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 ...
F. Freidrich and B. Strobel, "Liquefaction of Coal in the Federal Republic of Germany," International Seminar on the Replacement of Fuels, University of Liege, May 25-27, 1981. "Status of Synfuels Development in Japan." NEDO, Synfuels, 3rd Worldwide Symposium. Washington, DC, November 1-3, 1983. A.'S. Paranjape and D. E. Rhodes, "Use of Iron Oxide and Hydrogen Sulfide to Improve Integrated Two-Stage Liquefaction." Proceedinqs of DOE Direct Coal Liquefaction Contractors' Review Meeting, October 17-18, 1984. J. G. Gatsis et al., "Coal Liquefaction Co-Processing," Proceedings of DOE Direct Coal Liquefaction Contractors' Review Meeting, November 19-21, 1985. TABLE 1 U.S. Alaskan Mid- North Continent Kuwait Slope Lloydminster Hondo Maya Lloydminster Resid Name (Rl) (R2) (R3) (R4) (R5) (R6) (R8) Total Sample API Gravity Specific Gravity 0- 1160, "C IBP, VO~-% 5 10 20 30 EP Overhead, vol-% Analysis, wt-% Carbon Hydrogen Oxygen Sulfur Nitrogen Carbon Residue Petroleum Ash C7 Insolubles Nickel, ppm Vanadium, ppm Iron, ppm Molecular Weight Furol Visc., sec (121°C) pour Point. "C Salt, lb/1000 bbls 12.70 0.9813 473.0 510.0 525.0 546.0 ,568.0 568.0 30.0 87.30 10.25 0.30 1.0 0.45 16.50 0.030 8.29 35.0 113.0 62.0 839.0 755.0 38.00 2.90 7.90 8.90 1.0151 1.0078 472.0 422.0 505.0 494.0 517.0 515.0 542.0 541.0 556.0 550.0 26.0 24.0 84.15 84.10 10.55 10.85 0.35 0.27 4.9 2.3 0.35 0.55 18.00 17.30 0.020 0.020 5.95 4.80 28.0 38.0 100.0 79.0 4.5 2.0 1054.0 810.0 1016.0 ~~ 1295.0 ~~ 38.00 32.00 3.50 1.20 185 3.60 1.0474 406.0 509.0 509.0 6.0 82.70 10.15 0.29 5.6 0.62 22.20 0.090 18.10 122.0 278.0 82.0 1444.0 1921.0 91.00 3.30 3.70 2.80 1.0466 1.0536 478.0 452.0 512.0 515.0 524.0 532.0 - - 524.0 532.0 10.0 10.0 81.20 83.90 10.10 9.15 0.36 0.48 6.6 4.9 1.10 0.71 19.90 26.10 0.110 0.126 17.80 22.40 157.0 116.0 435.0 595.0 42.0 29.0 1125.0 1015.0 1126.0 2217.0 79.00 91.00 4.00 20.70 6.50 1.0254 369 2 0 432.0 463.0 505.0 - 523.0 26.5 83.70 10.00 - 5.1 0.48 17.30 0.051 13.91 83.0 165.0 3.6 255.0 266.1 120.0 5.2
TABLE 2 Coal Analyses I1 1 i noi s Kentucky Indiana Wyodak Wyodak Illinois No. 6 No. 9 No. V (As-Received) (Dried) No. 6 Coal Name 0 (C2) (C3) (C4.1) IC4.2) (C1.2) Ultimate Analysis, wt-% Ash 9.65 Carbon 68.60 Hydrogen 4.51 Nitrogen 1.39 Sulfur 3.04 Oxygen* 9.66 Proximate Analysis, wt-% Moisture 3.15 Ash 9.65 Volatile Matter 39.95 Fixed Carbon 47.25 *Difference Operating Conditions Catalyst Type Concentration 8.68 8.12 10.30 12.00 10.56 71.95 69.70 54.70 63.01 68.77 4.78 5.40 3.83 4.50 4.84 1.54 1.42 0.69 0.90 1.37 2.97 4.28 0.99 1.08 3.34 8.53 9.37 14.79 16.73 7.03 1.55 1.71 14.70 1.78 4.09 8.68 8.12 10.30 12.00 10.56 42.35 48.25 37.00 42.60 39.90 47.42 41.92 38.00 43.62 45.45 TABLE 3 Catalyst Comparison Study None Fe 0 UOP Catalyst 0 2 dase Base Performance Conversions, wt-% Coal 66.6 80.5 92.2 Heptane insolubles 21.3 63.9 81.3 Non-di st i 1 1 ables (510"C+) 69.3 73.6 72.1 Hydrogen Consumption, wt-% 1.84 1.68 2.66 186 , ' I
- Page 1 and 2: ABSTRACT LIQUEFACTION CO-PROCESSING
- 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: fractions and a decrease of heavier
- 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 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
