United States
Environmental Protection
Agency
Hazardous Waste Engineering
Research Laboratory
Cincinnati OH 45268
Research and Development
EPA/600/S2-86/059 Sept. 1986
v>EPA Project Summary
Field Evaluation of Resource
Recovery of Hazardous
Wastes
A. W. Wyss, C. Castaldini, and M. M. Murray
The overall objective of this study
was to evaluate the effectiveness of
two process kilns in destroying haz-
ardous wastes and quantify stack gas
emissions. During two 1-week field
testing programs, samples of the haz-
ardous wastes fired in the kilns were
collected and analyzed for principal or-
ganic hazardous constituents (POHCs),
selected trace metals, and chlorides. Air
emissions were sampled and analyzed
for paniculate matter (including trace
metals); volatile and semivolatile
POHCs found in the wastes and other
products of incomplete combustion
(PICs); and criteria pollutants including
sulfur oxides, nitrogen oxides, carbon
monoxide, and hydrochloric acid. Test
results indicated that destruction and
removal efficiencies (DREs) of POHCs at
one site failed to meet the 99.99 percent
level. POHC DREs at the second site
were generally above this level. This
disparity of results was attributed to a
difference in kiln operating tempera-
ture. Benzene, chlorobenzene, and car-
bon tetrachloride showed lowest DREs
at both sites. Total PIC mass emissions
accounted for 25 to 80 percent of the
total measured POHC breakthrough.
Trace element emissions, which were
generally below 10 percent of the meas-
ured input rate, were dependent on the
collection efficiency of the particulate
control devices and waste firing rates.
This Project Summary was devel-
oped by EPA's Hazardous Waste Engi-
neering Research Laboratory, Cincin-
nati, OH, to announce key findings of
the research project that is fully docu-
mented in a separate report of the same
title (see Project Report ordering infor-
mation at back).
Introduction
The full report describes emission re-
sults obtained from field testing of two
rotary process kilns burning liquid haz-
ardous chemical wastes. The primary
objective of the tests was to evaluate
the destruction and removal efficiency
(ORE) of principal organic hazardous
constituents (POHCs) in these waste
fuels and identify products of incom-
plete combustion (PICs) emitted from
the two kilns. This work was supervised
by the Hazardous Waste Engineering
Research Laboratory of the Environ-
mental Protection Agency (EPA-
Cincinnati) under contract no. 68-02-
3176, task 4B.
Kiln Descriptions
Figure 1 is a schematic of the site I kiln
facility tested in this program and sum-
marizes the key design and operating
features. Site I is a rotary kiln dryer
tested at a capacity of about 10 kg/s (40
tons/hr) when fired with a heat input ca-
pacity of approximately 11 MW (37.5
million Btu/hr). The kiln dries earth-type
clays, reducing the moisture content
typically from 50 percent to 8 percent.
The 8 percent clay product is marketed
as cat litter and as an impermeable liner
for ponds. This product can be further
processed to reduce the moisture to 0.5
percent, resulting in a product that is
-------
Surge Tank f~150 gal)
Raw Clay
Cl . Fuel
Electnc strainers
Preheaters
Exhaust
Gas
Waste
Oil
Storage
20,000 gal
I
Blended
Fuel
Storage
20,000 gal
Atomization
Air
I®
*Dryed Clay
Product
Collected
Dust
Fuel Pump
Compartmented Truck
Kiln length, m (ft)
Kiln diameter, m (ft)
Kiln rotation, rpm
Feed material
Process capacity, kg/s (tons/hr)
Feed material moisture, percent
Product moisture, percent
Process temperature, °C (°F)
Estimated gas residence time, sec
Typical heat input at capacity.
MW (million Btu/hr)
Fuel fired
Paniculate control device
Waste Solvent Storage
21.3(70)
2.1 (7)
6.25
Earth-type clays
10 (40)
50
8'
590 to 650
(1, WO to 1,200)
2.5
11.0(37.5)
Waste oils and waste
solvents
Fabric filter baghouse
Sample Collection
Location
"Product can be reprocessed for 0.5 percent moisture
Figure 1, Process flow schematic and sample collection locations—site I.
marketed as an oil and grease ab-
sorbant. However, the principal product
at site I is the 8 percent clay.
