CN102321704A - Method for treating starchy raw material and method for preparing citric acid - Google Patents
Method for treating starchy raw material and method for preparing citric acid Download PDFInfo
- Publication number
- CN102321704A CN102321704A CN201110220758A CN201110220758A CN102321704A CN 102321704 A CN102321704 A CN 102321704A CN 201110220758 A CN201110220758 A CN 201110220758A CN 201110220758 A CN201110220758 A CN 201110220758A CN 102321704 A CN102321704 A CN 102321704A
- Authority
- CN
- China
- Prior art keywords
- steam
- mixture
- liquefier
- temperature
- enzymolysis
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention relates to a method for treating a starchy raw material and a method for preparing citric acid. The method for treating the starchy raw material comprises the following steps of: mixing powder of the starchy raw material and water to obtain farinaceous size, and mixing the farinaceous size and first part amylase to obtain a mixture; performing primary injection on the mixture by using first steam at the temperature of between 80 and 100 DEG C to obtain primary emulsion, and performing secondary injection on the primary emulsion by using second steam at the temperature of between 120 and 150 DEG C to obtain secondary emulsion; performing flash evaporation and reducing the temperature; and mixing a product obtained through flash evaporation and temperature reduction and second part amylase, and performing enzymolysis. By the method, a dextrose equivalent (DE) value can be reduced, and the fermentation period of the citric acid can be shortened.
Description
Technical field
The present invention relates to a kind of treatment process of starchy material and the preparation method of Hydrocerol A.
Background technology
Hydrocerol A is a kind of organic acid that is widely used in industries such as beverage, food and medicine.At present; Hydrocerol A is mainly through the fermentation method preparation; General elder generation pulverizes starchy material, the product after pulverizing is mixed obtaining farinaceous size with water, farinaceous size is mixed with enzyme carry out enzymolysis; Obtain enzymolysis product (enzymatic liquefaction liquid), and black mold is seeded to fermentation generation Hydrocerol A in the fermented liquid that contains said enzymolysis product.
In above-mentioned technology, the enzymolysis of starchy material (liquefaction) is bigger to the fermentation period influence of Hydrocerol A.Present starchy material enzymolysis (liquefaction) technology adopts steam ejection liquefaction technology mostly, and promptly farinaceous size is injected into certain temperature liquefaction after enzyme-added, separates after flash distillation again, the cooling, and isolated liquid glucose gets into fermentation system.
There is following defective in this technology:
(1) gelatinization is not thorough; After the starchy material particle water-swelling of many greater particle sizes, only the surface is by the starch hydrolysis, the above particle of 0.85mm (being equivalent to 20 mesh sieve holes) for example; Have only the noncrystalline domain of starch and the crystal region swelling on surface, inner crystal region is difficult to reach the gelatinization effect.
(2) liquefaction is not thorough, and glycase is difficult to and does not have the effect of swollen starch crystal region, though added many glycase, starchy material still is difficult to liquefaction, in order to make the iodine examination qualified, just must add glycase more, causes diastatic waste.
(3) the DE value of liquefier (reducing sugar (with glucose meter) accounts for the degree of syrup dry) is higher; Under the similarity condition; The DE value increases with diastatic increase; The DE value of the liquefaction clear liquid that this method is obtained is 28-30%, causes the dextrin molecule too little, and the DE value scope that is beneficial to citric acid fermentation is at 15-20%.Be unfavorable for the saccharifying enzyme effect.Therefore, need the treatment process of a kind of starchy material of exploitation, be applied to citric acid fermentation.
Summary of the invention
The treatment process that the purpose of this invention is to provide a kind of starchy material adopts the enzyme-added second spraying technology of secondary, overcomes the above-mentioned defective that exists in the prior art.
To achieve these goals, the invention provides a kind of treatment process of starchy material, this method comprises the steps:
(1) the starchy material powder is mixed with water obtains farinaceous size, farinaceous size is mixed with first part glycase, obtain mixture;
(2) mixture that obtains in the step (1) is once sprayed under 80-100 ℃ with first steam, obtain liquefier one time, again a liquefier is carried out second spraying with second steam under 120-150 ℃, obtain the secondary liquefier;
(3) the secondary liquefier that obtains in the step (2) is carried out flash distillation and cooling;
(4) under the amylorrhexis condition, the product after the flash distillation that step (3) is obtained and the cooling mixes with second section glycase, carries out enzymolysis.
