CN1268760C - Method for producing fermented nucleotide typed antibiotics by using membrane - Google Patents
Method for producing fermented nucleotide typed antibiotics by using membrane Download PDFInfo
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- CN1268760C CN1268760C CN 200310112003 CN200310112003A CN1268760C CN 1268760 C CN1268760 C CN 1268760C CN 200310112003 CN200310112003 CN 200310112003 CN 200310112003 A CN200310112003 A CN 200310112003A CN 1268760 C CN1268760 C CN 1268760C
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- ultrafiltration
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- 239000012528 membrane Substances 0.000 title claims abstract description 23
- 239000003242 anti bacterial agent Substances 0.000 title abstract description 3
- 229940088710 antibiotic agent Drugs 0.000 title abstract description 3
- 239000002773 nucleotide Substances 0.000 title abstract 2
- 125000003729 nucleotide group Chemical group 0.000 title abstract 2
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 50
- 238000000855 fermentation Methods 0.000 claims abstract description 29
- 230000004151 fermentation Effects 0.000 claims abstract description 29
- 238000001728 nano-filtration Methods 0.000 claims abstract description 26
- 108090000765 processed proteins & peptides Proteins 0.000 claims abstract description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 18
- 239000000706 filtrate Substances 0.000 claims abstract description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 33
- 238000000034 method Methods 0.000 claims description 31
- AMNAZJFEONUVTD-KEWDHRJRSA-N (2s,3s,4s,5r,6r)-6-(4-amino-2-oxopyrimidin-1-yl)-4,5-dihydroxy-3-[[(2s)-3-hydroxy-2-[[2-(methylamino)acetyl]amino]propanoyl]amino]oxane-2-carboxamide Chemical compound O1[C@H](C(N)=O)[C@@H](NC(=O)[C@H](CO)NC(=O)CNC)[C@H](O)[C@@H](O)[C@@H]1N1C(=O)N=C(N)C=C1 AMNAZJFEONUVTD-KEWDHRJRSA-N 0.000 claims description 27
- FEACDOXQOYCHKU-UHFFFAOYSA-N Gougerotin Natural products CNCC(=O)NC1=NC(=O)N(C=C1)C2OC(C(O)C(NC(=O)C(N)CO)C2O)C(=O)N FEACDOXQOYCHKU-UHFFFAOYSA-N 0.000 claims description 27
- 229920002521 macromolecule Polymers 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 239000002777 nucleoside Substances 0.000 claims description 19
- 125000003835 nucleoside group Chemical group 0.000 claims description 19
- 230000003115 biocidal effect Effects 0.000 claims description 12
- 239000000049 pigment Substances 0.000 claims description 10
- 102000004169 proteins and genes Human genes 0.000 claims description 9
- 108090000623 proteins and genes Proteins 0.000 claims description 9
- 239000012141 concentrate Substances 0.000 claims description 7
- 230000009849 deactivation Effects 0.000 claims description 7
- 239000012535 impurity Substances 0.000 claims description 7
- 238000005406 washing Methods 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 6
- 238000000502 dialysis Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 150000004676 glycans Chemical class 0.000 claims description 3
- 229920001282 polysaccharide Polymers 0.000 claims description 3
- 239000005017 polysaccharide Substances 0.000 claims description 3
- 238000005352 clarification Methods 0.000 claims description 2
- 239000000047 product Substances 0.000 abstract description 18
- 238000005516 engineering process Methods 0.000 abstract description 10
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- 238000001694 spray drying Methods 0.000 abstract description 2
- 108010053950 Teicoplanin Proteins 0.000 abstract 4
- BJNLLBUOHPVGFT-QRZIFLFXSA-N teichomycin Chemical compound CCCCCCCCCC(=O)N[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@H]1OC(C(=C1)OC=2C(=CC(=CC=2)[C@@H](O[C@H]2[C@@H]([C@@H](O)[C@H](O)[C@@H](CO)O2)NC(C)=O)[C@H]2C(N[C@H](C3=CC(O)=CC(O[C@@H]4[C@H]([C@@H](O)[C@H](O)[C@@H](CO)O4)O)=C3C=3C(O)=CC=C(C=3)[C@@H](NC3=O)C(=O)N2)C(O)=O)=O)Cl)=C(OC=2C(=CC(C[C@H](C(N4)=O)NC(=O)[C@H](N)C=5C=C(O6)C(O)=CC=5)=CC=2)Cl)C=C1[C@H]3NC(=O)[C@@H]4C1=CC6=CC(O)=C1 BJNLLBUOHPVGFT-QRZIFLFXSA-N 0.000 abstract 4
