Liquefaction co-processing of coal shale oil at - Argonne National ...

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2nd Stage Catalyst Table 2 THE EFFECT OF RESIDENCE TIME ON CONVERSION FOR THE SOLUBILIZATION OF HIGHVALE COAL IN BITUMEN WITH CO/STEAM OR H2 AT 390°C Time (min') Coal Conversion (on daf coal ) 0 15 30 60 CO/Steam Table 3 H7 58 10 65 34 85 65 86 68 PRODUCT YIELDS AND COAL CONVERSIONS FROM THE TWO-STAGE CO-PROCESSING OF BITUMEN AND HIGHVALE COAL K2Mo04 - CH3SSCH3 1st Stage Reducing Gas H2 CO/H20 CO/H20-K2C03 - Yielda Hydrocarbon Gas (C,-C5) 7.2 (20.8) 5.2(+0.2) 5.3c Distillable Oil (IBP-525"C) 62.3(+0.9) 57.7 (+0.8 ) 66.2 (20.7 ) Soluble Extract 18.0 (20. 2 ) 19.3 (20. 9) 18.7 (+O .3 ) Material Balance 94.1 (23.1 ) 90.4 (20.2) 96.1' Coal Conversion (X daf coal) 90 (21 ) 91 (21) 98 (20 1 a) Yields are presented as % daf organic feed (bitumen + coal). b) All data are quoted as the average values of two duplicate experiments. Figures in brackets show the spreads for the two experiments. c) Single data point. 205 ~
Table 4 OVERALL MASS BALANCE FOR THE OPTIMIZED ARC TWO-STAGE CO/H2O-K2CO3 - H2 COALDITUMEN PROCESS Bitumen Coal - 2.5/1 Basis 100 kg - feed (daf) Component Input output c5-2000c 3.1 11.0 200-375OC 15.0 40.1 375-525OC 16.1 19.0(2) + 525OC 37.2 12.3 Coal 28.6 Ash 1.5(1) Unconverted Coal Residue Water co c02 10.26 0.6 26.1 H2S NH4 '1-'4 Catalyst 0.34 2.7 1.84 44.7 1.5 0.46 5.2 138.8 138.8 (1) Ash reduced to 5% by deashing. (2) Estimate of yield after optimization. 206
Page 1 and 2:
ABSTRACT LIQUEFACTION CO-PROCESSING
Page 3 and 4: eaction temperature, 1000-1500 psig
Page 5 and 6: 6. 7. 8. 9. 10. 11. 12. 13. 14. 15
Page 7 and 8: I 0" 100- I I I WyO-3 P 3: 1500 psi
Page 9 and 10: 11.3 A-6 yJ 600 OF, 1500 psig CO, 3
Page 11 and 12: Experimental UDqradinq and Cooroces
Page 13 and 14: catalytic to the thermal hydrogenat
Page 15 and 16: the reaction with oil production re
Page 17 and 18: TET did not promote the production
Page 19 and 20: MICROAUTOCLAVE DESCRIPTION AND PROC
Page 21 and 22: FEEDSTOCK PROPERTIES Some propertie
Page 23 and 24: CONCLUSIONS HRI's microautoclave ha
Page 25 and 26: 176
Page 27 and 28: 100. 2 8%. M = ?8. 38. .... . . . .
Page 29 and 30: CATALYTIC CO-PROCESSINS OF OHIO NO.
