EPA-600/2-77-042
January 1977
PARTICULATE CONTROL
MOBILE TEST UNITS:
SECOND YEAR'S OPERATION
by
D.L. Zanders
Monsanto Research Corporation
1515 Nicholas Road
Dayton, Ohio 45407
Contract No. 68-02-1816
ROAP No. 21ADM-034
Program Element No. 1AB012
EPA Project Officer: Dale L. Harmon
Industrial Environmental Research Laboratory
Office of Energy, Minerals, and Industry
Research Triangle Park, NC 27711
Prepared for
U.S. ENVIRONMENTAL PROTECTION AGENCY
Office of Research and Development
Washington, DC 20460
::,L PROTECTION
'
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ABSTRACT
This report summarizes the second year of operation for EPA-owned
mobile test units. Due to the recent contractual acquisition of
a mobile unit designed for energy R&D work, usage divides into
two principal areas.
Three units (baghouse, wet scrubber, and electrostatic precipita-
tor) are designed to be used in the field to study the applica-
bility of different methods for controlling fine particulate emit-
ted from a wide variety of sources. A fourth unit (energy van)
is designed to demonstrate the feasibility of unconventional
energy supply systems to support residential and commercial
buildings.
Three units are described herein: (1) fabric filter (baghouse),
(2) wet scrubber, and (3) energy van. The fourth unit (electro-
static precipitator) is still under construction.
Results from baghouse tests on a kraft mill lime recovery kiln
indicate an overall, integrated collection efficiency of
99.98+ wt %. On the basis of collection efficiency alone, a high
level of control can be afforded by a baghouse on lime kiln par-
ticulate emissions. However, on the basis of projected operating
problems due to high moisture content of the gas, baghouse con-
trol of a lime recovery kiln is not recommended.
Baghouse control of a black liquor recovery boiler would also be
discouraged on the basis of high moisture content in the gas,
although no collection efficiency data were obtained for such
control.
Operation of the mobile scrubber unit during the year was con-
fined to startup field testing and correction of mechanical and
operating difficulties.
The energy van, a newly acquired mobile unit, has not undergone
testing to date.
111
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CONTENTS
Abstract iii
Figures vi
Tables vi
Acknowledgements vii
1 Introduction and Objectives 1
2 Conclusions 3
3 Review of Operations 4
3.1 Baghouse Unit 4
3.1.1 Background 4
3.1.2 Plymouth, N.C. Testing 5
3.1.3 Baghouse Repackaging and Upgrading 22
3.2 Mobile Scrubber Unit 22
3.2.1 Background 22
3.2.2 Events of Second Year 24
3.3 Mobile Energy Van 24
References 31
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FIGURES
Number Page
1 Schematic of kraft pulping process flow 6
2 Relative position of baghouse to lime kiln 7
3 Relative position of baghouse to recovery boiler 9
4 Current baghouse enclosure 23
5 End view - baghouse 23
6 External view of mobile scrubber unit 25
7 Mobile scrubber unit process area 26
8 Sieve tray column 27
9 Scrubber flow schematic 28
10 Energy van - side view 29
11 Energy van - interior living area 29
12 Energy van - fuel delivery system 29
TABLES
1 Gas and Flue Characteristics at Lime Kiln 7
2 Gas and Breaching Characteristics at Recovery
Boiler 8
3 Composition of Flyash from Boiler No. 3 9
4 Original Plymouth Test Plan 10
5 Bag Characteristics " 11
6 Actual Run Conditions 12
7 Impactor Mass Resultants 16
8 Size and Fractional Efficiency Results 17
9 Pressure Drop Results 18
VI
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ACKNOWLEDGMENTS
The unstinting cooperation and aid given the field test crew by
the management and technical operating personnel at the Weyerhauser
Corporation, Plymouth, North Carolina, pulp mill are acknowledged
with sincere thanks.
The Project Officer, Mr. Dale L. Harmon, provided valuble assis-
tance in negotiating entrance to the test site and helpful sug-
gestions throughout the entire program.
viz
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SECTION 1
INTRODUCTION AND OBJECTIVES
The purpose of EPA Contract No. 68-02-1816 is to provide the oper-
ational effort required to obtain field laboratory and pilot
plant test data from EPA-owned equipment and systems. Contract
operations are currently divided into four areas:
MOBILE TEST UNITS
The mobile test units consist of truck-mounted items of
conventional dust collection equipment: fabric filter
(baghouse), venturi scrubber, sieve tray scrubber, and
electrostatis precipitator (not yet operational). The
main objective is to assess the ease/difficulty associ-
ated with this type of equipment in controlling partic-
ulate-laden gas streams of varying characteristics
obtained at different types of emission sources in the
field.
AERODYNAMIC TEST CHAMBER
This wind-tunnel-like chamber provides for gas movement
in a wide range of velocities at temperatures from ambi-
ent to above 149°C (300°F) and accommodates a broad
spectrum of gas composition and particulate loading.
The objectives for its use are calibration and testing
of fine particulate measurement equipment. It is also
being used as a source of test dust for the mobile
field units.
PILOT SO SCRUBBER
J\.
This unit consists of twin 23-cm (9-inch) diameter
scrubbers and associated systems capable of several
types of scrubbing modes operating in parallel or
series. The objective of their operation is to deter-
mine quick, easy, inexpensive solutions to operating
and technical problems encountered in the development
of full-size SO scrubbing systems.
X
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ENERGY VAN
The EPA energy van is a towable mobile home containing
an energy supply system that utilizes environmentally
clean and energy-conserving components. These compo-
nents include fuel cells, a solar energy collector, a
heat pump, and catalytic appliances. The objective of
the mobile system is to develop and demonstrate an
energy supply system for residential and commercial
buildings which could cut pollution and energy consump-
tion by as much as 50%.
The aerodynamic test chamber and pilot scrubber system are semi-
permanent installations at the Environmental Research Center
(ERG) in Research Triangle Park, North Carolina. Although the
truck-mounted units use this location as a service base, the
majority of their operating time is spent in the field at various
plant sites throughout the country. The energy van has been
temporarily located at ERG for a performance testing period of
approximately 1 year.
The four operational areas represent, to varying degrees, differ-
ent program interests and different groups or sections within
the Industrial Environmental Research Laboratory. The contractor's
objective is to fulfill the needs of each interest within the con-
tract scope. Thus, the level of involvement varies in each oper-
ational area. For example, in the areas of the aerodynamic test
chamber and pilot SOX scrubbers, the activities of program and
test planning and interpretation of results are mainly conducted
by EPA personnel. The contractor schedules and executes the
test plans under specified conditions, and collects and reduces
data to usable form. The nature of the current program, expe-
cially for the pilot SOX scrubber project, dictates this type of
relationship. In the mobile test unit area, however, the con-
tractor is also largely responsible for developing the test plans
and interpreting the results obtained.
