CN1865230A - Method for extracting L-threonine from fermentation liquor - Google Patents
Method for extracting L-threonine from fermentation liquor Download PDFInfo
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- CN1865230A CN1865230A CN 200610014342 CN200610014342A CN1865230A CN 1865230 A CN1865230 A CN 1865230A CN 200610014342 CN200610014342 CN 200610014342 CN 200610014342 A CN200610014342 A CN 200610014342A CN 1865230 A CN1865230 A CN 1865230A
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- threonine
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- AYFVYJQAPQTCCC-GBXIJSLDSA-N L-threonine Chemical compound C[C@@H](O)[C@H](N)C(O)=O AYFVYJQAPQTCCC-GBXIJSLDSA-N 0.000 title claims abstract description 146
- 239000004473 Threonine Substances 0.000 title claims abstract description 74
- 229960002898 threonine Drugs 0.000 title claims abstract description 74
- 238000000855 fermentation Methods 0.000 title claims abstract description 44
- 230000004151 fermentation Effects 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000013078 crystal Substances 0.000 claims abstract description 20
- 239000002184 metal Substances 0.000 claims abstract description 14
- 238000000605 extraction Methods 0.000 claims abstract description 8
- 238000005374 membrane filtration Methods 0.000 claims abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract 6
- 238000004042 decolorization Methods 0.000 claims abstract 4
- 239000012528 membrane Substances 0.000 claims description 30
- 238000001471 micro-filtration Methods 0.000 claims description 14
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 239000012452 mother liquor Substances 0.000 claims description 8
- AYFVYJQAPQTCCC-UHFFFAOYSA-N Threonine Natural products CC(O)C(N)C(O)=O AYFVYJQAPQTCCC-UHFFFAOYSA-N 0.000 claims description 4
- 239000012141 concentrate Substances 0.000 claims description 4
- 239000012153 distilled water Substances 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 239000010935 stainless steel Substances 0.000 claims description 4
- 238000010612 desalination reaction Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 238000000909 electrodialysis Methods 0.000 claims description 2
- 238000005342 ion exchange Methods 0.000 claims description 2
- 238000001728 nano-filtration Methods 0.000 claims description 2
- 230000001954 sterilising effect Effects 0.000 claims description 2
- 239000000243 solution Substances 0.000 claims 2
- 238000003756 stirring Methods 0.000 claims 2
- 108010077805 Bacterial Proteins Proteins 0.000 claims 1
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- 238000004064 recycling Methods 0.000 claims 1
- 239000011550 stock solution Substances 0.000 claims 1
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- 239000000047 product Substances 0.000 abstract description 9
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- 229940024606 amino acid Drugs 0.000 abstract description 5
- 150000001413 amino acids Chemical class 0.000 abstract description 5
- 241000894006 Bacteria Species 0.000 abstract description 4
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- 108090000623 proteins and genes Proteins 0.000 description 8
- 102000004169 proteins and genes Human genes 0.000 description 8
- 230000009467 reduction Effects 0.000 description 8
- 230000007306 turnover Effects 0.000 description 8
- FRXSZNDVFUDTIR-UHFFFAOYSA-N 6-methoxy-1,2,3,4-tetrahydroquinoline Chemical compound N1CCCC2=CC(OC)=CC=C21 FRXSZNDVFUDTIR-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
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- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Chemical compound NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 description 4
- 235000001014 amino acid Nutrition 0.000 description 4
- 235000013339 cereals Nutrition 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000004471 Glycine Substances 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
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- 238000001179 sorption measurement Methods 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 1
- 241000238557 Decapoda Species 0.000 description 1
- 208000004930 Fatty Liver Diseases 0.000 description 1
- 241000287828 Gallus gallus Species 0.000 description 1
- 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 description 1
- 206010019708 Hepatic steatosis Diseases 0.000 description 1
- 206010020751 Hypersensitivity Diseases 0.000 description 1
