Chevron Research Company

Chevron Research & Technology Company

Other

Chevron Chemical Company LLC

Robert L Jacobson

Richard C Robinson

Leslie Ann Field

Kirk R Gibson

Thomas R Hughes

Dennis L Holtermann

Lawrence W Jossens

William A Blanton, Jr

Charles R Wilson

Donald Henry Mohr

Paul W Tamm

Dean A Van Leirsburg

Harris E Kluksdahl

Manfred J Michlmayr

Warren E Brown

William C Hecker

Robert J Houston

Robert M Ormiston

K R Gibson

John H Arndt

Ann Marie Hall

William R Prince

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Interactive legal citation checker

Provided is a method for removing residual sulfur from a hydrotreated naphtha feed. The process comprises contacting the naphtha feed with massive nickel catalyst in the presence of hydrogen. The contacting is generally accomplished in the temperature range of 300.degree. F. to about 450.degree. F. Such contacting has been found to achieve quite effective removal of sulfur, particularly thiophenes.

Method for removing sulfur from a hydrocarbon feed

A process is disclosed for removing residual sulfur from a hydrotreated naphtha feedstock. The feedstock is contacted with molecular hydrogen under reforming conditions in the presence of a less sulfur sensitive reforming catalyst to convert trace sulfur compounds to H.sub.2 S, and to form a first effluent. The first effluent is contacted with a solid sulfur sorbent to remove the H.sub.2 S and form a second effluent. The second effluent is then contacted with a highly selective reforming catalyst under severe reforming conditions. Also disclosed is a method using a potassium containing sulfur sorbent made from nitrogen-free potassium compounds.

Sulfur removal systems for protection of reforming catalysts

Sulfur removal systems for protection of reforming crystals

A process for removing residual sulfur from a hydrotreated naphtha feedstock is disclosed. The feedstock is contacted with molecular hydrogen under reforming conditions in the presence of a less sulfur sensitive reforming catalyst, thereby converting trace sulfur compounds to H.sub.2 S, and forming a first effluent. The first effluent is contacted with a solid sulfur sorbent, removing the H.sub.2 S and forming a second effluent. The second effluent is contacted with a highly selective reforming catalyst under severe reforming conditions.

Sulfur removal system for protection of reforming catalysts

A catalyst composition and process for using said catalyst is disclosed wherein the catalyst comprises 0.24 to 0.26 weight percent platinum and 0.48 to 0.52 weight percent rhenium disposed on an alumina spheroidal carrier.

Platinum-rhenium catalyst

Sulfur removal system for protection of reforming catalyst

The present invention is a process for regenerating a sulfur-contaminated, highly selective, large-pore zeolite catalyst. It comprises a multistep process involving exposure of the catalyst to a combination of oxidizing conditions, reducing conditions and treatment with a halogen acid gas. These conditions are effective to agglomerate a Group VIII metal and remove sulfur. Thereafter, the catalyst is oxychlorinated to redisperse the Group VIII metal over the catalyst surface. A carbon removal step is optionally included.

Process for regenerating sulfur contaminated reforming catalysts

A process is disclosed wherein a naphtha feed is contacted in a reaction vessel with a dehydrocyclization catalyst comprising a large-pore zeolite containing at least one Group VIII metal to produce an aromatics product and a gaseous stream, the aromatics product is separated from the gaseous stream and is passed through a molecular sieve which adsorbs paraffins present in the aromatics product, then the gaseous stream is used to strip the paraffins from the molecular sieve, and the gaseous stream and the paraffins are recycled to the reaction vessel. Preferably, the dehydrocyclization catalyst comprises a type L zeolite containing from 8% to 15% by weight barium and from 0.6% to 1.0% by weight platinum, wherein at least 80% of the crystals of the type L zeolite are larger than 1000 Angstroms, and an inorganic binder selected from the group consisting of silica, alumina, and aluminosilicates.

Dehydrocyclization process

A naphtha feed is contacted in a reaction vessel with a dehydrocyclization catalyst comprising a large-pore zeolite containing at least one Group VIII metal to produce an aromatics product and a gaseous stream, the aromatics product is separated from the gaseous stream and is passed through a molecular sieve which adsorbs paraffins present in the aromatics product, then the gaseous stream is used to strip the paraffins from the molecular sieve, and the gaseous stream and the paraffins are recycled to the reaction vessel.

Method of producing high aromatic yields through aromatics removal and

In a process for reforming light naphtha with a bimetallic or multimetallic reforming catalyst, such as a platinum-rhenium-halogen catalyst, at conventional reforming conditions, wherein the catalyst is used for an extended continuous on-stream period, the aromatics selectivity of the catalyst is rapidly increased by contacting the naphtha and hydrogen with the catalyst at increased severity operating conditions, such as a reduced pressure less than 90% of the normal reforming pressure, during an initial portion of the on-stream period.

Naphtha reforming process

Small amounts of lower alcohols are admixed with sour hydrocarbons and the mixture is contacted with a copper-containing catalyst at an elevated temperature. The alcohol serves as the oxygen source for the catalytic oxygenative conversion to disulfides of mercaptans souring the hydrocarbon.

Use of lower alcohols as oxygen source in hydrocarbon sweetening

Isomerizable light paraffinic hydrocarbon feeds are isomerized in an improved process using a particular super-chlorided reforming catalyst under isomerizing conditions. A chloride source in the feed stabilizes the catalyst. This process provides for a material octane improvement of the feed without excessive loss thereof to normally gaseous hydrocarbons.

Isomerization process for upgrading low-octane light paraffinic feeds

Thiol impurities are absorbed and removed from hydrocarbon oils by contacting the oil in the absence of molecular oxygen with a scavenger at a temperature in the range of about 120.degree. to 400.degree. C. The scavenger is a composite having a copper component and an inorganic porous carrier component and having a surface area in the range 20 to 1000 square meters per gram. The contacting must be discontinued when the thiol impurity content of the effluent product exceeds about 0.3 ppm.

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Vallejo, CA, United States of America

Robert L Jacobson