- 230000002779 inactivation Effects 0.000 abstract 2
- 230000020477 pH reduction Effects 0.000 abstract 2
- 238000009833 condensation Methods 0.000 abstract 1
- 230000005494 condensation Effects 0.000 abstract 1
- 238000000926 separation method Methods 0.000 abstract 1
- 235000011149 sulphuric acid Nutrition 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 18
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- LPQOADBMXVRBNX-UHFFFAOYSA-N ac1ldcw0 Chemical compound Cl.C1CN(C)CCN1C1=C(F)C=C2C(=O)C(C(O)=O)=CN3CCSC1=C32 LPQOADBMXVRBNX-UHFFFAOYSA-N 0.000 description 3
- 150000001720 carbohydrates Chemical class 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 229910017053 inorganic salt Inorganic materials 0.000 description 3
- 241000700605 Viruses Species 0.000 description 2
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- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
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- 238000005342 ion exchange Methods 0.000 description 2
- 238000005096 rolling process Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
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- 235000001018 Hibiscus sabdariffa Nutrition 0.000 description 1
- 244000061176 Nicotiana tabacum Species 0.000 description 1
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 1
- 229930182764 Polyoxin Natural products 0.000 description 1
- 235000005291 Rumex acetosa Nutrition 0.000 description 1
- 240000007001 Rumex acetosella Species 0.000 description 1
- 241000208292 Solanaceae Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 244000098338 Triticum aestivum Species 0.000 description 1
- 241001272684 Xanthomonas campestris pv. oryzae Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
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- 239000003905 agrochemical Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
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- YEBIHIICWDDQOL-YBHNRIQQSA-N polyoxin Polymers O[C@@H]1[C@H](O)[C@@H](C(C=O)N)O[C@H]1N1C(=O)NC(=O)C(C(O)=O)=C1 YEBIHIICWDDQOL-YBHNRIQQSA-N 0.000 description 1
- 229920001184 polypeptide Polymers 0.000 description 1
- 230000003449 preventive effect Effects 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 235000003513 sheep sorrel Nutrition 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Peptides Or Proteins (AREA)
Abstract
The present invention discloses a method for producing fermented nucleotide peptide type antibiotics by using a membrane, which comprises the steps of fermentation, H2SO4 acidification /NaOH callback inactivation, ultrafiltration of large molecular weight, ultrafiltration of small molecular weight and condensation of a nanofiltration membrane to obtain nanofiltration concentrated solution. A membrane technology separation technology is used for replacing traditional bactericide (such as Ningnan teichomycin) manufacturing technology in the present invention. After fermentation and acidification / callback inactivation, sheet frame filtration is replaced by large molecular weight ultrafiltration. Filtrate is further filtered by small molecular weight ultrafiltration, the purity of the product is further enhanced, and the concentrated solution is made into 1 to 3% Ningnan teichomycin solution. Finally, the small molecular weight ultrafiltration filtrate is concentrated by a nanofiltration membrane, 7 to 10% Ningnan teichomycin solution is made, and concentrated solution can be made into powder by spray drying. The purity of the product is enhanced by the present invention, and simultaneously, the added value of the product is enhanced (feed and low-concentration Ningnan teichomycin solution are simultaneously made). Thus, the manufacturing cost is reduced, and the environment pollution is reduced.
Description
Technical field
The present invention relates to use the antibiotic method of film manufacturing fermentation class nucleosides peptide type, special and Ningnanmycin etc. are relevant by the antibiotic extracting method of nucleosides peptide type of fermentation generation.
