CN103667369A - Method for producing dihydroxyacetone by converting glycerin by virtue of biological fermentation process - Google Patents
Method for producing dihydroxyacetone by converting glycerin by virtue of biological fermentation process Download PDFInfo
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- CN103667369A CN103667369A CN201210360914.XA CN201210360914A CN103667369A CN 103667369 A CN103667369 A CN 103667369A CN 201210360914 A CN201210360914 A CN 201210360914A CN 103667369 A CN103667369 A CN 103667369A
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- otan
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- glycerine
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Abstract
The invention relates to a new method for producing dihydroxyacetone by converting glycerin by virtue of a biological fermentation process. The new method mainly comprises the following steps: producing dihydroxyacetone by fermenting a clavispora lusitaniae strain G10 with high glycerin resistance with two-order reactors and extracting dihydroxyacetone from the fermentation liquor. When the concentration of the glycerin substrate is 400g/L, the glycerin conversion rate is more than 85% and the yield is more than 75% after continuous fermentation is performed for 420 hours, so that the inhibiting effects of too high concentrations of the glycerin substrate of dihydroxyacetone prepared by existing microbiological fermentation methods and the product on the fermentation yield are effectively solved. The method adopted by the invention is simple to operate, is low in separation and extraction costs, is short in production time and is suitable for industrial production.
Description
Technical field
The present invention relates to a kind of novel method of producing otan, belong to biological technical field, be specially the glycerol dehydrogenase that Clavispora lusitaniae yeast (Clavispora lusitaniae) bacterial strain G10 fermentation produces and glycerine be oxidized to the novel method of production otan.
Technical background
Otan is a kind of naturally occurring ketose, there is biodegradability, edible and active to human body and environment toxicological harmless, its chemical property, of many uses and usage quantity is large, it is the imitative composition that shines agent of a kind of important medicine intermediate, industrial chemicals and foodstuff additive, makeup, also can be used as Anti-virus agent, can be used for the anti-corrosive fresh-keeping of fruits and vegetables, fishery products, meat product simultaneously.
Otan belongs to natural product, extracts difficulty large, and expensive, is difficult to form commercial size.People utilize the constructional feature of its three carbon ketose to carry out chemosynthesis, but will use expensive catalyzer, make it with high costs, are difficult to enter and commercially produce.Have report abroad, British Petroleum Co. has realized and has utilized formaldehyde method produce 1,3-Dihydroxyacetone and declared patent a few days ago, yet because formaldehyde method is produced 1,3-Dihydroxyacetone pollution greatly, facility investment is large, and Industry Promotion difficulty is large.Though the domestic suitability for industrialized production for otan is used biological fermentation process in batches to produce, but because the substrate glycerol concentration that can carry is low, fermented material rate of consumption is high, and the energy, water resources consumption are serious, the drawbacks limit such as waste discharge amount is larger the development of otan.
The principle of microbial transformation glycerol production otan is exactly the glycerol dehydrogenase that utilizes microbial metabolism to produce, and the hydroxyl on 2 C in glycerol molecule structure is reacted, and generates otan.Therefore, everyly in theory can utilize glycerine, and the production that the microorganism with corresponding glycerol dehydrogenase system carries out dihydro benzylacetone all has reaction conditions gentleness, substrate utilization ratio is high, by product is few, technique is simply easy to the advantages such as control.From Bertrand in 1898, find to utilize bacterium transformation of glycerol can be become after otan, various countries scientific research personnel produces otan to microorganism ferment glycerin and has carried out many-sided research, if find really to have microbial host bacillus aceticus, gluconobacter suboxydans, yeast and the neurospora etc. of bio-transformation otan industrial value, wherein the oxidizing glucose acidfast bacilli of acetobacter is the important bacterial classification that industrial fermentation is produced otan.Zymotechnique has batch fermentation culture method, immobilized cell method, resting cell method, stream to add fermentation culture method and the continuous working system of multistage reactor etc.
As far back as the 20 century 70s biotransformation method that just begins one's study, produce otan abroad, the Xian Yi U.S., Britain, Germany and Japan realize industrial applications, represent that enterprise is Japanese Daicel chemical industrial company, and annual capacity is 1100 tons of left and right.The research and development of China's Production by Microorganism Fermentation otan are later than abroad, mainly contain the units such as Zhejiang Polytechnical University, East China University of Science, Tianjin industrial microorganism institute and carried out relevant research and development, the many chemical industry in existing Shanghai hundred adopt batchwise to produce otan, but in fermenting process, if during the excessive concentration of substrate glycerine and product otan (when accumulative total meets or exceeds 80-120g/L), high osmotic pressure be will produce, thereby cellular lysate, inactivation made to ferment.Because substrate glycerol concentration is restricted, the productive rate of whole technique is reduced, water, electricity, combustion gas, raw material consumption are larger, and the production time is longer, thereby causes cost to increase.
