Process for the manufacture of fatty acid nitriles and glycerol from glycerides, especially from natural fats and oils

Claim 2

A process for producing simultaneously glycerol and saturated or olefinically unsaturated fatty acid nitriles without isolating intermediates by treating fatty acid glycerides or mixtures of fatty acid glycerides with gaseous ammonia at elevated temperatures in the presence of catalysts, wherein the improvement comprises contacting the liquid fatty acid glyceride at temperatures of from about 220° to about 300° C. with a flow of at least 200 liters ammonia per kilogram of fatty acid glyceride per hour in the presence of metal salt of a carboxylic or sulfonic acid as a catalyst, wherein in said metal salt the metal cation is lead, cadmium, iron, cobalt, zinc, tin, titanium, zirconium, chromium, antimony, manganese, or nickel and the anion is selected from the group consisting of saturated aliphatic mono- and polycarboxylic acids; olefinically unsaturated aliphatic mono- and polycarboxylic acids; mono-, di-, and trialkylated benzene and naphthalene mono- and polycarboxylic acids; alkane mono- and disulfonic acids; fluorosubstituted alkane monosulfonic acids; monohydroxy-substituted alkane monosulfonic acids; mono-, di-, and trialkylated benzene- and naphthalene- mono- and polysulfonic acids; and (monocarboxy)alkyl and (dicarboxy)alkyl benzene and naphthalene mono- and polysulfonic acids; or mixtures of said catalysts; removing a product mixture containing said nitriles, glycerol, and water formed from the liquid fatty acid glycerides, and subjecting the product mixture to a phase separation into a nitrile phase and a glycerol/water phase.

Claim 3

The process as claimed in claim 1, wherein said glycerides are vegetable or animal fats and oils.

Claim 4

The process as claimed in claim 1, wherein said glycerides are tri-, di-, and monoglycerides of the formula ##STR3## wherein X is H or CO--R 2 ; Y is H or CO--R 3 , and R 1 , R 2 , R 3 , are selected from the group consisting of (a) alkyl radicals containing from 3 to 23 carbon atoms; (b) olefinically unsaturated aliphatic hydrocarbon radicals containing from 3 to 23 carbon atoms and having from 1 to 6 isolated or conjugated double bonds; (c) monohydroxy-substituted alkyl radicals containing from 3 to 23 carbon atoms; (d) monohydroxy-substituted olefinically unsaturated aliphatic hydrocarbon radicals containing from 3 to 23 carbon atoms and having from 1 to 6 double bonds.

Claim 5

The process as claimed in claim 1, wherein the temperature is raised from about 220° C. at the beginning of the reaction to about 300° C. at the end of the reaction.

Claim 6

The process as claimed in claim 1, which comprises maintaining a temperature level in the range of from about 220° to about 240° C. until between 30 and 70 percent of the theoretical amount of glycerol is removed, then raising the temperature over a period from about 0.5 to about 5 hours to a temperature level in the range of from about 270° to about 300° C. and completing the reaction.

Claim 7

The process as claimed in claim 1, which comprises subjecting fatty acids and fatty acid amides contained in said product mixture as by-products to an aftertreatment with ammonia prior to or following the phase separation.

Claim 8

The process as claimed in claim 1, which comprises removing the product mixture by means of fractionated distillation, whereby recycling fatty acids and fatty acid amides contained in said product mixture as by-products, and then subjecting the product mixture to the phase separation.

