CN108410719A - A kind of new process of purification saccharified liquid - Google Patents
A kind of new process of purification saccharified liquid Download PDFInfo
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- CN108410719A CN108410719A CN201810163239.9A CN201810163239A CN108410719A CN 108410719 A CN108410719 A CN 108410719A CN 201810163239 A CN201810163239 A CN 201810163239A CN 108410719 A CN108410719 A CN 108410719A
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- 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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
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- 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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/26—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pH
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- 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
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Abstract
The application belongs to the production method of sugar, and in particular to and a kind of new process of purification saccharified liquid, steps are as follows,（1）It sizes mixing；（2）Liquefaction；（3）Saccharification；（4）Decoloration；（5）Ion-exchange；（6）Chromatography front evaporator concentrates；（7）Chromatographic isolation.
Description
Technical field
The application belongs to the production method of sugar, and in particular to a kind of new process of purification saccharified liquid.
Background technology
The method system that seperator detaches after preceding DX values in 99.5% or more liquid glucose are crystallized using traditional material
, i.e., corn starch milk by sizing mixing, liquefying, be saccharified, decolourize, ion-exchange, evaporation and concentration, crystallization, after separation, isolated crystalline substance
Body is re-dissolved in pure water.This conventional method period length, high energy consumption, product yield are low.
The application is using patent CN2017214368200, CN2017214368215 as priority.
Invention content
To solve the problems, such as that conventional method exists, this patent devises a kind of new process of purification saccharified liquid, and the application is
It is realized by following proposal：
A kind of new process of purification saccharified liquid, steps are as follows, and (1) sizes mixing：With water by corn starch milk wave in tank of sizing mixing
U.S. degree is adjusted to 17 ° of ± 0.5B é, rear that the Na that mass fraction is 5-10% is added2CO3PH in solution to tank of sizing mixing is 5.5~6.0,
The starch milk mixed up in tank of sizing mixing is got in material feeding jar afterwards；
(2) it liquefies：Liquefaction workshop section uses the techniques of 2 injection 4 flash distillations of liquefaction, and primary injection liquefaction addition three/
One α-amylase, 110 DEG C of temperature simultaneously maintain 1 minute, and then flash distillation is cooled to 95 DEG C and reacts 20 minutes；Secondary injection liquefies starch
Breast is warming up to 135 DEG C and maintains 15 seconds, and then flash distillation cools to 93 DEG C and adds remaining 2/3rds α-amylases, reacts 90 minutes, so
Liquefier cools the temperature to 58~62 DEG C by flash distillation and four flash distillations three times afterwards, at this time the mass concentration of liquefier for 30~
35%；
(3) it is saccharified：It is 4.2~4.5 that dilute hydrochloric acid is added after liquefying to step (2) in feed liquid and adjusts the pH value of feed liquid, after with
Compounded saccharifying enzyme, saccharification period 42-54h is added in the ratio of 0.40~0.50kg/T (butt)；
(4) it decolourizes：It is decolourized using seed activity charcoal post, charcoal post blade diameter length ratio is 8,50~60 DEG C of bleaching temperature, feed flow rate 2
~4BV/h；
(5) ion-exchange：Using the continuous ion-exchange equipment of fixed bed, 50~55 DEG C of ion-exchange temperature, 2~4BV/h of flow velocity；
(6) chromatography front evaporator concentrates：Chromatography front evaporator concentration section is using six effect falling film evaporator equipment, driving drop
The steam of film evaporator is the steel-making waste vapour of steel plant of company of this group, temperature discharge at 80~85 DEG C, after concentration BX55~
65%；
(7) chromatographic isolation：Advanced technology is combined using sequential type simulated moving bed chromatography piece-rate system and high-temperature material film；
55~60 DEG C of chromatographic isolation temperature, material-water ratio 1.5:1~2.0:1, charging rate 2BV/h.