This report primarily summarizes operation of and experience with
the mobile baghouse and scrubber units during the second contract
year.
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SECTION 2
CONCLUSIONS
During the one completed mobile unit field test (baghouse opera-
ting on effluent from a kraft mill lime recovery kiln), all clean-
ing mode/bag type combinations performed at maximum collection
efficiency, both integrated mass and fractional, within the test
regimen.
Overall, integrated collection efficiency was 99.98+%. Overall
averages of mean fractional efficiencies by size range were as
follows:
Size, pm Efficiency, %
1-3 99.815
4-6 99.814
7-10 99.918
On the basis of collection efficiency alone, a high level of
control of lime recovery kiln emissions can be afforded by a
baghouse.
On the basis of bag differential pressure at comparable operating
conditions, shake cleaning was significantly more efficient than
reverse flow cleaning.
On the basis of projected operating problems due to high moisture
content in the gas, baghouse control of a lime recovery kiln is
not recommended.
Although no collection efficiency data were obtained for it, bag-
house control of a black liquor recovery boiler would also be
discouraged on the basis of high moisture content in the gas.
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SECTION 3
REVIEW OF OPERATIONS
3.1 BAGHOUSE UNIT
3.1.1 Background
The mobile fabric filter system (baghouse unit) was designed and
fabricated by GCA/Technology Division, Bedford, Massachusetts.
The unit was mounted on a 1.36-metric-ton (1-1/2-ton) truck and
is described at length in GCA reports.1'2 Briefly, it has the
following capabilities:
• Filtration can be conducted at cloth velocities as
high as 0.102 m/s (20 fpm) with a pressure differen-
tial up to 4.98 kPa (20 in. water) and at a gas
temperature up to 288°C (550°F).
• The mobile system is adaptable to cleaning by
mechanical shaking, pulse jet, or low pressure
reverse flow, with cleaning parameters which vary
over broad ranges.
• The system can be operated in a series filtration
mode.
• One to seven filter bags of any medium, 1.22 m to
3.05 m (4 ft to 10 ft) long and up to 0.3 m (12 in.)
in diameter, can be used.
• Automatic instruments and controls enable 24-hour
operation of the system.
After brief field tests, the unit was delivered to present con-
tractor personnel for use in a field testing program for the In-
dustrial Environmental Research Laboratory of EPA.
1Hall, R. Mobile Fabric Filter System - Design Report. GCA/Tech-
nology Division. Contract No. 68-02-1075. October 1974.
2Hall, R. Mobile Fabric Filter System - Final Report. GCA/Tech-
nology Division. Contract No. 68-02-1075. May 1975.
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For several reasons, the baghouse unit, as received, required
preliminary "dry run" testing at the RTF Environmental Research
Center, and intensive shakedown tests in the field under severe
conditions. The dry run tests at RTF were directed at operational
checks of system components and training of new operators.
The unit was then given shakedown tests in the field on a pulp mill
lime recovery kiln. After a brief return to RTF for refurbishing,
the unit was taken to Sunbury, Pennsylvania for tests on Pennsyl-
vania Power and Light Company's Shamokin Dam, coal-fired generating
station on 16 December 1974. These tests lasted through 26 Febru-
ary 1975.
On completion of these tests, about 2 months were required to re-
furbish the unit and sample trains, after which the unit was placed
at a lime recovery kiln at Weyerhauser Corporation's pulp mill in
Plymouth, North Carolina from 21 April 1975 to 19 September 1975.
Results of that test are summarized below.
3.1.2 Plymouth, N.C. Testing
Two test sites at the Weyerhauser pulp mill were initially con-
sidered: (1) exhaust duct of the lime recovery kiln, and (2)
exhaust duct of the black liquor recovery boiler. Difficulties
encountered throughout the program limited the test to the lime
kiln only.
3.1.2.1 Test Site Description—
Figure 1 shows, in general, typical kraft pulping process flow,
wherein the major sources of particulate emission are seen to be
the recovery boiler and lime kiln.
3.1.2.1.1 Lime kiln—At the Plymouth mill the lime recovery area
included three rotary calciners essentially identical in all re-
spects with rated capacity of 109 metric tons (120 tons) per day
lime. Testing was conducted at No. 3 kiln solely because of
accessibility. Effluent for testing was taken from the hood on
the exhaust end of the kiln through a 63.5-mm (2-1/2-in.) diameter
curved probe that extended into the gas stream 0.61 m (24 in.).
The open end of the probe faced the oncoming gas. The slipstream
so obtained was conducted to the baghouse through approximately
16.8 m (55 ft) of insulated, 63.5-mm diameter pipe. Characteris-
tics of the slipstream duct were as follows:
I.D. - 61.7 mm (2.43 in.)
Area - 0.00287 m2 (0.0309 ft2)
Length - 16.8 m (55 ft)
Test flow range - 3.68 x 10~2 to 6.18 x 10~2 m3/s (78 to 131 acfm)
Test flow velocity - 12.8 to 21.3 m/s (42 to 70 fps)
Test pressure drop - 0.5 to 1.2 kPa (2 to 5 in. w.c.)
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Characteristics of the exhaust gas and flue at the slipstream port
are shown in Table 1. Figure 2 indicates relative equipment posi-
tions at the site.
TABLE 1. GAS AND FLUE CHARACTERISTICS AT LIME KILN
Gas composition, wet basis
02
CO 2
H2O
N2
Mol. wt. - wet basis
dry basis
Grain loading
Temperature
Dew point
Static pressure
Density - wet (0°C)
(299°C)
dry (0°C)
(299°C)
Hood section
(perpendicular to flow)
Superficial gas velocity
Flow
- 7.1%
- 15.4%
- 25.0%
- 52.5%
- 28.25
- 31.66
-7.25 g/m3 (3.17 avg., gr/dscf)
- 260°C-299°C (500°F-570°F)
- 65.6°C (150°F)
- 0.075 kPa (0.30 in. w.c.)
- 1.26 kg/m3 (0.0788 lb/ft3)
- 0.60 kg/m3 (0.0376 lb/ft3)
- 1.46 kg/m3 (0.0909 lb/ft3)
- 0.70 kg/m3 (0.0434 lb/ft3)
- 2.37 m2 (25.5 ft2)
-6.4 m/s (21 ft/s)
- 15.2 m3/s (32,160 acfm)
TO VENTURI SCRUBBER
-6.1m (20 ft
MOBILE
BAGHOUSE
6.1m (20ft)
u-=
V
4.6m (15ft)
Figure 2. Relative position of baghouse to lime kiln,
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It is not surprising that there was no indication of free sulfur
dioxide in the presence of such high loading of lime dust. Sul-
fur present in the kiln feed either carried over as undecomposed
calcium salt (CaS03 and/or CaSOiJ or formed through combination,
or recombination, in the gas stream leaving the kiln. Aqueous
solution (slurry) of the exhaust solids showed pH in the range
of 10.0 to 12.0.
