CN104480174A - Culture medium for producing virginiamycin through streptomyces virginiae fermentation and feeding method of culture medium - Google Patents
Culture medium for producing virginiamycin through streptomyces virginiae fermentation and feeding method of culture medium Download PDFInfo
- Publication number
- CN104480174A CN104480174A CN201410829651.1A CN201410829651A CN104480174A CN 104480174 A CN104480174 A CN 104480174A CN 201410829651 A CN201410829651 A CN 201410829651A CN 104480174 A CN104480174 A CN 104480174A
- Authority
- CN
- China
- Prior art keywords
- fermentation
- controls
- virginiamycin
- culture medium
- content
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Micro-Organisms Or Cultivation Processes Thereof (AREA)
- Fodder In General (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention relates to a culture medium for producing virginiamycin through streptomyces virginiae fermentation and a feeding method of the culture medium. A seed culture medium comprises rice vinasse and low-temperature pressed soybean cake powder; a fermentation culture medium comprises rice vinasse, low-temperature pressed soybean cake powder, Dow macroporous ion exchange resin and a nonionic surfactant. Through the adoption of the culture medium and the feeding method, the cost problem of raw and supplemental materials is solved, the environment influence on the sources of the raw and supplemental materials is reduced to the greatest degree, the sources of the raw and supplemental materials are guaranteed to be fed sufficiently, the stable and efficient production of the virginiamycin is achieved, and meanwhile, the fermentation unit can be increased by using the culture medium and a culturing method.
Description
Technical field
The invention belongs to fermentation technical field, particularly relate to substratum and feed process that a kind of Wei Jini streptomycete fermentation produces virginiamycin.
Background technology
Virginiamycin has another name called virginiamycin, virgimycin, SKF-7988, loose mycin etc.Being divided into chain positive Antibiotics from structure, is the comparatively novel veterinary antibiotic of a class formation.
At present, domestic employing Wei Jini streptomycete fermentation produces virginiamycin, and the subject matter of existence is:
1 fermentation unit maintains about 1000 ~ 3000u/ml, causes fermentation yield lower.
2 animality nitrogenous source quality influence fermented liquid quality and ferment effects.At present, add fish meal or peptone or yeast extract or select two or more nitrogenous source to add simultaneously in the substratum of domestic fermentative production virginiamycin.Cause fermentation later stage remaining protein more, fermentation broth viscosity is higher, reduces extract yield.
The production cost of 3 virginiamycins is higher, and wherein the cost of nitrogenous source accounts for about 40% of fermentation costs.
Summary of the invention
The object of the invention is just the defect overcoming above-mentioned prior art, one is provided effectively to improve fermentation unit, reduce supplementary material consumption to greatest extent simultaneously, reduce production cost, and supplementary material source is not affected by environment, ensure that it is in liberal supply, realize the substratum that virginiamycin is stablized, the Wei Jini streptomycete fermentation of High-efficient Production produces virginiamycin.
Another object of the present invention is to provide the feed process utilizing above-mentioned substratum to produce virginiamycin.
Technical scheme taked for achieving the above object is:
A kind of Wei Jini streptomycete fermentation produces the substratum of virginiamycin, comprise seed culture medium and fermention medium, it is characterized in that consisting of of described seed culture medium: maltose 20 ~ 30ml/L, mixing starch 10 ~ 20g/L, sweet oil 1 ~ 5ml/L, low temperature pressing soybean cake powder 15 ~ 25g/L, large rice distiller grain 20 ~ 30g/L, Zein powder 10 ~ 15g/L, light calcium carbonate 1 ~ 5g/L, ammonium sulfate 1 ~ 5g/L, maltin 0.01 ~ 0.03g/L;
Consisting of of described fermention medium: maltose 30 ~ 40ml/L, mixing starch 20 ~ 40g/L, sweet oil 1 ~ 5ml/L, low temperature pressing soybean cake powder 20 ~ 30g/L, large rice distiller grain 30 ~ 40g/L, Zein powder 20 ~ 30g/L, potassium primary phosphate 0.8 ~ 1.2g/L, light calcium carbonate 6 ~ 8g/L, ammonium sulfate 5 ~ 8g/L, sodium acetate 0.5 ~ 1.5g/L, magnesium sulfate 1 ~ 5g/L, ferrous sulfate 0.3 ~ 0.7g/L, nonionogenic tenside 0.01 ~ 0.05g/L, Tao Shi macroporous resin 1 ~ 5g/L, maltin 0.04 ~ 0.07g/L.
