CN1594303A - Method for separation purification of sclareolide from synthetic sclareol composites - Google Patents
Method for separation purification of sclareolide from synthetic sclareol composites Download PDFInfo
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- CN1594303A CN1594303A CN 200410019874 CN200410019874A CN1594303A CN 1594303 A CN1594303 A CN 1594303A CN 200410019874 CN200410019874 CN 200410019874 CN 200410019874 A CN200410019874 A CN 200410019874A CN 1594303 A CN1594303 A CN 1594303A
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- sclareolide
- sclareol
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- composites
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Abstract
The invention provides a method for separation purification of sclareolide from synthetic sclareol composites by using molecular distillation device for operation under pressure of 0.01-100.0Mpa, evaporative temperature 50-200 deg. C, cool-down temperature -15-80 deg. C, temperature difference between the evaporator and condenser 30-215 deg. C, the agitating speed 10-1000 rp.
Description
Technical field
The present invention relates to a kind of method of from sclareol reaction synthetics, separating the purification Sclareolide, belong to the deep processing of sclareol and utilize technology.
Background technology
Sclareolide generally obtains by the sclareol reaction is synthetic, and CN92104935 has reported the method for extracting sclareol from fragrant Asian puccoon residue.US5247100, US5212078, WO2004013069, JP2002371031, patent report such as JP2001247561 and US5525728 the synthetic method of Sclareolide: use the organic solvent dissolution sclareol, add alkaline matter, hypochlorite, ruthenium catalyst and phase-transfer catalyst then, can obtain Sclareolide through oxidation step, heating.US5906993, US5372834, US4999207, US4988532, US4960603, US4917913, US20030072777 (A1), patent reports such as WO03007734 and US6331551 the effect of high purity Sclareolide: be used for the treatment of the communicable disease that causes by microorganism (as fungi, bacterium); In blended type cigarette,, can cover the thick assorted gas of tobacco as the special efficacy flavouring correctives of tobacco; Can be used in the food that contains pleasantly sweet seasoning matter,, increase the aroma effect of food as seasonings; In coffee industry, add a small amount of Sclareolide, can increase the weight of the coffee bitter taste, improve the effect of refreshing oneself of coffee; In addition, Sclareolide still is one of main component of anti-acne medicine.In the Sclareolide building-up reactions thing, Sclareolide content generally is lower than 95.0%, does not reach purity required in food, the pharmaceutical industries (the Sclareolide mass content is greater than 99.0%).So, need the Sclareolide mixture is further separated purification.US5945546 has reported the method for purification Sclareolide from sclareol reaction synthetics.Institute's reported method is at first to remove fragment (as the microorganism cells fragment), and then with the organic solution of acid solvent extraction Sclareolide, the Sclareolide of purifying with basic solvent extraction part obtains the high purity Sclareolide at last.Though aforesaid method can obtain the Sclareolide of required purity, in this process, added extraction agent, make the finished product contain residual solvent, this has limited the application of Sclareolide as medicine and food odorant greatly; In addition, this method complex process, operating time are long, and will consume a large amount of solvents.
Summary of the invention
The object of the present invention is to provide a kind of method of from sclareol reaction synthetics, separating the purification Sclareolide.This method technology is simple, the yield height, and process is pollution-free.
The present invention is realized by following technical proposals: spacing is the short-path evaporator device of 2～15cm between employing generating surface and the condensing surface, the method of separation and Extraction Sclareolide from sclareol reaction synthetics, it is characterized in that operating with following processing condition: evaporator operation pressure is 0.01-100Pa, vaporization temperature is 50-200 ℃, cooling temperature is-15-80 ℃, and stir speed (S.S.) is 10-1000rpm.And distill repeatedly is carried out in the above single distilled last running conduct flow process of distillatory raw material next time, and 65～215 ℃ of the each distillation maintenance vaporizer and the condenser temperature difference are till reaching the product purity requirement.
