Uop Lcc

Tamotsu Imai

Hayim Abrevaya

Joseph A Kocal

Jeffery C Bricker

Paul T Barger

Edwin H Homeier

Chi-Wen Hung

Bipin Virpal Vora

David E Mackowiak

Deng-Yang Jan

Robert J Schmidt

Christopher D Gosling

Mark J O'Hara

Paul J Kuchar

Robert R Frame

Paula L Bogdan

Gregory J Thompson

Raymond R Herber

Alan R Dodds

Maureen L Bricker

Peter R Pujado

Tai-Hsiang Chao

Harold U Hammershaimb

Carlos A Cabrera

Lisa M Lane

Peter J Pujado

Catherine E Guzolek

Anthony H Eck

A process for the desulfurization of hydrocarbonaceous oil wherein the hydrocarbonaceous oil is contacted with a hydrodesulfurization catalyst in a hydrodesulfurization reaction zone to reduce the sulfur level to a relatively low level and then contacting the resulting hydrocarbonaceous stream from the hydrodesulfurization zone with an oxidizing agent to convert the residual, low level of sulfur compounds into sulfur-oxidated compounds. The resulting hydrocarbonaceous oil stream containing the sulfur-oxidated compounds is separated after decomposing any residual oxidizing agent to produce a stream containing the sulfur-oxidated compounds and a hydrocarbonaceous oil stream having a reduced concentration of sulfur-oxidated compounds.

Process for the desulfurization of a hydrocarbonaceous oil

A novel catalyst and the use thereof in a reforming process is disclosed. The dual-function catalyst comprises a refractory inorganic oxide, indium, Group IVA(IUPAC 14) metal, and a platinum-group metal concentrated in the surface layer of each catalyst particle. Utilization of this catalyst in the conversion of hydrocarbons, especially in reforming, results in significantly improved selectivity to the desired gasoline or aromatics product.

Process for reforming NAPHTHA feedstock using selective

A process for separating 1,3-butadiene from a crude C.sub.4 stream containing butanes, butenes, butadienes and acetylenes has been developed. The process begins with introducing hydrogen, a solvent, and the crude C.sub.4 stream to a catalytic extractive distillation unit having a reaction zone containing a catalyst capable of hydrogenating acetylenes. Butanes and butenes, being less soluble in the solvent, are distilled in an overhead stream from the catalytic extractive distillation unit. Butadienes and acetylenes, being more soluble in the solvent, are carried with the solvent to the reaction zone located within the catalytic extractive distillation unit. In the reaction zone the acetylenes are converted to hydrogenation products. The hydrogenation products other than butadiene are separated from the butadienes by the extractive distillation occurring in the unit. The solvent and butadiene mixture is removed from the catalytic extractive distillation unit in a distillate stream. The distillate stream is then introduced to a solvent stripping column to separate by distillation a solvent bottoms stream from a butadiene overhead stream. The butadiene overhead stream is introduced to a butadiene distillation column to separate a 1,3-butadiene overhead stream from a 1,2-butadiene bottoms stream. The solvent bottoms stream may be purified and recycled to the catalytic distillation unit.

1,3-Butadiene separation from a crude C.sub.4 stream using catalytic

Selective multimetallic-multigradient reforming catalyst

An improved process for the catalytic dehydrogenation of paraffinic hydrocarbons is disclosed. Feed paraffinic hydrocarbons are dehydrogenated by means of contacting the dehydrogenatable hydrocarbon with a dehydrogenation catalyst in a first dehydrogenation zone wherein the endothermic dehydrogenation reaction reduces the temperature of the resulting hydrocarbon stream containing dehydrogenated hydrocarbon compounds. The resulting effluent from the preceding dehydrogenation zone is then contacted with a hot hydrogen-rich gaseous stream having a temperature greater than the hydrocarbon stream to increase the temperature of the hydrocarbon stream and then the resulting heated stream is introduced into a subsequent dehydrogenation zone to produce additional dehydrogenated hydrocarbon compounds.

Process for the dehydrogenation of paraffinic hydrocarbons

An etherification process combines an alkylation zone with a skeletal olefin isomerization zone in an arrangement that rejects isoalkanes and normal alkanes with only minor loss of valuable olefin isomers. The invention also provides a balanced feed to an alkylation zone for the production of high octane gasoline components. This invention can be used to provide ethers and gasoline boiling range alkylates from either C.sub.4 or C.sub.5 feedstocks. The invention fully utilizes all olefin isomers improve octane and vapor pressure charactristics of the gasoline components.

Balanced alkylation feed from etherification and isomerization

An improved process for the catalytic dehydrogenation of paraffinic hydrocarbons is disclosed. Feed paraffinic hydrocarbons are dehydrogenated by means of contacting the dehydrogenatable hydrocarbon with a dehydrogenation catalyst in a first dehydrogenation zone wherein the endothermic dehydrogenation reaction reduces the temperature of the resulting hydrocarbon stream containing dehydrogenated hydrocarbon compounds. The resulting effluent from the first dehydrogenation zone is then contacted with a hot hydrogen-rich gaseous stream having a temperature greater than the hydrocarbon stream to increase the temperature of the hydrocarbon stream and then introducing the resulting heated stream into a second dehydrogenation zone to produce additional dehydrogenated hydrocarbon compounds.

