Mobil Oil Corporation

Other

Mobile Oil Corporation

Nai Y Chen

Thomas F Degnan

William J Reagan

Dennis E Walsh

Stephen S Wong

Sharon B McCullen

Rene B LaPierre

William E Garwood

Bruce P Pelrine

Randall D Partridge

Joseph N Miale

Tracy J Huang

Clinton R Kennedy

Tsoung Y Yan

Werner O Haag

David S Shihabi

Anil B Ketkar

Leonard R Koenig

Tai-Sheng Chou

Grant G Karsner

Billy K Huh

Richard J Quann

Melcon G Melconian

Clarence D Chang

Ralph M Dessau

Tsoung-Yuan Yan

Darrell D Whitehurst

Robert A Ware

Stephen M Oleck

Paul B Weisz

Lillian A Rankel

Thomas R Stein

Henry R Ireland

Bernard M Gillespie

Ikai Wang

Steven S Wong

Scott S Han

Stuart Damon Hellring

Costandi A Audeh

Ernest W Valyocsik

Quang N Le

Paul G Rodewald, Jr

Leslie R Rudnick

Richard F Socha

Chaya R Venkat

Ying-Yen P Tsao

Rudolph M Lago

John D Lutner

Donald M Nace

Eric J Scott

Alan W Peters

Stanley J Lucki

Anthony Y Kam

Vern W Weekman, Jr

Heinz Heinemann

Randall D Partride

Cynthis T Chu

Thomas E Degnan

Randell D Partridge

Susan M Leiby

Thomas F Degman, Jr

Nitrogenous compounds especially bases such as ammonia vapor are used to control the operation of a hydrocracker or catalytic dewaxer. Catalyst activity and selectivity may be controlled by addition of the base to the feed, for example, to control the balance between isomerization and hydrocracking in an operation using a zeolite beta catalyst. Runaway conditions may be controlled by the addition of nitrogenous compounds to regulate the temperature profile within the reactor.

Method for controlling hydrocracking and isomerization dewaxing operations

Method for controlling hydrocracking and isomerization dewaxing

The invention includes a ZSM-5 composition and the preparation thereof which comprises treating ZSM-5 with solutions of salts of weak acids. The resulting ultrasmall crystal size ZSM-5 component has a sorption capacity for 2,2-dimethylbutane of at least 10 mg/g zeolite and a sorption time for 30% capacity zeolitic sorption at 60.degree. C. and P(2,2-dimethylbutane) of 60 torr, of less than about 4 minutes.

Activation of zeolites

Hydrocarbon lubricants having a high viscosity index (V.I.) and low pour point are produced by hydroisomerizing a waxy lube feed such as slack wax or a waxy gas oil over zeolite beta after which aromatic components are removed by extraction, e.g. with furfural. The raffinate is then dewaxed, preferably by solvent dewaxing to target pour point with a final hydrofinishing step. The hydroisomerization coupled with the aromatics extraction and dewaxing increases the range of crudes that can be processed into high V.I. lubes while maintaining equivalent product qualities. Hydrogen consumption in the process is relatively low.

Lubricant production process

Nitrogenous compounds especially bases such as amines are used to control the operation of a hydrocracker. Catalyst activity and selectivity may be controlled by addition of the base to the feed, for example, to control the balance between isomerization and conversion in an operation using a zeolite beta catalyst. Runaway conditions may be controlled by the addition of nitrogenous compounds and if they are added at intermediate points along the length of the reactor, the temperature profile within the reactor can be effectively regulated.

Method for controlling hydrocracking operations

High purity benzene and high octane alkylaromatic gasoline can be obtained via a dual stage reforming process utilizing a non-acidic Group VIII metal containing microporous crystalline silicate catalyst in the first stage followed by first stage effluent treatment over acidic zeolite catalyst operating under conditions in the second stage to upgrade the first stage effluent in RON, in aromatic content or both.

Integrated low pressure aromatization process

Improved, dehydrocyclization and low-pressure reforming processes based on a non-acidic metal containing crystalline microporous indium catalyst, in which the feed is rich in C.sub.6 -C.sub.7 low octane hydrocarbons, such as paraffins, and in which the reformate has increased aromatic content and increased octane value over that of the feed are disclosed.