Preferably, the starch milk of the step (2) enters a spray coil pipe after once spraying liquefaction, by full flashing
Enter secondary injection afterwards to liquefy, liquefy by secondary injection and enter secondary liquefaction maintenance device, the secondary liquefaction maintains device
Including by the sequentially connected Jet liquefier of pipeline (11), coil pipe (12) and flash vessel (13), the coil pipe (12) is by difference
The coil pipe connection composition of caliber；The coil pipe (12) is by three kinds of coil pipe connection groups that caliber DN is respectively 125/150/200mm
At；The coil pipe (12) is connected by three kinds of coil pipes that caliber DN is respectively 125/150/200mm successively along the direction of Flow of Goods and Materials
Composition；Pipeline between the Jet liquefier (11) and coil pipe (12) is made of the pipeline connection of different tube diameters；The injection
Pipeline between liquefier (11) and coil pipe (12) is respectively successively 100/125/ by caliber DN along the direction of Flow of Goods and Materials
Three kinds of pipelines connection composition of 150mm；The caliber DN of pipeline between the coil pipe (12) and flash vessel (13) is 125mm；Institute
The total length for stating coil pipe (12) is 208 meters；It is additionally provided with DCS control systems；It is set between the coil pipe (12) and flash vessel (13)
It is equipped with DCS control systems.
Preferably, the DCS control systems pass through EtherNet/IP communication instrument Ring
When realizing real-time displays, alarm and the unlatchings of valve such as start and stop, speed control and the electric current pumped, power, frequency, state, operation
Between；
The liquefier that temperature is 110 DEG C after primary injection liquefaction is flashed to the indirect steam of 95 DEG C of generations, secondary injection liquid
The liquefier that temperature is 135 DEG C after change is flashed to the indirect steam of 93 DEG C of generations, 93 DEG C of liquefier is flashed to 58-62 DEG C of generation
Indirect steam introduce evaporator；
Liquefaction feed liquid after flashing three times enters spiral heat exchanger, and liquefaction feed liquid is expected with the saccharified liquid after slagging-off
Expect heat exchange, liquefaction feed liquid achievees the purpose that cooling, and saccharified liquid reaches the requirement of heating after removing the gred；
Flash distillation waste vapour is collected to six effect falling film evaporators, and the evaporation and concentration of chromatographic isolation raffinate is used for；The BX of liquefier
It is 32.5%~34.0%；DE values are 11~14, filtering velocity≤3.5min/20ml, and iodine examination is iodine true qualities.
Preferably, the step (3) is realized by the processing unit that feeds, and the charging processing unit includes pH tune before saccharification
Save tank (1), saccharification feed pump (2), enzyme injector (3), carbohydrase measuring tank (4) and saccharifying tank (6), pH tune before the saccharification
The discharge port of section tank (1) is connect by pipeline with the import of saccharification feed pump (2), and the outlet of the saccharification feed pump (2) passes through
Pipeline is connect with the feed(raw material)inlet of enzyme injector (3), and the outlet of the enzyme injector (3) passes through pipeline and saccharifying tank (6)
Feed inlet connection, the carbohydrase import that the discharge port of the carbohydrase measuring tank (4) passes through pipeline and enzyme injector (3) connects
It connects；The carbohydrase measuring tank (4) is transparent organic glass measuring tank；The enzyme injector (3) and saccharifying tank (6) it
Between be provided with saccharification maintain coil pipe (5)；The saccharification maintains coil pipe (5) to be made of the coil pipe connection of different tube diameters；The saccharification
Preceding pH is adjusted and is both provided with solenoid valve on the pipeline between tank (1), saccharification feed pump (2), enzyme injector (3), saccharifying tank (6)
(7), it is provided with solenoid valve on the pipeline between the carbohydrase measuring tank (4) and enzyme injector (3)；It further include control system
System, the control system includes controller and control panel, and the controller and control panel electrically connect, the solenoid valve, sugar
Change feed pump (2), enzyme injector (3) and carbohydrase measuring tank (4) to electrically connect with the controller.
Preferably, plate heat exchanger is increased in step (4) decoloration, realizes the material of liquefier and saccharified liquid to be decolourized
Expect heat exchange.
Preferably, the step (5) washes technique using the cloudy column string of sun.
