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 is comprising the following steps: a) Hydrolysing a triglyceride oil with water in presence of an enzyme and obtaining an 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 for maintaining 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, c) Condensing and/or interesterifying in presence of an enzyme the glyceride containing fraction, and d) Collecting a deodorized oil containing less than 1% w/w, preferably less than 0.5% free fatty acids and containing from 1.5 to 25% mono-acyl glycerides.

2-15. (canceled)

16. The process according to claim 1 wherein the collected deodorized oil contains less than 0.5% free fatty acids.

17. The process according to claim 1 wherein the collected oil is freed from enzyme by filtration and/or bleaching.

18. The process according to claim 1 wherein the collected oil is bleached.

19. The process according to claim 1 wherein the collected oil is deodorized at a temperature not higher than 210 C.

20. The process according to claim 1 wherein the collected oil is deodorized at a temperature not higher than 190 C.

21. The process according to claim 1 wherein the glyceride containing fraction is a di-acyl-glyceride rich product containing at least 20% w/w of di-acyl-glycerides.

22. The process according to claim 1 wherein in step b) the free fatty acids are removed by decanting 20 to 80% w/w of the hydrophobic phase and maintaining the 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.

23. The process according to claim 22 wherein the glyceride containing fraction is refined into a di-acyl glyceride rich fraction containing at least 20% w/w of di-acyl-glycerides.

24. The process according to claim 1 wherein in step b) the glyceride containing fraction is obtained by neutralization and/or distilling the formed free fatty acids.

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

26. The process according to claim 1 wherein the interesterifying enzyme and the hydrolysing enzyme are different in selectivity and/or stability.

27. A deodorized oil comprising 30 to 70% triglycerides, 20 to 50% di-acyl glycerides, and 1.5 to 25% mono-acyl glycerides.

28. The deodorized oil according to claim 27 wherein the mono-acylglycerides are present in an amount of from 3% to 15%,

29. The deodorized oil according to claim 27 wherein the mono-acylglycerides are present in an amount of from 5% to 10%.

30. The deodorized oil according to claim 27 wherein the di-acyl glycerides are present in an amount from 30 to 45%.

31. The deodorized oil according to claim 27 wherein the amount of triglycerides is from 35 to 60%, the amount of di-acyl glycerides is from 30 to 45%, and the amount of mono-acyl glycerides is from 3 to 10%.

32. The deodorized oil according to claim 27 wherein the amount of free fatty acids is less than 0.1%.

Description

EXAMPLES

Example 1

[0042] Palm Stearin (Low MAG)

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

[0043] Palm Stearin (High MAG)

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

[0044] DAG From Short Path Evaporation (SPE) Distillate

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

[0045] DAG From SPE Distillate

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.