The specification of quality of described large rice distiller grain is: protein content is more than 50%, and moisture content controls within 5%, and the raw material of 80% can pass through 60 mesh sieves.
Described low temperature pressing soybean cake powder specification of quality is: soya bean squeezes 1 time under lower than the condition of 80 DEG C, and require that its oil-contg controls 7 ~ 10%, protein content is more than 45%, and the raw material of 80% can pass through 80 mesh sieves.
Described mixing starch refers in starch the pantothenic acid of 0.006% and the Thioctic Acid of 0.004% that add its weight.
Described nonionogenic tenside is the smooth or polysorbate of glycerin fatty acid ester or lipid acid sorb.
Utilize a feed process for above-mentioned substratum fermentative production virginiamycin, it is characterized in that carrying out feed supplement during the fermentation, comprise repairing, moisturizing, benefit sugar, mend alkali and mend nitrogenous source, wherein
A repairing controls: adopt stream addition to mend sweet oil,
Before fermentation, 10h need not carry out repairing,
Fermentation 11h ~ 20h: period controls lipid content 3.5 ~ 4.5%, when lipid content is lower than 4%, fills into sweet oil, when lipid content is more than 6%, then stop repairing, repairing amount (L)=(5-lipid content-resid amount) % × fermentating liquid volume (L)
21h is to fermentation ends in fermentation: period controls lipid content 1.5 ~ 2%, when lipid content is lower than 1.5%, fill into oil, when lipid content is more than 2%, then stop repairing, repairing amount (L)=(1.7-lipid content-resid amount) % × fermentating liquid volume (L);
B moisturizing:
Before fermentation, 10h need not carry out moisturizing,
Fermentation 11h ~ 20h: as fermented liquid cell concentration > 50%, adopts the moisturizing of stream addition, controls cell concentration 40 ~ 50%,
21h is to fermentation ends in fermentation: as fermented liquid cell concentration > 40%, adopts the moisturizing of stream addition, controls cell concentration 30 ~ 40%;
C pH controls:
Before fermentation, 10h, pH do not control,
Fermentation 11 ~ 20h: when the pH of fermented liquid is lower than 6.5, the sodium hydroxide solution adding 5 ~ 10% controls its pH 6.5 ~ 7.0,
21h is to fermentation ends in fermentation: when the pH of fermented liquid is lower than 6.0, the sodium hydroxide solution adding 5 ~ 10% controls its pH 6.0 ~ 6.5;
D fills into nitrogenous source: fermentation period respectively at 60h and 100h time fill into the ammonium sulfate that concentration is 5 ~ 10%, its amount of filling into is 1 ~ 1.5% of fermentating liquid volume;
E mends sugar:
10h before fermentation, does not add maltose,
Fermentation 11 ~ 20h, as reducing sugar content < 4%, add maltose, when reducing sugar content is more than 6%, then stop adding maltose, mend sugar amount (kg)=(5-reducing sugar amount) % × fermentating liquid volume (L);
21h is to fermentation ends in fermentation, as reducing sugar content < 2%, add maltose, when reducing sugar content is more than 2%, then stop adding maltose, mend sugar amount (kg)=(2-reducing sugar amount) % × fermentating liquid volume (L).
Technical superiority of the present invention is:
1) fermentation costs is low.First large rice distiller grain output is larger, market value is lower, be convenient to buying, secondly the nitrogenous source in the conventional seed culture medium of large rice distiller grain replacement virginiamycin, fermention medium is used, reduce consumption, reduce the production cost of more than 30%, avoid the unfavorable factor because of nitrogenous source quality influence seed liquor and fermented liquid quality.
2) the present invention adopts large rice distiller grain to instead of peptone in conventional medium and fish meal, meets amino acid whose demand in virginiamycin fermentation culture process.Primary amino acid needed for the fermentation of pertinent literature report virginiamycin is α-amino-isovaleric acid, glycine, Serine, proline(Pro) respectively.Protein content in fermention medium of the present invention reaches more than 55%, and aminoacids content, apparently higher than domestic cellar culture based formulas, is conducive to improving Wei Jini streptomycete hypha form; Improve quality and the fermentation technique level of fermented liquid.