High-purity saccharified liquid of 99.50% or more DX values can be directly prepared by the application, the application is using the cloudy column string of sun
Wash the generation that technique avoids fructose in operation；Ion-exchange charging is reduced using sugared pattern on flow step because of discharge system wave
The dynamic influence to concentration, conductance, coloration, pH value；Using across column operational mode, in the case where not stopping production, can to resin into
The abnormal conditions such as row outside backwash and processing cylinder, ensure that the stability of system.
Description of the drawings
Fig. 1 is the application process flow chart；
Fig. 2 the embodiment of the present application charging processing device structure diagram；
Fig. 3 is that the secondary liquefaction of the embodiment of the present application maintains apparatus structure schematic diagram；
In figure, 1, pH adjusts tank before saccharification, 2, saccharification feed pump, 3, enzyme injector, 4, carbohydrase measuring tank, 5, sugar
Change and maintains coil pipe, 6, saccharifying tank, 7, solenoid valve；
11, Jet liquefier, 12, coil pipe, 13, flash vessel, 14, solenoid valve, 15, DCS control systems, 16, steam pipe
Road, 17, condensed water discharge outlet, 18,19, liquefier entrances of pressure-control valve, 20, sewage draining exit, 21, pipe joint.
Specific implementation mode
Embodiment 1
A kind of new process of purification saccharified liquid, steps are as follows, and (1) sizes mixing：With water by corn starch milk wave in tank of sizing mixing
U.S. degree is adjusted to 17 ° of ± 0.5B é, rear that the Na that mass fraction is 5-10% is added2CO3PH in solution to tank of sizing mixing is 5.5~6.0,
The starch milk mixed up in tank of sizing mixing is got in material feeding jar afterwards；
(2) it liquefies：Liquefaction workshop section uses the techniques of 2 injection 4 flash distillations of liquefaction, and primary injection liquefaction addition three/
One α-amylase, 110 DEG C of temperature simultaneously maintain 1 minute, and then flash distillation is cooled to 95 DEG C and reacts 20 minutes；Secondary injection liquefies starch
Breast is warming up to 135 DEG C and maintains 15 seconds, and then flash distillation cools to 93 DEG C and adds remaining 2/3rds α-amylases, reacts 90 minutes, so
Liquefier cools the temperature to 58~62 DEG C by flash distillation and four flash distillations three times afterwards, at this time the mass concentration of liquefier for 30~
35%；
(3) it is saccharified：It is 4.2~4.5 that dilute hydrochloric acid is added after liquefying to step (2) in feed liquid and adjusts the pH value of feed liquid, after with
Compounded saccharifying enzyme, saccharification period 42-54h is added in the ratio of 0.40~0.50kg/T (butt)；
(4) it decolourizes：It is decolourized using seed activity charcoal post, charcoal post blade diameter length ratio is 8,50~60 DEG C of bleaching temperature, feed flow rate 2
~4BV/h；
(5) ion-exchange：Using the continuous ion-exchange equipment of fixed bed, 50~55 DEG C of ion-exchange temperature, 2~4BV/h of flow velocity；
(6) chromatography front evaporator concentrates：Chromatography front evaporator concentration section is using six effect falling film evaporator equipment, driving drop
The steam of film evaporator is the steel-making waste vapour of steel plant of company of this group, temperature discharge at 80~85 DEG C, after concentration BX55~
65%.
(7) chromatographic isolation：Advanced technology is combined using sequential type simulated moving bed chromatography piece-rate system and high-temperature material film；
55~60 DEG C of chromatographic isolation temperature, material-water ratio 1.5:1~2.0:1, charging rate 2BV/h.
Preferably, the starch milk of the step (2) enters a spray coil pipe after once spraying liquefaction, by full flashing
Enter secondary injection afterwards to liquefy, liquefy by secondary injection and enter secondary liquefaction maintenance device, the secondary liquefaction maintains device
Including by the sequentially connected Jet liquefier of pipeline (11), coil pipe (12) and flash vessel (13), the coil pipe (12) is by difference
The coil pipe connection composition of caliber；The coil pipe (12) is by three kinds of coil pipe connection groups that caliber DN is respectively 125/150/200mm
At；The coil pipe (12) is connected by three kinds of coil pipes that caliber DN is respectively 125/150/200mm successively along the direction of Flow of Goods and Materials
Composition；Pipeline between the Jet liquefier (11) and coil pipe (12) is made of the pipeline connection of different tube diameters；The injection
Pipeline between liquefier (11) and coil pipe (12) is respectively successively 100/125/ by caliber DN along the direction of Flow of Goods and Materials
Three kinds of pipelines connection composition of 150mm；The caliber DN of pipeline between the coil pipe (12) and flash vessel (10) is 125mm；Institute
The total length for stating coil pipe (12) is 208 meters；It is additionally provided with DCS control systems；It is set between the coil pipe (12) and flash vessel (13)
It is equipped with DCS control systems.
