CN104230859A - Preparation technique of sorbitan monooleate - Google Patents
Preparation technique of sorbitan monooleate Download PDFInfo
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- CN104230859A CN104230859A CN201410427597.8A CN201410427597A CN104230859A CN 104230859 A CN104230859 A CN 104230859A CN 201410427597 A CN201410427597 A CN 201410427597A CN 104230859 A CN104230859 A CN 104230859A
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- C—CHEMISTRY; METALLURGY
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- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/04—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having no double bonds between ring members or between ring members and non-ring members
- C07D307/18—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having no double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D307/20—Oxygen atoms
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The invention discloses a preparation technique of sorbitan monooleate, which comprises the following steps: sequentially adding oleic acid, sorbitol and a composite catalyst into a vacuum reaction kettle, and starting a material circulating pump when the material temperature is greater than 165 DEG C; reacting for 8.5-9 hours, taking samples every other 15-30 minutes, observing the product transparency, and discharging the heat-conducting oil when the product is transparent; and cooling to 80-90 DEG C, and removing the vacuum of the reaction kettle to obtain the sorbitan monooleate product. The technique is simple and easy to operate, greatly shortens the reaction time and lowers the production cost; by adopting the composite catalyst of sodium hydroxide and high-purity phosphite, the reaction time is shortened, and the production technique is simplified; the product has the advantages of light color, favorable interior regularity, favorable flowability, no need of decolorization and lower cost; and the reaction temperature of the technique is 20-40 DEG C lower than that of the traditional technique, thereby saving the energy.
Description
Technical field
The present invention relates to a kind of preparation technology of sorbitan monooleate.
Background technology
Dehydrating sorbitol monooleate belongs to polyol-based non-ionic surfactant, is commonly used for w/o type emulsifying agent.Due to the surfactivity such as emulsification, dispersion of excellence, the feature such as the higher and micella Gibbs free energy of nontoxic, nonirritant, low volatilization, micelle-forming concentration is lower in addition, so it has purposes widely: the medicine processing being mainly used in various formulation, the solubilizing agent of injection liquid and oral liquid, emulsifying agent, the disintegrating agent of tablet, capsule dispersion agent, ointment emulsifying agent and matrix, it is also emulsifying agent the most frequently used in foodstuffs industry level.The synthesis of current home products also has a lot of defect with production.
Summary of the invention
The object of the invention is to prior art defect, a kind of preparation technology of sorbitan monooleate is provided.
Object of the present invention can be achieved through the following technical solutions:
A preparation technology for sorbitan monooleate, described technique specifically comprises the following steps:
(1) successively oleic acid, sorbyl alcohol, composite catalyst are dropped into vacuum reaction still, steam is warming up to 160 DEG C, and vacuum tightness remains on 0.07-0.09MPa, and the heat-up rate of material temperature rises to 155-160 DEG C in 2-2.5h, when material temperature is greater than 165 DEG C, open Matter Transfer pump;
(2) steam off, use thermal oil instead and heat up, now thermal oil temperature controls at 220-240 DEG C, when material temperature reaches 190 DEG C, thermal oil temperature is brought up to 240-260 DEG C;
(3) material final temperature controls at 210-220 DEG C, and vacuum degree control is at 0.09-0.098MPa;
(4) react 8.5-9h, start, every 15-30min sampling, to see product transparency, after product is transparent, release thermal oil, cooling to material temperature is 80-90 DEG C, breaks reactor vacuum, obtaining sorbitan monooleate product, controlling at 9-10h from being warmed up to the cooling end time.
Preferably, the mass ratio of described oleic acid, sorbyl alcohol is 1.75-1.85: 1.
Preferably, the mass ratio of described oleic acid, sorbyl alcohol is 1.8: 1.
Preferably, described composite catalyst is sheet alkali and phosphorous acid mixture.
Dehydration reaction due to sorbyl alcohol is actually very complicated, and resultant is the mixture of multiple compounds, and therefore, its esterification reaction product is also diversified.Product is mono fatty acid ester mainly, but also containing complicated products such as di fatty acid ester, tri-fatty acid ester, four fatty acid esters.If not exclusively, when having water to exist, the reversed reaction of esterification also can be there is, will seriously reduce the content of ester in product in dehydration.And the too high local superheating that can make of dehydration temperaturre causes carbonization, the method for lesser temps, condition of high vacuum degree therefore should be taked to dewater, the problem that should be noted that prevents punching material.Esterification should be carried out under certain high temperature, to obtain the mixture of the higher sorbitan ester of content.Esterification time is short, and esterification is incomplete, and product acid number is high; Esterification time increases, and acid number declines; If the reaction times is long, the decomposition reaction of ester increases, and shows acid number and is gone up on the contrary by low.Therefore, the processing condition that certain temperature and time is obtained high-quality Arlacel-80 key are controlled.
