CN106047954A - Method for production of lactic acid and joint production of protein feed by cyclic fermentation - Google Patents
Method for production of lactic acid and joint production of protein feed by cyclic fermentation Download PDFInfo
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Abstract
The invention belongs to the technical field of lactic acid fermentation, and particularly relates to a method for production of lactic acid and joint production of protein feed by cyclic fermentation. The method is characterized in that the existing lactic acid production technology of simultaneous saccharification and fermentation is used as the basis, the pretreatment method of lactic acid fermentation bacteria residues is combined, and the bacteria can be cyclically utilized; by utilizing single batch of bacteria, the multi-cycle fermentation can be realized, the disposal problem of fermentation waste residues is solved, and the consumption of raw and auxiliary materials is decreased; the composite medium can be cyclically used, so that the resources can be recycled. The method for production of lactic acid and joint production of protein feed by cyclic fermentation has the advantages that by using an automatic plate frame filter technique, the corn starch residues in the saccharification process are quickly separated; the separated corn starch residues are solidly fermented to jointly produce the protein feed, the content of amino acids is obviously increased, the components of starch residues can be conveniently digested and absorbed by animals, and the corn protein feed with high addition value is prepared.
Description
Technical field
The invention belongs to lactate fermentation technical field, be specifically related to a kind of circulating fermentation and produce lactic acid co-production albumen feedstuff
Method.
Background technology
Lactic acid, as one of three big organic acid (including lactic acid, citric acid, acetic acid), is with starchiness as raw material, through micro-life
A kind of organic acid that thing fermentation is refined, is all widely used in fields such as food, medicine and chemical industry.
In field of food industry, owing to the acidity of lactic acid is soft and stable, be widely used as in the food industry acidic flavoring agent,
Preservative is used, and therefore, in field of food, the consumption figure of lactic acid accounts for about the 60% of world's lactic acid aggregate consumption.Due in human body
Only having the enzyme of metabolism Pfansteihl, D-ALPHA-Hydroxypropionic acid then can not be absorbed by the body, and it is poisonous to human body to be excessively used meeting.Therefore,
World Health Organization (WHO) advocates using Pfansteihl as food additive and medicine for oral administration, replaces the DL-LACTIC ACID commonly used at present.With
Time, in Beer Production field, oneself prohibits the use of the pH value of phosphoric acid regulation beerwort, and uses Pfansteihl instead as regulator.According to tune
Looking into, the lactic acid of 1/4th is used for producing the stearic cruel lactic acid of phthalein breast in the world, and its esters is then owing to can make the preservation of bread
Phase, the elongated bread that is largely used to produced.It addition, make an addition in Nicotiana tabacum L. by lactic acid, it is possible to keep the humidity of Nicotiana tabacum L., improve Medicated cigarette
Quality.
In medical industry field, lactic acid particularly Pfansteihl, because having the strongest bactericidal action, even its bactericidal action
Higher than common disinfectants such as citric acid, tartaric acid, succinic acid, can serve as the places such as operating room, ward, laboratory, workshop
Disinfectant.Research shows, Pfansteihl, Pfansteihl sodium and glucose, aminoacid etc. are compound is configured to transfusion, can therapic acid poisoning and
Hyperpotassemia, Pfansteihl ferrum, Pfansteihl sodium, L-calcium lactate supplement the good medicine of metallic element especially.
In the fields such as chemical industry, lactic acid can be used as the deliming agent in leather industry, may further be used to process textile fabric,
Make it easy to coloring, increase gloss, make soft-touch.Ethyl lactate can be in electronics, aviation and boat as " green solvent "
As fine metal cleaning agent in it and semi-conductor industry.In cosmetics, lactic acid, sodium lactate and calcium lactate can provide moisturizing
The performance of aspect, and phthalidyl zirconium lactate is effective emulsifying agent in cosmetics and care products, material filling and stabilizer, can change
Kind skin texture, prevents aging, plays the effect of protection skin.
Along with global warming, environmental pollution gradually increase the weight of, and petroleum resources worsening shortages, exploitation clean energy resource with
Environment-friendly material is the task that country is the most urgent.In numerous degradable polymers, polylactic acid has become 21 generation
Record the most promising green material.The production of the synthetic material of polylactic acid--Pfansteihl then directly influences poly-breast
The synthesis of acid.It can be said that the development of Pfansteihl technology and industry is the important prerequisite of polylactic acid industry development.
At present, the technique producing Pfansteihl both at home and abroad is most of with corn starch as primary raw material, by suitable lactic acid
Bacterium fermentation prepares Pfansteihl.In China's lactate fermentation commercial process, saccharifying and fermentation procedure mostly are and carry out step by step, cause
The production of lactic acid cycle is long, and operating unit is many, is difficult to produce continuously；In existing patent and document, some are also had to refer to synchronize
Diastatic fermentation produces the technology of lactic acid, and due to the difference of raw material, technique is the most different, and due to the limit of the required pH value of fermentation
System, simultaneous saccharification and fermentation is the most wayward, causes fermentation liquid residual sugar high, and sugar utilization is low, separation of fermentative broth purification difficult, it is difficult to
Industrializing implementation.On this basis, Chinese patent CN103789362A discloses a kind of premashing and simultaneous saccharification and fermentation produces
The method of lactic acid, comprises the steps: prepared by (1) raw material: Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction and filter；System
Obtaining the liquefaction sugar liquid that DE value is 22%-28%, in liquefaction sugar liquid, total sugar content is 120-180g/L；(2) premashing: will liquefaction sugar
Liquid adds through sterilizing and carrying out premashing in the fermentation tank of sterilizing, obtains fermented feed liquid；(3) limit saccharifying limit fermentation.The method
Can substantially shorten the time of saccharifying, and then shorten the production of lactic acid cycle, but, this technique separates after product carrying out fermentation,
In the thalline slag of fermentation gained in addition to containing thalline, possibly together with other metal ions such as the nutrition not run out of and calcium, one
Aspect causes the nutrient substance in fermentation medium to cause waste, there is also the problem that fermentation residue pollutes simultaneously, causes resource
Waste.
