CN111139273B - Method for preparing, separating and extracting L-tryptophan - Google Patents
Method for preparing, separating and extracting L-tryptophan Download PDFInfo
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- CN111139273B CN111139273B CN201911297165.9A CN201911297165A CN111139273B CN 111139273 B CN111139273 B CN 111139273B CN 201911297165 A CN201911297165 A CN 201911297165A CN 111139273 B CN111139273 B CN 111139273B
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- QIVBCDIJIAJPQS-VIFPVBQESA-N L-tryptophane Chemical compound C1=CC=C2C(C[C@H](N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-VIFPVBQESA-N 0.000 title claims abstract description 81
- 229960004799 tryptophan Drugs 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000000855 fermentation Methods 0.000 claims abstract description 81
- 230000004151 fermentation Effects 0.000 claims abstract description 81
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 238000013375 chromatographic separation Methods 0.000 claims abstract description 15
- 239000000919 ceramic Substances 0.000 claims abstract description 12
- 238000001035 drying Methods 0.000 claims abstract description 12
- 230000008569 process Effects 0.000 claims abstract description 8
- 238000005374 membrane filtration Methods 0.000 claims abstract description 7
- 238000001704 evaporation Methods 0.000 claims abstract description 6
- 230000008020 evaporation Effects 0.000 claims abstract description 6
- IFGCUJZIWBUILZ-UHFFFAOYSA-N sodium 2-[[2-[[hydroxy-(3,4,5-trihydroxy-6-methyloxan-2-yl)oxyphosphoryl]amino]-4-methylpentanoyl]amino]-3-(1H-indol-3-yl)propanoic acid Chemical compound [Na+].C=1NC2=CC=CC=C2C=1CC(C(O)=O)NC(=O)C(CC(C)C)NP(O)(=O)OC1OC(C)C(O)C(O)C1O IFGCUJZIWBUILZ-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000004042 decolorization Methods 0.000 claims abstract description 5
- 238000005119 centrifugation Methods 0.000 claims abstract description 3
- 235000015097 nutrients Nutrition 0.000 claims description 30
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 26
- OUYCCCASQSFEME-QMMMGPOBSA-N L-tyrosine Chemical compound OC(=O)[C@@H](N)CC1=CC=C(O)C=C1 OUYCCCASQSFEME-QMMMGPOBSA-N 0.000 claims description 19
- OUYCCCASQSFEME-UHFFFAOYSA-N tyrosine Natural products OC(=O)C(N)CC1=CC=C(O)C=C1 OUYCCCASQSFEME-UHFFFAOYSA-N 0.000 claims description 19
- SIKJAQJRHWYJAI-UHFFFAOYSA-N Indole Chemical compound C1=CC=C2NC=CC2=C1 SIKJAQJRHWYJAI-UHFFFAOYSA-N 0.000 claims description 18
- COLNVLDHVKWLRT-QMMMGPOBSA-N L-phenylalanine Chemical compound OC(=O)[C@@H](N)CC1=CC=CC=C1 COLNVLDHVKWLRT-QMMMGPOBSA-N 0.000 claims description 14
- 239000004202 carbamide Substances 0.000 claims description 14
- 229960005190 phenylalanine Drugs 0.000 claims description 13
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 12
- GFHNAMRJFCEERV-UHFFFAOYSA-L cobalt chloride hexahydrate Chemical compound O.O.O.O.O.O.[Cl-].[Cl-].[Co+2] GFHNAMRJFCEERV-UHFFFAOYSA-L 0.000 claims description 12
- 239000008103 glucose Substances 0.000 claims description 12
- COLNVLDHVKWLRT-UHFFFAOYSA-N phenylalanine Natural products OC(=O)C(N)CC1=CC=CC=C1 COLNVLDHVKWLRT-UHFFFAOYSA-N 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- SQUHHTBVTRBESD-UHFFFAOYSA-N Hexa-Ac-myo-Inositol Natural products CC(=O)OC1C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C1OC(C)=O SQUHHTBVTRBESD-UHFFFAOYSA-N 0.000 claims description 9
- PZOUSPYUWWUPPK-UHFFFAOYSA-N indole Natural products CC1=CC=CC2=C1C=CN2 PZOUSPYUWWUPPK-UHFFFAOYSA-N 0.000 claims description 9
- RKJUIXBNRJVNHR-UHFFFAOYSA-N indolenine Natural products C1=CC=C2CC=NC2=C1 RKJUIXBNRJVNHR-UHFFFAOYSA-N 0.000 claims description 9
- CDAISMWEOUEBRE-GPIVLXJGSA-N inositol Chemical compound O[C@H]1[C@H](O)[C@@H](O)[C@H](O)[C@H](O)[C@@H]1O CDAISMWEOUEBRE-GPIVLXJGSA-N 0.000 claims description 9
- 229960000367 inositol Drugs 0.000 claims description 9
- CDAISMWEOUEBRE-UHFFFAOYSA-N scyllo-inosotol Natural products OC1C(O)C(O)C(O)C(O)C1O CDAISMWEOUEBRE-UHFFFAOYSA-N 0.000 claims description 9