The amino nitrogen content contrast table of different supplementary material
3) add tensio-active agent and macroporous resin in fermention medium, not only change membrane passage, and improve the flow state of gas-liquid surface state and fermented liquid, be conducive to improving fermentation technique level.
4) adopt this technique fermentative production virginiamycin, be applicable to single batch fermentation scale at 10m
3above, fermentation unit reaches more than 4000u/ml.
Embodiment
Be explained the present invention with example below, it should be understood that example is for illustration of the present invention instead of limitation of the present invention.Scope of the present invention and core content are determined according to claims.
In following embodiment
The specification of quality of large rice distiller grain is: protein content is more than 50%, and moisture content controls within 5%, and the raw material of 80% can pass through 60 mesh sieves.
Low temperature pressing soybean cake powder specification of quality is: soybean cake powder squeezes 1 time under lower than the condition of 80 DEG C, and require that its oil-contg controls 7 ~ 10%, protein content is more than 45%.The raw material of 80% can pass through 80 mesh sieves.
Seed culture technique:
Tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 32 ~ 36h.Seed culture terminates, cell concentration 20 ~ 30%, without other living contaminants.
Fermentating culturing process
First by fermention medium sterilizing, cooling, and use sterile air pressurize, after fermention medium sterilizing, fat controls 4.5 ~ 5.5%, then seed liquor is all moved into fermentor tank and cultivates.Its culture transferring amount controls 10 ~ 15%.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 65 ~ 75h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 30 ~ 40%; More than fermentation unit 4000u/ml.
Embodiment 1
1m
3seed tank culture:
Maltose 20L, mixing starch 10kg, sweet oil 1L, low temperature pressing soybean cake powder 15kg, large rice distiller grain 20kg, Zein powder 10kg, light calcium carbonate 1kg, ammonium sulfate 1kg, maltin 10g.
In seed culture process, tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 32h.Seed culture terminates, cell concentration 21%, without other living contaminants.
10m
3fermentor cultivation:
Maltose 300L, mixing starch 200kg, sweet oil 10L, low temperature pressing soybean cake powder 200kg, large rice distiller grain 300kg, Zein powder 200kg, potassium primary phosphate 8kg, light calcium carbonate 60kg, ammonium sulfate 50kg, sodium acetate 5kg, magnesium sulfate 10kg, ferrous sulfate 3kg, fatty acid glycerine fat 0.1kg, Tao Shi macroporous resin 10kg, maltin 0.4kg.
First by fermention medium sterilizing, cooling, and use sterile air pressurize, then seed liquor is all moved into fermentor tank and cultivate.Its culture transferring amount controls 10%.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 65h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 31%; Fermentation unit 4103u/ml.
According to circumstances feed supplement is carried out in above-mentioned fermenting process.
Embodiment 2
1m
3seed tank culture:
Maltose 30L, mixing starch 13kg, sweet oil 2L, low temperature pressing soybean cake powder 17kg, large rice distiller grain 23kg, Zein powder 11kg, light calcium carbonate 2kg, ammonium sulfate 2kg, maltin 30g.
In seed culture process, tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 33h.Seed culture terminates, cell concentration 25%, without other living contaminants.
10m
3fermentor cultivation:
Maltose 330L, mixing starch 400kg, sweet oil 20L, low temperature pressing soybean cake powder 220kg, large rice distiller grain 330kg, Zein powder 220kg, potassium primary phosphate 9kg, light calcium carbonate 60kg, ammonium sulfate 60kg, sodium acetate 7kg, magnesium sulfate 20kg, ferrous sulfate 4kg, sapn 0.2kg, Tao Shi macroporous resin 20kg, maltin 0.5kg.
First by fermention medium sterilizing, cooling, and use sterile air pressurize, then seed liquor is all moved into fermentor tank and cultivate.Its culture transferring amount controls 12%.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 67h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 33%; Fermentation unit 4237u/ml.
According to circumstances feed supplement is carried out in above-mentioned fermenting process.
