TTE2E5IB1JL1T Y OF FABRIC FILTER
AS GAS - SOLID CONTACTOR TO
CONTROL GASEOUS POLLUTANTS
F. M. Veazie
W. H. Kiehneyer
OWENS-CORNING FIBEEGLAS CORPORATION
GRANVILLE, OHIO
FINAL REPORT
UNITED STATES DEPARTMENT OF HEALTH,
EDUCATION, AND WELFARE
CONTRACT No. PH 22 - 68 - 64
-------
FEASIBILITY OF FABRIC FILTER AS GAS-SOLID
CONTACTOR TO CONTROL GASEOUS POLLUTANTS
.FINAL REPOR T
F. ~unro Veazie
WIlliam H. Kle1meyer
Owens-Corning Fiberglas Corporation
Granville, Ohio 43023
August, 1970
Contract No. PH-22-68-64
Prepared for
Department of Health. Education and Wc1fare
U. S. Public HeaJ th Servlce
National Air Pollution Control Administration
-------
FEASIBILITY OF FABRIC FILTER AS GAS-SOLID
CONTACTOR TO CONTROL GASEOUS POLLUTANTS
F. Munro Veazie
-------
FORWORD
TABLE OF CONTENTS
Page' No,
PAR T I - PROGRAM DIGEST
I. INTRODUCTION 1
II. BRIEF DESCRIPTION OF TES l' EQUIPMENT AND
OPERATING PROCEDURES 4
III. SUMMARY OF RESULTS AND DISCUSSION 8
A. Slaked Limes and Slaked Dolomitic Limes 8
B. Manganes e Dioxide 15
C. Alkalized A1 umina 16
D. Nahcolite 17
E. Precoating versus Continuing Addltion 17
F. Fly Ash Addition ZO
IV. CONCLUSIONS Zl
V. RECOMMENDA TIONS ZZ
PART II - PROGRAM DETAIL
I.
EQUIPMENT DESCRIPTION
Z5
II.
A.
B.
C.
D.
E.
TEST PROCEDURE
35
General
Additive Study
Flue Gas Flow Rate Study
Fly Ash Study
Pre coated Bag Study
35
38
39
40
41
III.
RESULTS
43
A.
B.
C.
D.
Effect of Reactanl Type on SOZ Removal
Eff"ct of Flue Gas Flow Rate on SOz Removal by
Various AddItives
Effect of Fl y Ash on SOZ Removal
Effect of Gas-Solids Contacling Methods on
SOZ Removal
43
53
64
-------
TABLE OF CONTENTS (ConLmued)
AppendlX A -
B -
C -
D -
E -
F -
G -
Derl vaUoll of Stoic.hlomeLJ.'y Equalion
ReprcsC"ntaLive Test Data
Computed Tes t Data
Sulfur Anal ysis
ReacLant Physical Properties
Coulter Counter Particle Size Analysis
-------
LIST OF FIGUHES
Page
Figure 1 Schematic Drawing of Process
Filter Bag PIlot Test FacIlity 5
Figure 2 Typical S02 Breakthrough Pattern-
Contlnuous Reactant Injectlon 9
Figure 3 Typical S02 Breakthrough Pattern -
Precoated Bags 10
Figure 4 Removal of Sulfur Dioxide with Slaked Lime at
Air /Cloth Rabo of 6. 0 £t/min 11
Figure 5 Filter Bag Test Facility 26
Figure 6 FIlter Bag Chamber 31
FIgure 7 Schematic Drawing of Process
S02 Sampling System 33
Figure 8 Removal of Sulfur Dioxide with Slaked LIme
(1% NaCl) at Air/Cloth Ratio of 6.0 £t/min 44
Figure 9 Removal of Sulfur Dioxide with Slaked Dolomitic
Lime at Au /Cloth Ratio of 6. 0 £t/min 45
FIgure 10 Removal of Sulfur Dioxide with Slaked Dolomitic
Lime (1% NaCl) at Air/Cloth Ratio of 6. 0 ft/min 46
Figure 11 Removal of Sulfur DIoxide with Manganese
Dioxide at Air/Cloth Rab.o of 6.0 £t/min 47
Figure 12 Removal of Sulfur DIoxide with Slaked Lime
at Air /Cloth Ratlo of 8. 0 ft/mll1 54
Figure 13 Removal of Sulfur DIoxide wIth Slaked Dolomitic
-------
LIST OF FIGUH1';S (Contil1ue'd)
Figure 14
Flgure 15
Figure 16
Flgure 17
Removal of Sulfur Dioxlde Wllh Slak('d
Dolomitlc Llme (1% NaCJ) at Au/C)oth Ralio
8. 0 ft/mln
Removal of Sulfur DlOxlde with Manganese Dl0xlde
at Air /Clolh Ratio of 8. 0 It/min
Efficiency of Alkalized Alumina
Reaction Versus Temperature
Sulfur DioXlde
Removal of Sulfur Dloxide with Manganese
Dioxide on Bag Surfaces at Air/Cloth Ratio =
8.0 ft/min
Page'
56
57
58
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Table I
Table 2
Table 3
Table 4
Table 5
Table 6
Table 7
Table 8
LIST OF TAB LES
Sulfur Dloxidc Removal wIth Contmuous
Reactant Injectlon
Flue Gas Analysis
Maximum Average Mole Percent S02 Removed
Maximum Average Mole Percent S02 Removed
per Molar EquIvalent of Reactant
Sulfur Dioxide Removal Efficiencies of
Reactants
Sulfur Analysis of Reacted Dusts from Selected
Alkalyzed Alumina Trials
Results of Fly Ash Study
Results of Precoated Bag Study
Page
12
29
48
52
59
63
65
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FOIUO:WORD
ThIS repo rt covers the work perfoJ"med by Owens- Corning FIberglas
Corporation at GranvIlle, Ohio under Conlract No. PH-22-68-64 during
the period April, 1968 to February, 1970.
The contract was under the technical direction of James F. Durham,
NAPCA, Cinclnnah, OhIO.
The program was conducted by the New Glass Development Department
of the Owens- Corning Fiberglas Technical Center.
Mr. F. Munro Veazie
was program technical manager, Mr. WIlliam H. Kielmeyer was prin-
cipal invest,gator and Mr. T. F. McGann was administrative manager.
Many of the pieces of equipment mentioned in this report were commercial
items that were not developed to operate as applied during this study.
Any failure to meet the objectives of this study is no reflection on any of
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PAR T 1
-------
I.
INTHODUCTION
Fabric filters have, for many years, beC'n used by various mdubtries for
removing fine solid matter from exhaust or flue gas streams.
Recently,
the metals industries have found lhat when reactive materials are injected
into the flue gas streams, such filters can also be used to reduce certain
objectionable gaseous components in these streams.
The materials act to
combine physically or chemically with such gases, converting them to
solid form.
The fabric, in turn. provides a surface upon which the prod-
ucts of the reaction can be collected and also functions to keep the unreacted
material in the path of the gas flow.
In the aluminum industry, injecting
activated alumina dust into a fabric filter house resulted in a substantial
decrease in the concentration of gaseous hydrogen fluoride emanating from
the electrolytic reduction of aluminum oxide.
For its role in objectionable gas removal. the fabric filter seems particularly
well suited, for several reasons.
It permits, for example, the use of
extremely fine reactant particles to enhance both the rate and extent of gas
absorption.
Because fabric fillration is dry, it provides the products of
reaction in a form that normally requires little or no treatment before
either disposal or subsequent use.
Also, the fabric filter affords at least
two ways t~t the reactant can be introduced to the waste stream - either by
direct injection into the slream ahC'ad of the fabric or by exposure after
being deposited on the fabric surfaces -- and C'ach of these methods can
-------
lead to Idnc'( icaHy diffeJ:cnt gas-solid rcsponses.
SpecificaJly, if the method
of introduction is by direct inj(~ctiol1. the reactant behaves like a fluidized
(transport) bed from the point of mjectlon to the' point of cOUection on the
filter surface's and thereupon it acts like a fixed bed.
When deposited on
the fabric surfaces initially, the reactant functions exclusively like a fixed
bed.
The principal limitation of fabric filters in general is temperature, most
commercially available filters are unable to survive for long periods much
above 550°F.
This limits the use of many of the more promising gas re-
actants which function most efficiently at temperatures well above the
filter capability.
Slaked lime. a strong 502 absorbent, for example, has
its highest removal capacity at around 800°F.
Recognizing that a need existed for a filter fabric able to withstand high
temperatures. Owens-Corning Fiberglas Corporation (OCF) carried out
an extensive in-house program to develop such a material.
The result
was an S-glass cloth treated with a proprietary inorganic finish which
preliminary investigations indicated would resist degradation by temperature
to l200°F.
In order to evaluate the new fabric as a filtermg media, OCF
subsequently built at corporate expense a stainless steel fabric filter test
facility capable of simulating many field applications to tempcratures
-------
up to lOOO"F.
The lebl facUity can be usc.d Lo assess bolh the fllLrallOn
characteristics of a fabric and lhe chemical contacting characteristics
of fabric filtl"rs.
Under contract with lhe Division of Process Control Engineering of the
National Air Pollution Control AdministratioJl, Owens-Corning embarked
on a program to evaluate the chemical contacting potential of fabric filters
with emphasis on the 600-l000°F temperature range according the new
fabric capability.
The gas selected for investigation was 50Z, a toxic air
pollutant, currently being discharged into the atmosphere by industrial
sources at a rate of 3Z million tons annually.
In this investigation, the
50Z was carried in flue gases that closely resembled in composition the
effluent of coal-burning facilities, since these
units constitute the major
50Z emission sources. The reactants chosen for consideration consisted
of materials which had demonstrated ability to remove 50Z in other inves-
tiga tions.
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II.
TEST EQUIPMI'~NT ANn OPERA TING PHOCJ<;DURE
OCF had made several equipment changes* in lhelr &mall scale fIlter bag
test facility lo meet th(' conditions rcquired for obtaimng m('anful data on
SOz removal.
A schematic representation of thlS test facility is presenled in Figure 1.
Arrows indicate the direction of flue gas flow during test operalion.
Currently the facility is equipped to provide:
1.
A preselected effluent gas composition from a natural gas
source (see Table Z of Part II).
2.
Controlled effluent gas temperatures in the range from 3000 F
to 1000°F.
3.
Injection of special gases such as SOZ at various concentrations.
4.
Reactant lnjections at various stolchiometric ratios**.
5.
S02 monitoring on both the input side and the output side of
the bag house.
6.
Reactant and particulate matter collection in a six bag (each
5 3/4" diameter x 68" long) stainless steel bag house.
7.
Measurement and control of gas flow rate between ZOO and 600 cfm.
A detailed description of the equipment is included in Part II of this report.
*
All changes were corporately funded.
**
Stoichiome tric ra tio, as applied to this report, represents thE" ratio of
the weighl of reactant injected to the weight which would theoretically
be required to combine with all of the special gas in the stream. A
stoichiometric ratio of 2.0 indicatC's that twice as much material is
addC'd as is required by chemica! balancing.
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-
lJ
3.
MIDDLE
DUCT
@
FILTER
SCHEMATIC DRAWING OF PROCESS
BAG PILOT TEST FACILITY
*=ELECTRONICALLY CONTROLLED VALVE
-e- PNEUMATICALLY ACTUATED VALVE
-0- MANUAL VALVE
. THERMOCOUPLE
r-' S02 SAMPLING PROBE
o BAG PRESSURE TAP
"'1"1
-.
ca
.
~@
l..
...
REACTAN
INJECTIO
I :->t.
, ..i:~ .~...'
4~v;1~i~tt~f!t~~~1':~~:
, ,'-~'"
... '-.:"
. .- .
0, .....
-------
The testing program lnvolved the evaluahon of seven fine-grained materials
as SOZ sorbents under various conditions of gas stream temperature, flue
gas flow rate, and reactant Input level.
The reactants examIned were
slaked lime, slaked dololnitic lime, promoted slaked lime (slaked lime
containing 1% NaGl which was dissolved in the slaking water), promoted
slaked dolomitic lime (also containing 1% NaCl), manganese dioxide,
alkalized alumina, and Nahcolite (a mIneral composed of approximately
700/0 sodium bicarbonate).
Each of these was tested in a narrow range of
temperatures which, according to previous Investigations, resulted in
peak capacities for SOZ.
Two methods were used to introduce the reactant to the SOZ: (1) continuous
injection into the flue stream before the bag chamber, and (Z) deposition
on the bag surfaces in advance of the stream.
In one investigation, fly
ash was admitted along with reactant to ascertain whether or not the fabric
filter could be used to remove both solid and gaseous pollutants simul tan-
eously.
In all cases, the SOZ content of the input gas was held to approximately
Z800 ppm.
In each experiment, the test equipment was fust brought to equilibrium
at the selected tes t temperature.
The flue gas flow rate was set at the
required value, and depending on whether the reactant and SOZ were
-------
brought logethC'r by continuous jnjC"ctlon or by bag precoatmg, the S02 or
reactant was admitted to Lhe gas stream.
In continuous injC'ction. the S02
injection rate was adjus ted to briug the effluent to the es LaLli&hcd S02
content and after stream conditions had stabIlized, Lhe reactant was Intro-
duced at the selected stoichiometric level.
In bag pre coating, 50Z was
admitted after the stream had transported all of the required amount of
reactant to the surfaces of the bags.
WIth either mode of reactant-gas
contact, measurements were made of the SOZ content of the Input and out-
put gases, the pressure drop across the bags. and the temperature of the
bag house dur.ng SOZ-reactant interaction.
Bag cleaning was accomplished by reverse air flow and shaking of the
bag s .
Between the test and cleaning periods, samples of solids which
had fallen to the base of the bag chamber were taken for sulfur determina-
tion.
A new set of bags was installed for each new reactant or every 7Z
operating hours whichever occurred first.
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III.
~ESUL TS AND DISCUSSION
Typical 502 breakthrough palterns oblained during experimenlation are
shown in Figures 2 and 3.
The sharp drop followed by a more gradua] de-
cline in S02 concentration pictured in Figure 2 is common among tests in-
vol ving continuous injection of reactant.
The S- shaped curve of Figure 3,
on the other hand, accrues to tests in which the bags were precoatedj this
latter curve is representative of breakthrough patterns obtained with many
fixed bed reactors.
If, in Figure 2 or 3, the area between the breakthrough curve and the line
representing the initial S02 concentration in the flue gases is divided by
the time of the test, the average concentration of SOZ removed during the
run is obtained.
Joining together the average removal values from several
related tests yields a set of curves like that of Figure 4, which shows the
association between percent SOZ removal, bag temperature. and reactant
input level for one absorbent.
Curves such as these have been used to com-
pile Table I. which summarizes the findings of all tests involving continuous
reactant injection.
A.
Slaked Limes and Slaked Dolomitic Limes
As Table I indicates, the slaked Urnes and slaked dOlomitic limes
look particularly attractive for removing SOZ from gas streams at
high temperatures.
Of the two types of reactant, though. the slaked
lime demonstratC'd a slightly higher removal capacIty under the same
operating conditions.
Maximum absorption with both types of lnaterial
occurl"ed at 800°F.
-------
TYPICAL 502 BREAKTHROUGH PATTERN
CONTINUOUS REACTANT INJECTION
3000
2500
E 2000
a-
a-
...
~
o
VI 1500
t-
III
...
t-
::)
o
1000
500
. 0
UPL-14F
o
30
15
45
60
TIME, min.
Fig. 2
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TYPICAL 502 BREAKTHROUGH PATTERN
PRECOATED BAGS
3000
2500
E 2000
a.
a.
,
C"4
o
en 1500
t-
III
...
t-
:)
o
1000
500
o
o
15
30
MN-10B
45
60
TIME, min.
Fig.3
-------
80.0
~
::»
o
% 70.0
.~
I
8/
ft
/ 0
X; /
/ I
/ I
fIx
I
I
I
8
III
"'Z
Zo
...
u
~ Z 60.0
...-
LO
III
III>
= 0 50.0
.!
III~
~ ~
o 40.0
8ft
o
.
BAG CHAMB[R TEM! (oF)
700 o-.__..~
800 . .
900 ..----x
II.
o
.
