Liquefaction co-processing of coal shale oil at - Argonne National ...
Liquefaction co-processing of coal shale oil at - Argonne National ... Liquefaction co-processing of coal shale oil at - Argonne National ...
2nd Stage Catalyst Table 2 THE EFFECT OF RESIDENCE TIME ON CONVERSION FOR THE SOLUBILIZATION OF HIGHVALE COAL IN BITUMEN WITH CO/STEAM OR H2 AT 390°C Time (min') Coal Conversion (on daf coal ) 0 15 30 60 CO/Steam Table 3 H7 58 10 65 34 85 65 86 68 PRODUCT YIELDS AND COAL CONVERSIONS FROM THE TWO-STAGE CO-PROCESSING OF BITUMEN AND HIGHVALE COAL K2Mo04 - CH3SSCH3 1st Stage Reducing Gas H2 CO/H20 CO/H20-K2C03 - Yielda Hydrocarbon Gas (C,-C5) 7.2 (20.8) 5.2(+0.2) 5.3c Distillable Oil (IBP-525"C) 62.3(+0.9) 57.7 (+0.8 ) 66.2 (20.7 ) Soluble Extract 18.0 (20. 2 ) 19.3 (20. 9) 18.7 (+O .3 ) Material Balance 94.1 (23.1 ) 90.4 (20.2) 96.1' Coal Conversion (X daf coal) 90 (21 ) 91 (21) 98 (20 1 a) Yields are presented as % daf organic feed (bitumen + coal). b) All data are quoted as the average values of two duplicate experiments. Figures in brackets show the spreads for the two experiments. c) Single data point. 205 ~
Table 4 OVERALL MASS BALANCE FOR THE OPTIMIZED ARC TWO-STAGE CO/H2O-K2CO3 - H2 COALDITUMEN PROCESS Bitumen Coal - 2.5/1 Basis 100 kg - feed (daf) Component Input output c5-2000c 3.1 11.0 200-375OC 15.0 40.1 375-525OC 16.1 19.0(2) + 525OC 37.2 12.3 Coal 28.6 Ash 1.5(1) Unconverted Coal Residue Water co c02 10.26 0.6 26.1 H2S NH4 '1-'4 Catalyst 0.34 2.7 1.84 44.7 1.5 0.46 5.2 138.8 138.8 (1) Ash reduced to 5% by deashing. (2) Estimate of yield after optimization. 206
- Page 3 and 4: eaction temperature, 1000-1500 psig
- Page 5 and 6: 6. 7. 8. 9. 10. 11. 12. 13. 14. 15
- Page 7 and 8: 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: 8. 6. Ignasiak, L. Lewkowicz, G. Ko
- 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'
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- 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
Table 4<br />
OVERALL MASS BALANCE FOR THE OPTIMIZED ARC TWO-STAGE<br />
CO/H2O-K2CO3 - H2 COALDITUMEN PROCESS<br />
Bitumen Coal - 2.5/1<br />
Basis 100 kg - feed (daf)<br />
Component Input output<br />
c5-2000c 3.1 11.0<br />
200-375OC 15.0 40.1<br />
375-525OC 16.1 19.0(2)<br />
+ 525OC 37.2 12.3<br />
Coal 28.6<br />
Ash 1.5(1)<br />
Un<strong>co</strong>nverted Coal<br />
Residue<br />
W<strong>at</strong>er<br />
<strong>co</strong><br />
c02<br />
10.26<br />
0.6<br />
26.1<br />
H2S<br />
NH4<br />
'1-'4<br />
C<strong>at</strong>alyst 0.34<br />
2.7<br />
1.84<br />
44.7<br />
1.5<br />
0.46<br />
5.2<br />
138.8 138.8<br />
(1) Ash reduced to 5% by deashing.<br />
(2) Estim<strong>at</strong>e <strong>of</strong> yield after optimiz<strong>at</strong>ion.<br />
206
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