CN112920094A - Method for adjusting production load and improving yield of N-methyl sodium taurate - Google Patents
Method for adjusting production load and improving yield of N-methyl sodium taurate Download PDFInfo
- Publication number
- CN112920094A CN112920094A CN202110129121.6A CN202110129121A CN112920094A CN 112920094 A CN112920094 A CN 112920094A CN 202110129121 A CN202110129121 A CN 202110129121A CN 112920094 A CN112920094 A CN 112920094A
- Authority
- CN
- China
- Prior art keywords
- reaction
- sodium
- mixed solution
- series
- taurate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/32—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of salts of sulfonic acids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1862—Stationary reactors having moving elements inside placed in series
Abstract
The invention relates to the technical field of industrial production, in particular to a method for producing N-methyl sodium taurate by utilizing a multi-kettle series reaction device. The method provided by the invention provides a method for continuously producing the N-methyl sodium taurate, and the yield of the product can be increased while the capacity is flexibly adjusted and the production intensity is improved.
Description
Technical Field
The invention relates to the technical field of industrial production, in particular to a method for adjusting the productivity and improving the yield of N-methyl sodium taurate.
Background
The N-methyl sodium taurate (also called methyl sodium taurate) is widely applied in industry, and the main production method is as follows: the method takes monomethylamine and sodium isethionate as raw materials, and produces the monomethylamine and the sodium isethionate in a batch mode under the conditions of high temperature (260 ℃ and 270 ℃) and high pressure (20 MPa). The production intensity of a batch reaction kettle with a given volume is severely restricted by the sequential process of feeding, preheating, reacting and discharging in a batch production mode. If the production capacity needs to be increased, the number of reaction kettles can only be increased to meet the production requirement. In addition, high pressure conditions present a potential for frequent intermittent operation shifts.
Due to the defects of the existing process, the development of a new production method of N-methyl sodium taurate, which can flexibly adjust the productivity, improve the production intensity and increase the product yield, is urgently needed in the field.
Disclosure of Invention
The invention mainly aims to provide a production method of N-methyl sodium taurate, which can flexibly adjust the productivity, improve the production strength and increase the product yield. In particular, the invention relates to a method for producing N-methyl sodium taurate by utilizing a multi-kettle series reaction system, which can increase the yield of the N-methyl sodium taurate and improve the production intensity, and can flexibly adjust the productivity by adjusting the material loading coefficient, the material volume and the material residence time in a reaction kettle.
In a first aspect of the present invention, there is provided a method for producing sodium N-methyltaurate, comprising the steps of:
s1) providing a first mixed solution containing sodium isethionate, monomethylamine, and sodium hydroxide;
s2) preheating the first mixed solution to obtain a second mixed solution;
s3) allowing the second mixed solution to enter a multi-kettle series reaction system for reaction to obtain a first reaction solution;
s4) leading the first reaction solution to enter an energy recovery unit to obtain the sodium N-methyltaurate solution.
In another preferred embodiment, the first mixed solution contains 25 wt% to 30 wt% of sodium isethionate, 25 wt% to 30 wt% of monomethylamine, and 0.01 wt% to 0.2 wt% of sodium hydroxide, based on the total weight of the first mixed solution.
In another preferred example, the step S2) includes a subdividing step:
s20) pressurizing the first mixed solution to 3 to 30MPa, preferably 5 to 25 MPa;
s21) the pressurized first mixed solution in the step S20) enters a preheating unit for preheating;
s22) the first mixed solution in the step S21) is subjected to multi-stage heat exchange in a preheating unit, wherein the temperature reaches 100-400 ℃, preferably 150-350 ℃, and more preferably 180-300 ℃.
In another preferred embodiment, the multi-kettle series reaction system comprises 2 to 6 reaction kettles in series, preferably 3 to 4 reaction kettles in series.
In another preferred embodiment, the charging factor in each reaction vessel is 0.3 to 0.95, preferably 0.60 to 0.85.
In another preferred embodiment, the residence time of the materials in each reaction kettle is 1-60min, preferably 3-10 min.
