Patent GB-1140778-A (GB)
Title: Process for the conversion of hydrocarbon oils
Inventor: CASE LYNN HAROLD
IPC: B01J23/00
Filed: 1968-01-05
Abstract: 1,140,778. Conversion of hydrocarbons. SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ N.V. 5Jan.,1968, No. 777/68. Heading C5E. A process for the conversion of hydrocarbon oils comprises (1) dehydrogenating and dehydroisomerizing a hydrocarbon oil boiling below 220‹ C. over a catalyst containing one or more metals of groups VI B  and/or VIII of the Periodic Table of Elements deposited on a refractory carrier, at a temperature in the range of from 400‹ to 540‹ C., a pressure in the range of from 7 to 55 atmospheres gauge, a liquid hourly space velocity in the range of from 4 to 15 volumes of oil per hour per volume of catalyst and a mole ratio of hydrogen to oil in the range of from 2À5 to 1 to 12 to 1 and (2) hydrocracking the dehydrogenated and dehydroisomerized hydrocarbon oil at a temperature in the range of from 250 to 450‹ C., a pressure in the range of from 7 to 55 atmospheres gauge, a liquid hourly space velocity in the range of from 1 to 5 volumes of oil per hour per volume of catalyst and a mole ratio of hydrogen to oil in the range of from 1 to 1 to 12 to 1 over a catalyst containing one or more of the metals rhenium, copper, silver, iron, cobalt, nickel, chromium, tungsten, molybdenum, platinum and palladium deposited on a molecular sieve carrier or intimately associated with an acid-acting refractory support, the intimate association having been achieved by contacting the support in hydrogel form with an aqueous solution of one or more soluble compounds of the said metal or metals, or by precipitating the support in hydrogel form in the presence of an aqueous solution of one or more soluble compounds of the said metal or metals. The dehydrogenation and dehydroisomerization result in the formation of aromatics and in the formation of sixmembered rings at the expense of five-membered rings. The dehydrogenation and dehydroisomerization may take place in a single reactor or in two consecutive reactors; in the latter case dehydrogenation is the main reaction in the first reactor and dehydroisomerization is the main reaction in the second reactor. The hydrocracking stage may be followed by a further dehydrogenation stage. The catalyst for the dehydrogenation and dehydroisomerization stages may comprise chromium, molybdenum, tungsten, iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, or platinum, supported on alumina containing not more than 5% of silica. Chlorine and/or fluorine may also be included. When an acidacting refractory support is used in the hydrocracking stage it may comprise from 50 to 90% of silica and 50 to 10% of one or more of alumina, magnesia, zirconia and boria. The hydrocracking catalyst may contain from 0À1 to 5% by weight of fluorine. They may be, but preferably are not, sulphided. The catalyst for the second dehydrogenation stage may be similar to that in the first dehydrogenation stage, and a preferred composition is 0À1 to 1% by weight of platinum and 0À1 to 1% by weight of chlorine on a carrier consisting of alumina containing not more than 0À5% by weight of silica.