Catalyzer has: NaOH, H3PO3, H3PO4 etc., no matter adopts which kind of catalyzer, and its action principle is all release H+ or OH-, enhance esterification speed.
Under the condition that alkyd mass ratio (1.8: 1) is identical, in temperature 210 DEG C, vacuum degree control at 0.095MPa.Add different catalysts, investigate different catalysts to the impact of building-up reactions, as following table 1;
The relation of the different types of catalyzer of table 1 and product
| Catalyzer | Time | Acid number | Hydroxyl value | Color |
| NaOH | 12 | 3.5 | 215 | Brown |
| NaOH+H 3PO 4 | 9.5 | 1.5 | 195 | Yellow |
| H 3PO 3(technical grade)+NaOH | 10 | 2.1 | 190 | Amber |
| H 3PO 3(high purity)+NaOH | 9 | 0.9 | 200 | Faint yellow |
Can be found out by upper table, use the quality of different catalysts to product to have very large difference.Be used alone sodium hydroxide, the catalytic activity of its esterification is large, and its etherification activity is little, its reaction is etherificate after first esterification, so hydroxyl value is larger, the reaction times is long, be oxidized relatively more serious in reaction, color is dark, and mix mode catalyst effect is significantly better than independent catalysis.Sodium hydroxide and phosphorous acid (high purity) is mixed to be used to mix with sodium hydroxide and phosphorous acid (technical grade) and to use and compared with sodium hydroxide mixes use with phosphoric acid, sodium hydroxide and phosphorous acid (high purity) mix and use indices all will get well, and use so select sodium hydroxide and phosphorous acid (high purity) to mix.
Catalyst levels
Under alkyd mass ratio is 1.8: 1 identical conditions, add sodium hydroxide and high purity phosphorous acid mix mode catalyzer, investigate add different amount sodium hydroxide on the impact of product index, as following table 2:
The consumption of table 2 catalyzer and the relation of product
| Catalyzer | Time | Acid number | Hydroxyl value | Color |
| 0.2％H 3PO 3，0.1％NaOH | 13 | 3.5 | 188 | Faint yellow |
| 0.2％H 3PO 3，0.2％NaOH | 11 | 1.8 | 195 | Faint yellow |
| 0.2％H 3PO 3.0.3％NaOH | 9 | 0.9 | 200 | Yellow |
| 0.2％H 3PO 3，0.4％NaOH | 7.5 | 0.8 | 225 | Brown |
As can be seen from the above table, along with the increase adding amount of sodium hydroxide, hydroxyl value, the color of product also increase thereupon, although shorten the reaction times, comprehensive finished product index request, can draw and add 0.2%H
3pO
3under (high purity) condition, add 0.3%NaOH, total reaction time is best when 9h, just can obtain good product.
After 70% sorbyl alcohol dehydration etherificate, proportion increases a lot, and make whole material system layering, cause sorbyl alcohol to contact minimizing with oleic acid, speed of response slows down.This technique adds material circulation device, sorbyl alcohol is fully contacted with oleic acid, fast reaction speed, and reduces temperature of reaction, and in 8.5-9 hour, system acid value just can be made to reach within 1, and this is that traditional technology is inaccessiable.
Beneficial effect of the present invention: the present invention adopts one-step synthesis method Arlacel-80, have technique relative to two-step approach reaction and simply easily operate, the reaction times shortens greatly, reduces production cost; The present invention selects sodium hydroxide and high purity phosphorous acid composite catalyst, and it not only can carry out simultaneously in etherificate, esterification, and the whole production time is 8.5-9 hour, shortens the reaction times, simplifies production technique; And the product color of institute's output is shallow, inner regularity is good, good fluidity, without the need to decolouring, reduces cost; This technological process temperature of reaction 20-40 DEG C lower than traditional technology, has saved the energy.
Embodiment
Below in conjunction with specific embodiment, the present invention is described in further detail.
