CN105348122A - Method for purifying L-alanine final mother liquor - Google Patents
Method for purifying L-alanine final mother liquor Download PDFInfo
- Publication number
- CN105348122A CN105348122A CN201510734714.XA CN201510734714A CN105348122A CN 105348122 A CN105348122 A CN 105348122A CN 201510734714 A CN201510734714 A CN 201510734714A CN 105348122 A CN105348122 A CN 105348122A
- Authority
- CN
- China
- Prior art keywords
- alanine
- liquid
- mother liquor
- permeate
- product
- 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
Classifications
-
- 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
Abstract
The invention belongs to the technical field of microbe broth aftertreatment and relates to a method for purifying an L-alanine final mother liquor. The method comprises 1, adjusting pH of a mother liquor to 6-8, and carrying out filtration to remove solid impurities and to obtain a crude filtrate, 2, carrying out microfiltration treatment on the crude filtrate to obtain a transparent filtrate, 3, carrying out chromatography on the transparent filtrate by calcium ion-exchange resin to obtain a product material liquid, 4, carrying out condensation and crystallization on the product material liquid, carrying out centrifugation and carrying out drying to obtain an L-alanine product. The method can remove a lot of impurities of the mother liquor, has an L-alanine yield of 90%, and realizes product purity of 95%. The method can improve an L-alanine fermentation production technology yield. The discharged waste water subjected to purifying treatment has low organic matter content and small pollution on the environment.
Description
Technical field
The invention belongs to fermentation technical field, particularly relate to a kind of purification process of ALANINE extreme trace mother liquor.
Background technology
ALANINE (L-Alanine, hereinafter referred to as L-Ala), has another name called L-α-aminopropionic acid, is a kind of non-essential amino acid.ALANINE is a kind of non-essential amino acid, but the amino acid that in blood of human body, content is the highest.It can be transaminase and provides amino group donor, often adds in transfusion clinically; In the food industry, ALANINE is as sweeting agent and the positive more and more welcomed by the people of tasty agents and attention; In pharmaceutical industries, ALANINE is the main raw material producing vitamin B6 and L-aminopropanol; In addition, in macromolecular material, in discovered in recent years poly(lactic acid), add the performance that ALANINE effectively can improve poly(lactic acid).
Along with the continuous research and development to ALANINE, it constantly expands in the application of the industries such as medicine, food, and has growing trend.But more late to the exploitation of ALANINE, the beginning of the eighties just produces in Japanese industryization.There is small serial production in China at the end of the eighties, and suitability for industrialized production is just at the early-stage.The production method of L-Ala has the extraction of proteolysis extraction method, fermentation method, enzyme transforming process is produced.Because the cost of fermentative Production ALANINE is lower, and meet American-European countries's green, healthy consumption concept, there are wide market outlook.After fermentative Production ALANINE terminates, the how subcrystalline mode of general employing is purified ALANINE, general also containing part ALANINE in crystal waste, in addition, organism (being mainly ALANINE, amino acid, polypeptide etc.) in crystal waste is more, crystal waste directly discharges the ALANINE that not only can lose part and not reclaim, simultaneously can to environment.Therefore, develop a treatment process to ALANINE extreme trace mother liquor, to improve the extract yield of ALANINE, reduce environmental protection pressure, there is very large realistic meaning.
Summary of the invention
The object of this invention is to provide a kind of purification process of ALANINE extreme trace mother liquor, comprise the steps:
(1) get ALANINE extreme trace mother liquor, under 50-70 DEG C of condition, adjust ph is to 6-8, separates out solid impurity, and filtering described solid impurity obtains ALANINE coarse filtration liquid excessively;
(2) described ALANINE coarse filtration liquid is carried out micro-filtration process, obtain ALANINE permeate and concentrating spent liquor;
(3) described ALANINE permeate is passed into chromatographic system, carry out chromatography, collect product feed liquid;
(4) described product feed liquid is concentrated, crystallization, solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, described ALANINE crystal is dried to obtain ALANINE finished product.
The present invention adopts chromatographic separation technology to reclaim ALANINE from ALANINE extreme trace mother liquor, improves the overall extract yield of ALANINE, reduces the production cost of ALANINE.In addition, because the ALANINE in ALANINE extreme trace mother liquor is separated by chromatographic system, purifies and reclaim, so in the waste liquid of discharging from chromatographic system, organism (is mainly ALANINE, and the impurity amino acid of some trace, polypeptide class) content reduces greatly, significantly reduces environmental protection pressure.
