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

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The mathematical model developed here has been used successfully to describe these hydropyrolysis reactors. Reasons for small discrepancies in experimental and predicted reactor performances are attributable to inadequacies in model formulation, unavailability of experimental data particularly reactor wall temperature profiles, and uncertainties in the experimental data. / A detailed parametric study has been performed using this model to identify important reactor parameters for the design of commercial entrained flow hydropyrolysis reactors. The results are given elsewhere (1). Acknowledgement The authors are grateful to Dr. S. Weil for providing many helpful suggestions and criticisms throughout this entire study. Nomenclature Contact area between solids and gas per unit reactor volume Number of carbon atoms per mole of gas species (CHzIa Reactor cross-sectional area Number of carbon atoms per mole of gas species (CHpf)b Rate of gas species j going from solid phase to gas phase (i.e. crossing boundary) per unit reactor volume Fractional coal conversion (moisture-free) Fractional coal conversion (moisture-ash-free) Heat capacity of gas species j Heat capacity of solid species i Derivative with respect to distance along reactor (x) Helix diameter Particle diameter Reactor diameter Drag force exerted by fluid on the particles per unit volume of particles Frictional force between the gas and the wall of the reactor Solids flow rate per unit reactor cross-sectional area Gravitational acceleration Conversion factor (32.2 lbm-ft/sec2/lbf) Gas flow rate per unit reactor cross-sectional area Total enthalpy of gas species j Overall heat transfer coefficient between gas and solid particle Overall heat transfer coefficient between gas and wall Total enthalpy of solid species i Rate of gaseous hydrogen reacting with solid phase per unit reactor volume Wall heat losses fron reactor per unit reactor length (due to convection between gas and wall) 60
1: I !. Hlsa M Total wall heat losses from reactor per unit reactor length per unit reactor cross-sectional area Atomic ratio of hydrogen to carbon in oils and tars (also in species CHK) \ Mj Molecular weight of gas species j p Total reactor pressure Qash R Universal gas constant R, Reg Gas Reynolds number Ri Ash flow rate per unit reactor cross-sectional area Char to gas weight ratio Reaction rate (d
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
Page 9 and 10: A comparison of the results obtaine
Page 11 and 12: was used, however, general trends a
Page 13 and 14: 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 62 and 63: si sio Fraction of solid species i
Page 64 and 65: Table 2. Differential Equations Mod
Page 66 and 67: 1 60 I I RUN KE-5 50 T.1121K(1557'F
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
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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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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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