Embodiment 1
Get the raw materials ready: oleic acid 2250kg, sorbyl alcohol 1250kg (70%), phosphorous acid (high purity) 7kg, sheet alkali 10.5kg, feeding sequence: oleic acid, sorbyl alcohol, composite catalyst (phosphorous acid and sheet alkali);
Preparation process:
(1) successively oleic acid, sorbyl alcohol, composite catalyst are dropped into vacuum reaction still, steam is warming up to 160 DEG C, and vacuum tightness is 0.07MPa, and material temperature heats up and reaches 160 DEG C in 2.5h.Material temperature to 165 DEG C, opens material circulation device.
(2) steam off, use thermal oil instead and heat up, thermal oil temperature controls at 240 DEG C, when material temperature reaches 190 DEG C, improves thermal oil temperature value 260 DEG C.
(3) material final temperature controls at 220 DEG C, and vacuum degree control is at 0.098MPa.
(4) reaction times 8.5h, start, every 15min sampling, to observe product transparency, after product is transparent, releases thermal oil, cooling to material temperature is 80 DEG C, and broken reactor vacuum, obtains sorbitan monooleate product.
Embodiment 2
Get the raw materials ready: oleic acid 2188kg, sorbyl alcohol 1250kg (70%), phosphorous acid (high purity) 7kg, sheet alkali 10.5kg, feeding sequence: oleic acid, sorbyl alcohol, composite catalyst (phosphorous acid and sheet alkali);
Preparation process:
(1) successively oleic acid, sorbyl alcohol, composite catalyst are dropped into vacuum reaction still, steam is warming up to 160 DEG C, and vacuum tightness is 0.07MPa, and material temperature heats up and reaches 160 DEG C in 2h.Material temperature to 165 DEG C, opens material circulation device.
(2) steam off, use thermal oil instead and heat up, thermal oil temperature controls at 230 DEG C, when material temperature reaches 190 DEG C, improves thermal oil temperature value 250 DEG C.
(3) material final temperature controls at 215 DEG C, and vacuum degree control is at 0.095MPa.
(4) reaction times 8.7h, start every 30min sampling, observe product transparency, after product is transparent, release thermal oil, cooling to material temperature is 80 DEG C, and vacuum breaker reactor, obtains sorbitan monooleate product.
Embodiment 3
Get the raw materials ready: oleic acid 2312kg, sorbyl alcohol 1250kg (70%), phosphorous acid (high purity) 7kg, sheet alkali 10.5kg, feeding sequence: oleic acid, sorbyl alcohol, composite catalyst (phosphorous acid and sheet alkali);
Preparation process:
(1) successively oleic acid, sorbyl alcohol, composite catalyst are dropped into vacuum reaction still, steam is warming up to 160 DEG C, and vacuum tightness is 0.07MPa, and material temperature heats up and reaches 160 DEG C in 2.5h.Material temperature to 165 DEG C, opens material circulation device.
(2) steam off, use thermal oil instead and heat up, thermal oil temperature controls at 220 DEG C, when material temperature reaches 190 DEG C, improves thermal oil temperature value 240 DEG C.
(3) material final temperature controls at 210 DEG C, and vacuum degree control is at 0.090MPa.
(4) reaction times 9h, start every 15min sampling, observe product transparency, after product is transparent, release thermal oil, cooling to material temperature is 80 DEG C, and vacuum breaker reactor, obtains sorbitan monooleate product.
Above content is only to structure example of the present invention and explanation; affiliated those skilled in the art make various amendment to described specific embodiment or supplement or adopt similar mode to substitute; only otherwise depart from the structure of invention or surmount this scope as defined in the claims, protection scope of the present invention all should be belonged to.
Claims (4)
1. a preparation technology for sorbitan monooleate, is characterized in that, described technique specifically comprises the following steps:
(1) successively oleic acid, sorbyl alcohol, composite catalyst are dropped into vacuum reaction still, steam is warming up to 160 DEG C, and vacuum tightness remains on 0.07-0.09MPa, and the heat-up rate of material temperature rises to 155-160 DEG C in 2-2.5h, when material temperature is greater than 165 DEG C, open Matter Transfer pump;
(2) steam off, use thermal oil instead and heat up, now thermal oil temperature controls at 220-240 DEG C, when material temperature reaches 190 DEG C, thermal oil temperature is brought up to 240-260 DEG C;
(3) material final temperature controls at 210-220 DEG C, and vacuum degree control is at 0.09-0.098MPa;
(4) react 8.5-9h, start, every 15-30min sampling, to see product transparency, after product is transparent, release thermal oil, cooling to material temperature is 80-90 DEG C, breaks reactor vacuum, obtaining sorbitan monooleate product, controlling at 9-10h from being warmed up to the cooling end time.
