CN102321686B - Processing method and application of starch raw material - Google Patents
Processing method and application of starch raw material Download PDFInfo
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Abstract
The invention provides a processing method of a starch raw material, which comprises the following steps that: (1) starch raw material powder is mixed with water to obtain starch slurry, and the starch slurry is mixed with amylase; (2) the secondary injection is carried out; (3) by flash vaporization and cooling, a liquefied liquid is obtained after the flash vaporization; (4) the liquefied fluid is in contact with a protein flocculant, and a mixture obtained after the contact keeps stand and is settled and separated to obtain a first liquefied serum layer and a flocculation layer; and (5) the flocculation layer is filter-pressed to obtain a second liquefied serum layer and residues. The invention also provides application of the method in the fermentation preparation of citric acid. The processing method provided by the invention has the advantages of reducing the consumption of energy and equipment of liquefied serum, reducing the production cost and improving the production efficiency.
Description
Technical field
The present invention relates to a kind for the treatment of process and application of starchy material.
Background technology
Citric acid is a kind of organic acid being widely used in the industries such as beverage, food and medicine.At present, citric acid is prepared mainly through fermentation method, is generally first pulverized by starchy material, the product after pulverizing and water is mixed to get farinaceous size, is mixed by farinaceous size and carry out enzymolysis, obtain enzymolysis product (enzymatic liquefaction liquid) with enzyme.Adopt plate-and-frame filter press to filter enzymatic liquefaction liquid, the liquefier stirred is separated liquefaction clear liquid and filter residue by pressure filter, removing filter residue is to obtain the liquefaction clear liquid being more conducive to subsequent fermentation.Aspergillus niger is seeded to fermentation in the fermented liquid containing described liquefaction clear liquid and produces citric acid.
There is following defect in this technique:
(1) citric acid fermentation needs low DE value liquid glucose.DE value (reducing sugar (with glucose meter) accounts for the degree of syrup dry) the more low saccharification being more conducive to aspergillus niger in Citric Acid Fermentation of enzymolysis product, is beneficial to and reduces fermentation period and improve transformation efficiency.But the DE value of enzymatic liquefaction liquid is lower, and filtration velocity also declines to a great extent, and affects liquid glucose and produces efficiency.
(2) in enzymatic liquefaction liquid, dispersion contains a large amount of albumen and dregs, turbidity is larger, in order to ensure to realize solid-liquid separation in the limited production time, whole liquefier all needs to carry out press filtration, required equipment and energy consumption are comparatively large, and produce a large amount of filter wash cloth waste water, and filter cloth consumption is large, automatization level is low, and human resources consumption is large.
Summary of the invention
The object of the invention is the above-mentioned defect in order to overcome prior art, providing a kind for the treatment of process of starchy material, the method can reduce the energy and devices consume of producing liquefaction clear liquid, reduces production cost, enhances productivity.
To achieve these goals, the invention provides a kind for the treatment of process of starchy material, the method comprises the following steps:
(1) starchy material powder and water are mixed to get farinaceous size, farinaceous size is mixed with amylase, obtain mixture;
(2) mixture obtained in step (1) is once sprayed with the first steam at 90-105 DEG C, obtain a liquefier, then liquefier second steam is carried out second spraying at 130-145 DEG C, obtain secondary liquefier;
(3) the secondary liquefier obtained in step (2) is carried out flash distillation, cooling, obtain the liquefier after flash distillation;
(4) liquefier after the flash distillation in step (3) is contacted with protein flocculant, and gained mixture after contact is left standstill carry out settlement separate, obtain the first liquefaction supernatant liquid and flocbed;
(5) flocbed in step (4) is carried out press filtration, obtain the second liquefaction clear liquid and filter residue.
Present invention also offers the application of aforesaid method in preparation of citric acid by fermentation.
