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 ...
Configuration Run No. Catalyst Type Unit Contributions(3) Thermal Stage Catalytic Stage Table 3 UNIT CONTRIBUTIONS TO DISTILLATE PRODUCTION ITSL 244 Shell 324 55 45 (1) Without interstage vapor separation. (2) With interstage vapor separation. (3) W t % of total distillate production. Relative Capital Cost Relative Operating Cost Re1 ative Production Rate(2) Relative Required Product Selling Price(3) Thermal Efficiency ($1 Table 4 CC-ITSL(~) 2508 Shell 324 0 100 ECONOMIC SCREENING STUDY(^) (10,000 TPD PLANT) CC-ITSL (2) 250D Amocat 1C 25 75 ITSL (e SE \ cc- TSL 1 .oo 1 .oo 1 .oo 1.00 (1) Performed by Lumnus Crest, Inc. under EPRI RP832-11. (2) Based on barrels of crude oil equivalent with consideration for quality of di sti 11 ate products. (3) First year. 245 68.1 1.04 1.01 1.10 0.93 69.6
tl f 246
- 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 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: omw '??h 4NO WNID ?N? 000 wmm c9'1'
- 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 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
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- Page 143 and 144: INTEGRATED TWO-STAGE LIQUEFACTION:
Configur<strong>at</strong>ion<br />
Run No.<br />
C<strong>at</strong>alyst Type<br />
Unit Contributions(3)<br />
Thermal Stage<br />
C<strong>at</strong>alytic Stage<br />
Table 3<br />
UNIT CONTRIBUTIONS TO DISTILLATE PRODUCTION<br />
ITSL<br />
244<br />
Shell 324<br />
55<br />
45<br />
(1) Without interstage vapor separ<strong>at</strong>ion.<br />
(2) With interstage vapor separ<strong>at</strong>ion.<br />
(3) W t % <strong>of</strong> total distill<strong>at</strong>e production.<br />
Rel<strong>at</strong>ive Capital Cost<br />
Rel<strong>at</strong>ive Oper<strong>at</strong>ing Cost<br />
Re1 <strong>at</strong>ive Production R<strong>at</strong>e(2)<br />
Rel<strong>at</strong>ive Required Product Selling Price(3)<br />
Thermal Efficiency ($1<br />
Table 4<br />
CC-ITSL(~)<br />
2508<br />
Shell 324<br />
0<br />
100<br />
ECONOMIC SCREENING STUDY(^)<br />
(10,000 TPD PLANT)<br />
CC-ITSL (2)<br />
250D<br />
Amoc<strong>at</strong> 1C<br />
25<br />
75<br />
ITSL (e SE \ cc- TSL<br />
1 .oo<br />
1 .oo<br />
1 .oo<br />
1.00<br />
(1) Performed by Lumnus Crest, Inc. under EPRI RP832-11.<br />
(2) Based on barrels <strong>of</strong> crude <strong>oil</strong> equivalent with <strong>co</strong>nsider<strong>at</strong>ion for quality <strong>of</strong><br />
di sti 11 <strong>at</strong>e products.<br />
(3) First year.<br />
245<br />
68.1<br />
1.04<br />
1.01<br />
1.10<br />
0.93<br />
69.6
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