Fractional Efficiency of an Electric Arc Furnace Baghouse


EPA
United States
Environmental Protection
Agency
Office of
Research and
Development
EPA-600/7-77-023
Industrial Environmental Research        EPA-600/7-';
Laboratory
Research Triangle Park, North Carolina 27711   March 1977
             FRACTIONAL EFFICIENCY OF AN
             ELECTRIC ARC FURNACE
             BAGHOUSE
             Interagency
             Energy-Environment
             Research and Development
             Program Report

-------
                   RESEARCH REPORTING SERIES
Research reports of the Office of Research and Development, U.S. Environmental
Protection Agency, have been grouped into seven series. These seven broad categories
were established to facilitate further development and application of environmental
technology. Elimination of traditional grouping was consciously planned to foster
technology  transfer and  a maximum interface in related fields. The seven series
are:

     1.  Environmental Health Effects Research
     2.  Environmental Protection Technology
     3.  Ecological Research
     4.  Environmental Monitoring
     5.  Socioeconomic Environmental Studies
     6.  Scientific and Technical Assessment Reports (STAR)
     7.  Interagency Energy-Environment Research and Development

This report has been assigned to the  INTERAGENCY  ENERGY-ENVIRONMENT
RESEARCH AND DEVELOPMENT series. Reports in this series result from the effort
funded under the 17-agency Federal Energy/Environment Research and Development
Program. These studies relate to EPA's mission to protect the public health and welfare
from adverse effects of poljutants associated with energy systems. The goal of the
Program is to assure the rapid development of domestic energy supplies in an environ-
mentally-compatible manner  by  providing the necessary environmental data and
control technology. Investigations include analyses of the transport of energy-related
pollutants and their health and ecological effects; assessments of, and development
of, control technologies for energy systems; and integrated assessments of a wide
range of energy-related environmental issues.
                            REVIEW NOTICE

This report has been reviewed by the participating Federal Agencies, and approved
for publication. Approval does not signify that the contents necessarily reflect the
views and policies of the Government, nor does mention of trade names or commercial
products constitute endorsement or recommendation for use.

This document is available to the public through the National Technical Information
Service, Springfield, Virginia 22161.

-------
                                   EPA-600/7-77-023

                                   March 1977
      FRACTIONAL EFFICIENCY

        OF AN  ELECTRIC ARC

         FURNACE BAGHOUSE
                                     , ...... •3i:rr.1-^n"2!
                                  I" •'\  • '•'•'  't.an uewurca

                                    '"• -v (' 'i'Ti)
                                   Lt'.'.vl \» '    i
                     by

      Reed W. Cass and John E. Langley

          GCA/Technology Division
              Burlington Road
        Bedford,  Massachusetts 01730
       Contract No. 68-02-1438, Task 4
        Program Element No. EHE624
     EPA Task Officer:  James H. Turner

 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

-------
                           TABLE OF CONTENTS

Sections                                                             Page

I      Conclusions                                                   1

II     Recommendations                                               3

III    Introduction                                                  4

IV     Marathon LeTourneau Steel Mill                                6

V      Equipment and Methods                                         11

VI     Results                                                       29

VII    References                                                  .  56

Appendix

A      Particle Size Distribution Curves                             57

B      Differential Size Distribution Curves                         69

C      Andersen In-Stack Irapactor Substrate Anomalous Weight
       Gains                                                         81

D      Calculator Inputs/Outputs for Total Mass Measurements         89

E      Calculator Inputs/Outputs for Inertial Impactor
       Measurements                                                  110

F      Fine Particle Measurements                                    151
                                 iii

-------
                            LIST OF FIGURES


No.                                                                   Page

1     Photograph of Side of Fabric Filter                              7

2     Photograph of End of Fabric Filter                               8

3     Location of Baghouse Inlet Test Ports and Sampling Points        12

4     Location of Baghouse Outlet Test Ports and Sampling Points       13
      in North Stack

5     Photograph of Inlet Sampling Location                            14

6     Photograph of Outlet Sampling Location                           15

7     Andersen Impactor Manufacturer's Curves and Measured             19
      Stage Size Cutoff Points as a Function of Flow Elate

8     Correlation Between the Outlet Mass Concentrations Determined    24
      by the RAC Stack Sampler and the Inertial Impactor and
      Prefilter

9     Fine Particle Dilution System Components                         27

10    Inlet Concentration as a Function of Events in the Process       33
      Cycle

11    Time in Process Cycle at Which Inlet Samples Were Collected      35

12    Inlet HMD as a Function of Process Cycle and Testing Day         36

13a   Differential Size Distribution Curves of Baghouse Inlet          37
      Aerosol During First Melt Phase of Process Cycle When
      One Electric Arc Furnace is Operating

13b   Differential Size Distribution Curves of Baghouse Inlet          38
      Aerosol During Back Charge Phase of Process Cycle When
      One Electric Arc Furnace is Operating
                                iv

-------
                      LIST OF FIGURES (continued)
No.                                                                    Page
13c   Differential Size Distribution Curves of Baghouse Inlet          39
      Aerosol During Second Melt Phase of Process Cycle When
      One Electric Arc Furnace is Operating

13d   Differential Size Distribution Curves of Baghouse Inlet          40
      Aerosol During Tap Phase of Process Cycle When One
      Electric Arc Furnace is Operating

14    Composited Differential Size Distribution Curves of Baghouse     42
      Inlet Aerosol For a Process Cycle With One and Two Furnaces
      Operating (190 Minute Furnace Cycle)

15a   Concentration Versus Process Cycle for 1 urn Particles            43

15b   Concentration Versus Process Cycle For 2 urn Particles            44

15c   Concentration Versus Process Cycle For 4 urn Particles            45

15d   Concentration Versus Process Cycle For 6 urn Particles            46

15e   Concentration Versus Process Cycle For 8 urn Particles            47

15f   Concentration Versus Process Cycle For 10 pm Particles           48

16    Average Outlet Differential Size Distribution Curves For         49
      Tests With One and Two Furnaces Operating

17    Fabric Filter Fractional Penetration Curves                      50

18    Condensation Nuclei Counter Measured Concentrations as a         54
      Function of the Process Cycle and Compartment Cleaning

19    Dust Counter Measured Concentrations as a Function of the        55
      Process Cycle and Compartment Cleaning

-------
                             LIST OF TABLES


No.                                                                   Page

1     Results of Physical Characterization Tests On Fabric             10
      Filter Bags

2     Velocities in Fabric Filter Inlet Duct                           16

3     Impactor Calibration Parameters                                  18

4     Probe Losses of Impactors Sampling the Fabric Filter             21
      Influent and Effluent

5     Results of Particulate Sampling at Marathon LeTourneau           30

6     Flue Gas Properties                                              32

7     Outlet Concentration and Penetration Statistics                  31

8     Results of Fluoride Analyses                                     51

9     Results of Fine Particle Measurements on the Baghouse            53
      Influent and Effluent at Marathon LeTourneau
                                 vi

-------
CONVERSION FACTORS FOR BRITISH AND METRIC UNITS
To convert from
°F
ft.
2
ft.
ft.3
ft./min. (fpm)
ft.3/min.
in.
2
in.
oz.
/ ^ 2
oz . /yd .
grains
2
grains/ft.
grains/ft.3
Ib. force
Ib . mass
lb./ft.2
in. H20/ ft./min.
Btu
To
°C
meters
2
meters
3
meters
centimeters/sec .
3
centimeters /sec.
centimeters
2
centimeters
grams
grams /meter
grams
grams/meter
grams /meter
dynes
kilograms
2
grams /centimeter
cm. H20/cm/sec.
calories
Multiply by
f (°F-32)
0.305

0.0929
0.0283
0.508
471.9
2.54

6.45
28.34
33.89
Of\f./. -]
• Uo4/
0.698
2.288
4.44 x 105
To


centimeters
2
centimeters
3
centimeters
meters /sec.
3
meters /hr.
meters
2
meters
grains
2
grams /centimeter




New tons
0.454 grams
2
0.488 grams/meter
5.00
1 CO
252
2
Newtons/meter /cm/sec.

Multiply


30-5

929.0
28,300.0
5.08 x
1.70
2.54 x

6.45 x
438.0
3.39 x




0.44
454.0
4,880.0
490.0
by





lO'3

lO'2
-4
10

ID'3

-------
                           ACKNOWLEDGMENTS

The many contributions of Dr. James H. Turner, Environmental Protection
Agency Project Officer, are gratefully appreciated.  The outstanding co-
operation of Mr. David H. Thomas and the staff of the Marathon LeTourneau
Steel Mill, especially Mr. William McClelland and Mr. James Hodges made this
program possible and is sincerely appreciated.

Several members of the GCA/Technology Division staff made significant con-
tributions to the field program.  They include Messrs. Stephen Brenan,
Mark Daniels, Robert Engelman and Manuel Rei.

The GCA/Technology Division Administrator was Mr. Norman F. Surprenant and
the project manager was Mr. Robert M. Bradway.
                                 viii

-------
                              SECTION I
                             CONCLUSIONS

The test results show that a fabric filter utilizing two year old
      TM
Dacron   bags is an effective means of controlling particulate emissions
from the electric arc furnace tested which produces a high strength, low
alloy specially steel.  The results of the tests with one and two furnaces
operating determined the baghouse mean mass removal efficiencies to be
97.9 percent and 98.7 percent, respectively, corresponding to mean ef-
fluent concentrations of 0.0014 and 0.0019 grains/dscf.   The maximum
effluent concentrations for the total mass samples for the tests with
one and two furnaces in operation were 0.0016 and 0.0021 gr/dscf, respec-
tively.  These effluent concentrations are well within the Environmental
Protection Agency's Standard of Performance for Steel Plants:  Electric
Arc Furnaces Standard for Particulate Matter of 0.0052 gr/dscf.

The findings of the baghouse influent and effluent inertial sizing mea-
surements were contrary to what would be predicted by fabric filtration
theory based on interception and inertial and differential capture mech-
anisms.  The fact that the particles with aerodynamic diameters of 6 urn
exhibited the highest penetration and particles of 1 urn the least pene-
tration through the baghouse suggests agglomeration of the smaller par-
ticles.  These results support the contention that a large percentage of
particles in the fabric filter effluent have not passed directly through
the filter media but instead are dislodged agglomerated particles which
were previously collected.
*
 Although it is EPA s policy to use the metric system for quantitative
descriptions, the British system is used in this report because not to do
so would tend to confuse the reader.  Readers who are more accustomed to
metric units may use the table of conversions on the preceding page.

-------
The time of maximum condensation nuclei emissions from the baghouse was
determined to be immediately after compartment cleaning.  This time was
pinpointed by monitoring the stack aerosol with real time particle coun-
ters.  The period immediately following compartment cleaning is a time
of maximum emissions for a properly functioning filtration system because
the filter cake is removed or damaged during cleaning and the fabric is
least efficient until the cake has been repaired or replaced.

-------
                             SECTION II
                           RECOMMENDATIONS

It is recommended that the experience of personnel operating and maintain-
ing fabric filters be compiled emphasizing the methods of detecting and
locating defective bags.  This problem was pointed out during the subject
program when an inspection of each compartment made it apparent that the
presence of a leaking bag would be nearly impossible to detect.  The
thimble plates had considerable buildup of dust and a loose bag would
likely go unnoticed.  A leaking bag was in fact discovered several weeks
after the test program was completed, but it is impossible to determine
if the bag was leaking at the time of the tests.  It would also be useful
to find out when an operator feels it is necessary to replace a leaking
bag and what levels of emissions occur shortly before the bag replacement.

More research needs to be conducted on the problems associated with in-
stack cascade impactors and the problems and experiences of people using
the impactors needs to be compiled and compared.  Principle areas of fur-
ther study should include:  particle depositions in the impactor probe
and body, weight losses of greased collection plates and anomalous weight
gains of glass substrates.  Also, the practicality of using impactors with
stainless steel collection plates at low flow rates to reduce anomalous
weight gains and losses without appreciable bounce problems should be
studied.  There is also a need for a combination of impactors to be used
when performing a fractional efficiency/penetration type of evaluation on
a control device which would allow simultaneous baghouse influent and
effluent sampling thereby reducing the effect of temporal variations.
Simultaneous sampling is especially desirable when sampling a cyclic pro-
cess such as an electric arc furnace.

-------
                             SECTION III
                             INTRODUCTION

BACKGROUND

The work reported in this publication represents one phase of a program
whose purpose is to characterize the performance of several industrial
size fabric filter systems.  The fabric filter tested at the Marathon
LeTourneau Company in Longview, Texas cleaned the emissions of either
one or two 30-ton electric arc furnaces which produce a high strength,
low-alloy specialty steel.  Each furnace is fitted with a side draft hood
and a canopy hood which is only used during charging and pouring.  The
hoods are ducted through a spark arrester to a 10-compartment American
                                         TM
Air Filter baghouse which utilizes Dacron   bags.

APPROACH

The performance of the fabric filter was characterized by determination
of the particulate removal efficiency as a function of total mass and
particle size.  In addition, the influent and effluent total fluoride
concentrations were measured simultaneously with the particulate concen-
trations during three tests to qualitate the fluoride levels to which
the filter bags are exposed during normal service.  The apparent frac-
tional efficiency, defined as the measured change in the particulate
concentrations as a function of particle size that results from the fil-
tration process, was determined by upstream and downstream sampling
using inertial cascade impactors.  The baghouse influent and effluent
streams were also monitored with a condensation nuclei counter and an

-------
optical dust counter to determine variations in submicron particle con-
centrations as a function of the process and the cleaning cycle.

A pretest survey was performed primarily to determine the following:  the
sample time necessary for the outlet impactors to collect weighable samples,
the presence and magnitude of impactor substrate anomalous weight gains,
the mass removal efficiency of the filter papers used in the fluoride tests,
the best diluter configurations for the baghouse inlet and outlet fine
particle monitors, the variations in inlet mass concentration as a function
of the process cycle, and the variability of baghouse operation and process
cycle parameters.  The tests in the major program were performed when there
were either one or both furnaces in operation.  Originally, it was planned
to sample for 4 days with two furnaces in operation and 6 days with one
furnace in operation.  This plan was modified because of a change in the
production schedule at the steel mill.  The resulting testing program had
only 2 test days with two furnaces but 8 test days with one furnace in
operation.  The greatest effect of having two furnaces in operation instead
of one appears to have been than the inlet loading to the baghouse and
hence the cloth loading rate was doubled.  The change in the outlet con-
centration through the baghouse resulting from the increased inlet loading
is an indication of whether the fabric filter's particle removal efficiency
is dependent upon inlet loading.

-------
                            SECTION IV
                  MARATHON LETOURNEAU STEEL MILL

The steel mill at Marathon LeTourneau produces high strength, low alloy,
specialty steel in two electric arc furnaces of 30 tons each, nominal
capacity.  The furnaces are 10,000 kVA swing roof top charged units with
individual combination side-draft and canopy hooding.  The side-draft
hoods operate while the furnace roof is in place and the canopy hoods
operate when the roof is removed for charging and tapping.  The furnaces
use the basic steel making process with cold number one oil-free scrap.
The furnaces must be back charged once to reach holding capacity, and
the double slag method of refining is used.  Additions of fluorspar are
commonly made for slag conditioning and oxygen lancing is used to lower
the carbon content of the melt.

The furnace hoods are ducted to a 10-compartment American Air Filter
baghouse installed in 1973.  Photographs of the baghouse are presented
                                                               2
in Figures 1 and 2.  The baghouse has a cloth area of 52,778 ft  which
results in an air-to-cloth ratio of 3.22:1 at the design flow of
170,000 acfm at 150°F.  The net air-to-cloth ratio increases to 3.58:1
with one compartment off-line for cleaning.  The cleaning cycle is ac-
tuated by timer such that there is no delay time between cycles.  The
normal cleaning cycle schedule for each compartment is as follows:
             Time, min.          Operation
                0:00     Gas outlet damper closes
                0:30     Bags begin shaking
                1:00     Bags end shaking
                1:40     Gas outlet damper opens
               12:40     Next gas outlet damper closes

-------


Figure 1.  Photograph of side of fabric filter

-------
Figure 2.  Photograph of end of fabric filter

-------
                                             T*M
Each baghouse compartment contains 288 Dacron   filter tubes which are
5 inches in diameter by 14 feet long.  The filter tubes were fabricated
by the Carborundum Company.  The manufacturer's specifications for the
filter material are as follows:
                                               2
    •   Weight                      = 6.1 oz/yd
    •   Thread count                = 79 x 89
    •   Weave                       =3x1 twill
                                                     2
    •   Permeability at 0.5 in. H^O = 15 to 25 cfm/ft

The results of the physical characterization tests performed on a new
and used bag are presented in Table 1.  The used bag tested was randomly
selected from the bags removed from a compartment after about two years
service.  All the bags were replaced in the compartment because of dif-
ficulty locating a leaking bag.  The physical characterization tests
show that the air permeability of the used bag (~2 years service) is
much less, 40 percent, than that for a new bag.  The reduced air per-
meability or blinding of the fabric is most likely due to dust particles
lodged in the fabric interstices.  The tests also show that the breaking
strenght and elongation has been reduced 15 to 20 percent indicating
wear, however, bags which were not replaced are still in service after
3 years without breakage problems.  It was also found that the used fa-
brics flexural rigidity was 43 percent higher than that of the new medium
and is presumably due to particles in the intersticies of the fabric.

-------
         Table  1.  RESULTS  OF PHYSICAL CHARACTERIZATION TESTS ON
                    FABRIC FILTER BAGS
Test description
ASTM D 1910, Sample weight ,b os/aq yd
ASTM D 1777, Sample thickness,' nils
Range:
Average :
ASTM D 737, Air permeability,0 cfra/aq ft at V HjO AP
Range:
Average :
ASTM D 1682, Breaking strength and elongation
Breaking strength, Ib
Warp: Range -
Average :
Fill: Range:
Average :
Elongation at break, percent
Warp: Range:
Average :
Fill: Range:
Average:
Flexural rigidity - beam method,*1 (ID'S inch Ib
Warp:
Fill-
Average :
Adjusted for difference in mass
Warp:
Fill:
Average
New bag
$.23, 6.59

13.4 - 14.0
13.7
19.7 - 27.2
24.2


225 - 234
229
149.1 - 172.4
160.6

31.5 - 34.1
32.7
37.9 - 42.?
40.1

3.32, 3.51
0.77, 0.85
1.66



Used bag
7.13. 7.37

12.4 - 13.8
13.2
9.2 - 10.2
9.8


189.1 - 193.5
191.6
117.8 - 148.1
127.3

26.6 - 28.5
27.7
31.7 - 36.4
34 0

3.14. 3 75
1.58, 1.71
2 38
2.78. 3.31
1.40. 1 51
2.10
 Bag in service  for approximately 2 years,  vacuumed prior to testing.
 Single measurements, sample area 6" x 6".
 Five tests each.
dAverage of four tests,  each reading (four  up, four down)
                                      10

-------
                             SECTION V
                       EQUIPMENT AND METHODS

The baghouse filtering the effluent of the electric arc furnaces at the
Marathon LeTourneau Company was evaluated for the total particulate pen-
etration and the particulate penetration as a function of size.  Total
mass samples and size-classified samples for gravimetric analysis were
collected before and after the fabric filter.  The total mass samples
from the first 3 test days were also analyzed for total fluorides.  The
influent and effluent of the baghouse were alternatively monitored for
fine particulate with a condensation nuclei counter and an optical dust
counter.  Since most of the sampling methods were straightforward, they
do not require extensive descriptions.  Only the novel or unusual tech-
niques will be described in detail.

MASS MEASUREMENTS

The baghouse influent and effluent mass concentrations were determined by
sampling isokinetlcally utilizing a Research Appliance Company (RAC)
           TM
Staksamplr.    The location of the baghouse inlet and outlet sampling
ports and the points sampled are shown in Figures 3 and 4.  Photographs
of the inlet and outlet sampling locations are presented in Figures 5 and
6.  The baghouse effluent is exhausted through two identical stacks and
the north stack was arbitrarily chosen for testing purposes.  Table 2 is
a tabulation of the velocities measured in the inlet duct during the pre-
test survey.  These velocities are fairly uniformly distributed in the
duct.  During the actual test series it was not possible to sample the
bottom port (F) because of the height of the inlet platform and so to
maintain symmetry, the top port (A) was also omitted.  The inlet and

                                 11

-------
        TO
     BAGHOUSE
                      INLET TEST  PORT
                           CNC AND
                           DC TEST PORT
                                                            FROM
                                                          _ ARC
                                                           FURNACE
 IMPACTOR PORT
'-  -I
*.  :-  I
         U
              5

                           T
                           Z1
                      .   .  .4.  .  .
                          -64'A-
                                         -CNC AND DC PORT
                                               PORTS B-E FOR TOTAL  MASS
                                               PORT  C  FOR  IMPACTORS
                                       9C1
Figure 3.  Location of baghouse  inlet test ports and sampling points
                               12

-------
                     T
                      9'
                              -6'-
                                      -CMC AND DC PORT
                                       e'/e
                                      •IMPACTOR PORTS
        CMC  AND
        DC PORT
                                                TOTAL  MASS PORTS
                                                        IMPACTOR
                                                        PORTS
Figure 4.   Location of baghouse outlet  test ports and  sampling points
            in north stack
                                 13

-------
Figure 5.  Photograph of inlet sampling location

-------
Figure 6.  Photograph of outlet sampling location

-------
 outlet ducts were sampled simultaneous for 4 hours during test No. 1 and
 for 6 hours for tests Nos. 2 through 10.  The 6-hour sampling period was
 selected because it encompassed approximately two complete arc furnace
 cycles.  The filter media used for the total mass determinations was
 Whatman No. 1 filter, as required for the fluoride analysis.  The penetra-
 tion of particulate through the Whatman No.  1 cellulose filter was measured
 during the pretest survey to be less than 1  percent at face velocities
 comparable to those at the RAC filter and, therefore,  suitable for total
 mass measurements.