In another preferred example, in the step S3), the second mixed solution flows through each of the serially connected reaction kettles with the same residence time.
In another preferred embodiment, the material temperature in each reaction vessel is 150-.
In another preferred embodiment, the temperature of each reaction vessel in the multi-vessel series reaction system is the same or different.
In another preferred example, the temperature of the materials in each reaction kettle is reduced from kettle to kettle.
In another preferred embodiment, the pressure in each reaction kettle is 3-30MPa, preferably 7-25MPa, and more preferably 8-15 MPa.
In another preferred embodiment, the pressure of each reaction kettle is the same.
In another preferred embodiment, in the first mixed solution, the molar ratio of methylamine to sodium isethionate is 3: 1-12: 1; the content of sodium hydroxide is 0.05-1.0 wt% based on the total weight of the first mixed solution.
In a second aspect of the present invention, there is provided an apparatus for producing sodium N-methyltaurate, the apparatus comprising: a preheating unit; a multi-kettle series reaction system containing 2-6 reaction kettles; an energy recovery unit.
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, four kettles are N-methyl sodium taurate apparatus for producing in series
FIG. 2, two kettles are connected in series N-methyl sodium taurate apparatus for producing
FIG. 3 shows the time required for each step of the batch process for producing N-methyltaurate
FIG. 4, Effect of the Material residence time in a given tubular reactor on the yield of sodium N-methyltaurate
Detailed Description
The present inventors have made extensive and intensive studies and have surprisingly found that a multi-pot series reaction system can increase the yield of sodium N-methyltaurate, and have completed the present invention.
Specifically, the invention provides a method for producing N-methyl sodium taurate by a multi-kettle series reaction system, wherein the method produces the N-methyl sodium taurate in a continuous reaction mode, not only can improve the production strength and increase the product yield, but also can adjust the productivity by adjusting the material loading coefficient, the material volume and the material retention time in a reaction kettle.
Term(s) for
N-methyl sodium taurate (sodium methyl taurate)
N-methyl sodium taurate (also known as sodium methyl taurate)Is a daily chemical intermediate, has the English name of Sodium 2- (methyliminon) ethanesulfosalt, CAS number of 4316-74-9 and molecular formula C3H8NNaO3S, molecular weight 165.2 g/mol. Sodium N-methyltaurate can be used to produce sodium cocoyl methyltaurate, sodium N-oleoyl-N-methyltaurate, sodium polyacrylyldimethyltaurate, sodium N-acylmethyltaurate, polydimethylsiloxane PEG-7 sodium acetylmethyltaurate, hydroxyethyl acrylate/sodium acryloyldimethyltaurate copolymer, and sodium methyl lauroyl taurate.
Multi-kettle series reaction device for producing N-methyl sodium taurate
The invention provides a multi-kettle series reaction device, and the multi-kettle series reaction system refers to a reaction system for producing N-methyl sodium taurate by using the multi-kettle series reaction device.
The multi-tank series reaction apparatus of the present invention comprises 2 to 6 reaction tanks, preferably 2 to 4 reaction tanks, in series.
The method for producing the sodium N-methyltaurate of the invention
As used herein, "the method of the present invention", "the method of producing sodium N-methyltaurate of the present invention" are used interchangeably and refer to a method of producing sodium N-methyltaurate using a multi-pot tandem reaction system comprising the steps of:
s1) providing a first mixed solution containing sodium isethionate, monomethylamine, and sodium hydroxide;
s2) preheating the first mixed solution to obtain a second mixed solution;
s3) allowing the second mixed solution to enter a multi-kettle series reaction system for reaction to obtain a first reaction solution;
s4) leading the first reaction solution to enter an energy recovery unit to obtain the sodium N-methyltaurate solution.
In another preferred embodiment, the first mixed solution contains 25 wt% to 30 wt% of sodium isethionate, 25 wt% to 30 wt% of monomethylamine, and 0.01 wt% to 0.2 wt% of sodium hydroxide, based on the total weight of the first mixed solution.