A combination of an etherification process and a process for the isomerization of linear alkenes to isoalkenes uses an adsorptive separation zone for olefin and paraffin separation upstream of the MTBE unit to reduce olefin losses associated with the rejection of butanes. The location of the MTBE unit downstream of the adsorptive separation zone facilitates the essentially complete removal of isobutane from the process. Supplemental rejection of isobutane downstream of the adsorptive separation permits the use of low purity adsorptive separation zone and also allows the recovery of a high purity butene-1 product.

Alkane rejection in C.sub.4 etherification and isomerization process

A process for converting C.sub.2 to C.sub.6 aliphatic hydrocarbons to aromatics is described. The process uses a catalyst which contains a zeolite, an aluminum phosphate binder and a gallium component. Examples of zeolites which can be used are the ZSM family of zeolites, with ZSM-5 being a specific example. The catalyst is characterized in that it is tolerant to exposure to hydrogen at temperatures of about 500.degree. to about 700.degree. C. The catalyst's tolerance to hydrogen exposure is the result of treating the catalyst with an aqueous solution of a weakly acidic ammonium salt or a dilute acid solution at a temperature of about 50.degree. to about 100.degree. C. for a time of about 1 to about 48 hours, followed by calcination.

Process for producing aromatic compounds from C2-C6 aliphatic

This invention relates to a process for reactivating a dehydrocyclodimerization catalyst. Dehydrocyclodimerization catalysts which contain an aluminum phosphate binder can be deactivated when they are exposed to hydrogen at temperatures above 500.degree. C. The instant process restores substantially all of the catalyst's lost activity. The process involves treating the catalyst with an aqueous solution of a weakly acidic ammonium salt or a dilute acid solution at a temperature of about 50.degree. to about 100.degree. C. for a time of about 1 to about 48 hours. An ammonium nitrate solution is preferred. Next the catalyst is calcined at a temperature of about 500.degree. to about 700.degree. C. for a time of about 1 to about 15 hours to provide a reactivated catalyst. The catalyst can be reactivated several times using this process.

Process for reactivating a deactivated dehydrocyclodimerization catalyst

A catalyst for converting C.sub.2 to C.sub.6 aliphatic hydrocarbons to aromatics is described. The catalyst contains a zeolite, an aluminum phosphate binder and a gallium component. Examples of zeolites which can be used are the ZSM family of zeolites, with ZSM-5 being a specific example. The catalyst is characterized in that it is tolerant to exposure to hydrogen at tempertures of about 500.degree. to about 700.degree. C. The catalyst's tolerance to hydrogen exposure is the result of treating the catalyst with an aqueous solution of a weakly acidic ammonium salt or a dilute acid solution at a temperature of about 50.degree. to about 100.degree. C. for a time of about 1 to about 48 hours, followed by calcination. A process for preparing the catalyst is also described.

Catalyst and process for producing aromatic compounds from C.sub.2 -C.sub.6

Methane is upgraded to higher molecular weight hydrocarbons in a process using a novel catalyst comprising oxides of boron, tin and zinc. The feed admixture also comprises oxygen. The novel catalyst may comprise one or more Group I-A or II-A elements, preferably potassium and is characterized by its method of manufacture.

Process and catalyst for upgrading methane to higher carbon number

Alkyl aromatic compounds may be prepared by reacting an aromatic compound such as benzene with an alkylating agent such as an olefin or alkyl halide in the presence of an alkylation catalyst. The alkylation catalyst of the present invention comprises a clay which has been coextruded with a multi-valent metal and preferably a metal selected from the group consisting of Groups IIIA, IIIB and IVB of the Periodic Table. The resultant extrudate is then impregnated with a dissimilar multi-valent metal selected from the above named groups followed by calcination to form the desired composite. By utiilzing this catalytic composite in an alkylation reaction it is possible to obtain improved yields of alkyl aromatic compounds which may then be used in the preparation of biodegradable detergents.

Production of alkyl aromatic compounds

Catalyst particles which are employed in reactions involving the conversion of organic compounds should possess a desired configuration in order to maintain a desired voidage which will permit passage of the feedstock through the catalyst bed during the conversion reaction. Solid phosphoric acid catalysts which comprise an admixture of an acid of phosphorus and a solid binder such as a siliceous material may be formed into polylobular, tubular, ridged, fluted, or channeled cylindrical particles which will permit a sufficient amount of voidage in the catalyst bed to be maintained even though the catalyst particles will swell during the reaction due to the formation of coke on the surface thereof.

Shaped catalyst particles utilizable for the conversion of organic

Hydrogen sulfide can be conveniently removed from streams containing up to about 1,000 ppm of H.sub.2 S by reacting the latter with an olefin using a bed of an acidic solid catalyst in a non-oxidative process for the removal of hydrogen sulfide. The reaction can be effected under relatively mild conditions and is very selective for the removal of hydrogen sulfide without being attended by other unwanted reactions such as oligomerization, disproportionation, and skeletal rearrangement. Levels of hydrogen sulfide in the treated product of no more than about 5 ppm can be readily attained using a broad variety of acidic solid catalysts and unsaturated hydrocarbons, especially olefins.

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Mt. Prospect, IL, United States of America

Tamotsu Imai