CN106191159A - The production technology of starch syrup prepared by a kind of rice - Google Patents
The production technology of starch syrup prepared by a kind of rice Download PDFInfo
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Abstract
The invention discloses a kind of rice and prepare the production technology of starch syrup, it comprises the following steps: 1) pulverizes, size mixing；2) liquefaction；3) streamline column insulation, solid-liquid separation；4) rice protein nitrogen source is extracted；5) saccharifying；6) filter without solid waste；7) mixed bed refines, concentrates.The technique of the present invention, during preparing starch syrup, reduces energy consumption by modulation high concentration starch slurry, controls water temperature shortening liquefying time of sizing mixing；And the sugar grain produced in production process is reclaimed residual sugar, use fat in alkaline lipase hydrolysis sugar grain, then use protease hydrolysis rice candy Egg preserved in wine to produce organic nitrogen source in vain, obtain the fermentation raw material of food, pharmaceutical purpose.The technique of the present invention is significantly better than traditional rice and prepares starch syrup technique, and production cost is low, improves value-added content of product, and in product, content of beary metal is far below traditional starch syrup product, and the solid waste produced is few, economic and environment-friendly.
Description
Technical field
The present invention relates to a kind of rice and prepare the production technology of starch syrup, belong to rice field of deep.
Background technology
Starch sugar is widely used in the food such as beverage, confection, cake, medicated beer, easy to use, by vast food processing
The favor of enterprise.Starch sugar is with a long history in China, the most on the books in the Important Arts for the People's Welfare in more than 500 year Christian era, and in detail
Describe with rice sugaring method.Starch sugar kind is proportionately grouped into and point is broadly divided into glucose, maltose, really
Sugar, maltodextrin, oligosaccharide, sugar alcohol, glycoconjugates (alcohol) etc..
At present, the manufacturing process of starch sugar is first to carry out saccharifying to carry out sugar slag again and separate mostly, protein in saccharifying,
The impurity self such as fat react or are combined with saccharide and produce more by-product, and compete the effect position of enzyme with saccharide
Point, reduces the growing amount of starch sugar.Further, since the sugar liquid of traditional handicraft manufacture contains the impurity such as a large amount of protein, fat, must
The filter aid such as kieselguhr or perlite and activated carbon must be used can to filter by Sugarcane juice decolorization and smoothly, containing filter aid or work
Property charcoal sugared grain cannot be again with, discharge only as solid waste, environment adversely affected.
Oryza glutinosa is the most important cereal crops of south China, and the rice yield of China occupies first place in the world.Rice has well
Aminoacid composition and ratio, containing the essential amino acids needed for organism, quality is better than wheat protein and zein, and has low
Anaphylaxis and high nutritive value, be one of desirable feedstock preparing starch sugar, have huge application prospect.With rice as raw material
Producing starch sugar and rice protein many employings traditional handicraft, soak time length, used device are many, conversion ratio is relatively low, and by environment
Factor impact is relatively big, causes rice grinding particle size uneven, thus affects product quality.
Summary of the invention
It is an object of the invention to provide a kind of rice and prepare the production technology of starch syrup.
