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 ...
I i Three-phase SeDarator For the three-phase separator overheads, the effect of the correlation option is given in Table 3. There is some improvement using the petroleum-liquids option set. Use of the coal-liquids option set results in an overall error for total mass flow of overhead of 1.862, and the petroleum-liquids option set results in an error of 0.73%. TABU 3. Comparison of Calculated and Experimental Overhead Flows (lb/hr) for the Three-phase Separator as a Function of Physical Properties Calculations Method Correlation Option Set Components Coal Liquids Petroleum Liquids Experimental Hz 0.0591 0.0589 0.0587 co 0.0051 0.0051 0.00513 HIS 0.0516 0.0511 0.0498 CH z 0.0629 0.0626 0.0621 CZH6 0.0349 0.0346 0.0340 CsHs 0.0233 0.0229 0.0225 C*HIO 0.0086 0.0084 0.00849 I-C~HI o 0.0024 0.0023 0.00212 CSHI z 0.0023 0.0022 0.00263 I-CSHI z 0.0025 0.0023 0.00263 Debutanizer For the debutanizer overheads, the effect of the correlation option is given in Table 4. There is improvement using the petroleum-liquids option set. Use of the coal-liquids option set results in an overall error for total mass flow of over- head of 16.42, and the petroleum-liquids option set results in an error of only 1.37%. TABLE 4. Comparison of Calculated and Experimental Overhead Flows (lb/hr) for the Debutanizer as a E’unction of Physical Properties Calculations Method Correlations Options Set Components Coal Liquids Petroleum Liquids Experimental 2.31 x lo-’ 2.79 10-~ 3.5 io-’ 7.84 x lo-’ 1.4 10-~ 2.1 io-’ 1.5 x lo-: 3.34 x 10- 6.15 x lo-: 6.10 x 10- 1.05 x lo-’ 3.91 x lo-* 4.59 10-~ 3.9 x lo-’ 1.1 x lo-’ 1.8 x lo-’ 2.5 x io-’ 1.8 x lo-; 4.02 x 10- 7.41 x lo-* 7.31 x lo-* 1.35 x lo-’ 6.09 x io-* -- -- 1.60 x lo-’ 2.35 x 10-~ 2.96 x lo-: 1.95 x 10- 6.51 x lo-* 8.08 x lo-* 8.08 x lo-’ 2.88 x lo-’ Vacuum Fractionator As a measure of simulation adequacy, total vapor and, liquid flows computed by simulation were compared with experimental data. Total mass flow of overhead and 219
ottoms is less sensitive to the number of theoretical stages than are the individual distillate fraction flows. The effect Of the correlation option set (coal-liquids vs. petroleum-liquids) on the vacuum fractionator simulation perfor- mance was determined. Since simulated distillate flows were in considerable dis- agreement with experimental values for the reported operating pressure of 0.94 psia, additional simulation runs were made to observe the effect of assumed column pressures. For the petroleum-liquids option set, a value of 4.5 psia gave the best match of calculated total overhead and bottom flows to experimental flows. Correspondingly, a value of 6.0 psia was found for the coal-liquids option set. Given that the reported column pressure, 0.94 psia, is closer to 4.5 psia than to 6.0 psia, this result gives ail indirect indication that the petroleum-based option set better describes the experimental system. The actual operating pressure for the vacuum fractionator was known to increase above 0.94 psia during the experi- mental run, but no information is available as to the extent of increase. The results for the flows of the distillate fractions are presented in Tables 5-7. Table 5 represents results for vacuum bottoms flows, and Table 6, for vacuum over- head flows (calculated vacuum overhead flows also include values for debutanizer bottoms flows in order to agree with experimental measurements). Table 7 gives a comparison of the pressure and correlation option set in terms of an overall per- centage error for both bottoms and overhead at the operating pressure of 0.94 psia. Use of the petroleum-liquids option set gives better agreement, although the percentage of error relative to experimental error is still considerable. TABLE 5. Comparison of Calculated and Experimental Vacuum Bottoms Flows (lbhr) as a Function of Physical Properties Calculation kthod and System Pressure P = 6.0 psia Petroleum Liquids P = 0.94 psia P = 4.5 psia ~ ~ Boiling Point Correlation Option Set Range, OF Calculated Exper imen tal Coal Liquids P = 0.94 psia IBP-350 1.52 x lo-' -- 350-450 8.46 x 10-~ -- 450-950 950+ 5.60 x lo-' 3.24 x lo-' 5.16 x lo-' 5.92 x lo-' Total 3.80 x lo-' 1.11 x lo-' IBP-350 5.38 x 10-5 -- 350-450 2.94 x lo-* -- 450-950 950+ 5.41 x lo-' 5.67 x lo-' 5.16 x lo-' 5.92 x lo-' Total 1.12 x 10-I 1.11 x 10-I IBP-350 4.92 x lo-' -- 350-450 2.47 x 10-~ -- 450-950 950+ 1.40 x lo-' 5.38 x 10-2 5.16 x lo-' 5.92 x lo-' Total 6.78 x lo-' 1.11 x lo-' IBP-350 5.59 x 10-~ -- 350-450 2.75 x io-' -- 450-950 5.21 x lo-' 5.16 x lo-' 950+ 5.79 x lo-' 5.92 x lo-' Total 1.10 x 10-1 1.11 x lo-' 220