Background technology
The nucleosides peptide type antibiotics wide-spectrum bactericide that a new generation generates by fermentation (as Ningnanmycin etc.), be a kind of novel biological environmental production agricultural chemicals, bacterial blight of rice, culm rot, wheat powdery mildew, plant of Solanaceae mosaic virus, tobacco, chilli pepper mosaic virus are had excellent preventive effect.This series bactericidal agent is the biological pesticide that develops green food, non-polluted farm product, protection environmental safety both at home and abroad, and its market outlook are very good, at present in Yunnan, farmlands, ground such as Shandong, Sichuan, Hebei, Zhejiang, Jilin are extensively on probation, effect is very good.
This series bactericidal agent, the production technique traditional as Ningnanmycin is as follows:
Fermentation → deactivation/acidifying PH5 → Plate Filtration → ion-exchange → evaporation concentration → 2% Ningnanmycin (or 8% Ningnanmycin)
Wherein, because " Plate Filtration " step can not effectively be removed impurity such as soluble proteins, carbohydrate, polypeptide, pigment, filtrate is of poor quality; And the temperature of " evaporation concentration " step is very high, energy consumption is big, and " evaporation concentration " can deepen the color and luster and the loss product of product, and the purity of product is lower, and " evaporation concentration " is sprayed into behind the dry powder the very easily moisture absorption of product; So this production technique can only be made the Ningnanmycin aqua, and is unfavorable for that production becomes pulvis, the purity of product is lower, and value-added content of product is low, and this production technique has much room for improvement really.
Summary of the invention
The object of the present invention is to provide the antibiotic method of a kind of application film manufacturing fermentation class nucleosides peptide type, to improve the purity and the added value of product, reduce manufacturing cost, and reduce environmental pollution.
For reaching above-mentioned purpose, solution of the present invention is:
Use the antibiotic method of film manufacturing fermentation class nucleosides peptide type, the steps include: fermentation; H
2SO
4NaOH readjustment deactivation after the acidifying; The macromolecule ultrafiltration; The small molecular weight ultrafiltration; Nanofiltration membrane concentrates, and promptly gets the nanofiltration concentrated solution.
Wherein, when fermentation class nucleosides peptide type microbiotic is Ningnanmycin, it is the ultra-filtration membrane of 30000-150000MWCO that molecular weight cut-off is adopted in above-mentioned macromolecule ultrafiltration, working pressure is 4-9bar, temperature is lower than 50 ℃, cycles of concentration is calculated as 4-6 doubly with feeding liquid, adds water washing amount amount and is calculated as 0.4-0.8 doubly with feeding liquid; It is the ultra-filtration membrane of 3000-10000MWCO that molecular weight cut-off is adopted in the small molecular weight ultrafiltration, and working pressure is 15-30bar, and temperature is lower than 50 ℃, and cycles of concentration is calculated as about 5-15 times with feeding liquid; Nanofiltration membrane concentrates and adopts molecular weight cut-off is the ultra-filtration membrane of 200MWCO, and working pressure is 20-35bar, and temperature is lower than 50 ℃, and cycles of concentration is calculated as about 12-18 times with feeding liquid.
When fermentation class nucleosides peptide type microbiotic was Ningnanmycin, the fermented liquid raw material in the above-mentioned fermentation step needed process sulfuric acid acidation (pH2.5) deactivation 1hr earlier, adjusts back the feed liquid of pH to 4.5-5.5 again with NaOH.
Above-mentioned macromolecule ultrafiltration step is removed mycelium, most of soluble proteins, partial pigment, a remaining step of substratum, and it is bright to see through the liquid clarification, and the filter residue of gained promptly makes feed through centrifugal drying.
When fermentation class nucleosides peptide type microbiotic is Ningnanmycin, above-mentioned small molecular weight ultrafiltration step will further adopt the film of small molecular weight to carry out ultrafiltration through the filtrate of macromolecule ultrafiltration, further remove a spot of soluble proteins, macromolecular polysaccharide, macromole pigment and macromole impurity etc., concentrated solution promptly makes the Ningnanmycin solution of 1-3%, enters nanofiltration through liquid and concentrates.
