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

More documents

Recommendations

Info

I 5 I comparable CTSL oils. Probably, the higher hydrogen content was a result Of the higher severity required for the single-stage process. In contrast, Figure 3 shows that within a given boiling range, the two-stage products had higher hydrogen contents than comparable H-Coal oils. Together, these two sets of observations may seem to present a paradox. However, the results are explained by the boiling distributions--the H-Coal oils contained more of the comparatively hydrogen-rich low-boiling components than the two-stage oils. HYDROTREATING PILOT PLANT TESTS Discussion. The major goals of the hydrotreating runs were either (1) to make specification jet fuel or diesel fuel and a naphtha suitable for catalytic reforming in a single hydrotreating step; or (2) to make a product suitable for hydrocracking in a second step. To meet either goal, almost all of the heteroatom contaminants-sulfur, nitrogen, and oxygen--had to be removed by the hydrotreatment. Typically, the control target for product nitrogen content was 0.5 ppm or below. Sulfur is relatively easy to remove compared to nitrogen, and therefore was of little concern in this study. [Although sulfur is much easier to remove than nitrogen, the equilibrium concentrations of sulfur are somewhat higher than nitrogen in products hydrotreated in a single stage.] Oxygen-containing compounds can be as hard or harder remove than nitrogen compounds. However, when the nitrogen was removed to 0.5 ppm, organic oxygen content was also removed to less than 10 ppm (based on limited analytical results). Most of the reported 50-100 ppm oxygen in the products was dissolved water. In addition to removing the heteroatoms, it is necessary to hydrogenate most of the aromatics compounds in these fractions if finished jet fuel or diesel are to be the main products from a single hydrotreating step. One of the purposes of this work was to show the degree of aromatics saturation needed for specification diesel and jet fuel. The amount of hydrogen consumed will be determined by the hydrogen contents of the feed and products, and the amounts of heteroatoms removed. If the hydrotreated product is to be hydrocracked, the hydrotreating severity can be somewhat less severe than if jet and diesel fuels are to be finished product. Additional hydrogen will be added in the second-stage hydrocracker. 283
Table I11 HYDROTREATING TESTS WITH ICR 106 CATALYST Syncrudes listed in increasing Order of hydrotreating difficulty LHSV H~ Pressure, psia. wyodak CTSL B (EPx634OF) Temperature, OF H2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% Wyodak H-Coal A (EP=603OF)* Illinois H-Coal B (EP=58g°F) Temperature, OF H2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% Wyodak ITSL B (EP=731°F) Temperature, OF n2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% wyodak H-Coal A (EP=785'F) Temperature, O F H2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% Illinois ITSL B (EP=763OF) Temperature, OF n2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% Illinois H-Coal A (EP=765OF) Temperature, OF H2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% Wyodak CTSL A (EP=85E°F) Temperature , OF H2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, LV% Illinois ITSL A (EP=859'=F)* Wyodak ITSL A (EP=941°F) Temperature, OF n2 Consumption, SCF/B Product Nitrogen, ppm Product Aromatics, Lv% 0.5 1.0 1.5 1.5 1.5 1.5 2300 2300 2300 1800 1400 1000 680 775 0.5 3 6 16
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 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-
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: Process Identification LV% Of AS- R
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?