CN101709038A - Method for extracting L-phenylalanine from fermentation broth - Google Patents
Method for extracting L-phenylalanine from fermentation broth Download PDFInfo
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Abstract
The invention discloses a method for extracting L-phenylalanine from fermentation broth, and the method comprises the following steps: firstly carrying out microfiltration on the tyrosine deficient L-phenylalanine high-production strain mature fermentation broth for removing bacteria, then carrying out nano-filtration for decoloring or carrying out ion exchange, further sequentially carrying out concentration, crystallization, filtration, decoloration, re-crystallization and drying on filtrate or eluate, and finally cooling for obtaining an L-phenylalanine product. The adoption of the method can improve the yield and the purity of the L-phenylalanine; strong-acid cation exchange resin is adopted for absorption, thereby improving the utilization rate of the resin by 30% and improving the extraction capability of the unit resin by 3-5 times; and the adoption of the way of firstly carrying out the microfiltration and then carrying out the nano-filtration can improve the purity of the L-phenylalanine to 99-100% from the existing 50%, and improve the yield to 80-97% from the existing 40%.
Description
Technical field
The present invention relates to a kind of amino acid whose extracting method, is a kind of method of extracting the L-phenylalanine from fermented liquid specifically.
Background technology
The chemical name of phenylalanine (Phenylalanine) is pantonine-phenylpropionic acid, and molecular formula is C
6H
5C
2H
3(NH
2) CO
2H, molecular weight are 165.19.Commodity mainly contain L-phenylalanine, D-phenylalanine and DL-phenylalanine, and main application fields is food and medical department.The L-phenylalanine is white crystals or crystalline powder, and is slightly bitter, 283 ℃ of fusing points (decomposition), and specific optical rotation-35.1 ° (C=1.94 is in the water), the decompression distillation, water-soluble, be insoluble in methyl alcohol, ethanol, ether etc.The L-phenylalanine is one of 8 kinds of necessary amino acid, and it also is the important source material of synthetic hydroxyphenylaminopropionic acid in the organism simultaneously.Phenylalanine is some amino acid medicine and the necessary composition of amino acid nutrient food, is the intermediate of synthetic some cancer therapy drug, as phenylpropyl alcohol ammonia benzyl, formic acid Sarkolizin etc.Its most important purposes be with the synthetic two peptide product aspartame of L-aspartic acid (Aspartame, APM); The another one important use of L-phenylalanine is the composition as nutrition-fortifying agent, amino acid transfusion and mixed amino acid.
The L-phenylalanine is the indispensable amino acid of human body and animal.In fields such as medicine, food, healthcare products very big use being arranged, is novel sweetener aspartame (Aspartame, APM) main raw material of Sheng Chaning that be in fashion in the whole world.The L-phenylalanine has been the fastest-rising amino acid kind of the market requirement since the last century the eighties, and product 90% is used for production aspartame sweeting agent, and 10% is used for aspects such as medicine.The L-phenylalanine is mainly used in propylhomoserin acid transfusion and amino acid drug in pharmaceutical industries, and as antitumor drug P-fluoropnenylalanine, phenylpropyl alcohol ammonia benzyl, formic acid Sarkolizin etc., market is very well sold and in short supply, and Future Development has a bright future.China's pharmaceutical industries is annual at present need consume about about 400 tons of L-phenylalanine, main dependence on import.
At present, because the development and use of domestic amino acid infusion solutions and anticarcinogen, particularly asccharin production is carried out under the situation of restriction, stevioside sweetener product experience trouble, the aspartame demand is increased sharply, and stimulates and promoted the production and the development of L-phenylalanine greatly.L-phenylalanine preparation method mainly contains direct fermentation, chemical synthesis and enzyme process.Direct fermentation is to utilize raw materials such as glucose to go out the L-phenylalanine through the microbial fermentation direct production; The chemical synthesis route is long, by product is many, and product is the optics raceme, need carry out optical resolution, the cost height; Production by Enzymes is that to utilize the synthetic precursor of L-phenylalanine such as phenyl-pyruvic acid or styracin be the synthetic L-phenylalanine of catalysis through the microorganism cells endoenzyme.Need in the process with fermentative Production L-phenylalanine fermented liquid extracted just and can obtain the L-phenylalanine, present employed extracting method mainly is an ion exchange method, but employed ion exchange resin is the large hole strong acid styrene system cation exchange resin, this resin is difficult to the L-phenylalanine is separated from fermented liquid, and the multipotency of yield reaches 40%, purity is up to 50%.