The present invention also provides a kind of preparation method of Hydrocerol A, and this method comprises according to aforesaid method to be handled starchy material, obtains enzymolysis product, and this enzymolysis product is fermented in the presence of black mold.
Through technique scheme, the enzyme-added second spraying technology of secondary makes that the DE value of liquefier is lower, helps the black mold saccharification, reduces the fermentation residual sugar, shortens fermentation period, improves fermentation level; Second spraying makes that simultaneously liquefaction is more thorough, has reduced the residual starch content in the enzymolysis residue, has improved the sugaring yield, has reduced the grain consumption.Secondary is enzyme-added to have guaranteed diastatic activity simultaneously.
Other features and advantages of the present invention will partly specify in embodiment subsequently.
Embodiment
Following specific embodiments of the invention is elaborated.Should be understood that embodiment described herein only is used for explanation and explains the present invention, is not limited to the present invention.
The invention provides a kind of treatment process of starchy material, this method comprises the steps:
(1) the starchy material powder is mixed with water obtains farinaceous size, farinaceous size is mixed with first part glycase, obtain mixture;
(2) mixture that obtains in the step (1) is once sprayed under 80-100 ℃ with first steam, obtain liquefier one time, again a liquefier is carried out second spraying with second steam under 120-150 ℃, obtain the secondary liquefier;
(3) the secondary liquefier that obtains in the step (2) is carried out flash distillation and cooling;
(4) under the amylorrhexis condition, the product after the flash distillation that step (3) is obtained and the cooling mixes with second section glycase, carries out enzymolysis.
Glycase is meant the general name of class of enzymes that can the starch-splitting glycosidic link, and said glycase generally comprises AMS, beta-amylase, saccharifying enzyme and isoamylase.
AMS is claimed starch 1 again, the 4-dextrinase, and it can cut the inner α-1 of starch chain at random, brokenly, and the 4-glycosidic link is hydrolyzed to starch SANMALT-S, contains the oligosaccharides of 6 glucose units and has the oligosaccharides of side chain.
Beta-amylase is claimed starch 1 again, and 4-maltoside enzyme can cut 1 from the starch molecule non reducing end, and the 4-glycosidic link generates SANMALT-S.The product that this enzyme acts on starch is SANMALT-S and limit dextrin.
Saccharifying enzyme is claimed starch α-1 again, the 4-glucuroide, and this enzyme acts on the non reducing end of starch molecule, is unit with glucose, acts on the α-1 in the starch molecule successively, and the 4-glycosidic link generates glucose.The product that saccharifying enzyme acts on behind the pulullan has glucose and has α-1, the oligosaccharides of 6-glycosidic link; The product that acts on after the amylose starch almost all is a glucose.
Isoamylase is claimed starch α-1 again, and 6-glucuroide, branching enzyme, this enzyme act on the α-1 at pulullan molecule branching-point place, and the 6-glycosidic link is with whole side chain cutting-out the becoming amylose starch of pulullan.
According to the present invention, preferably use AMS and/or isoamylase.More preferably use high temperature resistant AMS.High temperature resistant AMS has excellent heat resistance; Be to adopt Bacillus licheniformis to cultivate through deep layer; Operations such as extraction are refining to form, and ability random hydrolysis starch, glycogen and inner α-1,4 glucoside of degradation product thereof are good for and are made the viscosity of gluey starch solution descend rapidly; Produce soluble dextrins and oligosaccharide, the over-drastic hydrolysis can produce a small amount of glucose and SANMALT-S.
Contriver's discovery of the present invention, the pH value of controlling well when the starchy material powder is sized mixing are further to control the preferred version of DE value well, possibly be the reasons owing to the zymin correlation properties.Therefore, under the preferable case of the present invention, said starchy material powder and water blended condition comprise: temperature is 45-60 ℃, and the pH value is controlled at 5.5-6.2, and the weight ratio of starchy material powder and water is 1: 1.8-4.Further preferred said starchy material powder and water blended condition comprise: temperature is 50-55 ℃, and the pH value is controlled at 5.6-6, and the weight ratio of starchy material powder and water is 1: 2-3.
More abundant for enzymolysis, under the preferable case, in step (1), farinaceous size and first part's glycase blended condition comprise: temperature is 45-60 ℃, and the time is 30-60 minute.Under the preferable case, in step (4), said enzymatic hydrolysis condition comprises: hydrolysis temperature is 85-99 ℃, and enzymolysis time is 60-150 minute.
