CN114031526A - Continuous preparation method of fatty acyl amino acid type surfactant by one-step condensation method - Google Patents
Continuous preparation method of fatty acyl amino acid type surfactant by one-step condensation method Download PDFInfo
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Abstract
The invention discloses a new process for continuously preparing fatty acyl amino acid type surfactant by a one-step condensation method. The method comprises the following steps: under the action of a catalyst, fatty acid and amino acid (salt) are mixed in a micro mixer and then enter a micro-channel reactor for direct dehydration and condensation to prepare the fatty acyl amino acid type surfactant. The method reduces the step of preparing acyl chloride from carboxyl, avoids the generation of salt in the production process of fatty acyl amino acid type surfactant, and obviously improves the safety and environmental protection of the novel preparation process compared with the prior art.
Description
Technical Field
The invention belongs to the field of chemical synthesis, and particularly relates to a novel continuous preparation method of a fatty acyl amino acid type surfactant by a one-step condensation method.
Background
The fatty acyl amino acid type surfactant has a sulfonic group combined with an amido group in a molecule, and has good compatibility with anionic, nonionic and amphoteric surfactants. The fatty acyl amino acid type surfactant is an anionic surfactant with high safety, has excellent water solubility, hard water resistance, alkali resistance, acid resistance and foaming property, has good hand feeling after being used, and is suitable for preparing various cosmetics such as middle-grade and high-grade shampoos, facial cleansers, bath agents and the like. Can impart mild, moist and smooth feeling to hair and skin, and can be used as refining agent and cleaning agent in wool spinning and silk printing industry.
Fatty acyl amino acid type surfactants are prepared by both indirect and direct methods. The indirect method is a method which adopts a Showden-Bowman condensation reaction to prepare a product from fatty acyl chloride and amino acid (salt) under an alkaline condition, and the generated salt is remained in the product and is difficult to remove, so the indirect method is a common method in the current industrial production. The direct method is to prepare a product by directly dehydrating and condensing fatty acid and amino acid (salt), but is difficult to be industrially applied due to low reaction yield, harsh reaction conditions and the like.
In the process of preparing fatty acyl amino acid type surfactant by a direct method of fatty acid and amino acid (salt), fatty acid and amino acid (salt) are firstly complexed to generate a viscous intermediate, and then the viscous intermediate is dehydrated continuously at high temperature to generate a product. In the tank-type stirred reactor, the reaction raw materials, fatty acid and amino acid (salt), cannot be sufficiently mixed due to the increased viscosity and poor mass transfer effect of the reaction system, resulting in low reaction yield, long reaction time, and increased by-products with the increase of reaction time.
The microchannel reactor has the characteristics of high mass and heat transfer efficiency, easy control of reaction process (temperature, time and mixing efficiency), easy amplification, good safety performance and the like due to the huge specific surface area, and is increasingly widely applied to the production of fine chemical engineering and pharmaceutical intermediates. Because the micro-reactor has small liquid holdup and good high temperature and high pressure resistance, the intrinsic safety can be improved for the operation under harsh conditions in the kettle type process. The method has good applicability to the direct method for preparing fatty acyl amino acid type surfactant by fatty acid and amino acid (salt) with high operation requirement.
Disclosure of Invention
The invention aims to provide a method for continuously preparing fatty acyl amino acid type surfactant by a one-step condensation method in a microchannel reactor.
In a first aspect of the present invention, there is provided a continuous production method of a one-step condensation method of a fatty acyl amino acid type surfactant, comprising the steps of:
(a) providing a feed liquid A and a feed liquid B, wherein the feed liquid A is an amino acid solution (preferably an aqueous solution of amino acid or salt thereof) containing a catalyst, and the feed liquid B is fatty acid;
(b) pumping the material liquid A and the material liquid B into a micro mixer for mixing to obtain a material liquid mixture;
(c) introducing the feed liquid mixture into a micro-channel reactor for reaction to obtain reaction liquid; wherein the reaction temperature is 160-300 ℃;
(d) and introducing the reaction solution into a high-temperature stirring kettle to remove water, thereby obtaining the fatty acyl amino acid type surfactant.
