CN211111802U - Purification device of antibiotic zymotic fluid - Google Patents
Purification device of antibiotic zymotic fluid Download PDFInfo
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- CN211111802U CN211111802U CN201920966573.8U CN201920966573U CN211111802U CN 211111802 U CN211111802 U CN 211111802U CN 201920966573 U CN201920966573 U CN 201920966573U CN 211111802 U CN211111802 U CN 211111802U
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D503/00—Heterocyclic compounds containing 4-oxa-1-azabicyclo [3.2.0] heptane ring systems, i.e. compounds containing a ring system of the formula:, e.g. oxapenicillins, clavulanic acid derivatives; Such ring systems being further condensed, e.g. 2,3-condensed with an oxygen-, nitrogen- or sulfur-containing hetero ring
- C07D503/10—Heterocyclic compounds containing 4-oxa-1-azabicyclo [3.2.0] heptane ring systems, i.e. compounds containing a ring system of the formula:, e.g. oxapenicillins, clavulanic acid derivatives; Such ring systems being further condensed, e.g. 2,3-condensed with an oxygen-, nitrogen- or sulfur-containing hetero ring with a carbon atom having three bonds to hetero atoms with at the most one bond to halogen, e.g. an ester or nitrile radical, directly attached in position 2
- C07D503/12—Heterocyclic compounds containing 4-oxa-1-azabicyclo [3.2.0] heptane ring systems, i.e. compounds containing a ring system of the formula:, e.g. oxapenicillins, clavulanic acid derivatives; Such ring systems being further condensed, e.g. 2,3-condensed with an oxygen-, nitrogen- or sulfur-containing hetero ring with a carbon atom having three bonds to hetero atoms with at the most one bond to halogen, e.g. an ester or nitrile radical, directly attached in position 2 unsubstituted in position 6
- C07D503/14—Heterocyclic compounds containing 4-oxa-1-azabicyclo [3.2.0] heptane ring systems, i.e. compounds containing a ring system of the formula:, e.g. oxapenicillins, clavulanic acid derivatives; Such ring systems being further condensed, e.g. 2,3-condensed with an oxygen-, nitrogen- or sulfur-containing hetero ring with a carbon atom having three bonds to hetero atoms with at the most one bond to halogen, e.g. an ester or nitrile radical, directly attached in position 2 unsubstituted in position 6 with hydrogen atoms, hydrocarbon or substituted hydrocarbon radicals, other than a carbon atom having three bonds to hetero atoms with at the most one bond to halogen, attached in position 3
- C07D503/16—Radicals substituted by hetero atoms or by carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. an ester or nitrile radical
- C07D503/18—Radicals substituted by hetero atoms or by carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. an ester or nitrile radical by oxygen atoms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- 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
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Abstract
The utility model discloses a purification device of antibiotic zymotic fluid, include: the ceramic membrane is used for filtering the fermentation liquor obtained in the process of producing the antibiotics by the fermentation method by adopting the ceramic membrane; the nanofiltration membrane is connected to the permeation side of the ceramic membrane and is used for carrying out nanofiltration concentration desalination treatment on the permeation liquid of the ceramic membrane; the concentration device is connected to the interception side of the nanofiltration membrane and is used for concentrating the intercepted liquid of the nanofiltration membrane; the permeation side of the nanofiltration membrane is connected with a feed inlet of the ceramic membrane through a clear liquid tank; the fermentation device is used for decomposing the bacteria liquid of the trapped liquid of the ceramic membrane; the drying device is used for drying the waste liquid decomposed in the fermentation device to prepare the organic fertilizer; the fermentation system also comprises a bacteria liquid storage tank which is connected with the first fermentation device and used for adding bacteria liquid to the first fermentation device; further comprising: the resin column, the infiltration side of ceramic membrane is connected to the feed inlet of receiving the filter membrane through the resin column, and the resin column is used for carrying out resin edulcoration to the permeate liquid of ceramic membrane and handles.
Description
Technical Field
The utility model relates to a purification device of antibiotic zymotic fluid belongs to the fermentation separation field.
