CN106191159B - A kind of rice prepares the production technology of starch syrup - Google Patents
A kind of rice prepares the production technology of starch syrup Download PDFInfo
- Publication number
- CN106191159B CN106191159B CN201610559076.7A CN201610559076A CN106191159B CN 106191159 B CN106191159 B CN 106191159B CN 201610559076 A CN201610559076 A CN 201610559076A CN 106191159 B CN106191159 B CN 106191159B
- Authority
- CN
- China
- Prior art keywords
- rice
- sugar
- value
- added
- liquid
- 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.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/02—Monosaccharides
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/04—Polysaccharides, i.e. compounds containing more than five saccharide radicals attached to each other by glycosidic bonds
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/16—Preparation of compounds containing saccharide radicals produced by the action of an alpha-1, 6-glucosidase, e.g. amylose, debranched amylopectin
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/22—Preparation of compounds containing saccharide radicals produced by the action of a beta-amylase, e.g. maltose
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P21/00—Preparation of peptides or proteins
- C12P21/06—Preparation of peptides or proteins produced by the hydrolysis of a peptide bond, e.g. hydrolysate products
Landscapes
- Organic Chemistry (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Wood Science & Technology (AREA)
- Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biotechnology (AREA)
- Biochemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- Microbiology (AREA)
- Genetics & Genomics (AREA)
- Molecular Biology (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Non-Alcoholic Beverages (AREA)
- Enzymes And Modification Thereof (AREA)
- Cereal-Derived Products (AREA)
Abstract
The invention discloses the production technologies that a kind of rice prepares starch syrup comprising following steps: 1) crushing, sizes mixing；2) it liquefies；3) streamline column heat preservation, separation of solid and liquid；4) rice protein nitrogen source is extracted；5) it is saccharified；6) it is filtered without solid waste；7) mixed bed purification, concentration.Technique of the invention reduces energy consumption during preparing starch syrup, through modulation high concentration starch slurry, controls water temperature of sizing mixing and shortens liquefying time；And residual sugar is recycled to the sugar-free grains generated in production process, organic nitrogen source is produced using fat in alkaline lipase hydrolysis sugar-free grains, then using protease hydrolytic rice sugar-free grains albumen, obtains the fermentation raw material of food, pharmaceutical purpose.Technique of the invention is significantly better than traditional rice and prepares starch syrup technique, and production cost is low, improves value-added content of product, and content of beary metal is far below traditional starch syrup product in product, and the solid waste generated is few, economic and environment-friendly.
Description
Technical field
The present invention relates to the production technologies that a kind of rice prepares starch syrup, belong to rice field of deep.
Background technique
Starch sugar is widely used in the food such as beverage, candy, cake, beer, easy to use, by vast food processing
The favor of enterprise.Starch sugar is with a long history in China, just on the books in Christian era more than 500 years Important Arts for the People's Welfare, and in detail
Ground describes the method refined sugar with rice.Starch sugar type is proportionately grouped as to divide and be broadly divided into glucose, maltose, fruit
Sugar, maltodextrin, oligosaccharide, sugar alcohol, glycoconjugate (alcohol) etc..
Currently, the manufacturing process of starch sugar is first to be saccharified to carry out sugar residue separation again mostly, protein in saccharifying,
The impurity such as fat itself react or generate in conjunction with carbohydrate more by-products, and the effect position with carbohydrate competition enzyme
Point reduces the production quantity of starch sugar.In addition, since the liquid glucose of traditional handicraft manufacture contains the impurity such as a large amount of protein, fat, it must
It must use the filter aids such as diatomite or perlite and active carbon that can filter by Sugarcane juice decolorization and smoothly, contain filter aid or work
Property charcoal sugar-free grains can not utilize again, can only as solid waste discharge, environment is adversely affected.
Paddy is the most important cereal crops of south China, and the rice yield in China occupies first place in the world.Rice has good
Amino acid composition and ratio, containing essential amino acid needed for organism, quality is better than wheat gluten and zein, and has low
Anaphylaxis and high nutritive value are to prepare one of desirable feedstock of starch sugar, have huge application prospect.Using rice as raw material
Production starch sugar and rice protein mostly use traditional handicraft, and soaking time is long, used device is more, conversion ratio is lower, and by environment
Factor is affected, and causes rice grinding particle size uneven, to influence product quality.
Summary of the invention
The purpose of the present invention is to provide the production technologies that a kind of rice prepares starch syrup.
