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

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esults would be expected to be similar to those previously reported for naphthas from single stage processes (7).1 Jet. To make jet fuel meeting the ASTM smoke point specification of 20mm.(minimum), most of the aromatics in the coal liquids had to be hydrogenated. Figure 4 is a plot of smoke point versus aromatic content of kerosene jet fuels from the various syncrudes. The results fall into two rough groups, those from Wyodak coal and those from Illinois coal. At a given aromatics content, those from Wyodak coal had smoke points 2-3 mm higher than those from Illinois coal, a consequence of the higher Wyodak paraffin content. [The Wyodak jet contained about 10 LV% paraffins; the Illinois jet, 1-3 LV%.] The Illinois jet fuels met the jet smoke specification of 20 mm at 10% aromatics or lower; the Wyodak jet fuels met the specification at about 16 LV% aromatics. [Some of the scatter in results for products from a given coal was due to different boiling distributions. Those jet fuels containing more low boiling material had somewhat higher smoke points.] Jet fuels from coal offer some unique advantages over those from petroleum. Because they contain high concentrations of naphthenes, they are very dense and have high heating values by volume. Therefore, they could have specialized uses, such as for military fuels. FOK example, Figure 5 shows the densities of narrow boiling fractions of hydrotreated ITSL oil. Jet fuel of a desired density could be made by adjusting the boiling range. The ASTM specification for jet fuel gravity is 37OAPI (minimum). However, this specification is probably unnecessary for aircraft with modern flow controllers, and lower gravity (higher density) fuels could be acceptable. Also, these jet fuels have unusually low freezing points, because of low normal paraffin contents. Diesel. Diesel products from both single-stage and two-stage procemet typical ASTM specifications. A relatively high degree of hydrogenation was needed to meet the cetane-number specification of 40 (minimum). Figure 6 shows the relationship for cetane number versus aromatics content for products from single-stage and two-stage processes. With the two-stage oils, the specification was met with an aromatics content of about 20 Lv%; with single-stage oils, an aromatic content of less than 10 LV% was needed. These differences, however, were not necessarily the result of single-stage versus two-stage processing. Rather, they appear to be due to changes in boiling ranges of the diesels. For example, Table VI compares pairs of samples of different boiling ranges. The aromatics and paraffin contents within a given pair were about the same. Within each pair, the higher boiling sample had the higher cetane number. Also, in other comparisons (1). the more paraffinic diesels had higher cetane numbers, when other properties were about equal. AS with the jet fuels described above, these coal-derived diesel fuels had excellent cold weather properties, and high volumetric energy contents. 287
Table VI EFFECT OF BOILING RANGE ON CETANE NUMBER Source Initial, Midpoint, Cetane Aromatics, Paraffins, O F (TBP) OF (TBP) No. LV, % LV% Wyodak CTSL 250 414 44.2 3.9 9.5 350 454 48.7 4.6 7.7 Illinois ITSL 250 520 43.1 9.8
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ABSTRACT LIQUEFACTION CO-PROCESSING
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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
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TET did not promote the production
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MICROAUTOCLAVE DESCRIPTION AND PROC
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FEEDSTOCK PROPERTIES Some propertie
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CONCLUSIONS HRI's microautoclave ha
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176
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100. 2 8%. M = ?8. 38. .... . . . .
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CATALYTIC CO-PROCESSINS OF OHIO NO.
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CATALYST COMPARISON STUDY The premi
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fractions and a decrease of heavier
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TABLE 2 Coal Analyses I1 1 i noi s
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Temperature WHSV, G/hr/cc TABLE 6 C
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z FIGURE 3 COAL REACTIVITY SCREENIN
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COPROCESSING USING HzS AS A PROMOTE
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- 3 - that product yields depend on
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- 5 - occurs in the yields of aspha
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Table 1 Analysis of Feedstocks Fore
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THO-STAGE COPROCESSING OF SUBBITUMI
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esult in retrogressive reactions ta
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8. 6. Ignasiak, L. Lewkowicz, G. Ko
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Table 4 OVERALL MASS BALANCE FOR TH
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BACKGROUND COAL LIQUEFACTION/RESID
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system, which could be operated wit
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TABLE 1 EFFECT OF LC-FINING~"' TEMP
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Figure 1. SCHEMATIC OF LCI CO-PROCE
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SIMULATION OF A COAL/PETROLEuII RES
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20 pseudocomponents was developed t
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ottoms is less sensitive to the num
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Low Pressure Separator A temperatur
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7. Gallier, P.W., Boston, J.F., Wu,
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I I I I I I I I I 100- --- Experime
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Coprocessing Schemes The coprocessi
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processing 25,000 and 150,000 bbl/d
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FIGURE 1 I DISTRIBUTION OF REFINERI
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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: Table IV HYDROTREATING TO 0.2 PPM N
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
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4 (u I t + 9 (u I 337 - Q 0
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