CN102876464A - Process for preparing high-purity molecular distillation monoacylglycerol - Google Patents
Process for preparing high-purity molecular distillation monoacylglycerol Download PDFInfo
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- CN102876464A CN102876464A CN2012103242056A CN201210324205A CN102876464A CN 102876464 A CN102876464 A CN 102876464A CN 2012103242056 A CN2012103242056 A CN 2012103242056A CN 201210324205 A CN201210324205 A CN 201210324205A CN 102876464 A CN102876464 A CN 102876464A
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Abstract
The invention relates to a process for synthesizing high-purity molecular distillation monoacylglycerol. The process comprises the following steps of: (1) mixing glycerol and a catalyst A, vacuumizing, stirring for heating, adding hydrogenated oil added with a catalyst B into a reaction system in batches to perform ester exchange reaction, after the ester exchange reaction is finished, keeping temperature, adding phosphoric acid for neutralizing, cooling and standing a reactant for demixing, wherein an upper layer is a crude glyceride layer, a lower layer is materials which are not reacted completely and impurities generated in the reaction process; (2) dehydrating and degassing the crude glyceride layer by primary distillation; (3) performing secondary distillation on the product, and removing free fatty acid and excessive glycerol; and (4) performing third-level distillation on the product to obtain a distillment and a distillation remnant, wherein the distillment is the high-purity molecular distillation monoacylglycerol, and the distillation remnant is diglyceride and triglyceride. By the process, the content of total monoester in crude ester can be improved obviously, the abrasion of equipment in subsequent molecular distillation process is reduced, the energy consumption of distillation is reduced, and the economic benefit is improved obviously.
Description
Technical field
The invention belongs to the food emulsifier preparation field, be specifically related to the preparation technology of the molecular distillation Tegin 55G (fatty monoacylglycerol) of a kind of novel energy-conserving, consumption reduction.
Background technology
Mono-glycerides is a kind of broad-spectrum nonionic emulsifier, and as good w/o type emulsifying agent, it has good emulsifying, softness, antistatic, lubrication, is widely used in daily-use chemical industry/food/medicine/fields such as weaving/macromolecular material.In food service industry, mono-glycerides is important food emulsifier, and its consumption accounts for 2/3 of the total consumption of food emulsifier.In other non-food product industry, also be widely used.For example at Polymer Industry, mono-glycerides can be used for the cutting oil emulsifying agent, in textile softener, lubricant, EPS, PE, PP, thermosetting resin plastics, the printing-ink.Because its solubility property in PVC is fabulous, in PVC processing as internal lubricant, also at the static inhibitor as polyethylene, polypropylene, styrofoam.
Molecule distillating monoglyceride is that to use molecular distillation apparatus be that about 45% common mono-glycerides is further purified with content, content can reach the high purity product more than 95%, it has the characteristics such as usefulness height, purity be high, of light color, is the development trend that all trades and professions improve its quality product.
(Li Jian according to the literature, the application of molecular distillation glyceryl monostearate, Surfactant Industry, 1998,3:40-41.), take triglyceride level as raw material, under the effect of basic catalyst, with glycerine generation alcoholysis reaction, obtain the mixture of mono-glycerides and two sweet esters, be industrial production method commonly used.Its reaction equation is as follows:
The production of mono-glycerides, most domestic manufacturer all adopts interrupter method production, and general esterification technique proportioning raw materials is triglyceride level/glycerine mol ratio=1:1 ~ 3.Acid, alkali or the metal oxides of adopting are made catalyzer more; under nitrogen protection, be heated to 190 ~ 200 ℃; reaction times is 1 ~ 3 hour; then add the phosphoric acid neutralization, be cooled to 90 ℃, deslagging; remove and under 150 ℃, do again the short period of time behind the free fatty acids and add heat extraction impurity and volatile matter; the product of esterification is carried out molecular distillation again and purify, the content of last mono-glycerides is according to the difference of technique, can reach 95% or more than.
