CN103508933A - Separating and purifying method for L-tryptophan - Google Patents
Separating and purifying method for L-tryptophan Download PDFInfo
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- CN103508933A CN103508933A CN201310375366.2A CN201310375366A CN103508933A CN 103508933 A CN103508933 A CN 103508933A CN 201310375366 A CN201310375366 A CN 201310375366A CN 103508933 A CN103508933 A CN 103508933A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D209/00—Heterocyclic compounds containing five-membered rings, condensed with other rings, with one nitrogen atom as the only ring hetero atom
- C07D209/02—Heterocyclic compounds containing five-membered rings, condensed with other rings, with one nitrogen atom as the only ring hetero atom condensed with one carbocyclic ring
- C07D209/04—Indoles; Hydrogenated indoles
- C07D209/10—Indoles; Hydrogenated indoles with substituted hydrocarbon radicals attached to carbon atoms of the hetero ring
- C07D209/18—Radicals substituted by carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals
- C07D209/20—Radicals substituted by carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals substituted additionally by nitrogen atoms, e.g. tryptophane
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Abstract
The invention relates to a method for separating and purifying L-tryptophan from fermentation liquid. The method comprises the following steps: (1) adjusting the pH value of tryptophan fermentation liquid to a range of 2.5 to 4.0, filtering to remove bacteria by using a ceramic membrane with a hole diameter of 50 to 100 nm; (2) removing impurities in the ceramic membrane filtrate through a reverse-rotating continuous ion-exchanging movable bed, wherein the continuous ion-exchanging movable bed is divided into the following areas in a clock-wise direction, namely a material washing area, a material feeding area, a hydrochloric acid regenerating and acid washing area, an ammonia water degrading and ammonia water-washing area, and a product backwater area; (3) discoloring the desorbed desorption liquid by subjecting the liquid to go through a nano filtering membrane with a molecular weight of 300 to 1000 Da; (4) subjecting the discolored material liquid to go through a reverse osmosis membrane to carry out a drying and condensing treatment. The separated and purified L-tryptophan solution is crystallized after the process of pressure reduced concentration, the total yield of L-tryptophan is about 89%, and the product purity is 99% or more.
Description
Technical field
The present invention relates to a seed amino acid separating and purifying method, particularly relate to a kind of from fermented liquid the method for separating-purifying L-Trp.
Background technology
L-Trp is the die aromatischen Aminosaeuren that contains indyl, humans and animals grow and metabolic aspect play an important role, be one of eight seed amino acids of needed by human, its crystal white or slightly yellow.Tryptophane can synthesize multiple hormone and physiologically active substance in human body, and the nervous physiology that also participates in balance the body is movable, and relatively lacks in vegetable-protein, and therefore, tryptophane has just been widely used in the industries such as medicine, food and feed.L-Trp production method has chemical synthesis, proteolysis method, microbe transformation method, enzyme process and direct fermentation etc., and wherein direct fermentation is the main stream approach that current tryptophane is produced.
The fermented liquid that contains tryptophane that direct fermentation produces also needs further separation and purification to obtain highly purified tryptophane crystallization.From fermented liquid, the usual method of separating-purifying tryptophane is: fermented liquid is removed tropina through membrane filtration or flocculation sediment, feed liquid is passed through from handing over ADSORPTION IN A FIXED BED, resolving tryptophane, reach the object of removal of impurities, desorbed solution improves product printing opacity by activated carbon decolorizing, finally concentrate feed liquid, crystallizing and drying is made tryptophane finished product.In aforesaid method, the use of flocculation agent, has increased production cost, contaminate environment, and the feed clarification degree obtaining is very poor, affects the purifying products process in downstream; And from the use of handing over fixed bed, also can cause the waste of acid, alkali and water; The use meeting of gac is to environment, and the difficult thoroughly removal of gac, its residual quality that affects the finished product.