Summary of the invention
To this end, the technical problem to be solved is that providing a kind of circulating fermentation to produce lactic acid co-production albumen raises
The method of material.
For solving above-mentioned technical problem, circulating fermentation of the present invention produces the method for lactic acid co-production albumen feedstuff,
Comprise the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, through filtering
After separation, obtain liquefy sugar liquid and corn starch residue；
(2) premashing: prepared liquefaction sugar liquid added in fermentation tank, adds saccharifying enzyme and carries out premashing process, obtain
Fermented feed liquid；
(3) after premashing terminates, in fermented feed liquid add yeast extract, and inoculate into lactobacillus suspension and saccharifying enzyme carry out with
Step diastatic fermentation, detects the yield of lactic acid simultaneously；
(4) gained fermented feed liquid is filtered, and gained solid thalline slag is carried out pretreatment with complex media, preprocessed
After thalline slag be separated by filtration acquisition solvable nutrient substance and soluble impurity；The solvable battalion obtained after simultaneously filtering separation
Foster material is recycled in fermentation tank and carries out the fermentation of subsequent cycle and be used；
Described complex media includes ammonium sulfate, disodium EDTA, dodecyl sodium sulfate and sodium citrate；
(5) take the corn starch residue separated in described step (1), access thermophilic lactobacillus and carry out solid fermentation, and will
The corn starch protein slurry of fermentation gained carries out rotary drying, size-reduced, prepares albumen feedstuff.
In described complex media, described ammonium sulfate, disodiumedetate, dodecyl sodium sulfate and sodium citrate
Mass ratio be 1-5:1-3:1-4:1-3.
The consumption of described complex media accounts for the 10-20wt% of described thalline slag amount；Mixed to thalline slag and complex media
Compound adds water, and thalline slag and complex media are made aqueous solution mixing, thalline slag and complex media total matter in aqueous
Amount concentration is 10-50wt%.
Described thalline slag pre-treatment step processes 30-50min at 20-30 DEG C.
Described thalline slag pretreated filtration separating step is centrifugal filtration, and described centrifugal rotational speed is 1000-
1200rpm。
In described step (3), saccharifying limit, described limit fermentation step specifically includes: after premashing terminates, in fermented feed liquid
Add yeast extract, and the pH adding ammonia spirit regulation fermented feed liquid in fermented feed liquid is 6.0 ± 0.1, treats fermented feed liquid
Add the lactobacillus suspension accounting for fermented feed liquid cumulative volume 6%-12% when temperature reaches 50 ± 2 DEG C, treat the OD of lactobacillus suspension620Value reaches
During to 9.5-12, in fermentation tank, it is passed through filtrated air, and keeps continuation fermentation at a temperature of this；Treat the OD of fermented feed liquid620Value reaches
During to 10, regulation fermented feed liquid pH is 5.5 ± 0.1, and continues to add saccharifying enzyme 50-according to every gram of total sugar in liquefaction sugar liquid
100U/g adds saccharifying enzyme and carries out simultaneous saccharification and fermentation.
In described step (1), described filtration separating step, for using filter press to filter, controls sheet frame charging pressure
Power is 0.4-0.45Mp, and controlling sheet frame compaction pressure is 18-20Mpa.
In described step (5), the inoculum concentration of described thermophilic lactobacillus is 10%, and the temperature of described solid fermentation step is
30-35 DEG C of fermentation 45-48h, the temperature of described rotary drying step is 90 DEG C.
In described step (2), in described pre-saccharification step, the addition of described saccharifying enzyme is according in liquefaction sugar liquid every gram
Total sugar adds 400-600U/g meter, and control fermentation liquid in 50-70 DEG C, carry out premashing process under the conditions of pH4.5 ± 0.1.
In described step (4), also include being dried by the soluble impurity of isolated and preparing the step of desulfurizing agent.
Circulating fermentation of the present invention produces the method for lactic acid co-production albumen feedstuff, with the breast of saccharifying limit, existing limit fermentation
Based on acid production process, the preprocess method in conjunction with described lactate fermentation thalline slag realizes recycling of thalline, utilizes single
Batch strain can realize multi cycle fermentation.The preprocess method of described lactate fermentation thalline slag utilizes ammonium sulfate, ethylenediamine tetraacetic
Acetic acid disodium salt, dodecyl sodium sulfate and sodium citrate are complex media, and the thalline slag after fermentation is carried out pretreatment, by
In fermentation thalli slag in addition to containing thalline, the nutrition that do not runs out of, affect other metal of prior fermentation possibly together with calcium etc.
Ion, the solvable and insoluble material that complex media of the present invention can efficiently separate in thalline slag (prevents acidic group in bacterium solution from losing
Lose), the solvable nutrient substance (comprising thalline and the nutrition not consumed) after complex media of the present invention processes can continue
Continuous participation is fermented.Data show, described thalline slag is after pretreatment, and not only the efficiency of its fermentation lactic acid does not reduce, on the contrary
Contribute to because of the remaining nutrient substance carried in fermentation liquid promoting the saccharic acid conversion ratio in following cycle, it is achieved that lactic acid
The maximum gain of fermenting and producing.And isolated metal ion is mainly calcium ion, drying can be as desulfurizer for thermal power plant
Use.And, the present invention uses the method sharp separation of centrifugation to go out thalline, and isolated thalline returns as nutrition nitrogen source
Fermentation procedure recycles, the consumption of the nutrient substance in minimizing fermentation medium, has both solved fermentation residue problem of outlet, again
Reduce raw and auxiliary material consumption, and complex media also can be recycled, it is achieved that resource circulation utilization.
And, circulating fermentation of the present invention produces the method for lactic acid co-production albumen feedstuff, introduces automatic sheet frame filtering technique
To the corn starch residue sharp separation during sugaring；Take solid fermentation coproduction albumen to raise the corn starch residue separated simultaneously
Material, can significantly improve amino acid content, make each composition in fecula more utilize animal digestion to absorb, and prepares the jade of high added value
Rice gluten feedstuff.