In another preferred embodiment, the concentration of the aqueous solution of the amino acid (salt) is 41%.
In another preferred example, the fatty acid of the feed liquid B is in a molten state during feeding.
In another preferred embodiment, in step (c), the reaction is a dehydration condensation reaction.
In another preferred example, step (d) further comprises removing condensed water by vacuum.
In another preferred embodiment, the reaction temperature of dehydration condensation in the microchannel reactor is 200-270 ℃, preferably 240-260 ℃.
In another preferred example, the amino acid (salt): the molar ratio of the fatty acid is 1.0-5.0: 1.
In another preferred example, the amino acid (salt): the molar ratio of the fatty acid is 1-3: 1, preferably 1.5-2: 1.
In another preferred embodiment, the catalyst is used in an amount of 0.1 to 20 wt% based on the amino acid (salt).
In another preferred embodiment, the catalyst is used in an amount of 1-5 wt% of the amino acid (salt).
In another preferred embodiment, the catalyst is selected from the group consisting of: boric acid, phosphoric acid, polyphosphoric acid, titanium tetrachloride, tin tetrachloride, or combinations thereof.
In another preferred embodiment, the catalyst is boric acid, phosphoric acid, or a combination thereof.
In another preferred embodiment, the catalyst is a dehydration catalyst.
In another preferred embodiment, the flow rate of the amino acid (salt) aqueous solution in the microchannel reactor is 0.01-1000L/min; the flow rate of the fatty acid in the microchannel reactor is 0.01-1000L/min.
In another preferred embodiment, the flow rate of the aqueous amino acid (salt) solution and the flow rate of the fatty acid in the microchannel reactor are the same.
In another preferred embodiment, the flow rates of the aqueous amino acid (salt) solution and the fatty acid in the microchannel reactor are different.
In another preferred example, the flow rate of the aqueous amino acid (salt) solution in the microchannel reactor is 0.05-100L/min; the flow rate of the fatty acid in the microchannel reactor is 0.05-100L/min.
In another preferred embodiment, the flow rate of the amino acid (salt) aqueous solution in the microchannel reactor is 0.15-10L/min; the flow rate of the fatty acid in the microchannel reactor is 0.15-10L/min.
In another preferred embodiment, the flow rate of the aqueous amino acid (salt) solution in the microchannel reactor is 0.3-0.5L/min; the flow rate of the fatty acid in the microchannel reactor is 0.2-0.4L/min.
In another preferred example, the type of the micromixer is selected from the group consisting of: y type, T type, J type, two-step T type, inner interdigital type, separation convergent type and SK type.
In another preferred example, the type of the micromixer is selected from the group consisting of: t-type, inter-digitated, SK-type.
In another preferred example, the model of the micromixer is T-shaped.
In another preferred embodiment, the fatty acid is C2-C30Straight or branched chain fatty acids; preferably, the fatty acid is selected from the group consisting of: palmitic acid, stearic acid, oleic acid, linoleic acid, linolenic acid, coconut oil acid, lauric acid, arachidonic acid, eicosapentaenoic acid, docosahexaenoic acid, or combinations thereof.
In another preferred embodiment, the amino acid (salt) is selected from the group consisting of: sulfamic acid, sodium sulfamate, potassium sulfamate, N-methyltaurine, sodium N-methyltaurine, potassium N-methyltaurine, N-ethyltaurine, sodium N-ethyltaurine, potassium N-ethyltaurine, or combinations thereof.
In another preferred embodiment, the inner diameter of the microchannel reactor is 0.5-15 mm, and the length is 0.5-500 m.
In another preferred example, the inner diameter of the microchannel reactor is 1-3 mm, and the length is 10-20 m.
In another preferred embodiment, the temperature of the stirring tank is 160-300 ℃, preferably 200-280 ℃, and more preferably 240-260 ℃.
It is to be understood that within the scope of the present invention, the above-described features of the present invention and those specifically described below (e.g., in the examples) may be combined with each other to form new or preferred embodiments. Not to be reiterated herein, but to the extent of space.