3.1.2.1.2 Recovery boiler—Of the two boilers accessible for test-
ing (Nos. 3 and 4), No. 3 was selected because of greater accessi-
bility. Nominally, operation of both boilers was the same. This
subsequently proved untrue, and an unsuccessful attempt was made
to test No. 4 boiler. In either case, entry to the breaching was
by a 63.5-mm (2-1/2-in.) diameter probe extending 0.61 m (24 in.)
into the gas stream. The entry port was located approximately
midway between the cascade evaporators and electrostatic precipi-
tator (refer to Figure 1). Gas for test purposes was taken to the
baghouse through 41.1 m (135 ft) of 63.5-mm diameter insulated
ducting. Characteristics of the slipstream duct were as follows:
I.D. - 61.7 mm (2.43 in.)
Area - 0.00287 m2 (0.0309 ft2)
Length - 41.1 m (135 ft)
Test flow range - 3.68 x 10~2 to 6.18 x 10~2 m3/s (78 to 131 acfm)
Test flow velocity - 12.8 to 21.3 m/s (42 to 70 fps)
Test pressure drop - 0.5 to 1.2 kPa (2 to 5 in. w.c.)
Characteristics of the exhaust gas and breaching at the slipstream
port are shown in Table 2. Figure 3 shows relative equipment
positions at the site.
TABLE 2. GAS AND BREACHING CHARACTERISTICS AT RECOVERY BOILER
Gas composition, wet basis
02 -
C02 -
H20 -
N2 -
Mol. wt. - wet basis -
dry basis -
Grain loading -
Temperature -
Dew point -
Static pressure -
Density - wet (0°C) -
(299°C) -
dry (0°C) -
(299°C) -
Breach section -
Superficial gas velocity -
Flow -
9.5%
10.6%
24.0%
55.9%
27.67
30.74
7.5 g/m3 (3.3 avg., gr/dscf)
177°C (350°F)
64°C (148°F)
#3 boiler - 0.6 kPa (-2.5 in,
#4 boiler - 1.4 kPa (-5.5 in,
1.23 kg/m3 (0.0771 lb/ft3)
0.67 kg/m3 (0.0417 lb/ft3)
1.37 kg/m3 (0.0856 lb/ft3)
0.74 kg/m3 (0.0463 lb/ft3)
4.16 m2 (44.8 ft2)
7.8 m/s (25.6 fps)
32.48 m3/s (68,813 acfm)
w.c.)
w.c.)
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TO
ELECTROSTATIC
PRECIPITATOR
Figure 3. Relative position of baghouse to recovery boiler.
Again, there was no indication of free sulfur dioxide in the flue
gas. Inorganic salts in black liquor are mainly those of sodium.
Table 3 shows analysis of the solids emitted from the recovery
boiler. Allowing for some error in analysis, results indicate
the solids are about 17% Na2S03, 45% Na2SO4, 40% Na2C03, and
2-3% NaOH. Solution of the solids showed pH 10.6.
TABLE 3. COMPOSITION OF FLYASH FROM BOILER NO. 3
Na2SO3, mg/g
Na2SOt|, mg/g
NaOH, mg/g
Na2C03, mg/g
pH
Moisture, %
Moisture, 24-hr regain, %
173
455
35
420
10.6
5
1.5
3.1.2.2 Equipment Operating Cycles--
Pulping operations, especially of the magnitude at Weyerhauser's
Plymouth Mill, normally are stable, steady-state processes. As
noted in Figure 1, surge capacity is provided throughout the
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system. These chests and tanks are maintained at levels that will
permit a period of continued operation on either of their sides in
the event of equipment outage. Nominally, this surge capacity is
adequate for the time required to get equipment back on line.
Aside from process upsets caused by equipment malfunction, the
only "short" term cycles in the overall system occur at the diges-
ter end of the process where digesters are blown in a cyclic manner,
Consequently, the lime kilns, in particular, operate in a very
stable mode, unless outage occurs at the kiln itself. In the
present case, plant operating personnel assured steady-state oper-
ation at the test kiln by accommodating rate changes on the two
remaining kilns. So far as could be determined, the test kiln ran
steadily at capacity throughout testing, although the tests had
to be interrupted on two occasions because of kiln outage.
While similar stable operation was expected at the black liquor
recovery boilers, such was not the case. At the boiler selected
for testing, erratic operation derived from frequent, unpredictable
outages caused by malfunctioning of electrostatic precipitators
and induced draft fans. At the alternate boiler, No. 4, erratic
operation was due either to poor control of combustion air rates
or unstable operation of the cascade evaporator set. The result
was a heavy concentration of small beads of tarry black liquor
taken into the slipstream to the baghouse. This combination of
atypical performances contributed in large measure to the frus-
tration of testing at the recovery boilers.
3.1.2.3 Test Plan—
The Plymouth testing scheme is shown in Table 4. Bag fabrics
selected were woven and felted Nomex, which are described in
Table 5. For each set of test parameters, new bags were installed
and conditioned for 24 hours at an air-to-cloth (A/C) ratio of
1.5 x 10~2 m/s (3 fpm).
TABLE 4. ORIGINAL PLYMOUTH TEST PLAN3
(Lime kiln recovery boiler, Weyerhauser Corporation)
Cleaning
mode
Shake
Reverse
A/C ratio, m/s
Low High
0.01(0.015)
0.01(0.015)
0.03 (0.025)
0.01(0.015)
0.01(0.015)
0.01(0.015)
0.03 (0.025)
Filtration
period, min
Low High
30
50
30
30
50
30
30
Cleaning
period, s
Low High
5
5
5
5(20)
5(40)
20(40)
5
Woven and felted Nomex both tested at each condition shown.
10
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TABLE 5. BAG CHARACTERISTICS3
MATERIALS
Fabric
Nomex-woven
Nomex-f elt
Count
W F
98 x 99
Weave
3x1 twill
needled
Weight,
oz/yd2
4.5
14
Permeability,
cfm/ft @ 2 in.
18
40
r
H2O
CONSTRUCTION
Cleaning Diameter, Length,
mode in. in. Other
Shake 5 9/16 72 2-in. cuff and bolt rope one
end, loop one end
Reverse 5 9/16 72 2-in. cuff and bolt rope one
end, loop one end; three
spreader rings: middle and
one each 18 in. from top and
bottom
All bags were manufactured by Globe Albany Corporation, Buffalo,
New York. The materials specifications shown are theirs.
