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

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i 0 However, the reduction in the said solvent/coal ratio did adversely affect syncrude characteristics and net distillate yields. It should be kept in mind that the high LC-FiningSm severity used in this particular test campaign was aimed at assessing per pass performance (e.g., conversion, desulfurization, etc.) 1 imits during co-processing. In the conceptual commercial concept Qgpicted in Figures 1 and 2, it is anticipated that the first-stage LC-Finer located immediately downstream of the SCT reactor will be operated under optimal conditions for generating recycle gas oil solvents having higb hydrogen donor capacity. At these severities, it is anticipated that the 524 Ct conversions would be lower than the values shown in Table 4. The additional required feed conversions, i .e., overall swversions in exce~ss of 80 percent, could be achieved in a second-stage LC-Finer operated at higher, more conventional petroleum hydrocracking severities. In test BSCL-20, a 524OC- recycle solvent during co-processing was simulated by blending a neat coal-derived hydrogenated solvent with a neat petroleum-derived hydrogenated solvent in the same ratio as that of the coal and petroleum resid fed in that run. By comparing these results to those of test BSCL-9 made only with coal-derived 524OC- solvent, it is possible to estimate the relative solvent quality index (SQI) of the petroleum-derived gas oil solvent in comparison to that of the coal-derived gas oil solvent. The SQI of the particular petroleum gas oil utilized in this test has been estimated to be about 60 percent of that of the coal -derived solvent based on relative solvent performance as measured by observed net distillate yields. Optimization of the petroleum resid hydrocracking step in which the simulated gas oil solvent was generated has the potential to increase the latter's SQI value closer to that of the coal-based solvent. FUTURE WORK The continuous bench-scale unit will be operated in the recycle mode to demonstrate the effect of solvent maintenance on co-processing performance as a function of feedstock types (Pittsburgh seam and Wyodak coals; Arab Heavy and Athabasca residua); coal/resid ratios; solvent/coal ratio and catalyst age. These data will serve as the basis for formulating a conceptual commercial plant design. Towards the end of the Task 4 experimental program, a catalyst life test at preferred co-processing conditions will be made to demonstrate the technical feasibility of the base case design. ACKNOWLEDGEMENTS The LCI co-processing program is being jointly funded by the Department of Energy under Contract No. DE-AC22-84PC70042. We would like to acknowledge the technical support of Ness Mazzocco, DOE Project Manager; Dr. Eneo Moroni, DOE Program Manager; and Dr. Harvey Schindler, Science Applications International Corporation. 211
TABLE 1 EFFECT OF LC-FINING~"' TEMPERATURE ON CLOSE-COUPLED CO-PROCESSING PERFORMANCE RunNo. (8SCL-) 1. Test Conditions SCT Tempeg,ture, OC (OF) LC-Fining Temperature, OC (OF) Coal Space Velocity to SCT, Kg/Hr/M3 Solvent/Coal Ut. Ratio Resid/Coal Wt. Ratio 11. Test Results SUMMARY OF TEST CONDITIONS AND RESULTS Coal Conversion. Wt.% MAF 524OCt (975Ft) Conversion, W8.X Net Distillate Yield, Kg 524 C-/lo0 Kg 524OC+ Desulfurization, % Denitrogenation, % Resid Demetallization, % Preasphaltenes Concentration, % - 9 449 (840) 432(810) 3400 1.5 1.5 96.0 75.8 58.1 82.5 71.7 76.0 1.7 - 10 449(840) 416 (780) 3400 1.5 1.5 93.8 67.3 55.9 75.7 55.0 72.0 1.5 - 11 449(840) 404(760) 3400 1.5 1.5 93.7 58.4 48.3 66.0 43.0 59.0 1.9 (1) Feedstocks: Pittsburgh seam coal ; Prehydrotreated 524OC+ Athabasca resid (2) Solvent: 524OC- gas oil characteristic of a coal-derived recycle solvent produced in LCI's ITSL PDU during Wyodak coal operations (3) SCT Condition: 137 atm; 360 M3 H2/M3 feed (4) LC-FininqSm Conditions: Shell 324M catalyst; 137 atm; 0.4R hr-'; 530 M3 H,/M3 feed 212
Page 1 and 2:
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
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 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: system, which could be operated wit
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
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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
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REACTOR SOLIOS HTOROGEN/CARBON ATOl
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TRANSPORTATION FUELS FROM TWO-STAGE
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Process Identification LV% Of AS- R
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Table I11 HYDROTREATING TESTS WITH
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Table IV HYDROTREATING TO 0.2 PPM N
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Table VI EFFECT OF BOILING RANGE ON
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(4) In all cases studied, the jet f
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292
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INTEGRATED TWO-STAGE LIQUEFACTION:
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are over-riding features in its fav
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Complementary fundamental studies o
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Comparative Economics of Two-Stage
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The variation in hydrotreating cost
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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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