Embodiment 3
1m
3seed tank culture:
Maltose 25L, mixing starch 15kg, sweet oil 3L, low temperature pressing soybean cake powder 15kg, large rice distiller grain 25kg, Zein powder 15kg, light calcium carbonate 3kg, ammonium sulfate 3kg, maltin 20g.
In seed culture process, tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 34h.Seed culture terminates, cell concentration 25%, without other living contaminants.
10m
3fermentor cultivation:
Maltose 350L, mixing starch 200kg, sweet oil 30L, low temperature pressing soybean cake powder 250kg, large rice distiller grain 400kg, Zein powder 250kg, potassium primary phosphate 10kg, light calcium carbonate 70kg, ammonium sulfate 65kg, sodium acetate 10kg, magnesium sulfate 30kg, ferrous sulfate 5kg, polysorbate 0.3kg, Tao Shi macroporous resin 30kg, maltin 0.55kg.
First by fermention medium sterilizing, cooling, and use sterile air pressurize, then seed liquor is all moved into fermentor tank and cultivate.Its culture transferring amount controls 13%.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 70h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 35%; Fermentation unit 4387u/ml.
According to circumstances feed supplement is carried out in above-mentioned fermenting process.
Embodiment 4
1m
3seed tank culture:
Maltose 27L, mixing starch 20kg, sweet oil 4L, low temperature pressing soybean cake powder 23kg, large rice distiller grain 20kg, Zein powder 14kg, light calcium carbonate 4kg, ammonium sulfate 4kg, maltin 25g.
In seed culture process, tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 35h.Seed culture terminates, cell concentration 27%, without other living contaminants.
10m
3fermentor cultivation:
Maltose 350L, mixing starch 350kg, sweet oil 40L, low temperature pressing soybean cake powder 250kg, large rice distiller grain 350kg, Zein powder 270kg, potassium primary phosphate 12kg, light calcium carbonate 75kg, ammonium sulfate 70kg, sodium acetate 12kg, magnesium sulfate 40kg, ferrous sulfate 6kg, glycerin fatty acid ester 0.4kg, Tao Shi macroporous resin 50kg, maltin 0.62kg.
First by fermention medium sterilizing, cooling, and use sterile air pressurize, then seed liquor is all moved into fermentor tank and cultivate.Its culture transferring amount controls 13%.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 73h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 38%; Fermentation unit 4213u/ml.
According to circumstances feed supplement is carried out in above-mentioned fermenting process.
Embodiment 5
1m
3seed tank culture:
Maltose 30L, mixing starch 20kg, sweet oil 5L, low temperature pressing soybean cake powder 25kg, large rice distiller grain 30kg, Zein powder 15kg, light calcium carbonate 5kg, ammonium sulfate 5kg, maltin 30g.
In seed culture process, tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 36h.Seed culture terminates, cell concentration 30%, without other living contaminants.
10m
3fermentor cultivation:
Maltose 400L, mixing starch 400kg, sweet oil 50L, low temperature pressing soybean cake powder 250kg, large rice distiller grain 400kg, Zein powder 300kg, potassium primary phosphate 12kg, light calcium carbonate 80kg, ammonium sulfate 80kg, sodium acetate 15kg, magnesium sulfate 50kg, ferrous sulfate 7kg, the smooth 0.5kg of lipid acid sorb, Tao Shi macroporous resin 50kg, maltin 0.7kg.
First by fermention medium sterilizing, cooling, and use sterile air pressurize, then seed liquor is all moved into fermentor tank and cultivate.Its culture transferring amount controls 15%.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 73h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 40%; Fermentation unit 4120u/ml.
According to circumstances feed supplement is carried out in above-mentioned fermenting process.
In above-described embodiment 1-5, control of additive raw material realizes in the following manner:
A repairing controls: adopt stream addition to mend sweet oil,
Fat controls: after fermention medium sterilizing, fat controls 4 ~ 6%; 10h before fermentation, lipid content controls more than 4.5%; Fermentation 11 ~ 20h, lipid content controls 3.5 ~ 4.5%; 21h is to fermentation ends, and lipid content controls 1.5 ~ 2%.
Before fermentation, 10h need not carry out repairing.
Fermentation 11h ~ 20h: if lipid content is lower than 4%, fill into sweet oil; If lipid content is more than 6%, then stop repairing.Its calculation formula is: repairing amount (L)=(5-lipid content-resid amount) % × fermentating liquid volume (L).