The technical solution used in the present invention is:
The production technology of starch syrup prepared by a kind of rice, comprises the following steps:
1) pulverizing, size mixing: rice carries out remove impurity, cleans, mill, add 54～the water of 57 DEG C, regulate pH value, obtaining concentration is 25
～28 ° of B é, pH value is the rice serosity of 5.6～6.0；
2) liquefaction: add α-amylase in rice serosity, stir, carries out one-level injection liquefaction at 98～105 DEG C, dodges
It is incubated 30～50min after steaming, then at 125～130 DEG C, carries out two-stage injection liquefaction, obtain liquefier；
3) streamline column insulation, solid-liquid separation: after liquefier flash distillation decrease temperature and pressure, stream adds α-amylase, enters back into multistage streamline column,
At 95～100 DEG C, the control laminar flow time is 60～90min, enters back into solid-liquid layering tank, adds dilute hydrochloric acid at 85～95 DEG C
Solution regulation pH value to 5.8～6.4, stand 5～10min, add dilute hydrochloric acid solution regulation pH value to 4.6～5.6, stand 5
～10min, clear liquid to be released from solid-liquid separation pot bottom, sugar slag is retained by tank inner hole plate；
4) rice protein nitrogen source is extracted: the sugared slag of step 3) is added the hot water of 65～75 DEG C, stirs, filter pressing, will obtain
Sugar grain clean after be transferred to collecting tank, homoiothermic to 55～65 DEG C, regulation pH value to 7.5～8.5, add alkaline lipase, water
Solving 20～40h, then regulation pH value is to 5.0～6.5 or to isoelectric points of proteins, is warming up to 90～95 DEG C, stirs, mistake
Filter, obtains rice candy Egg preserved in wine white, adds 55～60 DEG C of water, stir in rice candy Egg preserved in wine is white, regulation pH value to 2.0～5.0,
Add protease A, stirring fully reaction, regulation pH value, to 9.0～10.5, adds Cathepsin B, and stirring fully reaction is filtered,
Concentrate, obtain rice protein nitrogen source；
5) saccharifying: regulating step 3) the pH value of clear liquid to 4.2～5.6, homoiothermic to 56～66 DEG C, add saccharifying enzyme, the most instead
Should, obtain saccharified liquid；
6) filter without solid waste: the temperature of regulation saccharified liquid, to 75～85 DEG C, carries out microfiltration of ceramic membrane, respectively obtains clear liquid and slag inclusion
Concentrated solution, is centrifuged slag inclusion concentrated solution, and the centrifugal supernatant obtained carries out microfiltration of ceramic membrane again, merges microfiltration of ceramic membrane
The stillness of night obtained, the extraction sugar Egg preserved in wine that the centrifugal sugared grain obtained carries out step 4) operates in vain；
7) mixed bed refines, concentrates: the clear liquid of step 6) is introduced MVR vaporizer, carries out pre-concentration, then it is refined, dense to carry out mixed bed
Contracting, obtains starch syrup.
Step 2) and step 3) described in α-amylase consumption is rice quality 0.01%～0.04%.
In clear liquid described in step 3), the weight/mass percentage composition of solid content is 35～40%.
The consumption of alkaline lipase described in step 4) is the 0.001%～0.1% of sugar grain quality.
Protease A described in step 4) is at least one in Fungal Acid Protease, pepsin, the consumption of protease A
For rice candy grain albumen quality 0.1%～1.0%.
Cathepsin B described in step 4) is at least one in trypsin, Chymotrypsin, and the consumption of Cathepsin B is rice
The 0.1%～1.0% of sugar grain albumen quality.
In rice protein nitrogen source described in step 4), the percentage by weight of alpha-amido state nitrogen is 13.5%～15.0%.
Saccharifying enzyme described in step 5) is barley beta-amylase, fungal amylase, glucoamylase, pullulanase, fat
At least one in enzyme.
The consumption of saccharifying enzyme described in step 5) is in step 3) the 0.001%～0.07% of the quality of giving money as a gift of the stillness of night.
