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

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probe-filter assembly was not changed, thus no secondary filter tests were Conducted at this sampling location. Quartz Tube Versus Stainless Steel Tube Performance Data The original probe-filter assemblies used at the furnace gas outlet and freeboard sample locations contained a quartz tube through which the gas sample was drawn. Due to the fragile nature of the quartz, it was desirable to eliminate the quartz tube and instead use a stainless steel tube. Some concern existed that a gas-stainless steel reaction -- more likely at high gas temperatures -- could possibly produce incorrect gas concentrations (particularly with NO ). By adjusting the water cooling rate on the probe, the temperature of the gas aloig its path of contact with the stainless steel was reduced to a low, non-reactive temperature level (200O to 400'F). The results of the quartz tube versus stainless steel tube tests, conducted at the furnace gas outlet and freeboard sample locations, are shown in the following performance tabulation: S W R Y Sample Gas Sample Tube Source Gas Temperature Sample Location DiameterIMaterial Temperature In Probe Gas Concentration Comparisons (Inch) (OF) (OF) Furnace Outlet 518 SS 800 300 Max Gas concentrations for 0 , CO , CO, SO , and NO were essent?ally2 Furnace Outlet 518 Quartz 800 300 Max idfntical f& both the quartz and stainless steel tube sample probes. Free board 518 SS 1700 280 - 305 Gas concentrations for 02. CO , CO, Freeboard 318 ss 1700 325 - 400 SO , and NO were essentially' idzntical f0"r the quartz tube and the two (518" and 318" diameter) Freeboard 518 Quartz 1700 155 - 220 stainless steel tube sample probes. Gas sampling and analysis form a major portion of the performance evaluation of the 6' x 6' AFBC facility. The analysis requires measuring the concentration of six different gases at three sample locations -- in-bed, freeboard, and furnace gas outlet. Sample flow rates of 6 to 10 liters per minute are needed for analyzing these gases. Accurate sampling and analysis from the high-temperature - high velocity, dust- laden environment of the fluidized bed unit requires the use of a system that includes certain special equipment. An "efficient particulate filter" is needed to clean the large-volume gas samples removed from the adverse environment of the 6' x 6' unit. A ceramic filter -- constructed of inert material, self-cleaning, having minimum pressure drop, and able to withstand high temperatures and abrasive wear -- served as the primary particulate filter in our final design. A cartridge-type secondary filter eliminated the glassware and decreased connection joints, while serving its main function of protecting the remaining sample system components in the case of a failure of the primary (ceramic) filter. Eliminating the quartz tube has produced a design that includes no fragile (glassware or quartz) components. 214
' ' The modifications have been combined to produce a refined gas sampling system that can be used at sample locations of interest in fluidized beds. It has been used for collecting and for accurately analyzing gas data over extended test periods for a multiple number of planned test conditions. These results have played a major role in the evaluation of the AFBC performance. The refined gas sampling system -- developed for the 6' x 6' fluidized bed application -- is recommended as a reliable system for fluidized bed units. 215
Page 1 and 2:
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
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I. INTRODUCTION DIRECT METHANATION
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The catalyst development program fo
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Preparing process flow diagrams and
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\ \ i 1. 2,000 4,000 6,000 8,000 10
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(JMS-OlBM-2). The mass spectra were
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I I Fairbridge, R.W. (ed.) 1972, En
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v- W V z d 3 z m 4 ? P m W c3 W m N
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e. \ I , W 2 m 4 t- CI 99-79 noooo
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L Table I: Compositions of High Tem
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\ " \ I For all three coals, the pr
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4 , 1024 1024 3a 3b J Mineral Parti
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The Determination of Mineral Distri
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pyrite crystals in framboids locate
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FIG. 1. TEM MICROGRAPH OF A HIGH VO
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\ \ FIG. 5. SEM MICROGRAPH SHOWING
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\ , species. In fact, combustion ex
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1, It is possible to make a reasona
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\ i SURFACE AND BULK ENRICHMENT OF
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I Coal Ash Sintering Model and the
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5 carried out such sintering measur
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I this ash and other bituminous coa
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forming propensity. However, none o
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t I 153
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CENTRAL ELECTRICIN RESEARCH LABORAT
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157 18 I I a I
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temperature, sulfur species concent
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The facility is fired with coal usi
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
Page 211 and 212: GAS SAMPLING WITH ORIGINAL PROBE-FI
Page 213: Remove the quartz tube (gas sample
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Page 219 and 220: With regard to the similarity parti
Page 221 and 222: i \ ' 2.2. soz Emission and NOx Emi
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Page 225 and 226: Figure 9: Sulphur captLTre as 0 fun
Page 227 and 228: P SUMMARY OF TESTS Testing complete
Page 229 and 230: I Table 1 Comparison of Sulfur Capt
Page 231 and 232: , NITROGEN OXIDE REDUCTION Single-S
Page 233 and 234: 0 The addition of air at the 96-inc
Page 235 and 236: m- Y i? 4: BO n 8 c Y l0- Bo- I I I
Page 237 and 238: E! w 2 z e Y 100 - 3 t 5 80- 0, 40
Page 239 and 240: 0 f 0.so o'm: 0.300 0.zo - - A 5m 4
Page 241 and 242: &e- -A \ \ \ : ERCENT OVERBED AIR I
Page 243 and 244: PARTICLE ENTRAINMENT AND NITRIC OXI
Page 245 and 246: i 1' 1 ! I. i Chaung (15) showed th
Page 247 and 248: The maximum height that a large par
Page 249 and 250: 3.0 Nitric Oxide Reduction in the F
Page 251 and 252: assumed to be identical to that of
Page 253 and 254: Nomenclature A *t cD ‘NO $3 _ _ _
Page 255 and 256: TABLE 2. OPERATING CONDITIONS AND E
Page 257 and 258: i 1 \ ', References 1. 2. ( 3. 1 4.
Page 259 and 260: \ ” Y) I 259
Page 261 and 262: t I 100 - - I I ] , I , I , I 'ii 9
Page 263 and 264: Feeding of the carbonaceous materia
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! Table 2 Proximate and ultimate an
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lb, , --pp---p-- 4 p? CHAR 1 Tu-IWO
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I CHAR Y Y /I TIME O i ' ' ' ' 1 '
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could not be assumed constant. Thus
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\ greatly acknowledged. Literature
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constructed and operated to demonst
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The experimental procedure for the
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atmospheric pressure fluidized bed
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1' TABLE 2 Screen Analysis of Sand
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n RECORDER I Ill I ’ NO. NOX THER
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\ 285 Y 0 I- 5 B 5 3 m "9 E5 3 uz 0
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CHAR1 TOC 0.85 M3/k 600 0 700 V 750
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f Durin all the experimental runs t
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Assuming that large coal particles
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i 7 -_ 0 m\o --n 0 W i 293 a\o 0
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The influence of particle size dist
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all the initial values of x for whi
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\ - + 1) x. = 1 bL/n YO Defining di
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$ 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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