The technical solution used in the present invention is:
A kind of rice prepares the production technology of starch syrup, comprising the following steps:
1) it crushes, size mixing: being cleaned, cleaned, milled to rice, add 54~57 DEG C of water, adjust pH value, obtain concentration
For 25~28 ° of B é, the rice slurries that pH value is 5.6~6.0；
2) it liquefies: alpha-amylase is added in rice slurries, stirs evenly, level-one is carried out at 98~105 DEG C and sprays liquid
Change, 30~50min is kept the temperature after flash distillation, then carry out two-stage injection liquefaction at 125~130 DEG C, obtains liquefier；
3) streamline column heat preservation, separation of solid and liquid: liquefier flashes stream plus alpha-amylase after decrease temperature and pressure, enters back into multistage laminar flow
Column, it is 60~90min that the laminar flow time is controlled at 95~100 DEG C, enters back into solid-liquid layering tank, dilute salt is added at 85~95 DEG C
Acid solution adjusts pH value to 5.8~6.4, stands 5~10min, adds dilute hydrochloric acid solution and adjust pH value to 4.6~5.6, stand
5~10min releases clear liquid from pot bottom is separated by solid-liquid separation, and sugar residue is retained by tank inner hole plate；
4) it extracts rice protein nitrogen source: the sugar residue of step 3) being added to 65~75 DEG C of hot water, is stirred evenly, filters pressing, it will
It is transferred to collecting tank after obtained sugar-free grains cleaning, temperature adjustment adjusts pH value to 7.5~8.5, alkaline fat is added to 55~65 DEG C
Enzyme hydrolyzes 20~40h, then adjusts pH value to 5.0~6.5 or to isoelectric points of proteins, is warming up to 90~95 DEG C, stirring is equal
Even, filtering obtains rice sugar-free grains albumen, and 55~60 DEG C of water are added in rice sugar-free grains albumen, are stirred evenly, and adjusts pH value to 2.0
~5.0, protease A is added, stirs sufficiently reaction, Cathepsin B is added in adjusting pH value to 9.0~10.5, sufficiently reaction is stirred,
Filtering, concentration, obtains rice protein nitrogen source；
5) be saccharified: regulating step 3) clear liquid pH value to 4.2~5.6, temperature adjustment is added carbohydrase, fills to 56~66 DEG C
Divide reaction, obtains saccharified liquid；
6) filtered without solid waste: adjusting the temperature of saccharified liquid to 75~85 DEG C, carry out microfiltration of ceramic membrane, respectively obtain clear liquid and
Slag inclusion concentrate is centrifuged slag inclusion concentrate, and the supernatant being centrifuged carries out microfiltration of ceramic membrane again, merges ceramic membrane
The stillness of night that micro-filtration obtains, the sugar-free grains being centrifuged carry out the extraction sugar-free grains albumen operation of step 4)；
7) mixed bed purification, concentration: introducing MVR evaporator for the clear liquid of step 6), carry out pre-concentration, then carries out mixed bed essence
System, concentration, obtain starch syrup.
The dosage of alpha-amylase described in step 2 and step 3) is the 0.01%~0.04% of rice quality.
The mass percentage of solid content is 35~40% in clear liquid described in step 3).
The dosage of alkaline lipase described in step 4) is the 0.001%~0.1% of sugar-free grains quality.
Protease A described in step 4) is at least one of Fungal Acid Protease, pepsin, the dosage of protease A
It is the 0.1%~1.0% of rice sugar-free grains albumen quality.
Cathepsin B described in step 4) is at least one of trypsase, chymotrypsin, and the dosage of Cathepsin B is rice
The 0.1%~1.0% of sugar-free grains albumen quality.
The weight percent of alpha-amido state nitrogen is 13.5%~15.0% in rice protein nitrogen source described in step 4).
Carbohydrase described in step 5) is barley beta-amylase, fungal amylase, glucoamylase, Pullulanase, fat
At least one of enzyme.
The dosage of carbohydrase described in step 5) is 0.001%~0.07% of the quality of giving money as a gift of the stillness of night in step 3).
The filtration pressure difference of microfiltration of ceramic membrane described in step 6) is 0.1MPa~0.5MPa, and cocnentration factor is 5~50.
The beneficial effects of the present invention are:
(1) the rice protein nitrogen source that the present invention produces can both be compounded with various starch syrups, and production different fermentations are special
Rice protein nitrogen source, can be also used for the production of the healthy food such as fermented product or rice protein powder by the nitrogen-containing starch syrup of property,
Improve the added value of rice converted products；
(2) concentration of sizing mixing is 25~28 ° of B é, improves the solid content of rice slurries to greatest extent, saves water and steaming
Vapour, and can be reduced the cost and energy consumption of subsequent drying, for producing 100000 tons of rice starch syrup per year, it can save water 135~
It 202 ton/days, saves and uses 26~39 ton/days of vapour；
(3) water temperature of sizing mixing is 54~57 DEG C, and maintains 54~56 DEG C of rice flour cream temperature, moistens rice starch granule sufficiently
It is swollen, be conducive to the decomposition of rice starch internal structure and the hydrolysis of enzyme preparation when injection liquefaction, hence it is evident that shorten liquefying time, reduce
Insoluble starch granules improves rice flour conversion ratio；
(4) using second level consecutive spraying fluidification and multistage streamline column heat preservation method, can make the liquefaction effect of rice flour more thoroughly,
Sufficiently, and in solid-liquid layering tank pH technology is adjusted using two stages, realization sugar residue is efficiently separated with the clear liquid that liquefies, improved
The yield of clear liquid；
(5) present invention extracts sugar-free grains after liquefaction, is conducive to utmostly extract rice sugar-free grains albumen, while utmostly
The influence to subsequent techniques such as saccharification such as protein, fat, ash content in sugar-free grains is reduced, transformation efficiency is improved, reduces filtering
Pressure；
(6) saccharified liquid passes through microfiltration of ceramic membrane system after purification, and slag inclusion concentrate is returned again with microfiltration of ceramic membrane system
Saccharic is received, sugar-free grains then further extracts rice protein, improves the yield of rice starch syrup and the comprehensive utilization ratio of byproduct；
(7) content of beary metal in rice starch syrup of the invention is low, 2 μ g/Kg of cadmium <, 2 μ g/Kg of arsenic <, 8 μ of lead <
G/Kg, far below traditional rice starch syrupy product；
(8) content of alpha-amido state nitrogen is 13.5~15.0wt.% in rice protein nitrogen source of the invention, and purity is much higher than
Similar product.