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 invention has the beneficial effects as follows:
(1) the rice protein nitrogen source that the present invention produces both can compound with various starch syrups, produces different fermentations characteristic
Nitrogen-containing starch syrup, also can be used for the production of the health food such as fermented product or rice protein powder by rice protein nitrogen source, improves
The added value of rice converted products；
(2) concentration of sizing mixing is 25～28 ° of B é, improves the solid content of rice serosity to greatest extent, saves water and steam, and
Follow-up dry cost and energy consumption can be reduced, as a example by producing 100000 tons of rice starch syrup per year, can using water wisely 135～202 tons/
My god, economize on vapour 26～39 ton day；
(3) water temperature of sizing mixing is 54～57 DEG C, and maintains rice flour breast temperature 54～56 DEG C, makes the abundant swollen of rice starch granule, has
Be beneficial to the decomposition of rice starch internal structure and the hydrolysis of enzyme preparation during injection liquefaction, hence it is evident that shorten liquefying time, reduce insoluble
Starch granules, improves rice flour conversion ratio；
(4) use two grades of consecutive spraying fluidifications and multistage streamline column heat preservation method, can make the liquefaction effect of rice flour more thoroughly, fill
Point, and in solid-liquid layering tank, using two benches regulation pH technology, it is achieved sugar slag efficiently separates with liquefaction clear liquid, improves clear
The yield of liquid；
(5) present invention extracts sugar grain after liquefaction, is conducive at utmost extracting rice candy Egg preserved in wine white, at utmost reduces simultaneously
Protein in sugar grain, fat, ash grade the impact on subsequent techniques such as saccharifying, improve transformation efficiency, reduce filter pressure；
(6) saccharified liquid is through microfiltration of ceramic membrane system after purification, and slag inclusion concentrated solution microfiltration of ceramic membrane system reclaims sugar again
Matter, sugar grain is extracted rice protein the most further, is improve the yield of rice starch syrup and the comprehensive utilization ratio of side-product；
(7) content of beary metal in the rice starch syrup of the present invention is low, cadmium ＜ 2 μ g/Kg, arsenic ＜ 2 μ g/Kg, lead ＜ 8 μ g/Kg,
Far below traditional rice starch syrupy product；
(8) in the rice protein nitrogen source of the present invention, the content of alpha-amido state nitrogen is 13.5～15.0wt.%, and purity is far above similar
Product.
Accompanying drawing explanation
Fig. 1 is the production technological process of the present invention.
Detailed description of the invention
The production technology of starch syrup prepared by a kind of rice, comprises the following steps:
1) pulverizing, size mixing: rice carries out remove impurity, cleans, mill, add 54～the water of 57 DEG C, regulate pH value, obtaining concentration is 25
～28 ° of B é, pH value is the rice serosity of 5.6～6.0；
2) liquefaction: add α-amylase in rice serosity, stir, carries out one-level injection liquefaction at 98～105 DEG C, dodges
It is incubated 30～50min after steaming, then at 125～130 DEG C, carries out two-stage injection liquefaction, obtain liquefier；
3) streamline column insulation, solid-liquid separation: after liquefier flash distillation decrease temperature and pressure, stream adds α-amylase, enters back into multistage streamline column,
At 95～100 DEG C, the control laminar flow time is 60～90min, enters back into solid-liquid layering tank, adds dilute hydrochloric acid at 85～95 DEG C
Solution regulation pH value to 5.8～6.4, stand 5～10min, add dilute hydrochloric acid solution regulation pH value to 4.6～5.6, stand 5
～10min, clear liquid to be released from solid-liquid separation pot bottom, sugar slag is retained by tank inner hole plate；
4) rice protein nitrogen source is extracted: the sugared slag of step 3) is added the hot water of 65～75 DEG C, stirs, filter pressing, will obtain
Sugar grain clean after be transferred to collecting tank, homoiothermic to 55～65 DEG C, regulation pH value to 7.5～8.5, add alkaline lipase, water
Solving 20～40h, then regulation pH value is to 5.0～6.5 or to isoelectric points of proteins, is warming up to 90～95 DEG C, stirs, mistake
Filter, obtains rice candy Egg preserved in wine white, adds 55～60 DEG C of water, stir in rice candy Egg preserved in wine is white, regulation pH value to 2.0～5.0,
Add protease A, stirring fully reaction, regulation pH value, to 9.0～10.5, adds Cathepsin B, and stirring fully reaction is filtered,
Concentrate, obtain rice protein nitrogen source；
5) saccharifying: regulating step 3) the pH value of clear liquid to 4.2～5.6, homoiothermic to 56～66 DEG C, add saccharifying enzyme, the most instead
Should, obtain saccharified liquid；
6) filter without solid waste: the temperature of regulation saccharified liquid, to 75～85 DEG C, carries out microfiltration of ceramic membrane, respectively obtains clear liquid and slag inclusion
Concentrated solution, is centrifuged slag inclusion concentrated solution, and the centrifugal supernatant obtained carries out microfiltration of ceramic membrane again, merges microfiltration of ceramic membrane
The stillness of night obtained, the extraction sugar Egg preserved in wine that the centrifugal sugared grain obtained carries out step 4) operates in vain；
7) mixed bed refines, concentrates: the clear liquid of step 6) is introduced MVR vaporizer, carries out pre-concentration, then it is refined, dense to carry out mixed bed
Contracting, obtains starch syrup.