Reforming and dehydrocyclization

The catalytic properties of a metal-containing shape selective crystalline silicate zeolite are significantly improved by converting said metal to an intermetallic compound. Thus, for example, zeolite beta containing the intermetallic component platinum zeolite demonstrates improved catalytic properties for dewaxing a hydrocarbon feedstock compared to zeolite beta containing platinum metal alone.

Shape selective crystalline silicate zeolite containing intermetallic

An FCC or fluidized catalytic cracking process and apparatus for converting heavy metals laden crudes is disclosed. The heavy feed, conventional catalyst and an additive or vanadium getter contact the feed in a riser reactor. The additive is segregated from conventional FCC catalyst upstream of the conventional FCC regenerator. An elutriating, upflow riser reactor may be used with a coarse, rapidly settling getter. A fine, slowly settling getter may be used, with getter segregation achieved by using an elutriating cyclone on the riser outlet, an elutriating catalyst stripper, a sieve, or the like. The spent getter may be used once through, regenerated in a separate getter regenerator, or used as a source of fuel. Alumina and sponge coke are preferred getters.

Apparatus for FCC process with catalyst separation

A process for the catalytic cracking of a hydrocarbon oil is provided which comprises contacting the oil under cracking conditions with a large pore, alkali metal crystalline silicate zeolite cracking catalyst which is essentially free of shape selective combustion catalyst in the presence of a cracking-promoting amount of oxygen. A cracking catalyst of alkali metal zeolite and shape selective cracking catalyst is also disclosed.

Catalytic cracking of hydrocarbons with oxygen promoted alkali metal

Dewaxing, preferably catalytic dewaxing over zeolite beta or ZSM-5, improves the crackability of a heavy, waxy feed to a catalytic cracking unit. When the catalytic dewaxing occurs at temperatures above about 360.degree. C., using ZSM-5 dewaxing catalyst, high octane gasoline is obtained as a by product of catalytic dewaxing.

Integrated catalytic dewaxing and catalytic cracking process

Cellulosic materials are converted to hydrocarbons by hydrolyzing cellulosic materials to produce a mixture of fermentable sugars and unfermentable furfural, fermenting the mixture to obtain a fermented mixture containing fermented product and unfermented furfural and contacting the fermented mixture with a highly siliceous crystalline zeolite catalyst under conditions of temperature and pressure to convert the fermented mixture to a hydrocarbon-containing product. Preferably, an oxygenated organic compound such as methanol, ethanol or dimethylether is mixed with the fermented mixture prior to contact with the catalyst.

Process for converting cellulosic materials to hydrocarbon products

A process for producing lubricant oils of low pour point and high viscosity index by first carrying out a partial dewaxing of a lubricant base stock in an initial catalytic dewaxing operation, followed by a selective dewaxing step. The initial catalytic dewaxing step is carried out using a large pore, high silica zeolite dewaxing catalyst such as high silica Y or zeolite beta which dewaxes by isomerizing the waxy components of the base stock to less waxy brance chain isoparaffins but the severity of the operation is controlled so as to effect only a partial removal of the waxy components. Further removal of the waxy components is effected during the subsequent dewaxing step which is selective for the removal of the more waxy n-paraffin components, leaving the branched chain isoparaffins which contribute to a high VI in the product. The selective dewaxing step may be either a solvent, e.g. MEK dewaxing operation or a catalytic dewaxing using a highly shape selective zeolite such as ZSM-22 or ZSM-23. The severity of the initial catalytic dewaxing operation may be controlled so as to effect a net increase in the content of isoparaffins and because of the selective nature of the solvent dewaxing step, this increased isoparaffins concentration may be retained, producing a product of high VI. The pour point of the feedstock is preferably reduced during the initial catalytic dewaxing step to a value which is no lower than 10.degree. F. and preferably no lower than 20.degree. F., above the target pour point for the products. Generally, this will entail a reduction of at least 10.degree. F. and preferably at least 20.degree. F. in the pour point of the feed.

Heavy hydrocarbon oils of high paraffin content are catalytically cracked using zeolite beta. The paraffin content of the oil is at least 20 weight percent or higher. The gasoline cracking products have a high octane rating and the higher boiling products a decreased pour point resulting from the dewaxing activity of the zeolite beta. The use of cracking temperatures above 500.degree. C., preferably above 550.degree. C., also improves iso-butene production.

Catalytic cracking of paraffinic feedstocks with zeolite beta

FCC process with catalyst separation

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Titusville, NJ, United States of America

Nai Y Chen