Preferably, the purification process that the present invention relates to, is particularly useful for processing the extreme trace mother liquor that ALANINE content is 10%-20%; Preferred further, be applicable to process the extreme trace mother liquor that ALANINE content is 14%-16%; Preferred further again, being applicable to process ALANINE content is 14%-16%, and transmittance is 0%, and dry matter content is the extreme trace mother liquor of 40-45%.
Preferably, micro-filtration process adopts rete material to be TiO
2/ ZrO
2ceramic membrane; More preferably, employing aperture is 40-60nm, the multi-channel type ceramic membrane element of preferred 50nm.
In order to better realize being separated, in microfiltration process, controlled filter temperature 50-60 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa; More preferably, controlled filter temperature 55 DEG C, feed pressure 0.23MPa, discharge pressure 0.2MPa.
In order to improve the yield of ALANINE, in microfiltration process, when the volume of described concentrating spent liquor is the 15%-20% of the thick filtrate volume of described ALANINE, add the deionized water being equivalent to described ALANINE thick filtrate volume 10-15% to dialyse described concentrating spent liquor, obtain dialyzate, described dialyzate and described permeate are merged.
In order to reclaim the L-Phe in mother liquor to greatest extent, chromatography adopts calcium ion type exchange resin to be stationary phase, and water is moving phase.Calcium ion type resin has the feature strong with L-Phe binding ability, when processing, and not only its good separating effect, and the consumption of eluting water can be saved.Preferably, grain diameter is adopted to be the resin particle of 0.2-0.3mm.Preferred further, adopt the DTF-01 calcium ion type resin of the particle diameter 0.2-0.3mm of Jiangsu Su Qing engineering of water treatment group company.
In order to improve the separating effect of chromatography, control chromatogram column temperature 55-65 DEG C, feed rate 0.2-0.3BV/h, eluting water flow 1.0-1.5BV/h, load 0.3-0.7BV/h, go out wastewater flow rate 1.15-1.35BV/h; More preferably, chromatogram column temperature 60 DEG C, feed rate 0.25BV/h, eluting water flow 1.5BV/h, load 0.5BV/h, go out wastewater flow rate 1.25BV/h.
In the present invention, the scale of chromatographic separation is not particularly limited, and the scale of the pending feed liquid of Main Basis determines, such as treatment capacity hour, can adopt a root chromatogram column to be separated; During the fairly large process of industrialization, the mode that many root chromatogram columns can be adopted to connect is separated, such as 9,12,24 etc., when many root chromatogram column series connection are separated, the conventional technique means in this area is adopted to determine feed entrance, eluting water entrance, product extraction mouth and go out waste water mouth.
In order to improve crystallization yield, in step (4), product feed liquid being concentrated into solid content is that 55%-65% stops, then 5-15 DEG C of crystallization is cooled to, after crystallization terminates, carry out solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, ALANINE finished product is dried and obtained to described ALANINE crystal.
Preferred further, product feed liquid being concentrated into solid content is 60% stopping, being then cooled to 10 DEG C of crystallizations.
Further preferred, adopt centrifugal method to carry out solid-liquid separation, and add and be equivalent to ALANINE crystalline mother solution volume 5%-10%, preferably the deionized water of 7% washes crystalline substance.
Further, at 55-65 DEG C, preferably dry crystal under 60 DEG C of conditions.
The scheme of optimum of the present invention is: a kind of purification process of ALANINE extreme trace mother liquor, comprises the steps:
(1) get ALANINE extreme trace mother liquor, under 50-70 DEG C of condition, adjust ph is to 6-8, separates out solid impurity, and filtering described solid impurity obtains ALANINE coarse filtration liquid excessively;
(2) described ALANINE coarse filtration liquid is crossed the ceramic membrane that aperture is 40-60nm, controlled filter temperature 50-60 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa, filter after terminating and obtain ALANINE permeate and concentrating spent liquor; Further, when the volume of described concentrated solution is the 15%-20% of the thick filtrate volume of described ALANINE, the deionized water adding the 10-15% being equivalent to the thick filtrate volume of described ALANINE is dialysed described concentrating spent liquor, obtains dialyzate, described dialyzate and described permeate is merged;
(3) described ALANINE permeate is passed into chromatographic column, the stationary phase of described chromatographic column is calcium ion type exchange resin, moving phase is water, control the temperature 55-65 DEG C of chromatographic column, feed rate 0.2-0.3BV/h, eluting water flow 1.0-1.5BV/h, load 0.3-0.7BV/h, go out wastewater flow rate 1.15-1.35BV/h;
(4) described product feed liquid being concentrated into solid content is 55%-65%, crystallization under 5-15 DEG C of condition, after crystallization, carries out solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, described ALANINE crystal is dried under 55-65 DEG C of condition and obtains ALANINE finished product.