Detailed description of the invention
Fig. 1 is production technological process of the invention.
Specific embodiment
A kind of rice prepares the production technology of starch syrup, comprising the following steps:
1) it crushes, size mixing: being cleaned, cleaned, milled to rice, add 54~57 DEG C of water, adjust pH value, obtain concentration
For 25~28 ° of B é, the rice slurries that pH value is 5.6~6.0；
2) it liquefies: alpha-amylase is added in rice slurries, stirs evenly, level-one is carried out at 98~105 DEG C and sprays liquid
Change, 30~50min is kept the temperature after flash distillation, then carry out two-stage injection liquefaction at 125~130 DEG C, obtains liquefier；
3) streamline column heat preservation, separation of solid and liquid: liquefier flashes stream plus alpha-amylase after decrease temperature and pressure, enters back into multistage laminar flow
Column, it is 60~90min that the laminar flow time is controlled at 95~100 DEG C, enters back into solid-liquid layering tank, dilute salt is added at 85~95 DEG C
Acid solution adjusts pH value to 5.8~6.4, stands 5~10min, adds dilute hydrochloric acid solution and adjust pH value to 4.6~5.6, stand
5~10min releases clear liquid from pot bottom is separated by solid-liquid separation, and sugar residue is retained by tank inner hole plate；
4) it extracts rice protein nitrogen source: the sugar residue of step 3) being added to 65~75 DEG C of hot water, is stirred evenly, filters pressing, it will
It is transferred to collecting tank after obtained sugar-free grains cleaning, temperature adjustment adjusts pH value to 7.5~8.5, alkaline fat is added to 55~65 DEG C
Enzyme hydrolyzes 20~40h, then adjusts pH value to 5.0~6.5 or to isoelectric points of proteins, is warming up to 90~95 DEG C, stirring is equal
Even, filtering obtains rice sugar-free grains albumen, and 55~60 DEG C of water are added in rice sugar-free grains albumen, are stirred evenly, and adjusts pH value to 2.0
~5.0, protease A is added, stirs sufficiently reaction, Cathepsin B is added in adjusting pH value to 9.0~10.5, sufficiently reaction is stirred,
Filtering, concentration, obtains rice protein nitrogen source；
5) be saccharified: regulating step 3) clear liquid pH value to 4.2~5.6, temperature adjustment is added carbohydrase, fills to 56~66 DEG C
Divide reaction, obtains saccharified liquid；
6) filtered without solid waste: adjusting the temperature of saccharified liquid to 75~85 DEG C, carry out microfiltration of ceramic membrane, respectively obtain clear liquid and
Slag inclusion concentrate is centrifuged slag inclusion concentrate, and the supernatant being centrifuged carries out microfiltration of ceramic membrane again, merges ceramic membrane
The stillness of night that micro-filtration obtains, the sugar-free grains being centrifuged carry out the extraction sugar-free grains albumen operation of step 4)；
7) mixed bed purification, concentration: introducing MVR evaporator for the clear liquid of step 6), carry out pre-concentration, then carries out mixed bed essence
System, concentration, obtain starch syrup.
Preferably, the dosage of alpha-amylase described in step 2 and step 3) is the 0.01%~0.04% of rice quality.
Preferably, alpha-amylase described in step 2 and step 3) is Liquozyme Supra 2.2X, Liquozyme
One of Supra.
Preferably, the mass percentage of solid content is 35~40% in clear liquid described in step 3).
Preferably, multistage streamline column described in step 3) is the liquefaction column that concatenated 6~8 ratio of height to diameters are 8~10, under material
Into it is upper go out.
Preferably, the ratio of height to diameter of the layering of solid-liquid described in step 3) tank is 3~5, is internally provided with agitating device and perforated
From top to bottom successively decrease in the aperture of the orifice plate of 0.8~1.2mm of diameter, orifice plate.
Preferably, the dosage of alkaline lipase described in step 4) is the 0.001%~0.1% of sugar-free grains quality.
Preferably, protease A described in step 4) is at least one of Fungal Acid Protease, pepsin, protease A
Dosage be rice sugar-free grains albumen quality 0.1%~1.0%.
Preferably, Cathepsin B described in step 4) is at least one of trypsase, chymotrypsin, the dosage of Cathepsin B
It is the 0.1%~1.0% of rice sugar-free grains albumen quality.