In another preferred example, the step S2) includes a subdividing step:
s20) pressurizing the first mixed solution to 3 to 30MPa, preferably 5 to 25 MPa;
s21) the pressurized first mixed solution in the step S20) enters a preheating unit for preheating;
s22) the first mixed solution in the step S21) is subjected to multi-stage heat exchange in a preheating unit, wherein the temperature reaches 100-400 ℃, preferably 150-350 ℃, and more preferably 180-300 ℃.
The main advantages of the invention include:
(a) the method can increase the yield of the N-methyl sodium taurate.
(b) The method of the invention can improve the production strength.
(c) The method can flexibly adjust the productivity by adjusting the charging coefficient, the material volume and the material residence time in the reaction kettle.
(d) The method can maintain the yield of the N-methyl sodium taurate and improve the productivity at the same time.
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. Experimental procedures without specific conditions noted in the following examples, generally followed by conventional conditions, such as Sambrook et al, molecular cloning: the conditions described in the Laboratory Manual (New York: Cold Spring Harbor Laboratory Press,1989), or according to the manufacturer's recommendations. Unless otherwise indicated, percentages and parts are percentages and parts by weight.
Example 1: 4 kettles are connected in series to produce the sodium N-methyltaurate (the charging coefficient is 0.6, the volume of the liquid phase in a single reaction kettle is 54L)
The reaction raw material is a mixture of sodium isethionate, monomethylamine, sodium hydroxide and water. Wherein, the weight percentage of monomethylamine is 29.6 percent, the weight percentage of sodium isethionate is 28.2 percent, and the weight percentage of sodium hydroxide is 0.1 percent. The reaction raw materials are pressurized to 8MPa, preheated to 280 ℃ and then enter a 4-kettle series reaction device shown in figure 1. The material temperature in the reaction kettles 1-4 is controlled at 280 deg.C, 260 deg.C, 240 deg.C and 220 deg.C respectively, and the pressure in the reaction kettles is controlled at 8MPa by nitrogen gas cabinet. The volume of a single reaction kettle is 90L, and the total volume of four reaction kettles is 360L. By controlling the charging coefficient of a single reaction kettle to be 0.6, the volume of a liquid phase in the single reaction kettle is 54L, and the total volume of materials in four reaction kettles is 216L. The residence time of the materials in each reaction kettle was 1.83min, and the total residence time in the four reaction kettles was 7.3 min. The structure of the series reaction kettle is combined with the implementation of specific process conditions, so that the yield of the N-methyl sodium taurate reaches 93 percent, and the production capacity of 3000 tons/year of the N-methyl sodium taurate is met (the working day is 300 days per year).
Example 2: 4 kettles are connected in series to produce the N-methyl sodium taurate (the charging coefficient is 0.85, the volume of the liquid phase in a single reaction kettle is 77L)
The reaction raw material composition is the same as that of example 1, pressurized to 8MPa, preheated to 280 ℃ and then fed into a 4-kettle series reaction device shown in figure 1. The material temperature in the reaction kettles 1-4 is respectively controlled at 280 ℃, 260 ℃, 240 ℃ and 220 ℃, and the pressure in the reaction kettles is controlled at 8MPa through a nitrogen gas cabinet. The volume of a single reaction kettle is 90L, and the total volume of four reaction kettles is 360L. By controlling the charging coefficient of a single reaction kettle to be 0.85, the volume of a liquid phase in the single reaction kettle is adjusted to be 77L, and the total volume of materials in the four reaction kettles is 306L. The residence time of the materials in each reaction kettle was kept at 1.83min, and the total residence time in the four reaction kettles was kept at 7.3 min. The structure of the series reaction kettle is combined with the implementation of specific process conditions, so that the yield of the N-methyl sodium taurate reaches 93 percent, and the production capacity of 4200 tons of N-methyl sodium taurate per year is met (300 days per year).
