CN103539688A - Method for separating and extracting L-serine from corynebacterium glutamicum fermentation liquor - Google Patents
Method for separating and extracting L-serine from corynebacterium glutamicum fermentation liquor Download PDFInfo
- Publication number
- CN103539688A CN103539688A CN201310508490.1A CN201310508490A CN103539688A CN 103539688 A CN103539688 A CN 103539688A CN 201310508490 A CN201310508490 A CN 201310508490A CN 103539688 A CN103539688 A CN 103539688A
- Authority
- CN
- China
- Prior art keywords
- serine
- concentrated
- afterwards
- crystallization
- add
- 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.)
- Granted
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a method for separating and extracting L-serine from corynebacterium glutamicum fermentation liquor. The method comprises the following steps of: flocculating fermentation liquor; absorbing and decoloring an extracting solution subjected to solid-liquid separation through active carbon, then removing macromolecules through ultrafiltration, and absorbing amino acid by adopting cationic resin; eluting by utilizing ammonia water; carrying out vacuum concentration on an eluent, and carrying out cooling crystallization by adding ethanol to obtain an L-serine crystal. The method disclosed by the invention is high in extraction efficiency, can achieve the one-way extraction rate more than 56%, can achieve the integrated extraction rate more than 80% through mother solution recovery and retreatment and has the advantages of easiness for industrialization realization, relatively low extraction cost and large-batch treatment.
Description
Technical field
The present invention relates to a kind of extraction process, particularly from the fermented liquid of Corynebacterium glutamicum, extract the method for Serine.
Background technology
Serine (L-serine writes a Chinese character in simplified form L-ser), molecular formula is C
3h
7nO
3, chemical structure is HO-CH
2cH (NH
3)-COOH, molecular weight 105.10, chemistry pantonine-hydroxy-propionic acid by name.Serine belongs to nonessential amino acid; it is glycogenic amino acid; important role in during proliferation process; when Growth of Cells, Serine is the synthetic main one-carbon unit donor of purine nucleotides and phosphoric acid deoxythymidine, is also the precursor substance of other amino acid (as halfcystine, taurine), lipid messenger molecule (as phosphatidylserine, ceramide) and neuromodulator (glycine, D-Ser) simultaneously.Serine has wide application in foodstuffs industry, medicine, makeup, and its market demand constantly increases.
At present, the method for producing Serine both at home and abroad mainly contains chemical synthesis, silk hydrolysis method, enzyme process, Precurosor fermentation method etc.Domestic rarely have the report that directly utilizes microorganism fermentation direct production Serine.Southern Yangtze University from occurring in nature screen the Corynebacterium glutamicum that a strain can directly utilize saccharine material fermentative production Serine (
corynebacterium glutamicum), systematic research has been launched to this strain Corynebacterium glutamicum in this laboratory.The normal grade of Luo Yu built a strain Serine by molecular biology method
c.glutamicumproducing Strain 33a △ SSA (culture presevation number), through fermentation optimization, its fermentation for meeting pilot scale and mass-producing fermentation, need to be studied the extraction and purification process of Serine more than producing that Serine level is stable and reaching 25g/L.
The process for refining of early stage Serine mainly for be the stock liquids such as hydrolyzed solution such as silk, hair, owing to containing multiple other amino acid and impurity in feed liquid simultaneously, extraction process is complicated, yield is low, especially in alkali process hydrolysis technique, also contain more D-Ser, need to split and make the transition (Feng Rongbao. improved ion exchange method is extracted l-Serine, chemical communication, 2000.04; From reeling waste silk, extract a production technique for Serine, Chinese patent 201010507725.1).Because hydrolysis method extraction process is polluted greatly, cost is high, only there is at present a small amount of production.In recent years, utilize enzyme method technique to produce Serine and also have report, as employing serine hydroxymethylase, take glycine and formaldehyde as substrate, take tetrahydrofolic acid (THFA) and pyridoxal phosphate as cofactor can obtain Serine, utilize the technology such as ultrafiltration and ionic adsorption to complete to extract separated (Wei Pinghe etc. the separation and purification of Production by Enzymes Serine, Chinese Journal of New Drugs, 2012.20), but also have the problems such as complex process.And enzymatic conversion method liquid and fermented liquid production concentration, impurity form and content aspect there is bigger difference, therefore in method, can not simply apply mechanically.