Background
Antibiotics are a class of secondary metabolites with antipathogenic or other activities produced by microorganisms (including bacteria, fungi, actinomycetes) or higher animals and plants during life, and chemical substances capable of interfering with other life cell development functions. The method mainly comprises the following steps: erythromycin, cephalosporins, colistin sulfate, clavulanic acid, streptomycin sulfate, vancomycin, lincomycin, penicillin, abamectin, spectinomycin, tylosin, tiamulin, daunorubicin, capreomycin sulfate, neomycin sulfate, teicoplanin, sisomicin and the like, occupy an important position in the field of medicine. It is mainly used for treating various bacterial infections or pathogenic microorganism infections, and generally has no serious side effect on the host.
Currently, there are two main ways for purifying antibiotic fermentation broth: one is plate and frame filtration and extraction for purification. The purification method has the defects that the automation degree of plate-frame filtration is low, the labor cost is high, the filtrate after the plate-frame treatment still contains more soluble protein, and the emulsification phenomenon is easy to occur in the extraction process; the extraction needs to consume a large amount of solvent, and the equipment investment is high, the operation cost is high, and the yield is lower. Another method is membrane integration and resin purification. The membrane integration process is a two-step method filtering by using a ceramic membrane and an organic membrane, so that the impurities of the treated filtrate are few, the burden of subsequent resin adsorption is reduced, the resin is protected, and the service life of the resin is prolonged. The purification method not only greatly reduces the use of solvents, reduces the investment of wastewater treatment, but also improves the yield and quality of products. But still has the following disadvantages: the membrane integration process has long clarification time consumption, short service life of the organic membrane, normally one year service life, high investment cost and unsuitability for large-scale application. In view of this, it is still necessary to find a new method for purifying an antibiotic fermentation broth.
SUMMERY OF THE UTILITY MODEL
The utility model provides an antibiotic fermentation liquor purification method with energy saving, environmental protection and low investment, which has the characteristics of no pollution, short process flow, low energy consumption, low investment, high efficiency and the like.
A method for purifying antibiotic fermentation liquor comprises the following steps:
step 1, filtering fermentation liquor obtained in the process of producing antibiotics by a fermentation method by adopting a ceramic membrane;
and 2, feeding the penetrating fluid of the ceramic membrane into a nanofiltration membrane for concentration treatment, and obtaining purified antibiotics from the concentrated solution.
In one embodiment, the concentrated solution of the ceramic membrane is added with bacterial liquid for decomposition treatment, and the treated liquid is sent to the production process of the organic fertilizer.
In one embodiment, the antibiotic is selected from the group consisting of: erythromycin, cephalosporins, colistin sulfate, clavulanic acid, streptomycin sulfate, vancomycin, lincomycin, penicillin, abamectin, spectinomycin, tylosin, tiamulin, daunorubicin, capreomycin sulfate, neomycin sulfate, teicoplanin, sisomicin, and the like.
In one embodiment, the bacterial liquid is selected from an EM bacterial liquid or an alcohol yeast bacterial liquid.
In one embodiment, the permeate from the ceramic membrane obtained in step 1 is subjected to resin purification treatment, and then enters the nanofiltration membrane concentration step in step 2.
In one embodiment, the resin is an ion exchange resin or a macroporous adsorbent resin.
In one embodiment, the resin purification is after a divalent or multivalent salt removal treatment with an ion exchange resin.
In one embodiment, the ceramic membrane has a pore size of 1-50nm, preferably a membrane pore size of 4-20nm, and most preferably 8 nm; the temperature of the feed liquid in the ceramic membrane filtration process is 5-60 ℃; the pressure is 0.1-0.5 Mpa; the flow velocity of the membrane surface is 2-5 m/s; the concentration times are 1-10 times.
In one embodiment, in the ceramic membrane filtration process, water is required to be supplemented at the later stage to dialyze the ceramic membrane concentrated solution, and the added water can be clear liquid filtered by a nanofiltration membrane; in the dialysis operation, the water adding amount is generally 0.1-5 times of the original liquid amount.
In one embodiment, the nanofiltration membrane is a ceramic or organic nanofiltration membrane, the molecular weight cut-off is 200-1000 Da, and the filtration pressure is 0.4-4.0 MPa.
