Process for separating para-xylene

Claim 2

A process for separating para-xylene from a feed stream comprising para-xylene and at least one other C 8 aromatic isomer which process comprises the steps of: a. contacting said feed stream at adsorption conditions with an adsorbent comprising type X or type Y zeolite containing barium and strontium in a weight ratio of barium to strontium of from about 1:1 to about 15:1 at the exchangeable cationic sites to effect the selective adsorption of para-xylene; b. removing a raffinate component comprising a less selectively adsorbed C 8 aromatic from said adsorbent; c. contacting said adsorbent with a desorbent material comprising para-diethylbenzene at desorption conditions to effect the desorption of para-xylene from said adsorbent; and, d. removing from said adsorbent an extract component comprising para-xylene.

Claim 3

The process of claim 1 further characterized in that said feed stream contains C 8 non-aromatics.

Claim 4

The process of claim 1 further characterized in that said feed stream contains ethylbenzene.

Claim 5

The process of claim 1 further characterized in that said feed stream contains ortho-xylene.

Claim 6

The process of claim 1 further characterized in that said feed stream contains meta-xylene.

Claim 7

The process of claim 1 further characterized in that said feed stream contains meta-xylene, ortho-xylene and ethylbenzene.

Claim 8

The process of claim 1 further characterized in that said adsorbent comprises type X zeolite.

Claim 9

The process of claim 1 further characterized in that said adsorbent contains a weight ratio of barium to strontium of from about 5:1 to about 15:1.

Claim 10

The process of claim 1 further characterized in that said adsorption conditions and desorption conditions include a temperature within the range of from about 20° to about 230° C. and a pressure within the range of from about atmospheric to about 500 psig. to insure liquid phase.

Claim 11

A process for the separation of para-xylene from a feed stream comprising para-xylene and at least one other C 8 aromatic isomer which process employs an adsorbent comprising type X or type Y zeolite containing barium and strontium in a weight ratio of barium to strontium of from 1:1 to about 15:1 at the exchangeable cation sites and which process comprises the steps of: a. maintaining net fluid flow through a column of said adsorbent in a single direction, which column contains at least three zones having separate operational functions occurring therein and being serially interconnected with the terminal zones of said column connected to provide a continuous connection of said zones; b. maintaining an adsorption zone in said column, said zone defined by the adsorbent located between a feed input stream at an upstream boundary of said zone and a raffinate output stream at a downstream boundary of said zone; c. maintaining a purification zone immediately upstream from said adsorption zone, said purification zone defined by the adsorbent located between an extract output stream at an upstream boundary of said purification zone and said feed input stream at a downstream boundary of said purification zone; d. maintaining a desorption zone immediately upstream from said purification zone, said desorption zone defined by the adsorbent located between a desorbent input stream at an upstream boundary of said zone and said extract output stream at a downstream boundary of said zone; e. passing said feed stream into said adsorption zone at adsorption conditions to effect the selective adsorption of para-xylene by said adsorbent in said adsorption zone and withdrawing a raffinate output stream from said adsorption zone; f. passing a desorbent material comprising para-diethylbenzene into said desorption zone at desorption conditions to effect the displacement of para-xylene from the adsorbent in said desorption zone; g. withdrawing an extract stream comprising para-xylene and desorbent material from said desorption zone; h. passing at least a portion of said extract output stream to a separation means and therein separating at separation conditions para-xylene from said desorbent material to produce a para-xylene product substantially free of desorbent material; and, i. periodically advancing through said column of adsorbent in a downstream direction with respect to fluid flow in said adsorption zone the feed input stream, raffinate output stream, desorbent input stream, and extract output stream to effect the shifting of zones through said adsorbent and the production of extract output and raffinate output streams.

Claim 12

A process for the separation of para-xylene from a feed stream comprising para-xylene and at least one other C 8 aromatic isomer which process employs an adsorbent comprising type X or type Y zeolite containing barium and strontium in a weight ratio of barium to strontium of from 1:1 to about 15:1 at the exchangeable cation sites and which process comprises the steps of: a. maintaining net fluid flow through a column of said adsorbent in a single direction, which column contains at least three zones having separate operational functions occurring therein and being serially interconnected with the terminal zones of said column connected to provide a continuous connection of said zones; b. maintaining an adsorption zone in said column, said zone defined by the adsorbent located between a feed input stream at an upstream boundary of said zone and a raffinate output stream at a downstream boundary of said zone; c. maintaining a purification zone immediately upstream from said adsorption zone, said purification zone defined by the adsorbent located between an extract output stream at an upstream boundary of said purification zone and said feed input stream at a downstream boundary of said purification zone; d. maintaining a desorption zone immediately upstream from said purification zone, said desorption zone defined by the adsorbent located between a desorbent input stream at an upstream boundary of said zone and said extract output stream at a downstream boundary of said zone; e. passing said feed stream into said adsorption zone at adsorption conditions to effect the selective adsorption of para-xylene by said adsorbent in said adsorption zone and withdrawing a raffinate output stream from said adsorption zone; f. passing a desorbent material comprising para-diethylbenzene into said desorption zone at desorption conditions to effect the displacement of para-xylene from the adsorbent in said desorption zone; g. withdrawing an extract stream comprising para-xylene and desorbent material from said desorption zone; h. passing at least a portion of said extract output stream to a separation means and therein separating at separation conditions para-xylene from said desorbent material to produce a para-xylene product substantially free of desorbent material; and, i. periodically advancing through said column of adsorbent in a downstream direction with respect to fluid flow in said adsorption zone the feed input stream, raffinate output stream, desorbent input stream, and extract output stream to effect the shifting of zones through said adsorbent and the production of extract output and raffinate output streams.

Claim 13

The process of claims 10 further characterized in that said feed stream contains C 8 non-aromatics.

Claim 14

The process of claim 10 further characterized in that said feed stream contains ethylbenzene.

Claim 15

The process of claim 10 further characterized in that said feed stream contains ortho-xylene.

Claim 16

The process of claim 10 further characterized in that said feed stream contains meta-xylene.

Claim 17

The process of claim 10 further characterized in that said feed stream contains meta-xylene, ortho-xylene and ethylbenzene.

Claim 18

The process of claim 10 further characterized in that said zeolite comprises type X zeolite.

Claim 19

The process of claim 10 further characterized in that said adsorbent contains a weight ratio of barium to strontium of from about 5:1 to about 15:1.

Claim 20

The process of claim 10 further characterized in that it includes the step of passing at least a portion of said raffinate output stream to a separation means and therein separating at separation conditions raffinate components from desorbent material to produce a raffinate product substantially free of desorbent material.

Claim 21

The process of claim 10 further characterized in that it includes the step of maintaining a buffer zone immediately upstream from said desorption zone, said buffer zone defined as the adsorbent located between the desorbent input stream at a downstream boundary of said buffer zone and a raffinate output stream at an upstream boundary of said buffer zone.

Claim 22

The process of claim 10 further characterized in that said adsorption conditions and desorption conditions include a temperature within the range of from about 20° to about 230° C. and a pressure within the range of from about atmospheric to about 500 psig to insure liquid phase.