Page 31 and 32: CATALYST COMPARISON STUDY The premi
Page 33 and 34: fractions and a decrease of heavier
Page 35 and 36: TABLE 2 Coal Analyses I1 1 i noi s
Page 37 and 38: Temperature WHSV, G/hr/cc TABLE 6 C
Page 39 and 40: z FIGURE 3 COAL REACTIVITY SCREENIN
Page 41 and 42: COPROCESSING USING HzS AS A PROMOTE
Page 43 and 44: - 3 - that product yields depend on
Page 45 and 46: - 5 - occurs in the yields of aspha
Page 47 and 48: Table 1 Analysis of Feedstocks Fore
Page 49 and 50: THO-STAGE COPROCESSING OF SUBBITUMI
Page 51 and 52: esult in retrogressive reactions ta
Page 53: 8. 6. Ignasiak, L. Lewkowicz, G. Ko
Page 57 and 58: BACKGROUND COAL LIQUEFACTION/RESID
Page 59 and 60: system, which could be operated wit
Page 61 and 62: TABLE 1 EFFECT OF LC-FINING~"' TEMP
Page 63 and 64: Figure 1. SCHEMATIC OF LCI CO-PROCE
Page 65 and 66: SIMULATION OF A COAL/PETROLEuII RES
Page 67 and 68: 20 pseudocomponents was developed t
Page 69 and 70: ottoms is less sensitive to the num
Page 71 and 72: Low Pressure Separator A temperatur
Page 73 and 74: 7. Gallier, P.W., Boston, J.F., Wu,
Page 75 and 76: I I I I I I I I I 100- --- Experime
Page 77 and 78: Coprocessing Schemes The coprocessi
Page 79 and 80: processing 25,000 and 150,000 bbl/d
Page 81 and 82: FIGURE 1 I DISTRIBUTION OF REFINERI
Page 83 and 84: Table 1. Samples Analyzed PNLNumber
Page 85 and 86: the coal itself. The chemical compo
Page 87 and 88: - - ITSL PAH Fraction PAH Fraction
Page 89 and 90: PROCESS DEVELOPMENT STUDIES OF TWO-
Page 91 and 92: SUMMARY e The major effect of close
Page 93 and 94: omw '??h 4NO WNID ?N? 000 wmm c9'1'
Page 95 and 96: tl f 246
Page 97 and 98: 248
Page 99 and 100: qkCqQ r! o! 0 0 0 0 0 0 0 I-UH ')I
Page 101 and 102: Materials The catalyst was shell 32
Page 103 and 104: CONCLUSIONS Separation of a light h
Page 105 and 106:
Table 3. Results of activity testin
Page 107 and 108:
feed coal and plant configuration a
Page 109 and 110:
P1 #2 #3 114 115 #6 ITSL subbitumin
Page 111 and 112:
temperature, time and solvent power
Page 113 and 114:
TABLE 1 EXPERIMENTAL CONDITIONS AND
Page 115 and 116:
la Figure 1. lH-NMR spectra of samp
Page 117 and 118:
PERFORMANCE OF THE LOW TEMPERATURE
Page 119 and 120:
BENCH UNIT DESCRIPTION Process deve
Page 121 and 122:
Recycle Residuum Hydrogenati On Res
Page 123 and 124:
FIRST STAGE HRI'S CATALYTIC TWO STA
Page 125 and 126:
FIRST-STAQ COAL CONVERSION (W I IIA
Page 127 and 128:
REACTOR SOLIOS HTOROGEN/CARBON ATOl
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TRANSPORTATION FUELS FROM TWO-STAGE
Page 131 and 132:
Process Identification LV% Of AS- R
Page 133 and 134:
Table I11 HYDROTREATING TESTS WITH
Page 135 and 136:
Table IV HYDROTREATING TO 0.2 PPM N
Page 137 and 138:
Table VI EFFECT OF BOILING RANGE ON
Page 139 and 140:
(4) In all cases studied, the jet f
Page 141 and 142:
292
Page 143 and 144:
INTEGRATED TWO-STAGE LIQUEFACTION:
Page 145 and 146:
are over-riding features in its fav
Page 147 and 148:
Complementary fundamental studies o
Page 149 and 150:
Comparative Economics of Two-Stage
Page 151 and 152:
The variation in hydrotreating cost
Page 153 and 154:
FIGURE 1: COMPARISONS OF ILLINOIS N
Page 155 and 156:
Process TABLE 1: TWO-STAGE PROCESSE
Page 157 and 158:
Abstract Temperature-Staged Catalyt
Page 159 and 160:
Results and Discussion Reactions in
Page 161 and 162:
2. 3. 4. 5. 6. Derbyshire, F. J. an
Page 163 and 164:
I LL a rJJW ., .. ;> 0 i s W 8 a 31
Page 165 and 166:
Materials Feeds to the WGS-solvent
Page 167 and 168:
products. Thus, coupling the WGS an
Page 169 and 170:
5. R. J. Xottenstette, Sandia Natio
Page 171 and 172:
ENHANCED COAL LIQUEFACTION WITH STE
Page 173 and 174:
change in weight being compared to
Page 175 and 176:
I I aromatic ring. The group of sig
Page 177 and 178:
T,\llI.l< I ASAI,YSIS OP \\YOl)Al\:
Page 179 and 180:
00 3000 2000 le00 1600 1400 1200 IO
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THE EFFECT OF REACTION CONDITIONS O
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and may ultiontely form methyl-subs
Page 185 and 186:
! 5. Narain, N.K., Utz, B.R., Appel
Page 187:
4 (u I t + 9 (u I 337 - Q 0
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