
-B-
-B-
-B-
0.056 (2.728)

-B-
0.171 (8.329)
-B-
-B-
0.009 (0.438)
0.026 (1.266)
-B-

0.027 1.315)
0.116 5.650)
0.179 8.719)
99 % **
0.135 (6.576)
-B-
104 % **
-B-
-B-
-B-

* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
          THE NUMBERS REPORTED ARE % RECOVERED
-------
TABLE 5.  ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST 5,  1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)


VOST COMPOUNDS :


M/C
1.1-DCEENE
1.1-DCEANE
T-1,2-DCEENE
CHLOROFORM
1,2-DCEANE +
2-BUTANONE
1.1,1-TCEANE
CCL4
BDCM
1.2-DCPRANE
T-1.3-DCPHENE
CL3-EENE
BENZENE
1.1,2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/QNE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-DCBZ
1,2-DCBZ
1,4-OCBZ
- GREATER THAN CALldRAtl






QUANTIFICATION
LIMIT
(M9/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
E08051111V
E-DUCT
VOST
19.446
E08051318V
E-DUCT
VOST
19.858
I

1
E08051410V
E-DUCT
VOST
20.073



DETECTED AMOUNT, MS/TRAIN (CONCENTRATION, ug/TRAIN)

0.196 (10.079)
-B-
-B-
0.055 (2.828)

0.003 0.154)
0.064 J3. 291)
— B—
0.010 (0.514)
-B-
0.0126 -B-
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
0.020 (1.028)
0.020 (1.028)

0.029 (1.491)
0.088 4.525)
0.068 (3.597)
64 \ **
0.096 (4.937)
114 % **
-B-
-B-
-B-

0.403 (20.294)
-B-
-B-
0.049 (2.468)

-B-
0.112 (5.640)
-B-
-B-
-B-
0.026 (1.309)

0.059 (2.971)
0.141 (7.100)
0.175 (8.813)
138 % **
0.124 (6.244)
106 * **
-B-
-B-
-B-

0.260 (12.953)
-B-
-B-
0.039 (1.943)

-B-
0.084 (4.185)
0.015 (0.747)
-B-
-B-
-B-
0.038 (1.893)

0.017 (0.847)
0.197 J9.814)
72 i **
0.194 (9.665)
110 * **
-B-
-B-
-B-
JN RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS. THE NUMBERS REPORTED ARE % RECOVERED
B - BELOW QUANTIFICATION LIMIT
-------
                       TABLE 6.   ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST  7,  1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (OSL)
VOST COMPOUNDS :


M/C
1.1-DCEENE
1,1-DCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-DCEANE +
2-BUTANONE
1,1,1-TCEANE
CCL4
BDCM
1,2-DCPRANE
T-1.3-DCPRENE
CL3-EENE
BENZENE
1.1,2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/QNE
ISO-OCTANE
TOL + HEP
CL-B2
OCTANE
1,3-DCBZ
1.2-DCBZ
1,4-DCBZ




QUANTIFICATION
LIMIT
(M9/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
- - - - -
E0807 1000V
E-DUCT
VOST
16.851

E08071135V
E-DUCT
VOST
19.735

E08071330V
E-DUCT
VOST
16.461

DETECTED AMOUNT, |4g/TRAIN (CONCENTRATION, pg/TRAIN)

*0.859 (50.976)
0.066 (3.917)
-B-
-B-
0.094 (5.578)
-8-

0.192 (11.394)

0.455 (23.055)
0.042 (2.128)
-B-
-B-
0.087 (4.408)
*0.861 (43.628)

-B-
*0.367 (21.779) " *0.189 (9.577)
-B-
-B-
-B-
-B-
-B- -B-
-8-
-B-
-B-
0.029 (1.469)
-B- : -B-

-B-
-B-
0.237 (14.064)
93 % **
0.212 (12.581)
50 % **
-B-
-B-
-B-
_

0.015 (0.760)
0.033 (1.6721
0.250 (12.668)
172 % **
0.179 (9.070)
114 % **
-B-
-B-
-B-

*0.721 (43.80)
0.21 (1.278)
-B-
-B-
0.070 (4.252)
-B-

0.048 (2.916)
*0.307 (18.650)
-B-
-B-
-B-
-B-
-B-
-B-

0.018 (1.093)
-B—
*0.412 (25.029)
69 % **
0.245 (14.884)
-fi-
ne % **
-B-
-B-
-B-
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % RECOVERED
-------
                       TABLE 7.    ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST  12, 1986
SAMPLE 10 NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :

M/C
1,1-DCEENE
1 , 1 -OCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-DCEANE +
2-BUTANONE
1,1,1-TCEANE
CCL4
BDCM
1,2-OCPRANE
T-1.3-DCPRENE
CL3-EENE
BENZENE
1,1,2-TCEANE *
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-OCBZ
1,2-DCBZ
1,4-OCBZ




QUANTIFICATION
LIMIT
(M9/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
E08121007V
E-DUCT
VOST
21.274
DETECTED /

*1.193 (72.474)
-B-
-B-
-B-
0.060 (3.645)
-B-

0.023 (1.397)
*0.521 (31.651)
-B-
-B-
-B-
-B-
0.023 (1.397)

-B-
-B-
-B-
75 % **
0.116 (7.047)
112 % **
-B-
-B-
0.063 | -B-
E08121138V
E-DUCT
VOST
26.659
iMOUNT, pg/TRAIN (CON(

0.586 (21.981)
-B-
-B-
0.046 (1.725)
-B-

-B-
*0.218 (8.117)
-B-
-B-
-B-
0.008 TO. 300)

0.115 (4.314)
0.055 2.063
0.035 1.313)
56 % **
0.072 (2.701)
103 \ **
-B-
-B-
-B-
E08121300V
E-DUCT
VOST
20.909
IENTRATION, M9/TRAIN)

*0.860 (41.131)
-B-
-B-
0.088 (4.209(
-B-

-B-
*0.312 M4.922)
-B-
-B-
-B-
0.050 72.391)

0.214 (10.235)
0.063 3.013)
0.095 4.543)
52 * **
0.086 (4.113)
-B-
54 % **
-B-
-B-
-B-
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE * RECOVERED
-------
                       TABLE 8.   ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST 13, 1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (OSL)
VOST COMPOUNDS :

M/C
1,1-DCEENE
1 , 1 -DCEANE
T-Q.2-DCEENE
CHRLOROFORM
1,2-DCEANE +
2-BUTANONE
1.1.1-TCEANE
CCL4
BDCM
1,2-OCPRANE
T-1.3-DCPRENE
CL3-EENE
BENZENE
1.1,2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-DCBZ
1,2-DCBZ
1,4-OCBZ



QUANTIFICATIOI
LIMIT
(Mg/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063

E0813100W
E-DUCT
VOST
20.055
I
DETECTED
*176.116
-B-
-B-
-B-
3.241
-B-

-B-
*19.845
-B-
E08131136V
E-DUCT
VOST
22.598

AMOUNT. ng/TRAIN (COK
I
*9.042 (400.124)
-B-
-B-
-B-
0.070 (3.098)

-B-
*0.281 (12.435)
-R-
-B- -B-
-B- -B-
-B-
0.997
-B-

*11.468
2.493
2.493
62 % **
2.244
-8-
90 % **
-B-
-B-
-B-
-B-
0.018 (0.797)

*0.150 (6.638)
0.053 12.345)
48 % **
0.040 M.7700
90 % **
-B-
-B-
-B-
i
E08131330V
E-DUCT
VOST
21.466

CENTRATION, pg/TRAIN)
*2.169 (101.044)
-B-
LJ
-B-
U
-B-
0.204 (9.503)
• D _
o
-B-
*0.449 (20.917)
-B-
U
-B-
-B-
-B-
0.038 (1.770)

*0.230 10.715)
0.109 5.078)
0.101 4.705)
50 % **
0.134 (6.242)
76 % **
-B-
-B-
-B-

* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % COVERED
-------
                       TABLE 9.  ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST 14,  1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (OSL)
VOST COMPOUNDS :


M/C
1,1-DCEENE
t,1-DCEANE
T-1.2-DCEENE
CHLOROFORM
1,2-OCEANE +
2-BUTANONE
1,1.1-TCEANE
CCL4
BDCM
1,2-OCPRANE
T-1.3-DCPHENE
CL3-EENE
BENZENE
1,1.2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-DCBZ
1,2-DCBZ
1,4-OCBZ





QUANTIFICATION
LIMIT
(Mg/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E08141015V
E-DUCT
VOST
19.636
E08141206V ! E08141330V
E-DUCT ! E-DUCT
VOST
17.427
I
VOST
19.208

DETECTED AMOUNT, M9/TRAIN (CONCENTRATION, pg/DSCM)
	 	 i 	 L 	
0.332 (19.051)
-B-
-B-
0.070 73.565)

-B-
*0.255 (12.986)
-B-
-B-
-B-
0.024 (1.222)

0.023 (1.171)
-8-
0.110 (5.602)
62 % **
0.116 (5.908)
-B-
112 % **
-B-
-B-
-B-
0.332 (19.051)
-B-
-B-
0.050 (2.869)
-B-

-B-
*0.247 714.173)
-B-
-B-
-B-
0.026 (1.492)
-B-

0.016 (0.918)
0.132 (7.574)
62 % **
0.082 (4.705)
99 % **
-B-
-B-
-B-
0.317 (16.504)
-B-
-B-
0.060 73.124)

-B-
*0.289 (15.046)
-B-
-B-
-B-
0.061 (3.176)

0.017 (0,885)
0.047 2.447)
0.130 6.768)
67 % **
0.094 (4.984)
101 % **
-8-
-B-
-B-
•! I
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % RECOVERED
-------
                       TABLE 10.  ANALYTICAL RESULTS OF VOST SAMPLES ON AUGUST 28,  1986
                     TEST VOID DUE TO LOOSE CONNECTION SUCKING IN SMOKE FUMES FROM  PROBE PULLED
                     INTO ADSORBING TUBE.  (JHL)
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :

M/C
1,1-DCEENE
1 , 1 -DCEANE
T-1.2.DCEENE
CHLOROFORM
1.2-DCEANE +
2-BUTANONE
1,1,1 -TCEANE
C6L4
BDCM
1,2-DCPRANE
T-1.3-DCPRENE
CL3-EENE
BENZENE
1,1,2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-DCBZ
1.2-OCBZ
1,4-DCBZ




QUANTIFICATION
LIMIT
(M9/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063


VOST



VOST

1
DETECTED AMOUNT, M9/TRAIN (CC
_ . -J. J























\


i





]
I


VOST


)NCENTRATION, pg/TRAIN)

























* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE * RECOVERED
-------
                       TABLE 11.  ANALYTICAL RESULTS OF VOST SAMPLES ON SEPTEMBER 3,  1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :


M/C
1,1-DCEENE
1,1-DCEANE
T-1,2,DCEENE
CHLOROFORM
1,2-DCEANE +
2-BUTANONE
1.1.1-TCEANE
CCL4
BDCM
1.2-OCPRANE
T-1,3-DCPRENE
CL3-EENE
BENZENE
1,1,2-TCEANE +
CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1,3-DCBZ
1,2-DCBZ
1,4-OCBZ




QUANTIFICATION
LIMIT
(M9/TRAIN)
0.063
0.0126
0.0126
0.0126
0.0211
0.0253

0.0126
0.0126
0.0211
0.0126
0.0252
0.0126
0.0127
0.0337

0.0127
0.0211
0.0252
0.0127
0.0254
0.063
0.0127
0.063
0.063
0.063
E09030940V
E-DUCT
VOST
20.486

E0903 1200V
E-DUCT
VOST
19.625

E09031330V
E-DUCT
VOST
19.457

DETECTED AMOUNT, pg/TRAIN (CONCENTRATION, pg/TRAIN)

0.084 (4.100)
-B-
-B-
0.081 (3.954)

-B-
0.127 (6.199)
0.025 (1.220)
0.051 (2.490)
0.113 (5.516
-B-

0.075 (3.661)
0.150 (7.322)
64 % **
0.074 f3. 612)
106 % **
— B —
-B-
-B-

0.367 (18.701)
-B-
-B-
0.086 (4.382)

-B-
0.091 (4.637)
0.042 (2.140)
0.073 (3.720)
*0.333 (16.968)
i -B-

0.092 (4.688)
0.170 (8.662)
88 % **
0.134 f6.828)
122 % **
-B-
-B-
-B-

0.185 (9.508)
-B-
-B-
0.175 (8.994)

-B-
0.088 (4.523)
0.018 (0.925)
0.082 (4.214)
0.053 (2.724)
-B-

*0.383 (19.684)
0.204 (10.485)
146 % **
0.097 U.985)
114 % **
-B-
-B-
-B-
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % RECOVERED
-------
                      TABLE  12.  ANALYTICAL RESULTS OF VOST SAMPLES ON SEPTEMBER 4, 1986
SAMPLE ID NUMBER
SAMPLE LOCATION
SAMPLE METHOD
GAS SAMPLE VOLUME (DSL)
VOST COMPOUNDS :

M/C
1 1-DCEENE
1.1-OCEANE
T-1.2.DCEENE
CHLOROFORM
11,2-DCEANE +
• 2-BUTANONE
.1.1 ,1-TCEANE
•CCL4
! nnrM
:1.2-OCPRANE
|T-1,3-DCPRENE
CL3-EENE
BENZENE
;1,1.2-TCEANE +
i CDBM
HEXANE
BROMOFORM
CL4-EENE/ANE
ISO-OCTANE
TOL + HEP
CL-BZ
OCTANE
1 ,3-DCBZ
1 2-DCBZ
1,4-DCBZ




QUANTIFICATION
LIMIT
E09040930V
E-DUCT
VOST
20.032
DETECTED /
(M9/TRAIN) i I
0.063 • 0.568 (28.355)
0.0126 ! -B-
0.0126 0.140 (6.989)
0.0126 -B-
0.0211 ' *0.258 (12.879)
0.0253 -B-

0.0126 . -B-
0.0126 -B-
0.0211 ' -B-
0.0126 i 0.026 (1.298)
0.0252 ; -B-
0.0126 . 0.068 (3.395)
0.0127 0.151 (7.538)
0.0337 -B-
0.0127 0.066 (3.295)
0.0211 -B-
0.0252
0.0127
0.0254
0.063
0.0127
-B-
161 % **
0.078 (3.894)
102 % **
0.063 -B-
0.063 -B-
0.063
-B-
E09041120V
E-DUCT
VOST
21.693
IMOUNT, Mg/TRAIN (CONC

*1.166 (53.750)
-B-
0.037 (1.706)
0.156 (7.191)

-B-
-B-
-B-
-B-
-B-
0.041 (1.890)
0.041 (1.890)
-B-
0.045 (2.074)
-B-
102 % **
0.038 M.752)
100 % **
-B-
-B-
-B-
E09041330V
E-DUCT
VOST
19.650
ENTRATION. pg/TRAIN)

0.059 (3.003)
0.083 (4.224)
0.146 (7.430)

-B-
-B-
-B-
0.016 (0.814)
0.039 (1.985)
0.196 (9.975)
-B-
0.025 (1.272)
134 % **
0.062 T3.155)
100 % **
-B-
-B-
-B-
* -  GREATER THAN CALIBRATION RANGE
** - THESE COMPOUNDS ARE INTERNAL STANDARDS.
B -  BELOW QUANTIFICATION LIMIT
THE NUMBERS REPORTED ARE % RECOVERED
-------
  ACUREX
  Corporation
                                                       Energy & Environmental Division

October 3, 1986                                                  page  ] of 3
Dr. Larry R. Waterland
Program Manager
US EPA Combustion Research Facility  (CRF)
c/o NCTR, Building 45
Jefferson, Arkansas 72079
Subject:          Chloride Analysis Results

Reference:        EPA Contract 68-03-3267


Dear Dr. Waterland:
      This communication summarizes the results of chloride  analyses  performed
on EPA Method 5 impinger catches taken at the CRF between July  8  and
September 4. 1986.  These data are associated with the performance  of the
rotary kiln system during incineration of the following:  Askarel  * Auto Dry;
BROS surface oil; BROS soil; BROS soil + sludge and BROS sludge.

      Measurements of chloride ion concentration were made with a specific ion
electrode, calibrated on each analytical day at three levels which  encompassed
those found in the samples.  Samples are identified as specified  in the CRF
Quality Assurance Project Plan, August 35, 1986.  All values are  reported as
total mg HC1.