             Table 2.  VELOCITIES  IN  FABRIC FILTER  INLET DUCT
Port
A
B
C
D
E
F
Velocity, fpm
Point
1
3281
3341
4287
4363
4131
3713
Point
2
3380
4724
4511
4210
4210
4210
Point
3
3800
4928
4438
3969
3969
4051
Point
4
4438
4724
4287
3886
4051
4051
Point
5
4287
4654
4511
4131
3969
3713
Point
6
4363
4793
4928
4654
4287
4210
          Note:  Average velocity = 4207.

TOTAL FLUORIDES MEASUREMENTS

The baghouse influent and effluent samples collected in the total mass
samplers during the first three tests were analyzed for total fluorides,
Particulate samples from the probe wash, glass wash and filter and an
aqueous sample from the impingers that capture gaseous fluorides were
composited for analysis.  The samples were analyzed in accordance with
              2
EPA Method 13A  which utilizes the SPADNS Zirconium Lake colorimetric
method.
                                 16

-------
IMPACTOR MEASUREMENTS

The penetration of particles through the bag filter as a function of
size and the inlet and outlet particle size distributions over the
range of approximately 0.5 urn to 20 um were determined using inertial
impactors.  The two types of impactors used were the Andersen Mark III
Stack Sampler and the University of Washington (U of W) Mark III Source
Test Cascade Impactor.

The lower four stages of each impactor used at Marathon LeTourneau were
calibrated in the lab to determine the inertial impaction parameter at
50 percent efficiency in accordance with the procedure described by
Calvert et al.   The calibration procedure consists of measuring the
concentration of monodispersed polystyrene latex spheres with a Bausch
and Lomb Dust Counter to determine the flow rate corresponding to 50 per-
cent penetration of the particles.  The flow rate for 50 percent penetra-
tion of the particles of known size is then used to calculate the inertial
impaction parameter at 50 percent efficiency which is used to calculate
the 50 percent particle size cutoff of a stage during sampling.  The
inertial impaction parameter for each impactor stage plus the pertinent
impactor and particle parameters are presented in Table 3.  Figure 7 pre-
sents the measured flow rates through the Andersen impactors for 50 per-
cent penetration as a function of known size spheres.  Figure 7 also has
the manufacturer's curves for the Andersen impactor 50 percent cutpoints.
The figure shows that equivalent impactor stages have similar size cutoffs,
but these size cutoffs are smaller than indicated by the manufacturer for
comparable flow rates.

The baghouse inlet stream was sampled several times during each test with the
U of W impactor which collected the sample from the midpoint of port C as
shown in Figure 3.  The pipe supporting the impactor had a long radius
bend allowing the impactor to be pointed directly into the stream, thereby
eliminating the need for sampling through a gooseneck nozzle.  The straight
nozzle approach was employed to minimize probe losses.  The influent
                                17

-------
Table 3.  IMPACTOR CALIBRATION PARAMETERS

Impactor
type
Andersen
2000 INC
Andeisen
2000 INC
Andersen
2000 INC
Andersen
2000 INC
Andersen
2000 INC
Andersen
2000 INC
Andersen
2000 INC
Andersen
2000 INC
University of
Washington
University of
Washington
University of
Washington
University of
Washington
University of
Washington
University of
Washington
University of
Washington
University of
Washington
Impactor
stage number
7A

6A

5A

4A

7B

68

5B

48

7A

6A

SA

4A

7B

6B

SB

48

Impactor parameters
Number holes
Impactor
stage
156

264

264

264

156

264

264

264

40

110

110

SO

40

110

110

SO

Stage jet
diameter,
cm
0.0259

0.0259

0.0376

0.0579

0.0254

0.0259

0.0368

0.05S6

0.0356

0.0361

0.0528

0.0792

0.0333

0.0325

0.0498

0.0772

Impactor
flow rate,
cc/sec
186 44

90.40

191.52

306 80

174.64

9/.70

200. 60

311.52

101.48

103.84

125.08

264 32

96.76

92.04

106.20

254.88

Particle parameters
Particle
diameter ,
urn
0.481

1 10

1 10

2.02

0.481

1. 10

1.10

2.02

0.600

1.10

2.02

2.02

0.600

1.10

2.02

2.02

Part icle
density,
g/cc
1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05

1.05


Inert lal
impact ion
parameter
0 1739

0.2325

0.15S8

0.2143

0.1727

0.2406

0.1722

0.2458

0.2104

0.2267

0.2765

0.2116

0.2451

0.2754

0.2798

0.2204

                  18

-------
VO
            OQ

            n
            (0
          co >
          rr 5
          p, Q.
         OQ n>
          n> n
            co
          co to
          H. 3
          N
          ft-H-
rt O
O rt
Hi O
MI H

•0 S
O 5
H- 0
a c
rt i-h
CO Pi

» R
CO C

CO (D
         C  CO
         a
         n  o
         rt  c
         H-  M
         o
         Itl

         ft,
         M
         O  3

         *
            g
E
*-
o
 •»
UJ
 1.0

0.9

0.8

0.7

0.6


0.5


0.4



O.3





0.2
                                                                                                  I I
             O.I
               0.2
                                03   0.4   0.5
                            0.7
         fl)  n>
            a.
                                        1.0

                                       D'p
                                                             2.0     3.0    4.0      6.0  B.O  10

                                                    AERODYNAMIC  DIAMETER, microns
20
30    40

-------
impactor probe losses, which at times were considerable (20.00 to 51.04
percent) are presented in Table 4.  These losses are believed to be larger
particles which should have been collected on the upper impactor stages.
Microscopic examination of resuspended dust removed from the baghouse
hopper showed a population of large particles which could have accounted
for the losses.  The shape of the influent cumulative size distribution
curves in Appendix A indicates that the larger particles were selectively
removed in the probe.  The affect of the probe losses is that the cumula-
tive and differential size distribution curves in Appendix B are probably
lower than actual for the larger particles.  However, the actual size
distribution of the particulate caught in the probe was not measured and
this should be remembered when interpreting the impactor results.

During the first 4 testing days, the stainless steel inserts of the inlet
impactor were coated with polyethylene glycol and dried for 2 to 3 hours
at 300 F.  It is not fully understood why some of the impactor inserts
lost weight even though there were particles visible on the inserts.
The weight loss problem was not anticipated because of the low temperature
at the inlet of 130 F, the low flow rate of 0.3 acfm through the impactor
and the short sampling time of 15 to 30 minutes.  In tests 5 through 10,
the inserts were not coated and weight loss was not a problem.  While
realizing the disadvantage of using uncoated inserts and the resulting
increase in problems with particle bounce, it was believed that bounce
would not be a serious problem at the low flow rate through the impactor.
Inspection of the impactors after each sample was collected showed some
evidence of bounce but the amount of particulate that was deposited on
the bottom of the preceding jet stage was very small compared to the
amount on the corresponding impaction surface.  Therefore, sampling with
uncoated inserts was considered to be better than with coated inserts
when the problems associated with each were weighed.

The duration of inlet impactor sampling to collect a weighable sample
on each stage without overloading was quite variable due to differences
in the mass concentration as a function of the process cycle.  After the

                                 20

-------
   Table 4.  PROBE LOSSES OF IMPACTORS SAMPLING THE FABRIC FILTER INFLUENT AND EFFLUENT

Test
number
1
2
3
4
5
6
7
8
9
10
INRb
2NR
3NR
Baghouse influent
Impactor run A,
percent
24.13
35.04
ND3
ND
ND
31.54
24.75
49.06
25.28
48.41


Impactor run B,
percent

32.92
ND
ND
ND
27.45
20.00
44.74
24.91
50.69


Impactor run C,
percent




34.85

28.68
25.35
22.19
41.67


Impactor run D,
percent







51.04
20.63
36.80


Baghouse
effluent
Impactor,
percent
18.67
11.15
17.65
10.43
28.78
25.00
17.12
23.78
12.73
18.62
9.88
14.95
12.56
SND means no data due to impactor substrate weight loss problems.
 NR refers to an impactor run overnight.

-------
first few tests, it was noticed that an increase of 0.2 to 0.4 in. Hg of
meter static pressure caused by loading the impactor back up filter
coincided with sufficient sample collection and was used in the remaining
tests to determine the sampling duration.

The influent to the baghouse was sampled isokinetically by measuring
the velocity, pressure and temperature at the impactor sampling point
prior to sampling.  The influent velocity, pressure and temperature were
used with the other necessary parameters to calculate the pressure drop
across the calibrated orifice necessary for isokinetic sampling.  During
sampling the flow through the impactor was kept constant.

The baghouse effluent was sampled for 9 hours during each test day with
two instack Andersen cascade impactors in the locations shown in Figure 4.
The outlet impactors sampled through straight nozzles so they could be
pointed into the direction of flow to minimize probe losses.  The resulting
probe losses were from 9.88 percent to 28.78 percent and are included in
Table 4.  These probe losses were much less than the influent impactor
probe losses and are considered to have only a minimal effect on the cumu-
lative and differential size distribution curves.  Reeve Angel 934 AH type
glass filter substrates were used in the impactors because they have been
found to be less reactive with stack gases than the Gelman Type A glass
              4
fiber filters.   Two impactors were run simultaneously during each testing
day with one of the impactors sampling filtered flue gas to indicate any
anomalous weight gains.  The figures in Appendix C show the suspected
anomalous weight gains for each stage of the impactor sampling flue gas
and the corresponding stage of the impactor sampling filtered flue gas
during the 10 test days.  Examination of the figures in Appendix C indi-
cates considerable weight gain in a number of cases and in a few cases the
weight gain of the impactor stage sampling filtered flue gas was greater
than that of the impactor sampling unfiltered flue gas.  In only one case
was there no apparent anomalous weight gain.  It is most difficult to
quantify the apparent anomalous weight gain because it did not follow a
pattern with respect to amount of weight gained by any particular stage.
                                  22

-------
Since a systematic error was not apparent and since the outlet differential
distributions in Appendix B do not appear to be dependent upon the apparent
anomalous weight gain, no corrections were made to the weight gained by
the substrates of the impactor sampling unfiltered effluent.

In addition to the impactors run during each normal test day, there were
three sets of outlet impactors run from 13 to 15 hours overnight.  These
impactors were run as an experiment to see if cascade impactors could be
run unattended.  Running the impactors unattended seemed to be a success
with the flow in the morning being the same as that set the preceding
evening.  The overnight impactors were also run in pairs with one sampling
prefiltered flue gas.  These impactors, however, utilized Gelman Type A
glass filter substrates.  The apparent anomalous weight gain for the night
runs, also shown in Appendix C, appears to be higher than during most of
the day runs in which the Reeve Angel substrates were used.

A comparison was made among the outlet mass concentrations measured by the
              TM
RAC Staksamplr  , which is considered to be the true concentration in the
duct, the mass concentration measured by the impactor and the mass concen-
tration measured by the prefliter on the blank impactor.  This comparison
is presented graphically in Figure 8 and includes the line that would re-
sult from perfect correlation and the actual line of best fit.  It can be
seen that the impactor measurements consistently indicate a lower concen-
tration than the RAC train.  This may be caused by the fact that the im-
pactors sampled at single points in the duct while the RAC train traversed
many points, or it may indicate an inherent inconsistency between the mea-
surement methods.  The lower mass concentration measured by the impactors
would appear to be contraindicative of serious anomalous weight gain
problems as observed in another similar comparison.
                                 23

-------
    0.0025
_   0.0020
u
O
P
<
o
u
V)
    0.0015
Jfj   0.0010
   0.0005
                                                         X4-LINE OF  BEST FIT
                                                      /  »=0.8I74« + O.0007
                                                        LINE OF  PERFECT
                                                        CORRELATION
O = PREFILTER

A= IM FACTOR
                    0.0005      0.0010      0.0015       0.0020     0.0025
                  INERT! AL  IMPACTOR  MASS  CONCENTRATION, groins/dscf
 Figure 8.  Correlation between the outlet mass  concentrations determined  by  the RAG
           stack sampler and the inertial impactor and prefilter

-------
FINE PARTICULATE MEASUREMENTS

The penetration of fine particles through the fabric filter was determined
by sampling the baghouse influent and effluent streams with a Dust Counter
(DC) and a Condensation Nuclei Counter (CNC) with a Diffusion Denuder (DD).
The particle concentrations were measured by a Bausch and Lomb 40-1 DC and
by a Rich Model 100 CNC.  Particle sizing was accomplished directly with
the DC and the CNC utilizing the DD.  The DC has seven size ranges with
the following smallest detectable particle sizes:  0.3 pm, 0.5 pm, 1.0 pm,
2.0 pm, 3.0 pm, 5.0 pm and 10 pm.  The CNC measures particles of 0.0025 pm
and larger diameter  in the concentration range of 1,000 to 300,000 par-
ticles/cc.  The theoretical upper size limit measurable by the CNC has been
estimated to be 0.3 to 0.5 pm.

Sizing with the CNC and DD is accomplished by drawing the sample through
the DD where particles less than a particular size, dependent upon the
flow rates, are removed.  The CNC then measures the concentration of the
particles remaining.  The five DD flow rates utilized at Marathon
LeToruneau resulted in the removal of all particles over the range of
less than 0.014 pm at the highest flow rate and less than 0.078 pm at
the lowest flow rate.

The temperature and moisture content of the influent and effluent of
the baghouse were in a range to allow sampling without dilution.  Dilution
was not necessary at the outlet and the sample was extracted through
a stainless steel probe, and tygon tubing to a "Y" where part of the
sample went to the CNC and part to the DC.  When the DD was used, it
was inserted between the "Y" and the CNC.

Dilution of the sample was required at the inlet because of the high
static pressure in the duct and the high concentration of fine particles.
A two-stage dilution was effected utilizing two basic diluter designs.
A sample of the flue gas was extracted through a stainless steel probe
                                  25

-------
and through the air ejector diluter shown in Figure 9(a).  A portion of
the diluted sample from the air ejectro diluter was then drawn through
a capillary tube diluter, Figure 9(b), to a "Y" where the sample flow
split with part going to the CNC and part to the DC.  When the DD was
used, it was inserted between the "Y" and the CNC as on the outlet.

The air ejector diluter is limited to a maximum dilution of approximately
90 to 1.  Its main value is its ability to extract a sample from a low
pressure location and to discharge the diluted sample at about atmospheric
pressure.  The CNC and DC will not operate properly when the pressure of
the sample entering the CNC or DC is too far below atmospheric, ~2 in.
H_0.  In the air ejector diluter, the sample is drawn through an orifice
by an air ejector in which the sample stream and a filtered compressed
air stream are mixed before being discharged through an orifice which
meters the combined flow.

The capillary tube diluter is capable of providing a 12 to 1 dilution.
A capillary tube meters the sample flow which is combined with regulated
filtered dilution air in a tee.   The combined sample and dilution flow
is equal to the flows through the CNC and DC.  The capillary tube diluter
was also used to vary the sample flow rates through the DD to provide
sizing data.  In this case, the combined sample and dilution flow is
equal to the flow through the CNC.

The DD is made of three closely spaced (0.097 cm) concentric cylinders
on which diffused particles are collected.   The d  , which is the par-
ticle diameter removed in the DD with 50 percent efficiency, is depen-
dent upon the flow rate through the DD.  The DD is most applicable for
particle sizes ranging from 0.01 to 1 urn diameter.

Particle sizing was accomplished by first sampling with the CNC alone
which corresponded to particles >_ 0.0025 um.  Next, flows varying from
approximately 2 cc/sec to 50 cc/sec were passed through the DD.  The
                                26

-------
(A) AIR  EJECTOR  DILUTER
DILUTED
SAMPLE
CALIBRATED
  ORIFICE
  ..  _ ..
        i
  AIR    I
EJECTOR
                            |

                                        CALIBRATED
                                          ORIFICE
                                           ./"?._
                                       - "V— *- SAMPLE
                                   t
                                FILTERED
                             COMPRESSED  AIR
(B) CAPILLARY   TUBE  DILUTER
                                CALIBRATED
                                CAPILLARY
                                  TUBE
                             PINCH CLAMP
                               FILTER
                           t
                        DILUTION
                          AIR
 Figure 9.  Fine particle dilution system  components
                        27

-------
approximate flows and resulting DD size cutoffs were 2 cc/sec and
0.078 urn, 5 cc/sec and 0.048 ym, 10 cc/sec and 0.034 ym, 25 cc/sec and
0.021 ym, and 50 cc/sec and 0.014 ym.
                                 28

-------
                             SECTION VI
                               RESULTS

The primary purpose of the sampling program at Marathon LeTourneau was to
define the total and fractional particulate penetration through a fabric
filter cleaning the emissions from an electric arc furnace.  The secondary
reasons for testing were to determine the effect of approximately doubling
the particulate loading to the baghouse on the total and fractional pene-
tration and to measure the influent and effluent total fluoride concen-
                                                   TM
trations to estimate the levels to which the Dacron   filter bags are ex-
posed during normal service.  In addition, the baghouse inlet and outlet
submicrometer particle concentrations were measured as a function of the
process cycle and the baghouse cleaning cycle to determine if periods of
high penetration are a function of the process cycle, the cleaning cycle
or both.  Finally, the inlet particle size distributions were measured as
a function of the process cycle.

TOTAL MASS MEASUREMENTS

The baghouse inlet and outlet particulate mass concentrations for the 3
pretest survey testing days and for the 10 regular testing days are pre-
sented in Table 5.  These concentrations were measured with total mass
samplers, impactors (without prefilters) and an impactor prefilter.

The data summary sheets with measured parameters and the calculated results
for the total mass and impactor samples are presented in Appendixes D and E,
respectively.  The properties of the baghouse influent and effluent flue
                                 29

-------
                      Table  5.   RESULTS OF PARTICULATE  SAMPLING AT  MARATHON LETOURNEAU
Teat
day
lb
2b
3b
1
2
3
4
5
6
7
8
9
10
68
8g
9«
No. furnaces
In operation
1
1
-
2
2
1
1
1
1
1
1
1
1
.
_
-
Pressure drop
across
compartment
No. 6, In. H20
_
.
-
_
_
3.50
_
3.40
3.40
3.24
3.12
3 35
3.34
.
_
-
Face
velocity,
ft/mln
3.32
3 48
-
3.39
3.58
3.37
3.34
3.35
3.41
3.36
3.56
3.43
3.42
.
_
-
Baghouse Inlet; concentration, gralns/dscf
Total mass
sampler
0.0627°
0.0804
-
0 1506
0.1438
0.0603
0.0729
0.0650
0.0672
0.0675
0 0736
0.0615
0.0617E
_
_
-
Impactor
run A
0.0579d
0.0414d
-
1.9185e
0 0765e
_
_
_
0.0369e
0.06646
0.0594e
0 0682*
0.05716
_
_
-
Impactor
run B
_
0.0903d
-
0.05948
0.09116
_
_
_
0.02876
0.10226
0.05386
0 05336
0 0497e
_
_
-
Impactor
run C
_
_
-
_
_
_
_
0.0500e
_
0.09476
0.04856
0.12866
0.08566
_
_
-
Impactor
run D
_

-
_
_
_
_
_
_
_
0. 0368s
0.14436
0.08686
_
_
-
Baghouse outlet, north stack,
concentration, gralns/dscf
Total mass
sampler
_
0.0019
-
0.0017
0.0021
0.0012
0.0016
0.0015
0.0013
0.0011
0.0016
0.0014
0.0012
_
_
-
Impactor
prefllter
0.0018d
0.00036d
0.0007d
o.oond
0.0011d
o.ooiod
o.ooiod
0.0007d
0.0009d
0.0008d
0.0013d
o.oond
0.0009d
0.0007d
0.0008d
0.0009d
Impactor
A
0.0022d
0.00025d
-
o.ooiod
0.0011d
0.0009d
0.0009d
0.0008d
0.0006d
0.0006°
0.0009d
0.0009d
0.0008d
0.0007d
0.0005d
0.0008d
Fabric filter
mass penetration,9
percent
_
2.3632
-
1.1288
1.4604
1.9900
2.1948
2.3077
1.9345
1.6296
2.1739
2.2764
1.9449
_
_
-
aCalculated from the Inlet  and outlet total mass concentrations.
b
 Pretest survey.
GEvldence of partlculate leakage around the filter indicating that the reported mass concentration may be lower than the actual mass
concentration.
 Andersen Impactor.
eUniverslty of  Washington Impactor.
 Sample was Inadvertently extracted  nonlsoklnetlccally
^lopactors run  overnight.

-------
gas are presented in Table 6.  The penetrations which are included in
in Table 5 were calculated from the inlet and outlet total mass
concent rat ions.

Examination of Table 5 shows that the inlet concentrations for the test
days during which there were two furnaces in operation were approximately
twice that of the runs in which there was only one furnace in operation.
The table also shows wide variations in inlet concentration measured by
the inlet impactors as a result of these samples being collected at
various points in the process cycle.  The variation in concentration over
a process cycle was measured during the pretest survey by taking a series
of total mass samples in succession over the cycle.  It was found that
the inlet concentration varied by a factor of 2.5 with the alloy addition
phase being the period of maximum concentration and the tap being the
period of minimum concentration as shown in Figure 10.

