CN1928104B - Secondary fermentation technology of lysine fermentation liquor - Google Patents
Secondary fermentation technology of lysine fermentation liquor Download PDFInfo
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- CN1928104B CN1928104B CN2006100687809A CN200610068780A CN1928104B CN 1928104 B CN1928104 B CN 1928104B CN 2006100687809 A CN2006100687809 A CN 2006100687809A CN 200610068780 A CN200610068780 A CN 200610068780A CN 1928104 B CN1928104 B CN 1928104B
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- lysine
- fermentation
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- methionin
- yeast
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- 238000000855 fermentation Methods 0.000 title claims abstract description 87
- 230000004151 fermentation Effects 0.000 title claims abstract description 87
- 239000004472 Lysine Substances 0.000 title claims abstract description 45
- KDXKERNSBIXSRK-UHFFFAOYSA-N Lysine Natural products NCCCCC(N)C(O)=O KDXKERNSBIXSRK-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000005516 engineering process Methods 0.000 title abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims abstract description 23
- 230000001105 regulatory effect Effects 0.000 claims abstract description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 32
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 claims description 21
- 239000002253 acid Substances 0.000 claims description 19
- 238000003756 stirring Methods 0.000 claims description 16
- 241000235646 Cyberlindnera jadinii Species 0.000 claims description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 5
- 238000011017 operating method Methods 0.000 claims 1
- 238000005342 ion exchange Methods 0.000 abstract description 32
- 239000013078 crystal Substances 0.000 abstract description 18
- 238000004519 manufacturing process Methods 0.000 abstract 2
- 239000012528 membrane Substances 0.000 abstract 1
- 230000000813 microbial effect Effects 0.000 abstract 1
- XUYPXLNMDZIRQH-LURJTMIESA-N N-acetyl-L-methionine Chemical compound CSCC[C@@H](C(O)=O)NC(C)=O XUYPXLNMDZIRQH-LURJTMIESA-N 0.000 description 40
- 229930182817 methionine Natural products 0.000 description 40
- 239000002932 luster Substances 0.000 description 30
- 238000005469 granulation Methods 0.000 description 18
- 230000003179 granulation Effects 0.000 description 18
- 238000005374 membrane filtration Methods 0.000 description 16
- 230000004907 flux Effects 0.000 description 15
- 239000002054 inoculum Substances 0.000 description 6
- 238000009434 installation Methods 0.000 description 6
- 239000011259 mixed solution Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- 238000009423 ventilation Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 235000020776 essential amino acid Nutrition 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- FFEARJCKVFRZRR-BYPYZUCNSA-N L-methionine Chemical compound CSCC[C@H](N)C(O)=O FFEARJCKVFRZRR-BYPYZUCNSA-N 0.000 description 1
- 229930195722 L-methionine Natural products 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 108010064851 Plant Proteins Proteins 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000012262 fermentative production Methods 0.000 description 1
- 238000011081 inoculation Methods 0.000 description 1
- 238000011169 microbiological contamination Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 230000000050 nutritive effect Effects 0.000 description 1
- 235000021118 plant-derived protein Nutrition 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The present invention relates to deep microbial fermentation technology in bioengineering technology, and is especially secondary fermentation technology through adding active yeast to fermented lysine liquid. After the fermented lysine liquid is regulated to proper pH value, cultured yeast is added for secondary fermentation. The secondary fermentation can lower residual sugar content, improve viscosity of the fermented liquid, raise the membrane filtered amount by one time, raise ion exchange yield and crystal purity, and improve lysine crystal granularity and color. In the production of 65wt% concentration feed level lysine product, the secondary fermentation can facilitate the downstream treatment of lysine, lower production cost and raise efficiency.
Description
Technical field:
The present invention relates to the microorganism submerged fermentation technology in the technical field of bioengineering, be specifically related to add yeast in a kind of lysine fermentation liquor after fermenting lysine finishes and regulates pH and carry out second fermentation process with physiologically active.
