CN206051902U - A kind of capreomycin production system based on membrane technology - Google Patents
A kind of capreomycin production system based on membrane technology Download PDFInfo
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- CN206051902U CN206051902U CN201620979878.9U CN201620979878U CN206051902U CN 206051902 U CN206051902 U CN 206051902U CN 201620979878 U CN201620979878 U CN 201620979878U CN 206051902 U CN206051902 U CN 206051902U
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- 108010065839 Capreomycin Proteins 0.000 title claims abstract description 81
- 229960004602 capreomycin Drugs 0.000 title claims abstract description 81
- VCOPTHOUUNAYKQ-WBTCAYNUSA-N (3s)-3,6-diamino-n-[[(2s,5s,8e,11s,15s)-15-amino-11-[(6r)-2-amino-1,4,5,6-tetrahydropyrimidin-6-yl]-8-[(carbamoylamino)methylidene]-2-(hydroxymethyl)-3,6,9,12,16-pentaoxo-1,4,7,10,13-pentazacyclohexadec-5-yl]methyl]hexanamide;(3s)-3,6-diamino-n-[[(2s,5s,8 Chemical compound N1C(=O)\C(=C/NC(N)=O)NC(=O)[C@H](CNC(=O)C[C@@H](N)CCCN)NC(=O)[C@H](C)NC(=O)[C@@H](N)CNC(=O)[C@@H]1[C@@H]1NC(N)=NCC1.N1C(=O)\C(=C/NC(N)=O)NC(=O)[C@H](CNC(=O)C[C@@H](N)CCCN)NC(=O)[C@H](CO)NC(=O)[C@@H](N)CNC(=O)[C@@H]1[C@@H]1NC(N)=NCC1 VCOPTHOUUNAYKQ-WBTCAYNUSA-N 0.000 title claims abstract description 77
- 239000012528 membrane Substances 0.000 title claims abstract description 59
- 238000005516 engineering process Methods 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 64
- 238000005374 membrane filtration Methods 0.000 claims abstract description 32
- 239000000243 solution Substances 0.000 claims abstract description 28
- 239000000919 ceramic Substances 0.000 claims abstract description 23
- 238000010612 desalination reaction Methods 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 22
- 238000001728 nano-filtration Methods 0.000 claims abstract description 18
- 238000001694 spray drying Methods 0.000 claims abstract description 18
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 13
- 239000012510 hollow fiber Substances 0.000 claims abstract description 11
- 238000000855 fermentation Methods 0.000 claims abstract description 10
- 230000004151 fermentation Effects 0.000 claims abstract description 10
- 239000011550 stock solution Substances 0.000 claims abstract description 4
- 239000012466 permeate Substances 0.000 claims description 30
- 238000012545 processing Methods 0.000 claims description 20
- 238000001223 reverse osmosis Methods 0.000 claims description 15
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 8
- 239000000047 product Substances 0.000 claims description 7
- 238000002425 crystallisation Methods 0.000 claims description 6
- 230000008025 crystallization Effects 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 239000011575 calcium Substances 0.000 claims description 3
- QXDMQSPYEZFLGF-UHFFFAOYSA-L calcium oxalate Chemical compound [Ca+2].[O-]C(=O)C([O-])=O QXDMQSPYEZFLGF-UHFFFAOYSA-L 0.000 claims description 3
- VEPSWGHMGZQCIN-UHFFFAOYSA-H ferric oxalate Chemical compound [Fe+3].[Fe+3].[O-]C(=O)C([O-])=O.[O-]C(=O)C([O-])=O.[O-]C(=O)C([O-])=O VEPSWGHMGZQCIN-UHFFFAOYSA-H 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- UHNWOJJPXCYKCG-UHFFFAOYSA-L magnesium oxalate Chemical compound [Mg+2].[O-]C(=O)C([O-])=O UHNWOJJPXCYKCG-UHFFFAOYSA-L 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 235000006408 oxalic acid Nutrition 0.000 claims description 2
- 238000012958 reprocessing Methods 0.000 claims 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims 1
- 239000011777 magnesium Substances 0.000 claims 1
- 238000004062 sedimentation Methods 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 8
- 238000001914 filtration Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 239000002158 endotoxin Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 230000008014 freezing Effects 0.000 abstract description 2
- 238000007710 freezing Methods 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 238000002834 transmittance Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 239000012141 concentrate Substances 0.000 abstract 1
- 239000010408 film Substances 0.000 description 22
- 239000012530 fluid Substances 0.000 description 20
- 238000011033 desalting Methods 0.000 description 19
- 238000000034 method Methods 0.000 description 10
- 230000008569 process Effects 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 239000003814 drug Substances 0.000 description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000005352 clarification Methods 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 238000001471 micro-filtration Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 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 2