c.glutamicumin fermented liquid, main amino acid impurity is α-amino-isovaleric acid, L-Ala, and other assorted histidine contents are less, and non-amino acids impurity is mainly thalline, pigment, albumen and residual medium component.Its composing system is compared relative simple with hydrolyzed solution, also do not have D type amino acid, but α-amino-isovaleric acid, L-Ala and Serine are comparatively approaching in nature, and separation is difficulty comparatively.Therefore, need to be for
c.glutamicumthe feature of fermented liquid, sets up the extraction process that a kind of extraction efficiency is high, separation costs is low, to meet the production of fermentation method Serine.
Summary of the invention
The object of the invention is to a kind of method of extracting Serine from the fermented liquid of Corynebacterium glutamicum.
The technical solution used in the present invention is:
A method of extracting Serine the fermented liquid of Corynebacterium glutamicum, comprises the steps:
1) flocculation: add flocculation agent to flocculate in Corynebacterium glutamicum fermented liquid, solid-liquid separation is removed throw out afterwards, obtains clear liquid;
2) decolouring: add decolorizing adsorbent in clear liquid, solid-liquid separation, obtains destainer afterwards;
3) ultrafiltration: by destainer ultrafiltration, molecular weight cut-off, at 2000～5000 Da, merges ultrafiltrated;
4) absorption and wash-out: by ultrafiltrated by cationic exchange coloum with absorption amino acid, wash-out, obtains elutriant afterwards;
5) concentrated: elutriant is concentrated, obtain concentrated solution;
6) crystallization: add ethanol in concentrated solution, mix, be cooled to afterwards 5～10 ℃, make Serine crystallization, collect crystal the washes clean separated out;
7) dry: the Serine of washes clean is dry, obtain finished product.
As a further improvement on the present invention, during flocculation operation, by the pH regulator of fermented liquid, be first 3～5, add afterwards flocculation agent polyacrylamide, making its concentration in fermented liquid is 100～200 mg/ml.
As a further improvement on the present invention, the decolorizing adsorbent adopting during decolouring is Powdered Activated Carbon.
The ion exchange resin of filling in cationic exchange coloum as a further improvement on the present invention, is 732 storng-acid cation exchange resins.
As a further improvement on the present invention, the eluent that absorption is used in operating with wash-out is ammoniacal liquor.Further, the concentration of ammoniacal liquor is 0.2～0.5mol/L.
As a further improvement on the present invention, during crystallization operation, the volumetric concentration of ethanol in concentrated solution is 40～80%.
As a further improvement on the present invention, adopt the crystallization of ethanolic soln washing Serine.
The invention has the beneficial effects as follows:
The inventive method can be extracted Serine high efficiency, low cost from the fermented liquid of Corynebacterium glutamicum, and the Serine purity obtaining is high.Meanwhile, the inventive method does not affect extracts other amino acid from fermented liquid, is conducive to the comprehensive utilization of fermented liquid.
The present invention adopts flocculation and centrifugal separation to carry out thalline removal, by ultrafiltration, remove macromolecular substance again, then adopt ion exchange method to carry out amino acid adsorption and desorption, and utilize reverse osmosis process to concentrate stripping liquid, finally by cooling and crystallizing process, obtain Serine.The inventive method, extraction efficiency is high, and one way extraction yield can reach more than 56%, by mother liquor, is reclaimed and is processed, and comprehensive extraction yield can reach more than 80%.The inventive method is easy to realization of industrialization, and extraction cost is relatively cheap, can carry out mass disposal.