F. Freidrich and B. Strobel, "<strong>Liquefaction</strong> <strong>of</strong> Coal in the Federal Republic <strong>of</strong><br />
Germany," Intern<strong>at</strong>ional Seminar on the Replacement <strong>of</strong> Fuels, University <strong>of</strong><br />
Liege, May 25-27, 1981.<br />
"St<strong>at</strong>us <strong>of</strong> Synfuels Development in Japan." NEDO, Synfuels, 3rd Worldwide<br />
Symposium. Washington, DC, November 1-3, 1983.<br />
A.'S. Paranjape and D. E. Rhodes, "Use <strong>of</strong> Iron Oxide and Hydrogen Sulfide to<br />
Improve Integr<strong>at</strong>ed Two-Stage <strong>Liquefaction</strong>." Proceedinqs <strong>of</strong> DOE Direct Coal<br />
<strong>Liquefaction</strong> Contractors' Review Meeting, October 17-18, 1984.<br />
J. G. G<strong>at</strong>sis et al., "Coal <strong>Liquefaction</strong> Co-Processing," Proceedings <strong>of</strong> DOE<br />
Direct Coal <strong>Liquefaction</strong> Contractors' Review Meeting, November 19-21, 1985.<br />
TABLE 1<br />
U.S. Alaskan<br />
Mid- North<br />
Continent Kuwait Slope Lloydminster Hondo Maya Lloydminster<br />
Resid Name (Rl) (R2) (R3) (R4) (R5) (R6) (R8)<br />
Total Sample<br />
API Gravity<br />
Specific Gravity<br />
0- 1160, "C<br />
IBP, VO~-%<br />
5<br />
10<br />
20<br />
30<br />
EP<br />
Overhead, vol-%<br />
Analysis, wt-%<br />
Carbon<br />
Hydrogen<br />
Oxygen<br />
Sulfur<br />
Nitrogen<br />
Carbon Residue<br />
Petroleum Ash<br />
C7 Insolubles<br />
Nickel, ppm<br />
Vanadium, ppm<br />
Iron, ppm<br />
Molecular Weight<br />
Furol Visc.,<br />
sec (121°C)<br />
pour Point. "C<br />
Salt, lb/1000 bbls<br />
12.70<br />
0.9813<br />
473.0<br />
510.0<br />
525.0<br />
546.0<br />
,568.0<br />
568.0<br />
30.0<br />
87.30<br />
10.25<br />
0.30<br />
1.0<br />
0.45<br />
16.50<br />
0.030<br />
8.29<br />
35.0<br />
113.0<br />
62.0<br />
839.0<br />
755.0<br />
38.00<br />
2.90<br />
7.90 8.90<br />
1.0151 1.0078<br />
472.0 422.0<br />
505.0 494.0<br />
517.0 515.0<br />
542.0 541.0<br />
556.0 550.0<br />
26.0 24.0<br />
84.15 84.10<br />
10.55 10.85<br />
0.35 0.27<br />
4.9 2.3<br />
0.35 0.55<br />
18.00 17.30<br />
0.020 0.020<br />
5.95 4.80<br />
28.0 38.0<br />
100.0 79.0<br />
4.5 2.0<br />
1054.0 810.0<br />
1016.0 ~~ 1295.0<br />
~~<br />
38.00 32.00<br />
3.50 1.20<br />
185<br />
3.60<br />
1.0474<br />
406.0<br />
509.0<br />
509.0<br />
6.0<br />
82.70<br />
10.15<br />
0.29<br />
5.6<br />
0.62<br />
22.20<br />
0.090<br />
18.10<br />
122.0<br />
278.0<br />
82.0<br />
1444.0<br />
1921.0<br />
91.00<br />
3.30<br />
3.70 2.80<br />
1.0466 1.0536<br />
478.0 452.0<br />
512.0 515.0<br />
524.0 532.0<br />
-<br />
-<br />
524.0 532.0<br />
10.0 10.0<br />
81.20 83.90<br />
10.10 9.15<br />
0.36 0.48<br />
6.6 4.9<br />
1.10 0.71<br />
19.90 26.10<br />
0.110 0.126<br />
17.80 22.40<br />
157.0 116.0<br />
435.0 595.0<br />
42.0 29.0<br />
1125.0 1015.0<br />
1126.0 2217.0<br />
79.00 91.00<br />
4.00 20.70<br />
6.50<br />
1.0254<br />
369 2 0<br />
432.0<br />
463.0<br />
505.0<br />
-<br />
523.0<br />
26.5<br />
83.70<br />
10.00<br />
-<br />
5.1<br />
0.48<br />
17.30<br />
0.051<br />
13.91<br />
83.0<br />
165.0<br />
3.6<br />
255.0<br />
266.1<br />
120.0<br />
5.2
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