The mass penetration and the total mass sample outlet concentration sta-
tistics for the entire series of tests, for the subseries of tests with
two furnaces in operation and for the subseries of tests with one furnace
in operation are presented in Table 7.  These statistics show that the
penetration is lower even though the outlet concentration is higher
(40 percent) with the two furnaces in operation indicating the baghouse
particulate removal efficiency varies with inlet grain loading.  Thus
the baghouse dampens changes in the outlet concentration or emission
rate caused by variations in the inlet concentration.
        Table 7.  OUTLET CONCENTRATION AND PENETRATION STATISTICS
Tests
All
With 2 furnaces on
With 1 furnace on
Penetration, %
Mean
1.904
1.295
2.056
Standard
deviation
0.3862
0.2345
0.2263
Outlet concentration,
grains, dscf
Mean
0.0015
0.0019
0.0014
Standard
deviation
0.0003
0.0003
0.0002
                                 31

-------
                                           Table 6.  FLUE GAS PROPERTIES

Test No.
1
2
3
4
5
6
7
8
9
10
No. Furnaces
in operation
2
2
1
1
1 '
1
1
1
1
1
Influent
Volumetric
flow rate,
dscfm
164,406
166,623
154,056
153,606
152,550
154,066
154,311
166,142
151,374
157,354
Avg. gas
temp , F
107
131
140
128
132
134
130
127
155
134
Moisture,
percent
1.31
1.42
1.51
2.51
2.65
3.19
2.28
1.89
2.32
1.56
Effluent (North Stack)
Volumetric
flow rate,
dscfm
67,046
66,208
66,558
65,942
67,684
66,523
66,692
72,089
67,658
66,659
Avg. gas
temp , F
120
130
132
126
131
129
125
128
133
130
Moisture.
percent
2.22
1.47
1.55
1.53
1.99
1.85
2.15
2.43
2.46
2.10
Particulate
emission rate,
Ib./hr
0.994
1.220
0.664
0.930
0.848
0.737
0.642
0.995
0.830
0.676
to

-------
OJ
u>
                     0.10
                    0.09
                    0.08
                    0.07
                    0.06
                K   0.09
0.04
                    0.09
                    0.02
                    0.01
                        •M
                       tJ  L
      _  -lit
CHARGE |   MELT

    POWER
      ON
               SO
                          60
90
                                                 120
                                                              ISO
                                                   2nd
                                                  CHARGE
                                          2nd
                                         MELT
                                                        CTCLE  TIME, mlnutct
180 f
OXYGEN
                                           ALLOY
                                         ADDITION
                                                                                   TAP  AND
                                                                                   POWER  Off
                      Figure  10.  Inlet concentration as a  function  of events in the process cycle

-------
IMPACTOR MEASUREMENTS

The task of determining the average or representative inlet particulate
cumulative and differential size distributions is difficult because it
cannot be measured directly.  A direct measurement of size distribution
is impossible because a process cycle lasts approximately 3 hours and
the in-stack impactors which measure the size distributions were limited
to about 15 minutes sampling duration due to the high inlet mass concen-
tration causing overloading of impactor stages.  The problem was attacked
by making individual measurements at various points in the process with
samples taken during the major events of the process cycle.  Figure 11
shows the time in the process cycle over which each of the inlet impactor
samples was collected during each test day and also indicates the frequency
of sample collection during the entire testing program.  It shows that the
inlet was sampled for nearly every minute of the process cycle over the
testing sequence.  Since it was impossible to collect an ideal inlet
sample, it was necessary to composite several typical or average differ-
ential size distributions to enable calculation of the fractional penetra-
tion.  The construction of a representative inlet size distribution would
be further supported if day-to-day variations were not observed.  Although
this is not the case, the compositing of several runs appears to be the
best approach.  Figure 12 presents the measured mass median diameter
(HMD's) as a function of the process cycle and testing day.  From Figure 12
it is clear that variations in MMD's did occur on a daily basis and were
most pronounced immediately before the slag-off part of the cycle.
Figure 13 (a through d) shows the differential size distribution curves
for different test days for the sample collected during the first melt,
back charge, second melt, and tap.  These curves show that there was con-
siderable variation in the differential size distribution on a daily
basis.  The next step in constructing a composite inlet curve was to
average the curves for each part of the process.  These curves are also
presented in Figure 13 (a through d).  These average curves were then
weighted with respect to the time portion represented by their individual
                                 34

-------
                                                    AVERAGE  HEAT =190 mm



                              POWER  ON            BACK CHARGE          SLAG OFF    REBOIL    TAP



                                  |      _      ,      .*    .      .      .   *  .      ,1   .   *  .


                        INLET     °     2°    4°    6°     80    '°°    I2°   I4°   I6°    I8°   20°
                      RUN  NQ                           CYCLE  TIME, minutes



                         5                   .   RUNC  .




                                                                       RUN A              RUN B

w                        6                                             I	>              I	1
in


                                                RUN B        RUN C                        RUN A



                                                                          RUN C

                                                        RUN A          s-**~^*~^          RUN D
                         8                              I	1           I      I 1           1	1

                                           RUN A                          "—->s—

                                         '^^^^~^_   RUN B    RUN B        RUN B



                                      RUN C

                                                   RUN C  RUN A       RUN  B+D
                         10                        I	1	1        I	1



              SAMPLING  FREQUENCY: I 0 I I  121 I I 2 13121  3  |2I3|2)3|3| 2 I I 101213151 3 I2IH   0  I  I  I 3 |2|
                      Figure 11.  Time in process cycle at which  inlet samples were  collected

-------








E
4.
3
2










12.0
II. 0
10.0
9.0
8.0


7.0

6.0


5.0

4.0
3n
• w
2.0

1.0
°,
1
ROW
•
mf


M>
RUN2B
RUN IOD
I 	 1


RUN 2A
' '

RUN 6 A

1 RUN 9A 1 RUM QC -R"N 8B. J^66


QiiM7B|«"N9D RUN7C RUN IA
_ 1 1 t '
RUN 8C
-
i i i i i i 1 i i 1
> 20 40 60 4 80 100 120 4 140 160 | 180 * 20
BACK SLAG REBOIL TAP
fER CHARGE OFF
ON tYCLE TIMP minul«B
Figure 12.  Inlet HMD as a function of process cycle and
            testing day
                        36

-------
c
  .01
.001
           I    I   I  I  I  I I I
                                                       x  RUN 7B
                                                       O  RUN 9A
                                                       4  RUN 9C
                                                       D  RUN 90
                                                          RUN IOC
                                                          AVERAGE CURVE
               i   i  i  I  I i i I
   O.I
                           1.0                      10
                      PARTICLE AERODYNAMIC DIAMETER,/um
100
 Figure 13a.  Differential  size distribution curves  of  baghouse inlet
              aerosol during  first melt phase of process  cycle when
              one electric  arc  furnace is operating
                                   37

-------
               T	T
                                                 I II
                                                                 T—I—I I IT
                                                        X   RUN  5C
                                                       O   RUN  8A
                                                       A   RUN  IOA
                                                       ©   AVERAGE CURVE
u
€
Q
9
  .01
•o
.OOI
                 J—I I  I I  I I
                      i  i i  i i (
                                                              J	1—''''
   0.1
     1.0                       10
PARTICLE AERODYNAMIC DIAMETER./jm
                                                                         100
  Figure  13b.   Differential size distribution curves of baghouse inlet
                aerosol during back  charge phase of process  cycle when
                one electric arc furnace is operating
                                   38

-------
                                                          RUN 6A
                                                          RUN 7C
                                                          RUN 88
                                                          RUN 8C
                                                          RUN 9B
                                                          RUN 10 D
                                                          AVERAGE CURVE
.001
                           1.0                      |0
                      PARTICLE AERODYNAMIC  DIAMETER,/urn
  Figure 13c.  Differential size  distribution curves of baghouse  inlet
               aerosol during  second  melt phase of process cycle  when
               one electric arc furnace is operating
                                    39

-------
I
o
o
  .01
•a
.001
                                                        X   RUN 6B
                                                       O   RUN 7A
                                                       A   RUN IOB
                                                        •   AVERAGE COURSE
                                  J_
                                      J	L
                                              I  l I i I
                                                              J	1
   O.I
                           1.0                      10
                      PARTICLE AERODYNAMIC DIAMETER,/jm
100
  Figure 13d.  Differential size distribution curves of baghouse  inlet
               aerosol during tap phase of  process cycle when one
               electric arc furnace is operating

-------
part of the cycle to the complete cycle.  The composite inlet curves for
one and two furnaces in operation are presented in Figure 14.  The com-
posite inlet differential distribution curve for two furnaces in operation
was calculated by multiplying the composite inlet curve for one furnace
operation by the ratio of the average inlet concentration measured by the
inlet total mass sampler during two furnace operation to that average
concentration measured during one furnace operation.  The average dif-
ferential distribution curves in Figure 13 (a through d) were also used
to determine the differential concentrations for 1, 2, 4, 6, 8, and 10 \im
particles as a function of the process cycle.  These curves are presented
in Figure 15 (a through f).  These curves show the first melt to have the
highest concentration for all particle sizes and the back charge and the
tap phases to have the lowest concentrations for most sizes.

The composited inlet differential size distribution curves were then used
with the averaged outlet differential distribution curves for one and two
furnace operation (Figure 16) to calculate their respective fractional
penetration curves presented in Figure 17.  A comparison of the inlet
and outlet differential size distributions (Figures 14 and 16) shows the
curves to have somewhat similar shapes with a slightly larger outlet par-
ticle size (4 pm outlet and 2 ym inlet) having the maximum concentration.
The similarity in curve shape indicates that some of the influent aerosol
is passing through the baghouse without capture and would suggest bag leakage
during sampling.  The shapes of the fractional penetration curves are un-
usual in that they show the 1.0 urn particles to have the least penetration
while the 6.0 urn particles have the greatest penetration.  These shapes
would not be predicted by fabric filtration theory.  The lower penetration
of smaller particles as well as the higher penetration of the larger ones
indicates agglomeration of the smaller particles.  The agglomerates in the
effluent are believed to result mainly from fabric rear face dislodgment
of collected particles.
                                 41

-------
     0.2
u
«e
S
•o
  O.I
0.09
0.08
0.07
0.06
£  0.05
o   0.04
    0.03
    0.02
    0.01
                                                i     r     i      i
                                               X ONE  FURNACE  ON
                                               O TWO  FURNACES ON
                   23456     78
                    PARTICLE AERODYNAMIC DIAMETER,
                                                             10
   Figure 14.  Composited differential  size distribution curves of baghouse
              inlet aerosol for a process cycle with one and two furnaces
              operating (190-minute furnace cycle)
                                42

-------
     0.10
     0.05
u
10
o
w
O>
     0.01
o
a>
o

•o  0.005
-s.
E
    0.001
              20    40

               1st MELT
60..   80    100   120   140   160    180.  .200

     	 2nd  MELT 	
                           BACK
                         CHARGE

                           CYCLE  TIME, minutes
                                                                   TAP
 Figure 15a.  Concentration versus process cycle for 1 um particles
                                    43

-------
     0.10
     0.05
u
in
TJ
     0.01
o
o
•o  0.005
E
    0.001
              20    40    60    60     100    120    140   160   ISO   200
               1st MELT	Jli	2nd  MELT 	J A
                          BACK                                   TAP
                         CHARGE
                          CYCLE TIME, minutes
  Figure  15b.   Concentration versus process  cycle for 2 urn particles

-------
     o.io i	,	1	,	1	1	1	r
     0.05
 0
 10
 o


 a
     0.01
    0.005
    0.001
                                                                I
         0     20    40   60..    80    100   120    140   160   180   .200
               1st  MELT
t
BACC
2nd  MELT
                          BACK
                         CHARGE
i.r
  TAP
                           CYCLE  TIME .minutes
Figure 15c.   Concentration versus  process cycle for 4 urn particles
                               45

-------
     0.10
     0.09
M
C
'5
9
 •»
o

o
E
•o
     0.01
   0.005
    0.001
              20    40    60    80    100    120    140   160    180.   .200

               lat MELT	JJ-	2nd  MELT 	

                           BACK                                   TAP
                         CHARGE

                           CYCLE  TIME, minutes
 Figure 15d.  Concentration versus process cycle for 6 \im  particles

-------
     0.10
    0.05
u
-------
     0.10
     0.05
u
M
o

9
     0.01
•o  0.005

E
•o
    0.001
              20    40    60    80    100    120    140   160    180.   .200

               1st MELT	41*	 2nd  MELT 	
t
                           BACK
                         CHARGE


                           CYCLE  TIME, minutes
¥
  TAP
  Figure  15f.   Concentration versus process  cycle for 10 pm particles
                                    48
-------
     0.002
     0.001
    O.OOO9
    0.0008

    0.0007
•j;   0.0006
M
M
    0.0005
 -  0.0004
    0.0003
    0.0002
    0.0001
                                                  I     I      I      I
                                              A TESTS WITH ONE FURNACE ON

                                              • AVERAGE OF  TESTS WITH
                                                ONE  FURNACE
                                              X TESTS WITH TWO  FURNACES
                                                ON
                                              • AVERAGE OF TESTS  WITH
                                                TWO  FURNACES ON
                     23456789
                       PARTICLE  AERODYNAMIC DIAMETER,
10    II
       Figure 16.  Average outlet differential size distribution curves for
                  tests with one and two furnaces operating
                                   49
-------
  10

   9


   8


   7



   6




   5
«
u
0
a
z
UJ

a.
    I


  0.9


  0.8


  0.7



  0.6



  0.5.
                 X ONE  FURNACE  ON

                 OTWO  FURNACES ON
_L
_L
_L
_L
                            4567

                           PARTICLE SIZE.pm
                       8
                       9
                       10
        Figure 17.  Fabric filter fractional penetration curves
                              50
-------
FLUORIDE MEASUREMENTS

The inlet and outlet total mass samples collected during the first three
tests were analyzed for fluorides.  The results of the fluoride analyses
are presented in Table 8.  The total fluoride levels to which the bags
were subjected are indicated by the inlet concentrations.  The calculated
penetrations (19 to 37 percent) were much higher than the total mass pen-
etrations and are probably attributable to that portion of the fluorides
in the gaseous form which passes through the baghouse without significant
collection.  Despite the fluoride levels measured, which are believed to
                                                 TM
be representative of normal operation, the Dacron   bags are still in
service after 3 years without breakage problems.  However, the physical
characterization tests summarized in Table 1 show that the breaking
strength and elongation of a 2-year old bag compared to a new bag had
been reduced 15 to 20 percent.  It is impossible to ascertain whether the
reduction in breaking strength and elongation was the result of fabric
deterioration due to fluorides or wear due to bag shaking during cleaning.
                 Table 8.  RESULTS OF FLUORIDE ANALYSES
Test No.
1
2
3
Number of
furnaces in
operation
2
2
1
Inlet fluoride
concentration,
gr/dscf
0.001062
0 .0005651
0.0005218
Outlet fluoride
concentration,
gr/dscf
0.0002013
0.0002087
0.0001768
Penetration,
percent
18.95
36.93
33.88
CONDENSATION NUCLEI COUNTER AND DUST COUNTER MEASUREMENTS

A condensation nuclei counter (CNC) and an optical dust counter (DC) were
used to monitor the fine particulate concentration in the baghouse in-
fluent and effluent to determine the total and fractional penetration of
the fine particulate.  The fine particle measurements have been tabulated
in Appendix F.  The measurements on each test day have been averaged and
                                 51
-------
are listed in Table 9.  The average daily mean inlet and outlet CNC mea-
surements, which include particles over the range of 0.0025 pm to 0.5 pm,
indicate penetrations of 0.14 percent and 0.17 percent by number for one
and two furnace operation, respectively.  When the DC inlet (except Test 9,
which was suspiciously high) and outlet test day means were averaged, the
penetrations for the DC which counts particles ^0.3 urn were 4.9 percent
and 1.0 percent by number for one and two furnace operations, respectively.
Sizing with the CNC and diffusion denuder (DD) was inconclusive due to the
variability of the fine particle concentration of the influent and effluent.
Most of the inlet sizing with the DC was done during Test 9 which was
inordinately high and therefore not presented.  The inlet and outlet CNC
measurements for tests 9 and 10 and the DC measurements for tests 5 and
10 are presented in Figures 18 and 19, respectively.  The CNC inlet curve
in Figure 18 shows a fluctuation of the inlet concentration which does not
seem to correlate with events in the process or cleaning cycles.  The CNC
inlet measurements with the DD indicate that the majority of particles are
_>_ 0.015 pm.  The CNC outlet curve shows a strong dependence of concentra-
tion on compartment cleaning with every compartment cleaning corresponding
to a peak outlet concentration.  The CNC outlet sizing measurements indicate
particles in the range of _>_ 0.0025 and < 0.015 pm, few particles in the
range of >_ 0.015 and <_ 0.078 pm with the remaining particles > 0.078 urn.
The DC inlet measurements in Figure 19 show that the particles >_ 0.3 urn
seem to follow the process with their maximum concentration occurring at
"power on" and the beginning of the "second melt."  The outlet measurements
show little fluctuation for particles >_ 0.3 pm; however, the _>. 0.5 and
j^ 1.0 pm outlet particles show some relationship between concentration and
compartment cleaning, but the relationship is not always evident.
                                 52
-------
                       Table 9.  RESULTS OF FINE PARTICLE MEASUREMENTS ON THE BAGHOUSE INFLUENT AND
                                 EFFLUENT AT MARATHON LETOURNEAU
Ul
u>
Run No. furnaces
No. in operation
1 2
2 2
3 1
4 1
5 1
6 1
7 1
8 1
9 I
10 1
Influent
Particle concentration,
part./m3 x 1 0.0025 um.
            Dust counter, counts particles > 0.3 um.
           Concentration seems inordinately high compared  with the other  inlet DC concentrations.
-------
10
I
o
M
n


K
UJ
m
2
3
 0!
§
o
Ul
_l
u
    10'


     7

     5
   10°

     7

     9
    10"
    10
    10 o
    POWER
     ON
                                   IFM     ,t
                                   •     L*  \^^f
                                                   TEST 9  BAGHOUSE INFLUENT
                                                   SYMBOL       DD CUT SIZE. Um
                                                      X           NONE (OOOZ9)
                                                      A           OOIS
                                                      y           0021
                                                      Z           0033
                                                      O           COM
                                                             TEST 10  BACHOUSE EFFLUENT
                                               1
                                                  I
                                                                SYMBOL

                                                                  O
                                                                  A
                           DO CUT SIZE.Un

                              NONE (00029)
                              0 019
                              0 OJI
                              0 093
                              0 O«8
                              0 076
                         CCCCCCCCCC
             50 |
               BACK
              CHARGE
                      100
  TsoT  200
SLAG   REBOIlJ
                            OFF
                                    TAP
                                                 C  C C  C  C C • COMPARTMENT CLCANINt

                                                        L.
                                       POWER
                                        ON
250  I    300

  BACK
  CHARGE


CYCLE  TlME.oiinulM
|350
                                                                       400
                                                                               450
                                                                    REBOIL
                                                                         POWER
                                                                          ON
 500

 BACK
CHARGE
    Figure 18.   Condensation  nuclei counter measured concentrations  as a
                  function of the process cycle and compartment  cleaning
                                          54
-------
   10"
"E
oc
111
a
3
O
U
u
-I
u
   10

    7
    5
   10
                                                                TEST S  BAGHOUSE INFLUEN
                                                               TEST 10 BAGHOUSE EFFLUENT
                                           CC CC,CC  CC,C C  C a COMPARTMENT
                                                                             LEANINO
     0
   POWER
     ON
50 |
  BACK
 CHARGE
                      100
  | ISO   |
SLAG  REBOIL
 OFF
1
POWER
 ON
                                                         300
BACK
CHARGE
350  |  |  400
  SLAG  REBOIL
   OFF
                                                                                    450
                                                                              TAP
                                  CYCLE  TIME, minutes
       Figure 19.   Dust counter measured  concentrations  as a  function of
                     the process cycle and  compartment cleaning
                                         55
-------
                            SECTION VII

                            REFERENCES


1.  Federal Register.  Vol. 40, No. 185, September 23, 1975.

2.  Federal Register.  Vol. 39, No. 206, October 23, 1974.

3.  Calvert, S., C. Lake, and R. Parker.  Cascade Impactor Calibration
    Guidelines.  U.S. Environmental Protection Agency.  Publication
    Number EPA-600/2-76-118.

4.  Personal communication with Joe McCain, Southern Research Institute.

5.  Cass, R. W. and R. M. Bradway.  Fractional Efficiency of a Utility
    Boiler Baghouse:  Sunbury Steam-Electric Station.  EPA-600/2-76-077a.

6.  Instrument Instruction Manual for Condensation Nuclei Monitor Model
    Rich 100, Environmental/One Corporation, Schenectady, New York.