- 239000000706 filtrate Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- QDGAVODICPCDMU-UHFFFAOYSA-N 2-amino-3-[3-[bis(2-chloroethyl)amino]phenyl]propanoic acid Chemical compound OC(=O)C(N)CC1=CC=CC(N(CCCl)CCCl)=C1 QDGAVODICPCDMU-UHFFFAOYSA-N 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 5
- 239000002518 antifoaming agent Substances 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 238000004587 chromatography analysis Methods 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000000843 powder Substances 0.000 claims description 4
- 108090000623 proteins and genes Proteins 0.000 claims description 4
- 102000004169 proteins and genes Human genes 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
- 241000588724 Escherichia coli Species 0.000 claims description 3
- 239000003337 fertilizer Substances 0.000 claims description 3
- 239000001963 growth medium Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000010009 beating Methods 0.000 claims description 2
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 claims description 2
- 238000012258 culturing Methods 0.000 claims description 2
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- 238000011081 inoculation Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 21
- 239000012535 impurity Substances 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 34
- QIVBCDIJIAJPQS-UHFFFAOYSA-N Tryptophan Natural products C1=CC=C2C(CC(N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-UHFFFAOYSA-N 0.000 description 22
- 230000000694 effects Effects 0.000 description 15
- 229940024606 amino acid Drugs 0.000 description 12
- 239000002253 acid Substances 0.000 description 11
- -1 aromatic amino acid Chemical class 0.000 description 9
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 9
- 239000002609 medium Substances 0.000 description 9
- YBJHBAHKTGYVGT-ZKWXMUAHSA-N (+)-Biotin Chemical compound N1C(=O)N[C@@H]2[C@H](CCCCC(=O)O)SC[C@@H]21 YBJHBAHKTGYVGT-ZKWXMUAHSA-N 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- FPWMCUPFBRFMLH-UHFFFAOYSA-N prephenic acid Chemical compound OC1C=CC(CC(=O)C(O)=O)(C(O)=O)C=C1 FPWMCUPFBRFMLH-UHFFFAOYSA-N 0.000 description 6
- 102000003960 Ligases Human genes 0.000 description 5
- 108090000364 Ligases Proteins 0.000 description 5
- 229910001429 cobalt ion Inorganic materials 0.000 description 5
- XLJKHNWPARRRJB-UHFFFAOYSA-N cobalt(2+) Chemical compound [Co+2] XLJKHNWPARRRJB-UHFFFAOYSA-N 0.000 description 5
- 230000037361 pathway Effects 0.000 description 5
- RWZYAGGXGHYGMB-UHFFFAOYSA-N anthranilic acid Chemical compound NC1=CC=CC=C1C(O)=O RWZYAGGXGHYGMB-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 230000005764 inhibitory process Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 239000001763 2-hydroxyethyl(trimethyl)azanium Substances 0.000 description 3
- 235000019743 Choline chloride Nutrition 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 150000001413 amino acids Chemical class 0.000 description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 3
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 229960002685 biotin Drugs 0.000 description 3
- 235000020958 biotin Nutrition 0.000 description 3
- 239000011616 biotin Substances 0.000 description 3
- 229940041514 candida albicans extract Drugs 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 229960003178 choline chloride Drugs 0.000 description 3
- SGMZJAMFUVOLNK-UHFFFAOYSA-M choline chloride Chemical compound [Cl-].C[N+](C)(C)CCO SGMZJAMFUVOLNK-UHFFFAOYSA-M 0.000 description 3
- ZPWVASYFFYYZEW-UHFFFAOYSA-L dipotassium hydrogen phosphate Chemical compound [K+].[K+].OP([O-])([O-])=O ZPWVASYFFYYZEW-UHFFFAOYSA-L 0.000 description 3
- 229910000396 dipotassium phosphate Inorganic materials 0.000 description 3
- 235000019797 dipotassium phosphate Nutrition 0.000 description 3
- 239000003797 essential amino acid Substances 0.000 description 3
- 235000020776 essential amino acid Nutrition 0.000 description 3
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 description 3
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 description 3
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- LWIHDJKSTIGBAC-UHFFFAOYSA-K potassium phosphate Substances [K+].[K+].[K+].[O-]P([O-])([O-])=O LWIHDJKSTIGBAC-UHFFFAOYSA-K 0.000 description 3