The main drawback of existing molecular distillation Tegin 55G production technique is: (1) transesterification reaction is balanced reaction, and because glycerine is poorly soluble at winterized stearin, and in the crude product, content of monoglyceride only is 35 ~ 40%, is difficult to break through 60%.On this basis, method with molecular distillation obtains high purity (〉 95%) mono-glycerides, generally need the monoglyceride raw material of 3 ton of 40% content could obtain 1 ton of highly purified mono-glycerides finished product, (1 ~ 0.5Pa), power consumption is (about 200 ℃) greatly, and the equipment knifing is easy to wear because molecular distillation apparatus needs the ultrahigh vacuum(HHV) degree, therefore, under the traditional technology, equipment loss is serious, deficiency in economic performance.(2) in order to improve the content of total monoesters in the thick ester, the ratio of glycerine in the often increase system of original technique, but excessive glycerine is under the basic catalyst existence condition, polymerization occurs easily, be difficult to distill in the follow-up distil process, can remain in two sweet esters and the triglyceride, can't return in the reaction system and go, utilization ratio is low, has reduced the economic benefit of enterprise.
Summary of the invention
The objective of the invention is for the deficiencies in the prior art part, the high purity molecule distillating monoglyceride preparation technology of a kind of novel energy-conserving, consumption reduction is provided;
The present invention includes following processing step:
(1) the molecular distillation Tegin 55G is synthetic: the ratio 1:1 ~ 1:3 by the mole number of winterized stearin and glycerine takes by weighing winterized stearin and glycerine, the catalyst A that in glycerine, adds qualities of glycerin 0.1 ~ 0.3%, after mixing, be decompressed to 3000Pa, be heated to 190 ~ 250 ℃, the winterized stearin that will be added with again catalyst B joins in three batches and goes to carry out transesterification reaction in the reaction system; The temperature of reaction is 190 ~ 250 ℃, and the reaction times is 2 ~ 4 hours, and reaction pressure is 3000Pa; The add-on of catalyst B is 1 ~ 5% of total quality of material;
Described catalyst A is a kind of in basic metal, alkaline earth metal hydroxides and its oxide compound; Described catalyst B is a kind of in quaternary ammonium salt, quaternary alkylphosphonium salt, polyethers and the crown ether;
(2) after transesterification reaction finishes, add strong phosphoric acid and neutralize system pH for neutral, cooling, leave standstill system layering behind the 30min, the upper strata is raw glycerine ester layer, lower floor is the impurity that unreacted produces in material and the reaction process completely, and after lower floor emitted as slag charge, residuum was raw glycerine ester layer;
(3) the raw glycerine ester of step (2) gained is carried out first step distillation, distillation temperature is 140 ℃, and pressure is 500Pa, dewaters, degassed processing; The gained material carries out secondary distillation again, and distillation temperature is 175 ℃, and pressure is 75Pa, the free fatty acids in the removal system and glycerine;
(4) the raw glycerine ester with step (3) gained carries out third stage molecular distillation, and distillation temperature is 210 ℃, and pressure is 0.5Pa, obtains distillment and steams excess; Described distillment is the high purity molecule distillating monoglyceride, and steaming excess is fatty acyl two sweet esters and fatty acyl triglyceride.
The present invention compared with prior art has following advantage and beneficial effect:
The present invention adopts phase-transfer catalyst to increase the solubleness of glycerine in winterized stearin, promotes the transesterification reaction balance to move to the product direction by the effective content that improves glycerine in the reaction system, improves the content of total monoesters in the thick ester with this.
(1) content of total monoesters has reached about 80% in the thick ester for preparing of technique of the present invention.Only need about 1.5 tons thick ester can obtain by molecular distillation high-purity molecular distillation Tegin 55G of 1 ton of purity 〉=95%, its loss and energy consumption to equipment has been reduced to below 50% of existing processing condition, has improved greatly the economic benefit of enterprise.