21h is to fermentation ends in fermentation: if lipid content is lower than 1.5%, fill into oil; If lipid content is more than 2%, then stop repairing.Its calculation formula is: repairing amount (L)=(1.7-lipid content-resid amount) % × fermentating liquid volume (L).
B moisturizing:
Before fermentation, 10h need not carry out moisturizing.
11h ~ 20h: as fermented liquid cell concentration > 50%, controls cell concentration 40 ~ 50%.
21h is to fermentation ends: as fermented liquid cell concentration > 40%, adopts the moisturizing of stream addition, controls cell concentration 30 ~ 40%.
C pH controls:
Before fermentation, 10h, pH do not control.
Fermentation 11 ~ 20h: if the pH of fermented liquid is lower than 6.5, the sodium hydroxide solution adding 5 ~ 10% controls its pH 6.5 ~ 7.0.
21h is to fermentation ends in fermentation: if the pH of fermented liquid is lower than 6.0, the sodium hydroxide solution adding 5 ~ 10% controls its pH 6.0 ~ 6.5.
D fills into nitrogenous source: fermentation period respectively at 60h and 100h time fill into 5 ~ 10% ammonium sulfate, its amount of filling into is 1 ~ 1.5% of fermentating liquid volume.
E mends sugar:
10h before fermentation, does not add maltose.
Fermentation 11 ~ 20h, if reducing sugar content < 4%; Add maltose; If reducing sugar content is more than 6%, then stop adding maltose.Its calculation formula is: mend sugar amount (kg)=(5-reducing sugar amount) % × fermentating liquid volume (L).
21h is to fermentation ends, if reducing sugar content < 2% in fermentation; Add maltose; If reducing sugar content is more than 2%, then stop adding maltose.Its calculation formula is: mend sugar amount (kg)=(2-reducing sugar amount) % × fermentating liquid volume (L).
Comparative example
Seed culture:
At 1m
3glucose 14L, Zulkovsky starch 22kg, Semen Maydis oil 3L, soybean cake powder 31kg, peptone 12kg, fish meal 13kg, light calcium carbonate 2.6kg, ammonium sulfate 3.4kg is added in first class seed pot.
First by seed culture medium sterilizing, cooling, and use sterile air pressurize, and then under flame protection, cultured Wei Jini strepto-starter bottle fermented liquid is accessed seeding tank and cultivates, inoculum size is 1L.In seed culture process, tank pressure 0.02 ~ 0.04MPa; Tank temperature 25 ~ 28 DEG C; Air flow quantity 80m
3/ h; Mixing speed 60 ~ 80r/min; PH6 ~ 8; Incubation time 34h.Seed culture terminates, cell concentration 21%, without other living contaminants.
Fermentation culture:
At 10m
3glucose 200kg, starch 320kg, Semen Maydis oil 20L, soybean cake powder 350kg, peptone 130kg, fish meal 120kg, potassium primary phosphate 7kg, light calcium carbonate 45kg, ammonium sulfate 43kg, sodium acetate 10kg, magnesium sulfate 34kg, ferrous sulfate 6kg is added in fermentor tank.
First by fermention medium sterilizing, cooling, then all moves into fermentor tank and cultivates by seed liquor.20h before fermentation, culture temperature controls at 26 ~ 28 DEG C; Fermentation 21h ~ fermentation ends, culture temperature controls at 25 ~ 26 DEG C; Mixing speed 120r/min; Incubation time 75h; The omnidistance tank pressure that ferments controls at 0.03 ~ 0.05MPa; PH6.5 ~ 7.5 in fermenting process; Carry out bacterium inspection in fermenting process, require without other miscellaneous bacteria; Airflow 500 ~ 700m
3/ h, fermentation culture terminates, cell concentration 32%; Fermentation unit 2641u/ml.