The test scheme has two restraints. First, maximum pressure drop
across the bags is limited to 2.5 kPa (10 in. w.c.) by instrument
range. Second, flow through the unit must be high enough to main-
tain the gas above its dew point. In Table 4, figures in paren-
theses in the A/C columns are values resulting from these restraints.
With felted Nomex bags in reverse mode, the only viable A/C value
was 1.5 x 10~2 m/s. In the cleaning period columns, parenthetical
figures are values associated only with felted Nomex bags. Other
baghouse parameters employed during the tests are shown in Table 6.
The test plan further considered use of mass efficiency at each
set of conditions as a quick screening device, since experience
at Sunbury showed such sampling could be done in a matter of min-
utes. After review of such mass efficiency results, the condition(s)
showing best efficiency would then be reimposed and sampled for
size distribution. The intent was to limit the time-consuming
operation of size distribution sampling. However, filtration
efficiency at Plymouth was so great that a period of hours was
required to collect sufficient samples for reliable measurement.
The mass efficiency screening approach has another time-consuming
aspect; namely, the baghouse must be rearranged back to a pre-
ceding configuration, and bags must be reinstalled and conditioned.
Consequently, mass sampling was abandoned and replaced by impactor
sampling at all test conditions.
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TABLE 6. ACTUAL RUN CONDITIONS
Shake mode
Filtration period
First pause
Cleaning period
Second pause
Shake frequency
Amplitude
Shaker-arm acceleration
Bag tension
A/C
30
30
5
30
7
22
43
, 50 min
s
s
s
cps
,2 mm (0.875 in.)
,1 m/s2 (4.4 g's)
0.68 kg (1.5 Ib)
0.015, 0.025 m/s
(3, 5 fpm)
Reverse mode
Filtration period
First pause
Cleaning period
Second pause
Bag tension
A/C
R.F. air temperature
R.F. air flow
30, 50 min
30 s
5, 20, 40 s
30 s
0.68 kg (1.5 Ib)
0.015, 0.025 m/s (3, 5 fpm)
113°C (235°F)
4.5 x 10~2 m3/s (95 acfm)
In subsequent data tabulation, test conditions are coded as fol-
lows (some nonmetric units were used in original data tabulation
and these are included below):
Cleaning mode: Shake - S
Reverse - R
Bag fabric:
Woven Nomex - WN
Felted Nomex - FN
Example: S-WN-3-30-5
First letter - cleaning mode
Second set of letters - bag fabric
First number - A/C, fpm
Second number - filtration period, min
Third number - cleaning period, s
3.1.2.4 Sampling Procedures—
For test purposes,Brink® impactors were used for inlet gas samp-
ling, and Andersen impactors for outlet gas sampling.
Static and velocity pressure measurements for determining gas
velocities in inlet and outlet ducts were made with a standard
pitot tube. The sampling duct was 63.5 mm (2.5 in.) in diameter,
and measurements were made at the average velocity point. EPA
Method 4 and Orsat analysis were used for determining gas compo-
sition and gas density calculations.
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3.1.2.4.1 Sampling duration—The lengths of sampling periods were
regulated by mass concentration in the gas, size distribution, and
flow rate through the impactor. Sample periods were first estima-
ted from nominal time, grain loading, and flow rate graphs, and
then adjusted so that a maximum of 10 mg of dust was deposited on
any one stage.
3.1.2.4.2 Impactor preparation—After assembly, impactors were
leak tested at 50.7 kPa (15 in. Hg) and wrapped with heating tape
covered with insulation. A thermocouple was inserted between the
heating tape and impactor body to indicate impactor surface tem-
perature. Warmup periods lasted 30 min for the Brink impactor
and 20 to 30 min for the Andersen impactor. Temperature controllers
maintained and indicated impactor temperatures.
3.1.2.4.3 Sampling operation—Each complete sampling train was
leak tested at 50.7 kPa (15 in. Hg) before start of sampling.
After sufficient warmup, the appropriate probe was inserted into
the duct and connected to the impactor, and sampling was begun.
With the Andersen impactor, insertion and removal of the probe
was accomplished while the baghouse was in the bypass condition.
This practice had two advantages: (1) elimination of unwanted
collection of dust in the probe (or impactor) before and after
the sampling period, and (2) provision for incremental cycle
sampling. The latter ensured representative dust loading by
negating the substantial change in effluent concentration with
respect to elapsed time from the start of the filtering cycle.
Brink impactor—A sixth stage was added to extend collection
capability to a smaller size range. The external precollector
cyclone formerly used was replaced by a cyclone integral with the
impactor body. This effectively eliminated line losses between
the external cyclone and the impactor, and simplified preparation
and disassembly of the device.
While probe losses are inherent in extractive sampling techniques,
their extent was reduced by selection of the largest probe size
compatible with isokinetic sampling. Probe losses were typically
about 10%, with occasional values up to 50%.
Andersen impactor—In view of difficulties previously en-
countered wherein the fiber glass substrates suffered significant
weight gain through reaction with S02 in the stack gas, Andersen
substrates were preconditioned for 24 hours in filtered stack gas
from the lime kiln. No measurable weight gain was observed from
preconditioning. In retrospect, this is logical since it was
subsequently shown that SO2 is not present in the lime kiln
effluent gas.
13
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In this testing episode, Andersen backup filters were employed to
extend the collection capability to a smaller size range than was
permitted during tests at Sunbury.
The sampling period had to be extended to 8 hours in order to ob-
tain measurable amounts of dust on the substrates. Though measur-
able, such weight gain was typically less than 2 mg/stage.
The high moisture content of the kiln gas dictated addition of a
condenser just before the drying columns in the sample train. The
protracted sampling period required frequent drainage of the con-
denser and replacement of the drying columns, which was performed
during the bag cleaning period when the sample train was inactive.
3.1.2.5 Data Reduction Procedures—
The processing of raw data to reported results was accomplished
by computer through a program modified to include virtually all
calculations formerly executed manually.
Impactor sample data input to the computer was unchanged and con-
sisted of:
• Weight gain per stage, mg
• Sample period, min
• Particle density, g/cc
• Gas temperature, °F
• Barometric pressure, in. Hg
• Impactor pressure drop, in. Hg
• Impactor flow rate, cfm
• Upper size estimate, ym
• Flue gas composition, component fraction
Output from the modified program consisted of:
• Total grain loading, gr/acf and gr/sdcf
• D50 size per stage, ym
• Mass per stage, g (also an input)
• Cumulative gr/acf by stages
• Cumulative mass by stages, g
• Percent cumulative mass by stages
• Grain loading per stage, gr/sdcf
• dM/dlogD
• Particle geometric mean diameter per stage
*• Plot of cumulative distribution
*• Tabulation of fractional efficiency and
penetration
*• Plot of fractional efficiency
The output items noted by asterisk are former manual operations.