The main innovation of above-mentioned technique is: the one, and utilize ultrafiltration technology to remove macromole, reduce the pollution of impurity to ion exchange resin, improve the efficiency of ion-exchange, reduce the process procedure of ion-exchange; The 2nd, utilize reverse osmosis process to concentrate, reduce the production load of vacuum concentration, energy-saving effect is remarkable; The 3rd, utilize cooling and crystallizing process to obtain high purity Serine, and L-Ala, α-amino-isovaleric acid are stayed in mother liquor with this understanding, can be used as by product and reclaim.
Accompanying drawing explanation
Fig. 1 is the solubility curve of Serine in pure water and ethanolic soln;
Fig. 2 is the elution curve of different aminoacids.
Embodiment
A method of extracting Serine the fermented liquid of Corynebacterium glutamicum, comprises the steps:
1) flocculation: add flocculation agent to flocculate in Corynebacterium glutamicum fermented liquid, solid-liquid separation is removed throw out afterwards, obtains clear liquid;
2) decolouring: add decolorizing adsorbent in clear liquid, solid-liquid separation, obtains destainer afterwards;
3) ultrafiltration: by destainer ultrafiltration, molecular weight cut-off, at 2000～5000 Da, merges ultrafiltrated;
4) absorption and wash-out: by ultrafiltrated by cationic exchange coloum with absorption amino acid, wash-out, obtains elutriant afterwards;
5) concentrated: elutriant is concentrated, obtain concentrated solution;
6) crystallization: add ethanol in concentrated solution, mix, be cooled to afterwards 5～10 ℃, make Serine crystallization, collect crystal the washes clean separated out;
7) dry: the Serine of washes clean is dry, obtain finished product.
As a further improvement on the present invention, during flocculation operation, by the pH regulator of fermented liquid, be first 3～5, add afterwards flocculation agent polyacrylamide, making its concentration in fermented liquid is 100～200 mg/ml.Generally, after adding flocculation agent, stir 20～60min, after standing 1～8h, centrifugation throw out can be removed most macromole impurity.
As a further improvement on the present invention, the decolorizing adsorbent adopting during decolouring is Powdered Activated Carbon.Generally speaking, in the supernatant liquor after flocculation, add the powdered active carbon of 5～50g/L, under the condition of 20～80 ℃, stir 20～60min, filter or centrifugally can obtain good decolorizing effect.
Ultrafiltration can be used general ceramic super-filtering film or organic ultra-filtration membrane device.For raising interest rates, trapped fluid can repeatedly add purified water to wash, and leaches rear merging filtrate.
The ion exchange resin of filling in cationic exchange coloum as a further improvement on the present invention, is 732 storng-acid cation exchange resins.Control suitable flow velocity and add volume, the Serine component in ultrafiltrated is fully adsorbed.By effluent liquid is monitored, after saturated to absorption, stop feeding in raw material, by the purified water of 1.5～3.0 times of column volumes, wash, adopting concentration is the ammoniacal liquor wash-out of 0.2～0.5mol/L again, by aminoacids content and composition in monitoring elutriant, ammonia concn and flow velocity are optimized, control suitable condition and make Serine flow out peak shape to concentrating.Collect the concentrated elution peak of Serine.
When concentrated, can utilize reverse osmosis unit or multi-effect vacuum thickener, or the mode of upper reverse osmosis and Multi-effect concentration coupling concentrates to elutriant, in suitable concentrated solution, solid content is 20～40%.
As a further improvement on the present invention, the eluent that absorption is used in operating with wash-out is ammoniacal liquor.Further, the concentration of ammoniacal liquor is 0.2～0.5mol/L.
Because Serine is very easily dissolved in water, at 5 ℃, in saturated solution, Serine content still has 18.9%, and therefore the simple cooling method that adopts carries out crystallization, and its rate of recovery is low.And under 5% solution system, in its saturated solution, Serine content drops to 2.5%.The solubleness of Serine in pure water and ethanolic soln is as shown in table 1, and the solubility curve of Serine in pure water and ethanolic soln as shown in Figure 1.