- QIVBCDIJIAJPQS-VIFPVBQESA-N L-tryptophane Chemical compound C1=CC=C2C(C[C@H](N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-VIFPVBQESA-N 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
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- 108010013296 Sericins Proteins 0.000 description 1
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- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- QIVBCDIJIAJPQS-UHFFFAOYSA-N Tryptophan Natural products C1=CC=C2C(CC(N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-UHFFFAOYSA-N 0.000 description 1
- 239000006035 Tryptophane Substances 0.000 description 1
- WDJHALXBUFZDSR-UHFFFAOYSA-M acetoacetate Chemical compound CC(=O)CC([O-])=O WDJHALXBUFZDSR-UHFFFAOYSA-M 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000005576 amination reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- WZPBZJONDBGPKJ-VEHQQRBSSA-N aztreonam Chemical compound O=C1N(S([O-])(=O)=O)[C@@H](C)[C@@H]1NC(=O)C(=N/OC(C)(C)C(O)=O)\C1=CSC([NH3+])=N1 WZPBZJONDBGPKJ-VEHQQRBSSA-N 0.000 description 1
- 229960003644 aztreonam Drugs 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- 239000005018 casein Substances 0.000 description 1
- BECPQYXYKAMYBN-UHFFFAOYSA-N casein, tech. Chemical compound NCCCCC(C(O)=O)N=C(O)C(CC(O)=O)N=C(O)C(CCC(O)=N)N=C(O)C(CC(C)C)N=C(O)C(CCC(O)=O)N=C(O)C(CC(O)=O)N=C(O)C(CCC(O)=O)N=C(O)C(C(C)O)N=C(O)C(CCC(O)=N)N=C(O)C(CCC(O)=N)N=C(O)C(CCC(O)=N)N=C(O)C(CCC(O)=O)N=C(O)C(CCC(O)=O)N=C(O)C(COP(O)(O)=O)N=C(O)C(CCC(O)=N)N=C(O)C(N)CC1=CC=CC=C1 BECPQYXYKAMYBN-UHFFFAOYSA-N 0.000 description 1
- 235000021240 caseins Nutrition 0.000 description 1
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- 210000004027 cell Anatomy 0.000 description 1
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- 238000009295 crossflow filtration Methods 0.000 description 1
- 239000008121 dextrose Substances 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 235000013681 dietary sucrose Nutrition 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 208000010706 fatty liver disease Diseases 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
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- 229920002401 polyacrylamide Polymers 0.000 description 1
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- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
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- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 210000001082 somatic cell Anatomy 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000011146 sterile filtration Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229960004793 sucrose Drugs 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229960004799 tryptophan Drugs 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
一种从发酵液中分离提取L－苏氨酸的方法。解决现有分离提取方法，菌体去除率和产品质量不高的问题。本发明包括：L－苏氨酸发酵液经灭菌后进行金属膜过滤、活性炭脱色、浓缩、结晶等操作步骤，对目标产物进行分离提取，得到精制L－苏氨酸结晶，L－苏氨酸的提取收率大于85％，经氨基酸分析仪分析纯度可达98.5％以上。本发明采用金属膜过滤菌体，改变了常规发酵液处理采用的离心、压滤机压滤等方法，降低了维修费用，降低了工人的劳动强度，除去菌体彻底，过滤液澄清透明；且金属膜使用寿命长，耐高温、耐酸碱、易于清洗且装置维护方便，投资少。提取过程全部采用物理分离方法，过程中消耗的酸、碱及蒸汽低，提取成本大为降低。A method for separating and extracting L-threonine from fermentation broth. It solves the problems of the existing separation and extraction methods, the removal rate of bacteria and the low quality of products. The invention includes: after the L-threonine fermentation liquid is sterilized, the operation steps such as metal membrane filtration, activated carbon decolorization, concentration and crystallization are carried out, and the target product is separated and extracted to obtain refined L-threonine crystals, L-threonine The extraction yield of the acid is greater than 85%, and the purity can reach more than 98.5% through the analysis of an amino acid analyzer. The present invention adopts the metal film to filter the bacteria, changes the centrifugation, filter press filtration and other methods used in the conventional fermentation liquid treatment, reduces the maintenance cost, reduces the labor intensity of the workers, removes the bacteria completely, and the filtrate is clear and transparent; and The metal film has a long service life, high temperature resistance, acid and alkali resistance, easy cleaning and device maintenance, and less investment. The extraction process all adopts physical separation method, the consumption of acid, alkali and steam in the process is low, and the extraction cost is greatly reduced.
Description
[technical field]: originally relate to a kind of L-Threonine extraction process in the producing l-threonine by fermentation process, belong to technical field of producing amino acid by fermentation.
[background technology]: the L-Threonine is a necessary seed amino acid in people and the animal body, and self can not synthesize, and must absorb from food, and it is widely used in fodder industry, protective foods and medicine industry as foodstuff additive.
The L-Threonine gets main application: (1) is a kind of important nutrition-fortifying agent, can intensified cereal, cake, milk-product, and the same with tryptophane have a recovery human-body fatigue, promotes the effect of growing; (2) owing to contain hydroxyl, human body skin is had the water holding effect, combine with oligonucleotide chain, the protection cytolemma is played an important role, can promote the synthetic and Fatty Acid Oxidation of phosphatide in vivo, its preparation has the medicinal usefulness of human development's anti-fatty liveranti-fatty liver of promotion, is a composition in the aminoacids complex transfusion; (3) be to make efficient low microbiotic hypersensitive---the raw material of monobactam.(4) be used to add pig starter feed, kind pig feed, broiler fodder, prawn feed and eel feed etc.
The production method of L-Threonine mainly contains three kinds of albumen hydrolysis, chemical synthesis and fermentation methods.Albumen hydrolysis be with casein, silk-protein, sericin with acid or alkali and enzymic hydrolysis after, in the uncommon acid of fourth,, carry out amination with ammonia again with the methanol solution effect of bromine, separate and get through ion exchange resin.This is a kind of traditional amino acid production method, but adopts less at present.Chemical synthesis is to be that raw material synthesizes with Ba Dousuan, acetoacetate or glycine, in the concrete reaction according to used medium difference, two kinds of synthesis modes of water react and nonaqueous phase reaction are arranged again, wherein are that the operational path of raw material is short, product yield is high with the glycine.It is low that fermentation method utilizes Production by Microorganism Fermentation L-Threonine to have a raw materials cost, and reaction conditions is gentle and easily realize advantage such as scale operation, is a kind of very economical production method.Fermentation method is that the employing dextrose plus saccharose is a raw material, and re-refining to extract after fermentation obtains finished product.It is the main method of present suitability for industrialized production Threonine.
Exist a large amount of thalline and foreign protein in the L-threonine fermentation liquid, the existence of these materials descends L-Threonine yield and crystalline quality.Therefore, before carrying out the separation of L-Threonine, must be removed earlier.L-threonine fermentation liquid viscosity is big, and the bacterium somatic cells is little, is difficult to sedimentation, and the centrifuging energy consumption is big, trivial operations, and speed is slow, and investment is big, this experimental selection of factor membrane filtering method of comprehensive each side.
Membrane separation technique is development in recent years emerging high efficient separation technology faster.Along with updating and the expansion of Application Areas of mould material, membrane separation unit, membrane separation technique has become the important chemical unit operation, is causing the major transformation of isolation technique.Metallic membrane demonstrates huge development potentiality at the aspects such as high gas purification, gas phase separation, sterile filtration and little (surpassing) filter in fields such as ultrapure separation, catalytic reaction, biological environmental production and electronics, nuclear energy, medicine, food.
The filter method that often uses has microfiltration method, ultrafiltration process, tubular fibre membrane filtration, ceramic membrane filter and metal membrane filter at present.Remove cell debris with microfiltration method and hollow-fibre membrane, easily produce film and block.There is a spot of monomer in the polyacrylamide flocculant, has certain toxicity, be not suitable for food and medicine.At present, traditional in the industry separating and extracting method, thallus removing rate are not high, and quality product is not high.
[summary of the invention]: main purpose of the present invention is to solve existing separating and extracting method, and the problem that thallus removing rate and quality product are not high provides a kind of method of utilizing metallic membrane isolation technique extracting L-threonine from fermented liquid.
Provided by the invention from the fermented liquid of producing l-threonine by fermentation the method for extracting L-threonine, its concrete extraction step is as follows:
A, the L-threonine fermentation liquid is entered the metal microfiltration membrane and carries out micro-filtration after sterilization, remove tropina impurity, obtain clarifying L-threonine fermentation liquid; Described metallic membrane adopts stainless steel tubular type film separating system, and its aperture is 50nm～100nm, molecular weight cut-off 2000～50000MW, and pH scope 0～14, service temperature are 0～80 ℃, operation pressure reduction is 0.1～1.0MPa;
B, will go up the step and obtain clarifying L-threonine fermentation liquid to adjust pH be 3.0～9.0, and add gac and decolour, the gac add-on is 0.2～2% of a fermentating liquid volume, and bleaching temperature is 10～80 ℃; Using 752 spectrophotometers to survey printing opacity down in 430nm reaches more than 85%;
C, the L-threonine fermentation liquid that will go up after the step decolouring carry out reduction vaporization, concentrate volume to 20%～80% of stoste, stop evaporation when having crystallization to separate out;
It is 3.0～9.0 that d, concentrated solution are transferred pH, and mixing speed is 0～300rpm, and optimum revolution is 100～150rpm, crystallization 0-20h, and best crystallization 12h, filtration, washing obtain L-Threonine crystal and mother liquor;
E, d is gone on foot the gained crystal be dissolved in certain distilled water, make L-Threonine concentration reach 16～20%, add equal-volume 95% ethanol, mixing speed is 0～300rpm, growing the grain 0-20h, and (optimum revolution is 100～150rpm, crystallization 12h), can make with extra care the L-threonine crystal.
Above-mentioned b is in the step, and it is 4.0～5.0 that clarifying L-threonine fermentation liquid is adjusted pH the best.
Above-mentioned d is in the step, and concentrated solution pH the best is 5.0～7.0.
The mother liquor that above-mentioned d obtained in the step repeats b, c, d step, obtains L-Threonine crystal and secondary mother liquid, and the gained crystal was handled with the e step, must make with extra care the L-threonine crystal; After the secondary mother liquid desalination with membrane filtration after the fermented liquid mixed cycle use;
Ion exchange unit or nanofiltration device or electrodialysis unit are adopted in desalination.
Advantage of the present invention and positively effect:
Compare with existing technology, method of the present invention has following characteristics:
1, the present invention adopts the metal membrane filter thalline, and methods such as centrifugal, the pressure filter press filtration that has changed that conventional fermentation liquor treatment adopts have reduced maintenance cost, have reduced working strength of workers, and it is thorough to remove thalline, the filtered liquid clear;
2, membrane filtration is held back particulate and macromolecular substance greater than the filter membrane micropore by sieving action, can guarantee quantitatively to hold back.Membrane filtration divides static filtering and cross flow filter.Cross flow filter can filter the higher liquid of turbidity, its mode of action is, liquid flows through the film surface with tangential direction, the shearing force that produces during through the film surface can make the muddy particle that is deposited on the film surface spread back main body stream, thereby make the film surface contamination layer remain on thin maintenance level, prevent quick obstruction.
The present invention adopts thalline and the albumen in the stainless steel tubular type film separating system cross flow filter removal fermented liquid.Compare with other cross-flow filtration device, this equipment mainly has the following advantages: (1) film all adopts expanded and welded tube joint to be connected with the film shell, need not any web member that adds, and stops the possibility of seepage; (2) physical strength height; (3) anti-organic solvent; (4) anti-pollution easy cleaning.
3, the metallic membrane long service life that adopts of the present invention, is easy to clean and convenience for device maintenance less investment high temperature resistant, acid and alkali-resistance;
4, leaching process all adopts physical separation method, and the acid that consumes in the process, alkali and steam are low, and extraction cost greatly reduces; And have mild condition, easy and simple to handle, characteristics such as separating step is few, discharge of wastewater is few, yield is high, good product quality;
5, the L-Threonine solution quality after the present invention makes with extra care significantly improves, and the L-Threonine product that obtains through pure precipitation and crystallization reaches more than 99% through the amino acidanalyser purity assay.
[embodiment]:
Embodiment 1:
A, get L-threonine fermentation liquid 20L in 80 ℃ the heating 10min more than, regulate about pH6.0, add the microfiltration equipment batch can, microfiltration membrane is that (this film system serves as a lining body sintering TiO2 inert coating with asymmetric porous 316L powder of stainless steel to metallic membrane, aperture 50nm-100nm, molecular weight cut-off 50000MW, film bore 18.3mm, film external diameter of pipe 21.6mm, effective filtration area 0.1m
2, single hole road, wall thickness 1.65mm, film pipe range 80cm, the highest working pressure 4-6kg/cm
2, 200 ℃ of maximum operating temperatures, pH scope 0-14, system flow rate 5-10m/s).The molecular weight cut-off of system is 2000～50000MW, feeds water coolant in the prolong, about 40 ℃ of controlled temperature, and whether monitoring device is in standard state, starts microfiltration equipment, and regulating the film inlet outlet pressure differential is 0.6kg/cm
2, utilize the difference of microfiltration membrane to differing molecular quantity of material interception capacity, thalline, foreign protein are trapped in the filter residue, when turnover mould difference obviously reduces, mend appropriate amount of deionized water; Obtain L-Threonine filtrate 25L after having filtered, filtrate albumen clearance is more than 95%.
B, will go up the step and obtain clarifying L-threonine fermentation liquid to adjust pH be 4.5, and add gac and decolour, the gac add-on is 1.0% of a fermentating liquid volume, and bleaching temperature is 60 ℃; Using 752 spectrophotometers to survey printing opacity down in 430nm reaches more than 90%;
C, the L-threonine fermentation liquid that will go up after the step decolouring carry out reduction vaporization, concentrate volume to about 50% of stoste, stop evaporation when having crystallization to separate out;
It is 6.5 that d, concentrated solution are transferred pH, and mixing speed is 110rpm, crystallization 12h, and filtration, washing obtain L-Threonine crystal and mother liquor;
E, d is gone on foot the gained crystal be dissolved in certain distilled water, make L-Threonine concentration reach 18%, add equal-volume 95% ethanol, mixing speed is 110rpm, and growing the grain 12h can make with extra care the L-threonine crystal, and L-Threonine total recovery is 86.2%.
Embodiment 2:
A, get L-threonine fermentation liquid 15L in 80 ℃ the heating 10min more than, regulate about pH6.0, add the microfiltration equipment batch can, microfiltration membrane is a metallic membrane, and the molecular weight cut-off of system is 2000～50000MW, feeds water coolant in the prolong, about 25 ℃ of controlled temperature, whether monitoring device is in standard state, starts microfiltration equipment, and regulating the film inlet and outlet pressure is 0.6kg/cm
2, utilize the difference of microfiltration membrane to differing molecular quantity of material interception capacity, thalline, foreign protein are trapped in the filter residue, advance film pressure and go out film pressure to be respectively 3.0kg/cm
2And 2.4kg/cm
2, when turnover mould difference obviously reduces, mend appropriate amount of deionized water, obtain the albumen clearance and be the L-Threonine filtrate 20L more than 95%.
B, will go up the step and obtain clarifying L-threonine fermentation liquid to adjust pH be 6.0, and add gac and decolour, the gac add-on is 2.0% of a fermentating liquid volume, and bleaching temperature is 60 ℃; Use 752 spectrophotometers to survey printing opacity down and reach 86.0% in 430nm;
C, the L-threonine fermentation liquid that will go up after the step decolouring carry out reduction vaporization, concentrate volume to about 50% of stoste, stop evaporation when having crystallization to separate out;
It is 6.5 that d, concentrated solution are transferred pH, and mixing speed is 110rpm, crystallization 8.0h, and filtration, washing obtain L-Threonine crystal and mother liquor;
E, d is gone on foot the gained crystal be dissolved in certain distilled water, make L-Threonine concentration reach 17.0%, add equal-volume 95.0% ethanol, mixing speed is 110rpm, and growing the grain 8h can make with extra care the L-threonine crystal, and L-Threonine total recovery reaches 85.1%.
Embodiment 3:
Turnover mould difference is to the influence of metal membrane filter
The mode of metal membrane filter is a cross flow filter, cross flow filter can filter the higher liquid of turbidity, its mode of action is: liquid flows through the film surface with tangential direction, the shearing force that produces during through the film surface can make the muddy particle that is deposited on the film surface spread back main body stream, thereby make the film surface contamination layer remain on thin maintenance level, prevent mountain obstruction fast now.The variation of pressure can have influence on the thickness of film surface contamination layer, so influential to filtering speed etc. in filtration procedure.During to the influencing of metal membrane filter result, because main difference is to pass in and out the pressure reduction of film, and the resistance to pressure of metallic membrane is good especially, so can tolerate bigger pressure and pressure reduction in filtration procedure at research pressure.This cover pilot plant can withstand voltage 70MPa, in filtering fermentation liquor, is below the 4.0MPa for saving the pressure that energy consumption selects; Consider filtering rate, turnover mould difference should remain on more than the 0.4MPa.Different pressures and pressure reduction see Table 1 to the Threonine filter effect.