Pass through technique scheme, farinaceous size and diastatic mixture are passed through second spraying technique, starchy material protein denaturation can be made to flocculate, add the layered effect that flocculation agent can improve the follow-up standing sedimentation separation of liquefier, not only separation time can be reduced, and the liquefaction clear liquid that press filtration fore portion meets fermentation standard can be realized extract in advance, need to enter the liquefier that press filtration step produces liquefaction clear liquid and reduce in a large number, thus reduce working load and the pressure of press filtration.Experiment shows, use present method, liquefier (can reduce microbiological contamination probability) at 80-95 DEG C, leave standstill 1 hour, solid-liquid separation rate is 45-60%, and under similarity condition, does not take second spraying technique, and not adding flocculation agent, the solid-liquid separation rate adopting standing sedimentation to be separated is only 10-20%.
Visible, the present invention realizes being separated of the first liquefaction supernatant liquid and flocbed in the short period of time, it is limpid that the first liquefaction clear liquid obtained meets liquid glucose color after testing, and turbidity is less than 600NTU, can directly enter fermentation system and ferment, the liquefier of about 40-60% is without the need to carrying out press filtration, improve the solid concentration of feed liquid to be filtered, decrease the discharge of wastewater such as the filter cloth water for cleaning of press filtration, be conducive to environmental protection, and decrease the energy and devices consume, improve production efficiency.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The invention provides a kind for the treatment of process of starchy material, it is characterized in that, the method comprises the following steps:
(1) starchy material powder and water are mixed to get farinaceous size, farinaceous size is mixed with amylase, obtain mixture;
(2) mixture obtained in step (1) is once sprayed with the first steam at 90-105 DEG C, obtain a liquefier, then liquefier second steam is carried out second spraying at 130-145 DEG C, obtain secondary liquefier;
(3) the secondary liquefier obtained in step (2) is carried out flash distillation, cooling, obtain the liquefier after flash distillation;
(4) liquefier after the flash distillation in step (3) is contacted with protein flocculant, and gained mixture after contact is left standstill carry out settlement separate, obtain the first liquefaction supernatant liquid and flocbed;
(5) flocbed in step (4) is carried out press filtration, obtain the second liquefaction clear liquid and filter residue.
Amylase refers to can the general name of class of enzymes of starch-splitting glycosidic link, and described amylase generally comprises α-amylase, beta-amylase, saccharifying enzyme and isoamylase.
α-amylase is also known as starch Isosorbide-5-Nitrae-dextrinase, and it can cut the α-Isosorbide-5-Nitrae-glycosidic link of starch chain inside at random, brokenly, is maltose, the oligosaccharides containing 6 glucose units and the oligosaccharides with side chain by Starch Hydrolysis.
Beta-amylase, also known as starch Isosorbide-5-Nitrae-maltoside enzyme, can cut Isosorbide-5-Nitrae-glycosidic link from starch molecule non reducing end, generate maltose.The product that this enzyme acts on starch is maltose and limit dextrin.
Saccharifying enzyme is also known as starch α-Isosorbide-5-Nitrae-glucuroide, and this enzyme acts on the non reducing end of starch molecule, in units of glucose, acts on the α-Isosorbide-5-Nitrae-glycosidic link in starch molecule successively, generates glucose.Product after saccharifying enzyme acts on amylopectin has glucose and the oligosaccharides with α-1,6-glycosidic link; Acting on the product after amylose starch is all almost glucose.
Isoamylase is also known as starch α-1,6-glucuroide, branching enzyme, and this enzyme acts on α-1, the 6-glycosidic link at branched amylopectin molecules branching-point place, is cut by the whole side chain of amylopectin and becomes amylose starch.
According to the present invention, preferably use α-amylase and/or isoamylase.More preferably Thermostable α-Amylase is used.Thermostable α-Amylase has excellent heat resistance, adopt Bacillus licheniformis through deep drainpipe, the operations such as extraction are refining to be formed, can random hydrolysis starch, glycogen and degradation product inside thereof α-1,4 glucosides are good for and the viscosity of colloidal starch solution are declined rapidly, produce soluble dextrins and oligosaccharide, excessive hydrolysis can produce a small amount of glucose and maltose.Above-mentioned Thermostable α-Amylase can be commercially available, such as can purchased from Novozymes Company.
Under preferable case of the present invention, the condition that described starchy material powder mixes with water comprises: temperature is 45-60 DEG C, and the weight ratio of starchy material powder and water is 1: 1.8-4.The condition that further preferred described starchy material powder mixes with water comprises: temperature is 50-55 DEG C, and pH value controls at 5-7, and the weight ratio of starchy material powder and water is 1: 2-3.
Amylase of the present invention can add farinaceous size by one or many.Under preferable case, with the dry weight basis of every gram of starchy material powder, described diastatic total consumption is 8-24 enzyme activity unit.More preferably 10-20 enzyme activity unit.
Define according to GB 8275-2009: 1g solid enzyme powder (or 1ml liquid enzymes), in 70 DEG C, under pH=6.0 condition, the enzyme amount in 1min required for liquefaction 1mg Zulkovsky starch, is 1 enzyme activity unit, represents with u/g (or u/ml).In the present invention, enzyme activity unit continues to use this definition.
According to the present invention, in step (2), the weight ratio of mixture (or a liquefier) and injection steam, spray regime and injecting time are not particularly limited, can at injector known in those skilled in the art (such as, the long water heater of million smooth injectors or sky) in carry out injection contact, preferably, the weight ratio of described first steam and mixture is 0.05-0.1: 1, first steam and mixture duration of contact are 1-5 second, and Contact Temperature is 95-100 DEG C; The weight ratio of described second steam and mixture is 0.05-0.1: 1, and steam and mixture duration of contact are 1-3 second, and Contact Temperature is 135-140 DEG C.In more preferred situation, once the timed interval of injection and second spraying is 120-180 minute.
In the present invention, the temperature that the first steam contacts with mixture refers to that the first steam reaches thermally equilibrated temperature after contacting with mixture; The temperature that second steam contacts with mixture refers to that the second steam reaches thermally equilibrated temperature after contacting with mixture.Due to steam and mixture very short for duration of contact, the temperature after the steam recorded contacts with mixture with steam with the Contact Temperature of mixture is basically identical.Above-mentionedly reach thermally equilibrated temperature and can be controlled by steam regulation flow and mixture flow rate.Described first steam and the second steam can be identical or different, as long as by adjust flux, can reach above-mentioned Contact Temperature.Under preferable case, the temperature of described first steam can be 140-160 DEG C.The temperature of described second steam can be 140-160 DEG C.
Flash distillation of the present invention, be in order to reach better brought by temperature variation fast make the expansion of starch molecule more abundant, to such an extent as to macrobead starch swelling fracture can be made to be the object of starch granule, and make the contact better effects if of amylase and starch granules, to reach better hydrolysis result.Under preferable case, the temperature of flash distillation is 95-110 DEG C, and the pressure of flash distillation is-0.06 ~-0.09MPa (gauge pressure), and lower the temperature after flash distillation 5-10 DEG C.In more preferred situation, the steam obtained is returned in step (2) and be used as the first steam after flash distillation; The water of condensation obtained after flash distillation is returned in step (1) for the preparation of farinaceous size.Like this can Resource Recycling Utilization, reduce production cost.
Albumen flocculation agent of the present invention can be all kinds of flocculation agents that can realize albumen flocculation.Such as: inorganic flocculating agent (such as: wherein one or more such as ferric sulfate, aluminium sulfide, poly-silicic acid iron sulfate, poly-phosphorus iron(ic) chloride, alum), or organic floculant (such as: in acrylamide, polyacrylamide, ligninsulfonate, sodium polyacrylate, polymine etc. one or more).Different according to the purposes of the liquefaction clear liquid obtained, the albumen flocculation agent preferably used is different.If liquefaction clear liquid is used for fermentation produce common citric acid, preferred natural organic floculant (such as: in chitosan, gelatin, dextran, chitin derivativ, Sodium Alginate, Xylo-Mucine etc. one or more).If liquefaction clear liquid is used for producing food grade citric acid, then must select the natural organic food-grade flocculation agent of toxicological harmless.
Under preferable case, relative to the liquefier after often liter of flash distillation, the add-on of protein flocculant is 2-40mg.Be more preferably 5-25mg.More preferably 5-15mg.Settlement separate temperature is 80-90 DEG C, and the settlement separate time is more than 1 hour.
Press filtration of the present invention is solid-liquid separating method, realizes filtration operation by applying positive pressure in filtration medium side.The parameter such as scope, action time of the present invention to this positive pressure is not particularly limited, and can realize the object of the invention parameter.Under preferable case, the pressure of described press filtration is 0.2-0.7MPa, and the time is 1-4 hour.In preferred situation, the pressure of described press filtration is 0.4-0.6MPa, and the time is 2-3 hour.Can promote that liquid glucose leaches better like this.
The temperature of the present invention to press filtration is not particularly limited, and under preferable case, the temperature of described press filtration is 60-85 DEG C.
The pressure filter of the available use of the inventive method is comparatively extensive, such as, and chamber-type press filter, plate-and-frame filter press, belt filter press, vertical type blotter press, diaphragm pressing pressure filter etc.The press filtration of preferred van-type filter.
According to the application of aforesaid method provided by the invention in preparation of citric acid by fermentation, be directly used in subsequent fermentation together with the clear liquid that the first liquefaction supernatant liquid or the first liquefaction supernatant liquid and second can be liquefied and prepare citric acid.According to a preferred method of the present invention, the first liquefaction supernatant liquid and second is liquefied after clear liquid merges and carries out oily water separation, obtain crude oil and liquefaction clear liquid, then liquefaction clear liquid is used for subsequent fermentation and prepares citric acid.Crude oil is separated, the quality of follow-up liquid glucose preparation of citric acid by fermentation can be improved further.Press filtration can make the crude oil be attached on filter residue leach under stress thereupon, and promotion crude oil is separated with liquid glucose.
According to the present invention, described starchy material can be the various raw material containing starch that may be used for enzymolysis, fermentation well known in the art, such as, can be selected from least one in corn, potato class (as cassava), wheat and Chinese sorghum.
In the filter residue of press filtration gained of the present invention, due to aforementioned throwing out, contained protein ratio is higher, is the protein raw materials of high-quality, may be used for producing protein powder etc.
The present invention is further illustrated for the following examples.In following examples, the measuring method of the separation rate of the first liquefaction clear liquid is: get this first liquefaction clear liquid of 100mL and leave standstill 1 hour in graduated cylinder, read the per-cent that the limpid liquid level of isolated color accounts for this first liquefaction clear liquid cumulative volume.Therefore, for the identical first liquefaction clear liquid, this per-cent is higher, and the separation rate of the first liquefaction clear liquid is higher, thus separating effect is better.
The measuring method of liquid glucose fermentation standard (color is limpid, and turbidity is less than 600NTU) is: measure with the liquid glucose QS certification special digital turbidimeter be purchased from Shanghai Zheng Hui Trade Co., Ltd. ZD1 type.
In the embodiment of the present invention, amylase used is the Thermostable α-Amylase purchased from Novozymes Company; Injector used is million smooth injectors; Albumen flocculation agent used is purchased from the natural organic protein flocculation agent of Qingdao Honghai Biotechnology Co., Ltd.'s food grade chitosan; Pressure filter used is the full automatic plate frame filter press purchased from Jingjin Filter Press Group Co., Ltd X2MS2 100/1000-J model.
Embodiment 1
100 parts by weight Corn are pulverized, obtains the crushed products that average particle diameter is 400 microns, by the product after pulverizing and 400 weight parts waters, mix at 45 DEG C, obtain farinaceous size.
At 50 DEG C, be that the α-amylase of 6.4 enzyme activity units/g Semen Maydis powder mixes 60 minutes by farinaceous size and consumption, obtain mixture, this mixture and the steam of 156 DEG C are carried out spraying in injector and contacts (weight ratio of steam and mixture is 0.05: 1), the time of contact is 5 seconds, make the temperature of the mixture after contacting with steam be 95 DEG C, and laminar flow maintains 120 minutes, obtain a liquefier.
An above-mentioned liquefier is carried out spraying with the steam of 156 DEG C again in injector and contacts (weight ratio of steam and mixture is 0.05: 1), the time of contact is 1 second, make the temperature of the mixture after again contacting with steam be 135 DEG C, and keep 5 minutes at such a temperature;
By above-mentioned again contact with steam after mixture carry out flash distillation (pressure is-0.06MPa, and the time is 10 seconds) and, to 95 DEG C, be cooled to 90 DEG C, iodine tries qualified color and shows light red, obtains liquefier.And the steam obtained after flash distillation is returned in above-mentioned first time injecting step, water of condensation is returned in the step for above-mentioned modulation farinaceous size.
At 80 DEG C, be that the α-amylase of 1.6 enzyme activity units/g Semen Maydis powder mixes 150 minutes by this liquefier and consumption, obtain mixture, the amount of 10mg protein flocculant is added according to often liter of this mixture, add protein flocculant, and 1 hour is left standstill at 80 DEG C, isolate the first liquefaction supernatant liquid and flocbed, the first liquefaction clear liquid is collected in Clear liquid tank.The separation rate and the first liquefaction clear liquid turbidity that record the first liquefaction clear liquid are as shown in table 1.
Flocbed is carried out press filtration at 60 DEG C, stops charging when pressure reaches 0.2MPa, through 4 hours, isolate the second liquefaction clear liquid and filter residue.
Embodiment 2
100 parts by weight Corn are pulverized, obtains the crushed products that average particle diameter is 400 microns, by the product after pulverizing and 180 weight parts waters, mix at 60 DEG C, obtain farinaceous size.
At 50 DEG C, be that the α-amylase of 24 enzyme activity units/g Semen Maydis powder mixes 100 minutes by farinaceous size and consumption, obtain mixture, this mixture and the steam of 160 DEG C are carried out spraying in injector and contacts (weight ratio of steam and mixture is 0.1: 1), the time of contact is 1 second, make the temperature of the mixture after contacting with steam be 100 DEG C, and laminar flow maintains 180 minutes, obtain a liquefier.
An above-mentioned liquefier is carried out spraying with the steam of 160 DEG C again in injector and contacts (weight ratio of steam and mixture is 0.1: 1), the time of contact is 3 seconds, make the temperature of the mixture after again contacting with steam be 140 DEG C, and keep 5 minutes at such a temperature;
By above-mentioned again contact with steam after mixture carry out flash distillation (pressure is-0.09MPa, and the time is 10 seconds) and, to 110 DEG C, be cooled to 100 DEG C, iodine tries qualified color and shows light red, obtains liquefier.
Add the amount of 5mg protein flocculant according to often liter of this liquefier, add protein flocculant, and leave standstill 1.2 hours at 90 DEG C, isolate the first liquefaction supernatant liquid and flocbed, the first liquefaction clear liquid is collected in Clear liquid tank.The separation rate and the first liquefaction clear liquid turbidity that record the first liquefaction clear liquid are as shown in table 1.
Flocbed is carried out press filtration at 85 DEG C, stops charging when pressure reaches 0.7MPa, through 1 hour, isolate the second liquefaction clear liquid and filter residue.
Comparative example 1
According to the method for embodiment 2, unlike, do not add albumen flocculation agent, by the liquefier stratification after flash distillation.Concrete grammar is as follows:
100 parts by weight Corn are pulverized, obtains the crushed products that average particle diameter is 400 microns, by the product after pulverizing and 180 weight parts waters, mix at 60 DEG C, obtain farinaceous size.
At 50 DEG C, be that the α-amylase of 24 enzyme activity units/g Semen Maydis powder mixes 100 minutes by farinaceous size and consumption, obtain mixture, this mixture and the steam of 160 DEG C are carried out spraying in injector and contacts (weight ratio of steam and mixture is 0.1: 1), the time of contact is 1 second, make the temperature of the mixture after contacting with steam be 100 DEG C, and laminar flow maintains 180 minutes, obtain a liquefier.
An above-mentioned liquefier is carried out spraying with the steam of 160 DEG C again in injector and contacts (weight ratio of steam and mixture is 0.1: 1), the time of contact is 3 seconds, make the temperature of the mixture after again contacting with steam be 140 DEG C, and keep 5 minutes at such a temperature;
By above-mentioned again contact with steam after mixture carry out flash distillation (pressure is-0.09MPa, and the time is 10 seconds) and, to 110 DEG C, be cooled to 100 DEG C, iodine tries qualified color and shows light red, obtains liquefier.
Above-mentioned liquefier is left standstill 5 hours at 90 DEG C, and the separation rate and the first liquefaction clear liquid turbidity that record the first liquefaction clear liquid are as shown in table 1.
Comparative example 2
According to the method for embodiment 2, unlike, only use a high-temperature injection.Concrete grammar is as follows:
100 parts by weight Corn are pulverized, obtains the crushed products that average particle diameter is 400 microns, by the product after pulverizing and 180 weight parts waters, mix at 60 DEG C, obtain farinaceous size.
At 50 DEG C, be that the α-amylase of 24 enzyme activity units/g Semen Maydis powder mixes 100 minutes by farinaceous size and consumption, obtain mixture, this mixture and the steam of 160 DEG C are carried out spraying in injector and contacts (weight ratio of steam and mixture is 0.1: 1), the time of contact is 4 seconds, make the temperature of the mixture after contacting with steam be 100 DEG C, and laminar flow maintains 180 minutes, obtain a liquefier.
An above-mentioned liquefier is carried out flash distillation (pressure is-0.09MPa, and the time is 10 seconds) and, to 110 DEG C, be cooled to 100 DEG C, iodine tries qualified color and shows light red, obtains liquefier.
Add the amount of 5mg protein flocculant according to often liter of this liquefier, add protein flocculant, and leave standstill 1.2 hours at 90 DEG C, isolate the first liquefaction supernatant liquid and flocbed, the first liquefaction clear liquid is collected in Clear liquid tank.The separation rate and the first liquefaction clear liquid turbidity that record the first liquefaction clear liquid are as shown in table 1.
Embodiment 3
100 parts by weight Corn are pulverized, obtains the crushed products that average particle diameter is 400 microns, by the product after pulverizing and 300 weight parts waters, mix at 50 DEG C, obtain farinaceous size.
At 50 DEG C, be that the α-amylase of 20 enzyme activity units/g Semen Maydis powder mixes 150 minutes by farinaceous size and consumption, obtain mixture, this mixture and the steam of 160 DEG C are carried out spraying in injector and contacts (weight ratio of steam and mixture is 0.08: 1), the time of contact is 3 seconds, make the temperature of the mixture after contacting with steam be 97 DEG C, and laminar flow maintains 150 minutes, obtain a liquefier.
An above-mentioned liquefier is carried out spraying with the steam of 160 DEG C again in injector and contacts (weight ratio of steam and mixture is 0.08: 1), the time of contact is 2 seconds, make the temperature of the mixture after again contacting with steam be 138 DEG C, and keep 5 minutes at such a temperature;
By above-mentioned again contact with steam after mixture carry out flash distillation (pressure is-0.07MPa, and the time is 10 seconds) and, to 100 DEG C, be cooled to 93 DEG C, iodine tries qualified color and shows light red, obtains liquefier.
Add the amount of 15mg protein flocculant according to often liter of this liquefier, add protein flocculant, and leave standstill 1.1 hours at 85 DEG C, isolate the first liquefaction supernatant liquid and flocbed, the first liquefaction clear liquid is collected in Clear liquid tank.The separation rate and the first liquefaction clear liquid turbidity that record the first liquefaction clear liquid are as shown in table 1.
Flocbed is carried out press filtration at 70 DEG C, stops charging when pressure reaches 0.5MPa, through 2 hours, isolate the second liquefaction clear liquid and filter residue.
First liquefaction clear liquid and the second liquefaction clear liquid are merged and sends into Clear liquid tank, at 65 DEG C, leave standstill 2 hours, isolate crude oil layer and liquefaction supernatant liquid.
Table 1
Data as can be seen from above embodiment and table 1, adopt the starchy material of method process of the present invention, and the separation rate of the first liquefaction clear liquid is higher; The the first liquefaction clear liquid conformance with standard fermentation condition obtained, directly can enter fermentation system.
Comparative example 1 adopts second spraying, does not add albumen flocculation agent, and the separation rate recording the first liquefaction clear liquid is lower, and settlement separate speed is slow, and turbidity is higher; The the first liquefaction clear liquid obtained does not meet standard fermentation conditions, directly can not enter fermentation system.
Comparative example 2 adopts once sprays, and adds albumen flocculation agent, and the separation rate recording the first liquefaction clear liquid is lower; The the first liquefaction clear liquid obtained does not meet standard fermentation conditions, directly can not enter fermentation system.
Claims (11)
1. a treatment process for starchy material, is characterized in that, the method comprises the following steps:
(1) starchy material powder and water are mixed to get farinaceous size, farinaceous size is mixed with amylase, obtain mixture;
(2) mixture obtained in step (1) is once sprayed at 90-105 DEG C with the first steam, obtain a liquefier, again liquefier second steam is carried out second spraying at 130-145 DEG C, obtain secondary liquefier, the timed interval of described once injection and second spraying is 120-180 minute;
(3) the secondary liquefier obtained in step (2) is carried out flash distillation, cooling, obtain the liquefier after flash distillation;
(4) liquefier after the flash distillation in step (3) is contacted with protein flocculant, and gained mixture after contact is left standstill carry out settlement separate, obtain the first liquefaction supernatant liquid and flocbed;
(5) flocbed in step (4) is carried out press filtration, obtain the second liquefaction clear liquid and filter residue.
2. method according to claim 1, wherein, the condition that described starchy material powder mixes with water comprises: temperature is 45-60 DEG C, and the weight ratio of starchy material powder and water is 1:1.8-4.
3. method according to claim 1, wherein, with the dry weight basis of every gram of starchy material powder, described diastatic consumption is 8-24 enzyme activity unit.
4. method according to claim 1, wherein, the weight ratio of described first steam and mixture is 0.05-0.1:1, and the first steam and mixture duration of contact are 1-5 second, and Contact Temperature is 95-100 DEG C; The weight ratio of described second steam and a liquefier is 0.05-0.1:1, and the duration of contact of steam and a liquefier is 1-3 second, and Contact Temperature is 135-140 DEG C.
5. method according to claim 1, wherein, described in step (3), the temperature of flash distillation is
95-110 DEG C, the pressure of flash distillation is-0.06 ~-0.09MPa, and lower the temperature after flash distillation 5-10 DEG C.
6. method according to claim 1 or 5, wherein, the method also comprises the steam obtained after flash distillation to return in step (2) and is used as the first steam; The water of condensation obtained after flash distillation is returned in step (1) for the preparation of farinaceous size.
7. method according to claim 1, wherein, relative to the liquefier after often liter of flash distillation, the add-on of protein flocculant is 2-40mg; Settlement separate temperature is 80-90 DEG C, and the settlement separate time is more than 1 hour.
8. the method according to claim 1 or 7, wherein, described protein flocculant is natural organic floculant.
9. method according to claim 1, wherein, the pressure of described press filtration is 0.2-0.7MPa, and time of filter pressing is 1-4 hour, and the temperature of described press filtration is 60-85 DEG C.
10. method according to claim 1, wherein, described starchy material comprise in corn, potato class, wheat, Chinese sorghum one or more.
11. methods according to claim 1, wherein, the method also comprises and liquefy after clear liquid merges and carry out oily water separation by the first liquefaction supernatant liquid and second, obtains crude oil and the clear liquid that liquefies.
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| CN102747121B (en) * | 2012-07-19 | 2014-10-22 | 中粮生物化学（安徽）股份有限公司 | Starchy material enzymolysis product and preparation method and application thereof and method for preparing citric acid by fermentation |
| CN102839203B (en) * | 2012-09-19 | 2014-01-01 | 中粮生物化学（安徽）股份有限公司 | Enzymolysis method of starch raw material and method for preparing citric acid by fermenting |
| CN103146768B (en) * | 2013-03-28 | 2014-10-29 | 中粮生物化学（安徽）股份有限公司 | Method for preparing citric acid |
| CN103146763B (en) * | 2013-03-28 | 2016-01-13 | 中粮生物化学（安徽）股份有限公司 | A kind of method preparing ethanol |
| CN109157870B (en) * | 2018-09-30 | 2022-04-26 | 北京盛美诺生物技术有限公司 | Composition for clarifying suspensions containing viscous materials |
| CN109157871B (en) * | 2018-09-30 | 2022-04-26 | 北京盛美诺生物技术有限公司 | Method for carrying out solid-liquid separation on suspension containing viscous substances |
| CN113087813B (en) * | 2021-03-17 | 2021-11-02 | 广州芊亮科技有限公司 | Tea bran extraction process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007000144A (en) * | 2005-06-22 | 2007-01-11 | Natl Starch & Chem Investment Holding Corp | Use of starch having low gelatinization temperature for production of fermentation product |
| CN100999767A (en) * | 2006-11-29 | 2007-07-18 | 甘肃昆仑生化有限责任公司 | Tech, process of producing high pureness oligoiso maltose by yeast |
| CN101492701A (en) * | 2008-01-21 | 2009-07-29 | 黄石兴华生化有限公司 | Process for fermentation production of lemon acid with fresh sweet potato as raw material |
| CN101696437A (en) * | 2009-09-10 | 2010-04-21 | 万福生科(湖南)农业开发股份有限公司 | Method for producing maltodextrin by using rice |
| CN101787382A (en) * | 2010-01-19 | 2010-07-28 | 广州双桥股份有限公司 | Method for recovering coin protein sugar dregs and preparing protein nitrogen sources and nitrogen-containing syrup |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101565762B (en) * | 2009-05-25 | 2011-09-28 | 安徽汇佳生物科技有限公司 | Production process for starch sugar |
-
2011
- 2011-09-14 CN CN201110271718.0A patent/CN102321686B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007000144A (en) * | 2005-06-22 | 2007-01-11 | Natl Starch & Chem Investment Holding Corp | Use of starch having low gelatinization temperature for production of fermentation product |
| CN100999767A (en) * | 2006-11-29 | 2007-07-18 | 甘肃昆仑生化有限责任公司 | Tech, process of producing high pureness oligoiso maltose by yeast |
| CN101492701A (en) * | 2008-01-21 | 2009-07-29 | 黄石兴华生化有限公司 | Process for fermentation production of lemon acid with fresh sweet potato as raw material |
| CN101696437A (en) * | 2009-09-10 | 2010-04-21 | 万福生科(湖南)农业开发股份有限公司 | Method for producing maltodextrin by using rice |
| CN101787382A (en) * | 2010-01-19 | 2010-07-28 | 广州双桥股份有限公司 | Method for recovering coin protein sugar dregs and preparing protein nitrogen sources and nitrogen-containing syrup |
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