2012.02.08 the Chinese invention patent that disclosed application number is CN201110227776.3 discloses a kind of method that ion exchange resin directly extracts tryptophane in fermented liquid, by the fermented liquid that contains tryptophane through deactivation, after the pre-treatment that acid adjustment to pH value is 3～4, by the amount of corresponding every 20 grams of the tryptophane that contains in fermented liquid, add 0.8～1.5 fermented liquid of going up after being diluted after clear liquid after the useless bacterium slag of batch separation mixes, then enter the exchange adsorption that circulates in ion exchange resin column, after washing down, ion exchange resin resolves through ammoniacal liquor, obtain the desorbed solution of enrichment tryptophane, desorbed solution obtains finished product tryptophane through further purification process.The ion-exchange unit that the method adopts belongs to from handing over fixed bed, can not realize the continuous separation and purification of tryptophane fermented liquid, and cause the waste of acid, alkali and water.
2009.07.29 the Chinese invention patent that disclosed application number is CN200910024690.3 discloses a kind of method from separation of fermentative broth tryptophane, by micro-pore-film filtration, remove thalline, membrane sepn except the larger molecular organics matter such as colloid albumen and pigment, electrodialysis are except inorganic salt and reverse osmosis concentration, finally obtain tryptophane crystal.The method has adopted membrane technique to carry out separation and purification tryptophane, but adopts multistage film to process the overall yield that has reduced tryptophane.
2009.03.04 the Chinese invention patent that disclosed application number is CN200710059347.3 discloses a kind of ion exchange extraction technique of utilizing direct fermentation to produce L-Trp, adopt stainless steel tubular type film separating system filtering fermentating liquid, application ion exchange method is extracted the concentrated and crystallization of L-Trp and product, and extracting total recovery is 63.4%.The ion-exchange unit that the method adopts belongs to from handing over fixed bed, can not realize the continuous separation and purification of tryptophane fermented liquid, and cause the waste of acid, alkali and water, and overall yield is on the low side.
2010.05.19 the Chinese invention patent that disclosed application number is CN200910211061.1 discloses a kind of extracting method of L-Trp, comprises the steps: 1) the pH value of L-Trp fermented liquid is adjusted to 1.5-4.5, then carry out membrane filtration; 2) membrane filtration fluid is carried out separation with the simulation moving-bed of Zeo-karb is housed from friendship system; 3) elutriant adjust pH is to 6-7; 4) elutriant after acid adjustment adds heat decoloring; Destainer obtains L-Trp through aftertreatment.The simulation moving-bed waste that can cause acid, alkali and water from friendship system that the method adopts, and desorbed solution decolours by gac, and gac cannot thoroughly be removed, and has affected the quality of product.
Summary of the invention
The invention provides a kind of from fermented liquid the method for separating-purifying L-Trp, to solve the above-mentioned problems in the prior art.
The present invention adopts following technical scheme:
A separating and purifying method for L-Trp, comprises the steps:
1) by tryptophane fermented liquid with acid for adjusting pH to 2.5-4.0, adopt aperture 50-100nm ceramic membrane filter degerming;
2) ceramic membrane filtrate is by the continuous ionic exchange moving-bed removal of impurities rotating counterclockwise, and continuous ionic exchange moving-bed is divided into washing material district, intake zone, regeneration of hydrochloric acid and washing acid district in the direction of the clock, ammoniacal liquor is resolved and washing ammonia district and pool, product top;
3) from continuous ionic exchange moving-bed, resolve the desorbed solution getting off and pass through the nanofiltration membrane decolouring that retaining molecular weight is 300-1000Da;
4) feed liquid after decolouring is dewatered concentrated by reverse osmosis membrane.
Further, in described step 1), regulating the acid used of pH value is sulfuric acid, and filtration temperature is 0-80 ℃, and entrance pressure 3-4bar goes out to press 1-2bar.
Further, when in described step 1), fermented liquid concentrates 3-6 times, Jia Shuiding washes, and the 0.6-0.8 that amount of water is fermentating liquid volume doubly.
Further, described step 2) in, continuous ionic exchange moving-bed resin used is strongly-acid or acidulous cation resin, for example D001,732 or LH-2; Parsing ammonia concn is 2-3%, and concentration of hydrochloric acid is 4-6%, and continuous ionic exchange moving-bed operating temperature is 40-60 ℃, 10 hours rotating disk cycles.