- KBIWNQVZKHSHTI-UHFFFAOYSA-N 4-n,4-n-dimethylbenzene-1,4-diamine;oxalic acid Chemical compound OC(=O)C(O)=O.CN(C)C1=CC=C(N)C=C1 KBIWNQVZKHSHTI-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 241001655322 Streptomycetales Species 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- FIVPIPIDMRVLAY-UHFFFAOYSA-N aspergillin Natural products C1C2=CC=CC(O)C2N2C1(SS1)C(=O)N(C)C1(CO)C2=O FIVPIPIDMRVLAY-UHFFFAOYSA-N 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 238000000502 dialysis Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000000909 electrodialysis Methods 0.000 description 2
- FIVPIPIDMRVLAY-RBJBARPLSA-N gliotoxin Chemical compound C1C2=CC=C[C@H](O)[C@H]2N2[C@]1(SS1)C(=O)N(C)[C@@]1(CO)C2=O FIVPIPIDMRVLAY-RBJBARPLSA-N 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000000049 pigment Substances 0.000 description 2
- 229920001184 polypeptide Polymers 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 108090000765 processed proteins & peptides Proteins 0.000 description 2
- 102000004196 processed proteins & peptides Human genes 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 101800000263 Acidic protein Proteins 0.000 description 1
- 241000193830 Bacillus <bacterium> Species 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 241001269524 Dura 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
- 235000010469 Glycine max Nutrition 0.000 description 1
- 244000068988 Glycine max Species 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical group C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 241000187479 Mycobacterium tuberculosis Species 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 239000001888 Peptone Substances 0.000 description 1
- 108010080698 Peptones Proteins 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- -1 Semen Maydis pulp Substances 0.000 description 1
- 241000191940 Staphylococcus Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 241000194017 Streptococcus Species 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 230000002365 anti-tubercular Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012531 culture fluid Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003480 eluent Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 235000001727 glucose Nutrition 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229940029329 intrinsic factor Drugs 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 210000004072 lung Anatomy 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 235000019319 peptone Nutrition 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 210000000582 semen Anatomy 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 238000003980 solgel method Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000012086 standard solution Substances 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 210000000433 stratum disjunctum Anatomy 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 201000008827 tuberculosis Diseases 0.000 description 1
- 238000009941 weaving Methods 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
本实用新型公开一种基于膜处理技术的卷曲霉素生产系统，包括：预处理系统、原液罐、膜过滤系统、脱盐处理系统、卷曲霉素分离系统、喷雾干燥系统以及生化系统。本实用新型所提供的基于膜处理技术的卷曲霉素生产系统通过膜过滤系统中的陶瓷膜对发酵液进行澄清过滤，能源消耗减少，过滤工序的收率提高，酸碱废液排放量减少，环境污染减轻，经济效益和社会效益显著；通过脱盐处理系统中的纳滤膜对卷曲霉素进行脱盐处理，使得浓缩液透光率达到95%，减少活性炭的消耗量，同时降低蒸汽消耗和冷冻水用量，达到节能减排效果；通过卷曲霉素分离系统中空纤维超滤膜去除卷曲霉素浓缩液的细菌内毒素，产品质量得以提高，经济价值提升。
The utility model discloses a capreomycin production system based on membrane treatment technology, comprising: a pretreatment system, a stock solution tank, a membrane filtration system, a desalination treatment system, a capreomycin separation system, a spray drying system and a biochemical system. The capreomycin production system based on the membrane treatment technology provided by the utility model clarifies and filters the fermentation liquid through the ceramic membrane in the membrane filtration system, reduces energy consumption, improves the yield of the filtration process, and reduces the discharge of acid-base waste liquid. The environmental pollution is reduced, and the economic and social benefits are remarkable; capreomycin is desalted through the nanofiltration membrane in the desalination treatment system, so that the light transmittance of the concentrated solution reaches 95%, reducing the consumption of activated carbon, and reducing steam consumption and freezing Reduce water consumption to achieve energy saving and emission reduction effects; remove bacterial endotoxin from capreomycin concentrate through hollow fiber ultrafiltration membrane of capreomycin separation system, improve product quality and increase economic value.