The major work-saving step in the program is that which provides
the tabulation, at preselected particle size, e.g., 1, 2, 3, etc.
14
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and the plot of fractional efficiency. Previously, dM/dlogD
vs. GMD size was plotted manually for each inlet and outlet sample,
and fractional efficiency at 1, 2, 3, etc. ym was calculated man-
ually and plotted for each test run. These operations are now
performed by the computer.
Not addressed before is the fact that particle size reported re-
lates to "aerodynamic diameter." This represents the diameter of
a sphere of unit density (1.0 g/cc) attaining, at low Reynolds
numbers, the same final settling velocity as the real particle.
The rationale for selection of aerodynamic diameter stems from
the desire to normalize, or standardize, particle size indepen-
dent of real particle density and thus facilitate comparison of
fractional efficiencies between different types of sources where-
in real particle densities vary significantly. The major differ-
ence in use of unit compared to actual density is a shift of
particle size related curves toward the lower end of the size range.
3.1.2.6 Results and Discussion—
Table 7 shows grain loading in the gas entering and leaving the
baghouse, and collection efficiency and penetration values for
each set of test conditions. The test sets fall into four major
groups by cleaning mode and bag type:
• Shake/woven Nomex
• Shake/felted Nomex
• Reverse/woven Nomex
• Reverse/felted Nomex
Cursory inspection of Table 7 suggests essentially equal perfor-
mance in the four combinations. This is generally supported by
the values of the average mean penetration, except in the case of
shake/felted Nomex. Inspection of test data for this case reveals
that at one test condition (S-FN-3-50-5), inlet grain loading was
abnormally low, differing from the mean by a factor of about 15.
At another test condition (S-FN-5-30-5), grain loading in was in-
consistent between the duplicate samples. Thus, it is not clear
whether the apparent discrepancy in the average mean penetration
value for the shake/felted Nomex combination is due to inconsis-
tent test conditions or is a real function of this particular
combination. More credence is allotted the former possibility,
and the tendency is to remain with the statement that collection
efficiency overall was insensitive to changes in the test con-
ditions imposed. This observation of insensitivity within the
test regimen suggests that collection performance is at, or
approaching, a maximum value.
The suggestion gains support on examination of fractional effi-
ciency results in Table 8. These results do indicate that
fractional collection efficiency is size dependent, but penetra-
tion is less than 1% for (aerodynamic) diameters of 1 pm to 10 ym
almost without exception. Consequently, it appears that, at all
15
-------
TABLE 7. IMPACTOR MASS RESULTS
Run
S-WN-3-30-5
S-WN-3-50-5
S-WN-5-30-5
Average
S-FN-3-30-5
S-FN-3-50-5
S-FN-5-30-5
Average
R-WN-3-30-5
R-WN-3-30-20
R-WN-5-30-5
R-WN-3-50-5
Average
R-FN-3-30-20
R-FN-3-50-40
R-FN-3-30-40
Average
Grain loading
In
8.65(3.78)
8.65(3.78)
7.83(3.42)
2.79(1.22)
2.33(1.02)
4.39(1.92)
5.77(2.52)
6.86(3.00)
6.86(3.00)
0.597(0.261)
0.309(0.135)
4.35(1.90)
8.21(3.59)
4.53(1.98)
11.2(4.91)
8.58(3.75)
6.80(2.97)
5.95(2.60)
24.9(10.9)
5.84(2.55)
5.88(2.57)
5.95(2.60)
9.40(4.11)
8.56(3.74)
4.97(2.17)
6.80(2.97)
9.15(4.00)
13.9(6.08)
7.94(3.47)
8.56(3.74)
, g/m3 (gr/sdcf)
Out
0.00291(0.00127)
0.00318(0.00139)
0.000191(0.0000835)
0.000149(0.0000649)
0.000359(0.000157)
0.00130(0.000569)
0.00135(0.000589)
0.000613(0.000268)
0.000897(0.000392)
0.000831(0.000363)
0.000570(0.000249)
0.00220(0.000963)
0.00563(0.00246)
0.00179(0.000783)
0.00102(0.000444)
0.00281(0.00123)
0.00110(0.000482)
0.00105(0.000459)
0.00118(0.000516)
0.00113(0.000492)
0.000755(0.000330)
0.00146(0.000638)
0.00131(0.000574)
0.000931(0.000407)
0.00112(0.000490)
0.000490(0.000214)
0.00166(0.000726)
0.00166(0.000726)
0.00180(0.000788)
0.00128(0.000559)
Collection
efficiency,
%
99.97
99.96
99.99
99.99
99.98
99.97
99.98
99.99
99.99
99.86
99.82
99.95
99.93
99.96
99.99
99.97
99.98
99.98
99.99
99.98
99.98
99.97
99.99
99.99
99.98
99.99
99.98
99.99
99.98
99.99
Penetration ,
%
0.0336
0.0368
0.00244
0.00532
0.0154
0.0300
0.0233
0.00893
0.0130
0.139
0.184
0.0507
0.0685
0.0395
0.00904
0.0328
0.0162
0.0176
0.00471
0.0193
0.0128
0.0245
0.0140
0.0109
0.0226
0.00721
0.0182
0.0119
0.0227
0.0149
16
-------
TABLE 8. SIZE AND FRACTIONAL EFFICIENCY RESULTS
Mass median
diameter, ym
Run
S-WN-3-30-5
S-WN-3-50-5
S-WN-5-30-5
S-FN-3-30-5
S-FN-3-50-5
S-FN-5-30-5
R-WN-3-30-5
R-WN-3-30-20
R-WN-3-50-5
R-WN-5-30-5
R-FN-3-30-20
R-FN-3-30-40
R-FN-3-50-40
R-FN-3-50-40
In
7.7
7.7
7.5
7.4
7.4
8.3
7.7
7.6
0.4
1.2
8.2
8.2
7.8
7.8
7.6
7.5
7.3
7.2
8.4
8.2
7.8
7.6
7.7
7.6
8.0
8.0
Out
3.6
1.1
0.46
0.45
0.5
0.7
0.5
0.5
2.8
0.6
10.0
5.7
4.5
3.2
3.8
4.7
7.1
5.9
7.0
9.6
4.8
4.9
2.3
3.5
3.2
1.9
Fractional efficiency
Min
99.61
99.28
a
~a
a
~a
99.89
99.51
99.80
99.21
99.84
99.20
99.87
99.08
99.89
99.92
99.97
99.97
99.67
_a
99.97
99.85
99.80
97.15
99.95
97.90
Max.