Preferably, the weight percent of alpha-amido state nitrogen is 13.5%~15.0% in rice protein nitrogen source described in step 4).
Preferably, filters pressing described in step 4) carries out in diaphragm pressing filter press.
Preferably, carbohydrase described in step 5) is barley beta-amylase, fungal amylase, glucoamylase, Propiram
At least one of enzyme, lipase.
Preferably, the dosage of carbohydrase described in step 5) is 0.001%~0.07% of the quality of giving money as a gift of the stillness of night in step 3).
Preferably, the filtration pressure difference of microfiltration of ceramic membrane described in step 6) is 0.1MPa~0.5MPa, and cocnentration factor is 5~50.
The present invention will be further explained combined with specific embodiments below and explanation, and process flow chart of the invention is as schemed
Shown in 1.
Embodiment 1:
1) it crushes, size mixing: weighing the rice of 100 mass parts, be transported to after removal visible foreign and wash a meter tank, soaked in water,
It is passed through compressed air, makes grain of rice rolling, friction, rinses the impurity on grain of rice surface, release water in which rice has been washed after rinsing, is repeated once,
The grain of rice is cleaned, then mills and is slurried through roll-type crushing homogenizer, 54~55 DEG C of water are added, adjust pH value, obtaining concentration is 25
~26 ° of B é, the rice slurries that pH value is 5.6~5.7；
2) it liquefies: the Liquozyme Supra 2.2X alphalise starch for accounting for rice quality 0.03% being added in rice slurries
Enzyme stirs evenly, and level-one injection liquefaction is carried out at 100~102 DEG C, 30min is kept the temperature after flash distillation, then at 125~126 DEG C
Two-stage injection liquefaction is carried out, liquefier is obtained；
3) streamline column heat preservation, separation of solid and liquid: stream, which adds, after liquefier flash distillation decrease temperature and pressure accounts for rice quality 0.03%
Liquozyme Supra 2.2X alpha-amylase, enters back into multistage streamline column, and it is 80min that the laminar flow time is controlled at 100 DEG C,
Separation of solid and liquid tank is entered back into, dilute hydrochloric acid solution is added while stirring at 90~92 DEG C and adjusts pH value to 6.2~6.4, stops stirring
It mixes, stands 8min, then dilute hydrochloric acid solution is added while stirring and adjusts pH value to 4.6~4.8, stopping stirring standing 8min, will be clear
Saccharifying tank is released and imported to liquid from pot bottom is separated by solid-liquid separation, and sugar residue is retained by tank inner hole plate；
4) it extracts rice protein nitrogen source: the sugar residue of step 3) being added in 70~72 DEG C of hot water, stirred evenly, filters pressing,
Sugar-free grains is collected, collecting tank is transferred to after cleaning, temperature adjustment adjusts pH value to 7.5~7.6, addition is equivalent to sugar-free grains to 56~58 DEG C
Then the alkaline fat enzyme hydrolysis 30h of quality 0.003% adjusts pH value to 6.3~6.4, is warming up to 90 DEG C, stirs 20min, mistake
Filter obtains rice sugar-free grains albumen, and 5 times 58 DEG C of volume of water is then added, and adjusts pH value to 2.5~2.8, sugar-free grains albumen is added
The Fungal Acid Protease of 0.3% weight after being stirred to react 10h, adjusts pH value to 9.0~9.1, addition is equivalent to sugar-free grains quality
0.2% trypsase continues to be stirred to react 10h, and refined filtration, being concentrated in vacuo to concentration is 77wt.%, obtains food-grade rice protein
Nitrogen source, protein content 88.2wt.%, alpha-amido state nitrogen are 13.9wt.%；
5) it is saccharified: the clear liquid (solid content is 36~38wt.%) of step 3) is adjusted with the dilute hydrochloric acid solution of 4wt.%
PH value is added and is equivalent to liquid glucose and gives money as a gift the glucoamylase of quality 0.06% to 4.2~4.6, and 66 DEG C of saccharification obtain DE value and are
98 saccharified liquid；
6) it is filtered without solid waste: the saccharified liquid of step 5) being warming up to 75 DEG C, into microfiltration of ceramic membrane system, filtration pressure difference is
0.2MPa, cocnentration factor 50 obtain clear liquid and slag inclusion concentrate, the clear liquid reflux that slag inclusion concentrate is obtained by supercentrifuge
Into microfiltration of ceramic membrane system, merge the stillness of night that microfiltration of ceramic membrane obtains, the sugar-free grains being centrifuged then enters step the receipts in 4)
Collect tank；
7) mixed bed purification, concentration: the clear liquid that step 6) obtains passes through MVR evaporator pre-concentration to solid content and is
46wt.%, pre-concentration liquid carries out isomery conversion by fixed glucose isomerase column, then carries out mixed bed purification and concentration, obtains fruit
Glucose slurry.
Through detecting, content of beary metal is as follows in fructose syrup manufactured in the present embodiment: 2 μ g/Kg of cadmium <, and arsenic is 1.0 μ g/
Kg, lead are 2 μ g/Kg.
