Abstract: In a fluid catalytic cracking process, the regeneration temperature can be eliminated as an operating constraint, catalyst losses can be held constant or reduced, carbon on regenerated catalyst can be reduced and the coke burning capacity of the regenerator can be increased by the combination of cooling the hot regenerated catalyst and increasing the oxygen content of the inlet regeneration air.

Abstract: Sulfur oxides are removed from a gas by an absorbent which comprises alumina in association with free or combined lanthanum, wherein the ratio by weight of alumina to lanthanum is from about 0.1 to about 30,000. Absorbed sulfur oxides are recovered as a sulfur-containing gas comprising hydrogen sulfide by contacting the spent absorbent with a hydrocarbon in the presence of a hydrocarbon cracking catalyst at a temperature from about 375.degree. to about 900.degree. C. The absorbent can be circulated through a fluidized catalytic cracking process together with the hydrocarbon cracking catalyst to reduce sulfur oxide emissions from the regeneration zone.

Abstract: A hydrocracking process is provided in which the heavy bottoms fraction recovered from the hydrocracked product is heat treated prior to being recycled to the hydrocracking zone. The resulting hydrocracked product has an increased amount of constituents boiling in the middle distillate range.

Abstract: In processes for the catalytic treatment of hydrocarbon feedstream containing organic sulfur comprising contacting said feedstream with a catalyst for a time at a temperature and pressure sufficient to effect the desired catalytic change on the feedstream, the improvement comprising using as the catalyst a layered composition of the formula MX.sub.y wherein M is a transition metal selected from the group consisting of Group IVb, Vb, VIb, VIIb and uranium, X is a chalcogen selected from the group consisting of sulfur, selenium, tellurium, and mixtures thereof, y is a number ranging from about 1.5 to about 3. The catalyst is prepared by reacting neat or in the presence of a nonaqueous solvent a Group IVb to VIIb or uranium metal salt, and a source of sulfide, selenide or telluride ions, and mixing the reactants at temperatures below 400.degree. C. and at atmospheric pressures.

Abstract: Octane and total yield improvement in catalytic cracking processes can be attained by the addition to conventional cracking catalysts of very small amounts of additive catalyst comprising a class of zeolites characterized by a silica to alumina mole ratio greater than about 12 and a constraint index of about 1 to 12. The additive catalyst is added to the conventional cracking catalyst in the cracking process in an amount which provides the zeolite component of the additive catalyst at from about 0.01 weight percent to about 1.0 weight percent of the conventional cracking catalyst in the cracking process.

Abstract: The regeneration of cracking catalyst containing both manganese and antimony in a temperature range of 1260.degree.-1280.degree. F. has been found to result in unexpected sharp maximum of the CO.sub.2 /CO ratio in the regenerator off-gas.

Abstract: Efficient utilization of hydrogen in a hydrocracking system is obtained by recovering in a first gas-liquid separation zone hydrogen by gas-liquid separation of hydrocrackate at a pressure of at least about 75 percent of the pressure in the hydrocracking zone, and recovering in a second gas-liquid separation zone hydrogen from the separated liquid phase from the first gas-liquid separation zone, said second gas-liquid separation zone being at a pressure less than 75 percent of the pressure in the first gas-liquid separation zone and at conditions sufficient to provide a separated vapor phase containing at least about 50 volume percent of hydrogen and having a hydrogen partial pressure of at least about 20 atmospheres. At least a portion of the separated vapor phase from the second gas-liquid separation zone is contacted with the feed side of a polymeric membrane exhibiting a high selectivity to the permeation of hydrogen as compared to the permeation of methane. The opposite side, i.e.

Abstract: A process for upgrading a heavy hydrocarbonaceous oil is provided in which the oil is hydrorefined, heat-treated and hydrocracked to increase the selectivity of the hydrocracked product to components boiling in the range of 350.degree. to 675.degree. F.

Abstract: A hydrocarbon cracking catalyst is treated with zinc to passivate contaminant metals, e.g., nickel, copper, vanadium, and iron, which are deposited on the catalyst during the catalytic cracking of hydrocarbon feedstocks.

Abstract: Heavy carbonaceous liquid having a melting point below 250.degree. C. is upgraded to lighter products by hydrogen donor solvent cracking, using recycled solvent derived at least in part from a middle distillate fraction of either the heavy carbonaceous liquid or from the cracked products which is subjected to one or more catalytic hydroprocessing steps before recycling.