                            Sample
                          Identifier             •£ HCL
                         S07081606I1              <3.7

                         S07081606I2              <2.2

                         S07081606I3              <2.1

                         S0709160311              <3.4

                         S07091603I2              <3.7

                         S07091603I3              <3.4

                         S07101325I1              <4.0

                         S07103325I2              <3.7

                         S07101325I3              <3.5
              NCTR. Building 45. Jefferson. AR 72079  (501)541-0004  FAX (501) 536-6446


    555 Clyde Avenue. PO Box 7555. Mountain View. CA 94039 (415) 964-3200 Telex 34-6391  TWX  910-7796593
-------
                                         page 2   o
Sample
Identifier
A07211207I1
A07211207I2
A07281116I1
A0728116I2
A07291404I1
A07291404I2
J22 HCI
9.7
<2.2
14.2
<2.2
24.9
<1.9
A08041319I1             26.3
A08041319I2             <1.8
A08051100I12            10.8
A08071001I12            12.6
S08041324I1             <4.2
S08041324I2             <5.1
S08051105I12            <6.5
S08071008I12            <7.6

A08121004I12            15.8
A08131001I12            21.8
A08141020I12            17.4
S08121002I123           <9.1
S08131000I123           <9.9
S08141015I123           <9.4

S08191150I              <8.8

A08280955I12            <4.8
A09030951I123            7.6
A09040937I123            5.2
S08280945I123           <9.3
S09030950I123           <10.3
S09040930I123           <9.9
-------
                                                                   page  3  of  3
Each batch of impinger collection meduim (0.1N sodium  acetate)  used  was
analyzed and found to contain <10 mg/L chloride,  the detection  limit of  the
analytical method.
Sincerely,
R.W. Ross, II
Senior Chemist
RWR:Sf 048L
CC:  Johannes Lee
     Jerry Lewis
     Sharon King
-------
   kftflV W  SAU««AITH •- 3
    CM*IHM«M or TMI «o*«o
   KENNETH S WOODS
      MICtlOCMT
  SAIL » MUTCHCNS

KICUTIVC VICt- r
VCLMA w «ussei.;_
1ICK
-------
 Mr. Ralph Vocque

 November 14, 1986
 Your #,

 USEPA-CRF
 B07211315
Our #,      Total Metals in Filtrates,

Q-6926     mg/liter Arsenic            < 0.2
            mg/liter Barium             0.58
            mg/liter Cadmium           < o.l
            mg/liter Chromium          0.17
            mg/liter Lead               o.28
            mg/liter Mercury            < o.2
            mg/liter Selenium           < 0.2
            mg/liter Silver              < o.l
Your #,

 USEPA-CRF
 B07281335   *
Our#,

 Q-6927
Your*,

 USEPA-CRF
 B07291645  «
Our #,

 Q-6928
Your #,

 USEPA-CRF
 B08041407  *
Our #,

 Q-6929
Total Metals in Filtrates,

mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium
mg/liter Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Filtrates,

mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium
mg/liter Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Filtrates,
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
Arsenic
Barium
Cadmium
Chromium
Lead
Mercury
Selenium
Silver
                    < 0.2
                    0.43
                    < 0.1
                    0.20
                    0.73
                    < 0.2
                    < 0.2
                    < 0.1
                    < 0.2
                    0.61
                    < 0.1
                    < 0.1
                    1.10
                    < 0.2
                    < 0.2
                    < 0.1
< 0.2
0.30
< 0.1
0.18
2.58
< 0.2
< 0.2
< 0.1
   There were no Solids remaining from filtering the blowdown water.
                         GALBRAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986
 Your #,

USEPA-CRF
B08051325
 Our #,      Total Metals in Filtrates,

Q-6930      mg/liter Arsenic            < 0.2
            mg/liter Barium            o.39
            mg/liter Cadmium          < o.l
            mg/liter Chromium         Q.39
            mg/liter Lead              1.15
            mg/liter Mercury           < 0.2
            mg/liter Selenium          < o.2
            mg/liter Silver             < o.l
                                  Total Metals in Solids,

                                  ppm Arsenic               < 26
                                  ppm Barium                87?
                                  ppm Cadmium              < 26
                                  ppm Chromium             89
                                  ppm Lead                  1008
                                  ppm Mercury               < 26
                                  ppm Selenium              < 26
                                  ppm Silver                 < 26
Your #,

USEPA-CRF
B08071100
Our f,      Total Metals in Filtrates,

Q-6931      mg/liter Arsenic
            mg/liter Barium
            mg/liter Cadmium
            mg/liter Chromium
            mg/liter Lead
            mg/liter Mercury
            mg/liter Selenium
            mg/liter Silver


            Total Metals in Solids,

            ppm Arsenic
            ppm Barium
            ppm Cadmium
            ppm Chromium
            ppm Lead
            ppm Mercury
            ppm Selenium
            ppm Silver
< 0.2
0.29
< 0.1
0.29
0.14
< 0.2
< 0.2
                                                            < 60
                                                            1085
                                                            < 60
                                                            119
                                                            3787
                                                            < 60
                                                            <60
                                                            < 60
                        GALBMAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986
 Your #,

USEPA-CRF
B08121030
Our #,      Total Metals in Filtrates,

Q-6932      mg/liter Arsenic            < 0.2
            ing/liter Barium            o.35
            mg/liter Cadmium          < o.l
            mg/liter Chromium         Q.26
            mg/liter Lead              o.l4
            mg/liter Mercury           < o.2
            mg/liter Selenium          < 0.2
            mg/liter Silver             < o.l
                                 Total Metals in Solids,

                                 ppm Arsenic               < 23
                                 ppm Barium               737
                                 ppm Cadmium             < 23
                                 ppm Chromium            75
                                 ppm Lead                 2723
                                 ppm Mercury              < 23
                                 ppm Selenium              < 23
                                 ppm Silver                < 23
Your #,

USEPA-CRF
B08131030
Our #,      Total Metals in Filtrates,

Q-6933      mg/liter Arsenic
            mg/liter Barium
            mg/liter Cadmium
            mg/liter Chromium
            mgAiter Lead
            mg/liter Mercury
            mg/liter Selenium
            mg/liter Silver


            Total Metals in Solids,

            ppm Arsenic
            ppm Barium
            ppm Cadmium
            ppm Chromium
            ppm Lead
            ppm Mercury
            ppm Selenium
            ppm Silver
< 0.2
0.39
< 0.1
0.31
0.11
< 0.2
< 0.2
< 0.1
                                                            < 35
                                                            1206
                                                            < 35
                                                            66
                                                            4065
                                                            < 35
                                                            < 35
                                                            < 35
                                                            < 35
                        GALBMAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986
 Your #,"

USEPA-CRF
B08281005  *
 Our #,       Total Metals in Filtrates,

Q-6935       mg/liter Arsenic            < 0.2
             mg/liter Barium            0.29
             mg/liter Cadmium          < 0.1
             mg/liter Chromium         0.13
             mg/liter Lead              < 0.1
             mg/liter Mercury           < 0.2
             mg/liter Selenium          < 0.2
             mg/liter Silver             < 0.1
 Your #,

USEPA-CRF
B09031010  *
 Our #,

Q-6936
 Your #,

USEPA-CRF
B09041050 *
 Our #,

Q-6937
 Your #,

USEPA-CRF
B09241100BK *
 Our#,

 Q-6938
Total Metals in Filtrates,

mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium
mg/liter Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Filtrates,

mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium
mg/liter Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Filtrates,
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
mg/liter
Arsenic
Barium
Cadmium
Chromium
Lead
Mercury
Selenium
Silver
                  < 0.2
                  0.65
                  < 0.1
                  0.18
                  < 0.1
                  < 0.2
                  < 0.2
                  < 0.1
                  < 0.2
                  0.30
                  < 0.1
                  0.20
                  < 0.1
                  < 0.2
                  < 0.2
                  < 0.1
0.2
0.1
0.1
0.1
0.1
0.2
0.2
0.1
 * There were no Solids remaining from filtering the blowdown water.
                         OALBRAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986
 Your f,

USEPA-CRF
B07281335SK
 Our #,      Total Metals in Filtrates,

Q-6939      mg/liter Arsenic           < 0.2
            mg/liter Barium            1.64
            mg/liter Cadmium          < 0.1
            mg/liter Chromium         4.73
            mg/liter Lead              11.39
            mg/liter Mercury           12.49
            mg/liter Selenium          < 0.2
            mg/liter Silver             < 0.1
                                  Total Metals in Solids,

                                  ppm Arsenic               < 26
                                  ppm Barium                4771
                                  ppm Cadmium              < 26
                                  ppm Chromium             9733
                                  ppm Lead                  46.41
                                  ppm Mercury               3,58
                                  ppm Selenium              < 26
                                  ppm Silver                 656
 Your #,

USEPA-CRF
B08131030SK
 Our #,      Total Metals in Filtrates,

Q-6940      mg/liter Arsenic
            mg/liter Barium
            mg/liter Cadmium
            mg/liter Chromium
            mg/liter Lead
            mg/liter Mercury
            mg/liter Selenium
            mg/liter Silver


            Total Metals in Solids,

            ppm Arsenic
            ppm Barium
            ppm Cadmium
            %  Chromium
            % . Lead
            ppm Mercury
            ppm Selenium
            ppm Silver
< 0.2
< 0.1
< 0.1
< 0.1
32
3.69
< 0.2
< 0.1
                                                            131
                                                            108
                                                            < 11
                                                            3.83
                                                            38.67
                                                            571
                                                            < 11
                                                            145
                        GALBNAITH LABORATORIES. INC.
-------
Mr. Ralph Vocque

November 14, 1986
Your #,
Our #,
USEPA-CRF           Q-6941
70828(09(3,4) 1200
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310.
            mg/liter Arsenic
            mg/liter Barium
            mg/liter Cadmium
            mg/liter Chromium, Total
            mg/liter Lead
            mg/liter Mercury
            mg/liter Selenium
            mg/liter Silver


            Total Metals in Kiln Ash,

            ppm Arsenic
            ppm Barium
            ppm Cadmium
            ppm Chromium
            ppm Lead
            ppm Mercury
            ppm Selenium
            ppm Silver
                          < 0.1
                          < 0.1
                          < 0.1
                          < 0.1
                          0.12
                          < 0.1
                          < 0.1
                          < 0.1
                                                            < 2
                                                            632
                                                            < 2
                                                            113
                                                            796
                                                            < 2
                                                            < 2
                                                            < 2
Your #,
USEPA-CRF
T08141200
Our#,
Q-6942
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310,
mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium, Total
mg/liter-Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Kiln Ash,

ppm  Arsenic
ppm  Barium
ppm  Cadmium
ppm  Chromium
ppm  Lead
ppm  Mercury
ppm  Selenium
ppm  Silver
< 0.1
0.43
                                                              0.1
                                                              0.1
                                                              0.1
                                                              0.1
                                                              0.1
                                                              0.1
                                                            < 2
                                                            504
                                                            < 2
                                                            66
                                                            228
                                                            < 2
                                                            < 2
                                                            < 2
                        GALBRAITH LABORATORIES. INC.
-------
Mr. Ralph Vocque

November 14, 1986
Your #,
USEPA-CRF
T08131200
Our #,


Q-6943
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310.
mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium, Total
mg/liter Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver


Total Metals in Kiln Ash,

ppm Arsenic
ppm Barium
ppm Cadmium
ppm Chromium
ppm Lead
ppm Mercury
ppm Selenium
ppm Silver
< 0.1
0.43
< 0.1
< 0.1
< 0.1
< 0.1
< 0.1
< 0.1
                                                            < 2
                                                            983
                                                            < 2
                                                            97
                                                            382
                                                            < 2
                                                            < 2
                                                            < 2
Your #,
 USEPA-CRF
 T08071200
Our#,


Q-6944
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310,
mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium, Total
mg/liter-Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Kiln Ash,

ppm Arsenic
ppm Barium
ppm Cadmium
ppm Chromium
ppm Lead
ppm Mercury
ppm Selenium
ppm Silver
  0.1
  ,99
  0.1
  0.1
  0.1
  0.1
  0.1
  0.1
                                                            < 2
                                                            844
                                                            < 2
                                                            95
                                                            489
                                                            < 2
                                                            < 2
                                                            <2
                        GALBKAITH LABORATORIES. INC.
-------
  Mr. Ralph Vocque

  November 14, 1986
  Your #, -
USEPA-CRF
T08051200
 Our #,
Q-6U45
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310.
mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium, Total
mg/liter Lead
mg/liter Mercury
mg/liter Selenium
mg/liter Silver


Total Metals in Kiln Ash,

ppm Arsenic
ppm Barium
ppm Cadmium
ppm Chromium
ppm Lead
ppm Mercury
ppm Selenium
ppm Silver
< 0.1
0.10
  0.1
  0.1
  0.1
  0.1
  0.1
  0.1
                                                            < 2
                                                            296
                                                            < 2
                                                            192
                                                            1825
                                                            < 2
                                                            < 2
                                                            < 2
 Your #,
USEPA-CRF
T08041200
 Our ff,
Q-6946
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310,

mg/liter Arsenic           < o.l
mg/liter Barium           o.26
mg/liter Cadmium         < o.l
mg/liter Chromium, Total  < o.l
mg/liter-Lead             < o.l
mg/liter Mercury          < o.l
mg/liter Selenium         < o.l
mg/liter Silver            < o.l

Total Metals in Kiln Ash,

ppm Arsenic              < 2
ppm Barium               498
ppm Cadmium             < 2
ppm Chromium            94
ppm Lead                 408
ppm Mercury              < 2
ppm Selenium             < 2
ppm Silver                < 2
                        GALBHAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986
Your #,
Our #,
USEPA-CRF           Q-6947
707(21,28,29) 1200
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310,

mg/liter Arsenic            < 0.1
mg/liter Barium            0.33
mg/liter Cadmium          < 0.1
mg/liter Chromium, Total   < 0.1
mg/liter Lead              0.23
mg/liter Mercury           < 0.1
mg/liter Selenium          < 0.1
mg/liter Silver             < 0.1
                                 Total Metals in Kiln Ash,

                                 ppm Arsenic               < 2
                                 ppm Barium                121
                                 ppm Cadmium              < 2
                                 ppm Chromium             1088
                                 ppm Lead                  2161
                                 ppm Mercury               < 2
                                 ppm Selenium              < 2
                                 ppm Silver                 < 2
                        GALBRAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986


 Your #,

USEPA-CRF
F0828(09)(3,4) 1200
 Our #,      Total Metals in Feed,

Q-6949      ppm Arsenic               < 1
            ppm Barium               23
            ppm Cadmium             < 5
            ppm Chromium            12
            ppm Lead                 46
            ppm Mercury              < 1
            ppm Selenium              < 1
            ppm Silver                 < 5
                                  Ultimate Analysis,

                                  % Carbon
                                  % Hydrogen
                                  % Nitrogen
                                  % Sulfur
                                  % Chlorine
                                  % Oxygen
                                      0.96
                                      11.12
                                      0.038
                                      0.99
                                      0.0094
                                      81.78
                                  Based on Leachate of Feed by EP Toxicity
                                  Test Procedure » 1310,
                                  mg/liter Arsenic
                                  mg/liter Barium
                                  mg/liter Cadmium
                                  mg/liter Chromium, Total
                                  mg/liter Lead
                                  mg/liter Mercury
                                  mg/liter Selenium
                                  mg/liter Silver
                                      0.19
                                      < 0.1
                                        0.
                                        0.
                                        0.
< 0.1
< 0.1
< 0.1
                                      < 0.1
                        GALBRAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November 14, 1986
 Your #,

USEPA-CRF
F08(4,5,7) 1200
 Our #,      Total Metals in Feed,

Q-6950      ppm Arsenic               < i
            ppm Barium               744
            ppm Cadmium             < i
            ppm Chromium             55
            ppm Lead                 756
            ppm Mercury               < i
            ppm Selenium              < i
            ppm Silver                 < 5
                                  Ultimate Analysis,

                                  % Carbon
                                  % Hydrogen
                                  % Nitrogen
                                  % Sulfur
                                  % Chlorine
                                  % Oxygen
                                      11.35
                                      4.60
                                      0.099
                                      0.38
                                      0.037
                                      25.03
                                  Based on Leachate of Feed by EP Toxicity
                                  Test Procedure # 1310,

                                  mg/liter Arsenic            < 0.1
                                  mg/liter Barium            0.12
                                  mg/liter Cadmium          < 0.1
                                  mg/liter Chromium, Total   < 0.1
                                  mg/liter Lead              0.46
                                  mg/liter Mercury           < 0.1
                                  mg/liter Selenium          < 0.1
                                  mg/liter Silver             < 0.1
                         GALBRAITH LABORATORIES. INC.
-------
Mr. Ralph Vocque

November 14, 1986
  Your f,
USEPA-CRF
T08121200
  Our #,
Q-8049
Based on Leachate of Kiln Ash by EP Toxicity
Test Procedure # 1310,
mg/liter Arsenic
mg/liter Barium
mg/liter Cadmium
mg/liter Chromium, Total
mg/liter-Lead '
mg/liter Mercury
mg/liter Selenium
mg/liter Silver

Total Metals in Kiln Ash,

ppm  Arsenic
ppm  Barium
ppm  Cadmium
ppm  Chromium
ppm  Lead
ppm  Mercury
ppm  Selenium
ppm  Silver
0.1
0.1
0.1
0.1
0.1
0.1
0.1
0.1
                                                            < 2
                                                            738
                                                            < 2
                                                            99
                                                            767
                                                            < 2
                                                            < 2
                                                            < 2
                       GALBRAITH LABORATORIES. INC.
-------
 Mr. Ralph Vocque

 November. 14, 1986
 Your #,

USEPA-CRF
F08U2,13,14) 1200
Our #,      Total Metals in Feed,

           ppm Arsenic               n
           ppm Barium               823
           ppm Cadmium             4
           ppm Chromium            65
           ppm Lead                 1034
           ppm Mercury              < 1
           ppm Selenium              < i
           ppm Silver                 < 5
                                  Ultimate Analysis,

                                  % Carbon
                                  % Hydrogen
                                  % Nitrogen
                                  % Sulfur
                                  % Chlorine
                                  % Oxygen
                                     13.13
                                     4.67
                                     0.11
                                     0.43
                                     0.058
                                     32.29
                                 Based on Leachate of Feed by HP Toxicity
                                 Test Procedure #  1310,

                                 mg/liter Arsenic            < 0.1
                                 mg/liter Barium            0.30
                                 mg/liter Cadmium          < 0.1
                                 mg/liter Chromium, Total    < 0.1
                                 mg/liter Lead               0.12
                                 mg/liter Mercury            < 0.1
                                 mg/liter Selenium           < 0.1
                                 mg/liter Silver              < 0.1
                        GALIRAITH LABORATORIES. INC.
-------
  Mr. Ralph Vocque

  November 14, 1986


  Your #,

 USEPA-CRF
  F07(21,28,29) 1200
 Our #,

Q-8050
Total Metals in Feed,

ppm  Arsenic            2
ppm  Barium             1035
ppm  Cadmium           < 10
ppm  Chromium          45
ppm  Lead               2888
ppm  Mercury            < i
ppm  Selenium           < i
ppm  Silver              < 10
                                   Ultimate Analysis,

                                   % Carbon              54.53
                                   % Hydrogen             10.85
                                   % Nitrogen             0.085
                                   % Sulfur                o.69
                                   % Chlorine             o.lO
                                   % Oxygen              29.87

                                   Based on Leachate of Feed by EP Toxicity
                                   Test Procedure # 1310,

                                   mgAiter Arsenic         < o.l
                                   mg/liter Barium         < o.l
                                   mg/liter Cadmium       < o.l
                                   mg/liter Chromium, Total< o.l
                                   mg/liter Lead           < o.l
                                   mg/liter Mercury        < 0.1
                                   mg/liter Selenium       < o.l
                                   mg/liter Silver          < 0.1
 Sincerely yours,

 GALBRATTH LABORATORIES, INC.
'Gail R. Hutchenk
 Exec. Vice-President

 GRH:sc
                         GALBRAITH LABORATORIES. INC.
-------
                                        EPA/540/2-89/026
      SUPERFUND TREATABILITY
            CLEARINGHOUSE
               Document Reference:
Shirco Infrared Systems, Inc. "Abstract On-site Incineration Testing of Shirco Infrared
  Systems Portable Demonstration Unit-Contaminated Soils Treatability Study."
    Prepared for Dakonta Gmbh Hamburg and Ingelheim, West Germany, 3 pp.
                     June 1987.
              EPA LIBRARY NUMBER:

            Superfund Treatability Clearinghouse -EWQD
-------
                SUPERFUND TREATABILITY CLEARINGHOUSE ABSTRACT
 Treatment  Process:

 Media:

 Document Reference:
 Document  Type:

 Contact:
Site Name:
Location of Test:
Thermal Treatment - Infrared

Soil/Generic

Shirco Infrared Systems, Inc.   "Abstract On-site
Incineration Testing of Shirco Infrared Systems
Portable Demonstration Unit-Contaminated Soils
Treatability Study."  Prepared for Dakonta Gmbh
Hamburg and Ingelheim, West Germany,  3 pp.  June
1987.

