Abstract: Sulfur oxides are removed from a gas with absorbents and then are removed from the absorbents by contact with a hydrocarbon in the presence of a cracking catalyst. The absorbents comprise an exhaustively-exchanged rare-earth-form zeolite and a free form of an inorganic oxide selected from the group consisting of the oxides of aluminum, magnesium, zinc, titanium, and calcium. The sulfur oxides are removed from the absorbents as a sulfur-containing gas which comprises hydrogen sulfide.

Abstract: Sulfur oxides are removed from a gas by an absorbent comprising at least one inorganic oxide selected from the group consisting of the oxides of aluminum, magnesium, zinc, titanium, and calcium in association with at least one free or combined rare earth metal selected from the group consisting of lanthanum, cerium, praseodymium, samarium, and dysprosium, wherein the ratio by weight of inorganic oxide or oxides to rare earth metal or metals 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: 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 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: There is disclosed a catalyst, which catalyst comprises a physical particle-form mixture of a Component A and a Component B, said Component A comprising one or more Group VIII noble metals and a combined halogen deposed on a refractory inorganic oxide and said Component B comprising a metal from Group IVB or Group VB of the Periodic Table of Elements and a combined halogen deposed on a refractory inorganic oxide. Such catalyst is suitable for use in a hydrocarbon conversion reaction zone.The catalyst can be employed in a process for the reforming of a hydrocarbon stream, which process comprises contacting said stream in a reaction zone under reforming conditions and in the presence of hydrogen with said catalyst. The catalyst is not presulfided. A preferred process comprises contacting a hydrocarbon stream that contains a substantial amount of sulfur.

Abstract: An improved fluid catalytic cracking process comprises a method for the regeneration of the fluidizable hydrocarbon conversion catalyst, particularly of the molecular sieve type, which has been deactivated with coke deposits while employed in a hydrocarbon catalytic cracking process, in which the coke-containing hydrocarbon conversion catalyst is contacted with an oxygen-containing gas to burn the coke from the catalyst under conditions providing substantially complete combustion of carbon monoxide and substantially complete combustion of the coke on the catalyst. In the regenerator, particles of the hydrocarbon conversion catalyst are in association with particles of a platinum group metal or rhenium oxidation catalyst which promotes the combustion of carbon monoxide to carbon dioxide. The catalyst composite contains a mixture of cracking catalyst particles and particles having the platinum group metal or rhenium oxidation catalyst supported on a substrate.

Abstract: An improved fluid catalytic cracking process comprises a method for the regeneration of the fluidizable hydrocarbon conversion catalyst, particularly of the molecular sieve type, which has been deactivated with coke deposits while employed in a hydrocarbon catalytic cracking process, in which the coke-containing hydrocarbon conversion catalyst is contacted with an oxygen-containing gas to burn the coke from the catalyst under conditions providing substantially complete combustion of carbon monoxide and substantially complete combustion of the coke on the catalyst. In the regenerator, particles of the hydrocarbon conversion catalyst are in association with particles of a platinum group metal or rhenium oxidation catalyst which promotes the combustion of carbon monoxide to carbon dioxide. The catalyst composite contains a mixture of cracking catalyst particles and particles having the platinum group metal or rhenium oxidation catalyst supported on a substrate.

Abstract: Process for disproportionation of petroleum hydrocarbons which comprises contacting in a reaction zone said petroleum hydrocarbon under suitable disproportionation conditions with a catalytic composition comprising a tungsten/molybdenum component, said tungsten/molybdenum component deposited upon an acidic cracking component comprising a mordenite large pore crystalline aluminosilicate material and a refractory inorganic oxide.

Abstract: A novel catalyst for the oxidation of butane to produce maleic anhydride comprising a phosphorus and vanadium mixed oxide promoted by zinc wherein the catalyst is prepared by using an organic medium and has two specific phases identified by characteristic X-ray pattern. A process for the manufacture of maleic anhydride from butane feedstock utilizing the novel catalyst.

Abstract: A hydrocarbon conversion catalyst system comprising a mixture of a first catalyst containing a noble metal component deposed on a refractory inorganic oxide and a second catalyst containing a non-noble metal component deposed on a support containing a refractory inorganic oxide and a crystalline aluminosilicate material, and a reforming method employing such catalyst system are disclosed.

Abstract: There is disclosed a catalyst, which catalyst comprises a physical particle-form mixture of a Component A and a Component B, said Component A comprising at least one Group VIII noble metal deposed on a solid catalyst support material providing acidic catalytic sites and said Component B comprising rhenium or a compound of rhenium deposed on a solid catalyst support material, said catalyst having been prepared by thoroughly blending finely-divided particles of Component A and Component B to provide a thoroughly-blended composite, said finely-divided particles having a particle diameter that is less than 100 mesh (150 microns), and forming said composite into particles having a size that is greater than 100 mesh (150 microns) and being suitable for use in a hydrocarbon conversion reaction zone.

