Texaco Inc.

Paul H Lewis

Eugene P Dai

Edward H Holst

Joseph A Durkin

Joseph A Froelich

James C Vartuli

Tansukhlal G Dorawala

Gerald V Nelson

Russell R Reinhard

A composition of matter, useful for removing sulfur oxides from gases, comprising a porous refractory support bearing as a first component (i) at least one component containing bismuth, chromium, or a rare earth, said first component being in the form of crystals of oxide of crystal size less than about 90 Angstrom units, and as second component at least one alkali metal--a typical composition containing 0.6 w % K and 4.8 w % Ce on alumina, the Ce being present as cystals of CeO.sub.2 of particle size of about 66 Angstrom units.

Catalyst for control of emission of sulfur oxides

Isomerization is effected at improved conversion and selectivity by use of a 0.5 w %-2.5 w % platinum-palladium group metal on hydrogen mordenite catalyst, the catalyst having been calcined at 1200.degree. F.-1500.degree. F. prior to use whereby it acquires activated sites not present in mordenite calcined at lower temperature.

Process of preparing a catalyst containing activated isomerization sites

A catalyst composition for catalytic cracking contains a catalytic cracking catalyst and 1-10 weight %, of the total, of additive containing a porous refractory support bearing 0.5-10 weight % of at least one of bismuth, chromium or a rare earth metal and 0.4-10 weight % of an alkali metal.

Catalyst composition for catalytic cracking

Sulfur oxides are removed from gases by contact with a composition containing potassium and cerium on alumina, the cerium being present in the form of crystals of oxide of crystal size below about 90 Angstrom Units.

Control of SO.sub.x emission

Sulfur oxides are removed from gases by contact with a composition containing 3 w % potassium and 3 w % cerium or alumina.

Catalytic dewaxing is effected with reduced coking by use of catalyst containing 0.5 w %-2.5 w % platinum-palladium group metal on hydrogen mordenite, the catalyst having been calcined at 1200.degree. F.-1600.degree. F. prior to use whereby it acquires activated sites (not present in mordenite products calcined at lower temperature) which are retained under anhydrous conditions.

Process for catalytic dewaxing with mordenite

Process for dewaxing with mordenite

Isomerization is effected at improved conversion and selectivity by use of a 0.5 w %-2.5 w % platinum-palladium group metal on hydrogen mordenite catalyst, silica to alumina mole ratio in the range of 10:1 to 20:1, the catalyst having been calcined at 1200.degree. F.-1500.degree. F. prior to use whereby it acquires activated sites not present in mordenite calcined at lower temperature.

Hydrocarbon isomerization

A method for separating straight chain hydrocarbons from a hydrocarbon fraction having straight chain hydrocarbons, nonstraight chain hydrocarbons, and a sulfur compound, includes the steps of contacting the hydrocarbon fraction with a 5A zeolite having crystals of an average size larger than about 700 angstroms which selectively absorbs the straight chain hydrocarbons to the substantial exclusion of the nonstraight chain hydrocarbons and sulfur compound. Large zeolite crystals are found to have a much longer useful life in this separation method than zeolite crystals having an average size of less than about 700 angstroms as measured along one edge of the zeolite crystal. The hydrocarbon fraction has more than about 800 wppm total sulfur including more than about 15 wppm mercaptan.

Method for separating straight chain hydrocarbons using zeolites having

An improved process for fluid catalytic cracking or hydrocarbons employing a Y zeolite in a silica-alumina matrix and containing from about 0.1 to about 5 weight percent fluorine. The catalyst is prepared by contacting a Y zeolite in a silica-alumina matrix with an aqueous solution of a fluorine compound, preferably an aqueous solution of hydrogen fluoride, for a period of 16 to 24 hours, followed by drying and calcining the resultant fluorided cracking catalyst. The process of cracking hydrocarbons with these catalysts produces improved yields of motor fuel fractions of improved octane number as compared with processes employing unfluorided cracking catalysts.

Catalytic cracking process

An improved cracking catalyst prepared by treating a metallic reforming catalyst with an aqueous solution containing a fluorine compound, drying and calcining the fluorided catalyst, and then physically mixing the fluorided catalyst with a zeolite-containing cracking catalyst. The composite yields higher octane products than conventional cracking catalysts.

Fluorided composite catalyst

An improved zeolite-containing cracking catalyst prepared by treating a zeolite-containing cracking catalyst with an aqueous solution containing a fluorine compound, drying and calcining the fluorided catalyst. In a preferred embodiment, the fluorinating solution is an aqueous solution of hydrogen fluoride. The fluorided catalyst may be used per se as a cracking catalyst, or may be physically mixed with a metallic reforming catalyst for use as a cracking catalyst. The fluorided cracking catalysts exhibit improved activity and yield higher octane products than unfluorided cracking catalysts.

Fluorided cracking catalyst

Alkylaromatic hydrocarbons are steam dealkylated in the presence of catalyst, typically containing oxides of nickel, potassium, chromium and aluminum, and particularly characterized by the presence of free nickel metal having a metallic surface area of preferably at least about 8 square meters per gram of catalyst.

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Groves, TX, United States of America

Paul H Lewis