Abstract

Scott P. Berdine
Ecova Corporation (formerly Shirco)
1415 Whitlock Lane
Suite 100
Carrollton, TX  7506
214-404-7540

Boehringer's Lindane Facility  (Non-NPL)

West Germany
BACKGROUND;  In August of  1986, Shirco was contracted by Dekonta GmbH, a
West German hazardous waste  treatment company, to perform treatability
studies at one of  the largest dioxin-contaminated sites in the world.  The
Shirco Infrared process was  selected by Dekonta after a two year study and
evaluation of existing and emerging technologies for soils decontamination.
    The West German hazardous waste management regulations, which are
established and enforced on  a state by state basis, differ somewhat from
those in the US.  Transportation of dioxin-bearing wastes, for instance, is
strictly prohibited.  Hence, mobile technologies offer distinct advantages
for multiple site remediation.
OPERATIONAL INFORMATION;  Tests were conducted using the Shirco Portable
Demonstration Unit during  the months of November 1986 and February 1987.
Over 3000 kg of contaminated soil were processed in 100 hours of testing.
Various operating condition's including soil contaminant level, feed rate,
primary chamber temperature  and residence time, co-flow and counterflow
operation, and gas atmosphere (air vs. nitrogen) were tested to determine
the effect on soils decontamination levels and exhaust gas emissions.  The
organic contaminants in the  soils included dioxins, furans, chlorobenzenes,
chlorophenols, 2,4,5-T, and  hexachlorocyclohexanes.  Contaminant concen-
trations on soils ranged from 4 to 7500 ppb for dioxins, 3 to 5700 for
furans and from 33 to 16,600 ppm for chlorobenzenes.  No QA/QC data was
presented.
PERFORMANCE;  Results of approximately 20 tests indicate exhaust gas con-
centrations of 2,3,7,8 TCDD  from less than 20 pg/m  to 88-pg/m , whereas
field "blanks" showed concentrations ranging from 33 pg/m  to 73 pg/m  .
3/89-47                                              Document Number:  EWQD

   NOTE:  Quality assurance of data may not be appropriate for all uses.
-------
The  source  of  the high  blank  concentrations is currently under investi-
gation,  therefore,  the  validity of  the reported values cannot be estab-
lished at present.  A brief summary of the data is on the attached table.
CONTAMINANTS;

Analytical data  is  provided  in  the  treatability study report,
breakdown of contaminants by  treatability group is:
                                The
Treatability Group

WOl-Halogenated Aromatic
     Compounds

W02-Dioxins/Furans/PCBs
CAS Number       Contaminants
108-90-7         Total Chlorobenzenes
HEPCDD           Total Heptachlorodibenzo-
                  dioxin
OCDF             Octachlorodibenzofurans
OCDD             Octachlorodibenzodioxin
PCDD             Total Pentachlorodibenzo-
                  dioxin
HEXCDD           Total Hexachlorodibenzo-
                  dioxin
TCDF             Total Tetrachlorodibenzo-
                  furan
1746-01-6        2,3,7,8-Tetrachlorodibenzo-
                  p-dioxin (TCDD)
TCDD             Total Tetrachlorodibenzo-
                  dioxins
HEPCDD           Total Heptachlorodibenzo-
                  dioxin
PCDF             Total Pentachlorodibenzo-
                  furans
HEXCDF           Total Hexachlorodibenzo-
                  furans
HEPCDF           Total Heptachlorodibenzo-
                  furans
NOTE:  This is a partial listing of data.
       information.
            Refer to the document for more
3/89-47                                              Document Number:  EWQD
   NOTE:  Quality assurance of data may not be appropriate for all uses.
-------
                                                   TABLE 1
VEST GERMANY DIOXIN TEST SUMMARY
SOIL FEED AND ASH QUALITY DATA
DIOXINS
SOIL
IDENTIFICATION
2 Feed (ppb)
2 Ash
2 Feed (ppb)
2 Ash (ppt)
1 Feed (ppb)
1 Ash (ppt)
4 Feed (ppb)
4 Ash (ppt)
6 Feed (ppb)
6 Ash (ppt)
2 Feed (ppb)
2 Ash (ppt)
1 Feed (ppb)
1 Ash (ppt)
2,3,7,8
TCDD
6.7
ND
4.4
ND
24
ND
38
ND
34
ND
NOT
NOT
TCDD PCDD
6.7
ND
6.0
ND
33
ND
42
ND
38
ND
YET
YET
4.0
ND
18
ND
36
ND
41
ND
27
ND
AVAILABLE
AVAILABLE
HXCDD
17
ND
121
5.1
115
ND
109
17
90
15


HPCDD
50
ND
340
18
292
15
280
6.8
238
9.2


OCDD
202
ND
2301
60
7458
50
5940
15
5160
20


TCDF
ND
12
15
33
52
67
125
49
70


PCDF
3.1
ND
53
27
41
45
44
111
34
54


FURANS
HXCDF
9.4
ND
58
20
54
26
129
58
80
24



HPCDF
14.6
ND
98
24
174
23
128
34
106
13



OCDF
35.3
ND
358
12
3151
12
5660
12
4700
6.2


CHLOROBENZENES
58,000
1,200
169,000
9,600
242,000
4,700
33,000
16,000
40,000
4,600
16,612,000
11,000
16,526,000
7,400
NOTE:  ND = Not Detectable

Primary Chamber Temperature:
Solid Phase Residence Time:
1550-1650UF
15 minutes
                          Detection Limits:   a.   2,3,7,8 TCDD = 1-2 ppt
                                                 b.   All others = 5 ppt
3/89-47
   Document Number:

fnr all
                                                                   EWQD
-------
                                                          7-7
   U- Systems
Incorporated
                                    ABSTRACT


                          ON-SITE INCINERATION TESTING


                                        OF


              SHIRCO  INFRARED SYSTEMS  PORTABLE DEMONSTRATION UNIT
                      CONTAMINATED SOILS TREATABILITY  STUDY


                              HAMBURG,  WEST GERMANY

                             INGELHEIM,  WEST GERMANY
      1195 Empire Central

      Dallas, Texas 75247-4301

      '214] 630-7511
-------


In August of 1986, Shirco was contracted by Dekonta GmbH, a West
German hazardous waste treatment company, to perform treatability
studies at one of the largest dioxin-contaminated sites in the
world.  The Shirco Infrared process was selected by Dekonta after
a two year study and evaluation of existing and emerging
technologies for soils decontamination.

The West German hazardous waste management regulations, which are
established and enforced on a state by state basis, differ
somewhat from those in the US.  Transportation of dioxin-bearing
wastes, for instance, is strictly prohibited.  Hence, mobile
technologies offer distinct advantages for multiple site
remediation.  Notable regulations for hazardous waste
incineration in the State of Hamburg include the following stack
gas limitations:

     Particulate Matter:                 30 mg/dscm
     CO:                                100 mg/dscm
     SO :                               100 mg/dscm
     HC1:                                50 mg/dscm
     TOC:                                20 mg/dscm
     2,3,7,8 TCDD:                      100 pg/dscm

Required soils treatment levels include a 1 ppb 2,3,7,8  TCDD
standard; other organic compounds must be reduced to levels
compatible with US EPA "listing" guidelines.

Note that the stack gas standards do not include a destruction
and removal efficiency  (ORE) requirement.  Rather, the  standard
stipulates a single maximum exhaust gas  concentration which must
be satisfied regardless of feedstock concentration or  feed rate.
This "zero" emission  standard  (which also affects byproduct
emissions from  chemical manufacturing  facilities) along with  the
transportation  prohibition for  dioxin-bearing  wastes and public
and political pressure, resulted  in the  closure  of Boehringer's
lindane production facility  in  Hamburg.  This  site,  with an
estimated 80,000  cubic meters  of  dioxin-contaminated soil, was
the focal point of this treatability study.

Tests  were  conducted  using the  Shirco  Portable Demonstration  Unit
during the  months of  November,  1986 and  February,  1987.  Over
3000 kg of  contaminated soil  was  processed  in  100  hours of
testing.  Various operating  conditions including soils
contaminated  level,  feed'rate,  primary chamber temperature and
residence time,  co-flow and  counterflo**--operation,  and gas
atmosphere  (air vs.  nitrogen)  were tested-tajdetermine the effect
on soils decontamination  levels and  exhaust gas emissions.  The
organic contaminants in the  soils included dioxins,  furans,
 chlorobenzenes,  chlorophenols,  2,4,5-T,  and
 hexachlorocyclohexanes.   A brief summary of the soils
 decontamination data is presented in the attached table.
-------
Results of approximately 20 tests indicate exhaust gas
concentrations of 2,3,7,8 TCDD from less than 20 pg/m3 to 88
pg/m3 / whereas field "blanks" showed concentrations ranging from
33 pg/m3 to 73 pg/m3.  The source of the high blank
concentrations is currently under investigation, therefore, the
validity of the reported values cannot be established at present.

Upon completion of the Hamburg test program, the unit was moved
to Ingelheim, West Germany to continue soils treatability tests
at Boehringer's active facility.  Three test series were
conducted during the months of March, May and June, 1987.   A
final report for both the Hamburg and Ingelheim test  programs
will be issued upon  completion of all analytical work.
-------
                                        WEST  GElttlANY  DIOXIN  TEST  SUWtARY
                                          SOIL FEED AiND ASH QUALITY  DATA

                                             pioxiti;

"Ill IDENTIFICATION
b-2 Feed (ppb)
R-2 Ash (ppt)
..-2 Feed (ppb)
A-2 Ash (ppt)
•1 Feed (ppb)
F-i Ash (ppt)
4 Feed (ppb)
n-4 Ash (ppt)
6 Feed (ppb)
6 Ash (ppt)
n reed (ppb)
5h (ppt)
D-l Feed (ppb)
I Ash (ppt)
1 n -7
i,o,/.
Trpp
6.7
ND
4.4
ND
24
ND
38
ND
34
ND
NOT YET

NOT YET

a
TCPD FCPP HOP !!PCPP OCPD TCDF FCPF IIKCDF HPCPF OCDF
6.7 4.0 17 50 202 -- 3.1 3.4 14.6 35.3 5B,OOn
ND ND ND ND 73 ND ND ND (ID ND 1,100
6.0 18 121 340 2301 12 53 58 38 353 163, M
ND ND 5.1 10 60 15 27 20 24 12 'j.GOu
33 36 115 2)2 7458 33 41 54 174 3151 242,000
NO ND ND 15 50 52 45 26 23 12 4,70'.i
42 41 109 260 5940 67 44 129 128 5660 33,000
ND ND 17 6.8 15 125 111 58 34 12 16,00u
38 27 30 233 5160 43 34 80 106 4700 40,000
ND ND 15 3.2 20 70 54 24 13 6.2 4,600
AVAILABLE 16,G12,»uO
11,000
AVAILABLE lE.SL&.i'iiQ
7,40tj
NOTE;
    ND = Not Detectable
    Detection Limits:
    i.  2,3,7,8 TCD3 =  1-2  ppt
    h.   All others  =  5 ppt

    Primary Chdfflber Teaperature:  1550-1G50  F
    Solid Phase Residence Ti»e:   15  Minutes
-------
                                      EPA/540/2-89/025
     SUPERFUND TREATABILITY
           CLEARINGHOUSE
              Document Reference:
Ogden Environmental Services, Inc. "BOAT Treatabiiity Data for Soils, Sludges and
 Debris From the Circulating Bed Combustion (CBC) Process." Technical report
            prepared for U.S. EPA. 31 pp. June 1987.
             EPA LIBRARY NUMBER:

          Super-fund Treatabiiity Clearinghouse - EWHC
-------
                SUPERFUND TRKATABILITY CLEARINGHOUSE ABSTRACT
 Treatment Process:


 Media:

 Document  Reference:
 Document  Type:

 Contact:
 Site Name:
Location  of Test:
Thermal Treatment - Circulating Bed Combustion
(CBC)

Soil/Clayey

Ogden Environmental Services, Inc.  "BOAT Treat-
ability Data for Soils, Sludges and Debris From the
Circulating Bed Combustion (CBC) Process."
Technical report prepared for U.S. EPA. 31 pp.
June 1987.

Memo and Conference Paper

Major Terry Stoddart
U.S. DOD/AFESC
Bldg 1117
Tyndall Air Force Base, FL  32403
904-283-2949

Circulating Bed Combustion Demonstration Facility
(Non-NPL)

California
BACKGROUND:  The  two  papers  provide  a general overview of  the Ogden
circulating  bed combustion and summary data or  both PCB  laden soils  for
EPA-TSCA and a test on RCRA  liquid organic wastes  for the  California Air
Resources Board (GARB).  This abstract will discuss the  results of the PCB
test, which  was planned, monitored and approved  by the EPA.
OPERATIONAL  INFORMATION;  The primary CBC components are the combustion
chamber, hot cyclone  collector,  flue gas cooler, baghouse, and stack.
Auxiliary systems  include feeders (solids, liquids, sludges), forced-draft
and induced-draft  fans, ash  conveyer, compressed air, cooling tower, and
building ventilation.  Operating parameters, schematic diagram and cost
estimates are provided.
    Atmospheric primary air  is pumped into the lower portion of the
combustion chamber where the bed material is fluidized by  turbulent  mixing
of the air and solids.  Larger solids gravitate downward to form a more
dense fluidized bed in the lowest combustor zone.  The forced-draft  primary
air carries  smaller solids up to the top of the combustor.  Secondary air
is supplied  to various locations in  the combustion chamber to ensure
complete combustion and minimize formation of nitrogen oxides (NO ).
    Auxiliary fuel and pressurized contaminated soil feed are individually
introduced into the lower combustion chamber.  Capability also exists to
feed liquid wastes.  Dry limestone sorbent is added to control gaseous
emissions of sulfur, phosphates, chlorines, or other halogens.
    Elutriated solids are separated  from the flue gas by a hot cyclone and
reinjected into the lower combustor  using a proprietary non mechanical
seal.   Injection,  burning and reaction of fuel, contaminated soil feed,
3/89-46                                              Document Number:  EWHC
   NOTE:  Quality assurance of data nay not be appropriate for all uses.
-------
 sorbent,  and ash components are the  inputs  and  outputs  of  a  continuing
 chemical  process which destroys the  hazardous wastes.
     A trial burn of PCB-contaminated soils  was  completed in  GA Technologies
 transportable Circulating Bed  Combustor  (CBC).   Over 4000  pounds  of  soil
 containing IK PCB were treated in three  identical  4-hour runs at  1800°  F.
 The  sampling and analysis and  the resulting data were obtained in
 accordance with  the QA/QC protocol of EPA.   Third  party sampling  and
 analysis  contractors were used (along) with on-site and in-lab observation
 by EPA.
 PERFORMANCE:   Destruction and  removal efficiencies (DREs)  were greater  than
 99.9999%  and PCB levels in combustor ash were less than 200ppb (see
 Table 1).   No chlorinated dioxins or furans were detected  in the  stack  gas,
 bed  ash,  or fly  ash.   In addition, no significant  concentrations  of  the
 Products  of Incomplete Combustion (PICs) were detected. Combustion
 efficiencies were greater than 99.9%,  with  CO concentrations less than  50
 ppm  and NO  concentrations less than 75  ppm.  Particulate  emissions  were
 generally below  0.08 grain/dscf and  HCL  emissions were  maintained below 4.0
 Ib/hr by  introducing limestone directly  into the combustor.   It is noted
 that  PCB  test data led to the  first  TSCA permit  for transportable PCB
 incinerator operation in all 10 EPA  regions.