In addition, contriver of the present invention also finds, under equal processing condition, the enzyme concentration of controlling well also is further to control the preferred version of DE well.Therefore, under the preferable case of the present invention, with the dry weight basis of every gram starchy material powder, said diastatic total consumption is the 8-24 enzyme activity unit.Further be preferably the 10-20 enzyme activity unit.The diastatic consumption of said first part and the adjustable a wider range of the diastatic consumption of second section; Comprehensive hydrolysis result and cost consideration; The diastatic consumption of preferred said first part is the 20-50 weight % of diastatic total consumption, and the diastatic consumption of said second section is the 50-80 weight % of diastatic total consumption.Further the diastatic consumption of preferred said first part is the 30-40 weight % of diastatic total consumption, and the diastatic consumption of said second section is the 60-70 weight % of diastatic total consumption.
Define according to GB 8275-2009: 1g solid enzyme powder (or 1ml liquid enzymes), under 70 ℃, pH=6.0 condition, the needed enzyme amount of liquefaction 1mg Zulkovsky starch is 1 enzyme activity unit in the 1min, representes with u/g (or u/ml).Enzyme activity unit is continued to use this definition among the present invention.
According to the present invention, in step (2), mixture (or a liquefier) does not limit with the weight ratio, spray regime and the injecting time that spray with steam especially; Can be (for example at injector known in those skilled in the art; The long water heater of million smooth injectors or sky) spray contact in, preferably, the weight ratio of said first steam and mixture is 0.05-0.1: 1; First steam and mixture duration of contact are 1-5 second, and the contact temperature is 80-100 ℃; The weight ratio of said second steam and mixture is 0.05-0.1: 1, and steam and mixture duration of contact are 1-3 second, the contact temperature is 120-150 ℃.Under the more preferred situation, once the timed interval of injection and second spraying is 120-180 minute.
Flash distillation according to the invention; Be more abundant in order to reach the expansion that makes starch molecule that brings by temperature variation fast better; To such an extent as to can make macrobead starch swelling fracture is the purpose of starch granule; And make the better effects if that contacts of glycase and starch granules, to reach better hydrolysis result.Under the preferable case, the temperature of flash distillation is 100-103 ℃, and cooling is 5-10 ℃ after the flash distillation, the pressure of flash distillation is-0.06～-0.09MPa.Under the more preferred situation, under the preferable case, the steam that obtains after the flash distillation returned in the step (2) be used as first steam; The water of condensation that obtains after the flash distillation returned in the step (1) be used to prepare farinaceous size.Like this can the recycle resource, reduce production costs.
The present invention preferably before in step (4), the product after the flash distillation that step (3) is obtained and the cooling carries out press filtration, the liquid that press filtration is obtained mixes with second section glycase.Press filtration can make attached to the crude oil on the filter residue and under pressure, leach thereupon, and the promotion crude oil separates with liquid glucose, thereby improves the crude oil yield; Simultaneously owing to do not have filter residue, the grease separate easily in the liquefaction clear liquid; In addition, the subsequent sedimentation disengaging time shortens, and enhances productivity.Under the preferable case, the pressure of said press filtration is 0.1-0.6MPa.
According to the present invention, said starchy material can be the various raw materials that contain starch that can be used for enzymolysis, fermentation well known in the art, for example, can be selected from least a in corn, potato class (like cassava), wheat and the Chinese sorghum.
The present invention also provides a kind of preparation method of Hydrocerol A, and this method comprises according to aforesaid method to be handled starchy material, obtains enzymolysis product, and this enzymolysis product is fermented in the presence of black mold.Under the preferable case, with said enzymolysis product as fermented liquid, 80-90 ℃ of down sterilization 15-30 minute, be cooled to 36-38 ℃ after, black mold is seeded in the fermented liquid, ferment.
Because the preparation method of Hydrocerol A provided by the invention relates generally to the improvement to the treatment process of starchy material before fermenting, therefore the process to fermentation does not have special qualification, can be identical with prior art.For example, the condition of the kind of black mold and consumption and fermentation can be carried out with reference to prior art, and the present invention no longer repeats at this.
Following embodiment will be further described the present invention.In following examples; The measuring method of residual starch content is in the enzymolysis solid phase residue: the enzymolysis residue of getting two parts of equivalent; A glycase and the water (enzymolysis residue) of adding; The water (dissolved residue) of the gross weight equivalent of a adding and glycase and water; Detect in the dissolved residue enzymolysis sugar contents C weight % among the diastatic total sugar content B weight %, enzymolysis residue of dissolving sugar contents A weight %, adding with the Fehling method respectively, detect contents on dry basis W weight % in the enzymolysis residue again, then the residual starch content of butt in the enzymolysis residue=(C-B-A) * 0.9/W.