7.  Personal communication with Mr. Ernie Demetrie, Environment/One
    Corporation, Schenectady, New York.
                                 56
-------
            APPENDIX A




PARTICLE SIZE DISTRIBUTION CURVES
             57
-------
 or
 u
 5
 
-------
 E
 4
 e
 bJ
 z
 •f
 2
 >
 O
 O
   100
    90
    80
    70
    60
    50

    40

    30
    ZO
10
 9
 8
 7
 6
    09
    08
    07
    06
    0 5

    04

    03
    0 2
    O.I
                         = 2A INLET, FURNACES D AND E ON 2nd MELT
                         -?n IMIPTFURNACE ° ON 2rd MELT
                           o lrlLtl«FURNACE E ON 1st MELT
                         = 2 OUTLET
                     JL
                                         J_
                                                  _L
                                                              J..
            9     IO  IS 20   30  40  90  60  70   80     90   99
            PERCENTAGE OF MASS  LESS  THAN OR EQUAL  TO STATED  SIZE
Figure A-2.   Cumulative  particle size distribution of  fabric filter
              influent and  effluent during  test 2, two  furnaces in
              operation
                                 59
-------
 E
 4
 a
 o
 o
 a:
   100
    90
    80
    70
    60
    50

    40

    30
    20
10
 9
 8
 7
 6
 5

 4
    0.9
    08
    07
    06
    0.5

    O.4

    0.3
    0.2
    O.I
                            T	1	1	1	

                                 • = 3 OUTLET
                             _L
                                         J_
                                             J_
                                                        J_
             5     10   15 20   30  40  50  60  70   80     90    95
             PERCENTAGE  OF MASS  LESS  THAN OR EQUAL TO STATED  SIZE
                                                               98
Figure A-3.   Cumulative particle  size distribution of  fabric filter
              effluent during test 3,  one furnace in  operation
                                60
-------
     100
      90
      80
      70

      60

      90

      40


      30
      20
      10
       9
   E    8
   i   7
  or
  IU
  ui
  S
  o
  Z
  o
  o
       I
      09
      08
      07

      06

      0.5

      04


      03
     0 2
      O.I
T	1	1	1	

    • = 4 OUTLET
                                                   JL
                                                          J-
                                                               J_
              5     10  15  20   30   40   90  60  70   80     90   99
              PERCENTAGE OF MASS LESS THAN OR  EQUAL  TO STATED  SIZE
                                  98
Figure A-4.   Cumulative particle  size distribution of  fabric filter
              effluent during test 4,  one furnace in  operation
                                61
-------
  
-------
    100
    90
    80
    70

    60

    50

    40


    30



    20
     10
     9
     8

     7
     6

     5
T
            T
                     T
                            T
                                                              -T
 <
 a
 o
 o
 K
    09
    08
    07

    06

    0.5

    04


    03



    0.2
    0 I
A=6A INLET, FURNACE D OFF,
           FURNACE E ON 2nd MELT
O=6B  INLET, FURNACE D OFF, FURNACE E ON TAP

• = 6 OUTLET

              40
             5    10  15  20  30  40   50  60  70   80     90   95
             PERCENTAGE  OF MASS  LESS THAN OR  EQUAL  TO STATED SIZE
                                       98
Figure A-6.   Cumulative particle size distributions of fabric filter
              influent and  effluent during  test 6, one furnace in

              operation
                                 63
-------
 E
 i

 £C
 111

 111
 s
 Z

 0
 o
 K
    100
     90
     80
     70

     60

     50

     40


     30



     20
10
 9
 8
 7
 6

 5

 4
       I
     0.9
     08
     0.7

     06

     0.5

     04


     03
    0.2
     O.I
        T	1	1	1	1	1	1	1	1	1	1     I
          A-7A  INLET, FURNACE D OFF, FURNACE R ON ALLOY ADDITION
          Q = 7B  INLET, FURNACE D ON 1st  MELT, FURNACE E OFF

          D = 7C  INLET, FURNACE D ON 2nd MELT, FURNACE E OFF

          • =7 OUTLET

                                          PA Q
                      J_
                                      J_
                                     _L
                                              _L
                                                          J_
                                                                _L
       2     S     10   15  20   30  40   50  60  70   80     90   95     98
             PERCENTAGE  OF MASS  LESS THAN OR  EQUAL  TO STATED SIZE


Figure A-7.   Cumulative particle size distributions of fabric  filter
              influent and effluent  during test  7,  one furnace  in

              operation
                                 64
-------
  E
  4
 <
 5
 o
 O
 K
 UJ
    100 r
     90 L
     80
     70

     60

     50

     40


     30
     20
10
 9
 8
 7
 6

 5

 4
       I
     09
     08
     07

     06

     0.5

     04


     03
     0.2
     O.I
             -1	1	1	1	1	1	1	1	1	1	1	
             A =8A INLET, FURNACE 0 ON BACK CHARGE, FURNACE  E OFF
             O = 8B INLET, FURNACE D ON 2nd MELT, FURNACE E OFF
             Q =8C INLET, FURNACE D ON 2nd MELT. FURNACE E OFF
             x = 8D INLET, FURNACE D ON SLAG OFF? AND REBOIL,FURNACE E
             • = 8 OUTLET                                  OFF

                                  0
                       J	L
                                   _L
                                               _L
                                                   J_
                                                          _L
                                                                J_
              5     10  IS  20   30   40   50  60   70   80     90    95
              PERCENTAGE  OF MASS  LESS THAN  OR  EQUAL TO STATED  SIZE
                                                                98
Figure A-8.   Cumulative  particle size distributions of fabric  filter
              influent  and effluent during test 8,  one furnace  in
              operation
                                 65
-------
    E
    i
   UJ
   Z
   u
   I
   o
   o
   (t
      100
       90
       80
       70
       60

       SO

       40


       30
       20
10
 9
 8
 7
 6

 5

 4
       09
       0 8
       07
       06
       05

       04


       03 -
       0 2 -
       0 I
             —i	1—i	1	1	1	1	1	1	1	r
             A-9A INLET, FURNACE D OFF, FURNACE E ON ist MELT
             O -9B INLET, FURNACE 0 OFF,  FURNACE E ON 2nd  MELT
             D = 9C INLET, FURNACE 0 OFF, FURNACE E ON Ist  MELT
             X =90 INLET, FURNACE D OFF, FURNACE E ON 1st MELT
                  OUTLET
               JL
                            _L
                                    JL
                                        J_
                                            _L
                                                     _L
                                                            JL
                                                                 _U
               5     10  15 20   30  40  90  60  70   80     90   95    98
               PERCENTAGE  OF MASS  LESS  THAN OR  EQUAL  TO STATED  SIZE
Figure A-9.   Cumulative  particle size  distributions of  fabric filter
              influent and  effluent during test 9, one furnace in
              operation
                                 66
-------
        100
        90
        80
        70
        60

        50

        40

        30


        20
        04
        03
        0 2
        O.I
-1	1	1	1	1	1	1	1	1	1	1
 A: 10A INLET, FURNACE  D OFF, FURNACE E  ON BACK CHARGE
 O = IOB INLET, FURNACE D OFF, FURNACE E  ON 2nd  MELT
 D = IOC INLET, FURNACE D OFF, FURNACE E  ON 1st  MELT
 x =IOD INLET, FURNACE D OFF, FURNACE E ON 2nd  MELT
 • = 10 OUTLET
                          J	L
                 S     10  15  20   30  40  SO  60
                 PERCENTAGE OF MASS LESS THAN OR
                                  70    80     90
                                  EQUAL TO STATED
93
SIZE
98
Figure A-10.   Cumulative particle  size distributions of fabric filter
               influent  and effluent  during test  10,  one furnace in
               operation
                                  67
-------
   E
   a.
   oc
   UJ
   u
   2
   o
   o
   K
   Ul
100
 90
 80
 70
 60
 50

 40

 30
       20
 10
  9
  8
  7
  6
  5

  4
        I
       09
       08
       07
       06
       0.5

       04

       03
      0.2
       O.I
                                     	1	1	1	1	1	T

                                      As 6/24 TO 6/25, OUTLET NR # I
                                      O=6/28 TO 6/29, OUTLET NR#2

                                      X = 6/29 TO 6/30,  OUTLET NR#3
                    _L
                        J	L
                                       J_
                                               _L
                                                    _L
               5    10  IS  20  30  40   SO  60  70   80     90   95
               PERCENTAGE OF MASS  LESS  THAN OR EQUAL  TO  STATED  SIZE
                                                                98
Figure A-11.   Cumulative particle  size distributions  of  fabric filter
               effluent during  three special tests during which the im-
               pactors were run unattended overnight with one furnace
               in operation
                                  68
-------
              APPENDIX B




DIFFERENTIAL SIZE DISTRIBUTION CURVES
                69
-------
E


of

H
Ul


5

u
2
<
o
o
DC
    100

     70

     SO

     40

     30


     20




     10

      7

      5

      4

      3


      2
    0.7

    0.5
    QA

    0.3


    0.2
                                                      INLET FURNACE  D ON  ist  MELT
                                                      INL.KI, FURNACE  E ON  2nd MELT
                                                  = l  OUTLET
     O.I
                            I
,1
      0.0001
                           0.001                 0.01

                                      dm/d log D,groins/dscf
                     0.10
1.0
        Figure B-l.  Differential particle size  distribution of baghouse influent and

                     effluent during test 1,  two furnaces in operation
-------
    100


     70


     SO

     40

     30



     20





     10


      7


      5

      4


      3



      2
     0.7


    0.5

    0.4


    0.3



    0.2
T	1—I  I  I I I |	1	1	1—I 1  I I I |	1	1	1  I I I I U


            X=2A INLET, FURNACES D 8 E ON 2nd  MELT

            A=2B INLET, FURNACE 0 ON  2nd  MELT


            • =2 OUTLET
                 T	1—I  I I I
E
4.
o
o
tc
111
     O.I
                        I I
                            I
      0.0001
                           0.001                 0.01


                                      dm/d log D,groins/dscf
                                 0.10
1.0
         Figure B-2.
                     Differential particle size distribution of baghouse  influent and

                     effluent during test 2, two furnaces in operation
-------
IK

UJ

H

Ul
o


u

2
<
z
>
o
o

ui
     100


     70


     SO

     40

     30



     20
     O.I
                                               1  ' ' ' I


                                               3  OUTLET
                              il
      0.0001
        Figure B-3.
       0.001                 0.01


                   dm/d  log D,groins/dscf
0.10
1.0
Differential particle  size  distribution of baghouse effluent during

test 3, one furnace  in operation
-------
OJ
          Or
          Ul
          H
          iu
100

70

SO
40

30

20



 10

  7

  5
  4

  3

  2
          i     i
          oe
          3   0.7

              0.5
              0.4
              0.3

              0.2
                                                     I  I  I I I I
                                                                                          I    1   I  I  I I I 1.
                                                                              4 OUTLET
               O.I
                         I
i il
                0.0001
                        0.001                  0.01

                                   dm/d log 0,groins/dscf
                       0.10
1.0
                   Figure B-4.
                  Differential particle size distribution of baghouse effluent during
                  test 4, one furnace in operation
-------
100

 70

 SO
 40
 30

 20


 IO

  7

  5
  4
  3

  2


   I

0.7

0.5
0.4
0.3

0.2
                                                                                     I  I
UJ
2

5

u
o
ae
                                                0 = 5C  INLET, ™*g J  ™cBACK  CHARGE

                                                •=5 OUTLET
     O.I
                         I
,1
      0.0001
                       0.001                 0.01

                                   dm/d log D,groins/dscf
                      0.10
1.0
     Figure B-5
                      Differential particle size distribution of baghouse influent and
                      effluent during test 5, one furnace in operation
-------
o
in
H
IU
O
O
oe
ui
    100

     70

     50

     40

     30


     20
10


 7

 5

 4

 3


 2
     0.7


    0.5

    0.4

    0.3


    0.2
     O.I
                                      i  i i  ii i
      0.0001
                                            X = 6A INLET. FURNACE D OFF, FURNACE  E ON  2nd MELT

                                           A = 6B INLET, FURNACE D OFF, FURNACE  E ON TAP

                                           O = 6 OUTLET
                         I
,1
                       0.001                  0.01

                                   dm/d log D,grains/dscf
                       0.10
1.0
        Figure B-6.  Differential particle size distribution of baghouse  influent and

                     effluent  during test 6, one  furnace in operation
-------
DC
Ul
H
Ul
2
V
o
o
oc.
     100

     70

     SO
     40

     30


     20
    0.3

    0.2
                     I  I  I I I I I       I    I   I  I  I I  I I I       I    I  I I I  I I

                     X=7A INLET, FURNACE 0 OFF, FURNACE E ON ALLOY ADDITION
                     A=7B INLET, FURNACE D ON lit MELT, FURNACE  E OFF

                     O = 7C INLET, FURNACE D ON 2nd MELT, FURNACE  E OFF
                     • =7 OUTLET
     O.I
       I
il
      0.0001
      0.001                  0.01

                 dm/d log D,groins/dscf
                      0.10
1.0
          Figure B-7,
Differential  particle size distribution  of  baghouse influent and
effluent during  test 7,  one furnace  in operation
-------
E
 =t
of
Hi
o
o
o
oc
100

70

50
40
30

20


 10

  7

  5
  4
  3

  2
     0.7

     0.5
     0.4
     0.3

     0.2
                                                 I I I I      I   I   I  I  I  I I I I       I    I   I  I  I I I I

                                                 X = 8A INLET, FURNACE D ON BACK CHARGE, FURNACE E OFF
                                                  §=8B INLET, FURNACE D ON 2nd  MELT, FURNACE E OFF
                                                  =8C INLET, FURNACE D ON 2nd  MELT. FURNACE E  OFF  .
                                                 + =8D INLET, FURNACE  D  ON SLAG OFF AND REBOIL,
                                                           FURNACE  E  OFF
                                                  -OIL OUTLET
     O.I
                         I
,1
      0.0001
         Figure B-8.
                        0.001                  0.01

                                    dm/d log D,groins/dscf
                       0.10
1.0
                 Differential particle size  distribution of baghouse influent and
                 effluent during test 8,  one furnace in operation
-------
oo
           E
            4.
            •»
           ae
           Iti
           i-
           bl
           u
           o
           
-------
vo
           o
           u
           H
           Ul
o
2

I
O
ui
100
70

SO
40
30

20


 10

  7
  5
  4
  3

  2
                0.7

                0.5
                0.4
                0.3

                0.2
                O.I
                                                                       I    I   I  I  I 1 I I I      I   I  I  I  I  I
                                                                    X:IOA INLET, FURNACE 0 OFF.
                                                                               FURNACE E  ON BACK CHARGE
                                                                    A=IOB  INLET, FURNACE D OFF, FURNACE  E
                                                                                              ON 2nd MELT
                                                                    O-IOC  INLET, FURNACE D  OFF,
                                                                                FURNACE E ON HI  MELT
                                                                    + =10 D INLET,  FURNACE  0 OFF, FURNACE  E
                                                                                               ON 2nd  MELT
                                                                                 • =10 OUTLET
              i	i
                              I
                                               ,|
                  0.0001
                   Figure  B-10.
                             0.001                  0.01

                                         dm/d  log D,groins/dscf
                                                                      0.10
1.0
                       Differential particle size distribution  of  baghouse influent  and
                       effluent during  test  10,  (one furnace  in operation)
-------
§
E
i


bl
t-
bl



5


o
         o
         o
         oe
         ui
                                                          T
                                                           A NR#I   6/24  TO 6/25


                                                           O NR#2   6/28  TO 6/29


                                                           X NR#3   6/29  TO 6/30
              O.I
                             I
i il
               0.0001
                           0.001                 0.01


                                      dm/d log D,groins/dscf
                       0.10
                                                                                               i i  11 i
1.0
             Figure B-ll.  Differential particle size distributions of baghouse  effluent  during  three

                           special tests during which the impactors were run unattended overnight with

                           one furnace in operation
-------
                         APPENDIX C
ANDERSEN IN-STACK IMPACTOR SUBSTRATE ANOMALOUS WEIGHT GAINS
                           81
-------
   e
   M
6.0


5.0


4.0


o 0


2.0


1.0
            NOTE THAT SHADED PORTION INDICATES MASS
            COLLECTED ON STAGE IN IM FACTOR SAMPLING
            FILTERED  FLUE  GAS
                     2345
                       STAGE  NUMBER
Figure C-l.  Mass collected on  stages of impactors sampling
             flue gas and filtered  flue gas, outlet  test  1
     v>





60
50
40
30
20
i n

O
•

-
-
.

ftVC<



AV\>
\\\\



^
^




^
^\\V




\\\\N
\\W











S\\M

NOTE THAT
SHADED PORTION
INDICATES
MASS
COLLECTED ON
STAGE IN IMPACTOR
SAMPLING
FLUE GAS






\\\\\






WWW
FILTERED






^^^^^^n
                       ?    3    4    5
                         STAGE NUMBER
Figure C-2.  Mass collected on stages of impactors sampling
              flue gas and filtered  flue gas, outlet test  2
                           82
-------
         6 0
         50
         40
         5.0
         20
         1 0
              NOTE  THAT SHADED  PORTION  INDICATES MASS
              COLLECTED ON STAGE IN  IMPACTOR  SAMPLING
              FILTERED FLUE GAS
            V\\\V t t ti' v n \v
                        2345
                          STAGE NUMBER
Figure C-3.   Mass collected  on stages of  impactors sampling
              flue gas and  filtered flue gas,  outlet test 3
         6 0 |- NOTE THAT  SHADED  PORTION INDICATES  MASS
              COLLECTED  ON STAGE  IN IMPACTOR SAMPLING
             .FILTERED  FLUE  GAS
         40 -
3O
2.0
I.O
0
m










\\\\\


V\\\\\ 1
                        2345
                           STAGE  NUMBER
Figure C-4.   Mass collected  on stages of impactors sampling
              flue gas and  filtered flue gas,  outlet test 4
                           83
-------
E
w
        6.0


        9.0


        4.0


        3.0


        2.0


        1.0
         NOTE THAT SHADED PORTION INDICATES MASS
         COLLECTED ON STAGE IN IMPACTOR SAMPLING
         FILTERED  FLUE  GAS
                       2945
                          STAGE  NUMBER
Figure C-5.   Mass collected on stages of  impactors sampling
              flue gas and  filtered flue gas,  outlet test  5
        6.0

        so
          NOTE THAT SHADED PORTION INDICATES MASS
          COLLECTED ON STAGE IN IMPACTOR  SAMPLING
          FILTERED  FLUE GAS
        4.0 -
3.0
2.0
1.0
o 1


v\\\V



,\\\\\





VVVWItumi
                       2    3    4    S    6
                          STAGE  NUMBER
Figure C-6.   Mass collected on stages of  impactors sampling
              flue gas and  filtered flue gas,  outlet test  6
                           84
-------
     E
     en"
6 Oi-

   I
5 0 '


4.0


3 0


20


I 0
                 NOTE THAT SHADED PORTION INDICATES MASS
                 COLLECTED ON STAGE IN IMPACTOR SAMPLING
                 FILTERED FLUE GAS
                                             I     I
                       23    4    5    6    7    F
                          STAGE NUMBER
Figure C-7.   Mass collected  on stages of  impactors sampling
              flue gas and  filtered flue gas,  outlet test  7
         60  •

         5O  -


         4O
        NOTE THAT SHADED PORTION INDICATES  MASS
        COLLECTED ON STAGE IN IMPACTOR SAMPLING
        FILTERED FLUE GAS
e
w 30
S
2.0
1 0
O

.













                        2345
                          STAGE NUMBER
Figure  C-8.   Mass collected on stages of  impactors sampling
              flue gas and  filtered flue gas,  outlet test  8
                           85
-------
       6
       w
               NOTE THAT SHADED PORTION INDICATES MASS
          60r COLLECTED ONSTAGE  IN IM FACTOR SAMPLING
               FILTERED  FLUE  GAS
          5 0
40


5 0


2.0
             I
                         2345
                           STAGE NUMBER
Figure C-9.   Mass collected  on stages of impactors  sampling
              flue gas and  filtered flue gas, outlet test 9
6 0


50


40
       8  30
          20
          I 0
                NOTE THAT SHADED PORTION INDICATES MASS
                COLLECTED ON STAGE IN IMPACTOR SAMPLING
                FILTERED  FLUE  GAS
-
s\\\V

l\\\\v

TTTTT

V\\\\\l





tVrtYfcWffl
                        23456
                           STAGE  NUMBER
Figure C-10.   Mass collected  on  stages of impactors  sampling
               flue gas and  filtered flue gas, outlet test 10
                           86
-------
5.0
         4.0
              NOTE THAT  SHADED PORTION  INDICATES MASS
              COLLECTED  ON STAGE  IN IMPACTOR SAMPLING
              FILTERED  FLUE GAS
     VI
     V
                            349
                          STAGE NUMBER
Figure C-ll.
      Mass  collected on stages  of impactors  sampling
      flue  gas and filtered  flue gas, outlet  night
      run 1 (6/24 - 25/76)
       OT
       in
          50 -
          4.0 •
          20 -
          I 0  -
        NOTE  THAT  SHADED  PORTION INDICATES  MASS
        COLLECTED ON STAGE IN IMPACTOR SAMPLING
        FILTERED FLUE GAS



























IVVVV






s\\\S\






kvvvv






k \Y\\\






"~|
                         2345
                           STAGE  NUMBER
Figure C-12.
      Mass  collected on stages  of impactors sampling
      flue  gas  and filtered  flue gas, outlet night
      run 3 (6/29 - 30/76)
                           87
-------
5.0
4.0
2.0
1.0
n
- NOTE THAT SHADED
COLLECTED ON STAGE
FILTERED FLUE GAS

-
-

^\\Vs






NSNNV
PORTION INDICATES MASS
IN IMPACTOR SAMPLING

\\\\s




^


sW

\\\\
                    2345
                       STAGE  NUMBER
Figure C-13.
Mass collected on stages  of  impactors sampling
flue gas and filtered  flue gas, outlet night
run 3 (6/29 - 30/76)
                         88
-------
             APPENDIX D
CALCULATOR INPUTS/OUTPUTS FOR TOTAL
         MASS MEASUREMENTS
                 39
-------
                     HP 65  DATA FORM      R.A.C  TWIN.




                             INIJJT      X-	
DATF.
                           OUTLET
              INPUT
  Ah" H00
    Run




OUTPUT
                                                                 ±
                                                            (ML)
  Vcl  (ML)
                                                      V.STD (Ft3)
  Vm  (Ft)
                                                      C.ffrn/Ft3)
  l\n
  Pb
                                                      7. Dry Gnc
  Mn  (mg)
                                                      M.W.  (vet)
  % CO
       y
  7. CO
  TSTK (R)
  Ps
                      .J
                                                        D.
    V (FPM)
                                                      Wp  'i-rC

7. 0?
'"?• 3 ^ ^...,
.3 // V.
r..
A.
^9- •' "
   O(min)
  An  (Ft2)
Area Duct
             (ft2)
                                         90
-------
                   HP  65   DATA FORM


                           INLET
R.A.C  TRAIN.
DATE ^/' ^ OUTLET
INPUT
««BMVHHiM
Ah" U00 tJ.Aaf
Vcl (ML) >7rf.
Vm (Ft3) &J3,C>Vy
TRI (°R) ^^
Pb ("HO jC.c'r
Mn (me) ££. . 9
2 //f1?O
Ps ("H.O) O
z
X Run 1?
OUTPUT
Vu510 (ML) # 6/
..5TD /r.3. ^
X'ai (FL ) ^Lo^-,77
C.ffrn/Fu3) "?'//
             2
Arna Duel  (Kt )
                                        91
-------
                     HP 65  DATA FORM     R.A.C  TRAIN.


                             INIJJT       X
DATE
              INPUT


  Ah" H00     0*373
                           OUTLET
    Run


OUTPUT
                                                           (ML)
  Vcl  (ML)
                                                     Vai5TD (Ft3)
  Vm
Tin <°R)
                                                         H0
  Pb  ("HG)
                                                     % Dry G«s
                                                       M.W.  (wet)
  7. CO.
                                                         E.A.
    CO
           0,?
  TSTK (  R)
    V (FPM)
                                                         "STD~
  Ps  <"H20)
  K
   G(n.in)
  An  (Ft2)
                2
  Area  Duct.  (Ft )
                                        92
-------
                    IIP 65  DATA  FORM


                            INIJZT
             R.A.C  TRAIN.
DATE

OUTLET
             INPUT
  Ah"
    Run  ft


OUTPUT
                         V,,51'0 (ML)
  vci OIL)
                               (Ft3)
     (Ft)  3 jo.
                                                     7. 1120
  Pb ("HG)  .
                         7. Dry Gns
  Mn (ing)
                         M.W.  (vet)
                                          . .  • ..
                                          '  *  X
  %°
  % CO
  TSTK
     ("H20)
                       ,,  .
                                                     D
                                                     D-
                                                     -/, C.A.
                         ~7~i,TD~T^T"



                         ~wiT*fi'rt/hr.)
   O(min)


  An  (Ft2)
  Area Duct (Ft )
                                        93
-------
                     HP 65  DATA FORM     R.A.C  TRAIN.




