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

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conditions generally employed. They cannot survive the severe processing conditions. Small amounts of dihydroxyl aromatics have been obtained in Bash or fsst pyrolysis conditions. The very rapid heating allows the dihydroxyl aromatics to escape the coal matrix before they can undergo retrogrrssive reactions. CONCLUSIONS The steam pretreatmentextraction process produces enhanced extractan yields. The extract has a high H/C ratio due to the presence of long chain polymethylene compounds which may or may not be attached to aromatic rins. The extract contains significant amounts of oxygenated compounds, some of which are present as dihydroxyl aromatics. A highly condensed residue (low H/C ratio) is obtained which can be attractive a8 a solid fuel lor combustion. ACKNOWLEDGEMENTS This work has been supported by the Electric Power Research Institute through research project 2147-9. Shu-Yen Huang performed the IR and NMR analysis and prepared the FlMS samples. We thank Linda F. Atberton for helpful discussions. LITERATURE CITED 1. Atherton, L.F., Kulik, C.J. "Advanced Coal Liquefaction" paper presented at AIChE Annual Meet ing, Los Angeles, CA, November 1982. 2. Coal Technology Report Vol. 2, No. 11, p.1, May 28, 1984. 3. Kushaw, J.R.; Bagnell, L.J. ACS Div. Fuel Chem. 1985,30(3), 101. 4. Kenhaw, J.R.; Jezko, J.; Separation Science and Technolou 1982, 17(1), 151. 5. Kershaw J.R.; Fuel Processing Technology 1982, 5, 241. 6. Jezko, J.; Gray, D.; Kershaw, J.R.; Fuel Proces. Tech. 1982, 5, 229. 326 !
T,\llI.l< I ASAI,YSIS OP \\YOl)Al\: (;O.\l, s.wri.i; A 11 c \Vet Wct Vnruum Drird Carhn. 59.51 59.72 58.17 Ilydrqcn 4.70 4.13 4.35 OXYP 17.90 2?.44 18.9-1 Nitrryrn Chlorine 0.70 - 0.76 0.62 Sulfur 1.m 1.55 3.K Ash I3.W 13.47 16.48 TOTAL 90.55 103.07 101.02 BTU/lb 10,814 - 10.I41 An.- .I q L r mu pwfarnwd by I!uUmu Laboratory. Sham. pi. 750 38.5 1500 a0 ?GOO 36.0 32 7 TABLE 4 EIemeabl h dysh d ExCut, Raidn, A ~4 ~(RU n Wt% Extract R d u Fwd C n 51.21 6.77 u.n 60.71 3.69 4.!3 0 N 23.42 4.00 ILIO 1.01 22.44 0.70 S kh 4- 8.04 1.71 1T.U 2.s 13.47 Atomic Ralw II/C 1.28 0.08 0.05 O/C 0.32 0.13 0.28
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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
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
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: I I aromatic ring. The group of sig
Page 179 and 180: 00 3000 2000 le00 1600 1400 1200 IO
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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