Embodiment
Following examples for illustration of the present invention, but are not used for limiting the scope of the invention.
The ALANINE extreme trace mother liquor related in following examples obtains by the following method: adopt strain Escherichia coli, be inoculated into LB substratum, at 32 ± 2 DEG C, fermentation culture is carried out under pH=6.5 condition, after cultivation terminates, fermented liquid is heated to 60 DEG C of pre-treatment, pretreated fermented liquid obtains high purity ALANINE nanofiltration liquid through ultrafiltration, nanofiltration, nanofiltration liquid obtains ALANINE finished product and ALANINE one mother liquor through condensing crystal, one mother liquor again condensing crystal obtains a female crystallographic and two mother liquors, by that analogy, repeatedly crystallization is carried out.
Chromatographic system in following examples is composed in series by 9 root chromatogram columns, and the weighting material in every root chromatogram column is the DTF-01 calcium ion type resin of Jiangsu Su Qing engineering of water treatment group company, and the moving phase adopted during chromatographic separation is water.
The ceramic membrane related in following examples is aperture 50nm, and rete material is TiO
2/ ZrO
2multichannel ceramic membrane element.
Embodiment 1
A purification process for ALANINE extreme trace mother liquor, comprises the steps:
(1) 20kgL-alanine content 14.2% is got, dry matter content 41.5%, the ALANINE extreme trace mother liquor of transmittance 0% is placed in water-bath, insulation is stirred under 60 DEG C of conditions, Feeding ammonia water regulates pH to be 6.0, and separate out solid impurity in feed liquid, solids removed by filtration impurity obtains 17.5kgL-L-Ala coarse filtration liquid, wherein, ALANINE content 16.07%; Dry matter content 35.71%; Filter yield 99.1%;
(2) the ALANINE coarse filtration liquid of 17.5kg is crossed ceramic membrane, controlled filter temperature 55 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa, filter after terminating and obtain ALANINE permeate and concentrating spent liquor; In microfiltration process, when the volume of concentrated solution is 15% of the thick filtrate volume of described ALANINE, adds the deionized water dialysis concentrating spent liquor being equivalent to the thick filtrate volume 10% of ALANINE, obtain dialyzate, described dialyzate and described permeate are merged; Filter and terminate, obtain 19.3kgL-L-Ala permeate, wherein ALANINE content 14.43%, dry matter content 29.94%, filter yield 99%;
(3) 19.3kgL-L-Ala permeate is passed into chromatographic system, the temperature controlling every root chromatogram column is 60 DEG C, feed rate 0.25BV/h, eluting water flow 1.5BV/h, load 0.5BV/h, go out wastewater flow rate 1.25BV/h, obtain product feed liquid 38.6kg, wherein ALANINE content 6.62%, dry matter content 6.96%, yield 91.73%;
(4) 38.6kg product feed liquid being concentrated into product feed liquid dry matter content is 60%, then 10 DEG C of crystallizations are cooled to, after crystallization terminates, centrifugally carry out solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, further, add deionized water and wash crystalline substance, the amount added is 7% of ALANINE crystalline mother solution volume;
(5) described ALANINE crystal is dried to obtain ALANINE finished product under 60 DEG C of conditions, final product quality 2.43kg, yield 95%, final product quality meets Chinese Pharmacopoeia standard, and described ALANINE crystalline mother solution is mixed into the ALANINE permeate recycled in step (2).
Embodiment 2
A purification process for ALANINE extreme trace mother liquor, comprises the steps:
(1) 20kgL-alanine content 14.9% is got, purity 35.11%, dry matter content 42.44%, the ALANINE extreme trace mother liquor of transmittance 0% is placed in water-bath, under 60 DEG C of conditions, stir insulation, and Feeding ammonia water regulates pH to be 7.0, solid impurity is separated out in feed liquid, solids removed by filtration impurity obtains 17.9kgL-L-Ala coarse filtration liquid, wherein, and ALANINE content 16.48%; Dry matter content 36.22%; Filter yield 99%;
(2) the ALANINE coarse filtration liquid of 17.5kg is crossed the ceramic membrane that aperture is 50nm, in microfiltration process, controlled filter temperature 55 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa, filter after terminating and obtain ALANINE permeate and concentrated solution; Further, in microfiltration process, when the volume of concentrated solution is 20% of the thick filtrate volume of described ALANINE, add the deionized water dialysis concentrating spent liquor being equivalent to the thick filtrate volume 15% of ALANINE, obtain dialyzate, described dialyzate and described permeate are merged; Filter and terminate, obtain 19.7kgL-L-Ala permeate, wherein ALANINE content 14.82%, dry matter content 30.56%, filter yield 99%;
(3) 19.7kgL-L-Ala permeate is passed into chromatographic system, the temperature controlling every root chromatogram column is 60 DEG C, feed rate 0.25BV/h, eluting water flow 1.5BV/h, load 0.5BV/h, go out wastewater flow rate 1.25BV/h, obtain product feed liquid 39.4kg, wherein ALANINE content 6.74%, dry matter content 7.07%, yield 91%;
(4) 38.6kg product feed liquid being concentrated into product feed liquid dry matter content is 60%, then 10 DEG C of crystallizations are cooled to, after crystallization terminates, centrifugally carry out solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, further, add deionized water and wash crystalline substance time centrifugal, the amount added is 7% of ALANINE crystalline mother solution volume;
(5) described ALANINE crystal is dried to obtain ALANINE finished product under 60 DEG C of conditions, final product quality 2.5kg, yield 96.2%, final product quality meets Chinese Pharmacopoeia standard, and described ALANINE crystalline mother solution is mixed into the ALANINE permeate recycled in step (2).
Embodiment 3
A purification process for ALANINE extreme trace mother liquor, comprises the steps:
(1) 20kgL-alanine content 13.8% is got, dry matter content 40.84%, the ALANINE extreme trace mother liquor of transmittance 0% is placed in water-bath, insulation is stirred under 60 DEG C of conditions, Feeding ammonia water regulates pH to be 7.5, and separate out solid impurity in feed liquid, solids removed by filtration impurity obtains 17.2kgL-L-Ala coarse filtration liquid, wherein, ALANINE content 15.89%; Dry matter content 35.62%; Filter yield 99%;
(2) the ALANINE coarse filtration liquid of 17.2kg is crossed the ceramic membrane that aperture is 50nm, in microfiltration process, controlled filter temperature 55 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa, filter after terminating and obtain ALANINE permeate and concentrated solution; Further, in microfiltration process, when the volume of concentrated solution is 18% of the thick filtrate volume of described ALANINE, add the deionized water dialysis concentrating spent liquor being equivalent to the thick filtrate volume 12% of ALANINE, obtain dialyzate, described dialyzate and described permeate are merged; Filter and terminate, obtain 18.9kgL-L-Ala permeate, wherein ALANINE content 13.87%, dry matter content 29.32%, filter yield 99%;
(3) 19.7kgL-L-Ala permeate is passed into chromatographic system, the temperature controlling every root chromatogram column is 60 DEG C, feed rate 0.25BV/h, eluting water flow 1.5BV/h, load 0.5BV/h, go out wastewater flow rate 1.25BV/h, obtain product feed liquid 37.8kg, wherein ALANINE content 6.72%, dry matter content 6.6%, ALANINE purity 95%; Yield, 90.4%;
(4) 37.8kg product feed liquid being concentrated into product feed liquid dry matter content is 60%, then 10 DEG C of crystallizations are cooled to, after crystallization terminates, centrifugally carry out solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, further, add deionized water and wash crystalline substance time centrifugal, the amount added is 7% of ALANINE crystalline mother solution volume;
(5) described ALANINE crystal is dried to obtain ALANINE finished product under 60 DEG C of conditions, final product quality 2.45kg, yield 96.5%, final product quality meets Chinese Pharmacopoeia standard, and described ALANINE crystalline mother solution is mixed into the ALANINE permeate recycled in step (2).
Although above with general explanation, embodiment and test, the present invention is described in detail, and on basis of the present invention, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, all belong to the scope of protection of present invention.
Claims (10)
1. a purification process for ALANINE extreme trace mother liquor, is characterized in that, comprises the steps:
(1) get ALANINE extreme trace mother liquor, under 50-70 DEG C of condition, adjust ph is to 6-8, separates out solid impurity, and filtering described solid impurity obtains ALANINE coarse filtration liquid excessively;
(2) described ALANINE coarse filtration liquid is carried out micro-filtration process, obtain ALANINE permeate and concentrating spent liquor;
(3) described ALANINE permeate is passed into chromatographic system, carry out chromatography, collect product feed liquid;
(4) described product feed liquid is concentrated, crystallization, solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, described ALANINE crystal is dried to obtain ALANINE finished product.
2. method according to claim 1, is characterized in that, in described ALANINE extreme trace mother liquor, ALANINE content is 10%-20%, is preferably 14-16%.
3. method according to claim 1, is characterized in that: micro-filtration process uses ceramic membrane, and the rete material of described ceramic membrane is TiO
2/ ZrO
2, further, the aperture of described ceramic membrane is 40-60nm, is preferably 50nm.
4. the method according to claim 1 or 3, is characterized in that: the method for described micro-filtration process is: described ALANINE coarse filtration liquid is crossed ceramic membrane, controlled filter temperature 50-60 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa.
5. method according to claim 4, it is characterized in that: when the volume of described concentrating spent liquor is the 15%-20% of the thick filtrate volume of described ALANINE, add the deionized water being equivalent to described ALANINE thick filtrate volume 10-15% to dialyse described concentrating spent liquor, obtain dialyzate, described dialyzate and described permeate are merged.
6. method according to claim 1, is characterized in that: the stationary phase that chromatography uses is calcium ion type exchange resin, and moving phase is water.
7. method according to claim 6, is characterized in that: the grain diameter of described calcium ion type exchange resin is 0.2-0.3mm.
8. the method according to claim 1 or 6 or 7, is characterized in that, the condition of chromatography is: chromatogram column temperature 55-65 DEG C, feed rate 0.2-0.3BV/h, eluting water flow 1.0-1.5BV/h, load 0.3-0.7BV/h, go out wastewater flow rate 1.15-1.35BV/h; Be preferably, chromatogram column temperature 60 DEG C, feed rate 0.25BV/h, eluting water flow 1.5BV/h, load 0.5BV/h, go out wastewater flow rate 1.25BV/h.
9. method according to claim 1, is characterized in that: in step (4), and product feed liquid being concentrated into solid content is that 55%-65% stops, and is then cooled to 5-15 DEG C of crystallization, after crystallization terminates, carries out solid-liquid separation, to obtain final product; Preferably, product feed liquid being concentrated into product feed liquid solid content is 60% stopping, being then cooled to 10 DEG C of crystallizations, after crystallization terminates, carries out solid-liquid separation, to obtain final product.
10. method according to claim 1, is characterized in that, comprises the steps:
(1) get ALANINE extreme trace mother liquor, under 50-70 DEG C of condition, adjust ph is to 6-8, separates out solid impurity, and filtering described solid impurity obtains ALANINE coarse filtration liquid excessively;
(2) described ALANINE coarse filtration liquid is crossed the ceramic membrane that aperture is 40-60nm, controlled filter temperature 50-60 DEG C, feed pressure 0.2-0.25MPa, discharge pressure 0.15-0.23MPa, filter after terminating and obtain ALANINE permeate and concentrating spent liquor; Further, when the volume of described concentrated solution is the 15%-20% of the thick filtrate volume of described ALANINE, the deionized water adding the 10-15% being equivalent to the thick filtrate volume of described ALANINE is dialysed described concentrating spent liquor, obtains dialyzate, described dialyzate and described permeate is merged;
