Chevron Research Company

Chevron U.s.a. Inc.

Chevron Research & Technology Company

Other

Chevron Chemical Company LLC

Donald S Santilli

Stacey Ian Zones

Dennis L Holtermann

James Nathan Ziemer

Robert A Innes

Theresa A Pecoraro

Andrew Rainis

Lawrence W Jossens

Thomas Van Harris

Robert T Lewis

John J Long

Cong-Yan Chen

Roger F Vogel

James V Kennedy

Mohammad M Habib

Donald W Blakely, Deceased

Bowman Lee

Stacy I Zones

R Norm Reynolds, Jr

A dewaxing process for lowering the haze point of a bright stock which includes contacting a bright stock in the presence of added hydrogen gas with a Zeolite EU-1 catalyst in combination with a ZSM-48 and/or SSZ-32 catalyst.

Process for reducing haze point in bright stock

The invention discloses a method of making 2,6-dimethylnaphthalene from any DMN with one methyl on each ring in a two-step hydroisomerization/dehydrogenation process. The catalyst used in the hydroisomerization step is an acidic catalyst such as a silica aluminum catalyst with a hydrogenation/dehydrogenation metal. The catalyst used in the dehydrogenation step is a reforming type catalyst.

Method of making 2,6-dimethylnaphthalene from other dimethylnaphthalene

A crystalline zeolite SSZ-25 is prepared using an adamantane quaternary ammonium ion as a template.

Isomerization process using zeolite SSZ-25

A crystalline low-aluminum boron beta zeolite is used for dewaxing hydrocarbonaceous feeds.

Low-Aluminum boron beta zeolite

Alkylation process using zeolite SSZ-25

A device provides pointing device functions in a keyboard without requiring a keyboard operator to move his hands from their normal typing positions. Position sensitive elements at the top surfaces of a set of keys are used together to provide a large touch surface to allow accurate pointing. The position sensitive elements detect the position of a pointing object such as a finger on the top surfaces of these keys as an indication of information to be conveyed by the user.

Computer keyboard pointing device

The present invention relates to new crystalline zeolite SSZ-41 which comprises oxides of (1) silicon or a mixture of silicon and germanium, and (2) zinc, said zinc being present in an amount from about 2 wt % to about 5 wt % of zinc metal based on the total weight of metals in said zeolite. Zeolite SSZ-41 may also optionally contain oxides of aluminum, iron, gallium or mixtures thereof. Zeolite SSZ-41 has the X-ray diffraction lines of Table I and has an argon adsorption capacity of at least about 0.06 cc/gm at 87.degree. K. Also disclosed are methods of making and using zeolite SSZ-41.

Hydrocarbon conversion processes using zeolite SSZ-41

A crystalline low-aluminum boron beta zeolite is prepared using a diquaternary ion as a template.

Low-aluminum boron beta zeolite

Dewaxing process using zeolite SSZ-25

Hydrocarbon conversion process using zeolite SSZ-25

A crystalline zeolite SSZ-32 of novel composition is prepared using an N-lower alkyl-N'-isopropyl-imidazolium cation as a template. Also disclosed is a process for converting hydrocarbons with crystalline zeolite SSZ-32.

Hydrocarbon conversion process using zeolite SSZ-32 having constraint

Hydrocarbon conversion utilizing a low-aluminum boron beta zeolite

Heavy waxy oil is dewaxed by a mild cracking and isomerization process using a catalyst comprising SSZ-32 and at least one Group VIII metal. The heavy oil contains naphthenic wax, which includes only a relatively small amount of normal alkanes. Naphthenic wax containing a minor amount of oil may also be dewaxed using the process.

Process for producing heavy lubricating oil having a low pour point

Hydrocarbon conversion process using zeolite SSZ-32 as catalyst

A process is disclosed for dewaxing a hydrocarbon feed to produce a dewaxed lube oil. The feed includes straight chain and slightly branched chain paraffins having 10 or more carbon atoms. In the process the feed is contacted under isomerization conditions with an intermediate pore size molecular sieve having a crystallite size of no more than about 0.5.mu. and pores with a minimum diameter of at least 4.8.ANG. and with a maximum diameter of 7.1.ANG. or less. The catalyst has sufficient acidity so that 0.5 g thereof when positioned in a tube reactor converts at least 50% of hexadecane at 370.degree. C., a pressure of 1200 psig, a hydrogen flow of 160 ml/min, and a feed rate of 1 ml/hr. It also exhibits 40 or greater isomerization selectivity when used under conditions leading to 96% conversion of hexadecane to other chemicals. The catalyst includes at least one Group VIII metal. The contacting is carried out at a pressure from about 15 psig to about 3000 psig.

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Larkspur, CA, United States of America

Donald S Santilli