Liquefaction co-processing of coal shale oil at - Argonne National ...

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TABLE 6. Comparison of Calculated and Experimental Vacuum Overhead Flows (lb/hr) as a Function of physical Properties Calculation Method and System Pressure Boiling Point Correlation Option Set Range, OF Calculated Experimental Coal Liquids P = 0.94 psia P = 6.0 psia Petroleum Liquids P = 0.94 psia P = 4.5 psia IBP-350 1.07 x lo-' 1.34 x lo-' 3 5 0 - 4 5 0 1.28 x lo-' 1.90 x 10-2 450-950 1.43 x lo-' 8.97 x lo-' 950+ 2.60 x lo-' 8.17 x 10-~ Total 1.93 x lo-' 1.22 x 10-1 IBP-350 1.07 x lo-' 1.34 x lo-' 350-450 1.25 x lo-' 1.90 x 450-950 9.38 x lo-' 8.97 x lo-' 950+ 1.70 x lo-' 8.17 x 10-~ Total 1.19 x 10-1 1.22 x lo-' IBP-350 350-450 4 5 0 - 9 5 0 950+ Total 1.05 x lo-' 1.28 x lo-' 1.34 x lo-' 4.60 x lo-' 1.62 x lo-' 1.34 x lo-' 1.90 x lo-' 8.97 x lo-' 8.17 x 10-~ 1.22 x lo-' IBP-350 350-450 4 5 0 - 9 5 0 950+ Total 1.05 x lo-' 1.25 x lo-' 9.64 x lo-' 5.08 x lo-' 1.24 x lo-' 1.34 x 10-i 1.90 x 10- 8.97 x lo-' 8.i~ x 10-~ 1.22 x 10-f TABLE 7. Comparison of Physical Properties Calculation Method on Vacuum Fractionator Effluent Stream Hass Flow Rates Correlation Option Set ~ ~~ Coal Liauids $ Error" Vacuum Bottoms Vacuum Overhead P = 0.94 psia 65.8 58.2 Petroleum Liquids P = 0.94 38.9 32.8 *Absolute value of (Calculated - Experimental)/Experimental. Effects of pressure and correlation option set on pseudocomponent composition for the vacuum fractionator are reflected in Figures 3-6. Figures 3 and 4 represent the effect on the vacuum bottoms stream, and Figures 5 and 6, the effect on the overhead stream. These figures indicate that the petroleum-liquids option set gives better values than the coal-liquids option set and that the effect of pressure is considerable. 221 ~~~
Low Pressure Separator A temperature of 284OF was used for the operating condition of the low-pressure separator in the simulator. Since, experimentally, a temperature range of 2480F- 2840F was given, it was decided to make a simulation run at the lower temperature to determine any effects of the assumed temperature on the effluent flow rates. Results for the lower temperature indicate only a small increase in bottoms flows of 1.3% and an decrease in overhead flows of 11.8%. Effect of Free Water Phase on the Debutanizer Simulations were carried out on the debutanizer to determine the impact of the presence of a free water phase (Table 8). Without the invocation of the option to test for the presence of free water, no distillate and only a small amount of lighter gases are predicted by the simulator to be present in the debutanizer bottoms. With the test for the presence of water invoked, the presence of a free water phase is confirmed, and results indicate a substantial increase in bottoms flow and a decrease in overhead. Both of these predictions agree with experiment, as shown in Table 8. All simulations have tested for the presence of a free water phase. TABLE 8. Effect of Treatment of Water on the Debutanizer Effluent Product Flows (lb/hr) Assumed Absence of Free Water Phase Assumed Presence of Free Water Phase Experimental Products Overhead Bottoms Overhead Bottoms Overhead Gases-Cs 6.93 x lo-’ 3.90 x 1.11 x lo-* 1.16 x lo-’ 1.18 x lo-* IBP-1500F 3.79 x lo-’ 0 1.05 10-3 4.86 IO-’) 35003500~ i.53 x 10-3 0 1.08 10-7 iIi6 X 10-3 } 450°-9500F 1.31 x 0 4.69 x lo-’ 8.46 x lo-* 2‘88 lo-’ 950°F+ 1.02 10-7 0 0 6.52 x IO-~J TABLE 9. Effect of Treatment of Heavy Resid on Vacuum Bottoms Heaw Residue Treated as Solid Material Pseudocomponent Product (Flows, lb/hr) (Flows, lb/hr) Gases-Cs I BP-3500F 350°-4500F 450°-9500F 950°F+ Nondistillate Solid 0 0 0 0 0 0.0456 1.44 x 10-a 1.52 x 8.47 x lo-‘ 5.59 10-~ 3.25 x lo-‘ 0 Effect of Treatment of Heavy Resid on Vacuum Bottoms The method of treatment of heavy resid has an impact on predicted composition and flow rate of vacuum bottoms as reflected in Table 9. The data are for the simulation of the vacuum fractionator at the pressure of 0.94 psia and using coal- liquids correlations. When the heavy resid is treated as a nondistillate solid, i.e., material with negligible vapor pressure, no distillates are predicted to appear in the vacuum bottoms. When the heavy resid is treated as a 1091°F pseudo- 222 I
Page 1 and 2:
ABSTRACT LIQUEFACTION CO-PROCESSING
Page 3 and 4:
eaction temperature, 1000-1500 psig
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6. 7. 8. 9. 10. 11. 12. 13. 14. 15
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I 0" 100- I I I WyO-3 P 3: 1500 psi
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11.3 A-6 yJ 600 OF, 1500 psig CO, 3
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Experimental UDqradinq and Cooroces
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catalytic to the thermal hydrogenat
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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 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: ottoms is less sensitive to the num
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
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
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FIRST STAGE HRI'S CATALYTIC TWO STA
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FIRST-STAQ COAL CONVERSION (W I IIA
Page 127 and 128:
REACTOR SOLIOS HTOROGEN/CARBON ATOl
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TRANSPORTATION FUELS FROM TWO-STAGE
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Process Identification LV% Of AS- R
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Table I11 HYDROTREATING TESTS WITH
Page 135 and 136:
Table IV HYDROTREATING TO 0.2 PPM N
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Table VI EFFECT OF BOILING RANGE ON
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(4) In all cases studied, the jet f
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292
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INTEGRATED TWO-STAGE LIQUEFACTION:
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are over-riding features in its fav
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Complementary fundamental studies o
Page 149 and 150:
Comparative Economics of Two-Stage
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The variation in hydrotreating cost
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FIGURE 1: COMPARISONS OF ILLINOIS N
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Process TABLE 1: TWO-STAGE PROCESSE
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Abstract Temperature-Staged Catalyt
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Results and Discussion Reactions in
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2. 3. 4. 5. 6. Derbyshire, F. J. an
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I LL a rJJW ., .. ;> 0 i s W 8 a 31
Page 165 and 166:
Materials Feeds to the WGS-solvent
Page 167 and 168:
products. Thus, coupling the WGS an
Page 169 and 170:
5. R. J. Xottenstette, Sandia Natio
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ENHANCED COAL LIQUEFACTION WITH STE
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change in weight being compared to
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I I aromatic ring. The group of sig
Page 177 and 178:
T,\llI.l< I ASAI,YSIS OP \\YOl)Al\:
Page 179 and 180:
00 3000 2000 le00 1600 1400 1200 IO
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THE EFFECT OF REACTION CONDITIONS O
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and may ultiontely form methyl-subs
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! 5. Narain, N.K., Utz, B.R., Appel
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4 (u I t + 9 (u I 337 - Q 0
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