Claim 9

A process for producing simultaneously glycerol and saturated or olefinically unsaturated fatty acid nitriles without isolating intermediates by treating fatty acid glycerides or mixtures of fatty acid glycerides with gaseous ammonia at elevated temperatures in the presence of catalysts, wherein the improvement comprises contacting the liquid fatty acid glyceride at temperatures of from about 220° to about 300° C. with a flow of at least 200 liters ammonia per kilogram of fatty acid glyceride per hour in the presence of metal salt of a carboxylic or sulfonic acid as a catalyst, wherein in said metal salt the metal cation is lead, cadmium, iron, cobalt, zinc, tin, titanium, zirconium, chromium, antimony, manganese, or nickel and the anion is selected from the groups consisting of saturated aliphatic mono- and polycarboxylic acids; olefinically unsaturated aliphatic mono- and polycarboxylic acids; mono-, di- and trialkylated benzene and naphthalene mono- and polycarboxylic acids; alkane mono- and disulfonic acids; fluoro-substituted alkane monosulfonic acids; monohydroxy-substituted alkane monosulfonic acids; mono-, di-, and trialkylated benzene and naphthalene mono- and polysulfonic acids; and (monocarboxy)alkyl and (dicarboxy)alkyl benzene and naphthalene mono- and polysulfonic acids; or mixtures of said catalysts; removing a part of the product mixture containing substantially the entire amount of glycerol and a proportional portion of water and of the nitrile formed from the liquid fatty acid glycerides, subjecting said part of the product mixture to a phase separation into a nitrile phase and a glycerol/water phase, water-extracting and combining the separated nitrile phase with the unremoved nitrile portion and treating said combined nitriles with a flow of ammonia of from about 5 to about 150 liters ammonia per kilogram nitrile per hour at temperatures of from about 200° to about 320° C. in the presence of said catalysts defined hereinbefore.

Claim 10

A process for producing simultaneously glycerol and saturated or olefinically unsaturated fatty acid nitriles without isolating intermediates by treating fatty acid glycerides or mixtures of fatty acid glycerides with gaseous ammonia at elevated temperatures in the presence of catalysts, wherein the improvement comprises contacting the liquid fatty acid glyceride at temperatures of from about 220° to about 300° C. with a flow of at least 200 liters ammonia per kilogram of fatty acid glyceride per hour in the presence of metal salt of a carboxylic or sulfonic acid as a catalyst, wherein in said metal salt the metal cation is lead, cadmium, iron, cobalt, zinc, tin, titanium, zirconium, chromium, antimony, manganese, or nickel and the anion is selected from the groups consisting of saturated aliphatic mono- and polycarboxylic acids; olefinically unsaturated aliphatic mono- and polycarboxylic acids; mono-, di- and trialkylated benzene and naphthalene mono- and polycarboxylic acids; alkane mono- and disulfonic acids; fluoro-substituted alkane monosulfonic acids; monohydroxy-substituted alkane monosulfonic acids; mono-, di-, and trialkylated benzene and naphthalene mono- and polysulfonic acids; and (monocarboxy)alkyl and (dicarboxy)alkyl benzene and naphthalene mono- and polysulfonic acids; or mixtures of said catalysts; removing a part of the product mixture containing substantially the entire amount of glycerol and a proportional portion of water and of the nitrile formed from the liquid fatty acid glycerides, subjecting said part of the product mixture to a phase separation into a nitrile phase and a glycerol/water phase, water-extracting and combining the separated nitrile phase with the unremoved nitrile portion and treating said combined nitriles with a flow of ammonia of from about 5 to about 150 liters ammonia per kilogram nitrile per hour at temperatures of from about 200° to about 320° C. in the presence of said catalysts defined hereinbefore.

Claim 11

The process of claim 1 or 8, wherein said cation of the metal salt catalyst is lead, cadmium, iron, cobalt, and zinc; and wherein the anion is selected from the group consisting of (a) alkanemonosulfonic acids, monohydroxyalkanesulfonic acids, and fluoro-substituted alkanesulfonic acids, having from 4 to 24 carbon atoms; (b) mono-, di-, and trialkylated benzene- and naphthalene-mono- and disulfonic acids, containing alkyl radicals of from 1 to 24 carbon atoms; and (c) (monocarboxy)monoalkyl and (dicarboxy)monoalkyl benzene and naphthalene mono- and disulfonic acids, containing alkyl radicals of from 1 to 26 carbon atoms.