- 230000035755 proliferation Effects 0.000 description 3
- 239000012138 yeast extract Substances 0.000 description 3
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- 108010082495 Dietary Plant Proteins Proteins 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 2
- PVNIIMVLHYAWGP-UHFFFAOYSA-N Niacin Chemical compound OC(=O)C1=CC=CN=C1 PVNIIMVLHYAWGP-UHFFFAOYSA-N 0.000 description 2
- 239000003674 animal food additive Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- SEOVTRFCIGRIMH-UHFFFAOYSA-N indole-3-acetic acid Chemical compound C1=CC=C2C(CC(=O)O)=CNC2=C1 SEOVTRFCIGRIMH-UHFFFAOYSA-N 0.000 description 2
- 230000002503 metabolic effect Effects 0.000 description 2
- 239000002207 metabolite Substances 0.000 description 2
- 230000028327 secretion Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- QZAYGJVTTNCVMB-UHFFFAOYSA-N serotonin Chemical compound C1=C(O)C=C2C(CCN)=CNC2=C1 QZAYGJVTTNCVMB-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 108010080376 3-Deoxy-7-Phosphoheptulonate Synthase Proteins 0.000 description 1
- 241000251468 Actinopterygii Species 0.000 description 1
- FFEARJCKVFRZRR-BYPYZUCNSA-N L-methionine Chemical compound CSCC[C@H](N)C(O)=O FFEARJCKVFRZRR-BYPYZUCNSA-N 0.000 description 1
- KDXKERNSBIXSRK-UHFFFAOYSA-N Lysine Natural products NCCCCC(N)C(O)=O KDXKERNSBIXSRK-UHFFFAOYSA-N 0.000 description 1
- 239000004472 Lysine Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 229930013930 alkaloid Natural products 0.000 description 1
- 150000003797 alkaloid derivatives Chemical class 0.000 description 1
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- 239000003617 indole-3-acetic acid Substances 0.000 description 1
- 125000001041 indolyl group Chemical group 0.000 description 1
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- 229930182817 methionine Natural products 0.000 description 1
- 210000000653 nervous system Anatomy 0.000 description 1
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- 235000001968 nicotinic acid Nutrition 0.000 description 1
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- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
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- 230000001954 sterilising effect Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 235000019605 sweet taste sensations Nutrition 0.000 description 1
- 229940125725 tranquilizer Drugs 0.000 description 1
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- 238000002834 transmittance Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P13/00—Preparation of nitrogen-containing organic compounds
- C12P13/04—Alpha- or beta- amino acids
- C12P13/22—Tryptophan; Tyrosine; Phenylalanine; 3,4-Dihydroxyphenylalanine
- C12P13/227—Tryptophan
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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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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
- C12N1/20—Bacteria; Culture media therefor
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- General Engineering & Computer Science (AREA)
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- Chemical Kinetics & Catalysis (AREA)
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Abstract
The invention belongs to the technical field of L-tryptophan production, and discloses a method for preparing, separating and extracting L-tryptophan, which is characterized by comprising the following steps: step 1) fermentation, step 2) ceramic membrane filtration, step 3) chromatographic separation, step 4) decolorization, step 5) concentration and evaporation, and step 6) centrifugation and drying. The L-tryptophan feed liquid is subjected to the processes of ceramic membrane filtration, sequential simulated moving bed chromatographic separation, decoloration in a decoloration tank and the like, so that the impurities in the feed liquid are greatly removed, and the purity and the yield of the product are greatly improved.
Description
Technical Field
The invention belongs to the technical field of L-tryptophan production, and particularly relates to a method for preparing, separating and extracting L-tryptophan.