Claims (6)
1. Yi Zhong Wei Jini streptomycete fermentation produces the substratum of virginiamycin, comprise seed culture medium and fermention medium, it is characterized in that consisting of of described seed culture medium: maltose 20 ~ 30ml/L, mixing starch 10 ~ 20g/L, sweet oil 1 ~ 5ml/L, low temperature pressing soybean cake powder 15 ~ 25g/L, large rice distiller grain 20 ~ 30g/L, Zein powder 10 ~ 15g/L, light calcium carbonate 1 ~ 5g/L, ammonium sulfate 1 ~ 5g/L, maltin 0.01 ~ 0.03g/L;
Consisting of of described fermention medium: maltose 30 ~ 40ml/L, mixing starch 20 ~ 40g/L, sweet oil 1 ~ 5ml/L, low temperature pressing soybean cake powder 20 ~ 30g/L, large rice distiller grain 30 ~ 40g/L, Zein powder 20 ~ 30g/L, potassium primary phosphate 0.8 ~ 1.2g/L, light calcium carbonate 6 ~ 8g/L, ammonium sulfate 5 ~ 8g/L, sodium acetate 0.5 ~ 1.5g/L, magnesium sulfate 1 ~ 5g/L, ferrous sulfate 0.3 ~ 0.7g/L, nonionogenic tenside 0.01 ~ 0.05g/L, Tao Shi macroporous resin 1 ~ 5g/L, maltin 0.04 ~ 0.07g/L.
2. the substratum of virginiamycin is produced according to Wei Jini streptomycete fermentation according to claim 1, it is characterized in that the specification of quality of described large rice distiller grain is: protein content is more than 50%, moisture content controls within 5%, and the raw material of 80% can pass through 60 mesh sieves.
3. the substratum of virginiamycin is produced according to Wei Jini streptomycete fermentation according to claim 1, it is characterized in that described low temperature pressing soybean cake powder specification of quality is: soya bean squeezes 1 time under lower than the condition of 80 DEG C, require that its oil-contg controls 7 ~ 10%, protein content is more than 45%, and the raw material of 80% can pass through 80 mesh sieves.
4. produce the substratum of virginiamycin according to Wei Jini streptomycete fermentation according to claim 1, it is characterized in that described mixing starch refers in starch the pantothenic acid of 0.006% and the Thioctic Acid of 0.004% adding its weight.
5. produce the substratum of virginiamycin according to Wei Jini streptomycete fermentation according to claim 1, it is characterized in that described nonionogenic tenside is glycerin fatty acid ester or lipid acid sorb smooth (sapn) or polysorbate.
6. utilize a feed process for substratum fermentative production virginiamycin described in claim 1-5 any one, it is characterized in that carrying out feed supplement during the fermentation, comprise repairing, moisturizing, benefit sugar, mend alkali and mend nitrogenous source, wherein
A repairing controls: adopt stream addition to mend sweet oil,
Before fermentation, 10h need not carry out repairing,
Fermentation 11h ~ 20h: period controls lipid content 3.5 ~ 4.5%, when lipid content is lower than 4%, fills into sweet oil, when lipid content is more than 6%, then stops repairing, repairing amount (L)=(5-lipid content-resid amount) % × fermentating liquid volume (L),
21h is to fermentation ends in fermentation: period controls lipid content 1.5 ~ 2%, when lipid content is lower than 1.5%, fill into oil, when lipid content is more than 2%, then stop repairing, repairing amount (L)=(1.7-lipid content-resid amount) % × fermentating liquid volume (L);
B moisturizing:
Before fermentation, 10h need not carry out moisturizing,
Fermentation 11h ~ 20h: as fermented liquid cell concentration > 50%, adopts the moisturizing of stream addition, controls cell concentration 40 ~ 50%,
21h is to fermentation ends in fermentation: as fermented liquid cell concentration > 40%, adopts the moisturizing of stream addition, controls cell concentration 30 ~ 40%;
C pH controls:
Before fermentation, 10h, pH do not control,
Fermentation 11 ~ 20h: when the pH of fermented liquid is lower than 6.5, the sodium hydroxide solution adding 5 ~ 10% controls its pH 6.5 ~ 7.0,
21h is to fermentation ends in fermentation: when the pH of fermented liquid is lower than 6.0, the sodium hydroxide solution adding 5 ~ 10% controls its pH 6.0 ~ 6.5;