The plant receives and stores burn-
able liquid wastes. These wastes are
blended with reclaimed or virgin oil be-
fore being fired in the kiln. The single
burner is fired with a typical 20/80 mix-
ture of waste fuel and reclaimed oil, re-
sulting in an early combustible fuel. The
kiln process temperature ranges be-
tween 590° and 650°C (1,100 and
1,200°F) with an estimated gas resi-
dence time of 2.5 sec. This is a relatively
low-temperature environment for effi-
cient hazardous waste destruction. Flue
gas paniculate emissions are controlled
with a fabric filter baghouse.
Figure 2 is a schematic of the site II
kiln facility tested in this program and
summarizes the key design and operat-
ing features. Site II is a rotary aggregate
kiln that processes shales into a
lightweight aggregate material by pro-
moting various heat activated chemical
reactions and liberating carbon dioxide
from the raw material. This causes the
aggregate to expand, resulting in a
lightweight product. A process temper-
ature greater than 1,040°C (1,900°F) is
generally required to achieve this reac-
tion. The kiln capacity of site II is about
2.5 kg/s (12 tons/hr). Its typical produc-
tion rate is between 2.3 and 2.5 kg/s (9 to
12 tons/hr), requiring a heat input on the
order of 7.9 to 8.8 MW (26 to 30 million
Btu/hr). The gas residence time is about
equal to that of the site I kiln at 2.3 sec.
The fuel burned is generally a combina-
tion of pulverized coal and hazardous
waste solvents injected through two
concentric burners.
Liquid waste solvents, transferred
from an isolated tank farm, are air atom-
ized and injected into the kiln along with
pulverized coal. Additional air is pulled
into the kiln through openings near the
flame end of the kiln by an induced draft
(ID) fan. Fuel flow is adjusted by a con-
troller that measures the temperature of
the kiln wall, compares this value with a
present level, and adjusts the fuel flow
accordingly. The maximum permitted
liquid fuel firing rate is 370 ml/s (350
gph). Dust-laden gases from each kiln
are treated in separate air cleaning sys-
tems consisting of a multiclone fol-
lowed by a crossflow gravity spray wet
scrubber. Spent scrubber water is sent
to a settling pond for clarification before
being discharged to a local stream. Dust
collected by the multiclone is landfilled
or sometimes reprocessed in the kiln.
-------
Atomization I Expanded
Blower for j Product
Solvent \^_Pulverized_ Coal
Shale From Conveyor
Mechanical
Collector
^ v Exhaust
r-i -. x Gas
V \
\ Water
Hopper \ From ~~]
led „ \ Lake i
fl'e/- V/ \ |
> \ LJ
Dust Emergency'^
1 \ Bypass
"*==^ Coal From^.. ,
Lciassff^r Blower 1 ^ CM/fl//j /D Fa/,
-J-H-^fCp-n ! kj
SfacA
S'°raffe *(9)
Tank I&1
Pump '
CP~i® !
,.L,-.,..T.., |
Scrubber i®
To D/fc/7, Settling
Ponds, and Streams
fla//
,,,>
Kiln length, m (ft)
Kiln diameter, m (ft)
Kiln rotation, rpm
Feed material
Process capacity, kg/s (tons/hr)
Feed material moisture, percent
Product moisture, percent
Process temperature, °C (°F)
Estimated gas residence time, sec
Typical heat input at capacity,
MW (million Btu/hr)
Fuel fired
Paniculate control device
NA—not available.
38.1 (125)
2.7(9)
1.1
Shale
2.3 to 2.5 (9 to 10)
NA
NA
1,120 to 1,180
(2,050 to 2,150)
2.3
7.9 to 8.8
(27 to 30)
Pulverized coal and
liquid waste
Mechanical collector
and wet scrubber
Coal
Exhaust gas
Scrubber water
= Aggregate
Waste solvent
® Sample collection locations
figure 2. Process flow schematic and sample collection locations—site II.
