liquefaction pathways of bituminous subbituminous coals andtheir
liquefaction pathways of bituminous subbituminous coals andtheir liquefaction pathways of bituminous subbituminous coals andtheir
The vacuumdried coal shows a similar H2consumption value as that of the coal dried in air for 2 h in thermal as well as catalytic runs. But during thermal liquefaction of the raw coal the HFconsumption is higher than that of the vacuum- and air-dried coal for 2 h. In the catalytic liquefaction of the raw coal in presence of solvents the H2ansumption is not much different from that of the vacuum- or air-dried coal for 2 h, but in the solvent-free catalytic run the H2-consumption is remarkably higher. These results may account for the beuer conversions in the case of lilw coal liquefaction compared to that of the vacuum- or airdried coal. Hydrogen-transfer from tetralin (Figure 4) increases (in the thermal liquefactions) with the extent of oxidation of coal. Vacuum-dried and the raw coal show a lower H-transfer compared to that of the airdried coal. In the catalytic runs the H-transfer from teualin is relatively lower than that in the corresponding thermal run and does not make any noticeable difference as the coal is dried at 100 "C in air up to 100 h. When the coal is dried ai 150 'C for 20 h the H-uansfer is slightly higher. The vacuumdried coal shows a lowest value for the H-transfer from d i n in the catalytic run. CONCLUSIONS The airdried coal at 100 OC for up to 20 h gave similar conversions as the vacuum-dried coal in the solvent- free thermal and catalytic liquefactions. In the presence of solveno, better conversions were obtained from the coal dried in air at 100 "C for 2 h compared to the vacuumdried coal. The extensive oxidation of coal decreased the coal conversions in thermal as well as caralytic runs. These resulu suggests that air-drying of coal to some extent may be beneficial for liquefaction. The raw coal gave the best conversions in the solvent-free runs. The improved conversion Seems to be due to the prescnce of water, which enhances the removal ofcarbony1 functionalities during liquefaction making coal network less rehctory for liquefaction. ACKNOWLEDGEMENTS REFERENCES This work was supported by the US. DOE Pittsburgh Energy Technology Center. 1. Athenon. L.F.; Pmc. 1985 Int. Conf. Coal Sci., p.553. 2. Navel, R.; Fuel 1976.55.237. 3. Cronauer. D.C.. Rubeno, R.G.. Silver, R.S., Jenkins, R.G., Davis, A.. and Hoover. D.S.; Fuel, 1984. 63, 77. 4. Vorres, K.S.. Wem. D.L., Malhoua, V., Dang. Y., Joseph, J.T., and Fisher, R.: Fuel. 1992, 71, 1047. 5. Saini, A.K.. Song, C., Schoben. H.H.. and Hatcher, P.G.; ACS Fuel Chem. Div. Prepr. 1992, 37(3). 1235. 6. Petit. J.C.; Fuel, 1991, 70.1053. 596