 CONTAMINANTS:

 Analytical data  is provided in the treatability  study report.  The
 breakdown  of  the contaminants  by treatability group is:

 Treatability  Group             CAS Number        Contaminants

 W02-Dioxins/Furans/PCBs         1336-36-3         Total  PCBs
3/89-46                                              Document Number:  EWHC
   NOTE:  Quality assurance of data Bay not be appropriate for all uses.
-------
                                       TABLE 1
PCB TRIAL
Parameter
Test Duration, hr
Operating Temperature, F
Soil Feed Rate, Ib/hr
Total Soil Feed, Ib
PCB Concentration in Feed.
ORE Z
PCB Concentration
- Bed Ash, ppm
- Fly Ash, ppm
Dioxin/Furan Concentration
- Stack Gas, ppm
- Bed Ash, ppm
- Fly Ash, ppm
Combustion Efficiency, %
Acid Gas Release, Ib/hr
Particulate Emissions,
grain/set (dry)
Excess Oxygen, %
CO , ppm
co2, %
N0x, ppm
BURN OPERATIONAL
TSCA
Requirement
4
-
-
-
ppm
>99.9999

<2
<2

-
-
-
>99.9
<4.0

<0.08
>3.0
-
-
—
DATA AND TEST RESULTS

1
4
1800
328
1592
11,000
99.999995

0.0035
0.066
i
ND
ND
ND
99.94
0.16
o
0.095^
7.9
35
6.2
26
Test Number
2
4
1800
412
1321
12,000
99.999981 99.

0.033
0.0099

ND
ND
ND
99.95
0.58

0.043
6.8
28
6.0
25

3
4
1800
324
1711
9,800
999977

0.186
0.0032

ND
ND
ND
99.97
0.70

0.0024
6.8
22
7.5
76
2 ND » Not Detected
Note:  This is a partial listing of data.
       information.
Refer to the document for more
3/89-46                                              Document Number:  EWHC

   NOTE:  Quality assurance of data may not be appropriate for all uses.
-------
OGDEN  ENVIRONMENTAL

SERVICES,  INC.
                                                                        <^9S^^
POST OFFICE BOX 85178            10955 JOHN JAY HOPKINS DRIVE                    -"• -
SAN DIEGO. CALIFORNIA 92138-5178      SAN DIEGO, CALIFORNIA 92121
HAROLD R DIOT
DIRECTOR SALES AND MARKETING
(6'9) 455-2383
                                                   June 3,  1987
          Mr. James Antizzo
          U.S. EPA ( Mail  Code WH-548E)
          401 M Street, S.W.
          Washington, D.C. 20006

          Dear Mr. Antizzo:

          The enclosed abstract and package of information is sent to you  in response
          to the Agency's  need for treatability data for soils  and debris to use in
          establishing BOAT  standards  under the land disposal  restrictions program.
          We are pleased to  respond to this need as stated in a May 18, 1987 letter
          to Mr. Richard  Fortuna of the  Hazardous  Waste Treatment Council  from
          Mr. Bill Hanson, Acting Chief, Site Policy and Guidance Branch.

          We think that the  attached Abstract and brief answers  to  the "TREATABILITY
          STUDY ATTACHMENT"  reflect the excellent performance of our Circulating Bed
          Combustion  technology  and  the  responsible  and  precise  controls  and
          standards of the Agencies involved in our test work.

          We look forward  to supplying any additional information.  Please call  me at
          (619) 455-2383  or  Derrell  Young  at  (619) 455-3045  if you have any
          questions.
                                                   Sincerely,
                                                   Harold R. Diot
         HRDrmat
         Enclosure
         cc:  Richard Fortuna, Hazardous  Waste Treatment Council
-------
                                 ABSTRACT
            BOAT TREATABTITY DATA FOR SOILS, SLUDGES AND DEBRIS
                                 FROM THE
                 CIRCULATING BED COMBUSTION (CBC) PROCESS
                               June 3, 1987
      The CBC has demonstrated its effective destruction of hazardous  and
toxic compounds in soils, sludges and liquids.   These  demonstrations have
been done in tests  in commercial size  equipment in a facility  recognized  as
one of the  leading  fluid bed research centers in the world.   There  have
been over 5000 hours  of testing logged in this  facility.  The key tests
discussed below represent only a small sample  of the data available.

      The two key tests discussed here and in  the attached brief answers  to
the "TREATABILITY STUDY ATTACHMENT" include a  test  on PCS for  EPA-TSCA and
a test on RCRA  compounds for the California Air Resources  Board (CAR.B).
Both of these tests were planned, monitored and  approved by the  respective
agencies.   The sampling and analysis  and the   resulting data obtained was
gained under the QA/QC protocols of these agencies. Third party sampling
and  analysis contractors  were  used  under with on-site  and  in-lab
observation by these  agencies.   The PCB  test  data  led  to  the first  TSCA
permit for  transportable PCB incinerator  operation  in  all  10  EPA regions.
The CARB data  (along  with the PCB and other  test data) have  formed the
basis of the "operating boundary" permit conditions for the  RCRA  RD&D
permit given by EPA Region IX for the facility.

      Some major points regarding the data:

      o  The PCB tests  were done on actual site soils (clay-like,  rocky
         material).

      o  Greater than  99.9999Z  DRE  was obtained on PCB and no dioxin or
         furan was  detected and ash was well below TSCA requirements.

      o  FICs were studied  to  the extent that all  peaks in the National
         Bureau of  Standards Mass Spectral library were quantitated.

                                     1
-------
o  PICs have  been related  to continuously monitored  CO and  HC
   emissions.
-------
                             TREATABILITY  STUDY
                                 ATTACHMENT
 1.   Facility  identification, description, and waste characteristics.

 1.1.   Identification

       Ogden Environmental Services, Inc.  (OES)
       Circulating Bed Combustion  (CBC) Demonstration Facility
       10955 John J. Hopkins Drive
       San Diego, CA 92121

       EPA Permit Number:  CAD 981613789

 1.2.   Description

       A CBC thermal  destruction facility including all auxiliary hardware
 for  solids, liquids or sludge waste treatment are instrumented specifically
 for  rigorous  data collection.   A schematic  and  photographs  of the  facility
 are  shown in  Figures 1.2-1, 1.2-2, and 1.2-3.

       This CBC is a  transportable treatment unit with a 2 million  Btu/hour
 thermal rating*.  The  transportable CBC  has  a  TSCA permit  for PCS soils
 treatment in  all  10  EPA regions.  This CBC facility  also has  an EPA-RCRA
 Research, Development and Demonstration  (RDD) permit  for test work on RCRA
waste.  The waste characteristics tested  already  and allowed to be tested
 by the EPA RDD permit are described in Section  1.3 below.
      OES  provides  full  waste  thermal  destruction services  with
      transportable CBCs up to  10 million Btu/hour and with fixed CBCs up
      to over 50 million Btu/hour.
-------
                                                                 toni me
                                                                 •til* out  ii'fMi
                                                                        mviion
KIMII

HIM
                   Fig.  1.2-1.   Schematic  of OES 16-in. pilot-scale  CBC
-------
                  840311-3C
  Fig.  1.2-2.    OES 16-in. pilot-scale circulating bed combustor
                 •S0238-19C
Fig. 1.2-3.    Pilot-scale CBC control console  and data acquisition
-------
1.3.  Waste Characteristics

1.3.1.  Hazardous Wastes Already Tested* in CBC

      o  Soil containing up to:
         -  12,000 ppm PCB (arochlor 1260)
            2,100 ppm 1,2,A trichlorobenzene
         -  350 ppb total furans (estimated)
            7 ppb total dioxins  (estimated)

      o  Liquids containing:
         -  Freon 113
            Carbon tetrachloride
         -  Hexachlorobenzene
         -  Ethylbenzene
            Xylene                                                      ~~
         -  Trichlorobenzene
         -  Toluene
            Sulfur hexafluoride

1.3.2.  Hazardous Wastes Allowed for CBC Tests  by EPA ROD  Permit

      All RCRA wastes listed  in  40 CFR,  number  261,  except:

      1)   F020, F021, F022, F023, F026, F027, F028 wastes (specific dioxin
          and furan compounds) with a concentration  of 1 ppm or higher.

      2)   Wastes with a concentration of greater than 1000 ppm mercury (Hg,
          lead (Pb), arsenic  (AS),  barium  (Ba),  cadmium  (Cd), chromium
          (Cr),  selenium (Se), or silver (Ag).
     Successful test  demonstration work on many other materials  not listed
     as  hazardous  has been done  including:   aluminum smelter potliners,
     refuse derived fuels, high sulfur  coals,  etc.
-------
       3)   Wastes with a PCB  content  of  50  ppm or greater, (only if the
           Permittee's TCCA permit to burn PCB's is no longer valid .  .  .
           note this permit allows up  to  9,800 ppm PCB soils).

       4)   Chemical warfare agents.

       5)   Radioactive materials.

       6)   Forbidden and  Class A explosives  as  defined  in  40 CFR 173.51  and
           173.53.

       7)   Waste  with a total  organic  sulfur content greater than 5 wt.Z.

 2.     Treatment  Technology Selected for Treatability Testing

 2.1.    Treatment Category  (i.e., Thermal Destruction. Physical  Chemicalr
 Biological. Solidification/Stabilization)

       Thermal destruction

 2.2.   Criteria for Technology Selection

       In-house technology  or technology provided by a vendor.   Vendor name.
Reason for selection.

      The  CBC  is in-house  technology.  The CBC  technology for hazardous
waste  wa*  developed by GA Technologies, Inc.  (GA).   GA and Ahlstrom  of
Finland formed Pyropower Corporation in 1980 to supply CBCs for  the U.S.
boiler market.   Pyropower  and Ahlstrom have many CBC units installed  and
operating worldwide  burning a variety of fossil  fuels, biomass  and wastes.
OES has a licensing  agreement to us*  the same CBC technology to develop and
build hazardous waste  incinerators.   Also,  the 2 million Btu per hour CBC
facility and  the  key  CBC  program personnel were transferred  to Ogden
Corporation as OES in December 1986,  and OES continues to develop the CBC
technology for hazardous waste destruction.
-------
 2.3.   Process  Description,  Requirements and Limitations

       The  process  description  is given below.

 Requirements

       Requirements  for operations vary depending upon the CBC size and feed
 type.   An  example  is given below for the  36-inch diameter CBC,  the  largest
 transportable  version.    Note:   ~10  MM  Btu/hr  .  .  .  hazardous  waste
 treatment  CBCs  are available  in sizes from ~16-inch  diameter  (2 MM  Btu/hr)
 to ~120-inch diameter (50 MM Btu/hr).

                     36-inch CBC Operating Requirements
     o   Temperatures

     o   Thermal Rating
     o   Auxiliary Fuel Required (if no
          heat value of feed)
     o   Electricity (connected)
     o   Water

     o   CBC Area
UOO°F to 1800°F (normal
 range)*
10 MM Btu/hr
10 therms/hr
250 kva
None (closed loop cooling
 system)
50 x 50 feet
Limitations

     Feed limits  for solids are  ~l-inch ring size  on  the largest feed
input.    Liquids/sludges  must  be  pumpable.    Ash melting  limits
(glass-formers) in feed materials vary depending upon application.
     Higher than 1800 F  temperatures  can be accommodated  in  the CBC but
     have not been necessary to achieve the desired waste destruction.
-------
 Typically,  several wtZ of low-temperature «1600 F) melting material can be
 handled without  special procedures.  We have developed procedures to handle
 >30 wtS glass-formers.

 Process Description

      The CBC  is  a complete, self-contained thermal process plant capable of
 destroying, through combustion, hazardous components of various contami-
 nated solid feedstocks.   It will produce inert  by-products  that satisfy
 federal, state,  and local regulatory requirements.

      Commercial  units  in  Europe and the U.S.  are designed to burn  a wide
 variety of  fuels such as coal, peat, wood wastes,  municipal wastes,  and
 oil,  primarily for the purpose of  raising steam or generated electricity.
Application of  this process  to the treatment  of hazardous wastes was
 developed in the US since 1980  (Ogden Environmental Services, Inc. acquired
 this  technology  in December 1987 from GA Technologies, Inc.).

      The CBCs  process  advantages are derived  principally from   (1) the
 extremely high fluidizing velocities and the resulting intrinsic turbulence
 and   (2) the recirculation of solids to the combustion chamber.

      The ability of  the  CBC to efficiently destroy organic  waste at low
combustion  temperatures and  low excess  air levels  without an afterburner
 results in very high waste processing rates for given-sized hardware.  With
 typical operating  conditions,  the  CBC  system  can handle a  maximum soil
                               2
waste  throughput of  1100 Ib/ft  of combustor  cross section and requires
                 2
 only  850  Ib/h/ft  of  combustion  air.   This  specific  throughput  is
 significantly  higher than  can  be obtained using other  incineration
 technologies.  Thus, CBC  units do  more  work than other equivalently sized
 incinerator types.
-------
Ma-jor  Equipment Components and Function

     The  primary  CBC components are the  combustion  chamber,  hot  cyclone
collector, flue gas cooler, baghouse, and stack.  Auxiliary systems include
feeders  (solids,  liquids,  sludges),  forced-draft and induced-draft fans,
ash  conveyor,  compressed air,  cooling  tower,  and building ventilation.
Figure 2-1.1 is a schematic representation of the process.

     Atmospheric  primary air is  pumped into the  lower  portion of the
combustion chamber where the  bed  material is  fluidized by  turbulent mixing
of the air  and solids.  Larger solids  gravitate downward  to  form a more
dense  fluidized bed in the lowest combustor zone.  The forced-draft primary
air carries smaller solids up to the top of the combustor.

     Secondary  air  is supplied to various locations in the  combustion
chamber to ensure complete combustion and minimize  formation of  nitrogen-
oxides (NO ).

     Auxiliary fuel and  pressurized contaminated soil feed are individually
introduced into the  lower  combustion chamber.   Capability also exists  to
feed liquid  wastes.   Dry  limestone  sorbent  is added to control  gaseous
emissions of sulfur, phosphates, chlorines, or other halogens.

     Elutriated solids are separated from the flue gas by a hot cyclone  and
reinjected into the lower combustor using a proprietary nonmechanical seal.
Ignition, burning,  and  reaction  of  the  fuel,  contaminated  soil  feed,
sorbent,  and ash components  are  a  continuing  chemical process  which
destroys the hazardous wastes.

     The loop design is  such  that essentially all of the pollution control
occurs in the combustion loop itself.   Efficient mixing of the fuel, soil
feed,  and combustion  air assures  that all hazardous organic  constituents
are oxidized with minimum emissions of  both CO and  NO  .   Flue gas wet
scrubbers are not  required.
                                     10
-------
                COMOUSTOR
LIMESTONE AM)
SOLID WASTE
LIOUIO WASTE
AUXILIARY FUEL
      CONTHOLflOOM
         . AND
      MOTOR CONTnOL
         CENTEII
                                                        CinCUlATlNG
                                                        CUULINU
                                                        WATER
         7   n
         UAGIUlUSt
         iyijj
ASIICONVEYOH
                                                                             II) FAN
                            ASH
                          SIOflAGL
       -305
                          Fig. 2-1.1.    CBC schematic
-------
      The  high velocity of combustion-air and circulating solids creates a
 uniform temperature  (+50  F)  around  the  combustion  loop which  is  controlled
 at  a value between 1400 F and  1800  F.   Residence  times  in the combustor
 range from about 2 seconds  for  gases to about  30  minutes for solid feed
 material  (less than 1.0-inch ring size).

      During operation,  ash is periodically removed from the CBC by means of
 a water-cooled ash removal  system.  The hot gas leaving the  cyclone  is
 cooled  in a  flue gas  cooler;   the  fly ash  escaping  the cyclone  is
 continuously  collected by baghouse  filters.  These  filters  reduce the
 particulate loading in the  flue gas  from as  high as  130  to 0.01  grains/scf
 (the  EPA  RCRA particulate emission limit is  0.08 grains/scf).  The fabric
 filters  are  acid-resistant  and normally operate at  temperatures  up to
 350 F.  No post-treatment of the dry, inert  ash  is necessary.

 CBC Advantage

      The  extreme turbulence and high  recirculation  rates of  the  solids
 within  the combustor make the CBC combustion process relatively  insensitive
 to feed properties.  The  100-to-l ratio  of hot-inert-solids-to-feed and the
 high  internal  combustor heat transfer ensures that moisture  in  the waste
 feed  rapidly  evaporates with little  (if any) depression  in local combustor
 temperature.   The  only significant  effect  of  feed moisture  on the
 incineration  process  is  on  the combustor energy  overall heat balance.
 Energy that would otherwise  go to processing contaminated soil must be used
 to evaporate water (as with  any thermal  system).

     The CBC is  insensitive  to  large amounts of fines in the  feed stream.
 Feed  fines  benefit the solid  circulation that  produces the  isothermal
 combustor conditions.

     The  turbulence  in  the  CBC atomizes liquid waste  feeds,  thereby
eliminating the  need for  troublesome spray nozzles which could  clog.  The
bed effectively disperses viscous sludges.
                                     12
-------
      The  acid  gases formed by chemical reactions are rapidly absorbed by
 the  large surface area of fine circulating sorbent (such as limestone or
 other inexpensive local sorbent).   The  intermediate  reactions form the
 final ash products of benign salts  such  as  CaCl.  and CaSO,.   The rapid
                                                 &          *t
 combustion  of  the flue gas  and  quick neutralization of  the  acid gases
 within  the  combustion chamber are in contrast to other incinerator types
 that  rely on afterburners  to complete combustion and add-on scrubbers to
 complete  acid gas  capture.

