Uop Lcc

Herman A Zinnen

Charles P McGonegal

Maureen L Bricker

Gregory A Funk

Hemant W Dandekar

Ralph D Gillespie

Simon H Hobbs

Mark J Gattuso

Masami Kojima

Blaise J Arena

Laszlo T Nemeth

Jennifer R Holmgren

A process for separating at least one C alkylaromatic hydrocarbon from a mixture containing at least one C alkylaromatic hydrocarbon and at least one C or C alkylaromatic hydrocarbon using dealuminated sodium zeolite Y.

Process for separating alkylaromatic hydrocarbons

Improved processes for preparation of sertraline or sertraline analogs in high enantiomeric purity centers on resolution using simulated moving bed chromatography of isomeric racemic sertraline or sertraline analogs. Resolution is effected with high enantiomeric purity, and the undesired enantiomer may be racemized and recycled to the resolution phase to avoid loss.

Process for preparation of pharmaceutically desired sertraline and sertraline analogs

Improved processes for preparation of tetralones in high enantiomeric purity centers on resolution using simulated moving bed chromatography of a racemic tetralone derivative. Resolution is effected with high enantiomeric purity, and subsequent reactions of the desired tetralone derivative enantiomer performed with high optical specificity to maintain enantiomeric purity. The undesired enantiomer may be racemized and recycled to the resolution phase to avoid loss.

Process for preparation of pharmaceutically desired chiral tetralone from tetralones

A process for separating at least one C alkylaromatic hydrocarbon from a mixture containing at least one C alkylaromatic hydrocarbon and at least one C or C alkylaromatic hydrocarbon using sodium zeolite Y, dealuminated sodium zeolite Y or dealuminated zeolite Y ion exchanged with a metal selected from the group consisting of calcium, sodium, strontium, a Group IB element, a Group VIII element and mixtures thereof.

A process for separating at least one C,alkylaromatic hydrocarbon from a mixture containing at least one C,alkylaromatic hydrocarbon and at least one C,or C,alkylaromatic hydrocarbon using zeolite Y or zeolite Y ion exchanged with a metal selected from the group consisting of calcium, sodium, strontium, a Group IB element, a Group VIII element and mixtures thereof.

A process for separating meta-xylene from a mixture containing meta-xylene, para-xylene, and ortho-xylene has been developed. The process involves contacting the mixture with zeolite Beta to effect the adsorption of the para-xylene, ortho-xylene, and ethylbenzene in preference to the meta-xylene and recovering the meta-xylene.

Process for separating meta-xylene

A process to isomerize at least one normal or mono-methyl-branched alkane to form at least one multi-methyl-branched alkane has been developed. At least one normal or mono-methyl-branched is introduced to a reaction zone to form at least one multi-methyl-branched alkane. The reaction zone is located between a first and a second adsorption zone with the adsorption zones containing an adsorbent effective to selectively adsorb normal and mono-methyl-branched alkanes relative to multi-methyl-branched alkanes. A desorbent is introduced to the first adsorption zone and an effluent containing at least one multi-methyl-branched alkane is withdrawn from the second adsorption zone. After a period of time, the introduction of the desorbent is redirected to the second adsorption zone and concurrently the withdrawal of the effluent is moved to the first adsorption zone.

Alkane isomerization using reversible flow

A process to separate multimethyl-branched alkanes from a mixture of multimethyl-branched alkanes, monomethyl-branched alkanes, and normal alkanes has been developed. The mixture is introduced to a simulated moving bed of solid adsorbent particles having the selectivity normal alkanes&gt;monomethyl-branched alkanes&gt;multimethyl-branched alkanes. The adsorbent may be silicalite, ferrierite, zeolite Beta, MAPO-31, SAPO-31, SAPO-11, zeolite X ion exchanged with alkaline cations, alkaline earth cations, or a mixture thereof, and zeolite Y ion exchanged with alkaline cations, alkaline earth cations, or a mixture thereof. A raffinate stream enriched in multimethyl-branched alkanes is removed from the simulated moving bed. The monomethyl-branched alkanes are desorbed from the solid adsorbent particles using a first desorbent capable of desorbing the monomethyl-branched alkanes but incapable of desorbing the normal alkanes and first extract stream enriched in the desorbed monomethyl-branched alkanes is removed from the simulated moving bed. The normal alkanes are desorbed from the solid adsorbent particles using a second desorbent, and a second extract stream enriched in the desorbed normal alkanes is removed from the simulated moving bed. The process may be incorporated into an isomerization flowscheme.

Process for separating and recovering multimethyl-branched alkanes

A process for the transalkylation of benzene, toluene and alkylaromatic hydrocarbons containing nine and ten carbon atoms form alkylaromatic hydrocarbons containing eight carbon atoms has been developed. The fixed bed reaction and adsorption zone contains a transalkylation catalyst and an adsorbent effective to selectively adsorb C.sub.9 and C.sub.10 alkylaromatic hydrocarbon reactants relative to the C.sub.8 alkylaromatic hydrocarbon products. Hydrogen and a desorbent are introduced to a first portion of the zone and an effluent containing at least one C.sub.8 alkylaromatic hydrocarbon product is withdrawn from a second portion of the zone. After a period of time, the desorbent is redirected to the second portion of the zone and concurrently the effluent containing at least one C.sub.8 alkylaromatic hydrocarbon product is withdrawn from the first portion of the zone. The alternation of introducing the desorbent to a first portion and then a second portion of the zone while concurrently withdrawing the effluent from the second portion and then the first portion of the zone is continued, thereby retaining the C.sub.9 and C.sub.10 alkylaromatic hydrocarbons within the zone until they are consumed.