Preferably, step 2) and step 3) described in α-amylase consumption is rice quality 0.01%～0.04%.
Preferably, step 2) and step 3) described in α-amylase be Liquozyme Supra 2.2X, Liquozyme
One in Supra.
Preferably, in clear liquid described in step 3), the weight/mass percentage composition of solid content is 35～40%.
Preferably, multistage streamline column described in step 3) is the liquefaction post that 6～8 ratio of height to diameters are 8～10 of series connection, under material
Go out on entering.
Preferably, described in step 3), the ratio of height to diameter of solid-liquid layering tank is 3～5, is internally provided with agitating device and perforated
The orifice plate in footpath 0.8～1.2mm, from top to bottom successively decreases in the aperture of orifice plate.
Preferably, the consumption of alkaline lipase described in step 4) is the 0.001%～0.1% of sugar grain quality.
Preferably, protease A described in step 4) is at least one in Fungal Acid Protease, pepsin, protease A
Consumption is rice candy grain albumen quality 0.1%～1.0%.
Preferably, Cathepsin B described in step 4) is at least one in trypsin, Chymotrypsin, the consumption of Cathepsin B
For rice candy grain albumen quality 0.1%～1.0%.
Preferably, in rice protein nitrogen source described in step 4), the percentage by weight of alpha-amido state nitrogen is 13.5%～15.0%.
Preferably, filter pressing described in step 4) is carried out in diaphragm pressing pressure filter.
Preferably, saccharifying enzyme described in step 5) is barley beta-amylase, fungal amylase, glucoamylase, Pullulan
At least one in enzyme, lipase.
Preferably, during the consumption of saccharifying enzyme described in step 5) is step 3) the 0.001%～0.07% of the quality of giving money as a gift of the stillness of night.
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.
Below in conjunction with specific embodiment, the present invention is made further explanation and description, the process chart of the present invention such as figure
Shown in 1.
Embodiment 1:
1) pulverize, size mixing: weigh the rice of 100 mass parts, be transported to wash a meter tank after removing visible foreign, soak, be passed through
Compressed air, makes grain of rice rolling, friction, the impurity on rinsing grain of rice surface, releases rice-washed water, repeat once, by rice after rinsing
Grain is cleaned, and then pulverizes homogenizer through roll-type and mills pulping, adds 54～55 DEG C of water, and regulation pH value, obtaining concentration is 25～26 °
B é, pH value is the rice serosity of 5.6～5.7；
2) liquefaction: add the Liquozyme Supra 2.2X α-amylase accounting for rice quality 0.03% in rice serosity, stir
Mix uniformly, at 100～102 DEG C, carry out one-level injection liquefaction, be incubated 30min after flash distillation, then carry out at 125～126 DEG C
Two-stage injection is liquefied, and obtains liquefier；
3) streamline column insulation, solid-liquid separation: after liquefier flash distillation decrease temperature and pressure, stream adds the Liquozyme accounting for rice quality 0.03%
Supra 2.2X α-amylase, enters back into multistage streamline column, and at 100 DEG C, the control laminar flow time is 80min, enters back into solid-liquid
Knockout drum, add while stirring at 90～92 DEG C dilute hydrochloric acid solution regulation pH value to 6.2～6.4, stop stirring, stand
8min, then addition dilute hydrochloric acid solution regulation pH value, to 4.6～4.8, stops stirring, stands 8min while stirring, by clear liquid from admittedly
Releasing and import saccharifying tank bottom liquid knockout drum, sugar slag is retained by tank inner hole plate；
4) rice protein nitrogen source is extracted: added by the sugared slag of step 3) in the hot water of 70～72 DEG C, stir, filter pressing, collect