Background technology:
Methionin is the indispensable amino acid of humans and animals nutrition, and is the primary amino acid that only only L type just can be used effectively in eight kinds of indispensable amino acids, is the amino acid that lacks most in the plant proteins such as wheat, corn, rice.Therefore, Methionin is widely used in aspects such as nutritive food, food fortifier, feed and medicine.Because internal feed industry alarming development speed, the market requirement of L-Methionin grows with each passing day.But when fermentative Production Methionin is purified, because residual sugar height in the fermented liquid causes problems such as membrane filtration difficulty, ion-exchange yield and purity are low; If fermented liquid directly concentrate to be made feed, Maillard reaction can take place, cause Methionin to be damaged and make the easy moisture absorption of product and bond.There is research to point out to consume residual sugar, increases protein content simultaneously at the yeast of the different amounts of different steps inoculation of lysine fermentation process.But this processing requirement yeast sterile culture and add yeast in the process of fermenting lysine, thereby increased the complicacy and the microbiological contamination probability of technology may produce the growth of bacterium and produce acid simultaneously and produces certain negative impact Methionin.Thereby seek a kind of more simple, convenient and effective means, be necessary.
Summary of the invention:
In order to solve the problems referred to above in lysine fermentation process, improve the yield of Methionin, the invention provides a kind of yeast that in the lysine fermentation liquor of fermentation ends, adds and carry out second fermentation process with physiologically active.
Purpose of the present invention can realize by following technical measures: the fermented liquid that fermenting lysine finishes to obtain is used about acid for adjusting pH value 3.0-6.0, inserted the yeast with physiologically active and carry out Secondary Fermentation.
The controlled variable of fermentor tank is in the fermenting process: temperature 28-32 ℃, ventilating ratio 1: 1-1: 2vvm, stir speed (S.S.) 80-150rpm, fermentation time 6-12 hour.
The 5-10% that the sophisticated yeast-inoculated amount of fermentation culture is pressed fermentating liquid volume adds.
Used yeast is Candida utilis, bread yeast etc.
The acid of used adjusting pH can be sulfuric acid or hydrochloric acid, and the vitriolic effect is better than hydrochloric acid.
In the pH3.0-6.0 scope, yeast all can be grown, and yeast growth is better in the pH3.0-5.0 scope, zymic growth result the best in the lysine fermentation liquor when pH is 4.0.
Above-mentioned fermenting process both can carry out in gnotobasis, also can carry out in non-sterile environment, and was lower to environmental requirement, and in non-sterile environment, fermenting process is easier to carry out.
The operation of above-mentioned Secondary Fermentation technology can be a batch operation, also can be operate continuously.
Effect during batch operation: reduced the viscosity of residual sugar and fermented liquid, improved Methionin yield and purity etc.; Directly avoided sticking wall during granulation.During operate continuously when effect and batch operation effect but compare the utilization ratio that has improved fermentor tank much at one with batch operation, reduced non-fermentation time.
By fermentation, residual sugar is reduced to below 1% in the fermented liquid, and fermented liquid can directly enter Methionin purification workshop section or granulation workshop section produces the product that needs.
Characteristics of the present invention are: can reduce the residual sugar and the viscosity of fermented liquid, thereby significantly improve physics, the chemical property of fermented liquid, help the refining extraction of Methionin and the granulation preparation of lysine feed.Help the improvement of the outward appearance of Methionin crystal finished product and finished feed simultaneously.
Embodiment:
Embodiment 1:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 2.1%, under the non-sterile situation with sulfuric acid with its pH regulator to 4.0 after, to wherein adding about 11m
3Residual sugar reduces to 0.8% after cultivating sophisticated Candida utilis rear venting fermentation culture 8h, and fermentation broth viscosity descends, and the membrane filtration flux is by 19m
3/ h is increased to 45m
3/ h, Methionin ion-exchange yield is increased to 95% by 90%, and ion-exchange purity is increased to 75% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, and the direct granulation wall sticking phenomenon of treated fermented liquid reduces, and granularity and color and luster all improve.
