Process for separating an ester of a monoethanoid fatty acid

Claim 2

A process for separating an ester of a monoethanoid fatty acid from a mixture comprising an ester of saturated fatty acid and an ester of an unsaturated fatty acid consisting essentially of an ester of a monoethanoid fatty acid which process comprises contacting at a temperature within the range of from about 20° C. to about 200° C. and a pressure within the range of from about atmospheric to about 500 psig. said mixture with an adsorbent comprising a X or a Y zeolite containing at exchangeable cationic sites copper cations and one or more second cations selected from the group consisting of sodium, potassium, rubidium and cesium, thereby selectively adsorbing said ester of a monoethanoid fatty acid and thereafter recovering said ester of a monoethanoid fatty acid.

Claim 3

The process of claim 1 further characterized in that said second cation is potassium and that said adsorbent is essentially completely exchanged with potassium and copper cations.

Claim 4

The process of claim 2 further characterized in that the weight ratio of copper cations to potassium cations is from about 1:1 to about 10:1.

Claim 5

The process of claim 1 further characterized in that it is effected in the liquid phase.

Claim 6

The process of claim 1 further characterized in that said ester of a monoethanoid fatty acid and said ester of a saturated fatty acid each contain from about 8 to about 26 carbon atoms per molecule.

Claim 7

The process of claim 5 further characterized in that said ester of a monoethanoid fatty acid and said ester of a saturated fatty acid are methyl esters.

Claim 8

The process of claim 6 further characterized in that said ester of a saturated fatty acid is methyl palmitate or methyl stearate.

Claim 9

The process of claim 6 further characterized in that said ester of a monoethanoid fatty acid is methyl oleate.

Claim 10

The process of claim 1 further characterized in that said ester of a monoethanoid fatty acid is recovered by desorption with a desorbent material comprising a monocyclic aromatic hydrocarbon.

Claim 11

A process for separating an ester of a monoethanoid fatty acid from a mixture comprising an ester of a saturated fatty acid and an ester of an unsaturated fatty acid consisting essentially of an ester of a monoethanoid fatty acid which process comprises the steps of: a. contacting said mixture at a temperature within the range of from about 20° C. to about 200° C. and a pressure from about atmospheric pressure to about 500 psig, with an adsorbent comprising a X or a Y zeolite essentially completely exchanged with potassium and copper cations thereby selectively adsorbing said ester of a monoethanoid fatty acid; b. removing from the adsorbent a raffinate stream comprising said ester of a saturated fatty acid; c. contacting said adsorbent at a temperature within the range of from about 20° C. to about 200° C. and a pressure from about atmospheric pressure to about 50 psig. with desorbent material comprising a monocyclic aromatic hydrocarbon to effect the desorption of said ester of a monoethanoid fatty acid from said adsorbent; and, d. removing from said adsorbent an extract stream comprising said ester of a monoethanoid fatty acid.

Claim 12

A process for separating an ester of a monoethanoid fatty acid from a mixture comprising an ester of a saturated fatty acid and an ester of an unsaturated fatty acid consisting essentially of an ester of a monoethanoid fatty acid which process comprises the steps of: a. contacting said mixture at a temperature within the range of from about 20° C. to about 200° C. and a pressure from about atmospheric pressure to about 500 psig, with an adsorbent comprising a X or a Y zeolite essentially completely exchanged with potassium and copper cations thereby selectively adsorbing said ester of a monoethanoid fatty acid; b. removing from the adsorbent a raffinate stream comprising said ester of a saturated fatty acid; c. contacting said adsorbent at a temperature within the range of from about 20° C. to about 200° C. and a pressure from about atmospheric pressure to about 50 psig. with desorbent material comprising a monocyclic aromatic hydrocarbon to effect the desorption of said ester of a monoethanoid fatty acid from said adsorbent; and, d. removing from said adsorbent an extract stream comprising said ester of a monoethanoid fatty acid.

Claim 13

The process of claim 10 further characterized in that the weight ratio of copper cations to potassium cations is from about 1:1 to about 10:1.

Claim 14

The process of claim 10 further characterized in that said ester of a monoethanoid fatty acid and said ester of a saturated fatty acid each contain from about 8 to about 26 carbon atoms per molecule.

Claim 15

The process of claim 12 further characterized in that said ester of a monoethanoid fatty acid and said ester of a saturated fatty acid are methyl esters.

Claim 16

The process of claim 13 further characterized in that said ester of a saturated fatty acid is methyl palmitate or methyl stearate.

Claim 17

The process of claim 13 further characterized in that said ester of a monoethanoid fatty acid is methyl oleate.

Claim 18

The process of claim 10 further characterized in that said monocyclic aromatic hydrocarbon is selected from the group consisting of benzene, toluene, xylenes, ethylbenzene and diethylbenzenes.

Claim 19

A process for separating an ester of a monoethanoid fatty acid from a mixture comprising an ester of a saturated fatty acid and an ester of an unsaturated fatty acid consisting essentially of an ester of a monoethanoid fatty acid which process employs an adsorbent comprising a X or a Y zeolite essentially completely exchanged with potassium and copper cations 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 mixture into said adsorption zone at (adsorption conditions) a temperature within the range of from about 20° C. to about 200° C. and a pressure within the range of from about atmospheric to about 500 psig. to effect the selective adsorption of said ester of a monoethanoid fatty acid by said adsorbent in said adsorption zone and withdrawing a raffinate output stream from said adsorption zone; f. passing a desorbent material comprising a monocyclic aromatic hydrocarbon into said desorption zone at a temperature within the range of from about 20° C. to about 200° C. and a pressure in the range of from about atmospheric to about 500 psig. to effect the displacement of said ester of a monoethanoid fatty acid from the adsorbent in said desorption zone; g. withdrawing an extract output stream comprising said ester of a monoethanoid fatty acid and desorbent material from said adsorption zone; h. passing at least a portion of said extract output stream to a separation means and therein separating at separation conditions at least a portion of said 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 20

A process for separating an ester of a monoethanoid fatty acid from a mixture comprising an ester of a saturated fatty acid and an ester of an unsaturated fatty acid consisting essentially of an ester of a monoethanoid fatty acid which process employs an adsorbent comprising a X or a Y zeolite essentially completely exchanged with potassium and copper cations 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 mixture into said adsorption zone at (adsorption conditions) a temperature within the range of from about 20° C. to about 200° C. and a pressure within the range of from about atmospheric to about 500 psig. to effect the selective adsorption of said ester of a monoethanoid fatty acid by said adsorbent in said adsorption zone and withdrawing a raffinate output stream from said adsorption zone; f. passing a desorbent material comprising a monocyclic aromatic hydrocarbon into said desorption zone at a temperature within the range of from about 20° C. to about 200° C. and a pressure in the range of from about atmospheric to about 500 psig. to effect the displacement of said ester of a monoethanoid fatty acid from the adsorbent in said desorption zone; g. withdrawing an extract output stream comprising said ester of a monoethanoid fatty acid and desorbent material from said adsorption zone; h. passing at least a portion of said extract output stream to a separation means and therein separating at separation conditions at least a portion of said 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 21

The process of claim 17 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 at least a portion of said desorbent material to produce a raffinate product having a reduced concentration of desorbent material.

Claim 22

The process of claim 17 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 the raffinate output stream at an upstream boundary of said buffer zone.

Claim 23

The process of claim 17 further characterized in that said adsorption conditions and desorption conditions include a temperature within the range of from about 20° C. to about 200° C. and a pressure within the range of from about atmospheric to about 500 psig. to insure liquid phase.

Claim 24

The process of claim 17 further characterized in that the weight ratio of copper cations to potassium cations is from about 1:1 to about 10:1.

Claim 25

The process of claim 17 further characterized in that said ester of a monoethanoid fatty acid and said ester of a saturated fatty acid each contain from about 8 to about 26 carbon atoms per molecule.

Claim 26

The process of claim 22 further characterized in that said ester of a monoethanoid fatty acid and said ester of a saturated fatty acid are methyl esters.

Claim 27

The process of claim 23 further characterized in that said ester of a saturated fatty acid is methyl palmitate or methyl sterate.

Claim 28

The process of claim 22 further characterized in that said ester of a monoethanoid fatty acid is methyl oleate.

Claim 29

The process of claim 10 further characterized in that it is effected in the liquid phase.

Claim 30

The process of claim 17 further characterized in that it is effected in the liquid phase.