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

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i Table 1. Compositions of the V-178 stream and the four chemical classes in weight percents. --- C H N o H / C V-178 87.69 10.05 0.23 1.08 1.38 wt a of V-178 Aliphatic hydrocarbons 46 87.27 12.36 cO.10 0.10 1.70 Neutral polycyclic 35 90.15 8.70 0.10 0.17 1.16 aromatic compounds (PAC) Nitrogen polycyclic aromatic compounds (N-PAC) 5 83.60 7.93 3.61 2.81 1.14 Hydroxy polycyclic 9 78.18 8.25 1.13 9.44 1.27 aromatic compounds (HPEH) Table 2. Analyses of aged catalysts from microreactor runs (reported as weight percents). Catalyst -- C N V-178 run 3.87 0.3 Aliphatic hydrocarbon run 2.36 0.1 PAC run 2.71 0.1 N-PAC run 4.53 0.6 HPAH run 5.02 0.5 255
Table 3. Results of activity testing experiments (for fresh catalyst F = 1.00, a = 0.0) F a F* Reactor Feed measured measured - V-178 0.44 0.72 0.52 Aliphatic 0.72 0.39 0.78 hydrocarbons PAC m-PAC 0.59 0.58 0.64 0.05 0.90 0.13 HPAH 0.19 0.92 0.26 * Corrected for changes in effective diffusivity. F 0.2 O - t 01 0 hydrocarbons a V-l78\ a, N-PAC 0.2 0.4 0.8 0.8 1 .o Figure 1. F vs a plot for V-178 and the four chemical classes. 256 I
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ABSTRACT LIQUEFACTION CO-PROCESSING
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eaction temperature, 1000-1500 psig
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6. 7. 8. 9. 10. 11. 12. 13. 14. 15
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I 0" 100- I I I WyO-3 P 3: 1500 psi
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11.3 A-6 yJ 600 OF, 1500 psig CO, 3
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Experimental UDqradinq and Cooroces
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catalytic to the thermal hydrogenat
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the reaction with oil production re
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TET did not promote the production
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MICROAUTOCLAVE DESCRIPTION AND PROC
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FEEDSTOCK PROPERTIES Some propertie
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CONCLUSIONS HRI's microautoclave ha
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176
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100. 2 8%. M = ?8. 38. .... . . . .
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CATALYTIC CO-PROCESSINS OF OHIO NO.
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CATALYST COMPARISON STUDY The premi
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fractions and a decrease of heavier
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TABLE 2 Coal Analyses I1 1 i noi s
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Temperature WHSV, G/hr/cc TABLE 6 C
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z FIGURE 3 COAL REACTIVITY SCREENIN
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COPROCESSING USING HzS AS A PROMOTE
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- 3 - that product yields depend on
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- 5 - occurs in the yields of aspha
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Table 1 Analysis of Feedstocks Fore
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THO-STAGE COPROCESSING OF SUBBITUMI
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esult in retrogressive reactions ta
Page 53 and 54: 8. 6. Ignasiak, L. Lewkowicz, G. Ko
Page 55 and 56: Table 4 OVERALL MASS BALANCE FOR TH
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: CONCLUSIONS Separation of a light h
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
Page 129 and 130: 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
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Process TABLE 1: TWO-STAGE PROCESSE
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Abstract Temperature-Staged Catalyt
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Results and Discussion Reactions in
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2. 3. 4. 5. 6. Derbyshire, F. J. an
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I LL a rJJW ., .. ;> 0 i s W 8 a 31
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Materials Feeds to the WGS-solvent
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products. Thus, coupling the WGS an
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5. R. J. Xottenstette, Sandia Natio
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ENHANCED COAL LIQUEFACTION WITH STE
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change in weight being compared to
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I I aromatic ring. The group of sig
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T,\llI.l< I ASAI,YSIS OP \\YOl)Al\:
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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
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! 5. Narain, N.K., Utz, B.R., Appel
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4 (u I t + 9 (u I 337 - Q 0
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