Refining of Synthetic Crudes: Based on a symposium sponsored by Editors: Martin L. Gorbaty, Brian M. Harney

By Editors: Martin L. Gorbaty, Brian M. Harney

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01 wt % because all of the feed passes through the whole-oil hydrotreater. Net diesel yield from such a refinery would be about 50 L V % , and gasoline yield would approach 40 L V % . Detailed yields for a similar refinery operating with F C C feed containing somewhat more nitrogen are given in Refs. I , 2, and 3. A hydrotreating/FCC refinery is compared with a proposed refinery i n which hydrocracking is the major conversion process. It also is compared with one i n which the shale oil is coked prior to hydrotreatment.

Comparison of results for petroleum stocks from the two units indicate that results should be comparable. For a given conversion and feed nitrogen level, the shale o i l feeds produced less coke. A t the lower nitrogen level, the shale o i l feed produced less gasoline and a correspondingly higher amount of C3-C4 product. Octane numbers of the gasolines for the hydrotreated shale o i l and Arabian Light vacuum gas o i l are compared i n Table I X . Again, the results are similar. A t the higher nitrogen level, the octanes are virtually identical on the shale and vacuum gas o i l feeds.

The reaction studies were carried out at various temperatures. The stability of the catalyst was checked at the end of a series by repeating the first experiment in the series. Feed for this bench-scale unit was obtained from the thermal hydrocracking experiment described previously (14). It consisted of the light ends from pilot plant run R-2-1-2 with properties as in Table I V . This 3 Table II. 0 883 58 REFINING Table III. 76 All yields based on feed. light-ends stream contained about 86% of the total distillate product resulting from fractionation i n the hot separator which had only one stage of separation.

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