30.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
5.0
REMOVAL OF SULFUR DIOXIDE WITH
SLAKED LIME
AT AIR/CLOTH RATIO OF 6.0 ft./min.
Fig. 4
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Table 1
SuI fur Dioxide Removal with
Continuous Reactant Injection
Reactant: Slaked Lime
Flow Rate:
Stoichiometric Level:
Bag Temperature
100°F
8000 F
9000 F
1.0
290 cfm
2.0
3.0
385 cfm
2. 0 3. 0
400/0
46%
65%
52%
64%
18%
10%
51%
81%
65%
14%
91%
81%
Reactant: Promoted Slaked Lime (l% NaCl)
Flow Rate:
Stoichiometric Level:
Bag Temperature
1000 F
8000 F
9000 F
1.0
290 cfm
2.0
41%
55%
66%
56%
Reactant: Slaked Dolomitic Lime
Flow Rate:
Stoichiometric Level:
Bag Temperature
100°F
8000 F
9000 F
1.0
290 cfm
2.0
3.0
68%
80%
10%
3.0
385 cfm
2.0 3.0
30%
40%
52%
34%
54%
64%
49%
40%
55%
44%
52%
10%
60%
Reactant: Promoted Slaked Dolomitic Lime (l% NaCl)
Flow Rate: 290 cfm 385 cfm
Stoichiometric Level: 1.0 2.0 3.0 Z.O 3.0
Bag Temperature
1000 F: 43% 55% 44% 60%
800°F 28% 51% 69% 55% 13%
9000 F 50% 65% 60% 69%
-------
Reactant: Manganese Dioxide
Flow Rate: 290 cfm 385 cfm
Stoichiometric Level: 1.0 2.0 3.0 2.0 3.0
Bag Temperature
5000 F 620/0 72% 56% 70%
6000 F 28% 54% 74% 57% 74%
700°F 58% 73% 60% 73%
Reactant: Alkalized Alumina
Flow Rate: 290 cfm 385 cfm
Stoichiometric Level: 1.0 1.0
Bag Temperature
3000F 97%
4000 F 80% 93%
5000 F 60% 74%
,
Reactant: Nahcoli te
Flow Rate: 290 cfm 385 cfm
Stoichiometric Level: 0.8 0.7
Bag Temperature
3000 F 59% 60%
Increasing the gas stream flow rate sharply increased the S02 con-
version. Also. promoting the lime reactants tended in general to en-
hance"a.bsorption, but the effect was rel&.tively minor except for
-------
slaked dolomitic lime at 9000 F.
Increased removal at higher flow
.-
rates indicates LhaL diffusion or mass transfer is controlhng the gas-
solids reacLion.
Despite the high SOZ removal values obtainable with the slaked limes
and slaked dolomitic limes, the relatively high stoichiometric input
rates necessary to achieve these results show that the reactant
utilization (the proportion of reactant involved in the conversion) and
hence the reaction efficienc y were very low.
In fact, as can be de-
termined by dividing the removal values in Table I by the appropriate
stoichiometric terms and then comparing the results. increasing the
reactant input to absorb more SOZ netted a decrease in reactant
utilization.
Slaked lime, for example. at one stoichiometric input
level, captured 40% of the 50Z from an 800°F gas stream flowing at
Z90 cfmi however. when discharged into the same stream at three
times stoichiometric requirements, it removed less than twice as
much SOZ -- its efficiency (removal per stoichiometric input value)
had dropped from 40 to Z6%.
Obviously, consideration of the slaked
limes and slaked dolomitic limes as reactants in a commercial 50Z-
removing venture musL take into account the added cost per unit
quantity of SOZ removed which would accompany a rise in 50Z con-
versioh.
The low efficienc y of SOZ removal by slaked lime and
-------
slaked dolomite may require. for economic reasons, the regenera-
tion of the products of reaction in specific emission cases.
B.
Mangane s e DIoxide
Manganese dioxide is unique among the candidate reactants tried.
Within experimental conditions, its ability to remove SOZ did not
appear to be affected by either flue gas flow rate or temperature.
Moreover, increasing the stoichiometric input level of MnOZ in-
creased SOZ conversion but not at a major expense to reactant
utiliza. tion.
Because of its high cost, the utility of manganese dioxide as a re-
actant in commercial applications depends strongly on its ability
to be regenerated.
Beinstock and Field* found several ways of
converting the product of reaction, MnS04, to a reactive form of
manganese oxide; chemical oxidation with either (NH4}ZSZOa or
NaZC03 and electrolysis looked especially promising from a tech-
nical standpoint.
However, before MnOz can be considered for large-scale SOZ-
removing applications, the efficiencies and expense of these re-
generation processes would have to be evaluated.
* Beinstock, D. and Field, F. S. "Bench-scale Investigatlon on Removing
Sulfur DIoxide from Flue Gases." J. Air Pollution Control Ass'n.,
v. 10 n. Z, April 1960. pp lZI-1Z5.
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C.
Alkalized Alumina
Clearly. alkalized alumina ranks as a very prom] sing absorbent.
As Table I shows, it functioned well at low temperatures, its re-
moval efficiency was high, and like the slaked limes and slaked
dolomitic limes, it became more respondent to SOZ at hlgher flue
gas flow rates.
At a temperature of 300DF and a flow rate of 385 cfm.
one stoichiometric level of alkalized alumina absorbed nearly 100%
of the 502 present in the gas stream.
The high removal value obtalnable with alkalized alumina in a
filter baghouse is meaningful. for fabric filters can accept reactant
particles down to 0.5 micron in diameter.
The use of finel y divided
. reactant largely eliminates the problem of mechanical attrition of
particles, a factor which has plagued many removal processes
requiring large alkalized alumina grains.
The regeneration of fine particle size reacted alkalyzed alumina has
not been investigated on a large scale.
The economics of such re-
generation would have to be determined before the overall economics
of the use of alkalyzed alumina can be established.
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D. Nahcolitc
Although a subject of limited experimentation, Nahcolite responded
favorably with sulfur dioxide in all cases. Like alkalized alumina,
it operated at low temperatures and was efficient, absorbing 75 and
85% of its potential capacity at 290 cfm and 610 cfm respectively.
It is not known if Nahcolite can be regenerated. Also, accurate
data on the cost of the material are not currently available. The
use of Nahcolite in many emission source streams would probably
be too expensive unless regeneration were possible or some applica-
tion could be made for the reaction products. Sodium sulfate, the
principal product of conversion, is extremely water soluble; if
deposited or otherwise left to itself without further processing, it
could develop into a serious water pollution problem.
E. Precoating versus Continuous Addition
All of the results reported above pertain to reactants which were
introduced directly into the sulfur-bearing stream. As mentioned
earlier (Page 1), there are two regions in the filter bag chamber
where chemical combination can occur: one is the "so-called" transport
section in front of the bags where the reactant particles are entrained
in the gas stream, and the other is on the surfaces of the bags where
the particles are finally deposited. It is of interest to know what
-------
portion of the SOZ convcl"sion is traccablc to whIch scction. and in
particular, what proPQrtion can bc relcgatcd to the fixed bed on lhe
bag surfaces.
Onc possibilily for doing this lies in a comparIson of
the sulfur contents of solids which had collected in the base of lhe
bag chamber before and after the bags were cleaned.
Presumably,
the solids which had settled out before cleaning (the "fallout") were
those which had initially been captured by the gas stream but lacked
sufficient momentum to reach the surfaces of the bags. A sulfur
analy~is of this material would reflect reaction in the transport
region on1y*.
The material recovered after cleaning (the "dus t cake ")
on the other hand consisted of particles which had traveled the entire
length of the reaction zone in the bag unit and then became attached
to the bags.
Its sulfur content would reflect reaction in both regions.
The portion of SOZ conversion taking place specifical1 y on the bags
could be determined by noting the difference in the analyses of the
two samples.
* Presuming the fallout to be representative of entrained material may
be an oversimplification. All fallout deposits contained some solids
which had been part of the dust cake. but bccame dislodged from the
bags at the end of the run due to a sudden easing of bag flexure. More-
over, the assumption was made that once the solids had settled out of the
stream they were no longer capable of absorbing SOZ. Observations
indicate that the sulfur contribution made to the fallout by the dust cake
and the stream after particle settling was slight.
-------
The sulfur concenLral1ons of reaction product& from several repre-
sentativc tests are contained in Appendix D.
Because Lhese values
are presented as weight percents. only approximate indications of
the extent of reaction in each region can be given. According to
this listing, the siLe of the reaction depended on the reactant in-
volved.
WIth promoted slaked dolomitic lime, 40 to 60% of the con-
version occurred on the bags.
With alkalized alumina, manganese
dioxide. the slaked limes and unpromoted slaked dolomitic lime,
more than 700/0 of the appropriate reaction took place during transport.
These percentage figures are onl y approximate.
Further experimen-
tation would be required to establish the exact values.
When precoating was used to introduce reactant into the filtering
system. bag coating was achieved by entraining the reactants in a
hot 50Z-free flue gas stream directed through the bag house.
When
the desired stoichiometric ratio of material had built up on the
bags. 50Z was admitted to the stream above the baghouse and the
concentration of the gas beyond the bag house was monitored. All
of the calcium-based reactants -- the slaked limes and slaked
dolomitic limes -- responded poorly to the 502' because they had
reacted with C02 in the flue gas stream prior to 502 introduchon.
-------
Manganese dioxidc. noL being affcctcd by COZ in the coatmg sLream.
was capable of removing large amounts of SOZ. At a stoichlOmetrlc
ratio of 3.0 and a gas flow of 385 clm, lt consumcd nearl y 900/'0 of the
SOz aL temperatures between 500 and 7000 F.
F.
Fly Ash Addltion
With reactant and fly ash both entrained in the flue gas s tream, no
loss of reactant activity with SOZ was observed.
In facti two of the
five reactants tested - promoted dolomitic lime and Mn0Z - actually
removed more SOZ with fly ash present than when it was absent.
Based on these f1ndings. a filter bag unit could serve both as a
chemical contactor for gas removal and as a collector of particulate
matter simultaneously.
Elimination of solid pollutants upstream
from a baghouse would depend on factors other than gas removal
efficiency I factors such as the end use of the solids collected in the
baghouse and the expense of processing them for this use.
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IV.
CONCLUSIONS
The results of this study have demonstrated the technical feasibility of
using a glass fabric filter bag house as a collector of reacted materials
and as a contactor for reactants to remove objectionable gases from ex-
haust gas streams up to temperatures of 900° F.
Of the reactant materials investigated in the temperature range of 700° F
to 900°F. slaked lime and slaked dolomite are possible candidates for
502 remova.l in the filter bag system from a standpoint of reactant effi-
ciency, total 502 removal and potential economical cost.
In the temperature range of 300°F to SOO°F, alkalyzed alumina proved to
be very effective for 502 removal. but would probably require regeneration
for its econo:mical use.
Nahcolite. a naturally occurring sodium bicarbonate, is also effective
in removing 502 in the temperature range of 300°F to SOO°F but would
also require regeneration to be economical.
Manganese dioxide can be used most effectively in the temperature range
of SOO°F to 700°F. but also requires regeneration to be economically
us e ful.
-------
v.
RECOMMENDA TIONS
The results and conclusions reached under this contract lead to several
questions. the answers to which would lead to better unders landing of the
mechanism of SOZ removal and permIt an economic analysis of the system
to be made.
In the filter bag house test facility at OCF. the distance from reactant
injection to the entrance of the effluent gas into the bags is only two feet.
If this distance were increased, it might result in increased SOZ removal
because of increased exposure time of reactant to SOZ gas.
Lower
stoichiometric ratios could show better reactant utilization under the
longer exposure time and thus reduce reactant costs in field applications.
This factor should be investigated.
Referring to the observation of increased SOZ removal at higher effluent
gas flow rates, no attempt was made to determine the effect of reactant
particle size and shape on SOZ removal at different gas and flow rates.
It is possible that reactant particle size and shape will be a factor under
such conditions.
If acceleration of the reactant particle is part of the
phenomenon of increased SOZ removal at higher flow rates. it seems
logical that reactant particle physical characteristics are unimportant.
The effect of reactant particle size and shape on SOZ removal at various
-------
effluent gas flow rates should be established.
This can be an important
factor in the economics of 502 removal.
In thes e studies. the 502 content of the input effluent gas was maintamed
at 2800 ppm in all experiments.
The effect of higher and lower 502
effluent gas contents on the removal rate of the various reactants should
be studied.
It is quite possible that there may be fairly large differences
in the reaction rates of the various reactants at varying 502 effluent gas
con ten ts .
The cos ts for 502 removaL couLd be majorl y effected by this
factor.
The mechanism for 502 reaction under dynamic conditions should be
studied in more detail.
It can have major effects on the choice of re-
actant and its physical characteristics, and on the amount of reactant
used.
Economics for field applications of the bag house system can be
more firmly set when the reaction mechanism is established.
The high temperature filter bag developed by OCF has not had large scale
field trials.
This can be an important economic factor in the use of the
lower cost reactants such as slaked limes and doLomites.
Bag life should
be established to allow economics for field applications to be projected.
No work in this investigation was carrit."d out on techniques of regeneratIon
of the reactants after use.
There are some reports in the literature of
-------
the possibility of transforming CaS04 and MnS04 to the basic oxides.
The regeneration of the reactants can have an important impact on the
economics of field operation and on waste disposal problems.
This
should be established.
-------
PAR T II
-------
I.
EQUIPMENT DESCRIPTION
The re are four basic elements which compos e the equipment used in the
project: (1) a boiler assembly which produces flue gases that are channelled
to the remainder of the test facility; (Z) a system for injecting SOZ into the
flue gas stream; (3) a reactive dust feeder which discharges into the
stream; (4) a filter bag chamber which serves to collect the solid material
in the stream and also to support any reaction between the injected dust
and SOZ.
In addition to these elements. there are various regulatory and
control mechanisms to rnaintain strearn temperature, stream flow rate,
and the concentration of SOZ in the flue gases. Also provided are sensors
for rneasuring and recording pertinent test information such as SOZ con-
tent upstrearn and downstream of the bag chamber, and bag pressure loss.
All of these components are shown in functional perspective in Figure 1
(which was presented in Part Iof this report). An actual picture of the
tes t facility appears in Figure 5.
The function of the boiler assembly, shown on the left of Figure 1, is to
provide simulated flue gases representative of the products of coal-burning
but without SOZ.
To form these gases, natural gas and air are combined
in a special nozzle-mixing burner system, rated at 1,980.000 Btu/hr.
A
gas lair ratio regulator located in the natural gas line ahead of the burner
permits adjustments in the air inlet supply to vary the quantity of flue
gases generated without varying their compositions.
-------
FILTER
BAG
TEST
FACILITY
-------
The boiler proper':<
consists basically of a long combustion tube which
connects to the burner. a vertical transport shaft, and a parallel arrange-
ment of 116 small cooling tube s; all of thcs care sealed and immer sed in
water, as shown in the schematic in Part I of this report.
Exhaust gases
from the burner pass along the combustion tube and then divide into two
branch streams; one of these streams passes directly through to the out-
side of the boiler at a temperature of approximately l400°F; the other
branch stream passes back into the upper part of the boiler box through
the small cooling tubes where its temperature is lowered to about 250° F.
The proportion of gases flowing through each branch is regulated by a
butterfly valve in the stream outside the boiler proper,
Valve B**,which
is in the 250°F line, is manually operable; Valve A in the l400°F branch
is governed by a thermocouple located downs tream from Tee 1 where the
two branch streams rejoin.
By automatic manipulation of Valve A and
manual adjus tment of Valve B, confluent stream temperatures (tempera-
tures downstream of Tee 1) ranging from 250°F to 1000°F are possible
without the need for changing natural gas and air valve positions in the lines
leading to the burner. Becaus e of the heat exchanger- boiler and. a gas lair ratio
*
designed for Owens-Corning Fiberglas by Babcock and Wilcox Company,
Barberton, Ohio.
**
refer to' Figure 1 for the locations of valves and other designated items
-------
regulator employed in the unit, the boiler assembly as a whole is capable
of supplying flue gases at variable flow rates and temperatures without
significantly affecting their composition.