(2) technique of the present invention, the slag charge of discharging are about 20% of raw material total mass, with existing technique comparatively speaking, the Reducing exhaust emission of waste about 50%, reduced the environmental protection cost of enterprise.
Description of drawings
Fig. 1 is the preparation were established figure of high purity molecule distillating monoglyceride of the present invention.
Embodiment
Embodiment 1
(1) fatty acyl monoglyceride is synthetic: get glycerine 1kg, NaOH 10g adds in the reactor, mixes, and is decompressed to 3000Pa, is heated to 200 ℃, behind the 30min.Adding 1.5kg winterized stearin and 30g benzyltriethylammoinium chloride mix in mixing kettle, and are heated to 200 ℃, divide to join in the reactor every minor tick 30min three times.After all reaction masses all join in the reactor, continue reaction 30min.After esterification finishes, add the phosphoric acid neutralization, and leave standstill 30min, the reactant layering.The upper strata is the glyceryl ester layer, and lower floor is the impurity that generates in unreacted material and the reaction process.Emit successively glyceryl ester layer and slag charge layer.The glyceryl ester layer uses the described method mensuration of GB GB15612-1995 content of monoglyceride wherein, and the result shows that content of monoglyceride reaches 75.89% in the thick ester.
(2) the glyceryl ester layer that obtains in the step (1) is changed in the water distilling apparatus, the distillation temperature that the first step is distilled is set as 140 ℃, and pressure is 500Pa, and the condenser temperature in the first step water distilling apparatus is 50 ℃; Continuously feeding is dewatered, degassed operation.Glyceryl ester continues to enter second stage molecular distillation as the heavy phase that is not distilled out of.
(3) the glyceryl ester layer that obtains in the step (2) is changed in the molecular distillation apparatus of the second stage, setting distillation temperature is 175 ℃, and pressure is 75Pa, and wherein free fatty acids and glycerine is not steamed.Glyceryl ester continues to enter third stage molecular distillation as the heavy phase that is not distilled out of.
(4) the glyceryl ester layer that obtains in the step (3) is changed in the third stage molecular distillation apparatus, setting distillation temperature is 201 ℃, and pressure is 0.5Pa.Fatty acyl monoglyceride is distilled out of, the light phase product 1.7kg that in inner condenser, collects, and mono-glycerides purity is by gas chromatographic detection, and its purity reaches 95.07%.
Embodiment 2
(1) fatty acyl monoglyceride is synthetic: get glycerine 1kg, NaOH 10g adds in the reactor, mixes, and is decompressed to 3000Pa, is heated to 200 ℃, behind the 30min.In mixing kettle, add 1.5kg winterized stearin and 20g benzyltriethylammoinium chloride and 18g polyoxyethylene glycol dialkyl ether and mix, and be heated to 200 ℃, divide to join in the reactor every minor tick 30min three times.After all reaction masses all join in the reactor, continue reaction 30min.After esterification finishes, add the phosphoric acid neutralization, and leave standstill 30min, the reactant layering.The upper strata is the glyceryl ester layer, and lower floor is the impurity that generates in unreacted material and the reaction process.Emit successively glyceryl ester layer and slag charge layer.The glyceryl ester layer uses the described method mensuration of GB GB15612-1995 content of monoglyceride wherein, and the result shows that content of monoglyceride reaches 81.27% in the thick ester.
(2) the glyceryl ester layer that obtains in the step (1) is changed in the water distilling apparatus, the distillation temperature that the first step is distilled is set as 140 ℃, and pressure is 500Pa, and the condenser temperature in the first step water distilling apparatus is 50 ℃; Continuously feeding is dewatered, degassed operation.Glyceryl ester continues to enter second stage molecular distillation as the heavy phase that is not distilled out of.
(3) the glyceryl ester layer that obtains in the step (2) is changed in the molecular distillation apparatus of the second stage, setting distillation temperature is 175 ℃, and pressure is 75Pa, and wherein free fatty acids and glycerine is not steamed.Glyceryl ester continues to enter third stage molecular distillation as the heavy phase that is not distilled out of.
