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 ...
c RECICLE COMPRESSOR MAKE-UP H2 LEGEND R = RwmR S = HIGH PRESSURE SEPARATOR Sl = KIRIPPER D = DEBUTANIZER VF = VACUUM FRACTIONATOR FIGURE 5 PILOT PLANT FLOW SCHEME I . I 191 vF I Cq MINUS cq PLUS PRODUCT DISTILLATE 10M'F EP HEAVY PROWCT
COPROCESSING USING HzS AS A PROMOTER P.M. Rahimi, S.A. Fouda and J.F. Kelly CANMET, Energy, Mines and Resources Canada, 555 Booth Street, Ottawa, Ontario K1A OG1 INTRODUCTION Coprocessing heavy oils, bitumens or petroleum residues with coal can be considered as a bridge between coal liquefaction and hydrocracking. The existing technologies of liquefaction and hydrocracking can be applied with modification to coprocessing. In terms of operation, coprocessing is less complicated than liquefaction because recylce solvent is eliminated. Since the coprocessing solvent is upgraded simultaneously with coal the reactor volume is utilized more effectively. If residuum conversion levels during coprocessing are as high as those in hydrocracking then coprocessing also offers a significant saving in feedstock costs by substituting a significant portion of the heavy oil with less expensive coal. CANMEl coprocessing involves the simultaneous upgrading of coal and heavy oil or bitumen in a once-through mode of operation using a disposable iron catalyst. The CANMET additive (pulverized coal impregnated with iron sulphate), hereinafter referred to as FeS04, ha8 been identified as both an hydrogenation and coke-reducing catalyst. Process feasibility has been investigated using a variety of coals and heavy oils/bitumens(l). Also, it has been demonstrated that in terms of product yields for subbituminous coals, CANMET coprocessing is superior to liquefaction and is comparable to hydrocracking (2-3). The effect of H2S in hydrocracking of model compounds and in liquefaction is well documented (4-11). The ability of H2S to reduce coke formation and increase liquid yield in coal liquefaction has been patented by Exxon Research and Engineering Company (12). It has also been shown that HpS has benefical effects in non-catalytic crude oil hydrorefining processes (13). In a previous batch autoclave study the use of H2S in coprocessing subbituminous coal and bitumen resulted in high coal conversion and distillate yield (14). The increase in product yields in the presence of H2S was attributed to its ability to donate its hydrogen to radicals derived from coal and bitumen (15). The objective of the present study was to verify the positive effects of H2S under coprocessing conditions using a continuous-flow bench scale pilot plant and to compare the activity of H2S with FeSO4 under similar operating conditions. 192
- 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 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: z FIGURE 3 COAL REACTIVITY SCREENIN
- 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-
c<br />
RECICLE<br />
COMPRESSOR<br />
MAKE-UP H2<br />
LEGEND<br />
R = RwmR<br />
S = HIGH PRESSURE SEPARATOR<br />
Sl = KIRIPPER<br />
D = DEBUTANIZER<br />
VF = VACUUM FRACTIONATOR<br />
FIGURE 5<br />
PILOT PLANT FLOW SCHEME<br />
I . I<br />
191<br />
vF I<br />
Cq MINUS<br />
cq PLUS<br />
PRODUCT<br />
DISTILLATE<br />
10M'F EP<br />
HEAVY<br />
PROWCT
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