the coking properties of coal at elevated pressures. - Argonne ...

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Post Flame Cavity -(TJ 0 Temperature OF Figure 1. Effect of Temperature and Stoichiometric P,atio on Equilibrium Calcium Distribution - % Ca as CaS04 or CaS (Ca/S = 1) 4-L Air + Coal- Radiant 0 Sample Locations 0 Sorbent Injection A Internal Air Staging External Air Staging - Cooling Air II II 0 Exhaust Figure 2. Schematic of Test Furnace Showing Location of Sample Ports, Staged Air Addition and Sorbent Injection. 160
The facility is fired with coal using a small scale low NOx burner which could be operated in two modes - internally and externally staged. When the burner was operated with the second stage air supplied at the firing face through the staged air injectors, only the burner zone was fuel rich. This is referred to as internally staged. Alternatively, when the staging air was added downstream in the post flame cavity, the whole of the radiant furnace operated fuel rich. This is referred to in the text as external staging. The sorbent was added in any of four locations: 1) with the coal, 2) with the staged air at the burner face, 3) at the entry of the post flame cavity, and 4) with the dowixtream staged air when operating in the externally staged mode. The measurement of sulfur species in combustion products containing active sorbents introduces several problems related to sample acquisition. A "phase discrimination" probe has been designed, constructed and tested which minimizes gassolid contacting after sample extraction. SO2 was measured with a non-dispersive ul tra-violet absorption instrument. H2S and COS were measured by gas chromatography using a flame photometric detector. Sulfur capture was based on SO2 measurements with and without sorbent in every test case. 3. RESULTS A series of experiments has been carried out with the coal and sorbent listed in Tables 1 and 2 in both the external and internal staging modes. Indiana Coal Ultimate Analysis, % Dry Basis C 69.91 N 5.13 H 1.54 S 2.53 0 11 .OD Ash 9.84 Cslorific Value (dry bais) 12,515 Btu/lb Moisture, average, as burned 7.0% Internal Staging Table 1. Coal Properties Vicron 45-3, Pfizer Composition, typical, % CaC03 97.0 MgC03 1.6 sio2 1 .o 2'3 0.5 Fe203 Moisture 0.05 0.2 Specific Gravity Particle Shape Oil absorption Surface area (m2/gm) ~~ Table 2. Sorbent Properties 2.71 rhombic 4 1.4 Figure 3 shows the Percentage capture as a function of the calcium to sulfur molar ratio when the sorbent was added with the staged air (location 2), and an additional 15% (over the normal heat loss) of the input heat was extracted from the radiant zone. Data are presented showin the relative capture in the radiant zone (sample port 11, the post flame section ?between 1 and 2) and the overall capture (sample port 3). The capture in the post flame section is based upon the gas phase sulfur dioxide concentration entering the section and free calcium oxide (that which was not used in the radiant section). The data presented in Figure 3 indicate that when heat is extracted from the radiant zone capture occurs in both the radiant zone and the post flame section. These data were obtained with the burner zone operating at a stoichiometric ratio of 0.6 and a total air input equal to 120% of stoichiometric . 161
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I / The Coking Properties of Coal a
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Procedure : Hand picked lunips of c
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Apparatus: The equipment for this t
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the total pressure on the swelling
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A comparison of the results obtaine
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was used, however, general trends a
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1 D 13 3 G
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Table 8 L_ Effect os FaeO Compo.lrl
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i-l SPARE SAblPLE Plortlc 209 Figur
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- z c 100,000 50,000 10,000 0 n 5,0
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Flnure 9 SWELLltlG PROPERTIES OF PI
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Fi ure 13 EFFECT OF TOTAL PRESSQRE,
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TABLE 1. OPERATING CONDITIONS Opera
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1. . 2. 3. 4. 5. 6. 7. 8. 9. REFERE
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Figure 4. SCANNING ELECTRON MICROGR
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Turkgodan et al. (18) studied the p
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Materidl balance on packed bed Boun
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These phenomena iiiay be described
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Walker, P. L., Rusinko, F., and Aus
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-""I- *I,".. I Dlrf".,on Co.1flcl.n
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After a variable residence time, th
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Changes in Char Chemistry The infra
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20. 21. 22. 23. 24. 25. 26. 27. 28.
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0s-a 00-a OS'S 00-E os-2 00-2 02.1
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COAL PYROLYSIS AT HIGH TEMPERATURES
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actions, decreasing the secondary c
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01 40 60 TI MEISeC) 80 100 120 140
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Reaction Temperature OC In-situ Ini
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and the gas velocity is often repre
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The mathematical model developed he
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si sio Fraction of solid species i
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Table 2. Differential Equations Mod
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1 60 I I RUN KE-5 50 T.1121K(1557'F
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to condense excess steam, the press
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conversion-time data.* The integrat
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catalyzed and uncatalyzed runs were
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CATALYTIC EFFECTS OF ALKALI METAL S
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%me thermogravimetric measurements
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than in steam. Figure 9 shows data
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C - C02 REACTION C - H20 REACTION L
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1. 2. 3. 4. 5. 6. 7. 8. 9. 10. 11.
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n 'm L u. t m - L 84
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i 5360-096bw \ KINETICS OF POTASSIU
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t 5360-096pj There is an interactio
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1 I > \ i I 5360-096bw bed data. Be
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I 1. I 5360-096bw ranging from atmo
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uY.ku ICHlMAlIC OF MINI-FLUID BE0 R
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800-12-1133 -9 FIGURE IO CALCULATED
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Mexico coal. Table 1 shows an analy
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', Complete results from all runs c
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I the methanol down to atmospheric
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TABLE 3 -----______________________
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\ "I N z 107 c. . 0 0
Page 109 and 110: I. INTRODUCTION DIRECT METHANATION
Page 111 and 112: The catalyst development program fo
Page 113 and 114: Preparing process flow diagrams and
Page 115 and 116: \ \ i 1. 2,000 4,000 6,000 8,000 10
Page 117 and 118: (JMS-OlBM-2). The mass spectra were
Page 119 and 120: I I Fairbridge, R.W. (ed.) 1972, En
Page 121 and 122: v- W V z d 3 z m 4 ? P m W c3 W m N
Page 123 and 124: e. \ I , W 2 m 4 t- CI 99-79 noooo
Page 125 and 126: L Table I: Compositions of High Tem
Page 127 and 128: \ " \ I For all three coals, the pr
Page 129 and 130: 4 , 1024 1024 3a 3b J Mineral Parti
Page 131 and 132: The Determination of Mineral Distri
Page 133 and 134: pyrite crystals in framboids locate
Page 135 and 136: FIG. 1. TEM MICROGRAPH OF A HIGH VO
Page 137 and 138: \ \ FIG. 5. SEM MICROGRAPH SHOWING
Page 139 and 140: \ , species. In fact, combustion ex
Page 141 and 142: 1, It is possible to make a reasona
Page 143 and 144: \ i SURFACE AND BULK ENRICHMENT OF
Page 145 and 146: I Coal Ash Sintering Model and the
Page 147 and 148: 5 carried out such sintering measur
Page 149 and 150: I this ash and other bituminous coa
Page 151 and 152: forming propensity. However, none o
Page 153 and 154: t I 153
Page 155 and 156: CENTRAL ELECTRICIN RESEARCH LABORAT
Page 157 and 158: 157 18 I I a I
Page 159: temperature, sulfur species concent
Page 163 and 164: Tests have been carried out to dete
Page 165 and 166: under which conditions sulfur speci
Page 167 and 168: I TITANIUM L Corn AS A TRACER FOR D
Page 169 and 170: E 6 i i h \ 1 1 \ on the XRF is cau
Page 171 and 172: \ ? CONCLUSIONS Titanium can accura
Page 173 and 174: NY) m * oa
Page 175 and 176: GFETC constructed a 0.2 square mete
Page 177 and 178: \: Stage 3. Sulfated ash-cemented a
Page 179 and 180: I FIG. 1. Initial ash coating on qu
Page 181 and 182: FIG 9. Limestone bed material alter
Page 183 and 184: (4) Since the operating temperature
Page 185 and 186: I I maximum particle diameter leavi
Page 187 and 188: ! suspension chambers and cyclone f
Page 189 and 190: Pilot Plant of a Coal Fired Fluidiz
Page 191 and 192: After the fiscal year 1982, the fol
Page 193 and 194: MBC CBC Fig. 1 Boiler Structure 193
Page 195 and 196: \ i Table 2. Coal Properties Planne
Page 197 and 198: -2- more than 3 years, since 1977.
Page 199 and 200: , I B. 2 which temporarily raised t
Page 201 and 202: -6- abrasion rate at the bottom of
Page 203 and 204: \if F3.3 - Particulate Circulation
Page 205 and 206: \' I/O. analog 1/13. industrial I/O
Page 207 and 208: ACQUISITION DATA UNIT < I L- J (T)
Page 209 and 210: SAMPLING SYSTEM FOR FLUIDIZED BED A
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GAS SAMPLING WITH ORIGINAL PROBE-FI
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Remove the quartz tube (gas sample
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' ' The modifications have been com
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n n D 217
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With regard to the similarity parti
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i \ ' 2.2. soz Emission and NOx Emi
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223
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Figure 9: Sulphur captLTre as 0 fun
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P SUMMARY OF TESTS Testing complete
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I Table 1 Comparison of Sulfur Capt
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, NITROGEN OXIDE REDUCTION Single-S
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0 The addition of air at the 96-inc
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m- Y i? 4: BO n 8 c Y l0- Bo- I I I
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E! w 2 z e Y 100 - 3 t 5 80- 0, 40
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0 f 0.so o'm: 0.300 0.zo - - A 5m 4
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&e- -A \ \ \ : ERCENT OVERBED AIR I
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PARTICLE ENTRAINMENT AND NITRIC OXI
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i 1' 1 ! I. i Chaung (15) showed th
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The maximum height that a large par
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3.0 Nitric Oxide Reduction in the F
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assumed to be identical to that of
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Nomenclature A *t cD ‘NO $3 _ _ _
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TABLE 2. OPERATING CONDITIONS AND E
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i 1 \ ', References 1. 2. ( 3. 1 4.
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\ ” Y) I 259
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t I 100 - - I I ] , I , I , I 'ii 9
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Feeding of the carbonaceous materia
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! Table 2 Proximate and ultimate an
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lb, , --pp---p-- 4 p? CHAR 1 Tu-IWO
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I CHAR Y Y /I TIME O i ' ' ' ' 1 '
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could not be assumed constant. Thus
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\ greatly acknowledged. Literature
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constructed and operated to demonst
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The experimental procedure for the
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atmospheric pressure fluidized bed
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1' TABLE 2 Screen Analysis of Sand
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n RECORDER I Ill I ’ NO. NOX THER
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\ 285 Y 0 I- 5 B 5 3 m "9 E5 3 uz 0
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CHAR1 TOC 0.85 M3/k 600 0 700 V 750
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f Durin all the experimental runs t
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Assuming that large coal particles
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i 7 -_ 0 m\o --n 0 W i 293 a\o 0
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The influence of particle size dist
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all the initial values of x for whi
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\ - + 1) x. = 1 bL/n YO Defining di
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$ m. 1 Results and Discussion Evalu
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kl k2 k' KC KD m m. m P N P R R g t
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UNBURNT FRACTION UNBURNT FRACTION m
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