CN110804633A - Production method of R-3-aminobutyric acid - Google Patents
Production method of R-3-aminobutyric acid Download PDFInfo
- Publication number
- CN110804633A CN110804633A CN201911106588.8A CN201911106588A CN110804633A CN 110804633 A CN110804633 A CN 110804633A CN 201911106588 A CN201911106588 A CN 201911106588A CN 110804633 A CN110804633 A CN 110804633A
- Authority
- CN
- China
- Prior art keywords
- solution
- aminobutyric acid
- product
- conversion
- temperature
- 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
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P13/00—Preparation of nitrogen-containing organic compounds
- C12P13/005—Amino acids other than alpha- or beta amino acids, e.g. gamma amino acids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
- C07C227/38—Separation; Purification; Stabilisation; Use of additives
- C07C227/40—Separation; Purification
Landscapes
- Organic Chemistry (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Biotechnology (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a production method of R-3-aminobutyric acid, which comprises the following steps: s1, preparing a R-3-aminobutyric acid coarse material; s2, performing ultrafiltration treatment on the prepared coarse material; s3, nano-filtering the product obtained in the step S2; s4, decoloring the product obtained in the step S3; s5, concentrating the product obtained in the step S4; s6, crystallizing the product processed in the step S5; s7, centrifuging the crystals; s8, drying the product processed in the step S7; s9, finally packaging the dried product, and when preparing the R-3-aminobutyric acid coarse material in the S1 step, firstly selecting proper seeds for culturing. The invention adds the monopotassium phosphate, the dipotassium phosphate and the ammonia water to adjust the easy PH and adjust the temperature of the solution, thereby obtaining the maximum catalytic effect under the catalytic condition of certain temperature and PH value, obtaining the maximum conversion rate of the product and being beneficial to the large-scale production requirement of enterprises.
Description
Technical Field
The invention relates to the technical field of medicine production, in particular to a production method of R-3-aminobutyric acid.
Background
R-3-aminobutyric acid (R-3-aminobutyricacid), CAS: 3775-73-3, which is mainly used as the precursor of R-3-aminobutanol as the medical intermediate. R-3-aminobutanol (R-3-amino-1-butanol), CAS: 61477-40-5, is a key intermediate of medicine for treating AIDS, Dolutegravir. Dolutegravir is an integrase inhibitor of human immunodeficiency virus type I (HIV-1), a chemical synthesis thereofMore raw materials are needed, and R-3-aminobutyric acid is one of important raw materials. The molecular structural formula of the R-3-aminobutyric acid is shown as the formula (I):
at present, when R-3-aminobutyric acid is prepared, an enzyme catalysis method is mainly adopted, and catalytic preparation is carried out by using enzyme, however, when the enzyme is used for catalytic reaction, reaction conditions need to be strictly controlled, such as temperature and pH of the reaction need to be strictly controlled, because the enzyme is very sensitive to temperature and pH, the catalytic efficiency of the enzyme is affected by slight changes of temperature and pH, the enzyme can be seriously inactivated, in order to meet production requirements of enterprises, a preparation method of R-3-aminobutyric acid with high conversion rate is obtained, a method for knowing the optimal temperature and pH of the enzyme catalysis preparation of R-3-aminobutyric acid is urgently needed, and therefore, a production method of R-3-aminobutyric acid is provided.
Disclosure of Invention
The invention aims to solve the defects in the prior art and provides a production method of R-3-aminobutyric acid.
In order to achieve the purpose, the invention adopts the following technical scheme:
a production method of R-3-aminobutyric acid comprises the following steps:
s1, preparing a R-3-aminobutyric acid coarse material;
s2, performing ultrafiltration treatment on the prepared coarse material;
s3, nano-filtering the product obtained in the step S2;
s4, decoloring the product obtained in the step S3;
s5, concentrating the product obtained in the step S4;
s6, crystallizing the product processed in the step S5;
s7, centrifuging the crystals;
s8, drying the product processed in the step S7;
and S9, finally packaging the dried product.
Preferably, when preparing the R-3-aminobutyric acid coarse material in the step S1, firstly, selecting proper seeds for culturing, firstly, culturing the seeds in a shake flask overnight, then transferring the seeds into a seeding tank for continuous culture until OD reaches a specified range, thereby obtaining a seed solution.
