Process for purifying sucrose fatty acid esters

• US 5,008,387 A
• Filed: 04/14/1989
• Issued: 04/16/1991
• Est. Priority Date: 04/18/1988
• Status: Expired due to Fees

• Current Assignee: Dai-Ichi Kogyo Seiyaku Company Limited
• Original Assignee: Dai-Ichi Kogyo Seiyaku Company Limited
• Inventors: Nakajima, Akihiko, Matsumoto, Shusaku, Hatakawa, Yoshio
• Primary Examiner(s): Griffin, Ronald W.
• Assistant Examiner(s): White, Everett
• Application Number:
  US07/338,012
• Time in Patent Office: 732 Days
• Field of Search: 536/127, 536/124, 536/119, 536/115, 536/120
• US Class Current: 536/119
• CPC Class Codes: C07H 13/06 Fatty acids

Abstract

From a reaction mixture obtained by reaction of sucrose and a fatty acid alkyl ester in the presence of a catalyst, a purified sucrose fatty acid ester is prepared without using organic solvents for purification by adding water to the reaction mixture and subjecting the resulting aqueous solution to ultrafiltration, thereby removing the unreacted sucrose, the catalyst or a salt derived from the catalyst, and the volatile component used as the reaction medium together with water. A powder of the purified sucrose fatty acid ester is easily, economically and safely prepared by subjecting the aqueous solution remaining in the ultrafiltration to reverse osmosis and spray-drying the resulting concentrate.

Claims

1. A process for treating a reaction mixture containing a sucrose fatty acid ester produced by the reaction of sucrose and a fatty acid alkyl ester in the presence of catalyst, which comprises subjecting to ultrafiltration an aqueous solution of a sucrose fatty acid ester containing the unreacted sucrose, the unreacted fatty acid alkyl ester, the catalyst, a soap, a fatty acid and a volatile component, wherein said reaction mixture is adjusted to pH in the range between 7.1 to 8.2 by adding an acid to the reaction mixture prior to addition of water.

2. The process of claim 1, wherein the membrane used for the ultrafiltration is made of a polysulfone or a polyvinylidene fluoride.

3. The process of claim 2, wherein said membrane for ultrafiltration has a fractionation molecular weight of 1,000 to 100,000.

4. The process of claim 1, wherein said aqueous solution of a sucrose fatty acid ester is prepared from the reaction mixture obtained by the reaction of sucrose and a fatty acid methyl ester by adding water to the reaction mixture in a reaction mixture/water ratio of 1:

5 to 1;

40 by weight.

5. The process of claim 1, wherein said aqueous solution is maintained at a temperature of 40°

to 60°

C.

6. The process of claim 1, wherein said ultrafiltration is a carried out under a pressure of 1.0 to 20.0 kg/cm² G.

7. The process of claim 1, wherein said reaction mixture is composed of 15 to 95% by weight of a sucrose fatty acid ester, 1 to 80% by weight of the unreacted sucrose, 0.5 to 10% by weight of an unreacted fatty acid methyl ester, 0.05 to 7% by weight of K₂ CO₃ as a catalyst, 1 to 60% by weight of soap, 0.5 to 10% by weight of a fatty acid and 0 to 50% by weight of a volatile component.

8. The process of claim 1, wherein the fatty acid residues of said fatty acid alkyl ester, soap and fatty acid are the same and have 8 to 22 carbon atoms.

9. The process of claim 1, wherein said volatile component is a member selected from the group consisting of water, dimethylsulfoxide and dimethylformamide.

10. A process for preparing a powder of a sucrose fatty acid ester which comprises subjecting an aqueous solution of a reaction mixture obtained by the reaction of sucrose and a fatty acid methyl ester in the presence of a catalyst to ultrafiltration, said reaction mixture containing the unreacted sucrose, the unreacted fatty acid methyl ester, the catalyst, a soap, a fatty acid and a volatile component, thereby separating the unreacted sucrose, a salt drived from the catalyst and the volatile component with water, bringing the remaining aqueous solution containing the sucrose fatty acid ester, the unreacted fatty acid methyl ester, the soap and the fatty acid into contact with a reverse osmosis membrane, thereby concentrating the aqueous solution, and spray drying the resulting concentrate.

11. The process of claim 10, wherein said reaction mixture is composed of 1 to 80% by weight of the unreacted sucrose, 0.5 to 10% by weight of the unreacted fatty acid methyl ester, 0.05 to 7% by weight of the catalyst as K₂ CO₃, 1 to 60% by weight of the soap, 0.5 to 10% by weight of the fatty acid, 0 to 50% by weight of the volatile component and 15 to 95% by weight of the sucrose fatty acid ester.

12. The process of claim 10, wherein said aqueous solution of reaction mixture is prepared by adjusting the reaction mixture to pH 7.1 to 8.2 with an acid selected from the group consisting of lactic acid, acetic acid, sulfuric acid and hydrochloric acid and adding water to the reaction mixture in a reaction mixture/water ratio of 1:

5 to 1;

40 by weight.

13. The process of claim 10, wherein said ultrafiltration is carried out at a temperature of 40°

to 60°

C. under a pressure of 1 to 20 kg/cm² G.

14. The process of claim 10, wherein the membrane used for said ultrafiltration is made of a polysulfone or a polyvinylidene fluoride and has a fractionation molecular weight of 1,000 to 100,000.

15. The process of claim 10, wherein said fatty acid methyl ester has a C₈ to C₂₂ fatty acid residue, said sucrose fatty acid ester has a softening point or melting point of at least 47°

C., and the fatty acid residues of the soap and the fatty acid are the same as the fatty acid residue of the fatty acid methyl ester.

16. The process of claim 10, wherein said reverse osmosis membrane is made of a polyether resin and has a fractionation molecular weight of 60.

17. The process of claim 10, wherein the reverse osmosis is carried out under a pressure of 50 to 65 kg/cm² G.

18. The process of claim 10, wherein the solid content of said concentrate to be spray-dried is from 4 to 40% by weight.

19. The process of claim 10, wherein said spray drying is carried out while blowing dry air having an absolute humidity of 0.008 to 0.05 kg water/kg dry air and maintained at a temperature of 10°

to 100°

C.