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

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00 3000 2000 le00 1600 1400 1200 IO00 800 SO0 WAVENUMBER CM" rlgure 3: Infrared Spect- <strong>of</strong> Stem Eltract <strong>of</strong> Run 27 From. 10.00 100.50 PPM Imte9r.I. 100.00 329 cn, vw &rYity k Aromolic
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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
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8. 6. Ignasiak, L. Lewkowicz, G. Ko
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Table 4 OVERALL MASS BALANCE FOR TH
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BACKGROUND COAL LIQUEFACTION/RESID
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system, which could be operated wit
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TABLE 1 EFFECT OF LC-FINING~"' TEMP
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Figure 1. SCHEMATIC OF LCI CO-PROCE
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SIMULATION OF A COAL/PETROLEuII RES
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20 pseudocomponents was developed t
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ottoms is less sensitive to the num
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Low Pressure Separator A temperatur
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7. Gallier, P.W., Boston, J.F., Wu,
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I I I I I I I I I 100- --- Experime
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Coprocessing Schemes The coprocessi
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processing 25,000 and 150,000 bbl/d
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FIGURE 1 I DISTRIBUTION OF REFINERI
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Table 1. Samples Analyzed PNLNumber
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the coal itself. The chemical compo
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- - ITSL PAH Fraction PAH Fraction
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PROCESS DEVELOPMENT STUDIES OF TWO-
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SUMMARY e The major effect of close
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omw '??h 4NO WNID ?N? 000 wmm c9'1'
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tl f 246
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248
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qkCqQ r! o! 0 0 0 0 0 0 0 I-UH ')I
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Materials The catalyst was shell 32
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CONCLUSIONS Separation of a light h
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Table 3. Results of activity testin
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feed coal and plant configuration a
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P1 #2 #3 114 115 #6 ITSL subbitumin
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temperature, time and solvent power
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TABLE 1 EXPERIMENTAL CONDITIONS AND
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la Figure 1. lH-NMR spectra of samp
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PERFORMANCE OF THE LOW TEMPERATURE
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BENCH UNIT DESCRIPTION Process deve
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Recycle Residuum Hydrogenati On Res
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FIRST STAGE HRI'S CATALYTIC TWO STA
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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
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: T,\llI.l< I ASAI,YSIS OP \\YOl)Al\:
Page 181 and 182: THE EFFECT OF REACTION CONDITIONS O
Page 183 and 184: 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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