Table 1. Products dismbutions (dmmf wt %) for the thermal liquefactions of the raw and dried coal at 350 OC with different solvents. Drying Conditions. blv -fra Raw-undricd 7.7 (9.5) Air-dricd.2h.100°C 5.0 (6.3) Airdricd.2Oh.1000C 5.7 (7.3) Air-dricd.IOOh.100"C 8.5 (12.0) Air-dricd.2Oh.l SOT 9.8 (I 3.2) Vac.-dricd.2h.I00"C 3.3 (5.9) bL.alin Raw-undried 5.8 (7.7) Air-dricd.2h.100°C 5.4 (6.3) Air-dried.20h.lOO"C 5.9 8.7) Air-dried, 1 OOh.l OOOC 8.7 (1 1.6) Air-dried.20h.150"C 11.8(16.6) Vac.-dricd.2h.100°C 4.2 (5.4) I-Mcthvln- c e Raw-undried 5.9 (8.4) Air-dricd.2h. 100°C 5.1 (7.6) Airdri~d.20h.100~C 6.2 (7.5) Air-dricd.IOOh.100"C 9.0 (12.7) Drying Conditions. Raw-undricd Air-dricd.2h.100°C Airdri~d.20h.100~C Air-dricd.lOOh.lOO°C Air-dricd.2Oh.lSO'C Vac.-dricd.2h.100°C Solvent Tetrak Raw-undricd Air-dricd.2h.IOO'C Air-dricd.20h.100°C Air-dried.lOOh.lOO°C Air-dricd,20h.15OoC Gas* - 5.4 3.3 6.0 1.2 0.6 2.1 15.8 11.7 11.1 6.1 2.1 4.1 15.9 4.2 8.0 1.7 Oil Asphal 2.2 (4.3) 16.9 9.2 3.3 (6.2) 12.6 3.2 4.8 (6.8) 14.6 3.1 7.6 (9.3) 13.3 2.4 11.2(11.2) 5.1 0.5 3.0 (2.9) 10.0 5.4 2.8 (4.9) 16.0 11.5 3.9 (5.5) 15.7 11.1 5.6 (7.4) 18.6 8.6 6.7 (9.7) 16.5 10.8 1 l.g(l3.2) 9.6 2.3 Vac.-dricd.2h.l0OoC 3.0 (2.9) 10.2 12.9 Snlvcnt 1 -m Raw-undried 3.2 (5.0) 10.4 10.4 Air-dried.2h.100"C 3.0 (5.8) 10.3 8.1 Air-dricd.20h.100°C 6.4(10.0) 14.1 8.7 Air-dricd.100h.10O0C 5.2( 10.3) 14.4 8.7 Air-dricd.20h,15O0C 12.1 (I 3.0) 5.3 2.8 Vac.-dricd.2h.100°C 2.6 (3.7) 6.1 10.1 ,: 2.2 2.5 < Q I ,.-, I.. 2." , ' lh figvnr in parenthesis give the total gas yidds calculated from GC ar - Total - Conv. 25.0 14.8 15.5 12.7 10.9 12.5 - 43.3 35.1 32.4 30.8 19.9 25.9 - 39.9 22.7 24.5 21.1 18.0 18.3 ris. - Table 2. Products distributions (dmmf wt 410) for the catalytic liquefactions of the raw and dried coal at 350 OC with different solvents. 597 UlaIYdS.
- Page 71 and 72: areas of the particles and the SEM
- Page 73 and 74: Experimental Catalyst Precursors an
- Page 75 and 76: impregnating solvent. Table 3 shows
- Page 77 and 78: of MoCo-TC2 at the level of 0.5 wt%
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- Page 85 and 86: Reaction Time Figure 1 - Schematic
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- Page 89 and 90: A much more def~tive trend is seen
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- Page 93 and 94: same conditions and an extraction t
- Page 95 and 96: ACKNOWLEDGEMENT The authors thank t
- Page 97 and 98: THE STRUCTURAL &=RATION OF HUMINlTE
- Page 99 and 100: to be originally derived from demet
- Page 101 and 102: 145 30 I --/---Jh I , , I I , 250 2
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- Page 105 and 106: 1 for the Zap lignite. These result
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- Page 111 and 112: 585 I
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- Page 115 and 116: of some of the thermobalance runs.