Summary of the invention
Goal of the invention: the objective of the invention is in order to overcome the deficiencies in the prior art, a kind of method of extracting the L-phenylalanine from fermented liquid that can improve product yield and purity is provided.
Technical scheme: in order to solve the problems of the technologies described above, a kind of method of from fermented liquid, extracting the L-phenylalanine of the present invention, the concrete steps of this method are as follows:
1) extract: with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 1～5m
3The flow velocity of/h extracts the solution that obtains containing the L-phenylalanine;
2) concentrate: the solution of gained in the step 1) is carried out the falling film type vacuum concentration, and thickening temperature is 60～70 ℃, and vacuum degree control concentrates when concentrated solution concentration reaches 90～100g/L and finishes at 0.096～0.098MPa;
3) primary crystallization: with mass concentration is that 10% phosphoric acid or mass concentration be that 10% sodium hydroxide solution regulates the pH value of concentrated solution and make the pH value are 4.5～4.8, then the concentrated solution temperature is reduced to that crystallization 8～14h obtains mother liquor and solid materials below 5 ℃;
4) decolouring: the solid materials that crystallization is obtained is dissolved in water and the mother liquor reuse is made the mass concentration of solution is 30～35%, with mass concentration is that 10% phosphoric acid or mass concentration are the pH value of 10% sodium hydroxide solution regulator solution and to make the pH value be 4.5～4.8, add gac then and be heated to 60～70 ℃, 60～70 ℃ of decolourings 30～45 minutes;
5) filter: the solution that decolouring is obtained filters, and gets filtrate;
6) secondary crystal: filtrate is reduced to below 5 ℃, and crystallization 8～14h obtains solid materials and mother liquor;
7) drying: the solid materials dry 6～8h under 40～60 ℃ with secondary crystal obtains at 75～80 ℃ of down dry 2～4h, promptly obtain described L-phenylalanine product then after the cooling.
The mode of extracting described in the step 1) is a nanofiltration decolouring mode behind the first micro-filtration removal thalline.Way of NF is behind the described first micro-filtration: adopt the film of 0.1～10 μ m to filter under 0.7～7kPa working pressure fermented liquid earlier, obtain filtrate and thalline waste residue, then filtrate is obtained containing the filtrate of L-phenylalanine behind the membrane filtration by 0.8～1nm under 0.3～0.7MPa working pressure.Adopt this suction type can make the purity of L-phenylalanine bring up to 99-100% by existing 50%, yield brings up to 80～97% by existing 40%.
Extracting mode described in the step 1) adsorbs by ion-exchange method for elder generation, and then contains the ion exchange resin of L-phenylalanine and collect elutriant with the eluent wash-out, and the pH value is 1～3 in this adsorption process.Described ion exchange resin system is made up of a plurality of ion exchange resin columns polyphones.Described ion exchange resin is strongly-acid ammonium type Zeo-karb.Described eluent is a 0.5mol/L ammoniacal liquor.With described eluent with 2～4m
3The speed wash-out of/h.
Adopt strongly-acid ammonium type Zeo-karb to adsorb, can make the resin utilization ratio improve 30%, the extractability of unit resin improves 3～5 times, and the purity of L-phenylalanine brings up to 99～100% by existing 50%, and yield brings up to 70～97% by existing 40%.
Described thalline waste residue is obtained protein fodder after drying; Like this can be so that filter residue is reused, thus turn waste into wealth.
In order to improve product yield, with the mother liquor of gained in the above-mentioned steps decolour successively again, filtration, crystallization, drying process.
Beneficial effect: compared with prior art, adopt the present invention can improve the yield and the purity of L-phenylalanine; Adopt strongly-acid ammonium type Zeo-karb to adsorb, can make the resin utilization ratio improve 30%, the extractability of unit resin improves 3～5 times; Way of NF can make the purity of L-phenylalanine bring up to 99～100% by existing 50% after adopting first micro-filtration, and yield brings up to 80～97% by existing 40%, and the mother liquor reuse can improve product yield.
Embodiment
The present invention is described in further detail below in conjunction with embodiment, should understand these embodiment and only be used to the present invention is described and be not used in and limit the scope of the invention.
Embodiment 1: with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 1～3m
3The flow velocity of/h filters by the film of 10 μ m and under 5～7kPa working pressure and obtains filtrate and thalline waste residue, and the film absorption by 1nm under 0.3～0.7MPa working pressure of gained filtrate is obtained L-phenylalanine crude product, and the pH value in this adsorption process is 1～3; With 0.5mol/L ammoniacal liquor as eluent and with this eluent with 2～4m
3The speed wash-out of/h contains L-phenylalanine crude product, collects elute soln; Elute soln is carried out the falling film type vacuum concentration, and thickening temperature is 60～70 ℃, and vacuum degree control concentrates when concentrated solution concentration reaches 90～100g/L and finishes at 0.096～0.098MPa; With mass concentration is that 10% phosphoric acid or mass concentration be that 10% sodium hydroxide solution regulates the pH value of concentrated solution and make the pH value are 4.5～4.8, then the concentrated solution temperature is reduced to that crystallization 10～14h obtains mother liquor and solid materials below 5 ℃, the solid materials that crystallization is obtained is dissolved in water and the mother liquor reuse is made that the mass concentration of solution is 30～35%, with mass concentration is that 10% phosphoric acid or mass concentration are the pH value of 10% sodium hydroxide solution regulator solution and to make the pH value be 4.5～4.8, add gac then and be heated to 60～70 ℃, 60～70 ℃ of decolourings 30～45 minutes; The solution that decolouring is obtained filters, and gets filtrate; Filtrate is reduced to below 5 ℃, and crystallization 8～14h obtains solid materials and mother liquor; The solid materials that secondary crystal is obtained is at 40～60 ℃ of down dry 6～8h, then at 75～80 ℃ of down dry 2～4h, promptly obtains described purity after the cooling and be 99% L-phenylalanine.Above-mentioned mother liquor is sent into bleaching process to be recycled.The L-phenylalanine yield that can make with this extracting method reaches 80%.The thalline waste residue that obtains in the absorption process is made protein fodder after drying.
Embodiment 2: with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 3～5m
3The flow velocity of/h filters by the film of 0.1 μ m and under 0.7～2kPa working pressure and obtains filtrate and thalline waste residue, the film absorption by 0.8nm under 0.3～0.7MPa working pressure of gained filtrate is obtained L-phenylalanine crude product, and the pH value in this adsorption process is 1～3; With 0.5mol/L ammoniacal liquor as eluent and with this eluent with 2～4m
3The speed wash-out of/h contains L-phenylalanine crude product, collects elute soln; Elute soln is carried out the falling film type vacuum concentration, and thickening temperature is 60～70 ℃, and vacuum degree control concentrates when concentrated solution concentration reaches 90～100g/L and finishes at 0.096～0.098MPa; With mass concentration is that 10% phosphoric acid or mass concentration be that 10% sodium hydroxide solution regulates the pH value of concentrated solution and make the pH value are 4.5～4.8, then the concentrated solution temperature is reduced to that crystallization 8～10h obtains mother liquor and solid materials below 5 ℃, the solid materials that crystallization is obtained is dissolved in water the mother liquor reuse is made that the mass concentration of solution is 30～35%, with mass concentration is that 10% phosphoric acid or mass concentration are the pH value of 10% sodium hydroxide solution regulator solution and to make the pH value be 4.5～4.8, add gac then and be heated to 60～70 ℃, 60～70 ℃ of decolourings 30～45 minutes; The solution that decolouring is obtained filters, and gets filtrate; Filtrate is reduced to below 5 ℃, and crystallization 8～10h obtains solid materials and mother liquor; The solid materials that secondary crystal is obtained is at 40～60 ℃ of down dry 6～8h, then at 75～80 ℃ of down dry 2～4h, promptly obtains described purity after the cooling and be 99.3% L-phenylalanine product.Above-mentioned mother liquor is sent into bleaching process to be recycled.The L-phenylalanine yield that can make with this extracting method reaches 97%.
Embodiment 3: with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 2～3m
3The flow velocity of/h adsorbs by the continuous ionic exchange system of being made up of three strongly-acid ammonium type cation exchange resin columns, obtains L-phenylalanine crude product, and the pH value is 1～3 in this adsorption process; With 0.5mol/L ammoniacal liquor as eluent and with this eluent with 2～4m
3The speed wash-out of/h contains the ion exchange resin of L-phenylalanine crude product, collects elute soln; Elute soln is carried out the falling film type vacuum concentration, and thickening temperature is 60～70 ℃, and vacuum degree control concentrates when concentrated solution concentration reaches 90～100g/L and finishes at 0.096～0.098MPa; With mass concentration is that 10% phosphoric acid or mass concentration be that 10% sodium hydroxide solution regulates the pH value of concentrated solution and make the pH value are 4.5～4.8, then the concentrated solution temperature is reduced to that crystallization 8～14h obtains mother liquor and solid materials below 5 ℃, the solid materials that crystallization is obtained is dissolved in water the mother liquor reuse is made that the mass concentration of solution is 30～35%, with mass concentration is that 10% phosphoric acid or mass concentration are the pH value of 10% sodium hydroxide solution regulator solution and to make the pH value be 4.5～4.8, add gac then and be heated to 60～70 ℃, 60～70 ℃ of decolourings 30～45 minutes; The solution that decolouring is obtained filters, and gets filtrate; Filtrate is reduced to below 5 ℃, and crystallization 8～14h obtains solid materials and mother liquor; The solid materials that secondary crystal is obtained is at 40～60 ℃ of down dry 6～8h, then at 75～80 ℃ of down dry 2～4h, promptly obtains purity after the cooling and be 99.6% L-phenylalanine product.Above-mentioned mother liquor is sent into bleaching process to be recycled.The L-phenylalanine yield that can make with this extracting method reaches 90%.
Embodiment 4: substantially the same manner as Example 1, different is with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 2～3m
3The flow velocity of/h filters by the film of 5 μ m and under 3～5kPa working pressure and obtains filtrate and thalline waste residue, and the film absorption by 0.9nm under 0.3～0.7MPa working pressure of gained filtrate is obtained L-phenylalanine crude product.The L-phenylalanine yield that can make with this extracting method reaches 85%, purity reaches 99.8%.
Embodiment 5: substantially the same manner as Example 1, different is with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 1～2m
3The flow velocity of/h filters by the film of 2 μ m and under 3～5kPa working pressure and obtains filtrate and thalline waste residue, and the film absorption by 0.9nm under 0.3～0.7MPa working pressure of gained filtrate is obtained L-phenylalanine crude product.The L-phenylalanine yield that can make with this extracting method reaches 95%, purity reaches 99.1%.
Embodiment 6: substantially the same manner as Example 3, different is to have adopted the continuous ionic exchange system of two strongly-acid ammonium type cation exchange resin column compositions to adsorb.The L-phenylalanine yield that can make with this extracting method reaches 70%,, purity reaches 99%.
Claims (8)
1. method of extracting the L-phenylalanine from fermented liquid is characterized in that the concrete steps of this method are as follows:
1) extract: with concentration is that the tyrosine defective type L-phenylalanine superior strain maturing fermentation liquid of 10～20g/L is with 1～5m
3The flow velocity of/h extracts the solution that obtains containing the L-phenylalanine;
2) concentrate: the solution of the resulting L-of containing phenylalanine in the step 1) is carried out the falling film type vacuum concentration, and thickening temperature is 60～70 ℃, and vacuum degree control concentrates when concentrated solution concentration reaches 90～100g/L and finishes at 0.096～0.098MPa;
3) primary crystallization: with mass concentration is that 10% phosphoric acid or mass concentration be that 10% sodium hydroxide solution regulates the pH value of concentrated solution and make the pH value are 4.5～4.8, then the concentrated solution temperature is reduced to that crystallization 8～14h obtains mother liquor and solid materials below 5 ℃;
4) decolouring: the solid materials that crystallization is obtained is dissolved in water and the mother liquor reuse is made the mass concentration of solution is 30～35%, with mass concentration is that 10% phosphoric acid or mass concentration are the pH value of 10% sodium hydroxide solution regulator solution and to make the pH value be 4.5～4.8, add gac then and be heated to 60～70 ℃, 60～70 ℃ of decolourings 30～45 minutes;
5) filter: the solution that decolouring is obtained filters, and gets filtrate;
6) secondary crystal: filtrate is reduced to below 5 ℃, and crystallization 8～14h obtains solid materials and mother liquor;
7) drying: the solid materials dry 6～8h under 40～60 ℃ with secondary crystal obtains at 75～80 ℃ of down dry 2～4h, promptly obtain described L-phenylalanine product then after the cooling.
