Process for separating a monoethanoid fatty acid

Claim 2

A process for separating a monoethanoid fatty acid from a mixture of fatty acids comprising a monoethanoid fatty acid and a diethanoid fatty acid, wherein said monoethanoid fatty acid possesses a lesser degree of unsaturation than said diethanoid fatty acid, which comprises contacting said mixture at adsorption conditions with a nonionic hydrophobic insoluble crosslinked polystyrene polymer adsorbent to selectively adsorb said monoethanoid fatty acid having a lesser degree of unsaturation and to permit said diethanoid fatty acid having a greater degree of unsaturation to elute through said adsorbent.

Claim 3

The process of claim 1 further characterized in that said monoethanoid fatty acid is recovered by desorption with a desorbent at desorption conditions.

Claim 4

The process of claim 2 further characterized in that said adsorption 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.

Claim 5

The process of claim 3 further characterized in that it is effected in the liquid phase.

Claim 6

The process of claim 4 further characterized in that said monoethanoid fatty acid and said diethanoid fatty acid each contain 18 carbon atoms per molecule.

Claim 7

The process of claim 5 further characterized in that said desorbent comprises one of the mixtures in the group of mixtures comprising acetonitrile and methanol; acetonitrile, tetrahydrofuran and water; acetone and water; dimethyl acetamide and water; methanol and water; dimethyl formamide and water; quarternary methyl ammonium hydroxide, water and methanol; and quarternary propyl ammonium hydroxide.

Claim 8

A process for separating a monoethanoid fatty acid from a mixture of fatty acids comprising a monoethanoid fatty acid and a diethanoid fatty acid, wherein said diethanoid fatty acid possesses a higher degree of unsaturation than said monoethanoid fatty acid, which process employs a nonionic hydrophobic insoluble crosslinked polystyrene polymer adsorbent 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 to effect the selective adsorption of said monoethanoid fatty acid having a lesser degree of unsaturation by said adsorbent in said adsorption zone and withdrawing a raffinate output stream consisting essentially of said diethanoid fatty acid having a greater degree of unsaturation from said adsorption zone; (f) passing a desorbent material into said desorption zone at desorption conditions to effect the displacement of said monoethanoid fatty acid from the adsorbent in said desorption zone; (g) withdrawing an extract output stream consisting essentially of said monoethanoid fatty acid 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 at least a portion of said desorbent material from said monoethanoid fatty acid; 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 9

A process for separating a monoethanoid fatty acid from a mixture of fatty acids comprising a monoethanoid fatty acid and a diethanoid fatty acid, wherein said diethanoid fatty acid possesses a higher degree of unsaturation than said monoethanoid fatty acid, which process employs a nonionic hydrophobic insoluble crosslinked polystyrene polymer adsorbent 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 to effect the selective adsorption of said monoethanoid fatty acid having a lesser degree of unsaturation by said adsorbent in said adsorption zone and withdrawing a raffinate output stream consisting essentially of said diethanoid fatty acid having a greater degree of unsaturation from said adsorption zone; (f) passing a desorbent material into said desorption zone at desorption conditions to effect the displacement of said monoethanoid fatty acid from the adsorbent in said desorption zone; (g) withdrawing an extract output stream consisting essentially of said monoethanoid fatty acid 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 at least a portion of said desorbent material from said monoethanoid fatty acid; 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 10

The process of claim 7 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 from said diethanoid fatty acid to produce a raffinate product having a reduced concentration of desorbent material.

Claim 11

The process of claim 7 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 12

The process of claim 7 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 13

The process of claim 10 further characterized in that said monoethanoid fatty acid and said diethanoid fatty acid each contain 18 carbon atoms per molecule.

Claim 14

The process of claim 11 further characterized in that said desorbent comprises one of the mixtures in the group of mixtures comprising acetonitrile and methanol; acetonitrile, tetrahydrofuran and water; acetone and water; dimethyl acetamide and water; methanol and water; dimethyl formamide and water; quarternary methyl ammonium hydroxide, water and methanol; and quarternary propyl ammonium hydroxide.