Further, described step 2) in, continuous ionic exchange moving-bed adopts the system of 20 posts, is divided into successively:
1) washing material district: 1#, 2#, flow velocity 1.35L/H; Material is washed in two series connection, and the feed liquid washing out enters the second stage of intake zone;
2) intake zone: 3-10#, flow velocity 6L/H; Divide three grades, first step 3#, 4# are in parallel, and second stage 5-7# is in parallel, and third stage 8-10# is in parallel;
3) regeneration of hydrochloric acid and washing sour district: 11-14#, flow velocity is respectively 0.9L/H and 1.35L/H; 13# enters acid regeneration, and acid is washed in 11# water inlet, and 12# washing after sour water and 13# acid out mix out continues to enter 14# regeneration;
4) ammoniacal liquor is resolved and washing ammonia district: 15-19#, and flow velocity is respectively 2.7L/H and 2.9L/H; 17# enters ammoniacal liquor and resolves, and ammonia is washed in 15#, 16# series connection water inlet, enters 18#, 19# and continue to resolve after the ammoniacal liquor that 16# comes out and the ammoniacal liquor of 17# mix;
5) product top pool: 20#, flow velocity 0.8L/H.
Further, working pressure 5-10bar in described step 3), filtration temperature 20-45 ℃; When desorbed solution concentrates 8-10 times, Jia Shuiding washes, and amount of water is 0.3-0.4 times of desorbed solution volume.
Further, in described step 4), the working pressure of reverse osmosis membrane is 25-33bar, and working temperature is 20-45 ℃.
The invention has the beneficial effects as follows:
Present method combines connection ion-exchange moving-bed system with membrane technique, adopt membrane technique that tryptophane fermented liquid is filtered, decoloured and concentrates, adopt connection ion-exchange moving-bed to carry out purifying to tryptophane fermented liquid, when guaranteeing overall yield and product purity, reduced the consumption of acid, alkali, water and resin, avoid the impact of activated carbon decolorizing on quality product, reduced production cost and the wasting of resources.
Accompanying drawing explanation
Fig. 1 is continuous ionic exchange moving-bed workflow schematic diagram of the present invention
Embodiment
Below in conjunction with specific embodiment, further describe technical scheme of the present invention, but content of the present invention is not limited to this.
Embodiment 1
1) ceramic membrane filter fermented liquid: 200L tryptophane fermented liquid, product concentration is 33g/L, pass through 40%(w/w) sulphur acid for adjusting pH to 3.0, with the ceramic membrane 40-60 ℃ filtration sterilization of 50nm, when concentrated solution volume is 50L, starts to add water top and wash product, add altogether water 140L, the average flux of film is 75L/ (㎡ .H), product mean concns is 22.1g/L, yield is 98.3%;
2) Continuous Moving Bed removal of impurities: by Continuous Moving Bed removal of impurities, Continuous Moving Bed adopts the system that spool is 4mm by ceramic membrane filtrate, filling 13.5L resin, rotating disk cycle 10H.Feed liquid enters system by 3#, 4# post, charging flow velocity 6.1L/H, and after one-level absorption, feed liquid series connection enters that 5-7# carries out secondary absorption and 8-10# carries out three grades of absorption; After absorption finishes, 1#, 2# post washing series-connection, washing flow velocity is 1.35L/H, washing feed liquid enters the second stage absorption of adsorption zone; 17# post passes into 2.5% ammoniacal liquor with the flow velocity of 2.9L/H and resolves, and 15# post is with the flow velocity washing ammonia of 2.7L/H, the ammonia of washing out with 16# and 17# resolve the ammino that flows out and after enter 18#, 19# and continue parsing; Desorbed solution pumps into 20# capital and washes the water in pillar, flow velocity 0.8L/H; After parsing finishes, 13# passes into 5% resolving hydrochloric acid, flow velocity 0.9L/H, and 11# passes into and washes sour water, flow velocity 1.35L/H, the acid merging that the acid that 12# is washed out and 13# flow out enters the further regenerating resin of 14#.The product concentration obtaining is 27.7g/L, and yield is 98.5%.
