Abstract: A fluid coking process is provided in which a carbonaceous feed is first coked in a dense fluidized bed first coking zone and the effluent of the dense bed is passed as a suspension through a transferline second coking zone. A major portion of the solids is separated from the effluent of the upper end of the transferline and passed to a third coking zone which is operated at a higher temperature than the other coking zones and in which the first and second coking zones are positioned.

Abstract: A fluid coking process is provided in which inert particles, such as coke, are added to the coker feed, in a specified amount.

Abstract: An integrated catalytic fluid coking and gasification process is provided in which a portion of the coke produced in the coker is steam gasified to produce a hydrogen-containing gas and a catalytic partially gasified coke. Subsequently, a portion of the catalytic partially gasified coke is burned to provide heated partially gasified coke which is recycled to the gasification zone. A portion of the catalytic partially gasified coke is passed from the gasification zone to the coker to contact the coker vapor phase product comprising normally liquid hydrocarbons and to crack at least a portion of the normally liquid hydrocarbons. Optionally, solid fines recovered from the gaseous effluent of the gasification zone may be recycled to the carbonaceous chargestock of the coker.

Abstract: A fluid coking process is provided in which the recycling of coke particles of less than about 44 microns in diameter to the coking reactor is minimized by passing the stream of coke withdrawn from the coking reactor to a vessel comprising a fluidized bed of solids separated into two zones. The coke withdrawn from the coker is passed into one zone where seed generation for the process is performed. Coke recycled to the coker is withdrawn from the second zone which is operated as an elutriation zone. The solid fines of less than 44 microns are removed overhead from the vessel with the gaseous effluent of the vessel. This improvement is particularly suitable for once-through fluid coking to minimize small fines being present in the coker liquid product.

Abstract: An integrated fluid coking and gasification process is provided in which a solid cracking catalyst is added to the coker chargestock and in which a partially gasified coke matrix comprising the cracking catalyst is recycled to the coker vapor phase product.

Abstract: The quantity and quality of liquids produced from solid coal can be enhanced by a process comprising a liquefaction zone and a pyrolysis reactor, preferably a fluid coking zone, wherein the heavy liquids obtained in the pyrolysis reactor, e.g., 1000.degree. F.+ materials having a Conradson Carbon content of at least 15 wt. % are recycled to the liquefaction zone, rather than to the pyrolysis reactor, for further treatment under hydrogenation conditions and, consequently, conversion of the heavy liquids to lower boiling liquids which may be removed from the pyrolysis reactor feed by distillation is achieved.

Abstract: A low metals coke is produced in a two-stage coking process in which the first coking stage is once-through fluid coking, and the heavy oil separated from the fluid coking zone effluent is coked in a second coking stage, which is delayed coking.

Abstract: A combination slurry hydroconversion, coking and coke gasification process is provided wherein carbonaceous solids having an average particle size of less than 10 microns in diameter or the ashes thereof are used as a catalyst in the hydroconversion stage.

Abstract: A low density particulate vanadium-containing metallic ash concentrate, at least 50 percent of the articles of said concentrate having a diameter not greater than about 1 micron, is produced from a partially gasified coke comprising metallic components including vanadium components by heating the partially gasified coke in an oxidizing atmosphere at a temperataure below the fusion point of the metallic components.

Abstract: A combination slurry hydroconversion, coking and coke gasification process is provided wherein solid fines having an average particle size of less than 10 microns in diameter or the ashes thereof recovered from a gaseous product derived from the coke gasification are used as a catalyst in the hydroconversion stage in combination with a catalyst produced from an oil soluble metal compound in situ in the chargestock of the hydroconversion zone.

Abstract: A combination slurry hydroconversion, coking and coke gasification process is provided wherein solid fines having an average particle size of less than 10 microns in diameter or the ashes thereof recovered from a gaseous product derived from the coke gasification are used as a catalyst in the hydroconversion stage.

Abstract: The liquid product of a slurry hydrogen treating zone is separated into fractions in the same separation zone used to obtain the heavy hydrocarbonaceous oil fraction used as feed for the hydrogen treating zone. A separate portion of coarser solids is withdrawn from the hydrogen treating zone.

Abstract: A hydrocarbonaceous oil is introduced to a quench and scrubbing zone mounted on a fluid coking reactor. Heat from the coker vapor product vaporizes a portion of the hydrocarbonaceous oil. The unvaporized portion of the oil is used to quench and scrub the coker vapor product. The bottoms fraction of the quench and scrubbing zone is passed to a vacuum distillation zone to recover a heavy oil fraction and to produce a vacuum residuum for use as coker feed.

Abstract: A fluid coking process is provided in which a relatively large amount of hydrogen sulfide is added to the coker fluidizing gas. A preferred fluidizing gas is a mixture of hydrogen and hydrogen sulfide.

Abstract: This invention relates to a novel activated fluid coke composition, a method for forming same, and an improved process for removing organic material from waste water by contacting said waste water under adsorption conditions with said activated fluid coke. The activated fluid coke may be prepared by contacting fluid coke with a gaseous mixture containing steam at temperatures of at least about 1500.degree. F. for a period of time sufficient to convert at least 35 weight % of the fluid coke to gaseous products. The activated fluid coke so formed preferably has a total surface area of at least 400 square meters per gram, and a pore volume of at least 0.20 cubic centimeters per gram.

Abstract: A low sulfur coke product is obtained in an integrated fluid coking and gasification process in which an oxygen-containing gas is introduced into the upper portion of the gasification zone and steam is introduced into the lower portion of the gasification zone. The desired degree of coke desulfurization is controlled by controlling the thickness of the gasifier coke layer on the gaseous reactor leaving solids per pass.

Abstract: An oxidizing gas is injected through a nozzle into a bed of carbonaceous particles in a downward direction at an angle of declination at least as great as the angle of repose of the bed particles and at a gas inlet velocity of about 50 to 500 feet per second to supply the gas needed to fluidize the bed of carbonaceous particles.