Background
L-tryptophan has the molecular formula C11H12O2N2Molecular weight 204.21, nitrogen content 13.72%. L-tryptophan is neutral aromatic amino acid containing indolyl, has silky luster, hexagonal flaky self-color crystal, no odor, sweet taste, water solubility of 1.14g/L (25 deg.C), solubility in dilute acid or dilute alkali, stability in alkaline solution, decomposition in strong acid, slight solubility in ethanol, and insolubility in chloroform and diethyl ether.
L-tryptophan is one of eight essential amino acids in human and animal life activities, plays an important role in growth, development and metabolism of human and animals, and is called as a second essential amino acid. In vivo, from L-tryptophan, bioactive substances such as 5-hydroxytryptamine, indoleacetic acid, nicotinic acid, pigment, alkaloid, coenzyme and the like can be synthesized. It is mainly used in medicine in clinic, and its content in nervous system is related to nervous excitement and inhibition state, so as to promote sleep and tranquilization, and can be used as health food and tranquilizer. L-tryptophan is also a relatively deficient amino acid in some vegetable proteins, and the enhancement of food and feed additives by using it has an important effect on improving the utilization rate of the vegetable proteins. It is the third largest feed additive amino acid after methionine and lysine. In addition, the L-tryptophan has the functions of preventing mildew, sterilizing and preventing oxidation, and can be used as a fish preservative.
In recent years, L-tryptophan has been expensive as an essential amino acid, and is often restricted by production costs in industrial production, and among the constitution of production costs, the costs of production, separation and extraction, etc. are the most important. Therefore, the research on the method for improving the production and extraction yield of the L-tryptophan has important theoretical significance and practical value.
Disclosure of Invention
The previous patent technology of the applicant optimizes the fermentation process by 'a method for improving the production efficiency of L-tryptophan', and improves the fermentation efficiency. On the basis, the applicant further performs separation and extraction to obtain the L-tryptophan product with high purity and high yield.
In order to solve the above problems, the present invention provides a method for preparing, isolating and extracting L-tryptophan.
The invention is realized by the following technical scheme.
A method for preparing, isolating and extracting L-tryptophan, comprising the steps of: step 1) fermentation, step 2) ceramic membrane filtration, step 3) chromatographic separation, step 4) decolorization, step 5) concentration and evaporation, and step 6) centrifugation and drying.
Specifically, the method comprises the following steps:
step 1) fermentation: inoculating Escherichia coli seed liquid producing L-tryptophan with an inoculum size of 5-12% into a fermentation tank filled with fermentation culture medium, culturing at 36-37 deg.C with dissolved oxygen of 20-30%, maintaining the pH of the system in the tank at 6.8-7.2 by numerical control automatic feeding ammonia water, and defoaming by feeding defoaming agent; the total fermentation time is 40-42h, and fermentation liquor is obtained;
step 2) ceramic membrane filtration: heating the fermentation liquor to 50 ℃, filtering by a ceramic membrane, collecting filtrate, and carrying out plate-and-frame filter pressing and drying on retentate to obtain feed protein powder;
step 3) chromatographic separation: performing chromatographic separation on the filtrate obtained in the step 2) by a sequential simulated moving bed to obtain an extracting solution, and uniformly beating waste liquid generated in the chromatographic separation process to a fertilizer workshop for treatment;
step 4), decoloring: the extracting solution obtained by chromatographic separation enters a decoloring tank for decoloring;
step 5), concentration and evaporation: feeding the decolorized solution obtained in the step 4) into a double-effect evaporator to obtain a concentrated solution;
step 6), centrifuging and drying: crystallizing, centrifuging and drying the concentrated solution to obtain the high-purity L-tryptophan.
Preferably, the step 1) of fermentation further comprises the following steps:
when the fermentation time is 12 hours, feeding the nutrient solution A into the fermentation tank until the fermentation is finished;
when the fermentation time is 24 hours, feeding the nutrient solution B into the tank until the fermentation is finished;
the component of the nutrient solution A comprises cobalt chloride hexahydrate;
the nutrient solution B comprises glucose, indole, inositol, phenylalanine and tyrosine.
Preferably, in the step 2), the molecular weight cut-off of the ceramic membrane is 1 ten thousand Da, and the filtering temperature is 50 ℃.