D fills into nitrogenous source: fermentation period respectively at 60h and 100h time fill into the ammonium sulfate that concentration is 5 ~ 10%, its amount of filling into is 1 ~ 1.5% of fermentating liquid volume;
E mends sugar:
10h before fermentation, does not add maltose,
Fermentation 11 ~ 20h, as reducing sugar content < 4%, adds maltose, when reducing sugar content is more than 6%, then stops adding maltose, mends sugar amount (kg)=(5-reducing sugar amount) % × fermentating liquid volume (L);
21h is to fermentation ends in fermentation, as reducing sugar content < 2%, adds maltose, when reducing sugar content is more than 2%, then stops adding maltose, mends sugar amount (kg)=(2-reducing sugar amount) % × fermentating liquid volume (L).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410829651.1A CN104480174B (en) | 2014-12-26 | 2014-12-26 | A kind of Wei Jini streptomycete fermentations produce the culture medium and feed process of virginiamycin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410829651.1A CN104480174B (en) | 2014-12-26 | 2014-12-26 | A kind of Wei Jini streptomycete fermentations produce the culture medium and feed process of virginiamycin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104480174A true CN104480174A (en) | 2015-04-01 |
| CN104480174B CN104480174B (en) | 2017-09-12 |
Family
ID=52754777
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410829651.1A Active CN104480174B (en) | 2014-12-26 | 2014-12-26 | A kind of Wei Jini streptomycete fermentations produce the culture medium and feed process of virginiamycin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104480174B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104846045A (en) * | 2015-06-02 | 2015-08-19 | 宁夏泰益欣生物科技有限公司 | Culture medium and culture method for producing sanglifehrin through fermentation of streptomyces flaveolus |
| CN105296464A (en) * | 2015-11-25 | 2016-02-03 | 曾志刚 | Method for screening 25hydroxyvitamin D3 high-yielding strain and screening polysorbate-80 content of fermentation medium |
| CN105368892A (en) * | 2015-11-05 | 2016-03-02 | 桂林电子科技大学 | Fermentation medium for increasing yield of nonactin and fermentation method |
| CN105441505A (en) * | 2015-12-29 | 2016-03-30 | 宁夏泰瑞制药股份有限公司 | Novel culture medium and culture method for fermentation production of mitomycin through Streptomyces caespitosus |
| CN106119314A (en) * | 2016-07-01 | 2016-11-16 | 宁夏泰瑞制药股份有限公司 | A kind of Harbin streptomycete fermentation produces culture medium and the cultural method of mibemycin |
| CN108753879A (en) * | 2018-06-26 | 2018-11-06 | 北京泛球生物科技有限公司 | A kind of fermentation method for producing improving virginiamycin yield |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101538539A (en) * | 2008-03-18 | 2009-09-23 | 上海医药工业研究院 | Culture medium for biosynthesis of virginiamycin M |
| CN102943102A (en) * | 2012-11-20 | 2013-02-27 | 江西兴鼎科技有限公司 | Method for biosynthesizing virginiamycin by streptomycete |
| CN103937848A (en) * | 2014-04-14 | 2014-07-23 | 宁夏泰瑞制药股份有限公司 | Novel culture medium for producing monensin by fermenting streptomyces cinnamonensis and culture method |
-
2014
- 2014-12-26 CN CN201410829651.1A patent/CN104480174B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101538539A (en) * | 2008-03-18 | 2009-09-23 | 上海医药工业研究院 | Culture medium for biosynthesis of virginiamycin M |
| CN102943102A (en) * | 2012-11-20 | 2013-02-27 | 江西兴鼎科技有限公司 | Method for biosynthesizing virginiamycin by streptomycete |
| CN103937848A (en) * | 2014-04-14 | 2014-07-23 | 宁夏泰瑞制药股份有限公司 | Novel culture medium for producing monensin by fermenting streptomyces cinnamonensis and culture method |
Non-Patent Citations (1)
| Title |
|---|
| 《中国酿造》: "表面活性剂偶联原位萃取发酵对阿维拉霉素产量的影响", 《中国酿造》 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104846045A (en) * | 2015-06-02 | 2015-08-19 | 宁夏泰益欣生物科技有限公司 | Culture medium and culture method for producing sanglifehrin through fermentation of streptomyces flaveolus |
| CN105368892A (en) * | 2015-11-05 | 2016-03-02 | 桂林电子科技大学 | Fermentation medium for increasing yield of nonactin and fermentation method |
| CN105368892B (en) * | 2015-11-05 | 2018-12-18 | 桂林电子科技大学 | It is a kind of for improving the fermentation medium and fermentation process of nonactin yield |