Sugar grain, is transferred to collecting tank after cleaning, homoiothermic to 56～58 DEG C, and regulation pH value, to 7.5～7.6, adds and is equivalent to sugar grain quality
The alkaline fat enzyme hydrolysis 30h of 0.003%, then regulation pH value is to 6.3～6.4, is warming up to 90 DEG C, stirs 20min, filters
White to rice candy Egg preserved in wine, it is subsequently adding the water of 5 times of volumes 58 DEG C, regulation pH value, to 2.5～2.8, adds sugar white 0.3% weight of Egg preserved in wine
The Fungal Acid Protease of amount, after stirring reaction 10h, regulation pH value, to 9.0～9.1, adds and is equivalent to sugar grain quality 0.2%
Trypsin, continues stirring reaction 10h, fine straining, and being concentrated in vacuo to concentration is 77wt.%, obtains food stage rice protein nitrogen source,
Protein content is 88.2wt.%, and alpha-amido state nitrogen is 13.9wt.%；
5) saccharifying: by the clear liquid (solid content is 36～38wt.%) of the step 3) dilute hydrochloric acid solution regulation pH value of 4wt.%
To 4.2～4.6, and adding and be equivalent to sugar liquid and give money as a gift the glucoamylase of quality 0.06%, it is 98 that 66 DEG C of saccharifying obtain DE value
Saccharified liquid；
6) filtering without solid waste: the saccharified liquid of step 5) is warming up to 75 DEG C, enter microfiltration of ceramic membrane system, filtration pressure difference is
0.2MPa, cocnentration factor is 50, obtains clear liquid and slag inclusion concentrated solution, the clear liquid backflow that slag inclusion concentrated solution obtains through high speed centrifuge
Entering microfiltration of ceramic membrane system, merge the stillness of night that microfiltration of ceramic membrane obtains, the centrifugal sugar grain obtained then enters the receipts in step 4)
Collection tank；
7) mixed bed refines, concentrates: the clear liquid that step 6) obtains is 46wt.% through MVR vaporizer pre-concentration to solid content,
Pre-concentration liquid carries out isomery conversion by fixed glucose isomerase post, then it is refined and concentrate to carry out mixed bed, obtains high fructose syrup.
After testing, in high fructose syrup prepared by the present embodiment, content of beary metal is as follows: cadmium ＜ 2 μ g/Kg, and arsenic is 1.0 μ g/
Kg, lead is 2 μ g/Kg.
Embodiment 2:
1) pulverize, size mixing: weigh the rice of 100 mass parts, be transported to wash a meter tank after removing visible foreign, soak, be passed through
Compressed air, makes grain of rice rolling, friction, the impurity on rinsing grain of rice surface, releases rice-washed water, repeat once, by rice after rinsing
Grain is cleaned, and then pulverizes homogenizer through roll-type and mills pulping, adds 56～57 DEG C of water, and regulation pH value, obtaining concentration is 27～28 °
B é, pH value is the rice serosity of 5.8～5.9；
2) liquefaction: add the Liquozyme Supra α-amylase accounting for rice quality 0.04% in rice serosity, stirring is all
Even, at 104～105 DEG C, carry out one-level injection liquefaction, be incubated 40min after flash distillation, then at 128～129 DEG C, carry out two grades
Injection liquefaction, obtains liquefier；
3) streamline column insulation, solid-liquid separation: after liquefier flash distillation decrease temperature and pressure, stream adds the Liquozyme accounting for rice quality 0.01%
Supra α-amylase, enters back into multistage streamline column, and at 95 DEG C, the control laminar flow time is 90min, enters back into solid-liquid separation tank,
Add while stirring at 87～88 DEG C dilute hydrochloric acid solution regulation pH value to 5.9～6.1, stop stirring, stand 5min, then limit stir
Mix limit add dilute hydrochloric acid solution regulation pH value to 4.9～5.2, stop stirring, stand 5min, by clear liquid from solid-liquid separation pot bottom