The solubleness (g) of table 1 Serine in pure water and ethanolic soln
From table 1 and Fig. 1, although add a large amount of ethanol, can make solubleness significantly decline, industrial production need to be used a large amount of ethanol, and alcohol concn is too high will increase the cost recovery of ethanol, is unfavorable for safety in production simultaneously.Therefore, from industrial economy angle and security consideration, during crystallization operation, should control the volumetric concentration of ethanol in concentrated solution is 40～80%, best, adopt the ethanolic soln of 50% left and right to carry out crystallization.
Loss when reducing the crystallization of washing Serine, adopt ethanolic soln to Serine crystallization wash, preferred, adopt 70%(v/v) above cold ethanol carries out drip washing, best, adopts 85%(v/v) cold ethanol carry out drip washing.
Below in conjunction with embodiment, further illustrate the present invention.
Before and after flocculating by mensuration, fermented liquid is evaluated (formula 1) in the variation of the OD of 562nm place to thalline removal effect, and before and after decolouring by mensuration, liquid is investigated pigment removal effect (formula 2) in the variation of the OD of 400nm place.
Thalline decreasing ratio (%)=(1-OD
before 562 flocculations/ OD
after 562 flocculations) * 100%---(formula 1)
Percent of decolourization (%)=(1-OD
before 400 decolourings/ OD
after 400 decolourings) * 100%------(formula 2)
In following examples, if no special instructions, the concentration of ethanol all refers to concentration expressed in percentage by volume.
The pre-treatment of 732 Zeo-karbs is undertaken by the ordinary method of this area, first uses saturated common salt water soaking 8～10 hours, after clear water rinsing, then uses 2%～4% NaOH solution soaking 2～4 hours, drains rear clear water rinsing; Finally use 5%HCL solution, soak 8～10 hours, clear water drifts about to neutral, stand-by.
embodiment 1
flocculation:get Corynebacterium glutamicum fermented liquid 50 L, with hydrochloric acid, the pH of fermented liquid is adjusted to 3.0,30 ℃ of fluid temperatures,, add the 20g/L polyacrylamide liquid of 0.5 L, stir 40min, centrifugal after standing one hour, remove precipitation, obtain 47.5L clear liquid, after testing, polyacrylamide flocculation is to thalline decreasing ratio 98.49%;
decolouring:in above-mentioned clear liquid, add the powdered active carbon of 0.5 kg, be warming up to 60 ℃, stir decolouring 30min, remove by filter gac, obtain destainer 46L, after testing, the percent of decolourization of gac is 92.73%, and by flocculating and decolour operation, the yield of Serine is 90.2%;
ultrafiltration:adopt spiral wound membrane pilot unit contained (pvdf membrane, filtration area 0.5m
2) the 46L destainer obtaining is carried out to ultrafiltration, its molecular weight cut-off is 3000Da, filter pressure is 0.2～0.3MPa, when the destainer of holding back remains 5～8L, add purified water 5～10 L to wash, washing operation 3 times, merges and obtains about 60L ultrafiltrated again, after testing, the Serine quality percentage composition in ultrafiltrated is 1.81%;
absorption and wash-out: 732 pretreated Zeo-karbs are inserted to the pillar of Φ 150 * 2000mm, the flow velocity upper prop by ultrafiltrated with 500ml/min, to the complete upper prop of 60L ultrafiltrated, then uses the 90 L water washing pillars of pH5.0; After washing, then with same flow velocity, carry out wash-out with the ammoniacal liquor of 0.5mol/L, obtain the elutriant 30L that is rich in Serine component, the yield that HPLC detects Serine is 83.96%; Utilize ninhydrin method to detect elutriant, find that amino acids main component concentrates in 40～70L elutriant, HPLC analytical results shows, in this part elutriant, still contain the compositions (Fig. 2) such as α-amino-isovaleric acid, L-Ala, show that this resin cation (R.C.) does not have good centrifugation to these impurity amino acid, therefore still need follow-up crystallization operation;
concentrated: by 30L elutriant vacuum-concentrcted, thickening temperature, not higher than 65 ℃, obtains 3L concentrated solution, and HPLC measures Serine content in solution and is about 30%;
crystallization: for ease of operation, slowly add isopyknic ethanol in above-mentioned concentrated solution, after stirring, slow cooling to 5 ℃, more than standing 6h, makes Serine sufficient crystallising leach Serine crystal, and carries out drip washing with 85% cold ethanol;
dry: the crystallization after washing at 80 ℃ more than dry 5h to constant weight 730 g, the rate of recovery of crystallisation step is 79.6%.
embodiment 2
flocculation: get Corynebacterium glutamicum fermented liquid 50 L, with hydrochloric acid, the pH of fermented liquid is adjusted to 5.0,40 ℃ of fluid temperatures, adding polyacrylamide to adjust its concentration is 150 mg/L, stirs 60min, centrifugal after standing 3 h, removes precipitation, obtains clear liquid;
decolouring: in above-mentioned clear liquid, add powdered active carbon, addition is 20g/L, is warming up to 50 ℃, stirs decolouring 60min, removes by filter gac, obtains destainer;
ultrafiltration: adopt spiral wound membrane pilot unit contained to carry out ultrafiltration to destainer, its molecular weight cut-off is 5000Da, when the destainer of holding back remains 5～8L, then adds purified water 5～10 L to wash, and washing operation 3 times merges and obtains ultrafiltrated;
absorption and wash-out: 732 pretreated Zeo-karbs are inserted to the pillar of Φ 150 * 2000mm, the flow velocity upper prop by ultrafiltrated with 600ml/min, to the complete upper prop of ultrafiltrated, then uses the 60 L water washing pillars of pH 3.0; After washing, then with same flow velocity, carry out wash-out with the ammoniacal liquor of 0.3mol/L, obtain the elutriant that is rich in Serine component;
concentrated: elutriant by reverse-osmosis treated, is obtained to solid content and is 20% concentrated solution;
crystallization: adding ethanol to its concentration is 80%, and after stirring, slow cooling to 10 ℃, more than standing 6h, makes Serine sufficient crystallising leach Serine crystal, and carry out drip washing with 85% cold ethanol
dry: at 80 ℃, more than dry 5h, obtain Serine finished product.
embodiment 3
flocculation: get Corynebacterium glutamicum fermented liquid 50 L, with hydrochloric acid, the pH of fermented liquid is adjusted to 4.0,30 ℃ of fluid temperatures, adding polyacrylamide to adjust its concentration is 10 mg/L, stirs 90min, centrifugal after standing 6 h, removes precipitation, obtains clear liquid;
decolouring: in above-mentioned clear liquid, add powdered active carbon, addition is 5g/L, is warming up to 65 ℃, stirs decolouring 60min, removes by filter gac, obtains destainer;
ultrafiltration: adopt Ceramic excessive filtration membrane pilot unit contained to carry out ultrafiltration to destainer, its molecular weight cut-off is 2000Da, when the destainer of holding back remains 5～8L, then adds purified water 5～10 L to wash, and washing operation 3 times merges and obtains ultrafiltrated;
absorption and wash-out: 732 pretreated Zeo-karbs are inserted to the pillar of Φ 150 * 2000mm, the flow velocity upper prop by ultrafiltrated with 400ml/min, to the complete upper prop of ultrafiltrated, then uses the 70 L water washing pillars of pH 4.0; After washing, then with same flow velocity, carry out wash-out with the ammoniacal liquor of 0.2mol/L, obtain the elutriant that is rich in Serine component;
concentrated: by elutriant vacuum-concentrcted, thickening temperature is not higher than 65 ℃, and obtaining solid content is 40% concentrated solution;
crystallization: adding ethanol to concentration is 40%, and after stirring, slow cooling to 7 ℃, more than standing 6h, makes Serine sufficient crystallising leach Serine crystal, and carry out drip washing with 70% cold ethanol;
dry: at 80 ℃, more than dry 5h, obtain Serine finished product.