When fermentation class nucleosides peptide type microbiotic was Ningnanmycin, the concentrated solution of above-mentioned nanofiltration membrane enrichment step was 7-10% left and right sides Ningnanmycin strong solution.
Above-mentioned nanofiltration dialysis water can be delivered to fermentation again and the macromolecule ultrafiltration adds the water wash step reuse.
After adopting aforesaid method, the present invention substitutes traditional sterilant (as Ningnanmycin etc.) manufacturing process with the membrane technique separating technology, after fermentation and acidifying, the macromolecule ultrafiltration is replaced Plate Filtration, mycelium, most of soluble proteins, partial pigment, a remaining step of substratum are removed and make feed, and obtain clarifying ultrafiltrate; Adopt the process of small molecular weight ultrafiltration substitution ion exchange again, removals such as a spot of soluble proteins, macromolecular polysaccharide, macromole pigment and macromole impurity in the ultrafiltrated that the macromolecule ultrafiltration is obtained, obtain flaxen solution, simultaneously, the concentrated solution held back of small molecular weight ultrafiltration can make 1-3% as Ningnanmycin solution; At last, the filtrate of small molecular weight ultrafiltration, the process nanofiltration membrane is concentrated again, and concentration reaches 7-10%, removes small molecular weight impurities such as part monose, inorganic salt simultaneously, thereby further improves the purity of product; The dialysis water colorless that nanofiltration obtains is transparent, can be with it as producing reuse water.
Like this, using membrane separating technology of the present invention is made sterilant (as Ningnanmycin), not only improve the purity of product, can spray drying one-tenth pulvis, and, improved value-added content of product (making the Ningnanmycin solution of feed and 1-3% simultaneously), and, reduce manufacturing cost, reduced environmental pollution; Simultaneously, the dialysis water that nanofiltration obtains has further reduced manufacturing cost as the reuse water utilization.
Description of drawings
Fig. 1 is the method flow diagram that application film of the present invention is made Ningnanmycin.
Specific embodiment
Consult shown in Figure 1ly, the most preferred embodiment that utilization the present invention produces Ningnanmycin is:
At first, the same traditionally, the Ningnanmycin fermentation raw material is fermented, make the fermented liquid raw material;
Again the fermented liquid raw material is passed through sulfuric acid acidation to pH=2.5 deactivation 1hr, acid adjustment acidifying purpose is sterilization, pull back to the feed liquid of pH=4.5-5.5 again with NaOH, the purpose of readjustment is recovered former ph value, make feed liquid character more stable, feed liquid is tired about 10000u/ml, solid content 3-5% (total solid content), feed liquid is thickness comparatively, this makes feed liquid just can also be eager to excel a lot than the finished product (traditional technology can only make the thick product of Ningnanmycin about lower concentration and 8%) of traditional technology through the concentrated solution of aftermentioned Ultra-flo macromolecule ultrafiltration (also can adopt other macromolecule ultrafiltration), so Ultra-flo macromolecule hyper-concentration liquid has made full use of again.
Then, carry out committed step of the present invention, fermented feed liquid enters the ultrafiltration of Ultra-flo macromolecule, small molecular weight ultrafiltration, nanofiltration concentration systems successively.
The molecular weight cut-off of packing in the Ultra-flo macromolecule ultrafiltration system is the flat plate ultrafiltration membrane of 30000-150000MWCO (50000MWCO the best) (or film of other form), fermented feed liquid is added in the batch can, feeding water coolant in the equipment interchanger (is used for the operation controlled temperature and is not higher than 50 ℃, 40 ℃ of the bests), check each valve, switch, make valve and switch all be in standard state.Starting outfit transfers to 5-6bar with pressure, and regularly measures filtration velocity, and volume is filtered in metering.Feed liquid adds water washing when being concentrated to 5 times, adopt a small amount of water mode that adds repeatedly, and amount of water is 0.7 times of stock liquid, and the washing dialyzate is collected in the lump, and filtrate mixing tires about about 8000u/ml, and the average film flux is about 80LMH in the system operation process; Behind EO, get rid of concentrated solution, after the flushing with clean water system, add the aqueous solution that contains the film clean-out system and clean film, 40-45 ℃ of operation 30-45 minute, totally get final product with flushing with clean water then, in order to using next time.
