EPA/600/9-91/010
April 1991
OPERATIONS AND RESEARCH AT
THE U.S. EPA INCINERATION
RESEARCH FACILITY: ANNUAL
REPORT FOR FY90
By
1. R. Waterland and J. W. Lee
Acurex Corporation
Environmental Systems Division
Incineration Research Facility
Jefferson, Arkansas 72079
EPA Contract 68-C9-0038
EPA Project Officer: R. C. Thurnau
Waste Minimization, Destruction, and Disposal Research Division
Risk Reduction Engineering Laboratory
Cincinnati, Ohio 45268
RISK REDUCTION ENGINEERING LABORATORY
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
CINCINNATI, OHIO 45268
Printed on Recycled Paper
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NOTICE
This material has been funded wholly or in part by the
United States Environmental Protection Agency under Contract #68-
C9-0038 to Acurex Corporation. It has been subject to the
Agency's review and it has been approved for publication as an
EPA document. Mention of trade names or commercial products does
not constitute endorsement or recommendation for use.
11
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ABSTRACT
The U.S. Environmental Protection Agency's Incineration Research Facility in Jefferson,
Arkansas, is an experimental facility that houses two pilot-scale incinerators and the associated
waste handling, emission control, process control, and safety equipment; as well as onsite
laboratory facilities.
During fiscal year 1990, two major test programs were completed at the facility: an
evaluation of the thermal-stability-based principal organic hazardous constituent incinerability
ranking for the Office of Solid Waste (OSW), and an incinerability evaluation of five
contaminated materials from the Purity Oil Sales and the McColl Superfund sites for Region 9
and the Office of Emergency and Remedial Response (OERR). In addition, results of two test
programs completed in FY89 were reported: an evaluation of the fate of trace metals fed to a
rotary kiln incinerator equipped with a single-stage ionizing wet scrubber for air pollution control
for OSW, and an incinerability evaluation of arsenic and pesticide contaminated soils from the
Baird and McGuire Superfund site for Region 1 and OERR. Several facility and equipment
construction and upgrade efforts were also completed.
in
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TABLE OF CONTENTS
Section
1
2
3
Page
ABSTRACT .... iii
FIGURES vii
TABLES ..... . ...... . . i viii
INTRODUCTION . 1
ROTARY KILN INCINERATION SYSTEM
RECONFIGURATION AND UPGRADE 4
2.1 ROTARY KILN SYSTEM UPGRADES . ....... . . . 4
2.1.1 Combustion System Repairs . . . ... ,- 4
2.1.2 Venturi/Packed Column ScrubBer Reconfiguration 6
2.1.3 RKS Automation with the Foxboro Process Control System 7
2.1.4 Ram Feeder . 7
2.2 BUILDING AND GROUNDS IMPROVEMENTS 8
2.2.1 Office Space . . 8
2.2.2 Flammable Chemical Storage Building . 8
2.2.3 Building Roof Repair ... ..... . . . ; . .' 8
2.2.4 Secured Tools/Parts Storage . 8
2.2.5 Worker Shower and Cool Down Facility ..;'".' 9
2.2.6 Electrical systems 9
2.2.7 IRF Scale Model ...... 9
2.3 MISCELLANEOUS PROJECTS FOR FUTURE
IMPLEMENTATION ........ ........ .... ;. Xi . v 9
2.3.1 RCRA Slowdown Tank Storage System ... . VI. .. ...-.'.' 9
2.3.2 Scrubber Suspended Solids Removal System . -. .......;......... 9
2.3.3 Slagging Kiln Recommendation .........................;.. 10
FATE OF TRACE METALS IN THE ROTARY KILN
INCINERATION SYSTEM WITH AN IONIZING WET SCRUBBER 11
3.1 TEST PROGP.AM . 11
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TABLE OF CONTENTS (concluded)
Section
4.3
5
7
8
Page
3.1.1 Synthetic Waste Mixture u
3.1.2 Test Conditions . ;*. 14
3.2 TEST RESULTS .-. 14
3.2.1 Average Trace Metal Discharge Distributions . 14
3.2.2 Effects of Incinerator Operating Conditions on Metal
Distributions ..:.... 19
3.2.3 Metal Distributions in Flue Gas Particulate by Particle Size 19
3.2.4 Apparent Scrubber Collection Efficiencies 21
3.3 CONCLUSIONS , 23
INCINERABILITY TESTING OF ARSENIC-CONTAMINATED SOIL
FROM THE BAIRD AND MCGUIRE SUPERFUND SITE 27
4.1 MUFFLE FURNACE EXPERIMENTS 28
4.2 PILOT-SCALE INCINERATION TESTS . 29
4.2.1 Test Program 29
4.2.2 Test Results , ,[ 29
CONCLUSIONS 34
INCINERABILITY TESTING OF CONTAMINATED SOILS FROM THE
PURITY OIL SALES AND THE McCOLL SUPERFUND SITES 37
5.1 TEST PROGRAM 38
5.2 TEST RESULTS 40
5.3 CONCLUSIONS 44
PARAMETRIC TESTING TO EVALUATE THE PROPOSED POHC
INCINERABILITY RANKING . 46
6.1 TEST PROGRAM 46
6.2 SAMPLING AND ANALYSIS 47
63 TEST RESULTS ; 50
EXTERNAL COMMUNICATIONS ...,:........... 52
PLANNED EFFORTS FOR FY91 . .......... ... ... 56
VI
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FIGURES
Number Page
1 Schematic of the IRF rotary kiln incineration system .. . 12
2 Sampling protocol 17
3 Normalized distribution of metals in the discharge streams . 18
4 Effects of kiln temperature on the discharge distributions of cadmium,
bismuth, and lead 20
5 Average of metal distributions in the afterburner exit flue gas particle
size fractions 21
6. Effects of kiln temperature, afterburner temperature and waste feed
chlorine content on the distribution of metals in the afterburner exit flue
gas particle size fractions 22
7 Apparent scrubber collection efficiencies for metals . 23
8 Apparent scrubber collection efficiencies for metals showing associated
variations with changes in kiln exit temperature and waste feed chlorine
content 24
9 Sampling matrix 30
10 Sampling matrix 39
11 Sampling matrix . . . ; 51
vu
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TABLES
Number
1
2
3
4
5
6
7
8
9
10
11
12
13.
14
15
16
17
Page
Design characteristics of the IRF rotary kiln system 13
POHC concentrations in clay/organic liquid feed -.,.... 15
Average integrated feed metal concentrations 15
Target and average achieved test conditions 16
Semivolatile organic hazardous constituents in test soils 31
Normalized metal discharge distributions for the Baird and McGuire
incineration tests
32
Apparent particulate and metal scrubber collection efficiencies 33
Arsenic fractions TCLP leachable 33
Nominal incinerator system operating conditions for Purity Soil Sales and
McColl Site soil incineration tests . . 38
Ultimate analysis of the test soils and resulting kiln ashes 41
Semivolatile organic hazardous constituents in test soils 41
Lead distributions for the Purity Oil Sales site soil tests . . : 42
Lead discharge distributions for the Purity Oil Sales site soil tests . 44
Incinerability ranking mixture composition 48
Test conditions 49
IRF program reports and presentations in FY90 53
Visitors to the IRF 54
Vlll
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SECTION 1
INTRODUCTION
The U.S. Environmental Protection Agency's (EPA) Incineration Research Facility
(IRF) in Jefferson, Arkansas, is an experimental facility that currently houses two pilot-scale
incinerators (a rotary kiln incineration system and a liquid injection incineration system) and
their associated waste handling, emission control, process control, and safety equipment. The
IRF also has onsite laboratory facilities for waste characterization and analysis of process
performance samples.
The objectives of research projects conducted at the IRF have been and continue to be
as follows: -'._-.
To develop technical information on the performance capability of the hazardous
waste incineration process to assist EPA Regional Offices and state environmental
agencies in the review, assessment, and issuance of reasonable and responsible
permits for regulated hazardous waste incineration facilities, and to assist waste
generators and incinerator operators in the preparation of permit applications
To develop incinerator system performance data for regulated hazardous wastes
to support current Resource Conservation and Recovery Act (RCRA) incinerator
regulations and performance standards, and to provide a sound technical basis for
any necessary future standards
To promote an understanding of the hazardous waste incineration process and
develop methods to predict the performance of incinerators of varying scale and
design for the major classes of incinerable hazardous wastes as a function of key
process operating variables. These methods would also help to simplify and
perhaps reduce the cost of permit and compliance testing.
To develop methods of improving reliability and control of the incineration
process, including the use of destruction and removal efficiency (DRE) surrogates
To provide a means of conducting specialized test burns (particularly for high
hazard or special waste materials such as Superfund site wastes) in support of
specific Regional Office permitting or enforcement actions and Regional Office
or private party Superfund site remediation efforts
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To test the performance of new and advanced incinerator components and
subsystems, and emission control devices
During fiscal year 1989 (FY89, October 1, 1988, through September 30, 1989) the IRF
underwent a major expansion and reconfiguration construction effort, detailed in the annual
report for FY891. As part of this expansion and reconfiguration effort, a new building
encompassing the former 3100 ft2 facility building was erected to .bring total enclosed space to
15,200 ft2. During construction, the facility's rotary kiln incineration system (RKS) was relocated
entirely inside the former building area; an ionizing wet scrubber was installed as a second
primary air pollution control system (APCS) for use in place of the venturi/packed column
scrubber originally installed; and a new carbon bed/high-efficiency particulate (HEPA) filter
secondary APCS was installed.
The FY89 RKS reconfiguration effort, as originally planned was not completed in FY89.
Instead, an interim configuration in which the ionizing wet scrubber could be operated was
completed. This configuration was used to support two incineration test projjrams in FY89.
Thus, completion of many aspects of the originally planned RKS reconfiguration and upgrade
was suspended in FY89 so that the two test programs could be performed. As a consequence,
a significant RKS reconfiguration and upgrade effort continued during FY90, resulting in the
completion of the original reconfiguration plans. This effort included:
9 Relocating the venturi/packed column scrubber system within the former building
area
» Replacing the RKS kiln refractory
» Installing a refractory-lined afterburner extension so that afterburner flue gas
residence times could be increased into the more typically encountered range, and
so that isokinetic afterburner exit flue gas sampling was possible
« Installing a new afterburner flue gas quench system
0 Installing new scrubber exit ductwork, sampling platforms, and stack
o Installing the automated process control system purchased in FY89, and bringing
it into operation
Much of this reconfiguration and upgrade effort was completed in the October through
December 1989 time period. A period of testing activity followed in January and February 1990.
The reconfiguration and upgrade effort was then completed during the March through May 1990
period, followed by another period of testing activity in June and July 1990.
Two major EPA Program/Regional Office programs were supported through test
activities in FY90.
i .
c The hazardous waste incinerator regulation development program within the
Office of Solid Waste (OSW), via testing to evaluate the principal organic
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hazardous constituent (POHC) incinerability ranking developed under other OSW
support efforts
The Superfund site remediation program within the Office of Emergency and
Remedial Response (OERR) as administered by EPA Region 9, via treatability
testing of contaminated soil from the Purity Oil Sales and McColl Superfund sites
in California
In addition, the results of a series of trace metal fate tests in the RKS with an ionizing wet
scrubber for particulate and acid gas control, and the results of treatability testing of
contaminated soil from the Baird and McGuire Superfund site in Massachusetts, both completed
at the end of FY89, were assembled and reported in FY90.
Activities completed during FY90 are discussed in more detail in the following sections.
Section 2 describes the RKS reconfiguration and upgrade efforts completed. Section 3 discusses
the results of the trace metal ionizing wet scrubber tests reported in FY90. Section 4 discusses
results of the Region 1 Superfund treatability tests reported in FY90. Section 5 discusses results
of the Region 9 Superfund soil treatability tests completed in February 1990. Section 6 describes
the POHC incinerability ranking tests completed in July 1990. Section 7 discusses external
communication activities associated with the facility and its operation. Section 8, the final
section, presents an outline of plans for activities to be completed in FY91.
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SECTION 2
ROTARY KILN INCINERATION SYSTEM RECONFIGURATION AND UPGRADE
During FY90, significant efforts were devoted to improving the reliability and ease of
operation of the RKS, and to implementing features required for good functioning of the
expanded building completed in FY89.
RKS-related tasks in FY90 included repairing and replacing hardware components;
completing the reconfiguration of the RKS; installing an automatic process control system; and
formulating plans and designs for further improvements to be implemented in FY91. Facility
and building related activities included installing a secured tools/parts storage area, installing a
flammable chemical storage building; implementing a shower and cool-down facility for test
support staff; and arranging for more adequate office space. These activities are discussed in
the following sub-sections.
2.1
ROTARY KILN SYSTEM UPGRADES
The following discussion focuses on the activities related to the RKS. Needed repairs
and upgrades that were either completed or initiated in FY90 are discussed in turn.
2.1.1 Combustion System Repairs
I
Several components of the RKS required maintenance or repair during FY90. Efforts
completed are discussed in the following.
RKS Refractory
The IRF RKS has seen extensive use since 1985. As would be expected, by 1989 the
refractory linings of the combustion chambers were nearing the end of their useful 'lives. In
FY89, the refractory in the afterburner chamber was replaced. In FY90, the refractory in the
kiln chamber had deteriorated to the point that hot spots were beginning to develop on the kiln
outer steel shell.
Between October 9 and 12, 1989, the RKS kiln refractory was removed and replaced.
The incinerator was operated for several days per manufacturer prescribed heat- up schedule to
cure the refractory. However, on November 17, during routine operation of the RKS in a
shakedown mode, the IRF staff discovered that the newly-installed RKS kiln chamber refractory
had developed severe cracks. The refractory installation contractor was called in to inspect the
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failed refractory. The contractor attributed the failure to the selection of incorrect materials for
the application.