In one embodiment, NaCl is added to the permeate of the ceramic membrane such that the concentration of NaCl is 5 to 10 times the concentration of divalent salt ions; and Na is removed from the nanofiltration concentrated solution by adopting monovalent salt selective electrodialysis＋。
An apparatus for purifying an antibiotic fermentation broth, comprising:
the ceramic membrane is used for filtering the fermentation liquor obtained in the process of producing the antibiotics by the fermentation method by adopting the ceramic membrane;
the nanofiltration membrane is connected to the permeation side of the ceramic membrane and is used for carrying out nanofiltration concentration desalination treatment on the permeation liquid of the ceramic membrane;
and the concentration device is connected to the interception side of the nanofiltration membrane and is used for concentrating the intercepted liquid of the nanofiltration membrane.
In one embodiment, the permeate side of the nanofiltration membrane is connected to the feed inlet of the ceramic membrane.
In one embodiment, the device further comprises a fermentation device for performing bacteria liquid decomposition treatment on the trapped fluid of the ceramic membrane.
In one embodiment, the fermentation device further comprises a drying device for drying the decomposed waste liquid in the fermentation device to form organic fertilizer.
In one embodiment, the fermentation system further comprises a bacteria liquid storage tank connected to the first fermentation device and used for adding bacteria liquid to the first fermentation device.
In one embodiment, the bacterial liquid is selected from an EM bacterial liquid or an alcohol yeast bacterial liquid.
In one embodiment, further comprising: the resin column, the infiltration side of ceramic membrane is connected to the feed inlet of receiving the filter membrane through the resin column, and the resin column is used for carrying out resin edulcoration to the permeate liquid of ceramic membrane and handles.
In one embodiment, the resin packed in the resin column is ion exchange resin or macroporous adsorption resin.
In one embodiment, the ceramic membrane has a pore size of 1-50nm, preferably 4-20nm, and most preferably 8 nm.
In one embodiment, the nanofiltration membrane is a ceramic or organic nanofiltration membrane, and the molecular weight cut-off is 200-1000 Da.
The utility model also provides the use of foretell device in being arranged in producing the antibiotic.
Advantageous effects
The utility model provides a purification method of antibiotic fermentation liquor, which replaces two-step clarification in the prior art by a one-step ceramic membrane method. The new purification process of the antibiotic simplifies the production flow, avoids the consumption and the residue of the organic solvent, reduces the investment cost and the operation cost, improves the yield of the product, and realizes the green, environment-friendly and energy-saving manufacture of the antibiotic.
Drawings
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is a diagram of the device of the present invention.
Wherein, 1, ceramic membrane; 2. a nanofiltration membrane; 3. resin column; 4. a fermentation device; 5. a drying device; 6. a concentration device; 7. a clear liquid tank; 8. and (5) a bacteria liquid storage tank.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments. It will be understood by those skilled in the art that the following examples are illustrative of the present invention only and should not be taken as limiting the scope of the invention. The examples do not specify particular techniques or conditions, and are performed according to the techniques or conditions described in the literature in the art or according to the product specifications. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products commercially available.
The recitation of values by ranges is to be understood in a flexible manner to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a concentration range of "about 0.1% to about 5%" should be interpreted to include not only the explicitly recited concentration of about 0.1% to about 5%, but also include individual concentrations (e.g., 1%, 2%, 3%, and 4%) and sub-ranges (e.g., 0.1% to 0.5%, 1% to 2.2%, 3.3% to 4.4%) within the indicated range.
Reference throughout this specification to "one embodiment," "another embodiment," "an implementation," or the like, means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment described generally throughout this application. The appearances of the same phrase in various places in the specification are not necessarily all referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with any embodiment, it is submitted that it is within the purview of this application to effect such feature, structure, or characteristic in connection with other ones of the embodiments.
It will be understood that when an element is referred to as being "connected" to another element, it can be directly connected to the other element or be indirectly connected to the other element with the element interposed therebetween. Unless explicitly stated to the contrary, the terms "comprising" and "having" are to be understood as meaning the inclusion of the listed elements, but not the exclusion of any other elements.
The words "include," "have," or any other variation thereof, as used herein, are intended to cover a non-exclusive inclusion. For example, a process, method, article, or apparatus that comprises a list of elements is not necessarily limited to those elements, but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
The utility model discloses the zymotic fluid that will handle is mainly used for producing the antibiotic through the fermentation mode, and the antibiotic of being suitable for includes but not limited to erythromycin, cephalosporin, colistin sulfate, clavulanic acid, streptomycin sulfate, vancomycin, lincomycin, penicillin, abamectin, spectinomycin, tylosin, tiamulin, daunorubicin, sulfuric acid capreomycin, neomycin sulfate, teicoplanin or sisomicin etc.. As a common knowledge in the field of fermentation, cell debris, mycelia, soluble proteins of macromolecules, residual medium, fermentation products, and the like remain in the fermentation broth.