Accompanying drawing explanation
In order to make present disclosure be more likely to be clearly understood, below according to the specific embodiment of the present invention and combine
Accompanying drawing, the present invention is further detailed explanation, wherein,
Fig. 1 is the process chart that circulating fermentation of the present invention produces lactic acid co-production albumen feedstuff.
Detailed description of the invention
Embodiment 1
The present embodiment circulating fermentation produces the method for lactic acid co-production albumen feedstuff, comprises the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, described jade
Rice & peanut milk liquid uses filter press to carry out filtering and solid-liquid separation, and controlling sheet frame feed pressure is 0.4Mp, controls sheet frame and compresses pressure
Power is 18Mpa, after being separated by filtration, obtains liquefaction sugar liquid and corn starch residue that DE value is 22%, and in liquefaction sugar liquid, total sugar contains
Amount is 120g/L；
(2) premashing: premashing temperature is 59 DEG C, adds liquefaction sugar liquid and carries out in the fermentation tank of sterilization and sterilizing
Premashing；Adding hydrochloric acid regulation liquefaction sugar liquid pH that mass fraction is 3% is 4.5 ± 0.1, and the addition of saccharifying enzyme is according to liquefaction
In sugar liquid, every gram of total sugar adds saccharifying enzyme 400U, and is passed through filtrated air in fermentation tank, keeps pressure inside the tank 0.2Mpa, pre-sugar
4 hours change time, obtain fermented feed liquid；In gained fermented feed liquid, DX value is 88%；
(3) limit saccharifying limit fermentation: premashing terminates to add in backward fermented feed liquid yeast extract, and adds in fermented feed liquid
Mass fraction be 30% ammonia spirit with keep fermented feed liquid pH for 5.9, add when the temperature of fermented feed liquid drops to 48 DEG C
Add the lactobacillus suspension of fermented feed liquid cumulative volume 6%, the OD of lactobacillus suspension620Value is 10, and to be always maintained at temperature in fermentation tank be 48
DEG C, and in fermentation tank, it is passed through filtrated air, the OD of detection fermented feed liquid620Value, treats the OD of fermented feed liquid620Value rises to 10
Time, regulating fermented feed liquid pH to 5.5, again add saccharifying enzyme, the addition of saccharifying enzyme adds according to every gram of total sugar in liquefaction sugar liquid
Enter saccharifying enzyme 100U, detect lactic acid bacteria after fermenting 46 hours and no longer produce acid, fermentation ends；
(4) being filtered by gained fermented feed liquid, solid-liquid separation obtains solid dreg and lactic acid feed liquid, by gained solid thalline slag
Weigh, and add account for described dreg weight 10wt% complex media (in the present embodiment, complex media includes that mass ratio is 1:3:
The ammonium sulfate of 1:3, disodium EDTA, dodecyl sodium sulfate and sodium citrate) carry out pretreatment, to thalline slag
Adding water with the mixture of complex media, thalline slag and complex media are made aqueous solution mixing, thalline slag and complex media exist
Total mass concentration in aqueous solution is 20wt%, at a temperature of 20 DEG C standing process 50min, and will process after bacterium solution in
Centrifugal filtration under 1000-1200rpm rotating speed, solid-liquid separation respectively obtains solvable nutrient substance and soluble impurity again；
Described solvable nutrient substance is used for being recycled in fermentation tank the fermentation carrying out subsequent cycle, and gained impurity can
It is used for preparing desulfurizing agent after drying, pulverizing；
The lactic acid feed liquid obtained after solid-liquid separation obtains, containing lactic acid concentrated solution, detecting Fermented Condensed liquid after evaporation and concentration
In residual total sugar content be 0.4%, residual reducing sugar is 0.15%, and saccharic acid conversion ratio reaches 95.3%；
(5) taking the corn starch residue separated in described step (1), the inoculum concentration according to 10% accesses thermophilic lactobacillus,
And at a temperature of 30 DEG C, carry out solid fermentation 48h, the corn starch protein slurry of fermentation gained is carried out rotary drying in 90 DEG C,
Size-reduced, prepare albumen feedstuff；Detect according to GB/T 18246-2000, in the albumen feedstuff prepared, 18 kinds of aminoacid (Radix Asparagis
Propylhomoserin, threonine, serine, glutamic acid, glycine, alanine, cystine, valine, methionine, isoleucine, leucine,
Tyrosine, phenylalanine, lysine, histidine, tryptophan, arginine, proline) total content is 27.76wt%, its two-story valley
The content of propylhomoserin, alanine, leucine and proline is respectively 5.04wt%, 2.00wt%, 3.53wt%, 2.43wt%.
According to above-mentioned steps (1)-(5) condition circulating fermentation produce lactic acid, the strain in described step (3) be through
In a upper circulation step (4), pretreatment Posterior circle is back to the strain of fermentation tank, is carried out continuously the continuous fermentation of 5 circulations, inspection
Survey the residual sugar situation that every circulating fermentation terminates in rear lactic fermentation liquid, and calculate saccharic acid conversion ratio.
In the present embodiment, after carrying out 5 circulating fermentations process according to above-mentioned condition, the saccharic acid in 2-4 cyclic process turns
Rate is respectively 95.5%, 95.8%, 96.1%, 96.8%.Visible, circulating fermentation of the present invention produces lactic acid parallel connection and lays eggs
The method of white feedstuff, utilizes single batch strain can realize multi cycle fermentation, described thalline slag after pretreatment, not only its
The efficiency of kefir milk acid does not reduce, and contributes to because carrying the remaining nutrient substance in fermentation liquid on the contrary promoting following cycle
In saccharic acid conversion ratio, it is seen then that circulating fermentation of the present invention produce lactic acid co-production albumen feedstuff method, not only maximize
The nutrient substance that make use of in fermentation liquid, solve simultaneously discarded thalline slag pollute problem.
And, circulating fermentation of the present invention produces the method for lactic acid co-production albumen feedstuff, introduces automatic plate-and-frame filtration
Technology is to the corn starch residue sharp separation during sugaring；The corn starch residue separated is taked solid fermentation coproduction egg simultaneously
White feedstuff, can significantly improve amino acid content, make each composition in fecula more utilize animal digestion to absorb, and prepares high added value
Maize gluten feed.