Abstract: There is disclosed a catalyst, which catalyst comprises a physical particle-form mixture of a Component A and a Component B, said Component A comprising at least one Group VIII noble metal deposed on a solid catalyst support material providing acidic catalytic sites and said Component B comprising rhenium or a compound of rhenium deposed on a solid catalyst support material, said catalyst having been prepared by thoroughly blending finely-divided particles of Component A and Component B to provide a thoroughly-blended composite, said finely-divided particles having a particle diameter that is less than 100 mesh (150 microns), and forming said composite into particles having a size that is greater than 100 mesh (150 microns) and being suitable for use in a hydrocarbon conversion reaction zone.

Abstract: A hydrocarbon conversion catalyst comprising at least one platinum-group metal deposited on a composite comprising (I) alumina and (II) rhenium deposited on silica. The catalyst eliminates the need for presulfiding treatment required by conventional rhenium-promoted catalyst in reforming service, without comparative loss in reforming performance.

Abstract: A method for hydroconversion of coal solids in a solvent by contact with molecular hydrogen and catalyst solids in a reactor. The catalyst solids are catalytically active substances including promoted or unpromoted molybdenum on an alumina support material. The support is characterized by bimodal pore distribution with the average diameter of the smaller pores ranging from about 100-200 angstroms and preferably 120-140 angstroms, and average diameter of the larger pores being in excess of 1,000 angstroms.

Abstract: An improved process for the reforming of a hydrocarbon stream, which process comprises contacting said hydrocarbon stream under reforming conditions and in the presence of hydrogen with a catalyst which comprises platinum, rhenium, a small amount of palladium, and combined halogen on a refractory inorganic oxide, such as an alumina, and which has not been presulfided. The improvement comprises a rhenium-containing catalyst which has not been presulfided and which contains a small amount of palladium, i.e., about 0.05 wt. % to about 1 wt. % palladium. The feedstock being reformed can contain up to about 50 ppm sulfur.

Abstract: A method for hydroconversion of coal solids in a solvent by contact with molecular hydrogen and catalyst solids in a reactor. The catalyst solids are catalytically active substances including promoted or unpromoted molybdenum on an alumina support material. The support is characterized by bimodal pore distribution with the average diameter of the smaller pores ranging from about 100-200 angstroms and preferably 120-140 angstroms, and average diameter of the larger pores being in excess of 1,000 angstroms.

Abstract: Isomerization process for petroleum light hydrocarbons with a boiling point within the range of from about 100.degree. F. (38.degree. C.) to about 210.degree. F. (99.degree. C.) wherein said process comprises contacting said hydrocarbons with a catalyst consisting essentially of an ultrastable, large pore crystalline zeolite aluminosilicate material containing less than 1 (wt)% alkali metal and characterized by well-defined hydroxyl infra-red bands and a maximum unit cubic cell dimension of 24.55 A and a metal component selected from the metals, oxides or sulfides of the Group VIII elements of the Periodic Table, under suitable isomerization conditions.

Abstract: The process comprises contacting a hydrocarbon feedstock containing a substantial amount of organic nitrogen-containing compounds in a first reaction zone under hydrocracking conditions and in the presence of hydrogen with a first catalyst comprising nickel and molybdenum or nickel and tungsten, their oxides, and/or their sulfides on a co-catalytic acidic cracking support comprising ultrastable, large-pore crystalline alumino-silicate material and a silica-alumina matrix to produce a first hydrocracked effluent and contacting said first hydrocracked effluent in a second reaction zone under hydrocracking conditions and in the presence of hydrogen with a second catalyst comprising cobalt and molybdenum, their oxides, and/or their sulfides on a co-catalytic acidic cracking support comprising ultrastable, large-pore crystalline aluminosilicate material and a silica-alumina matrix to produce a second hydrocracked effluent.

Abstract: Catalyst comprising magnesium oxide and aluminum oxide is prepared by dry blending particulate alumina with a dried composite of magnesia impregnated with hydrogenation metals of Group VIB and Group VIII; the catalyst is employed in selective hydrodesulfurization of cracked naphtha.

Abstract: Ethyl aromatics contained in the C.sub.9 aromatic fraction from fractionated reformate are selectively converted to xylenes via ethyl scission in the presence of a catalyst comprising a carrier of highly purified gamma alumina containing essentially no silica and of a surface area of at least 100 m.sup.2 /g and a metal selected from the group consisting of a Group VIII metal and a Group VIII metal promoted with zinc.