| CN105296464A (en) * | 2015-11-25 | 2016-02-03 | 曾志刚 | Method for screening 25hydroxyvitamin D3 high-yielding strain and screening polysorbate-80 content of fermentation medium |
| CN105441505A (en) * | 2015-12-29 | 2016-03-30 | 宁夏泰瑞制药股份有限公司 | Novel culture medium and culture method for fermentation production of mitomycin through Streptomyces caespitosus |
| CN105441505B (en) * | 2015-12-29 | 2019-01-29 | 宁夏泰瑞制药股份有限公司 | A kind of culture medium and cultural method of streptomyces caespitosus fermenting and producing mitomycin |
| CN106119314A (en) * | 2016-07-01 | 2016-11-16 | 宁夏泰瑞制药股份有限公司 | A kind of Harbin streptomycete fermentation produces culture medium and the cultural method of mibemycin |
| CN108753879A (en) * | 2018-06-26 | 2018-11-06 | 北京泛球生物科技有限公司 | A kind of fermentation method for producing improving virginiamycin yield |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104480174B (en) | 2017-09-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104480174B (en) | A kind of Wei Jini streptomycete fermentations produce the culture medium and feed process of virginiamycin | |
| CN104561180B (en) | A kind of culture medium and feed process for being mutated Avid kyowamycin fermenting and producing doractin | |
| CN103074402B (en) | Culture medium for producing tylosin through fermentation of streptomyces fradiae and fermentation method | |
| CN103484514B (en) | Culture medium for producing tylosin by fermenting streptomyces fradiae, and fermenting method | |
| CN103484509B (en) | Culture medium for fermentation production of spectinomycin through streptomyces spectabilis and fermentation method | |
| CN103146792B (en) | Culture medium for producing oxytetracycline through streptomyces rimosus fermentation and fermentation method | |
| CN103276031B (en) | A kind of heat-resisting streptomycete fermentation produces substratum and the fermentation process of acetylisovaleryl tylosin | |
| CN101560537B (en) | Fermentation method for producing high viscocity xanthan gum by xanthomonas campestris | |
| CN101613726A (en) | Utilize microbial fermentation to prepare the method for transparent xanthan gum | |
| CN103602714A (en) | Method for producing tetracycline by fermentation of streptomyces aureus | |
| CN111484959A (en) | Culture medium and culture method for producing pleocidin by utilizing saccharopolyspora spinosa fermentation | |
| CN101041837B (en) | Preparation method of new natural abscisic acid | |
| CN110846362B (en) | Neomycin sulfate fermentation clean production method | |
| CN103773831A (en) | Novel culture medium and culture method for producing aureomycin by fermenting streptomyces aureus | |
| CN110551783B (en) | Fermentation method for producing gentamicin by using continuous flow feeding material with oxygen consumption rate as key control parameter | |
| CN103642886A (en) | Medium for producing demethylchlortetracycline by fermenting streptomyces aureus and culturing method | |
| CN105754913B (en) | A kind of culture medium and cultural method of Str. lincolnensis fermenting and producing lincomycin | |
| CN103484515B (en) | A kind of substratum of streptomyces erythareus fermentative production erythromycin and cultural method | |
| CN104651431B (en) | A kind of culture medium and cultural method of micromonospora fermenting and producing gentamicin | |
| CN103642881B (en) | Medium for producing daunorubicin by fermenting streptomyces peucetius or streptomyces coeruleorubidus and fermentation method | |
| CN102660596A (en) | Medium of producing pleuromutilin by fermenting Pleurotus sp and its fermentation method | |
| CN112251472A (en) | Culture medium and culture method for producing coenzyme Q10 by fermentation of rhodobacter sphaeroides | |
| CN104195203A (en) | Culture medium for fermentation production of enramycin by using streptomyces fungicidicus and supplement method | |
| CN103642865A (en) | Medium for producing ivermectin by fermenting streptomyces avermitilis and fermenting method | |
| CN109576196A (en) | A kind of production method of the fermentation medium for producing doractin and doractin |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |