Oil composition with mono-acylglycerides

Abstract

The present invention relates to a process for preparing a deodorized oil with in-situ prepared mono-acylglycerides and the oil obtained as such. It relates to a process for preparing a deodorized oil containing in-situ prepared mono-acylglycerides by interesterifying in presence of an enzyme a glyceride containing fraction wherein the ratio of free and esterified hydroxyl groups (OH) to free and esterified fatty acids (FA) is greater than 1.07 and obtaining an oily composition containing less than 1% w/w, preferably less than 0.5% free fatty acids. Furthermore it relates to a deodorized oil containing 30 to 70% triglycerides, 20 to 50% di-acyl glycerides, 1.5 to 25% mono-acyl glycerides.

Claims

1. A process for preparing a deodorized oil containing in-situ prepared mono-acylglycerides wherein the process consisting of the following steps: a) hydrolyzing a triglyceride oil with water in the presence of a hydrolyzing enzyme and obtaining a hydrophobic phase wherein up to 50% w/w of free fatty acids are formed, b) removing from 20% to 100% w/w of the formed free fatty acids and maintaining a glyceride containing oil fraction wherein the ratio of free and esterified hydroxyl groups (OH) to free and esterified fatty acids (FA) is greater than 1.07, c) interesterifying the glyceride containing oil fraction of b), wherein the interesterifying is carried out in a composition consisting of the glyceride oil fraction of b) and an interesterifying enzyme, so as to yield a deodorized oil, and d) collecting the deodorized oil from c) containing less than 1% w/w free fatty acids and containing from 1.5 to 25% w/w of mono-acylglycerides, 35 to 65% w/w of triacylglycerides, and 20 to 50% w/w of di-acylglycerides; and e) optionally freeing the collected deodorized oil of d) from the enzyme of a) and/or c) by filtration and/or bleaching; f) optionally deodorizing the collected deodorized oil of d) at a temperature of from 150° C. to 210° C.; wherein: the triglyceride oil is selected from the group consisting of tropical oils, palm oil, palm kernel oil, palm stearin, coconut oil, babassu oil, rapeseed oil, canola oil, sunflower oil, high oleic sunflower oil, soybean oil, corn oil, peanut oil, walnut oil, hazelnut oil, olive oil, camelina oil, linseed oil, hemp oil, safflower oil, cottonseed oil, high oleic cottonseed oil, low linolenic cottonseed oil, high oleic canola oil, low linolenic soybean oil, high stearic sunflower oil, and mixtures thereof.

2. The process according to claim 1 wherein the collected deodorized oil of d) contains less than 0.5% w/w free fatty acids.

3. The process according to claim 1 wherein the collected deodorized oil of d) is freed from the enzyme of a) and/or c) by filtration and/or bleaching.

4. The process according to claim 1 wherein the collected deodorized oil of d) is bleached.

5. The process according to claim 1 wherein the collected deodorized oil of d) is deodorized at a temperature of from 150° C. to 210° C.

6. The process according to claim 1 wherein in step b) the formed free fatty acids are removed by decanting 20 to 80% w/w of the hydrophobic phase and maintaining the glyceride containing oil fraction wherein the ratio of free and esterified hydroxyl groups (OH) to free and esterified fatty acids (FA) is greater than 1.07.

7. The process according to claim 1 wherein in step b) the glyceride containing oil fraction is obtained by neutralizing, deodorizing and/or distilling the formed free fatty acids.

8. The process according to claim 1 wherein in step a) the enzyme is a mono/di-acylglyceride selective enzyme.

9. The process according to claim 1 wherein the interesterifying enzyme of c) and the hydrolyzing enzyme of a) are different in selectivity and/or stability.

10. The process of claim 1, wherein the glyceride containing oil fraction is a di-acylglyceride rich product containing 30 to 46% w/w of di-acylglycerides.

Description

EXAMPLES

Example 1

(1) Palm Stearin (Low MAG)

(2) 37.5 kg Palm Stearin (Cargill Botlek) was mixed in Pilot reactor with 3 l water at 70° C. 200 g Lipozyme 435 was added. After 48 h the content of FFA was 23.7%. Stirring was stopped and after 30 minutes settling, 15 kg of the upper layer were taken out from the reactor. The stirring was started again, and carefully vacuum was applied to remove water and initiate condensation. After 22 h at 50-100 mbar, FFA was 1.0%. According gel permeation chromatography (GPC), the composition was 62% TAG, 33.2% DAG, 3.4% MAG, and 0.8% FFA according titration.

Example 2

(3) Palm Stearin (High MAG)

(4) 37.5 kg Palm Stearin (Cargill Botlek) was mixed in Pilot reactor with 5 l water at 70° C. 300 g Lipozyme 435 was added. After 94 h the content of FFA was 36.7%. Stirring was stopped and after 30 minutes settling, 16 kg of the upper layer were taken out from the reactor. The stirring was started again, and carefully vacuum was applied to remove water and initiate condensation. After 29 h at 50-100 mbar, FFA was 0.99%. According gel permeation chromatography (GPC), the composition was 35.25% TAG, 45.51% DAG, 8.94% MAG, and 0.96% FFA according titration.

Example 3

(5) DAG From Short Path Evaporation (SPE) Distillate

(6) 100 g distillate fraction from a short path evaporation of RBD Palm Oil with 1.8% MAG, 49% DAG, 42% TAG was interesterified under vacuum using 1% Lipozyme TL IM. After 48 h product was isolated by filtration. Composition of the final material was 6.5% MAG, 34% DAG, 54% TAG according Gel Permeation Chromatography with FFA of 0.23% according titration.

Example 4

(7) DAG From SPE Distillate

(8) 100 g distillate fraction from a short path evaporation of RBD Palm Oil with 1.7% MAG, 48% DAG, 47% TAG was interesterified under vacuum using 1% Lipozyme 435. After 48 h product was isolated by filtration. Composition of the final material was 5.3% MAG, 33.5% DAG, 58% TAG according Gel Permeation Chromatography with FFA 0.58% according titration.