Embodiment 2
The present embodiment circulating fermentation produces the method for lactic acid co-production albumen feedstuff, comprises the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, described jade
Rice & peanut milk liquid uses filter press to carry out filtering and solid-liquid separation, and controlling sheet frame feed pressure is 0.45Mp, controls sheet frame and compresses
Pressure is 20Mpa, after being separated by filtration, obtains liquefaction sugar liquid and corn starch residue that DE value is 28%, total sugar in liquefaction sugar liquid
Content is 180g/L；
(2) premashing: controlling premashing temperature is 70 DEG C, adds liquefaction sugar liquid in the fermentation tank of sterilization and sterilizing
Carry out premashing；Adding sulphuric acid regulation liquefaction sugar liquid pH that mass fraction is 2% is 4.4, and the addition of saccharifying enzyme is according to liquefaction
In sugar liquid, every gram of total sugar adds saccharifying enzyme 400U, and is passed through filtrated air in fermentation tank, keeps pressure inside the tank 0.1Mpa, pre-sugar
6 hours change time, obtain fermented feed liquid；In gained fermented feed liquid, DX value is 89%；
(3) limit saccharifying limit fermentation: premashing terminates to add in backward fermented feed liquid yeast extract, and adds in fermented feed liquid
The ammonia spirit of mass fraction 20%, to keep the pH of fermented feed liquid for 6.0, added when the temperature of fermented feed liquid drops to 50 DEG C
The lactobacillus suspension of fermented feed liquid cumulative volume 10%, the OD of lactobacillus suspension620Value is 12, and to be always maintained at temperature in fermentation tank be 50
DEG C, and in fermentation tank, it is passed through filtrated air, the OD of detection fermented feed liquid620Value, treats the OD of fermented feed liquid620Value rises to 10
Time, regulating fermented feed liquid pH to 5.4, continuously add saccharifying enzyme, the addition of saccharifying enzyme adds according to every gram of total sugar in liquefaction sugar liquid
Entering saccharifying enzyme 100U, after fermenting 47 hours, detection lactic acid bacteria no longer produces acid, now fermentation ends；
(4) being filtered by gained fermented feed liquid, solid-liquid separation obtains solid dreg and lactic acid feed liquid, by gained solid thalline slag
Weigh, and add and account for the complex media of described dreg weight 15wt% and (include that mass ratio is the ammonium sulfate of 5:1:4:1, ethylenediamine
Sequestrene AA, dodecyl sodium sulfate and sodium citrate) carry out pretreatment, to thalline slag and the mixture of complex media
Adding water, thalline slag and complex media are made aqueous solution mixing, thalline slag and complex media gross mass in aqueous is dense
Degree is for 15wt%, and at a temperature of 30 DEG C, standing processes 30min, and the bacterium solution after processing is centrifugal under 1000-1200rpm rotating speed
Filtering, solid-liquid separation respectively obtains solvable nutrient substance and soluble impurity again；
Described solvable nutrient substance is used for being recycled in fermentation tank the fermentation carrying out subsequent cycle, and gained impurity can
It is used for preparing desulfurizing agent after drying, pulverizing；
The lactic acid feed liquid obtained after solid-liquid separation obtains, containing lactic acid concentrated solution, detecting Fermented Condensed liquid after evaporation and concentration
In residual total sugar content be 0.4%, residual reducing sugar is 0.15%, and saccharic acid conversion ratio reaches 95.3%；
(5) taking the corn starch residue separated in described step (1), the inoculum concentration according to 10% accesses thermophilic lactobacillus,
And at a temperature of 35 DEG C, carry out solid fermentation 45h, the corn starch protein slurry of fermentation gained is carried out rotary drying in 90 DEG C,
Size-reduced, prepare albumen feedstuff；Detect according to GB/T 18246-2000, in the albumen feedstuff prepared, 18 kinds of aminoacid (Radix Asparagis
Propylhomoserin, threonine, serine, glutamic acid, glycine, alanine, cystine, valine, methionine, isoleucine, leucine,
Tyrosine, phenylalanine, lysine, histidine, tryptophan, arginine, proline) total content is 27.83wt%, its two-story valley
The content of propylhomoserin, alanine, leucine and proline is respectively 5.07wt%, 2.03wt%, 3.50wt%, 2.41wt%.
According to above-mentioned steps (1)-(5) condition circulating fermentation produce lactic acid, the strain in described step (3) be through
In a upper circulation step (4), pretreatment Posterior circle is back to the strain of fermentation tank, is carried out continuously the continuous fermentation of 5 circulations, inspection
Survey the residual sugar situation that every circulating fermentation terminates in rear lactic fermentation liquid, and calculate saccharic acid conversion ratio.
