Phillips Petroleum Company

Conocophillips Company

Fan-Nan Lin

Filippo Pennella

John S Parsons

Edgar Durand Davis

Donald H Macahan

Marvin M Johnson

Brian H Limoges

Raul Adarme

An-hsiang Wu

Edward L Sughrue

Donald H Kubicek

Stephen L Parrott

John Cowan

Daniel T Fernald

Floyd H Holland

Stephen L Ege

Peter C Stynes

Thomas A Lessard

Nak J Sung

Johnnie R Pierce

Edwin P Sasscer

A substantially water-free hydrocarbon feed is charged to a reformer reactor operated under reforming conditions; thereafter, a chlorine-containing additive is introduced, without the simultaneous introduction of water, into the substantially water-free hydrocarbon feed being charged to the reformer reactor in an amount and for a time period that are effective to inhibit deactivation of the reformer catalyst; thereafter, the introduction of the chlorine-containing additive is terminated and the charging of the substantially water-free hydrocarbon feed to the reformer reactor is continued.

Catalytic reforming process

A reforming catalyst containing a Group VIII metal, or a Group VII B metal, or tin, or germanium, or copper, or selenium or combinations of any two or more metals or oxides thereof is activated by: a) continuously flowing a reducing gas over the catalyst for contact with the catalyst; (b) during step a), flowing a halogen-containing compound over the catalyst for contact with the catalyst for a first time period, wherein the first time period is greater than about 1 minute, and wherein the first time period is less than about 60 minutes; and (c) following step b), and during step a), substantially discontinuing the flow of the halogen-containing compound over the catalyst for a second time period, wherein the second time period is greater than about 1 minute. Alternatively, the catalyst can be activated in an activation zone by: 1) removing water from the activation zone; 2) reducing iron oxide contained in the activation zone in the presence of a reducing gas thereby forming reduced iron and water; 3) removing water from the activation zone; 4) reducing the metal oxide of the catalyst in the presence of a reducing gas thereby forming reduced metal and water; 5) removing water from the activation zone; 6) during step 4), flowing a halogen-containing compound over the catalyst for contact with the catalyst for a first time period; and 7) following step 6) and during step 4), substantially discontinuing the flow of halogen-containing compound over the catalyst for a second time period.

Catalytic reforming catalyst activation

While a substantially water-free hydrocarbon feed is being charged to a catalytic reformer reactor, an organic chloride is contacted with the reformer catalyst in an amount and for a time period that are effective to restore at least a portion of the activity of the reformer catalyst.

A process and/or system is provided for isomerizing a hydrocarbon feedstock comprising saturated C hydrocarbons by contacting the hydrocarbon feedstock, in the presence of hydrogen and optionally a chloride, with a first isomerization catalyst composition in a first isomerization reactor defining a first reaction zone operated at a first reaction temperature, withdrawing a first intermediate stream comprising cyclohexane and n-hexane from the first reaction zone, separating the first intermediate stream, via a first separator, into a first product stream comprising cyclohexane and a second intermediate stream comprising n-hexane, contacting the second intermediate stream, in the presence of hydrogen and optionally a chloride, with a second isomerization catalyst composition in a second isomerization reactor defining a second reaction zone operated at a second reaction temperature greater than the first reaction temperature, and withdrawing from the second reaction zone a second product stream comprising isohexane.

Two-stage isomerization of saturated C6 hydrocarbons

Deactivation of a reformer catalyst is inhibited by charging a hydrocarbon feed having a concentration of an organic aluminum halide compound to a reformer reactor operating under reforming conditions and containing a reformer catalyst.

Catalytic reforming process including the addition of organic aluminum halide

Catalyst activation of a platinum reforming catalyst system contained in a multiple reactor system by simultaneously reducing the catalyst with hydrogen while introducing a nonmetallic chlorine-containing compound into a reactor of the multiple reactor system in an amount to add from about 0.05 to about 0.3 weight percent chlorine to the catalyst and thereafter purging the system with about 100 to about 50,000 cubic feet of hydrogen per cubic foot of catalyst resulting in a reforming system having increased activity and providing enhanced RON values with reduced cracking of feedstock.