Preferably, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and a tube membrane is used for collecting the obtained enzyme concentrated solution.
Preferably, during the conversion operation, adding the substrate into a conversion tank filled with a certain amount of water under the stirring condition, heating to a specified range, adjusting the pH to the specified range by using ammonia water after the substrate is completely dissolved, then adding other raw materials and an enzyme concentrated solution to start conversion, controlling the temperature and the pH during the conversion process, stopping the conversion when the content of the substrate is less than the specified range, and controlling the temperature to be 32-46 ℃ and the pH to be 8.3-9.7 during the conversion process.
Preferably, after the conversion is completed, the conversion solution is filtered through a tube membrane, a hollow membrane or a nanofiltration membrane to remove bacteria, proteins and other impurities, thereby obtaining a membrane filtration clear solution.
Preferably, a decoloring tank is needed in the decoloring operation, membrane filtration clear liquid is transferred into the decoloring tank when in use, a certain amount of activated carbon is added for decoloring for a certain time, and then the decolored liquid is decarburized.
Preferably, an evaporator is needed in the evaporation concentration process, and the decolorized solution is transferred to the evaporator to be evaporated to obtain a product concentrated solution.
Preferably, a crystallizing tank is needed in the crystallization operation, the product concentrated solution is added into the crystallizing tank, the temperature is controlled to be continuously evaporated to a certain concentration range, and the temperature is reduced for crystallization.
Preferably, a centrifugal machine is needed in the centrifuging, drying and packaging operations, the feed liquid after crystallization is centrifuged by the centrifugal machine, the wet product crystals are collected, the wet product crystals pass through drying equipment to obtain dry products, then sampling and inspecting are carried out, qualified dry products are detected, the mixed and packaged finished products are processed, and unqualified products are processed by reworking.
According to the invention, the PH value is easily adjusted by adding the monopotassium phosphate, the dipotassium phosphate and the ammonia water, and the temperature of the solution is adjusted, so that the maximum catalytic effect can be obtained under the catalytic condition of a certain temperature and a certain PH value, the maximum conversion rate of the product is obtained, and the requirement of large-scale production of enterprises is facilitated.
Drawings
FIG. 1 is a schematic view of a process structure of a method for producing R-3-aminobutyric acid according to the present invention;
FIG. 2 is a schematic view of a detailed flow structure of the production method of R-3-aminobutyric acid provided by the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments.
Example one
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In the embodiment, during the conversion operation, a substrate is added into a conversion tank filled with a certain amount of water under the stirring condition, the temperature is increased to a specified range, after the substrate is completely dissolved, the pH is adjusted to the specified range by ammonia water, then other raw materials and an enzyme concentrated solution are added to start the conversion, the temperature and the pH are controlled in the conversion process, the conversion is stopped when the content of the substrate is less than the specified range, the temperature is controlled at 32 ℃ in the conversion process, and the pH is controlled at 8.3.
Example two
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In the embodiment, during the conversion operation, a substrate is added into a conversion tank filled with a certain amount of water under the stirring condition, the temperature is increased to a specified range, after the substrate is completely dissolved, the pH is adjusted to the specified range by ammonia water, then other raw materials and an enzyme concentrated solution are added to start the conversion, the temperature and the pH are controlled in the conversion process, the conversion is stopped when the content of the substrate is less than the specified range, the temperature is controlled at 34 ℃ in the conversion process, and the pH is controlled at 8.5.
EXAMPLE III
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In the embodiment, during the conversion operation, a substrate is added into a conversion tank filled with a certain amount of water under the stirring condition, the temperature is increased to a specified range, after the substrate is completely dissolved, the pH is adjusted to the specified range by ammonia water, then other raw materials and an enzyme concentrated solution are added to start the conversion, the temperature and the pH are controlled in the conversion process, the conversion is stopped when the content of the substrate is less than the specified range, the temperature is controlled at 36 ℃ in the conversion process, and the pH is controlled at 8.7.
Example four
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In this example, during the conversion operation, the substrate was added to a conversion tank containing a certain amount of water under stirring, the temperature was raised to a predetermined range, after the substrate was completely dissolved, the PH was adjusted to a predetermined range with ammonia water, then other raw materials and an enzyme concentrate were added to start the conversion, the temperature and PH were controlled during the conversion, the conversion was stopped when the substrate content was less than the predetermined range, the temperature was controlled at 38 ℃ during the conversion, and the PH was controlled at 8.9.
EXAMPLE five
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In the embodiment, during the conversion operation, a substrate is added into a conversion tank filled with a certain amount of water under the stirring condition, the temperature is increased to a specified range, after the substrate is completely dissolved, the pH is adjusted to the specified range by ammonia water, then other raw materials and an enzyme concentrated solution are added to start the conversion, the temperature and the pH are controlled in the conversion process, the conversion is stopped when the content of the substrate is less than the specified range, the temperature is controlled at 40 ℃ in the conversion process, and the pH is controlled at 9.1.
Sixth embodiment
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In the embodiment, during the conversion operation, a substrate is added into a conversion tank filled with a certain amount of water under the stirring condition, the temperature is increased to a specified range, after the substrate is completely dissolved, the pH is adjusted to the specified range by ammonia water, then other raw materials and an enzyme concentrated solution are added to start the conversion, the temperature and the pH are controlled in the conversion process, the conversion is stopped when the content of the substrate is less than the specified range, the temperature is controlled at 42 ℃ in the conversion process, and the pH is controlled at 9.3.
The seventh embodiment
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In this example, during the conversion operation, the substrate was added to a conversion tank containing a certain amount of water under stirring, the temperature was raised to a predetermined range, after the substrate was completely dissolved, the PH was adjusted to a predetermined range with ammonia water, then other raw materials and an enzyme concentrate were added to start the conversion, the temperature and PH were controlled during the conversion, the conversion was stopped when the substrate content was less than the predetermined range, the temperature was controlled at 44 ℃ during the conversion, and the PH was controlled at 9.5.
The eighth embodiment
In this embodiment, when preparing the R-3-aminobutyric acid coarse material, a suitable seed is first selected for cultivation, the seed is first cultivated in a shake flask overnight, and then transferred to a seed tank for further cultivation until the OD reaches a specified range, thereby obtaining a seed solution.
In the embodiment, in the fermentation operation, prepared raw materials of peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under the stirring condition, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and a pipeline are subjected to steam sterilization, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is not increased any more or is slowly increased, the culture is stopped, and an enzyme concentrated solution is obtained by collecting a tube membrane.
In this example, during the conversion operation, the substrate is added into a conversion tank filled with a certain amount of water under stirring, the temperature is raised to a specified range, after the substrate is completely dissolved, the PH is adjusted to a specified range with ammonia water, then other raw materials and an enzyme concentrate are added to start the conversion, the temperature and the PH are controlled in the conversion process, the conversion is stopped when the substrate content is less than the specified range, the temperature is controlled at 45 ℃ and the PH is controlled at 9.7 in the conversion process.
Through the adjustment of the temperature and the pH in the above examples, the following conversion rates under the respective conditions were obtained by detection:
| temperature/. degree.C | 32 | 34 | 36 | 38 | 40 | 42 | 44 | 46 |
| PH | 8.3 | 8.5 | 8.7 | 8.9 | 9.1 | 9.3 | 9.5 | 9.7 |
| Conversion rate/% | 96.4 | 97.3 | 98.6 | 99.87 | 99.32 | 98.4 | 97.1 | 96.6 |
In summary, it can be clearly seen from the table that, under the catalysis conditions of 38 ℃ and 8.9 of PH, the enzyme has the highest catalytic efficiency, and the conversion rate of the product can reach 99.87%, and by adding potassium dihydrogen phosphate and dipotassium hydrogen phosphate, phosphate ions and potassium ions in the enzyme are biological culture ions, and when the PH of the solution is changed, the activity of the enzyme is not affected, so that the invention has higher conversion rate by adding the raw materials for culture catalysis, which is beneficial to the requirement of industrial production.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (9)
1. A production method of R-3-aminobutyric acid is characterized by comprising the following steps:
s1, preparing a R-3-aminobutyric acid coarse material;
s2, performing ultrafiltration treatment on the prepared coarse material;
s3, nano-filtering the product obtained in the step S2;
s4, decoloring the product obtained in the step S3;
s5, concentrating the product obtained in the step S4;
s6, crystallizing the product processed in the step S5;
s7, centrifuging the crystals;
s8, drying the product processed in the step S7;
and S9, finally packaging the dried product.
2. A method for producing R-3-aminobutyric acid according to claim 1, wherein said raw material of R-3-aminobutyric acid is prepared in step S1, wherein said raw material is prepared by selecting suitable seeds for cultivation, said seeds are first cultivated in a shake flask overnight, then transferred to a seed tank for further cultivation until OD reaches a specified range, thereby obtaining seed liquid.
3. The method for producing R-3-aminobutyric acid according to claim 1, wherein in the fermentation operation, prepared peptone, yeast extract, potassium dihydrogen phosphate and dipotassium hydrogen phosphate are put into a fermentation tank filled with a certain amount of water, the pH of the solution is 5.3-6.6 due to weak acidity of potassium dihydrogen phosphate and dipotassium hydrogen phosphate solution, the pH of the solution is adjusted to a process specified range by ammonia water under stirring, the pH of the solution is adjusted to 8.7-10.2 by ammonia water, after the fermentation tank and pipeline steam sterilization is finished, the cultured seed solution is transferred into the fermentation tank for continuous culture, and when the culture is stopped until OD does not rise or rises slowly, the culture is stopped and enzyme concentrated solution is collected by a tube membrane.
4. The method for producing R-3-aminobutyric acid according to claim 1, wherein during the conversion operation, the substrate is added into a conversion tank filled with a certain amount of water under stirring, the temperature is raised to a specified range, after the substrate is completely dissolved, the pH is adjusted to a specified range by using ammonia water, then other raw materials and the enzyme concentrate are added to start the conversion, the temperature and the pH are controlled during the conversion process, the conversion is stopped when the substrate content is less than the specified range, and the temperature is controlled to be 32-46 ℃ and the pH is controlled to be 8.3-9.7 during the conversion process.
5. The method for producing R-3-aminobutyric acid according to claim 1, wherein said converting solution is filtered through a tube membrane, a hollow membrane, a nanofiltration membrane to remove bacteria, proteins and other impurities, thereby obtaining a membrane filtration clear solution.
6. The method for producing R-3-aminobutyric acid according to claim 1, wherein a decolorizing tank is required in decolorizing operation, membrane filtered clear liquid is transferred into the decolorizing tank in use, a certain amount of activated carbon is added for decolorizing for a certain time, and then decolorized decolorizing liquid is decarbonized.
7. The method for producing R-3-aminobutyric acid according to claim 1, wherein an evaporator is required in the evaporation concentration process, and the decolorized solution is transferred to the evaporator for evaporation to obtain a product concentrated solution.
8. The method for producing R-3-aminobutyric acid according to claim 1, wherein a crystallizing tank is required in the crystallizing operation, the product concentrated solution is added into the crystallizing tank, the temperature is controlled to continue evaporating to a certain concentration range, and the temperature is reduced for crystallization.
9. The method for producing R-3-aminobutyric acid according to claim 1, wherein a centrifuge is required for the centrifugation, drying and packaging operations, the crystallized feed liquid is centrifuged by the centrifuge, the wet product crystals are collected, the wet product crystals pass through a drying device to obtain a dried product, the dried product is sampled and inspected, the qualified dried product is detected, the packaged finished product is mixed, and the unqualified product is reworked.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911106588.8A CN110804633A (en) | 2019-11-13 | 2019-11-13 | Production method of R-3-aminobutyric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911106588.8A CN110804633A (en) | 2019-11-13 | 2019-11-13 | Production method of R-3-aminobutyric acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110804633A true CN110804633A (en) | 2020-02-18 |
Family
ID=69502359
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911106588.8A Pending CN110804633A (en) | 2019-11-13 | 2019-11-13 | Production method of R-3-aminobutyric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110804633A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302549A (en) * | 2007-05-09 | 2008-11-12 | 浙江医药股份有限公司新昌制药厂 | High-purity miglitol production process |
| CN101418327A (en) * | 2008-11-21 | 2009-04-29 | 大连珍奥生物技术股份有限公司 | The new process of production of high purity 5 ' Nucleotide |
| CN101550101A (en) * | 2009-01-20 | 2009-10-07 | 福建省建阳武夷味精有限公司 | Method for clean purifying L-tryptophan by utilizing fermented liquid |
| CN108374027A (en) * | 2018-03-09 | 2018-08-07 | 长兴制药股份有限公司 | A kind of preparation method of R-3- aminobutyric acids |
| CN109576317A (en) * | 2017-09-29 | 2019-04-05 | 上海弈柯莱生物医药科技有限公司 | The method that enzyme process prepares R-3- aminobutyric acid |
-
2019
- 2019-11-13 CN CN201911106588.8A patent/CN110804633A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101302549A (en) * | 2007-05-09 | 2008-11-12 | 浙江医药股份有限公司新昌制药厂 | High-purity miglitol production process |
| CN101418327A (en) * | 2008-11-21 | 2009-04-29 | 大连珍奥生物技术股份有限公司 | The new process of production of high purity 5 ' Nucleotide |
| CN101550101A (en) * | 2009-01-20 | 2009-10-07 | 福建省建阳武夷味精有限公司 | Method for clean purifying L-tryptophan by utilizing fermented liquid |
| CN109576317A (en) * | 2017-09-29 | 2019-04-05 | 上海弈柯莱生物医药科技有限公司 | The method that enzyme process prepares R-3- aminobutyric acid |
| CN108374027A (en) * | 2018-03-09 | 2018-08-07 | 长兴制药股份有限公司 | A kind of preparation method of R-3- aminobutyric acids |
Non-Patent Citations (1)
| Title |
|---|
| 夏焕章: "《发酵工艺学》", 31 July 2007 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108285912B (en) | Method for preparing and extracting pharmaceutical grade valine by fermentation | |
| WO2008134936A1 (en) | Method for extracting threonine from threonine fermentation liquor | |
| CN107099563B (en) | Method for preparing monosodium glutamate by using isoelectric technology | |
| CN101525645B (en) | Membrane-sterilization method for sorbose fermentation medium by using ceramic microfiltration membranes | |
| CN109136299B (en) | Method for preparing, extracting and purifying threonine | |
| CN110904163A (en) | Method for improving lactic acid content of corn steep liquor | |
| CN108251476B (en) | Method for extracting vitamin B12 from enzyme preparation wastewater | |
| CN107201384A (en) | A kind of method of separation and Extraction D-ALPHA-Hydroxypropionic acid in sodium zymotic fluid from D-ALPHA-Hydroxypropionic acid | |
| CN103113440A (en) | Preparation method of erythromycin thiocyanate | |
| CN103695490B (en) | High-purity arginine production process | |
| CN102719502A (en) | Method for producing L-alanine by mutating lactate-production bacteria | |
| CN110804633A (en) | Production method of R-3-aminobutyric acid | |
| CN112359150A (en) | Crystallization process of crystallized glucose | |
| CN109266578A (en) | Escherichia coli ACThr1032 and its application in production of L-threonine by fermentation | |
| CN108220351B (en) | Method for preparing L-arginine-alpha-ketoglutaric acid by biological enzyme method | |
| CN111065644B (en) | Method for preparing high-purity NAD | |
| CN111440830A (en) | Method for producing xylitol by fermenting corncob hydrolysate | |
| EP3581658A1 (en) | Method for producing alcohol by continuous fermentation and continuous fermentation apparatus to be used therefor | |
| CN109182407A (en) | A kind of tryptophan preparation method and its fermentation medium and tryptophan that use fermentation special nutritional member | |
| CN109929884A (en) | A kind of preparation method of ketoglutaric acid | |
| CN114410504A (en) | Method for extracting theanine by fermentation | |
| CN114058653B (en) | Method for preparing gamma-aminobutyric acid by biological synthesis method | |
| CN112694504A (en) | Novel glucose crystallization process | |
| CN116676200B (en) | Aspergillus niger strain and application thereof in preparation of citric acid | |
| CN106434822A (en) | Method for preparing high-content cholic acid by microorganism transformation method |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200218 |
|
| RJ01 | Rejection of invention patent application after publication |