Preferably, the parameters of the sequential simulated moving bed chromatography are as follows: flow rate of 5m3H, temperature 50 ℃ and differential pressure 0.5 MPa.
Preferably, the components of the nutrient solution a include cobalt chloride hexahydrate and urea.
More preferably, the nutrient solution A comprises the following components: 10-30mg/L of cobalt chloride hexahydrate, 5-20g/L of urea and the balance of water.
More preferably, the nutrient solution B comprises the following components: 100g/L glucose, 1g/L indole, 0.5g/L inositol, 0.3-0.8g/L phenylalanine, 0.2-0.7g/L tyrosine, and the balance water.
Most preferably, the nutrient solution A comprises the following components: 20mg/L of cobalt chloride hexahydrate, 10g/L of urea and the balance of water.
Most preferably, the nutrient solution B comprises the following components: 100g/L glucose, 1g/L indole, 0.5g/L inositol, 0.5g/L phenylalanine, 0.4g/L tyrosine, and the balance water.
The technical scheme of the invention has the following outstanding advantages and uniqueness:
the invention starts from the pathway of synthesizing aromatic amino acid by escherichia coli, adopts various modes to regulate metabolic pathways, and improves the yield and acid production rate of tryptophan by mutual synergy;
according to the invention, phenylalanine and tyrosine are added in the middle stage of fermentation, and the yield of aromatic amino acid is in the process of rapid accumulation, so that the feedback inhibition effect on the conversion of the mycolic acid to the prephenate is generated, and the mycolic acid flows to the anthranilic acid way more, so that the yield of tryptophan is increased;
the research shows that the addition of cobalt ions in the initial fermentation stage has a limited effect on the activity of the DAHP synthase and cannot improve the yield of tryptophan, and that the aromatic amino acid synthesis pathway is not started in the initial fermentation stage, and the secretion amount of the enzyme is relatively small, so that the cobalt ions are added at the time point of synthesizing a large amount of tryptophan, and the yield of tryptophan can be effectively improved.
The urea is added at the initial stage of fermentation, is mainly used as an inorganic nitrogen source for the proliferation of the strain, does not influence the activity of the DAHP synthetase, and is slowly proliferated when the fermentation is carried out for 12 hours, so that the activity of the DAHP synthetase can be improved by mainly using synthetic metabolites, the metabolic flux of an aromatic amino acid synthetic pathway is promoted to be increased, and the yield of tryptophan is promoted to be increased.
The invention adopts the sequential simulated moving bed chromatography technology to extract the L-tryptophan, compared with the traditional three-series ion exchange method, the acid-base consumption and the water consumption are greatly reduced, the exchange medium resin can be regenerated and reused in the production process, the production process is energy-saving and environment-friendly, and the environmental pollution is reduced.
The waste liquid produced in the production process is prepared into the feed protein powder and the organic fertilizer, and the whole production process has no pollutant discharge and is green and environment-friendly.
The L-tryptophan feed liquid is subjected to processes such as ceramic membrane filtration, sequential simulated moving bed chromatographic separation, decoloration in a decoloration tank and the like, so that salt and other amino acids are greatly removed, and the purity and yield of the product are greatly improved.
Drawings
FIG. 1: the effect of phenylalanine and tyrosine on tryptophan production;
FIG. 2: the influence of phenylalanine and tyrosine on the fermentation acid production rate;
FIG. 3: the effect of cobalt chloride hexahydrate concentration on tryptophan yield;
FIG. 4: influence of urea concentration on tryptophan production.
Detailed Description
Those skilled in the art can modify the process parameters appropriately to achieve the desired results with reference to the disclosure herein. It is expressly intended that all such similar substitutes and modifications which would be obvious to one skilled in the art are deemed to be included in the invention. While the products and methods of this invention have been described in terms of preferred embodiments, it will be apparent to those of skill in the art that variations and modifications, or appropriate alterations and combinations, of the products and methods described herein may be made and utilized without departing from the spirit, scope, and spirit of the invention. For a further understanding of the present invention, reference will now be made in detail to the following examples.
