Mobil Oil Corporation

Werner O Haag

Weldon K Bell

Tracy J Huang

Darrell D Whitehurst

David H Olson

Mohsen N Harandi

Hartley Owen

Rudolph M Lago

Nai Y Chen

Paul G Rodewald, Jr

Donald J Klocke

John G Tsikoyiannis

Jose G Santiesteban

Albin Huss, Jr

Garry W Kirker

Paul B Weisz

Daria N Lissy

Tsoung Y Yan

Ralph M Dessau

John Scott Buchanan

Ernest W Valyocsik

David O Marler

David S Shihabi

Jane C Cheng

Stephen S Wong

Lewis B Young

Dominick N Mazzone

Robert A Ware

Hye Kyung Timken

Roger A Morrison

Chaya R Venkat

Reuel Shinnar

Robert E Palermo

Minas R Apelian

Roland H Heck

James C Kuo

Anthony S Fung

Charles M Sorensen

Iraj I Rahmim

Norman J Rouleau

Iraj Rahmin

David G Freyman

James W Kuo

This is a process for upgrading a petroleum naphtha fraction. The naphtha is subjected to reforming and the reformate is cascaded to a benzene and toluene synthesis zone over a benzene and toluene synthesis catalyst comprising a molecular sieve of low acid activity. The preferred molecular sieve is steamed ZSM-5. The benzene and toluene synthesis zone is operated under conditions compatible with the conditions of the reformer such as pressures of above about 50 psig (446 kPa) and temperatures above about 800.degree. F. (427.degree. C). In one aspect of the invention, the benzene and toluene synthesis catalyst includes a metal hydrogenation component such as cobalt, nickel, platinum or palladium. In one mode of operation, the benzene and toluene synthesis catalyst replaces at least a portion of the catalyst of the reformer. The process produces a product containing an increased proportion of benzene and toluene, and a reduced proportion of C8 aromatics, particularly ethylbenzenes, as compared to the reformate.

Hydrocarbon conversion

A process is disclosed for the highly selective skeletal isomerization of linear olefin-containing organic feeds to iso-olefins at high levels of feed conversion wherein linear olefins, e.g., n-butenes, are contacted with catalyst comprising ZSM-35 under skeletal isomerization conditions which can include temperatures of 100 to 750.degree. C. The process uses a catalyst composition comprising ZSM-35, e.g., microcrystalline ZSM-35 having a crystal size whose largest dimension is no greater than 0.5 micron and whose ratio of its second largest dimension to said largest dimension ranges from 0.5 to 1. The process exhibits enhanced catalyst cycle life where the ZSM-35 is composited with a silica-containing matrix to provide a catalyst composite having a total pore volume greater than 0.6 cc/g or 300.sup.+ angstroms pore volume of greater than 0.1 cc/g.

Highly selective n-olefin isomerization process using ZSM-35

A process is disclosed for the highly selective skeletal isomerization of linear olefin-containing organic feeds wherein linear olefins, e.g., n-butenes, are contacted with catalyst comprising ZSM-35 under isomerization conditions to produce iso-olefins of corresponding carbon number, e.g., isobutene. High iso-olefin selectivities thus can be obtained, even at relatively low temperatures and high linear olefin partial pressures.

A method is disclosed for the double bond isomerization of alpha olefin-containing feeds, e.g., conversion of 1-butene-containing hydrocarbon streams to 2-butene-rich product streams, wherein oligomer by-products are minimized. The process uses a catalyst composition comprising a zeolite whose surface has been at least partially deactivated for acid catalyzed reactions by treatment with an aluminum chelating agent, e.g., oxalic acid, which possesses an average cross section diameter greater than that of the zeolite pores.

Double bond isomerization of olefin-containing feeds with minimal

A process for catalytically converting cyclohexanone oxime to epsilon caprolactam. The conversion catalyst is a crystalline aluminosilicate zeolite having a Constraint Index greater than 1 and a reduced surface acidity. The surface acidity is reduced by selective surface dealumination of the crystalline aluminosilicate zeolite by contacting the zeolite with dicarboxylic acid, such as oxalic acid.

Synthesis of caprolactam using catalysts

A process is disclosed for the production of tertiary alkyl ethers wherein linear olefins, particularly n-butene, are isomerized in the vapor phase at high temperature in contact with shape selective metallosilicate catalyst to produce iso-olefin vapor, particularly isobutene. The vaporous iso-butene is then etherified with alkanol to provide alkyl tert-alkyl ether such as MTBE. Unreacted iso-olefin and/or linear olefin and product ether are separated by fractionation and unreacted olefin components recycled. Fractionation of the vapor phase etherification product is carried out by using the fresh liquid linear olefin feedstream as a reflux stream to the fractionator.