      Avoiding  the requirement for  a wet scrubber  not  only simplifies
 operation  of the  incinerator  and avoids acid gas  attack of internals
 between the  combustor and  the scrubber,  but also completely eliminates
 aqueous waste streams.

      Two  features  of  the CBC make it much more energy-conserving in soil
 decontamination applications.  The  first  derives  from the CBCs  ability tcr
 destroy contaminants  in a  temperature range of  1400  to  1800  F - several
hundred degrees lower than required  in other types  of incinerators.   This
 ability to clean up soil without heating it to highly elevated temperatures
 greatly reduces the  amount of auxiliary  fuel required  in the CBC versus
 other types of incinerators.

      The  second feature of the CBC that conserves energy is the  very  low
 excess  air  required  in the destruction of  contaminants.   Because of the
highly  turbulent  bed  and intimate contact between the contaminated solids
 and air,  the CBC  operates  in the  range  of  20Z to 401 excess air.   This
 compares  to several hundred  percent excess air  in  a rotary kiln,  for
 example, where most of  the air bypasses  the soil without  reacting with it.
Although much of the air bypasses the soil, it still picks up heat from  the
 rotary kiln  and makes  necessary  additional  auxiliary fuel to replace this
 lost  heat and additional water flow  to cool the bypass air.

     When an upset occurs  in a CBC (e.g., fan failure,  power  outage,  etc.)
the bed material  slumps into the lower  combustion chamber, thus  retaining
pollutants  in  the limestone  and ash.   In  contrast,  the conventional
                                     13
-------
 bubbling bed is  not  easily slumped because lower velocities  invite  bed
 agglomeration.    When  a scrubber  is  involved,  as for  kilns  and grate
 incinerators, scrubber bypass  is  required  in an upset.  Scrubber bypass can
 release large amounts  of untreated pollutants.

      The key CBC components,   the combustor,  provides  these benefits
 inherently  and  automatically, without  complicated  controls.    Other
 components  (pumps,  fans,  etc.) are standard hardware.  Scrubbers or other
 chemical treatment  equipment are unnecessary.   The innovation represented
 by the CBC  is  in the total system, i.e., in the arrangement and  particular
 function that  has been designed  into  the  incinerator using this standard
 hardware.

 2.4.   Rate  of Process  and  Length  of Treatment Time.

      The largest transportable 36-inch  CBC will process soils  at  up  to  _
 12,000  Ib/hr on  a 24-hour  per  day, 7-day per week basis.   The system will
 also  process  contaminated sludges  and liquids  concurrent  with  soils  or
 separately.

      Length of treatment time  is  interpreted as residence time of materials
 at  temperature  in the  CBC combustion loop.  There  is  a minimum "gas"
 residence time and longer  residence for  solids as described below:

Gas Residence Time

     The gas residence time is controlled  by the superficial velocity in
the combustion chamber,  and is approximately 2.5 to  3  seconds at 1600°F.
Exact  operating  conditions are  selected based on  test and  trial  burn
results  to meet  or  exceed all  requirements.  Upon leaving the  combustor
loop,  the gas  flows through the  flue gas  cooler where  it  is cooled to
   Q
350 F,  over  a  6  second time  interval.    The  gas temperature  remains
essentially constant  throughout  the   rest  of  the  system,  with about
3 seconds passing before discharge to  the atmosphere.
                                     14
-------
     The  gas  residence time  (at  1600 F) calculation  is  summarized as
follows:
Component
Combustion chamber
Chamber to cyclone
Cyclone
Cyclone to FGC
Length
(ft.)
35
12
20
24
Velocity
(ft./s)
20
50
50
50
Time at
1600°F
(seconds)
1.75
0.24
0.40
0.48
                                                               2.87
Solids Residence Time
      Due to extensive backmixing and solids recirculation in the CBC, the
solids residence time at operating temperature  is much greater than for the
gas.  While this residence time is dependent on particle size and attrition
rates, on  average  the bed  is  replaced  about twice per hour.   Thus, a
typical  solid  residence time  is  about  30  minutes.   Solids  leave  the
combustor through  either the bed ash discharge or the gas  exit  in the
cyclone.   Solids in  the  gas stream  are  cooled  along  with the gas, and are
separated in the baghouse.   Bed ash is  transferred by a water-cooled  screw
conveyor, taking about 30 minutes to cool from operating temperature to the
cool ash temperature.

      Not* that  even very  finely divided  solids have a reasonably  long
system residence time due to the solids  recirculation.

2.5.  Material  Handling Equipment Requirements  (i.e.,  Material  Transport
and Excavation)
      Solids  material transport  to  the  36-inch  diameter CBC  on  a
remediation site typically involves  loading  a  solids  feed hopper once per

                                     15
-------
 day from a large storage pile or excavation area using a front-end loader.
 From the solids feed hopper,  the solids  are  activated  and fed automatically
 by mechanical feeders.

       Sludge/liquid material  transport involves  pumping out of a surge tank
 and feeding directly into the CBC.  The surge tank may be sized  to receive
 daily,  weekly or other  periodic  loads from the site.

       Excavation equipment requirements  vary depending  upon  the site.
 Standard loader/excavators  may be used  on soils sites with digs up to 40'
 deep.   Special equipment (and/or shoring, etc.)  may be required  for  deeper
 excavations.

 2.6.    Pretreatment  Requirements (i.e.. Oversize Material.  Removal.
 Disaggregation.  Sorting.  Dewatering.  Chemical/Physical Treatment. Control
 of  Volatile Release. Control  of Particulate Release) Description Criteri-a
 for Application

      A  solids  size maximum of 1-inch ring  size.  Pumpable  liquids/sludges
 need  no pretreatment (filtering,  etc.)  because there  are  no atomizers
 required on the CBC.  Dewatering  of liquids  stream is not necessary for the
 process  (dewatering may be an economic benefit).  Some oversized impervious
 materials such as metal parts may be washed and the  surfaces certified
 clean of contamination.  The  contaminated  wash material would  then be
 incinerated in the CBC.

      Volatile and  particulate release  in pretreatment is minimized  due to
 the minimal pretreatment required  for  CBC  feeds.   Fugitive dust/vapor
 control  for screening/shredding/crushing and  solids handling typically
 requires simple  dust enclosures.   Negative  pressure systems or  spray
wetting systems may  be  added  in   some cases as  necessary.  Volatile vapor
 control  is  required usually only if  thermal pretreatment (dewatering)  is
 used.  This volatile  vapor  control would involve drawing hazardous vapors
 through the inlet fans of the combustor or alternatively  absorbing vapors
                                     16
-------
on  activated  carbon or  condensing the  vapors  and  then  burning the
contaminated residues.

      Criteria for application of  these  pretreatment requirements  may be
summarized as:

      o  Oversize Solids >1" - Screen,  Crush - Dirt,  rock,  etc.,  1"  to  4"
                               Screen,  Shred - Metal, wood,  paper,  fibre,
                                etc.,  1"  to 4"+
                               Screen,  Wash - Metal,  rock,  selected  others
                                A"
      o  Dewater - If economics show favorable
      o  Volatile and To meet local, state and Federal standards
         Particle Control -(may include insitu monitoring)

2.7.  Post-Treatment Requirements.   Description.   Criteria for Application

      Residuals from the CBC include  dry  cementitious  (pozzulanic)  ash.
This ash in site soils cleanups would include inert soils  and limestone and
lime salts  of chlorine,  sulfur and other  solid  lime-absorbed materials.
Tests on RCRA and TSCA materials indicate such  low organics levels in the
ash  residue that the  ash  residue may  be  either delisted  (RCRA)  or
non-regulated (TSCA).

2.8.   Byproducts and Other Process Effluent.   Type.  Quantities,  and
Concentrations.  Environmental Controls
                                                                       are
                                                                     x
      Th« off-ga* is primarily  CO.,  0_,  N.  and H-0 vapor.  CO and NO
typically <150 ppm and HC1  and  unburned  HC  (total)  are typically <100 ppm.
Offgas particulate is «0.08 grains per acf as controlled by a baghouse.

      The baghouse  flyash and bedash  are dry solids.   These  solids  are
primarily silica sand  and lime  and lime salts (CaCl.  or  CaSO^)  since dry
limestone is injected into the combustor to capture acid  gas formers before
they leave  the  combustor.   The resultant ash  is  a very  low  leachable
cementitious (pozzularius) dry powder.  No wet scrubber sludge is produced.
                                     17
-------
 2.9.  Monitoring and Data Collection Requirements (i.e., QA/QC Protocols)

      Modified Method 5, VOST,  (SW8A6 methods) solids sampling and analysis
 procedures  (methods, chain-of-custody) as approved by EPA have been used to
 obtain  the  data supporting the CBC TSCA  permit  for  PCB and the  CBC RDD
 permit  for  RCRA compounds.

 3.0.  Treatability Test

 3.1.   Scale Used  for  Testing  (i.e., Bench.  Pilot,  Full) and  Scale-up
 Limitations

      A  16-inch  diameter commercial-scale unit  was  used for test work.
 There are no scale-up limitations as already demonstrated by demonstrations
 in  this  commercial-size test  rig  as  applied to other  larger commercial
 units burning varied solids/liquids whose bed cross-sections are many feet.
 The data from the  16-inch  rig has  been basically the same as  in the  larger
 rigs with no scale-up surprises.

 3.2.  Number of Tests Conducted Under Variable Conditions.  Test Results in
 a. Summary Table Showing Both Operating Conditions and Performance Results

      There have been  over 5,000 test hours logged  in  the pilot  plant  on
various non-hazardous and hazardous feeds.

      Two key  examples of  test data on  hazardous  feeds are given in
 Tables 3.2-1 and 3.2-2  for the TSCA  PCB  test and the  RCRA liquids  test
 (California Air Resources Board), respectively.

      See also Appendix A for more details on the PCB test for  TSCA.
                                     18
-------
                                   TABLE 3.2-1
                             SUMMARY OF TEST RESULTS
                       TRIAL BURN OF PCB-CONTAMINATED SOIL
PROCESS CONDITIONS

    T«st number

    Average combustion
    temperature,  F

    Gas residence tiro*,
    seconds

    PCB in feed, ppm

    PCB in •»h, ppm
                           1

                           1,806


                           1.16
2

1,806


1.16
3         A

1,796     1,600
                                                 1.19
                                                           1.32
B

1,800


1.18
                           11,000     12,000     9,800     12,000     47
DESTRUCTION REMOVAL EFFICIENCY. X**J

    PCB                    >99.9999   >99.9999   >99.9999  >99.9999   >99.9999
         Regulatory requirement is 99.9999.

    Not*:  Test planned/monitored by EPA-TSCA.
-------
                                                       TABLE 3.2-2
                                  SUMMARY OF TEST RESULTS EVALUATION OF THE CBC PROCESS
                                       FOR DESTRUCTION OF LIQUID ORGANIC WASTES*"'
                    PROCESS CONDITIONS
K>
O
Test number
Average combustion
temperature, F
Gas residence time,
seconds
la
1480
2.69
Ib
1416
2.08
Ic
1630
2.03
le
1680
1.97
DESTRUCTION REMOVAL EFFICIENCIES. X(b)
Freon 113
Carbon tetrach 1 or i de
Hexachlorobenzene
Ethy 1 benzene
Xy lene
99.9999
99.9998
99.9999
99.9971
99.9930
99.9724(C)
99.9996
99.9995
99.9989
99.9991
99.9997
99.9996
99.9999
99.9991
99.9978
99.9999
99.9999
99.9999
99.9991
99.9978
                               Fuel  analysis   included   Freon   113,   Carbon  TetrachI oride,
                    Hexachlorobenzene,  EthyI benzene, Xylene, TrichIorobenzen, plus other compounds,
                          (b)
                              RCRA r«quir«m«nt is 99.99X.
                          (c)                                              o
                              B*d  t«mp«ratur«  momentarily dropped  to 1300 F during  th*  sampling
                    per i od.

                          NOTE:   Test planned/monitored by the California Air Resources Board.
-------
 3.3.  Performance Evaluation (i.e..  Removal  Efficiency).  Could Performance
 be Improved?  How?   (Operating Conditions Change, Additional Pretreatment.
 etc. )

       Performance improvements  are centered  only  in maintaining consistent,
 reliable and optimum feed rates of  sorbent  (limestone)  solids  and the
 contaminated solids  and liquids  feeds.   The CBC  turbulence and  residence
 time have demonstrated well above the required DREs at temperatures which
 are much lower  than other  incinerators.

 4.0.  Processed Residual

 4-1.  Physical Chemical Characteristics  and  Analysis,  Volume Increase or
 Decrease

       The  dry ash produced has  been well below TSCA standards for PCB  (s«
 Appendix A)  and has  been  at delistable  levels,  if  such delisting were
 appropriate,  for  RCRA materials.

       Volume  decreases  of  over 20 to 1  have been noted for  some  low-ash
 liquids/sludges.  Volume stays essentially constant for contaminated soils.

 4.2.   Regulatory Test Protocol Results  (i.e..  EP Toxicity, TCLP, etc.).
 Specify  Test  Performed

       Organics have b«en quantified  for PCB as given in Appendix A.  Metals
 leachability  tests have not been performed, though there have been perti-
 nent studies  on fluoride leachability.

 4.3.  Residual Disposal Method Used.  Reasons for Selection

      Pilot plant ash is either  returned to  the test  customer or  sent  to a
Class I  facility under contract to the test customer.  Though the  ash  could
be delisted,  the volume (a few drums) are too small.
                                     21
-------
4.4.   Cost Requirements  (Per  Unit  of Time and  Unit  of Mass of  Waste
Treated)

      Costs depend  upon the  size  of combustor  and  the type of  feed.
Examples of CBC treatment costs on varied moisture content  soil  for  36-inch
and 104-inch diameter CBCs are given below:
Soil
Moisture
TL
10
16
30
Total
36-inch CBC
117
131
166
S/t
104-inch CBC
78
84
98
4.5.  Permit Requirements (Type of Permit Required,  Used)

     The following 5  permits  have been obtained for the pilot plant CBC:
(1) EPA-TSCA transportable  PCB  incineration permit -  the  first for all
10 EPA  regions;    (2)  EPA-RCM  RD&D permit,  the first in  California;
(3) California Department of  Health Services RD&D  Permit  (Draft)  .  .  .
(also, a Mitigated Negative Declaration of no  significance environmental
impact under the California Environmental  Quality Act);  (4)  San Diego  Air
Pollution Control District  Permit including a hazardous emissions impact
assessment, and;  (5) San Diego Industrial User Discharge Permit.

     The commercial CBCs (nonhazardous  fuels) have  obtained air permits in
"nonattaliment)M areas such as Bakersfield and Colton, California.
                                     22
-------
                           APPENDIX A
             PCB-CONTAI-IINATED SOIL TREATMENT IN A
            TRANSPORTABLE CIRCULATING BED COMBUSTOR
(Paper present to the Hazardous Materials Management Conference
and Exposition at Anaheim, California, April 29 - May I, 1986.)
-------
OGDEN
ENVIRONMENTAL SERVICES, INC,
  PCB-CONTAMINATED SOIL
  TREATMENT IN A TRANSPORTABLE
  CIRCULATING BED COMBUSTOR
  by

  D. D. JENSEN
  Staff Scientist

  D. T. YOUNG
  Manager, Combustion Projects
  Presented at
  Hazardous Materials Management
  Conference and Exposition
  Anaheim, California
  April 29 - May 1, 1986
  OES was formerly the Hazardous Waste Management Division
  of GA Technologies Inc.
-------
                 PCB-CONTAMINATED  SOIL TREATMENT  IN A
             TRANSPORTABLE CIRCULATING BED COMBUSTOR
                                           by
                      D. D. Jensen, Ph. D.  and D.  T.  Young


                                GA Technologies  Inc.
                                San Diego,  California
               ABSTRACT

    A trial burn of PCB-contaminated soils was
completed in GA  Technologies'  transportable
Circulating Bed Combustor  (CBC). Over  4000
pounds of soil containing 1% PCB were treated
in three identical 4-hr runs at 1800° F. The re-
sults showed excellent compliance with U.S. En-
vironmental Protection  Agency (EPA) Toxic
Substances  Control Act (TSCA) requirements.
Destruction  and  removal efficiencies  (DREs)
were greater than 99.9999%  and PCB  in com-
bustor ash was less than 200 ppb. No chlorinated
dioxins or furans were detected in the stack gas,
bed ash, or fly ash. In addition, no significant
concentrations of other Products of Incomplete
Combustion  (PICs) were  detected. Combustion
efficiencies  were greater  than  99.9%, with CO
concentrations less than 50 ppm and NOX  con-
centrations  less than 75 ppm. Particulate emis-
sions were generally below 0.08 grain/dscf and
HC1 emissions were maintained below 4.0 Ib/hr
by introducing limestone directly into the com-
bustor. These results led to the first TSCA per-
mit for a transportable incinerator which can
be used in  all ten EPA regions. This demon-
strates that the CBC is an environmentally ac-
ceptable means of treating contaminated soil
containing PCB  and other organic wastes. In
addition,  the high thermal efficiency, the ab-
sence of afterburners or scrubbers, and the use
of simple feed systems make  CBC treatment
competitive with soil removal and transport to
landfills and other potential treatment/disposal
options.
            INTRODUCTION

    Polychlorinated biphenyls, or PCBs, have
perhaps received more scrutiny than any other
hazardous chemicals found in waste sites around
the country. This group of 209 synthetic chlor-
inated organic compounds found wide use~as a
dielectric fluid  in utility  transformers and ca-
pacitors, and as a high-temperature heat trans-
fer medium (1). However, because of their ex-
ceptional  resistance to  degradation in the
biosphere and apparent toxicity, the manufac-
ture and sale of PCBs were banned in 1976 for
virtually all purposes. The control, treatment,
and disposal of PCBs was mandated by TSCA
and is currently handled  through EPA's Office
of Toxic Substances.