The fermentation raw material used in the medium may be a raw material which promotes the growth of the cultured microorganism species and enables the desired fermentation product to be produced well, and for example, a liquid medium containing a carbon source, a nitrogen source, inorganic salts, and, if necessary, organic micronutrients such as amino acids and vitamins may be preferably used. As the carbon source, for example, sugars such as glucose, sucrose, fructose, galactose, lactose and maltose, starch saccharification liquid containing these sugars, sweet potato molasses, beet molasses, high-grade molasses (hightest mortases), cane juice extract or concentrated solution, raw material sugar purified or crystallized from cane juice, purified sugar purified or crystallized from cane juice, organic acids such as acetic acid and fumaric acid, alcohols such as ethanol, and glycerin can be preferably used. The saccharide is a primary oxidation product of a polyhydric alcohol, has one aldehyde group or ketone group, and is a carbohydrate classified into aldose and ketose, preferably glucose, sucrose, fructose, galactose, lactose or maltose. The carbon source may be added together at the start of the culture, or may be added in portions or continuously during the culture. Examples of the nitrogen source include ammonia gas, ammonia water, ammonium salts, urea, nitrates, and other organic nitrogen sources used in combination, such as oil meals, soybean hydrolysate, casein hydrolysate, other amino acids, vitamins, corn steep liquor, yeast or yeast extract, meat extract, peptides such as peptone, various fermented cells, and hydrolyzed products thereof. As the inorganic salts, for example, phosphate, magnesium salt, calcium salt, iron salt, manganese salt, and the like can be added as appropriate. Further, an antifoaming agent may be added and used as needed. The fermentation culture conditions are not particularly limited as long as the culture can be performed, but the fermentation culture conditions are preferably performed at a pH of 4 to 8 and a temperature of 20 to 40 ℃. The pH of the fermentation broth is adjusted to a predetermined value within the above range using an inorganic or organic acid, an alkaline substance, urea, calcium carbonate, ammonia gas, or the like.
The above-mentioned fermentation liquid can be clarified by the ceramic membrane, and the material of the porous membrane of the ceramic separation membrane can be appropriately selected from conventionally known ceramic materials, for example, composite oxide materials such as alumina, zirconia, magnesia, silica, titania, ceria, yttria, barium titanate, cordierite, mullite, forsterite, steatite, sialon, zircon, ferrite, and the like, nitride materials such as silicon nitride, aluminum nitride, carbide materials such as silicon carbide, hydroxide materials such as hydroxyapatite, elemental materials such as carbon, silicon, and the like, or inorganic composite materials containing two or more of them can be used, natural minerals (clay, clay mineral, ceramic slag, silica sand, pottery, feldspar, white sand) or blast furnace slag, fly ash, and the like can be used, wherein 1 or 2 or more selected from among alumina, zirconia, titania, magnesia, silica, and silica are preferably used in the ceramic membrane field, more preferably in which the pore diameter of alumina, zirconia, or titania is selected from alumina, alumina powder, and the ceramic separation membrane has a pore diameter of 0.5 to 5 nm, preferably a pore diameter of 0 to 5 nm, and a pore diameter of alumina is preferably a pore diameter of 0 to 5 nm, and a pore diameter of a ceramic membrane is more preferably a ceramic membrane having a high mechanical strength, and a high mass ratio of alumina, and a ceramic membrane is preferably a ceramic membrane is suitable for use in the ceramic membrane for the ceramic membrane production of a ceramic membrane having a high mechanical separation process, and a high mechanical separation efficiency, and a high pore diameter of a ceramic membrane having a high mechanical strength of a high pore diameter of a ceramic membrane of a high value of a ceramic membrane of a high value of a ceramic membrane of a ceramic.
In one embodiment, in the ceramic membrane filtration process, water is required to be supplemented at the later stage to dialyze the ceramic membrane concentrated solution, and the added water can be clear liquid filtered by a nanofiltration membrane; in the dialysis operation, the water adding amount is generally 0.1-5 times of the original liquid amount.