Conversion of normal alkenes to tertiary alkyl ethers

A method is disclosed for the double bond isomerization of alpha olefin-containing feeds, e.g., conversion of 1-butene-containing hydrocarbon streams to 2-butene-rich product streams, wherein oligomer by-products are minimized. The process uses a catalyst composition comprising a zeolite whose surface has been at least partially deactivated for acid catalyzed reactions by chemisorption of a surface-deactivating agent, e.g., collidine, which possesses an average cross section diameter greater than that of the zeolite pores.

The invention relates to improving the selectivity of the production of isobutylene or 2-methylpropene during fluid catalytic cracking of heavy C.sub.9 + aromatic containing feeds including resids and/or gas oils by employing two catalyst components, one of which comprises ZSM-23, ZSM-22, ZSM-35 or similarly structured catalysts and the other catalyst component being effective under the fluid catalytic cracking conditions to produce high octane gasoline.

Catalytic cracking process utilizing an iso-olefin enhancer catalyst

The present invention discloses a process for increasing the selectivity of the production of isobutylene in an admixture of C.sub.4 olefins, in a process comprising producing isobutylene, with high selectivity, comprising catalytically producing a first composition comprising at least one C.sub.4 olefin selected from the group consisting of 1-butene, cis-2-butene, trans-2-butene, admixtures thereof and 2-methylpropene admixed with at least one of said 1-butene, cis-2-butene, and trans-2-butene, by passing paraffin containing feed, which feed is free of aromatics, and in which the paraffin contains 5 to 20 carbon atoms, in the vapor phase, over a first catalyst composition, wherein the catalyst comprises ZSM-5 or ZSM-12, and increasing the isobutylene content of the first composition by producing a second composition, by contacting the first composition with a second catalyst composition comprising ZSM-23 under conditions in which the second composition is in the vapor phase, while maintaining the total C.sub.4 olefin content of the second composition substantially identical to the total C.sub.4 olefin content of the first composition.

Iso-olefin production

A process is disclosed for the production of alkyl tertiary alkyl ether from alkanol and iso-olefin employing zeolite catalyst, particularly zeolite Beta, that results is a high ether selectivity and a significant reduction in the formation of olefin oligomer by-product. The improvement is realized by incorporating a catalyst pretreatment step in the overall etherification process. The zeolite catalyst pretreatment comprises either steaming or a hydrothermal treatment using liquid water at elevated temperature. The process is particularly effective in reducing the formation of dimer by-product in the zeolite Beta catalyzed process for the formation of MTBE with high selectivity.

Production of tertiary alkyl ether using improved zeolite catalyst

A method for isomerizing a 1-olefin-containing organic feedstock having an average carbon number of about 4 to 5, e.g., 1-butene, to convert 1-olefin to 2-olefin at temperatures less than 200.degree. C., with a double bond isomerization catalyst comprising a zeolite sorbing 30 to 55 mg n-hexane at 90.degree. C., 83 torr, and 15 to 40 mg 3-methylpentane at 90.degree. C., 90 torr, per g dry zeolite in the hydrogen form, e.g., ZSM-22, ZSM-23, or ZSM-35. Catalyst aging is minimal despite operation at low temperatures and high pressures.

Double bond isomerization of 1-olefin containing feeds using ZSM-22,

A process for synthesizing di-isopropyl ether (DIPE) by etherification of isopropanol. A multi-stage process can employ propene in mixture with other feedstock materials, such as propane from refinery gas, in a primary hydration stage to produce isopropanol. The isopropanol is enriched between stages to remove water. In the second reaction stage the isopropanol is converted catalytically with large pore acidic zeolite to yield DIPE, which can be separated to recover pure propene.

Ether production

Process for the conversion of normal alkenes to tertiary alkyl ethers

A process is provided for catalytic conversion of organic compounds in a conversion zone containing a synthetic, non-composited microporous membrane comprising a continuous array of crystalline molecular sieve material.

Catalytic conversion over membrane composed of a pure molecular sieve

A method is provided for the preparation of a synthetic, non-composited microporous membrane comprising a continuous array of crystalline molecular sieve material. A non-porous forming surface is contacted, under crystallization conditions, with a chemical mixture capable of forming the molecular sieve material. After a layer of the molecular sieve material is crystallized on the forming surface, the layer and the forming surface are recovered from the chemical mixture and the layer is separated from the forming surface.

Synthesis of membrane composed of a pure molecular sieve

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Lawrenceville, NJ, United States of America

Werner O Haag