    Until recently, it has  been common practice
to remove contaminated soils for burial in a se-
cured landfill. However, this option is becoming
less desirable as landfill costs escalate, the num-
ber of available landfill sites drop, and gener-
ators or potential responsible parties (PRPs)
become increasingly aware of retained liability
associated with the contaminated soils, even  in
a secured landfill. Treatment of PCB-contami-
nated soil by incineration in the CBC can elim-
inate or significantly reduce the potential lia-
bility of generators or PRPs at a cost competitive
with landfill prices.

    The use of CBC technology for hazardous
waste treatment builds on over 15  years expe-
rience at GA in the design, development, and
-------
operation of fluidized bed combustors.  In 1980
GA and Ahlstrom of Finland formed Pyropower
Corporation to supply CBCs for the U.S. boiler
market. These units are designed to burn a wide
variety of fuels such as coal, peat, wood, munic-
ipal wastes, and oil. Over 2o units are operating
or under construction worldwide.  Three  units
are currently in  operation in  the  U.S. In ]9S3,
GA began concentrating its efforts on  the ap-
plication of CBC technology to incineration  of
hazardous wastes. Table 1 presents examples of
wastes that have been burned in the CBC during
this time. Successful treatment of this diversity
of wastes  provided assurar.ee that PCBs  could
be destroyed in a CBC at a lower temperature
than used in conventional incinerators.

            CBC DESCRIPTION

    The CBC is a new generation of incinerator
that uses high velocity air to entrain circulating
solids  in a  highly turbulent  combustion loop.
This design allows combustion along  the entire
length of the reaction zone. Because of its high
thermal efficiency, the CBC is ideally suited  to
treat feed with low heat content, including con-
taminated  soil. Figure 1 shows the major com-
ponents of a CBC for soil treatment.  Soil  is in-
troduced into the combustor loop at the loop seal
where it immediately contacts hot recirculating
soil from the hot cyclone. Hazardous materials
adhering to soil are rapidly heated when intro-
duced into the loop and continue to be exposed
to high temperatures throughout their residence
time in the CBC. Upon entering the combustor,
high velocity air (14 to 20 ft/s) entrains the cir-
culating soil which travels upward through the
combustor into the hot cyclone. Retention times
in the combustor range from 2 seconds for gases
                    to -30 minutes for larger feed materials (<1.0
                    in.). The cyclone separates the combustion gases
                    from  the hot solids, which are returned to the
                    combustion chamber via  a  proprietary  non-
                    mechanical seal. Hot flue gases and fly ash pass
                    through a convective gas cooler and on to a bag-
                    house filter where fly ash  is removed. Filtered
                    flue gas then exhausts to the atmosphere. Heav-
                    ier particles of purified soil  remaining in the
                    combustor lower  bed are  slowly removed by a
                    water cooled ash  conveyor system. As a conse-
                    quence of the highly turbulent combustion zone,
                    temperatures around the  entire  loop (combus-
                    tion chamber, hot cyclone, return leg) are uni-
                    form  to within zr50°F.  The uniform low  tem-
                    perature and high  solids  turbulence also help
                    avoid ash slagging encountered  in other types
                    of incinerators.

                        Acid gases formed  during destruction re-
                    actions are rapidly captured in situ by limestone
                    added directly into the combustor. The reaction
                    of limestone and  HC1, released during PCB in-
                    cineration, forms dry calcium chloride, a benign
                    salt. The rapid combustion and quick neutrali-
                    zation of the acid gases within the combustion
                    chamber eliminates the need for afterburners
                    and add-on scrubbers to complete destruction
                    and acid  gas capture, respectively. Emissions of
                    CO and NOX are controlled to low levels by ex-
                    cellent mixing, relatively low temperatures (1450
                    to 1800°F), and staged combustion, achieved  by
                    injecting secondary air at higher locations in the
                    combustor. Because of its efficient combustion
                    and highly turbulent mixing, the  CBC is capable
                    of attaining required DREs for both hazardous
                    wastes (99.99 7c) and toxic wastes (99.9999 9c) at
                    temperatures below those used in conventional
                    incinerators (typically >2000°F).
                                         TABLE 1
                            CIRCULATING BED TEST RESULTS
       Waste
   Form
Destruction
Efficiency, %
   HC1
Capture, %
Ca/Cl2
Ratio
 Carbon Tetrachloride
 Freon
 Malathion
 Dichlorobenzene
 Aromatic Xitrile
 Trichloroethane
Liquid
Liquid
Liquid
Sludge
Tacky solid
Liquid
    99.9992
    99.9995
  > 99.9999
     99.999
  > 99.9999
    99.9999
   99.3
   99.7

     99

     99
  2.2
  2.4

  1.7

  1.7
-------
  COMBUSTOR

LIMESTONE
FEED
                                          	,     FLUE GAS
                                           —•»       I  Xr.nfUER
      SOIL
      FEED
                                                             FLUE GAS
                                                              (DUST)
                                                              FILTER
                                                                               STACK
           FD
                                COOLING
                                WATER
                                                                           ASH
                                                                           CONVEYOR
                                                                           SYSTEM
         Fig. 1. Schematic flow diagram of circulating bed combustor for soil treatment
          TEST DESCRIPTION

    A  variety  of  requirements  are imposed
prior to and during a PCB trial burn (2). The
key target of a trial burn is to ensure that PCB
DREs are > 99.9999% at  the operating condi-
tions chosen for the incinerator. In addition, the
concentration of PCB in ash from the unit must
not exceed 2 ppm. The potential  formation  of
PICs is also carefully evaluated, with particular
attention  given to polychlorinated dibenzo-p-
dioxins (PCDDs) and polychlorinated dibenzo-p-
furans  (PCDFs). The combustion efficiency  of
the unit must be >99.9% and particulate emis-
sion must not exceed 0.08  grain/dscf.

    The CBC trial burn was carried out in GA's
transportable  unit, shown  in  Figure 2. Soil
treated in the test was obtained from a former
chemical processing site known to contain pock-
ets of PCB up  to 6000 ppm, as well as other
organic and inorganic wastes. In order to ensure
that the CBC would  be permitted to treat all
likely site concentrations of PCB, uncontami-
nated soil from the site was "spiked" with liquid
PCB to 10,000 ppm. Spiking  was carried out  by
blending a 50:50 commercial mixture of PCB
                                    "1248"  and trichlorobenzene  with a  ribbon
                                    blender in 1000 Ib lots. Approximately 4000 Ib
                                    of soil was spiked for the three burns required
                                    by the TSCA trial burn permit.


                                         While the CBC was maintained at 1800°F
                                    using natural gas as the auxiliary fuel, several
                                    barrels of clean site soil were introduced into
                                    the CBC prior  to the addition of  spiked soil.
                                    During this time all operating parameters and
                                    system components  were confirmed to be in the
                                    required operating ranges. Process parameters
                                    monitored included:
                                            Temperature around the loop
                                            Pressure drop across the loop
                                            Soil feed rate
                                            Primary air flow
                                            Secondary air flow
                                            Loop seal air flow
                                            Total air flow
                                            Methane flow
                                            CO concentration
                                            COo concentration
                                            Excess oxygen level
                                            NON concentration.
-------
Fig. 2. Transportable 16-inch circulating bed combu?tor
-------
     Spiked soil was pneumatically transported
to a bunker and screw feeder. Soil feeding, lime-
stone addition, and stack gas monitoring were
started  simultaneously.  An  EPA  Modified
Method 5 sample train (3) was used to sample
stack gas emissions. In addition, a separate Vol-
atile Orpanic Sampling Train (VOSi) (4) was
used to sample for volatile organic PICs. Feed,
bed ash, and fly ash samples were also gathered
throughout the test (see Figure 1 for sample port
locations). Three  identical tests  of spiked soil
(4 hours each) were carried out over two days
in late May 1985. Each test was observed and/
or audited by EPA personnel or representatives.
All feed, ash, and stack gas samples were sub-
sequently analyzed  for  PCBs,  PCDDs, and
PCDFs. Fly ash, bed ash, and stack gas samples
were also analyzed for other PIC? (both volatile
and semivolatile). Stack gases were analyzed for
fly ash -and chloride release as well.

                RESULTS

    Table 2 presents a summary of the trial
burn operational data and test results gathered
during the tests. Near-identical conditions were
maintained for each of the tests. In each case
PCB DREs were well in excess of the EPA-re-
quired 99.9999 * . PCB concentration in the bed
ash and the fly ash did not exceed 200 ppb. No
PCDDs or PCDFs were detected in the stack gas.
bed ash, or fly ash. Combustion efficiencies were
                                         TABLE 2
               PCB TRIAL BURN OPERATIONAL DATA AND TEST RESULTS
Parameter
Test Duration, hr
Operating Temperature, °F
Soil Feed Rate, Ib/hr
Total Soil Feed, Ib
PCB Concentration in Feed,
ppm
DRE, %
PCB Concentration
— Bed Ash, ppm
— Fly Ash, ppm
Dioxin/Furan Concentration
— Stack Gas, pp
— Bed Ash, ppm
— Fly Ash, ppm
Combustion Efficiency, %
Acid Gas Release, Ib/hr
Particulate Emissions,
grain/scf (dry)
Excess Oxygen, %
CO, ppm
COo, %
NOX, ppm
TSCA
Requirement
-4
—
—
—


> 99.9999

<2
<2

—
—
—
>99.9
<4.0
<0.08

>3.0
—
—
—
1
4
1800
328
1592
11,000

99.999995

0.0035
0.066

ND(a)
ND
ND
99.94
0.16
0.095(b)

7.9
35
6.2
26
Test Number
2
4
1800
412
1321
12,000

99.999981

0.033
0.0099

ND
ND
ND
99.95
0.58
0.043

6.8
28
6.0
25
3
4
1800
324
1711
9,800

99.999977

0.186
0.0032

ND
ND
ND
99.97
0.70
0.0024

6.8
22
7.5
76
(a'ND - Not detected.
(b)Derived from 2-hr makeup test.
-------
greater than 99.9f/~< and acid gas release was well
below  the required 4 Ib/hr. Particulate emis-
sion? were generally less than the required 0.08
grain/di-cf. Only the grain loading from the first
lest, obtained from a 2-hr makeup test after the
completion of Tests 1 through ?,, showed  a value
slightly higher than the limit. This is attributed
to off-normal  process  conditions for  the bag-
house,  i.e.. excessive blowback air pressure along
with a  higher-than-normal number of  blowback
cycles.  Nitrogen oxides and CO levels  remained
low as  a result of the staged combustion utilized
in the  CBC  and the relatively low combustion
temperature (1SOO°F).  These results demon-
strate  that  the CBC is an effective  mean? to
destroy PCBs contained in a soil matrix, without
the need for high temperatures, afterburners,
or wet  scrubbers. In particular,  the absence of
undesirable  combustion byproducts helps  en-
sure that effective treatment of soil can be ob-
tained in an environmentally acceptable manner.

     These  results confirm  the design of GA's
transportable CBC shown in Figure 3. The com-
bustor and all other plant  components are de-
signed as  modular units which can be trans-
ported by truck or rail. These units are assembled
at the site into  an operating unit  in four to six
weeks. The major components of this CBC plant
include  the combustor loop, feed  system, and
pollution control  and air induction equipment.
GA's 30-inch  transportable  CBC  is capable of
processing up to 4 t/hr of dry soil on a 24-hour
basis, requiring an operating crew of only two
persons per shift.  Soil treatment  costs may  W
as low as $100/ton for a large site. For smaller
sites or sites having unique treatment require-
ments, costs may approach  ^$400/ton.
                               STACK
                                                                FLUE GAS
                                                                COOLER
                COMBUSTION
                CHAMBER
                CYCLONE
                INDUCED
                DRAFT FAN
                SOLIDS
                FEED
                                                                       BAGHOUSE
                                                                       FLY ASH
                                                                       CONVEYOR
                COMBUSTOR
                ASH REMOVAL
                      FORCED
                      DRAFT
                      FAN
                  Fig. 3. Isometric of site-assemblied circulating bed combustor
-------
              CONCLUSION
          REFERENCES
    The results of the PCE soil trial burn in
GA's CBC demonstrated compliance with EPA
TSCA requirements. The CBC is now one of only
seven  incinerators nationwide permitted to burn
PCB. and one of only t\vo permitted transport-
able incinerator?, the other being the EPA ro-
tar\ kiln. It i? the first transportable incinerator
to be  permitted  in all ten EPA  regions. Stack
emissions from the CBC are well  within regu-
latory requirement? and residual PCB in bed ash
and fly ash is well  below regulatory require-
ments. The superior thermal efficiency, high
throughput, and  small staffing requirements of
the CBC provide a soil treatment option that is
cost competitive  with landfill disposal while at
the same time reducing  overall  liability  of the
generator or PRP.
SCS  Engineers, Inc.. "PCB Disposal  Man-
ual." Palo Alto, CA: Electric Power Research
Institute, Report No. CS-409S, June 19S~>.

"Polychlorinated Riphenyls d'CBsi Manu-
facture. Processing. Distribution  in  Com-
merce and Use Prohibition," 40 CFR TCl.Tc.

"Test Methods for Evaluating Solid Waste."
U.S.  EPA Report SW-84G, 2nd  Edition. 19S4.

"Proposed Sampling and Analytical Meth-
odologies for  Addition to Test Methods for
Evaluating Solid Waste: Physical/Chemical
Methods (SW-S4G.  2nd  Edition)," U.S. EPA
Report PB55-103026, 1984.
-------
                                        EPA/540/2-89/024
      SUPERFUNDTREATABILITY
             CLEARINGHOUSE
               Document Reference:
International Technology Corp., AFESC, EG&G Idaho, Inc. 'Technology Demonstration
of a Thermal Desorption/UV Photolysis Process for Decontaminating Soils Containing
    Herbicide Orange." Prepared for EG&G Idaho. 14pp. Technical report.
              EPA LIBRARY NUMBER:

            Superfund Treatability Clearinghouse -EWGE
-------
               SUPERFUND TREATABILITY CLEARINGHOUSE ABSTRACT


Treatment Process:      Physical/Chemical - UV Photolysis

Media:                  Soil/Generic

Document Reference:     International Technology Corp., AFESC, EG&G Idaho,
                        Inc.  "Technology Demonstration of a Thermal
                        Desorption/UV Photolysis Process for Decontamin-
                        ating Soils Containing Herbicide Orange."
                        Prepared for EG&G Idaho.  14 pp.  Technical report.

Document Type:          Contractor/Vendor Treatability Study

Contact:                Major Terry Stoddart
                        U.S. DOD/AFESC
                        BLDG 1117
                        Tyndall Air Force Base, FL 32403
                        904-283-2949

Site Name:              NCBC Gulfport, MS; Johnston Island; and Guam
                        (Non-NPL)

Location of Test:       Gulfport, MS and Guam

BACKGROUND;  This treatability study report presents the results of
laboratory and field tests on the effectiveness of a new decontamination
process for soils containing 2,4-D/2,4,5-T and traces of dioxin.  The
process employs three operations, thermal desorption, condensation and
absorption of contaminants into a solvent and photo decomposition.
Bench-scale tests were conducted to establish the relationships between
time and temperature and treatment efficiency.  A pilot-scale (100 Ibs/hr)
system evaluation was conducted at two sites to evaluate system performance
and develop scale-up information.
OPERATIONAL INFORMATION;  The intent of the laboratory and pilot-scale
tests was to reduce the combined dibenzo dioxin and furan constituents,
which originate from Herbicide Orange (HO), to less than 1 ng/g.  This
level represents the anticipated soil cleanup criteria.  The soils used had
similar concentrations of HO contaminants, but were different types of
soil.  In the laboratory the contaminated soil is passed through thermal
desorber and the off gases from the soils, including the contaminants, are
passed through a scrubber that uses a hydrocarbon solvent.  Contaminants
dissolve in the solvent and the solvents are passed through a flow reactor
which subjects the contaminant to UV radiation to decompose the contaminant
molecules.  Testing was conducted on soil samples from three HO contami-
nated sites; Johnson Island, Eglin AFB and NCBC in Biloxi, MS.  The soils
tested had 2,3,7,8-TCDD concentrations greater than 100 ng/g of soil and
2,4,-D/2,4,5-T levels greater than 1000 ng/g soil.  Tests were run at three
different temperatures and two different power levels using high intensity
UV quartz mercury vapor lamps.
    Pilot tests were conducted at the NCBC site using a rotary indirect
calciner as the desorber, an off gas transfer and scrubber system and a
3/89-43                                              Document Number:  EWGE
   NOTE;  Quality assurance of data may not be appropriate for all uses.
-------
photo chemical reactor to irradiate the contaminants contained in the
scrubber solution.  A 1200-watt high intensity mercury vapor lamp was used
to irradiate the contaminated scrubber solution.  No QA/QC plan was con-
tained in the document.  No discussion of analytical techniques utilized to
detect HO and associated compounds is contained in the paper.  A detailed
list of soil properties (particle size distribution, surface area, organic
matter, etc.) from the three different sites is contained in the document.
PERFORMANCE;  Laboratory studies revealed that thermal desorption/UV
photolysis destroyed all compounds to below their analytical detection
limit (which was generally less than 0.1 ng/g).  The concentration of
2,3,7,8-TCDD was reduced from 200 ng/g to less than 1 ng/g.  Insoluble
brown tars (presumably phenolic tars) were deposited on the surfaces of the
reactor vessel and lamp well.  Reaction kinetics quantum yields' and rate
constants were determined.  Pilot tests also produced soil containing less
than 1 ng/g of 2,3,7,8-TCDD.  Table 1 shows the results of the tests.

CONTAMINANTS!

Analytical data is provided in the treatability study report.  The
breakdown of the contaminants by treatability group is:

Treatability Group             CAS Number        Contaminants

W02-Dioxins/Furans/PCBs        1746-01-6         2,3,7,8-Tetrachlorodibenzo-
                                                  p-dioxin (TCDD)
                                  TABLE 1

          EFFECT OF TREATMENT CONDITIONS ON RESIDUAL 2,3,7,8-TCDD
                 DURING NCBC PILOT THERMAL DESORPTION TESTS

           Soil Feed    Residence         Soil           2,3,7,8-TCDD
             Rate         Time3       Temperature           (ng/g)
Test No.    (kg/hr)       (min)           (°C)       Initial     Residual

   1          13.6         40             560          260         ND
   2          13.6         40             560          272         ND
   3          25           19             560          236         ND
   4          44           10.5           560          266         ND

   5          20           24             460          233         0.5
Notes: a)  Soil residence time in heated zone.
       b)  Detection level for 2,3,7,8-TCDD was generally less than 0.1
           ng/g with a range of 0.018 to 0.51 ng/g.
       c)  This is a partial listing of data.  Refer to the document for
           more information.
3/89-43                                              Document Number:  EWGE
   NOTE:  Quality assurance of data may not be appropriate for all uses.
-------
   Technology Demonstration of a Thermal Desorption/UV Photolysis
    Process for  Decontaminating  Soils Containing Herbicide Orange

         R.  Helsel,  E.  Alperin,  T.  Geisler,  A.  Groen,  R.  Fox
     International  Technology  Corporation,  312  Directors  Drive,
                     Knoxville,  Tennessee  37923

                          Major  T.  Stoddart
          U.S. Air Force, Engineering and Services Center,
                Tyndall Air  Force  Base,  Florida 32U03

                            H.  Williams
            EG4G Idaho, Inc.,  Waste Technology Programs,
                      Idaho  Falls,  Idaho 83415
         Laboratory and  field testing  determined the  effec-
         tiveness of a  new decontamination process  for  soils
         containing 2,*I-D/2,M,5-T and  traces  of dioxin.   The
         process employs  three primary  operations  -  thermal
         desorption to  volatilize  the  contaminants,  conden-
         sation  and  absorption   of  the  contaminants  in  a
         solvent,  and  photochemical  decomposition  of  the
         contaminants.    Bench-scale  experiments  established
         the relationship between desorption conditions  (time
         and temperature) and  treatment  efficiency.    Labora-
         tory   tests  using  a  batch  photochemical  reactor
         defined  the  kinetics  of  2,3,7,8-TCDD  disappear-
         ance.   A pilot-scale system was assembled to  process
         up to   100  pounds  per  hour  of  soil.    Tests  were
         conducted  at  two  sites  to evaluate  treatment  per-
         formance and develop scale-up information.  Soil  was
         successfully   decontaminated   to  less  than  1   ng/g
         2,3,7,8-TCDD  at temperatures above 460°C.
As part of a major program  being  conducted by  the U.S.  Air  Force  to
restore  to  normal use several  Department  of  Defense  sites  where
soils  have  been contaminated  with low  levels  of Herbicide Orange
(HO),  International  Technology Corporation  (IT), .under subcontract
to EG&G  Idaho,  has  been  conducting  a project  involving  laboratory
bench-scale and  field pilot-scale tests  to  demonstrate a new soil
treatment process  -  thermal desorption/UV photolysis (TD/UV).  The
intent  of the  demonstration  was to  reduce  the  combined  tetra-,
penta-, and  hexa-chlorinated  dibenzodioxin  (CDD) and  furan  (CDF)
congeners, which originated  from  the HO,  to less than 1 ng/g,  which
represented  the anticipated  soil  clean-up  criteria.    Treatment
should also effectively  remove the  primary  HO constituents,  2,U-D
-------
and  2,4,5-T.    Two  sites were  included  in the field  demonstration
project  for  the TD/UV process, each  having  substantially  different
types  of  soil  but  reasonably  similar  concentrations of  the  HO
constituents.   Testing at the Naval  Construction  Battallion  Center
(NCBC)  at Gulfport,  Mississiopi  was conducted  by  IT during  May
1985;  testing  at Johnston Island  (JI) in'the Pacific  Ocean occurred
in July  1986.   Based on  the  results  of these field pilot demonstra-
tions,  an engineering and  cost  evaluation  is being  performed  for
applying  TD/UV technology using  large, mobile systems for  these  two
sites  or  other sites having  similar contaminated soil  problems.
This  paper describes  the technology, highlights the  results  of  the
initial  laboratory  test  phase, and summarizes  the  field demonstra-
tion  results.

Process Description

The   thermal   desorption/UV  photolysis   process   developed   by   IT
accomplishes substantial  volume  reduction  and toxicity reduction  by
concentrating  the hazardous  constituents  contained in the  soil  into
a  small  volume  which  is  easier  to  treat  than large  quantities  of
soil.  The process incorporates three steps:

      Desorption - heating the soil to volatilize  the  organic
                   contaminants
      Scrubbing  - collecting  the volatilized  organics in  a
                   suitable  solvent
      Photolysis - converting  the contaminants  to  relatively
                   non-hazardous  residues  through  photochemical
                   reactions.

      A  schematic  block-flow  diagram  is  presented   as  Figure  1.
Contaminated  soil  is  passed  continuously  through  an indirectly
heated  desorber which  can  be one  of many  types of  conventional
equipment  applicable for  thermal processing of solids.  The  treat-
ment  performance of the  desorber  is controlled  by   the  residence
time  and  temperature of  the  soil.   Treatment requirements  (i.e.,
operating  conditions)  are determined by the volatility of the soil
contaminants and the required  contaminant  removal  efficiency  (final
versus initial concentration).
      The  off-gas leaving  the  desorber   contains  organic vapors,
water  vapor   originating  as   initial  soil   moisture,  and  small
quantities of  air which  enter with  the  soil.   Scrubbing using a
high  boiling  hydrocarbon solvent  is  used to  treat the off-gas  to
remove the organic contaminants and water  vapor by  cooling, conden-
sation, and absorption.   Particulates  (e.g.,  fine soil)  which may
be entrained  by  the  off-gas  are also collected  by   the  scrubbing
solvent.   Scrubbed  off-gas  is  passed through a conventional emis-
sion control system,  such as  carbon  adsorption,  to ensure that  no
organic  contaminants  or  solvent  vapors  are  released.   Scrubber
solvent  is recirculated  to  the scrubber  after  being   processed
through  a system  of  phase separation,   filtration,  and  cooling.
Condensed water, which is immiscible  with  the  solvent,  is  separated
and either directly  treated  using conventional tecnniques, such  as
filtration and  carbon  adsorption,  or discharged to  an  existing
-------
wastewater  treatment  facility.   Filtered  solids  are  recycled  to  the
desorber  or  packaged  as  process  waste'  for  off-site   disposal,
depending on the relative quantity and composition.
      A  small  portion   of   the  recirculated   solvent   stream   is
diverted  to a UV photolysis  system  to  treat (detoxify)  and  remove
the  organic contaminants, with  the  treated solvent purge  recycled
to  the  scrubbing  system.    The equilibrium  concentration of  the
contaminants  in  the  scrubber   solvent  is  maintained  as  high  as
practical to minimize the purge  stream and afford  higher  photolysis
reaction  rates,  thereby decreasing the  size  of  the  photolysis
treatment system.  The concentration limitation  is dependent  on  the
solubility  properties and partial pressure of the contaminants  in
the  solvent,  and the resultant effect on scrubber  efficiency  and
emission  potential.    The photolysis system  contains  a  specially
designed  flow  reactor which  subjects the  contaminant-laden solvent
to UV  radiation to  induce molecular  decomposition.  High intensity
mercury  vapor  lamps  produce'  a   band  of wavelengths,  some  of  which
match the absorption  energy of  the specific organic molecules being
treated.  Cooling is  provided to the reactor to remove the thermal
output  of the  lamp.   The photolyzed solvent is  treated  by  using
selected  conventional physical  or   thermal,  separation  processes,
such  as  distillation,   to  remove   the  reaction  product  residue.
Alternatively,  a  purge  of the  photolyzed solvent can be discarded
as  waste  to  control  the  levels  of  reaction  products in  the
recirculated solvent  system.
      Other  configurations  of   treatment  processes  using thermal
desorption  as  the primary  separation technique  can  be  applied  to
organically  contaminated  soils.     Alternative   physical/chemical
processes  can  be  used   to   treat   the  desorber  off-gas  and  the
contaminants.   To  achieve complete contaminant  destruction,  the
off-gas  can  be treated  by using conventional fume incineration  or
other  thermal   treatment  technology.   The  choice of  the type  of
desorber and off-gas  treatment   system depends on  the concentration
and  properties  of the chemical  contaminants, soil characteristics,
quantity of contaminated material, site characteristics,  availabil-
ity of off-site disposal, and regulatory and related requirements.

Laboratory Testing and Results - Thermal Desorption

Thermal  desorption    is   a  physical   separation   process,  although
chemical  transformation  of  the  organic  contaminants  may   occur
depending on  the  thermal stability  and  the operating  temperatures
required  to  achieve   adequate decontamination  efficiency.  Thermal
desorption has  been  used only  in  a  limited  number  of cases  (1-M)
for  treating   contaminated   soil,   and   these  applications  have
involved  relatively  volatile  organic compounds,  such as  solvents.
Because  of   the extremely  low  volatility  of CCD  and  CDFs,  the
development'  of basic treatability  data  was  essential  to confirm
that 1 ng/g levels in soil  could be  achieved and  that  the  required
desorption  conditions   were   practical,   considering  the  design
features and operating rates  of equipment  available for  performing
such treatment.
      Desorption treatability testing- was  conducted  on  samples  of
contaminated soil from three  HO contaminated sites - NCBC, JI,  and
-------
 Eglin  Air  Force  Base.   The  goals  of  the  test  effort  were  to
 evaluate the effect of time and temperature on 2.3,7,8-TCDD removal
 efficiency and  to  establish  the  importance  of soil  type.    The
 samples were  selected by the  Air Force  based  on  results  of site
 surveys to yield  high contamination  levels in order to investigate
 a broad range  of treatability.   This testing was  an  extension  of
 earlier testing  performed for the  EPA on  two  dioxin-contaminated
 soil  samples  from  Missouri  to  support  EPA's  mobile  incinerator
 trial burn in 1985 (5).
       After each  soil sample was blended,  air  dried,  and screened
 (2 mm  sieve  opening)  triplicate  aliquots were  taken  and analyzed
 for   2,3,7,8-TCDD,  CDD and  CDF congeners,  and  2,4-D  and 2,4,5-T.
 The   three  prepared   soils  had  2,3,7,8-TCDD   levels  greater  than
 TOO  ng/g and 2,4-0/2,4,5-T levels of  about  1000  ug/g.   The  JI soil
 had  significant concentrations of hepta and octa CDD  compared with
 the  other  two samples.  In addition,  selected  physical and chemical
 properties  presented  in Table  I,  were measured (6).   The EPA test
 program (5)  had   indicated  that  soil  properties  had  only  a  minor
 influence  on  removal  efficiencies  for 2,3,7,8-TCDD.

   Table I.   Physical-Chemical  Analysis of Prepared  Soil Samples
            Used for Laboratory Thermal Desorption Tests
Parameter
PH
Conductivity (millimhos/cm)
Organic matter (percent)
Cation exchange capacity
milliequivalents/100g)
Oil and grease content
( grams/ 100g)
Surface area (nr/g)
Particle size distribution
(percent)
Medium sand
Fine sand
Silt
Clay (<5 microns)
Moisture
JI
8.4
5.0
4.2
0.73

0.19

6.7


41
37
19
3
2.3
Eglin
3.8
0.15
1.2
0.77

0.41

2.5


41
52
5
2
0.79
NCBC
8.6
0.21
2.3
2.4

0.34

12.3


26
59
12
3
1.1
      A   series   of  10   individual   tests  was  performed   using
temperatures between  430 and 560°C and  treatment  times of 8  to  30
minutes.   Table  II  presents the test results, which are  comparable
to the earlier results  for  Missouri soils.   The  objective of  1  ng/g
2,3,7,8-TCDD  residual  in  soil  was  achieved  for all  three  soils
subjected  to the  highest temperature.  There was some difference  in
treatability observed between  the  three  soils at the lower tempera-
tures.   Also, longer treatment times  were required  for the  NCBC
soil because of the higher  initial 2,3,7,3-TCDD  level (500 ng•g vs.
100 ng.'g).   One   set  of treated test  samples  which contained  less
than  1  ng'g  2,3,7,8-TCDD was  also analyzed for  the  other CDD and
CDF congeners  and  2,4-0/2,4,5-T.   These results, shown in  Table
III,   indicate  greater  than  99.999 percent  removal of  the initial
-------
 2.4-D/2,4,5-T and  the  effective  removal of higher chlorinated CDDs
 and CDFs.

  Table  II.   Effect  of Treatment Conditions  on  Residual 2,3,7,8-TCDD
          in  Soil  During Laboratory Thermal  Desorption Tests
 Nominal Test
 Temperature
Soil
Time at Test
Temperature
2,3,7,8-TCDD
Concentration
   (ng/g)
CO
430


481





558


Identification
JI
Eglin
NCBC
JI
JI
Eglin
Eglin
NCBC
NCBC
JI
Eglin
NCBC
(min)
20
20
30
15
30
15
30
15
30
8
8
15
Initial
106
101
494
106
106
101
101
494
494
106
101
494
Final
38.5
4.4
26. 6a
4.5
1.6
1.1a
0.45
10.1
4.6
0.56a
0.71
0.76a
 'Average  of  duplicate  tests  or  duplicate  analyses.
  Table III.  Residual 2,4-D, 2,4,5-T, and CDD/CDF in Soil Samples
       Treated at  558°C  in  Laboratory  Thermal  Desorption  Tests
Concentration (ng/g)
Compound
2,4-D
2,4,5-T
TCDF
OCDFb
JI
ND*
16
0.6
0.3 .
Eglin
ND
0.8
0.4
ND
NCBC
ND
3
ND
ND
 *ND  = Not detected.
DNo  other CDD and CDF congeners were detected.

Laboratory Testing and Results - Photolysis

Photolysis has  had limited application  for treatment of hazardous
waste or  detoxification  of chemically contaminated materials.  The
susceptibility of  chlorinated aromatics, including herbicides such
as  2,4-D  and 2,4,5-T,  to UV-induced  decomposition  is well  estab-
lished  (7.8).    Photodecomposition  of  such   compounds  leads  to
successive  dechlorination  followed by  condensation  reactions  to
form phenolic polymers (7,8).  Other research-has demonstrated that
CDD  and  CDF  decompose   in   the  presence  of  UV  light  (8.9,10).
Development of a  photochemical process  for Destroying 2.3,7,8-TCDD
in  a waste tar  indicated similar  dechlorination  and condensation
reactions and products (8). The high-molecular  weight  end products.
which are similar in structure to humic  acids,  would be expected to
have low  toxicity and mobility.    Therefore,  essentially complete
-------
 conversion of toxic  constituents  could produce  a  potentially non-
 hazardous (according  to RCRA),  easily disposable residue.
       Laboratory photolysis  experiments were  designed to  confirm
 that 2,3,7,8-TCDD contained  in  the  selected  scrubber  solvent could
 be reduced  to  1 ng/g  and to determine  the  reaction  rates  of the
 primary HO constituents and 2,3,7,8-TCDD in that solvent matrix.   A
 previous  photolysis  process  for  2,3,7,8-TCDD  used  hexane  as  a
 solvent (8).  The solvent selected for use in the TD/UV process was
 different -  a  high  boiling (kerosene-like)  mixture  of  isoparaf-
 fins.    This hydrocarbon solvent  was  selected  because of  its very
 low  vapor pressure and  water solubility,  nontoxic  and nonflammable
 characteristics,  relatively low cost,  chemical  stability,  and good
 solvent properties  for  HO  constituents.  A second  major difference
 from earlier IT  photolysis studies was the  presence in the scrubber
 solution of  significant concentrations of other chlorinated organic
 reactants (2,4-D and 2,4,5-T)  which were also  subject  to photoly-
 sis.    In fact,   the  typical concentration ratio between 2,4-D  or
 2,4,5-T and  2,3,7,8-TCDD in the soil samples  used in the desorption
 treatability testing  was 2000:1.
       The three  steps of the laboratory program included generation
 of scrubber  solution, bench-scale  batch photolysis  reactions,  and a
 pilot  system trial.   In order  to generate a  representative  sample
 of scrubber  solution for  photolysis tests, a small desorption and
 scrubbing system was  assembled. .  A  portion of  the  prepared  samples
 of both NCBC and JI soil used for the  thermal desorption  tests was
 used  to generate scrubber solution.   Contaminated soil (-100  g) was
 placed  in a standard tube  furnace  apparatus which was  heated  to
 about  500°C  for 15  to 30  minutes.   A  nitrogen  purge swept  the
 vapors   into  the  scrubbing  system,  which  consisted  of  several
 solvent-filled   impingers.    Analysis  of  the   prepared   scrubber
 solutions indicated  thermochemical  conversion  of the  2,4-D  and
 2,4,5-T in the contaminated soil to  the corresponding  chlorophenols
 at  molar  equivalents.     In  addition  to  using  prepared  scrubber
 solutions, solvent  spiked with  2,4-D and 2,4,5-T, the  corresponding
 chlorophenols,  or  2,3,7,8-TCDD  was  used   for  baseline photolysis
 tests.
      Most  photolysis  experiments were conducted  in   a 0.5  liter
 capacity   standard   quartz   photochemical   reactor   using   either
 recirculation or  bottom  agitation  for heat  and mass transfer.   Both
 100- and  450-watt high  pressure quartz  mercury  vapor lamps (Canrad-
 Hanovia,  Inc., Catalog  Nos. 608A and 679A) were  used,  depending  on
 the   initial  reactant   concentration  in   the   particular solvent
 solution  being  tested.     The  wavelengths  of  interest  based  on
 spectrophotometric  absorbance measurements of 2,3,7,8-TCDD,  2,4-D
 and  2,4,5-T  were in  the 280 to 320 nra region.   Isopropyl alcohol
 (-0.05  g/g solvent  solution)  was used as a  proton donor  to minimize
 formation of polymeric  reaction by-products which  tend  to  foul  the
 light  transmission  surfaces (8).   The  bench-scale  photolysis  tests
 gave  the  following results:

 1.  All  compounds disappeared  to  below  the  analytical  detection
    limits.
2.  The  concentration  of 2,3,7,8-TCDD  was  reduced   to  less  than
    1 ng/g from initial concentrations as high as 200  ng/g.
-------
 3.  For  a  given  reactor  configuration  and  lamp  wattage,  the
     reaction rates  of 2,3,7,8-TCDD  and  2.4,5-trichloropnenol were
     proportional  to  the  concentration,  indicating  pseudo-first
     order kinetics in agreement with previous work (8).
 4.  Absorbence of UV  energy by the solvent,  which increased during
     irradiation,  resulted  in  low  quantum  yields  and  low  rate
     constants.
 5.  Insoluble  brown  reaction  products  (presumably  phenolic  tars)
     were deposited on  the surfaces of the reactor  vessel  and lamp
     well.   This  expected phenomenon plus the  high  solvent absorb-
     ence demanded a careful reactor selection and photolysis system
     design.

 Trials  using  a  pilot  reactor  system described  in the  following
 section  were   performed   in  the  laboratory   to  establish  reactor
 efficiencies and  operating characteristics  prior to transport  to
 the field.   A  synthetic  scrubber  solution was prepared  containing
 2,4,5-trichlorophenol at a concentration (-2,000 ug/g)  projected to
 be  representative  of  the  planned  field  tests.    Kinetics  were
 determined to  be first-order with a rate  constant  of 0.07  sec~1.

 On-site Pilot Testing and Results

 Based   on  the   information developed  from   the  laboratory   test
 program,  a  pilot-scale TD/UV  system was  designed  and  assembled.
 Three   skids  were  used  to   mount  the  desorber,   scrubber,  and
 photolysis  systems;   the  largest  skid  was  1.5  meters  by  4.3
 meters.      A   conventional  pilot-scale,  rotary,   indirect-fired
 calciner  was used  as the  desorber.   The  calciner  consisted of  a
 3-3  meter long  by  16  cm internal  diameter  rotating tube  through
 which  the  soil  was  transferred,  and  a gas-fired  furnace  which
 surrounded  the  middle 2.0 meters  of the  tube  length.  The  initial
 and  final tube sections  were  used for  soil  feeding and  cooling.
 The  flow  rate  and residence  time of soils  traveling  through  the
 desorber  were  controlled  by  varying  the  tube  inclination  and
 rotational   speed.     Temperature  of  the  soil   was measured   at
 different locations  by  a thermowell  probe  extending  inside  the
 tube.   Soil was  fed to  the desorber from a  small  hopper using  a
 variable  speed  screw  conveyor.   Soil leaving  the  tube was  collected
 in a sealed  metal can.
      The off-gas  transfer  and  scrubbing  system was  designed  to
 enable  recirculation  of  scrubbed off-gas  through  the  desorber.   The
 entire  off-gas  treatment  and   recirculation  system,  including  the
 desorber  and scrubber, was operated at a  slightly  negative  pressure
 to  prevent  potential  fugitive emissions.   A  small  amount of  air
 entered  the system  with  the  soil  feed  or  through  seal  leakage.
 Nitrogen  was added to the  recirculated  gas  stream to maintain  the
 oxygen  concentration  below the  level  necessary to support  combus-
 tion.  This  was an extra  safety  feature since  the  vapor pressure  of
 the solvent  at  normal scrubber  operating  conditions  is very  low.   A
 portion  of  the  scrubbed  off-gas  was vented  from the recircuiation
system  to maintain  proper  pressure  in  the   system.    This  purge
stream was  passed through a small  HEPA  filter and caroon adsoroer
before  being discharged  to the atmosphere.    The  soivent system
-------
 consisted  of  a scrubber,  receiving and  separation  tank,  storage
 tank,  recirculation  pump,  filters  for  removing suspended  solids,
 and  solvent  cooler.
      The  photolysis  system was  independent  of  the  desorber  and
 scrubber  systems;  its design  capacity  was lower than necessary  to
 match the  desorber's soil-processing rate.   A  portion  (about UO  kg)
 of  contaminant-laden  solvent  was  taken  from  the  scrubber  system
 after completion of one  or  more  desorption  tests and transferred  to
 the  photolysis  system.     This  system  consisted  of  an agitated
 storage tank,  solvent recirculation pump,  and  photochemical  reactor
 with  associated  cooling,  DC  power supply,  and  controls.   The
 selected  type  reactor  was a  standard quartz  falling-film  unit,
 approximately  10  cm  in  diameter and 50 cm  long (Ace Glass,  Inc.,
 Part No.  7898).   A 1200  watt high  intensity mercury vapor lamp was
 inserted  through  a  central  quartz tube  within  the  reactor   to
 irradiate  the  solvent as  it  flowed by  gravity down  the  circum-
 ference of  the reactor body.  The  solvent was  recirculated  through
 the  reactor  for   many  cycles   to  achieve  sufficient  irradiation
 (e.g., reaction) time.
      Five  desorption tests were   carried  out  at  NCBC  at  various
 treatment  conditions.   A total  of 800 kg  of soil was  processed;
 soil was  prepared  by drying and crushing  to less than  1/2  inch  to
 allow proper flow  in the desorber  feed mechanism, and blending for
 uniformity.   Each  test lasted  5  to  10 hours,  including  the  heat-up
 and  cool-down  cycle.  Samples of   feed soil and treated soil were
 taken during steady-state  operation,  and  samples  of  the scrubber
 solvent and  vent  carbon  were taken  at  the conclusion  of each run.
 Samples  were  analyzed  for 2,4-D,  2,4,5-T,  other HO   indigenous
 compounds,  priority  pollutant  organics and  metals,  and  tetra-hexa
 congeners of CDD and  CDF.   In addition, 2,3,7,8-TCDD concentrations
 of treated soil and  photolyzed solvent samples  were determined on a
 quick-response  basis  to  enable  adjustment  of  the operating  condi-
 tions in subsequent  tests.   Fresh  solvent  and  carbon were used for
 each test, and  the entire desorber  and scrubber  network  was  cleaned
 out  between  tests.   This  cleaning  enabled  thorough  inspection of
 the  condition  of   the  equipment   and  provided  several different
 compositions  of  contaminated  solvent  to  use  in the   photolysis
 tests.
      Table  IV  shows  the effect  of different soil temperatures and
 residence  times on   residual  2,3,7,8-TCDD  for NCBC  pilot   tests.
Table V  presents  the analytical  results  for  2,4-D,  2,4,5-T, and
 total CDD  and CDF.   Analytical detection  levels for 2,3,7,8-TCDD
and  the  various congeners  were  generally  less than  0.1  ng/g but
varied from sample to sample, ranging from 0.018 ng/g to 0.51 ng/g.
-------
 Table  IV.  Effect of Treatment Conditions on Residual 2,3,7,8-TCDD
             During NCBC Pilot Thermal Desorption Tests


Test No.
1
2
3
4
5
Soil Feed
Rate
(kg/hr)
13.6
13.6
25
44
20
Residence
Timea
(min)
40
40
19
10.5
24
Soil
Temperature
2,3

,7,8-TCDD
(ng/g)
(°C) Initial Residual
560
560
560
560
460
260
272
236
266
233
ND
ND
ND
ND
0.5
       residence  time  in  heated  zone.
          Table V.   Residual  2,4-D,  2,4,5-T,  and  CDD/CDF in
                 NCBC Pilot Thermal Desorption Test
Concentration (ng/g)
Compound
2,4-D
2,4,5-T
TCDD
PCDD
HCDD
TCDF
PCDF
HCDF
CDD and
Test 1
180
500
NDa
ND
ND
ND
ND
ND
ND
Test 2
150
270
0.23
ND
ND
ND
0.14
ND
0.37
Test 3
20
60
0.11
ND
ND
ND
ND
ND
0.11
Test 4
-
_
0.61
ND
ND
0.13
0.5^
ND
1.28
Test 5
170
1240
0.75
ND
ND
0.95
1.0
ND
2.70
  CDFC
aND  = not detected.
bTotal of quantified values  for detected cogeners.

      All test  conditions  produced  soil  containing  less  than  1  ng/g
2,3,7,8-TCDD.   The total quantified tetra-hexa congeners  were  less
than the treatment goal  of 1 ng/g for the first three tests, which
were  performed  at the  lower feed  rates.   Test  4,  made  at  the
highest  feed rate, nearly  met this value,  whereas the much lower
soil temperature used  for  the final test resulted  in almost 3  ng/g
combined residual  CDD  and  CDF.  A longer residence time could  have
improved this  performance.   Residual  2,4-D  and 2,4,5-T concentra-
tions were   less  than  1  ug/g for  all but  the final  test.    This
reduction represents greater than 99.97 percent removal efficiency
for these primary  HO constituents.
      Because of  the very  low  moisture content  of the prepared  soil
feed, an  insufficient  volume  of  aqueous  condensate  was  collected
from the tests  to perform analysis or  treatability tests.  A  venc
gas sample  was  taken,  but no  valid  analytical  results were gener-
ated because of delays in  sample  processing.  However, analysis of
the  carbon   used   in the  emission  control  adsorbers  enabled   some
evaluation  of  scrubber  performance  and  process  emission  poten-
tial.  Or.ly  tne  front  (upstream)  portion of  carbon  from one of  the
-------
 tests showed  detectable levels of  any  CDD or CDF.   No HO consti-
 tuents were  detected in the downstream portion  of carbon.   Calcu-
 lated scrubber  removal  efficiencies exceeded 99.9 percent for CDD,
 CDF, 2,4-D, and  2,4,5-T.   Vent gas  volume was about 0.05 nP/minute
 for all tests.
       Results of the photolysis  tests  are presented  in  Table VI.
 The  total  solvent  volume  (-10.5 1)  was  recirculated  through the
 reactor at 0.75 1/min  for 6.5  hr,  resulting in 28  cycles  with an
 irradiation  time of about  1.5 sec/cycle.   The  photolysis  system
 operating  time   was  selected  based on  the  laboratory  trials  to
 achieve less than 1 ng/g 2,3,7,8-TCDD; the actual residual level of
 0.36 ng/g  represented  greater than  99  percent  conversion.    The
 reaction conversion of  the other  CDD  and  CDF congeners varied from
 85  to  99  percent.   Photolysis reduced  the  concentrations  of 2,4-
 dichlorophenol   (2,4-DP)   and  2,4,5-trichlorophenol   (2,4,5-DP),
 (corresponding  to the  2,4-D   and  2,4,5-T present  in  the  initial
 soil) by 85 and  97  percent respectively.  Figure  2  shows the rate
 of  disappearance  of  2,3,7,8-TCDD,  2,4-DP,  and  2,4,5-TP.     As
 demonstrated  during  the  laboratory tests,  the reaction  kinetics
 were pseudo-first order over  the  given  range of  concentrations.
 The  reaction  rate  constants   were  similar  for  the three  species
 (0.11 sec"1,  0.04 sec"1,  and  0.08  sec"  ,  respectively);  the  rate
 constant  for  2,4,5-TP  was  comparable  to that  determined  in  the
 laboratory  trials of the pilot  system.

   Table  VI.   Initial vs  Final  Concentration of Selected Compounds
        in Scrubber Solution  from NCBC  Pilot Photolysis  Tests
Compound
2 , 4-Dichlorophenol
2,4,5-Trichlorolorophenol
2,3,7,8-TCDD
Total TCDD
Total PCDD
Total HCDD
Total TCDF
Total PCDF
Total HCDF
Concentration
Initial
490,000
977,000
43.3
46.3
15.7
0.84
31.0
3,7
1.7
(ng/g)
Final
82,000
31,000
0.36
0.92
2.3
0.037
3.8
1.1
0.0031
      Three desorption  tests  and  one  photolysis  test  were  conducted
at  JI  to compare the effects of different soil  characteristics  and
investigate higher  processing rates.   The coral-like soil used  for
the  tests contained  lower  levels of  HO contamination  than NCBC
(about 50 ng/g  versus  250 ng/g).   As much as  95 kg/hr of soil  was
successfully decontaminated  to  less  than 1 ng/g 2.3,7,8-TCDD  using
desorption  temperatures  of  550°C.   Treated  soil from  all  three
desorption tests  had  nondetectable residual  tetra-hexa CDD  and  CDF
cogeners,  2,4-D  and   2,4,5-T,   and  corresponding   chiorophenols.
Analysis of carbon  removed from  the  desorber-scrubber system vent
showed  no detectable  concentration  of  CDD  or  CDF.    Gas  samples
taken  downstream  of   the  carbon  adsorber  showed  nondetectable
concentratio-s  of CDD  and  CDF,   2,4-D  and  2,4.5-T,  and  chloro-
-------
 phenols.     Photolysis  test  results  were  comparable  with  NCBC
 tests.   Initial concentrations of HO  contaminants  were much higher
 in  the  scrubber solvent due to processing of considerably more soil
 and  use of  less solvent.   The  concentration  of  2,3,7,8-TCDD  was
 reduced  from  780  ng/g to  less  than  0.7 ng/g  during  12 hours  of
 system  operation  (representing about 80 sec reaction  or irradiation
 time).   Total  chlorophenols were  reduced from 130 ug/g to less than
 6 ug/g,  and  tetra-hexa  CDD  and  CDF  cogeners  were  effectively
 treated.    Reaction  rate  constants  for  specific  compounds  were
 essentially  the same between the  NCBC and JI photolysis  tests.   At
 JI  as  at  NCBC,  brown  residues were  deposited  on  the  reactor
 surfaces,  and  solvent discoloration  was obvious, but  there  was  no
 evidence of rate retardation.

 Conclusions

 The  effectiveness  of  thermal  desorption  to   decontaminate  soil
 containing HO and of UV photolysis to  destroy HO toxic constituents
 has  been  demonstrated  in   bench-  and  pilot-scale  tests.     Some
 additional technical information  is needed  for a  complete  evalua-
 tion of  the process  and  to  provide the basis for design  of  a full-
 scale system for on-site  remedial action.  This  project illustrates
 the  requirements  for  developing   and   implementing   new   process
 technology  for  solving  contaminated-soil  environmental problems.
Only through such demonstration efforts  can more  cost-effective and
environmentally  sound   remedial  action  alternatives   be  made
available.

Literature Cited

 1.    Noland,  J. W.; NcDevitt, N.  P.; Koltuniak,  D. L.  Proc.  of the
      National   Conference   on   Hazardous   Wastes   and  Hazardous
      Materials. Atlanta.  GA. March 4-6. 1986. DP. 22Q-232.
 2.    Hazaga,   D;  Fields,   S;  Clemmons,  G.  P.   The   5th National
      Conference on   Management  of   Uncontrolled  Hazardous  Waste
      Sites.  Washington,  DC, November 7-9, 1984, pp 404-406.
 3.    Webster,   David M.    J.  Air  Pollution Control   Association.
      1986, 36,  pp  1156-1161"'
 4.    Hoogendoorn,  D.    Proc.  of the  5th  National  Conference on
      Management of Uncontrolled Hazardous Waste Sites. Washington.
      DC, November  7-9, 1984, pp 569-575.
 5.    Helsel, R.; Alperin, £.; Groen,  A.; and Catalario,  D. "Laboratory
      Investigation  of Thermal Treatment  of Soil Contaminated With
      2,3,7,8-TCDD,"  draft  report to U.S.  EPA,   Cincinnati,  OH on
      Work  Order BAD001,  D.U.D-109,  IT Corporation, Knoxville, TN,
      Dec.  1984.
 6.  ..Arthur, M. F.;  Zwick,  T.  C. "Physical-Chemical  Characteriza-
      tion  of Soils," Battelle  Columbus Laboratories,  Columbus, OH,
      1984.
 7.    "Report  on 2,4,5-T,  A Report  on  the  Panel on  Herbicides of
      the President's Science Advisory Committee," Executive  Office
      of  the President,  Office of Sciences  and  Technology,  March
      1971.
-------
  8.   Exner, J.  H.;  Johnson,  J. D.;  Ivins,  0.  D. ;  Wass, M.N.;  and
       Miller,  R.  A.   "Detoxication  of Hazardous Waste," Ann  Arbor
       Science Publishers, Ann Arbor, MI, 1982, p 269.
  9.   Exner,  J.   H.;  Alperin,  E.   S.;  Groen,  A.;  Morren,  C.  E.;
       Kalcevic,  V.;  Cudahy, J.  J.; and Pitts,  D.  M. "Chlorinated
       Dioxins  and Dibenzofurans in  the  Total Environment," Keith,
       L.   H.;   Rappe,   C.;  Choudhary,   G.;   Eds.,    Butterworth
       Publishers, Stoneham, MA,  1985, p 47.
 10.   Exner,  J.   H.,   Alperin,  E.  S.;  Groen,  A;   Morren,  C.  E.
       Hazardous Waste. J_, 1984,  pp 217-223.
WPR:thermal
-------
Contaminated
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Solvent Residues
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                             \	i
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-------
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-------