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

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1 60 I I RUN KE-5 50 T.1121K(1557'F) PARTICLE RESIDENCE TIME, rnr 5 IO 50 100 200 1 1 I l l 500 I IO00 1650 I I P. IO 3 i 1o6Po~150OPr~o) 40 s i 2 30 U > 0 " 20 IO ' . . . 01 I I I 0001 0 01 01 10 I REACTOR LENGTH. rn Figure 5. Carbon and Moisture-Ash-Free Coal Conversions along Reactor Length 30 Z RUN KE-5 w 5 REACTOR LENGTH, 11 0 01 01 I 10 20 I I I I I T.1121 K (1557'Fl P = IO 3% IO~PO (1500 pria~ .. REACTOR LENGTH. m Figure 6. Distribution of Total Carbon Conversion to Different Species along Reactor Length REACTOR LENGTH, 11 0 40- 4 I a I 12 16 I I (100.1. - HZ' * - P. IO 3" l06PO (1500prtol - I 2 3 4 5 6 REACTOR LENGTH, rn Figure 7. Gas Composition along Reactor Length 66 to
The Effect of Potassium Carbonate on the Gasification of Illinois No. 6 Coal A.H. Pulsifer and J.F. McGehee, Department of Chemical Engineering and Engineering Research Institute, Iowa State University, Ames, Iowa 50011. L. SarOff, U.S. Department of Energy, Pittsburgh Energy Technology Center, Pitts- burgh, Pennsylvania 15213. Catalyzed coal gasification can lead to reduced gasifier size and lower gasification temperatures which give greater thermal efficiencies. Therefore, an investigation of the steam gasification of a bituminous coal under moderately high Pressures was conducted. The primary objective of the study was to determine the influence of an alkali metal carbonate catalyst on the kinetic parameters of the gasification reaction. The coal chosen for the study was an Illinois No. 6 coal and this material was gasified both with and without the addition of potassium carbonate. Experiments were carried out at temperatures between 700 and 900°C and at a pressure of 2.17 MPa (21.4 atm). The partial pressures of steam, carbon dioxide and hydr0g.c:. were also varied during the investigation. The carbon gasification rate was modeled using an unreacted, shrinking-core model and kinetic constants and activation energies were determined. Experiment a 1 Met hods The apparatus used to gasify the coal was a high-pressure, tubular, fixed bed reactor with an external heat supply. One of the unique features of this apparatus was its charging system. A 10 g sample of coal was held at a temperature near ambient in a pressurized vessel located above the reactor. Actuatioq of a ball valve allowed the sample to fall into the reactor, commencing the experimental run. The apparatus was able to gasify a sample of coal with steam, or mixtures of steam and H2,N2, or C02. Carbon gasification rates were determined from the product gas flowrate and composition. shown in Fig. 1. The essential features of the apparatus are The reactor and coal charging vessel were constructed from type 316 stainless steel. The reactor body was a 21-inch (53.3 cm) long, 3/4-inch schedule 150 tube with an outside diameter of 1.050 in. (26.7 mm) and an inside diameter of 0.514 in. (15.6 mm). A 0.125-in. (3.2 mm) thick porous stainless steel disc was located inside the tube, 6.5 in. (16.5 cm) from the bottom. This disc supported the bed of coal inside the reactor. The coal charging vessel, a cylindrical funnel-shaped container with a volume of approximately 50 cm3, was connected to the top of the reactor by a vertical 3/4-inch schedule 160 tube with an inside diameter of 0.464 in. (11.8 mm). A t the bottom of this vessel was a ball valve. Charging the reactor was accomplished by opening the valve by means of a pneumatic actuator. The coal then fell a distance of 11 in. (27.9 cm) into the reactor. The heat necessary to generate steam and gasify the coal was supplied externally through electric resistance heaters. There were three separate electrical heating circuits. These supplied the gas preheater and steam vaporizer, the reactor furnace, and the bottom flange heater. Water for steam generation was delivered to the system by a high-precision 57
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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
Page 16 and 17: Table 8 L_ Effect os FaeO Compo.lrl
Page 18 and 19: i-l SPARE SAblPLE Plortlc 209 Figur
Page 20 and 21: - z c 100,000 50,000 10,000 0 n 5,0
Page 22 and 23: Flnure 9 SWELLltlG PROPERTIES OF PI
Page 24 and 25: Fi ure 13 EFFECT OF TOTAL PRESSQRE,
Page 26 and 27: TABLE 1. OPERATING CONDITIONS Opera
Page 28 and 29: 1. . 2. 3. 4. 5. 6. 7. 8. 9. REFERE
Page 30 and 31: Figure 4. SCANNING ELECTRON MICROGR
Page 32 and 33: Turkgodan et al. (18) studied the p
Page 34 and 35: Materidl balance on packed bed Boun
Page 36 and 37: These phenomena iiiay be described
Page 38 and 39: Walker, P. L., Rusinko, F., and Aus
Page 40 and 41: -""I- *I,".. I Dlrf".,on Co.1flcl.n
Page 42 and 43: After a variable residence time, th
Page 44 and 45: Changes in Char Chemistry The infra
Page 46 and 47: 20. 21. 22. 23. 24. 25. 26. 27. 28.
Page 48 and 49: 0s-a 00-a OS'S 00-E os-2 00-2 02.1
Page 50 and 51: COAL PYROLYSIS AT HIGH TEMPERATURES
Page 52 and 53: actions, decreasing the secondary c
Page 54 and 55: 01 40 60 TI MEISeC) 80 100 120 140
Page 56 and 57: Reaction Temperature OC In-situ Ini
Page 58 and 59: and the gas velocity is often repre
Page 60 and 61: The mathematical model developed he
Page 62 and 63: si sio Fraction of solid species i
Page 64 and 65: Table 2. Differential Equations Mod
Page 68 and 69: to condense excess steam, the press
Page 70 and 71: conversion-time data.* The integrat
Page 72 and 73: catalyzed and uncatalyzed runs were
Page 74 and 75: CATALYTIC EFFECTS OF ALKALI METAL S
Page 76 and 77: %me thermogravimetric measurements
Page 78 and 79: than in steam. Figure 9 shows data
Page 80 and 81: C - C02 REACTION C - H20 REACTION L
Page 82 and 83: 1. 2. 3. 4. 5. 6. 7. 8. 9. 10. 11.
Page 84 and 85: n 'm L u. t m - L 84
Page 87 and 88: i 5360-096bw \ KINETICS OF POTASSIU
Page 89 and 90: t 5360-096pj There is an interactio
Page 91 and 92: 1 I > \ i I 5360-096bw bed data. Be
Page 93 and 94: I 1. I 5360-096bw ranging from atmo
Page 95 and 96: uY.ku ICHlMAlIC OF MINI-FLUID BE0 R
Page 97 and 98: 800-12-1133 -9 FIGURE IO CALCULATED
Page 99 and 100: Mexico coal. Table 1 shows an analy
Page 101 and 102: ', Complete results from all runs c
Page 103 and 104: I the methanol down to atmospheric
Page 105 and 106: TABLE 3 -----______________________
Page 107 and 108: \ "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
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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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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
Page 305 and 306:
UNBURNT FRACTION UNBURNT FRACTION m
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