Test Program
The test program at site I consisted of
three tests with the kiln firing a blend of
liquid waste and waste oil. Four tests
were performed at site II. During the
first two tests the kiln fired a combina-
tion of pulverized coal and liquid waste.
This mode of operation is typical for this
site. During the remaining two tests, the
kiln was fired with liquid waste only.
Table 1 summarizes the operation of
both kilns during these tests. Significant
burner combustion stability problems
were experienced during the first test at
site I. These problems, which caused in-
terruptions in the test program, were
believed to result from excessive pre-
heating of the waste fuel mixture. This
excessive preheating was corrected
during the second and third tests. Kiln
operation at site II was uninterrupted by
any recorded upsets due to combustion
conditions.
Sampling and Analytical
Protocols
The primary objective of the test pro-
gram was to evaluate the DRE of haz-
ardous organic compounds in the liquid
waste fuel and to determine the type
and quantities of PIC emissions. There-
fore, the sampling and analytical proto-
cols focused on measuring the hazr
ardous organic constituents in the
liquid waste fuels and flue gas streams
and quantifying the mass flow rate of
each stream. Tables 2 and 3 summarize
the protocols used at each test site. Fig-
ures 1 and 2 indicate sample collection
locations.
Composite samples of the waste fuels
were collected and analyzed for POHC
concentrations of volatile and non-
volatile organics. Trace metals, total
chlorides and proximate/ultimate analy-
ses were also performed on each fuel
burned during the tests. All flue gas
emissions were measured at the stack
downstream of particulate collection
devices. Measurement equipment used
at both sites included continuous gas
monitors, volatile organic sampling
train (VOST) and a modified version of
the EPA Method 6 sampling train for HCI
-------
Table 1. Summary of Kilns Operation
Kiln
Test production
Site number kg/s (tons/hr)
Waste fuel flowrate,
ml/s (gph)
Waste fuel heat input
Test MW Percent
Range average (million Btu/hr)a of total
1
II
1
2
3
1C
2c
3
4
-6.8
-7.6
-7.6
2.17
2.25
2.19
(27)b
(30)b
(30)"
(8.62)
(8.94)
(8.69)
NA
205-216
226-263
220-252
220-284
142-255
270-348
270-354
(195-205)
(215-250)
(209-240)
(209-270)
(135-243)
(257-331)
(257-337)
210
238
237
242
197
315
318
(200)
(226)
(225)
(230)
(187)
(300)
(302)
7.45
8.41
8.39
6.07
5.01
8.50
8.71
(25.4)
(28.7)
(28.6)
(20.7)
(17.1)
(29.0)
(29.7)
100
100
100
59
47
100
100
Calculated from the fuel higher heating values.
bNot a measured value.
cTests 1 and 2 correspond to the kiln firing a combination of waste fuel and pulverized coal.
During Tests 3 and 4, the waste fuel accounted for 100 percent of the fuel fired in the kiln.
NA—Not available.
measurements. Paniculate emissions
were also sampled using the EPA
Method 5 equipment and protocol. This
sampling train was modified for site I to
allow sampling of semivolatile and non-
volatile organics using an organic sor-
bent cartridge. Solid and liquid waste
discharge streams from particle collec-
tion devices were also sampled. Analy-
ses of these streams were limited to wet
scrubber effluents for volatile organics,
trace metals and chlorides. No volatile
organics were detected in the wet
scrubber effluent collected during these
tests. Kiln products were not part of the
sampling and analysis protocol.
Waste fuels at both sites were artifi-
cially spiked with a known quantity of
1,1,2-trichloro-2,2,1-trifluoroethane
(Freon 113) to permit a direct compari-
son of ORE results between these two
kilns and to investigate the feasibility of
using this compound as a surrogate for
DRE measurements of other major
POHCs present in the waste fuels.