In this process, Ultra-flo macromolecule ultra-filtration technique is compared with other filter method has following superiority:
Need not add flocculating aids when (1) filtering, save the expenditure of a large amount of flocculating aids costs;
(2) owing to adopt mycelium, most of soluble proteins, partial pigment, a remaining step of substratum to hold back filtration method, operation technological process is simplified, and running cost reduces, and the filtrate quality is good; And the feed that the filter residue of removing the impurity gained promptly makes through centrifugal drying;
(3) filter the yield height, lose lessly, the clarity of filtrate and quality are good, can satisfy manufacturing technique requirent;
(4) Ultra-flo macromolecule ultrafiltration system is carried out the system lock filtration, and can realize full automatic control, and filtrate is not subjected to artifact pollution, and deslagging need not be manual, and operation labour intensity alleviates;
(5) owing to Ultra-flo macromolecule ultrafiltration system special structure design, system design and supporting cleaning program, make stability, efficient, the contamination resistance of system and be applicable to that the filtering ability of high viscosity feed liquid has significant superiority than other filter method.
Also contain materials such as more carbohydrate, small molecular protein, pigment in the filtrate quality by the ultrafiltration of Ultra-flo macromolecule, it influences the purity and the quality of product, by adopting the small molecular weight ultra-filtration membrane further the filtrate of Ultra-flo macromolecule ultrafiltration to be filtered, can remove most albumen, carbohydrate, pigment etc., reduce simultaneously because impurity too much causes the overload of follow-up nanofiltration technique.Its operating process is with the ultrafiltration of Ultra-flo macromolecule, it is the rolling ultra-filtration membrane (or film of other form) of 3000-10000MWCO (5000MWCO is for best) that molecular weight cut-off is adopted in the small molecular weight ultrafiltration, working pressure is 20-25bar, temperature is not higher than 50 ℃ (40 ℃ of the bests), cycles of concentration is (to calculate with feeding liquid) about 10 times, and the average film flux is about 20LMH.Through the small molecular weight ultrafiltration, filtrate is become light yellow by original sorrel, sees through tiring to about 6500u/ml of liquid, and sugar is removed more than 50%, and effect is remarkable, and the filtrate quality reaches the requirement of back technology.Can make 2% Ningnanmycin solvent for the concentrated solution part simultaneously.Like this, concentrated solution need not to adopt and adds water washing, and it can be used as product and sells on the one hand, secondly can water saving and energy consumption, reduce scale and back operation pressure, and also reduce in addition because the environmental pollution of concentrated solution after the washes clean.
By also containing small-molecule substances such as more monose, inorganic salt in the small molecular weight ultrafiltrate quality, by adopting nanofiltration membrane, further the small molecular weight ultrafiltrate to be filtered, the dialyzate part can be removed most monose and inorganic salt etc.Nanofiltration membrane concentrates and adopts molecular weight cut-off is the rolling ultra-filtration membrane (or film of other form) of 200MWCO, working pressure is 25-30bar, and temperature is not higher than 50 ℃, and 40 ℃ is best, cycles of concentration is (to calculate with feeding liquid) about 15 times, and the average film flux is about 35LMH.Nanofiltration filtrate is water white transparency, does not have the loss of tiring, and can be used as the production reuse water.The concentrated solution quality reaches the requirement of back technology, and concentrated solution is tired and can be reached 80000u/ml, can make 8% Ningnanmycin solvent or spray and do as pulvis.
Certainly, the present invention also can apply to produce other nucleosides peptide type microbiotic such as polyoxin, antimycoin 120, qingfengmeisu, golden caryomycin, the steps include: earlier raw material to be fermented; Again by H
2SO
4NaOH readjustment deactivation after the acidifying; Then, fermented feed liquid is entered macromolecule ultrafiltration, small molecular weight ultrafiltration, nanofiltration concentration systems successively, promptly get the nanofiltration concentrated solution, concrete production stage is similar to Ningnanmycin, does not do at this and gives unnecessary details.