Advantage of the present invention is: technology is simple, the operating time is short, yield is high, not with an organic solvent, and does not produce any other high boiling material matter, also not polymerization, environmentally safe.Compare with existing method, it is the distill repeatedly process that present method purification Sclareolide mixture reaches required concentration process, and need not be through extraction and solvent recuperation and the finished product repeatedly remove treatment steps such as solvent.
Embodiment:
(feeder volume 250ml, 4.8 square decimeters of evaporation areas add 200g Sclareolide blocks of solid mixture in the feeder of blade applicator rotating speed 50～1000rpm), contain Sclareolide 90.5% at molecular distillation apparatus.Open raw material preheating device, be warmed up to 97 ℃, make the solid dissolving and keep constant temperature.The open cold radiator cooler, keeping cooling temperature is 35 ℃, adds liquid nitrogen in cold-trap, open rotary-vane vaccum pump, make the working pressure of system reach 1.5Pa, the exact constant temperature groove that unlatching evaporation material is used heats thermal oil, makes temperature-stable 99 ℃ of required vaporization temperatures, begin feed valve then, feeding rate is 100g/h, and the rotating speed of blade applicator is 138rpm, after still-process finishes, get overhead product 18.5g, last running 181.5g; To distill gained last running for the first time is to distill under 101 ℃ as raw material in vaporization temperature, light constituent overhead product 15.4g last running 166.1g; As next step separate raw materials, vaporization temperature raises 2 ℃ at every turn with the separating obtained last running of per step, carries out (being decolouring for the last time behind five circulation lock out operation, vaporization temperature is 108.5 ℃), get light yellow product 120g, yield 65.83%, wherein Sclareolide content 99.3%; Fusing point 103-105 ℃.
It is as follows that the finished product of above embodiment are formed mass percent:
Sclareol 0.34%
Rosin alcohol 0.36%
Sclareolide 99.3%
Claims (1)
1, a kind of method of from sclareol reaction synthetics, separating the purification Sclareolide, spacing is the short-path evaporator device of 2～15cm between this method employing generating surface and the condensing surface, it is characterized in that operating with following processing condition: evaporator operation pressure is 0.01-100Pa, vaporization temperature is 50-200 ℃, cooling temperature is-15-80 ℃, stir speed (S.S.) is 10-1000rpm, and distill repeatedly is carried out in the above single distilled last running conduct flow process of distillatory raw material next time, 65～215 ℃ of the each distillation maintenance vaporizer and the condenser temperature difference are till reaching the product purity requirement.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410019874 CN1285585C (en) | 2004-07-05 | 2004-07-05 | Method for separation purification of sclareolide from synthetic sclareol composites |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410019874 CN1285585C (en) | 2004-07-05 | 2004-07-05 | Method for separation purification of sclareolide from synthetic sclareol composites |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1594303A true CN1594303A (en) | 2005-03-16 |
| CN1285585C CN1285585C (en) | 2006-11-22 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410019874 Expired - Fee Related CN1285585C (en) | 2004-07-05 | 2004-07-05 | Method for separation purification of sclareolide from synthetic sclareol composites |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1285585C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101323559B (en) * | 2008-08-05 | 2010-12-22 | 延安禾馨生物制品有限公司 | Preparing process of sclareol |
| CN101781276B (en) * | 2010-01-20 | 2011-09-28 | 华东理工大学 | Modified method for preparing sclareolide from sclareol |
| CN102766123A (en) * | 2011-05-04 | 2012-11-07 | 焦作市馨之源科技有限公司 | Production technology of sclareolide synthesized from sclareol |
-
2004
- 2004-07-05 CN CN 200410019874 patent/CN1285585C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101323559B (en) * | 2008-08-05 | 2010-12-22 | 延安禾馨生物制品有限公司 | Preparing process of sclareol |
| CN101781276B (en) * | 2010-01-20 | 2011-09-28 | 华东理工大学 | Modified method for preparing sclareolide from sclareol |
| CN102766123A (en) * | 2011-05-04 | 2012-11-07 | 焦作市馨之源科技有限公司 | Production technology of sclareolide synthesized from sclareol |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1285585C (en) | 2006-11-22 |
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