@3
03
@1
@1
?6
@4
@6
§3
@3
@4
@4
@3
@4
@5
@5
@4
@4
@3
@4
@7
@4
99.99
99.99
a
a
a
~a
99.99
99.99
99.86
99.99
99.99
99.95
99.99
99.98
99.99
99.99
99.99
99.98
99.96
_a
99.99
99.99
99.99
99.99
99.99
99.99
(?10
@10
@10
@ 8
@10
@ 8
100%.
17
-------
conditions tested, collection performance was equivalent and maxi-
mum, and it thus does not provide a basis for ranking the four
combinations of cleaning mode and bag type.
In the present test series a considerable amount of bag pressure
drop (dp) data was obtained, summarized as average values in
Table 9. The results show marked differences in bag dp both within
and between mode/bag groups. The variation within groups is in
the direction expected in response to changing test conditions.
A comparison of results between cleaning modes clearly shows shake
mode operating at significantly lower dp. In other words, shake
appears to provide considerably more efficient cleaning than re-
verse flow.
TABLE 9. PRESSURE DROP RESULTS
Run
AP
AP
K
S-WN-3-30-5
S-WN-3-50-5
S-WN-5-30-5
S-FN-3-30-5
S-FN-3-50-5
S-FN-5-30-5
R-WN-3-30-5
R-WN-3-30-20
R-WN-3-50-5
R-WN-5-30-5
R-FN-3-30-20
R-FN-3-30-40
R-FN-3-50-40
0.60(2.4)
0.52(2.1)
1.44(5.8)
0.17(0.7)
0.32(1.3)
0.67(2.7)
0.65(2.6)
0.90(3.6)
0.85(3.4)
1.84(7.4)
1.54(6.2)
1.94(7.8)
1.97(7.9)
1.00(4.0)
0.95(3.8)
1.94(7.8)
0.40(1.6)
0.70(2.8)
1.29(5.2)
1.17(4.7)
1.19(4.8)
1.37(5.5)
2.44(9.8)
2.07(8.3)
2.31(9.3)
2.44(9.8)
40.2(0.82)
34.8(0.71)
56.8(1.16)
11.3(0.23)
21.1(0.43)
26.9(0.55)
42.1(0.86)
58.8(1.20)
55.4(1.13)
72.5(1.48)
99.4(2.03)
128.4(2.62)
129.3(2.64)
65.1(1.33)
61.7(1.26)
75.9(1.55)
26.0(0.53)
45.6(0.93)
50.9(1.04)
76.4(1.56)
78.4(1.60)
89.6(1.83)
96.0(1.96)
135.2(2.76)
153.8(3.14)
159.2(3.25)
39,400(33.9)
25,100(21.6)
18,300(15.7)
29,400(25.3)
29,400(25.3)
28,700(24.7)
32,900(28.3)
18,700(16.1)
19,800(17.0)
13,700(11.8)
35,100(30.2)
25,100(21.6)
19,100(16.4)
Where AP = Effective pressure drop, kPa (in. w.c.)
AP = Residual pressure drop, kPa (in. w.c.)
S = Effective drag = AP /U, kPa/m/s (in. w.c./fpm)
S = Residual drag = AP /U, kPa/m/s (in. w.c./fpm)
K = Cake specific resistance, kPa/m/s • kg • m2 (in. w.c./fpm-lb-ft2)
For comparable filtration velocities and periods, the four mode/
bag groups can be ranked in order of ascending residual pressure
drop (AP ) as follows:
3-30
3-50
5-30
S-FN 0.40(1.6)
S-WN 1.00(4.0)
R-WN 1.19(4.8)
R-FN 2.07(8.3)
0.70 (2.8)
0.95(3.8)
1.37 (5.5)
2.44 (9.8)
1.29(5.2)
1.94 (7.8)
2.44 (9.8)
18
-------
In comparing bag types in the above ranking, as well as in Table 9,
the following paradox appears. In reverse mode, felted Nomex
operates at higher dp than woven Nomex. This might be expected
since reverse cleaning is relatively inefficient and felted ma-
terial is difficult to clean compared to woven material. However,
opposite results are observed in shake mode. A tentative expla-
nation for this reversal follows. Felted Nomex, having much
greater permeability than woven, should operate at lower dp. If
the cleaning mode is very efficient, the felted bag may well re-
tain its high permeability; and shake cleaning has been shown to
be considerably more efficient that reverse cleaning.
It is generally considered that collection efficiency is a direct
function (nonlinear) of bag dp. In the present case, it is noted
that incremental changes in bag dp had negligible effect on col-
lection efficiency. This further supports the contention that
the bags operated at maximum efficiency under all test conditions.
It also implies that high collection efficiency might also be
obtained at lower bag dp at conditions outside the test regimen.
3.1.2.7 Operating Problems—
A plague of mechanical malfunctions of the baghouse systems de-
scended on the operation almost coincidentally with start of
operations. Since operating problems from this source have been
detailed before, it would be monotonous to repeat the descriptions
here. Overall attrition of the baghouse unit is so severe as to
dictate major overhaul before its return to the field.
One type of operating problem deserves comment since it relates
to the application of baghouses to emission sources characterized
by high moisture content in the gas; namely, mud deposit caused
by condensation. At both the lime kiln and recovery boiler, dew
point of the stack gas was about 66°C (150°F). Any substantial
leakage of ambient air into the slipstream cools the gas below
its dew point, and the resultant combination of condensate and
solid particulate deposits mud throughout the baghouse system,
especially in the bags. This is disastrous since the bags must
be replaced and conditioned. At the lime kiln, with a relatively
short run of accessible ducting (ca. 16.8 m) and high stack gas
temperature (260°C-288°C), it was relatively uncomplicated to
detect and stop significant leaks, and the high temperature gas
kept the system hot after relatively rapid preheat of the system
with a space heater.
At the recovery boiler, the stack gas temperature was lower (ca.
177°C) and most of the duct run was not readily accessible for
leak testing (see Figure 3). When, finally, it was judged that
significant leakage had been stopped, it was found that no man-
ner of adding heat to the system at the baghouse end of the duct
was adequate to maintain gas reaching this area above its dew
point. It was ultimately necessary to take a space heater to
the roof of the boiler, tee it into the duct at the stack port
19
-------
and pull hot gas from the heater through the entire system for 1 to
2 hours in order to bring the system to high enough temperature to
maintain the ensuing stack gas above its dew point throughout.
A third type of operating problem, encountered after resolution
of the condensation problem, related to rapid loading of the bags,
excessive bag dp, and ultimate restriction of flow through the
baghouse. The end result occurred within 2 to 3 minutes after
start of filtration. While grain load at the boiler did not
appear to be excessive, the solids visually appeared much finer
than those at the lime kiln. It seemed reasonable that some
combination of filtration period and cleaning period would per-
mit operation, but to determine this combination required execu-
tion of a fractional factorial design. The optimum combination
was determined as 10-min filtration, 20-s cleaning period, com-
pared with 30 min and 5 s, respectively, proposed in the test
plan. Bag dp was 1.24-2.49 kPa (5-10 in. w.c.).