Claims (10)
1. from the fermented liquid of Corynebacterium glutamicum, extract a method for Serine, comprise the steps:
1) flocculation: add flocculation agent to flocculate in Corynebacterium glutamicum fermented liquid, solid-liquid separation is removed throw out afterwards, obtains clear liquid;
2) decolouring: add decolorizing adsorbent in clear liquid, solid-liquid separation, obtains destainer afterwards;
3) ultrafiltration: by destainer ultrafiltration, molecular weight cut-off, at 2000～5000 Da, merges ultrafiltrated;
4) absorption and wash-out: by ultrafiltrated by cationic exchange coloum with absorption amino acid, wash-out, obtains elutriant afterwards;
5) concentrated: elutriant is concentrated, obtain concentrated solution;
6) crystallization: add ethanol in concentrated solution, mix, be cooled to afterwards 5～10 ℃, make Serine crystallization, collect crystal the washes clean separated out;
7) dry: the Serine of washes clean is dry, obtain finished product.
2. method according to claim 1, is characterized in that: during flocculation operation, by the pH regulator of fermented liquid, be first 3～5, add afterwards flocculation agent polyacrylamide, making its concentration in fermented liquid is 100～200 mg/ml.
3. method according to claim 1, is characterized in that: the decolorizing adsorbent adopting during decolouring is Powdered Activated Carbon.
4. method according to claim 1, is characterized in that: the ion exchange resin of filling in cationic exchange coloum is 732 storng-acid cation exchange resins.
5. method according to claim 4, is characterized in that: the eluent that absorption is used in operating with wash-out is ammoniacal liquor.
6. method according to claim 1, is characterized in that: during crystallization operation, the volumetric concentration of ethanol in concentrated solution is 40～80%.
7. according to the method described in claim 1 or 6, it is characterized in that: in concentration operation, it is 20～40% that elutriant is concentrated into solid content.
8. method according to claim 5, is characterized in that: the concentration of ammoniacal liquor is 0.2～0.5mol/L.
9. method according to claim 1, is characterized in that: adopt the crystallization of ethanolic soln washing Serine.
10. method according to claim 1, is characterized in that: when concentrated, adopt reverse osmosis method to concentrate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310508490.1A CN103539688B (en) | 2013-10-24 | 2013-10-24 | A kind of method of separation and Extraction Serine from Corynebacterium glutamicum fermented liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310508490.1A CN103539688B (en) | 2013-10-24 | 2013-10-24 | A kind of method of separation and Extraction Serine from Corynebacterium glutamicum fermented liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103539688A true CN103539688A (en) | 2014-01-29 |
| CN103539688B CN103539688B (en) | 2015-08-12 |
Family
ID=49963597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310508490.1A Expired - Fee Related CN103539688B (en) | 2013-10-24 | 2013-10-24 | A kind of method of separation and Extraction Serine from Corynebacterium glutamicum fermented liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103539688B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112479935A (en) * | 2020-12-03 | 2021-03-12 | 江苏优普生物化学科技股份有限公司 | Arginine purification and refining process |
| CN114085160A (en) * | 2021-10-30 | 2022-02-25 | 新泰市佳禾生物科技有限公司 | Method for separating and purifying L-serine from fermentation liquor |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108486133B (en) * | 2018-06-29 | 2021-06-01 | 江南大学 | Application method of L-serine transport protein |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1227264A (en) * | 1998-01-12 | 1999-09-01 | 味之素株式会社 | Method of producing L-serine by fermentation |
| CN1966704A (en) * | 2006-11-21 | 2007-05-23 | 江南大学 | Strain for production of L-serine and method for production of L-serine by using same |
| CN102432482A (en) * | 2010-09-29 | 2012-05-02 | 杨永前 | Production process for extracting L-serine from reeling waste silk |
-
2013
- 2013-10-24 CN CN201310508490.1A patent/CN103539688B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1227264A (en) * | 1998-01-12 | 1999-09-01 | 味之素株式会社 | Method of producing L-serine by fermentation |
| CN1966704A (en) * | 2006-11-21 | 2007-05-23 | 江南大学 | Strain for production of L-serine and method for production of L-serine by using same |
| CN102432482A (en) * | 2010-09-29 | 2012-05-02 | 杨永前 | Production process for extracting L-serine from reeling waste silk |
Non-Patent Citations (2)
| Title |
|---|
| 冯容保: "改进的离子交换法提取l一丝氨酸", 《发酵科技通讯》 * |
| 韦平和 等: "酶法生产L-丝氨酸的分离纯化", 《中国新药杂志》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112479935A (en) * | 2020-12-03 | 2021-03-12 | 江苏优普生物化学科技股份有限公司 | Arginine purification and refining process |
| CN114085160A (en) * | 2021-10-30 | 2022-02-25 | 新泰市佳禾生物科技有限公司 | Method for separating and purifying L-serine from fermentation liquor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103539688B (en) | 2015-08-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105669560A (en) | Method for separating and extracting tetrahydropyrimidine from fermentation broth | |
| CN102040531B (en) | Method for extracting L-isoleucine | |
| CN101781346B (en) | Method for separating uridylic acid from biocatalytic conversion solution | |
| CN102702274A (en) | Method for preparing high-purity soybean oligosaccharide from soybean whey wastewater | |
| CN101914054A (en) | Comprehensive method for extracting L-tryptophan from fermentation liquor | |
| CN102432479B (en) | Method for extracting L-valine from L-valine fermentation liquid | |
| CN102363594A (en) | Method for separating and purifying succinic acid from fermentation broth | |
| CN103232353A (en) | Method for separating and extracting L-valine from broth with high efficiency | |
| CN104529755A (en) | Method for separating alpha-ketoglutaric acid from conversion solution | |
| CN103709235B (en) | A kind of method reducing the extraction high-purity enramycin that solvent uses | |
| CN111518857A (en) | Enzyme method for producing glucosamine salt and purification method thereof | |
| CN115417822A (en) | Extraction and purification process of tetrahydropyrimidine | |
| CN103539688B (en) | A kind of method of separation and Extraction Serine from Corynebacterium glutamicum fermented liquid | |
| CN106544372A (en) | A kind of method that gamma aminobutyric acid is purified from zymotic fluid | |
| CN103965064A (en) | Method for extraction of L-alanine from L-alanine fermentation broth | |
| CN101586129A (en) | Method of preparing sodium gluconate from xylose crystallization mother liquor | |
| CN103772086A (en) | Pretreatment process for preparing fractions of marine microorganism small molecule metabolites | |
| CN104404094A (en) | Method for extracting taurine by use of enzymatic conversion method on the basis of clams | |
| CN104152508A (en) | Method for direct extraction of genipin from waste liquid in gardenia yellow pigment production | |
| CN104357493A (en) | Method for preparing xylitol from viscose fiber squeezed alkali liquor | |
| CN101514155A (en) | Method for separating and extracting pyruvic acid from fermentation broth by an ion exchange method | |
| CN109836468A (en) | A method of the purifying citicoline sodium from microbial fermentation solution | |
| CN102863433A (en) | Mupirocin purification method | |
| CN104892693A (en) | Method for recovering 2-one-L-gulonic acid from gulonic acid crystal mother solution | |
| CN101003795A (en) | Method for preparing peroxidase of radish |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150812 Termination date: 20211024 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |