CN103508933B - Separating and purifying method for L-tryptophan - Google Patents
Separating and purifying method for L-tryptophan Download PDFInfo
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- CN103508933B CN103508933B CN201310375366.2A CN201310375366A CN103508933B CN 103508933 B CN103508933 B CN 103508933B CN 201310375366 A CN201310375366 A CN 201310375366A CN 103508933 B CN103508933 B CN 103508933B
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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 kind of separation for amino acids method of purification, particularly relate to a kind of method of separating-purifying L-Trp from fermented liquid.
Background technology
L-Trp is the die aromatischen Aminosaeuren containing indyl, humans and animals grow and metabolic in play an important role, be one of eight seed amino acids of needed by human, its crystal white or yellowish.Tryptophane can synthesize multiple hormone and physiologically active substance in human body, and also participate in regulating the nervous physiology of human body movable, and compare shortage in vegetable-protein, 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 containing 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 removes tropina through membrane filtration or flocculation sediment, feed liquid is passed through from friendship ADSORPTION IN A FIXED BED, is resolved tryptophane, reach the object of removal of impurities, desorbed solution improves product printing opacity by activated carbon decolorizing, finally concentrated feed liquid, crystallizing and drying makes tryptophane finished product.In aforesaid method, the use of flocculation agent, adds production cost, contaminate environment, and the feed clarification degree obtained is very poor, affects the purifying products process in downstream; And from handing over the use of fixed bed, the waste of acid, alkali and water also can be caused; The use of gac can to environment, and gac is difficult thoroughly removes, its remaining influence quality of the finished product.
2012.02.08 disclosed application number is the method that the Chinese invention patent of CN201110227776.3 discloses tryptophane in a kind of ion exchange resin extracting directly fermented liquid, by the fermentation liquor deactivation containing tryptophane, acid adjustment to pH value is after the pre-treatment of 3 ~ 4, add 0.8 ~ 1.5 by the amount of corresponding every 20 grams of the tryptophane that contains in fermented liquid to go up after the clear liquid after batch being separated useless bacterium slag mixes and obtain the fermented liquid after diluting, then enter in ion exchange resin column and carry out circulation exchange adsorption, resolve through ammoniacal liquor after ion exchange resin washes down, 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 friendship fixed bed, and what can not realize tryptophane fermented liquid is continuously separated purifying, and causes the waste of acid, alkali and water.
2009.07.29 disclosed application number is that the Chinese invention patent of CN200910024690.3 discloses a kind of method from separation of fermentative broth tryptophane, by micro-pore-film filtration except thalline, membrane sepn are except the larger molecular organics such as colloid protein and pigment matter, electrodialysis are except inorganic salt and reverse osmosis concentration, finally obtain tryptophane crystal.The process employs membrane technique and carry out separation and purification tryptophane, but adopt multistage film process to reduce the overall yield of tryptophane.
2009.03.04 disclosed application number is that the Chinese invention patent of CN200710059347.3 discloses a kind of ion exchange extraction technique utilizing direct fermentation to produce L-Trp, adopt stainless steel tubular type film separating system filtering fermentating liquid, application ion exchange method extracts 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 friendship fixed bed, and what can not realize tryptophane fermented liquid is continuously separated purifying, and causes the waste of acid, alkali and water, and overall yield is on the low side.
2010.05.19 disclosed application number is the extracting method that the Chinese invention patent of CN200910211061.1 discloses a kind of L-Trp, comprises the steps: 1) pH value of L-Trp fermented liquid is adjusted to 1.5-4.5, then carry out membrane filtration; 2) membrane filtration fluid is separated from friendship system with being equipped with the simulation moving-bed of Zeo-karb; 3) elutriant adjust pH is to 6-7; 4) elutriant after acid adjustment adds heat decoloring; Namely 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 is decoloured by gac, gac cannot thoroughly be removed, and have impact on the quality of product.
Summary of the invention
The invention provides a kind of method of separating-purifying L-Trp from fermented liquid, 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 acid for adjusting pH to 2.5-4.0, adopt aperture 50-100nm ceramic membrane filter degerming;
2) ceramic membrane filtrate exchanges moving-bed removal of impurities by the continuous ionic rotated counterclockwise, and continuous ionic exchange moving-bed is divided into washing material district, intake zone, regeneration of hydrochloric acid and washing acid district, ammoniacal liquor resolve and wash ammonia district and pool, product top in the direction of the clock;
3) desorbed solution of resolving from continuous ionic exchange moving-bed decolours through the nanofiltration membrane that retaining molecular weight is 300-1000Da;
4) feed liquid after decolouring is carried out dehydration by reverse osmosis membrane and is concentrated.
Further, the acid that in described step 1), adjust ph is used is sulfuric acid, and filtration temperature is 0-80 DEG C, and entrance pressure 3-4bar goes out to press 1-2bar.
Further, when in described step 1), fermented liquid concentrates 3-6 times, the top that adds water is washed, and amount of water is 0.6-0.8 times of fermentating liquid volume.
Further, described step 2) in continuous ionic to exchange moving-bed resin used be strongly-acid or acidulous cation resin, such as D001,732 or LH-2; Parsing ammonia concn is 2-3%, and concentration of hydrochloric acid is 4-6%, and it is 40-60 DEG C that continuous ionic exchanges moving-bed operating temperature, 10 hours rotating disk cycles.
Further, described step 2) in continuous ionic exchange the system that moving-bed adopts 20 posts, be 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 washed 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, 12# out wash sour water and 13# acid mixing out after continue 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# water inlet of connecting, and enters 18#, 19# and continue to resolve after the ammoniacal liquor of the ammoniacal liquor that 16# comes out and 17# mixes;
5) pool, product top: 20#, flow velocity 0.8L/H.
Further, working pressure 5-10bar in described step 3), filtration temperature 20-45 DEG C; When desorbed solution concentrates 8-10 times, the top that adds water is washed, 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 DEG C.
The invention has the beneficial effects as follows:
Connection ion-exchange moving-bed system combines with membrane technique by present method, membrane technique tryptophan fermented liquid is adopted to carry out filtering, decolour and concentrating, connection ion-exchange moving-bed tryptophan fermented liquid is adopted to carry out purifying, the consumption of acid, alkali, water and resin is decreased while guaranteeing overall yield and product purity, avoid the impact of activated carbon decolorizing on quality product, reduce production cost and the wasting of resources.
Accompanying drawing explanation
Fig. 1 is that continuous ionic of the present invention exchanges moving-bed workflow schematic diagram
Embodiment
Further describe technical scheme of the present invention below in conjunction with specific embodiment, 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 DEG C filtration sterilization of 50nm, when concentrated solution volume is 50L, product is washed on the top that starts to add water, add water 140L altogether, the average flux of film is 75L/ (㎡ .H), product mean concns is 22.1g/L, and yield is 98.3%;
2) Continuous Moving Bed removal of impurities: by ceramic membrane filtrate by Continuous Moving Bed removal of impurities, Continuous Moving Bed adopts spool to be the system of 4mm, filling 13.5L resin, rotating disk cycle 10H.Feed liquid enters system by 3#, 4# post, charging flow velocity 6.1L/H, and after primary adsorption, feed liquid series connection enters 5-7# and carries out secondary absorption and 8-10# carries out three grades of absorption; After absorption terminates, 1#, 2# post washing series-connection, washing flow velocity is 1.35L/H, and washing feed liquid enters the second stage absorption of adsorption zone; The ammoniacal liquor that 17# post passes into 2.5% with the flow velocity of 2.9L/H is resolved, 15# post with the flow velocity of 2.7L/H washing ammonia, the ammonia washed out with 16# and 17# resolve the ammino that flows out and after enter 18#, 19# and continue to resolve; Desorbed solution pumps into 20# capital and washes water in pillar, flow velocity 0.8L/H; After parsing terminates, 13# passes into the resolving hydrochloric acid of 5%, and flow velocity 0.9L/H, 11# pass into and wash sour water, flow velocity 1.35L/H, and the acid merging that the acid of being washed out by 12# and 13# flow out enters the further regenerating resin of 14#.The product concentration obtained is 27.7g/L, and yield is 98.5%.
3) nanofiltration membrane decolouring: get Continuous Moving Bed desorbed solution 200L, employing molecular weight cut-off is that the rolled film of 600Da decolours, enter film pressure 8bar, go out film pressure 6bar, service temperature 25-35 DEG C, after concentrated 10 times, add 60L water top and wash product, film average flux is 28L/(㎡ .H), the dialyzate printing opacity obtained is 73%, product concentration 22.4g/L, yield is 97.1%.
4) reverse osmosis concentration: adopt reverse osmosis membrane to concentrate nanofiltration membrane dialyzate, service temperature is 30-40 DEG C, 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 obtained is 46.7g/L, yield 99.2%.
5) subsequent technique: nanofiltration membrane is concentrated the feed liquid obtained and carry out the concentrated and crystallization of reduction vaporization, in the product obtained, 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 ceramic membrane 40 DEG C of-60 DEG C of filtration sterilizations of 50nm, when concentrated solution volume is 37L, product is washed on the top that starts to add water, add water 115L altogether, the average flux of film is 83L/ (㎡ .H), product mean concns is 20.8g/L, and yield is 98.6%;
2) Continuous Moving Bed removal of impurities: by ceramic membrane filtrate by Continuous Moving Bed removal of impurities, Continuous Moving Bed adopts spool to be the system of 4mm, filling 13.5L resin, rotating disk cycle 10H.Feed liquid enters system by 3#, 4# post, charging flow velocity 6.5L/H, and after primary adsorption, feed liquid series connection enters 5-7# and carries out secondary absorption and 8-10# carries out three grades of absorption; After absorption terminates, 1#, 2# post washing series-connection, washing flow velocity is 1.35L/H, and washing feed liquid enters the second stage absorption of adsorption zone; The ammoniacal liquor that 17# post passes into 2.5% with the flow velocity of 2.9L/H is resolved, 15# post with the flow velocity of 2.7L/H washing ammonia, the ammonia washed out with 16# and 17# resolve the ammino that flows out and after enter 18#, 19# and continue to resolve; Desorbed solution pumps into 20# capital and washes water in pillar, flow velocity 0.8L/H; After parsing terminates, 13# passes into the resolving hydrochloric acid of 5%, and flow velocity 0.9L/H, 11# pass into and wash sour water, flow velocity 1.35L/H, and the acid merging that the acid of being washed out by 12# and 13# flow out enters the further regenerating resin of 14#.The product concentration obtained is 27.5g/L, and yield is 98.1%.
3) nanofiltration membrane decolouring: get Continuous Moving Bed desorbed solution 180L, employing molecular weight cut-off is that the rolled film of 400Da decolours, enter film pressure 7bar, go out film pressure 5bar, service temperature 35-45 DEG C, after concentrated 10 times, add 63L water top and wash product, film average flux is 33L/(㎡ .H), the dialyzate printing opacity obtained is 75%, product concentration 22.5g/L, yield is 97.5%.
4) reverse osmosis concentration: adopt reverse osmosis membrane to concentrate nanofiltration membrane dialyzate, service temperature is 30-40 DEG C, and entering film pressure is 30bar, going out film pressure is 28bar, concentrates 2.0 times, and film average flux is 15L/(㎡ .H), the concentrated solution product concentration obtained is 44.66g/L, yield 99.1%.
5) subsequent technique: nanofiltration membrane is concentrated the feed liquid obtained and carry out the concentrated and crystallization of reduction vaporization, in the product obtained, 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 thereto, those of ordinary skill in the art is to be understood that, the technical scheme of invention is modified or equivalent replacement, but do not depart from the spirit and scope of technical solution of the present invention, it all should be encompassed in right 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 acid for adjusting pH to 2.5-4.0, adopt aperture 50-100nm ceramic membrane filter degerming;
2) ceramic membrane filtrate exchanges moving-bed removal of impurities by the continuous ionic rotated counterclockwise, and continuous ionic exchange moving-bed is divided into washing material district, intake zone, regeneration of hydrochloric acid and washing acid district, ammoniacal liquor resolve and wash ammonia district and pool, product top in the direction of the clock;
3) desorbed solution of resolving from continuous ionic exchange moving-bed decolours through the nanofiltration membrane that retaining molecular weight is 300-1000Da;
4) feed liquid after decolouring is carried out dehydration by reverse osmosis membrane and is concentrated.
2. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: described step 1) in adjust ph acid used be sulfuric acid.
3. the separating and purifying method of a kind of L-Trp as claimed in claim 1, is characterized in that: described step 1) in filtration temperature be 0-80 DEG C, 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: step 1) in ceramic membrane filter degerming, when fermented liquid concentrates 3-6 times, the top that adds water is washed, amount of water be the 0.6-0.8 of 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) in continuous ionic to exchange moving-bed resin used be strongly-acid or acidulous cation resin.
6. the separating and purifying method of a kind of L-Trp as claimed in claim 1, it is characterized in that: described step 2) in resolve ammonia concn be 2-3%, concentration of hydrochloric acid is 4-6%, and it is 40-60 DEG C that continuous ionic exchanges moving-bed operating temperature, 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) in continuous ionic exchange moving-bed and adopt the system of 20 posts, be 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 washed 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, 12# out wash sour water and 13# acid mixing out after continue 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# water inlet of connecting, and enters 18#, 19# and continue to resolve after the ammoniacal liquor of the ammoniacal liquor that 16# comes out and 17# mixes;
5) pool, product top: 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: described step 3) middle working pressure 5-10bar, filtration temperature 20-45 DEG C; When desorbed solution concentrates 8-10 times, the top that adds water is washed, 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: described step 4) in the working pressure of reverse osmosis membrane be 25-33bar, working temperature is 20-45 DEG C.
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| CN104592047B (en) * | 2014-12-24 | 2016-09-07 | 三达膜科技（厦门）有限公司 | A kind of process for separation and purification of valine |
| CN104817449B (en) * | 2014-12-31 | 2016-09-07 | 三达膜科技（厦门）有限公司 | A kind of process for separation and purification of 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 |
| 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 |
| 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 |
| CN113842779A (en) * | 2021-10-19 | 2021-12-28 | 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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| 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 |
| CN101709048B (en) * | 2009-11-11 | 2011-10-26 | 安徽丰原发酵技术工程研究有限公司 | Method for extracting L-tryptophan |
| CN103059105B (en) * | 2012-12-28 | 2014-12-10 | 三达膜科技（厦门）有限公司 | Method for extraction of colistin sulphate |
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