Uop Lcc

Universal Oil Products Company

Jeffery C. Bricker

Laurence O. Stine

Thomas a. Verachtert

Robert R. Frame

Laurence O Stine

Robert R Frame

Jeffery C Bricker

Thomas A Verachtert

Steven C Gimre

Brian S Muldoon

Bipin Virpal Vora

Robert J Schmidt

Hayim Abrevaya

Christopher Naunheimer

Clayton Colin Sadler

Mary Jo Wier

Charles L Hemler

Anil Rajaram Oroskar

Paul T Barger

David A Lomas

Dennis J Ward

Harold U Hammershaimb

Carlos A Cabrera

Darrell W Staggs

Simon J Hamper

Mark E Reno

William H Munro

Charles L Hemler, Jr

Te-Yu M Chen

W Patrick Dennler

Joseph A Kocal

Lubo Zhou

James A Johnson

Leonid B Galperin

Lynn H Rice

Gregory J Thompson

Michael R Smith

Thomas R Fritsch

Daniel H Wei

Patrick S O'Neill

Margaret A Stine

Elena Z Maurukas

Timur V Voskoboinikov

Howard E Fullerton

Malek Y S Ibrahim

Steven I Richter

Robert L Zhou

Stevem C Gimre

A process of oxidative dehydrogenation in a fluidized riser reactor is described. Hydrocarbon feed and catalyst are fed to the bottom of the fluidized riser reactor. Part of the hydrogen produced in the dehydrogenation reaction is oxidized using oxygen introduced into the riser reactor through oxygen injection ports to produce the heat required for the dehydrogenation reaction.

Fluidized catalyst circulation reactor for paraffin oxydative dehydrogenation

One exemplary embodiment can be a hydroprocessing method. The hydroprocessing method can include providing a feed and a stream including hydrogen to a vessel. The vessel may have a catalyst collector and an internal riser. Generally, a catalyst circulates within the vessel by at least partially rising within the internal riser.

Hydroprocessing method, or an apparatus relating thereto

Systems and processes for the alkylation of a hydrocarbon are provided that utilize a plurality of moving bed radial flow reactors. An olefin injection point can be provided prior to each reactor by providing a mixer that mixes olefin with a hydrocarbon feed, or with the effluent stream from an upstream reactor, to produce a reactor feed stream. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed radial flow reactors can be stacked in one or more reactor stacks.

Solid catalyst hydrocarbon alkylation using stacked moving bed radial flow reactors

Systems and processes for hydrocarbon conversion are provided that utilize a plurality of moving bed reactors. The reactors may be moving bed radial flow reactors. Optional mixers that mix a portion of a second hydrocarbon feed with the effluent stream from an upstream reactor, to produce reactor feed streams may be employed, and the reactor feed streams may be introduced at injection points prior to each reactor. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed reactors can be stacked in one or more reactor stacks.

Solid catalyst hydrocarbon conversion process using stacked moving bed reactors

Systems and processes for the hydroprocessing of a hydrocarbonaceous feed are provided that utilize a plurality of moving bed reactors. The reactors may be moving bed radial flow reactors. A hydrogen injection point can be provided prior to each reactor by providing a mixer that mixes hydrogen with a hydrocarbonaceous feed, or with the effluent stream from an upstream reactor, to produce a reactor feed stream. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed reactors can be stacked in one or more reactor stacks.

Solid catalyst liquid phase hydroprocessing using moving bed reactors

Enhanced recovery of crude oil from an oil well is provided by in-situ cracking of an oxygenated organic compound to form hydrogen. The crude oil is then hydrogenated and hydrogenation reaction products and crude oil are recovered from the oil well.

Oil recovery by in-situ cracking and hydrogenation

An improved alkylation reactor design is disclosed. The design uses reactor effluent recycle to reduce the difference in temperature across the reaction zone improving selectivity and insuring the maintenance of a liquid phase in the reactor.