Releasing and import saccharifying tank, sugar slag is retained by tank inner hole plate；
4) rice protein nitrogen source is extracted: added by the sugared slag of step 3) in the hot water of 67～68 DEG C, stir, filter pressing, collect
Sugar grain, is transferred to collecting tank after cleaning, homoiothermic to 60～62 DEG C, and regulation pH value, to 7.9～8.0, adds and is equivalent to sugar grain quality
The alkaline fat enzyme hydrolysis 25h of 0.006%, then regulation pH value is to 6.0～6.1, is warming up to 92 DEG C, stirs 18min, filters
White to rice candy Egg preserved in wine, it is subsequently adding the water of 6 times of volumes 60 DEG C, regulation pH value, to 4.9～5.0, adds sugar white 0.5% weight of Egg preserved in wine
The pepsin of amount, after stirring reaction 10h, regulation pH value, to 10.0～10.1, adds the rotten egg being equivalent to sugar grain quality 0.4%
White enzyme, continues stirring reaction 12h, and fine straining, being concentrated in vacuo to concentration is 80wt.%, obtains food stage rice protein nitrogen source, albumen
Matter content is 90.1wt.%, and alpha-amido state nitrogen is 14.3wt.%；
5) saccharifying: by the clear liquid (solid content is 38～40wt.%) of the step 3) dilute hydrochloric acid solution regulation pH value of 5wt.%
To 5.2～5.4, and add be equivalent to sugar liquid give money as a gift quality 0.01% glucoamylase, be equivalent to sugar liquid and give money as a gift quality
The fungal amylase of 0.005%, be equivalent to sugar liquid and give money as a gift quality 0.02% pullulanase and be equivalent to sugar liquid and give money as a gift quality 0.002%
Acid lipase enzyme, 60 DEG C of cooperative saccharifications, saccharified liquid DE value is to be warming up to 83 DEG C when 60, be incubated 45min enzyme denaturing；
6) filtering without solid waste: the saccharified liquid of step 5) is warming up to 80 DEG C, enter microfiltration of ceramic membrane system, filtration pressure difference is
0.5MPa, cocnentration factor is 40, obtains clear liquid and slag inclusion concentrated solution, the clear liquid backflow that slag inclusion concentrated solution obtains through high speed centrifuge
Entering microfiltration of ceramic membrane system, merge the stillness of night that microfiltration of ceramic membrane obtains, the centrifugal sugar grain obtained then enters the receipts in step 4)
Collection tank；
7) mixed bed refines, concentrates: the clear liquid that step 6) obtains is 55wt.% through MVR vaporizer pre-concentration to solid content,
Pre-concentration liquid is refined through mixed bed, concentration, obtains glucose syrup.
After testing, in glucose syrup prepared by the present embodiment, content of beary metal is as follows: cadmium ＜ 2 μ g/Kg, and arsenic is 1.5 μ g/
Kg, lead is 5 μ g/Kg, and copper is 7.5 μ g/Kg.
Embodiment 3:
1) pulverize, size mixing: weigh the rice of 100 mass parts, be transported to wash a meter tank after removing visible foreign, soak, be passed through
Compressed air, makes grain of rice rolling, friction, the impurity on rinsing grain of rice surface, releases rice-washed water, repeat once, by rice after rinsing
Grain is cleaned, and then pulverizes homogenizer through roll-type and mills pulping, adds 55～56 DEG C of water, and regulation pH value, obtaining concentration is 26～27 °
B é, pH value is the rice serosity of 5.7～5.8；
2) liquefaction: add the Liquozyme Supra 2.2X α-amylase accounting for rice quality 0.02% in rice serosity, stir
Mix uniformly, at 99～100 DEG C, carry out one-level injection liquefaction, be incubated 50min after flash distillation, at 126～127 DEG C, then carry out two
Level injection liquefaction, obtains liquefier；
3) streamline column insulation, solid-liquid separation: after liquefier flash distillation decrease temperature and pressure, stream adds the Liquozyme accounting for rice quality 0.02%