Embodiment 2:
1) it crushes, size mixing: weighing the rice of 100 mass parts, be transported to after removal visible foreign and wash a meter tank, soaked in water,
It is passed through compressed air, makes grain of rice rolling, friction, rinses the impurity on grain of rice surface, release water in which rice has been washed after rinsing, is repeated once,
The grain of rice is cleaned, then mills and is slurried through roll-type crushing homogenizer, 56~57 DEG C of water are added, adjust pH value, obtaining concentration is 27
~28 ° of B é, the rice slurries that pH value is 5.8~5.9；
2) it liquefies: the Liquozyme Supra alpha-amylase for accounting for rice quality 0.04%, stirring being added in rice slurries
Uniformly, level-one injection liquefaction is carried out at 104~105 DEG C, and 40min is kept the temperature after flash distillation, two are then carried out at 128~129 DEG C
Grade injection liquefaction, obtains liquefier；
3) streamline column heat preservation, separation of solid and liquid: stream, which adds, after liquefier flash distillation decrease temperature and pressure accounts for rice quality 0.01%
Liquozyme Supra alpha-amylase, enters back into multistage streamline column, and it is 90min that the laminar flow time is controlled at 95 DEG C, enters back into
It is separated by solid-liquid separation tank, dilute hydrochloric acid solution is added while stirring at 87~88 DEG C and adjusts pH value to 5.9~6.1, stops stirring, stands
5min, then addition dilute hydrochloric acid solution adjusts pH value to 4.9~5.2 while stirring, stops stirring, stands 5min, by clear liquid from admittedly
Liquid knockout drum bottom releases and imports saccharifying tank, and sugar residue is retained by tank inner hole plate；
4) it extracts rice protein nitrogen source: the sugar residue of step 3) being added in 67~68 DEG C of hot water, stirred evenly, filters pressing,
Sugar-free grains is collected, collecting tank is transferred to after cleaning, temperature adjustment adjusts pH value to 7.9~8.0, addition is equivalent to sugar-free grains to 60~62 DEG C
Then the alkaline fat enzyme hydrolysis 25h of quality 0.006% adjusts pH value to 6.0~6.1, is warming up to 92 DEG C, stirs 18min, mistake
Filter obtains rice sugar-free grains albumen, and 6 times 60 DEG C of volume of water is then added, and adjusts pH value to 4.9~5.0, sugar-free grains albumen is added
The pepsin of 0.5% weight after being stirred to react 10h, adjusts pH value to 10.0~10.1, addition is equivalent to sugar-free grains quality 0.4%
Chymotrypsin, continue to be stirred to react 12h, refined filtration, being concentrated in vacuo to concentration is 80wt.%, obtains food-grade rice protein nitrogen
Source, protein content 90.1wt.%, alpha-amido state nitrogen are 14.3wt.%；
5) it is saccharified: the clear liquid (solid content is 38~40wt.%) of step 3) is adjusted with the dilute hydrochloric acid solution of 5wt.%
PH value to 5.2~5.4, and add be equivalent to liquid glucose give money as a gift quality 0.01% glucoamylase, be equivalent to liquid glucose and give money as a gift quality
0.005% fungal amylase is equivalent to liquid glucose and gives money as a gift and 0.02% Pullulanase of quality and is equivalent to liquid glucose and gives money as a gift quality 0.002%
Acid lipase enzyme, 60 DEG C of cooperative saccharifications, saccharified liquid DE value is warming up to 83 DEG C when being 60, keeps the temperature 45min enzyme deactivation；
6) it is filtered without solid waste: the saccharified liquid of step 5) being warming up to 80 DEG C, into microfiltration of ceramic membrane system, filtration pressure difference is
0.5MPa, cocnentration factor 40 obtain clear liquid and slag inclusion concentrate, the clear liquid reflux that slag inclusion concentrate is obtained by supercentrifuge
Into microfiltration of ceramic membrane system, merge the stillness of night that microfiltration of ceramic membrane obtains, the sugar-free grains being centrifuged then enters step the receipts in 4)
Collect tank；
7) mixed bed purification, concentration: the clear liquid that step 6) obtains passes through MVR evaporator pre-concentration to solid content and is
55wt.%, pre-concentration liquid obtain glucose syrup by mixed bed purification, concentration.
Through detecting, content of beary metal is as follows in glucose syrup manufactured in the present embodiment: 2 μ g/Kg of cadmium <, and arsenic is 1.5 μ g/
Kg, lead are 5 μ g/Kg, and copper is 7.5 μ g/Kg.