The measuring method of the DE value of enzymolysis clear liquid is: the Fehling method is measured enzymolysis solution reducing sugar A1 (m/m), and the oven for drying method is measured enzymolysis solution dry matter content A2 (m/m), enzymolysis solution DE value=(A1/A2) * 100%.
Concentration (abbreviation acidity) according to GB 1987-2007 standard detection fermentation secondary fermentation liquid; And the transformation efficiency of calculating Hydrocerol A, weight * 100% of the volume/total reducing sugar of the concentration of transformation efficiency (%)=fermented liquid (abbreviation acidity) * fermented liquid (total reducing sugar=seeding tank total reducing sugar+fermentor tank total reducing sugar).
In the embodiment of the invention, used glycase is the high temperature resistant AMS available from Novozymes Company; Used black mold T01 is available from Tianjin industrial microorganism institute; Used injector is million smooth injectors.
Embodiment 1
100 weight part corns are pulverized, obtained average particle diameter and be 400 microns crushed products,,, obtain farinaceous size, and the pH value of this farinaceous size is adjusted to 5.5 45 ℃ of mixing down with product and 400 weight parts waters after pulverizing.
Under 45 ℃; With farinaceous size and consumption is that the AMS of 6.4 enzyme activity units/g Semen Maydis powder mixed 60 minutes, obtains mixture, this mixture and 156 ℃ steam is sprayed contact (weight ratio of steam and mixture is 0.05: 1) in injector; The time of contact is 5 seconds; Make that the temperature with mixture after steam contacts is 95 ℃, and laminar flow kept 120 minutes, obtain liquefier one time.
An above-mentioned liquefier sprayed in injector with 156 ℃ steam once more contact (weight ratio of steam and mixture is 0.05: 1); The time of contact is 3 seconds; Making once more the temperature with mixture after steam contacts is 120 ℃, and under this temperature, keeps 5 minutes;
Carry out flash distillation (pressure is-0.07MPa, and the time is 10 seconds) with mixture after steam contacts once more and, be cooled to 90 ℃ above-mentioned, obtain liquefier to 100 ℃.And the steam that obtains after the flash distillation returned in above-mentioned first time of the injecting step, water of condensation is returned the step that is used for above-mentioned modulation farinaceous size.
Under 85 ℃, be that the AMS of 1.6 enzyme activity units/g Semen Maydis powder mixed 150 minutes with this liquefier and consumption, obtain mixture.This mixture was left standstill under 80 ℃ 5 hours, isolate enzymolysis solution and enzymolysis solid phase residue, liquid collecting is gone in the clear liquid jar.The DE value of measuring enzymolysis solution is as shown in table 1.
With the above-mentioned liquid glucose that obtains,, be heated to 80 ℃ of sterilizations as fermented liquid; Keep after 30 minutes fast cooling to 36 ℃, insert aspergillus niger strain, ferment; And the total reducing sugar in the detection fermented liquid; Inoculum size is: 4 * 105 colony-forming units of every gram fermented liquid inoculation, and at 40 ℃, 0.2 volume: cultivated fermentation ends 55 hours under the condition of the ventilation of (volume minute).Calculate the acidity and the transformation efficiency of the fermented liquid after fermenting, the result is as shown in table 1.
Embodiment 2
100 weight part corns are pulverized, obtained average particle diameter and be 400 microns crushed products,,, obtain farinaceous size, and the pH value of this farinaceous size is adjusted to 6.2 60 ℃ of mixing down with product and 180 weight parts waters after pulverizing.
Under 60 ℃; With farinaceous size and consumption is that the AMS of 12 enzyme activity units/g Semen Maydis powder mixed 60 minutes, obtains mixture, this mixture and 160 ℃ steam is sprayed contact (weight ratio of steam and mixture is 0.1: 1) in injector; The time of contact is 1 second; Make that the temperature with mixture after steam contacts is 98 ℃, and laminar flow kept 180 minutes, obtain liquefier one time.
An above-mentioned liquefier sprayed in injector with 160 ℃ steam once more contact (weight ratio of steam and mixture is 0.1: 1); The time of contact is 3 seconds; Making once more the temperature with mixture after steam contacts is 125 ℃, and under this temperature, keeps 5 minutes;
Carry out flash distillation (vacuum tightness is-0.09MPa, and the time is 10 seconds) with mixture after steam contacts once more and, be cooled to 99 ℃ above-mentioned, obtain liquefier to 103 ℃.