Resolution of these two problems at the recovery boiler consumed
approximately 4 weeks. On the verge of starting testing/sampling
operations, No. 3 boiler suffered a series of malfunctions which
shut it down at unpredictable times. After 2 or 3 days, when it
became known that there would be no relief from this malady, the
baghouse connection was switched to No. 4 boiler, where it was
discovered that atypical performance of the cascade evaporators,
upstream of the slipstream port, resulted in a cloud of black
liquor beads in the stack gas entering the baghouse system.
These conditions at the boilers, together with continued deterior-
ation of the baghouse system overall, dictated termination of the
test program.
3.1.2.8 Conclusions—
In control of lime kiln emissions, all cleaning mode/bag type
combinations performed with maximum collection efficiency, i.e.,
both integrated mass and fractional, within the test regimen.
The term "maximum" is used in view of the insensitive responses
of collection efficiency to changes in test parameters.
Overall, integrated collection efficiency was 99.98+%. Overall
averages of mean fractional efficiencies by size range were as
follows:
Size, ym Efficiency, %
1-3 99.815
4-6 99.814
7-10 99.918
On the basis of collection efficiency, it appears that a high
level of control of lime recovery kiln emissions can be afforded
by a baghouse.
20
-------
On the basis of bag differential pressure at comparable operating
conditions, shake cleaning was significantly more efficient than
reverse flow cleaning.
The choice of baghouse control of lime kiln emissions cannot be
based on collection efficiency alone. On the contrary, projected
operating problems tend to discourage use of a baghouse in this
application. The specific problems are the high moisture content
of the flue gas, the probable frequency at which condensation and
mud deposition can occur, and the necessity for an auxiliary pre-
heat system to prevent this disastrous result. Such a system
would add both cost and complexity to the control installation.
At the outset of this study the lime recovery kiln effluent was
expected to be similar to that from dry process cement kilns. In
fact, the lime kiln tested more closely resembles a wet process
cement kiln whose stack gas also has a high moisture content; 20%
to 25%. It is notable that wet process cement kilns largely em-
ploy electrostatic precipitator (ESP) units for emission control
since the moisture enhances ESP performance, and high temperature
obviates condensation problems. In dry process plants, baghouses
are occasionally used as secondary collectors, preceded by some
type of mechanical collector. Glass bags appear to be the norm.
Collection efficiencies are noted as 99.8+%, essentially equiva-
lent to efficiency reported herein for Nomex bags at the lime kiln.
(In general, see References 3 through 7.)
The fact that the wet and dry process cement kilns require dif-
ferent types of control devices supports the rationale discouraging
use of a baghouse for control of lime recovery kiln emissions.
The same rationale would apply to use of a baghouse at the re-
covery boiler where moisture content of the flue gas is also at
a high level.
3Gagan, E. W. Air Pollution Emissions and Control Technology.
Cement Industry. Canada Air Pollution Control Directorate.
Environmental Protection Service Report Series. Economic and
Technical Review Report EPS-3-AP-74-3, April 1974.
4Gilliland, J. L. Air Pollution Control in the Portland Cement
Industry. 1st Air Pollution Control Conference. April 1971.
5Kreichelt, T. E., D. A. Kemnitz, and S. T. Cuffe. Atmospheric
Emissions from the Manufacture of Portland Cement. PHS-Pub-
999-AP-17. 1967.
6Squires, B. J. Fabric Filter Dust Collectors, Their Use in the
Ventilating, Steel, Non-Ferrous Metals, Cement, Power and Chemical
Industries. Filtration and Separation, pp. 228-239, May/June 1967,
7Tripler, A. B., Jr., and G. R. Smithson, Jr. A Review of Air
Pollution Problems and Control in the Ceramic Industries. Ameri-
can Ceramic Society, Columbus, Ohio, May 5, 1970.
21
-------
3.1.3 Baghouse Repackaging and Upgrading
After conclusion of testing at the Weyerhauser pulp mill, the bag-
house was returned to Research Triangle Park, North Carolina for
a complete repackaging and refurbishing effort.
As received, the baghouse unit was mounted in a 1.36-metric-ton
(1.5-ton), stake bed truck. Portions of the system were relocated
for operation outside the truck bed due to the truck size. This
mode of operation turned out to be extremely inconvenient and
detrimental to efficient field testing. Therefore, it was decided
to mount the entire baghouse system in a 12.2-m (40-ft) tractor-
trailer unit.
The trailer unit was purchased and delivered on 30 January 1976,
and repackaging commenced. In addition to transfer of the system
to the trailer, potential solutions to a number of operational
problems encountered during field operations were incorporated.
Figures 4 and 5 show the current baghouse unit.
As of this writing, the baghouse unit is scheduled to replace the
mobile scrubber system on a gray iron foundry effluent some time
during September 1976.
3.2 MOBILE SCRUBBER UNIT
3.2.1 Background
The mobile scrubber unit was designed and fabricated by the
Detection Branch, Chemical and Biological Sciences Division of
the Naval Surface Weapons Center (NSWC), Dahlgren, Va., under
project order No. 4-0105-(NOL)/EPA-1AG-133(D), Task 2. On com-
pletion of construction and brief equipment checkout by NSWC, the
unit was received by the Industrial Environmental Research Labora-
tory on 16 December 1974. The unit was subsequently placed on
site at Pennsylvania Power & Light Company's generating station
at Sunbury, Pa. on 15 January 1975, for initial field shakedown
testing. Shortly after startup of the unit at Sunbury the in-
duction fans failed, and NSWC retrieved the unit to determine
the cause of failure and repair the fans.
After completion of repairs and minor modifications, the unit was
returned to IERL and taken to the Research Triangle Park for ex-
tensive shakedown tests under simulated field conditions. It was
then taken to Weyerhauser Corporation's pulp mill at Plymouth, N.C.,
on 21 April 1975, and hooked up to a lime recovery kiln for execu-
tion of a test plan for evaluating dust control efficiency of the
two types of scrubbers involved (venturi and sieve tray). Before
a week of operation under field conditions was completed, the
induction fans failed once more.
22
-------
Figure 4. Current baghouse enclosure.
Figure 5. End view - baghouse.
23
-------
3.2.2 Events of Second Year
After the blowers had failed for the second time, the scrubber
unit was returned to Research Triangle Park, N.C. for modifica-
tions. New blowers of a different design were selected, purchased
and installed in the scrubber unit. These items were received
from the vendor during January 1976.
