Desulphurization of hydrocarbonaceous fuels

Abstract

Abstract 1440407 Hydrodesulphurization of heavy oils TEXACO DEVELOPMENT CORP 12 March 1974 12301/74 Heading C5E A turbulent stream of hydrogen and heavy oil feed 1 is heated to 600-1000‹ F. in a tubular heater 7 and then introduced as the stream 8 into a free-flow stripper vessel 9 which is free from catalyst and a stream 20 containing hydrogen and naphtha at 600-1000‹ F. is simultaneously introduced into the stripper vessel 9 in direct contact countercurrent to the stream 8; the heavy oil feed is simultaneously thermocracked and hydrotreated in the vessel 9 to provide an overhead stream 24 and a heavy bottoms stream 21. The overhead 24 is hydrocracked and hydrotreated at 28 in the presence of a catalyst, e.g. nickel sulphide on alumina, and the effluent 29 is cooled to liquefy naphtha and separated at 36 into a hydrogen recycle stream 39 and a liquid stream 43. The stream 43 is fractionated at 44 to provide a normally liquid substantially sulphur-free product 45 and a naphtha stream 49 at least a portion 12 of which is recycled, after the removal of tail gas 56 at 52, to form at least a portion of the naphtha in line 20. The weight ratio of naphtha in stream 20 to the heavy oil feed 1 is suitably between 0À2 and 5 and the weight ratio of the stripper bottoms 23 to the heavy oil feed 1 is suitably between 0À05 and 0À25. The pressure in heaters 7 and 15, stripper 9, reactor 28 and separator 36 is suitably 1000-6000 p.s.i.g. The hydrogencontaining gas separated at 36 can be scrubbed with a recycle-stream 38 of naphtha. The make up hydrogen 3 can be obtained by the partial oxidation of at least a portion of the stripper bottoms 23 with or without water-gas shift reaction and/or carbon dioxide removal.

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