Under 99 ℃, be that the AMS of 12 enzyme activity units/g Semen Maydis powder mixed 100 minutes with this liquefier and consumption, obtain mixture.This mixture is carried out press filtration under 95 ℃, use chamber-type press filter, when pressure reaches 0.5MPa, stop charging, isolate enzymolysis solution and enzymolysis solid phase residue, liquid collecting is gone in the clear liquid jar.The DE value of measuring enzymolysis solution is as shown in table 1.
With the above-mentioned liquid glucose that obtains,, be heated to 85 ℃ of sterilizations as fermented liquid; Keep after 20 minutes fast cooling to 37 ℃, insert aspergillus niger strain, ferment; And the total reducing sugar in the detection fermented liquid; Inoculum size is: 4 * 105 colony-forming units of every gram fermented liquid inoculation, and at 40 ℃, 0.2 volume: cultivated fermentation ends 58 hours under the condition of the ventilation of (volume minute).Calculate the acidity and the transformation efficiency of the fermented liquid after fermenting, the result is as shown in table 1.
Comparative Examples 1
According to the method among the embodiment 2, different is only to carry out once enzyme-added; Concrete operations are following: 100 weight part corns are pulverized; Obtain average particle diameter and be 400 microns crushed products, with product and 180 weight parts waters after pulverizing, 60 ℃ of mixing down; Obtain farinaceous size, and the pH value of this farinaceous size is adjusted to 6.2.
Under 60 ℃; With farinaceous size and consumption is that the AMS of 24 enzyme activity units/g Semen Maydis powder mixed 30 minutes, obtains mixture, this mixture and 160 ℃ steam is sprayed contact (weight ratio of steam and mixture is 0.1: 1) in injector; The time of contact is 1 second; Make that the temperature with mixture after steam contacts is 98 ℃, and laminar flow kept 180 minutes, obtain liquefier one time.
An above-mentioned liquefier sprayed in injector with 160 ℃ steam once more contact (weight ratio of steam and mixture is 0.1: 1); The time of contact is 3 seconds; Making once more the temperature with mixture after steam contacts is 125 ℃, and under this temperature, keeps 5 minutes;
Carry out flash distillation (vacuum tightness is-0.09MPa, and the time is 10 seconds) with mixture after steam contacts once more and, be cooled to 99 ℃ above-mentioned, obtain liquefier to 103 ℃.This liquefier is carried out press filtration under 95 ℃, use chamber-type press filter, when pressure reaches 0.5MPa, stop charging, isolate enzymolysis solution and enzymolysis solid phase residue, liquid collecting is gone in the clear liquid jar.
The DE value of measuring enzymolysis solution is as shown in table 1.
With the above-mentioned liquid glucose that obtains,, be heated to 85 ℃ of sterilizations as fermented liquid; Keep after 20 minutes fast cooling to 37 ℃, insert aspergillus niger strain, ferment; And the total reducing sugar in the detection fermented liquid; Inoculum size is: 4 * 105 colony-forming units of every gram fermented liquid inoculation, and at 40 ℃, 0.2 volume: cultivated fermentation ends 70 hours under the condition of the ventilation of (volume minute).Calculate the acidity and the transformation efficiency of the fermented liquid after fermenting, the result is as shown in table 1.
Embodiment 3
100 weight part corns are pulverized, obtained average particle diameter and be 400 microns crushed products,,, obtain farinaceous size, and the pH value of this farinaceous size is adjusted to 5.6 50 ℃ of mixing down with product and 300 weight parts waters after pulverizing.
Under 50 ℃; With farinaceous size and consumption is that the AMS of 8 enzyme activity units/g Semen Maydis powder mixed 60 minutes, obtains mixture, this mixture and 100 ℃ steam is sprayed contact (weight ratio of steam and mixture is 0.08: 1) in injector; The time of contact is 3 seconds; Make that the temperature with mixture after steam contacts is 92 ℃, laminar flow was kept 150 minutes, obtained liquefier one time.
An above-mentioned liquefier sprayed in injector with 160 ℃ steam once more contact (weight ratio of steam and mixture is 0.08: 1); The time of contact is 2 seconds; Making once more the temperature with mixture after steam contacts is 130 ℃, and under this temperature, keeps 5 minutes;
Carry out flash distillation (vacuum tightness is-0.06MPa, and the time is 10 seconds) with mixture after steam contacts once more and, be cooled to 98 ℃ above-mentioned, obtain liquefier to 102 ℃.
Under 98 ℃, be that the AMS of 12 enzyme activity units/g Semen Maydis powder mixed 60 minutes with this liquefier and consumption, obtain mixture.This mixture is carried out press filtration under 95 ℃, use chamber-type press filter, when pressure reaches 0.5MPa, stop charging, isolate enzymolysis solution and enzymolysis solid phase residue, liquid collecting is gone in the clear liquid jar.The DE value of measuring enzymolysis solution is as shown in table 1.
With the above-mentioned liquid glucose that obtains,, be heated to 90 ℃ of sterilizations as fermented liquid; Keep after 15 minutes fast cooling to 38 ℃, insert aspergillus niger strain, ferment; And the total reducing sugar in the detection fermented liquid; Inoculum size is: 4 * 105 colony-forming units of every gram fermented liquid inoculation, and at 40 ℃, 0.2 volume: cultivated fermentation ends 50 hours under the condition of the ventilation of (volume minute).Calculate the acidity and the transformation efficiency of the fermented liquid after fermenting, the result is as shown in table 1.
Comparative Examples 2
According to the method among the embodiment 3, different is only once to spray; Being about to 100 weight part corns pulverizes; Obtain average particle diameter and be 400 microns crushed products, with product and 300 weight parts waters after pulverizing, 50 ℃ of mixing down; Obtain farinaceous size, and the pH value of this farinaceous size is adjusted to 5.6.
Under 50 ℃; With farinaceous size and consumption is that the AMS of 8 enzyme activity units/g Semen Maydis powder mixed 100 minutes, obtains mixture, this mixture and 158 ℃ steam is sprayed contact (weight ratio of steam and mixture is 0.08: 1) in injector; The time of contact is 3 seconds; Make that the temperature with mixture after steam contacts is 95 ℃, laminar flow was kept 180 minutes, obtained liquefier one time.
An above-mentioned liquefier is carried out flash distillation (vacuum tightness is-0.06MPa that the time is 10 seconds), be cooled to 98 ℃, obtain liquefier to 102 ℃.
This liquefier is carried out press filtration under 95 ℃, use chamber-type press filter, when pressure reaches 0.45MPa, stop charging, isolate enzymolysis solution and enzymolysis solid phase residue, liquid collecting is gone in the clear liquid jar.The DE value of measuring enzymolysis solution is as shown in table 1.
With the above-mentioned liquid glucose that obtains,, be heated to 90 ℃ of sterilizations as fermented liquid; Keep after 15 minutes fast cooling to 38 ℃, insert aspergillus niger strain, ferment; And the total reducing sugar in the detection fermented liquid; Inoculum size is: 4 * 105 colony-forming units of every gram fermented liquid inoculation, and at 40 ℃, 0.2 volume: cultivated fermentation ends 68 hours under the condition of the ventilation of (volume minute).Calculate the acidity and the transformation efficiency of the fermented liquid after fermenting, the result is as shown in table 1.
Embodiment 4
According to the method among the embodiment 1, different is, the pH value of farinaceous size is adjusted to 7.0; Fermented 62 hours.Measure the DE value of enzymolysis solution; Calculate the acidity and the transformation efficiency of the fermented liquid after fermenting, the result is as shown in table 1.
Table 1
Data from above embodiment and table 1 can find out that the starchy material that adopts method of the present invention to handle has guaranteed that the residual starch content in the enzymolysis solid phase residue is low, and the DE value of enzymolysis solution is low, thereby has shortened the time of follow-up fermentation.
Comparative Examples 1 adopts once enzyme-added, and it is higher to record the DE value, reach same fermentation level, and the time of fermentation is longer.
Comparative Examples 2 adopts secondary enzyme-added, once sprays, though the DE value descends than Comparative Examples 1 to some extent, residual starch content is higher in the enzymolysis solid phase residue.
Embodiment 4 is adjusted to 7.0 with the pH value of farinaceous size, though fermentation time also reduces to some extent, the minimizing amplitude is less; Embodiment 2 is adjusted to 6.2 with the pH value of farinaceous size, and it is bigger that fermentation time reduces amplitude, explains the pH value to be controlled in the preferable range of the present invention better effects if.
Claims (13)
1. the treatment process of a starchy material is characterized in that, this method comprises the steps:
(1) the starchy material powder is mixed with water obtains farinaceous size, farinaceous size is mixed with first part glycase, obtain mixture;
(2) mixture that obtains in the step (1) is once sprayed under 80-100 ℃ with first steam, obtain liquefier one time, again a liquefier is carried out second spraying with second steam under 120-150 ℃, obtain the secondary liquefier;
(3) the secondary liquefier that obtains in the step (2) is carried out flash distillation and cooling;
(4) under the amylorrhexis condition, the product after the flash distillation that step (3) is obtained and the cooling mixes with second section glycase, carries out enzymolysis.
2. method according to claim 1, wherein, in step (1), said starchy material powder and water blended condition comprise: temperature is 45-60 ℃, and the pH value is controlled at 5.5-6.2, the weight ratio of starchy material powder and water is 1: 1.8-4.
3. method according to claim 1, wherein, in step (1), farinaceous size and first part's glycase blended condition comprise: temperature is 45-60 ℃, and the time is 30-60 minute.
4. method according to claim 1, wherein, in step (4), said enzymatic hydrolysis condition comprises: hydrolysis temperature is 85-99 ℃, enzymolysis time is 60-150 minute.
5. method according to claim 1, wherein, with the dry weight basis of every gram starchy material powder, said diastatic total consumption is the 8-24 enzyme activity unit.
6. according to claim 1 or 5 described methods, wherein, the diastatic consumption of said first part is the 20-50 weight % of diastatic total consumption, and the diastatic consumption of said second section is the 50-80 weight % of diastatic total consumption.
7. method according to claim 1, wherein, the weight ratio of said first steam and mixture is 0.05-0.1: 1, the first steam and mixture duration of contact are 1-5 second, the contact temperature is 100-110 ℃; The weight ratio of said second steam and a liquefier is 0.05-0.1: 1, and be 1-3 second the duration of contact of a steam and a liquefier, the contact temperature is 130-140 ℃.
8. according to claim 1 or 7 described methods, wherein, once the timed interval of injection and second spraying is 120-180 minute.
9. method according to claim 1, wherein, the temperature of flash distillation is 100-103 ℃, and cooling is 5-10 ℃ after the flash distillation, and the pressure of flash distillation is-0.06～-0.09MPa.
10. according to claim 1 or 9 described methods, wherein, this method also comprises the steam that obtains after the flash distillation returned in the step (2) and is used as first steam; The water of condensation that obtains after the flash distillation returned in the step (1) be used to prepare farinaceous size.
11. according to any described method among the claim 1-10, wherein, said starchy material is selected from least a in corn, potato class, wheat and the Chinese sorghum.
12. the preparation method of a Hydrocerol A, this method comprise according to any described method among the claim 1-11 starchy material is handled, obtained enzymolysis product, and this enzymolysis product is fermented in the presence of black mold.
13. method according to claim 12, wherein, with said enzymolysis product as fermented liquid, 80-90 ℃ of down sterilization 15-30 minute, be cooled to 36-38 ℃ after, black mold is seeded in the fermented liquid, ferment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110220758 CN102321704B (en) | 2011-08-03 | 2011-08-03 | Method for treating starchy raw material and method for preparing citric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110220758 CN102321704B (en) | 2011-08-03 | 2011-08-03 | Method for treating starchy raw material and method for preparing citric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102321704A true CN102321704A (en) | 2012-01-18 |
| CN102321704B CN102321704B (en) | 2013-06-12 |
Family
ID=45449537
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110220758 Expired - Fee Related CN102321704B (en) | 2011-08-03 | 2011-08-03 | Method for treating starchy raw material and method for preparing citric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102321704B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102796787A (en) * | 2012-09-07 | 2012-11-28 | 吉林中粮生化科技有限公司 | Novel preparation method of corn starch sugar |
| CN102839203A (en) * | 2012-09-19 | 2012-12-26 | 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 |
| CN103146768A (en) * | 2013-03-28 | 2013-06-12 | 中粮生物化学（安徽）股份有限公司 | Method for preparing citric acid |
| CN103146763A (en) * | 2013-03-28 | 2013-06-12 | 中粮生物化学（安徽）股份有限公司 | Method for preparing ethanol |
| CN103146783A (en) * | 2013-03-28 | 2013-06-12 | 中粮生物化学（安徽）股份有限公司 | Pretreatment method of starchy material |
| CN105586368A (en) * | 2016-03-16 | 2016-05-18 | 江苏国信协联能源有限公司 | Treatment method of sorghum grains and method for fermentation production of citric acid |
| CN105838754A (en) * | 2016-04-25 | 2016-08-10 | 冠龙（泉州）食品有限公司 | Enzyme-process secondary-circulation jet liquefaction technique and liquefaction system |
| CN110184185A (en) * | 2019-05-10 | 2019-08-30 | 孟州市厚源生物科技有限公司 | The secondary liquefaction device and liquefaction process of starchy material production alcohol |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
-
2011
- 2011-08-03 CN CN 201110220758 patent/CN102321704B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
Non-Patent Citations (2)
| Title |
|---|
| 杨连生等: "酶法淀粉连续液化喷射技术的研究与开发", 《食品工业科技》, 30 April 1995 (1995-04-30), pages 3 - 10 * |
| 樊亚鸣等: "鲜沙姜淀粉的酶解过程及其产物的分析研究", 《食品科技》, no. 09, 30 September 2006 (2006-09-30), pages 118 - 122 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102796787A (en) * | 2012-09-07 | 2012-11-28 | 吉林中粮生化科技有限公司 | Novel preparation method of corn starch sugar |
| CN102839203A (en) * | 2012-09-19 | 2012-12-26 | 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 |
| 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 |
| CN103146768A (en) * | 2013-03-28 | 2013-06-12 | 中粮生物化学（安徽）股份有限公司 | Method for preparing citric acid |
| CN103146763A (en) * | 2013-03-28 | 2013-06-12 | 中粮生物化学（安徽）股份有限公司 | Method for preparing ethanol |
| CN103146783A (en) * | 2013-03-28 | 2013-06-12 | 中粮生物化学（安徽）股份有限公司 | Pretreatment method of starchy material |
| 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 |
| CN105586368A (en) * | 2016-03-16 | 2016-05-18 | 江苏国信协联能源有限公司 | Treatment method of sorghum grains and method for fermentation production of citric acid |
| CN105586368B (en) * | 2016-03-16 | 2019-05-10 | 江苏国信协联能源有限公司 | A kind of method of the processing method and fermentation production of citric acid of sorghum seed |
| CN105838754A (en) * | 2016-04-25 | 2016-08-10 | 冠龙（泉州）食品有限公司 | Enzyme-process secondary-circulation jet liquefaction technique and liquefaction system |
| CN110184185A (en) * | 2019-05-10 | 2019-08-30 | 孟州市厚源生物科技有限公司 | The secondary liquefaction device and liquefaction process of starchy material production alcohol |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102321704B (en) | 2013-06-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102321704B (en) | Method for treating starchy raw material and method for preparing citric acid | |
| Paz et al. | Enzymatic hydrolysis of brewer’s spent grain to obtain fermentable sugars | |
| Aiyer | Amylases and their applications | |
| Shen et al. | Succinic acid production from duckweed (Landoltia punctata) hydrolysate by batch fermentation of Actinobacillus succinogenes GXAS137 | |
| US20090117630A1 (en) | Fermentation product processes | |
| CN103146768B (en) | Method for preparing citric acid | |
| CN101939442A (en) | Ph adjustment free system for producing fermentable sugars and alcohol | |
| CN102234672A (en) | Enzymolysis method for starchy material and method for preparing citric acid | |
| CN104204216A (en) | Method for making high maltose syrup | |
| CN102321686A (en) | Processing method and application of starch raw material | |
| WO2015057517A1 (en) | Use of hemicellulases to improve ethanol production | |
| Power | Enzymatic conversion of starch to fermentable sugars | |
| CN103421851B (en) | A kind of method preparing sugar and ethanol with sweet potato waste | |
| Rojas et al. | Recovery of starch from cassava bagasse for cyclodextrin production by sequential treatment with α-amylase and cyclodextrin glycosyltransferase | |
| US11549133B2 (en) | Preparation method of amylodextrin | |
| CN103146783B (en) | Pretreatment method of starchy material | |
| US20150152458A1 (en) | Low temperature method for making high glucose syrup | |
| CN102373254B (en) | Enzymolysis method of starchy material and preparation method of citric acid | |
| CN105274168B (en) | A kind of processing method of starchy material | |
| CN102851325A (en) | Fermentation method for producing ethanol by using enzymatic saccharification of corn cob | |
| CN103146763B (en) | A kind of method preparing ethanol | |
| CN107400687A (en) | A kind of method of biology enzyme polymerization production oligoisomaltose | |
| EP3472334A1 (en) | Process and system for separation of a starch rich flow | |
| CN111662933B (en) | Method for performing high amylopectin alcohol fermentation by using recombinant yeast | |
| CN102839203B (en) | Enzymolysis method of starch raw material and method for preparing citric acid by fermenting |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130612 Termination date: 20200803 |