Therefore,, in view of wide market application foreground and the good social benefit of otan, solving the problems referred to above that exist in the production of dihydro benzylacetone biological fermentation process is urgent tasks that face at present.
Summary of the invention
A kind of method that the object of this invention is to provide fermentative Production otan, the problem such as can overcome that the resistance to glycerol concentration of bacterial strain in current otan production process is low, batch fermentation easily makes cellular lysate inactivation and later separation extracts that the complex procedures, the separating power that exist in Product Process are little, cost is high and product recovery rate is low.The present invention adopts high glycerine patience bacterial strain effectively to improve the throughput of the otan of bacterial strain, adopts second-order reaction device, surpasses while defining numerical value and can automatically flow out fermented liquid, thereby reaction can be continued until fermented liquid concentration.
A kind of biological fermentation process glycerine converting provided by the invention is produced the novel process of otan, and its step comprises:
1) high efficiency production strain fermentation is produced otan
Clavispora lusitaniae yeast (Clavispora lusitaniae) G10 seed liquor is inoculated in the fermention medium of sterilizing, by sodium hydroxide or hydrochloric acid soln, control pH value during the fermentation, this fermenting process completes in the first rank reactor, afterwards bacteria suspension is mixed and banishes second-order reactor with sodium alginate soln and calcium chloride solution, glycerine stream after sterilizing adds in second-order reactor, after glycerol concentration gathers to a certain degree in second-order reactor, the pressure sensitive film of reactor lower part can be opened outflow fermented liquid by by-pass valve control;
2) from fermented liquid, extract otan
Adopt centrifugal or flocculence to remove the thalline in fermented liquid, by the fermented liquid of removing thalline in 10～100: 1 ratio concentrates, chromatography column on concentrated solution, adopt Zeo-karb, sherwood oil wet method dress post, take ethyl acetate-acetone mixed solvent as moving phase, and temperature is 10～20 ℃, bed aspect ratio is 15～50, sampling volume is than being 0.0.1～0.1BV, and flow velocity is 0.1～0.8BV/h, collects otan elutriant, vacuum concentration, obtains otan crude product; Otan crude product is dissolved in to the 0.5～1h that refluxes in ethyl acetate or acetone, reaction solution is cooled to 0 ℃～-15 ℃, have crystal to separate out, after filtration, vacuum-drying obtains otan crystal.
The method of microbe fermentation method oxidation glycerol production otan of utilizing provided by the invention has outstanding feature:
1) two-stage reactor is produced otan continuously, can create respectively the good environment that is applicable to microorganism cells growth and product production, avoided high concentration substrate, high density otan cell growth and the glycerine restraining effect to otan conversion process, realized cell abundant propagation and with the production of product;
2) in the reactor of subordinate phase, adopt the mode of glycerol feeding, effectively control the concentration of the interior substrate glycerine of reactor and product otan, thereby avoided the generation of high osmotic pressure, slow down thalline aging rate, improve thalline utilization ratio.
3) adopt cation exch ange adsorption technology separation and purification otan, in Continuous Fermentation Processes, utilize the selectivity filtration of film, immediately draw otan, reaction and separation processes is carried out simultaneously, simplified technological process, shorten the process time, improved product yield, reduced solvent consumption and environmental pollution.
Accompanying drawing explanation
Fig. 1 microbe fermentation method glycerine converting is produced the process flow sheet of otan
Embodiment
Below by embodiment, the present invention will be further described, and following embodiment is illustrative, is not determinate.
Embodiment 1
(1) high glycerine patience Clavispora lusitaniae yeast (Clavispora lusitaniae) bacterial strain G10 is inoculated in the first rank reactor that adds sterilization fermentation substratum, fermention medium is: yeast powder: 1%, and peptone: 3%, (NH
4)
2sO
4: 0.3%,, NH
2pO
4: 0.05%, MgSO
4: 0.01%, CaCO
3: 0.05%, with distilled water preparation, with NaOH solution, pH value is transferred to 7.0, through 120 ℃ and autoclaving.