Carryover liquid had also been noted as an operational problem
with the scrubber system, and the decision was made to replace
the mist eliminator with another unit of different design to try
and minimize this occurrence.
A third bothersome operational problem involved activation of
automatic shutdown sequence due to false signaling from the sump
tank overflow protection system. The cause turned out to be en-
trained mist. This problem was remedied by design change.
After the new equipment had been installed, the scrubber unit was
subjected to simulated field testing at Research Triangle Park
for 2 weeks. No problems surfaced during the testing, and a
concerted effort was then initiated to find a suitable testing
site.
In mid-June 1976, arrangements were finalized to place the scrub-
ber on stream at a gray iron foundry, and at the time of this
writing field testing is underway. Figures 6 through 9 illustrate
the scrubber unit configuration.
3.3 MOBILE ENERGY VAN
The EPA Energy Van is an energy research unit designed and con-
structed by Englehard Industries for the U.S. Environmental
Protection Agency. It contains energy supply systems for the
home which are designed to be environmentally clean and energy
conserving.
Integrated systems include fuel cells, a solar energy collector,
a heat pump, and catalytic appliances. These systems provide
the energy needed to heat space and water, and to cool, ventilate,
cook, light, operate appliances, and refrigerate within the van.
Figures 10 through 12 illustrate the van configurations.
Objectives in building the van were to develop and demonstrate
an energy supply system which cuts pollution and energy consump-
tion by as much as 50% for residential and commercial buildings.
This mobile unit was acquired by the contractor on 21 June 1976.
At the time of this writing, a testing program covering the
period 1 September 1976 through 30 June 1977 is being written.
The unit will be operated at the Environmental Research Center,
24
-------
-P
-H
C
0)
o
CO
0)
rH
•H
XI
O
M-l
O
S-l
a;
(U
M
•H
fa
25
-------
Figure 7. Mobile scrubber unit process area.
26
-------
Figure 8. Sieve tray column.
27
-------
|1( THKOTTLE VALVE
KJTTEHfLt VALVE
lUTTCMFUY VALVE
SOLENOID VALVE
Figure 9. Scrubber flow schematic,
28
-------
Figure 10. Energy van - side view.
Figure 11. Energy van - interior Figure 12,
living area.
Energy van - fuel
delivery system.
29
-------
Research Triangle Park, North Carolina, during the testing pro-
gram period. A separate final report will be issued for this
unit at the end of the testing program.
30
-------
REFERENCES
1. Hall, R. Mobile Fabric Filter System - Design Report.
GCA/Technology Division. Contract No. 68-02-1075.
October 1974.
2. Hall, R. Mobile Fabric Filter System - Final Report.
GCA/Technology Division. Contract No. 68-02-1075. May 1975.
3. Gagan, E. W. Air Pollution Emissions and Control Technology.
Cement Industry. Canada Air Pollution Control Directorate.
Environmental Protection Service Report Series. Economic
and Technical Reveiw Report EPS-3-AP-74-3, April 1974.
4. Gilliland, J. L. Air Pollution Control in the Portland
Cement Industry. 1st Air Pollution Control Conference.
April 1971.
5. Kreichelt, T. E., D. A. Kemnitz, and S. T. Cuffe. Atmospheric
Emissions from the Manufacture of Portland Cement. PHS-Pub-
999-AP-17. 1967.
6. Squires, B. J. Fabric Filter Dust Collectors, Their Use in
the Ventilating, Steel, Non-Ferrous Metals, Cement, Power
and Chemical Industries. Filtration and Separation,
pp. 228-239, May/June 1967.
7. Tripler, A. B., Jr., and G. R. Smithson, Jr. A Review of
Air Pollution Problems and Control in the Ceramic Industries.
American Ceramic Society, Columbus, Ohio, May 5, 1970.
31
-------
TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
1. REPORT NO. 2.
EPA-600/2-77-042
4. TITLE ANDSUBTITLE
Particulate Control Mobile Test Units: Second Year's
Operation
7. AUTHOR(S)
D. L. Zanders
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Monsanto Research Corporation
1515 Nicholas Road
Dayton, Ohio 45407
12. SPONSORING AGENCY NAME AND ADDRESS
EPA, Office of Research and Development
Industrial Environmental Research Laboratory
Research Triangle Park, NC 27711
3. RECIPIENT'S ACCESSION-NO.
5. REPORT DATE
January 1977
6. PERFORMING ORGANIZATION CODE
8. PERFORMING ORGANIZATION REPORT NO.
MRC-DA-578
1O. PROGRAM ELEMENT NO.
1AB012; ROAP 21ADM-034
11. CONTRACT/GRANT NO.
68-02-1816
13. TYPE OF REPORT AND PERIOD COVERED
Second Year; 7/75-6/76
14. SPONSORING AGENCY CODE
EPA-ORD
15. SUPPLEMENTARY NOTES IERL-RTP project officer for this report is D. L. Harmon, Mail
Drop 61, 919/549-8411 Ext 2925. EPA-600/2-76-042 was the first year's report.
i6. ABSTRACT The repOrt summarizes the second year's operation of EPA-owned mobile
test units. Unit use divides into two principal areas: (1) three units (baghouse, elec-
trostatic precipitator (ESP), and wet scrubber) are designed for use in the field to
study the applicability of different methods for controlling fine particulate emitted
from a wide variety of sources; and (2) a fourth unit (energy van) is designed to demon
strate the feasibility of unconventional energy supply systems to support residential
and commercial buildings. Results from baghouse tests on a kraft mill lime recovery
kiln indicate an overall, integrated collection efficiency of 99. 98+ wt %. Based on
collection efficiency alone, a high level of control can be afforded by a baghouse on
lime kiln particulate emissions. However, based on projected operating problems due
to high moisture content of the gas, baghouse control of a lime recovery kiln is not
recommended. Mobile scrubber unit operation during the year was confined to start-
up field testing and correction of mechanical and operating difficulties. The ESP unit
is still under construction. The newly acquired energy van has not yet undergone
testing.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.IDENTIFIERS/OPEN ENDED TERMS
COSATI Field/Group
Air Pollution
Dust
Dust Collectors
Mobile Equipment
Test Equipment
Field Tests
Woven Fabrics
Filters
Scrubbers
Kilns
Electrostatic Precip-
itators
Air Pollution Control
Stationary Sources
Fine Particulate
Baghouses
Wet Scrubbers
Energy Van
13B
11G
13A
15E
14 B
HE
07A
18. DISTRIBUTION STATEMENT
Unlimited
19. SECURITY CLASS (This Report)
Unclassified
21. NO. OF PAGES
37
20. SECURITY CLASS (This page/
Unclassified
22 PRICE
EPA Form 2220-1 (9-73)
32
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