Drawings
FIG. 1: the reaction process flow of the invention is shown schematically.
Detailed Description
The invention develops a novel method for continuously preparing fatty acyl amino acid type surfactant by a microchannel reactor for the first time through extensive and intensive research and large-scale screening. The method has the advantages of simple and convenient process flow, high product yield, greenness, safety and easy realization of large-scale industrial production. On the basis of this, the present invention has been completed.
The specific embodiment of the invention is as follows:
firstly, a micro mixer is used to ensure the sufficient contact and the sufficient mixing of two reaction raw materials, so that the raw materials are completely converted to obtain a viscous intermediate, and the problem that the materials are difficult to be uniformly mixed in the kettle type reaction is solved. And (3) pushing the high-viscosity reaction system into the microreactor under the high-pressure pushing of a plunger pump, and dehydrating at high temperature to form a product. Because the micro-reactor has small liquid holdup, can resist high temperature and high pressure, improves the intrinsic safety performance exponentially, and solves the problem of poor safety of a high-pressure system in the kettle reactor. Meanwhile, the method has the advantages of short residence time in the microreactor, no back mixing and easy regulation, and avoids the problem of increase of by-products in the reaction for a long time. With the progress of the reaction, the viscosity of the reaction system is reduced, and finally the reaction system is further dehydrated and cured in a stirring kettle, and water in the reaction system is rapidly removed by vacuumizing to obtain a high-quality final product. In conclusion, the micro mixer is used for strengthening the reaction raw material mixing process, the reaction process is strengthened in the micro reactor, the reaction time is shortened, the problems of byproduct increase and the like caused by the increase of the reaction time are solved, and the target product is quickly and efficiently obtained through curing and vacuum dehydration of the stirring kettle, so that the problems that the mixing effect is poor, the catalyst consumption is large, the reaction time is too long, the byproducts are more, the yield is low and the like, and the industrial amplification cannot be realized in the prior art can be solved.
Compared with the prior art, the invention has the advantages that:
(1) the invention uses the micro-mixer and the micro-channel reactor to continuously prepare the fatty acyl amino acid type surfactant, and has short reaction time, large reaction flux and low cost.
(2) The product prepared by the invention does not contain inorganic salt or organic salt and other impurities, has little pollution to the environment, and is green and environment-friendly.
(3) The method of the invention can realize continuous production, has stable product quality, is easy to realize large-scale industrial production, and effectively overcomes the defect that the fatty acyl amino acid type surfactant prepared by a direct method is difficult to be industrially produced in the traditional reaction kettle.
(4) The conversion rate of the raw materials is improved to 92-99%, and the yield is up to 90-98%.
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The experimental procedures, in which specific conditions are not noted in the following examples, are generally carried out under conventional conditions or conditions recommended by the manufacturers. Unless otherwise indicated, percentages and parts are by weight.
In the examples, room temperature means 25 ℃.
The starting materials and reagents used in the examples are all commercially available products.
Example 1
5000mL of 41% N-methyl potassium taurate aqueous solution is taken, 61.5g of catalyst boric acid is added, and dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4628g of product with the yield of 91%.
Example 2
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst boric acid is added, dissolved and used as material liquid A, and 5000g of lauric acid is melted and used as material liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4718g of a product, wherein the yield is 97%.
Example 3
5000mL of 41 percent N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst boric acid is added, dissolved to be used as material liquid A, and 5000g of stearic acid is melted to be used as material liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating out when no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4317g of a product with the yield of 95%.
Example 4
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst boric acid is added, and dissolved to be used as material liquid A, and 5000mL of oleic acid is used as material liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating out when no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4730g of a product, wherein the yield is 98%.
Example 5
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst boric acid is added, and dissolved to be used as material liquid A, and 5000mL of linolenic acid is used as material liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4707g of a product with the yield of 96%.
Example 6
5000mL of 41% N-methyl potassium taurate aqueous solution is taken, 61.5g of catalyst boric acid is added, dissolved to be used as feed liquid A, and 5000g of lauric acid is melted to be used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4820g of product with the yield of 99%.