Embodiment 2:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 2.0%, under the non-sterile situation with sulfuric acid with its pH regulator to 3.5 after, to wherein adding about 10m
3Cultivate behind the sophisticated bread yeast under the condition of 28 ℃ of temperature, ventilating ratio 1: 1vvm, stir speed (S.S.) 80rpm ventilating fermentation and cultivate 10h, residual sugar reduces to 0.6%, and fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 47m
3/ h, Methionin ion-exchange yield is increased to 95% by 88%, and ion-exchange purity is increased to 77% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 3:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 1.9%, under the non-sterile situation with sulfuric acid with its pH regulator to 4.5 after, to wherein adding about 15m
3Cultivate behind the sophisticated Candida utilis after ventilating fermentation under the condition of 30 ℃ of temperature, ventilating ratio 1: 1.5vvm, stir speed (S.S.) 120rpm is cultivated 7h residual sugar and reduce to 0.3%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 49m
3/ h, Methionin ion-exchange yield is increased to 96% by 90%, and ion-exchange purity is increased to 80% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 4:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 2.0%, under the non-sterile situation with sulfuric acid with its pH regulator to 4.0 after, to wherein adding about 12m
3Cultivate behind the sophisticated bread yeast after ventilating fermentation under the condition of 31 ℃ of temperature, ventilating ratio 1: 2vvm, stir speed (S.S.) 100rpm is cultivated 9h residual sugar and reduce to 0.3%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 45m
3/ h, Methionin ion-exchange yield is increased to 97% by 90%, and ion-exchange purity is increased to 78% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 5:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 2.3%, under the non-sterile situation with sulfuric acid with its pH regulator to 4.2 after, to wherein adding about 16m
3Cultivate behind the sophisticated bread yeast after ventilating fermentation under the condition of 29 ℃ of temperature, ventilating ratio 1: 1.4vvm, stir speed (S.S.) 150rpm is cultivated 10h residual sugar and reduce to 0.4%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 44m
3/ h, Methionin ion-exchange yield is increased to 96% by 90%, and ion-exchange purity is increased to 79% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 6:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 1.8%, under the non-sterile situation with sulfuric acid with its pH regulator to 4.8 after, to wherein adding about 14m
3Cultivate behind the sophisticated bread yeast after ventilating fermentation under the condition of 32 ℃ of temperature, ventilating ratio 1: 1.7vvm, stir speed (S.S.) 130rpm is cultivated 6h residual sugar and reduce to 0.5%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 48m
3/ h, Methionin ion-exchange yield is increased to 98% by 90%, and ion-exchange purity is increased to 80% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 7:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 2.0%, under the non-sterile situation with sulfuric acid with its pH regulator to 5.0 after, to wherein adding about 16m
3Cultivate behind the sophisticated Candida utilis after ventilating fermentation under the condition of 30 ℃ of temperature, ventilating ratio 1: 1.6vvm, stir speed (S.S.) 80rpm is cultivated 12h residual sugar and reduce to 0.4%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 45m
3/ h, Methionin ion-exchange yield is increased to 97% by 90%, and ion-exchange purity is increased to 82% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 8:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 1.9%, under the non-sterile situation with sulfuric acid with its pH regulator to 5.5 after, to wherein adding about 20m
3Cultivate behind the sophisticated Candida utilis after ventilating fermentation under the condition of 29 ℃ of temperature, ventilating ratio 1: 1.1vvm, stir speed (S.S.) 90rpm is cultivated 10h residual sugar and reduce to 0.5%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 45m
3/ h, Methionin ion-exchange yield is increased to 97% by 90%, and ion-exchange purity is increased to 81% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 9:
300m
3Fermentor tank in 200m is housed
3Lysine fermentation liquor, its residual sugar is 2.2%, under the non-sterile situation with hydrochloric acid with its pH regulator to 6.0 after, to wherein adding about 20m
3Cultivate behind the sophisticated bread yeast after ventilating fermentation under the condition of 31 ℃ of temperature, ventilating ratio 1: 1.8vvm, stir speed (S.S.) 140rpm is cultivated 8h residual sugar and reduce to 0.9%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 38m
3/ h, Methionin ion-exchange yield is increased to 95% by 90%, and ion-exchange purity is increased to 75% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 10:
Lysine fermentation liquor, residual sugar 2.1%, after regulating its pH to 3.5 with sulfuric acid in the acid adjustment jar, insert an amount of sophisticated Candida utilis of cultivation according to the volume of lysine fermentation liquor by 10% inoculum size after thorough mixing even, again to 300m
3Fermentor tank feed about 200m