Alkylation reactor design with effluent recycle and impure benzene regeneration

A process is disclosed for regenerating a hydrocarbon conversion catalyst comprising zeolite L with ozone. The catalyst is contacted with ozone at a temperature of from about 20 to about 250&#xb0; C. and a concentration of ozone of from about 0.1 to about 5 mol-%. The catalyst may contain coke. The process at least partially restores the activity of the catalyst. The process is particularly useful for reforming and dehydrocyclodimerization catalysts.

Low-temperature regeneration of zeolite L using ozone

A process for the production of C alkenes with high selectivities to 2,4,4-trimethylpentene by the oligomerization of isobutene and/or n-butene at lower temperatures is disclosed. Higher proportions of heavy paraffins mixed with the butene feed in the oligomerization zone improve the selectivity to 2,4,4-trimethylpentene along with better selectivity to octene and lower selectivity to dodecene. Additionally, we have found that n-butene codimerizes with isobutene selectively to 2,4,4-trimethylpentene.

Process for oligomer production and saturation

A hybrid reactor arrangement provides a reactive design that achieves higher acrylonitrile yield and lower catalyst circulating rate. The hybrid reactor design first passes a mixture of reactants and catalyst through a circulating bubbling bed reaction section. Heat exchange coils or other cooling medium in the bubbling bed reactor section maintain temperature in a range that will maximize the selectivity of reactants to the acrylonitrile product. The bubbling bed reactor section provides the initial conversion of the reactant. A circulating fluidized bed reaction zone finishes the conversion of reactants to a high yield under conditions that reduce the occurrence of secondary reactions that could otherwise produce unwanted by-products. The circulating fluidized bed reactor section maintains nearly plug flow conditions that allow continued conversion of unreacted feed components through primary reactions while limiting the time for secondary reactions to continue and diminish the final yield of products. Selectivity and conversion may also be improved by sequential addition of oxygen into the CFB reaction section. The sequential addition of oxygen may occur by the direct injection of an oxygen-containing gas or by the delivery of re-oxidized catalyst particles that are fully recharged with the lattice oxygen necessary for the reaction. Through this method the hybrid reactor provides the typical 5% improvement of higher acrylonitrile product yield from CFB-type reaction zones while reducing the required catalyst circulation by a factor of 10 or more.

Reaction process in hybrid reactor for propylene ammoxidation

A process for the production of C,and higher carbon number alkene oligomers by the oligomerization of light olefins to heavier olefins is improved by the addition of heavy paraffins to the oligomerization zone. The recycle of the heavy paraffins extends the catalyst activity and improves the catalyst life. The non-reactive paraffin stream may be recycled through the process with minimal losses and make-up.

An FCC apparatus places a quench chamber above a reactor vessel and a hot stripper below a reactor vessel to provide a progressively decreasing temperature profile up the structure of the FCC arrangement and equipment for sequential reaction control. A riser contains the primary catalytic reactions of the hydrocarbon vapor and delivers the reacted vapors to the reactor structure. Starting from the bottom of the structure the hot stripper has the highest temperature and desorbs or displaces hydrocarbons from the catalyst to terminate long residence time catalytic reactions. Above the hot stripper bulk separation equipment divides the main vapor and catalyst stream to limit residence time of major catalytic reactions. At a yet higher elevation and lower internal temperature quench equipment arrests thermal reactions of the vapor stream. This structure arrangement permits reliable control of reaction time to obtain desired products and enhances mechanical reliability of the structure.

FCC reactor arrangement for sequential disengagement and progressive temperature reduction

A process for the production of C.sub.8 and higher carbon number alkene oligomers by the oligomerization of light olefins to heavier olefins is improved by the addition of heavy paraffins to the oligomerization zone. The recycle of the heavy paraffins extends the catalyst activity and improves the catalyst life. The non-reactive paraffin stream may be recycled through the process with minimal losses and make-up.

A process for the production of C.sub.8 and higher olefins by the oligomerization of light olefins to heavier olefins is improved by the addition of cycloparaffins to the oligomerization zone. The recycle of the cycloparaffins extends the catalyst activity and improves the catalyst life. Cyclohexane provides an excellent solvent for removing deposits from the catalyst with chemical inertness to the process and a boiling range that allows its essentially complete recovery when producing nonenes and higher olefins from propylene feeds.

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Western Springs, IL, United States of America

Laurence O Stine