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 ...
Run No. (BSCL-) TABLE 2 EFFECT OF SOLVENT OUALITY AN0 SOLVENT/COAL RATIO ON CLOSE-COUPLE0 CO-PROCESSING PERFORMANCE I. Test Conditions Solvent/Coal Ut. Ratio Coal/Resid Ut. Ratio Coal Slurry Concentration, Ut.% 524OC- Solvent Comoosition. Ut.% ITSL* Petroleum Gas Oil** SCT Tempejdture, OC (OF) LC-Fining Temperature, OC (OF) Coal Space Velocity to SCT, Kg/Hr/M3 11. Test Results SUMMARY OF TEST CONDITIONS AND RESULTS Coah Conversion, Wt.% MAF 524 Ct (975Ft) Conversion, Wh.% Net Distillate Yield, Kg 524 C-/lo0 Kg 524OCt Desul furization, % Denitrogenation, % Resid Demetallization, % Preasphaltenes Concentration, % * ** 1.5 0.67 25.0 - 9 - 21 - 20 100 0 449 (840) 432(810) 3400 96.0 75.8 58.1 82.5 71.7 76.0 1.7 1.0 0.50 25.0 100 0 449(840) 432(810) 3400 93.4 66.2 51.0 75.0 65.0 69.0 2.2 1.5 0.67 25.0 40 60 449(840) 432(810) 3400 94.2 64.2 46.0 77.2 67.1 71.0 2.0 524OC- gas oil characteristic of a coal-derived recycle solvent produced in LCI's ITSL PDU during Wyodak coal operations. 524OC- gas oil cQgracteristic of a petroleum-derived recycle solvent produced during LC-Fining of virgin Athabasca bitumen. 1. Feedstocks: Pittsburgh seam coal ; prehydrotreated 524OCt Athabasca resjd 2. SCT Conditims: 137 atm; 360 M H2/M3 feed 3. LC-Fininq" Conditions: Shell 324M catalyst; 137 atm; 0.4R Hr-'; 530 M3 H2/M3 feed 213
Figure 1. SCHEMATIC OF LCI CO-PROCESSING CONCEPT WITH HYDROCRACKED PETROLEUM RESIDUA 0-:+ COAL - SCT c 1st-Stage REACTION I SYSTEM LC- F I NER * V/L SEPARATOR - 0 Hydrotreated Vac Resid - \ 2nd-Stage Hydrocracked LC-FINER OISTILLA- DDistil 1 ates 1-D Drag Stream To Gasifier - - Figure 2. SCHEMATIC OF LCI CO-PROCESSING CONCEPT WITH VIRGIN PETROLEUM RESIDUA COAL SYSTEM I 'Virgin Vac Resid - - Recycl e Hydrocracked Resid 2nd-Stage LC-FINER p DISTILLA- TION 214 r # SEPARATOR - Hydrocracked I Distillate Drag Stream To Gasifier 1
- 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 and 60: system, which could be operated wit
- Page 61: TABLE 1 EFFECT OF LC-FINING~"' TEMP
- 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
- Page 111 and 112: temperature, time and solvent power
Figure 1. SCHEMATIC OF LCI CO-PROCESSING CONCEPT WITH HYDROCRACKED PETROLEUM RESIDUA<br />
0-:+<br />
COAL<br />
-<br />
SCT<br />
c 1st-Stage<br />
REACTION I<br />
SYSTEM LC- F I NER<br />
* V/L<br />
SEPARATOR -<br />
0<br />
Hydrotre<strong>at</strong>ed Vac Resid<br />
- \<br />
2nd-Stage<br />
Hydrocracked<br />
LC-FINER OISTILLA- DDistil 1 <strong>at</strong>es<br />
1-D Drag Stream To Gasifier<br />
- -<br />
Figure 2. SCHEMATIC OF LCI CO-PROCESSING CONCEPT WITH VIRGIN PETROLEUM RESIDUA<br />
COAL<br />
SYSTEM<br />
I<br />
'Virgin Vac Resid<br />
-<br />
-<br />
Recycl e Hydrocracked Resid<br />
2nd-Stage<br />
LC-FINER p DISTILLA-<br />
TION<br />
214<br />
r #<br />
SEPARATOR<br />
- Hydrocracked I<br />
Distill<strong>at</strong>e<br />
Drag Stream To<br />
Gasifier<br />
1
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