C.sub.8 alkylaromatic hydrocarbon production using reversible flow

A process for producing at least one C.sub.8 alkylaromatic hydrocarbon product from a feedstock containing at least one C.sub.9 or C.sub.10 alkylaromatic hydrocarbon reactant using simulated moving bed reactive chromatography has been developed. At least a portion of the reactants are transalkylated to form at least one product in a zone of the simulated moving bed with concurrent separation of at least one alkylaromatic hydrocarbon using the adsorbent. The adsorbed alkylaromatic hydrocarbon is desorbed from the adsorbent in a subsequent zone of the simulated moving bed and the transalkylation of the reactants with concurrent separation of at least one alkylaromatic hydrocarbon using the adsorbent is continued.

Process for aromatic transalkylation using simulated moving bed reactive

Removal of aromatic sulfur compounds from an FCC feedstock with minimal adsorption of aromatic hydrocarbons is achieved using a zeolite Y exchanged with alkali or alkaline earth cations. KY is an especially effective adsorbent. Where the KY is impregnated with a group VIII metal, particular palladium or platinum, the adsorbent is effectively regenerated by treatment with hydrogen at elevated temperatures.

Removal of organic sulfur compounds from FCC gasoline using regenerable

A process for the transalkylation of benzene, toluene and alkylaromatic hydrocarbons containing 9 and 10 carbon atoms and at least one methyl or ethyl group to form alkylaromatic hydrocarbons containing 8 carbon atoms has been developed. The benzene, toluene, and alkylaromatic hydrocarbon reactants are introduced to a fixed bed reaction and adsorption zone operating under conditions effective for transalkylation and containing a catalyst effective to transalkylate the alkylaromatic hydrocarbons and benzene, and an adsorbent effective to selectively adsorb C.sub.9 and C.sub.10 alkylaromatic hydrocarbon reactants relative to the C.sub.8 alkylaromatic hydrocarbon products. Hydrogen and a desorbent capable of desorbing the C.sub.9 and C.sub.10 alkylaromatic hydrocarbons from the adsorbent is introduced to a first portion of the reaction and adsorption zone and an effluent containing at least one C.sub.8 alkylaromatic hydrocarbon product is withdrawn from a second portion of the reaction and adsorption zone. After a period of time, the desorbent is redirected to the second portion of the reaction and adsorption zone and concurrently the effluent containing at least one C.sub.8 alkylaromatic hydrocarbon product is withdrawn from the first portion of the reaction and adsorption zone. The alternation of introducing the desorbent to a first portion and then a second portion of the reaction and adsorption zone while concurrently withdrawing the effluent from the second portion and then the first portion of the reaction and adsorption zone is continued, thereby retaining the C.sub.9 and C.sub.10 alkylaromatic hydrocarbons within the reaction and adsorption zone until they are consumed.

Removal of organic sulfur compounds, especially aromatic sulfur compounds from an FCC feedstock with minimal adsorption of aromatic hydrocarbons is achieved using a zeolite X exchanged with alkali or alkaline earth cations. KX is an especially effective adsorbent. Where the KX is loaded with a group VIII metal, particular palladium or platinum, the adsorbent is effectively regenerated by treatment with hydrogen at elevated temperatures.

A process to isomerize at least one normal or mono-methyl-branched alkane containing from about 6 to about 8 carbon atoms to form at least one multi-methyl-branched alkane has been developed. The normal or mono-methyl-branched alkane is introduced to a reaction and adsorption zone operating under conditions effective to isomerize the normal or mono-methyl-branched alkane and containing a catalyst effective to isomerize the normal or mono-methyl-branched alkane and an adsorbent effective to selectively adsorb normal and mono-methyl-branched alkanes relative to multi-methyl-branched alkanes. Hydrogen and a desorbent comprising at least one alkane having from about 4 to about 8 carbon atoms is introduced to a first portion of the reaction and adsorption zone and an effluent containing at least one multi-methyl-branched alkane is withdrawn from a second portion of the reaction and adsorption zone. After a period of time, the desorbent is redirected to the second portion of the reaction and adsorption zone and concurrently the effluent containing at least one multi-methyl-branched alkane is withdrawn from the first portion of the reaction and adsorption zone. The alternation of introducing the desorbent to a first portion and then a second portion of the reaction and adsorption zone while concurrently withdrawing the effluent from the second portion and then the first portion of the reaction and adsorption zone is continued.

Alkane isomerization using reversible flow reactive chromatography

A process for the continuous isomerization of an alkane to produce an isomerized product through contacting the alkane with a simulated moving bed acting as a catalyst for isomerization and an adsorbent for the alkanes has been developed. The alkane may be n-butane and the isomerized product 2-methylpropane, the alkane may be n-pentane and the isomerized product 2-methylbutane or 2,2-dimethylpropane, the alkane may have from 6 up to about 8 carbon atoms with no more than one methyl branch and the isomerized product having the same number of carbon atoms and at least two methyl branches, or the reactant may be a mixture of the foregoing alkanes with the corresponding isomerized products being formed. In a zone of the simulated moving bed, the alkanes are catalytically isomerized to form the isomerized products. The unreacted alkanes are adsorbed, and the isomerized products are collected. In a subsequent zone of the simulated moving bed, the unreacted alkanes are desorbed using a desorbent and may be catalytically isomerized to form additional isomerized products which are also separated and collected. The catalyst used in the simulated moving bed may be platinum on tungstated zirconia, and the adsorbent used in the simulated moving bed may be EU-1, ZSM-12, SAPO-5, Y-82, faujasite, erionite, zeolite beta exchanged with sodium, lithium, potassium, barium, calcium, strontium or combinations thereof, zeolite X exchanged with calcium and strontium, mordenite exchanged with sodium, lithium, potassium, barium, calcium, strontium, or combinations thereof.

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Evanston, IL, United States of America

Herman A Zinnen