Example 3: 2-kettle series production of N-methyl sodium taurate
The reaction raw material is a mixture of sodium isethionate, monomethylamine, sodium hydroxide and water. Wherein, the weight percentage of monomethylamine is 29.6 percent, the weight percentage of sodium isethionate is 28.2 percent, and the weight percentage of sodium hydroxide is 0.1 percent. The reaction raw materials are pressurized to 15MPa, preheated to 260 ℃ and then enter a 2-kettle series reaction device shown in figure 2.
The volume of a single reaction kettle is 1000L, and the total volume of two reaction kettles is 2000L. By controlling the charging coefficient of a single reaction kettle to be 0.7, the volume of a liquid phase in the single reaction kettle is 700L, and the total volume of materials in the two reaction kettles is 1400L. The residence time of the materials in each reaction kettle is 10min, and the total residence time in the two reaction kettles is 20 min. The pressure in the reaction kettle is controlled at 15MPa through a nitrogen gas cabinet.
Reaction kettle temperature control scheme 1: the material temperature in the reaction kettles 1 and 2 is controlled at 260 ℃, the yield of the N-methyl sodium taurate reaches 90 percent, and the production capacity of 7000 tons of N-methyl sodium taurate per year is met (the working day per year is 300 days).
Reaction kettle temperature control scheme 2: the material temperature in the reaction kettles 1 and 2 is controlled at 260 ℃ and 220 ℃, respectively, the yield of the N-methyl sodium taurate reaches 92 percent, and the production capacity of 7000 tons of N-methyl sodium taurate per year is met (the working day is 300 days per year).
Comparative example 1 batch kettle production of sodium N-methyltaurate
The reaction mass was the same as in example 1, the reaction temperature in the batch still was 260 ℃ and the volume of the batch still was 1.62m3The loading factor was 0.75. As shown in FIG. 3, the actual reaction time of the materials in the reactor is 5.9min, and the auxiliary operation time including feeding, temperature and pressure rise, discharging and the like is far higher than the actual reaction time, about 30 min. Based on the device and the process conditions, the yield of the N-methyl sodium taurate is 92 percent, and the productivity reaches 3000 tons/year (300 days per working day).
Volume of batch reactor 1.63m3Far larger than the total volume of 0.36m of the multi-kettle series connection in example 13(ii) a On the other hand, there is a cumbersome manual intervention for intermittent operation. When the yield and the productivity of the N-methyl sodium taurate are similar, the production strength of the multi-kettle series method is obviously higher than that of the batch reaction method.
Comparative example 2 production of sodium N-methyltaurate in isothermal tubular reactor
The feed was the same as in example 1, and an isothermal tubular reactor was designed for the production of sodium N-methyltaurate. The designed capacity of the N-methyl sodium taurate is 3000 tons/year (300 days per working day), and the yield reaches 92 percent. When the reaction temperature is 260 ℃, the optimal reactor volume is 0.2m3The reaction residence time was 5.9 min.
As shown in FIG. 4, if the production capacity of the sodium N-methyltaurate is adjusted to 4200 tons/year (300 days per working day), the reaction residence time is shortened to 4.5min, and the yield of the sodium N-methyltaurate is reduced to 87%.
It can be seen that for a given isothermal tubular reactor, the yield of sodium N-methyltaurate decreases from 93% to 87% as the yield of sodium N-methyltaurate increases from 3000 tons/year to 4200 tons/year. Compared with the multi-kettle series production method, the method can adapt to the adjustment of the productivity of the N-sodium methyl taurate by only adjusting the charging coefficient of each reaction kettle, and maintain the yield of the N-sodium methyl taurate unchanged.
Discussion of the related Art
Patent CN201210138188.7 discloses a device for continuously producing N-methyl sodium taurate in a pipelining way and a production method thereof. After materials including monomethylamine, sodium isethionate and an alkaline catalyst are mixed in a storage tank, the mixture is pressurized to 10 to 25MPa by a booster pump and enters a continuous pipeline reactor, and the mixture stays for 10 to 60 minutes to achieve 90 percent of product yield. Although the use of the pipe reactor enables continuous production of sodium N-methyltaurate, the production method disclosed in this patent has drawbacks. For a given capacity of sodium N-methyltaurate, the residence time for the material to reach the specified yield in the pipeline reactor is fixed. When the productivity of the N-methyl sodium taurate needs to be improved, the retention time of materials in a given pipeline reactor is shortened, and the preset yield of the N-methyl sodium taurate cannot be achieved. Meanwhile, the synthesis of the N-methyl sodium taurate is an exothermic reaction, and the proper reduction of the reaction temperature is beneficial to improving the equilibrium yield of the product. The patent does not mention temperature control along the pipeline to increase the yield of sodium N-methyltaurate based on thermodynamic equilibrium.