3) nanofiltration membrane decolouring: get Continuous Moving Bed desorbed solution 200L, adopt the rolled film that molecular weight cut-off is 600Da to decolour, enter film pressure 8bar, go out film pressure 6bar, service temperature 25-35 ℃, after concentrated 10 times, add 60L water top to wash product, film average flux is 28L/(㎡ .H), the dialyzate printing opacity obtaining is 73%, product concentration 22.4g/L, yield is 97.1%.
4) reverse osmosis concentration: adopt the concentrated nanofiltration membrane dialyzate of reverse osmosis membrane, service temperature is 30-40 ℃, and entering film pressure is 33bar, going out film pressure is 31bar, and concentrated 2.1 times, film average flux is 13L/(㎡ .H), the concentrated solution product concentration obtaining is 46.7g/L, yield 99.2%.
5) subsequent technique: the concentrated feed liquid obtaining of nanofiltration membrane is carried out to reduction vaporization and concentrate and crystallization, in the product obtaining, L-Trp content is 99.5%, overall yield 89.1%.
Embodiment 2
1) ceramic membrane filter fermented liquid: 185L tryptophane fermented liquid, concentration is 30g/L, pass through 40%(w/w) sulphur acid for adjusting pH to 4.0, with 40 ℃ of-60 ℃ of filtration sterilizations of ceramic membrane of 50nm, when concentrated solution volume is 37L, starts to add water top and wash product, add altogether water 115L, the average flux of film is 83L/ (㎡ .H), product mean concns is 20.8g/L, yield is 98.6%;
2) Continuous Moving Bed removal of impurities: by Continuous Moving Bed removal of impurities, Continuous Moving Bed adopts the system that spool is 4mm by ceramic membrane filtrate, filling 13.5L resin, rotating disk cycle 10H.Feed liquid enters system by 3#, 4# post, charging flow velocity 6.5L/H, and after one-level absorption, feed liquid series connection enters that 5-7# carries out secondary absorption and 8-10# carries out three grades of absorption; After absorption finishes, 1#, 2# post washing series-connection, washing flow velocity is 1.35L/H, washing feed liquid enters the second stage absorption of adsorption zone; 17# post passes into 2.5% ammoniacal liquor with the flow velocity of 2.9L/H and resolves, and 15# post is with the flow velocity washing ammonia of 2.7L/H, the ammonia of washing out with 16# and 17# resolve the ammino that flows out and after enter 18#, 19# and continue parsing; Desorbed solution pumps into 20# capital and washes the water in pillar, flow velocity 0.8L/H; After parsing finishes, 13# passes into 5% resolving hydrochloric acid, flow velocity 0.9L/H, and 11# passes into and washes sour water, flow velocity 1.35L/H, the acid merging that the acid that 12# is washed out and 13# flow out enters the further regenerating resin of 14#.The product concentration obtaining is 27.5g/L, and yield is 98.1%.
3) nanofiltration membrane decolouring: get Continuous Moving Bed desorbed solution 180L, adopt the rolled film that molecular weight cut-off is 400Da to decolour, enter film pressure 7bar, go out film pressure 5bar, service temperature 35-45 ℃, after concentrated 10 times, add 63L water top to wash product, film average flux is 33L/(㎡ .H), the dialyzate printing opacity obtaining is 75%, product concentration 22.5g/L, yield is 97.5%.
4) reverse osmosis concentration: adopt the concentrated nanofiltration membrane dialyzate of reverse osmosis membrane, service temperature is 30-40 ℃, and entering film pressure is 30bar, going out film pressure is 28bar, has concentrated 2.0 times, and film average flux is 15L/(㎡ .H), the concentrated solution product concentration obtaining is 44.66g/L, yield 99.1%.
5) subsequent technique: the concentrated feed liquid obtaining of nanofiltration membrane is carried out to reduction vaporization and concentrate and crystallization, in the product obtaining, L-Trp content is 99.5%, overall yield 88.7%.