Example 1
A method for improving the production efficiency of L-tryptophan comprises the following steps:
the fermentation medium comprises the following components: 20g/L of glucose, 9g/L of dipotassium phosphate, 5g/L of yeast extract, 4.6g/L of citric acid, 1.8g/L of ammonium sulfate, 1.6g/L of magnesium sulfate heptahydrate, 0.4g/L of choline chloride, 65mg/L of ferrous sulfate heptahydrate and 0.2mg/L of biotin; the nutrient solution A comprises the following components: 20mg/L of cobalt chloride hexahydrate and 10g/L of urea;
the nutrient solution B comprises the following components: 100g/L glucose, 1g/L indole, 0.5g/L inositol, 0.5g/L phenylalanine, 0.4g/L tyrosine;
col, E.coliFor example, i TRTH, the seed liquid (OD) was inoculated at 8%600Value of 11.2) is inoculated into a 1000L fermentation tank filled with 600L fermentation medium, the culture temperature is 36.8 ℃, the dissolved oxygen is 20 percent, the pH value of the system in the tank is maintained between 7.0 and 7.2 by numerical control automatic feeding of 25 percent ammonia water, and defoaming is carried out by feeding defoaming agent; the total fermentation time is 42h, and L-tryptophan fermentation liquor is obtained.
When the fermentation time is 12 hours, feeding the nutrient solution A into the fermentation tank, wherein the feeding speed is 0.01ml/min per L of fermentation solution until the fermentation is finished;
when the fermentation time is 24 hours, the nutrient solution B is fed into the tank, and the sugar concentration in the tank is maintained to be 1g/L until the fermentation is finished.
Example 2
A method for improving the production efficiency of L-tryptophan comprises the following steps:
the fermentation medium comprises the following components: 20g/L of glucose, 9g/L of dipotassium phosphate, 5g/L of yeast extract, 4.6g/L of citric acid, 1.8g/L of ammonium sulfate, 1.6g/L of magnesium sulfate heptahydrate, 0.4g/L of choline chloride, 65mg/L of ferrous sulfate heptahydrate and 0.2mg/L of biotin;
the nutrient solution A comprises the following components: 30mg/L of cobalt chloride hexahydrate and 15g/L of urea;
the nutrient solution B comprises the following components: 100g/L glucose, 1g/L indole, 0.5g/L inositol, 0.4g/L phenylalanine, 0.3g/L tyrosine;
coli TRTH, the seed liquid (OD) was inoculated at 8%600Value of 11.8) is inoculated into a 1000L fermentation tank filled with 600L fermentation medium, the culture temperature is 36.8 ℃, the dissolved oxygen is 20 percent, the pH value of the system in the tank is maintained between 7.0 and 7.2 by numerical control automatic feeding of 25 percent ammonia water, and defoaming is carried out by feeding defoaming agent; the total fermentation time is 40h, and the L-tryptophan fermentation liquor is obtained.
When the fermentation time is 12 hours, feeding the nutrient solution A into the fermentation tank, wherein the feeding speed is 0.008ml/min per L of fermentation solution until the fermentation is finished;
when the fermentation time is 24 hours, the nutrient solution B is fed into the tank, and the sugar concentration in the tank is maintained to be 1g/L until the fermentation is finished.
Comparative example 1
A method for improving the production efficiency of L-tryptophan comprises the following steps:
the fermentation medium comprises the following components: 20g/L of glucose, 9g/L of dipotassium phosphate, 5g/L of yeast extract, 4.6g/L of citric acid, 1.8g/L of ammonium sulfate, 1.6g/L of magnesium sulfate heptahydrate, 0.4g/L of choline chloride, 65mg/L of ferrous sulfate heptahydrate and 0.2mg/L of biotin;
the nutrient solution comprises the following components: 100g/L glucose, 1g/L indole and 0.5g/L inositol;
coli TRTH, the seed liquid (OD) was inoculated at 8%600Value of 11.2) is inoculated into a 1000L fermentation tank filled with 600L fermentation medium, the culture temperature is 36.8 ℃, the dissolved oxygen is 20 percent, the pH value of the system in the tank is maintained between 7.0 and 7.2 by numerical control automatic feeding of 25 percent ammonia water, and defoaming is carried out by feeding defoaming agent; the total fermentation time is 42h, and L-tryptophan fermentation liquor is obtained.
When the fermentation time is 24 hours, nutrient solution flow is added into the tank, and the sugar concentration in the tank is maintained to be 1g/L until the fermentation is finished.