In the present embodiment, after carrying out 5 circulating fermentations process according to above-mentioned condition, the saccharic acid in 2-4 cyclic process turns
Rate is respectively 95.6%, 95.9%, 96.2%, 96.8%.Visible, circulating fermentation of the present invention produces lactic acid parallel connection and lays eggs
The method of white feedstuff, utilizes single batch strain can realize multi cycle fermentation, described thalline slag after pretreatment, not only its
The efficiency of kefir milk acid does not reduce, and contributes to because carrying the remaining nutrient substance in fermentation liquid on the contrary promoting following cycle
In saccharic acid conversion ratio, it is seen then that circulating fermentation of the present invention produce lactic acid co-production albumen feedstuff method, not only maximize
The nutrient substance that make use of in fermentation liquid, solve simultaneously discarded thalline slag pollute problem.Embodiment 3
The present embodiment circulating fermentation produces the method for lactic acid co-production albumen feedstuff, comprises the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, described jade
Rice & peanut milk liquid uses filter press to carry out filtering and solid-liquid separation, and controlling sheet frame feed pressure is 0.42Mp, controls sheet frame and compresses
Pressure is 19Mpa, after being separated by filtration, obtains liquefaction sugar liquid and corn starch residue that DE value is 25%, total sugar in liquefaction sugar liquid
Content is 140g/L；
(2) premashing: premashing temperature is 50 DEG C, adds liquefaction sugar liquid and carries out in the fermentation tank of sterilization and sterilizing
Premashing；Adding hydrochloric acid regulation liquefaction sugar liquid pH that mass fraction is 1% is 4.6, and the addition of saccharifying enzyme is according to liquefaction sugar liquid
In every gram of total sugar add saccharifying enzyme 600U, and in fermentation tank, be passed through filtrated air, keep pressure inside the tank 0.4Mpa, during premashing
Between 3.5 hours, obtain fermented feed liquid, in gained fermented feed liquid, DX value is 90%；
(3) limit saccharifying limit fermentation: premashing terminates to add in backward fermented feed liquid yeast extract, and adds in fermented feed liquid
Mass fraction be 30% ammonia spirit with keep fermented feed liquid pH for 6.2, add when the temperature of fermented feed liquid drops to 52 DEG C
Add the lactobacillus suspension of fermented feed liquid cumulative volume 8%, the OD of lactobacillus suspension620Value is 9.5, and temperature is in being always maintained at fermentation tank
52 DEG C, and in fermentation tank, it is passed through filtrated air, the OD of detection fermented feed liquid620Value, treats the OD of fermented feed liquid620Value rises to 10
Time, regulating fermented feed liquid pH to 5.6, add saccharifying enzyme, the addition of saccharifying enzyme adds sugar according to every gram of total sugar in liquefaction sugar liquid
Change enzyme 80U, detect lactic acid bacteria after fermenting 45 hours and no longer produce acid, fermentation ends；
(4) being filtered by gained fermented feed liquid, solid-liquid separation obtains solid dreg and lactic acid feed liquid, by gained solid thalline slag
Weigh, and add and account for the complex media of described dreg weight 15wt% and (include that mass ratio is the ammonium sulfate of 3:2:3:2, ethylenediamine
Sequestrene AA, dodecyl sodium sulfate and sodium citrate) carry out pretreatment, to thalline slag and the mixture of complex media
Adding water, thalline slag and complex media are made aqueous solution mixing, thalline slag and complex media gross mass in aqueous is dense
Degree is for 25wt%, and at a temperature of 25 DEG C, standing processes 40min, and the bacterium solution after processing is centrifugal under 1000-1200rpm rotating speed
Filtering, solid-liquid separation respectively obtains solvable nutrient substance and soluble impurity again；
Described solvable nutrient substance is used for being recycled in fermentation tank the fermentation carrying out subsequent cycle, and gained impurity can
It is used for preparing desulfurizing agent after drying, pulverizing；
The lactic acid feed liquid obtained after solid-liquid separation obtains, containing lactic acid concentrated solution, detecting Fermented Condensed liquid after evaporation and concentration
In residual total sugar content be 0.35%, residual reducing sugar is 0.13%, and saccharic acid conversion ratio reaches 95.6%；
(5) taking the corn starch residue separated in described step (1), the inoculum concentration according to 10% accesses thermophilic lactobacillus,
And at a temperature of 32 DEG C, carry out solid fermentation 46h, the corn starch protein slurry of fermentation gained is carried out rotary drying in 90 DEG C,
Size-reduced, prepare albumen feedstuff；Detect according to GB/T 18246-2000, in the albumen feedstuff prepared, 18 kinds of aminoacid (Radix Asparagis
Propylhomoserin, threonine, serine, glutamic acid, glycine, alanine, cystine, valine, methionine, isoleucine, leucine,
Tyrosine, phenylalanine, lysine, histidine, tryptophan, arginine, proline) total content is 26.92wt%, its two-story valley
The content of propylhomoserin, alanine, leucine and proline is respectively 5.00wt%, 2.01wt%, 3.52wt%, 2.45wt%.
According to above-mentioned steps (1)-(5) condition circulating fermentation produce lactic acid, the strain in described step (3) be through
In a upper circulation step (4), pretreatment Posterior circle is back to the strain of fermentation tank, is carried out continuously the continuous fermentation of 5 circulations, inspection
Survey the residual sugar situation that every circulating fermentation terminates in rear lactic fermentation liquid, and calculate saccharic acid conversion ratio.
In the present embodiment, after carrying out 5 circulating fermentations process according to above-mentioned condition, the saccharic acid in 2-4 cyclic process turns
Rate is respectively 95.8%, 96.0%, 96.2%, 96.7%.Visible, circulating fermentation of the present invention produces lactic acid parallel connection and lays eggs
The method of white feedstuff, utilizes single batch strain can realize multi cycle fermentation, described thalline slag after pretreatment, not only its
The efficiency of kefir milk acid does not reduce, and contributes to because carrying the remaining nutrient substance in fermentation liquid on the contrary promoting following cycle
In saccharic acid conversion ratio, it is seen then that circulating fermentation of the present invention produce lactic acid co-production albumen feedstuff method, not only maximize
The nutrient substance that make use of in fermentation liquid, solve simultaneously discarded thalline slag pollute problem.Embodiment 4
The present embodiment circulating fermentation produces the method for lactic acid co-production albumen feedstuff, comprises the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, described jade
Rice & peanut milk liquid uses filter press to carry out filtering and solid-liquid separation, and controlling sheet frame feed pressure is 0.4Mp, controls sheet frame and compresses pressure
Power is 20Mpa, after being separated by filtration, obtains liquefaction sugar liquid and corn starch residue that DE value is 28%, and in liquefaction sugar liquid, total sugar contains
Amount is 180g/L；
(2) premashing: premashing temperature is 60 DEG C, adds liquefaction sugar liquid and carries out in the fermentation tank of sterilization and sterilizing
Premashing；Adding sulphuric acid regulation liquefaction sugar liquid pH that mass fraction is 1% is 4.4, and the addition of saccharifying enzyme is according to liquefaction sugar
In liquid, every gram of total sugar adds saccharifying enzyme 500U, and is passed through filtrated air in fermentation tank, keeps pressure inside the tank 0.05Mpa, pre-sugar
3 hours change time, obtain fermented feed liquid；In gained fermented feed liquid, DX value is 90%；
(3) limit saccharifying limit fermentation: premashing terminates to add in backward fermented feed liquid yeast extract, and adds in fermented feed liquid
The ammonia spirit of mass fraction 25%, to keep the pH of fermented feed liquid for 6.0, added when the temperature of fermented feed liquid drops to 49 DEG C
The lactobacillus suspension of fermented feed liquid cumulative volume 6%, to the OD of lactobacillus suspension620Value is 9.5, and temperature is in being always maintained at fermentation tank
49 DEG C, and in fermentation tank, it is passed through filtrated air, the OD of detection fermented feed liquid620Value, treats the OD of fermented feed liquid620Value rises to 10
Time, regulating fermented feed liquid pH to 5.5, continuously add saccharifying enzyme, the addition of saccharifying enzyme adds according to every gram of total sugar in liquefaction sugar liquid
Enter saccharifying enzyme 50U, detect lactic acid bacteria after fermenting 45.5 hours and no longer produce acid, fermentation ends；
(4) being filtered by gained fermented feed liquid, solid-liquid separation obtains solid dreg and lactic acid feed liquid, by gained solid thalline slag
Weigh, and add and account for the complex media of described dreg weight 15wt% and (include that mass ratio is the ammonium sulfate of 2:2.5:2:2.5, second
Edetate disodium salt, dodecyl sodium sulfate and sodium citrate) carry out pretreatment, mixed to thalline slag and complex media
Compound adds water, and thalline slag and complex media are made aqueous solution mixing, thalline slag and complex media total matter in aqueous
Amount concentration is 30wt%, at a temperature of 25 DEG C standing process 40min, and will process after bacterium solution under 1000-1200rpm rotating speed
Centrifugal filtration, solid-liquid separation respectively obtains solvable nutrient substance and soluble impurity again；
Described solvable nutrient substance is used for being recycled in fermentation tank the fermentation carrying out subsequent cycle, and gained impurity can
It is used for preparing desulfurizing agent after drying, pulverizing；
The lactic acid feed liquid obtained after solid-liquid separation obtains, containing lactic acid concentrated solution, detecting Fermented Condensed liquid after evaporation and concentration
In residual total sugar content be 0.33%, residual reducing sugar is 0.12%, and saccharic acid conversion ratio reaches 95.4%；
(5) taking the corn starch residue separated in described step (1), the inoculum concentration according to 10% accesses thermophilic lactobacillus,
And at a temperature of 34 DEG C, carry out solid fermentation 45h, the corn starch protein slurry of fermentation gained is carried out rotary drying in 90 DEG C,
Size-reduced, prepare albumen feedstuff；Detect according to GB/T 18246-2000, in the albumen feedstuff prepared, 18 kinds of aminoacid (Radix Asparagis
Propylhomoserin, threonine, serine, glutamic acid, glycine, alanine, cystine, valine, methionine, isoleucine, leucine,
Tyrosine, phenylalanine, lysine, histidine, tryptophan, arginine, proline) total content is 28.92wt%, its two-story valley
The content of propylhomoserin, alanine, leucine and proline is respectively 5.15wt%, 2.05wt%, 3.61wt%, 2.53wt%.
According to above-mentioned steps (1)-(5) condition circulating fermentation produce lactic acid, the strain in described step (3) be through
In a upper circulation step (4), pretreatment Posterior circle is back to the strain of fermentation tank, is carried out continuously the continuous fermentation of 5 circulations, inspection
Survey the residual sugar situation that every circulating fermentation terminates in rear lactic fermentation liquid, and calculate saccharic acid conversion ratio.
In the present embodiment, after carrying out 5 circulating fermentations process according to above-mentioned condition, the saccharic acid in 2-4 cyclic process turns
Rate is respectively 95.8%, 96.2%, 96.6%, 96.9%.Visible, circulating fermentation of the present invention produces lactic acid parallel connection and lays eggs
The method of white feedstuff, utilizes single batch strain can realize multi cycle fermentation, described thalline slag after pretreatment, not only its
The efficiency of kefir milk acid does not reduce, and contributes to because carrying the remaining nutrient substance in fermentation liquid on the contrary promoting following cycle
In saccharic acid conversion ratio, it is seen then that circulating fermentation of the present invention produce lactic acid co-production albumen feedstuff method, not only maximize
The nutrient substance that make use of in fermentation liquid, solve simultaneously discarded thalline slag pollute problem.Embodiment 5
Circulating fermentation described in the present embodiment produces the method for lactic acid co-production albumen feedstuff, comprises the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, described jade
Rice & peanut milk liquid uses filter press to carry out filtering and solid-liquid separation, and controlling sheet frame feed pressure is 0.45Mp, controls sheet frame and compresses
Pressure is 18Mpa, after being separated by filtration, obtains liquefaction sugar liquid and corn starch residue that DE value is 27%, total sugar in liquefaction sugar liquid
Content is 175g/L；
(2) premashing: premashing temperature is 55 DEG C, adds liquefaction sugar liquid and carries out in the fermentation tank of sterilization and sterilizing
Premashing；Adding phosphoric acid regulation liquefaction sugar liquid pH that mass fraction is 1% is 4.5, and the addition of saccharifying enzyme is according to liquefaction sugar
In liquid, every gram of total sugar adds saccharifying enzyme 500U, and is passed through filtrated air in fermentation tank, keeps pressure inside the tank 0.4Mpa, premashing
1 hour time, obtaining fermented feed liquid, in gained fermented feed liquid, DX value is 93%；
(3) limit saccharifying limit fermentation: premashing terminates to add in backward fermented feed liquid yeast extract, and adds in fermented feed liquid
Mass fraction be 30% ammonia spirit with keep fermented feed liquid pH for 5.9, add when the temperature of fermented feed liquid drops to 51 DEG C
Add the lactobacillus suspension of fermented feed liquid cumulative volume 6%, the OD of lactobacillus suspension620Value is 11, and to be always maintained at temperature in fermentation tank be 51
DEG C, and in fermentation tank, it is passed through filtrated air, the OD of detection fermented feed liquid620Value, treats the OD of fermented feed liquid620Value rises to 10
Time, regulating fermented feed liquid pH to 5.6, add saccharifying enzyme, the addition of saccharifying enzyme adds sugar according to every gram of total sugar in liquefaction sugar liquid
Change enzyme 50U, detect lactic acid bacteria after fermenting 45 hours and no longer produce acid, fermentation ends；
(4) being filtered by gained fermented feed liquid, solid-liquid separation obtains solid dreg and lactic acid feed liquid, by gained solid thalline slag
Weigh, and add account for described dreg weight 15wt% complex media (include ammonium sulfate that mass ratio is 4:1.5:3.5:1.5,
Disodium EDTA, dodecyl sodium sulfate and sodium citrate) carry out pretreatment, to thalline slag and complex media
Mixture adds water, and thalline slag and complex media are made aqueous solution mixing, thalline slag and complex media in aqueous total
Mass concentration is 40wt%, at a temperature of 25 DEG C standing process 40min, and will process after bacterium solution in 1000-1200rpm rotating speed
Lower centrifugal filtration, solid-liquid separation respectively obtains solvable nutrient substance and soluble impurity again；
Described solvable nutrient substance is used for being recycled in fermentation tank the fermentation carrying out subsequent cycle, and gained impurity can
It is used for preparing desulfurizing agent after drying, pulverizing；
The lactic acid feed liquid obtained after solid-liquid separation obtains, containing lactic acid concentrated solution, detecting Fermented Condensed liquid after evaporation and concentration
In residual total sugar content be 0.30%, residual reducing sugar is 0.10%, and saccharic acid conversion ratio reaches 95.8%；
(5) taking the corn starch residue separated in described step (1), the inoculum concentration according to 10% accesses thermophilic lactobacillus,
And at a temperature of 30 DEG C, carry out solid fermentation 48h, the corn starch protein slurry of fermentation gained is carried out rotary drying in 90 DEG C,
Size-reduced, prepare albumen feedstuff；Detect according to GB/T 18246-2000, in the albumen feedstuff prepared, 18 kinds of aminoacid (Radix Asparagis
Propylhomoserin, threonine, serine, glutamic acid, glycine, alanine, cystine, valine, methionine, isoleucine, leucine,
Tyrosine, phenylalanine, lysine, histidine, tryptophan, arginine, proline) total content is 27.98wt%, its two-story valley
The content of propylhomoserin, alanine, leucine and proline is respectively 5.03wt%, 2.00wt%, 3.60wt%, 2.51wt%.
According to above-mentioned steps (1)-(5) condition circulating fermentation produce lactic acid, the strain in described step (3) be through
In a upper circulation step (4), pretreatment Posterior circle is back to the strain of fermentation tank, is carried out continuously the continuous fermentation of 5 circulations, inspection
Survey the residual sugar situation that every circulating fermentation terminates in rear lactic fermentation liquid, and calculate saccharic acid conversion ratio.
In the present embodiment, after carrying out 5 circulating fermentations process according to above-mentioned condition, the saccharic acid in 2-4 cyclic process turns
Rate is respectively 95.9%, 96.2%, 96.4%, 96.9%.Visible, circulating fermentation of the present invention produces lactic acid parallel connection and lays eggs
The method of white feedstuff, utilizes single batch strain can realize multi cycle fermentation, described thalline slag after pretreatment, not only its
The efficiency of kefir milk acid does not reduce, and contributes to because carrying the remaining nutrient substance in fermentation liquid on the contrary promoting following cycle
In saccharic acid conversion ratio, it is seen then that circulating fermentation of the present invention produce lactic acid co-production albumen feedstuff method, not only maximize
The nutrient substance that make use of in fermentation liquid, solve simultaneously discarded thalline slag pollute problem.
Obviously, above-described embodiment is only for clearly demonstrating example, and not restriction to embodiment.Right
For those of ordinary skill in the field, can also make on the basis of the above description other multi-form change or
Variation.Here without also cannot all of embodiment be given exhaustive.And the obvious change thus extended out or
Change among still in the protection domain of the invention.
Claims (10)
1. the method that a circulating fermentation produces lactic acid co-production albumen feedstuff, it is characterised in that comprise the steps:
(1) prepared by raw material: take Semen Maydis through remove impurity, pulverize, size mixing, spray liquefaction step and prepare Semen Maydis serosity, be separated by filtration
After, obtain liquefy sugar liquid and corn starch residue；
(2) premashing: prepared liquefaction sugar liquid added in fermentation tank, adds saccharifying enzyme and carries out premashing process, fermented
Feed liquid；
(3) after premashing terminates, in fermented feed liquid add yeast extract, and inoculate into lactobacillus suspension and saccharifying enzyme carry out synchronize sugar
Change fermentation, detect the yield of lactic acid simultaneously；
(4) gained fermented feed liquid is filtered, and gained solid thalline slag is carried out pretreatment with complex media, after pretreatment
Thalline slag is separated by filtration the solvable nutrient substance of acquisition and soluble impurity；The solvable nutrient obtained after simultaneously filtering separation
Matter is recycled in fermentation tank and carries out the fermentation of subsequent cycle and be used；
Described complex media includes ammonium sulfate, disodium EDTA, dodecyl sodium sulfate and sodium citrate；
(5) take the corn starch residue separated in described step (1), access thermophilic lactobacillus and carry out solid fermentation, and will fermentation
The corn starch protein slurry of gained carries out rotary drying, size-reduced, prepares albumen feedstuff.
Circulating fermentation the most according to claim 1 produces the method for lactic acid co-production albumen feedstuff, it is characterised in that described
In complex media, the mass ratio of described ammonium sulfate, disodiumedetate, dodecyl sodium sulfate and sodium citrate is 1-
5:1-3:1-4:1-3.