Abstract: The invention relates to a process to improve the stability of a catalyst to be used for lowering the cloud or turbidity point and the filterability limit temperature of gas-oils.The catalyst is formed of a composite system constituting 5 to 90% of a hydrodesulfuration type catalyst A and 95 to 10% of a hydroconversion type catalyst B, these two catalysts being either mixed or superposed, in which case catalyst A forms the top of the catalytic bed.

Abstract: This invention provides a process for upgrading a heavy hydrocarbon oil to motor fuel products.The heavy hydrocarbon oil is admixed with a metal halide catalyst and a solvent component under supercritical conditions to form (1) a dense-gas solvent phase which contains refined hydrocarbon crackate, and which is substantially free of metal halide catalyst content; and (2) a residual asphaltic phase.

Abstract: A hydrocrackate from a hydrocracking zone operating under hydrocracking conditions is separated into at least one liquid phase and a separated vapor phase wherein the separated vapor phase has a greater concentration of hydrogen than the minimum concentration of hydrogen in the vapor phase in the hydrocracking zone. At least a portion of the separated vapor phase is contacted with the feed side of a polymeric membrane selective to the permeation of hydrogen as compared to the permeation of methane, and the opposite side of the polymeric membrane is maintained at a pressure sufficiently below the pressure at the feed side of the polymeric membrane to permeate hydrogen to the opposite side of the polymeric membrane and to provide a hydrogen permeate having a concentration of hydrogen greater than the concentration of hydrogen in the separated vapor phase and greater than the concentration of hydrogen in the hydrogen feed gas. The hydrogen permeate is compressed and recycled to the hydrocracking zone.

Abstract: A two-step process for dewaxing and stabilizing hydrocracked lubricating oil stocks is disclosed. High-silica zeolite produces catalytic dewaxer effluent containing lower olefins for favorable stabilizing (alkylation) reactions by contact with acidic catalyst substantially free of hydrogenation activity.

Abstract: An improved catalytic dewaxing process using a CZH-5 zeolite having a hydrogenation component is disclosed.

Abstract: A process is disclosed for converting hydrocarbons with a particulate catalyst containing a crystalline solid which has pore openings and maximum cage dimensions of 5.5-7.0 Angstroms; an active metal with both dehydrogenation activity and oxidation activity is disposed within the interior of crystals of the crystalline solid; the catalyst is cycled between a reactor and a regenerator, and the active metal is used for (1) selectively dehydrogenating paraffins and aromatizing aliphatics in the reaction zone while large-diameter coke-forming hydrocarbons are inhibited from contacting the metal, (2) facilitating catalyst regeneration by accelerating combustion of carbon from within the pores of the crystalline solid in the regenerator, so as to assure very low residual carbon levels within the crystalline solid in regenerated catalyst; and (3) oxidizing carbon monoxide in the regenerator to make available additional heat to compensate for endothermic conversion reactions in the cracking reactor.

Abstract: A process for fluid catalytic cracking of a starting oil selected from the group consisting of a distillation residual oil, a solvent deasphalted oil derived therefrom and a hydrodesulfurized oil derived therefrom, which comprises withdrawing a part of catalyst particles circulating through a fluid catalytic cracking unit, sending the withdrawn catalyst particles by means of a carrier fluid selected from the group consisting of air, nitrogen, steam and the mixtures thereof at a rate of 0.01 to 100 meters/second in a particle concentration of 0.

Abstract: Yields of liquid product produced by coking a feed material comprising a mixture of a shale oil material, a petroleum residuum and a hydrocracking catalyst, are enhanced by feeding hydrogen to the reaction system during the coking operation.

Abstract: A waxy fuel oil that contains a catalytically deleterious contaminant is treated with a crystalline zeolite under sorption conditions followed by catalytic dewaxing with a crystalline zeolite exemplified by ZSM-5 to produce dewaxed fuel oil and high octane gasoline.

Abstract: This invention is concerned with removing metals and sulfur from oil, preferably from residual oil, by contact with a novel catalyst. Said catalyst comprises a Group VIII metal and a Group VI metal deposited within an amorphous porous glass support of controlled pore size distribution.