                             INIJ2T     -V	
DATE
              INPUT
  Ah"
OUTLET
    Run




OUTPUT
                                 (ML)    / 90
  Vcl  (ML)
                          V*5™  (Ft3)
  Vm  (Ft)
                          Cs8rn/Ft3)
   m  (°R)
  Pb  ("HG)
                          % Dry  Gas
                                                       M.W.  (wet)
  ''' C°
                          D.  (ltS/F?)
                                                       7. n.A.
  % CO
  TSTK  (°R)
  Ps  <"H20)
                          V  (FPM)
                          Wp~XPcr£/hr.)  79.
  An  (Ft')
        Duct  (Ft2)
-------
                     HP 63   DATA FORM
                              1NIJET
                                          R.A.C  TRAIN.
DATE
       £/&*/'}&>
              INPUT
Ah" H00
OUTLET
                                                     OUTPUT
                                                         vw51'0 (ML)    ^,
       OIL)      ;c-c>
                                                      'Vm5™  (Ft3)    Jt.A
      (Ft3)
                                                       C.8rn/Ft3)
  Pb  ("KG)
  Nn
                                                         X
                                                         Dry  Gas   9 Jr. /S""
                                                       M.\;.  (vet)    ^ v_ c'
  "'' C°
       2
             S.
  TSTK
                                                         V (FPM)
                                                        ~S!D~
                                                         Wp  Pc
         a.
   G (in in)
  An  (Ft2)
  Arr:a  Duct  (Ft ")
                                          95
-------
     HP 65   DATA  FORM


              INLET
                                          R.A.C   TRAIN.
DATE
              INPUT
  Ah" H00
              OUTLET
Run
                                    OUTPUT
                                        V,,5™ (ML)
  Vcl  (ML)
67
  Vm  (Ft)
  Pb  ("HG)
  TSTK  (R)
  Ps  ("H20)
V*5™ (FC3)
                                        % Dry Gae
                                                        M.U.  (wet)
                                                       ITP'/F?]
                                                        'L E.A.
                                                        V (FPM)
                                        Wp^'rt/hr.;
                                                             6&6
   G(min)
  An  (Ft2)
                o
  Area  Duel  (Ft )   */&,&¥
                                          96
-------
                     HP 65  DATA FORM




                             INIJET
                          R.A.C   TMIN.
DATE
           /< x A •-
           ei •* ./ 7 C?
             OUTLET
              INPUT
  Ah" 11.0
    Run ^




OUTPUT
                                              (ML)
                                                                       '
  Vcl  (ML)
97-5"
    Vm5™ (Ft3)   ^97,
  Vm  (Ft)
                                        C.8rn/FL3)
  Tm
                                        7. I120
  Pb  ("HG)
  Mn
                                        7. Dry Gns
                                        M.W.  (vet)
  7, C0
      ?
 , SV
                y v,
                                        D.  (lb'/Ft3)
                                                        Vo C.A.
  7. CO
  TS1K  (°R)
                                        V (FPM)
                                                        Wp
  rv"2

                                                    L/. 6
   O(m in)
  An  (Ft)
    ;c:£i  Duct  (Ft2)
                                           97
-------
                  HP 65   DATA  FORM


                           INLET
R.A.C  TRAIN.
DATE
Ah"
Vcl
Vm
^ /«^3/76
INPUT
HO <5>'36vr
(ML) 7/
(Ft3) /JO.J/
OUTLET Run # ^*"
OUTPUT
' - . Vw51'0 (ML)
V*5TD (Ft3)
3 * ' Cs9rn/Ft3)
•
3,37
sJ3.**
o.e&rc
•.
Xni \ R) ^J«T
(mg) ^/V i , v5
% Dry Gas
H.\7. (wet)
9->.*
-------
                   HP 65  DATA FORM




                           INLET
R.A.C  TllAIN.
DATE
Ah"
Vcl
Vm
Tra
Pb
Mn
/ ^^
5 /&"*/"?& OUTLET X Run tf "^
INPUT OUTPUT
H.O 3, 3 AS- • ' V,,51'0 (ML) £^3
(ML) XViy Vsn TD (Ft ) .?t.
-------
                     HP 65  DATA FORM     R.A.C  TRAIN.


                             INIJET      •*	
DATE
              INPUT
  Ah"
OUTLET
    Run


OUTPUT
                                 (ML)
  Vcl  (ML)
                           Vm5TD (Ft3)
  Vm  (Ft)
  Tn  (°R)
                           1 "2°
  Pb  ("1IG)
                           % Dry Gns
  Mn
                                                        M.W.  (vet)
    CO
  K
                           V (FPM)
TSTK
Ps ("
(°R) ^^
H20) US
Q Dry (Ft J) ^ r #«
Vp ^Sf£/hr.) ^.,.7?
PV* /./y6 I /;*.°±
     (min)
  An  (Ft )
                2
  Area  DUCL (Ft")
                                          100
-------
HP 65  DATA FORM



        INLET
                                         R.A.C  TRAIN.
DATE
.y, 7
                                                     M.1J. (vet)
  % C0
             y,
                                 .  ,/r. .
                                 D. (   /l-t )
                                                  .
                                                 .» ' v
                . -r
                                                     V. E.A.
  % CO
  TS1K
  Ps  ("
                                 V (FPM)
                                 __Dry

                                 Wp^fart/hr.)   ., -,
               . r- r
   O (in in)   ,3^6
  An  (Ft2)
       Duct  (KL ")    .;  -., j £,
                                        101
-------
DATE
      0' * 3»i / 76
              INPUT
  Ah" 1U
 •«M~B««M>M^«M««
HP 65  DATA FORM     R.A.C  TRAIN.




        INIJ2T      X	





        OUTLET 	       Run fl    7




                               OUTPUT




                                      ~'~  (ML)
  Vcl  (ML)
                                                      V5TD (Ft3)
  Vm  (Ft)
  Tm
                                                      I H20
  Pb  ("HG)
                                                      7. Dry Gas
  Mn  (nig)
                                                      M.W.  (wet)
  7=, co
      ?
                                                      D.  (lba/Ft3)
                    g"
                                                        'L T..A.
  7. CO
TSTK  ( R)




Ps  ("H..O)
                                                      V (FPM)
                                                        Wp
                                                                   //
  K
     (in in)
  An  (Ft2)
  Area  Duct.
                                         102
-------
                    IIP 65  DATA FORM



                            INLET
                                           R.A.C   TRAIN.
DATE
                            OUTLET
              INPUT
Ah" H00
  •	i* •  i
    Run 9



OUTPUT
                                                         Vw5™ (ML)
  Vcl  (ML)
  Vn  (Ft)
  Tw  (°R)
  Pb  ("HG)
              3C.C-/
  TSTK
  Ps  C"H20)
   O (in in)
  An  (I't2)
  Ai-c;a  Duct  (Ft ')
                                                       Vm5TD (Ft3)
                                                       Cs8r"/Ft3)
                                                       % Dry Gns
                                                         M.W.  (vet)


                                                        T,lbs i,,'J~*
                                                         7. E.A.
                                                         V (FPM)


                                                        T~STD~
                                                           Dry
                                                       Wp kPe
                                         103
-------
                  HP  65   DATA  FORM




                           INLET
R.A.C  TRAIN.
DATE ^/*Sy76 OUTLET
INPUT
Ah" H.,0 O. VA.
Vcl (ML) vTJ/V
Vm (Ft3) /39./^6
*W«« f T)\ ^ £ f
Aiti v K^ v5 oo
Pb ("HG) ^./^
Mn (rag) ^<£?.3
. o'
Run # o
OUTPUT
Vt» (ML) 
-------
                   HP 65  DATA FORM
                           INIJ:T
R.A.C  TRAIN.
- DATE & /£ &/7&
INPUT
Ah" H00 c3. 667
Vcl (ML) /&(> "3
Vm (Ft ) 337, £3S~
OUTLET ^ Run tf Q
OUTPUT
. vw51'0 (^^.) 7. ^
5TD .3 .
Vai QI'L ^ .j'-'i-/<-^>
_ Srn ,r 3. ,
Cs /Ft ) (-> , f-trvt?
•
Pb ("1IG) £C f/&
Mn (^s) 33./
% co? ^ ^^
% °? y9'^
% co ^.^
TSTK (°R) ^"£$
Ps ("H20) C
% Dry Gns -^7, ^-7
M.U. (vet) ,^r-. /.4.
D. (lb3/FtJ) 4..^%.?y
Vo F. .A. t;
V (FPH) ^?7?
0^°^ ^AA'V
Up tet/br.) ^^^5,
* I
K-^ i •* ^*""
(^ . e'vj
G(min) ,3£ O
p
An (1't") atrt~d3y/
Area Duct  (FL )    ,/i:
                                        105
-------
                    HP  65   DATA FORM     R.A.C  TRAIN.


                             INLET       X
DATE
              INPUT
  Ah"
  Vcl  (ML)
  Vm (Ft)
  Tm  (°R)
      ("HG)
  Mn  (mg)
  %C°
    co
   G(min)
  An  (Ft  )
                2
  Area  Duct  (Ft )
  OUTLET
-------
                     HP 65  DATA FORM     R.A.C  TRAIN.




                             INIET	
DATE
              INPUT
 Ah"  H00
••i—•• • •• • ^^*
  Vcl  (ML)
  Vm  (Ft)
  Tn
  PL  ("no
  K
   G(inin)
  An  (rf)
                            OUTLET
  Arc-a  Duct  (Kl ')   -sr?.Jt^
    Run




OUTPUT
                                                       Vw51'0 (ML)
                                                      v»5TD  (Ft3)
                                                      Cs8rn/Pt3)
                                                         Dry  Gno
                                                       M.W.  (vet)
                                                       n
                                                       D-
                                                       7. E.A.
V PO V\ ^ ^*N
TS1K (°R) J"^3
Ps (MH20) O
V (FPM) ^y
Q ^X (Ft ) ^ -> / /-v
Dry ^ -> e '
WP Wrt/hr.) ^95l.c
                                         107
-------
                     HP 65  DATA FORM


                             INLET
             R.A.C  TRAIN.
DATE
              INPUT
  Ah"
OUTLET
    Run


OUTPUT
                                 (ML)     vT-
  Vcl  (ML)
                          V*5™  (Ft3)
  Vm  (Ft)
  Tm  (°R)
  Pb  ("HG)
                             Dry GAG
      (mS)
                           M.W.  (wet)
                                                        D.  (lba/Ft3)
                                                        •JL E.A.
  TSTK (R)
                                                        V (FPM)
                           Vp tyert/hr.;
  Ps  ("H20)
   G(n,in)
  ATI  (Ft2)
                2
  Area  DiicL (Ft )
                                         108
-------
                      IIP  65   DATA  FORM
                                        R.A.C   TRAIN.
- DATE
^/y?o/75
                               INIJET
                           OUTLET
                                                                   /6
               INPUT
   Ah"
                                                     OUTPUT
                                                     V,,51'0 (ML)
    Vcl (ML)    Xv?>?/5*
                                                      Vai5TD (Ft3)
    Vn, (Ft)
                                                      Cs8rn/Ft3)
    Pb ("HG)
                 .63
                                                      7. Dry  Gno
                                                         M.W.  (wet)
                                                         D
                                                         D-
    TSTK (R)
                                                         V 
-------
              APPENDIX E
CALCULATOR INPUTS/OUTPUTS FOR INERTIAL
         IMPACTOR MEASUREMENTS
                 110
-------
                                       ANDERSEN IMPACTOR
Date
                    Run #
                           o
    Sample volume  at  STP  (ft )

    Moisture              (%)

    Concentration  (grains/ft3)

     Lnpactor flow rate (acfm)
                              £<3
                     Location  y/y/e:
                     Orifice
                     bar.  press.  ("Hg)
                     Mw
                     avg.  Pm (-"Hg)
                     avg.  Tm ( F)
                     H20 (grams or %).
                     meter volume  (ft  ]
                     avg.  Ps (±"H90)
                     avg.  Ts (°F)
                     time  (minutes)
                     correction factor
     Stage
           Net weight
              (gm)
7.  on
stage
Size cutoff
   (urn)
7. $ stated
  •size
dm/d log D
                                                                          Geo. Mean
   expander
                  f~C V
                      of 76°
                          y.v???
33
                                                     . 717;
              O.
                                 A 7-TV7
                                    , /Jfl
                                                 a. A
                                                            0,1127
     Total
                                           111
-------
                                    ANDERSEN IMPACTOR
Date
                 Run #
 Sample volume at STP  (ft )

Moisture              (7.)

Concentration (grains/ft3)

 Impactor flow rate (acfm)
                               A

                               O. ooi&
                     Location
                     Orifice      £
                     bar.  press.  ("Hg)
                     Mw
                     avg.  Pm (-"Hg)
                     avg.  Tm ( F)
                       0 (grams or %).
                       ter volume  (ft  )
                     avg.  Ps (±"H20)
                     avg.  Ts (°F)
                     time  (minutes)
                     correction factor
                                                                   =  0
                                                                      /
  Stage
           Net weight
              (gm)
7. on
stage
                                Size cutoff
7. ^ stated
  •size
dm/d log D
Ceo. Mean
 ( /im)
Probe  &
expander
                      I8.67K
                       3.
                                 8.F99C
                                              73. V9J9
                                   O.&003.
                       '•*:«> 
-------
                                    ANDERSEN IMPACTOR
 Dace     *^^ Run t

 Sample volume at STP (ft)

 Moisture             ft)

 Concentration (grains/ft3)

 Xmpactor flow rate (acfm)
                     Location
                     1 /'M-V.
                     Orifice D
                     bar. press. ("Hg)
                     Mw
                     *vg. Pm (-"Hg)
                     avg. Tm (0F)
                     HjO (grams or %).
                     meter volume (ft )
                     avg. Ps
                     avg. Ts
                     time (minutes)
                     correction factor
                                                          8-3
  Stage
Net weight
   (gn>)
T. on
stage
Size cutoff
   (urn)
^ stated
•size
dm/d log D
                                                                       Geo. Mean
Probe  &
expander
           O.
                  O
                                                               o/'/o
    4
                                                               0/06
                                                            5-.s-j.ffjT
                                                            0.0*38
                                                             A
                                                ,0000
  Total
                                       113
-------
                                        ANDERSEN IMPACTOR
         Dace
                     Run #
    Sample volume at STP (ft3)

    Moisture             (%)

    Concentration (grains/ft3)

     Impactor flow rate  (acfm)
                     Location
                     TiM_ /?//- /7A/  >"w"1
                     Orifice   b
                     bar. press.  ("Hg)
                     Mw
                     avg. Pm (-"Hg)
                     avg. Tm (°F)
                     H20 (grams or %)3
                     meter volume  (ft  )
                     avg. Ps (+"H_0)
                     avg. Ts (°Fr
                     time (minutes)
                     correction factor
                                                                               -M

                                                                             3 o i j&
                                                                             OT8.-78-
      Stage
                   Net weight
                      (gn)
7. on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
                                                                           Geo. Mean
ft-
   Probe   &
   expander
                                                      Ill A
                                                                 . 0*39
-------
                                          ANDERSEN IMPACTOR
Data

Sample volume at STP (ft3)   -

Moisture             (%)     -

Concentration (grains/ft3).   -

 Zmpactor flow rate (acfm)   -
                                                   Location
                                                   Orifice   ^
                                                   bar. press.  ("Hg)
                                                   Mw
                                                   avg. Pm  (-"Hg)
                                                   avg. Tm  (°F)
                                                        (grains or 7.).
                                                     ter volume (ft )
                                                   «vg. Ps  (±"H,0)
                                                   avg. Te  (°Yr
                                                   time (minutes)
                                                   correction factor
                                                                 00
        Stage
Nee weight
   (gm)
                        7. on
                        stage
Size cutoff
   (urn)
^ stated
•size
dm/d log D
                                                                             Geo. Mean
    > Probe  &
      expander
                                       11.8/11
                             B.fSot
                                       A . W 0
                                                 o« 0007
                 o . ero
                                                              A
                    G-O/O
           3.
J3
        Total
                 0. C? .c
                                            115
-------
                                     ANDERSEN 1MPACTOR
Date     .'7    Run

Sample volume at STP  (ft  )    •

Moisture              (X)      -

Concentration (grains/ft3)    •

 Impactor flow rate (acfm)
Location
Orifice
bar. press.  ("Hg)
Mw
avg. Pm  (-"Hg)
•vg. Tm  (°F)
H-O (grams or %).
meter volume  (ft )
avg. Ps  (+"H70)
avg. Ts  ftr
time (minutes)
correction factor
                      /*•..
Stage
, Probe &
expander
0
1
2
3
4
5
6
7
V P
Total
Net weight
(gm)
^^3 * ^y^y ^s &*

^5 £7X3 ^^ ^r
^. -ro/T
O.^ro6
^,,^6
^•« - —^ /x 4
^^^
^O - ^^r^j i^i ^^
d>.«oLO

7. on
stage


\
V







Size cutoff
(urn)
r
f
k 1 x
\ y
\\\ /
\\
\ "





% £ stated
•size
y
'
7








dm/d log D











Geo. Mean











                                      116
-------
                                    ANDERSEN IMPACTOR
Data      Att Run 9

Sample volume  at STP (ft  )    •

Moisture              (I)      •

Concentration  (grains/ft3)

 Impactor flow rate  (acfm)    «
                     location
             Orifice  t)
             bar. press.  ("Hg)
             Mw
             avg. Pm (-"Hg)
             avg. Tm (°F)
             H-0 (grams or %).
             meter volume (ft )
             avg. Ps (+"H,0)
             avg. Ts (°>r
             tine (minutes)
             correction factor
                                                • X3
                                                fi 3 3
                                                                       /£>
  Stage
           Net weight
7. on
stage
Size cutoff
   (um)
$ stated
•size
dm/d log D
           Geo. Mean
Probe  &
expander
             >. 0-OfO
  Total
                                       117
-------
                                    ANDERSEN IMPACTOR
Data
                 Run t
 Sample volume  at  STP  (ft3)

 Moisture
Concentration  (grains/ft3)   -

  Lnpactor flow rate (acfm)   -
                     Location
                                             Orifice
                                             bar. press.  ("Hg)
                                             Mw
                                             avg. Pm  (-"Kg)
                                             avg. Tm  (°F)
                                             H-O  (grams or 7.)3
                                             meter volume  (ft )
                                             avg. Ps  (+"H 0)
                                             avg. Ts  (°F)
                                             time (minutes)
                                             correction factor
                                                 6?
                                                 3
                                                . /
  Stage
           Net weight
              (go)
7.  on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
Geo. Mean
 (
Probe  &
expander
                      /7.6V70
                                 13
                                                                         7-
                                                            049007
                                                                       H.
                                                            0*000 ?>
                                                            0,
                                              A
                                                           a. 000^
                      0*^000
  Total
                                       118
-------
                                            ANDERSEN IMPACTOR
         Date    *a7   Run

         Sample volume  at  STP  (ft)   •

         Moisture              (I)     •

         Concentration  (grains/ft3)

          Impactor flow rate (acfm)   •
Location
Orifice  u
bar. press.  ("Hg)
Mw
avg. Pm  (-"Hg)
avg. Tm  ( F)
H,0 (grams or %).
meter volume (ft )
avg. Ps  (+"H,0)
avg. Ts  (°>r
time (minutes)
correction factor
Stage
Probe &
expander
0
1
2
3
4
5
6
7
«/ P
Total
Net weight
(gm)
0.-K

0.**~>3
-*,**>£
^} f ^^*£i J O
^•* ^i
0.
0.OCS1/
o.*™*
o.<^**>

T» on
stage











Size cutoff
-------
                                     ANDERSEN IMPACTOR
Data
                  Run *
 Sample volume  at  STP (ft3)

Moisture              (fc)

Concentration  (grains/ft3)

 Impactor flow rate  (acfm)
                     Location

                     Orifice  t)
                     bar. press.  ("Hg)
                     Mw
                     avg. Pm (-"Kg)
                     avg. Tm CF)
                     H.O (grains or %)_
                     meter volume (ft )
                     avg. Ps (+"H,0)
                     avg. Ts (°Fr
                     time (minutes)
                     correction factor
  Stage
           Net weight
              (go)
7.  on
stage
Size cutoff
   (u«0
4 stated
•size
dm/d log D
Geo. Mean
 ( urn)
       &
expander
           C.
  Total
                                        120
-------
                                    ANDERSEN IMPACTOR
              £  Run 0

Sample volume at STP (ft )

Moisture
Concentration (grains/ft3)

 Lnpactor flow rate (acfm)
                                   Location
                                   Orifice  F
                                   bar.  press.  ("Hg)
                                   Mw
                                   avg.  Pm (-"Hg)
                                   avg.  Tm ( F)
                                   H.O (grams or %)_
                                   meter volume  (ft )
                                   avg.  Ps (+"H.O)
                                   avg.  Ts C5?)
                                   time  (minutes)
                                   correction factor
  Stage
 Met weight
    (8m)
TL on
stage
Size cutoff
   (urn)
% £ stated
  •size
dm/d log D
                                                                       Geo. Mean
Probe  &
expander
O • CrC /£.
           O
            514/23
                                                                        /.?..
             . o-o yo
             . *?<**<
  Total
                       35:^/73
               o-e
                                                              /•
                       ". */7j
                                                                 99*7
                      0.0000
0, ollf
                                       121
-------
ANDERSEN IMPACTOR
Data  ^13/76  Run t

Sample volume at STP (ft3)   •

Moisture             (X)     -

Concentration (grains/ft3)

 Xmpactor flow rate (acfm)   •
         location
         Orifice  b
         bar. press.  ("Hg>
         MM
         avg. Pm  (-"Hg)
         •vg. Tm  (°F)
         H.O (grains or %).
         meter volume (f t )
         •vg. Ps  (±"H,0)
         avg. Is  (°>r
         time (minutes)
         correction factor
. 63
Stage
Probe &
expander
0
1
2
3
4
5
6
7
> P
Total
Net weight
(gm)
0.-**