Embodiment 3:
1) it crushes, size mixing: weighing the rice of 100 mass parts, be transported to after removal visible foreign and wash a meter tank, soaked in water,
It is passed through compressed air, makes grain of rice rolling, friction, rinses the impurity on grain of rice surface, release water in which rice has been washed after rinsing, is repeated once,
The grain of rice is cleaned, then mills and is slurried through roll-type crushing homogenizer, 55~56 DEG C of water are added, adjust pH value, obtaining concentration is 26
~27 ° of B é, the rice slurries that pH value is 5.7~5.8；
2) it liquefies: the Liquozyme Supra 2.2X alphalise starch for accounting for rice quality 0.02% being added in rice slurries
Enzyme stirs evenly, and level-one injection liquefaction is carried out at 99~100 DEG C, 50min is kept the temperature after flash distillation, then at 126~127 DEG C
Two-stage injection liquefaction is carried out, liquefier is obtained；
3) streamline column heat preservation, separation of solid and liquid: stream, which adds, after liquefier flash distillation decrease temperature and pressure accounts for rice quality 0.02%
Liquozyme Supra 2.2X alpha-amylase, enters back into multistage streamline column, and it is 70min that the laminar flow time is controlled at 98 DEG C, then
Into tank is separated by solid-liquid separation, dilute hydrochloric acid solution is added while stirring at 94~95 DEG C and adjusts pH value to 5.8~5.9, stops stirring,
10min is stood, then dilute hydrochloric acid solution is added while stirring and adjusts pH value to 4.5~4.6, stopping stirring standing 10min, will be clear
Saccharifying tank is released and imported to liquid from pot bottom is separated by solid-liquid separation, and sugar residue is retained by tank inner hole plate；
4) it extracts rice protein nitrogen source: the sugar residue of step 3) being added in 66~67 DEG C of hot water, stirred evenly, filters pressing,
Sugar-free grains is collected, collecting tank is transferred to after cleaning, temperature adjustment adjusts pH value to 7.7~7.8, addition is equivalent to sugar-free grains to 63~64 DEG C
Then the alkaline fat enzyme hydrolysis 20h of quality 0.009% adjusts pH value to 5.9~6.1, is warming up to 95 DEG C, stirs 25min, mistake
Filter obtains rice sugar-free grains albumen, and 7 times 56 DEG C of volume of water is then added, and adjusts pH value to 4.0~4.1, addition is equivalent to sugar-free grains
The Fungal Acid Protease of quality 0.2% and the pepsin for being equivalent to sugar-free grains quality 0.2% after being stirred to react 11h, adjust pH value
To 9.3~9.4, addition is equivalent to the trypsase of sugar-free grains quality 0.1% and is equivalent to the chymotrypsin of sugar-free grains quality 0.1%, after
Continuous to be stirred to react 11h, refined filtration, being concentrated in vacuo to concentration is 85wt.%, obtains food-grade rice protein nitrogen source, protein content is
83.5wt.%, alpha-amido state nitrogen are 14.8wt.%；
5) it is saccharified: the clear liquid (solid content is 35~37wt.%) of step 3) is adjusted with the dilute hydrochloric acid solution of 5wt.%
PH value to 5.2~5.4, and add be equivalent to liquid glucose give money as a gift quality 0.01% barley beta-amylase and be equivalent to liquid glucose and give money as a gift matter
Amount 0.002% Pullulanase, in 62 DEG C of cooperative saccharification 6h, add be equivalent to liquid glucose give money as a gift quality 0.002% glucose form sediment
Powder enzyme continues to be saccharified, and saccharified liquid DE value is warming up to 84 DEG C of enzyme deactivations when being 53, keeps the temperature 1h enzyme deactivation；
6) it is filtered without solid waste: the saccharified liquid of step 5) being warming up to 85 DEG C, into microfiltration of ceramic membrane system, filtration pressure difference is
0.4MPa, cocnentration factor 30 obtain clear liquid and slag inclusion concentrate, the clear liquid reflux that slag inclusion concentrate is obtained by supercentrifuge
Into microfiltration of ceramic membrane system, merge the stillness of night that microfiltration of ceramic membrane obtains, the sugar-free grains being centrifuged then enters step the receipts in 4)
Collect tank；
7) mixed bed purification, concentration: the clear liquid that step 6) obtains passes through MVR evaporator pre-concentration to solid content and is
50wt.%, pre-concentration liquid obtain malt syrup by mixed bed purification, concentration.
Through detecting, content of beary metal is as follows in malt syrup manufactured in the present embodiment: 2 μ g/Kg of cadmium <, and arsenic is 1.7 μ g/
Kg, lead are 6 μ g/Kg.
The above embodiment is a preferred embodiment of the present invention, but embodiments of the present invention are not by above-described embodiment
Limitation, other any changes, modifications, substitutions, combinations, simplifications made without departing from the spirit and principles of the present invention,
It should be equivalent substitute mode, be included within the scope of the present invention.
Claims (8)
1. the production technology that a kind of rice prepares starch syrup, it is characterised in that: the following steps are included:
1) it crushes, size mixing: being cleaned, cleaned, milled to rice, add 54~57 DEG C of water, adjust pH value, obtaining concentration is 25
~28 ° of B é, the rice slurries that pH value is 5.6~6.0；
2) it liquefies: alpha-amylase is added in rice slurries, stirs evenly, level-one injection liquefaction is carried out at 98~105 DEG C, is dodged
30~50min is kept the temperature after steaming, then carries out two-stage injection liquefaction at 125~130 DEG C, obtains liquefier；
3) streamline column heat preservation, separation of solid and liquid: liquefier flashes stream plus alpha-amylase after decrease temperature and pressure, enters back into multistage streamline column,
It is 60~90min that the laminar flow time is controlled at 95~100 DEG C, enters back into solid-liquid layering tank, dilute hydrochloric acid is added at 85~95 DEG C
Solution adjusts pH value to 5.8~6.4, stands 5~10min, adds dilute hydrochloric acid solution and adjust pH value to 4.6~5.6, stand 5
~10min releases clear liquid from pot bottom is separated by solid-liquid separation, and sugar residue is retained by tank inner hole plate；
4) it extracts rice protein nitrogen source: the sugar residue of step 3) being added to 65~75 DEG C of hot water, stirs evenly, filters pressing, will obtain
Sugar-free grains cleaning after be transferred to collecting tank, temperature adjustment adjusts pH value to 7.5~8.5, alkaline lipase, water is added to 55~65 DEG C
20~40h is solved, pH value is then adjusted to 5.0~6.5 or to isoelectric points of proteins, is warming up to 90~95 DEG C, stirs evenly, mistake
Filter, obtains rice sugar-free grains albumen, and 55~60 DEG C of water are added in rice sugar-free grains albumen, are stirred evenly, adjusting pH value to 2.0~5.0,
Protease A is added, stirs sufficiently reaction, adjusts pH value to 9.0~10.5, Cathepsin B is added, stirs sufficiently reaction, filtering is dense
Contracting, obtains rice protein nitrogen source；
5) be saccharified: regulating step 3) clear liquid pH value to 4.2~5.6, carbohydrase is added to 56~66 DEG C in temperature adjustment, sufficiently anti-
It answers, obtains saccharified liquid；
6) it is filtered without solid waste: adjusting the temperature of saccharified liquid to 75~85 DEG C, carry out microfiltration of ceramic membrane, respectively obtain clear liquid and slag inclusion
Concentrate is centrifuged slag inclusion concentrate, and the supernatant being centrifuged carries out microfiltration of ceramic membrane again, merges microfiltration of ceramic membrane
Obtained clear liquid, the sugar-free grains being centrifuged carry out the extraction sugar-free grains albumen operation of step 4)；
7) mixed bed purification, concentration: introducing MVR evaporator for the clear liquid of step 6), carry out pre-concentration, then carries out mixed bed purification, dense
Contracting, obtains starch syrup；
Step 4) the protease A is at least one of Fungal Acid Protease, pepsin, and the dosage of protease A is big
The 0.1%~1.0% of rice sugar-free grains albumen quality；
Step 4) the Cathepsin B is at least one of trypsase, chymotrypsin, and the dosage of Cathepsin B is rice sugar-free grains
The 0.1%~1.0% of albumen quality.
2. production technology according to claim 1, it is characterised in that: the dosage of step 2) and the step 3) alpha-amylase
It is the 0.01%~0.04% of rice quality.
3. production technology according to claim 1, it is characterised in that: the quality percentage of solid content in the step 3) clear liquid
Content is 35~40%.
4. production technology according to claim 1, it is characterised in that: the dosage of the step 4) alkaline lipase is sugar-free grains
The 0.001%~0.1% of quality.
5. production technology according to claim 1, it is characterised in that: alpha-amido state in step 4) the rice protein nitrogen source
The weight percent of nitrogen is 13.5%~15.0%.
6. production technology according to claim 1, it is characterised in that: the step 5) carbohydrase be barley beta-amylase,
At least one of fungal amylase, glucoamylase, Pullulanase, lipase.
7. production technology according to claim 1 or 6, it is characterised in that: the dosage of the step 5) carbohydrase is step
3) clear liquid is given money as a gift the 0.001%~0.07% of quality in.
8. production technology according to claim 1, it is characterised in that: the filtration pressure difference of the step 6) microfiltration of ceramic membrane is
0.1MPa~0.5MPa, cocnentration factor are 5~50.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610559076.7A CN106191159B (en) | 2016-07-15 | 2016-07-15 | A kind of rice prepares the production technology of starch syrup |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610559076.7A CN106191159B (en) | 2016-07-15 | 2016-07-15 | A kind of rice prepares the production technology of starch syrup |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106191159A CN106191159A (en) | 2016-12-07 |
| CN106191159B true CN106191159B (en) | 2019-08-06 |
Family
ID=57474646
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610559076.7A Active CN106191159B (en) | 2016-07-15 | 2016-07-15 | A kind of rice prepares the production technology of starch syrup |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106191159B (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107475322A (en) * | 2017-07-25 | 2017-12-15 | 安徽万德生物科技有限公司 | A kind of technique for preparing fructose syrup |