Criteria Emissions
Table 4 summarizes the results of
criteria gaseous and paniculate emis-
sions at both test sites. The site I kiln
was operated at high excess air levels
averaging about 280 percent. This high
excess air level cooled the combustion
products, resulting in relatively low NOX
formation. S02 emissions corre-
sponded to about 30 to 100 percent of
the sulfur input from the waste fuel.
Low sulfur recovery may be attributed
to partial SO2 retention in the clay
product collected by the baghouse. Hy-
Table 2. Sampling and Analysis Protocol for Site I Rotary Kiln Clay Dryer
Sample/collection location
Atmospheric flue gas emissions/
stack downstream of
fabric filter
Type of sample/
monitoring equipment8
• Continuous monitors
• Modified EPA Method 5
Number of
samples13
Continuous (8 to
10 hr/test)
3 (1 run/test)
Analysis'
• O2, CO2, CO, NO/NOX, SO2
• Semivolatile and nonvolatile
Fuel (waste oil and liquid
burnable waste blend)/
fuel strainers
• VOST
• Modified EPA Method 6
• Composite sample
Fabric filter collected dust/
fabric filter hopper
Composite sample
organics by GC/MS
• Paniculate matter by gravimetry
• Trace metals by atomic absorption
9 (3 runs/test) • Volatile organics by GC/MS
6 (2 runs/test) • HCI by titration with silver nitrate
3(1 per test) • C, H, N, O, S, and HHV by ASTM
methods
• Total chloride, ASTM P808
• Volatile organics by GC/MS
• Semivolatile and nonvolatile organics
by GC/MS
• Trace metals by atomic absorption
3 (1 per test) No analysis performed
aAppendix A (Volume I) presents a detailed description of sampling equipment and protocols used.
bDoes not include blanks, spikes, or other quality control samples.
cAppendix B (Volume I) presents a detailed description of analytical equipment and protocols used.
-------
Table 3. Sampling and Analysis Protocol for Site II Rotary Aggregate Kiln
Type of sample/
Sample/collection location monitoring equipment3
Atmospheric flue gas emissions/ • Continuous monitors
stack downstream of
wet scrubber
• EPA Method 5
• VOST
• Modified EPA Method 6
Liquid waste • Composite sample
fuel/burner or
fuel storage tank
Coal/pulverized • Composite sample
coal hopper
Mechanical • Composite sample
collector dust/
multicyclone
hopper
Wet scrubber • Composite sample
influent and
effluent/inlet
and outlet of wet
scrubber
Number of
samples'1
Continuous (8 to
10 hr/test)
12 (3 runs/test)
12 (3 runs/test)
8 (2 runs/test)
4 (1 per test)
2 (1 per test)
4 (1 per test)
8 (1 per test for
each stream)
Analysis0
• 02, CO2, CO, NO/NOX, SO2
• Particulate matter by gravimetry
• Trace metals by atomic absorption
• Volatile organics by GC/MS
• HCI by titration with silver nitrate
• C, H, N, O, S, and HHV by ASTM
methods
• Total chloride, ASTM P808
• Volatile organics by GC/MS
• Trace metals by atomic absorption
• Trace metals by atomic absorption
• C, H, N, 0, S and HHV by ASTM methods
No analysis performed
• Volatile organics by GC/MS
• Trace metals by atomic absorption
• Total chlorides, ASTM PS08
"Appendix A presents a detailed description of sampling equipment and protocols used.
bDoes not include blanks, spikes, or other quality control samples.
c Appendix B presents a detailed description of analytical equipment and protocols used.
Table 4. Summary of Criteria Emission Results
Test O2 CO2
Site condition (percent) (percent)
Rotary kiln Waste fuel 14.9-16.4 3.6-4.0
dryer— firing (15.9)b (3.1)
site 1
Aggregate Cofiring 5.0-11.0 6.0-13.1
kiln— (coal and (8.9) (8.8)
site II waste fuel)
Waste fuel 5.0-10.0 6.7-11.9
firing (7.6) (9.4)
CO SO2
(ppm)3 (ppm)
15-1 10 3-63
-------
drochloric acid emissions represent 25
to 30 percent of the total chlorine fired
with the waste fuel.