The different pressure reduction of table 1 are to the filter effect of Threonine
| Batch | Turnover film pressure/MPa | The turnover mould poor/MPa | Flow velocity/mLmin -1 | Protein removal rate/% | Pigment removal/% | L-Threonine yield/% |
| 1 3 2 4 | 4.0/3.0 3.2/2.0 4.0/3.6 3.2/2.8 | 1.0 1.0 0.4 0.4 | 132 125 87 75 | 87.82 87.05 85.89 85.37 | 51.32 49.38 48.69 47.24 | 85.3 84.2 83.9 85.0 |
Embodiment 4:
Temperature is to the influence of metal membrane filter
When filtration temperature raise, the viscosity of L-threonine fermentation liquid reduced, and it is big that the Reynolds coefficient of fermented liquid becomes, and film surface flow speed increases, and film surface shear power increases, and makes the filtering layer attenuation, thereby filtering rate increases.This experimental study protein removal rate and the chroma removal rate influence of different filtration temperature to the L-threonine fermentation liquid, and measured the L-Threonine yield under the differing temps, the results are shown in Table 2.
The different filtration temperature of table 2 is to the influence of filtering effect
| Batch | Advance film pressure/MPa | Go out film pressure/MPa | Service temperature/℃ | Filtering velocity/mLmin -1 | Protein removal rate/% | Pigment removal/% | L-Threonine yield/% |
| 1 2 3 4 | 3.6 3.6 3.6 3.6 | 3.0 3.0 3.0 3.0 | 25 50 70 85 | 124 135 139 145 | 87.82 87.96 88.21 88.23 | 51.32 51.08 50.60 49.82 | 85.3 84.6 83.2 82.5 |
Embodiment 5:
L-threonine fermentation liquid pH changes the relation with filter quality
After the fermentation ends, L-threonine fermentation liquid pH is about 6.5.The variation of pH has bigger influence to protein, and protein can sedimentation under certain pH condition, and pH can have influence on the plastic resin treatment of back, and when carrying out plastic resin treatment, selecting pH is 3.0.L-threonine fermentation liquid pH changes and the relation of filter effect sees Table 3.
The different pH of table 3 influence L-threonine fermentation liquid filter effect
| Batch | Service temperature/℃ | Turnover film pressure/MPa | Fermented liquid pH | Albumen clearance/% | Pigment removal/% | L-Threonine yield/% |
| 1 2 3 4 | 25 25 25 25 | 4.0/3.0 4.0/3.0 4.0/3.0 4.0/3.0 | 3.0 5.0 7.0 10.0 | 87.36 85.58 85.23 83.46 | 48.61 46.25 46.54 45.72 | 88.2 89.5 82.8 83.9 |
Embodiment 6:
Flocculating aids is to the influence of metal membrane filter
Add flocculating aids in the fermented liquid, can make the filtration filter cake loose, reduce filtering resistance, thereby can improve the flow velocity of filtered liquid, flocculating aids has adsorption to impurity such as the albumen in the fermented liquid, pigments simultaneously, but flocculating aids also has adsorption to the L-Threonine, influences yield.This paper is flocculating aids with diatomite, and its influence to the metal membrane filter effect is as shown in table 4:
Table 4 diatomite influences L-threonine fermentation liquid filter effect
| Batch | Service temperature/℃ | Turnover film pressure/MPa | Fermented liquid pH | Diatomite add-on/% | Filtering velocity/mLmi n -1 | Albumen clearance/% | Pigment removal/% | L-Threonine yield/% |
| 1 2 3 4 5 | 25 25 25 25 25 | 4.0/3.0 4.0/3.0 4.0/3.0 4.0/3.0 4.0/3.0 | 3.0 3.0 3.0 3.0 3.0 | 0 0.1 0.3 0.8 1.2 | 124 132 129 135 137 | 87.36 87.69 87.89 88.21 89.25 | 48.61 49.12 50.23 50.21 51.94 | 88.2 88.2 87.51 87.85 86.31 |
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