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

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I Table I shows properties of pairs of H-Coal and ITSL syncrudes derived from Illinois coal. Table I1 shows properties of pairs of H-Coal, CTSL, and ITSL syncrudes derived from wyodak coal. In each case, the syncrude identified as "A" had a higher EP than that i identified as "B". The A syncrudes were blended from components supplied HRI and Lummus in ratios recommended by DOE to represent, as nearly as possible, "net whole-liquid prOdUCtS" from these processes. [Note: the heavy fractions of Illinois ITSL A and Wyodak CTSL A, 1 as-received, contained large quantities of hot-heptane insolubles and i Process Sample Identification LV% of As-Received Oil Inspections Gravity, "API Sulfur, ppm Nitrogen, ppm Oxygen, ppm Hydrogen, Wt % Carbon, Wt % Hot-Heptane Insolubles, ppm TBP Distillation, OF (ASTM D2887) St/5 10/30 50 70/90 95/99 Boiling Range, LV% St-40O0F 400-700'F 700O~+ Table I SYNCRUDES FROM ILLINOIS NO. 6 COAL A B 100 87 A B 95 69 25.8 28.1 13.6 17.6 2000 1400 865 700 4600 3300 1050 730 18000 19600 2600 1800 11.29 11.44 10.19 10.68 86.25 86.13 89.35 88.99 3500 54 375 290 56/177 56/170 97/275 97/214 213/333 200/310 375/532 314/471 404 380 602 56 0 476/588 440/508 665/745 609/676 654/765 538/589 793/859 703/763 49 57 48 43 3 0 281 12 18 69 76 19 6
Process Identification LV% Of AS- Received Oil Inspections Gravity , OAPI Sulfur, ppm Nitrogen, ppm Oxygen, ppm Hydrogen, Wt % Carbon, Wt % Hot-Heptane Insol., ppm TBP Dist., OF (ASTM D2887) St/5 10/3 0 50 70/90 95/99 Boiling Range, LV% St-40ODF 400-700°F 700°F+ Table I1 SYNCRUDES FROM WYODAK COAL 100 96 93 62 loo* 52* 35.1 410 1700 8500 35.1 250 1500 6700 29.0 140 1230 1500 36.1 88 935 1400 8.8 580 1670 4600 15.8 305 1020 3900 12.74 86.20 12.97 86.20 12.14 87.35 12.65 87.11 9.35 89.76 10.48 89.00 680
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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
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
Page 129: TRANSPORTATION FUELS FROM TWO-STAGE
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
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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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