The obtained ceramic membrane penetrating fluid also contains fermentation products, other inorganic salts and the like, and the fermentation products are separated from monovalent salt and divalent salt in a nanofiltration mode. Nanofiltration membranes are herein defined as "pressure driven membranes that block particles smaller than 2nm and dissolved macromolecules". Suitable for the utility model discloses an effective nanofiltration membrane is preferred to be such membrane: there is an electric charge on the membrane surface, and thus improved separation efficiency is exhibited by a combination of fine pore separation (particle size separation) and electrostatic separation benefiting from the electric charge on the membrane surface. Therefore, it is necessary to use a nanofiltration membrane capable of removing a high molecular substance by particle size separation while separating an alkali metal ion to be recovered from another ion having a different charge characteristic by means of charge. As the material of the nanofiltration membrane used in the utility model, high polymer materials such as cellulose acetate polymer, polyamide, sulfonated polysulfone, polyacrylonitrile, polyester, polyimide, vinyl polymer and the like can be used, and the material can also be ceramic material. The film is not limited to one composed of only one material, and may be a film containing a plurality of the materials. With respect to the membrane structure, the membrane may be an asymmetric membrane having a dense layer on at least one side of the membrane and having micropores with pore diameters gradually increasing from the dense layer toward the inside of the membrane or the other side; or a composite membrane having a very thin functional layer of another material on the dense layer of the asymmetric membrane. The molecular weight cut-off of the nanofiltration membrane is 200-1000 Da, and the filtration pressure is 0.4-4.0 Mpa.
In one embodiment, the concentrated solution after the ceramic membrane filtration mainly comprises mycelium, macromolecular soluble protein, residual culture medium, even little residual antibiotic and the like, and the antibiotic can be degraded by microorganisms and then made into organic fertilizer, compost and the like, so that the problem of environmental pollution caused by filter residue is solved, wherein the bacterial solution is selected from EM bacterial solution or alcohol yeast solution.
In one embodiment, the permeate of the nanofiltration membrane mainly contains monovalent salts, and the monovalent salts can be returned to the washing water in the ceramic membrane filtration for water reuse.
In one embodiment, the permeate from the ceramic membrane obtained is subjected to a resin purification treatment before entering the nanofiltration membrane concentration step. The traditional solvent extraction method can be replaced by a coupling resin process. The resin refers to ion exchange resin or macroporous adsorption resin, and can be ion exchange resin after divalent or multivalent salt removal treatment. The ceramic membrane penetrating fluid contains monovalent salt and divalent salt in a culture medium, and the existence of the divalent salt can reduce the retention rate of active ingredients of a fermentation product, so that the retention rate of the active ingredients on the surface of the nanofiltration membrane can be improved and the yield can be improved by removing the divalent salt.
In one embodiment, if the resin fails to remove all of the divalent salt, the divalent salt is trapped by the nanofiltration membrane and mixed with the fermentation product, affecting the purity of the product. NaCl can be added into the penetrating fluid of the ceramic membrane to ensure that the concentration of the NaCl is 5 to 10 times of that of the divalent salt ions; and Na is removed from the nanofiltration concentrated solution by adopting monovalent salt selective electrodialysis＋. The monovalent salt is added to force the permeability of the divalent salt on the nanofiltration membrane to be improved, so that the concentration of the divalent salt in the product is avoided, the product purity is improved, the rejection rate of the monovalent salt on the surface of the nanofiltration membrane is low, and the monovalent salt is easily removed by a subsequent monovalent salt selective electrodialysis mode.
Based on the above method, the device adopted by the utility model is shown in fig. 2, and comprises:
the ceramic membrane 1 is used for filtering fermentation liquor obtained in the process of producing antibiotics by a fermentation method by adopting a ceramic membrane;
the nanofiltration membrane 2 is connected to the permeation side of the ceramic membrane 1 and is used for carrying out nanofiltration concentration desalination treatment on the permeation liquid of the ceramic membrane 1;
and the concentration device 6 is connected to the interception side of the nanofiltration membrane 2 and is used for concentrating the intercepted liquid of the nanofiltration membrane 2.