Q * £r&^Q c£L
^? * £) O1 c?o*>
2>,^.7
"fi>.^«>o3
^> • ^^o c^o
-*,«»/o
^5 • ^^^^5 t^
-tf,£WA

7. on
stage











Size cutoff
(MB)


I
v\
U
p
"




Z ^ stated
•size


r
/
V)






dm/d log D











Geo. Mean











    122
-------
Data

Sample volume at STP  (ft )

Moisture              (X)

Concentration (grains/ft3)

 Lnpactor flow rate (aefm)
                                    ANDERSEN IMPACTOR
Location
Orifice
bar. press.  ("Hg)
to
avg. Pm  (-"Hg)
avg. Tm  ( F)
H20 (grams or 7.)3
meter volume  (ft )
«vg. Ps
•vg. Ts
time (minutes)
correction factor
. 63
Stage
T'C'VyProbe &
expander
0
& i
OP 2
^ 3
4/0 4
^ 5
^ 6
^5 7
AA& v
Total
Net veight
<8»>
0*<*r>&£~

G>,f--e.T •$•
~"e>. s-r/&.
~&. eX> c?oL
""£> .  . c*£~c *
^. £>-C>^L5u
0f£-C&1
£>, d^ y6

% on
stage











Sice cutoff
(urn)



\e \
\\
\ N
\




% $ stated
•size


/"'
( /
\ vy;
\
V1




dm/d log D











Geo. Mean
( *n)











                                     123
-------
                                         ANDERSEN IMPACTOR
Date   /a£ Run

Sample volume at STP (ft)

Moisture
                             3
                                  -  %.
     Concentration  (grains/ft3)   - 0,

      Impactor flow rate (acfm)   - ^
                                                  Location
                     Orifice b
                     bar. press.  ("Hg)
                     Mr
                     avg. Pm (-"Hg)
                     avg. Tm ( F)
                     H.O (grams or %)3
                     meter volume (ft )
                     •vg. Ps (i"H.O)
                     «vg. Is far
                     time (minutes)
                     correction factor
       Stage
           Net weight
              (gin)
% on
stage
Size cutoff
   (urn)
$ stated
•size
dtn/d log D
Geo. Mean
 (Mm)
            &
     expander
Go
                            V.faw
                                                                 0*0000
                                     /.
       Total
                                          124
-------
                                           ANDERSEN IMPACTOR
Date

Sample volume at STP (ft )    -

Moisture             (X)     •

Concentration (grains/ft3)

 Impactor flow rate  (acfm)
                                                     location
                                                     Orifice   1s
                                                     bar. press.  ("Hg)
                                                     Mw
                                                     avg. Pm  (-"Hg)
                                                     avg. Tm  (°F)
                                                     H.O (grams or 7.)o
                                                     meter volume  (ft )
                                                     avg. Ps  (+XO)
                                                     avg. Ts  (°F)
                                                     time (minutes)
                                                     correction factor
                                             J8-.6&
                                                                     e»
                                                                     A3/
                                                                     vTVO
          Stage
           Net weight
              fem)
7. on
stage
Size cutoff
   (um)
^ stated
•size
dm/d log D
Geo. Mean
 ( um)
rc- U3 Probe  &
        expander
                                        /J,
                                        X 76* 7 J
                                                                       7'0/n
                              IS. 8113
                                                           O- ooog
                                         /. 'y
                     c>t-
                                                                   a. oooo
   R/o
         Total
                                            125
-------
                                    ANDERSEN IMPACTOR
Date  ^/^fy/^e*  Run $

Sample volume at STP (ft3)   -

Moisture             (I)     •

Concentration (grains/ft3)

 Impactor flow rate (acfm)   -
                                                  Location ^
                                                  T.W  /feof-
                                                  Orifice  D
                                                  bar. press.  ("Hg)
                                                  Mw
                                                  avg. Pm  (-"Hg)
                                                  avg. Tm  (°F)
                                                  H.O (grams or %).
                                                  meter volume  (ft )
                                                  avg. Ps  (±"H,0)
                                                  avg. Ts  (°F)^
                                                  time (minutes)
                                                  correction factor
                                                                            f
                                                                  *U I* , l-fc cU
  Stage
           Met weight
              (8*0
                             7. on
                             stage
                                Size cutoff
$ stated
•size
dm/d log D
Geo. Mean
 ( pm)
Probe  &
expander
                                                 . Vf/JT
           O.
//

/A
           o .
                                If. 6 7£6
                                 3,/fyy
              c-c
                                                           <**
                      33,07*?
  Total
             . C--0-O-O
                                      126
-------
                                    ANDERSEN 1MPACTOR
Date

Sample volume  at  STP  (ft"*)   -  i,

Moisture              (X)     -

Concentration  (grains/ft3)   -  *.

 Lnpactor flow rate (acfm)   -  &*3Jioo>
                                   Location
                                   TV"-*. Hit -
                                   Orifice  fc
                                   bar. press. ("Hg)
                                   Mw
                                   avg. Pm (-"Hg)
                                   avg. Tm (°F)
                                   HjO  (grams or 7.)3
                                   meter volume (ft )
                                   avg. Ps
                                   avg. Ts
                                   time (minutes)
                                   correction factor
  Stage
 Net weight
    (gm)
7. on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
                                                                        Geo. Mean
expander
                                    7 A .
                                  19, SB 7e>
                                                             O.
                                                              /3
                                              So.
           CP. eT-t-r-T"
  Total
o.
                                      127
-------
                                       ANDERSEN IMPACTOR
    Data

    Sample volume at  STP (ft)

    Moisture
Concentration (grains/ft3)    -

 Impactor flow rate (acfm)
                                             location
                     Orifice   £
                     bar. press.  ("Hg)
                     MM
                     avg. Pm (-"Hg)
                     avg. Tm (°F)
                     H2° (grams or 7.).
                     miter volume  (ft )
                     avg. Ps (±"H90)
                     avg. Ts far
                     time (minutes)
                     correction factor
                                                                         ^3.3
     Stage
           Net weight
              (go)
7. on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
Geo. Mean
 ( pm)
   Probe  &
   expander
          0.
-A
                                                 7V.
                                                               6.000JL
                                                                           H.* fix-
                    s V
                                A
                                                                           0-67/3
              o.
     Total
          0.
                                           128
-------
                                       ANDERSEN IMPACTOR
Date

Sample volume at STP  (ftJ)

Moisture              (X)

Concentration (grains/ft3)

 Lnpactor flow rate (acfm)
                     '$5
                                      °. Ll 17°
                                                 Location
Orifice  ^
bar. press.  ("Hg)
Mw
avg. Pm  (-"Hg)
avg. Tm  ( F)
H.O (grains or %).
meter volume (ft )
avg. Ps  (±"H,0)
avg. Ts  (°Fr
time (minutes)
correction factor
                                                                         77f
     Stage
Net weight
   (gm)
                         7. on
                        stage
                                    Size  cutoff
  7. ^ stated
    •size
dm/d log D
           Geo. Mean
3-TProbe  &
   expander
                                    fr. >l*
              0,00/0
                                   PI. -3
               >. oc /3
                      9.4071
              tf, vc * o
            11-62
                                                               c.
                                                                        7.
              0, co
                                                 J" r. fr-t s-
                                                               c.f .
                                                             V.
              o. cc ^ &
                     /.
                                              U. i "/ '•''••
                                                               
-------
                                    ANDERSEN IMPACTOR
        Date
                 Run *
 Sample volume at STP  (ft3)

 Moisture              (X)

 Concentration (grains/ft3)

 Xmpactor flow rate (acfm)
                                    - O* 32Jo
             Location
             **
             Orifice  b
             bar. press. ("Hg)
             Mw
             avg. Pm (-"Hg)
             avg. Tm (°F)
             ILO (grams  or %).
             meter volume  (ft  )
             avg. Ps (+"H,0)
             avg. Ts (°F)'
             time (minutes)
             correction  factor
                                                                             JF.6*
  Stage
           Net weight
                                7. on
                                stage
Size cutoff
1. $ stated
  •size
                            dm/d  log D
Geo. Mean
 ( urn)
TC.
Probe  &
expander
                                                      7 r. a VAT
                                              73.
                                                                 f (
                      tt.fS/t
                                                                               /3.J-AT 7
                                                           0.
           0 .
                                                      3f.
  Total
             c? 3 o 3
                                     130
-------
                                        ANDERSEN IMPACTOR
Data 6/£,r/7£ Run *

Sample volume at STP (ft3)

Moisture             (X)

Concentration (grains/ft3)

 Impactor flow rate (acfm)   -0,3233
                                                  Location
                                                  Orifice b
                                                  bar.  press.  ("Hg)
                                                  Mw
                                                  avg.  Pm (-"Hg)
                                                  avg.  Tm (°F)
                                                  H.O (grains or 7.).
                                                  meter volume  (ft )
                                                  avg.  Ps (+%0)
                                                  avg.  Ts fry
                                                  time  (minutes)
                                                  correction factor
                                                            AS-. 60
       Stage
 Net weight
    (gm)
                         % on
                        stage
                                     Size cutoff
TL $ stated
  •size
dm/d log D
           Ceo. Mean
    probe  &
    expander
             .Z o. c.'f
                                              80.0000
37
                            '. Cceo
                  . £-0
                                                             /3 .
V/
               O.
            I (•£'!/<•(
                                 3 . /J-73
                „ ere 0 V1
               c?. cc
      Total
6 ' G A* $ 0
                                           131
-------
                                   ANDERSEN IMPACTOR
Date  £/A Run * y&

Sample volume ac STP (ft3)

Moisture             (X)

Concentration (grains/ft3)

 Impactor flow rate  (acfm)
                                   Location
                                                    Orifice  ft
                                                    bar. press. ("Hg)
                                                    Mw
                                                    avg. Pm (-"Hg)
                                                    avg. Tm (°F)
                                                    H.O (grams or %).
                                                    meter volume (ft )
                                                    avg. Ps (±"H 0)
                                                    avg. Ts (°Fr
                                                    time (minutes)
                                                    correction factor
                                                         J$
                                                            8-3.
                                                                    AT
  Stage
 Net weight
    (gm)
                                7. on
                                stage
Size cutoff
   (urn)
T. ^ stated
  •size
dm/d log D
                                                                      Geo. Mean
TC. 3*> Probe  &
       expander
                      36.6R
                                     /. 3/75
                      O.OOPO
                                                  &.OOOQ
                                                              ooJV
                                                              /3
                      AW79
                                              Z.7/3/
 Total
0.
                                        132
-------
                                    ANDERSEN IMPACTOR
Date 6./*r/7£  Run

Sample volume at  STP (ft3)    •

Moisture             (%)      »

Concentration (grains/ft3)

 Impactor flow rate  (acfm)    -
                                             Location
                                             Orifice  £
                                             bar. press.  ("Hg)
                                             Mw
                                             avg. Pm  (-"Hg)
                                             «vg. Tm  (°F)
                                             H.O (grams or %).
                                             meter volume (ft )
                                             «vg. Ps  (+"H,0)
                                             avg. Ts  (°Fr
                                             time (minutes)
                                             correction factor
                                                          7?
  Stage
 Net weight
    (8«0
                        7. on
                        stage
                                Size cutoff
^ stated
•size
dm/d log D
Geo. Mean
 (
Probe  &
expander
             I7.H7I
           o.
                                    #/.
-------
                                         ANDERSEN IMPACIOR
Date          >  Run

Sample volume at STP (ft3)

Moisture             (fc)

Concentration (grains/ft3)

 Impactor flow rate (acfm)
                    o.
                                          f y
                                                  Location
Orifice
bar. press.  ("Hg)
Mw
avg. Pm (-"Hg)
avg. Tm (°F)
H.O (grams or %).
meter volume (ft )
avg. Ps (i"H,0)
avg. Is (°Fr
time (minutes)
correction factor
       Stage
Met weight
   (gm)
                        7. on
                        stage
                                     Size cutoff
    $ stated
    •size
dm/d log D
           Geo. Mean
     Probe  &
     expander
                                   r*. 7733
                       «/
            l.6Sf/
                            /. Sgfy
                                                  . 00 H.
                                                    (/2,
                0. o-o /O
                                    37. 72 ?£
                                                                   , 005
0V
                 >. £~C J
                                                   t6. ££7
                O .00 J"7
           S,
       Total
                                            134
-------
                                            ANDERSEN IMPACTOR
        Date  <*   ?6 Run

        Sample volume at STP (ft)

        Moisture             (X)

        Concentration (grains/ft3)

         Impactor flow rate (acfm)
     - o. $07f
                                  Location
                                  Orifice   B
                                  bar. press.  ("Hg)
                                  Mw
                                  avg. Pm  (-"Hg)
                                  avg. Tm  (°F)
                                  H.O  (grams or %).
                                  miter volume  (f t )
                                  •vg. Ps  (±"H,0)
                                  avg. Ta  (°>r
                                  time (minutes)
                                  correction factor
                                                                              cJO
          Stage
Net weight
   (8«n)
T.  on
stage
                                        Size cutoff
$ stated
•size
dm/d log D
Geo. Mean
 (
fc*/7  Probe  &
        expander
                                                       5.5- . J *"J! /
  07
                               2 ./«
                      •;.,ry v
            4
                                                                    e.oo&f
                              /• V'/
                                                      ?- 6'.  -'
                                                0.
                                                                    0.
         Total
                                . '^ 2
                                              135
-------
                                       ANDERSEN IMPACTOR
     Dat.     >*> Run*  PC

     Sample volume at STP (ft3)   -

     Moisture             (X)     «

     Concentration (grains/ft3)   - 0. D

      Lapactor flow rate (acfm)   - 0
                    Location  s-++J-

                    Orifice   k
                    bar. press. ("Hg)
                    Mw
                    avg. Pm (-"Hg)
                    avg. Tm ( F)
                    H-0 (grams or %).
                    meter volume (ft )
                    avg. Ps (+"H20)
                    avg. Is (^F)
                    time (minutes)
                    correction factor
                                                          48,70
      Stage
Net weight
   (go)
X on
stage
Size cutoff
   Gin)
^ stated
•size
dm/d log D
                                                                          Geo. Mean
    Probe  &
    expander
0.00
                                   7H.6H19
sfV
                                         9^77
                                                              ®-
        4
                                    3.
                                               0.6438
                          A2 .
                                               c  cjof
                                                -£77 -7
               0 ,
                     !>***!
      Total
                                           136
-------
                                         ANDERSEN IMPACTOR
      Date     J fr>£  Run

      Sample volume at STP (ft)

      Moisture             (X)     -

      Concentration (grains/ft3)   -  0t 036j?

       Lnpactor flow rate  (acfm)
                                  Location
                                  Orifice  U      *
                                  bar. press. ("Hg)
                                  Mw
                                  avg. Pm (-"Hg)
                                  avg. To ( F)
                                  H.O (grains or 7.)3
                                  meter volume  (ft  )
                                  «vg. Ps (+%(>)
                                  avg. Ts ("F)
                                  time (minutes)
                                  correctinn factor
                                                                 0,4
        Stage
Net weight
   
7. on
stage
Size cutoff
   (pm)
$ stated
•size
dm/d log D
                                                                            Geo. Mean
      probe  &
      expander
0.
                      y 6,9^3
'•
                                                                 o.oo/G
                                                             3 *.
                                         . 6616
                                       1233
                                   O. OCT.1/
                                      /3.
          4
                            3./2S&
                      3.
                                   G.OCl'f
                            Wit
       Total
                                           137
-------
                                    ANDERSEN IMPACTOR
 Date    &       Run

 Sample volume aC STP (ft)

 Moisture             (%)

 Concentration (grains/ft3)

  Lnpactor flow rate (acfm)
                  - 2/7*.
                                  Location
                     Orifice   £
                     bar. press.  ("Hg)
                     Mw
                     avg. Pm  (-"Hg)
                     avg. Tm  (°F)
                     H.O (grains or 7.).
                     meter volume (ft )
                     avg. Ps  (+"H 0)
                     avg. Ts  (°F)
                     time (minutes)
                     correction factor
                                                          <*P.
                                                           fr3.fr
                                                          1c
                                                          o
  Stage
 Net weight
   (go)
7.  on
stage
                                Size cutoff
 T. $ stated
  •size
dm/d log D
           Geo.  Mean
Probe  &
expander
O .
                                              76.
          O . OD€> f
                      S.I'm
                                                           0,06
                      ft.
                        ,^1 Iff
             , 6-0 cl $
            7.4M
           060 f
9.7F&
                                                           0.
                                                            o.*/?*
                               a.
                      0,0000
  Total
                                        138
-------
                                           ANDERSEN IMPACTOR
Date

Sample volume at  STP  (ftJ)

Moisture              (X)

Concentration (grains/ft3)
                                        /.
                                           - i
       Impactor flow rate  (acftn)    - & ,  J//£
                                                    Location
             Orifice   F
             bar. press.  ("Hg)
             Mw
             avg. Pm  (-"Hg)
             avg. Tffl  ( F)
             H.O  (grains or 7.)_
             meter volume  (ft )
             «vg. Ps
             avg. Ts
             time (minutes)
             correction factor
                                                                             /• 7/0
        Stage
                  Net weight
                                 7. on
                                 stage
Size cutoff
   (urn)
                                                  $ stated
                                                  •size
dm/d log D
           Geo. Mean
7"C y£ Probe  &
        expander
                   . ,'  .
                                        3 . 2 3 J 7
                                                                                  1. 03 * -5
                  r /'v." ..'  (-
                               13. . £>C£> 
-------
                                         ANDERSEN IMPACTOR
      Date         >&  Run

      Sample volume at STP (ft)    -

      Moisture
      Concentration (grains/ft3)   *

       Impactor flow rate  (acfm)   -
                         ("Hg)
                    Location
                    Tf-«.  ote7-
                    Orifice  U
                    bar. press.
                    Mw
                    avg. Pm (-"Hg)
                    avg. Tm (°F)
                    H.O (grams or 7.).
                    meter volume (ft )
                    avg. Ps (+"H-0)
                    avg. Ts (OFT
                    time (minutes)
                    correct inn factor
                        . 06
        Stage
                 Net weight
7. on
stage
Size cutoff
   (urn)
7. £ stated
  •size
dm/d log D
Geo.  Mean
 (
      probe  &
      expander
                     7*7212-
"S
                                     /f
                                               30.2/7*
                                                   VA v/
                                   O
 AT
                            11.1771
       *•*?¥£
                           0. Of 7
                        A
                                                   7- 122.2.
       Total
                                             140
-------
                                          ANDERSEN IMPACTOR
      Data

      Sample volume at STP  (ft)

      Moisture              (X)

      Concentration (grains/ft3)

       Impactor flow rate (acfm)
                     Location   j^
                     TV***- o )$8 — /oz6 (I ~A
                     Orifice  &
                     bar. press.  ("Hg)
                     Mw
                     avg. Pm (-"Hg)
                     avg. Tin (°F)
                     H.O  (grams or %).
                     meter volume (ft )
                     avg. Ps (±"H,0)
                     avg. Ts (°Fr
                     time (minutes)
                     correction factor
                                                                              //
        Stage
                   Net weight
                      (go)
7.  on
stage
Size cutoff
   (ym)
$ stated
•size
dm/d log D
                                                                              Geo. Mean
TC
      Probe  &
      expander
                 0. cr-
                                          V i: • 9fr-(J". i 7- y
                                                                       tfjf-rf
       Total
                                           141
-------
                                    ANDERSEN IMPACTOR
Date
                 Run*
Sample volume at STP (ft )   •

Moisture             (I)     •

Concentration (grains/ft3)   -  O.)lf£

 Lopactor flow rate (acfm)   -  t> .3 j.j 7
                     Location
                     Orifice U
                     bar.  press.  ("Hg)
                     Mw
                     avg.  Pm (-"Hg)
                     avg.  Tm (°F)
                     1LO (grams or %)a
                     miter volume  (ft )
                     «vg.  Pa (+"H  0)
                     avg.  Ta (°F)^
                     time  (minutes)
                     correction factor
                                                                     /, Vo
  Stage
           Net weight
              (gm)
7. on
stage
Size cutoff
   (urn)
^ stated
•size
dm/d log D
Geo. Mean
 (
expander
          O,
                      1 J.I 61*
                                                 . 5 Id-
                      /
-------
                                   ANDERSEN 1MPACTOR
Date
                 Run*
 Sample volume at STP (ft)   -

 Moisture             (fc)     -

 Concentration (grains/ft3)   -

 Lapactor flow rate  (acfin)   -
                    Location
                    77 ~*.
                    Orifice  b
                    bar. press.  ("Hg)
                    MM
                    avg. Pm (-"Hg)
                    avg. Tm (°F)
                    H-0 (grains or %).
                    meter volume  (ft )
                    avg. Ps (+"H 0)
                    avg. Ts (°Fr
                    time (minutes)
                    correction factor
                                                                  At
                             O *  6 J
  Stage
          Net weight
             (gn>)
7. on
stage
                               Size cutoff
$ stated
•size
dm/d log D
Geo.  Mean
 ( pm)
       &
expander
           O- oo/o
           C> ,
                     *•'/?;.*-'
                     7r.
                                             72. V* £7
                 3$}
                               3. 11 63
                                ». 99*4
                                           37
                                             him
 Total
                                       143
-------
                                            ANDERSEN IMPACTOR
        Date           6 Run

        Sample volume at STP (ft)

        Moisture             (X)

        Concentration (grains/ft3)

         Impactor  flow rate  (acfm)
                                                      Location
                                                      Orifice  F
                                                      bar. press. ("Hg)
                                                      Mw
                                                      avg. Pm (-"Hg)
                                                      avg. Tm (°F)
                                                      1LO (grams  or %),
                                                      meter volume  (ft )
                                                      avg.
                                                      avg.
                                                      time (minutes)
                                                      correction  factor
                                                        .  Ps (+"H
                                                        .  Ts (°F)
                              i"H20)
         Stage
                    Net weight
                       (gm)
7.  on
stage
Size cutoff
   (urn)
7. ^ stated
  •size
dm/d log D
                                                                               Geo. Mean
Tc
       Probe  &
       expander
                                                          . i 7 2.7
                                        13
                                         8
                                                       74?.
                  0*0-0 j!f
                                                                    0.06 JO
K.
                   o • c-o D /
                                                                                3.0347
                  o .
                              £6646
                                                                   a. #000
                 O . ert?o
         Total
-------
                                           ANDERSEN IMPACTOR
Date   6/3C/7& Run 0
Sample volume at STP (ft)

Moisture
                               3    - 3?o.733i"
       Concentration (grains/ft3)    -

         Impactor flow rate (acfm)    -
                                                    Location
                    Orifice   ^
                    bar. press. ("Hg)
                    Mw
                    avg. Pm  (-"Hg)
                    avg. Tm  (°F)
                    H-O  (grams or %),
                    meter volume (ft )
                    avg. Ps  (+"H 0)
                    avg. Ts  faT
                    time (minutes)
                    correction factor
                                                                     93
         Stage
           Net weight
              (gm)
7. on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
Geo. Mean
 ( MB)
       Probe  &
       expander
                                                                  o> ,
                 0.0o
                             ff-t/31
                                                          6. one 3
                  ©- oof 7
                                             y.
                                   Q. tf Oo
                                       4.8 17 &
                                                                             *•£*"?*.
                 O,
-#"vs
 w  •*
         Total
         O.
                                             145
-------
                                        ANDERSEN IMPACTOR
Date

Sample volume at STP (ft)

Moisture             (%)

Concentration (grains/ft3)

 Impactor flow rate  (acfm)
                                  • *jm
             Location ^«*,£.t.J?:
             T»«*- oSlf-oSYV (bJ.
             Orifice  O       ^
             bar. press.  ("Hg)
             Mw
             avg. Pm (-"Hg)
             avg. Tm (°F)
             H.O (grains or 7.)3
             meter volume  (ft )
             avg. Ps (+"H 0)
             avg. Ts TO
             time (minutes)
             correction factor
                                            Jo. 0
                                                                            0,5
                                                                            .6?
       Stage
           Net weight
              (gm)
7. on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
Geo. Mean
 ( urn)
     Probe  &
     expander
XT
                                                               0 .
         4
                      3.8W
                           Wni
               O.
                                                          * oft 3
<*/
                O. £-0 /&
                                             //
                                   O.
      Total
                                          146
-------
                                    ANDERSEN IMPACTOR
Date      ?e>  Run

Sample volume at STP (ft)

Moisture             (X)

Concentration (grains /ft3)

 Impact or flow rate (acfm)
                                             Location
                             - ^ . /33Z.
                               