Flue gas analyses made on
samples taken from the confluent stream attest to this capability (see
Table 2).
After leaving the boiler assembly, flue gases may traverse any of three
paths in the course of a tes t run.
The routes taken depend on the stage
of the test--experimental, cleaning, or intermediate.
During the experi-
mental stage, sometimes referred to in this report as the filtering cycle,
some of the gases pass through the lower duct and enter into the base of
the filter bag chamber.
The res t of the s e combus tion produc ts. how eve r ,
bypass the bag chamber and go directly to the stack.
Control Val ve C in
the upper duct, activated by an orifice plate in the lower duct, determines
the proportions of gases following each route.
The main purpose of this
control system is to compensate for variations in flow resistance in the
bag house by forcing more or less of the flue gases through the lower duct
as the pressure rises or falls respectively.
In this way the flow rate of
gases into the bag house is maintained constant.
Valve D, located in the
upper duct, remains open during the entire filtering cycle.
As gases flow through the lower duct, they pick up 502 and 502 re-
actants.
The 502 used is commercial grade (99.9% pure) bottled gas
-------
Table 2
Flue Gas Analysis*
Flue Gas Inlet
Temperature Air
(at the rmo- Se tting
couple con- (frac tion Percent of Volume
trolling. of full
Val ve A) open) H20 N2 02 Ar C02
700°F 3/4 3. 80/0 82. 10/0 5. 10/0 1. 0 % 8. 00/0
300°F 1/2 2.8 83.1 4.7 1. 0 8. 5
700°F 1/2 3.8 80.1 7.3 . 9 7. 9
800°F 3/8 3.2 80.6 4.8 1.1 10.4
1l00°F 1/2 3.2 79.5 6. 1 .9 10.3
* by mass spectrometer
-------
material.
It is introduced into the flue gas stream ahead of the orifice
plate under 20 psig pres sure.
The rate of flow is regulated using a stand-
ard rotameter with a stainless steel float and 1/4 inch diameter tube.
A
commercially available vibrating screw feeder provides reactant injection
at a controlled rate.
An air jet at the end of the feeder tube aids in dis-
persing the reactive powder in the flue stream.
The filter bag chamber (Figure 6) is essentially a large stainless steel
cylinder with a shallow conical base.
The unit can accomodate eight bags
68 inches long by 5-3/4 inches I. D.; in this program only six bags were
used at a time.
As shown in Figures 1 and 6, the bags are fitted over
collars on two stainless steel baffle plates.
The lower mounting plate is
fixed, i. e. welded completely to the side of the chamber. and has openings
at the center of the collars.
The top plate, on the other hand, is completely
solid but is smaller than the bottom plate and is suspended by two rods from
an external bracket.
During the filtering cycle, gases flowing into the
bottom of the chamber rise through the openings in the lower mounting
plate into the center of the bags. pass through the bag walls where they
deposit entrained dust, and exit the chamber around the periphery of the
top mounting plate.
The gases enter the stack above the bag chamber by
means of the duct containing Valve G.
-------
FIL TER
BAG
CHAMBER
f
I
-------
In and around the bag chamber, there are three sets of sensors provided
to monitor the condition of the gas stream ~s it passes through the bags.
Thermocouples in the top, middle. and bottom sections of the chamber
sense gas temperatures.
Two ports. one below and one above the bags.
are provided for measuring pressure loss across the bags resulting from
the accumulation of reactive dust on their surfaces.
Additionally, two
gas sampling probes are inserted in the unit, one ups tream from the bag
house in the lower duct and one downstream in the duct containing Valve G.
Each samp~ing line is equipped with particulate matter and water vapor re-
moval apparatus as indicated in Figure 7.
Both of the lines feed into a
modified infrared detector which preferentially monitors SOZ concentration
in the gas stream.
The description of the test facility thus far has centered around the flow
of flue gases during the experimental stage of testing.
There are, as men-
tioned earlier. two other stages of the test operation -- a cleaning stage
and an intermediate stage.
In neither of these stages do the gases pass
through the lower duct into the base of the filter bag chamber.
In the
cleaning stage. designed to free the bags of dust accumulated during
filtering. some of the gases enter the top section of the bag chamber through
the middle duct. flow backwards through the bags. and exit to the stack
through the. duc t containing Valve H.
As during the filter cycle, a portion
-------
FLUE WALL
SAMPLE TUBE
WITH INLET FILTER
MEASURING
CELL
VENT
SAMPLE VENT
CONNECTION
1ft
CD
.
~
ANALYZER
FILTER
.;~~~~~~.
GAS SELECTOR
MANIFOLD
SCHEMATIC DRAWING OF PROCESS
S02 SAMPLING SYSTEM
:.:.:::'
,',',','
,',',','
I',',','
:::'::.:
~~:~~;:~:
:::::.;
.:..:.
~:t;~~
;I~~~;
,",','
::"':'::
WATER
~~;f:~~;~~t~~;~;~~~~~~
FILTER
(GASES AND VAPORS)
PRIMARY
CONDENSER
INTERCONNECTING
SAMPLE LINE
AIR BLOW-BACK
OR PURGE VALVE
VENT
.:.~:
l::.. . RELIEF VALVE
(SECONDARY) REFRIGERATED
CONDENSER
~~ .:;;:~ UPSCALE CALIBRATION
GAS (sPAN)
SAMPLE
::::~.::;:.tt:::::}>
:::.'i~;;:::::.~~~:i~:~~:
DOWNSCALE CALIBRATION
GAS (ZERO)
-------
of the gases goes directly to the stack through the upper duct.
Valve D
(rather than Valve C which is fully open during cleaning) controls the
proportion of gases entering the bag chamber.
It is fitted with mechanical
stops; the degree to which Valve D is opened depends on how encrusted the
dust layer is on the bag surfaces.
In addition to reverse air flow, cleaning is also effected through mechanical
shaking of the bags.
A motor-driven eccentric, connected to tie rods
above the top bag-mounting plate, vibrates the tops of the bags at about 200
cycles a minute over a 1-1/2 inch horizontal span.
Immediately before and after the cleaning stage, all of the combustion
gases pass through the upper duct.
These periods constitute the inter-
mediate stages of testing.
During these times, Valve I can be manually
opened to allow filtered dust to be deposited in a drum for sampling and
weighing.
-------
II.
TEST PROCEDURE
A.
General
The test procedure was generally the same from one run to the next.""
Before each run, hot flue gases from the boiler were introduced
into the base of the filter bag chamber to bring the chamber to the
required test temperature (as determined by the center thermocouple).
When this temperature was reached and could be maintained at the
gas flow rate specified for the test, 502 was injected into the flue
gas stream.
The rotameter on the 502 input line was adjus ted
until. according to the 502 analyzer, the concentration of the toxic
gas downstream from the bags had stabilized around 2800 ppm. At
this point, additive dust was injected into the stream at a controlled
rate, and the te st started.
During the run, which was timed and normally lasted one hour, the
following information was recorded continuously:
(a)
the temperatures at the top, middle, and bottom of the
bag chamber.
. (b)
the pressure drop across the bags.
*
with the exception of the Precoated Bag Study
-------
(c)
the concentration of 502 on the "clean" side of the
bags.
At the end of the run, the 502 and additive feed system shut off auto-
matically, Valves G and E closed, and all of the flue gases bypassed
the bag chamber completely.
Valve I was opened to remove material
which had settled to the bottom of the bag chamber during the run.
This fallout was weighed. and samples were taken for sulfur anal ysis.
After removal of fallout matter, the bags were cleaned.
The dust-
cake which was dislodged from the bags was collected for sampling
and weighing.
Examination of test equipment prior to the start of the project study
had revealed that the variable speed reactant feeder was unable, at
constant dial settings. to reproduce delivery rates within acceptable
limits.
This failing negated the planned method for determining the
weight of material expended during a test, which was based for each
reactant on a fixed relationship between reactant delivery rate and
feeder dial setting.
As an alternative approach. a volumetric pro-
cedure was devised.
This consisted of first establishing a reference
level of material in a narrow section of the hopper. adding a known
amount of reactant above this level before a run, and after the run.
adding or removing material until the reference level was again
-------
established.
The weight of material initially added, plus or minus
the weight of reactant added or removed at the end of the run re-
spectively was considered the weight of reactant consumed by the
te st.
In preliminary investigations, this volumetric approach netted
results that were within 2% of the actual weights delivered.
5ince
the margin of error is within the limits of accuracy for the entire
filter bag system, this method was adopted for use in the test
pro gram.
50 that comparisons could be made between the abilities of several
additives to remove 502 under similar conditions, the amount of
material injected into the stream was converted from a weight to a
stoichiometric basis*.
The formula for this conversion is:
5 =
Wr (T + 460)
5.95 x 10-4 cft M
Where 5
=
the stoichiometric ratio of additive to 502
Wr =
the weight in grams of solid sorbent used during the run
T =
the temperature of reaction in 0 F -- equivalent to the
middle bag chamber temperature
c
=
the concentration level of 502, in ppm, before reactant
contact
* one stoichiometric input level of additive is the amount (or weight) of
dust theoretically capable of reacting with all of the 502 in the gas stream.
-------
t
=
the time of the run, in minutes
M=
the gram equivalent weight of the solid additive, i. e.
the weight of material in grams necessary to completely
react with 64. 0 grams of S02 on a theoretical (non-
kinetic) basi s
Derivation of this formula appears in Appendix A.
All of the tests conducted as part of the program were incorporated
into four study series -- the Additive Study, Flue Gas Flow Rate
Study, Precoated Bag Study, and Fly Ash Study.
The following
sectic::ms describe the major objectives sought and test conditions
for each of these study series.
B.
Additive Study
In the first study series. major emphasis was placed on evaluating
seven promising materials as S02 sorbents under various conditions
of bag chamber temperature and additive level.
The seven candidates
were slaked lime, promoted slaked lime (10/0 NaCl), slaked dolomitic
lime, promoted slaked dolomitic lime (10/0 NaCl), manganese dioxide,
Nahcolite (a naturally occurring mineral consisting of 700/0 NaHC02),
and alkalized alumina.
Of these materials, Nahcolite and alkalized
alumina were in short supply and were added to the flue gas stream
only near 1. 0 stoichiometric level.
All other additives were dis-
charg"ed into the stream at from 1. 0 to 3.0 times stoichiometric
-------
input requirements.
Each type of additive dust was studied in a tem-
perature range which earlier reports indicated facilitated peak SOZ
removal.
For Nahcolite and alkalized alumina, this temperature
range was 300°F to 500°F; for MnOz, it was 500°F to 700°F; and
for the calcium based additives, the range was 700°F to 900°F.
All other factors which could affect the sorption rates were held con-
stant.
Except in the alkalized alumina tes ts, which ran for 30
minutes, the normal test operating or filtering time was 60 minutes.
In all of the tests the SOZ concentration in the flue gases did not vary
more than 100 ppm from Z800, cleaning time was maintained at 10
minutes, and the flow rate was Z90 cfm, which corresponds to an
air- to-cloth ratio of 6.0 it/min.
c.
Flue Gas Flow Rate Study
The second study series involved determination of the impact of the
flue gas flow rate on S02 removal.
The space velocity of the stream
was raised from its former value of 290 cfm to 385 cfm, a value
corresponding to 8.0 ft/min
air-to-cloth ratio.
Many of the tests
conducted under the additive study were rerun here, although with
the faster gas stream.
-------
D.
Fly Ash Study
The third study series treated the effect of fly ash on S02 removal.
The ash. an incombustible solid by-product of coal-burning, is
present in flue gas streams emanating from coal-fired boilers.
Fly
ash does not itself react with S02; however. in some removal pro-
cesses it interferes with the treatment of S02 and therefore must be
withdrawn from the flue gas stream ahead of the S02 reaction
chamber.
The third study series was executed to determine if fly
ash can be tolerated in the filter bag process, or if some means has
to be provided to eliminate it before the S02 can be treated.
In carrying out this investigation. it was necessary to blend the fly
ash with the solid reactant and feed both from the additive feeder,
for no provision in the test facility was made to inject fly ash singly.
Five reactants were considered - - two limes, two dolomitic limes
and manganese dioxide -- and each was mixed with the fly ash so
that under presumed tes t conditions. two stoichiometric levels of
reacti ve dus t would be injected and the concentration of fly ash
would be four grains / cu. ft. of flue gas.
Two runs were made per
mix (except in the case of Mn02), the second being essentially a
repeat of the first. All of the limes and dolomitic limes were tes ted
-------
at 8000 F bag temperature; the MnOZ runs were m.ade with the bag
temperatures at 6000 F.
The stream flowed constantly at 385 cfm.
E.
Precoated Bag Study
The fourth study series considered a second method of introducing
the reactive additive material to the SOZ.
In the first three study
series, unreacted dust was injected directly into the SOZ-laden
stream. and deposited (along with reacted material) on the filter bags.
In the second method, additive material was deposited on the bags
before the sulfur-containing gases were admitted into the filter bag
chamber.
The study was conducted principally to examine the per-
formance characteristics of a reactant as a thin fixed bed on the sur-
faces of the bags.
The procedure used in this test series differed only slightly from that
used previously.
To coat the bags, a precalculated quantity of re-
actant was discharged into the flue gas stream, which was free of
SOz, and transported to the bag surfaces.
The s tr earn flow ra te
and temperature were approximatel y equal to those required for the
ac tual run.
Before the test started, reactant which had settled to
the bottom of the bag chamber during coating was removed and
weigqed, and the difference between this weight and the weight of
ma~erial discharged into the stream was considered to be the amount
-------
of dust on the bags available for absorption.
When 502 was released
into the gas stream at a predetermined rate of flow, the run began.
The same bag temperature. gas flow rate, bag pressure drop and
502 concentration measurements taken during trials in the first
three study series were also recorded in these trials.
Dus t cake
and fallout were likewise sampled for sulfur content.
The choices of parameters to be investigated were nearly the same
as in the continuous-coating trials.
The low-temperature materials,
alkalized alumina and Nahcolite, were unavailable; manganese dioxide,
promoted and unpromoted slaked lime and dolomitic lime. the high
temperature reactants, were involved in these tests in the same ranges
of stoichiometries as in the Additive and Flow Rate Studies.
Gas
flow rates were 290 and 385 cfm as before; as in the earlier study,
temperatures of the bags were selected to complement the particular
reactant under consideration.
The only basic difference between
these studies and the series of studies which preceded them was the
manner in which the reactive material was brought into contact with
the S02-bearing stream.
-------
III.
RESU L TS
Sulfur dioxide breakthrough curves and bag pressure loss curves taken from
representative tests are pictured in Appendix B.
Appendix C contains in
tabular form pertinent data from all the tests performed.
The results of
sulfur analysis on several selected dustcake and fallout sample pairs are
found in Appendix C.
In both Appendices D and C the test findings are
grouped according to the study under which the tests were performed.
A.
Effect of Reactant Type on 502 Removal
If the findings of the various tests from the Additive Study are analyzed
and compared, several general observations can be made.
Some
trends are particularly evidenl in the curves in
Figure 4 and in
Figures 8 to 11, which summarize the 502 removal data obtained
from the lime and manganese dioxide trials.
The slaked lime and slaked dolomitic limes look very attractive as
502 sorbents at 8000 F.
Of the two, however, the slaked limes
demonstrated a much greater capacity for 502'
This finding is
supported in Table 3, which lists the reactants and the highest 502
removal values obtained with them at each of three stoichiometric
levels.
-------
90.0
~
5 80.0
%
.
.
III
t-Z
Z 0 70.0
III
~!
III
11.0
III 60.0
III>
~o
CI
~III
~ ~ 50.0
iC ~
o
en
II. 40.0
o
.
/
/X
. )//
~
Xt/,' 00 X
~I
Xl'
I
BAG CHAMBER TEMR ("F)
700 o---_..~
800 . .
900 X----X
30.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
5.0
REMOVAL OF SULFUR
SLAKED LIME
AT AIR/CLOTH RATIO
DIOXIDE WITH
(1 % NaCI)
OF 6.0 ft./min.
-------
70.0
~
:)
o
::t
.
60.0
o~
/7
II//x
1:1
/
x/x
III
t-Z
zo
III
U
~ ! 50.0
III
A.a
III
III>
eo
c ~ 40.0
~III
III~
~
COt
o 30.0
1ft
.
