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

More documents

Recommendations

Info

Table 4 Distillate Characteristics Severity Very low - Low Moderate Moderate-hiqh H2S FeSOg API H/C N,wt A S,wt A 0,wt A - fa Mn,g/mole no yes yes yes 15.2 13.3 1.59 1.53 0.26 0.37 3.15 3.11 0.89 1.30 26 - 31 - no Yes 17.0 1.56 0.39 2.98 1.28 29 107 yes yes no yes 15.9 15.8 1.57 1.54 0.41 0.41 2.A3 2.98 1.23 1.31 28 30 320 322 no yes 22.4 1.62 0.44 2.30 1.40 25 272 yes yes no yes 19.8 22.9 1.58 1.63 0.47 0.43 2.44 2.27 1.28 1.02 29 24 305 279 FIGURE 1 RESIDUE COMPOSITION no yes 25.4 1.58 0.50 1.64 1.46 30 293 - -very low low SEVERITY mderste mderatc-high 199 H2S H2S+FeS04 insoluble! FeS04 U 0 v) LL L Yes Yes 25.9 1.62 0.50 1.69 0.85 25 278
THO-STAGE COPROCESSING OF SUBBITUMINOUS COALS AND BITLMEN OR HEAVY OIL* ABSTRACT B. Ignasiak, T. Ohuchi, P. Clark, D. Aitchison and T. Lee Coal Research Department Alberta Research Council 1 O i l Patch Drive P.O. Bag #1310 Devon, A1 berta, Canada TOC 1EO Pretreatment of subbituminous coal with an appropriately formulated mix of carbon monoxide and water, in presence of bitumen or heavy oil, results in very fast reactions characterized by a high degree of coal solubilization and deoxy- genation. The reaction is catalysed by a mixture of alkali metal carbonates and proceeds readily at 380-400OC. The first-stage reaction product appears to be susceptible to further catalytic hydrogenation at 420-460T with gaseous hydrogen yielding 65-70% (on daf feed) of hydrogen-rich distillable oil, com- posed mainly of naphtha and middle oil. The process flowsheet is presented and the comparative economics of two-stage carbon nonoxide/steam-hydrogen and hydrogen-hydrogen coprocessing schemes are discussed. INTRODUCTION Alberta is endowed with immense reserves of subbituminous coals (11, bitumen and heavy oil (2). The concept of coprocessing coal and petroleum derived solvents is not a new one (3.4) and there is a consensus that this approach is more attractive economically than conventional coal 1 iquefaction (5). The most attractive feature of the coprocessing concept is its potential for elimination of oil recycle which may increase the output of the installation by up to three times. It has to be emphasized that under Alberta conditions the economics of a coprocessing plant have to be compared to a heavy oil and/or bitumen hydrocracking plant. The major advantage of coprocessing as opposed to bitumen or heavy oil hydrocracking is the low cost of coal. This has to be weighed against the increased hydrogen consumption, increased plant complexity (conversion of coal to distillate oil requires more severe conditions compared to bitumen) and the element of risk associated with implementation of the new coprocessing technology. A factor which may have a substantial effect on the economics of coprocessing as compared to bitumen or heavy oil hydrocracking is that of purely chemical nature. It has not been firmly established whether the interaction among coal- and bitumen-derived radical intermediates leads to an increase or a reduction in oil yield or its quality. On the other hand, it has been demonstrated that hydrocracking of bitumen in a one-stage process in the presence of small (1-3% by weight) quantities of subbituminous coal results in significant improvement in oil yield (6). Similar results can be obtained by employing chars generated from brown coals (4,7) and this furnishes a strong evidence that catalytic effects and not the chemistry of the components o f the substrate play a dominant role in a one-stage bituen * To be presented at the Fuel Division "Reactions of Coal in Novel Systems", Anaheim ACS Meeting, September 7-12. 1986 200
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 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: Table 1 Analysis of Feedstocks Fore
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-
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
Page 123 and 124:
FIRST STAGE HRI'S CATALYTIC TWO STA
Page 125 and 126:
FIRST-STAQ COAL CONVERSION (W I IIA
Page 127 and 128:
REACTOR SOLIOS HTOROGEN/CARBON ATOl
Page 129 and 130:
TRANSPORTATION FUELS FROM TWO-STAGE
Page 131 and 132:
Process Identification LV% Of AS- R
Page 133 and 134:
Table I11 HYDROTREATING TESTS WITH
Page 135 and 136:
Table IV HYDROTREATING TO 0.2 PPM N
Page 137 and 138:
Table VI EFFECT OF BOILING RANGE ON
Page 139 and 140:
(4) In all cases studied, the jet f
Page 141 and 142:
292
Page 143 and 144:
INTEGRATED TWO-STAGE LIQUEFACTION:
Page 145 and 146:
are over-riding features in its fav
Page 147 and 148:
Complementary fundamental studies o
Page 149 and 150:
Comparative Economics of Two-Stage
Page 151 and 152:
The variation in hydrotreating cost
Page 153 and 154:
FIGURE 1: COMPARISONS OF ILLINOIS N
Page 155 and 156:
Process TABLE 1: TWO-STAGE PROCESSE
Page 157 and 158:
Abstract Temperature-Staged Catalyt
Page 159 and 160:
Results and Discussion Reactions in
Page 161 and 162:
2. 3. 4. 5. 6. Derbyshire, F. J. an
Page 163 and 164:
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
Page 171 and 172:
ENHANCED COAL LIQUEFACTION WITH STE
Page 173 and 174:
change in weight being compared to
Page 175 and 176:
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
Page 181 and 182:
THE EFFECT OF REACTION CONDITIONS O
Page 183 and 184:
and may ultiontely form methyl-subs
Page 185 and 186:
! 5. Narain, N.K., Utz, B.R., Appel
Page 187:
4 (u I t + 9 (u I 337 - Q 0
show all

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

You also want an ePaper? Increase the reach of your titles

Delete template?

Save as template?