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- Page 131 and 132: CONCLUSIONS The characexizntion of
- Page 133 and 134: A b S 0 r b a n C e A b s 0 r b a n
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- Page 141 and 142: 2w 180 160 9 140 120 P loo f 80 P O
- Page 143 and 144: 25 I 20 ' + 0 Drying lime, hours Fi
- Page 145 and 146: substructure have been identified a
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- Page 151 and 152: Table 3. Pyridine Extraction Sample
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- Page 155 and 156: increased from 120°C to 135”C, r
- Page 157 and 158: * wt% based on the amount of naphth
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- Page 161 and 162: Results Enzyme Modification with Di
- Page 163 and 164: Conclusions Reducing enzymes can be
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- Page 167 and 168: where yi = (x-xi !/pi. The zero mom
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Table 1. Products dismbutions (dmmf wt %) for the thermal <strong>liquefaction</strong>s <strong>of</strong> the raw and<br />
dried coal at 350 OC with different solvents.<br />
Drying Conditions.<br />
blv -fra<br />
Raw-undricd 7.7 (9.5)<br />
Air-dricd.2h.100°C 5.0 (6.3)<br />
Airdricd.2Oh.1000C 5.7 (7.3)<br />
Air-dricd.IOOh.100"C 8.5 (12.0)<br />
Air-dricd.2Oh.l SOT 9.8 (I 3.2)<br />
Vac.-dricd.2h.I00"C 3.3 (5.9)<br />
bL.alin<br />
Raw-undried 5.8 (7.7)<br />
Air-dricd.2h.100°C 5.4 (6.3)<br />
Air-dried.20h.lOO"C 5.9 8.7)<br />
Air-dried, 1 OOh.l OOOC 8.7 (1 1.6)<br />
Air-dried.20h.150"C 11.8(16.6)<br />
Vac.-dricd.2h.100°C 4.2 (5.4)<br />
I-Mcthvln- c e<br />
Raw-undried 5.9 (8.4)<br />
Air-dricd.2h. 100°C 5.1 (7.6)<br />
Airdri~d.20h.100~C 6.2 (7.5)<br />
Air-dricd.IOOh.100"C 9.0 (12.7)<br />
Drying Conditions.<br />
Raw-undricd<br />
Air-dricd.2h.100°C<br />
Airdri~d.20h.100~C<br />
Air-dricd.lOOh.lOO°C<br />
Air-dricd.2Oh.lSO'C<br />
Vac.-dricd.2h.100°C<br />
Solvent Tetrak<br />
Raw-undricd<br />
Air-dricd.2h.IOO'C<br />
Air-dricd.20h.100°C<br />
Air-dried.lOOh.lOO°C<br />
Air-dricd,20h.15OoC<br />
Gas*<br />
-<br />
5.4<br />
3.3<br />
6.0<br />
1.2<br />
0.6<br />
2.1<br />
15.8<br />
11.7<br />
11.1<br />
6.1<br />
2.1<br />
4.1<br />
15.9<br />
4.2<br />
8.0<br />
1.7<br />
Oil Asphal<br />
2.2 (4.3) 16.9 9.2<br />
3.3 (6.2) 12.6 3.2<br />
4.8 (6.8) 14.6 3.1<br />
7.6 (9.3) 13.3 2.4<br />
11.2(11.2) 5.1 0.5<br />
3.0 (2.9) 10.0 5.4<br />
2.8 (4.9) 16.0 11.5<br />
3.9 (5.5) 15.7 11.1<br />
5.6 (7.4) 18.6 8.6<br />
6.7 (9.7) 16.5 10.8<br />
1 l.g(l3.2) 9.6 2.3<br />
Vac.-dricd.2h.l0OoC 3.0 (2.9) 10.2 12.9<br />
Snlvcnt 1 -m<br />
Raw-undried 3.2 (5.0) 10.4 10.4<br />
Air-dried.2h.100"C 3.0 (5.8) 10.3 8.1<br />
Air-dricd.20h.100°C 6.4(10.0) 14.1 8.7<br />
Air-dricd.100h.10O0C 5.2( 10.3) 14.4 8.7<br />
Air-dricd.20h,15O0C 12.1 (I 3.0) 5.3 2.8<br />
Vac.-dricd.2h.100°C 2.6 (3.7) 6.1 10.1<br />
,:<br />
2.2 2.5<br />
< Q I ,.-,<br />
I.. 2." ,<br />
' lh figvnr in parenthesis give the total gas yidds calculated from GC ar<br />
-<br />
Total<br />
- Conv.<br />
25.0<br />
14.8<br />
15.5<br />
12.7<br />
10.9<br />
12.5<br />
-<br />
43.3<br />
35.1<br />
32.4<br />
30.8<br />
19.9<br />
25.9<br />
-<br />
39.9<br />
22.7<br />
24.5<br />
21.1<br />
18.0<br />
18.3<br />
ris.<br />
-<br />
Table 2. Products distributions (dmmf wt 410) for the catalytic <strong>liquefaction</strong>s <strong>of</strong> the raw and<br />
dried coal at 350 OC with different solvents.<br />
597<br />
UlaIYdS.
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