Example 3
A method for separating and extracting L-tryptophan, comprising the steps of:
1) take the fermentation broth prepared in example 1 as an example;
2) heating the fermentation liquor to 50 ℃, filtering by a ceramic membrane, wherein the molecular weight cutoff is 1 ten thousand Da, the filtering temperature is 50 ℃, the pressure is 1.5Mpa, the filtrate enters an extraction process, and the feed protein powder is obtained by press-filtering and drying the cutoff substance by a plate frame.
3) Separating the filtrate obtained in the step 2) by a sequential simulated moving bed chromatography to obtain an extracting solution, wherein the sequential simulated moving bed chromatography control parameters are as follows: flow rate of 5m3H, the temperature is 50 ℃, and the pressure difference is 0.5 MPa; the waste liquid generated in the chromatographic separation process is treated in a fertilizer workshop all the time.
4) And (4) performing decolorization on the extract after chromatographic separation, starting to use a decolorization tank to reflux decolorized liquid until the decolorized liquid is clear, and after the light transmittance of the filtrate reaches 50%, putting the clear liquid into a clear liquid temporary storage tank for later use.
5) And (3) feeding the clear liquid obtained in the step 4) into a double-effect evaporator, and concentrating by 3 times to obtain a concentrated solution.
6) Crystallizing, centrifuging and drying the concentrated solution to obtain the high-purity L-tryptophan.
The measured L-tryptophan index is as follows:
l-tryptophan content: 99.4% specific rotation [ α ]: -31.3
pH value: 6.5 loss on drying: 0.3
Coarse ash content: 0.4
Example 4
The influence of phenylalanine and tyrosine on the yield of tryptophan and the fermentation acid production rate is verified, and the method 1: adding phenylalanine 0.5g/L and tyrosine 0.4g/L into a fermentation culture medium; mode 2: adding 0.5g/L phenylalanine and 0.4g/L tyrosine into the nutrient solution; as shown in figure 1, in the mode 2, phenylalanine and tyrosine are added into the nutrient solution, the yield of tryptophan and the fermentation acid production rate are both higher than those in the mode 1, the nutrient solution is added in the middle stage of fermentation, at the moment, the yield of aromatic amino acid is in the process of rapid accumulation, and the phenylalanine and tyrosine are added, so that the feedback inhibition effect on the conversion of the mycolic acid to the prephenate is generated, the mycolic acid flows to the anthranilic acid path more, and the yield of tryptophan is improved; on the other hand, the mode 1 is added into the fermentation medium, the accumulation of aromatic amino acids is less in the early stage of fermentation, the feedback inhibition of the phenylalanine and the tyrosine on the conversion of the mycolic acid into the prephenate is not started, and the phenylalanine and the tyrosine are added at the moment and absorbed and utilized by the bacterial cells, so that the positive regulation effect on the tryptophan synthesis is not good.
On the basis of the research, phenylalanine and tyrosine are added into the nutrient solution B; further discussing the influence of cobalt chloride hexahydrate on the yield of tryptophan; the research shows that the addition of cobalt ions in the initial fermentation stage has limited influence on the activity of the DAHP synthetase, the yield of tryptophan cannot be improved, the initial fermentation stage is possible, the aromatic amino acid synthesis pathway is not started, and the enzyme secretion amount is relatively small; therefore, the cobalt ions are added at the time point of mass synthesis of tryptophan, considering that the addition of an overlarge amount of nutrient solution can cause dilution effect on the fermentation liquor, the flow rate is set to be 0.01ml/min per L of the fermentation liquor, and the concentration is set to be 1,2.5,5,10,20,30,40,60 and 80(mg/L) respectively at the flow rate; as shown in FIG. 3, the yield of tryptophan is improved with the increase of the concentration of cobalt chloride hexahydrate, the influence on tryptophan is the greatest when the concentration is 20-30mg/L, the increase of the concentration is not obviously changed, the yield of tryptophan is reduced to some extent when the concentration is more than 60mg/L, and the growth of the strain is possibly inhibited by excessive cobalt ions.