2. a kind of method of extracting the L-phenylalanine from fermented liquid according to claim 1 is characterized in that: the mode of extracting described in the step 1) is a nanofiltration decolouring mode behind the first micro-filtration removal thalline.
3. a kind of method of from fermented liquid, extracting the L-phenylalanine according to claim 2, it is characterized in that: way of NF is behind the described first micro-filtration: adopt the film of 0.1～10 μ m to filter under 0.7～7kPa working pressure fermented liquid earlier, obtain filtrate and thalline waste residue, then filtrate is obtained containing the filtrate of L-phenylalanine behind the membrane filtration by 0.8～1nm under 0.3～0.7MPa working pressure.
4. a kind of method of from fermented liquid, extracting the L-phenylalanine according to claim 1, it is characterized in that: extracting mode described in the step 1) is for adsorbing by ion exchange system earlier, and then contain the ion exchange resin of L-phenylalanine and collect elutriant with the eluent wash-out, the pH value is 1～3 in this adsorption process.
5. a kind of method of extracting the L-phenylalanine from fermented liquid according to claim 4 is characterized in that: described ion exchange resin system is made up of a plurality of ion exchange resin columns polyphones.
6. according to claim 4 or 5 described a kind of methods of extracting the L-phenylalanine from fermented liquid, it is characterized in that: described ion exchange resin is strongly-acid ammonium type Zeo-karb.
7. a kind of method of extracting the L-phenylalanine from fermented liquid according to claim 4, it is characterized in that: described eluent is a 0.5mol/L ammoniacal liquor.
8. according to claim 4 or 7 described a kind of methods of from fermented liquid, extracting the L-phenylalanine, it is characterized in that: with described eluent with 2～4m
3The speed wash-out of/h.
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| CN200910234255A CN101709038A (en) | 2009-11-18 | 2009-11-18 | Method for extracting L-phenylalanine from fermentation broth |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102285895A (en) * | 2011-08-30 | 2011-12-21 | 无锡荣丰生物工程有限公司 | Triple-effect internal circulation continuous evaporation crystallization process of phenylalanine |
| 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 |
| CN102718671A (en) * | 2012-06-04 | 2012-10-10 | 江苏汉光生物工程有限公司 | Method for extracting L-phenylalanine from fermentation liquid |
| CN106986785A (en) * | 2017-01-14 | 2017-07-28 | 丽珠集团宁夏福兴制药有限公司 | A kind of L phenylalanines mother liquor reclaiming method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1425645A (en) * | 2002-12-23 | 2003-06-25 | 南京工业大学 | Film technological extracting method for L-phenylalanine |
| CN1541997A (en) * | 2003-04-30 | 2004-11-03 | 上海化工研究院 | Extraction process of 15N-L-phenylalanine |
| CN1629135A (en) * | 2004-06-10 | 2005-06-22 | 上海华震科技有限公司 | Method for separating L-phenylalanine from fermentation liquor |
-
2009
- 2009-11-18 CN CN200910234255A patent/CN101709038A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1425645A (en) * | 2002-12-23 | 2003-06-25 | 南京工业大学 | Film technological extracting method for L-phenylalanine |
| CN1541997A (en) * | 2003-04-30 | 2004-11-03 | 上海化工研究院 | Extraction process of 15N-L-phenylalanine |
| CN1629135A (en) * | 2004-06-10 | 2005-06-22 | 上海华震科技有限公司 | Method for separating L-phenylalanine from fermentation liquor |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102285895A (en) * | 2011-08-30 | 2011-12-21 | 无锡荣丰生物工程有限公司 | Triple-effect internal circulation continuous evaporation crystallization process of phenylalanine |
| CN102285895B (en) * | 2011-08-30 | 2013-08-07 | 无锡荣丰生物工程有限公司 | Triple-effect internal circulation continuous evaporation crystallization process of phenylalanine |
| 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 |
| CN102718671A (en) * | 2012-06-04 | 2012-10-10 | 江苏汉光生物工程有限公司 | Method for extracting L-phenylalanine from fermentation liquid |
| CN106986785A (en) * | 2017-01-14 | 2017-07-28 | 丽珠集团宁夏福兴制药有限公司 | A kind of L phenylalanines mother liquor reclaiming method |
| CN106986785B (en) * | 2017-01-14 | 2019-07-09 | 丽珠集团(宁夏)制药有限公司 | A kind of L-phenylalanine mother liquor reclaiming method |
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Application publication date: 20100519 |