The kiln at site II was operated at sig-
nificantly lower excess air levels, aver-
aging about 80 percent for the cofired
tests and 50 percent for the waste-fuel-
only tests. Lower combustion air vol-
umes resulted in higher kiln process
temperatures and lead to higher NOX
emissions compared with site I. Sulfur
dioxide emissions were significant for
both cofiring and waste-fuel-only tests.
Total sulfur input (coal and waste fuel)
could not account for all the S02 meas-
ured. Sulfur-out divided by sulfur-in
ranged from 3.3 to 12. It is likely that the
aggregate contributed S02 to the flue
gas. Sulfur removal efficiencies of the
wet scrubber could not be calculated
because of lack of sulfur measurements
in the flue gas entering the scrubber or
the waste discharge stream from the
scrubber.
Particulate emissions were signifi-
cantly higher for site II by as much as
two orders of magnitude than for site I.
This result is attributed primarily to a
lower collection efficiency of the wet
scrubber compared to the fabric filter of
site I. Furthermore, higher participate
emissions for the cofired tests at site II
were the result of flyash contribution
from pulverized coal and scrubber
water entrainment detected during
tesfl.
Volatile Organic Emissions and
ORE
Figure 3 illustrates the volatile POHC
ORE results obtained at both sites. Each
bar is indicative of the range in ORE ob-
tained for the major volatile POHCs.
Bars with upper dashed lines corre-
spond to ORE results greater than the
indicated level.
DREs for site I POHCs failed to meet
the 99.99 percent level, the current regu-
latory level for hazardous waste inciner-
ators. Several of the components failed
to meet the 99.9 percent level as well.
The low DREs are attributable primarily
to the relatively low process tempera-
tures in the kiln. However, test results
also point out the likelihood that low
concentration POHCs would fail to
achieve high DREs, possibly because of
the sensitivity of state-of-the-art sam-
pling and analytical techniques in
measuring low concentration organics
as well as the susceptibility of back-
ground contamination of these results.
More importantly, the contribution of
99.999990 -
99.99990
99.9990
*
Q 39.990
99.90
99.0
90.0
Freon 113
MEK, PCE. TCE
and1,1.1-TCA
Chlorobenzene
Toluene
Benzene
—1TCE
Freon
113.
MEK,
1,1,1-TCA
Toluene
PCE
PCE.
TCE. and
Toluene
MEK. Freon
113, and
1.1.1-TCA
Chlorobenzene
Carbon
Tetrachloride
L Benzene
Chlorobenzene
Carbon
Tetrachloride
L Benzene
Site I
Site II (Cofire)
Site II (Waste Fuel Only)
Figure 3. Summary of site I and site II ORE results.
PIC formation to total POHC emissions
may play a greater role in determining
the ORE results of low-concentration
POHCs. DREs for the spiked Freon 113
were the highest of any of the volatile
organic compounds detected in the
waste fuel at site I, exceeding the 99.990
percent level on the average. The firing
rate or concentration in the waste fuel of
Freon 113 was the highest of any of the
other volatile POHCs.
Site II DRE results indicate destruction
efficiencies exceeding 99.99 percent for
most volatile POHCs except for ben-
zene, Chlorobenzene, and carbon tetra-
chloride (cofiring tests only). These high
DREs were obtained for both the cofir-
ing and waste-fuel-only test conditions
and are attributable to the high kiln
process temperatures compared to
site I. Low DREs were obtained for
volatile POHCs present in the fuel in the
lowest concentrations, generally less
than 150 ppm corresponding to firing
rates lower than 58 mg/s. Again, this re-
sult of lower DREs associated with low
POHC concentrations may indicate the
significance of background organic
emission levels in combustion prod-
ucts. DREs for Freon 113 at site II also
exceeded DREs for any of the other
POHCs.
Products of Incomplete
Combustion
Table 5 summarizes emission results
of volatile organics that were not de-
tected in the waste fuels of site I or site
II. These compounds are identified as
products of incomplete combustion
6
-------
Table S. Volatile PIC Emissions, \ig/s
Site I
Site II
Compound
Carbon tetrachloride
Chloromethane
Bromomethane
Vinylchloride
Dichloromethane
1, 1-dichloroethane
Chloroform
Chloroethane
1 ,2-dichloropropane
1, 1,2,2-tetrachloroethane
Waste fuel only
(tests 1, 2, and 3)
4.1 to 494
(173)*
Oto67
(30)
5.2-11
(8.0)
18 to 44
(28)
Oto72
(30)
Oto55
(18)
0 to 3.9
(2.5)
0 to 4.1
(1.4)
0 to 2.8
(0.9)
0 to 2.6
(0.9)
Cofiring
(tests 1 and 2)
NA
156 to 547
(350)
7.2 to 37
(22)
12 to 19
(16)
NA
—
2.5 to 8.6
(5.5)
—
NA
—
Waste fuel only
(tests 3 and 4)
NA
600 to 968
(780)
8. 1 to 8.9
(8.4)
13 to 14
(14)
NA
—
5. 1 to 6.4
(5.8)
—
NA
—
1,1-dichloroethylene
Trans- 1,2-dichloroethylene
1.9 to 4.0
(3.0)
0.5 to 1.4
(1.0)
2.0 to 2.8
(2.4)
1.0 to 1.1
(1.1)
Total PICs
PICsfZPOHCsb
51 to 670
(290)
0.14 to 0.30
(0.25)
190 to 610
(400)
0.64 to 0.91
(0.83)
630 to 1,000
(810)
0.72 to 0.83
(0.76)
aEach entry is the arithmetic average of the measurements for each test. Number in paren-
theses is the average for number of tests indicated.
bSum of PIC emissions divided by the sum of breakthrough volatile POHC emissions includ-
ing toluene and benzene.
—Dashes indicate emission level or blank corrected emissions were below detection limits.
NA—Not applicable. Compound was a POHC.
(PICs). For site I, highest PIC emissions
were contributed by carbon tetrachlo-
ride. These high average emissions are
attributed to test 1 results, which indi-
cate high carbon tetrachloride emis-
sions of about 500 |jig/s. DREs for test 1
were also lower than DREs measured
during the remaining two tests. Total
volatile PIC emissions accounted for
about 14 to 30 percent of the total POHC
breakthrough measured.
For site II, Chloromethane emissions
accounted for nearly all the PICs de-
tected with 570 >i,g/s on the average for
all tests. Higher Chloromethane emis-
sions were measured for the waste fuel
firing tests 3 and 4. The ratio of total
PICs to total POHC breakthrough ranged
from 0.76 to 0.83.
Trace Metal Emissions
Selected trace metals were sought in
the analysis of fuels and flue gas emis-
sions to quantitate the emissions of the
inorganics from the two process kilns
burning hazardous liquid wastes. Anal-
ysis of metals was generally limited to
the 13 EPA-designated priority pollutant
elements. Table 6 summarizes the re-
sults of these measurements.
For site I, copper, lead, and zinc con-
stituted the major metals, heaving con-
centrations of 400 to 700 ppm in the
waste fuel. Other detected metals were
cadmium, chromium, and nickel, all
having fuel concentrations of less than 5
ppm. Emissions ranged from nonde-
tected for cadmium to 130 ^g/s for zinc.
Lead emissions were found to be about
80 M-g/s on the average. Emissions of
these trace metals generally constituted
less than 1 percent of the total input
rate. This was found to be especially the
case for lead, copper, and zinc. It is likely
that most of these metals were ab-
sorbed on baghouse-collected flyash or
trapped in the clay product of the kiln.
Lead and zinc were the major metals
in the waste fuel at site II, with average
concentrations of 860 ppm and 210
ppm, respectively. Chromium also ex-
ceeded 100 ppm. During cofiring (tests 1
and 2), pulverized coal contributed a
minor fraction of these metals. Highest
emissions were measured for lead (7.6
mg/s), followed by chromium (1.5 mg/
s), and zinc (1.0 mg/s). On the average,
the measured emissions of all trace
metals accounted for 1.7 to 8.0 percent
of the total input rate.
Results of waste firing only, tests 3
and 4 for site II, indicate an increase in
lead emissions to 25 mg/s, followed by
zinc at 4.4 mg/s, and chromium at 1.3
mg/s. With the exception of mercury,
nickel, and antimony, which were not
detected, total metal emissions ac-
counted for 3.9 to 17 percent of the total
input rate on the average. Therefore, the
results obtained during this test pro-
gram indicate that, although the site II
kiln was more efficient in thermal de-
struction of organics, it had a higher
percentage of trace metals emissions.
This result is attributed to the higher
process temperatures, which may pre-
vent metal adsorption on the flue gas
entrained particulate matter combined
with the lower efficiency of the wet
scrubber in controlling particulate emis-
sions. The increase in lead and other
metal emissions during the waste-fuel-
only tests may be the result of reduced
entrained particulate/metal interaction.
Coal flyash generated during the cofired
tests may have contributed to metal ad-
sorption.
-------
Table 6. Trace Element Emissions
Site 1
Element3
Antimony
Cadmium
Chromium
Copper
Lead
Mercury
Nickel
Zinc
Waste
Flue gas
emissions
(W/s)
—
<5.S
10 to 29
(20)
12 to 92
(52)
66 to 96
(81)
—
5.0 to 35
(20)
59 to 130
(95)
fuel only
Mass balance
out/in
(percent)
—
<2.5
1.2 to 2.9
(2.1)
0.01 to 0.11
(0.05)
0.05 to 0.07
(0.06)
—
20 to 13
(7.5)
0.05 to 0.11
(0.08)
Cofiring
Flue gas
emissions
(\ig/s)
<5.7
100 to 174
(140)
1,290 to 1,740
(1,500)
260 to 430
(350)
6,300 to 8,850
(7,600)
<0.6
<14to 190
(<100)
690 to 1,310
(1,000)
Site II
Mass balance
out/in
(percent)
NA
6.4 to 9.5
(8.0)
5.7 to 5.8
(5.8)
1.4 to 2.0
(1.7)
3.6 to 5.4
(4.5)
NA
<1.1 to 11
«5.5)
1.5 to 3.2
(2.4)
Waste
Flue gas
emissions
(pg/s)
<5.8
440 to 450
(450)
1,1 70 to 1,400
(1,300)
1,020 to 1,120
(1,070)
25,000
<0.6
<14
4,290 to 4,570
(4,400)
fuel only
Mass balance
out/in
(percent)
<0.2S
16 to 18
(17)
3.2 to 4.8
(4.0)
3.5 to 4.3
(3.9)
9.4 to 9.9
(9.7)
<0.5
<1.8
5.3 to 5.9
(5.6)
s'Analysis was limited to priority pollutant elements. Metals listed are those that were detected in the fuels and flue gas emission stream.
bNumber in parentheses is the arithmetic average of three test measurements for site I and two test measurements for site II. Averages are
generally rounded to two significant figures.
—Dashes indicate element not detected in the fuels or flue gas at site I.
NA—Not available. Mass balance cannot be computed because of unknown element contribution from coal.
A. W. Wyss, C. Castaldini, and M. M. Murray are with Acurex Corporation,
Mountain View, CA 94039.
Robert E. Mournighan is the EPA Project Officer (see below).
The complete report, entitled "Field Evaluation of Resource Recovery of Hazardous
Wastes,"(Order No. PB 86-211 869/AS; Cost: $ 16.95, subject to change) will
be available only from:
National Technical Information Service
5285 Port Royal Road
Springfield, VA 22161
Telephone: 703-487-4650
The EPA Project Officer can be contacted at:
Hazardous Waste Engineering Research Laboratory
U.S. Environmental Protection Agency
Cincinnati, OH 45268
-------
United States
Environmental Protection
Agency
Center for Environmental Research
Information
Cincinnati OH 45268
Official Business
Penalty for Private Use $300
EPA/600/S2-86/059
------- |