A substantially water-free hydrocarbon feed is charged to a multiple-reactor reformer system being operated under reforming conditions and comprising at least two reformer reactors serially connected in fluid-flow communication and each containing a reformer catalyst; and, simultaneously with the charging step, a chloriding agent is sequentially introduced, without simultaneously introducing water, immediately upstream from the inlets of all the reformer reactors in an amount and for a period of time that are effective to inhibit the deactivation of the reformer catalyst.

Catalytic reforming process with inhibition of catalyst deactivation

Catalyst activation of a platinum reforming catalyst system contained in a multiple reactor system by simultaneously reducing the catalyst with a sustained hydrogen flow through the multiple reactor system while introducing a nonmetallic chlorine-containing compound serially into each reactor of the multiple reactor system in an amount to add from about 0.05 to about 0.3 weight percent chlorine to the catalyst and thereafter purging the system with about 100 to about 50,000 cubic feet of hydrogen per cubic foot of catalyst prior to commencing use of the treated catalyst system for reforming hydrocarbon feed.

In a process for the dehydrocyclization of a dehydrocyclizable hydrocarbon contained in a dehydrocyclization feed stream which comprises contacting said dehydrocyclizable hydrocarbon in a dehydrocyclization zone under dehydrocyclization conditions in the presence of a dehydrocyclization catalyst, the improvement comprises carrying out said dehydrocyclization process in the presence of a metal chloride additive in said dehydrocyclization feed stream, said metal chloride additive being present in an amount sufficient to inhibit deactivation of such dehydrocyclization catalyst.

Hydrocarbon dehydrocyclization process

An isomerization process for converting an isomerization feed stream containing alkanes having about 4 carbon atoms to about 10 carbon atoms per molecule and cycloalkanes having about 5 carbon atoms to about 10 carbon atoms per molecule to at least one product hydrocarbon isomer. The isomerization feed stream, which contains at least one feed hydrocarbon and hydrogen, is contacted in an isomerization zone at effective isomerization conditions with a catalyst where deactivation of such catalyst occurs in the isomerization zone. The isomerization process includes the presence of an additive in the isomerization feed stream. The concentration of the additive is sufficient to alleviate or diminish the deactivation of the catalyst and to maintain a substantially constant conversion of the at least one feed hydrocarbon to the at least one product hydrocarbon isomer at effective isomerization conditions.

Isomerization of hydrocarbons

A process and/or system is provided for isomerizing a hydrocarbon feedstock comprising saturated C.sub.6 hydrocarbons by contacting the hydrocarbon feedstock, in the presence of hydrogen and optionally a chloride, with a first isomerization catalyst composition in a first isomerization reactor defining a first reaction zone operated at a first reaction temperature, withdrawing a first intermediate stream comprising cyclohexane and n-hexane from the first reaction zone, separating the first intermediate stream, via a first separator, into a first product stream comprising cyclohexane and a second intermediate stream comprising n-hexane, contacting the second intermediate stream, in the presence of hydrogen and optionally a chloride, with a second isomerization catalyst composition in a second isomerization reactor defining a second reaction zone operated at a second reaction temperature greater than the first reaction temperature, and withdrawing from the second reaction zone a second product stream comprising isohexane.

Two-stage isomerization of saturated C.sub. 6 hydrocarbons

Benzene is hydrogenated using a platinum containing catalyst in the presence of water and an organic chloride.

Hydrogenation of benzene in the presence of water

A well reasoned steady state model for simulation of pentane isomerization in a long tubular reactor predicts important reaction variables such as feed conversion, product yields, temperature and pressure. The predictions are based on inputs including feed flowrates, composition, temperature and pressure. The model includes a set of differential equations for component concentrations with respect to axial distance along the reactor, and reaction rate constants expressed in terms of physical properties. A method of programming a computer for simulating the reaction is disclosed.

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Bartlesville, OK, United States of America

Fan-Nan Lin