  Stage
           Net weight
              (gm)
7. on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
Geo. Mean
 <*•«>
       &
expander
                                              yi. 
                                 3
                                               a*.////
                                                                        a..
                                              It. toff i  6
  Total
                                       147
-------
                                   ANDERSEN 1MPACTOR
         Date      t>?  Run

         Sample  volume  at STP  (ft)

         Moisture              (X)

         Concentration  (grains/ft3)

         Impactor flow rate (acfm)
                            -  6 -
                     Location
                     Orifice   b
                     bar. press. ("Hg)
                     Ha
                     avg. Pm (-"Hg)
                     avg. Tm (°F)
                     HjO (grams or %),
                     meter volume (ft )
                     avg. Ps (J"H20)
                     avg. Ts O5?)
                     time (minutes)
                     correction factor
                                                                         i  \
                                                                     ----  J
                                                                    -3 0,0-5
 Stage
                   Net weight
                      (gm)
7» on
stage
Size cutoff
   (urn)
$ stated
•size
dm/d log D
Geo. Mean
 ( vm)
TC. ^ 5s Probe  &
        expander
                     V/,66^6'
             ooo
             CT&/&
                                                           0.0/77
         O ,
                               -7/92.
                      //. 81*
         O .
                                            l/J~ 7
Total
                   5, && so

                  0.022 8
                                      148
-------
                                      ANDERSEN IMPACTOR
   Date          £ Run

   Sample volume at STP  (ft3)   - 
-------
                                           ANDERSEN IMPACTOR
Data
                         Run 0
        Sample volume at STP (ft3)

        Moisture
        Concentration (grains/ft3)

         Lopactor flow rate  (acfm)
. /.3*lo
                Location
                                            Orifice  ^
                                            bar.  press.  ("Hg)
                                            Mu
                                            avg.  Pm (-"Hg)
                                            avg.  Tm ( F)
                                            H.O (grains or %).
                                            meter volume  (ft )
                                            avg.  Ps (+"H.O)
                                            avg.  Ts (°F)
                                            time  (minutes)
                                            correction factor
          Stage
                   Net weight
                        7. on
                       stage
   Size cutoff
      (um)
1. ^ stated
  •size
dm/d log D
           Geo.  Mean
TC  ^oprobe  &
        expander
                  0.00ft
                                                                      £.6876
                                          3/JV
                                                . Wl.
                                                                              /Sift
                                          u w
                                                                  0 0600
         Total
                                              150
-------
        APPENDIX F




FINE PARTICLE MEASUREMENTS
         151
-------
Table F-l.  FINE PARTICLE DATA FOR BAGHOUSE INFLUENT,  TEST 1
Clock
time
1521
1524
1526
1529
1533
1535
1537
1539
1541
1543
1554
1600
1604
1608
1612
1616
1619
1624
1627
1630
1634
1637
1640
1644
1647
1650
1654
1657
1659
1702
1706
1709
1712
1715
1718
1721
1724
1727
1730
Phase of
process
cycle







































Compartment
being
cleaned







































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10-°
9.6 x 10
1.1 x 10'
9.2 x 10°
5.7 x 10°
3.8 x 10°
5.8 x 10°
5.8 x I0j?
6.2 x 10°
7.0 x 10
—
7.4 x 10^
5.6 x 10;?
7.4 x 10^
4.4 x 10°
4.1 x 10)?
3.9 x 10^
6.6 x 10,
1.7 x 10'
7.7 x 10°
9.3 x 10°
6.6 x 10°
8.9 x lo£
8.6 x 10,
8.0 x 10,
8.0 x 10,
6.0 x IQ7
7.8 x lO)?
8.0 x 10°
8.1 x 10;?
8.2 x 10^
3.3 x 10^
3.0 x 10,
5.7 x 10?
3.8 x 10,
3.2 x 10,
.2.0 x 10'
2.0 x lO;?
2.9 x 10,
5.0 x 10
Particle
size,
> \im
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-6
2,400
180
160
0.41
2,400
2,300
2,500
2,300
2,000
29
2,200
1,600
2,300
54
19
0.38
2,300

2,700
2,500
120
22
0
1,600
1,400
300
20
70
0.59
2,100
1,600
1,500
1,200
16
23
0.00
1,600
2,400
1,300
Particle
size,
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.3
0.3
0.5
0.3
0.3
0.3
0.5
1.0
2.0
0.3

0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
                           152
-------
Table F-l (continued).   FINE PARTICLE DATA FOR BAGHOUSE  INFLUENT, TEST 1
Clock
time
1733
1735
1738
1741
1744
1747
1750
1753
1755
1758
1801
1804
1807
1810
1813
1816
1818
1821
1824
1827
1830
1833
1836
1838
1841
1843
1846
1848
1851
1854
1857
1859
1902
1905
1907
1910
1913
1916
1918
Phase of
process
cycle







































Compartment
being
cleaned







































Condensation nuclei
counter
Particle
concentration ,
particles/
m3 x ID'6
4.3 x 10,
4.7 x 10,
2.0 x 10,
2.2 x 10?
2.1 x 10,
3.4 x 10,
4.8 x 10;
3.1 x 10,
5.4 x 10,
3.2 x 10,
3.1 x 10,
3.2 x 10,
3.7 x 10,
1.6 x 10,
1.6 x 10,
2.6 x 10;
1.9 x 10;
1.2 x 10,
4.0 x 10;
4.4 x 10,
2.1 x 10,
1.6 x 10,
4.1 x 10,
1.9 x 10'
4.6 x 10*
2.8 x 10°
2.0 x 10^
1.2 x 10^
1.1 x 10°
3.1 x 10J?
3.7 x 10;
3.1 x 10°.
n f* i A Q
x Q v 1 n
J • 7 A ±\J -
2.5 x 10°
2.6 x 10*
3.0 x 10°
6.4 x 10°
6.4 x 10;?
3.8 x 10°
Particle
size,
_>_ urn
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-°
530
140
0.33
2,400
2,000
2,200
1,500
340
0.11
2,500
2,400
2,400
530
550
370
0.68
2,200
2,100
1,800
120
48
1.2
970
830
1,500
320
380
0.33
2,300
2,300
2,300
340
140
0.0
2,200
2,200
1,900
214
170
Particle
size,
> ym
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
                                 153
-------
Table F-l (continued).   FINE PARTICLE DATA FOR BAGHOUSE INFLUENT, TEST  1




Clock
time
1921
1924
1927
1929
1932
1934
1937
1940
1943
1945

1948
1950
1953



Phase of
process
cycle

















Compartment
being
cleaned














Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
6.3 x 10J?
5.1 x 10°
5.7 x 10r
2.5 x 107
2.8 x IQ7
6.1 x ID!
3.8 x 10,
5.8 x 107
5.8 x 10:
5.0 x 10,
7
4.9 x 10'
6.1 x 107
6.1 x 107

Particle
size,
> vim
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025

Dust counter
Particle
concentration ,
particles/
m3 x 10-6
1.2
2,200
2,000
1,600
92
26
0.11
420
1,500
1,700

140
19
1.1

Particle
size,
> pm
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3

0.5
1.0
2.0
                                154
-------
Table F-2.  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT,  TEST 2
Clock
time
1116
1118
1121
1126
1128
1130
1132
1143
1146
1148
1153
1155
1158
1200
1203
1205
1208
1210
1212
1215
1217
1219
1222
1224
1226
1228
1230
1233
1235
1238
1240
1242
1244
1246
1249
1252
Phase of
process
cycle




































Compartment
being
cleaned




































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x ID'6
5,000
6,000
12,000
160,000
80,000
13,000
36,000
10,000
16,000
50,000
14,000
14,000
8,000
20,000
14,000
14,000
22,000
150,000
12,000
10,000
12,000
12,000
80,000
20,000
12,000
12,000
10,000
60,000
22,000
12,000
10,000
15,000
22,000
17,000
15,000
16,000
Particle
size,
>_ \im
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x ID'6
17
11
7.4
70
47
35
22
10
6.7
38
8.4
4.5
6.5
24
3.4
3.1
2.9
43
6.1
3.8
3.4
2.4
61
8.9
5.4
3.7
3.7
42
5.4
4.8
3.6
6.9
37
4.0
3.3
13
Particle
size,
_>_ pm
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                             155
-------
Table F-2 (continued).  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT, TEST 2
Clock
time
1300
1306
1309
1312
1314
1316
1319
1321
1323
1325
1328
1330
1332
1345
1347
1349
1353
1405
1408
1410
1413
1415
1416
1417
1419
1422
1424
1425
1427
1428
1430
1432
1435
1436
1438
1439
1440
1443
Phase of
process
cycle






































Compartment
being
cleaned






































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
10,000
20,000
5,200
6,600
4,000
8,000
170,000
115,000
100,000
58,000
44,000
70,000
38,000
20,000
18,000
20,000
8,000
7,000
8,000
9,500
110,000



11,000
7,500
250,000



9,000
9,000
12,000



12,000
4,800
Particle
size,
> urn
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025



0.0025
0.0025
0.0025



0.0025
0.0025
0.0025



0.0025
0.0025
Dust counter
Particle
concentration.
particles/
m3 x 10~6
17
69
16
9.2
14
25
64
34
18
19
56
32
37
55
5.3
26
24
14
8.2
7.4
60
2.1
0.28
0.04
9.9
6.5
33
1.1
0.35
0.04
11
8.2
23
1.1
0.26
0.02
4.6
7.9
Particle
size,
> pm
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
                                    156
-------
Table F-2 (continued).  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT,  TEST 2
Clock
time
1445
1449
1450
1512
1515
1517
1518
1519
1520
1522
1524
1528
1529
1530
1531
1534
1536
1538
1544
1545
1546
1548
1552
1555
1556
1557
1558
1600
1603
1606
1608
1609
1610
1612
1616
1618
1620
1621
Phase of
process
cycle






































Compartment
being
cleaned






































Condensation nuclei
counter
Particle
concentration ,
particles/
m3 x 10~6
19,000


38,000
33,000
28,000



33,000
20,000
18,000



29,000
20,000
15,500



10,000
14,000
50,000



13,500
10,000
22,000



6,500
200,000
18,000


Particle
size,
> ym
0.0025


0.0025
0.0025
0.0025



0.0025
0.0025
0.0025



0.0025
0.0025
0.0025



0.0025
0.0025
0.0025



0.0025
0.0025
0.0025



0.0025
0.0025
0.0025


Dust counter
Particle
concentration,
particles/
m3 x ID"6
17
0.88
0.35
55
36
20
0.88
1.1
0.11
39
14
6.9
0.53
0.64
0
14
7.6
5.5
0.35
0.18
0.02
4.6
2.4
49
0.60
0.21
0.04
3.8
4.7
23
0.60
0.28
0
6.6
27
11
0.35
0.14
Particle
size,
> urn
0.3
0.5
1.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
                                   157
-------
Table F-2 (continued).  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT,  TEST 2



'
Clock
time
1622
1624
1626
1629
1631
1631*4
1632
1636
1637
1640
1642
1643
1644
1648
1650
1652
1653
1654
1656
1658
1700
1702
1704
1704*s
1705



Phase of
process
cycle




























Compartment
being
cleaned







1

















Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6

13,000
17,000
9,000
6,600
6,400
6,800
9,200
10,000
50,000
17,000
7,000
7,000
11,000
85,000
48,000
39,000
20,000
16,000
14,000
20,000
48,000
44,000
34,000
42,000

Particle
size,
> vim

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

Dust counter
Particle
concentration,
particles/
m3 x 10-6
0
3.9
39
34
0.53
0.21
0.02
3.3
35
25
0.14
0.18
0.02
1.7
57
5.6
0.42
0.18
0.04
6.0
31
78
11
5.3
0.18

Particle
size,
>_ pm0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
                                   158
-------
Table F-3.  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT,  TEST  4
Clock
time
1203
1205
1208
1210
1212
1216
1218
1219
1222
1225
1228
1230
1230
1232
1234
1236
1241
12424
1245
1247
1252
12524
12534
1255
1257
1259
1302
1309
1311
1313
1315
1329
1331
1337

1340
1342
1344
1348
1350
Phase of
process
cycle
Second
melt



Tap


First
melt























Back
charge
Second
melt



Compartment
being
cleaned







10



1




2




3











7




8

Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
36,000
72,000
45,000
70,000
5,000
28,000
27,000

25,000
6,000
6,000

8,000
11,000
4,000
9,000

27,000
4,000
3,000
1,000

32,000
6,000
23,000
3,000
3,000
4,000
2,000
5,000
6,000
4,000
3,000


29,000
35,000
1,000

10,000
Particle
size,
> ym
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025


0.0025
0.0025
0.0025

0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-6
36
15
26
42
34
44
40

15
24
14

18
32
16
17


21
11
4.0


54
14
6.8
5.0
5.8
5.6
4.3
18
15
4.1


48
24
6.1

75
Particle
size,
> )jm
0.3
0.3
0.3
0.3
0.3
0.3
0.3

0.3
0.3
0.3

0.3
0.3
0.3
0.3


0.3
0.3
0.3


0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3


0.3
0.3
0.3

0.3
                          159
-------
Table F-3 (continued).  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT, TEST 4
Clock
time
1353
1357
1359
1359
1402
1405
1408
1410
1410
1412
1414
1417
1421
1429
1431
1432
1434
1437
1439
1441
1443
1444
1446
1449
1452
1454
1455
1456
1459
1505
1506
1507
1510
1415
1517
1520
1527
1529
1531
1535
Phase of
process
cycle
































Slag
off


Reboil



Compartment
being
cleaned



9




10



1


2





3




4



5



6


7


Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
12,000
4,000
8,000

62,000
8,000
5,000
20,000

54,000
22,000
10,000

9,000
3,000

32,000
10,000
22,000
8,000
10,000

29,000
22,000
18,000
14,000

36,000
31,000
8,000

57,000
12,000
15,000
14,000
36,000
2,000

27,000
30,000
Particle
size,
> vim
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025

0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10~6
53
26
28

25
8.5
5.7
3.5

31
13
5.1

3.7
3.1

36
5.2
3.2
2.1
1.8

58
0.93
4.3
3.4

29
6.2
1.9

53
4
2.4
1.9
57
1.6

39
3.0
Particle
size,
> pm
0.3
0.3
0.3

0.3
0.3
0.3
0.3

0.3
0.3
0.3

0.3
0.3

0.3
0.3
0.3
0.3
0.3

0.3
0.3
0.3
0.3

0.3
0.3
0.3

0.3
0.3
0.3
0.3
0.3
0.3

0.3
0.3
                                  160
-------
Table F-3 (continued).  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT, TEST 4




Clock
time
1^41
1547
1551
1552
1557
1600
1604
1607
1609
1611
1614
1615
1628
1631
1632
1634
1640
1648
1655
1656
1656
1700
1702
1703
1708
1710
1712
1726
1727
1729

1734
1736
1737
1738



Phase of
process
cycle


Tap


First
melt






















Back
charge
Second
melt





Compartment
being
cleaned
8


9


10




























Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6

30,000


50,000
30,000

13,000
23,000
20,000
28,000

40,000
35,000
30,000
35,000
30,000
303,000
40,000
24,000

34,000
19,000
19,000
58,000
34,000
48,000
40,000
12,000
11,500

25,000
50,000
50,000
50,000

Particle
size,
> \im

0.0025


0.0025
0.0025

0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.021
0.021
0.021

0.033
0.033
0.033
0.047
0.047
0.047
0.072
0.074
0.074

0.074
0.074
0.074
0.074

Dust counter
Particle
concentration,
particles/
m3 x 10-6

36


21
28

26
24
15
8.4

30
1.1
0.79
0.02
35
21
0.12
0.05
0.0
9.3
0.28
0.05
0.97
0.23
0.21
0.94
0.11
0.02

58
38
2.6
1.1

Particle
size,
> pm




0.3
0.3

0.3
0.3
0.3
0.3

0.3
0.5
1.0
2.0
0.3
0.3
0.5
1.0
2.0
0.3
0.5
1.0
0.3
0.5
1.0
0.3
0.5
1.0

0.3
0.3
0.5
1.0
                                   161
-------
Table F-4.  FINE PARTICLE DATA FOR BAGHOUSE INFLUENT, TEST 5
Clock
time
1251
1254
1257
1300
1307
1310
1312
1314
1316
1318
1321
1323
1325
1327
1330
1332
1340
1343
1345
1347
1349
1351
1358
1400
1403
1405
1407
1410
1413
1415
1419
1422
1425
1427
1429
1431
1432
1435
1437
1440
Phase of
process
cycle
Second
melt

























Slag
off











Compartment
being
cleaned








































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x ID"6
5.6 x 10^
5.4 x 10,
30 i nO
.2 X 10
6.3 x 10g
1.9 x 10,
1.2 x 10°
1.6 x 10
2.6 x 10^
5.4 x 10
7.8 x 10g
7.4 x 10
1.1 x 10^
1.9 x 10°
2.1 x 10
2.0 x lOg
2.0 x 10,
8.2 x 10^
7.6 x 10:?
1.2 x 10°
2.7 x 10°
2.2 x 10*
2.4 x 10;?
4.9 x 10
4.4 x 10g
5.0 x 10,
6.9 x 101
1.1 x 10'
8.0 x 10;?
2.7 x 10*
2.1 x 10°
5.4 x 10,
6.5 x 10;?
9.5 x 10?.
7.9 x 10;
8.1 x 10°,
1.1 x 10,
1.2 x 10,
1.3 x 10,
1.0 x 10'
4.3 x 10°
Particle
size,
> \im
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-6
2,000
2,000
750
940
320
170
140
120
180
200
80
220
160
150
100
160
70
63
77
85
84
61
1,200
850
290
240
250
230
95
250
600
2,100
120
470
470
220
220
110
72
380
Particle
size,
> \im
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                          162
-------
Table F-4 (continued).   FINE PARTICLE DATA FOR BAGHOUSE INFLUENT,  TEST  5
Clock
time
1442
1444
1446
1448
1450
1453
1459
1501
1504
1506
1515
1517
1519
1521
1523
1525
1527
1529
1531
1533
1535
1538
1600
1613
1616
1619
1622
1624
1625
1628
1634
1636
1638
1642
1644
1646
1652
1655
1658
1700
Phase of
process
cycle

Reboil








Tap

First
melt











Back
charge
Second
melt











Compartment
being
cleaned








































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10-°
4.6 x 10J?
4.8 x 10^
4.4 x 10:
5.0 x 10:
4.4 x 10°
1.1 x lo£
4.0 x 10£
4.1 x 10^
3.5 x 10°
3.9 x ior
1.1 x 10,
1.2 x 10,
1.2 x 10'
3.5 x 10^
3.7 x 10°
2.3 x 10°
6.3 x 10^
7.5 x 10;?
8.5 x 10^
6.5 x 10;?
8.2 x 10^
1.6 x 10,
2.8 x 10;?
8.9 x 10g
1.0 x 10*?
7.0 x 10|?
4.2 x 10£
3.4 x ID,?
1.7 x 10^
1.6 x 10?
3.5 x lO^
1.3 x 10:?
1.1 x 10°
2.2 x 10°
1.4 x 10:
2.2 x lo£
1.6 x 10,
9.9 x 10;?
3.0 x 10:?
1.3 x 10°
Particle
size,
> um
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.021
0.021
0.021
0.021
0.021
0.021
0.021
0.021
0.033
0.033
0.033
0.033
0.033
0.033
0.048
0.048
0.048
0.071
Dust counter
Particle
concentration,
particles/
m3 x 10-6
1,600
1,500
290
310
570
270
300
1,500
1,300
1,400
3,500
4,700
4,900
2,900
990
2,600
4,300
2,500
2,100
2,800
2,700
1,800
440
150
250
220
190
830
4,200
1,400
190
210
470
540
150
270
580
590
260
400
Particle
size,
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                                 163
-------
Table F-4 (continued).  FINE PARTICLE DATA FOR BAGHOUSE INFLUENT, TEST 5




Clock
time
1703
1705
1707
1711
1714
1721
1724
1728
1730
1733



Phase of
process
cycle








Slag
off



Compartment
being
cleaned










Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
1.2 x lOg
1.5 x 10,
1.1 x 10°
2.5 x 10°
5.2 x 10°
1.2 x 10'
1.3 x 10,
1.3 x 10,
1.4 x 10'
1.3 x 107

Particle
size,
> urn
0.071
0.071
0.071
0.048
0.048
0.014
0.014
0.014
0.014
0.014

Dust counter
Particle
concentration,
particles/
m3 x 10-6
600
480
690
660
120
130
87
140
750
110

Particle
size,
> ym
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                               164
-------
Table F-5.  FINE PARTICLE DUST FOR BAGHOUSE EFFLUENT, TEST 6
Clock
time
1050
1054
1057
1059
1105
1108
1113
1119
1121
1124
1129
1135
1140
1144
1147
1150
1152
1156

1226
1230
1232
1235
1237
1243
1245
1247
1249
1253
1256
1300
1303
1307
1309
1310
1313
1316
1319
1321
Phase of
process
cycle
First
melt















Back
charge
Second
melt













Slag off




Compartment
being
cleaned


#10


//I

#2


#3

#4



#5


//8



#9



#10


//I



#2



#3
Condensation nuclei
counter
Particle
concentration ,
particles/
m3 x 10~6
2,000
2,000
90,000
12,000
5,000
43,000
14,000
4,000
22,000
4,000
12,000
12,000
7,000
72,000
21,000
12,000
6,000
12,000

85,000
54,000
39,000
33,000
90,000
70,000
35,000
36,000
85,000
25,000
25,000
26,000
11,000
11,000
4,000

30,000
3,000
3,000

Particle
size,
> ym
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025

Dust counter
Particle
concentration ,
particles/
m3 x 10-6
29
22
15
16
14
28
53
32
30
18
14
12
1.8
21
3.4
3.3
1.8
19

33
11
4.0
3.1
17
6.9
3.7
1.6
4.8
4.8
2.7
3.6
2.1
1.0
1.5

17
1.9
1.4

Particle
size,
> urn
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.?