Description
Technical field
This utility model belongs to capreomycin production field, more particularly, to a kind of capreomycin based on membrane technology
Production system.
Background technology
Capreomycin belongs to polypeptide antituberculotics also known as capreomycin, and it is by Eli Lilly companies of the U.S.
E.B.Herr et al. separated a kind of alkali water-soluble polypeptide for obtaining from the culture fluid of curling streptomycete and newly resists in 1961
Mycobacterium tuberculosis are had good inhibiting effect by rhzomorph.The medicine in addition to suppressing effectively to tuberculosis negative bacillus, also to lung
The gram-positive bacteriums such as scorching streptococcus, staphylococcuses have good inhibitory action.There are Eli Lilly and Roche in foreign countries at present
The companies such as Hellas, Dura Pharmaceuticals Inc produce capreomycin, and there is section's Pharmaceutical in Xinyang in domestic production producer
Medicine pharmacy company limited in company limited and Nanning.
Capreomycin Jing crimps streptomycete based on soybean cake powder, peptone, starch, glucose, Semen Maydis pulp, phosphate
Air agitation cultivation and fermentation, Jing three grade fermemtation biosynthesiss are carried out in wanting the fluid medium of carbon, nitrogen, phosphorus source at 28 ± 0.5 DEG C
Capreomycin.Capreomycin fermentation liquid dilute with water, oxalic acid are acidified to pH3.0 or so, are heated to 70～75 DEG C, by sheet frame mistake
Filter, removes the impurity such as a large amount of insoluble mycelium, acidic protein, calcium ions and magnesium ions, culture based draff, is cooled to less than 15 DEG C, then
With in NaOH and obtaining meeting the clarification capreomycin stock solution of ion-exchange process requirement.This process is referred to as fermented in production
The pretreatment of liquid.
Capreomycin in stock solution is dissociated into quadrivalent cation in aqueous, exchanges using sodium form Subacidity cation and sets
Fat is adsorbed, with becoming capreomycin eluent after dilute sulfuric acid eluting, the volume in making aqueous solution in this step extraction process
Aspergillin is enriched with, and content is concentrated to 10% or so by less than 0.8%, meanwhile, by the selection of ion exchange resin,
Remove pigment, albumen and visible solid content of the overwhelming majority etc..The Jing strong-acid cation-exchange resin desalinations of purification liquid elder generation obtain smart
Liquid processed, then Jing medicinal carbon desolventing technologies, adsorpting pigment, bacterial endotoxin, Jing decompression thin film evaporation are dense below 40 DEG C
Contracting, capreomycin content are concentrated to 40% by 10% or so.Finally in order to further improve finished product color level, a certain amount of medicine is added
The concentrated solution for obtaining conforming to quality requirements with activated carbon decolorizing process.The degerming membrane filtration of concentrated solution Jing micropores, it is spray-dried
To capreomycin finished product.Capreomycin refining technique studies less in decades both at home and abroad, and production technology is without big improvement, product
Quality is unstable, refines high cost.Therefore, it is necessary to optimization capreomycin of employing new technology refines production technology.
Membrane technology is just gradually widely applied in industrial every field in recent years, and membrane separation technique is using tool
Have and certain select the classification of material, separation, concentration, purification etc. are carried out through the filter medium of characteristic.After the sixties in 20th century,
Various membrane separation techniques are developed rapidly, occupy increasingly consequence in various isolation technics.Film has in separation process
Following function：The identification of material and transmission；Interface；Reacting field.The identification of material and through being to make in mixture between each component
Realize detached intrinsic factor；As interface, film will transmit through liquid and retain liquid be divided into it is mutually unmixed biphase；As reacting field film
Surface and internal surface of hole contain the functional group for having interaction ability with specific solute, by physical action, chemical reaction or
Biochemical reaction improves the selectivity and separating rate of membrance separation.Membrane separating process has under room temperature to be carried out, without phase change, energy consumption
Low, equipment is simple, convenient operation and control the features such as, oneself is applied to the neck such as chemical industry, medicine, light industry, food, weaving, electronics, metallurgy
Domain.According to the difference of retention component, membrane process can be divided into microfiltration (Microfiltration, MF), ultrafiltration
(Ultrafiltration, UF), reverse osmosiss (Reverse osmosis, RO), dialysis (Dialysis, DS), electrodialysis
(Electrodialysis, ED) and seepage slope (Pervaporation, PV) etc..
Ceramic membrane is with loose structure with 1600 DEG C of high temperature sinterings of the Jing such as aluminium oxide, titanium oxide, zirconium oxide
High technology ceramics filtering material.It is by the ceramic monolith of porosity 30% ~ 50%, aperture 50nm ~ 15 μm, using sol-gel process
Or the asymmetric compound film that other techniques are made.Its structure is usually " sandwich " formula：Supporting layer（Also known as carrier layer）、
Transition zone（Also known as intermediate layer）, film layer（Also known as function stratum disjunctum）.Wherein the aperture of supporting layer is generally 1 ~ 20 μm, and porosity is
30% ~ 65%, its effect is to increase the mechanical strength of film；The aperture of the aperture ratio supporting layer in intermediate layer is little, and its effect is to prevent film
Infiltration of the granule to porous support layer in layer preparation process, about 20 ~ 60 μm of thickness, porosity are 30% ~ 40%；Film layer has divides
From function, from 0.8 nm ~ 1 μm, about 3 ~ 10 μm of thickness, porosity are 40% ~ 55% in aperture.The pore-size distribution of whole film by
Supporting layer is gradually reduced to film layer, forms asymmetric structure distribution.Ceramic membrane can be divided into microfiltration according to aperture（Aperture is more than 50
nm）, ultrafiltration（2 ~ 50 nm of aperture）, nanofiltration（Aperture is less than 2 nm）Etc. species.Ceramic membrane filter is a kind of " cross flow filter " shape
The fluid separation process of formula：Material liquid flow at high speed in the membrane tube, the clarified permeation liquid containing small molecule component under pressure-driven
Edge and face vertical direction（Radially）Film is passed through outwards, the muddy concentrated solution containing macromolecular components is rejected by, so that fluid
Reach the purpose of separation, concentration, purification.
The retention characteristic of ultrafilter membrane is the usual molecular cut off scope characterizing with to the molecular cut off of standard Organic substance
In 1000-300000Da, therefore ultrafilter membrane can be to larger molecular organicses（Such as protein, antibacterial）, colloid, suspended solid etc. carry out point
From being widely used in the clarification of feed liquid, the isolating and purifying of larger molecular organicses, except thermal source.The retention characteristic of NF membrane is with right
Characterizing, corresponding molecular cut off scope is in 150-1000 Da, therefore NF membrane can be to little for the rejection of the standard solution such as MgSO4
Molecular organic etc. is separated with water, inorganic salt, is made desalination and is carried out while concentration.
The content of the invention
The purpose of this utility model is, for the deficiencies in the prior art, there is provided a kind of to be based on membrane technology
Capreomycin production system.
For this purpose, this utility model is adopted the following technical scheme that：
A kind of capreomycin production system based on membrane technology, the capreomycin based on membrane technology are produced
System includes：
- pretreatment system, the pretreatment system are used to remove the Ca in capreomycin fermentation liquid2+、Mg2+And Fe3+；
- original fluid container, the original fluid container are used for storage from the feed liquid of pretreatment system and form the solid-liquid separation of feed liquid；
- membrane filtration system, the membrane filtration system for carrying out membrane filtration process, film mistake to the feed liquid from original fluid container
The concentrated solution of filter system is back to original fluid container and is reprocessed, and the permeate of membrane filtration system is delivered to desalting processing system；
- desalting processing system, the desalting processing system is for carrying out at desalination to the permeate from membrane filtration system
Reason, the desalination solution of the desalting processing system are delivered to capreomycin piece-rate system and are processed；
- capreomycin piece-rate system, the capreomycin piece-rate system are used to separate the desalination from desalting processing system
Capreomycin in liquid, the permeate of the capreomycin piece-rate system is delivered to spray drying system to be carried out at spray drying
Reason, the concentrated solution of the capreomycin piece-rate system is delivered to biochemical system carries out biochemical treatment；
- spray drying system, the spray drying system is for spraying to the permeate of capreomycin piece-rate system
It is dried and obtains capreomycin product；And
- biochemical system, the biochemical system are arranged for the bottom of concentrated solution and original fluid container to capreomycin piece-rate system
The mycelia liquid for going out carries out biochemical treatment, discharges Jing after biochemical treatment is up to standard.
Preferably, the pretreatment system includes agitator tank, settling tank and wire gauze filter, the agitator tank, heavy
Shallow lake tank and wire gauze filter are sequentially arranged, and the agitator tank accommodates capreomycin fermentation liquid and adds industrial ethanedioic acid simultaneously fully
Stirring, the settling tank are used for calcium oxalate of the precipitation in the feed liquid of agitator tank, magnesium oxalate and ferric oxalate, the metal gauze
Filter is used for mechanical admixture of the filtration in the feed liquid of settling tank so that in the feed liquid before membrane filtration system not
There is mechanical admixture.
Preferably, the pore size filter of the wire gauze filter is 500 μm.
Preferably, the membrane filtration system is ceramic film device, and the ceramic film device is for the material from original fluid container
Liquid carries out membrane filtration process, and the concentrated solution of the ceramic film device is back to original fluid container and is reprocessed, the ceramic film device
Permeate be delivered to desalting processing system.
Preferably, alkali is set on the permeate outlet conduit of the ceramic film device and adjusts entrance.
Preferably, the desalting processing system is nanofiltration device, and the nanofiltration device is for from membrane filtration system
Permeate carries out desalting processing, and the concentrated solution of the nanofiltration device is delivered to capreomycin piece-rate system and is processed.
Preferably, the permeate of the nanofiltration device is delivered to reverse osmosis unit, and the reverse osmosis unit is for nanofiltration
The permeate of device carries out concentration, and the concentrated solution of the reverse osmosis unit is delivered to evaporation and crystallization system and is evaporated knot
Crystalline substance, the permeate reuse of the reverse osmosis unit are used to dissolve feed liquid to original fluid container.
Preferably, the capreomycin piece-rate system is hollow fiber uf membrane system, the doughnut membrane ultrafiltration dress
Put for separating the capreomycin in the desalination solution of desalting processing system, the permeate conveying of the hollow fiber uf membrane system
Spray drying treatment is carried out to spray drying system, the concentrated solution of the hollow-fibre membrane ultrafiltration apparatus is delivered to biochemical system and enters
Row biochemical treatment.
This utility model provides a kind of capreomycin production system based on membrane technology, has the advantage that：
1）Clarification filtration is carried out by the ceramic membrane in membrane filtration system to fermentation liquid, energy resource consumption is reduced, filter progress
Yield improve, acid-base waste fluid discharge capacity reduce, environmental pollution mitigate, economic benefit and social benefit it is notable；
2）Desalting processing is carried out to capreomycin by the NF membrane in desalting processing system so that concentrated solution light transmittance reaches
To 95%, the consumption of activated carbon is reduced, while reducing steam consumption and freezing water consumption, reach effects of energy saving and emission reduction；
3）The bacterial endotoxin of capreomycin concentrated solution is removed by capreomycin piece-rate system hollow fiber ultrafiltration membrane, is produced
Quality is improved, and economic worth is lifted；
4）Application of membrane be truly realized in capreomycin production technology the low cost required by industrialized production and
High stability, while also improving product quality and reducing cost.
Description of the drawings
Fig. 1 is a kind of schematic diagram of capreomycin production system based on membrane technology provided by the utility model；
In figure：101- agitator tanks；102- settling tanks；103- wire gauze filters；201- original fluid containers；301- ceramic membranes are filled
Put；302- alkali adjusts entrance；401- nanofiltration device；402- reverse osmosis units；501- hollow fiber uf membrane systems；601- sprays
Drying system；701- biochemical systems；801- evaporation and crystallization systems.
Specific embodiment
This utility model is described in further detail with specific embodiment referring to the drawings.
A kind of capreomycin production system based on membrane technology, including：
- pretreatment system, for removing the Ca in capreomycin fermentation liquid2+、Mg2+And Fe3+；
- original fluid container 201, for storing the solid-liquid separation of feed liquid and formation feed liquid from pretreatment system；
- membrane filtration system, for membrane filtration process, the concentration of membrane filtration system are carried out to the feed liquid from original fluid container 201
Liquid is back to original fluid container 201 and is reprocessed, and the permeate of membrane filtration system is delivered to desalting processing system；
- desalting processing system, for desalting processing, desalting processing system are carried out to the permeate from membrane filtration system
Desalination solution be delivered to capreomycin piece-rate system and processed；
- capreomycin piece-rate system, for separating the capreomycin in the desalination solution of desalting processing system, curling
The permeate of mycin piece-rate system is delivered to spray drying system 601 and carries out spray drying treatment, capreomycin piece-rate system
Concentrated solution is delivered to biochemical system 701 and carries out biochemical treatment；
- spray drying system 601, for the permeate of capreomycin piece-rate system is spray-dried and is rolled up
Aspergillin product；And
- biochemical system 701, for the bacterium of the bottom discharge of the concentrated solution to capreomycin piece-rate system and original fluid container 201
Silk liquid carries out biochemical treatment, discharges Jing after biochemical treatment is up to standard.
Pretreatment system includes agitator tank 101, settling tank 102 and wire gauze filter 103, agitator tank 101, settling tank
102 and wire gauze filter 103 be sequentially arranged, agitator tank 101 accommodates and capreomycin fermentation liquid and adds industrial ethanedioic acid and fill
Stirring, settling tank 102 is divided to be used for calcium oxalate of the precipitation in the feed liquid of agitator tank 101, magnesium oxalate and ferric oxalate, metal gauze
Filter 103 is used for mechanical admixture of the filtration in the feed liquid of settling tank 102 so that into the material before membrane filtration system
There is no mechanical admixture in liquid.The pore size filter of wire gauze filter 103 is 500 μm.
Membrane filtration system is ceramic film device 301, and ceramic film device 301 is for carrying out to the feed liquid from original fluid container 201
Membrane filtration process, the concentrated solution of ceramic film device 301 are back to original fluid container 201 and are reprocessed, the transmission of ceramic film device 301
Liquid is delivered to desalting processing system.
Alkali is set on the permeate outlet conduit of ceramic film device 301 and adjusts entrance 302.
Desalting processing system is nanofiltration device 401, and nanofiltration device 401 is for carrying out to the permeate from membrane filtration system
Desalting processing, the concentrated solution of nanofiltration device 401 are delivered to capreomycin piece-rate system and are processed.
The permeate of nanofiltration device 401 is delivered to reverse osmosis unit 402, and reverse osmosis unit 402 is for nanofiltration device 401
Permeate carry out concentration, the concentrated solution of reverse osmosis unit 402 is delivered to evaporation and crystallization system 801 and is evaporated crystallization,
The permeate reuse of reverse osmosis unit 402 is used to dissolve feed liquid to original fluid container 201.
Capreomycin piece-rate system be hollow fiber uf membrane system 501, hollow-fibre membrane ultrafiltration apparatus be used for separate it is de-
Capreomycin in the desalination solution of salt treatment system, the permeate of hollow fiber uf membrane system 501 are delivered to spray drying system
System 601 carries out spray drying treatment, and the concentrated solution of hollow-fibre membrane ultrafiltration apparatus is delivered to biochemical system 701 carries out biochemical place
Reason.
Above-mentioned specific embodiment be used for illustrate this utility model, preferred embodiment only of the present utility model and
, rather than to this utility model limit, in spirit of the present utility model and scope of the claims, to this reality
With new any modification, equivalent substitution and improvements made etc., protection domain of the present utility model is both fallen within.
Claims (8)
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| CN201620979878.9U CN206051902U (en) | 2016-08-29 | 2016-08-29 | A kind of capreomycin production system based on membrane technology |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112408681A (en) * | 2020-11-06 | 2021-02-26 | 陕西麦可罗生物科技有限公司 | Harmless comprehensive treatment process for different agricultural antibiotic fermentation hyphae and high-concentration organic wastewater |
| WO2024250372A1 (en) * | 2023-06-09 | 2024-12-12 | 天津北洋百川生物技术有限公司 | LOW-ENDOTOXIN γ-POLYGLUTAMIC ACID, AND SEPARATION AND EXTRACTION METHOD THEREFOR AND USE THEREOF |
-
2016
- 2016-08-29 CN CN201620979878.9U patent/CN206051902U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112408681A (en) * | 2020-11-06 | 2021-02-26 | 陕西麦可罗生物科技有限公司 | Harmless comprehensive treatment process for different agricultural antibiotic fermentation hyphae and high-concentration organic wastewater |
| WO2024250372A1 (en) * | 2023-06-09 | 2024-12-12 | 天津北洋百川生物技术有限公司 | LOW-ENDOTOXIN γ-POLYGLUTAMIC ACID, AND SEPARATION AND EXTRACTION METHOD THEREFOR AND USE THEREOF |
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