Circulating fermentation the most according to claim 2 produces the method for lactic acid co-production albumen feedstuff, it is characterised in that described
The consumption of complex media accounts for the 10-20wt% of described thalline slag amount；Water is added to the mixture of thalline slag and complex media, will
Thalline slag and complex media make aqueous solution mixing, and thalline slag and complex media total mass concentration in aqueous is 10-
50wt%.
Circulating fermentation the most according to claim 3 produces the method for lactic acid co-production albumen feedstuff, it is characterised in that described
Thalline slag pre-treatment step processes 30-50min at 20-30 DEG C.
Circulating fermentation the most according to claim 4 produces the method for lactic acid co-production albumen feedstuff, it is characterised in that described
Thalline slag pretreated filtration separating step is centrifugal filtration, and described centrifugal rotational speed is 1000-1200rpm.
6. the method producing lactic acid co-production albumen feedstuff according to the circulating fermentation described in any one of claim 1-5, its feature
Being, in described step (3), saccharifying limit, described limit fermentation step specifically includes: after premashing terminates, and adds in fermented feed liquid
Yeast extract, and in fermented feed liquid, the pH of addition ammonia spirit regulation fermented feed liquid is 6.0 ± 0.1, treats the temperature of fermented feed liquid
Add the lactobacillus suspension accounting for fermented feed liquid cumulative volume 6%-12% when reaching 50 ± 2 DEG C, treat the OD of lactobacillus suspension620Value reaches
During 9.5-12, in fermentation tank, it is passed through filtrated air, and keeps continuation fermentation at a temperature of this；Treat the OD of fermented feed liquid620Value reaches
When 10, regulation fermented feed liquid pH is 5.5 ± 0.1, and continues to add saccharifying enzyme 50-100U/g according to every gram of total sugar in liquefaction sugar liquid
Add saccharifying enzyme and carry out simultaneous saccharification and fermentation.
7. the method producing lactic acid co-production albumen feedstuff according to the circulating fermentation described in any one of claim 1-5, its feature
Being, in described step (1), described filtration separating step, for using filter press to filter, controls sheet frame feed pressure
For 0.4-0.45Mp, controlling sheet frame compaction pressure is 18-20Mpa.
8. the method producing lactic acid co-production albumen feedstuff according to the circulating fermentation described in any one of claim 1-5, its feature
Being, in described step (5), the inoculum concentration of described thermophilic lactobacillus is 10%, and the temperature of described solid fermentation step is 30-
35 DEG C of fermentation 45-48h, the temperature of described rotary drying step is 90 DEG C.
9. the method producing lactic acid co-production albumen feedstuff according to the circulating fermentation described in any one of claim 1-5, its feature
Being, in described step (2), in described pre-saccharification step, the addition of described saccharifying enzyme is total according in liquefaction sugar liquid every gram
Sugar adds 400-600U/g meter, and control fermentation liquid in 50-70 DEG C, carry out premashing process under the conditions of pH4.5 ± 0.1.
10. the method producing lactic acid co-production albumen feedstuff according to the circulating fermentation described in any one of claim 1-5, its feature
It is, in described step (4), also includes being dried by the soluble impurity of isolated and preparing the step of desulfurizing agent.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110904279A (en) * | 2019-12-22 | 2020-03-24 | 河南金丹乳酸科技股份有限公司 | Segmented pH control method in lactic acid fermentation production |
| CN112725385A (en) * | 2019-10-28 | 2021-04-30 | 中国石油化工股份有限公司 | Method for preparing long-chain dicarboxylic acid by fermentation |
| CN114343060A (en) * | 2021-12-30 | 2022-04-15 | 河南金丹乳酸科技股份有限公司 | Process for improving protein content in thallus residue in lactic acid production |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1130627A (en) * | 1995-11-24 | 1996-09-11 | 中原制药厂 | Process for preparing sodium (or potassium) L-ascorbate |
| CN101134976A (en) * | 2006-08-29 | 2008-03-05 | 武汉天惠生物工程有限公司 | Method for producing validamycin by circulating fermentation |
| CN103275875A (en) * | 2013-04-23 | 2013-09-04 | 马伟超 | Trichoderma koningii, and compound microbial agent composition and application thereof |
| CN103789362A (en) * | 2014-02-25 | 2014-05-14 | 河南金丹乳酸科技股份有限公司 | Method for producing lactic acid through previous saccharification and simultaneous saccharification and fermentation |
-
2016
- 2016-07-29 CN CN201610613703.0A patent/CN106047954B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1130627A (en) * | 1995-11-24 | 1996-09-11 | 中原制药厂 | Process for preparing sodium (or potassium) L-ascorbate |
| CN101134976A (en) * | 2006-08-29 | 2008-03-05 | 武汉天惠生物工程有限公司 | Method for producing validamycin by circulating fermentation |
| CN103275875A (en) * | 2013-04-23 | 2013-09-04 | 马伟超 | Trichoderma koningii, and compound microbial agent composition and application thereof |
| CN103789362A (en) * | 2014-02-25 | 2014-05-14 | 河南金丹乳酸科技股份有限公司 | Method for producing lactic acid through previous saccharification and simultaneous saccharification and fermentation |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112725385A (en) * | 2019-10-28 | 2021-04-30 | 中国石油化工股份有限公司 | Method for preparing long-chain dicarboxylic acid by fermentation |
| CN112725385B (en) * | 2019-10-28 | 2022-09-09 | 中国石油化工股份有限公司 | Method for preparing long-chain dicarboxylic acid by fermentation |
| CN110904279A (en) * | 2019-12-22 | 2020-03-24 | 河南金丹乳酸科技股份有限公司 | Segmented pH control method in lactic acid fermentation production |
| CN110904279B (en) * | 2019-12-22 | 2023-04-07 | 河南金丹乳酸科技股份有限公司 | Segmented pH control method in lactic acid fermentation production |
| CN114343060A (en) * | 2021-12-30 | 2022-04-15 | 河南金丹乳酸科技股份有限公司 | Process for improving protein content in thallus residue in lactic acid production |
| CN114343060B (en) * | 2021-12-30 | 2023-07-25 | 河南金丹乳酸科技股份有限公司 | Process for increasing protein content in thallus slag in lactic acid production |
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