| CN107287262A (en) * | 2017-07-25 | 2017-10-24 | 安徽万德生物科技有限公司 | A kind of preparation technology of starch syrup |
| CN108251471A (en) * | 2017-12-09 | 2018-07-06 | 吉林中粮生化有限公司 | A kind of method of paddy sugaring |
| CN107964554A (en) * | 2018-01-22 | 2018-04-27 | 武汉中粮食品科技有限公司 | A kind of amylolytic method |
| CN108796010A (en) * | 2018-05-26 | 2018-11-13 | 双桥（厦门）有限公司 | Starch syrup processing method |
| CN110343190A (en) * | 2019-08-21 | 2019-10-18 | 福建农林大学 | A kind of synchronous method for extracting hericium erinaceum polysaccharide and protein |
| CN110540330B (en) * | 2019-09-23 | 2021-06-22 | 南京钛净流体技术有限公司 | Membrane integrated rice washing water recycling device and recycling method |
| CN110819671B (en) * | 2019-11-05 | 2023-09-22 | 山东香驰健源生物科技有限公司 | Maltodextrin and its production process and application |
| CN110885867A (en) * | 2019-12-04 | 2020-03-17 | 双桥（厦门）有限公司 | Production process of corn starch syrup |
| CN112501226A (en) * | 2020-11-27 | 2021-03-16 | 广州双桥（重庆）有限公司 | Preparation method of syrup for medical lovastatin |
| CN113481259B (en) * | 2021-07-13 | 2023-06-13 | 山东省科学院菏泽分院 | Method for extracting starch syrup and rice protein isolate by using broken rice |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101536741A (en) * | 2008-12-23 | 2009-09-23 | 广州双桥股份有限公司 | Method for preparing protein nitrogen source applicable to fermentation and food by rice |
| CN101565762A (en) * | 2009-05-25 | 2009-10-28 | 安徽汇佳生物科技有限公司 | Production process for starch sugar |
| CN101695334A (en) * | 2009-09-09 | 2010-04-21 | 万福生科(湖南)农业开发股份有限公司 | Method for extracting rice protein 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 |
| CN102337316A (en) * | 2011-09-30 | 2012-02-01 | 广州双桥股份有限公司 | Process for producing starch sugar |
| CN103060402A (en) * | 2013-01-07 | 2013-04-24 | 安徽友勇生物科技有限公司 | Production method of starch syrup |
-
2016
- 2016-07-15 CN CN201610559076.7A patent/CN106191159B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101536741A (en) * | 2008-12-23 | 2009-09-23 | 广州双桥股份有限公司 | Method for preparing protein nitrogen source applicable to fermentation and food by rice |
| CN101565762A (en) * | 2009-05-25 | 2009-10-28 | 安徽汇佳生物科技有限公司 | Production process for starch sugar |
| CN101695334A (en) * | 2009-09-09 | 2010-04-21 | 万福生科(湖南)农业开发股份有限公司 | Method for extracting rice protein 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 |
| CN102337316A (en) * | 2011-09-30 | 2012-02-01 | 广州双桥股份有限公司 | Process for producing starch sugar |
| CN103060402A (en) * | 2013-01-07 | 2013-04-24 | 安徽友勇生物科技有限公司 | Production method of starch syrup |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106191159A (en) | 2016-12-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106191159B (en) | A kind of rice prepares the production technology of starch syrup | |
| CN107156563B (en) | Preparation process of decolorized concentrated juice of fresh momordica grosvenori | |
| SU1086012A1 (en) | Method for producing concentrate of kvass wort | |
| CN101536741B (en) | Method for preparing protein nitrogen source applicable to fermentation and food by rice | |
| CN106755204B (en) | Method for efficiently co-producing malt syrup and rice protein from rice processing byproducts | |
| CN102965284A (en) | Dual-purpose preparation process and equipment for maltodextrin and oligomerization isomaltose | |
| CN1330251C (en) | Method for extracting rice protein from rice | |
| CN105685936A (en) | Method for preparing malt fragrance-flavour matter by utilizing self protein of wheat bran and sugar | |
| CN103146782B (en) | Method for preparing glucose syrup by using rice bran as raw material | |
| CN113025672B (en) | Preparation method of high-purity fructose syrup | |
| CN101133785A (en) | Method for producing concentrated barley juice | |
| CN105623938B (en) | Highland barley fine brewing beer saccharification process | |
| CN103911409A (en) | Preparation method of malt syrup | |
| CN100532396C (en) | Process for preparing high purity pectin by using apple pomace | |
| CN106118933B (en) | Jerusalem artichoke beer brewing process | |
| CN105482933B (en) | A kind of preparation method of high-attenuation degree beer syrup | |
| AU2017365642B2 (en) | Method of preparing cereal extract | |
| CN102747118B (en) | Method for directly producing feeding isomaltooligosaccharide syrup by using wheat | |
| CN100532575C (en) | Processing process for producing cerealose using corn as raw material | |
| CN105218622A (en) | The method of rice cold induced proteins powder and β-amylose is prepared in a kind of coproduction of cracking rice | |
| CN1281154C (en) | Preparation method of wheat hydrolyzed malt extract | |
| CN101683107A (en) | Method for manufacturing potato cerealose | |
| CN103300433A (en) | Processing method of lotus nut buffing powder | |
| CN101899371B (en) | Jujube beer | |
| CN101724523A (en) | Method for preparing beer syrup |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A production process for preparing starch syrup from rice Effective date of registration: 20230828 Granted publication date: 20190806 Pledgee: Hankou Bank Co.,Ltd. Xiaogan Branch Pledgor: SHUANGQIAO (HUBEI) Co.,Ltd. Registration number: Y2023980054020 |