BAG CHAMBER JEMIC"F)
700 ~__n-o
800 . .
900 x-----x
II.
o
20.0
0.0
1.0
2.0
3.0
4.0
5.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
REMOVAL OF SULFUR DIOXIDE WITH
SLAKED DOLOMITIC LIME AT AIR/CLOTH
RATIO OF 6.0 ft./min.
-------
70.0
60.0
.
r
./
~
:)
o
:I:
1M
...z
zo
1M
Uz
~ - 50.0
1M
A.o
1M
1M>
~o
C I 40.0
~IM
IM~
~ ~
o 30.0
1ft
.
.
BAG CHAMBER TEMP. COF)
700 0-------0
800 - .
900 ",""----X
...
o
20.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
5.0
REMOVAL OF SULFUR DIOXIDE WITH
SLAKED DOLOMITIC LIME (1% NaCI)
AT AIR/CLOTH RATIO OF 6.0 ft./min.
-------
80.0
~
~
o
:z: 70.0
30.0
0.0
.
BAG CHAMBER TEMR (oF)
500 0-------0
600 . .
700 x- - --x
III
"'Z
Zo
III
~!: 60.0
III
A.Q
III
III>
~ 0 50.0
~!
III~
~ ~
o 40.0
en
u.
o
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
5.0
REMOVAL OF SULFUR DIOXIDE WITH
MANGANESE DIOXIDE AT AIR/CLOTH
RATIO OF 6.0 ft./min.
-------
Table 3
Maximum Average Mole Percent S02 Removed
Stoichiometric Levels
0.75 1. 0 2.0 3. 0
Reactant
4. Promoted Slaked Dolomitic Lime
28
660/0 800/0
65 78
62 74
51 69
52 64
1. Promoted Slaked Lime
410/0
2. Unpromoted Slaked Lime
40
3. Manganese Dioxide
28
5. Unpromoted Slaked Dolomitic Lime
30
6. Alkalized Alumina
650/0
7. Nahcolite
59
The slaked limes achieved between 40 and 800/0 removal of S02 at
8000 F and at stoichiometric levels of from 1. 0 to 3.0; the dolomitic
limes removed between 30 and 700/0 under the same conditions.
Promoting sla.ked lime with 1.,-. NaCl generally enhances its S02 re-
moval ability.
The effect is almost negligible when the bag temper-
ature is 8000 F, particularly at low stoichiometries. and also at high
additive levels when the bag temperature is 9000 F.
However, at
7000 F bag temperatures, there is an increase of about nine percent
points at 2.0 stoichiometry (from 46 to 550/0) and four percentage
-------
points at 3.0 stoichiometry (64 to 68%).
There is a four percentage
point increase at the Z.O stoichiometric level (5Z to 56%) when the
bag temperature is 9000 F.
Promoting slaked do1omitic lime with NaCl increases its capacity
for SOZ at high stoichiometric levels and high temperatures.
The
effect is particularly apparent at 9000 F; unpromoted dolomitic lime
absorbed only 340/0 of the SOZ at a stoichiometry of Z. 0 and on! y 49%
at 3.0; promoted dolomitic lime, on the other hand, removed 50%
at 2.0 and 65% at 3.0, a 16 percentage point increase at both additive
levels.
Virtually no difference in performance of the promoted and
unpromoted slaked dolomitic limes is observed at 700°F and at low
stoichiometries at 800 of.
Manganese dioxide falls slightly below the slaked limes in ability to
remove S02, according to Table 3.
However, it functions at lower
gas stream temperatures.
Figure 11 also shows that temperature
has little effect on the percent of S02 that manganese dioxide re-
moves.
The low temperature reactants I Nahcolite and alkalized alumina,
both have large capacities for SOZ.
Nahcolite, when introduced into
the gas stream at 300 ° F (mid- bag temperature) and O. 77 stoichio-
metric level, removed 59% of the gas - - a 77% reaction efficiency.
-------
Alkalized alumina' did somewhat better at the same temperature,
removing 64% of the S02 with onl y 0.78 stoichiometric requirements
of material.
The scarcity of Nahcolite prevented its use in more
than one trial in the Addi ti ve Stud y.
The fact that alkalized alumina demonstrated a high absorption
efficiency (82%) IS meaningful.
This material has drawn consider-
able attention as an S02 reactant, not only because of its affinity for
the gas but also beca.use it is regenerable and yields desirable sulfur
as a by-product of the regeneration process.
In the past, studies of alkalized alumina reactions have been restricted
to vertical absorption towers where the reactant was either suspended
in a rising column of flue gases or entrained in the gas stream and
collected in a plenum chamber for recycle.
In order that a reason-
ably fast current of gases could be maintained without solids carry-
over, it was necessary that the size of the reactant particles be
large, on the order of 1/16 inch in diameter.
Moreover, to be econom-
ical to use, alkalized alumina had to be able to undergo several re-
generation cycles without loss of absorption capacity.
The reactant
met the latter condition. but succes sive regenerations of the pellets
eventually weakened them to the point that they were vulnerable to
attrition damage and could no longer be used in the towers.
Largely
-------
because of this factor, alkalized alumina in pellet form is no longer
considered a
sufficient absorbing candidate in fluidized beds.
In
filter bag systems, by contrast, the mechanical stability of reactant
particles presents no problem since filter bags can contain solid
matter finer than one micron in size.
In fac t, fabric flltration re-
quires the use of much finer (spray-dried) alkalized alumina than
would be acceptable in most fluidized bed systems.
Whether or not
the finer particles are kinetically more active with SOZ than the
pellets and can be satisfactorily regenerated was not studied in this
program, but should be considered in future investigations.
The curves in Figure 4 and in Figures 8 to 10 indicate that although
there is an increase in the amount of SOZ absorbed with increasing
level of reactant added, the efficiency of the reaction or the reactant
utilization drops off.
The meaning of this trend in terms of the
economics of SOZ removal is clear; the higher the quantity of SOZ
removed with a given material under a fixed set of operational con-
ditions. the higher the unit cost (cost per quantity of SOZ removed)
of the process, of regeneration and of solid waste disposal.
Reactant
utilizations at various stoichiometric levels are presented in
Table 4.
-------
Ta bl e 4
Maximum Average Mole Percent S02 Removed per
Molar Equivalent of Reactant
Reactant
Stoichiometric Levels
0.75 1.0 2.0
3. 0
1. Promoted Slaked Lime
(1 % Na Gl )
3. Manganese Dioxide
41 % 330/0 270/0
40 33 26
28 31 25
28 26 23
2. Slaked Lime
4. Promo ted Slaked Dolomitic
Limes (10/0 NaGl)
5. Slaked Dolomitic Lime
30
26
21
6. Alkalized Alumina
800/0
7. Nahcolite
77
In summarizing the results of the additive study series, we note
that the inexpensive, readily available reactants, notably the
limes, require higher temperatures for absorption and are less
efficient than alkalized alumina and Nahcolite which are both costly
and hard to procure.
The addition of NaGl to the limes generall y
aids absorption.
Manganese dioxide, although not especially a
strong reactant, is less influenced by temperature than any of the
other materials tested.
-------
B.
Effect of Flue Gas Flow Rate on 502 Removal by Various Additives
The results of the flow rate test series are summarized in Figures
12 th!ough 15 for the various limes and Mn02, and in Figure 16 for
alkalized alumina.
Only two tests were run with Nahcolite, one at
a gas flow rate of 685 cfm (14. 0 fpm air-cloth ratio) and mid-bag
temperature of 500°F, the other at a gas flow rate of 610 cfm (12.0
fpm air/cloth ratios) and a temperature of 300°F.
These results
(along with those of the other materials) are listed in Appendix C.
Some of the numbers from the above sources are incorporated in
Table 5 which also contains (for comparison purposes) some results
from the additive study.
Excluded from the list of reactants is
promoted slaked lime; it could not be fed consistently enough at the
high flow rate to produce reliable data.
From the table it is apparent that with most of the reactants, the
increase in flue gas flow rate has resulted in an increase in the pro-
portion of 502 absorbed.
In terms of the kinetics of reaction between
gases and solids, this finding is significant for it indicates that
diffusion or mass transfer controls the rate of 502 conversion.
The fact that the residence time, or the time available for
ab-
sorption, is reduced at the higher gas flow rate is perhaps offset by
increased turbulence in the stream which would increase particles - 502
confrontation, by greater 502 striking force, and by more dust being
injected into the stream.
-------
90.0
~
S 80.0
:z:
"
x /
/
/
/
II !
I,
/ I'
X,
!
III
I-Z
Z 0 70.0
III
~Z
111-
A.O
III 60.0
III>
~O
CI
~III
> ~ 50.0
C'~
o
8ft
I&. 40.0
o
BAG CHAMBER TEMR (F)
700 0----..-0
800 . .
900 X-----X
30.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
4.0
REMOVAL OF SULFUR DIOXIDE WITH
SLAKED LIME
AT AIR/CLOTH RATIO OF 8.0 It./min.
-------
80.0
~
:)
o 70.0
:I:
x
...
...z
z 0 60.0
III
uz
~-
III
A.o
... 50.0
III>
~O
CI
8:...
~ ~ 40.0
4C ~
o
en
.
/
/
/ XX/O
/ , 0
/ '
x/
/ "
II
x
o 30.0
BAG CHAMBER TEMPo(OF)
700 0--. ----4)
800 . .
900 X-----X
20.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
5.0
REMOVAL OF SULFUR DIOXIDE WITH
SLAKED DOLOMITIC LIME AT AIR/CLOTH
RATIO OF 8.0 ft./min.
-------
80.0
~
:)
o
:z:: 70.0
x
/
/x
0/
,0
/
III
Z
"'0
Z 60.0
r;Z
~-
III
A.a
III
III > 50.0
~O
CI
~III
III~
~ 40.0
iC C'4
o
lit
xl
,
I
/
,
,
I
~ 30.0
o
BAG CHAMBER TEMR ("F)
700 o--._._~
800 . .
900 x----x
20.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
I
5.0
REMOVAL OF SULFUR DIOXIDE WITH
SLAKED DOLOMITIC LIME (1 % NaCI)
AT AIR/CLOTH RATIO 8.0 It./ min.
-------
80.0
a=
::)
o
:c 70.0
.
III
Z
...0
Z 60.0
~Z
at-
III
A.Q
III 50.0
III>
~O
cl
~III
;: a= 40.0
iC N
o
lit
I&. 30.0
o
.
x
.
BAG CHAMBER TEMR ('F)
500 0-.- --- ~
600 . .
700 x-- --x
20.0
0.0
1.0 2.0 3.0 4.0
STOICHIOMETRIC RATIO,
REACTANT TO 502
5.0
REMOVAL OF SULFUR DIOXIDE WITH
MANGANESE DIOXIDE AT AIR/CLOTH
RATIO OF 8.0 ft./min.
-------
1.00
.
.
N!:! .80
Oat:
",I-
1M
I
o 2 .70
:c
z!:!
00
-I-
~cn
U, .60
CO
D:IM
...>
o
I .50
1M
~
x
~
,
,
X 6 TO I AIR'CLOTH ~\
.
.
... .90
1M
>
1M
...
8 TO 1 AIR: CLOTH
x
.40
300
350 400 450 500
MID - BAG TEMPERATURE (F)
EFFICIENCY OF
ALKALIZED ALUMINA - SULFUR DIOXIDE
REACTION VERSUS TEMPERATURE
550
-------
Table 5
Sulfur Dioxide. Removal Efficiencies of Reactants
Reactant:
Manganese Dioxide
Flow Rate:
Stoichiometric Level:
Bag Temperature:
5000 F
6000 F
700°F
290 c fm
2. 0 3. 0
62%
54
58
Reactant:
Slaked Dolomitic Lime
Flow Rate:
Stoichiometric Level:
Bag Temperature:
700°F
8000 F
900°F
72%
74
73
290 cfm
2. 0 3. 0
40%
52
34
54%
64
49
385 cfm
2. 0 3. 0
56%
57
60
70%
74
73
385 cfm
2. 0 3. 0
40%
55
44
52%
70
60
Reactant:
Promoted Slaked Dolomitic Lime (1% NaCl)
Flow Rate:
Stoichiometric Level:
Bag Temperature:
7000 F
8000 F
9000 F
Reactant:
Slaked Lime
Flow Rate:
Stoichiometric Level:
Bag Temperature:
700 of
8000 F
9000 F
290 cfm
2.0 3.0
43%
51
50
55%
69
65
290 cfm
2. 0 3. 0
46%
65
52
64%
78
70
- 59 -
385 cfm
2. 0 3. 0
44%
55
60
60%
73
69
385 cfm
2. 0 3. 0
57%
81
65
74%
91
81
Percentage
Point Increase
at 385
2.0
-6
+3
+2
3.0
-2
o
o
Percentage
Point Increase
at 385
2.0
o
+3
+10
3.0
-2
+6
+11
Percentage
Point Increase
at 385
2.0
+1
+4
+10
3.0
+5
+4
+4
Percentage
Point Increase
at 385
2.0
+11
+16
+13
3.0
+10
+13
-------
Sulfur Dioxide Removal Efficiencies of Reactants (continued)
Reactant:
Alkalized Alumina
Flow Rate:
Stoichiometric Level:
Bag Temperature:
300 ° F
400 ° F
500°F
Reactant:
Nahcolite
~
Flow Rate:
Stoichio.:me tric Level:
Bag Temperature:
300 ° F
290 efm
1
Percentage
Point Increase
at 385
385 cfm
1
80%
60
97%
93
74
+13
+14
290 efm
0.8
610 cfm
O. 7
59%
60%
The influence which stream flow rate has on gas absorption varies
with different reactants.
On the one hand, manganese dioxide is
virtually unaffected by either flue gas flow rate or bag temperature.
At a stoichiometric ratio of 3. 0, it removes nearly the same per-
cen tage of 502 at 500 ° F as at 700 ° F whe the r the flow rate is 290
or 385 cfm.
On the other hand, flue gas flow rate has a tremendous bearing on
the sorption of 502 by unpromoted slaked lime at all the stoichiometric
-------
levels and reaction temperatures studied.
The increase in the
percentage points of S02 removed at the higher flow rate runs from
10 percentage points at 700 ° F and a 3.0 stoichiometric ratio to 16
percentage points at 800°F and a 2.0 stoichiometric ratio.
With the slaked dolomitic limes. the effec t of flue gas flow rate
on absorption depends on reaction temperature.
The inc rea s e in
flue gas flow rate significantly aided the reaction ,of S02 with the
dolomitic limestones at 900° F, but had little effect at 700°F.
The flue gas flow rate studies have brought to light some interesting
facts about alkalized alumina.
Firs t, alkalized alumina removed
more S02 at the higher flow rate than at the lower.
Between 400
and 500°F, for example, the increase in flue gas flow rate accounted
for a 15 percentage point rise in reaction efficiency.
Secondl y I the
removal efficiency increased with decreasing temperature in the
300 - 500 ° F range examined.
Third1 y I alkalized alumina achieved
nearly 100% reaction efficiency around 300°F.
All of these are
apparent from the curves in Figure 16.
-------
In view of these fhidings, the data in Table 6 are of special interest.
Lis ted under separate headings in this table are the proportions of
S04, S03' and total sulfur occurring in samples of reacted material
from some of the tests.
Because only the weight percents of the
sulfur forms are given and no other useful data such as the proportions
of sodium are provided, it is rather difficult to arrive at many
quantitative conclusions on the basis of this table.
It would be help-
ful, for example, to know what other oxide components exist in the
samples and in what amounts.
Such information could be combined
with the existing sulfur data to determine the removal efficiencies
of alkalized alumina for the tests covered, and serve as a check for
the removal efficiencies which are based on the alkalized alumina
data in Appendix C.
In the absence of this information. crude approximations of reaction
efficiency can be drawn as long as certain assumptions are made.
It is very evident from Table 6 that sulfur favors the development of
sulfates, not sulfites, with alkalized alumina.
This fact largely
sugges ts that NazS04 is the principle sulfur- bearing product.