0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3

0.3
0.3
0.3

                             165
-------
Table F-5 (continued).  FINE PARTICLE DUST FOR BAGHOUSE EFFLUENT, TEST 6
Clock.
time
1323
1325
1327
1331
1333
1334
1337
1340
1344
1349
1352
1355
1357
1400
1402
1405
1406
1407
1409
1416
1420
1426
1430
1432
1439
1445
1452
1455
1458
1504
1506
1510
1516
1520

Phase of
process
cycle





Reboil







Tap




First
melt













Back
charge
Compartment
being
cleaned




//4






#6




#4


*7



#9




//I




#3

Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
41,000
38,000
25,000
6,000

30,000
7,000
8,000
100,000
3,000
4,000
4,000
22,000
11,000
8,000
4,000

36,000
3,000
3,000
31,000
34,000
80,000
68,000
14,000
11,000
50,000
9,000
3,000
38,000
19,000
7,000
17,000
8,000

Particle
size,
> Mm
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015

Dust counter
Particle
concentration,
particles/
m3 x ID"6
31
6.8
2.8
2.7

29
4.9
2.5
1.2
6.9
5.3
3.2
5.2
8.2
8.6
7.9

44
8
1.8
48
3.1
32
6.2
9.7
23
5.6
2.4
1.4
31
2.1
1.1
5.7
1.8

Particle
size,
> pm
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3

0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3

                                   166
-------
Table F-5 (continued).   FINE PARTICLE DUST FOR BAGHOUSE EFFLUENT,  TEST 6




Clock
time
1524
1547
1550
1553
1557
1601
1603
1605
1609
1615
1618
1621
1623
1630
1630
1630
1630
1630
1630
1630
1632
1632
1632
1634
1634
1634
1634
1634
1634
1635



Phase of
process
cycle
Second
melt











Slag off



















Compartment
being
cleaned





















Unknown








Condensation nuclei
counter
Particle
concentration,
particles/
m3 x ID'6
16,000
69,000
45,000
24,000
28,000
20,000
5,000
2,000
7,000
10,000
20,000
13,000
13,000
40,000





36,000











Particle
size,
>_ ym
0.015
0.021
0.021
0.021
0.0025
0.033
0.033
0.033
0.0025
0.048
0.048
0.078
0.078
0.078

















Dust counter
Particle
concentration,
particles/
m3 x 10-6
1.3
40
1.1
0.78
0.87
3.3
2.9
2.9
1.9
7.0
6.6
18
8.5
110
14
11
3.5
3.5
1.8
3.5
11
2100
3500
350
35
18
11
3.5
1.8
140

Particle
size,
> vim
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.5
1.0
2.0
3.0
3.0
2.0
1.0
0.5
0.3
0.5
1.0
2.0
3.0
5.0
10.0
0.3
                                   167
-------
Table F-6.  FINE PARTICLE DATA FOR BAGHOUSE INFLUENT,  TEST 7
Clock
time
1'58
1303

1308
1314
1316
1323
1325
1334
1336
1340
1345
1350
1355
1402
1416
1421

1431
1441
1444
1451
1456
1502
1508
1525
1528
1530
1532
1534
1536
1538
1540
1551
1553
1555
1559
1601
1603
1605
1608
Phase of
process
cycle
Tap
First

melt












Back
charge
Second
melt









Slag
off










Compartment
being
cleaned









































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
1.7 x 10^
1.4 x 10..
7
1.3 x 10'
1.0 x 10'
8.8 x 10°
8.0 x KK?
8.1 x 10,
8.1 x 10°
1.7 x 10,
1.3 x 10'
4.4 x 10g
3.9 x 10,
8.4 x 10°
1.7 x 107
3.8 x lo£
4.3 x 10
7
1.3 x 10'
9.1 x 10,
1.0 x 10'
7.4 x 10?
9.5 x 101
1.0 x 10'
8.9 x 10g
5.4 x 10;?
9.4 x 10°
1.7 x 10,
1.7 x 10'
8.2 x 10b
3.9 x lO^
2.6 x 10
5.3 x 10°
4.0 x 10^
5.7 x lO;?
3.7 x 10,
2.0 x 10,
1.4 x 10,
1.6 x 10,
1.7 x 10,
1.5 x 10
Particle
size,
>_ pm
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-6
	
—

—
_
.^
—
—
—
—
_
—
—
—
—
—
—

—
—
—
	
	
—
—
650
540
560
510
530
570
540
580
600
840
480
530
540
280
280
360
Particle
size,
^_
—

—
—
^
—
—
—
—
—
—
—
—
—
—
—

—
—
—
	
	
—
—
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                          168
-------
Table F-6 (continued).   FINE PARTICLE DATA FOR BAGHOUSE INFLUENT,  TEST 7




Clock
time
1611
1617
1631
1633
1635
1638
1641
1644
1646
1648
1650
1652
1654
1656
1700
1710
1713
1715
1717
1719
1721
1723
1725



Phase of
process
cycle

Reboil


Tap

First
melt


















Compartment
being
cleaned























Condensation nuclei
counter
Particle
concentration ,
particles/
m3 x ID'6
1.8 x 10g
2.8 x 10:?
5.0 x 10
4.3 x 10°
5.6 x 10r
1.1 x 10,
1.1 x 10'
3.2 x 10°
4.0 x 10^
3.3 x 10°
3.8 x lO^
2.2 x 10°
1.9 x 10,
1.1 x 10,
1.7 x 10,
2.2 x 10,
2.2 x 10,
1.9 x 10,
1.5 x 10,
1.7 x 10,
8.2 x 10°
8.5 x 10*
1.6 x 107

Particle
size,
> pm
0.0025
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

Dust counter
Particle
concentration,
particles/
m3 x 10~6
260
400
79
130
59
54
39
150
310
320
190
170
540
2,200
1,100
610
890
960
680
1,800
1,900
3,800
4,200

Particle
size,
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                                169
-------
Table F-7.  FINE PARTICLE DATA FROM BAGHOUSE EFFLUENT, TEST 8
Clock
time
1130
1133
1135
1138
1140
1142
1143
1153
1155
1158
1200
1202
1204
1206
1214
1216
1219
1221
1223
1225
1227
1229
1231
1235
1236
1238
1241
1243
1245
1247
1252
1254
1256
1258
1300
1301
1305
Phase of
process
cycle
First
melt

















Back
charge
Second
melt














Compartment
being
cleaned




//10






//I
















#5








Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
29,000
50,000
22,000
3,500
15,000
9,000
24,000
2,000
5,000
8,000
5,000
32,000
4,000
4,000
95,000
65,000
14,000
7,000
10,000
4,000
4,500
7,500
24,000
25,000
55,000
25,000
12,000
10,000
15,000
50,000
15,000
10,000
12,000
52,000
25,000
15,000
17,000
Particle
size,
>_ jam
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration >
particles/
m3 x ID"6
21
6.8
7.6
4.0
23
7.4
4.2
2.5
1.8
1.8
4.4
25
2.6
1.6
15
16
7.1
5.6
7.8
3.1
11
7.0
1.8
26
8.1
1.8
2.4
1.5
22
27
2.1
0.90
1.3
46
2.7
2.68
1.5
Particle
size,
> ym
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
                              170
-------
Table F-7 (continued).  FINE PARTICLE DATA FROM BAGHOUSE EFFLUENT, TEST 8




Clock
time
1307
1310
1312
1314
1316
1319
1324
1331
1333
1335
1337
1339
1341
1343
1345
1355
1357
1359
1400
1404
1406
1409
1600
1603
1603
1611
1615
1621
1635



Phase of
process
cycle









Slag off











Reboil
First
melt








Compartment
being
cleaned







Shake





















Condensation nuclei
counter
Particle
concentration,
particles/
m3 x ID'6
8,000
115,000
130,000
70,000
65,000
35,000
35,000
185,000
100,000
13,000
8,500
15,000
34,000
40,000
34,000
16,000
17,000
12,000
9,000
50,000
58,000
41,000
4,000
3,000
5,000
4,000
14,000
6,600
11,000

Particle
size,
>_ pm
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.021
0.021
0.021
0.033
0.033
0.047
0.078

Dust counter
Particle
concentration,
particles/
m3 x 10-6
1.3
62
26
10
4.8
4.5
6.2
24
7.5
5.0
3.8
2.9
4.7
37
2.4
7.2
2.5
1.2
1.5
47
11
3.7
19
13
0
6.8
3.9
16
16

Particle
size,
> pm
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.5
0.3
0.3
0.3
0.3
                                   171
-------
Table F-8.  FINE PARTICLE DATA FOR EAGHOUSE INFLUENT, TEST 9
Clock
time
1120
1124
1126
1128
1130
1132
1134
1136
1138
1144
1146
1148
1150
1152
1154
1156
1204
1206
1208
1210
1212
1215
1220
1227
1250
1252
1255
1258
1304
1306
1308
1311
1314
1316
1318
1320

1322
1340
1343
Phase of
process
cycle
Second
melt







Reboil









Tap

First
melt












Back
charge
Second
melt

Compartment
being
cleaned








































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10-°
8.4 x 10*
4.3 x 10*
5.3 x 10^
1.3 x 10'
5.7 x 10*
6.7 x 10 £
1.2 x 10^
5.7 x 10*
1.1 x 10'
8 x 10*
9.8 x W
9.1 x 10g
9.1 x 10;!
6.3 x 10;?
9.9 x 10°
7.6 x 10°
6.8 x 10^
5.4 x 10g
4.4 x 10^
3.1 x 10*
6.3 x 10^
7.1 x 10:
1.0 x 10g
5.1 x 10
6.0 x 10;?
4.9 x 10*
6.1 x 10^
6.3 x 10*
6.0 x 10^
8.4 x 10g
7.6 x 10,
7.5 x 10*
1.2 x 10'
9.4 x 10g
3.5 x 10
4.8 x 106
7
1.1 x 10'
5.5 x 101
1.1 x 10
Particle
size,
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0..0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025

0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-6
2.3 x 10?
3.0 x 10?
2.8 x 10;
2.4 x 10J
300
4
2.7 x 10?
2.7 x 10?
2.5 x 10?
3.5 x HT
410
140
3
2.5 x 10?
2.9 x 10?
2.8 x 10?
3.6 x 10?
3.4 x 10;
6.3 x 103
730
6
2.5 x 10?
3.0 x 10?
3.0 x 10?
2.2 x 10?
2.0 x 10?
2.0 x 104
970
2.2 x 10?
2.1 x 10*
2.2 x 10,
1.3 x 10J
330
22
8
9

18
19
37
Particle
size,
> urn
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.3
0.3
0.3
0.5
0.3
0.3
0.3
0.5
1.0
2.0
3.0
5.0

10.0
0.3
0.3
                          172
-------
Table F-8 (continued).  FINE PARTICLE DATA FOR BAGHOUSE INFLUENT,  TEST 9
Clock
time
1346
1349
1352
1354
1356
1358
1400
1405
1407
1409
1411
1413
1416
1418
1421
1423
1459
1501
1503
1505
1507
1509
1511
1513
1525
1527
1530
1532
1534
Phase of
process
cycle



















Slag
off


Reboil





1536
1538
1540
1542
1550
1552
1554
1556
1600
1602
1604
1606
lap
First
melt






Compartment
being
cleaned









































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x ID"6
3.6 x 10J?
7.8 x 10^
5.1 x 10°
7.7 x 10°
1.7 x 10'
3.0 x 10°
1.5 x 10°
4.5 x 10°
5.2 x 10°
3.6 x 10°
5.7 x 10,
1.3 x 10£
5.1 x 10°
3.2 x 10;
4.2 x 10°
5.1 x 10^
2.2 x 10°
1.4 x lO^
3.0 x 10:?
9.0 x 10°
2.9 x 10*
8.0 x 10°
8.6 x 10°
9.8 x 10°
3.5 x 10°
1.9 x 10°
1.5 x 10°
3.1 x 10°
2.0 x 10°
1.3 x 10°
1.3 x 10°
9.2 x 10^
7.9 x 10*
3.4 x 10°
1.5 x 10°
8.1 x 10*
1.2 x 10°
1.3 x 10°
8.4 x 10*
1.2 x 10°
1.2 x 10°
Particle
size,
>_ Vim
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.015
0.048
0.048
0.048
0.048
0.048
0.068
0.068
0.068
0.068
0.033
0.033
0.033
0.033
0.021
0.021
0.021
0.021
Dust counter
Particle
concentration,
particles/
m3 x 10-6
2.1 x 10*
1.1 x 10J
550
16
16
17
16
2.2 x 10;
2.6 x 10*
2.4 x 10*
1.2 x 103
350
16
16
15
16 4
2.6 x 10*
2.6 x 10*
1.2 x 103
190
19
20
18
18 3
6.0 x 10;
5.9 x 103
1.1 x 103
7.9 x 103
7.2 x 103
6.4 x 10;?
3.6 x 103
4.4 x 103
1.6 x 103
9.2 x 103
5.3 x 10,
3.0 x 10J
18 3
1.6 x 10,
5.3 x 10;*
4.0 x 103
20
Particle
size,
>_ pm
0.3
0.5
1.0
2.0
3.0
5.0
10.0
0.3
0.3
0.3
0.5
1.0
2.0
3.0
5.0
10.0
0.3
0.3
0.5
1.0
2.0
3.0
5.0
10.0
0.3
0.3
0.5
0.5
0.3
0.3
0.3
0.5
1.0
0.3
0.5
1.0
2.0
0.3
0.5
1.0
2.0
                                173
-------
Table F-9.  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT TEST, 10
Clock
time
1229
1231
1233
1235
1237
1239
1241
1243
1245
1247
1249
1251
1253
1255
1257
1259
1301
1303
1305
1307
1309
1311
1314
1316
1318
1321
1323
1325
1327
1329
1331
1333
1335
1338
1340
1342
1344
1346
1348
1349
Phase of
process
cycle
Second
melt


















Slag
off












Reboil





Compartment
being
cleaned








































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
31,000
19,000
14,000
9,000
60,000
80,000
29,000
25,000
21,000
19,000
89,000
60,000
24,000
11,000
9,000
14,000
22,000
21,000
18,000
3,000
7,000
80,000
21,000
9,000
11,000
5,000
26,000
12,000
21,000
15,000
13,000
10,000
80,000
49,000
50,000
47,000
30,000
170,000
55,000
32,000
Particle
size,
> ym
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
Dust counter
Particle
concentration,
particles/
m3 x 10-6
67
67
67
67
66
69
69
68
67
67
42
20
8.8
9.3
7.1
6.0
14
2.9
2.0
1.8
0.0
1.0
71
6.1
1.6
0.0
67
70
66
4.7
1.27
0.06
59
61
65
29
14
0.64
70
71
Particle
size,
> pm
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.5
0.5
0.5
0.5
0.5
0.5
1.0
1.0
1.0
1.0
2.0
2.0
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
                           174
-------
Table F-9 (continued).  FINE PARTICLE DATA FOR BAGHOUSE EFFLUENT TEST,  10
Clock
time
1351
1353
1355
1357
1359
1401
1403
1405
1407
1409
1411
1413
1417
1419
1454
1456
1502
1504
1506
1509
1511
1513
1515

1517
1535
1537
1539
1545
1547
1555
1557
1559
1601
1603
1605
1607
1609
1611
1613
1616
1618
Phase of
process
cycle





Tap

First
melt













Back
charge
Second
melt
















Compartment
being
cleaned










































Condensation nuclei
counter
Particle
concentration,
particles/
m3 x 10~6
25,000
32,000
24,000
16,000
30,000
20,000
24,000
24,000
25,000
10,000
3,000
4,000
8,000
5,000
12,000
8,000
3,000
12,000
25,000
5,000
8,000
7,000
10,000

1,600
18,000
14,000
33,000
11,000
14,000
8,000
5,000
13,000
13,000
14,000
14,000
7,000
10,000
16,000
13,000
14,000
8,000
Particle
size,
> urn
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.0025
0.015
0.015
0.021
0.021
0.021
0.021
0.021
0.021
0.021

0.021
0.033
0.033
0.033
0.033
0.033
0.078
0.078
0.078
0.078
0.078
0.078
0.048
0.048
0.048
0.048
0.048
0.048
Dust counter
Particle
concentration,
particles/
m3 x 10-6
73
31
14
0.80
70
72
64
10
38
0.74
68
67
69
75
78
72
70
79
65
65
5.4
8.7
80

74
77
74
34
106
74
69
72
9.1
37
9.1
2.7
64
70
79
5.4
11
2.1
Particle
size,
> pm
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.5
1.0
2.0
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.3
0.5
1.0
0.3

0.3
0.3
0.3
0.5
0.5
0.3
0.3
0.3
0.5
1.0
0.5
1.0
0.3
0.3
0.3
0.5
0.5
1.0
                                 175
-------
                                TECHNICAL REPORT DATA
                          (Please read Instructions on the reverse before completing)
1  REPORT NO
EPA-600/7-77-023
                                                      3 RECIPIENT'S ACCESSION-NO.
4 TITLE ANDSUBTITLE
 FRACTIONAL EFFICIENCY OF AN ELECTRIC ARC
 FURNACE BAGHOUSE
            5. REPORT DATE
            March 1977
            6. PERFORMING ORGANIZATION CODE
7 AUTHORIS)

 Reed W. Cass and John E. Langley
            8. PERFORMING ORGANIZATION REPORT NO

             GCA-TR-76-34-G
9 PERFORMING ORGANIZATION NAME AND ADORESS
 GCA/Technology Division
 Burlington Road
 Bedford, Massachusetts 01730
                                                       10. PROGRAM ELEMENT NO.
             E HE 624
            11. CONTRACT/GRANT NO.
             68-02-1438, Task 4
12 SPONSORING AGENCY NAME AND ADORESS
 EPA, Office of Research and Development
 Industrial Environmental Research Laboratory
 Research Triangle Park, NC 27711
            13. TYPE OF REPORT AND PERIOD COVERED
             Task Final;  6/5/74-2/77
            14. SPONSORING AGENCY CODE
             EPA/600/13
15 SUPPLEMENTARY NOTES TERL-RTP task officer for this report is J.H.  Turner, Mail Droo
 61,  919/549-8411 Ext 2925.
is ABSTRACT
          The j-gp^j. gives results of an evaluation of the performance of a fabric
 filter system controlling emissions from either one or two 30-ton electric arc fur-
 naces producing a high-strength, low-alloy specialty steel.  The evaluation involved
 measuring the system's total mass collection efficiency and apparent fractional col-
 lection efficiency.  Testing involved 8 sampling days with one furnace operating,  and
 2 days with two furnaces.  Baghouse influent and effluent streams were sampled with
 total mass samplers, inertial impactors, a condensation nuclei counter (CNC), and
 an optical dust counter.  The influent and effluent total fluoride concentrations were
 measured for three of the tests to estimate the particulate and gaseous fluoride levels
 to which the Dacron filter bags are exposed during normal service.  Total mass tests
 showed baghouse mean mass efficiency to be 97. 9% with one furnace operating, and
 98.7% with two furnaces.  Mean mass concentrations for one- and two-furnace oper-
 ation were 0.0014 and 0.0019 grains /dscf, respectively.  Influent impactor tests
 showed considerable size distribution differences as a function of the phase of the
 process:  the greatest concentrations for the particles sized occurred during the
 first melt. Effluent impactor size distribution tests suggested agglomeration.
17
                             KEY WORDS AND DOCUMENT ANALYSIS
                DESCRIPTORS
                                          b IDENTIFIERS/OPEN ENDED TERMS
                         c.  COSATl Field/Group
 Air Pollution
 Dust
 Polyester Fibers
 Fabrics
 Filtration
 Electric Arc Furnaces
Air Pollution Control
Stationary Sources
Fabric Filters
Baghouses
Fractional Efficiency
13B
11G
HE

07D
13A
13 DISTRIBUTION STATEMENT

 Unlimited
19 SECURITY CLASS (This Report)
Unclassified
21 NO OF PAGES
 185
                                          20 SECURITY CLASS (This page)
                                           Unclassified
                                                                   22. PRICE
EPA Form 2220-1 (9-73)
                                         177
-------