After consulting with the refractory manufacturer, the contractor recommended a
different refractory, Plibrico HyResist 3000, to be used. This replacement refractory was
installed on December 8, and cured from December 11 through 18. Experience during that
period confirmed that the single layer cast replacement refractory had less insulating property,
when compared to the former two-layer construction. Kiln steel shell temperatures between 400
and 500°F were established when the kiln was operated at 1800°F. This was in reasonable
agreement with heat transfer calculations that predicted a metal shell temperature of about
400° F. These temperatures were judged to be acceptable. The refractory appeared to still be
in good condition at the end of FY90.
Induced-Draft Fan #2
Over the past four years, the induced-draft (ID) fan just upstream of the stack has failed
several times. On December 18, 1989, the same fan failed once again. Inspection of the ID fan's
fiberglass-reinforced-plastic (FRP) impeller revealed that its hub had developed a crack and had
opened sufficiently to lose the press-fit with its drive shaft. Several cracks had also developed
at the vane-to-hub joint. The IRF staff members explored options in an attempt to correct the
situation expeditiously but could not identify any reliable and minimal-effort approach to do so.
Therefore, an identical replacement impeller was purchased and installed on January 17.
On initial start-up, the fan operated with little vibration and appeared to function
properly. During the next several days, however, fan vibration and noise increased gradually but
noticeably. On January 23, the vibration level became alarmingly high. Inspection of the newly-
installed impeller revealed cracks that were similar to, but somewhat more severe than, those
found on the previously-failed impeller. The modes of failure during these two episodes were
consistent with earlier failures.
The repeated failure of the RKS induced-draft fan #2 prompted efforts to identify
alternative equipment options to replace the apparently unreliable fan component. The IRF staff
was able to locate a local fan manufacturer who could fabricate an impeller out of 316 stainless
steel material. The fan, using the stainless steel impeller, was reassembled and the RKS resumed
operation on January 30. An identical impeller was purchased and stored at the IRF as a ready
replacement in case the impeller should also fail prematurely. To date, the stainless steel
impeller has performed well, with only one malfunction that was related to a failed bearing. That
malfunction did not result in any extended system downtime.
Rotary Kiln Drive System
It has been known for some time that performance of the rotary kiln drive mechanism
is not optimal. For example, the rotating chamber tends to migrate axially. Often, the axial
travel is sufficiently large to cause the chamber to jam against the fixed end plates. This
resulting friction has caused excessive wear and can prevent the kiln drum from rotating at all.
In addition, deterioration of mechanical parts has reduced the range of kiln rotation speed
control. The increasingly limited rotation control limits flexibility in changing solid residence
times in the kiln.
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In August 1990, the IRF staff began investigation into possible solutions. By the end
of September, design concepts were finalized, and an improved kiln drive system will be
implemented in FY91.
Natural Gas Supply Pipe Repair
Small leaks from the natural gas supply system were discovered in the new building
during August 1990. The possibility of catastrophic natural gas explosion mandated the situation
be corrected before natural gas use resumed. The leaks were traced to pipe joints that
developed seepage since the time of the original installation. The IRF staff took this opportunity
to make a few improvements in the natural gas system. These included removing union joints
and directing pressure regulator vents out of the building. These corrective measures were
completed in September. It was further decided in September to replace all threaded pipe joints
at the gas supply main entry to the building by weld joints.
2.1.2 Venturi/Packed Column Scrubber Reconfiguration
As discussed above, plans to reconfigure the RKS air pollution control systems were
substantially completed in FY89. The reconfiguration resulted in the entire RKS residing in the
old incinerator test bay. A significant portion of this reconfiguration effort was completed in
FY89, including the installation of the new secondary air pollution control system (demister,
activated carbon adsorber, and high efficiency particulate filters) and the installation of the
ionizing wet scrubber. The RKS was returned to testing operations after this first phase of
reconfiguration in FY89.
The remaining reconfiguration efforts were scheduled to take place in FY90. They
involved relocating the venturi/packed column scrubber and the associated controls to a more
appropriate location; installing a heat exchanger system to cool the scrubber liquor; installing a
new refractory-lined afterburner exit duct; and installing a new flue gas quench unit.
Installation efforts were initiated in February 1990, immediately following completion
of the Region 9 Superfund soil treatability tests discussed in Section 5. The installation was
completed in April.
Some notable efforts completed included:
Fabricating and installing the scrubber flow control and heat exchanger modules,
and associated system surge tanks
Fabricating and installing the overhead supports for the fiberglass reinforced
plastic (FRP) duct work for the relocated scrubber and the refractory-lined
afterburner exit duct
Installing the new refractory-Lined afterburner exit duct,
Installing the new flue gas quench unit, the water seal, and the water-cooled
adaptor
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Relocating the venturi and packed column scrubbers
Fabricating and installing the induced-draft fan vibration-isolation mounts and
installing the fan in its final position
Completing the interconnecting plumbing and ducts within and between the
scrubber and heat exchanger systems
Installing process meters and sensing switches on the scrubber system
Implementing revised electrical power distribution and system safety-interlock
control logic
System checkout began in early April and was completed by the end of April. At this
time the reconfigured RKS and the heat exchanger system were operational and the newly
installed refractory and fiberglass reinforced plastic ducts were cured per manufacturer
recommendations.
2.13 RKS Automation with the Foxboro Process Control System
In FY89, concurrent with the RKS reconfiguration, an automatic process control system
(manufactured by Foxboro) was purchased. Efforts to install the system began in October 1989
in accordance with plans to develop control algorithms and systems in several phases.
The first phase included developing the controls for the burner management system and
implementing extensive data acquisition functions. This phase was initiated in January 1990 and
was completed and functional by June. It was used during the POHC incinerability ranking tests
discussed in Section 6.
Planning of the next phase of automatic control was initiated in July. The scope of the
second phase of implementation was defined in August and it included bringing the remaining
planned process parameter sensors on-line; implementing the required automatic waste feed cut-
off interlock functions mandated by the IRF's modified permit; enhancing the system's data
gathering and recording features; and refining the burner-controls for automatic gradual start-up
and shut-down. This effort will continue into FY91.
2.1.4 Ram Feeder ;
The RKS ram-feeder, as originally designed and supplied in FY85, was not fully
functional. The original system suffered from many short-comings, the most serious being an
inoperable control system for operating the moving belt, rams, and gates. In 1987, a
programmable logic control system was installed. Since that time, the ram feeder has been
functioning and has been used to feed wastes during numerous incineration tests, though not
with ease. However, with repeated use, the incidence of mechanical failure of several system
components has become increasingly frequent. In response, renewed and accelerated efforts to
seek a more acceptable solution to meet the ram feeder requirement were initiated during FY90.
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In September 1990, the performance requirements of a more appropriate ram feeder
were formulated. The major functional aspects include the ability to support testing with operator
attention required no more often than once every four hours, intrinsic reliability, ability to
contain spills from the waste containers, and compatibility with the RKS's automatic control and
data acquisition system. A tentative objective has been set to implement an appropriate ram
feeder by spring 1991.
22 BUILDING AND GROUNDS IMPROVEMENTS
Efforts continued in FY90 to bring the IRF physical plant to a point where it can better
support its testing activities. The following sections discuss these efforts.
22.1 Office Space
During the planning stages of the expanded building, consideration was given to arrange
for a more appropriate office space for the IRF staff. In March 1990, efforts resumed in this
regard. Competitive bids were solicited from building constructors to supply 5040 ft2 of modular
office space. By the end of FY90, a request to purchase the office complex was being considered
by the RREL. If approved, the office complex will most likely be completed and ready for
occupancy in March 1991. ;
222 Flammable Chemical Storage Building
Following the recommendations that resulted from an facility environmental audit in
1988, EPA sought to provide an adequate building for the IRF to store flammable chemicals.
In March 1990, the EPA Engineering, Planning, and Architecture Branch (EPAB) accelerated
efforts to procure the flammable chemicals storage building for the IRF. On May 17, the IRF
received the 9 by 24 ft modular chemical storage building.
Actual installation of the foundation, utilities, and access way was completed in
September, following the EPAB award of the installation contract. Completion of the building
systems repairs and function checks will continue into FY91.
223 Building Roof Repair
After several years of use, the old incinerator building roof suffered severe and wide-
spread leaks. In December 1989, efforts began to correct the problem. Bids were solicited from
roof repair contractors. Repairs were expected to begin in June but were delayed until
September 1990. They will continue into FY91.
22A Secured Tools/Parts Storage
Following completion of the expanded building, efforts began in December 1989 to
procure the partitions and shelves to install a secured tool and parts storage area. The shelves
were received in April. Assembly of these shelves and organization of the storage area followed
and became operational in May 1990.
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Worker Shower and Cool Down Facility
In June 1990, it became clear that the Level B personnel protection required during
testing of some hazardous materials was going to strain the ability of the test crew to cope with
potential heat exhaustion. The existing IRF, new building included, did not have the needed
facilities to allow test teams to rest between duty rotations. A temporary trailer, with proper
temperature controls "and shower stalls was leased and put into service. The building proved to
be indispensable during the POHC incinerability ranking test program discussed in Section 6.
2.2.6 Electrical systems
The new IRF building, as completed by the construction contractor, did not include
electrical outlets. The IRF staff installed a system of electrical receptacles in the new building
to mitigate the need to run excessive lengths of extension cords to power tools, pumps and other
electrical equipment. The project was completed in September. Additional electrical outlets
planned for the old incinerator test bay will be installed in FY91.
22.7 IRF Scale Model
Arrangements were made in FY90 to have a scale model of the IRF built for display at
meetings and conferences to inform the technical community of the IRF's capabilities and
features. The contractor selected for this project started work in late April and completed the
model in June 1990. The scale model was subsequently delivered to RREL in July.
2.3 MISCELLANEOUS PROJECTS FOR FUTURE IMPLEMENTATION
Several facility and incinerator related projects were explored and considered in FY90.
These are discussed in the following subsections.
2.3.1 RCRA Slowdown Tank Storage System .
A scrubber liquor blowdown tank system was designed and incorporated into the
application for the IRF modified hazardous waste management permit. Further design and
specification efforts proceed in FY90. System procurement may occur in FY91.
232 Scrubber Suspended Solids Removal System
One aspect of the RKS operation related to the solids suspended in the scrubber liquor
may require attention. The current scrubber arrangement prevents uncontrolled build up of
suspended particulates by discharging a portion of the solids with the scrubber blowdown stream.
While this is adequate for fine solids, it has proven ineffective for fibrous solids. Experience have
shown that fibers tend to collect in the scrubber liquor control system's'strainers eventually form
a sufficiently thick layer to block off effective scrubber liquor flow. While this condition can be
corrected by switching flow to a standby strainer, the frequent maintenance would render
operation unacceptably labor-intensive.
As an alternative, installation of a solids removal system to improve scrubber operation
flexibility is under consideration. Such a system had been studied during the early stages of the
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recently completed reconfiguration effort. It was not implemented during that effort, however,
so as not to delay system startup. With the RKS reconfiguration effort completed, the solid
removal system will be reexamined in FY91.
23.3 Slagging Kiln Recommendation
The desirability of having slagging kiln capability at the IRF has been discussed from
time to time over the past years. Interest in having this capability has remained high. In
response, the IRF staff was asked to prepare a conceptual design and cost estimate for two
approaches to adding slagging kiln capability to the IRF was completed in FY90. The two
approaches were (1) replacing the existing RKS with a new slagging system, and (2) fabricating
a separate, stand-alone system. A draft discussion document was completed in June. The
conceptual designs and cost estimates were completed in early July.
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SECTION 3
FATE OF TRACE METALS IN THE ROTARY KILN INCINERATION
SYSTEM WITH AN IONIZING WET SCRUBBER
The RCRA hazardous waste incinerator performance standards, promulgated by EPA
in January 1981, established particulate and HC1 emission limits and mandated 99.99 percent
DRE for POHCs. Subsequent risk assessments have suggested that, of the total risk to human
health and the environment from otherwise properly operated incinerators, hazardous constituent
trace metal emissions may pose the largest component. However, the data base on trace metal
emissions from incinerators is sparse; data on the effects of waste composition and incinerator
operation on these emissions are particularly lacking.
In response to these data needs, an extensive series of tests was conducted at the IRF
for OSW (R. Holloway, S. Garg, coordinators) in the investigation of the fate of trace metals fed
to a rotary kiln incinerator equipped with a single-stage ionizing wet scrubber. This program was
a continuation of a previous IRF test program, conducted in FY88, that employed a venturi/
packed-column scrubber as the primary APCS.
The primary objective of these test programs was to investigate the fate of five
hazardous and four nonhazardous trace metals fed to a rotary kiln incinerator in a synthetic solid
waste matrix. Of interest was the distribution of the metals as a function of incinerator
operating temperatures and feed chlorine content. The hazardous trace metals investigated were
arsenic, barium, cadmium, chromium, and lead. The nonhazardous metals were bismuth, copper,
magnesium, and strontium.
The actual tests were completed at the end of FY891. However, data reduction,
interpretation, and reporting occurred in FY90. An outline of the test program and test results
is given in the following subsections.
3.1 TEST PROGRAM
The test program consisted of nine parametric tests in which test waste feed contained
the nine metals identified above. All tests were performed in the IRF's RKS, which is illustrated
in Figure 1. The design characteristics of the system are summarized in Table 1.
3.1.1 Synthetic Waste Mixture
The synthetic waste contained a mixture of organic liquids added to a clay absorbent
material. Trace metals were incorporated by spiking an aqueous mixture of the metals of
11
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SINGLE-STAGE K3NEINQ
WETSCRUBBER
ROTARY
KILN
ROTARY KILN
INCINERATOR
MODULAR PRIMARY AIR
POLLUTION CONTROL
DEVICES
I REDUNDANT AIR
1 POLLUTION CONTROL.
! SYSTEM
Figure 1. Schematic of the IRF rotary kiln incineration system.
12
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TABLE 1. DESIGN CHARACTERISTICS OF THE IRF ROTARY KILN SYSTEM
Characteristics of the
Length
Diameter, outside
Diameter, inside
Chamber volume
Construction
Refractory
Rotation
Solids retention time
Burner
Primary fuel
Feed system:
Liquids
Sludges
Solids
Temperature (max)
Kiln Main Chamber
2.49 m (8 ft-2 in)
1.37 m (4 ft-6 in)
Nominal 1.00 m (3 ft-3.5 in)
1.90 m3 (67.3 ft3)
0.95 cm (0.375 in) thick cold-rolled steel
18.7 cm (7.375 in) thick high alumina castable refractory, variable depth to produce
a frustroconical effect for moving solids
Clockwise or counterclockwise, 0.2 to 1.5 rpm
1 hr (at 0.2 rpm)
North American burner rated at 800 kW (2.7 MMBtu/hr) with liquid feed
capability
Natural gas
Positive displacement pump via water-cooled lance
Moyno pump via front face, water-cooled lance
Metered twin-auger screw feeder or fiberpack ram feeder
1010°C (1850°F)
Characteristics of the Afterburner Chamber
Length
Diameter, outside
Diameter, inside
Chamber volume
Construction
Refractory
Gas residence time
Burner
Primary fuel
3.05 m (10 ft)
1.22m (4ft)
0.91 m (3 ft)
1.80 m3 (63.6 ft3) '
0.63 cm (0.25 in) thick cold-rolled steel
15.2 cm (6 in) thick high alumina castable refractory
0.8 to 2.5 s depending on temperature and excess air
North American Burner rated at 800 kW (2.7 MMBtu/hr) with liquid feed
capability ,
Natural gas
Temperature (max) 1200°C (2200°F)
Characteristics of the Ionizing Wet Scrubber APCS
System capacity, 85 m3/min (3000 acfm) at 78°C (172°F) and 101 kPa (14.7 psia)
inlet gas flow . . =
Pressure drop 1.5 kPa (6 in W.C.)
Liquid flow 230 L/min (60 gpm) at 345 kPa (50 psig)
pH control Feedback control by NaOH solution addition
Characteristics of the Venturi/Packed Column Scrubber APCS
System capacity,
inlet gas flow
Pressure Drop
Venturi scrubber
Packed column
Liquid flow
Venturi scrubber
Packed column
pH control
107 m3/min (3773 acfm) at 1200°C (2200°F) and 101 kPa (14.7 psia)
7.5 kPa (30 in W.C.)
1.0 kPa (4 in W.C.)
77.2 L/min (20.4 gpm) at 60 kPa (10 psig)
116 L/min (30.6 gpm) at 69 kPa (10 psig)
Feedback control by NaOH solution addition
13
-------
interest onto the clay/organic liquid material. The waste was fed to the rotary kiln via a twin-
auger screw feeder at a nominal rate of 63 kg/hr (140 lb/hr).
The organic liquid base consisted of toluene, with varying amounts of tetrachloroethylene
and chlorobenzene added to provide a range of chlorine contents. Synthetic waste chlorine was
varied from 0 to nominally 8 percent. The analyzed organic fractions for the three waste feed
mixtures are given in Table 2. Table 3 summarizes the average metal concentrations in the
combined waste feed over the nine tests.
1.12 Test Conditions
The test variables were kiln temperature, afterburner temperature, and the chlorine
content of the synthetic waste feed. Seven specific combinations of these variables were selected
as test points. Target and average achievejd values for these three variables are summarized in
Table 4. For all tests, excess air was nominally 11.5 and 8.0 percent oxygen in the kiln and the
afterburner exit flue gas, respectively. Estimated solids residence time within the kiln was one
hour. Figure 2 identifies the sampling locations for the tests. Flue gas samples were also
collected at the stack for evaluating hazardous waste management permit compliance.
3.2
TEST RESULTS
3.2.1 Average Trace Metal Discharge Distributions
Figure 3 shows the amounts of metal found in each discharge stream, as a fraction of
the total found in the three discharge streamskiln ash, scrubber exit flue gas, and scrubber
liquor. In Figure 3, the bar for each metal represents the range in the fraction accounted for
by each discharge stream over all nine tests, with the average fraction from all tests noted by the
midrange tick mark. Metal discharge distribution data in Figure 3 are plotted versus the
volatility temperature of each metal, which is the temperature at which the effective vapor
pressure of the metal is 10"* atm2. The effective vapor pressure is the sum of the equilibrium
vapor pressures of all species containing the metal. It reflects the quantity of metal that would
vaporize under a given set of conditions. A vapor pressure of 10"6 atm is selected because it
represents a measurable amount of vaporization. The lower the volatility temperature, the more
volatile the metal is expected to be.
Figure 3 indicates a correlation between observed volatility and volatility temperature
for all the metals tested, except arsenic. With the exception of arsenic, average normalized kiln
ash fractions generally increased with increasing volatility temperature. Cadmium and bismuth
were relatively volatile and were less prevalent in the kiln ash than were the more refractory
metals. Kiln ash fractions accounted for the majority of arsenic, lead, barium, copper, strontium,
magnesium, and chromium..
Based on volatility temperature, arsenic is expected to be the most volatile element.
However, the data show arsenic to be apparently refractory, remaining largely with the kiln ash.
The volatility temperature for arsenic is based on the vapor pressure of As£>v The fact that
arsenic is significantly less volatile than expected (were As^ the predominant arsenic species)
suggests that either some other, less volatile arsenic compound (perhaps an arsenate) was
14
-------
TABLE 2. POHC CONCENTRATIONS IN CLAY/ORGANIC LIQUID FEED
. Weight % in mixture
Test
1
2 through 8
(average)
9
Toluene
23.1
17.8
11.6
Tetrachloroethylene
o
3.1
6.0
Chlorobenzene
.0
3.0
5.6
Chlorine content8
o
3.6
6.9
"Calculated based on measured tetrachloroethylene and chlorobenzene concentrations.
TABLE 3. AVERAGE INTEGRATED FEED METAL CONCENTRATIONS
Metal
Arsenic
Barium
Bismuth
Cadmium
Chromium
Concentration
(rag/kg)
48
390
330
10
40
Metal
Copper
Lead
Magnesium
Strontium
Concentration
(rag/kg)
380
45
18,800
410
15
-------
TABLE 4. TARGET AND AVERAGE ACHIEVED TEST CONDITIONS
Feed mixture Cl
content
(%)
Test
1
2
3
4
5
6
T
8a
9
Date
8/17/89
8/2/89
8/4/89
8/1/89
8/16/89
8/15/89
8/9/89
8/11/89
7/28/89
Target
0
4
4
4
4
4
4
4
8
Actual
0
3i5
3.5
3.5
3.7
3.6
3.5
3.8
6.9
Kiln exit
temperature
- OC(OF)
Target
871 (1600)
816 (1500)
927 (1700)
871 (1600)
871 (1600)
871 (1600)
871 (1600)
871 (1600)
871 (1600)
Average
900 (1652)
819 (1507)
929 (1704)
877 (1610)
885 (1625)
887 (1629)
881 (1618)
879 (1615)
881 Q617)
Afterburner exit
temperature
°C (°F)
Target
1093 (2000)
1093 (2000)
1093 (2000)
1093 (2000)
1204 (2200)
982 (1800)
1093 (2000)
1093 (2000)
1093 (2000)
Average
1088 (1990)
1095 (2002)
1092 (1998)
1096(2006)
1163 (2125)
1017 (1863)
1103- (2018)
1098 (2008)
1087 (1988)
Test points 7 and 8 are replicates of test point 4; together the three tests provided the
components of an IRF trial burn.
16
-------
68-ffOQS3
QUENCH
i
ofc
ui
t
SECTION
i
BURNER
I ,
_i
^
«>
w
" «
"S a w
J 3 B
111
at
W ^
cj «^
> s
, aj"
« en a* -2
"3 Sc s ~ £7
5 2 13 ^2 u
§
o
e
s;
5
I
1
Sit
17
X X
X
X
X
XX
X X
X
X-
X X
§
oo
-------
KILN ASH
3tt
2 3
?S£
% S
i°
<$s
QC -*
u_
?*
IT
111
CD
&? . !-'!
i j
1 _ " -;. Cr- '
"4 1 * T SLr Mg4
T i i i i + i " i i 4- x ft
0 200 400 600 800 1000 1200 1400 1600
VOLATILITY TEMPERATURE/C) '"
SCRUBBER LIQUOR ^
tnn '*'" ' ' " r '
1 VA^
90
80
70
60
50
40
30
20
10
n
;
_ "-:
~ c -
~ ' "^ ,. ' *
at
Cd ' ' '
As
:^=
x
L^ B|a Cl- Sr Cr
T ,1,4^, ,4- wpd.
200 400 600 800 1000 1200
- VOLATILITY TEMPERATURE ('C)
1400
1600
Figure 3. Normalized distribution of metals in the discharge streams.
18
-------
preferred, or that some other chemical interaction, such as strong adsorption to the clay,
occurred.
322 Effects of Incinerator Operatiing Conditions on Metal Distributions
Increased kiln temperature caused a noticeable increase in the volatility of cadmium,
bismuth, and lead. Figure 4 shows that as the kiln temperature increased there was a significant
decrease in the kiln ash fraction of these metals, with corresponding increases in the scrubber
exit flue gas and scrubber liquor fractions. Although the volatility of lead increased with higher
kiln temperature, lead still remained relatively refractory and was found primarily in the kiln ash.
Kiln temperature within the tested range had no significant effect on the discharge distributions
of any of the remaining metals.
Afterburner temperatures within the tested range did not clearly affect the distributions
of any of the metals among the scrubber exit flue gas and scrubber liquor discharge streams.
Data on the effect of feed chlorine content are inconclusive pending investigation of an apparent
relationship between feed chlorine and the efficiency of the analytical procedure for metals in
kiln ash.
323 Metal Distributions in Flue Gas Particulate by Particle Size
The particulate samples from the afterburner exit flue gas sampling train were size-
fractionated, and trace metal distributions as a function of particle size were determined.
Figure 5 shows the metal distributions in the particle size range of less than 10 urn, averaged
over all nine tests. The average of the nine total particulate samples is also shown. The data
show a relationship between the relative volatility of each metal (as indicated by its volatility
temperature noted in the horizontal axis) and its propensity for redistribution to finer particulate.
This is indicated by the higher fractions of the metals with lower volatility temperatures in the
less than 10 um particle size fractions.
This behavior is consistent with expectation. Most metal vaporized at some point in the
incinerator will ultimately condense when the flue gas cools. Condensation occurs via fume
formation or condensation onto available flue gas particulate. Fume formation results in very
fine particulate. Condensation onto available particulate results in concentrating the metal in
fine particulate, since condensation is a per-unit of surface area event, and the surface-area-to-
mass ratio is increased in fine particulate. Both mechanisms tend to concentrate volatilized
metal in fine particulate. Interestingly, arsenic behaves as a volatile metal with respect to
enrichment in fine particulate.
The effects of kiln temperature, afterburner temperature, and waste feed chlorine
content are shown in Figure 6. The size distributions of the metals most nearly reflect the
overall entrained particle size distribution for Test 2 (lowest kiln temperature), Test 5 (highest
afterburner temperature), and Test 1 (no chlorine in the waste feed); very little redistribution
among the particulate was observed. For these three tests, about 20 to 25 percent of each metal
and the total particulate sample were in the less than 10 jim particulate.
With increased kiln temperature, the size distributions of all metals except chromium
shift to about 60 percent less than 10 ^m. Increased afterburner temperature caused the overall
19
-------
_ 80
CADMIUM DISCHARGE DISTRIBUTIONS
u.
?v 80
.-.100
o
111
oc
CO
35 90
I
fe 80
70
KILN ASH SE FLUE GAS LIQUOR
BISMUTH DISCHARGE DISTRIBUTIONS
KILN ASH
SE FLUE GAS
LIQUOR
LEAD DISCHARGE DISTRIBUTIONS
30
20
10
816'C
871'C
927'C
KILN ASH
SE FLUE GAS
LIQUOR
Figure 4. Effects of kiln temperature on the discharge distributions of cadmium, bismuth,
and lead.
20
-------
60
CUMULATIVE PERCENT <10 microns
40
20
As
Cd
Pb
Ba
Bi
Sr
*
SAMPLE
Cr
I
I
en
o
Q
CO
LU
0
2000
Figure 5.
600 1000 1500
VOLATILITY TEMPERATURE (*C)
Average of metal distributions in the afterburner exit flue gas particle size
fractions.
sample particle size distribution to shift to coarser participate, most likely because of fine
particles melting or softening and coalescing into larger particles. A corresponding shift in
metal-specific distributions to coarse particulate was observed.
The addition of chlorinated compounds to the synthetic waste feed mainly affected
cadmium, lead, copper and chromium distributions. With waste feed chlorine content increased
from 0 to 4 percent, the fraction of cadmium, lead and copper in the less than 10 |im particulate
increased from about 20 to roughly 55 percent. No further redistributions of these metals were
observed with chlorine content increased from 4 to 8 percent. For chromium, increasing chlorine
content from 0 to 4 to 8 percent caused a corresponding shift of 2 to 20 to 50 percent in
particulate of less than 10 |im.
3-2.4 Apparent Scrubber Collection Efficiencies
The apparent scrubber collection efficiency for flue gas metals was determined for each
test. The apparent scrubber efficiency represents the ratio of the normalized metal fraction
measured in the scrubber liquor to the sum of the normalized metal fractions measured in the
scrubber liquor and scrubber exit flue gas. Figure 7 summarizes the efficiency data. The bar for
each metal represents the range of scrubber efficiencies over the nine tests, with the overall
average for the nine tests noted by the midrange tick mark. Average metal collection efficiencies
ranged from 22 to 71 percent; the overall average for all metals was 43 percent. Figure 7 shows
that there were significant variations in the efficiencies for each metal. However, average
efficiencies were generally higher for the less volatile metals. It should be noted that industrial
applications of ionizing wet scrubbers are typically in multiple stages and, as such, would be
expected to collect metals more efficiently than the single-stage scrubber at the IRF.
21
-------
Variable: Kiln Exit Temperature
100
80
60
20
Cumulative'percent < 10 mlorons
AS nH
9 ^a
<
t
Bi
1
nPb C
0
1 .. i
Pb "Cu ; : -Mg-
Ba .*. « I
f f *
I . I *sampie
a 1 %
D Cr I 6
6OO . 10OO 1600 2000
Volatility temperature (*C)
* 882'C (1SOOT) * K»3'C (SOOO'F) ° 1204'C (2200'F)
Variable: Waste Feed Chlorine Content
80
60
40
20
n
Cumulative peroent < 10 mlorons
As
I
<
Cd
' Sir,
1
'
SPb .
J Ba
5°° . Mg,
Srj;'
1
<
,
1 1 < '
Cr
p
J sample
600 1OOO 1600
Volatility temperature (*C)
2000
Figure 6. Effects of kiln temperature, afterburner temperature and waste feed
chlorine content on the distribution of metals in the afterburner
exit flue gas particle size fractions.
22
-------
_ 100
o
o
Q.
.0.
80
cc 60
OJ
CO
CD
c 40
O
20
--As
Cd
-- Pb
Ba
Sr__
Mg
"--Cr
Cu
OJ,
o
Q
500 1000 1500
VOLATILITY TEMPERATURE CC)
Figure 7. Apparent scrubber collection efficiencies for metals.
2000
Figure 8 shows the effects of kiln temperature and waste feed chlorine content on the
collection efficiencies for the metals. Within the limits of data variability, none of the test
variables affected scrubber collection efficiencies for arsenic, barium, strontium, magnesium and
chromium. Apparent scrubber collection efficiencies for cadmium, bismuth, lead, and copper
increased with increased kiln temperature and waste feed chlorine content. Increased scrubber
collection efficiency might be expected with increased feed chlorine content if the presence of
chlorine leads to the formation of more soluble metal chlorides. However, it is unclear why
increased kiln temperature would directly lead to increased collection efficiency. Apparent
scrubber collection efficiencies for metals did not vary with afterburner exit temperature.
3.3 CONCLUSIONS
Test conclusions include the following:
Cadmium and bismuth were relatively volatile, with an average of less than
40 percent of the discharged metal accounted for by the kiln ash. Arsenic, barium,
chromium, copper, lead, magnesium, and strontium were relatively nonvolatile,
with an average of greater than 80 percent of the discharged metal accounted for
by the kiln ash.
Observed metal volatilities generally agreed with the order predicted by metal
volatility temperatures, with the notable exception of arsenic. Arsenic has the
lowest volatility temperature of the metals tested, but was observed to be one of
the least volatile of the metals. This suggests that AsjOs was not the predominant
arsenic species in the incinerator, or that the arsenic was adsorbed by the clay/ash
matrix.
23
-------
Variable: KILN EXIT TEMPERATURE
PPARENT SCRUBBER EFFICIENCY (°/
to .*>. a> co c
3 O O O O C
A As (DL=0) . ° Mg
. ? _ 4Tcr(DL=0)
I I
I J
iBa ; SrJ[ ^i
i
j, 1
^ i
Cr(DL)
L
1
O5
0
a
CO
LU
500 .. 1000 1500
. VOLATILITY TEMPERATURE fC)
816 'C (1500 T) A 871 °C (1600 T) n 92? °C (1700 T)
2000
Variable: WASTE FEED CHLORINE CONTENT
100
o
5 80
LL
U_
LU
ffi 6°
m
CO
§ 40
CO
Lu 20
D-
Q-
<
Q
\
...T _9
X As (DUO) Ba {
n 1 Sr
As (DL) Bi
|. JP ,.
W.....M..HM
-------
Kiln temperature affected the relative volatility of cadmium, bismuth, and lead.
The fractions of these metals retained in the kiln ash decreased with increasing
kiln temperature.
Afterburner exit temperature did not clearly affect metal partitioning among the
scrubber exit flue gas and scrubber liquor discharge streams.
Enrichment of metals in the fine-particulate fraction of the afterburner exit
particulate was observed, with an average of roughly 50 percent of flue gas
particulate metal in the less-than-10-nm size range, compared to an average of
about 30 percent of the total particulate sample. The distributions of the more
volatile metals were shifted to fine particulate more so than the less volatile
metals. Arsenic behaved as a volatile metal with respect to its distributions among
the afterburner exit flue gas particle size ranges. On average, roughly 40 percent
of flue gas particulate metal was less than 10 urn
Each test variable affected the distributions of at least some of the metals among
the flue gas particulate particle size ranges. Size distributions of the metals most
nearly reflected the overall sample particle size distribution for Test 2 (lowest kiln
temperature), Test 5 (highest afterburner temperature), and Test 1 (no chlorine
in the waste feed); very little redistribution among the particulate was observed.
For these three tests, about 20 to 25 percent of each metal and the total
particulate sample were in the less than 10 \im particulate.
Increasing kiln temperature to 816° to 927° C (1500° to 1700° F) caused the
average distributions to shift from roughly 20 percent less than 10 ym to an
average of 60 percent less than 10 \im for all test metals except chromium. For
cadmium, copper, and lead, an increase in waste feed chlorine content from 0 to
4 percent caused their distributions to shift from roughly 20 percent less than
10 \im to 55 percent less than 10 |im. No further effects with feed chlorine
increased to 8 percent were observed for these metals. For chromium, increasing
chlorine content from 0 to 4 to 8 percent caused a corresponding shift of 2 to 20
to 50 percent in particulate less than 10 jim.
The average apparent scrubber collection efficiencies for metals ranged from 22 to
71 percent, and generally increased with decreasing metal volatility. The overall
average collection efficiency for all metals was 43 percent.
Apparent scrubber collection efficiencies for cadmium, bismuth, lead, and copper
increased with increased kiln temperature and waste feed chlorine content.
Afterburner temperature had no discernible effect on apparent scrubber collection
efficiencies for any of the metals.
Test results were documented in the test report:
Fournier, Jr., D. J., and L. R. Waterland, "The Fate of Trace Metals in a Rotary
Kiln Incinerator with an Ionizing Wet Scrubber," draft April 1990.
25
-------
Test results were also presented in three technical papers:
Waterland, L. R., D. J. Fournier, Jr., J. W. Lee, and G. J. Carroll, 'Trace Metal
Fate in a Rotary Kiln Incinerator with an Ionizing Wet Scrubber," presented at the
Incineration Conference1990, San Diego, California, May 1990.
Fournier, Jr., D. J., L. R. Waterland, and G. J. Carroll, Trace Metal Size
Distributions in Flue Gas Particulate from a Rotary Kiln Incinerator," presented
at the American Association for Aerosol Research 1990 Annual Meeting,
Philadelphia, Pennsylvania, June 1990.
Fournier, Jr., D. J., L. R. Waterland, and G. J. Carroll, "Size Distributions of
Trace Metals in Flue Gas Particulate from a Pilot-Scale Rotary Kiln Incinerator,"
presented at the American Flame Research Committee 1990 Fall International
Symposium on NOX Control, Waste Incineration, and Oxygen-Enriched
Combustion, San Francisco, California, October 1990.
Test results are planned for presentation in two additional technical papers:
Waterland, L. R., D. J. Fourier, Jr., J. W. Lee, G. J. Carroll, and R. C. Thurnau,
"The Fate of Trace Metals in a Rotary Kiln Incinerator: Tests with Two Different
Scrubber Systems," for presentation at the Second International Conference of
Toxic Combustion By-Products, Salt Lake City, Utah, March 1991.
Fourier, Jr., D. J., L. R. Waterland, and G. J. Carroll, The Behavior of Trace
Metals in Rotary Kiln Incineration: An Overview of Incineration Research
Facility Studies," for presentation at the 17th Annual Research Symposium on the
Remedial Action, Treatment, and Disposal of Hazardous Waste, Cincinnati, Ohio,
April 1991.
26
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SECTION 4
INCINERABILITY TESTING OF ARSENIC-CONTAMINATED SOIL FROM
THE BAIRD AND MCGUIRE SUPERFUND SITE
One of the primary missions of the Environmental Protection Agency's (EPA)
Incineration Research Facility (IRF) is to support Regional Offices in evaluations of the
potential of incineration as a treatment option for contaminated soils at Superfund sites. One
priority site in Region 1 is the Baircl and McGuire site in Holbrook, Massachusetts., EPA
Region 1 (M. Sanderson, P. Fitzsimmons, Region 1; J. Ehresmann, USAGE, Coordinators)
requested that test burns be conducted at the IRF to support evaluations of the suitability of
incineration as a treatment technology for the contaminated site soil.
The soil at the Baird and McGuire site is contaminated with low levels of several
pesticide compounds and varying levels of arsenic and lead. Several areas of the site have
arsenic contamination levels of the order of 100 ppm, although two "hot spots" have arsenic levels
up to 3800 ppm. Thus, with respect to incinerability evaluation, the primary concern surrounds
the fate of arsenic and lead in the soil when it is subjected to incineration. The effect of
incineration on the fate of arsenic and lead in soil is currently unknown. A secondary concern
relates to whether incineration can effectively destroy the organic pesticide contaminants in the
soils. Therefore, the test conditions were designed to evaluate the effects of varying incinerator
operating conditions on organic contaminant destruction and on the fate of the arsenic and lead
in the soil. Specifically, the test program attempted to answer these questions:
What is the distribution of arsenic and lead in the discharge streams during
incineration of this metal-contaminated soil?
To what extent can rotary kiln incineration effectively destroy the organic
» constituents in the soil?
* What are the effects of incineration excess air and temperature on organic
constituent destruction and arsenic and lead distribution?
The test program consisted of two components. Initially, a series of bench scale
experiments, using a muffle furnace, was performed to evaluate the leachability characteristics
of the arsenic and the lead in the soil as a function of the arsenic/lead concentration in the soil.
The second component of this test program consisted of a set of five incineration tests in the
RKS. These tests were aimed at evaluating the fate of arsenic and lead in the soil as a function
of kiln temperature and excess air level.
27
-------
The muffle furnace testing and four of the five incineration tests were completed at the
end of FY891. The fifth incineration test and test program sample analyses, data evaluation and
interpretation, and test reporting were completed during FY90. An outline of the test program
and test results are given in the following subsections.
4.1 MUFFLE FURNACE EXPERIMENTS
A prerequisite to any onsite remediation treatment process is that the residue from the
process (the treated soil) be able to be landfilled at the site. For incineration treatment, this
would not be possible if the kiln ash residue had TCLP leachable arsenic and lead at levels
greater than the toxicity characteristic (TC) limit. In an actual site remediation via incineration,
soil with very high arsenic/lead levels can be blended with soils of low arsenic/lead
contamination to give an incineration feed that results in a low concentration of leachable
arsenic/lead in the kiln ash. But, the a priori unknown is how low the feed arsenic or lead
concentration must be. To partially address this unknown, a series of muffle furnace tests was
performed. The objective of these tests was to develop the data to guide the determination of
appropriate maximum feed arsenic/lead concentrations.
For these tests, the primary variable was the arsenic/lead concentration in the test
mixture. A contaminated soil containing 650 ppm arsenic and 45 ppm lead was mixed with
various amounts of a background soil containing less than 5 ppm arsenic and 14 ppm lead to
produce seven samples of varying arsenic/lead concentrations. Each sample was heated in a
muffle furnace at 982° C (1800°F) for one hour. Analysis of the soil mixtures and the resultant
ash residues show that:
Arsenic volatility increased with soil arsenic concentration.
volatility increased with soil lead concentration.
Similarly, lead
Soils containing less than 150 ppm arsenic would produce ash residues below the
arsenic TC limit of 5 mg/L
Lead content in all ash samples was constant at about 5 ppm
All ash TCLP leachate lead concentrations were below detection, regardless of
initial soil lead content
Organics and moisture in the soil contributed to 25 percent weight loss
To achieve a secondary objective of determining whether the potential additives lime
and alum can affect the distribution of metals to the resulting soil ash, two additional tests were
conducted. In both tests, the test mixture consisted of the highly-contaminated soil, mixed with
one of the additives to a level of 2 percent (wt). Analysis of the limited data suggests that:
r
Lime appeared to reduce the volatility of the arsenic; a greater fraction of the soil
arsenic remained with the resulting ash
Alum appeared to increase arsenic volatility; less soil arsenic remained in the
resulting ash
28
-------
Neither additive affected the volatility of lead .. ..,...-;
Lime may be added to soils with arsenic concentrations greater than 150 ppm
while yielding a thermal treatment ash that would not possess the toxicity
characteristic «
42 PILOT-SCALE INCINERATION TESTS
The pilot-scale incineration tests were conducted in the RKS to evaluate the fate of
arsenic and lead in the soil as a function of kiln temperature and excess air level. A schematic
of the RKS and its design characteristics are given in Figure 1 and Table 1 of Section 3.
42.1 Test Program
Four tests were performed at different combinations of kiln temperature of nominally
816° and 980°C (1500° and 1800°F) and kiln exit flue gas O2 of nominally 6 and 10 percent.
A fifth test was completed which was a repeat of the test that produced the kiln ash which
contained the lowest levels of TCLP leachable arsenic and lead.
A bulk sample (nominally 1350 kg, 3000 Ib) of arsenic-contaminated soil was excavated
from the Baird and McGuire site to serve as the test waste. The bulk soil sample was packaged
into four 55-gal drums and shipped to the IRF for testing. At the IRF the soil was re-packed
into polyethylene-lined 1.5-gal fiber pack drums. Each fiber pack drum held about 4.5 kg (10 Ib)
of the test soil. In the tests one fiber pack drum was fed into the RKS with a ram feeder every
5 min. Thus, test soil feedrate was nominally 55 kg/hr (120 Ib/hr). A kiln rotation speed of
0.65 rpm produced a solids residence time in the kiln of about 0.5 hr. Figure 9 identifies the
sampling locations for the tests and summarizes the sampling protocols employed.
422 Test Results
Throughout the test program, CO levels at the scrubber exit and the stack were at most
a few ppm. Total unburned hydrocarbons levels were similarly low at the afterburner exit,
scrubber exit, and in the stack. Average NOX concentrations at the scrubber exit ranged from
32 to 51 ppm, levels that are typical for the rotary kiln system.
Flue gas paniculate concentrations ranged from 6 to 17 mg/dscm (at 7 percent O2) at
the scrubber exit. In the stack, concentrations ranged from 2 to 29 mg/dscm (at 7 percent O2).
These levels fell below the hazardous waste performance standard of 180 mg/dscm (at 7 percent
02).
The only organic contaminants found in the test soils above method detection limits of
2 to 4 mg/kg were p,p'DDE, p,p'DDD, p.p'DDT, and methoxychlor. As shown in Table 5, DDE
was present at 39 to 74 mg/kg, DDD at 181 to 310 mg/kg, DDT at 257 to 501 mg/kg, and
methoxychlor at 54 to 81 mg/kg. None of these.were present in the TCLP leachates of the test
soils at a quantitation limit of 0.2 mg/L.
Organic analysis of kiln ash, kiln ash TCLP leachate, scrubber blowdown, and scrubber
exit flue gas Method 0010 samples for each test showed that all semivolatile organic hazardous
29
-------
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III
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o e 2
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S "a '
B M "S
JS
X
X X
X X
X
X
X
CN
30
-------
TABLE 5. SEMIVOLATILE ORGANIC HAZARDOUS CONSTITUENTS IN TEST SOILS
-Y-;:-;:' :-._.*. Soil : .-;-;. . v .
Test
p,p'-DDE
p,p'-DDD
p,p'-DDT
Methoxychlor
All other semivplatiles analyzed
Drum 15
(Test 1)
54
228
334
81
<4 "
Drum 16
(Test 2)
74
310
501
73
' -'<+
Drum 18
(Test 3)
, 45
197
247
54
'. -<4""
Drum 13
(Test 4)
39 ,-
181
' 277 '
: * ; ,73 . "
... .. ..., ^4 ,
constituents analyzed, including the pesticide contaminants in the test soil, were present at less
than method detection limits in all cases. The quantitation limits of the Method 0010 sampling
trains when combined with measured flue gas flow rates and soil feed'concentrations and feed
rates confirm that incineration destruction and removal efficiencies (DREs) for the pesticide
contaminants in the soil feeds were at least greater than 99.5 percent to greater than
99.97 percent for the tests performed.
Table 6 summarizes the distributions of arsenic and lead among the incinerator
discharge streams (kiln ash, scrubber blowdown and scrubber exit gas), expressed as fractions of
the total metals measured in the three discharge streams. The data in Table 6 show that kiln
temperature has a clear effect on both arsenic and lead distributions in that kiln ash
concentrations of arsenic and lead were lower at the higher incineration temperatures. This is
expected since both arsenic and lead are relatively volatile metals. Higher incineration
temperatures would be conducive to greater volatilization of these metals in the kiln, resulting
in decreased kiln ash concentrations. Scrubber blowdown and scrubber exit flue gas
concentrations of both metals appear to be increased at the higher incineration temperature.
Again, this is consistent with increased metal volatilization in the kiln at the higher temperature.
The data in Table 6 show no clear influence of kiln excess air level (as reflected in kiln
exit flue gas O2) on arsenic or lead distributions among the discharge streams at the low kiln
temperature conditions. At high kiln temperature conditions, increasing excess air had the
apparent effect of increasing the volatility of arsenic, as measured by the decreased kiln ash
arsenic fraction. However, this apparent increase is most likely the result of increased ash
entrainment and carryover by the increased kiln exit flowrate.
Scrubber inlet flue gas concentrations were not measured in these tests. However, if it
is assumed that the total amount of metal measured in the sum of the scrubber liquor and the
scrubber exit flue gas equals the amount present at the scrubber inlet, an apparent efficiency can
be calculated. This apparent scrubber efficiency is ((scrubber liquor fraction)/(scrubber liquor
fraction plus scrubber exit flue gas fraction)).
31
-------
TABLE 6. NORMALIZED METAL DISCHARGE DISTRIBUTIONS FOR THE BAIRD AND
MCGUIRE INCINERATION (TESTS
Test
Kiln exit temperature, °C
Kiln exit O2, %
Kiln exit flue gas flowrate,
acm/min"
Arsenic
Kiln ash
Scrubber liquor
Scrubber exit flue gas
Total
Lead
Kiln ash
Scrubber liquor
Scrubber exit flue gas
Total
1
(9-26-89)
832
(1529)
11.3
22.8
1
72
23
5
100
89
4
7
100
5
(10-5-90)
839
(1541)
11.2
22.6
Distribution <
66
29
5 ,
* 100
91
3
6
100
2
(9-29-89)
844
(1552)
6.8
11.1
;% of metal
76
22
2
100
93
3
4 .
100
3
(9-27-89)
994
(1822)
10.4
34.8
measured)
36
55
9
100
69
12
19
100
4
(9-28-89)
994
(1822)
7.5
21.6
56
38
6
100
69
13
18
100
'Actual wet m3/min.
As shown in Table 7, apparent scrubber collection efficiencies for arsenic ranged from
82 to 98 percent and were right in the range of overall particulate collection efficiencies. The
apparent collection efficiencies for lead were significantly lower and ranged from 33 to
43 percent. Neither arsenic nor lead apparent collection efficiencies showed atny significant
variation with test variables (kiln temperature or excess air).
Table 8 shows that both increasing kiln temperature and decreasing kiln excess air
increased the teachability of the kiln ash arsenic, with excess air level having the more significant
effect. At 11 percent kiln exit O2, between 8.3 and 13 percent of the kiln ash arsenic was
teachable. At 7 percent kiln exit O2, 28 and 67 percent of the arsenic was teachable, for kiln
temperatures of 844° and 994°C(1552° and 1822° F), respectively. Clearly, to minimize arsenic
teachability, the appropriate incineration conditions are low-temperature/high-excess air.
In contrast, the teachability of lead from the kiln ash was consistently low and lead was
not detected in any of the soil and ash TCLP leachates.
32
-------
TABLE 7. APPARENT PARTICULATE AND METAL SCRUBBER COLLECTION
EFFICIENCIES
Test
Kiln exit temperature, °C
Kiln exit O2, %
Arsenic
Lead
Overall particulate
TABLES.
Test
Kiln exit temperature, °C
Kiln exit O2, %
1
(9-26-89)
832
\ (1529)
11.3
82
36
92
5
(10-5-90)
839
(1541)
11.2
Apparent IWS
85
33
84
2 3'
(9-29-89) (9-27-89)
844 994
(1552) (1822)
6.8 10.4
collection efficiency (%)
92, 86
43 39
95 90
4
(9-28-89)
994
(1822)
7.5
86
42
82
ARSENIC FRACTIONS - TCLP LEACHABLE
1
(9-26-89)
832
1 (1529)
11.3
5
(10-5-90)
839
(1541)
11.2
2 3
(9-29-89) (9-27-89)
844 994
(1552) (1822)
6.8 10.4
4
(9-28-89)
994
(1822)
7.5
Fraction of As teachable (%)
Soil feed
Kiln ash
2.2
9.3
2.4
8.3
2.4 2.5
28 13
2.9
67
33
-------
CONCLUSIONS
Test conclusions include:
Both arsenic and lead remain predominantly in the kiln ash when incinerated at
a kiln temperature of nominally 840° C (1540°F). Between 66 and 76 percent of
the arsenic discharged and 89 to 93 percent of the lead discharged was accounted
for in this stream. Between 2 and 5 percent of the arsenic and 4 and 6 percent
of the lead was present in the APCS exit flue gas; and 22 to 29 percent of the
arsenic and 3 to 4 percent of the lead was collected by APCS.
Lead remains predominantly in the kiln ash when incinerated at a kiln
temperature of nominally 990°C (1820°F), with 69 percent of its amount
discharged accounted for in the kiln ash. The APCS flue gas contained 18 to
19 percent of the discharged lead. The APCS collected 12. to 13 percent of the
lead.
A significant amount of arsenic escapes the kiln when incinerated at a kiln
temperature of nominally 990° C (1820°F). At these higher temperatures, the
kiln ash fraction is reduced to between 36 to 56 percent due to arsenic
volatilization in the kiln. Most of this escaping arsenic is collected in the APCS
(38 to 55 percent of the arsenic discharged is accounted for in the APCS).
Between 6 and 9 percent of the arsenic discharged is found in the APCS exit flue
gas.
Incineration at both kiln temperatures noted above effectively destroys the organic
contaminants in the soil. Pesticide constituent contaminants were reduced from
soil levels ranging from 39 to 501 mg/kg to not detected at a level of 0.4 mg/kg
in the kiln ash. The APCS blowdown discharge contained no detectable pesticide
constituents at a level of 0.02 mg/L. No detectable pesticide constituents were
found in the APCS exit flue gas at detection limits of nominally 6 jj.g/dscm.
Increased incineration temperatures caused increased volatilization of both arsenic
and lead in the kiln with the result that kiln ash fractions were decreased as noted
above.
Changes in kiln excess air level did not affect lead distributions among incinerator
discharges and djd- not affect arsenic distributions at the low temperature
(nominally 840° C (1540°F)) kiln condition. Increasing kiln excess air from a kiln
exit flue gas of 7.5 to 10.4 percent apparently decreased the amount of arsenic
discharged in the kiln ash from 56 to 36 percent of the discharged amount, with
a corresponding increase in the APCS collected fraction from 38 to 55 percent.
Changing incineration conditions had no affect on APCS apparent removal
efficiency for either arsenic or lead. APCS apparent arsenic removal efficiency
was in the 82 to 92 percent range, the same as for overall particulate. APCS
apparent lead removal efficiency was lower, in the 33 to 43 percent range.
34
-------
Kiln ash lead was not teachable in the TCLP test (TCLP leachates contained no
detectable lead at a level of 0.05 mg/L). Between 9. and 62 percent of the kiln ash
arsenic was mobile, and found in the TCLP leachate. Increasing kiln temperature
marginally increased kiln ash arsenic teachability. Decreasing kiln excess air
significantly increased kiln ash arsenic teachability.
Other conclusions from the incineration tests include:
The observed relative volatilities^ arsenic and lead agree with expectations from
physical vapor pressure data; arsenic is significantly more volatile than lead at
both kiln temperatures tested
No incinerator discharge stream (kiln ash nor APCS blowdown) had TCLP
leachate concentrations exceeding TC limits for either arsenic or lead
Particulate emissions after the APCS were significantly below the federal
hazardous waste incinerator performance standard
Further conclusions from the muffle furnace tests include:.. '",
Adding lime to the site soil significantly decreases both the volatility of arsenic in
the soil, as well as the teachability of the arsenic remaining in the soil ash
Adding alum to the soil significantly increases arsenic volatility but does not affect
resulting ash arsenic teachability
Neither lime nor alum affects lead volatility nor resulting ash lead teachability
The results from the test program suggest that incineration is a viable treatment
technology for remediating the Baird and McGuire site. The muffle furnace results combined
with the incineration results suggest that a soil with arsenic content below about 150 mg/kg can
be incinerated under any combination of kiln temperature/kiln excess air level to given an
organically decontaminated ash with TCLP teachable arsenic below the limit which would prevent
its landfill disposal.
The incineration test results suggest that soil with arsenic levels as high as 1200 mg/kg
could be incinerated to give a kiln ash with TCLP leachate concentration less than 5 mg/L,
provided incineration was under low kiln temperature (nominally 840° C (1540°F))/high kiln
excess air (kiln exit flue gas O2 nominally 11 percent) conditions. The muffle furnace test results
suggest that even higher soil arsenic levels could be incinerated to give a kiln ash with TCLP
leachate arsenic concentration of less than 5 mg/L with lime addition to the soil.
Test results were documented in the test report:
King C., and L. R. Waterland, "Pilot-Scale Incineration of Arsenic-Contaminated
Soil from the Baird and McGuire Superfund Site," draft March 1990, revised May
1990.
35
-------
Test results were also presented in two technical papers:
Wall, H. O., and M. K. Richards, "The Incineration of Arsenic-Contaminated Soils
Related to the Comprehensive Environmental Response, Compensation, and
Liability Act (CERCLA)," presented at the Sixteenth Annual Research
Symposium on the Remedial Action, Treatment, and Disposal of Hazardous
Waste, Cincinnati, Ohio, April 1990.
