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

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1.01 I (a) Char N 0 x - 0.5- a - X 0- KEY1 11 I N0inbpn)lOZ in I %) A 1 01243-2531 0 I 0 1 73 I 251 -2561 1.83- 1.86 700 750 aoo 850 900 Temp. I T ) (b) Carbon Fig. 7 Increased extent of "NO" reduction caused by oxygen Concluding Remarks "NOx" This paper descirbed the recent findings concerning the behavior of formation in a fluidized bed combustor obtained by use of a variety of carbonaceous materials. The "NO" emission under an excess air condition was decreased with an increase in the volatile contents of fuels. The emission of "NO" and other nitrogeneous contents formed under a substoichiometric combustion was also strongly dependent on the volatile contents. The staged combustion of less volatile char and coke provided a radical reduction of "NO" emission. The steady state carbon concentration was measured and "NO" emission was found to be inversely related to the carbon concentration. The intrinsic conversion ratio of fuel nitrogen to "NO" was measured. The kinetics of "NO" destruction by char in both the absence and presence of oxygen was investigated. The rate for char was increased up to 75OOC. "NO" was reduced catalytically by carbon monoxide and hydrogen over a char surface, but the rate was not increased. Acknowledgement D. K. whishes to express his thanks to Grant-in-Aid for Energy Re- search (NO 311604, NO 411003 & NO 505021) of the Ministry of Education. T.F. received Grant-in-Aid for Scientific Research (NO 455363 & NO 555374) from the same body. The experimental assistance by Mr. A. Kat0 was 272
\ greatly acknowledged. Literature Cited Be&, J.M., A.F. Sarofim, L. Chan L A. Sprouce: Proceedings of the 5th Int. Conference on Fluidized Bed Combustion, p577 -p592 (1977) Be&, J.M., A.F. Sarofim L Y.Y. Lee, Proceedings of the 6th Int. Conference on Fluidized Bed Combustion, p942 -p955 (1980) Jonke, A.A., G.J. Vogel, E.L. Carls et al.: Series 68, NO 126, 241 (1972) Chem. Eng. Prog. Symp. Furusawa, T., T. Honda, J. Takano and D. Japan 11, 377 (1978) Kunii: J. of Chem. Eng. Furusawa, T., N. Yamada, T. Sendo and D. Japan 12, 71 (1979) Kunii: J. of Chem. Eng. Furusawa, T., T. Honda, J. Takano and D. Kunii: Fluidization, Proceedings of 2nd Eng. Found. Conf., Cambridge University Press (1978) Furusawa, T., D. Kunii, N. Yamada and A. Oguma: Int. Chem. Eng. E, 239 (1980) or Kagaku Kogaku Ronbunshu 4, 562 (1978) Furusawa, T., D. Kunii and T. Tsunoda: under preparation Gibbs, B.M., F.J. Pereira and J.M. Be&: 16th Symposium on Combustion, Cambridge, 461 (1976) 10) Kunii, D., K.T. Wu and T. Furusawa: Chem. Eng. Sci. 35, 170 (1980) 11) Kunii, D., T. Furusawa and K.T. Wu: ed. J.R. Grace a;;;i J.M. Matsen, Fluidization, Plenum Publishing Corp. New York, p175 -p183 (1980) 12) Cowley, L.T. and P.T. Roberts: Paper submitted for presentation at the Fluidized Combustion Conference, 28-30th Jan. (1981) held at the Energy Research Institute, University of Cape Town, South Africa 273
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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
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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
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Tests have been carried out to dete
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under which conditions sulfur speci
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I TITANIUM L Corn AS A TRACER FOR D
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E 6 i i h \ 1 1 \ on the XRF is cau
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\ ? CONCLUSIONS Titanium can accura
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NY) m * oa
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GFETC constructed a 0.2 square mete
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\: Stage 3. Sulfated ash-cemented a
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I FIG. 1. Initial ash coating on qu
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FIG 9. Limestone bed material alter
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(4) Since the operating temperature
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I I maximum particle diameter leavi
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! suspension chambers and cyclone f
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Pilot Plant of a Coal Fired Fluidiz
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After the fiscal year 1982, the fol
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MBC CBC Fig. 1 Boiler Structure 193
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\ i Table 2. Coal Properties Planne
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-2- more than 3 years, since 1977.
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, I B. 2 which temporarily raised t
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-6- abrasion rate at the bottom of
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\if F3.3 - Particulate Circulation
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\' I/O. analog 1/13. industrial I/O
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ACQUISITION DATA UNIT < I L- J (T)
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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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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
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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.
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Page 261 and 262: t I 100 - - I I ] , I , I , I 'ii 9
Page 263 and 264: Feeding of the carbonaceous materia
Page 265 and 266: ! Table 2 Proximate and ultimate an
Page 267 and 268: lb, , --pp---p-- 4 p? CHAR 1 Tu-IWO
Page 269 and 270: I CHAR Y Y /I TIME O i ' ' ' ' 1 '
Page 271: could not be assumed constant. Thus
Page 275 and 276: constructed and operated to demonst
Page 277 and 278: The experimental procedure for the
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Page 281 and 282: 1' TABLE 2 Screen Analysis of Sand
Page 283 and 284: n RECORDER I Ill I ’ NO. NOX THER
Page 285 and 286: \ 285 Y 0 I- 5 B 5 3 m "9 E5 3 uz 0
Page 287 and 288: CHAR1 TOC 0.85 M3/k 600 0 700 V 750
Page 289 and 290: f Durin all the experimental runs t
Page 291 and 292: Assuming that large coal particles
Page 293 and 294: i 7 -_ 0 m\o --n 0 W i 293 a\o 0
Page 295 and 296: The influence of particle size dist
Page 297 and 298: all the initial values of x for whi
Page 299 and 300: \ - + 1) x. = 1 bL/n YO Defining di
Page 301 and 302: $ m. 1 Results and Discussion Evalu
Page 303 and 304: kl k2 k' KC KD m m. m P N P R R g t
Page 305 and 306: UNBURNT FRACTION UNBURNT FRACTION m
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