Above are only a specific embodiment of the present invention, but design concept of the present invention is not limited to this, those of ordinary skill in the art is to be understood that, technical scheme to invention is modified or is equal to replacement, but the spirit and scope that do not depart from technical solution of the present invention, it all should be encompassed in claim scope of the present invention.
Claims (9)
1. a separating and purifying method for L-Trp, is characterized in that, comprises the steps:
1) by tryptophane fermented liquid with acid for adjusting pH to 2.5-4.0, adopt aperture 50-100nm ceramic membrane filter degerming;
2) ceramic membrane filtrate is by the continuous ionic exchange moving-bed removal of impurities rotating counterclockwise, and continuous ionic exchange moving-bed is divided into washing material district, intake zone, regeneration of hydrochloric acid and washing acid district in the direction of the clock, ammoniacal liquor is resolved and washing ammonia district and pool, product top;
3) from continuous ionic exchange moving-bed, resolve the desorbed solution getting off and pass through the nanofiltration membrane decolouring that retaining molecular weight is 300-1000Da;
4) feed liquid after decolouring is dewatered concentrated by reverse osmosis membrane.
2. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: in described step 1), regulating the acid used of pH value is sulfuric acid.
3. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: in described step 1), filtration temperature is 0-80 ℃, and entrance pressure 3-4bar goes out to press 1-2bar.
4. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: when in described step 1), fermented liquid concentrates 3-6 times, Jia Shuiding washes, and the 0.6-0.8 that amount of water is fermentating liquid volume doubly.
5. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: described step 2), continuous ionic exchange moving-bed resin used is strongly-acid or acidulous cation resin.
6. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: described step 2), resolving ammonia concn is 2-3%, and concentration of hydrochloric acid is 4-6%, and continuous ionic exchange moving-bed operating temperature is 40-60 ℃, 10 hours rotating disk cycles.
7. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: described step 2), continuous ionic exchange moving-bed adopts the system of 20 posts, is divided into successively:
1) washing material district: 1#, 2#, flow velocity 1.35L/H; Material is washed in two series connection, and the feed liquid washing out enters the second stage of intake zone;
2) intake zone: 3-10#, flow velocity 6L/H; Divide three grades, first step 3#, 4# are in parallel, and second stage 5-7# is in parallel, and third stage 8-10# is in parallel;
3) regeneration of hydrochloric acid and washing sour district: 11-14#, flow velocity is respectively 0.9L/H and 1.35L/H; 13# enters acid regeneration, and acid is washed in 11# water inlet, and 12# washing after sour water and 13# acid out mix out continues to enter 14# regeneration;
4) ammoniacal liquor is resolved and washing ammonia district: 15-19#, and flow velocity is respectively 2.7L/H and 2.9L/H; 17# enters ammoniacal liquor and resolves, and ammonia is washed in 15#, 16# series connection water inlet, enters 18#, 19# and continue to resolve after the ammoniacal liquor that 16# comes out and the ammoniacal liquor of 17# mix;
5) product top pool: 20#, flow velocity 0.8L/H.
8. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: working pressure 5-10bar in described step 3), filtration temperature 20-45 ℃; When desorbed solution concentrates 8-10 times, Jia Shuiding washes, and amount of water is 0.3-0.4 times of desorbed solution volume.
9. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: in described step 4), the working pressure of reverse osmosis membrane is 25-33bar, and working temperature is 20-45 ℃.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104592047A (en) * | 2014-12-24 | 2015-05-06 | 三达膜科技（厦门）有限公司 | Separation and purification method of valine |
| CN104817449A (en) * | 2014-12-31 | 2015-08-05 | 三达膜科技（厦门）有限公司 | Method for separating and refining succinic acid |
| CN104829519A (en) * | 2015-05-15 | 2015-08-12 | 南通荣泰生物科技有限公司 | Purification process of L-tryptophan |
| CN106631855A (en) * | 2016-12-09 | 2017-05-10 | 三达膜科技（厦门）有限公司 | Method or recycling threonine from threonine crystallization mother solution |
| CN112979482A (en) * | 2020-12-25 | 2021-06-18 | 安徽华恒生物科技股份有限公司 | High-purity L-valine and preparation method and application thereof |
| WO2023066140A1 (en) * | 2021-10-19 | 2023-04-27 | 浙江华康药业股份有限公司 | Continuous membrane filtration system and filtration method for erythritol fermentation liquor |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB842839A (en) * | 1957-12-20 | 1960-07-27 | Du Pont | Resolution of dl-ttryptophan |
| JPH03200765A (en) * | 1989-12-28 | 1991-09-02 | Res Assoc Util Of Light Oil | Method for purifying l-tryptophan |
| CN101492408A (en) * | 2009-02-26 | 2009-07-29 | 江苏赛奥生化有限公司 | Method for separating tryptophane from fermentation liquor |
| CN101565395A (en) * | 2009-05-25 | 2009-10-28 | 河南孟成生物药业股份有限公司 | Technique for extracting L-tryptophan in fermentation liquor |
| CN101709048A (en) * | 2009-11-11 | 2010-05-19 | 安徽丰原发酵技术工程研究有限公司 | Method for extracting L-tryptophan |
| CN103059105A (en) * | 2012-12-28 | 2013-04-24 | 三达膜科技（厦门）有限公司 | Method for extraction of colistin sulphate |
-
2013
- 2013-08-26 CN CN201310375366.2A patent/CN103508933B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB842839A (en) * | 1957-12-20 | 1960-07-27 | Du Pont | Resolution of dl-ttryptophan |
| JPH03200765A (en) * | 1989-12-28 | 1991-09-02 | Res Assoc Util Of Light Oil | Method for purifying l-tryptophan |
| CN101492408A (en) * | 2009-02-26 | 2009-07-29 | 江苏赛奥生化有限公司 | Method for separating tryptophane from fermentation liquor |
| CN101565395A (en) * | 2009-05-25 | 2009-10-28 | 河南孟成生物药业股份有限公司 | Technique for extracting L-tryptophan in fermentation liquor |
| CN101709048A (en) * | 2009-11-11 | 2010-05-19 | 安徽丰原发酵技术工程研究有限公司 | Method for extracting L-tryptophan |
| CN103059105A (en) * | 2012-12-28 | 2013-04-24 | 三达膜科技（厦门）有限公司 | Method for extraction of colistin sulphate |
Non-Patent Citations (4)
| Title |
|---|
| 于力涛: "连续离子交换在L-乳酸分离中的应用", 《合肥工业大学硕士学位论文》 * |
| 徐俭,等: "陶瓷膜在聚合级L-乳酸纯化工艺中的应用", 《安徽农业科学》 * |
| 韦平和,等: "酶法生产L-丝氨酸的分离纯化", 《中国新药杂志》 * |
| 黄彬生: "《分析化学》", 31 May 2008, 科学出版社 * |
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| CN104592047A (en) * | 2014-12-24 | 2015-05-06 | 三达膜科技（厦门）有限公司 | Separation and purification method of valine |
| CN104817449A (en) * | 2014-12-31 | 2015-08-05 | 三达膜科技（厦门）有限公司 | Method for separating and refining succinic acid |
| CN104829519A (en) * | 2015-05-15 | 2015-08-12 | 南通荣泰生物科技有限公司 | Purification process of L-tryptophan |
| CN106631855A (en) * | 2016-12-09 | 2017-05-10 | 三达膜科技（厦门）有限公司 | Method or recycling threonine from threonine crystallization mother solution |
| CN106631855B (en) * | 2016-12-09 | 2018-10-09 | 三达膜科技（厦门）有限公司 | A method of recycling threonine from threonine crystallization mother liquid |
| CN112979482A (en) * | 2020-12-25 | 2021-06-18 | 安徽华恒生物科技股份有限公司 | High-purity L-valine and preparation method and application thereof |
| CN112979482B (en) * | 2020-12-25 | 2024-02-02 | 安徽华恒生物科技股份有限公司 | High-purity L-valine as well as preparation method and application thereof |
| WO2023066140A1 (en) * | 2021-10-19 | 2023-04-27 | 浙江华康药业股份有限公司 | Continuous membrane filtration system and filtration method for erythritol fermentation liquor |
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