Selecting the concentration of cobalt chloride hexahydrate to be 20mg/L, and when the adding time is to ferment for 12 hours, the feeding speed is 0.01ml/min per L of fermentation liquor; the applicant tries to add urea into a fermentation medium without affecting the tryptophan yield, urea is added in the initial stage of fermentation and mainly used as an inorganic nitrogen source for strain proliferation without affecting the activity of DAHP synthetase, and when the fermentation is carried out for 12 hours, the strain proliferation is slowed, and at the moment, mainly synthetic metabolites are added, the activity of the DAHP synthetase can be improved by adding urea, so that the metabolic flux of an aromatic amino acid synthetic pathway is increased, the increase of the tryptophan yield is promoted, and the urea concentrations are respectively set to be 1,5,10,15,20,25 and 30 (g/L); as shown in FIG. 4, tryptophan production increased all the more with increasing urea concentration, with a 10g/L increase followed by a slower increase and then a plateau.
While the invention has been described with reference to specific embodiments, it will be apparent to those skilled in the art that the invention is not limited thereto, and that various changes and modifications can be made without departing from the spirit and scope of the invention.
Claims (5)
1. A method for preparing, isolating and extracting L-tryptophan, comprising the steps of: step 1) fermentation, step 2) ceramic membrane filtration, step 3) chromatographic separation, step 4) decolorization, step 5) concentration and evaporation, and step 6) centrifugation and drying;
the method comprises the following steps:
step 1) fermentation: inoculating Escherichia coli seed solution capable of producing L-tryptophan into a fermentation tank filled with fermentation culture medium at an inoculation amount of 5-12%, culturing at 36-37 deg.C with dissolved oxygen of 20-30%, maintaining system pH at 6.8-7.2 by adding ammonia water, and defoaming by adding defoaming agent; the total fermentation time is 40-42h, and fermentation liquor is obtained;
step 2) ceramic membrane filtration: heating the fermentation liquor to 50 ℃, filtering by a ceramic membrane, collecting filtrate, and carrying out plate-and-frame filter pressing and drying on retentate to obtain feed protein powder;
step 3) chromatographic separation: performing chromatographic separation on the filtrate obtained in the step 2) by a sequential simulated moving bed to obtain an extracting solution, and uniformly beating waste liquid generated in the chromatographic separation process to a fertilizer workshop for treatment;
step 4), decoloring: the extracting solution obtained by chromatographic separation enters a decoloring tank for decoloring;
step 5), concentration and evaporation: feeding the decolorized solution obtained in the step 4) into a double-effect evaporator for evaporation and concentration to obtain a concentrated solution;
step 6), centrifuging and drying: crystallizing, centrifuging and drying the concentrated solution to obtain high-purity L-tryptophan;
the step 1) of fermentation further comprises the following steps:
when the fermentation time is 12 hours, feeding the nutrient solution A into the fermentation tank, wherein the feeding speed is 0.01ml/min per L of fermentation solution until the fermentation is finished;
when the fermentation time is 24 hours, feeding the nutrient solution B into the tank, and maintaining the sugar concentration in the tank to be 1g/L until the fermentation is finished;
the nutrient solution A comprises the following components: 10-30mg/L of cobalt chloride hexahydrate, 5-20g/L of urea and the balance of water;
the nutrient solution B comprises glucose, indole, inositol, phenylalanine and tyrosine, and comprises the following components: 100g/L glucose, 1g/L indole, 0.5g/L inositol, 0.3-0.8g/L phenylalanine, 0.2-0.7g/L tyrosine, and the balance water.
2. The method according to claim 1, wherein in step 2), the ceramic membrane has a molecular weight cut-off of 1 ten thousand Da and a filtration temperature of 50 ℃.
3. The method according to claim 1, wherein the parameters of the sequential simulated moving bed chromatography are: flow rate of 5m3H, temperature 50 ℃ and differential pressure 0.5 MPa.
4. The method according to claim 1, wherein the nutrient solution a comprises the following components: 20mg/L of cobalt chloride hexahydrate, 10g/L of urea and the balance of water.
5. The method according to claim 1, wherein the nutrient solution B comprises the following components: 100g/L glucose, 1g/L indole, 0.5g/L inositol, 0.5g/L phenylalanine, 0.4g/L tyrosine, and the balance water.
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Application publication date: 20200512 Assignee: QIQIHAR LONGJIANG FUFENG BIOTECHNOLOGY CO.,LTD. Assignor: XINJIANG FUFENG BIOTECHNOLOGY Co.,Ltd. Contract record no.: X2023980054726 Denomination of invention: A method for preparing, separating, and extracting L-tryptophan Granted publication date: 20211207 License type: Common License Record date: 20231229 |