If
it is assumed that in 100% reactant utilization. the spent dust con-
sists completely of NaZS04 and AIZ03 in one-to-one molar cor-
respondence, the maximum quantity of total sulfur which can exist
-------
in any sample is 13% by weight.
Note that all of the samples listed
in Table 6 contain between 8% and 11% sulfur.
Under the as sumed
conditions, therefore, the reaction efficiencies relative to these
samples are roughly between 60% and 85%.
These are somewhat
below the 70-100% values shown in Figure 16. Nevertheless. although
based on crude techniques, they also indicate a fairly high percent
of reactant used in sorbing S02.
Table 6
Sulfur Analysis of Reacted Dusts from
Selected Alkalyzed Alumina Tr.ials
Tes t No. Sample % S04 % S03 % Total Sulfur*
AA-IF Fallout 25.03 1. 15 8.82
Dus t Cake 31. 59 0.70 10. 83
AA-4 Fallout 29. 81 1. 00 10.25
Dust Cake 24.63 1.25 8.73
AA-8F Fallout 19. 77 3.50 9.38
Dust Cake 23.84 2.25 8.86
AA-IOF Fallout 27.94 0.85 9.67
Dust Cake 32.36 0.55 11. 03
AA-12F Fallout 27.55 0.95 9.58
Dust Cake 30.37 0.65 10. 40
* Samples analyzed by Gilbert Associates, Inc., Reading, Penn-
sylvania, under Government direction
-------
c.
Effect of Fly Ash on SO?! Removal
The same set of filter bags used to support 502 conversion can be
used concurrently to control fly ash, according to experiments con-
ducted under the Fly Ash Study series.
The presence of the inert
phase does not impair reactant activity; in fact, with some reactants
it appears to be beneficial to it.
Table 7 lists data taken from the tests, in which mixtures of reactants
and fly ash were discharged into the flue gas stream.
The computed
value of fly ash concentration, which is contained in the last column.
was determined for each run from a knowledge of the percentage of
the material in the particular mix, the quantity of mix delivered
into the stream, and the stream flow rate.
The stoichiometric
figure was determined from the equation derived in Appendix A.
As in other tests, the average concentrations of 502 remuved were
computed by approximating the integral of the appropriate curve
relating 502 concentration to running time.
If the average removal percentages in Table 7 are compared with
related values obtained from the graphs in Figures 12 to 15 in this
report, it is found that many of the corresponding values coincide.
This is especially true of the figures for (unpromoted) slaked lime
-------
Table 7
Results of Fl y Ash Study
Average
Test .Filtering Stoich. :Mid Bag SOZ
Designa tion Reactive Dust Time Ratio Temp. Fly Ash Cone. Removed
UPL-FA-IF Slaked Lime 60 min. 1. 99 785°F 3. 96 gr leu. ft. 77. 6%
UPL-FA-2F II " 60 min. 2.02 795 3.99 84.5
UPD-FA-IF Slaked Dolomitic Lime 60 min. 1. 95 805 3.82 49.5
UPD-FA-2F " " " 60 min. 2.08 800 4.05 55.9
PD-FA-IF Sl aked Lime (1 % Na Cl) 60 min. 1. 89 800 3.71 60.0
PD-FA-ZF II " " 60 min. 1.99 800 3.91 69.7
0'
V1
PL-FA-1F Slaked Lime (1% NaC1) 60 min. 2.02 825 3.91 74.0
PL-FA-2F II II II 60 min. 1.96 800 3.84 73.3
-------
and slaked dolomitic lime.
The curve in Figure 12 for slaked lime
at 800°F gives a value of 80% at the 2.0 stoichiometric level which
,
is approximately the average figure of the two lime runs conducted
in the Fl y Ash Series.
Similarly; the 8000 F curve for unpromoted
dolomitic lime cuts the y-axis at 55% when the stoichiometric level
is 2.0, and this figure is very close to the corresponding values
obtained in Table 7.
Unfortunately, because of difficulties encountered in feeding promoted
slaked lime by itself into a 385 cfm gas stream, there is no data
available from earlier tests to compare with the outcomes of runs
involving mixtures of this reactant and fly ash.
It is apparent, never-
theless, that at 73% removal. fly ash has little or no opposing in-
fluence on the ability of the promoted lime to absorb 502.
Promoted slaked dolomitic lime and manganese dioxide are materials
which actually demonstrated better removal percentages with fly ash
in the stream than without it.
The earlier curve for the promoted
dolomitic lime indicated a 55'" removal figure at a 2. 0 stoichiometric
level; the current study shows a 65% removal rate, a 10 percentage
point jump.
Similarly, without fly ash, Mn02 at 6000 F and 2.0
stoich.iometry removed onl y about 60% of the 502 present in the gas
-------
stream; with fly ash and under the same operational conditions it
,
extracted almost 80%.
It should be noticed that this latter figure is
closer in value to the figure obtained under similar circumstances
in the Precoated Bag Study.
Despite the interesting jumps in 502 removal experienced by the
las t two materials, it is significant that with none of the reactants
did fly ash prove detrimental to activity.
One set of filter bags can,
therefore. be used to extract both fly ash and 502'
D.
Effect of Gas-Solids Contacting Methods on SOl Removal
Whether precoating or continuous injection contributes more to 502
absorption depends on the reactant invol ved, according to trial s run
under the Precoated Bag Study.
Slaked lime, when injected directly
into the sulfur- bearing stream. had a relatively high capacity for
absorption; however, when coated on the bags in advance of the
stream, it displayed markedly little affini ty for 502.
Mangane s e
dioxide, on the other hand, displayed a somewhat greater capacity
for 502 when precoated on the bags than when continuously injected.
The 502 removal values obtained from precoating the bags with the
four lime materials were generally low.
In fact, with the exception
-------
of slaked lime at twice stoichiometric requirements (Table 8), none
of the calcium- based reactants removed more than 15% of the gas,
despite changes in stream temperature and stoichiometric ratio.
At
first it was thought that these low values stemmed from the physical
state of the reactant on the bags; that is, the layer of deposited
material was thought to be too thin to kinetically favor reaction with
the fast-moving 502 molecules.
Further investigation, however,
disproved this notion; the answer was found to be more chemical
than P?ysical.
Opening the door of the filter bag chamber after
several disappointing runs disclosed a thick, heavy cementitious
deposit on the bags that obviously had not responded well to cleaning.
An. analysis of this material showed it to consist largely of carbonates.
5ince hydrated lime is very reactive toward both C02 and 502 be-
tween 7000 F and 9000 F, and because calcium carbonate is known not
to be receptive to 502 much below 10000 F, it is evident that the re-
actant had become a carbonate prior to making contact with the
sulfur- bearing stream.
Apparently this change came about while
the material was being laid over the bags.
Its exposure to C02 in
the gas stream during this time had caused the lime reactant to con-
vert to a chemical form more stable in the presence of 502'
Thus,
the precoating method shows considerably less removal with the
hydrated limes than the continuous injection method shows.
-------
Although deposited on the bags in the same manner as the limes
,
manganese dioxide gave unusually high 50Z removal values, as indicated
in Table 8 and Figure 17.
(Manganese dioxide, unlike the limes, is
not particularly receptive to COZ or other products of natural gas
combustion).
If figures in Table 8 are compared with values taken
from corresponding continuous-coating tests, it is found that MnOZ
extracted slightly more 50Z per stoichiometry when deposited on the
bags ahead of the gas stream, than when discharged directly into the
stream and subsequently deposited on the bags.
Because the precise amount of reactant available for combination
with 50Z is known. the precoated study on Mn0Z lends itself to a
meaningful comparison between the sulfur content of the dus t cake as
determined by chemical analysis and as computed from information
obtained in Table 8.
According to the table, for example. Z.91
parts (by mole) of Mn0Z combined with O. 81 parts of 50Z in tes t
MN-5FB.
Assuming the product of the MnOZ-50Z reaction to be
Mn504' the dus t cake at the end of the run should contain O. 81 parts
of Mn504 for each (Z. 91 - 0.81) or Z.lO parts Mn0Z'
The quantity of
sulfur in this mixture was calculated to be 8. 50/0 by weight.
Chemical
analysis (Appendix D ) of the dust cake (and fallout) indicated an
-------
100.0
~
::) 90.0
o
...
-
III
I-Z
Z 0 80.0
III
~!
III
a. Q 70.0
III
III>
~O
CI
~III
III ~ 60.0
~
~
o
Vt
... 50.0
o
..8"'"
/~
~
~
/
BAG CHAMBER TEMP. of
500 0-------0
600 . .
700 )t-----X
40.0
0.0
1.0
2.0
3.0
4.0
5.0
STOICHIOMETRIC
LEVEL
REMOVAL OF SULFUR DIOXIDE WITH
MANGANESE DIOXIDE ON BAG
SURFACES AT AIR/CLOTH = 8.0 ft. / min.
-------
8.8% sulfur conten.t.
Similarly, analysis of the expended dust cake
of test MN-4FB shows a 7.5% sulfur determination; on the basis of
removal test data, this quantity of sulfur should be 8.1%.
The re
appears to be good correlation in the sulfur contents of the samples
as determined from chemical analysis and reasoning from removal
data.
Table 8
Results of Precoated Bag Study
Test Mid- Average
Designa- Reactive Fil te ring Stoich. Bag Flue Gas 502
tion Dust Time Ratio Temp. Flow Rate Removal
UPL-lFB Slaked Lime 60 min. 2.28 695°F 385 cfm 27. 9%
UPL-2FB II II II 2. 19 785°F " 54. 5%
UPL-3FB " " " 2. 12 800°F " 33.4%
UPL-4FB " " II 2.09 895°F " 26. 7%
UPL-5FB " " " 1. 80 9000 F " 30. 7%
MN-1FB Mangane s e
Dioxide " 3.36 6000 F " 90. 4%
MN-2FB " " 3.35 6000 F " 88.6%
MN-3FB " " 3.49 7000 F " 88.4%
MN -4FB " " 3.47 6950 F " 89. 9%
MN-5FB II " 2.91 5000 F " 80. 5%
MN-6FB " " 1. 74 5000 F " 70.4%
MN-7FB " " 2.20 6000 F " 80.2%
MN- 8FB " " 2. 35 7000 F " 82. 9%
MN-9B " " 1. 96 6150 F 290 cfrn 46. 4%
MN..IOB II " 2. 30 705°F " 55.2%
-------
APPENDIX A
-------
APPENDIX A
Derivation of Stoichiometry Equation
The equation for calculating the stoichiometric ratio of reactant to S02 was
derived in the following way.
If the flue gas stream flowing at a volume rate
of f cubic feet/min. contains c parts per million of S02 at temperature T and
atmospheric pressure, the volume occupied by the S02 alone during time period
t under these conditions would be equal to cft x 10-6. On the assumption that
the gas is ideal--and since the pressure is near one atmosphere, this assump-
tion is realistic--the volume
of S02 at 320F is:
4.60 x 10-4 cft
T + 460
*
The density of S02 at this temperature is 0.1827 lbs/cu. ft.
Thus the weight
of S02 in grams is determined by the relation:
cft (4.60 x 10-4) (453.6) (0.1827)
T + 460
=
3.81 x 10-2 cft
T + 460
The final form of this equation is derived from simple chemical balancing
techniques.
Suppose the additive contains only one reactive component, the
other components being relatively nonparticipatory.
When S02 completely reacts
with the solid additive, the reaction follows the chemical relation:
aA + bS02 + cC +
. . . . . =
5T +) f\
. . .
. . .
where A represents the reacting component in the additive, C may be either a
nonparticipating component of the solid additive or a participating component
in the gas stream, and T and e are reaction products.
The amount of component
A in grams just necessary to react entirely with x grams of S02 is equal to
amx
64.0 b
*Handbook of Chemistry and Physics, 44th Edition, Chemical Rubber Publishing
-------
where m is the gram "molecular" weight of A.
If the additive contains n10 of
A by weight, then the total weight of the additive necessar,y to combine with the
SO is 100 amx
2 64.0 nb
In the principal formula above,
x = 3.81 x 10-2 cft
T + 460
andM=
100 am
nb
B,y definition, the stoichiometric level of additive is the ratio of the weight
of material, Wr, actually discharged into the stream to the amount required for
a theoretically complete reaction, or:
Wr
100 amx
b4.0 nb
=
Wr (T + 460) (64.0)
3.81 x 10-c cft M
=
Wr (T + 460)
5.95 x 10-4 cft M
The values of M for manganese dioxide, activated alkalized alumina, slaked lime,
and Nahcolite were based on these equivalents:
(a)
(b)
(c)
(d)
one molecule of Mn02 for each molecule of S02
two molecules of NaAl02 for each molecule of S02
one molecule of Cao for each one of S02
two molecules of NaHC03 for each molecule of S02
According to the chemical analyses of the raw additives, manganese dioxide is
95~ Mn02 by weight, alkalized alumina is 100~ NaAl02' slaked lime is 70% Cao,
and Nahocolite is 7O~ NaHC03' Therefore, M for manganese dioxide is 91.3; for
alkalized alumina, 240.0; slaked lime, 80.1, and for Nahcolite 24010.
For additives containing two or more reactive components, which act on the SO?
independently of one another, (e.g. dolomite) the gram molecular weight is re-
presented by the equation:
M=
100
k
~
i = 1
-------
where:
k
=
the total number of different tY]es of reactive components present
in the dust
b =
ai
the number of parts of S02 per part of component i necessary for a
complete reaction
ni =
the weight percent of component i in the dust
mi =
the gram formula weight of component i
This equation is easily derived with reasoning similar to that used in der~ving
the equation for one component additives.
Suppose the dust contains ni percent
by weigh:t of reactive oxide component 1, which has a gram formula weight (gfw)
of mll n2 percent of reactive component 2 with gfw of m2'... and nk percent of
reactant k, with gfw of mk.
In 100 grams of additive, the amount of S02 by
weight, Xi' which will react with component i is given by:
X. = b
~ -
a.
~
64.0 nj
mi
The total weight of 802 which will react with 100 grams of the additive is
mere~ the sum of the weights reacting with the additive's individual compoents.
Hence:
Xtotal
k
=E
=
64.0
k
~
[(l \ ~
a 1 mi
i = 1
1 = 1
The gram equivalent weight of the additive is determined by the relation:
= X~~~al = t [l(+ \ :~
i = 1 1
100
M
or
M = 100
k
~ (:) n1
m.
-------
Dolomitic limes may be regarded as containing two reactive specieo, CaO and MgO.
The unpromoted lime was found to consist of 44 (weight) % CaO (mCaO = 56.0) and
31% MgO (mMgO = 40.3), and the promoted lime to contain 43% CaO and 3010 ]lYgO.
Substituting the appropriate values in the equation derived nets a figure of
65.3 for unpromoted dolomite and 65.0 far the promoted material.
These values
of M are inserted into the relation:
S =
Wr (T + 460)
5.95 x 10-1t. cft M
to determine the stoichiometric level of the dolomites in the S02 containing
-------
APPENDIX B
-------
TYPICAL BREAKTHROUGH CURVES
CONTINUOUS REACTANT INJECTION
3000
2500
E 2000
a.
a.
...
co-t
o
en 1500
t-
1&1
....
t-
::)
o
1000
500
o
SD-4F
UPL-10
U PL -7F
UPL-FA-2F
o
15
30
45
-------
TYPICAL BREAKTHROUGH CURVES
PRECOATING
3000
2500
E 2000
a-
a-
...
c-c
o
en 1500
J-
III
...
J-
:;)
o
1000
500
. 0
UPL-1FB
.MN-5FB
o
15
30
45
60
-------
APPENDIX C
Data
-------
ADDITIVE STUDY
502 CO~c. A.,e::"a6~
Test :F:e2.cta.::-: r:-est Gas Flew Stoich. :Bag Temperature Pressure Drop Reco...ed FrOt:!. SC2 :t=tr.:Ya.l Cor:::"
:?,=s:.gn3.-:~c~ :;se:. !r.te::'".re.l Rate Ratio Bottom Middle ~ Avera.ge F1na.l To Bags Flue C'~ses ::",-:~=......:=..:
t,"F!.- 3 Slaked Lime ~O "'.&in. 290 c:f'1n 2.61 1015°F 920°F 815°F 1.3 in.~O 1.6 in. H20 2790 Ppm 151.0 pp:n 55~
UFL-4 " 2.24 1010°F 955°F 850°F 2.2 :In.~O 2.1 in. H20 2810 ppm 1330 ppm ~'7f:
UPL-5 " 2.14 1025°F 915°F 825 OF 2.0 in.~O 2.6 in. H20 2740 P7I 1460 ~ ~'Z~
~.; .
UFL-6 II " " 1.54 885°F 795°F 720°F 1., in.~O 1.8 in. ~O 284opp:: 1690 pp:n 6~r'
.... ,
UPL-7 " 900°F 790°F 700°F No Da.t.a 2820 Ppr.I 1geO pp:'! -~.J
2.52 v.
" 760°F 695°F 650°F 1. 9 in. H20 2.5 in. H20 2115 Pp:'! 1255 P::::n ' -'"
UPL-8 1.93 -::;-""
UPL-9 " 2.45 750°F 700°F 645°F 2.1 1n.~0 2.7 in.~O 2610 P:p:n 1605 p~ r~
UPL-l0 1.80 855°F 190°F 715 of 2.0 in.~O 2.4 in. H20 2750 PP-: 1600 pp:n 58~
UPL 11 " 2.24 875°F 800°F 125°F 1. 8 in.. H20 2.1 in. ~O 2750 pp:r. 2055 Pp:'! -.::..J
~ .
UPL-12 " 2.15 775°F 710°F 655°F 2.0 1n. ¥"20 2.1 in.~O 2840 pp::;. 15eO pp r:~':f
. - -
~-13 " 2.61 845°F 795°F 730 of 2.5 in.~O 2.9 in. H20 2870 P~ 1970 p:p-: .,.C~
UP.L-14 1.50 890°]' 795°F nO of 2.6 in. H20 2.7 1n. H20 2810 ppr! 1055 ~ J2<':
UPL-15 " 1.24 885 or 190°F 710°F 1. 7 in.~O 2.0 in. H20 2840 PP'll 9'0 P~ '=.31:
UPL-16 " " 3.08 900°F 800°F nO°ii' 2.1 in.H20 2.6 in. H20 28201'pr: 2100 1'P= 7-~
UFL-17 " 3.29 910°ii' 805 of nO of 2.3 in. H20 2.6 in. P'20 2830 pp::: 2255 ppm 6c~
UPL-18 II 3.12 10000r 900°F 800°F 2.0 in. H20 2.4 in. H20 2840 p1'm 2CCO pp."'l 1:~~
UPL-19 " " 3.19 750 or 705°F 660°F 2.0 in.~O 2.7 in.~O 2850 p:pm 15Z.0 1'1':::: ;-1.
UPL-20 '.19 725 of 690°F 650°F 2.0 in.H20 2.1 in.H20 2850 Pp::l 1885 Pp-:l 6(~
-------
ADDITIVE S'r'I.1DY
S02 Conc. Avera~
res :. Reac:tan~ Tes't Gas now Sto1ch. Bag Temperature Pressure DrO'D Re!':oved. From 502 ::e:n~v~ O':er
i5U;"1at:Lcn Used Interve.: ~e:te Ratio :Bo"tt.or1 M:Lddle To'D Average tinal To Bags Flue Gases ::nterval
...- - - ~
Jl'L-21 Slaked Lime 60 ZV..:!.n. 290 c:f':n '.59 965 "F 890°F 815 of 2.7 in.~O ,.4 in.~O 2840ppm 22'0 p~ ~S~
Jl'L-22 .. 2.6, 970°F 890°F 800°F 2.1 in.~O 2.6 in. H20 2800 ppr.1 1810 P:pI:! 65%
Jl'L-2:5 " " 2.26 990 "F 895 "F 795°F 1. 8 in. H.z0 2., in. ~O 2800 ppr.1 1"(75 P:;X:: 63~
/L-l Sla.ked Lime " 2.64 lOOO°F 900 of 815°F .9 in. ~O 1.3 in.~O 2810 ppm 1815 ~ 65~
C:. (""~ Na. Cl)
~2 " 2.25 1015 "F 895"F 800 "F 1.' in. H20 1.7 in. F-20 2800 ppm 1720 :P1= ',,<1
0-.'"
PL-; " " 3.69 1015 "F 900 of 800 of 1. 6 in. HaO 2.1 in. H20 2825ppm 1c90 :ppn 67;"
~ " 2.62 915°F 810°F 740"F 1.4 in. ReO 1.9 in.~O 2790 ppm 2040 pp1 7;~
:t-5 " 2.39 905°F 810°F 740°F 1. 5 in. ReO 2.0 in. H20 280op:pm 2050 :p:p::1 -_J
i; ~
'L-6 " 2.48 775°F 695 "F 655 "F 1. 5 in. H20 2.0 in. F-20 2700 p:p:n 16c5 :pp:"I 62~
!.-i 2.4, 770"F 700 or 660°F 1.6 in. ~O 2.1 in.~O 2780 p:p:n 1730 :ppm 62~
?I.-a '0 .. .. 1.28 890°F 800''F 730°F 1.1 in. H20 1.4 in.~O 280op:pm 13cO ~p::: IL9~
'!!,-9 " 1.50 900°F BoO of 730°F 1.9. in. H20 2., in.H~ 2790 pp:n 1540 ~::: -c:J
)/-
!.-l::l " " " 3.,4 890 of 800°F 740 "F 1.6 in. H20 2.0 in. H20 2790 ppm 2350 :?~ e...~
!.-ll 3.64 900°F 805 of 745°F 1.8 in.1f.20 2.5 in. H20 2800ppm 2390 p:p:': S5~
1'.....J2 " .. 3.78 975°F 915°F 825"F 2.0 in.HeQ 2.5 in.H20 2760 ppm 2120:?p::: 77<'..'
!.-13 ., .. " '.10 950°F 910°F 825 of 2.0 in. ReO 2.7 in. H20 2720 ~ 2050 :ppr.. '7l~
1"' " " 2.68 735"F 705°F 665°F 2.0 in.ReO '.1 in.~O 2800ppm 1975 ~ --,4
-~- I.J.~
-------
T~st
B5igIla.t::Lon
~
:::.r-lc
P:-17
PL-18
FL-lg
FL-1C
PL-2C
PL-3C
=-:'-:"C
?:.-5C
:?L-6c
~-1
5D-2
5D-3
5D-4
SD-5
5:;)-6
51>-7
Reacta:1~
Used.
Slaked Lime
(1 '0 Xa Cl)
"
Sla~ed. Dolo-
=lt1C Lcne
Tes~
Interval
60 :':J.r..
"
"
..
..
"
..
"
..
"
"
"
Gas Flow
Ra.te
290 efm
"
"
"
"
"
"
II
"
II
II
"
II
II
"
Stoieh.
Ratio
-
3.39
3.35
3.40
3.53
1..86
1.. 90
1.66
2.02
1.99
1.. 98
3.16
2.36
2.05
2.34
2.11
2.05
2.33
ADDI'l'IVE STt1DY
:Bag Tempera.ture Pressure Drop
~ Middle ~ Ave:-age.... FJ.r.a.l
720°F
725 of
845 OF
855°F
975°F
985°F
865°F
865~
760°F
745°F
970°F
980°F
975"F
865°F
870°F
755~
755°F
700°F
705°F
805°F
810°F
915°F
9100P
795 "F
795°F
705 "F
695~
89D OF
890"F
8gooF
790 "F
795 "F
700°F
705 "F
670°F
670°F
760 "F
755°F
815 OF
835°F
740°F
740°F
665°F
660°F
805°F
805~
805 OF
730 "F
7q.0°F
660 "F
670°F
2.3 in.HaO
2.7 in.H20
3.2 in.H20
2.6 in. 11:20
2.1 in.H~
3.2 in.~O
2.0 in.~O
3.2 in. H20
2.6 in. H20
3.6 in.~O
1.3 in.~
1..7 in.~
1.7 in.~
2., in.~
2.2 in.~O
2., in.~O
2.4 in.1I20
3.3 in.~O
3.8 in. H20
4.7 in.~O
3.8 in. H20
3.2 in.~O
4.2 in. H20
;.1 in. H20
4.2 J.n.H20
3.8 in. ~O
4.8 in. H20
2.0 in. P-20
2.2 in.~O
2.3 in.H.eO
2.9 in.H.eO
2.8 in. H20
'.0 in.H.eO
,.0 in.H.eO
To Bags
502 Cone.
Removed. Fro!!:
Flue Ge.s'!s
2790 P:tml
2760 ppm
2790 pp;n
2775 ~
2775 pp::l
2750 p~
2780 ~
2780 ppm
2760 pp:n
2810 ppm
2800 pp!II
2820 ppm
2810 ppm
2790p:p:n
2775 pp::l
2770 ppm
2790 ppm
1880 pp-:
1790 p:p:n
2350 p:pm
2285 pp:n
1830 ~
1585 ~
1905 ~-:.
1935 p:p.-:.
1440 PZ::
1480 pp::
1540 Pp:n
1060 ~
10'0 pp:
'1595 Pprl
1470 ~
1165 p~
1190 pp:!l
Averaae
502 Reffioval O.,e::-
Ir.te::-val
6-;
6_..1
;; J
c:"~
t2..
coS
-,...1
,c".
6S~
~:~
;2%
53~
55~
,8~
'>(-c;!
,; .
57:'
53~
. ,...1
~~....,
4:c'
-------
ADDITIVE STUDY
502 Cone. Avera~
test Reactant 'Iest Gas Flow Stoich. Bag Temperature Pressure Drop ReMoved FrO%!! 502 Remcval ever
~sr.a.t:ion Used Interval Rate Ratio Bottom Middle Top Averase. F1nal To :Bags F::"ue C-ases :nte::-'ral.
\00-
S!)-E Slaked Dolo- ;2~
1:1'11 h c: Llm e 60 :"_~. 290 cfm 0.94 840°F 790°F 740°F 2.0 in.~O 2.6 in. H20 2790 ppm 900 p~
;D-9 " 1.10 855°F 800°.F 745°F 2.0 in. ~O 2 . 6 in.:f.20 2800 pp:n 900 P~ '2~
5D-IO 3.09 860~ 795°F 740°F 2.4 in. H20 3.1 in.~O 2770 ppr.l 1890 pp:n ~.':"-
--'"
SD-:l ,.08 860°F 795°F 735°F 2.3 in.~O ,.0 in. H20 2820ppm 1740 P:p!!.! 53~
SD-:2 " 2.96 860°F 800 of 740°F 2.5 in. H20 3.2 in.:f.20 2830 pp:!1 1710 pp:~ 62~
SD-13 .t 2.89 970°F 895°F 815°F 2.2 in. H20 2.6 in. ~O 2750:pp!ll 1240 1'71 "'5~
SD-l LL 2.87 975°F 885°F 800 of 2.1 in. H20 2.7 in.~O 2770ppm 1370 ~ ::'9~
SD-1.5 2.59 750°F 695°F 660°F 2.3 in.~O 3.5 in.~O 2770 ppm. 1565 P~ 5'~S
m-16 " 3.12 740°F 695°t 665°F 2.3 in. H20 3.2 in. H20 2790 P:p::l 1~35 pp. 51~
pj)-l Slaked Dolo-
m.i t:. c: !..i::1 e " 3.34 9700F 9100F. 8400r 1.8 in.H.20 2.7 in. H20 2825 pp!!1 1930 ~ 6S~
(1 "': Xa Cl)
PJ-2 ., 2.58 9650F 895 of 825 of 3.1 in. ~O 4.1 in. H20 2800 pp!D. 1650 P:t=:l 5"''''
:t,
PD-3 2.42 975°F 915 or 8450r 4.5 in.~O 6.1 in.'~O 2770 pp:!I 1615 p~ 5c;:
PD-4 " 2.29 980 or 905°F 820°F 2.3 in.~O 2.9 in. ~O 2780 ppm :500 ~ 5~~
PD-5 2.50 980 or 795°F 7200r 2.1 in. ~O 2.8 in. ~O 2580 pp!I1 1475 P~ 63<"',
,p!)-6 2.53 890°F 795°F 710°F 2.0 in.~O 2.3 in.~o 2780 ~ 1505 pp:!: 5L~
PD-7 " 2.48 890°F 800or 710°F 2.1 in.~O 2.5 in.P"20 280op:pm 1670 PP=! ~C~
1D-S t. 2.41 750°F 695°F 650°F 3.0 in.~O 3.9 in.~O 2780 ppm 1330 Pp:!!. 4~~
-,'
PD-9 " 2.36 750°F 705°F 660°F 2.7 in.~O 3.4 in. H20 2760 P1C 1350 pp!: ::.~
- /"
-------
ADDITIVE SmDY
502 Cone. A-.~ra~
'l'es~ Reactant Test Gas Flow Stoich. Bag Temperature Pressure Drop Rer.:oved. Frot!! SC2 Re~oval Cver
_pe51 g:1ation Used Interval Rate RaUo Bottom Middle. Top Average F1r.al To !ags n....e Gases In:teT'lo-a1.
~
~.1l Sla.lc:ed :)010-
::'l:.t::.c :"lrn.e 60 :r.~n. 290 cfm 1.17 8400F 795°F 735°F 2.4 in. ReO 3.0 in. H20 2770 pp:n 7eO p1JC. 2~
(lr;~ ~aCl)
1))-12 1.09 840~ 795°F 735°F 2.7 in. 1I:!0 3.5 in.H.20 2750 ~ 915 P1=C 'Z:~
~~ .
1Ji-13 " " 2.81 8,o~ 79O~ 730°F 3.9 in. ReO 5.9 in. H20 2775 pp:n 1940 ~ TC~
'I).l~ " 3.11 840°F 805 OF 745°F 4., in. ReO 5.9 'tn. H20 2775:ppm 1930 p~ c9~
7l)-15 ,. " 3.01 845°F 800 of 735°F 3.7 in.HeO 5.3 :10..H.20 279O:ppm 1520 :;~ 651>
?I)-If " " " 3.01 730 of 695 "F 660°F 3.8 in. H20 5.7 in. 11.20 2790 ppr.1 1535 T~ 55~
PD-17 " 3.04 955°F 900~ 815°F 4.2 in.HeO 5.9 in. H20 2780 pp:n 1C25pP-: 66~
PD-1E " " 3.09 965°F 910°F 830°F 3.5 in.ReO 4.9 in. H20 2750 ppm 18!.0 ~ "'_4
C ..~
1f:,-1C Sla.ked
~""ne " 3.00 980"F 900 OF 820"F .9 in.HeO 1.5 in. H20 2735ppm 1975 p:;:n -2~
!JP:,-2C " " 2.66 975°F 9OO"F 825"F 1.6 in.~O 2.4 in. ReO 2740 pp:n 1S45ppm ",_oJ
o "
,.
tP:-3C ., " " 2.06 860 of 805°F 745°F 2.0 in. ReO 2.9 in. H20 2790 ppm 1940 P:;::1 69~
liPL-l:.c " " 1.64 840 of 800 "F 745°F 1. 9 in. HeO 2.6 in. H20 2780 ~ 1590 p:p::l r:::-d.
61. --=
UPL-5C " " " 1.67 730 "F 700°F 670 "F 1.9 in.HeO 2.7 in.BeO 2775 ppm 1020 P~ ",_oJ
, -J
11?-,-6C " " 2.00 725°F 700 "F 665~ 3.5 in.BeO 5.' in. H20 2770 ppm 1265 P~ I"'''
..c-",
JIN-I : fa.."lga.:les e
:::'o,..ide " " 2.05 665 "F 610°' 575 "F .7 in.BeO 1.0 in. BeO 2760:ppm 1360 p:p::l 5:::%
1!N-2 48 :-j.n. " 1.91 670 "F 610~ 575°F 1.1 in.BaO 1.3 in. H20 2770p:p:n 1435 :ppc. ;2~
.-3 60 %:!:in. " 2.44 795°' 705°F 660°F 1.8 in.BeO 2.2 in. H20 2770 pp::: lC20p:p:: 66:
fMN-.:. 2.46 800°' 710°' 665°' 2.0 in.BaO 2.6 in.BeO 2790ppr.I 1900 pp:::t cE:~
1
-------
ADDITIVE STUDY
S02 Cone. A:,.,~;:a~
!~st Reactant Test Gas Flow Stoich. Bag Temperature Pressure Drop Re:::oye:l Fron SO,;: Pe=c"",e.: Cve~
fS:.;=-...at:.on Used Interval Rate Ratio Bottom Middle -1'£E Average F1nal To Bags Flue Gases !!::t~:-,~:
-
).f 1.1a::.ganese 2.6 in. ~O 2800ppm 18,5 ppr.: '_oJ
~:'c,x1ie 60 min. 290 cfm 2.12 560DF 505DF 500DF 2.5 1n. ~O t:; .
1.;6 660 DF 600DF 570DF 2.0 in..~O 2.; in. H20 2775 ppm 970 p:pm --~
~-- ;; ~
,.E " 1.15 660DF 595DF 570DF 2.0 in. ~O 2.; in.~O 2745 ppm 1020ppn: .,,--i
~ ..;
Ci.9 " 2.77 660~ 595DF 570DF 2.5 in.~O 2.9 in. H20 2765 ppm 1925 ppm ..,.C~
6'-10 " " 2.70 66o~ 600DF 570DF 2.; in.~O ,.0 in. ~O 2760 ppm 1E80 ppn ~~'"
...C c
~-ll " 2.76 755DF 69O~ 645DF 2.6 in. ~O ;.1 in. H20 2790 ppm 1950 ppI1 -~-i
I ~ c
f,-12 " " 2.90 780DF 700DF 655DF 2.7 in ~O ;.1 in. ~O 2790 ppm 1920 pp!:. t::;......
-, .
~-:; " ;.07 540DF 500DF 490DF 2.5 in. ¥ ;.2 in.¥ 2770 ppm 19;5 ppt:: "'G~
r-~~ " " 2.92 540DF 500~ 490DF ;.1 iIl,,~O ;.9 in. ~O 2740 ppm 2010 ppm -"':f
A-:.? AL'ltalized
A1~I:a ;0 min. 290 cfm 0.89 ;6oDF ;40DF 330DF 2.; in. H~ ;.2 in. ~O 2795 ppm 1eOO ~ ' '"
~_.:
A-;3 ., " " 0.78 ;20DF ;15~ ;15DF 2.2 in. ~O 2.9 in.~O 2785 ppm 1800 ppI:1 6-1
~-l1 " " 0.74 410DF 4oo~ ;80~ 1.6 in. H~ 1.9 in. ~O 2720 ppm 1590 ppm 5:~
A-5 ., " " 0.81 510DF 500~ 460DF 2.0 in. ~O 2.4 in. ~O 2750 ppm 12,5 pp::l , -'"
..;..,
A-6 " " 0.75 515DF 500DF 470DF 1.9 ill. H~ 2.; in. ~O 2715 ppm 1;00 ppm ~c~
-------
FLUE GAS FtOW BATE STUDY
S02 Cone. A-crerage
'1'es't Reac1:ant Test Gas Flow Sto~eh. Bag Tempera.ture Pressure Dro"O Remove i From SC2 ~~~val ever
p~ation Used Inten-al Rat.e Rat:!.o Bottorn Middle ~ Average FJ.na1 To :B3.ss 'I:'J.. ue C'-'!se s :~terva:
.-- - - .
'J-lF Slaked Lime 1400 :p~
(10/: =':!.Cl) ';0 -;:.n. 385 ef:n 955°F 915°F 835°F 4.1 in. H20 6.3 in.~O 2-{50 ppm "'
2.01 ~_.
385 efm 955°F 900°F 835°F 6.9 in. H20 8.1 in. :F"20 2750 ppr. 1290 P:;=' -~
~-2F 50 :-::.~. 1.77 ~ -.
f.,-;F ~S ~in. 385 efm 1.24 980°F 905 OF 840°F 9.1 in.~O 10+ in. H20 2735 Pp:n 1420 P1= 52~
~-:"F L2 :"1::':1. 385 e:f'l:l 1.65 970 OF 910°F 845 OF 6.5 in. ~O 9.0 in.~O 2745 Pp:!1 1650 P:PC t:."J
_\.I":
;L-;F Eo z::~n. 385 efm 1.63 860°]' 795°F 755°F 5.9 in. ~O 8.0 in. ~O 2770 ppr: :5::.5 p~ 5::>:'
PL-cF 60 =.:..n. 385 ei'm 1.75 880°F 810°F 765°F 7.0 in. H20 9.1 in. H20 2750 pp-n 1810 p;.-: =~~
11- IF ~8 ::,,,in. 385 efm 1.95 850 or 800°F 745°F 6.1 in.~O 8.9 in. H20 2750 p:pm 2030 pr: -2~
pr-t:F 52 ::::.n. 385 efm 1.64 870°F 805 OF 765°F 7.0 in. ~O 9.7 in. ~O 2740 pp:n :950 Pp::l 7:~
PI. - ~F ~2 ::;.in. 385 efm' 1.50 750°F 710°F 675°F 6.1 in.~O 8.4 in. H20 2750 Pp;:1 1~35 p~= -..J
::;.:::.,.:
KG' -IF I~=-..ganese
D-_=y..:..de 60 r!i:1. 385 efm 2.53 735°F 7100r 650°F 2.0 in.~O 3.1 in. H20 2745 Ppm 1820 PP::: c6~
MI\ -2F 60 ::!:.n. 385 efm 1.93 720°F 695°F 645°F 3.4 in. H20 4.3 in. F'-20 2700 ppm 1485 ppr: .-.(
::>"'-.
" .
Mi\ -;iF 60 r:ir... 385 efm '.06 730°F 700°F 650 or 5.3 in. H20 7.0 in. H20 2770ppm 2050 ~ ..',J
...-.
,"
K!.\-:"F ~O :n~:l. 385 e:rm 2.37 725 OF 695°F 650°F 6.0 1n.~0 7.7 in. H20 2770 P:Pm 1960 1'::=t Pt'...~
-I'
Ml\-5F cO ~:l. 385 efm 1.88 630°F 605°F 575°F 6.2 in.lI20 7.4 in.H.20 2760 ppm :1,.50 p:p::: -_J
::> :;.~
Hli -6F 6;j ::::.n. 385 efm 1.92 625°F 595°F 5700r 7.7 in.~O 8.7 in. H20 2770ppm 1590 p~ 5T~
MK-iF " 60 r::.n. 385 efm 2.63 630°F 600°F 570 or 8.6 in. ~O 10.0 in. ~O 2780 ppm 2010 p:p:: -2S
X!\'-CF 60 :":.::. ;85 e:'m 3.32 630°F 600°F 575°F 8.7 in. H20 10.5 in. Hc!0 2775pp::! 2035 P:;:::1 -"Z.(
-------
FLUE GAS FLOW RATE STUDY
SO;:! Cone. .~verag~
Test Rea.etant Test Gas Flow Sto1eh. Bag Tempera.ture Pressure Drop Re!!:oved Fro!:! SC2 ~~o'la.l ever
DesJ. g-:.at J. on Used Interval Rate RatJ.o Bot'tom M:Lddle ~ Average fina.l To :Bags Flue Gas~s !~-:ervaj.
~..?F Ma;:ganese 9.4 in.~O It05 :;p:: ,,~J
I)1C:;::'~1: 6:) ~:.n. 385 cfm 2.19 530°]' 510°F 500°F 8.0 in. H.20 2775pP-:: c:;..
:"0 nin.. 385 c~ 540°]' 515°]' 495°F 6.4 in. ~O 2765 IJP."I1 1630 p:;:::: -_J
J!l\'-lOF 2.59 5.0 in. ~O "'-"..
./., -
~ -:li' 60 :Un. 385 cfm 2.88 510°F 490°F 480°]' 5.8 in.~O 7.5 in.H20 2765 pp:n lS60 pp: c-~
1j!i-12F 6:) ::-.in. 385 cfm 3.08 520°F 500°F 485°F 6.6 in. H20 8.4 'in. H.20 2750 pp::: 1920 pp: -:'-;
UP: - ;7 Sl2.~ed
.i..,L.~e 60 ::-.in. 385 cfm 2.16 1005 of 920°F 820°F 4.6 in. H.20 5.5 in. F-,20 2790 Ppn 1890 :p~ 68~
ttE.--F 60 min. 385 cfm 1.99 1000 of 910°F 815°F 4.5 in. H.20 5.7 in. H20 2720pp:n 1655 P~ e:;. J
...._":;
[JPL-5F 60 :::in. 385 efm 2.81 1010°F 905~ 810°F 4.5 in.H.20 6.0 in. H20 2750 Pp:n 2260 P:::= E2~
tJP:,-6F 60 :un. 385 cfm 3.39 1010°]' 915°F 835°F 6.3 in. H20 7.6 in. P..::!O 2735 Ppm 2305 P:p::I ~ J
:-"J
IJP!,-""F 60 min. 385 cfm 2.03 880 of 800°F 730°]' 4.8 in. H20 5.7 in.~O 2800pp::1 22:'0 p:;::: S:~
DF!.-BF 60 n:in. 385 cfm 1.87 890~ 795°]' 735 of 6.0 in. H.20 7.3 in. H20 2730 ppm 2230 Pp. Ee~
UPL-9F .. 60 :::in. 385 cfm 2.98 920 of 810°F 745~ 6.6 in. H.20 8.6 in. H20 2760 ppm 21,.40 ppr: "'-J
C:-.
UP:.-1CF ;0 !'l:.n. 385 c:f'm 2.67 875°F 805 of 740°F 5.9 in.H.20 6.9 in. P'-,20 2760 ppm 2450 :;:>=1 '=c.:'
'-, .
UP!. -lli' 60 :r':='n. 385 cfm 2.06 755°]' 710°F 670°]' 5.5 in. H20 6.4 in H20 2790 ppm 1610 p:;::: c::.....J
.,0.-
tJPL-12F 60 :::in. 385 cfm 1.97 750°F no of 670°]' 5.1 in. H.20 6.6 in. H20 2740 ppm 1:"30 P:p::l c;:.,"'"
,~ .
UPL-1.3F 60 r:in. 385 e:f'r.1 2.82 740°F 700°]' 680°]' 6.1 in. ~O 8.2 in.~O 2735 ppm 1980 p:;:.'" 7:-:'
1!PL-1~F t:0 l1".J.n. 385 cfm 2.85 750°F 705~ 670°F 6.5 in. H20 8.2 in. H20 2760 Pp::l 2010 ~ -~.:"'
J
B!-2:F Nahco:i"te 60 1".:':1.. 610 cf::! 0.66 330 OF 320°]' 335 0]' 1. 4 in. H20 2.1 in. H20 2830 pp:n 1700 ~ ',J
C,.I"J
Bii-3F .. 60 m::'n. 685 cfm 0.67 520°F 520°F 510°]' 2.3 in. H20 3.6 in. H2,O 2830 ppm 1670 P:P=1 o:c~
-------
FLUE GAS FLOW ElATE S'lUDY
802 Cone. Average
Test Rea.c:tant Test Gas Flow Stoich. Bag Temperature Pressure Dr0inar ReJ:IOVed From 802 RemovaL Cver
Jl5J.snat1on 't"sed Interval Rate Ratio :Bottom Middle Top Average :F1na To :Bags Flue ~ses Interva.l
-
pZ)-lF Slaked Dolo- 6~~
m1hc LU:'1e 60 ::l:ln. ,85 efm 2.'1 950°F 910 "F 84.5 OF '.9 in. H20 6.0 1n.~0 2750 ppm 1755 P:ii!::l
(17"~ Na Cl)
P:J-2F 60 min. ,85" cfm 1.5' 950 "F 900°F 840°F 6.1 in. BeO 8., in. H20 2720ppm 14.85 pprn 55~
F:J- 3F 60 min. ,85 cfm 2.04. 855°F 800 "F 755°F 6. 7 in.~O 8.8 in. ~O 2760 ppm 1600 p:pc 5~<'
c.
F:;)-4F 60 Inn. ,85 c:f'm 2.19 855 OF 800°F 14.0 of 5.6 in. ~O 7.8 in.~O 2175 ppm 1605 ppm 5e~
PD-5F " 60 ::lin. 385 cfm 2.24 14.5 OF 100°F 615°F 5.6 in. ~O 9.8 in. H20 2800 pp:n 1'10 P1=1 41rt.
F:>-6F " 60 :::in. 385 c1'm 1.96 140°F 700°F 680°F 5.9 in.~O 9.4 in. ~O 2740:ppr.l 1190 PP=! :'3~
¥.J-7F 60 .::in. ,85 cfm '.'1 94.0 OF 910 "F 850°F 10.+ in. ~O 10.+ in.~O 2140 ppm 1950 PF1 -ro:'
._0
P:J-cF 60 ::!in. ;85 c:f'm '.12 970°F 890°F 810 "F 6.5 in.RaO 8.2 in. ~O 2760 p:prn 1870 ppm cc~
P:J-9F .. La ~n. 385 cfm 3.24. 865 °F BlO"F 765°F 1.3 in.~O 9.9 in.H20 2720 ppm 2075 p:p:n 76~
PD-1CF " 1,.0 %:in. ,85 c:f':n '.20 855°F 810 "F 710"F 7.0 in. ~O 10.0 in. ~O 21:55 ppm 2060 pp:!l -->'.
1;1 .
PD-llF " 60 min. ,8, cfm 3.'1 14.0 "F 700°"1 685°F 6.5 in.~O 9.7 in.~O 2700 ppm 1690 ~ 6;s
PD-l2F 60 ::-.in. ,85 cfm '.24. 735 "F 695 "F 665°F 5.1 in. ~O 8.2 in.~O 2775 pp:n 1815 p:p:n 65%
SD-lF Sla.ked Dolo-
:::'ltic Lime cO :nino 365 cfm 2.1' 960°F 900 "F 840°F 2.6 in. ~O 3.8 in. ~O 2775 ppm 1305 ~ l-r%
5:J-2F " 60 mn. ,85 cfm 1.85 860"F 890 "F 825"F 3.' in. ~O 4.., in.~O 2725 ppc 950 ppm 35%
5:D-3F " 60 :nino ,85 ci'm 1.61 855°:' 8OO"F 750 "F 4..1 in. H20 5.5 in.~O 274.0 pp:I: 1350 pp:! l,.~
5:>-41' 60 r.r..n. 385 cfm 1.92 840°F 795 "F 750°F 3.5 in.~O 4..8 in.~O 2715ppm 1455 pp: 52~
-------
FLUE GAS 'FLOW RATE STr1Dr
802 Cone. Avera.ge
'1'e 5 t. Rea.ctant. Test Gas Flow 8to1eh. Bag Temperature Pressure Dro"O Remo\red:FrO!!! 502 Re~cva.l ~'er
.s~gnB..tion i1sed Interval Ra.te Ratio Bot to."II Midd:'e Top Average Final To Bags ?l'.l'!! C-ases I~":~:,va.!.
'-
':;!:'-tF S:2.~ec. Dolo-
:n:.~:.c ~~e 60 I:'JJ..n. 365 cfm 1.98 740°F 700°F 670°F 4.3 in.~O 6.0 in.~O 2780 ppm 1120 p~ :..C~
5D-7F 60 :r.in. 385 cf'm 2.77 945°F 895~ 835°F 4.9 in. ~O 6.7 in. B20 2740 Ppm 1460 ppm 5;~~
5J-c:r oa :r.in. 385 c:f'm 2.83 960°F 895 of 820°F 4.1 in. 1'''20 5.3 in.~O 2740 Pp::I ~..1:.60 p~ 5L..~
5~-gF 60 =n. 385 cfm 2.87 940~ 885°F 815°F 5.7 in. H20 7.6 in. ~O 2760 ppm 1760 ppI:I. 6L~
2J-1GF 6~ :n::.n. 385 efm 2.94 850°F 795°F 745°F 3. 7 :Ln. 1'''20 4.6 in.~O 2760 Pp::I 1)'30 p:r. 'i..~
SJ-:!.lF ,. 6::> :".in. 385 efm ,.07 845°F 795°i' 740°F 5.6 in.}bO 7.5 1n.~0 2760 P'Pll1 1930 P:p::1 -c~
3J-lC" 1,.8 lI"~n. :;85 efm 3.02 740°F 695°F 670°F 6'.2 in. H20 8.0 in.~O 2725ppm 11.95 P1= 55~
2J-13F 60 min. 385 e~ 3.21 730°F 700°F 68CoF 2.9 in. H20 4.5 in. H20 2720 pp:n 14:!.0 P:tr..' -~:I
,c: .
2J-17F' 60 :r.in. 385 cf'm 2.:;8 960°F 900°F 835°F 1.6 in.}bO 2.3 in. ~O 2760 ppm 1885 P:t'= ,.c:~
Cw J
S:::>-lCF 60 !!'.J. r... 365 cfm 1.75 840 OF 805~ 760°]' 2.1 in.~O 3 . 2 in. P'''20 2775 pp:n 1595 Pi= c;~
';' .
SD-~9F 60 ::,.in. 385 e:fm 1.79 840°F 810°F 760°F 3.3 in.1bO 4.4 in.~O 2425 ppm 1500 ~ 62~
-~lka.l1zec.
L_I!.-D' Al \UDJ.. =-..a. 30 ::in. ~85 ef:n 0.64 365°F 355°F 335 of .9 in.~O 1.2 in. H20 2775 ppm 1590 p~ 57%
.t4-2F 385 c=m 0.57 35CoF 345°F 335°F 2.5 in.H;>O 2.8 in.~O 2750 pp::l 154; Pi%! '561a
AA-3F 385 c~ 0.52 315°F 315°F 295°F 1.9 in. H20 2.4 in. H20 2800 pp:n 1335 p~ :..c~~
J>.A-TF 385 c:fm 0.77 520~ 510°F 480°F 3.0 in. H20 3.7 il1.H;>O 2740 ~ 1450 Pp::l --~
,j""
AA-eF 38; c:"r1 0.77 525°F 515°F 485°F 2.2 in. H20 3.0 in. H20 2735 ppm 150; Pp.'I1 551
AA-9'F " 385 c~ 0.60 525~ 515 of 495°F 3.0 in H20 4.0 in.:!.l20 2€20pp:n 1560 P:;:::I 5;~
AA-1CF " 385 c:':r. 0.58 415°]' /i.l0°F 395°F 3.7 in. H20 4.5 in. H20 2800ppm 1510 :;::p:: 54~
t.A-llF " 385 c~ 0.60 335°F 335 of 315°F 2.1 in. H20 2.9 in. H20 2790 pp:r. 1550 ppm 56~
-------
:BAG COA'l'ING STUD't
S02 Cone. A.,~~age
Test Re&C~~:lt 'rest Gas now Stoich. :Bag Temperature P!'essure Drop R~d From 502 :~:n~'.-~ Cver
%)e51 snati~:l :Is'!! Intenral Rate Ratio Botto.'Il )K.1dd1e ~ Averae;e. Final To Bags Flue Gases :n-:~r:a.l
-
UPL-LV3 Sl~ked 2a~
......:.::e 60 min. 385 ef:n 2.28 705°F 690°F 675°]' 8.1 in. ~O 9.6 in. H2O 2715 ppm 775 ppm.
UPL-2FB " 3e5 cfm. 2.19 835 "F 785°F 750 "F 5.2 in.~o 8.8 in.H20 2700 pp:n 14eo P:p::l 5'=.:'
~,'D
UE..-;F:B 385 cfm 2.12 835 oF- 800''F 755 "F 8.5 in. B20 8.5 in.H20 2125 ppm 925 ~ 33~
UPL-Ln " 385 cfm 2.09 995"F 900 "F 825 OF 8.2 in. H20 8., in. P''20 2750 ppm 740 pprn 271
UPL-5~ " 385 cfm 1.80 990°F 9OO"F 830°F 8.8 in.~O 9.6 in. H2O 2740 ppm 8401'~ ~-~
""-IJ
Ml\ -1F3 :.:a::.ga.::ese
-J - 385 cfm 3.36 635 "F 6oo"F 555 "F 2:6 in.H20 2.5 in.H20 2800 ppm 2530 1'1= 9V~
..._ox:..c.e
I-!F-2FB " 385 cfm. 3.35 635 "F 600°F 580°F 5.7 in.1t20 5.4 in. P''20 2820 ppm 2500 pp:n e9~
¥.I\-3FB " 385 cfm 3.49 755 "F 700 "F 670 "F 9..3 in. H20 9.3 in.H20 2750 ppm 2430 ppc &C~
"
Ml\-4FB " 385 cf:r. 3.41 735°F 695 OF 655°F 8.8 in. H20 8.1 in. Be0 2760 ppm 24SO pp 9"''''
",.3
MN-5FB "' " 385 cfm 2.91 535°F 505 "F 500°F No data -- off scale 2710 ppm 2230 ppm €C~
I-m-6F3 " " 385 efm 1.74 535 "F 500 "F 505°F 10.0 in. H2O 9.9 in.~O 2150 ppm ::"935 pp:':l 7C~
MN-7n " " 385 efm 2.20 655°F 600''F 595 "F No'data -- off scale 2750 pprn 2205 p~ e~~
I-m-8F3 " 385 efm 2.35 760°F 700 "F 680 "F No data -- off scale 2160 ppm 2290 1'P=1 e;~
MN-9B " 290 e:f'm 1.96 690°F 610 "F 590 "F 9.0 in. ~O 8.9 in. H20 2760 ppm 1280 ppm , ,...
...c,
-------
FLY ASR STUDY
502 CO~c. A..-erage
fes1: Feac~a:l~ Tes~ Gas Flow Sto1ch. :Bag Te%'Iperature Pressure Drop Re=oved From S02 Rerr.oval Over
,J~'t1=:1 <1sed Inte 1"\"2.l Rate Ratio :eottom z.'!~dd.lc Top Average l"itiU To :Bags Flue Gases In";~:'
- -
(,-l"A-l.F Slaked 7€~
Llme 6:) ='%1. ,85 cf'm 1.99 810°F 785°F 725°F 2.9 in. H20 5.1 in. H2O 2750 ppm 2135 ppm
tL-FP-'2F :;85 cfm 2.02 815 "F 790"F 740°F '.2 1n.JI20 4.4 in. H2O 2750 ppm 2;20 1'1=1 c5~
,..1"A-lF Slaked Do:'o-
:rr.i ti c Urn e ,85 cf':: 1.89 8500F 800 °F 750 "F 4.2 in.~O 6., in. H20 2740 ppm 1645 p~ 6o~
\170 X::.Cl}
1-FJI-2F " 385 cf'm 1.99 860 of Boo"F 730°F '.0 in. H20 4.9 in..B.20 2740 ppm 1910 ppm 7C~
L-Th-lF Slakei Lime
(1~ !~aC1) " 385 cfm 2.02 875 OF 825 OF 765°F 4.7 1n.H:i!O 7.9 in.B20 2750 ppm 20'5 ~ "1'1..~
~-FA-2F :;85 cfm 1.96 835°F 795 "F 750°F 4.2 1n.B20 7.4 in.B20 2740 pp:II 2010 ppc1 73~
:)-1' A-lF Slaked :>010-
:nutic Li..":le ., :;85 cf'm 1.95 840 °F 805 °F 765 °F 4.7 .in.~O 8.0 1n.B20 2750 pp:I1 1:;60 P!D 5~
)-FA-2F " :;85 cfm 2.08 8'0 of 800 of 750 "F 4.0 in.H20 5.8 1n.~O 2725 ppm 1525 ppr1 56~
r-FA-IT :'~~ese
-------
. APPENDIX D
-------
Sulfur Content of Fallout and Dustcake Samples.
From Representative Tests*
I Additive Study
Sample Description 10 S04 10 S03 10 Total Sulfur
UPL-9 Fallout 8.55 12.15 7.72
UPL-9 Dustcake 6.44 10.95 6.54
UPL-13 Fallout 12.09 11. 90 8.81
UPL-13 Dustcake 14.12 12.90 9.88
UPL-15 Fallout 11. 72 9.45 7.70
UPL-15 Dustcake 16.37 15.70 11.76
UPL-17 Fallout 11.10 10.05 7.73
UPL-17 Dustcake 12 . 06 10.60 8.27
UPL-18 Fallout 7.67 10.65 6.83
UPL-18 Dustcake 11.83 12.00 8.76
UPL-19 Fallout 5.69 12.00 6.71
UPL-19 Dustcake 5.05 10.55 5.91
UPL-22 Fallout 5.57 12.35 6.81
UPL-22 Dustcake
SD-4 Fallout 8.38 6.75 5.50
SD-4 Dustcake 11. 71 12.87 9.07
SD-14 Fallout 5.71 6.75 4.61
SD-14 Dustcake 11.40 8.35 7.15
SD-15 Fallout 8.08 12 .10 7.55
SD-15 Dustcake 6.77 7.47 5.25
PD-8 Fallout 12 . 09 4.20 5.72
PD-8 Dustcake 17.89 8.75 9.48
PD-1l Fallout 8.63 7.40 5.85
PD-11 Dustcake 25.24 9.85 12.37
PD-18 Fallout 32.41 2.37 11. 77
PD-18 Dustcake. 20.69 2.50 7.91
AA-4 Fallout 24.63 1.25 8.73
AA-4 Dustcake 29.81 LOO 10.35
-------
I Additive Study (Continued)
Sample Description 10 s04 10 S03 10 Total Sulfur
PL-5 Fallout 9.75 9.40 7.02
PL-5 Dustcake 13.02 12.35 9.30
PL-6 Fallout 5.23 11. 90 6.52
PL-6 Dustcake 8.41 12.95 8.00
PL-13 Fallout 2.08 5.45 2.88
PL-13 Dustcake 24.41 6.75 10.85
II Flue Gas Flow Rate Study
Sample Description 10 S04 10 S03 10 Total Sulfur
SD-2F Fallout 8.02 6.90 5.44
SD-2F Dustcake 16.97 9.90 9.63
SD-3F Fallout 5.39 8.15 5.07
SD-3F Dustcake 15.93 13.45 10.71
SD-5F Fallout 11. 07 9.45 7.48
SD-5F Dustcake 11. 79 9.00 7.54
SD-6F Fallout 8.77 8.15 6.20
SD-6F Dustcake 11. 56 13.65 9.33
SD-8F Fallout 8.72 6.95 5.70
SD-8F Dustcake 13.26 6.95 7.21
SD-9F Fallout 12.10 8.05 7.27
SD-9F Dustcake 14.13 12 . 00 9.53
SD-10F Fallout 10.13 6.80 6.11
SD-10F Dustcake 12.81 11. 45 8.87
SD-11F Fallout 4.96 7.70 4.74
SD-11F Dustcake 12.22 8.40 7.44
SD-12F Fallout 8.15 7.15 5.59
SD-12F Dustcake 12.69 14.75 10.15
SD-13F Fallout 5.32 7.60 4.82
-------
II Flue Gas Flow Rate Study (Continued)
Sample Description ~ SOI~ ~ S03 ~ Total Sulfur
PD-lF Fallout 1~.18 )~. ~O 6.12
PD-1F Dustcake 35.01 3.30 13.01
PD-~F Fallout 11.25 7:30 6.68
PD-3F Dustcake 34.28 5.80 13.77
PD-4F Fallout 11.17 6.70 6.41
PD-4F Dustcake 32.74 2.55 11.96
PD-5F Fallout 5.24 5.20 3.83
PD-5F Dustcake 24.3~ 7.45 11. 11
PD-7F Fallout 12.98 2.95 5.52
PD-7F Dustcake 27. 51 4.05 10.81
PD-IOF Fallout 10.35 5.95 5.84
PD-IOF Dustcake 29.70 4.65 11. 78
PD-12F Fallout 7.76 7.00 5.40
PD-12F Dustcake 14.49 8.05 8.06
MN-2F Fallout 16.22 0.30 5.54
MN-2F Dustcake 21. 50 0.65 7.44
MN-8F Fallout 18.59 0.35 6.35
MN-8F Dustcake 25.79 0.40 8.77
UPL-3F Fallout 14.38 14.30 10.53
UPL-3F Dustcake 20.63 9.85 10.84
UPL-10F Fallout 8.22 13.80 8.27
UPL-10F Dustcake 13.55 7.15 7.39
UPL-14F Fallout 2.48 13.35 6.18
UPL-14F Dustcake 7.12 14.70 8.24
AA-1F Fallout 25.03 1.15 8.82
AA-1F Dustcake 31.59 0.70 10.83
AA-8F Fallout 19.77 3.50 9.38
AA-8F Dustcake 23.84 2.25 8.86
AA-lOF Fallout 27.94 0.84 9.67
AA-lOF Dustcake 32.36 0.55 11. 03
AA-12F Fallout 27:55 0.95 9.58
-------
III Bag Coating Study
Sample Description ~ 804 ~ S03 % Total Sulfur
MN-4FB Fallout 24.23 0.60 8.33
MN-4FB Dustcake 23.46 0.50 7.49
MN-5FB Fallout 25.96 0.35 8.81
MN-5FB Dustcake 25.81 0.50 8.82
MN-10B Fallout 27. 30 0.40 9.27
MN-10B Dustcake 26.26 0.60 9.01
IV Fly Ash 8tudy
Sample Description ~ S04 ~ 803 ~ Total Sulfur
UPL-FA-1F Fallout 5.38 8.65 5.26
UPL-FA-1F Dustc~ke 9.76 7.90 6.42
8D-FA-1F Fallout 8.23 6.45 5.33
SD-FA-1F Dustcake 5.73 8.50 5.32
PL-FA-1F Fallout 3.62 7.10 4.05
PL-FA-1F Dustcake 5.98 13.50 7.41
PD-FA-2F Fallout 5.39 4.45 3.58
PD-FA-2F Dustcake 4.19 4.50 3.20
-------
APPENDIX E
-------
Reactant Physical Properties
B.E.T. Measured Coulter Counter
sur~ce Area* Density Pore Volume* Particle Size +
/ gram grams/cm3 cm3/gm Microns-Wt.Basis
MEAN MAXIMUM
1. Slaked Lime 9.1 3.03 1.09 6.0 19.0
2. Slaked Dolomite Lime 9.5 3.28 1.00 6.8 24.0
3. Slaked Dolomite Lime
(It,t, NaCl) 6.9 3.33 0.97 9.0 24.0
4. Slaked Lime (1% NaCl) 18.6 2.70 0.93 6.4 19.0
5. Manganese Dioxide 42.5 5.32 0.63 14 30.0
6. Alkalized Alumina 114.3 1.80 1.38 24 48.0
7. Nahcolite 6.1 2.53 0.63 13 38.0
*Determined by American Instrument Company, Silver Springs, Md.
-------
APPENDIX F
Coulter Counter Particle Size Analysis of
-------
Coulter Counter Particle Size Analysis *
of Reaction Products
Particle Diameter - Microns
Dustcake Fallout
Test
Designation Mean Maximum Mean Maximum
-
,
M.N -2 19 38 8.0 19
MN -5 15 31 8.2 19
NH-l 20 38 19 38
NH-4 19 38 11 30
UPL-9 10 24 10 24
UPL-17 12 24 16 30
UPL-22 14 30 12 30
SD-4 9.6 24 7.6 24
SD-14 7.8 24 9.4 24
PD-ll 10 24 6.4 19
PD-18 8.6 24 10.5 24
PL-6 11 24 10.5 24
PL-13 15 30 14 30
-------
APPENDIX G
-------
carbonate Analyses of Lime-Based Reaction Products
Wt. ~ Carbon Dioxide
Run No. Fallout Dustcake
SD - 4 8.9 9.5
SD - 14 10.9 10.6
SD - 15 8.3 10.4
SD-12 11.3 8.4
SD-2F 7.2 10.5
SD - 8F 13.4 10.1
PD- 1 9.5 4.7
PD - 10 12.8 7.9
PD- 8 6.3 5.7
PD - 18 8.1 9.1
PD - 11 10.7 7.2
PL- 5 14.5 12.3
PL - 13 24.1 16.8
PI, - 6 13.6 12.9
UPL- 9 11.0 1l.3
UPL- 13 13.9 8.1
UPL- 15 11.2 11.9
. . UPL- 19 1l.2 12.9
------- |