Claims (7)
1, use the antibiotic method of film manufacturing fermentation class nucleosides peptide type, it is characterized in that: fermentation class nucleosides peptide type microbiotic is a Ningnanmycin, and step is: fermentation; H
2SO
4NaOH readjustment deactivation after the acidifying; Macromolecule ultrafiltration, molecular weight cut-off are 30000-150000MWCO; Small molecular weight ultrafiltration, molecular weight cut-off are 3000-10000MWCO; Nanofiltration membrane concentrates, and molecular weight cut-off is 200MWCO, promptly gets the nanofiltration concentrated solution, and the nanofiltration concentrated solution is the Ningnanmycin concentrated solution.
2, the antibiotic method of application film manufacturing fermentation class nucleosides peptide type as claimed in claim 1 is characterized in that: the fermented liquid raw material in the fermentation step needs the 1hr of process sulfuric acid acidation pH2.5 deactivation earlier, adjusts back the feed liquid of pH to 4.5-5.5 again with NaOH.
3, the antibiotic method of application film manufacturing fermentation class nucleosides peptide type as claimed in claim 1, it is characterized in that: macromolecule ultrafiltration, working pressure are 4-9bar, and temperature is lower than 50 ℃, cycles of concentration is calculated as 4-6 doubly with feeding liquid, adds the water washing amount and is calculated as 0.4-0.8 doubly with feeding liquid; Small molecular weight ultrafiltration, working pressure are 15-30bar, and temperature is lower than 50 ℃, and cycles of concentration is calculated as 5-15 doubly with feeding liquid; Nanofiltration membrane concentrates, and working pressure is 20-35bar, and temperature is lower than 50 ℃, and cycles of concentration is calculated as 12-18 doubly with feeding liquid.
4, the antibiotic method of application film manufacturing fermentation class nucleosides peptide type as claimed in claim 1, it is characterized in that: the macromolecule ultrafiltration step is removed mycelium, soluble proteins, pigment, a remaining step of substratum, it is bright to see through the liquid clarification, and the filter residue of gained promptly makes feed through centrifugal drying.
5, the antibiotic method of application film manufacturing fermentation class nucleosides peptide type as claimed in claim 1, it is characterized in that: the small molecular weight ultrafiltration step will further adopt the film of small molecular weight to carry out ultrafiltration through the filtrate of macromolecule ultrafiltration, further remove soluble proteins, macromolecular polysaccharide, macromole pigment and macromole impurity, concentrated solution promptly makes the Ningnanmycin solution of 1-3%, enters nanofiltration through liquid and concentrates.
6, the antibiotic method of application film manufacturing as claimed in claim 1 fermentation class nucleosides peptide type is characterized in that: the concentrated solution of nanofiltration membrane enrichment step, be the concentrated solution of Ningnanmycin, and wherein concentration is 7-10%.
7, the antibiotic method of application film manufacturing fermentation class nucleosides peptide type as claimed in claim 1, it is characterized in that: nanofiltration dialysis water can be delivered to fermentation again and the macromolecule ultrafiltration adds the water wash step reuse.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310112003 CN1268760C (en) | 2003-10-29 | 2003-10-29 | Method for producing fermented nucleotide typed antibiotics by using membrane |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310112003 CN1268760C (en) | 2003-10-29 | 2003-10-29 | Method for producing fermented nucleotide typed antibiotics by using membrane |
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| CN1539990A CN1539990A (en) | 2004-10-27 |
| CN1268760C true CN1268760C (en) | 2006-08-09 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100463912C (en) * | 2006-12-20 | 2009-02-25 | 福州大学 | Membrane separating and purifying process for aminoglycoside antibiotics |
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2003
- 2003-10-29 CN CN 200310112003 patent/CN1268760C/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100463912C (en) * | 2006-12-20 | 2009-02-25 | 福州大学 | Membrane separating and purifying process for aminoglycoside antibiotics |
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|---|---|
| CN1539990A (en) | 2004-10-27 |
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