Patent CN201911369398.5 discloses a preparation method of sodium N-methyltaurate. The method takes ionic liquid as a reaction medium, and achieves 86-88% of yield of N-methyl sodium taurate under the conditions of 150-220 ℃, 3-12 MPa of reaction pressure and 0.5-5 h of reaction time by using hydroxyethyl sodium sulfonate and monomethylamine under the action of a zirconium and tungsten modified HY molecular sieve catalyst. The patent does not change the batch mode of operation of the prior art according to the drawings provided by the patent.
Patent CN201911271914.0 discloses a preparation method of sodium methyl taurate. The patent utilizes a sodium taurate one-pot two-step method to prepare the sodium methyl taurate, uses sodium taurate and formaldehyde as raw materials, and obtains the yield of the sodium methyl taurate of 90 percent by reacting under the action of a supported composite metal organic catalyst. The raw material route reported in the patent is inconsistent with the existing process route. This patent does not change the batch mode of operation of the prior art process, as described in the specific embodiment.
Patent cn201911290739.x discloses a preparation method of sodium N-methyltaurate. The patent takes sodium isethionate and methylamine as raw materials, a catalyst is selected from Zn5(CO3)2(OH)6, Ni2ZrO4 or Zn5(CO3)2(OH)6/Ni2ZrO4, and the yield of the sodium N-methyltaurate is 85.0-95.0% under the reaction conditions of 140 ℃ and 260 ℃ and 2-15 MPa. This patent does not change the batch mode of operation of the prior art process, as described in the specific embodiment.
The method utilizes the multi-kettle reaction devices connected in series, provides a method for continuously producing the N-methyl sodium taurate, changes the existing intermittent production method, improves the productivity and simultaneously does not reduce the product yield. The yield of the N-methyl sodium taurate is high, the productivity is high, and the production strength is high.
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 (9)
1. A method for producing sodium N-methyltaurate, which is characterized by comprising the following steps:
s1) providing a first mixed solution containing sodium isethionate, monomethylamine, and sodium hydroxide;
s2) preheating the first mixed solution to obtain a second mixed solution;
s3) allowing the second mixed solution to enter a multi-kettle series reaction system for reaction to obtain a first reaction solution;
s4) leading the first reaction solution to enter an energy recovery unit to obtain the sodium N-methyltaurate solution.
2. The process according to claim 1, wherein the multi-tank series reaction system comprises 2 to 6 reaction tanks connected in series, preferably 3 to 4 reaction tanks connected in series.
3. The process according to claim 1 or 2, wherein the charge factor in each reaction vessel is from 0.3 to 0.95, preferably from 0.60 to 0.85.
4. The method according to claim 1 or 2, wherein the material residence time in each reaction vessel is 1 to 60min, preferably 3 to 10 min.
5. The method according to claim 1 or 2, wherein the material temperature in each reaction vessel is 150-350 ℃, preferably 180-300 ℃, more preferably 220-280 ℃.
6. The method of claim 1 or 2, wherein the temperature of the contents of each reaction vessel is reduced from vessel to vessel.
7. The process according to claim 1 or 2, wherein the pressure in each reactor is 3 to 30MPa, preferably 7 to 25MPa, more preferably 8 to 15 MPa.
8. The method of claim 1, wherein the molar ratio of methylamine to sodium isethionate in the first mixed solution is 3: 1-12: 1; the content of sodium hydroxide is 0.05-1.0 wt% based on the total weight of the first mixed solution.