- 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: 20 pseudocomponents was developed t
- 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
- 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
ottoms is less sensitive to the number <strong>of</strong> theoretical stages than are the<br />
individual distill<strong>at</strong>e fraction flows. The effect Of the <strong>co</strong>rrel<strong>at</strong>ion option set<br />
(<strong>co</strong>al-liquids vs. petroleum-liquids) on the vacuum fraction<strong>at</strong>or simul<strong>at</strong>ion perfor-<br />
mance was determined. Since simul<strong>at</strong>ed distill<strong>at</strong>e flows were in <strong>co</strong>nsiderable dis-<br />
agreement with experimental values for the reported oper<strong>at</strong>ing pressure <strong>of</strong> 0.94<br />
psia, additional simul<strong>at</strong>ion runs were made to observe the effect <strong>of</strong> assumed <strong>co</strong>lumn<br />
pressures. For the petroleum-liquids option set, a value <strong>of</strong> 4.5 psia gave the<br />
best m<strong>at</strong>ch <strong>of</strong> calcul<strong>at</strong>ed total overhead and bottom flows to experimental flows.<br />
Correspondingly, a value <strong>of</strong> 6.0 psia was found for the <strong>co</strong>al-liquids option set.<br />
Given th<strong>at</strong> the reported <strong>co</strong>lumn pressure, 0.94 psia, is closer to 4.5 psia than to<br />
6.0 psia, this result gives ail indirect indic<strong>at</strong>ion th<strong>at</strong> the petroleum-based option<br />
set better describes the experimental system. The actual oper<strong>at</strong>ing pressure for<br />
the vacuum fraction<strong>at</strong>or was known to increase above 0.94 psia during the experi-<br />
mental run, but no inform<strong>at</strong>ion is available as to the extent <strong>of</strong> increase. The<br />
results for the flows <strong>of</strong> the distill<strong>at</strong>e fractions are presented in Tables 5-7.<br />
Table 5 represents results for vacuum bottoms flows, and Table 6, for vacuum over-<br />
head flows (calcul<strong>at</strong>ed vacuum overhead flows also include values for debutanizer<br />
bottoms flows in order to agree with experimental measurements). Table 7 gives a<br />
<strong>co</strong>mparison <strong>of</strong> the pressure and <strong>co</strong>rrel<strong>at</strong>ion option set in terms <strong>of</strong> an overall per-<br />
centage error for both bottoms and overhead <strong>at</strong> the oper<strong>at</strong>ing pressure <strong>of</strong><br />
0.94 psia. Use <strong>of</strong> the petroleum-liquids option set gives better agreement,<br />
although the percentage <strong>of</strong> error rel<strong>at</strong>ive to experimental error is still<br />
<strong>co</strong>nsiderable.<br />
TABLE 5. Comparison <strong>of</strong> Calcul<strong>at</strong>ed and Experimental Vacuum Bottoms Flows (lbhr)<br />
as a Function <strong>of</strong> Physical Properties Calcul<strong>at</strong>ion kthod and System Pressure<br />
P = 6.0 psia<br />
Petroleum Liquids<br />
P = 0.94 psia<br />
P = 4.5 psia<br />
~ ~<br />
B<strong>oil</strong>ing Point<br />
Correl<strong>at</strong>ion Option Set Range, OF Calcul<strong>at</strong>ed Exper imen tal<br />
Coal Liquids<br />
P = 0.94 psia IBP-350 1.52 x lo-' --<br />
350-450 8.46 x 10-~ --<br />
450-950<br />
950+<br />
5.60 x lo-'<br />
3.24 x lo-'<br />
5.16 x lo-'<br />
5.92 x lo-'<br />
Total 3.80 x lo-' 1.11 x lo-'<br />
IBP-350 5.38 x 10-5 --<br />
350-450 2.94 x lo-* --<br />
450-950<br />
950+<br />
5.41 x lo-'<br />
5.67 x lo-'<br />
5.16 x lo-'<br />
5.92 x lo-'<br />
Total 1.12 x 10-I 1.11 x 10-I<br />
IBP-350 4.92 x lo-' --<br />
350-450 2.47 x 10-~ --<br />
450-950<br />
950+<br />
1.40 x lo-'<br />
5.38 x 10-2<br />
5.16 x lo-'<br />
5.92 x lo-'<br />
Total 6.78 x lo-' 1.11 x lo-'<br />
IBP-350 5.59 x 10-~ --<br />
350-450 2.75 x io-' --<br />
450-950 5.21 x lo-' 5.16 x lo-'<br />
950+ 5.79 x lo-' 5.92 x lo-'<br />
Total 1.10 x 10-1 1.11 x lo-'<br />
220
Change language