3Mixed solution, after ventilating fermentation under the condition of 29 ℃ of temperature, ventilating ratio 1: 1.3vvm, stir speed (S.S.) 110rpm is cultivated 3.5h, squeezing into successively ventilates respectively in follow-up three acid adjustment jars that have ventilation installation under the same conditions again cultivates 2h, residual sugar reduces to 0.7%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 42m
3/ h, Methionin ion-exchange yield is increased to 95% by 90%, and ion-exchange purity is increased to 76% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 11:
Lysine fermentation liquor, residual sugar 2.0%, after regulating its pH to 4.0 with sulfuric acid in the acid adjustment jar, insert an amount of sophisticated Candida utilis of cultivation according to the volume of lysine fermentation liquor by 10% inoculum size after thorough mixing even, again to 300m
3Fermentor tank feed about 200m
3Mixed solution, after ventilating fermentation under the condition of 30 ℃ of temperature, ventilating ratio 1: 1.4vvm, stir speed (S.S.) 110rpm is cultivated 3h, squeezing into successively ventilates respectively in follow-up three acid adjustment jars that have ventilation installation under the same conditions again cultivates about 2h, residual sugar is reduced to below 0.8%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 42m
3/ h, Methionin ion-exchange yield is increased to 95% by 90%, and ion-exchange purity is increased to 76% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 12:
Lysine fermentation liquor, residual sugar 2.1%, after regulating its pH to 4.5 with sulfuric acid in the acid adjustment jar, insert an amount of sophisticated bread yeast of cultivation according to the volume of lysine fermentation liquor by 9% inoculum size after thorough mixing even, again to 300m
3Fermentor tank feed about 200m
3Mixed solution, after ventilating fermentation under the condition of 28 ℃ of temperature, ventilating ratio 1: 2vvm, stir speed (S.S.) 110rpm is cultivated 5h, squeezing into successively ventilates respectively in follow-up three acid adjustment jars that have ventilation installation under the same conditions again cultivates 2h, residual sugar is reduced to below 0.5%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 45m
3/ h, Methionin ion-exchange yield is increased to 96% by 90%, and ion-exchange purity is increased to 78% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 13:
Lysine fermentation liquor, residual sugar 1.9%, after regulating its pH to 5.0 with sulfuric acid in the acid adjustment jar, insert an amount of sophisticated Candida utilis of cultivation according to the volume of lysine fermentation liquor by 8% inoculum size after thorough mixing even, again to 300m
3Fermentor tank feed about 200m
3Mixed solution, after ventilating fermentation under the condition of 31 ℃ of temperature, ventilating ratio 1: 1.9vvm, stir speed (S.S.) 110rpm is cultivated 4h, squeezing into successively ventilates respectively in follow-up three acid adjustment jars that have ventilation installation under the same conditions again cultivates 2.5h, residual sugar is reduced to below 0.6%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 44m
3/ h, Methionin ion-exchange yield is increased to 97% by 90%, and ion-exchange purity is increased to 79% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 14:
Lysine fermentation liquor, residual sugar 1.8%, after regulating its pH to 5.5 with sulfuric acid in the acid adjustment jar, insert an amount of sophisticated bread yeast of cultivation according to the volume of lysine fermentation liquor by 5% inoculum size after thorough mixing even, again to 300m
3Fermentor tank feed about 200m
3Mixed solution, after ventilating fermentation under the condition of 32 ℃ of temperature, ventilating ratio 1: 1.5vvm, stir speed (S.S.) 100rpm is cultivated 3h, squeezing into successively ventilates respectively in follow-up three acid adjustment jars that have ventilation installation under the same conditions again cultivates 2.5h, residual sugar is reduced to below 0.7%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 45m
3/ h, Methionin ion-exchange yield is increased to 96% by 90%, and ion-exchange purity is increased to 80% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Embodiment 15:
Lysine fermentation liquor, residual sugar 2.2%, after regulating its pH to 6.0 with sulfuric acid in the acid adjustment jar, insert an amount of sophisticated bread yeast of cultivation according to the volume of lysine fermentation liquor by 12% inoculum size after thorough mixing even, again to 300m
3Fermentor tank feed about 200m
3Mixed solution, after ventilating fermentation under the condition of 30 ℃ of temperature, ventilating ratio 1: 2vvm, stir speed (S.S.) 90rpm is cultivated 4h, squeezing into successively ventilates respectively in follow-up three acid adjustment jars that have ventilation installation under the same conditions again cultivates 3h, residual sugar is reduced to below 0.5%, fermentation broth viscosity descends, and the membrane filtration flux is by 20m
3/ h is increased to 46m
3/ h, Methionin ion-exchange yield is increased to 97% by 90%, and ion-exchange purity is increased to 80% by 70%.Methionin crystal finished product color and luster becomes sparkling and crystal-clear, the no longer sticking wall of the direct granulation of treated fermented liquid, and granularity and color and luster all improve.