(3) described ALANINE permeate is passed into chromatographic column, the stationary phase of described chromatographic column is calcium ion type exchange resin, moving phase is water, control the temperature 55-65 DEG C of chromatographic column, feed rate 0.2-0.3BV/h, eluting water flow 1.0-1.5BV/h, load 0.3-0.7BV/h, go out wastewater flow rate 1.15-1.35BV/h;
(4) described product feed liquid being concentrated into solid content is 55%-65%, crystallization under 5-15 DEG C of condition, after crystallization, carries out solid-liquid separation, obtain ALANINE crystal and ALANINE crystalline mother solution, described ALANINE crystal is dried under 55-65 DEG C of condition and obtains ALANINE finished product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510734714.XA CN105348122B (en) | 2015-10-30 | 2015-10-30 | A kind of purification process of L alanine extreme trace mother liquor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510734714.XA CN105348122B (en) | 2015-10-30 | 2015-10-30 | A kind of purification process of L alanine extreme trace mother liquor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105348122A true CN105348122A (en) | 2016-02-24 |
| CN105348122B CN105348122B (en) | 2017-11-10 |
Family
ID=55324210
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510734714.XA Active CN105348122B (en) | 2015-10-30 | 2015-10-30 | A kind of purification process of L alanine extreme trace mother liquor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105348122B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107216264A (en) * | 2017-06-03 | 2017-09-29 | 秦皇岛华恒生物工程有限公司 | A kind of processing method of L alanine waste liquor |
| CN108484423A (en) * | 2018-07-05 | 2018-09-04 | 秦皇岛华恒生物工程有限公司 | A method of isolating and purifying l-Alanine from l-Alanine zymotic fluid |
| CN111574390A (en) * | 2020-05-21 | 2020-08-25 | 赵兰坤 | Efficient green production and extraction process of amino acid |
| CN114805103A (en) * | 2021-01-29 | 2022-07-29 | 安徽丰原生物技术股份有限公司 | Method for extracting L-alanine |
| CN115894267A (en) * | 2021-09-30 | 2023-04-04 | 秦皇岛华恒生物工程有限公司 | Separation method of product in beta-alanine mother liquor |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6551803B1 (en) * | 1999-11-03 | 2003-04-22 | Basf Aktiengesellschaft | Method for purification of amino acid containing solutions by electrodialysis |
| CN102432479A (en) * | 2011-12-30 | 2012-05-02 | 梅花生物科技集团股份有限公司 | Method for extracting L-valine from L-valine fermentation liquid |
| CN102603548A (en) * | 2012-02-22 | 2012-07-25 | 蒋光玉 | Method for extracting L-alanine from mother solution |
| CN102659612A (en) * | 2012-05-10 | 2012-09-12 | 杭州蓝然环境技术有限公司 | Process for purifying L-phenylalanine |
| CN103232354A (en) * | 2013-04-26 | 2013-08-07 | 新疆阜丰生物科技有限公司 | Method for separating heteroacid from valine fermentation liquid |
| CN103387502A (en) * | 2012-05-09 | 2013-11-13 | 上海医药工业研究院 | Method for extracting L-alanine from L-alanine fermentation liquid |
| CN103965064A (en) * | 2013-01-31 | 2014-08-06 | 上海医药工业研究院 | Method for extraction of L-alanine from L-alanine fermentation broth |
-
2015
- 2015-10-30 CN CN201510734714.XA patent/CN105348122B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6551803B1 (en) * | 1999-11-03 | 2003-04-22 | Basf Aktiengesellschaft | Method for purification of amino acid containing solutions by electrodialysis |
| CN102432479A (en) * | 2011-12-30 | 2012-05-02 | 梅花生物科技集团股份有限公司 | Method for extracting L-valine from L-valine fermentation liquid |
| CN102603548A (en) * | 2012-02-22 | 2012-07-25 | 蒋光玉 | Method for extracting L-alanine from mother solution |
| CN103387502A (en) * | 2012-05-09 | 2013-11-13 | 上海医药工业研究院 | Method for extracting L-alanine from L-alanine fermentation liquid |
| CN102659612A (en) * | 2012-05-10 | 2012-09-12 | 杭州蓝然环境技术有限公司 | Process for purifying L-phenylalanine |
| CN103965064A (en) * | 2013-01-31 | 2014-08-06 | 上海医药工业研究院 | Method for extraction of L-alanine from L-alanine fermentation broth |
| CN103232354A (en) * | 2013-04-26 | 2013-08-07 | 新疆阜丰生物科技有限公司 | Method for separating heteroacid from valine fermentation liquid |
Non-Patent Citations (1)
| Title |
|---|
| 蒋光玉: "发酵法生产L-丙氨酸提取工艺的研究", 《中国食品添加剂》 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107216264A (en) * | 2017-06-03 | 2017-09-29 | 秦皇岛华恒生物工程有限公司 | A kind of processing method of L alanine waste liquor |
| CN107216264B (en) * | 2017-06-03 | 2019-07-30 | 秦皇岛华恒生物工程有限公司 | A kind of processing method of l-Alanine waste liquor |
| CN108484423A (en) * | 2018-07-05 | 2018-09-04 | 秦皇岛华恒生物工程有限公司 | A method of isolating and purifying l-Alanine from l-Alanine zymotic fluid |
| CN108484423B (en) * | 2018-07-05 | 2021-02-09 | 秦皇岛华恒生物工程有限公司 | Method for separating and purifying L-alanine from L-alanine fermentation liquor |
| CN111574390A (en) * | 2020-05-21 | 2020-08-25 | 赵兰坤 | Efficient green production and extraction process of amino acid |
| CN114805103A (en) * | 2021-01-29 | 2022-07-29 | 安徽丰原生物技术股份有限公司 | Method for extracting L-alanine |
| CN114805103B (en) * | 2021-01-29 | 2024-03-15 | 安徽丰原生物技术股份有限公司 | Extraction method of L-alanine |
| CN115894267A (en) * | 2021-09-30 | 2023-04-04 | 秦皇岛华恒生物工程有限公司 | Separation method of product in beta-alanine mother liquor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105348122B (en) | 2017-11-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105348122A (en) | Method for purifying L-alanine final mother liquor | |
| CN101863783B (en) | Method for separating and purifying gamma-aminobutyric acid (GABA) from glutamine decarboxylase enzymolysis liquid | |
| CN102643209B (en) | Extraction method of L-glutamine | |
| CN101812009A (en) | Novel technique for extracting L-tryptophan from fermentation broth | |
| CN107513030B (en) | Method for separating and purifying L-hydroxyproline from L-hydroxyproline fermentation liquor | |
| CN101525306A (en) | Method for extracting and separating natural taurine from octopus leftovers | |
| CN102363594B (en) | Method for separating and purifying succinic acid from fermentation broth | |
| CN101633634A (en) | Method for extracting L-proline from fermentation liquor by membrane separation technology | |
| CN108285912A (en) | A method of fermentation prepares extraction pharmaceutical grade valine | |
| CN101497574B (en) | Method for extracting and separating L-isoleucine by membrane separation and plant chromatography separation | |
| CN101503366B (en) | Method for extracting and separating L-valine by membrane separation and plant chromatography separation | |
| CN101654413A (en) | Method for extracting and separating L-isoleucine employing three-stage film cascade | |
| CN105017360A (en) | Vitamin B12 preparation method | |
| CN101492408A (en) | Method for separating tryptophane from fermentation liquor | |
| CN109678743B (en) | A kind of isolation and purification method of Valine | |
| CN107383135A (en) | The method that β thymidines are isolated and purified from zymotic fluid | |
| CN109385414B (en) | Purification method of bromelain | |
| CN113005161A (en) | Preparation method of polysialic acid and polysialic acid product | |
| CN102344383B (en) | Method for concentrating and crystallizing L-phenylalanine | |
| CN112521487A (en) | Improved production process of human serum albumin | |
| CN105418461A (en) | Continuous ion exchange extraction technology of L-arginine | |
| CN103159643B (en) | Technology for whole membrane extraction of L-glutamine fermentation broth | |
| CN110627848A (en) | Method for removing impurities in sialic acid and application thereof | |
| CN112409426B (en) | Preparation method of sisomicin sulfate | |
| CN103145590B (en) | Clean L-arginine production technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190130 Address after: 233700 Guzhen County Economic Development Zone, Bengbu City, Anhui Province Patentee after: Fengyuan Biological Chemistry Co., Ltd., Anhui Prov. Address before: 233030 South of Huaiwu Road, Huaishang District, Bengbu City, Anhui Province Patentee before: Anhui Fengyuan Fermentation Technology Engineering Research Co., Ltd. |
|
| TR01 | Transfer of patent right | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 233700 Guzhen County Economic Development Zone, Bengbu City, Anhui Province Patentee after: Anhui Fengyuan Biotechnology Co.,Ltd. Address before: 233700 Guzhen County Economic Development Zone, Bengbu City, Anhui Province Patentee before: ANHUI BBCA BIOCHEMICAL Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder |