CN106811498A - A kind of method and system of sugaring - Google Patents
A kind of method and system of sugaring Download PDFInfo
- Publication number
- CN106811498A CN106811498A CN201710086134.3A CN201710086134A CN106811498A CN 106811498 A CN106811498 A CN 106811498A CN 201710086134 A CN201710086134 A CN 201710086134A CN 106811498 A CN106811498 A CN 106811498A
- Authority
- CN
- China
- Prior art keywords
- saccharification
- flash distillation
- steam
- evaporation process
- temperature
- 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.)
- Withdrawn
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
- C12P19/22—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
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/18—Apparatus specially designed for the use of free, immobilized or carrier-bound enzymes
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/10—Separation or concentration of fermentation products
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/12—Purification
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/20—Heating or cooling
-
- 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
- C12P19/20—Preparation of compounds containing saccharide radicals produced by the action of an exo-1,4 alpha-glucosidase, e.g. dextrose
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Zoology (AREA)
- Wood Science & Technology (AREA)
- Health & Medical Sciences (AREA)
- Biotechnology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Genetics & Genomics (AREA)
- Microbiology (AREA)
- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biomedical Technology (AREA)
- Sustainable Development (AREA)
- Molecular Biology (AREA)
- Clinical Laboratory Science (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The present invention relates to the field of refining sugar, a kind of method and system of sugaring is disclosed, the method includes starch milk being liquefied successively, being saccharified, decolourized and evaporation process, wherein, methods described also includes：The liquefier that obtains of liquefying is flashed and material after being obtained steam and flash distillation, gained vapor portion or be completely used for providing heat for evaporation process, material is for being saccharified after gained flash distillation.Heat of the present invention after by liquefaction in material is used to provide heat for evaporation process, reduces the consumption of steam in evaporation process, and then the cost that reduction is refined sugar.
Description
Technical field
The present invention relates to the field of refining sugar, in particular it relates to a kind of method and system of sugaring.
Background technology
Cornstarch is widely used in the raw material of the corn deep processing industry such as feed, starch sugar, and China is starch and starch
Sugared big producer, wherein starch sugar annual production exceed 6,000,000 tons, and production technology uses corn wet sugar refining technology mostly.Corn is wet
Method sugar refining technology refers to the technique for being beaten again after corn particle is soaked in water, liquefied, be saccharified, decolourizing and being concentrated by evaporation.
In traditional sugar refining technology, it is that raw material heats up to decolourize and needed in evaporation process with substantial amounts of steam, to control
Optimal technological temperature, the cost of sugar refining technology is increased due to consuming a large amount of steam.
The content of the invention
A kind of cost the invention aims to reduce sugar refining technology, there is provided method and system of sugaring.
To achieve these goals, the present invention provides a kind of method of sugaring, and the method includes successively carrying out starch milk
Liquefaction, saccharification, decolouring and evaporation process, wherein, methods described also includes：The liquefier that obtains of liquefying is flashed and
Obtain material after steam and flash distillation, gained vapor portion or be completely used for providing heat for evaporation process, gained flash after material
For being saccharified.
Present invention also offers a kind of system of sugaring, the system includes starch milk feedway, liquefying plant, saccharification dress
Put, decoloration device and vaporising device, the starch milk feedway connects with the liquefying plant, the liquefying plant with it is described
Saccharification apparatus are connected, and the saccharification apparatus are connected with the decoloration device, and the decoloration device is connected with the vaporising device, its
In, eddy flow flash distillation plant, the eddy flow flash distillation dress are provided with the pipeline between the liquefying plant and the saccharification apparatus
The steam (vapor) outlet put is connected with the vaporising device, and the material outlet of the eddy flow flash distillation plant is connected with the saccharification apparatus.
Heat of the present invention after by liquefaction in material is used to provide heat for evaporation process, in reducing evaporation process
The consumption of steam；A preferred embodiment of the invention, the steam that will be produced during evaporation process is used for saccharification
Material afterwards provides heat, reduces the quantity of steam used in decolorization, and then reduces the cost refined sugar, and is preferable to carry out at this
In mode, 1 ton of starch milk (in terms of dry) for the treatment of can be with steam saving 0.069-0.071 tons, by 70,000 tons of starch milks (with dry
Material meter)/year treatment gauge, 1 year can be with cost-effective 101-104 ten thousand (steam unit price is for 210 yuan/ton).
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Fig. 1 is a kind of system of the sugaring of preferred embodiment that the present invention is provided.
In figure：Starch milk feedway 1, liquefying plant 2, eddy flow flash distillation plant 3, saccharification apparatus 4, heat exchanger 5, decolouring dress
Put 6, ion interchange unit 7, vaporising device 8.
Specific embodiment
Specific embodiment of the invention is described in detail below.It should be appreciated that described herein specific
Implementation method is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The end points and any value of disclosed scope are not limited to the accurate scope or value herein, these scopes or
Value should be understood to comprising the value close to these scopes or value.For number range, between the endpoint value of each scope, respectively
One or more can be obtained with combination with one another between the endpoint value of individual scope and single point value, and individually between point value
New number range, these number ranges should be considered as specific open herein.
The invention provides a kind of method of sugaring, the method include starch milk is liquefied successively, is saccharified, being decolourized and
Evaporation process, it is characterised in that methods described also includes：By the liquefier that obtains of liquefying flashed and obtained steam and
Material after flash distillation, gained vapor portion or is completely used for providing heat for evaporation process, and material is used to be saccharified after gained flash distillation.
In the present invention, using the steam obtained after flash distillation for evaporation process provides heat, evaporation process can be effectively reduced
During steam consumption.
In the present invention, to the implementation method of the flash distillation, there is no particular limitation, can be the conventional selection of this area, example
Can such as be carried out in eddy flow flash vessel.
In the present invention, under preferable case, the condition of the flash distillation includes：The temperature of flash distillation is 95-98 DEG C, the pressure of flash distillation
It is -0.06MPa to -0.09MPa.Under conditions of above-mentioned flash distillation, the steam heat in material can be not only made full use of, may be used also
To ensure the quality of sugaring.
In the present invention, the starch milk can be prepared by starchy material, and starch milk is obtained by starchy material
Method can be used well known to a person skilled in the art various conventional methods, for example, starchy material is crushed, after crushing
Product and water be mixed to get starch milk.Wherein, the concentration to starch milk has no particular limits, it is preferable that the starch milk
The content of middle dry is 35-40 weight %.
According to the present invention, the starchy material can be known in the art it is various can be used for digesting, containing of fermenting
There is the raw material of starch, for example, one or more can be selected from corn, potato class, wheat and sorghum.
A preferred embodiment of the invention, methods described also includes：Material after saccharification is carried out into decolouring
Preceding elder generation carries out heat exchange with the steam that the evaporation process is produced, so that the material after saccharification heats up.In the preferred embodiment
In, the steam produced using evaporation process makes the material after saccharification heat up, and can effectively reduce and be taken off the material after saccharification
The amount of steam is consumed during color.
In the present invention, the material increasing extent of temperature after saccharification can be determined according to the temperature requirement for decolourizing, under preferable case,
The heat exchange causes that the temperature of the material after the saccharification increases to 65-75 DEG C.
In the present invention, the concrete operations to the heat exchange are not specially required, as long as heat can be made according to top
Formula is transmitted.Usually, heat exchange can be realized by heat exchanger, the heat exchanger can be various conventional heat
Exchanger, and can be by commercially available, such as heat exchanger with oblate of U.S. Brown companies.
In the present invention, to the liquefaction, saccharification and the condition decolourized, there is no particular limitation, can be the routine of this area
Selection.Under preferable case, the liquefied condition includes：Liquefied temperature is 110-120 DEG C, and the liquefied time is 2-2.5h；
And/or, the condition of the saccharification includes：The temperature of saccharification is 55-60 DEG C, and the time of saccharification is 36-48h；And/or, it is described de-
The condition of color includes：The temperature of decolouring is 65-75 DEG C, and the time of decolouring is 15-30min；And/or, the bar of the evaporation process
Part includes：The temperature of evaporation is 100-110 DEG C.
In the present invention, to time of the evaporation, there is no particular limitation, and under preferable case, the time of evaporation makes evaporated
The volume of material is 0.6-0.7 times of the volume of material before evaporation process after reason.
In the present invention, can be liquefied by the way of routine, for example, farinaceous size is carried out into liquefied mode can be with
For：The mixture of starch milk and amylase is contacted with steam.The amount of liquefaction amylase used can be the conventional choosing of this area
Select, under preferable case, relative to the dry in starch milk per ton, the amount of liquefaction amylase used is 400-450g.Wherein, liquid
It can be the amylase that this area routinely uses, such as AMS, beta amylase and isoamylase to change amylase used；Can also
It is fire resistant alpha-diastase.
In the present invention, the process of the saccharification is in order that starch milk is converted into monose as far as possible.In the present invention, using normal
The mode of rule is saccharified, for example, the mode of saccharification can be：By in gained liquefier addition saccharifying tank, carbohydrase is added simultaneously
Stirring.
Wherein, carbohydrase is also known as starch α-Isosorbide-5-Nitrae-glucuroide, this enzyme effect in the non reducing end of starch molecule,
In units of glucose, the α-Isosorbide-5-Nitrae-glycosidic bond in starch molecule is acted on successively, generate glucose.Carbohydrase acts on side chain
Product after starch has glucose and the oligosaccharides with α -1,6- glycosidic bonds；Acting on the product almost all after amylose is
Glucose.The carbohydrase can be by commercially available.
In the present invention, the concrete operations of decolouring can be the conventional discoloration method used in sugar refining technology, if once taken off
Color effect is bad, can also carry out secondary decolourization, and those skilled in the art can carry out selection judgement to this, no longer goes to live in the household of one's in-laws on getting married herein
State.
In the present invention, the process of the evaporation process is the concentration process to material, can be using the conventional side in this area
Formula is implemented, and will not be repeated here.
Another preferred embodiment of the invention, by the material after decolouring be evaporated treatment before first carry out from
Sub- exchange treatment.The process of the ion-exchange treatment is generally adopted by ion exchange resin.Liquid glucose still contains after decolouring
Part inorganic salts and organic impurities, therefore refined using ion exchange resin, play a part of ion exchange and absorption.From
The ability specific activity charcoal that sub-exchange resin removes protein, amino acid, hydroxymethylfurfural and coloring matter etc. is strong.
As shown in figure 1, present invention also offers a kind of system of sugaring, the system includes starch milk feedway 1, liquefaction
Device 2, saccharification apparatus 4, decoloration device 6 and vaporising device 8, the starch milk feedway 1 are connected with the liquefying plant 2,
The liquefying plant 2 is connected with the saccharification apparatus 4, and the saccharification apparatus 4 are connected with the decoloration device 6, the dress that decolourizes
Put 6 to be connected with the vaporising device 8, it is characterised in that on the pipeline between the liquefying plant 2 and the saccharification apparatus 4
Eddy flow flash distillation plant 3 is provided with, the steam (vapor) outlet of the eddy flow flash distillation plant 3 is connected with the vaporising device 8 and (makes flash distillation gained
Vapor portion is completely used for providing heat for evaporation process), the material outlet of the eddy flow flash distillation plant 3 and the saccharification are filled
Put 4 connections.
According to invention a kind of preferred embodiment, the system also include heat exchanger 5, the heat exchanger 5 respectively with saccharification
The material outlet of device 4 is connected with the steam (vapor) outlet of the vaporising device 8, for make saccharification apparatus 4 discharge material with it is described
The steam of the discharge of vaporising device 8 carries out heat exchange.The steam that the vaporising device 8 is discharged is made to described by the heat exchanger 5
The material of the discharge of saccharification apparatus 4 is heated, and reduces the use of steam when being decolourized to the material of the discharge of the saccharification apparatus 4
Amount.
According to another preferred embodiment of invention, the system also includes ion interchange unit 7, the ion exchange
Device 7 is located on the pipeline between the decoloration device 6 and the vaporising device 8.The effect of ion interchange unit 7 is to material
Refined.
Below will the present invention will be described in detail by embodiment.In following examples and comparative example temperature (remove by
The temperature change that heat exchange is produced) it is to be provided by consuming steam.
In following examples and comparative example, the starchy material for using is to crush corn (moisture is 13 weight %)
The particle mean size for obtaining afterwards is 10 microns of maize raw material；Heat exchange is carried out by tubular heat exchanger (Brown companies of the U.S.), specifically
Operation is referring to its specification；The step of decolouring is：Activated carbon (the specific surface area of 0.5g/100g liquid glucoses is added toward liquid glucose
1000m2/ g, granularity are less than 50 μm), stirring in water bath is filtered to remove activated carbon after decolourizing；The cation exchange that ion exchange is used
Resin be 732 storng-acid cation exchange resins, anion exchange resin be D311 weak-base anion-exchange resins, feed liquid according to
The secondary ion exchange resin filter bed by " sun-cloudy-sun-cloudy " series connection, the flow control of feed liquid is 2BV/h；The survey of light transmittance
Determine method reference standard QB/T2319-1997, instrument is spectrum SP-752 ultraviolet-uisible spectrophotometer (Shanghai spectrometers
Device Co., Ltd), light transmittance is higher, illustrates that the turbidity of liquid glucose is lower, and liquid glucose is purer.
Embodiment 1
Added water toward starchy material and be configured to dry matter content and be the starch milk of 35 weight %, and liquefied successively,
Saccharification, decolouring, ion exchange and evaporation process, concrete operations are as follows：
Calcium hydroxide regulation pH=6.0 is added in starch milk, (dry per ton adds the α-shallow lake of 420g to add AMS
Powder enzyme), liquefying plant is squeezed into pump after stirring, liquefied temperature is 110 DEG C, and the liquefied time is 2.5h；
The liquefier that liquefaction is obtained is flashed in eddy flow flash vessel, the condition of flash distillation includes：The temperature of flash distillation is
95 DEG C, the pressure of flash distillation is -0.06MPa.Gained steam is completely used for providing heat for evaporation process after flash distillation, after gained flash distillation
Material enters saccharification apparatus, at 56 DEG C, under pH value 4.4, addition carbohydrase (4060 compounded saccharifying enzymes of Genencor Company's production,
Dry per ton adds the carbohydrase of 550g), stir 48h；
The steam that the material (temperature is 56 DEG C, 41 ton hours) obtained after saccharification is produced with evaporation process carries out heat exchange,
Temperature of charge after heat exchange is 65 DEG C；
Material after heat exchange contacts and decolourized (temperature of decolouring is 65 DEG C, and the time of decolouring is with activated carbon
30min), and by the material after decolouring ion exchange is carried out, then the material after ion exchange is evaporated into treatment, and (temperature is
100 DEG C), the material obtained after the steam of evaporation process formation and saccharification carries out heat exchange.Volume of material after treatment to be evaporated
When being 0.6 times of volume of material before evaporation process, that is, stop evaporation, obtain liquid glucose, the light transmittance of the liquid glucose is 99%.
During the sugaring, the consumption of steam is 0.279 ton/ton starch milk (in terms of dry).
Embodiment 2
Added water toward starchy material and be configured to dry matter content and be the starch milk of 40 weight %, and liquefied successively,
Saccharification, decolouring, ion exchange and evaporation process, concrete operations are as follows：
Calcium hydroxide regulation pH=6.0 is added in starch milk, (dry per ton adds the α-shallow lake of 420g to add AMS
Powder enzyme), liquefying plant is squeezed into pump after stirring, liquefied temperature is 120 DEG C, and the liquefied time is 2h；
The liquefier that liquefaction is obtained is flashed in eddy flow flash vessel, the condition of flash distillation includes：The temperature of flash distillation is
98 DEG C, the pressure of flash distillation is -0.09MPa.Gained steam is completely used for providing heat for evaporation process after flash distillation, after gained flash distillation
Material enters saccharification apparatus, at 60 DEG C, under pH value 4.4, addition carbohydrase (4060 compounded saccharifying enzymes of Genencor Company's production,
Dry per ton adds the carbohydrase of 550g), stir 36h；
The steam that the material (temperature is 60 DEG C, 41 ton hours) obtained after saccharification is produced with evaporation process carries out heat exchange,
Temperature of charge after heat exchange is 75 DEG C；
Material after heat exchange contacts and decolourized (temperature of decolouring is 75 DEG C, and the time of decolouring is with activated carbon
15min), and by the material after decolouring ion exchange is carried out, then the material after ion exchange is evaporated into treatment, and (temperature is
110 DEG C), the material obtained after the steam of evaporation process formation and saccharification carries out heat exchange.Volume of material after treatment to be evaporated
When being 0.6 times of volume of material before evaporation process, that is, stop evaporation, obtain liquid glucose, the light transmittance of the liquid glucose is 98%.
During the sugaring, the consumption of steam is 0.281 ton/ton starch milk (in terms of dry).
Embodiment 3
Added water toward starchy material and be configured to dry matter content and be the starch milk of 37 weight %, and liquefied successively,
Saccharification, decolouring, ion exchange and evaporation process, concrete operations are as follows：
Calcium hydroxide regulation pH=6.0 is added in starch milk, (dry per ton adds the α-shallow lake of 420g to add AMS
Powder enzyme), liquefying plant is squeezed into pump after stirring, liquefied temperature is 115 DEG C, and the liquefied time is 2.2h；
The liquefier that liquefaction is obtained is flashed in eddy flow flash vessel, the condition of flash distillation includes：The temperature of flash distillation is
96 DEG C, the pressure of flash distillation is -0.07MPa.Gained steam is completely used for providing heat for evaporation process after flash distillation, after gained flash distillation
Material enters saccharification apparatus, at 57 DEG C, under pH value 4.4, addition carbohydrase (4060 compounded saccharifying enzymes of Genencor Company's production,
Dry per ton adds the carbohydrase of 550g), stir 40h；
The steam that the material (temperature is 57 DEG C, 41 ton hours) obtained after saccharification is produced with evaporation process carries out heat exchange,
Temperature of charge after heat exchange is 69 DEG C；
Material after heat exchange contacts and decolourized (temperature of decolouring is 69 DEG C, and the time of decolouring is with activated carbon
20min), and by the material after decolouring ion exchange is carried out, then the material after ion exchange is evaporated into treatment, and (temperature is
105 DEG C), the material obtained after the steam of evaporation process formation and saccharification carries out heat exchange.Volume of material after treatment to be evaporated
When being 0.7 times of volume of material before evaporation process, that is, stop evaporation, obtain liquid glucose, the light transmittance of the liquid glucose is 98.5%.
During the sugaring, the consumption of steam is 0.28 ton/ton starch milk (in terms of dry).
Embodiment 4
Added water toward starchy material and be configured to dry matter content and be the starch milk of 35 weight %, and liquefied successively,
Saccharification, decolourize, ion exchange and evaporation process, concrete operations are following (not including the material after saccharification to be carried out the step of heat exchange
Suddenly)：
Calcium hydroxide regulation pH=6.0 is added in starch milk, (dry per ton adds the α-shallow lake of 420g to add AMS
Powder enzyme), liquefying plant is squeezed into pump after stirring, liquefied temperature is 110 DEG C, and the liquefied time is 2.5h；
The liquefier that liquefaction is obtained is flashed in eddy flow flash vessel, the condition of flash distillation includes：The temperature of flash distillation is
95 DEG C, the pressure of flash distillation is -0.06MPa.Gained steam is completely used for providing heat for evaporation process after flash distillation, after gained flash distillation
Material enters saccharification apparatus, at 56 DEG C, under pH value 4.4, addition carbohydrase (4060 compounded saccharifying enzymes of Genencor Company's production,
Dry per ton adds the carbohydrase of 550g), stir 48h；
The material (temperature is 56 DEG C, 41 ton hours) that will be obtained after saccharification contacts the (temperature of decolouring of being decolourized with activated carbon
It is 65 DEG C to spend, and time of decolouring is 30min), and the material after decolouring is carried out into ion exchange, then by the material after ion exchange
Treatment (temperature is 100 DEG C) is evaporated, the volume of material after treatment to be evaporated is 0.6 times of volume of material before evaporation process
When, that is, stop evaporation, liquid glucose is obtained, the light transmittance of the liquid glucose is 99%.
During the sugaring, the consumption of steam is 0.29 ton/ton starch milk (in terms of dry).
Embodiment 5
Method according to embodiment 1 is refined sugar, unlike, the condition of flash distillation is：The temperature of flash distillation is 80 DEG C, the pressure of flash distillation
Power is -0.05MPa.
The light transmittance for obtaining liquid glucose is 99%.During the sugaring, the consumption of steam is 0.3 ton/ton starch milk (with dry
Material meter).
Comparative example 1
Added water toward starchy material and be configured to dry matter content and be the starch milk of 35 weight %, and liquefied successively,
Saccharification, decolourize, ion exchange and evaporation process, concrete operations are following (not including flash distillation and the step of heat exchange)：
Calcium hydroxide regulation pH=6.0 is added in starch milk, (dry per ton adds the α-shallow lake of 420g to add AMS
Powder enzyme), liquefying plant is squeezed into pump after stirring, liquefied temperature is 110 DEG C, and the liquefied time is 2.5h；
The liquefier that liquefaction is obtained enters saccharification apparatus, and at 56 DEG C, under pH value 4.4, (Genencor Company gives birth to add carbohydrase
4060 compounded saccharifying enzymes for producing, dry per ton adds the carbohydrase of 550g), stir 48h；
The material (temperature is 56 DEG C, 41 ton hours) that will be obtained after saccharification contacts the (temperature of decolouring of being decolourized with activated carbon
It is 65 DEG C to spend, and time of decolouring is 30min), and the material after decolouring is carried out into ion exchange, then by the material after ion exchange
Treatment (temperature is 100 DEG C) is evaporated, the volume of material after treatment to be evaporated is 0.6 times of volume of material before evaporation process
When, that is, stop evaporation, liquid glucose is obtained, the light transmittance of the liquid glucose is 99%.
During the sugaring, the consumption of steam is 0.35 ton/ton starch milk (in terms of dry).
Be can be seen that during method for manufacturing sugar of the present invention can effectively reduce sugar refining technology by the result of above-described embodiment and steamed
The consumption of vapour, so that sugar making cost is effectively reduced, and, after measured, the light transmittance of the final liquid glucose for obtaining is 98%-
99%.The steam that will be produced in evaporation process in the present invention is can be seen that by embodiment 4 and the results contrast of embodiment 1 to pass through
Heat exchange improves the temperature of the material after saccharification, effectively reduces the steam consumption of decolorization, and then reduce the total consumption of steam.By
Embodiment 5 can be seen that under flash conditions of the present invention with the results contrast of embodiment 1, can be evaporation process process
A large amount of steam are provided, so as to further reduce the steam consumption of sugaring process；The results contrast of comparative example 1 and embodiment 1 can be with
Find out, method for manufacturing sugar of the present invention can effectively reduce the consumption of steam during sugaring, and then reduce sugar making cost.
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited in above-mentioned implementation method
Detail, in range of the technology design of the invention, various simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned specific embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy is no longer separately illustrated.
Additionally, can also be combined between a variety of implementation methods of the invention, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of method of sugaring, the method includes starch milk being liquefied successively, being saccharified, decolourized and evaporation process, and it is special
Levy and be, methods described also includes：The liquefier that obtains of liquefying is flashed and material, institute after being obtained steam and flash distillation
Obtain vapor portion or be completely used for providing heat for evaporation process, material is used to be saccharified after gained flash distillation.
2. method according to claim 1, wherein, the condition of the flash distillation includes：The temperature of flash distillation is 95-98 DEG C, is dodged
The pressure of steaming is -0.06MPa to -0.09MPa.
3. method according to claim 1 and 2, wherein, methods described also includes：Material after saccharification is carried out into decolouring
Preceding elder generation carries out heat exchange with the steam that the evaporation process is produced, so that the material after saccharification heats up.
4. method according to claim 3, wherein, the heat exchange causes that the temperature of the material after the saccharification increases to
65-75℃。
5. method according to claim 1 and 2, wherein, the liquefied condition includes：Liquefied temperature is 110-120
DEG C, the liquefied time is 2-2.5h；
And/or, the condition of the saccharification includes：The temperature of saccharification is 55-60 DEG C, and the time of saccharification is 36-48h；
And/or, the condition of the decolouring includes：The temperature of decolouring is 65-75 DEG C, and the time of decolouring is 15-30min；
And/or, the condition of the evaporation process includes：The temperature of evaporation process is 100-110 DEG C.
6. method according to claim 1 and 2, wherein, methods described also includes：Material after decolouring is evaporated place
Ion-exchange treatment is first carried out before reason.
7. method according to claim 1 and 2, wherein, the content of dry is 35-40 weight % in the starch milk.
8. a kind of system of sugaring, the system includes starch milk feedway (1), liquefying plant (2), saccharification apparatus (4), decolourizes
Device (6) and vaporising device (8), the starch milk feedway (1) connect with the liquefying plant (2), the liquefying plant
(2) connected with the saccharification apparatus (4), the saccharification apparatus (4) connect with the decoloration device (6), the decoloration device (6)
Connected with the vaporising device (8), it is characterised in that the pipeline between the liquefying plant (2) and the saccharification apparatus (4)
On be provided with eddy flow flash distillation plant (3), the steam (vapor) outlet of the eddy flow flash distillation plant (3) is connected with the vaporising device (8), institute
The material outlet for stating eddy flow flash distillation plant (3) is connected with the saccharification apparatus (4).
9. system according to claim 7, wherein, the system also includes heat exchanger (5), the heat exchanger (5) respectively with
The material outlet of saccharification apparatus (4) is connected with the steam (vapor) outlet of the vaporising device (8), for making what saccharification apparatus (4) were discharged
The steam that material is discharged with the vaporising device (8) carries out heat exchange.
10. system according to claim 8 or claim 9, wherein, the system also includes ion interchange unit (7), the ion
Switch (7) is on the pipeline between the decoloration device (6) and the vaporising device (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710086134.3A CN106811498A (en) | 2017-02-17 | 2017-02-17 | A kind of method and system of sugaring |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710086134.3A CN106811498A (en) | 2017-02-17 | 2017-02-17 | A kind of method and system of sugaring |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106811498A true CN106811498A (en) | 2017-06-09 |
Family
ID=59111927
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710086134.3A Withdrawn CN106811498A (en) | 2017-02-17 | 2017-02-17 | A kind of method and system of sugaring |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106811498A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108893509A (en) * | 2018-06-28 | 2018-11-27 | 国粮武汉科学研究设计院有限公司 | A kind of device and method preparing starch sugar suitable for high temperature drying corn |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101736059A (en) * | 2009-11-30 | 2010-06-16 | 山东省鲁洲食品集团有限公司 | Method for recovering waste heat during processing of starchy material |
| CN105238829A (en) * | 2014-07-11 | 2016-01-13 | 武汉中粮食品科技有限公司 | Enzymolysis method for starchy material |
| CN105483186A (en) * | 2016-01-07 | 2016-04-13 | 中粮生化能源（衡水）有限公司 | Liquidation and evaporation integrated high fructose corn syrup production method |
-
2017
- 2017-02-17 CN CN201710086134.3A patent/CN106811498A/en not_active Withdrawn
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101736059A (en) * | 2009-11-30 | 2010-06-16 | 山东省鲁洲食品集团有限公司 | Method for recovering waste heat during processing of starchy material |
| CN105238829A (en) * | 2014-07-11 | 2016-01-13 | 武汉中粮食品科技有限公司 | Enzymolysis method for starchy material |
| CN105483186A (en) * | 2016-01-07 | 2016-04-13 | 中粮生化能源（衡水）有限公司 | Liquidation and evaporation integrated high fructose corn syrup production method |
Non-Patent Citations (1)
| Title |
|---|
| 葛德忠: "闪蒸技术在淀粉质原料燃料乙醇生产过程中液化工序节能应用", 《轻工科技》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108893509A (en) * | 2018-06-28 | 2018-11-27 | 国粮武汉科学研究设计院有限公司 | A kind of device and method preparing starch sugar suitable for high temperature drying corn |
| CN108893509B (en) * | 2018-06-28 | 2022-05-10 | 国粮武汉科学研究设计院有限公司 | Device and method suitable for preparing starch sugar by drying corn at high temperature |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Zhang et al. | Acetyl-assisted autohydrolysis of sugarcane bagasse for the production of xylo-oligosaccharides without additional chemicals | |
| Nabarlatz et al. | Purification of xylo-oligosaccharides from almond shells by ultrafiltration | |
| CN101182559B (en) | Method for preparing low polyxylose through squeezing-assisted wheat bran enzymolysis | |
| CN101855368B (en) | Process for preparing a sugar product | |
| CN101736631B (en) | Process for efficiently preprocessing lignocellulose | |
| CN101643795B (en) | Method for preparing xylose and xylitol by using bamboo | |
| US3505110A (en) | Sugar products prepared from hydroxypropylated starch | |
| CN103320548A (en) | Method for preparing xylooligosaccharide and cellulose by using crop straws | |
| Wang et al. | Selective removal of lignin with sodium chlorite to improve the quality and antioxidant activity of xylo-oligosaccharides from lignocellulosic biomass | |
| AU2012278950A1 (en) | Process of extraction of hemicellulose from corn fiber | |
| CN103614435B (en) | A kind of method of preparing xylo-oligosaccharide from bagasse | |
| DK149552B (en) | PROCEDURE FOR THE EXTRACTION OF XYLANES AND DECOLUTION PRODUCTS THEREOF, AND FIBER MATERIALS FROM XYLANEUS PLANTS | |
| Chen et al. | Evaluating the production of monosaccharides and xylooligosaccharides from the pre-hydrolysis liquor of kraft pulping process by acid and enzymatic hydrolysis | |
| Chen et al. | Novel process for the coproduction of xylo-oligosaccharide and glucose from reed scraps of reed pulp mill | |
| Nam et al. | Efficiency of ionic liquids in the dissolution of rice husk | |
| López-Linares et al. | A biorefinery based on brewers spent grains: Arabinoxylans recovery by microwave assisted pretreatment integrated with butanol production | |
| CN103740787A (en) | Method for producing xylooligosaccharide by use of broadleaf wood dissolving pulp prehydrolysis waste liquid enzyme process | |
| US20140171664A1 (en) | Furfural production from biomass | |
| Kundu et al. | Extraction of arabinoxylan from corncob through modified alkaline method to improve xylooligosaccharides synthesis | |
| CN105238829B (en) | A kind of enzyme solution of starchy material | |
| CN106811498A (en) | A kind of method and system of sugaring | |
| CN103725807B (en) | A kind of method utilizing leaf wood dissolving pulp prehydrolysis waste liquid Production by Enzymes wood sugar | |
| Sun et al. | Optimization of pretreatment and enzymatic hydrolysis coupled with ultrasonication for the production of xylooligosaccharides from corn cob | |
| CN105624235A (en) | Method for preparing xylose by using eucalyptus pulping waste liquid | |
| Wu | The Potential of Pre-Hydrolysis Liquor from the Dissolving Pulp Process as Recovery Source of Xylooligosaccharide-A Mini-Review. |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WW01 | Invention patent application withdrawn after publication | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20170609 |