CN109706195B - Production process of granular threonine - Google Patents
Production process of granular threonine Download PDFInfo
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Abstract
The invention belongs to the technical field of amino acid production, and discloses a production process of granular threonine, which comprises the following steps: step 1) preparing a fermentation culture medium, step 2) fermenting, step 3) centrifuging, and step 4) preparing the granular threonine. The invention has high threonine yield and less by-products.
Description
Technical Field
The invention belongs to the field of amino acid production, and particularly relates to a production process of granular threonine.
Background
Threonine is easily soluble in water but insoluble in organic solvents such as ethanol and diethyl ether, belongs to aliphatic amino acid, tastes slightly sweet, and is an essential amino acid for human and animal and plant proteins. Threonine plays an increasingly important role in human life as one of amino acids essential to the human body. With the development of the breeding industry and the rapid increase of the livestock and poultry feed demand, threonine plays a role in the nutritional ingredients which must be taken from the outside and is more and more emphasized. Has wide application in medicine, food, feed and other fields. Threonine belongs to one of products of industrial fermentation, and according to data statistics, the global threonine supply in 2017 reaches 68.5 ten thousand tons, the equivalent increase is 15.5 percent, or the global threonine supply increases 9.2 ten thousand tons, and the increase is 80 percent from China. In 2017, the supply of Chinese threonine reaches 53.5 ten thousand tons, and the increase is 15.6 percent on the same scale, which accounts for 78 percent of the global market. Since 2013, the average compound increase rate of the supply of the global threonine is 13.4 percent, and the increase rate is reduced by about half compared with the increase rate between 2003 and 2013. China threonine production enterprises in 2017 mainly use plum blossom, Fufeng, Yipin and Chengfu, and supplement Dacheng and Xijie; international enterprises mainly use ajinomoto and ADM. In 2017, the domestic threonine is exported 37.4 ten thousand tons, accounting for 69.9 percent of the yield, and the domestic supply is 16.1 ten thousand tons, and the domestic demand is 13 ten thousand tons.
The engineering strain of Escherichia coli is a main strain for producing threonine by microbial industrial fermentation, and can generate metabolic byproducts such as acetic acid, alanine, valine and arginine while producing L-threonine by fermentation, thereby influencing the growth of the strain and the synthesis and accumulation of L-threonine to a certain extent. The inhibiting effect of acetic acid is obvious, when the acetic acid is accumulated to a certain concentration, the specific growth rate of thalli is rapidly reduced, the product synthesis is greatly reduced, vicious circle is formed, and meanwhile, the expression of exogenous genes is also seriously influenced. The adverse effect of acetic acid accumulation on cell metabolism is a considerable problem in the expression of foreign proteins using E.coli as a host bacterium. How to reduce the content of acetic acid and thus increase biomass and threonine production is the focus of our research. In the literature, "control of acetic acid in the fermentation process of L-threonine, fermentation science and technology communication 2012", in the process of preparing threonine by fermentation of escherichia coli, the generation of acetic acid as a byproduct is controlled by selecting appropriate fermentation conditions, so that the generation of acetic acid can be reduced, but the reduction range is not obvious, the yield of threonine cannot be greatly improved, and the industrial popularization value is not high. The applicant's prior patent document "a method for producing threonine with ultra-low water content" describes a medium: 80g/L glucose, 20g/L corn steep liquor, 2g/L ammonium sulfate, 0.75g/L calcium carbonate and KH2PO4 0.2g/L，K2HPO4 0.2g/L, NaCl 0.2g/L and pH value 6.5; the content of threonine in the fermentation liquor can reach 10g/100ml at most, but the death rate of the strain in the later stage of fermentation is high, the glucose consumption is high, and the yield of threonine in the fermentation liquor is to be improved. On the basis of this, the applicant has continued to develop a process for the preparation of threonine in granular form by fermentation inThe chlamydomonas reinhardtii is inoculated in a fermentation manner, acetic acid in fermentation liquor can be used as a carbon source to perform non-light action, and glycerol is difficult to be used as the carbon source, so that the inhibition effect on threonine production of escherichia coli is relieved, and trace photosynthesis can be performed to release oxygen for the threonine production by escherichia coli fermentation; by adding chlamydomonas reinhardtii, the threonine yield can be improved, and the mycoprotein yield is correspondingly improved. However, the mixed fermentation process of the strains is difficult to control, the fermentation cost is increased, and the product separation in the later period has certain difficulty. Further improvements to this approach are needed.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides a production process of granular threonine. The process can improve the yield of the granular threonine, and has the advantages of simple and feasible process and wide application prospect.
The invention is realized by the following technical scheme:
a process for the production of particulate threonine comprising the steps of: step 1) preparing a fermentation culture medium, step 2) fermenting, step 3) centrifuging, and step 4) preparing the granular threonine.
Further, the step 1) of preparing a fermentation medium comprises the following steps:
step 1) preparation of a fermentation medium: 20-30g/L of glucose, 15-20g/L of glycerol, 15-20g/L of corn steep liquor, 1.5-2g/L of ammonium sulfate, 0.1-0.2g/L of monopotassium phosphate, 0.1-0.2g/L of dipotassium phosphate, 0.1-0.2g/L of magnesium sulfate heptahydrate, 5-10mg/L of ferrous sulfate heptahydrate, 5-10mg/L of manganese sulfate monohydrate, 50-400mg/L of isoleucine, 5-40mg/L of fulvic acid and 5.5-6.0 of pH value.
Further, the step 2) of fermentation comprises the following steps: inoculating the threonine-producing engineering bacteria seed liquid of escherichia coli into a fermentation tank containing a fermentation culture medium according to the inoculation amount of 10-12% for fermentation, wherein the temperature is 30 ℃, the tank pressure is 0.03-0.04MPa, the ventilation volume is 0.4-0.6vvm, the rotating speed is 100rpm, the fermentation time is 30-36h, then adding 100mg/L of inositol, continuing to perform fermentation culture for 24-30h, controlling the sugar content to be 0.3-0.5% by feeding glucose solution, stopping fermentation, and collecting fermentation liquid; in the whole fermentation process, ammonia water is fed to control the pH value to be 5.5-6.0.
Further, the step 3) of centrifugation comprises the following steps: centrifuging the fermentation liquor by a disc centrifuge at 4000rpm for 5min, and collecting the upper layer liquid;
further, the step 4) of preparing the granule-type threonine comprises the following steps: filtering the supernatant liquid obtained in the step 3) by a ceramic membrane, collecting filtrate, centrifuging the filtrate, and collecting supernatant liquid; then filtering through an ultrafiltration membrane, and collecting ultrafiltrate; concentrating and crystallizing the ultrafiltrate, centrifuging to collect crystals, drying until the water content is 0.8%, compressing into tablets, and putting into a granulation tower to be in a boiling state under the action of hot air flow; fluidized bed drying, crushing, granulating and sieving to obtain the granular threonine.
Preferably, in the fermentation medium, the isoleucine is 200-400mg/L, and the fulvic acid is 10-20 mg/L.
Preferably, the ceramic membrane has a molecular weight cut-off of 1 ten thousand Da.
Preferably, the ultrafiltration membrane has a molecular weight cut-off of 300 Da.
The starting point and the beneficial effects of the research of the invention mainly comprise but are not limited to the following aspects:
according to the invention, glucose and glycerol are selected as fermentation carbon sources, the thallus density is low in the early stage of fermentation, the oxygen supply is sufficient, and Escherichia coli preferentially utilizes glucose as a carbon source, so that thallus proliferation and threonine production can be promoted; in the middle and later stages of fermentation, the concentration of glucose is reduced, at the moment, the Escherichia coli utilizes glycerol as a carbon source, and the carbon flow entering glycolysis is reduced due to the low rate of glycerol absorption of cells, so that the accumulation of acetic acid is reduced, and the yield of threonine is increased;
oxaloacetate is derived from tricarboxylic acid cycle, the main route of oxaloacetate is flowing to a glutamic acid synthesis route, and threonine yield can be improved through feedback inhibition of the route; in the early stage of fermentation, the pH of fermentation liquor is regulated to be acidic, so that the synthesis of glutamic acid is facilitated, the permeability of cells is deteriorated, the glutamic acid cannot flow out of the cells, the rapid accumulation of the glutamic acid is facilitated, the feedback inhibition on a glutamic acid synthesis pathway is generated in a short time, and the oxaloacetic acid flows to an aspartic acid pathway earlier; however, the pH is too low to neutralize by-products such as acetic acid and lactic acid, and it is preferable to select 5.5 to 6.
Oxaloacetate is subjected to transamination to produce aspartic acid, so that threonine is synthesized, and the threonine can further synthesize isoleucine; feedback inhibition can be performed by adding isoleucine to the fermentation medium, thereby promoting threonine accumulation.
Proper amount of fulvic acid is added into the fermentation medium, contains a large amount of phenolic hydroxyl, carbonyl and other groups, has high electrolysis degree, and can promote the utilization of O in the amino acid synthesis process2Since pyruvic acid is reduced as a hydrogen acceptor, the amount of by-products such as lactic acid produced is reduced. Proper amount of inositol is added in the fermentation process to strengthen CO2The fixation reaction weakens the cycle of glyoxylate and improves the yield of amino acid.
The invention prepares the powdery threonine into the granular threonine, can improve the fluidity, is convenient for storage and transportation, controls the solubility and improves the quality and the added value of the threonine.
Drawings
FIG. 1: influence of fermentation factors on threonine content in fermentation broth;
FIG. 2: influence of fermentation factors on the content of acetic acid in fermentation liquor;
FIG. 3: influence of fermentation factors on the content of lactic acid in fermentation liquor;
FIG. 4: the influence of the addition of isoleucine in the medium on the threonine content of the fermentation broth;
FIG. 5: the influence of the addition of fulvic acid in the medium on the threonine content of the fermentation broth.
Detailed Description
Those skilled in the art can modify the process parameters appropriately to achieve the desired results with reference to the disclosure herein. It is expressly intended that all such similar substitutes and modifications which would be obvious to one skilled in the art are deemed to be included in the invention. While the products and methods of this invention have been described in terms of preferred embodiments, it will be apparent to those of skill in the art that variations and modifications, or appropriate alterations and combinations, of the products and methods described herein may be made and utilized without departing from the spirit, scope, and spirit of the invention. For a further understanding of the present invention, reference will now be made in detail to the following examples.
Example 1
A process for the production of particulate threonine comprising the steps of:
step 1) preparation of a fermentation medium: 25g/L of glucose, 20g/L of glycerol, 20g/L of corn steep liquor, 2g/L of ammonium sulfate, 0.1g/L of monopotassium phosphate, 0.1g/L of dipotassium phosphate, 0.1g/L of magnesium sulfate heptahydrate, 5mg/L of ferrous sulfate heptahydrate, 5mg/L of manganese sulfate monohydrate, 200mg/L of isoleucine, 10mg/L of fulvic acid and 5.5 of pH value;
step 2) fermentation: seed solution of Escherichia coli engineering bacteria K12 delta dapA (concentration of seed solution is 1 × 10)8cfu/mL) is inoculated into a fermentation tank containing a fermentation medium according to the inoculation amount of 12 percent for fermentation, the temperature is 30 ℃, the tank pressure is 0.03MPa, the ventilation volume is 0.4vvm, the rotating speed is 100rpm, the fermentation time is 36h, then 100mg/L inositol is added, the fermentation culture is continued for 24h, the sugar content is controlled to be 0.5 percent by feeding 100g/L glucose solution, the fermentation is stopped, and the fermentation broth is collected; in the whole fermentation process, 30% ammonia water is fed to control the pH value to be 5.5;
step 3) centrifugation: centrifuging the fermentation liquor by a disc centrifuge at 4000rpm for 5min, and collecting upper-layer liquid and precipitate;
step 4) preparation of granular threonine: filtering the upper layer liquid with ceramic membrane (molecular weight cut-off of 1 ten thousand Da), collecting filtrate, separating the filtrate with horizontal screw centrifuge at centrifugal speed of 5000rpm for 3min, and collecting supernatant (protein content less than 0.5%); then filtering through an ultrafiltration membrane, and collecting ultrafiltrate, wherein the molecular weight cut-off of the ultrafiltration membrane is 300 Da; crystallizing the ultrafiltrate in an intermittent single-effect concentration crystallizing pan, centrifuging to collect crystals, drying at 120 deg.C until the water content is 0.8%, compressing into sheet, and placing into a granulation tower to be in boiling state under the action of hot air flow; drying with a 65 deg.C fluidized bed, crushing, grading, sieving with 20 mesh and 50 mesh sieve to remove coarse and fine granules, collecting granule type threonine with target particle size, and packaging.
Example 2
A process for the production of particulate threonine comprising the steps of:
step 1) preparation of a fermentation medium: 30g/L of glucose, 15g/L of glycerol, 15g/L of corn steep liquor, 2g/L of ammonium sulfate, 0.2g/L of monopotassium phosphate, 0.2g/L of dipotassium phosphate, 0.2g/L of magnesium sulfate heptahydrate, 10mg/L of ferrous sulfate heptahydrate, 10mg/L of manganese sulfate monohydrate, 300mg/L of isoleucine, 20mg/L of fulvic acid and 5.5 of pH value;
step 2) fermentation: seed solution of Escherichia coli engineering bacteria K12 delta dapA (concentration of seed solution is 1 × 10)8cfu/mL) is inoculated into a fermentation tank containing a fermentation medium according to the inoculation amount of 10-12% for fermentation, the temperature is 30 ℃, the tank pressure is 0.04MPa, the ventilation volume is 0.6vvm, the rotating speed is 100rpm, the fermentation time is 32h, then 200mg/L inositol is added, the fermentation culture is continued for 28h, the sugar content is controlled to be 0.4% by feeding 100g/L glucose solution, the fermentation is stopped, and the fermentation broth is collected; in the whole fermentation process, the pH is controlled to be 6.0 by feeding 20-30% ammonia water;
step 3) centrifugation: centrifuging the fermentation liquor by a disc centrifuge at 4000rpm for 5min, and collecting upper-layer liquid and precipitate;
step 4) preparation of granular threonine: filtering the upper layer liquid with ceramic membrane (molecular weight cut-off of 1 ten thousand Da), collecting filtrate, separating the filtrate with horizontal screw centrifuge at centrifugal speed of 5000rpm for 3min, and collecting supernatant (protein content less than 0.5%); then filtering through an ultrafiltration membrane, and collecting ultrafiltrate, wherein the molecular weight cut-off of the ultrafiltration membrane is 300 Da; crystallizing the ultrafiltrate in an intermittent single-effect concentration crystallizing pan, centrifuging to collect crystals, drying at 120 deg.C until the water content is 0.8%, compressing into sheet, and placing into a granulation tower to be in boiling state under the action of hot air flow; drying with a 65 deg.C fluidized bed, crushing, grading, sieving with 20 mesh and 50 mesh sieve to remove coarse and fine granules, collecting granule type threonine with target particle size, and packaging.
Example 3
The influence of different factors on the yield of threonine and the content of byproducts such as acetic acid and lactic acid in the fermentation process is avoided.
Setting a group:
experimental groups: example 1;
control group 1: the same as in example 1 except that isoleucine was not added;
control group 2: the rest of the process was the same as example 1, except that no fulvic acid was added;
control group 3: the procedure of example 1 was repeated except that inositol was not added;
control group 4: the glycerol was replaced with an equivalent mass of glucose as in example 1.
The threonine, acetic acid and lactic acid contents of the final fermentation broths of each group are shown in FIGS. 1 to 3. Through setting a control group, the influence of fermentation factors such as glycerol, fulvic acid, isoleucine, inositol and the like on threonine, acetic acid and lactic acid is detected; as can be seen from fig. 1-3, fermentation factors such as glycerol, fulvic acid, isoleucine and inositol have a positive effect on threonine production, with the highest effect on inositol, the second to fulvic acid and isoleucine and the lowest effect on glycerol; but the influence of the glycerol on the byproducts is larger, the control group 4 does not add the glycerol, and the contents of the byproducts acetic acid and the lactic acid are the highest; the influence of isoleucine on the byproduct acetic acid is small, and the influence of fulvic acid on the byproduct lactic acid is small; by integrating the above influencing factors, the fermentation conditions are optimized, the yield of threonine can be increased, and the by-products are correspondingly reduced.
Example 4
The influence of the addition of isoleucine and fulvic acid in the culture medium on the threonine content of the fermentation broth.
The amounts of isoleucine added were set to 0,50,100,200,400,800 (mg/L), respectively; as shown in FIG. 4, with the increase of the addition amount of isoleucine, a certain feedback effect is generated on the metabolic pathway of threonine to isoleucine, so that the accumulation rate of threonine is increased, when the addition amount is increased to 200mg/L, the amplification is slowed, and when the addition amount is increased to 400mg/L, the threonine content is not obviously increased.
The addition amounts of fulvic acid are set to 0,5,10,20,40,80 (mg/L), respectively; as shown in FIG. 5, the increase of the amount of fulvic acid promotes the utilization of O in the process of amino acid synthesis2As a hydrogen acceptor, the content of the threonine is not obviously changed after the yield of the fulvic acid is continuously increased to 20 mg/L.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (4)
1. A process for the production of particulate threonine comprising the steps of:
step 1) preparation of a fermentation medium: 20-30g/L of glucose, 15-20g/L of glycerol, 15-20g/L of corn steep liquor, 1.5-2g/L of ammonium sulfate, 0.1-0.2g/L of monopotassium phosphate, 0.1-0.2g/L of dipotassium phosphate, 0.1-0.2g/L of magnesium sulfate heptahydrate, 5-10mg/L of ferrous sulfate heptahydrate, 5-10mg/L of manganese sulfate monohydrate, 50-400mg/L of isoleucine, 5-40mg/L of fulvic acid and 5.5-6.0 of pH value;
step 2) fermentation: inoculating the threonine-producing engineering bacteria seed liquid of escherichia coli into a fermentation tank containing a fermentation culture medium according to the inoculation amount of 10-12% for fermentation, wherein the temperature is 30 ℃, the tank pressure is 0.03-0.04MPa, the ventilation volume is 0.4-0.6vvm, the rotating speed is 100rpm, and the fermentation time is 30-36 h; then adding 100mg/L inositol, continuing fermentation culture for 24-30h, controlling the sugar content to be 0.3-0.5% by feeding glucose solution, stopping fermentation, and collecting fermentation liquor; in the whole fermentation process, ammonia water is fed in to control the pH value to be 5.5-6.0;
the Escherichia coli is K12 delta dapA;
step 3), centrifuging, namely centrifuging the fermentation liquor for 5min at 4000rpm by a disc centrifuge, and collecting upper-layer liquid;
step 4) preparing the granular threonine, which comprises the following steps: filtering the supernatant liquid obtained in the step 3) by a ceramic membrane, collecting filtrate, centrifuging the filtrate, and collecting supernatant liquid; then filtering through an ultrafiltration membrane, and collecting ultrafiltrate; concentrating and crystallizing the ultrafiltrate, centrifuging to collect crystals, drying until the water content is 0.8%, compressing into tablets, and putting into a granulation tower to be in a boiling state under the action of hot air flow; fluidized bed drying, crushing, granulating and sieving to obtain the granular threonine.
2. The process according to claim 1, wherein the fermentation medium contains isoleucine at 200-400mg/L and fulvic acid at 10-20 mg/L.
3. The process according to claim 1, wherein the ceramic membrane has a molecular weight cut-off of 10 KDa.
4. The process of claim 1, wherein the ultrafiltration membrane has a molecular weight cut-off of 300 Da.
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| CN110846349A (en) * | 2019-08-22 | 2020-02-28 | 赵兰坤 | Preparation method of feed additive threonine |
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