Example 7
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst phosphoric acid is added, dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating out when no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4832g of the product, wherein the yield is 95%.
Example 8
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst polyphosphoric acid is added, dissolved and taken as feed liquid A, and 5000mL of coconut oil acid is taken as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture is in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4881g of product with the yield of 96%.
Example 9
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst phosphoric acid is added, dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 255 ℃, and the temperature of the high-temperature stirring kettle is 265 ℃. Stopping feeding after 12min, evaporating until no moisture is in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4933g of product with yield of 97%.
Example 10
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst phosphoric acid is added, dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into an inner interdigital micro mixer by using a feeding pump, and directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m after mixing. The feed flow rate of feed liquid A was 390mL/min, and the feed flow rate of feed liquid B was 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture is in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4882g of product with the yield of 96%.
Example 11
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst phosphoric acid is added, dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into an SK type micro mixer by using a feeding pump, mixing, and then directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m, wherein the feeding flow rate of the material liquid A is 390mL/min, and the feeding flow rate of the material liquid B is 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4781g of a product with the yield of 94%.
Example 12
5000mL of 41% N-methyl sodium taurate aqueous solution is taken, 61.5g of catalyst phosphoric acid is added, dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, mixing, and then directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m, wherein the feeding flow rate of the material liquid A is 390mL/min, and the feeding flow rate of the material liquid B is 300 mL/min. The reaction temperature in the microreactor is 245 ℃, and the temperature of the high-temperature stirred tank is 255 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4730g of a product with the yield of 93%.
Comparative example 1
5000mL of 41% N-methyl sodium taurate aqueous solution is weighed, 61.5g of catalyst phosphoric acid is added, and dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, mixing, and then directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m, wherein the feeding flow rate of the material liquid A is 390mL/min, and the feeding flow rate of the material liquid B is 300 mL/min. The reaction temperature in the microreactor is 275 ℃, and the temperature of the high-temperature stirred tank is 265 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4170g of a product with the yield of 82%.
Comparative example 2
5000mL of 41% N-methyl sodium taurate aqueous solution is weighed, 61.5g of catalyst phosphoric acid is added, and dissolved to be used as feed liquid A, and 5000mL of coconut oil acid is used as feed liquid B. And pumping the material liquid A and the material liquid B into a T-shaped micro mixer by using a feeding pump, mixing, and then directly flowing into a micro-channel reactor with the inner diameter of 2.0mm and the length of 15m, wherein the feeding flow rate of the material liquid A is 390mL/min, and the feeding flow rate of the material liquid B is 300 mL/min. The reaction temperature in the microreactor is 235 ℃, and the temperature of the high-temperature stirring kettle is 265 ℃. Stopping feeding after 12min, evaporating until no moisture exists in the high-temperature stirring kettle, vacuumizing for 30min, and cooling to obtain 4374g of a product with the yield of 86%.
In the present invention, the process for preparing the surfactant is carried out by a tubular reaction, and therefore, it is necessary to obtain a sufficiently high yield and a suitable reaction rate. The applicant found that when the reaction temperature is lowered, the reaction is difficult to proceed, resulting in a large decrease in yield, and when the reaction temperature is too high, the product is easily carbonized, and by-products are generated, resulting in a decrease in yield, and therefore, the reaction is preferably performed at 240 ℃ to 260 ℃.
All documents referred to herein are incorporated by reference into this application as if each were individually incorporated by reference. Furthermore, it should be understood that various changes and modifications of the present invention can be made by those skilled in the art after reading the above teachings of the present invention, and these equivalents also fall within the scope of the present invention as defined by the appended claims.
Claims (11)
1. The continuous preparation method of the fatty acyl amino acid type surfactant by the one-step condensation method is characterized by comprising the following steps:
(a) providing a feed liquid A and a feed liquid B, wherein the feed liquid A is an amino acid solution (preferably an aqueous solution of amino acid or salt thereof) containing a catalyst, and the feed liquid B is fatty acid;
(b) pumping the material liquid A and the material liquid B into a micro mixer for mixing to obtain a material liquid mixture;
(c) introducing the feed liquid mixture into a micro-channel reactor for reaction to obtain reaction liquid; wherein the reaction temperature is 160-300 ℃;
(d) and introducing the reaction solution into a high-temperature stirring kettle to remove water, thereby obtaining the fatty acyl amino acid type surfactant.
2. The method of claim 1, wherein the reaction temperature of the dehydration condensation in the microchannel reactor is 200 ℃ to 270 ℃, preferably 240 ℃ to 260 ℃.
3. The method of claim 1, wherein the amino acid (salt): the molar ratio of the fatty acid is 1.0-5.0: 1.
4. The method of claim 1, wherein the catalyst is used in an amount of 0.1 to 20 wt% of the amino acid (salt).
5. The method of claim 1, wherein the catalyst is selected from the group consisting of: boric acid, phosphoric acid, polyphosphoric acid, titanium tetrachloride, tin tetrachloride, or combinations thereof.
6. The method of claim 1, wherein the flow rate of the aqueous amino acid (salt) solution in the microchannel reactor is 0.01 to 1000L/min; the flow rate of the fatty acid in the microchannel reactor is 0.01-1000L/min.
7. The method of claim 1, wherein the micromixer is selected from the group consisting of: y type, T type, J type, two-step T type, inner interdigital type, separation convergent type and SK type.
8. The method of claim 1, wherein the fatty acid is C2-C30Straight or branched chain fatty acids; preferably, the fatty acid is selected from the group consisting of: palmitic acid, stearic acid, oleic acid, linoleic acid, linolenic acid, coconut oil acid, lauric acid, arachidonic acid, eicosapentaenoic acid, docosahexaenoic acid, or combinations thereof.
9. The method of claim 1, wherein the amino acid (salt) is selected from the group consisting of: sulfamic acid, sodium sulfamate, potassium sulfamate, N-methyltaurine, sodium N-methyltaurine, potassium N-methyltaurine, N-ethyltaurine, sodium N-ethyltaurine, potassium N-ethyltaurine, or combinations thereof.
10. The method of claim 1, wherein the microchannel reactor has an inner diameter dimension of 0.5 mm to 15mm and a length of 0.5 m to 500 m.
11. The method as claimed in claim 1, wherein the temperature of the stirring vessel is 160 ℃ to 300 ℃, preferably 200 ℃ to 280 ℃, more preferably 250 ℃ to 260 ℃.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115160189A (en) * | 2022-08-11 | 2022-10-11 | 广州天赐高新材料股份有限公司 | Continuous preparation method of N-acyl methyl sodium taurate with high active matter content |
| CN115626884A (en) * | 2022-12-20 | 2023-01-20 | 江苏奥洁生物科技有限公司 | Method for synthesizing N-acyl amino acid surfactant |
| WO2023093560A1 (en) * | 2021-11-29 | 2023-06-01 | 江苏奥洁生物科技有限公司 | Method for preparing n-fatty acyl amino acid surfactant by means of high-temperature melting and direct condensation |
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| CN115160189A (en) * | 2022-08-11 | 2022-10-11 | 广州天赐高新材料股份有限公司 | Continuous preparation method of N-acyl methyl sodium taurate with high active matter content |
| CN115626884A (en) * | 2022-12-20 | 2023-01-20 | 江苏奥洁生物科技有限公司 | Method for synthesizing N-acyl amino acid surfactant |
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Effective date of registration: 20221206 Address after: 215635 No. 10, Dongxin Road, Jiangsu Yangzi River International Chemical Industrial Park, Suzhou, Jiangsu Applicant after: Jiangsu Aojie Biotechnology Co.,Ltd. Address before: 215635 No. 10, Dongxin Road, Jiangsu Yangzi River International Chemical Industrial Park, Suzhou, Jiangsu Applicant before: Jiangsu Aojie Biotechnology Co.,Ltd. Applicant before: Zhangjiagang Wenyong Jiying business management partnership (L.P.) |