(4) the glyceryl ester layer that obtains in the step (3) is changed in the third stage molecular distillation apparatus, setting distillation temperature is 201 ℃, and pressure is 0.5Pa.Fatty acyl monoglyceride is distilled out of, the light phase product 1.83kg that in inner condenser, collects, and mono-glycerides purity is by gas chromatographic detection, and its purity reaches 95.30%.
Embodiment 3
(1) fatty acyl monoglyceride is synthetic: get glycerine 1kg, NaOH 10g adds in the reactor, mixes, and is decompressed to 3000Pa, is heated to 200 ℃, behind the 30min.Adding 1.5kg winterized stearin and 28g chlorination 16 alkyl three fourth base Phosphonium mix in mixing kettle, and are heated to 200 ℃, divide to join in the reactor every minor tick 30min three times.After all reaction masses all join in the reactor, continue reaction 30min.After esterification finishes, add the phosphoric acid neutralization, and leave standstill 30min, the reactant layering.The upper strata is the glyceryl ester layer, and lower floor is the impurity that generates in unreacted material and the reaction process.Emit successively glyceryl ester layer and slag charge layer.The glyceryl ester layer uses the described method mensuration of GB GB15612-1995 content of monoglyceride wherein, and the result shows that content of monoglyceride reaches 80.65% in the thick ester.
(2) the glyceryl ester layer that obtains in the step (1) is changed in the water distilling apparatus, the distillation temperature that the first step is distilled is set as 140 ℃, and pressure is 500Pa, and the condenser temperature in the first step water distilling apparatus is 50 ℃; Continuously feeding is dewatered, degassed operation.Glyceryl ester continues to enter second stage molecular distillation as the heavy phase that is not distilled out of.
(3) the glyceryl ester layer that obtains in the step (2) is changed in the molecular distillation apparatus of the second stage, setting distillation temperature is 175 ℃, and pressure is 75Pa, and wherein free fatty acids and glycerine is not steamed.Glyceryl ester continues to enter third stage molecular distillation as the heavy phase that is not distilled out of.
(4) the glyceryl ester layer that obtains in the step (3) is changed in the third stage molecular distillation apparatus, setting distillation temperature is 201 ℃, and pressure is 0.5Pa.Fatty acyl monoglyceride is distilled out of, the light phase product 1.81kg that in inner condenser, collects, and mono-glycerides purity is by gas chromatographic detection, and its purity reaches 95.87%.
Claims (1)
1. the synthesis technique of a high purity molecular distillation Tegin 55G is characterized in that:
(1) the molecular distillation Tegin 55G is synthetic: the ratio 1:1 ~ 1:3 by the mole number of winterized stearin and glycerine takes by weighing winterized stearin and glycerine, the catalyst A that in glycerine, adds qualities of glycerin 0.1 ~ 0.3%, after mixing, be decompressed to 3000Pa, be heated to 190 ~ 250 ℃, the winterized stearin that will be added with again catalyst B joins in three batches and goes to carry out transesterification reaction in the reaction system; The temperature of reaction is 190 ~ 250 ℃, and the reaction times is 2 ~ 4 hours, and reaction pressure is 3000Pa; The add-on of catalyst B is 1 ~ 5% of total quality of material;
Described catalyst A is a kind of in basic metal, alkaline earth metal hydroxides and its oxide compound; Described catalyst B is a kind of in quaternary ammonium salt, quaternary alkylphosphonium salt, polyethers and the crown ether;
(2) after transesterification reaction finishes, add strong phosphoric acid and neutralize system pH for neutral, cooling, leave standstill system layering behind the 30min, the upper strata is raw glycerine ester layer, lower floor is the impurity that unreacted produces in material and the reaction process completely, and after lower floor emitted as slag charge, residuum was raw glycerine ester layer;
(3) the raw glycerine ester of step (2) gained is carried out first step distillation, distillation temperature is 140 ℃, and pressure is 500Pa, dewaters, degassed processing; The gained material carries out secondary distillation again, and distillation temperature is 175 ℃, and pressure is 75Pa, the free fatty acids in the removal system and glycerine;
(4) the raw glycerine ester with step (3) gained carries out third stage molecular distillation, and distillation temperature is 210 ℃, and pressure is 0.5Pa, obtains distillment and steams excess; Described distillment is the high purity molecule distillating monoglyceride, and steaming excess is fatty acyl two sweet esters and fatty acyl triglyceride.
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| CN103897808A (en) * | 2014-03-11 | 2014-07-02 | 复旦大学 | Method for synthesizing monoglyceride by using glycerol alcoholysis vegetable oil |
| CN104489426A (en) * | 2014-11-28 | 2015-04-08 | 广州嘉德乐生化科技有限公司 | Composition for food emulsification and preparation method thereof |
| CN104531365A (en) * | 2014-12-10 | 2015-04-22 | 柳州高通食品化工有限公司 | Preparation method of polyglycerol ester |
| CN105331648A (en) * | 2015-10-08 | 2016-02-17 | 中科田园(北京)农业科技有限公司 | High-purity alpha-linolenic acid monoglyceride and preparation method thereof |
| CN105418414A (en) * | 2015-12-22 | 2016-03-23 | 杭州富春食品添加剂有限公司 | Production method for glycerol monostearate and glycerol distearate |
| CN105647654A (en) * | 2016-01-18 | 2016-06-08 | 佳力士添加剂（海安）有限公司 | Monoglyceride preparation technology |
| CN106433998A (en) * | 2016-08-23 | 2017-02-22 | 佳力士添加剂（海安）有限公司 | Preparation method of glycerol monostearate |
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| CN107459457A (en) * | 2017-07-13 | 2017-12-12 | 佳力士添加剂（海安）有限公司 | A kind of preparation technology of high-purity molecule distillating monoglyceride |
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| CN111187174A (en) * | 2020-01-16 | 2020-05-22 | 广东丽臣奥威实业有限公司 | Production and purification method of fatty acyl glycinate or fatty derivative acyl glycinate |
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| CN112679344A (en) * | 2020-12-29 | 2021-04-20 | 浙江物美生物科技有限公司 | Preparation process of monoglyceride |
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| CN113893842A (en) * | 2021-09-24 | 2022-01-07 | 浙江工业职业技术学院 | Preparation method of modified supported magnesium oxide catalyst and monoglyceride production process |
| CN114133328A (en) * | 2021-10-22 | 2022-03-04 | 江苏环宇康力科技有限公司 | Production process and formula for preparing monoglyceride from grease |
| CN114456066A (en) * | 2022-01-29 | 2022-05-10 | 山东成武易信环保科技有限公司 | Distillation method for purifying glycerol monobutyrate |
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| CN103897808A (en) * | 2014-03-11 | 2014-07-02 | 复旦大学 | Method for synthesizing monoglyceride by using glycerol alcoholysis vegetable oil |
| CN104489426B (en) * | 2014-11-28 | 2018-03-13 | 广州嘉德乐生化科技有限公司 | A kind of composition for food emulsification and preparation method thereof |
| CN104489426A (en) * | 2014-11-28 | 2015-04-08 | 广州嘉德乐生化科技有限公司 | Composition for food emulsification and preparation method thereof |
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| CN105331648A (en) * | 2015-10-08 | 2016-02-17 | 中科田园(北京)农业科技有限公司 | High-purity alpha-linolenic acid monoglyceride and preparation method thereof |
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| CN105647654A (en) * | 2016-01-18 | 2016-06-08 | 佳力士添加剂（海安）有限公司 | Monoglyceride preparation technology |
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| CN113893842A (en) * | 2021-09-24 | 2022-01-07 | 浙江工业职业技术学院 | Preparation method of modified supported magnesium oxide catalyst and monoglyceride production process |
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