2. the preparation technology of sorbitan monooleate according to claim 1, is characterized in that, the mass ratio of described oleic acid, sorbyl alcohol is 1.75-1.85: 1.
3. the preparation technology of sorbitan monooleate according to claim 2, is characterized in that, the mass ratio of described oleic acid, sorbyl alcohol is 1.8: 1.
4. the preparation technology of sorbitan monooleate according to claim 1, is characterized in that, described composite catalyst is sheet alkali and phosphorous acid mixture.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105669607A (en) * | 2015-12-30 | 2016-06-15 | 江苏省海安石油化工厂 | Preparation method for sorbitan trioleate |
| CN106117167A (en) * | 2016-06-28 | 2016-11-16 | 江苏省海安石油化工厂 | The preparation method of Arlacel-60 |
| CN106167476A (en) * | 2016-07-20 | 2016-11-30 | 广州嘉德乐生化科技有限公司 | A kind of preparation method of Sorbitan Oleate |
| CN107325274A (en) * | 2017-08-28 | 2017-11-07 | 辽宁奥克医药辅料股份有限公司 | A kind of preparation method of low color polyoxyethylene sorbitan monoleate |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4297290A (en) * | 1980-07-17 | 1981-10-27 | Ici Americas Inc. | Process for preparing sorbitan esters |
| CN102260228A (en) * | 2011-03-03 | 2011-11-30 | 广东省肇庆市超能实业有限公司 | Production process for synthesizing pharmaceutic adjuvant of sorbitan oleate or Span-80 by one step |
| CN102731226A (en) * | 2011-04-11 | 2012-10-17 | 四川雅化实业集团股份有限公司 | Method for producing emulsifier used for emulsion explosive |
| CN102875793A (en) * | 2012-09-24 | 2013-01-16 | 辽宁科技大学 | Synthesis and application of sorbitan monooleate polyoxyethylene ether for iron ore flotation |
| CN103087015A (en) * | 2012-12-19 | 2013-05-08 | 湖北葛店人福药用辅料有限责任公司 | Preparation method of sorbitan oleate servicing as medicinal auxiliary material |
-
2014
- 2014-08-28 CN CN201410427597.8A patent/CN104230859A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4297290A (en) * | 1980-07-17 | 1981-10-27 | Ici Americas Inc. | Process for preparing sorbitan esters |
| CN102260228A (en) * | 2011-03-03 | 2011-11-30 | 广东省肇庆市超能实业有限公司 | Production process for synthesizing pharmaceutic adjuvant of sorbitan oleate or Span-80 by one step |
| CN102731226A (en) * | 2011-04-11 | 2012-10-17 | 四川雅化实业集团股份有限公司 | Method for producing emulsifier used for emulsion explosive |
| CN102875793A (en) * | 2012-09-24 | 2013-01-16 | 辽宁科技大学 | Synthesis and application of sorbitan monooleate polyoxyethylene ether for iron ore flotation |
| CN103087015A (en) * | 2012-12-19 | 2013-05-08 | 湖北葛店人福药用辅料有限责任公司 | Preparation method of sorbitan oleate servicing as medicinal auxiliary material |
Non-Patent Citations (4)
| Title |
|---|
| 冯西平: "催化剂对合成失水山梨醇油酸酯酯化反应的影响", 《科技资讯》, no. 17, 13 June 2010 (2010-06-13) * |
| 李晓光 等: "失水山梨醇油酸酯合成新工艺", 《化工时刊》, vol. 23, no. 3, 25 March 2009 (2009-03-25) * |
| 杨晓东 等: "优质失水山梨醇单油酸酯的合成", 《江苏化工》, vol. 32, no. 3, 30 June 2004 (2004-06-30) * |
| 毛连山 等: "优质失水山梨醇单油酸酯的合成", 《化工时刊》, vol. 19, no. 5, 31 May 2005 (2005-05-31) * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105669607A (en) * | 2015-12-30 | 2016-06-15 | 江苏省海安石油化工厂 | Preparation method for sorbitan trioleate |
| CN106117167A (en) * | 2016-06-28 | 2016-11-16 | 江苏省海安石油化工厂 | The preparation method of Arlacel-60 |
| CN106167476A (en) * | 2016-07-20 | 2016-11-30 | 广州嘉德乐生化科技有限公司 | A kind of preparation method of Sorbitan Oleate |
| CN107325274A (en) * | 2017-08-28 | 2017-11-07 | 辽宁奥克医药辅料股份有限公司 | A kind of preparation method of low color polyoxyethylene sorbitan monoleate |
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