9. An apparatus for producing sodium N-methyltaurate, the apparatus comprising: a preheating unit; a multi-kettle series reaction system containing 2-6 reaction kettles; an energy recovery unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110129121.6A CN112920094A (en) | 2021-01-29 | 2021-01-29 | Method for adjusting production load and improving yield of N-methyl sodium taurate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110129121.6A CN112920094A (en) | 2021-01-29 | 2021-01-29 | Method for adjusting production load and improving yield of N-methyl sodium taurate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112920094A true CN112920094A (en) | 2021-06-08 |
Family
ID=76168789
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110129121.6A Pending CN112920094A (en) | 2021-01-29 | 2021-01-29 | Method for adjusting production load and improving yield of N-methyl sodium taurate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112920094A (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101992055A (en) * | 2010-11-03 | 2011-03-30 | 天津大学 | Method and device of continuously synthesizing tetramethyl ammonium carbonate by multi-reactors in series |
| CN102675160A (en) * | 2012-05-07 | 2012-09-19 | 黄冈永安药业有限公司 | Device and method for continuously producing sodium methyl taurate in pipeline mode |
| CN103012160A (en) * | 2012-12-21 | 2013-04-03 | 江苏扬农化工集团有限公司 | Preparation method of o-phenylenediamine |
| CN103012769A (en) * | 2013-01-05 | 2013-04-03 | 扬州晨化科技集团有限公司 | Continuous hydro-ammonization or amination reaction method |
| CN103242206A (en) * | 2013-05-30 | 2013-08-14 | 湖南众业科技实业有限公司 | Production process for preparing fatty acyl-N-sodium methyl taurate surfactant |
| CN107629024A (en) * | 2017-10-13 | 2018-01-26 | 山东尚舜化工有限公司 | A kind of continuous synthesizer of rubber vulcanization accelerator M and its production technology |
| CN107935846A (en) * | 2017-11-03 | 2018-04-20 | 中国林业科学研究院林产化学工业研究所 | A kind of apparatus and method of continuous production environment-friendlyplasticizer plasticizer |
| CN109810074A (en) * | 2019-02-19 | 2019-05-28 | 蔚林新材料科技股份有限公司 | A kind of reaction unit of continuous synthesis 2-mercaptobenzothiazole |
| CN111499515A (en) * | 2020-04-28 | 2020-08-07 | 南京简迪环境工程有限公司 | Process for synthesizing sodium nitrophenolate by continuous hydrolysis of nitrochlorobenzene |
| CN112023833A (en) * | 2020-08-11 | 2020-12-04 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening system and method for preparing N-methyl sodium taurate |
| CN215799244U (en) * | 2021-01-29 | 2022-02-11 | 江苏奥洁生物科技有限公司 | A device for producing N-methyl sodium taurate |
-
2021
- 2021-01-29 CN CN202110129121.6A patent/CN112920094A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101992055A (en) * | 2010-11-03 | 2011-03-30 | 天津大学 | Method and device of continuously synthesizing tetramethyl ammonium carbonate by multi-reactors in series |
| CN102675160A (en) * | 2012-05-07 | 2012-09-19 | 黄冈永安药业有限公司 | Device and method for continuously producing sodium methyl taurate in pipeline mode |
| CN103012160A (en) * | 2012-12-21 | 2013-04-03 | 江苏扬农化工集团有限公司 | Preparation method of o-phenylenediamine |
| CN103012769A (en) * | 2013-01-05 | 2013-04-03 | 扬州晨化科技集团有限公司 | Continuous hydro-ammonization or amination reaction method |
| CN103242206A (en) * | 2013-05-30 | 2013-08-14 | 湖南众业科技实业有限公司 | Production process for preparing fatty acyl-N-sodium methyl taurate surfactant |
| CN107629024A (en) * | 2017-10-13 | 2018-01-26 | 山东尚舜化工有限公司 | A kind of continuous synthesizer of rubber vulcanization accelerator M and its production technology |
| CN107935846A (en) * | 2017-11-03 | 2018-04-20 | 中国林业科学研究院林产化学工业研究所 | A kind of apparatus and method of continuous production environment-friendlyplasticizer plasticizer |