Supra 2.2X α-amylase, enters back into multistage streamline column, and at 98 DEG C, the control laminar flow time is 70min, enters back into solid-liquid and divides
From tank, add while stirring at 94～95 DEG C dilute hydrochloric acid solution regulation pH value to 5.8～5.9, stop stirring, stand 10min,
Addition dilute hydrochloric acid solution regulation pH value is to 4.5～4.6 the most while stirring, stops stirring, stands 10min, divided from solid-liquid by clear liquid
Release and import saccharifying tank from pot bottom, sugar slag is retained by tank inner hole plate；
4) rice protein nitrogen source is extracted: added by the sugared slag of step 3) in the hot water of 66～67 DEG C, stir, filter pressing, collect
Sugar grain, is transferred to collecting tank after cleaning, homoiothermic to 63～64 DEG C, and regulation pH value, to 7.7～7.8, adds and is equivalent to sugar grain quality
The alkaline fat enzyme hydrolysis 20h of 0.009%, then regulation pH value is to 5.9～6.1, is warming up to 95 DEG C, stirs 25min, filters
White to rice candy Egg preserved in wine, it is subsequently adding the water of 7 times of volumes 56 DEG C, regulation pH value, to 4.0～4.1, adds and is equivalent to sugar grain quality
The Fungal Acid Protease of 0.2% and the pepsin being equivalent to sugar grain quality 0.2%, after stirring reaction 11h, regulate pH value extremely
9.3～9.4, add the trypsin being equivalent to sugar grain quality 0.1% and the Chymotrypsin being equivalent to sugar grain quality 0.1%, continue
Stirring reaction 11h, fine straining, being concentrated in vacuo to concentration is 85wt.%, obtains food stage rice protein nitrogen source, and protein content is
83.5wt.%, alpha-amido state nitrogen is 14.8wt.%；
5) saccharifying: by the clear liquid (solid content is 35～37wt.%) of the step 3) dilute hydrochloric acid solution regulation pH value of 5wt.%
To 5.2～5.4, and add and be equivalent to sugar liquid and give money as a gift the barley beta-amylase of quality 0.01% and be equivalent to sugar liquid and give money as a gift quality
The pullulanase of 0.002%, at 62 DEG C of cooperative saccharification 6h, adds and is equivalent to sugar liquid and gives money as a gift the glucoamylase of quality 0.002%
Enzyme, continues saccharifying, and saccharified liquid DE value is to be warming up to 84 DEG C of enzyme denaturing when 53, is incubated 1h enzyme denaturing；
6) filtering without solid waste: the saccharified liquid of step 5) is warming up to 85 DEG C, enter microfiltration of ceramic membrane system, filtration pressure difference is
0.4MPa, cocnentration factor is 30, obtains clear liquid and slag inclusion concentrated solution, the clear liquid backflow that slag inclusion concentrated solution obtains through high speed centrifuge
Entering microfiltration of ceramic membrane system, merge the stillness of night that microfiltration of ceramic membrane obtains, the centrifugal sugar grain obtained then enters the receipts in step 4)
Collection tank；
7) mixed bed refines, concentrates: the clear liquid that step 6) obtains is 50wt.% through MVR vaporizer pre-concentration to solid content,
Pre-concentration liquid is refined through mixed bed, concentration, obtains maltose syrup.
After testing, in maltose syrup prepared by the present embodiment, content of beary metal is as follows: cadmium ＜ 2 μ g/Kg, and arsenic is 1.7 μ g/
Kg, lead is 6 μ g/Kg.
Above-described embodiment is the present invention preferably embodiment, but embodiments of the present invention are not by above-described embodiment
Limit, the change made under other any spirit without departing from the present invention and principle, modify, substitute, combine, simplify,
All should be the substitute mode of equivalence, within being included in protection scope of the present invention.
Claims (10)
1. the production technology of starch syrup prepared by a rice, it is characterised in that: comprise the following steps:
1) pulverizing, size mixing: rice carries out remove impurity, cleans, mill, add 54～the water of 57 DEG C, regulate pH value, obtaining concentration is 25
～28 ° of B é, pH value is the rice serosity of 5.6～6.0；
2) liquefaction: add α-amylase in rice serosity, stir, carries out one-level injection liquefaction at 98～105 DEG C, dodges
It is incubated 30～50min after steaming, then at 125～130 DEG C, carries out two-stage injection liquefaction, obtain liquefier；
3) streamline column insulation, solid-liquid separation: after liquefier flash distillation decrease temperature and pressure, stream adds α-amylase, enters back into multistage streamline column,
At 95～100 DEG C, the control laminar flow time is 60～90min, enters back into solid-liquid layering tank, adds dilute hydrochloric acid at 85～95 DEG C
Solution regulation pH value to 5.8～6.4, stand 5～10min, add dilute hydrochloric acid solution regulation pH value to 4.6～5.6, stand 5
～10min, clear liquid to be released from solid-liquid separation pot bottom, sugar slag is retained by tank inner hole plate；
4) rice protein nitrogen source is extracted: the sugared slag of step 3) is added the hot water of 65～75 DEG C, stirs, filter pressing, will obtain
Sugar grain clean after be transferred to collecting tank, homoiothermic to 55～65 DEG C, regulation pH value to 7.5～8.5, add alkaline lipase, water
Solving 20～40h, then regulation pH value is to 5.0～6.5 or to isoelectric points of proteins, is warming up to 90～95 DEG C, stirs, mistake
Filter, obtains rice candy Egg preserved in wine white, adds 55～60 DEG C of water, stir in rice candy Egg preserved in wine is white, regulation pH value to 2.0～5.0,
Add protease A, stirring fully reaction, regulation pH value, to 9.0～10.5, adds Cathepsin B, and stirring fully reaction is filtered,
Concentrate, obtain rice protein nitrogen source；
5) saccharifying: regulating step 3) the pH value of clear liquid to 4.2～5.6, homoiothermic to 56～66 DEG C, add saccharifying enzyme, the most instead
Should, obtain saccharified liquid；
6) filter without solid waste: the temperature of regulation saccharified liquid, to 75～85 DEG C, carries out microfiltration of ceramic membrane, respectively obtains clear liquid and slag inclusion
Concentrated solution, is centrifuged slag inclusion concentrated solution, and the centrifugal supernatant obtained carries out microfiltration of ceramic membrane again, merges microfiltration of ceramic membrane
The stillness of night obtained, the extraction sugar Egg preserved in wine that the centrifugal sugared grain obtained carries out step 4) operates in vain；
7) mixed bed refines, concentrates: the clear liquid of step 6) is introduced MVR vaporizer, carries out pre-concentration, then it is refined, dense to carry out mixed bed
Contracting, obtains starch syrup.
Production technology the most according to claim 1, it is characterised in that: step 2) and step 3) described in the consumption of α-amylase
For rice quality 0.01%～0.04%.
Production technology the most according to claim 1, it is characterised in that: the percent mass of solid content in clear liquid described in step 3)
Content is 35～40%.
Production technology the most according to claim 1, it is characterised in that: the consumption of alkaline lipase described in step 4) is sugar grain
The 0.001%～0.1% of quality.
Production technology the most according to claim 1, it is characterised in that: protease A described in step 4) is Fungal Acid albumen
At least one in enzyme, pepsin, the consumption of protease A is the 0.1%～1.0% of rice candy grain albumen quality.
Production technology the most according to claim 1, it is characterised in that: Cathepsin B described in step 4) is trypsin, rotten egg
At least one in white enzyme, the consumption of Cathepsin B is the 0.1%～1.0% of rice candy grain albumen quality.
Production technology the most according to claim 1, it is characterised in that: alpha-amido state in rice protein nitrogen source described in step 4)
The percentage by weight of nitrogen is 13.5%～15.0%.
Production technology the most according to claim 1, it is characterised in that: saccharifying enzyme described in step 5) be barley beta-amylase,
At least one in fungal amylase, glucoamylase, pullulanase, lipase.
9. according to the production technology described in claim 1 or 8, it is characterised in that: the consumption of saccharifying enzyme described in step 5) is step
3) in, clear liquid is given money as a gift the 0.001%～0.07% of quality.
Production technology the most according to claim 1, it is characterised in that: the filtration pressure difference of microfiltration of ceramic membrane described in step 6)
For 0.1MPa～0.5MPa, cocnentration factor is 5～50.
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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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 |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| 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 |
| CN110540330A (en) * | 2019-09-23 | 2019-12-06 | 南京钛净流体技术有限公司 | Membrane integrated rice washing water recycling device and recycling method |
| 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 |
| CN110819671A (en) * | 2019-11-05 | 2020-02-21 | 山东香驰健源生物科技有限公司 | Maltodextrin and production process and application thereof |
| 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 |
| CN113481259A (en) * | 2021-07-13 | 2021-10-08 | 山东省科学院菏泽分院 | Method for extracting starch syrup and rice protein isolate from broken rice |
| 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 |
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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 |