Waterland, L. R., C. King, R. C. Thurnau, and M. K. Richards, "Incinerability
Testing of an Arsenic-Contaminated Superfund Site Soil," presented at the Pacific
Northwest International Section of the Air and Waste Management Association
1990 Conference, Portland, Oregon, November 1990.
In addition, test results are planned for presentation in a third technical paper:
Waterland, L. R., C. King, R. H. Vocque, M. K. Richards, and H. O. Wall, "Pilot-
Scale Incinerability Evaluation of Arsenic- and Lead-Contaminated Soils from
Three Superfund Sites," for presentation at the Incineration Conference 1991,
Knoxville, Tennessee, May 1991.
36
-------
SECTION 5
INCINERABILITY TESTING OF CONTAMINATED SOILS FROM
THE PURITY OIL SALES AND THE McCOLL SUPERFUND SITES
A second series of tests to evaluate the potential of incineration as a treatment option
for contaminated soils at Superfund sites was completed during FY90. This series of tests,
performed at the request of EPA Region 9 (J. Blevins, R. Blank, J. Rosati, P.: Wieman,
Coordinators), evaluated the incinerability of three contaminated materials from, the Purity Oil
Sales site in Fresno, California, and two contaminated soils from the McColl site in Fullerton,
California. ,
The Purity Oil Sales site is an abandoned oil recycling facility. The results of a soil
stratigraphy investigation of the site indicated that four contaminated subsurface layers are
present in the waste pit area at the site. The top layer is comprised primarily of construction
rubble, sand, and gravel. The second layer, or tar sludge, underlies the construction debris and
is mixed, to some extent, with soil and rubble. The third layer is comprised of contaminated silty
sand. The fourth layer is uncontaminated to slightly contaminated silty sand. The materials
tested in this program were from the first (A layer), second (B layer), and, third (C layer)
subsurface layers. The materials are contaminated to varying degrees with organic contaminants
and lead. Concentrations of both are highest in the B layer.
The McColl site is an abandoned refinery waste disposal area. The major contaminants
in soil at the site are organic constituents and sulfur. The soil borings excavated from the site
during the remedial investigation/feasibility study efforts were stored in drums at the site. The
physical characteristics of the materials do not vary significantly from drum to drum. Two
drums, one containing a high-sulfur-content material and a second containing a low-sulfur-
content material, were selected for testrng m this test program.
The overall objective of the test program was to determine whether treatment by
incineration would result in a treated soil residue suitable for redeposit at each site during full-
scale remediation. Specific technical objectives were as follows:
To determine the distribution of lead present in the Purity Oil Sales site soils
among the RKS discharges, and assist EPA in assessing the suitability of RKS
incineration for treating the Purity Oil Sales site soils by identifying metal fate
To determine the flue gas emission and incineration residuals concentrations of
the semivolatile organic hazardous constituents to verify the suitability of RKS
incineration for treating the materials
37
-------
To evaluate the effectiveness of the single stage ionizing wet scrubber APCS for
removing lead (Purity Oil Sales site), SO2 and SO3, and thereby determine the
suitability of this APCS for controlling flue gas lead, SO2, and SO3 emissions
To demonstrate compliance with the hazardous waste incinerator performance
standards for paniculate emissions
The tests were completed during January and February 1990. The draft test report
summarizing test results was completed in September 1990. An outline of the test program and
test results are given in the following subsections.
S.I
TEST PROGRAM
The test program consisted of five tests, one each with the three Purity Oil Sales soils
and the two McColl soils. All tests were performed in the RKS at the IRF with the ionizing wet
scrubber primary APCS in operation. A schematic of the RKS is given in Figure 1 and the
design characteristics of the system are given in Table 1, in Section 3.
Each soil tested was shipped to the IRF in a 55-gal drum. Nominally 200 kg (440 Ib)
of each material was shipped. Prior to testing, each material was packaged into 1.5-gal fiberpack
containers at the IRF for feeding to the RKS via the ram feeder system. Each fiberpack drum
was filled with nominally 4.1 kg (9 Ib) of test material. During the tests, each material was fed
to the kiln at a rate of 12 fiberpack drums per hr (1 drum every 5 min). Thus, test material
feedrate was approximately 49 kg/hr (108 Ib/hr). Each test was nominally 4 hr in duration. All
tests were conducted under nominally the same set of incinerator operating conditions. These
conditions are listed in Table 9. The kiln rotation speed noted in Table 9 corresponds to a solids
residence time in the kiln of about 1 hr.
Figure 10 identifies the sampling location for the tests and summarizes the sampling
protocols employed.
TABLE 9. NOMINAL INCINERATOR SYSTEM OPERATING
CONDITIONS FOR PURITY SOIL SALES AND
McCOLL SITE SOIL INCINERATION TESTS
Total waste/soil feedrate
Kiln temperature
Kiln exit flue gas O2
Afterburner
Afterburner exit flue gas O2
Kiln rotation speed
Scrubber blowdown flowrate
Scrubber liquor flowrate
Scrubber pressure drop
49 kg/hr (108 Ib/hr)
871°C (1600° F)
11 to 13%
982°C (1800°F)
9 to 11%
0.2 rpm
1.9 L/min (0.5 gpm)
230 L/min (60 gpm)
1.5 kPa (6 in W.C.)
38
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5.2
TEST RESULTS
Throughout the test program, CO levels at the scrubber exit and the stack were at most
a few ppm. Total unburned hydrocarbon levels were similarly low at the afterburner exit,
scrubber exit, and in the stack. Average NOX concentrations at the stack ranged from 20 to
38 ppm, levels typical for the RKS. Average SO2 levels measured using a continuous SO2
emission monitor at the stack were <1 ppm for the Purity Oil Sales site soil tests, and 4 to
7 ppm for the McColl site sulfur-contaminated soil tests.
Flue gas particulate levels-at the scrubber exit ranged from 6 mg/dscm (at 7 percent O2)
for the Purity C layer material test to 126 mg/dscm (at 7 percent O2) the McColl high-sulfur-
material test. In the stack, particulate levels ranged from 7 mg/dscm (at 7 percent O2) for the
Purity C layer material test to about 70 mg/dscm (at 7 percent O2) for both the Purity B layer
and McColl high-sulfur-material tests. All levels fell well below the federal hazardous waste
incinerator performance standard of 180 mg/dscm (at 7 percent O2).
Table 10 summarizes the ultimate analysis data for the soil samples from each test drum.
Table 10 also shows the carbon content of the kiln ash resulting from the incineration of each
test soil. The data suggest that incineration was quite effective in destroying the overall organic
content (as indicated by total carbon content) of the Purity site soils. However, the kiln ash
resulting from the incineration of the McColl site materials still had significant carbon content.
Table 11 summarizes the semivolatile organic hazardous constituent analysis results for
each soil. As shown, of the semivolatile organic hazardous constituents, naphthalene was found
in four of the five soils, and bis-(2-ethylhexyl)-phthalate was found in three of the five. Organic
analyses of kiln ash, kiln ash TCLP leachate, and scrubber blowdown TCLP leachate samples for
each test showed that all semivolatile organic hazardous constituents analyzed were present at
less than method detection limits in all cases. Thus, the kiln ash from all tests contained less
than detectable concentrations of the semivolatile constituents analyzed at detection limits of 1
to 2 mg/kg. Semivolatile organic contaminants were specifically not detected in the McColl soil
kiln ashes despite their significant residual carbon content noted above. Kiln ash and scrubber
blowdown TCLP leachate samples contained less than detectable concentrations of semivolatile
constituents at detection limits of 0.02 to 0.04 mg/L.
Scrubber exit and stack flue gas semivolatile organic concentrations were less than
detectable at detection limits of 4 to 12 ng/dscm for all constituents except bis-(2-ethylhexyl)-
phthalate. Apparent flue gas bis-(2-ethylhexyl)-phthalate concentrations of 8 to 80 jig/dscm are
ascribed to commonly-encountered laboratory contamination for this compound.
Test results with respect to lead distributions for the Purity Oil Sales site soil tests are
summarized in Table 12. The table shows lead concentrations measured in each soil feed, kiln
ash, scrubber blowdown, flue gas, soil feed EP toxicity and TCLP leachate, kiln ash EP toxiciry
and TCLP leachate, and scrubber blowdown EP toxicity and TCLP leachate sample analyzed.
As shown in Table 12, the lead concentrations of the Purity Oil Sales site soils ranged
from 780 to 10,200 mg/kg, with the highest concentrations found in the Purity B layer soil. Lead
concentrations in resulting kiln ash from the incineration treatment of all soils weire higher than
the parent soil concentrations, consistent with the volume reduction of the material with
40
-------
TABLE 10. ULTIMATE ANALYSIS OF THE TEST SOILS AND RESULTING KILN ASHES
Parameter
(wt%)
C
H
o
N
S
Cl
Ash
Total organic carbon
C
Purity A
layer
(Test 1)
2.14
0.99
5.27
<0.5
0.58
<0.18
86.09
1.74
0.19
Purity C
layer
(Test 2)
1.63
<0.5
2.75
<0.5
0.43
<0.21
86.15
1.61
0.12
Soil
Purity B
layer
(Test 3)
24.83
4.64
17.50
<0.5
2.43
<0.27
58.39
24.83
Kiln ash
3.39
McColl
low sulfur
(Test 4)
15.64
3.36
17.13
<0.5
3.58
<0.58
57.29
15.60
4.18
McColl
high sulfur
(Test 5)
19.88
3.65
20.83
<0.5
8.13
<0.28
41.40
19.88
6.65
TABLE 11. SEMIVOLATILE ORGANIC HAZARDOUS CONSTITUENTS IN TEST SOILS
Concentration (rag/kg)
Constituent
Naphthalene
Bis-(2-ethylhexyl)-phthalaie
All other semivolatiles analyzed
Purity A
flayer
(Test 1)
NDa
ND
<25
Purity C
layer
(Test 2)
35
77
<25
Purity B
layer
(Test3)
90
41
<25
McColl
low sulfur
(Test 4)
96
ND
<25
McColl
high sulfur
(Test 5)
340
43
<25
aND not detected.
41
-------
TABLE 12. LEAD DISTRIBUTIONS FOR THE PURITY OIL SALES SITE SOIL TESTS
Parameter
Lead concentration
Soil feed, mg/kg
Kiln ash, mg/kg
Scrubber blowdown, mg/L
Scrubber exit flue gas, mg/dscm
Stack gas, mg/dscm
Lead flowrate, g/hr
Soil feed
Kiln ash
Scrubber exit flue gas
Stack gas
Soil feed leachate
EP toxicity concentration, mg/L
Fraction leachable, %
TCLP concentration, mg/L
Fraction leachable, %
.Kiln ash leachate
EP toxicity concentration, mg/L
Fraction leachable, %
TCLP concentration, mg/L
Fraction leachable, %
Scrubber blowdown leachate
EP toxicity concentration, mg/L
TCLP concentration, me/L
Test 1
(1/19/90)
Purity A layer
860
1,620
2.8
1.6
1.2
42
61
3.3
2.8
2.1
4.9
5.7
13
<0.07
<0.1
10
12
1.4
1.4
Test 2
(1/23/90)
Purity C layer
780
1,830
3.2
1.0
0.47
39
63
1.9
1.0
2.6
2.8
18
46
0.23
0.25
15
16
1.2
1.2
Test3
d/31/90)
Purity B layer
10,200
23,800
45
24
21
510
588
46
45
2.6
0.5
21
4.1
0.33
0.03
110
9.2
19
17
42
-------
incineration. Kiln ash lead concentrations were roughly doubled over the parent soil
concentrations. Scrubber blowdown lead concentrations were in the 3 mg/L range for the Purity
A and C layer soils, and 45 mg/L for the Purity B layer soil. Similarly, scrubber exit flue gas
concentrations were in the 1 to 2 mg/dscm range for the Purity A and C layer soil tests, and
24 mg/dscm for the high-lead-concentration Purity B layer soil test. Measured stack gas
concentrations were generally slightly lower, and in the 0.5 to 1.2 mg/dscm range for the Purity
A and C layer soil tests, and 21 mg/dscm for the high-lead-concentration Purity B layer soil test.
EP toxicity leachates of all three Purity Oil Sales site soils had comparable lead
concentrations of about 2 mg/L. TCLPleachate concentrations were higher, ranging from 5.7 to
21 mg/L. The toxicity characteristic (TC) threshold concentration for lead is 5 mg/L. Thus, no
Purity Oil Sales site soil would be considered a characteristic hazardous waste for lead, based
on the EP toxicity test, but all three would be considered so based on the TCLP test.
Despite the fact that the kiln ash resulting from the incineration treatment of the Purity
Oil Sales soils contained roughly twice the lead concentrations of the parent soil, their EP
toxicity leachate concentrations were lower. TCLP leachate concentrations for the kiln ash of
both soils were significantly greater than corresponding EP toxicity leachate concentrations, and
generally greater than the parent soil TCLP leachate concentrations. As was the case with the
Purity Oil Sales site soils, these tests suggest that the kiln ash resulting from incineration
treatment of the soils would not be considered a characteristic hazardous waste for lead, based
on the EP toxicity test, but would be considered so, and thus banned from landfill disposal
without further treatment, based on the TCLP test (which is the current regulatory requirement).
Both the EP toxicity and TCLP leachate lead concentrations of the scrubber blowdown
from all three Purity Oil Sales site soils were comparable, and were lower than the parent
scrubber blowdown concentration. For the Purity materials, scrubber blowdown EP toxicity and
TCLP leachate concentrations were half or less than half of the concentrations of the parent
blowdown sample. This is understandable. Both the EP toxicity and TCLP methods for liquid
samples specify filtering the blowdown sample, then weighing the solid residue. If the solid
residue accounts for less than 0.5 percent of the original blowdown sample (as was the case for
these tests), the solid residue is discarded, and the resulting filtrate is defined to be the
corresponding leachate. The fact that scrubber blowdown EP toxicity and TCLP leachate
concentrations were similar for all Purity Oil Sales site material tests is to be expected, therefore,
since the procedures result in analyzing essentially the same sample (scrubber blowdown filtrate).
The fact that leachate (i.e., filtrate) samples contained less lead than the unfiltered blowdown
sample merely confirms that some of the blowdown lead was contained as insoluble lead in the
blowdown suspended soils (i.e., collected particulate) fraction.
Table 13 summarizes the lead discharge distributions measured in each test on a percent
of feed basis. Entries in Table 13 correspond to the fraction (in percent) of lead fed accounted
for by each of the incineration system discharge streams: kiln ash, scrubber liquor, and scrubber
exit flue gas. These fractions were calculated from the measured lead concentrations in samples
analyzed from Table 12, and the appropriate stream flowrate (i.e., soil feedrate, flue gas flowrate,
and kiln ash discharge rate). Also shown in Table 13 is the total ash fraction for each test. This
represents the ratio of the total weight of kiln ash discharged in a test to the total weight of soil
fed. The ash fractions measured from the RKS generally compare favorably to the ultimate
analysis results for soil feed samples noted in Table 10.
~ 43
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TABLE 13. LEAD DISCHARGE DISTRIBUTIONS FOR THE PURITY OIL
SALES SITE SOIL TESTS
Test
Parameter
Test 1 Test 2 . Test 3
Purity A layer Purity C layer Purity B layer
Total kiln ash discharge
(% of soil weight fed)
77
69
49
Lead distribution (% of lead fed)
Kiln ash
Scrubber liquor
Scrubber exit flue gas
Total
146
1
8
155
163
1
5
169
115
2
9
126
T.he data in Table 13 show that, for the Purity Oil Sales soil tests, between 5 and
9 percent of the soil lead was accounted for in the scrubber exit flue gas discharge, with 1 to
2 percent accounted for in the scrubber liquor. Most, between 115 and 163 percent, of the lead
fed for the Purity soils was discharged in the kiln ash. Total balance closure for the Purity tests
was 126 to 169 percent. This level of mass balance closure for lead in the system is considered
acceptable when viewed in light of past experience in achieving trace metal mass balance closure
from a variety of combustion sources, incinerators included. Typical mass balance closure results
from this past experience have been in the 30 to 200 percent range.
53 CONCLUSIONS
Test conclusions include:
The organic contaminants in all five test soils were completely destroyed based on
the analytical methods used to measure contaminant concentrations. No
detectable semivolatile organic constituents were present in the kiln ash, scrubber
blowdown, or flue gas resulting from the incineration of any of ithe five tested
contaminated soils, with the exception of bis-(2-ethylhexyl)-phthalate (a common
laboratory contaminant) in flue gas samples.
Particulate emissions at the exit of the single stage ionizing wet scrubber employed
for particulate and acid gas control ranged from 6 to 126 mg/dscm at 7 percent
O2, depending on the test soil. All measured levels were below the federal
hazardous waste incinerator performance standard of 180 mg/dscm at 7 percent
02.
For the Purity Oil Sales site soil tests, kiln ash lead concentrations were roughly
double the parent soil concentrations. Scrubber blowdown lead concentrations
44
-------
were about 3 mg/L for the two low-lead-concentration Purity soils (on the order
of 800 mg/kg lead contamination). Scrubber exit flue gas concentrations were 1 to
1.6 mg/dscm for these soils. For the high-lead-concentration Purity soil
(10,200 mg/kg lead), scrubber blowdown and exit flue gas concentrations were
increased to 45 mg/L and 24 mg/dscm, respectively. Between 5 and 9 percent of
the lead fed to the incinerator was accounted for in the scrubber exit flue gas for
all three soils. Lead concentrations in the scrubber blowdown, EP toxicity
leachates of the soil feed, kiln ash, and scrubber blowdown, and TCLP leachates
of scrubber blowdown, were less than the TC threshold defining a characteristic
hazardous waste for the two low-lead-concentration Purity soils. However, lead
concentrations in TCLP leachates of the soil feed and kiln ash exceeded the TC
threshold for these soils. Lead concentrations in the scrubber blowdown, EP
toxicity leachates of the scrubber blowdown, and TCLP leachates of the soil feed,
kiln ash, and scrubber blowdown, for the high-lead-concentration Purity soil,
exceeded the TC threshold. EP toxicity leachates of the soil feed and kiln ash for
this soil, however, did not exceed the TC threshold.
Test results suggest that incineration would be an acceptable treatment option for the
McColl site materials. Based on these results, organic contaminant destruction is complete;
particulate emissions comply with the federal hazardous waste incinerator performance
standards; SO2 emissions are low; and incineration residuals would not be considered
characteristic hazardous wastes.
Incineration could be considered applicable to the treatment of the Purity Oil Sales site
soils based on effective organic decontamination; in-compliance (with federal standards)
particulate emissions; and low SO2 emissions. However, these test results indicate that the
resulting kiln ash would require further treatment to stabilize or remove leachable lead, and that
the scrubber blowdown from the incineration of the high-lead-concentration soil would be
considered a characteristic hazardous waste if a wet scrubber were used for air pollution control.
Furthermore, the acceptability of lead emission levels from a wet scrubber control device would
require further evaluation.
Test results were documented in the test report:
Vocque R. H., and L. R. Waterland, "Pilot-Scale Incineration of Contaminated
Soil from the Purity Oil Sales and McColl Superfund Sites," draft September 1990.
In addition, test results are planned for presentation in a technical paper:
Waterland, L. R., C. King, R. H. Vocque, M. K. Richards, and H. O. Wall, "Pilot-
Scale Incinerabiliry Evaluation of Arsenic- and Lead-Contaminated Soils from
Three Superfund Sites," for presentation at the Incineration Conference1991,
Knoxville, Tennessee, May 1991.
45
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SECTION 6
PARAMETRIC TESTING TO EVALUATE THE
PROPOSED POHC INCINERABILITY RANKING
One of the primary functions of the IRF is to conduct research activities for OSW in
support of regulation development and implementation. One major regulatory issue of high
priority during FY90 concerned the evaluation of the thermal stability-based POHC" incinerability
ranking developed over the past several years by the University of Dayton Research Instkute
(UDRI) under contract to RREL. Current hazardous waste incinerator permits have been
issued based on the heat of combustion ranking of POHC incinerability. This ranking has
several acknowledged deficiencies. UDRI has developed an alternative ranking based on the
temperature required to achieve 99 percent destruction at 2 s residence: time under
oxygen-starved conditions as measured in laboratory experiments. The evaluation of this ranking
under actual incineration conditions became a high-priority research need in FY90.
The test program discussed in this section was designed to develop the data to evaluate
the POHC incinerability ranking. The specific objectives of the test program were to measure
each POHC's DRE under each of several modes of incinerator operation, and compare relative
POHC DREs as a function of incineration conditions and feed characteristics. In the tests, a
mixture (soup) of 12 POHCs with predicted incinerability spanning the range of the most
difficult to incinerate (refractory) class to the least difficult to incinerate (labile) class was tested.
This mixture was combined with a clay-based sorbent solid matrix and packaged into fiberpack
drums for batch feeding to the RKS at the IRF.
A series of five experiments were performed over which incinerator opera ting conditions
and test mixture composition were varied. Specific test program variables were kiLn temperature,
feed batch charge mass, and feed composition, specifically H/C1 ratio. One test was performed
under typical operating conditions with a baseline soup composition. The other tests varied the
above in an attempt to simulate various modes of incineration failure: thermal failure, mixing
failure, feed matrix effects, and a worst-case combination of these.
6.1
TEST PROGRAM
The test program was conducted in the IRF RKS with the venturi/packed column
scrubber APCS in use. Figure 1 in Section 3 shows a simplified schematic of the RKS, and
Table 1 gives the design characteristics of the key system components.
The 12 POHCs included in the test synthetic waste mixtures were selected in
consultation with UDRI, RREL, OSW, and EPA incinerator permit writer personnel. The
46
-------
incinerability ranking groups the 333 POHCs included in the ranking into 7 stability classes from
most refractory (Class 1) to most labile (Class 7). UDRI recommended that two compounds
from each class be included in the test mixture and provided a list of candidates for selection.
The compounds tested were selected from this candidate list, their selection guided by ease of
flue gas sampling and sample analysis, compound compatibility, compound availability, and safety
considerations. The compounds in the test POHC mixture are listed in Table 14. The table also
notes the target composition of two test mixtures containing the POHCs with different H/C1
ratios.
The POHC liquid mixtures prepared for the tests were combined with a clay-based oil
sorbent solid and packaged into 1.5-gal fiberpack drums for feeding to the RKS. Each fiberpack
contained nominally 3 Ib of POHC test mixture and 5 Ib of clay sorbent.
As noted above, the test program was designed to evaluate the relative incinerability of
the POHCs in the test mixture under typical, or normal, incineration condkions, and then
evaluate relative incinerability under several modes of potential incineration failure: thermal
failure, mixing failure, more challenging feed mixture, and a worst-case combination of these
three.
Table 15 summarizes the test conditions for each of the five tests performed. The nor-
mal incineration mode test was run at a kiln temperature of nominally 871°C (1600°F) with a
baseline soup/clay feedrate of 1 fiberpack drum charge every 5 min. Thermal failure was
achieved by decreasing kiln temperature to nominally 649° C (1200° F), by decreasing the
auxiliary fuel (natural gas) feedrate to the kiln, and by introducing water in the POHC/clay
mixture. Mixing failure was achieved by doubling the drum charge mass to two drums per
charge, although overall drum feedrate was kept constant by decreasing the charge frequency to
every 10 min. Doubling charge mass was expected to produce oxygen-starved pockets of
combustion gas in the kiln. Matrix effects were investigated by testing the low-H/Cl-ratio POHC
mixture at the baseline condition of nominally 871° C (1600° F) kiln temperature and 1 drum
charge every 5 min. A worst-case condition of nominally 649° C (1200°F) kiln temperature and
a 2-drum charge of the low-H/Cl-POHC mixture comprised the fifth test. Overall POHC feed
mixture feedrate was held constant for all tests.
62 SAMPLING AND ANALYSIS
Satisfying the test objectives required that the DRE of each POHC be measured for
each test, so that relative DREs among the test POHCs could be confirmed. For this purpose,
the primary flue gas sampling location was at the kiln exit since incinerator failure modes were
simulated in this test program by varying kiln conditions. However, it was also of interest to
evaluate the relative magnitude of additional POHC destruction and removal achieved in the
afterburner and APCS of the RKS, and to assess whether relative POHC DREs are preserved
through these processes. Thus, a secondary flue gas sampling location was at the APCS exit.
In addition, sampling was performed of the system's stack discharge, after further flue gas
treatment in the system's secondary APCS, to meet the requirements of the IRFs hazardous
waste management permit. Finally, POHC feed mixture, kiln ash, and APCS blowdown
discharge samples were taken for POHC analysis. The specific sampling and analysis protocol
employed for all five tests included:
47
-------
TABLE 14. INCINERABILITY RANKING MIXTURE COMPOSITION
Concentration (wt%)
Component
Benzene
Chlorobenzene
Tetrachloroethene
1,2,2-trichloro-
1, 1,2-trifluoroethane
(Freon 113)
Benzenethiol »
Nitrobenzene
Hexachlorocyclohexane
(Lindane)
Hexachloroethane
1, 1, 1-trichloroethane
p-dimethylaminoazobenzene
(Methyl yellow)
Nicotine
N-nitroso-di-n-butyl amine
Ultimate composition
C
H
O
N
S
Cl
F
Higher heating value,
MJ/kg
(Btu/lb)
H/C1 (molar)
Mixture 1
high H/C1
8
8
8
8
8
8
10
10
10
10
10 ;
2
46.0
3.9
2.3
4.9
2.3
38.2
2.4
19.6
(8450)
3.6
Mixture 2
low H/C1
4
4
33
4
4
4
5
25
5
5
5
2
29.8
2.1
1.2
2.6
1.2
61.9
1.2
12.0
(5170)
1.2
T99(2)8(°C)
1150
990
890
780
725
655
645
585
545
-400
<320
<320
..
Rank"
3
22 .
43
92
122
150,151
159
213
233
268
286 to 289
316 to 331
Stability
class
1
1
2
'3
3
4
4
5
5
6
7
7 ..
"Temperature required to achieve 99 percent destruction in 2 s.
blncinerability rank in list range from most refractory (No. 1) to most labile (No. 333).
48
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TABLE 15. TEST CONDITIONS
Parameter
Test 2, Test3,
Test 1 thermal mixing
baseline failure failure
(6/26/90) (7/17/90) (7/3/90)
Test 4,
matrix Test 5,
effect worst case
(6/29/90) (7/12/90)
1
Feed mixture (see Table 14)
Feedrate, kg/hr (Ib/hr)
Organic soup
Water
Organic/clay/water mixture
Feed regimen
Organic/clay/water per drum, 3.6(8)
1
1
17 (37) 17 (37) 17 (37)
11(24)
46 (98) 56 (122) 46 (100)
17(37) 17(37)
46 (98) 46 (100)
4.6(10) 3.6(8) 3.6(8) 3.6(8)
1
12
2
6
kg (Ib)
Drums/charge 1 1 2
Charges/hr 12 12 6
Kiln ,
Average temperature, °C (°F) 859(1579) 663(1226)863(1585)
Average exit O2, % 14.9
Afterburner
Average temperature, °C (°F) 988 (1810) 988 (1810) 988 (1810) 988 (1810) 988 (1810)
Average exit O2, % 9.0 9.5
876 (1609) 640 (1184)
12.2 15.2
Sampling the flue gas at the kiln exit, downstream of the APCS, and in the stack
for ;.'--.