(2) bacteria suspension in the first rank reactor is added to 5% sodium alginate soln and 2%CaCl
2solution, mix and banish second-order reactor, temperature 30-35 ℃, rotating speed 300r/min, ventilation 2vvm, pH value 5.0 left and right, carry out biocatalytic reaction with the speed stream glycerol adding of 15L/h, at second-order reactor outlet, increases pressure inductor, when glycerol concentration reaches 400g/L, can automatically flow out reaction solution.
(3) with whizzer, to reaction solution, carry out centrifugal, get supernatant concentration and obtain concentrated solution, chromatography column on concentrated solution, adopt PUROLITE PCR calcium type ion exchange resin, sherwood oil wet method dress post, adopting ethyl acetate-acetone mixed solvent that volume ratio is 70: 30 is moving phase, temperature is 10 ℃, bed aspect ratio is 25, sampling volume is than being 0.05BV, flow velocity is 0.25BV/h, collect otan effluent liquid, carry out vacuum concentration, otan crude product is dissolved in to the 0.5h that refluxes in ethyl acetate or acetone, reaction solution is cooled to 0 ℃ of left and right, there is crystal to separate out, after filtration, vacuum-drying obtains otan crystal.
(4) during substrate glycerol concentration 400g/L, otan concentration 368g/L, continuously ferments 420 hours, and glycerol conversion yield is 92.3%, and yield is 80%.
Embodiment 2
(1) high glycerine patience Clavispora lusitaniae yeast (Clavispora lusitaniae) bacterial strain G10 is inoculated in the first rank reactor that adds sterilization fermentation substratum, fermention medium is: yeast powder: 4%, and peptone: 1%, (NH
4)
2sO
4: 0.1%,, NH
2pO
4: 0.02%, MgSO
4: 0.05%, CaCO
3: 0.05%, with distilled water preparation, with NaOH solution, pH value is transferred to 5.0, through 120 ℃ and autoclaving.
(2) bacteria suspension in the first rank reactor is mixed with 8% sodium alginate soln and 2%CaCl
2solution mixes, banish second-order reactor, temperature 30-35 ℃, rotating speed 300r/min, ventilation 2vvm, pH value 5.0 left and right, carry out biocatalytic reaction with the speed stream glycerol adding of 20L/h, at second-order reactor outlet, increases pressure inductor, when glycerol concentration reaches 400g/L, can automatically flow out reaction solution.
(3) with whizzer, to reaction solution, carry out centrifugal, get supernatant concentration and obtain concentrated solution, chromatography column on concentrated solution, adopt PUROLITE PCR calcium type ion exchange resin, sherwood oil wet method dress post, adopting ethyl acetate-acetone mixed solvent that volume ratio is 65: 35 is moving phase, temperature is 15 ℃, bed aspect ratio is 30, sampling volume is than being 0.08BV, flow velocity is 0.5BV/h, collect otan effluent liquid, carry out vacuum concentration, otan crude product is dissolved in to the 0.5h that refluxes in ethyl acetate or acetone, reaction solution is cooled to 10 ℃ of left and right, there is crystal to separate out, after filtration, vacuum-drying obtains otan crystal.
(4) during substrate glycerol concentration 400g/L, otan concentration 361g/L, continuously ferments 420 hours, and glycerol conversion yield is 90.1%, and yield is 79%.
Embodiment 3
(1) high glycerine patience Clavispora lusitaniae yeast (Clavispora lusitaniae) bacterial strain G10 is inoculated in the first rank reactor that adds sterilization fermentation substratum, fermention medium is: yeast powder: 6%, and peptone: 4%, (NH
4)
2sO
4: 0.1%,, NH
2pO
4: 0.02%, MgSO
4: 0.05%, CaCO
3: 0.03%, with distilled water preparation, with NaOH solution, pH value is transferred to 4.0, through 120 ℃ and autoclaving.
(2) bacteria suspension in the first rank reactor is mixed with 10% sodium alginate soln and 4%CaCl
2solution mixes, banish second-order reactor, temperature 30-35 ℃, rotating speed 400r/min, ventilation 2vvm, pH value 5.0 left and right, carry out biocatalytic reaction with the speed stream glycerol adding of 25L/h, at second-order reactor outlet, increases pressure inductor, when glycerol concentration reaches 400g/L, can automatically flow out reaction solution.
(3) with whizzer, putting reaction solution carries out centrifugal, get supernatant concentration and obtain concentrated solution, chromatography column on concentrated solution, adopt PUROLITE PCR calcium type ion exchange resin, sherwood oil wet method dress post, adopting ethyl acetate-acetone mixed solvent that volume ratio is 50: 50 is moving phase, temperature is 15 ℃, bed aspect ratio is 50, sampling volume is than being 0.03BV, flow velocity is 0.5BV/h, collect otan effluent liquid, carry out vacuum concentration, otan crude product is dissolved in to the 1h that refluxes in ethyl acetate or acetone, reaction solution is cooled to 5 ℃ of left and right, there is crystal to separate out, after filtration, vacuum-drying obtains otan crystal.
(4) during substrate glycerol concentration 400g/L, otan concentration 349g/L, continuously ferments 420 hours, and glycerol conversion yield is 87.3%, and yield is 72%.
Embodiment 4
(1) high glycerine patience Clavispora lusitaniae yeast (Clavispora lusitaniae) bacterial strain G10 is inoculated in the first rank reactor that adds sterilization fermentation substratum, fermention medium is: yeast powder: 5%, and peptone: 3%, (NH
4)
2sO
4: 0.45%, NH
2pO
4: 0.02%, MgSO
4: 0.05%, CaCO
3: 0.02%, with distilled water preparation, with NaOH solution, pH value is transferred to 4.0, through 120 ℃ and autoclaving.
(2) bacteria suspension in the first rank reactor is mixed with 8% sodium alginate soln and 6%CaCl
2solution mixes, banish second-order reactor, temperature 30-35 ℃, rotating speed 400r/min, ventilation 2vvm, pH value 5.0 left and right, carry out biocatalytic reaction with the speed stream glycerol adding of 20L/h, at second-order reactor outlet, increases pressure inductor, when glycerol concentration reaches 400g/L, can automatically flow out reaction solution.
(3) with whizzer, putting reaction solution carries out centrifugal, get supernatant concentration and obtain concentrated solution, chromatography column on concentrated solution, adopt PUROLITE PCR calcium type ion exchange resin, sherwood oil wet method dress post, adopting ethyl acetate-acetone mixed solvent that volume ratio is 50: 50 is moving phase, temperature is 15 ℃, bed aspect ratio is 50, sampling volume is than being 0.03BV, flow velocity is 0.5BV/h, collect otan effluent liquid, carry out vacuum concentration, otan crude product is dissolved in to the 1h that refluxes in ethyl acetate or acetone, reaction solution is cooled to 5 ℃ of left and right, there is crystal to separate out, after filtration, vacuum-drying obtains otan crystal.
(4) during substrate glycerol concentration 400g/L, otan concentration 355g/L, continuously ferments 420 hours, and glycerol conversion yield is 89.2%, and yield is 78%.
Claims (6)
1. a technique of utilizing biological fermentation process glycerine converting existence otan, is characterized in that comprising the following steps:
1) superior strain fermentative production otan
Fermentation strain is inoculated in after seed culture in the fermention medium of sterilizing, by sodium hydroxide and hydrochloric acid soln, control pH value during the fermentation, this fermenting process completes in the first rank reactor, afterwards bacteria suspension is mixed and banishes second-order reactor with sodium alginate soln and calcium chloride solution, glycerine stream after sterilizing adds in second-order reactor, after glycerol concentration gathers to a certain degree in second-order reactor, the pressure sensitive device of reactor lower part can be opened outflow fermented liquid by by-pass valve control, fermented liquid is through filtering net, elimination thalline and other solids, by filtering membrane, draw otan and glycerol mixture,
2) from fermented liquid, extract otan
Fermented liquid is in 10～100: the ratio of 1 (V/V) is concentrated, chromatography column on concentrated solution, adopts Zeo-karb, sherwood oil wet method dress post, employing ethyl acetate-acetone mixed solvent is moving phase, temperature is 10～20 ℃, and bed aspect ratio is 15～50: 1, and sampling volume ratio is 0.01～0.1BV, flow velocity is 0.1～0.8BV/h, collect otan fragment, vacuum concentration, obtains otan crude product; Otan crude product is dissolved in to the 0.5～1h that refluxes in ethyl acetate or acetone, reaction solution is cooled to 0 ℃～-15 ℃, have crystal to separate out, after filtration, vacuum-drying obtains otan crystal.
2. a kind of processing method of utilizing biological fermentation process glycerine converting existence otan according to claim 1, it is characterized in that: fermentation strain is Clavispora lusitaniae yeast (Clavispora lusitaniae) bacterial strain G10, and its culture presevation is numbered CGMCC No.6414.
3. a kind of processing method of utilizing biological fermentation process glycerine converting existence otan according to claim 1, it is characterized in that: fermentation strain seed culture and consist of: yeast powder 1～7% (g/L), peptone 0.2～6% (g/L), (NH
4)
2sO
40.05～0.5% (g/L), NH
2pO
40.01～0.05% (g/L), MgSO
40.01～0.05% (g/L), CaCO
30.01～0.05% (g/L), all the other are distilled water, pH value is controlled at 4.0～7.0.
4. a kind of processing method of utilizing biological fermentation process glycerine converting existence otan according to claim 1, it is characterized in that: the first rank reactor and second-order reactor refer to a second-order reaction device, wherein in the first rank reactor, be mainly used in breeding and the growth of bacterial strain, the glycerine that second-order reactor mainly utilizes the glycerol dehydrogenase oxydasis stream in the bacteria suspension in the first rank reactor to add, second-order reactor lower end is connected with pressure inductor, pressure in question response device surpasses after certain numerical value, bottom by-pass valve control can be opened automatically, flow out fermented liquid.
5. a kind of processing method of utilizing biological fermentation process glycerine converting existence otan according to claim 1, is characterized in that: the flow velocity that glycerine flows into is 10～30L/h.
6. a kind of processing method of utilizing biological fermentation process glycerine converting existence otan according to claim 1, is characterized in that: the addition of sodium alginate soln is 1～10%, and calcium chloride solution is saturated calcium chloride solution, and its addition is 2～8%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104357340A (en) * | 2014-11-17 | 2015-02-18 | 中国食品发酵工业研究院 | Method for producing L-malic acid by virtue of biotransformation of fumaric acid |
| WO2017195870A1 (en) * | 2016-05-12 | 2017-11-16 | サントリーホールディングス株式会社 | L-hydroxyproline-containing yeast cell or cell culture product or extract of same, use thereof, and method for producing l-hydroxyproline |
| TWI837076B (en) | 2016-05-12 | 2024-04-01 | 日商三得利控股股份有限公司 | L-hydroxyproline-containing yeast cells, bacterial cell cultures, or extracts thereof, their uses, and methods for producing L-hydroxyproline |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1821418A (en) * | 2005-12-13 | 2006-08-23 | 浙江工业大学 | Producing dihydroxy acetone by microbe method |
| CN101591681A (en) * | 2009-04-13 | 2009-12-02 | 浙江工业大学 | A kind of method of producing dihydroxyacetone through microbial transformation |
-
2012
- 2012-09-26 CN CN201210360914.XA patent/CN103667369A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1821418A (en) * | 2005-12-13 | 2006-08-23 | 浙江工业大学 | Producing dihydroxy acetone by microbe method |
| CN101591681A (en) * | 2009-04-13 | 2009-12-02 | 浙江工业大学 | A kind of method of producing dihydroxyacetone through microbial transformation |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104357340A (en) * | 2014-11-17 | 2015-02-18 | 中国食品发酵工业研究院 | Method for producing L-malic acid by virtue of biotransformation of fumaric acid |
| WO2017195870A1 (en) * | 2016-05-12 | 2017-11-16 | サントリーホールディングス株式会社 | L-hydroxyproline-containing yeast cell or cell culture product or extract of same, use thereof, and method for producing l-hydroxyproline |
| KR20190006954A (en) * | 2016-05-12 | 2019-01-21 | 산토리 홀딩스 가부시키가이샤 | Cell culture or cell culture of yeast containing L-hydroxyproline, or extract thereof and use thereof, and method for producing L-hydroxyproline |
| KR102265246B1 (en) * | 2016-05-12 | 2021-06-15 | 산토리 홀딩스 가부시키가이샤 | Yeast cells or cultured cells containing L-hydroxyproline or extracts thereof and uses thereof, and methods for producing L-hydroxyproline |
| TWI837076B (en) | 2016-05-12 | 2024-04-01 | 日商三得利控股股份有限公司 | L-hydroxyproline-containing yeast cells, bacterial cell cultures, or extracts thereof, their uses, and methods for producing L-hydroxyproline |
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Application publication date: 20140326 |