| CN109810074A (en) * | 2019-02-19 | 2019-05-28 | 蔚林新材料科技股份有限公司 | A kind of reaction unit of continuous synthesis 2-mercaptobenzothiazole |
| CN111499515A (en) * | 2020-04-28 | 2020-08-07 | 南京简迪环境工程有限公司 | Process for synthesizing sodium nitrophenolate by continuous hydrolysis of nitrochlorobenzene |
| CN112023833A (en) * | 2020-08-11 | 2020-12-04 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening system and method for preparing N-methyl sodium taurate |
| CN215799244U (en) * | 2021-01-29 | 2022-02-11 | 江苏奥洁生物科技有限公司 | A device for producing N-methyl sodium taurate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP2825604B2 (en) | Method for producing methylene-bridged polyarylamine | |
| CN101679224B (en) | Enhanced process for the synthesis of urea | |
| CN215799244U (en) | A device for producing N-methyl sodium taurate | |
| CN103319391A (en) | Novel process for synthesizing N-vinyl pyrrolidone (NVP) | |
| CN112920094A (en) | Method for adjusting production load and improving yield of N-methyl sodium taurate | |
| CN112209813B (en) | One-step method for synthesizing methyl isopropyl ketone | |
| CN101805364A (en) | Producing method of triethyl aluminium | |
| CN101284783B (en) | Synthetic method of nitrobenzene ether compounds | |
| CN104829466A (en) | Method of synthesizing 3-methylamino-1,2-propylene glycol by pipeline reactor | |
| CN113024351A (en) | Production method of isopropanol | |
| CN110016001A (en) | A kind of continuous synthetic method of benzotriazole | |
| CN107721816A (en) | A kind of method of preparing cyclohexanol by cyclohexene hydration reaction | |
| CN109180501B (en) | Synthetic method of 4, 4' -diaminodiphenyl ether | |
| CN113880730B (en) | Industrial method for continuously preparing hexamethylene diisocyanate | |
| CN109824613B (en) | Method for producing BTA and co-producing TTA by one-step method | |
| CN101337862A (en) | Method for preparing 2,3-dichlorin fluorobenzene | |
| CN113683558A (en) | Preparation method for increasing yield of 2, 3-dichloropyridine | |
| CN111072551A (en) | Method for preparing piperidine amine by catalytic hydrogenation one-step method | |
| CN108947849A (en) | A kind of method of solvent-free catalytic hydrogenation production 2,4 difluorobenzene amine | |
| CN113548996B (en) | Synthesis process of N-ethyl pyrrolidone | |
| CN219540269U (en) | Device for continuously producing N-methyl sodium taurate | |
| CN115466255B (en) | Tropine and synthetic method thereof | |
| CN115583894B (en) | Method and device for continuously producing 2-nitro-4-methoxy acetanilide | |
| CN212246823U (en) | System for isoflurane ketone hydrogenation production 3,3, 5-trimethyl cyclohexanol | |
| WO2019008594A1 (en) | Continuous process for the preparation of 2-(1h-imidazol-4-yl) ethanamine and pharmaceutically acceptable salts thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210616 Address after: Room 448a, building a, emerging industry development center, Zhangjiagang Free Trade Zone, Suzhou, Jiangsu 215600 Applicant after: Jiangsu Aojie Biotechnology Co.,Ltd. Applicant after: Zhangjiagang Wenyong Jiying business management partnership (L.P.) Address before: Room 448a, building a, emerging industry development center, Zhangjiagang Free Trade Zone, Suzhou, Jiangsu 215600 Applicant before: Jiangsu Aojie Biotechnology Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20221201 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: Room 448a, building a, emerging industry development center, Zhangjiagang Free Trade Zone, Suzhou, Jiangsu 215600 Applicant before: Jiangsu Aojie Biotechnology Co.,Ltd. Applicant before: Zhangjiagang Wenyong Jiying business management partnership (L.P.) |