Volatile organic hazardous constituents using Method 0030 (VOST)
Semivolatile organic hazardous constituents using Method 0010 (MM5)
Additional sampling of the stack gas for particulate and HC1 emissions using
Method 5 with impingers charged with dilute caustic for HC1 capture
Obtaining composite samples of the kiln ash and APCS blowdown, and analyzing
them for both volatile and semivolatile organic hazardous constituents
Analyzing aliquots of the prepared synthetic waste feed for POHCs
49
-------
Continuous monitor sampling of location-specific combinations of flue gas O2,
CO2, CO, NO,, and heated and unheated TUHC at the kiln, afterburner, and
scrubber exits and in the stack
Figure 11 summarizes the test program sampling protocol.
63 TEST RESULTS
The test program was performed in late June and early July 1990. Most sample analysis
efforts were completed by the end of FY90. However, test data reduction and interpretation
were still underway.
Preliminary results indicate the following:
Benzenethiol, methyl yellow, nicotine, and N-nitroso-di-n-butyl amlne destruction
was essentially complete, even at the kiln exit, for all tests. These compounds
were not detected in the kiln exit flue gas in any test.
Kiln exit DREs for the other eight POHCs were, from test to test, comparable for
Test 1 (baseline), Test 3 (mixing failure), and Test 4 (matrix efftsct). Benzene,
chlorobenzene, tetrachloroethene, Freon 113, and 1,1,1-trichloroethane DREs
were in the 99.99 to 99.999 percent range for all three tests. Nitrobenzene,
Lindane, and hexachloroethane were not detected in the kiln exit flue gas in these
three tests
Kiln exit DREs for the other eight POHCs ranged from 99 to 99.9999 percent for
Test 2 (thermal failure) and Test 5 (worst case), and were generally comparable
for each POHC for both tests. From Freon 113 through hexachloroethane,
measured DRE generally agreed with the incinerability ranking. Apparent 1,1,1-
trichloroethane DRE was lower than would be predicted by the ranking; however,
1,1,1-trichloroethane is a common product of incomplete combustion (PIC) from
chlorinated hydrocarbon combustion. Benzene, chlorobenzene, and tetrachloro-
ethylene DREs were greater than the DRE for Freon 113, which is not expected
from the incinerability ranking
Data interpretation and test reporting will proceed through completion in FY91.
50
-------
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51
-------
SECTION 7
EXTERNAL COMMUNICATIONS
During FY90, four reports were prepared and submitted, and eight technical papers
were presented. These are listed in Table 16. This level of external communication and
technology transfer is comparable to levels experienced over the preceding three years and
testifies to the high level of important research being supported at the IRF.
Table 17 lists some of the visitors to the IRF during FY90. The length of the list attests
to the visibility to the incineration research community of the work being performed at the IRF.
52
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TABLE 16. IRF PROGRAM REPORTS AND PRESENTATIONS IN FY90
Reports
Waterland, L. R., "Operations and Research at the U.S. EPA Incineration Research Facility,
Annual Report for FY89," draft December 1989, revised January 1990, published as EPA/600/2-
90/012, March 1990
King C., and L. R. Waterland, "Pilot-Scale Incineration of Arsenic-Contaminated Soil from the
Baird and McGuire Superfund Site," draft March 1990, revised May 1990
Fournier, Jr., D. J., and L. R. Waterland, "The Fate of Trace Metals in a Rotary Kiln Incinerator
with an Ionizing Wet Scrubber," draft April 1990
Vocque, R. H., and L. R. Waterland, "Pilot-Scale Incineration of Contaminated Soil from the
Purity Oil Sales and McColl Superfund Sites," draft September 1990
Papers and Presentations
Carroll, G. J., L. R. Waterland, and D. J. Fournier, Jr., "Parametric Evaluation of Metal
Partitioning at the U.S. EPA Incineration Research Facility," presented at the Sixteenth Annual
Research Symposium on the Remedial Action, Treatment, and Disposal of Hazardous Waste,
Cincinnati, Ohio, April 1990
Wall, H. O., and M. K. Richards, "The Incineration of Arsenic-Contaminated Soils Related to the
Comprehensive Environmental Response, Compensation, and Liability Act (CERCLA),"
presented at the Sixteenth Annual Research Symposium on the Remedial Action, Treatment, and
Disposal of Hazardous Waste, Cincinnati, Ohio, April 1990
Thurnau, R. C., and J. W. Lee, "IRF Update," presented at the Sixteenth Annual Research
Symposium on the Remedial Action, Treatment, and Disposal of Hazardous Waste, Cincinnati,
Ohio, April 1990
Waterland, L. R., D. J. Fournier, Jr., J. W. Lee, and G. J. Carroll, "Trace Metal Fate in a Rotary
Kiln Incinerator with an Ionizing Wet Scrubber," presented at the Incineration Conference
1990, San Diego, California, May 1990
Waterland, L. R., "The EPA Incineration Research Facility: Capability, Availability," presented at
HazWaste Expo Atlanta 90, Atlanta, Georgia, May 1990, and at HazWaste Expo San Diego 90,
San Diego, California, June 1990
Fournier, Jr., D. J., L. R. Waterland, and G. J. Carroll, Trace Metal Size Distributions in Flue
Gas Particulate from a Rotary Kiln Incinerator," presented at the American Association for
Aerosol Research 1990 Annual Meeting, Philadelphia, Pennsylvania, June 1990
Fourier, Jr., D. J., L. R. Waterland, and G. J. Carroll, "Size Distributions of Trace Metals in Flue
Gas Particulate from a Pilot-Scale Rotary Kiln Incinerator," presented at the American Flame
Research Committee 1990 Fall International Symposium on NO, Control, Waste Incineration,
and Oxygen-Enriched Combustion, San Francisco, California, October 1990
Waterland, L. R., C. King, R. C. Thurnau, and M. K. Richards, "Incinerability Testing of an
Arsenic-Contaminated Superfund Site Soil," presented at the Pacific Northwest International
Section of the Air and Waste Management Association 1990 Conference, Portland, Oregon,
November 1990 ,
53
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TABLE 17. VISITORS TO THE IRF
Person
J. Lewtas
S. Harmon
P. Fu
K. Dooley
A. Shattuck
O. Kitaplioglu
H. Huppert
E. McNicholas
M. Gamboa
M. Kourhedar
D. Webster
J. Riseley
E. Holan
G. Minlnni
B. Blaney
E. Bates
F. Freestone
R. Olexsey
R. Loftus
B. Keogh
D. Brama
J. Smith
Affiliation
EPA/HERL
EPA/HERL
NCTR
NCTR
SAIC
SAIC
SAIC
SAIC
SAIC
ADPCE
EPA/Region 6
Koch Engineering
Koch Engineering
National Research
Council, Italy
EPA/RREL
EPA/RREL
EPA/RREL
EPA/RREL
USDA
CH2M Hill
AVS Video
AVS Video
Date
10-11-90
11-7-89
11-8-89
\ 1-24-90
1-25-90
1-29-90
1-30-90
2-5-90
2-6-90
Purpose of visit
Discuss possible bioassay testing
K088 BDAT test planning, facility
tour
Corrective action site inspection
Facility tour
Facility tour
Facility tour to assess capabilities to
support START program
Facility tour
Facility tour
Produce facility video
M. Abdulhafid ADPCE
G. Carroll
R. Hill
J. Whitney
R. Gentry
B. Blackburn
J. Frubob
G. Carroll
S-C. Yung
EPA/RREL
EPA/RREL
Rineco
Gentry & Assoc.
S-Cubed
ADPCE
EPA/RREL
Calvert
Environmental
2-7-90 Facility tour
3-12-90 Facility tour, project review
5-10-90 Discuss possible third party testing
5-17-90 QA review ...-.
6-1-90 Annual hazardous waste inspection
6-5,6-90 Project review
6-8-90 Discuss use of pilot scrubber in test
program
(continued)
54
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TABLE 17. CONCLUDED
Person
M. Henderson
B. Muler
F. Ryan
P. Espinosa
R. Peters
C-L. Ku
S-C. Chin
D-C. Lui
M. Cramer
R. Sevelte
T. McChesney
R. Mournighan
J. I. Guzman
R. Schrock
D. Johnson
N. Narane
C. Bisgard
M. Fisher
R. Wilson
H. Wong
J. Clayson
R. Hayes
Affiliation Date Purpose of visit
Burns & Roe 6-14-90 Facility tour
Burns & Roe
Burns & Roe
Burns & Roe
Burns & Roe . :
Republic of China, 6-26-90 Facility tour
ITRI
Arkansas 9-5-90 Facility tour
Department of
Health
EPA/RREL, 9-20-90 Drake Chemical test planning
EPA/RREL
EPA/Region 3
USAGE
USAGE
USAGE
USAGE
JMM
JMM
El Dorado Eng.
El Dorado Eng.
55,
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SECTION 8
PLANNED EFFORTS FOR FY91
One major test program was completed in the third quarter of FY90 for which sample
analyses and data evaluation efforts were underway at the end of FY90. This was the POHC
incinerability ranking evaluation discussed in Section 6. Remaining test sample analyses, test
data reduction and interpretation, and test reporting efforts will continue into FY91.
Most of the major facility construction and equipment upgrade efforts planned over the
past 2 years were substantially completed during FY90. However, several facility and equipment
improvements are planned for FY91. These include:
Installing 5000 ft2 of new modular office space to replace the current leased office
trailers, which have served their useful life
Completing the configuration of the automated process control system, extending
its control to the entire RKS with associated scrubbers system, and bringing into
operation its full data acquisition features
Replacing the aging RKS kiln drive and drum ram feeder.
With respect to test activities, six firm test programs of varying scope are planned for
FY91, as follows.
Evaluating the capability of the IRF RKS to perform low-temperature thermal
desorption studies. Scoping tests with garden topsoil were initiated in August
1990 and continued through October 1990. An additional series of tests with soil
from the Caldwell Trucking Superfund site in Region 2 (E. Finerty, Region 2, and
D. Hooker, USAGE, coordinators). The Caldwell site soil is contaminated with
high levels of volatile organics and lead. The Caldwell Trucking site soil low-
temperature desorption tests are planned for December 1990.
Residuals characterization tests to establish best demonstrated available
technology (BDAT) treatment standards for spent potliners from the primary
reduction of aluminum, listed waste K088 (R. Turner, J. Labiosa, L. Rosengrant,
coordinators); planned for completion in January 1991.
Incinerability testing of contaminated soils from the Drake Chemical Superfund
site in Region 3 (R. Schrock, Region 3 and D. Johnson, USAGE, coordinators).
56
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Much of the planning for these tests was completed during FY90. Tests of five
trace-metal-contaminated soils, two organic-contaminated soils, and two lagoon
sediments are planned for completion in January and February 1991.
Incinerability testing of PCB-contaminated marine sediments from the New
Bedford Harbor Superfund site in Region 1 (M. Sanderson, Region 1 and
M. Adoph, K. Howe USAGE, coordinators). A parametric test program
comprised of three tests at varying combinations of kiln temperatures and excess
air are planned for completion in March 1991. The effect of incinerator operation
on PCB destruction and contaminant trace metal fate will be evaluated.
Testing of the fate of trace metals in the RKS using a Calvert Flux Force
Condensation scrubber system for air pollution control. A test matrix similar to
that employed in the ionizing wet scrubber tests discussed in Section 3 is planned
for completion in May, June, and July 1991.
Incinerability testing of 'arsenic- and pesticide-contaminated soil from the
Chemical Insecticide Corporation Superfund site in Region 2 (J. Josephs,
coordinator) using the Calvert scrubber for air pollution control. A series of three
tests is planned for completion in August 1991.
Testing is expected to be initiated in December 1990 and continue relatively uninterrupted
through FY91.
Other test programs currently under discussion as possible candidates for late FY91 or
FY92 performance include:
A parametric test series to evaluate the effect of feed metal form on trace metal
fate in the RKS. Alternative feed metal forms other than the aqueous solution
co-fed with a clay-based hazardous waste analog include an aqueous metal
solution atomized into the kiln burner flame, and mixed metal oxide powders fed
with the clay-based hazardous waste analog.
A parametric field test series to evaluate a POHC surrogate "soup" for possible
trial burn applications. This test series was proposed for completion during FY90,
but was superseded by the incinerability ranking tests discussed in Section 6.
Incinerability testing of contaminated materials from the SCP/Carlstadt Superfund
site in Region 2
Incinerability testing of contaminated materials from the M.W. Manufacturing
Superfund site in Region 3
Parametric testing of a synthetic Superfund soil matrix to support the Superfund
Program Office
Private sector third-party testing to be defined.
57
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REFERENCES
2.
K -
Waterland. L. R., "Operations and Research at the U.S. EPA Incineration Research
Facility: Annual Report for FY89," EPA/600/2-90/012, March 1990.
Barton, R. G., et al. "Development and Validation of a Surrogate Metals Mixture."
Proceedings of the Fifteenth Annual Research Symposium: Remedial Action.
Treatment and Disposal of Hazardous Waste. EPA/600/9-90/006, February 1990.
58,
&U.S. GOVERNMENT PRINTING OFFICE: Wtl - 548-187/25617
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