Process for the separation of C9 aromatic isomers

Claim 2

An adsorptive separation process for separating paraethyltoluene from a hydrocarbon feed stream containing a mixture of C 9 aromatic isomers comprising: (a) contacting said hydrocarbon feed stream with a bed of an adsorbent of zeolite beta; (b) withdrawing from said bed of adsorbent a raffinate stream containing less of the selectively adsorbed C 9 aromatic isomer of the feed stream; (c) desorbing the adsorbed paraethyltoluene to effect displacement thereof; and (d) withdrawing from the adsorbent bed an extract stream containing the adsorbed paraethyltoluene.

Claim 3

Process of claim 1 wherein the mixture of C 9 aromatic isomers are ethyltoluenes which are selectively adsorbed in the order of para-ethyltoluene>ortho-ethyltoluene>meta-ethyltoluene.

Claim 4

Process of claim 1 further characterized in that said adsorbent contains at least one cation selected from the group consisting of potassium, barium, rubidium, lithium, sodium and cesium.

Claim 5

Process of claim 3 wherein the adsorbent has a cation exchanged with cesium.

Claim 6

Process of claim 1 wherein the adsorbed aromatic components are desorbed by passing a desorbent material through said bed.

Claim 7

Process of claim 1 further characterized in that said adsorbent contains at least one cation which imparts an (α) separation factor of at least 2.0 of the adsorbed aromatic isomer over at least one of the other components of the hydrocarbon feed stream.

Claim 8

Process of claim 5 wherein the desorbent is selected from the group consisting of toluene, benzene, paraffin, diethylbenzene, alkyl benzene, polycyclic hydrocarbons and mixtures thereof.

Claim 9

Process of claim 1 wherein the zeolite beta adsorbent comprises a silicate chosen from the group consisting of aluminosilicate, borosilicate and gallosilicate.

Claim 10

Process of claim 8 wherein the silicon is fully or partially substituted with an element chosen from the group consisting of germanium and phosphorus.

Claim 11

Process of claim 1 wherein the zeolite beta adsorbent is an aluminosilicate.

Claim 12

Process of claim 1 wherein the separation is carried out at a temperature within the range of ambient to 450° F. and a pressure within the range of atmospheric to 500 psig.

Claim 13

Process of claim 1 wherein the process is carried out in the liquid phase.

Claim 14

Process of claim 1 wherein the process is carried out in the vapor phase.

Claim 15

Process of claim 1 wherein the adsorbent is combined with a binder.

Claim 16

Process of claim 13 wherein the binder is selected from the group consisting of natural and synthetic clays and inorganic oxides.

Claim 17

Process of claim 1 further characterized in that said adsorbent has a capacity of at least 3% of hydrocarbon by weight of adsorbent.

Claim 18

An adsorptive separation process for separating at least one C 9 aromatic isomer from a hydrocarbon feed stream containing a mixture of C 9 aromatic isomers, wherein the mixture of C 9 aromatic isomers contain trimethylbenzenes which are selectively adsorbed in the order of pseudocumene and hemimellitene>mesitylene, comprising: (a) contacting said hydrocarbon feed stream with a bed of adsorbent of zeolite beta; (b) withdrawing from said bed of adsorbent a raffinate stream containing less of the selectively adsorbed C 9 aromatic isomer of the feed stream; (c) desorbing the adsorbed C 9 aromatic isomer to effect displacement thereof; and (d) withdrawing from the adsorbent bed an extract stream containing the adsorbed C 9 aromatic isomer.

Claim 19

An adsorptive separation process for separating at least one C 9 aromatic isomer from a hydrocarbon feed stream containing a mixture of C 9 aromatic isomers, wherein the mixture of C 9 aromatic isomers contain trimethylbenzenes which are selectively adsorbed in the order of pseudocumene and hemimellitene>mesitylene, comprising: (a) contacting said hydrocarbon feed stream with a bed of adsorbent of zeolite beta; (b) withdrawing from said bed of adsorbent a raffinate stream containing less of the selectively adsorbed C 9 aromatic isomer of the feed stream; (c) desorbing the adsorbed C 9 aromatic isomer to effect displacement thereof; and (d) withdrawing from the adsorbent bed an extract stream containing the adsorbed C 9 aromatic isomer.

Claim 20

Process of claim 17 further characterized in that said adsorbent contains at least one cation selected from the group consisting of potassium, barium, rubidium, lithium, sodium and cesium.

Claim 21

Process of claim 18 wherein the adsorbent has a cation exchanged with cesium.

Claim 22

Process of claim 17 wherein the adsorbed aromatic components are desorbed by passing a desorbent material through said bed.

Claim 23

Process of claim 17 further characterized in that said adsorbent contains at least one cation which imparts an (α) separation factor of at least 2.0 of the adsorbed aromatic isomer over at least one of the other components of the hydrocarbon feed stream.

Claim 24

Process of claim 20 wherein the desorbent is selected from the group consisting of toluene, benzene, paraffin, diethylbenzene, alkyl benzene, polycyclic hydrocarbons and mixtures thereof.

Claim 25

Process of claim 17 wherein the zeolite beta adsorbent comprises a silicate chosen from the group consisting of aluminosilicate, borosilicate and gallosilicate.

Claim 26

Process of claim 23 wherein the silicon is fully or partially substituted with an element chosen from the group consisting of germanium and phosphorus.

Claim 27

Process of claim 17 wherein the zeolite beta adsorbent is an aluminosilicate.

Claim 28

Process of claim 17 wherein the separation is carried out at a temperature within the range of ambient to 450° F. and a pressure within the range of atmospheric to 500 psig.

Claim 29

Process of claim 17 wherein the process is carried out in the liquid phase.

Claim 30

Process of claim 17 wherein the process is carried out in the vapor phase.

Claim 31

Process of claim 17 wherein the adsorbent is combined with a binder.

Claim 32

Process of claim 28 wherein the binder is selected from the group consisting of natural and synthetic clays and inorganic oxides.

Claim 33

Process of claim 17 further characterized in that said adsorbent has a capacity of at least 3% of hydrocarbon by weight of adsorbent.