Claims (5)
1. the second fermentation process of a lysine fermentation liquor, it is characterized in that: the fermented liquid that fermenting lysine finishes is adjusted to pH 3.0-6.0 with acid, the yeast that access has physiologically active carries out Secondary Fermentation, wherein the controlled variable in the fermentor tank is as follows in the fermenting process: temperature 28-32 ℃, ventilating ratio 1: 1-1: 2vvm, stir speed (S.S.) 80-150rpm, fermentation time 6-12 hour; The yeast with physiologically active that is adopted is Candida utilis or bread yeast; The yeast-inoculated amount with physiologically active that inserts is the 5-10% of the volume of fermented liquid.
2. the second fermentation process of lysine fermentation liquor according to claim 1 is characterized in that:
The fermented liquid that fermenting lysine finishes is adjusted to pH 3.0-5.0 with acid.
3. the second fermentation process of lysine fermentation liquor according to claim 1 and 2 is characterized in that:
The fermented liquid that fermenting lysine finishes is adjusted to pH 4.0 with acid.
4. the second fermentation process of lysine fermentation liquor according to claim 3 is characterized in that: regulating the used acid of pH is sulfuric acid or hydrochloric acid.
5. the second fermentation process of lysine fermentation liquor according to claim 1, it is characterized in that: operating procedure is batch operation or operate continuously.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006100687809A CN1928104B (en) | 2006-09-07 | 2006-09-07 | Secondary fermentation technology of lysine fermentation liquor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006100687809A CN1928104B (en) | 2006-09-07 | 2006-09-07 | Secondary fermentation technology of lysine fermentation liquor |
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| CN1928104A CN1928104A (en) | 2007-03-14 |
| CN1928104B true CN1928104B (en) | 2010-09-22 |
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| CN2006100687809A Expired - Fee Related CN1928104B (en) | 2006-09-07 | 2006-09-07 | Secondary fermentation technology of lysine fermentation liquor |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1148090A (en) * | 1995-10-18 | 1997-04-23 | 北京思拓粮食仓储应用技术研究所 | Two-step fermantation process for producing glycerine |
| CN1182133A (en) * | 1996-10-15 | 1998-05-20 | 味之素株式会社 | Method of fermentation producing L-amino-acid |
-
2006
- 2006-09-07 CN CN2006100687809A patent/CN1928104B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1148090A (en) * | 1995-10-18 | 1997-04-23 | 北京思拓粮食仓储应用技术研究所 | Two-step fermantation process for producing glycerine |
| CN1182133A (en) * | 1996-10-15 | 1998-05-20 | 味之素株式会社 | Method of fermentation producing L-amino-acid |
Non-Patent Citations (8)
| Title |
|---|
| 刘杰凤.固定化酵母产赖氨酸的研究.广东石油化工专科学校学报 第1期总第8期.1995,(第1期总第8期),65-68，具体参见摘要、第67页表3及第2.5节. |
| 刘杰凤.固定化酵母产赖氨酸的研究.广东石油化工专科学校学报 第1期总第8期.1995,(第1期总第8期),65-68,具体参见摘要、第67页表3及第2.5节. * |
| 富英华等.L-赖氨酸产生菌FH128菌株的研究.上海化工 2.2000,(2),16-18. |
| 富英华等.L-赖氨酸产生菌FH128菌株的研究.上海化工 2.2000,(2),16-18. * |
| 张明祥等.Lys-02菌株赖氨酸固态发酵工艺研究.粮食与饲料工业 8.2002,(8),28-30. |
| 张明祥等.Lys-02菌株赖氨酸固态发酵工艺研究.粮食与饲料工业 8.2002,(8),28-30. * |
| 龙万凯.我国赖氨酸工业技术新进展.化学工程31 5.2003,31(5),74-78. |
| 龙万凯.我国赖氨酸工业技术新进展.化学工程31 5.2003,31(5),74-78. * |
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| CN1928104A (en) | 2007-03-14 |
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