In one embodiment, the permeate side of the nanofiltration membrane 2 is connected to the feed inlet of the ceramic membrane 1.
In one embodiment, the apparatus further comprises a fermentation device 4 for performing bacteria liquid decomposition treatment on the retentate of the ceramic membrane 1.
In one embodiment, the fermentation device further comprises a drying device 5 for drying the decomposed waste liquid in the fermentation device 4 to produce organic fertilizer.
In one embodiment, the fermentation system further comprises a bacteria liquid storage tank 8 connected to the first fermentation device 4 for adding bacteria liquid to the first fermentation device 4.
In one embodiment, the bacterial liquid is selected from an EM bacterial liquid or an alcohol yeast bacterial liquid.
In one embodiment, further comprising: the resin column 3, the infiltration side of ceramic membrane 1 is connected to the feed inlet of receiving filter membrane 2 through resin column 3, and resin column 3 is used for carrying out resin impurity removal processing to the permeate liquid of ceramic membrane 1.
In one embodiment, the resin packed in the resin column 3 is ion exchange resin or macroporous adsorption resin.
In one embodiment, the ceramic membrane 1 has a pore size of 1-50nm, preferably a membrane pore size of 4-20nm, and most preferably 8 nm.
In one embodiment, the nanofiltration membrane 2 is a ceramic or organic nanofiltration membrane, and has a molecular weight cutoff of 200 to 1000 Da.
The utility model also provides the use of foretell device in being arranged in producing the antibiotic.
Example 1
Taking clavulanic acid fermentation broth 200L (containing clavulanic acid 0.37wt% and Mg)2+About 244ppm, Na+362 ppm), adjusting pH to 5.0-5.5, feeding the filtrate into a 8nm ceramic membrane for filtration, controlling the filtration temperature at 10-14 ℃, controlling the filtration pressure at 0.25Mpa, concentrating to 1.6 times, then starting to add softened water (the water is clear liquid after the nanofiltration membrane is filtered), washing and filtering with water amount of 600L, finally obtaining ceramic membrane penetrating fluid and ceramic membrane concentrated solution respectively, transferring the ceramic membrane concentrated solution into a storage tank, adding EM bacterial liquid to decompose clavulanic acid under proper conditions, after complete decomposition, drying the penetrating fluid and the like to prepare compost.
Example 2
Taking clavulanic acid fermentation broth 200L (containing clavulanic acid 0.37wt% and Mg)2+About 244ppm, Na+362 ppm), adjusting pH to 5.0-5.5, filtering with 8nm ceramic membrane at 10-14 deg.C under 0.25Mpa to 1.6 times, adding softened water (the water is the clear solution filtered by nanofiltration membrane), washing with 600L, and filtering to obtain ceramic membrane permeatePermeate and ceramic membrane concentrate. Transferring the ceramic membrane concentrated solution into a storage tank, adding EM bacterial solution to decompose clavulanic acid under proper conditions, and after complete decomposition, drying and other treatment to prepare compost. The ceramic membrane penetrating fluid is subjected to desalting treatment by sodium ion exchange resin, and treated Mg2+About 42ppm, Na+About 4527ppm, nanofiltration and concentration of the resin permeate, the molecular weight cut-off of the nanofiltration membrane is 500Da, the working pressure is 2.0MPa, and finally the nanofiltration permeate and the nanofiltration concentrate are obtained. And (4) the nanofiltration membrane concentrated solution enters the next working procedure, and the nanofiltration penetrating fluid is used as the ceramic membrane dialysis water for recycling.
Comparative example 1
Take clavulanic acid fermentation broth as an example, and the examples are that the prior membrane integration process and resin purification clavulanic acid fermentation broth are more applied:
adjusting pH to 5.0-5.5 with fermented clavulanic acid fermentation liquid 200L, filtering with 50nm ceramic membrane at 10-14 deg.C under 0.25Mpa at membrane surface flow rate of 4m/s, concentrating to 1.6 times, washing with softened water (the water is the clear liquid filtered by nanofiltration membrane) to obtain ceramic membrane penetrating fluid with water content of 600L, filtering with organic ultrafiltration membrane to obtain ceramic membrane penetrating fluid with molecular weight cutoff of 10000Da, removing impurities, filtering at 10-14 deg.C under 0.4 Mpa at circulation flow of 1.5m3H is used as the reference value. And feeding the obtained organic membrane penetrating fluid into resin for further impurity removal, transferring the resin penetrating fluid into nanofiltration equipment for concentration, wherein the cut-off molecular weight of the nanofiltration membrane is 500Da, and the working pressure is 2.0 MPa.
The test results are shown in Table 1
TABLE 1 evaluation of the properties of comparative example 1 and examples 1-2
As can be seen from the comparison example 1 and the example 1, the treatment effect of the new process is slightly better than that of the clarification effect of the existing process (two-step process), but the treatment effect of the two-step process is not obvious. The clarification cost of the new process is low, and only three-seventeent of the cost of the existing clarification process is needed; and the total yield of the clavulanic acid treated by the new process is 2.5 percent higher than that of the prior process and is 97.5 percent. In addition, the one-step treatment method of the 8nm ceramic membrane has already finished the pilot plant test, and succeed in obtaining the qualified product. Therefore, the one-step ceramic membrane method can replace the prior two-step clarification technology, not only improves the yield, but also reduces the investment cost and the operation cost; as can be seen from the examples 1 and the comparative examples 2, after the ceramic membrane penetrating fluid is treated by the resin, the divalent salt content in the fermentation liquid can be effectively reduced, and the surface retention rate of the clavulanic acid on the nanofiltration membrane and the product yield are improved.
Example 3
Collecting 150kg fermented liquid of fermented lincomycin (containing lincomycin 0.58wt% and Mg)2+About 227ppm, Na+About 330 ppm), adjusting the pH value to 3-3.5, and then filtering by a 50nm ceramic ultrafiltration membrane with the pressure of 0.2MPa and the membrane surface flow rate of 3 m/s to obtain a ceramic membrane leachate and a ceramic membrane concentrated solution. Transferring the ceramic membrane concentrated solution into a storage tank, adding EM bacterial solution and alcohol yeast to decompose lincomycin under proper conditions, and after complete decomposition, drying and the like to prepare compost. Adjusting the pH of the ceramic membrane leachate to 10-11 by using concentrated alkali. Then the mixture is filtered by a ceramic nanofiltration membrane, the molecular weight cut-off of the nanofiltration membrane is 1000Da, the pressure is 0.5MPa, and the membrane surface flow velocity is 4m/s, thus obtaining the ceramic nanofiltration membrane percolate. And then sending the obtained ceramic nanofiltration membrane percolate into ion exchange resin adsorption resin for adsorption, and then eluting by using n-butanol solvent to finally obtain resin elution clear liquid.
Example 4
Collecting 150kg fermented liquid of fermented lincomycin (containing lincomycin 0.58wt% and Mg)2+About 227ppm, Na+About 330 ppm), adjusting the pH value to 3-3.5, and then filtering by a 50nm ceramic ultrafiltration membrane with the pressure of 0.2MPa and the membrane surface flow rate of 3 m/s to obtain a ceramic membrane leachate and a ceramic membrane concentrated solution. Transferring the ceramic membrane concentrated solution into a storage tank, adding EM bacterial solution and alcohol yeast to decompose lincomycin under proper conditions, and after complete decomposition, drying and the like to prepare compost. Adding NaCl into the ceramic membrane leachate to make Na+Concentration is as high asWhen the concentration reaches 1320ppm, adding concentrated alkali to adjust the pH to 10-11. Then filtering with ceramic nanofiltration membrane with molecular weight cutoff of 1000Da, pressure of 0.5MPa and membrane surface flow rate of 4m/s to obtain ceramic nanofiltration membrane percolate, and selectively removing Na from the ceramic membrane percolate by electrodialysis with monovalent salt+Then, the solution is sent into macroporous absorption resin for absorption, and then is eluted by using n-butanol solvent, and finally resin elution clear liquid is obtained.
Comparative example 2
Taking lincomycin fermentation liquor as an example: the following examples are the prior art for purifying lincomycin fermentation liquor by using a plurality of ceramic membranes and solvent extraction methods:
taking 150kg of fermented lincomycin fermentation liquor, adjusting the pH value to 3-3.5, and filtering by a 50nm ceramic ultrafiltration membrane at the pressure of 0.2MPa and the membrane surface flow rate of 3 m/s to obtain the ceramic membrane leachate. Adjusting the pH of the ceramic membrane leachate to 10-11 by using concentrated alkali. Adding secondary octanol into the obtained ceramic membrane leachate, wherein the dosage of the secondary octanol is 1/10 of the volume of the leachate, stirring at room temperature for 5min, and standing for layering. And adding secondary octanol into the waste liquid after primary extraction, wherein the using amount is 1/10 of the volume of the percolate, stirring for 5min at room temperature, standing and layering. Mixing the organic phases, adding hydrochloric acid solution to adjust pH to 3, wherein the amount of hydrochloric acid solution is 1/5 of the organic phase, stirring for 5min, standing, and layering to obtain a first back extraction solution. Adjusting the pH value of the primary back extraction liquid to 12 by using concentrated alkali, and filtering by using a 20nm ceramic ultrafiltration membrane, wherein the pressure is 0.3MPa, and the membrane surface flow rate is 5 m/s; the filtered clear solution was diluted two-fold with purified water and the pH was adjusted to 12. Adding secondary octanol into the diluted clear liquid, wherein the dosage is 1/5 of the volume of the clear liquid, stirring for 5min, standing for layering to obtain an organic phase, adding hydrochloric acid solution with the pH value of 3, the volume of the hydrochloric acid solution is 1/7 of the volume of the organic phase, stirring for 5min, and standing for layering to obtain secondary back extraction liquid.
The test results are shown in Table 2
TABLE 2 evaluation of the properties of comparative example 2 and examples 3 to 4
As can be seen from comparative example 2 and example 3, the treatment effect of the new process is the same as that of the extraction of the existing processCompared with the method, the operation process is simple, the automation degree is high, the labor cost is greatly reduced, the production cost is reduced by 23%, the novel process can effectively remove protein and most impurities in the lincomycin fermentation liquor, the purity is improved by about 20%, and the total yield of the lincomycin is more than 97%. In addition, the discharge amount of high-concentration wastewater is reduced by 50 percent, and the requirement of clean production is met. As can be seen from examples 3 and 4, Mg can be made to be present in excess of NaCl in the ceramic film2+The retention rate in the nanofiltration process is reduced, the transmittance is improved, divalent salt is prevented from remaining in nanofiltration concentrated solution, and the product quality is improved.
Claims (5)
1. An antibiotic zymotic fluid purification device is characterized by comprising:
the ceramic membrane (1) is used for filtering fermentation liquor obtained in the process of producing antibiotics by a fermentation method by adopting a ceramic membrane;
the nanofiltration membrane (2) is connected to the permeation side of the ceramic membrane (1) and is used for carrying out nanofiltration concentration desalination treatment on the permeation liquid of the ceramic membrane (1);
the concentration device (6) is connected to the interception side of the nanofiltration membrane (2) and is used for concentrating the intercepted liquid of the nanofiltration membrane (2); the permeation side of the nanofiltration membrane (2) is connected with the feed inlet of the ceramic membrane (1) through a clear liquid tank (7);
the fermentation device (4) is used for decomposing the bacteria liquid of the trapped liquid of the ceramic membrane (1);
the drying device (5) is used for drying the waste liquid decomposed in the fermentation device (4) to prepare organic fertilizer;
the fermentation system also comprises a bacterial liquid storage tank (8) connected to the first fermentation device (4) and used for adding bacterial liquid to the first fermentation device (4);
further comprising: the permeation side of the ceramic membrane (1) is connected to a feed inlet of the nanofiltration membrane (2) through the resin column (3), and the resin column (3) is used for carrying out resin impurity removal treatment on permeate of the ceramic membrane (1).
2. The apparatus for purifying an antibiotic fermentation liquid according to claim 1, wherein the bacterial liquid is selected from EM bacterial liquid or alcohol yeast liquid.
3. The apparatus for purifying antibiotic fermentation liquid as claimed in claim 1, wherein the resin packed in the resin column (3) is ion exchange resin or macroporous adsorption resin.
4. The apparatus for purifying antibiotic fermentation broth according to claim 1, wherein the ceramic membrane (1) has a pore size of 1-50 nm.
5. The purification device of the antibiotic fermentation liquid, as claimed in claim 1, wherein the nanofiltration membrane (2) is a ceramic or organic nanofiltration membrane, and the molecular weight cut-off is 200-1000 Da.
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