Preferably, the DCS control systems pass through EtherNet/IP communication instrument Ring
When realizing real-time displays, alarm and the unlatchings of valve such as start and stop, speed control and the electric current pumped, power, frequency, state, operation
Between；
The liquefier that temperature is 110 DEG C after primary injection liquefaction is flashed to the indirect steam of 95 DEG C of generations, secondary injection liquid
The liquefier that temperature is 135 DEG C after change is flashed to the indirect steam of 93 DEG C of generations, 93 DEG C of liquefier is flashed to 58-62 DEG C of generation
Indirect steam introduce evaporator；
Liquefaction feed liquid after flashing three times enters spiral heat exchanger, and liquefaction feed liquid is expected with the saccharified liquid after slagging-off
Expect heat exchange, liquefaction feed liquid achievees the purpose that cooling, and saccharified liquid reaches the requirement of heating after removing the gred；
Flash distillation waste vapour is collected to six effect falling film evaporators, and the evaporation and concentration of chromatographic isolation raffinate is used for；The BX of liquefier
It is 32.5%~34.0%；DE values are 11~14, filtering velocity≤3.5min/20ml, and iodine examination is iodine true qualities.
Preferably, the step (3) is realized by the processing unit that feeds, and the charging processing unit includes pH tune before saccharification
Save tank (1), saccharification feed pump (2), enzyme injector (3), carbohydrase measuring tank (4) and saccharifying tank (6), pH tune before the saccharification
The discharge port of section tank (1) is connect by pipeline with the import of saccharification feed pump (2), and the outlet of the saccharification feed pump (2) passes through
Pipeline is connect with the feed(raw material)inlet of enzyme injector (3), and the outlet of the enzyme injector (3) passes through pipeline and saccharifying tank (6)
Feed inlet connection, the carbohydrase import that the discharge port of the carbohydrase measuring tank (4) passes through pipeline and enzyme injector (3) connects
It connects；The carbohydrase measuring tank (4) is transparent organic glass measuring tank；The enzyme injector (3) and saccharifying tank (6) it
Between be provided with saccharification maintain coil pipe (5)；The saccharification maintains coil pipe (5) to be made of the coil pipe connection of different tube diameters；The saccharification
Preceding pH is adjusted and is both provided with solenoid valve on the pipeline between tank (1), saccharification feed pump (2), enzyme injector (3), saccharifying tank (6)
(7), it is provided with solenoid valve on the pipeline between the carbohydrase measuring tank (4) and enzyme injector (3)；It further include control system
System, the control system includes controller and control panel, and the controller and control panel electrically connect, the solenoid valve, sugar
Change feed pump (2), enzyme injector (3) and carbohydrase measuring tank (4) to electrically connect with the controller.
Preferably, plate heat exchanger is increased in step (4) decoloration, realizes the material of liquefier and saccharified liquid to be decolourized
Expect heat exchange.
Preferably, the step (5) washes technique using the cloudy column string of sun.
When in use, the material that pH is adjusted in tank before being saccharified passes through original to the processing unit that feeds under the action of being saccharified feed pump
Expect that entrance enters in enzyme injector, the carbohydrase in carbohydrase measuring tank is entered by carbohydrase import in enzyme injector,
Enzyme injector allows saccharification charging to come into full contact with and be uniformly mixed with carbohydrase, and then mixed material is from enzyme spray
The outlet of emitter enters saccharification and maintains in coil pipe, maintains carbohydrase in coil pipe further to be mixed well with feed liquid in saccharification, finally
Into saccharifying tank.
Secondary liquefaction maintains device when in use, and one time liquefier is entered by pipeline in Jet liquefier, subsequently into
In coil pipe, subsequently into flash vessel, Jet liquefier is connect with jet chimney, and jet chimney is connect with vapour source, jet chimney
On be provided with condensed water discharge outlet, pressure-control valve is additionally provided on jet chimney, for controlling to adjust the pressure in jet chimney
Power.
Claims (6)
1. a kind of new process of purification saccharified liquid, which is characterized in that steps are as follows, and (1) sizes mixing：With water by corn in tank of sizing mixing
Starch milk Baume degrees is adjusted to 17 ° of ± 0.5B é, rear that the Na that mass fraction is 5-10% is added2CO3PH in solution to tank of sizing mixing is
5.5~6.0, after the starch milk mixed up in tank of sizing mixing is got in material feeding jar；
(2) it liquefies：Liquefaction workshop section uses the technique of 2 injection 4 flash distillations of liquefaction, primary injection liquefaction addition one third liquid
Change enzyme, 110 DEG C of temperature simultaneously maintains 1 minute, and then flash distillation is cooled to 95 DEG C and reacts 20 minutes；Secondary injection liquefies starch milk liter
Temperature maintains 15 seconds to 135 DEG C, and then flash distillation cools to 93 DEG C and adds remaining 2/3rds α-amylases, reacts 90 minutes, then liquid
Change liquid and cool the temperature to 58~62 DEG C by flash distillation and four flash distillations three times, the mass concentration of liquefier is 30~35% at this time；
(3) it is saccharified：It is 4.2~4.5 that dilute hydrochloric acid is added after liquefying to step (2) in feed liquid and adjusts the pH value of feed liquid, after with 0.40
Compounded saccharifying enzyme, saccharification period 42-54h is added in the ratio of~0.50kg/T (butt)；
(4) it decolourizes：It being decolourized using seed activity charcoal post, charcoal post blade diameter length ratio is 8,50~60 DEG C of bleaching temperature, feed flow rate 2~
4BV/h；
(5) ion-exchange：Using the continuous ion-exchange equipment of fixed bed, 50~55 DEG C of ion-exchange temperature, 2~4BV/h of flow velocity；
(6) chromatography front evaporator concentrates：Chromatography front evaporator concentration section is steamed using six effect falling film evaporator equipment, driving falling liquid film
The steam of hair device is the steel-making waste vapour of steel plant of company of this group, and temperature is at 80~85 DEG C, and discharge BX55~65% after concentration.
(7) chromatographic isolation：Advanced technology is combined using sequential type simulated moving bed chromatography piece-rate system and high-temperature material film；Chromatography
55~60 DEG C of separation temperature, material-water ratio 1.5:1~2.0:1, charging rate 2BV/h.
2. a kind of new process of purification saccharified liquid as described in claim 1, which is characterized in that the starch milk of the step (2) passes through
Enter a spray coil pipe after crossing primary injection liquefaction, entering secondary injection after full flashing liquefies, and liquefies by secondary injection
Device is maintained into secondary liquefaction, it includes passing through the sequentially connected Jet liquefier of pipeline that the secondary liquefaction, which maintains device,
(11), coil pipe (12) and flash vessel (13), the coil pipe (12) are made of the coil pipe connection of different tube diameters；The coil pipe (12) by
Caliber DN is respectively three kinds of coil pipes connection composition of 125/150/200mm；The coil pipe (12) along the direction of Flow of Goods and Materials successively
It is made of three kinds of coil pipes connection that caliber DN is respectively 125/150/200mm；The Jet liquefier (11) and coil pipe (12) it
Between pipeline by different tube diameters pipeline connection form；Pipeline between the Jet liquefier (11) and coil pipe (12) is along material
The direction of flowing is made of three kinds of pipelines connection that caliber DN is respectively 100/125/150mm successively；The coil pipe (12) and sudden strain of a muscle
The caliber DN of pipeline between steaming device (13) is 125mm；The total length of the coil pipe (12) is 208 meters；It is additionally provided with DCS controls
System；It is provided with DCS control systems between the coil pipe (12) and flash vessel (13).
3. a kind of new process of purification saccharified liquid as claimed in claim 2, which is characterized in that the DCS control systems pass through
EtherNet/IP communication instrument Ring realize start and stop, speed control and the electric current, power, frequency of pump
The real-time displays such as rate, state, alarm and the unlatching of valve, run time；
After the liquefier that temperature is 110 DEG C after primary injection liquefaction is flashed to the indirect steam of 95 DEG C of generations, secondary injection liquefaction
Temperature is that 135 DEG C of liquefier is flashed to the indirect steam of 93 DEG C of generations, 93 DEG C of liquefier is flashed to the two of 58-62 DEG C of generation
Secondary steam introduces evaporator；
Liquefaction feed liquid after flashing three times enters spiral heat exchanger, and liquefaction feed liquid carries out material material heat with the saccharified liquid after slagging-off
It exchanges, liquefaction feed liquid achievees the purpose that cooling, and saccharified liquid reaches the requirement of heating after removing the gred；
Flash distillation waste vapour is collected to six effect falling film evaporators, and the evaporation and concentration of chromatographic isolation raffinate is used for；The BX of liquefier is
32.5%~34.0%；DE values are 11~14, filtering velocity≤3.5min/20ml, and iodine examination is iodine true qualities.
4. as described in claim 1 it is a kind of purification saccharified liquid new process, which is characterized in that the step (3) by charging at
Manage device realize, the charging processing unit include saccharification before pH adjust tank (1), be saccharified feed pump (2), enzyme injector (3),
Carbohydrase measuring tank (4) and saccharifying tank (6), the discharge port of pH adjusting tanks (1) passes through pipeline and saccharification feed pump before the saccharification
(2) import connection, the outlet of the saccharification feed pump (2) are connect by pipeline with the feed(raw material)inlet of enzyme injector (3), institute
The outlet for stating enzyme injector (3) is connect by pipeline with the feed inlet of saccharifying tank (6), and carbohydrase measuring tank (4) go out
Material mouth is connect by pipeline with the carbohydrase import of enzyme injector (3)；The carbohydrase measuring tank (4) is transparent organic glass
Glass measuring tank；It is provided with saccharification between the enzyme injector (3) and saccharifying tank (6) and maintains coil pipe (5)；The saccharification maintains disk
Pipe (5) is made of the coil pipe connection of different tube diameters；PH adjusts tank (1), saccharification feed pump (2), enzyme injector before the saccharification
(3), solenoid valve (7), the carbohydrase measuring tank (4) and enzyme injector (3) are both provided on the pipeline between saccharifying tank (6)
Between pipeline on be provided with solenoid valve；Further include control system, the control system includes controller and control panel, described
Controller and control panel electrically connect, the solenoid valve, saccharification feed pump (2), enzyme injector (3) and carbohydrase measuring tank
(4) it is electrically connected with the controller.
5. a kind of new process of purification saccharified liquid as described in claim 1, which is characterized in that increase in step (4) decoloration
Plate heat exchanger realizes the material material heat exchange of liquefier and saccharified liquid to be decolourized.
6. a kind of new process of purification saccharified liquid as described in claim 1, which is characterized in that the step (5) is using the cloudy column of sun
String washes technique.
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| JP2005087141A (en) * | 2003-09-19 | 2005-04-07 | Nippon Rensui Co Ltd | Apparatus for purifying sugar syrup and sugar syrup purifying method |
| CN1928121A (en) * | 2006-09-20 | 2007-03-14 | 山东西王糖业有限公司 | Method of extracting high-purity glucose from saccharified glucose syrup |
| CN201668979U (en) * | 2009-12-31 | 2010-12-15 | 西安航天华威化工生物工程有限公司 | Sequential type simulated moving bed chromatography purification device |
| CN102586492A (en) * | 2011-12-31 | 2012-07-18 | 三达膜科技（厦门）有限公司 | Method for removing impurities from saccharification solution in glucose production process |
| CN206289257U (en) * | 2016-10-26 | 2017-06-30 | 山东百盛生物科技有限公司 | A kind of full-automatic continuous production Glucose Liquid system |
| CN107130007A (en) * | 2017-06-23 | 2017-09-05 | 安徽万德生物科技有限公司 | A kind of starch syrup production technology |
| 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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