CN109761434A - A kind of combined technical method for starch hydrolyzate desalination - Google Patents
A kind of combined technical method for starch hydrolyzate desalination Download PDFInfo
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- CN109761434A CN109761434A CN201910237174.2A CN201910237174A CN109761434A CN 109761434 A CN109761434 A CN 109761434A CN 201910237174 A CN201910237174 A CN 201910237174A CN 109761434 A CN109761434 A CN 109761434A
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- 238000000034 method Methods 0.000 title claims abstract description 69
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- 238000001816 cooling Methods 0.000 claims description 10
- 102000004190 Enzymes Human genes 0.000 claims description 9
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- 102000004169 proteins and genes Human genes 0.000 claims description 9
- 108090000623 proteins and genes Proteins 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 8
- 230000008020 evaporation Effects 0.000 claims description 8
- 230000000813 microbial effect Effects 0.000 claims description 8
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Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention provides a kind of combined technical methods for starch hydrolyzate desalination, the described method comprises the following steps: starch hydrolyzate successively being carried out secondary filter, ultrafiltration, obtains ultrafiltration fresh water and ultrafiltration concentrated water；Obtained ultrafiltration fresh water is subjected to electrolemma desalination, obtains primary desalination starch hydrolyzate and strong brine；Obtained primary desalination starch hydrolyzate is subjected to ion exchange desalination again, obtains the starch hydrolyzate of advanced desalination.The present invention can make the salt rejection rate of starch hydrolyzate reach 80% or more by the organic assembling and synergistic effect of different desalinating process, especially electrolemma desalination, then finally make the conductivity of starch hydrolyzate not higher than 5 μ S/cm by ion exchange desalination；The method can either significantly slow fouling membrane, and can greatly extend the period of resin regeneration, reduce the acid and alkali consumption amount and operating cost for being used for resin regeneration, desalting processing suitable for separate sources starch hydrolyzate, required low energy consumption, and stability is high, applied widely.
Description
Technical field
The invention belongs to carbohydrate desalting technology fields, are related to a kind of combined technical method for starch hydrolyzate desalination.
Background technique
With the fast development of glucose industry, the scale and production capacity of starch sugar enterprise constantly expand, and have become agricultural
One of industrialization and the important channel of further processing of grains.Currently, about 1100~12,000,000 tons of China's starch sugar annual output, desalination work
Skill is that purified starch syrup is made through ion exchange resin desalination using traditional male-female multipole ion exchange method.
Since ion exchange resin adsorption saturation capacity is limited, need through using softened water frequently with dilute hydrochloric acid and the regeneration of low concentration caustic soda
It rinses, the wash water of generation causes waste water treatmentntrol difficult containing the sodium chloride of higher concentration as sewage discharge, while in sewage；
In addition, ion exchange resin service life is limited, it is also desirable to which periodic replacement or partial replacement, operating cost is big, and spent resin
Processing is difficult.
Currently, about the existing many research reports of starch hydrolyzate desalinating process.Wang En great and Shao Guangwu (Liaoning chemical industry,
2000,29 (4): 242-246) application of the ion exchange resin in corn starch sugar production has been investigated, show to hand over by ion
Starch hydrolyzate decoloration, desalination etc. may be implemented in the process of changing.Li Haibo etc. (food science and technology, 2007,5:65-68) has investigated starch
The research and application of new process in sugar industry, the ion exchange system that starch sugar desalination new process uses is by two sets of cation exchanges
Resin column, two sets of anion-exchange resin columns, two sets of mixture iron exchange resin compositions.State of Zhao's will etc. (grain and grease,
2007,10:4-8) domestic and international starch saccharification processes and key technology are reported, it is indicated that at present both at home and abroad substantially using tradition
Ion exchange carries out starch sugar refining, removes inorganic salts, amino acid, organic acid etc. in liquid glucose.However, traditional starch sugar desalination
Technique not only needs to consume a large amount of acid, alkali and water, while generating a large amount of high concentrated organic wastewaters, is unfavorable for starch sugar industry
Clean manufacturing, therefore it is badly in need of research and development starch sugar desalination process for cleanly preparing.
It is a kind of new desalination process using the salinity in electroosmose process removing liquid glucose, has some research reports.
202803120 U of CN discloses a kind of electrodialysis plant system for syrup desalination, and described device system includes pre-treatment dress
Set system, electrodialysis plant system and cleaning device system, the desalting refinement for syrup feed liquid.102492782 A of CN is disclosed
It is a kind of using method electrodialysis removing syrup salinity and produce glucose syrup, its main feature is that will divide in proportion to desalination syrup
At two parts, the two sides of the amberplex of electrodialysis plant are respectively enterd, the ion under electric field action in the syrup of side turns
The other side is moved on to, which obtains desalination syrup, but does not handle the salt heavy syrup of the other side, causes the very big of sugar
Loss.105771663 A of CN discloses a kind of electrodialysis plant and method for starch sugar hydrolyzate desalination, its main feature is that
By ion-exchanger being filled into light room come enhancing ion migration and improving desalting efficiency.However above-mentioned apparatus or method electric osmose
The problem for still having that desalting efficiency is relatively low, sugared loss late is high or fouling membrane is serious when desalination is analysed, it is limited and further applies.
In conclusion in view of the existing advantage and disadvantage of electric dialysis desalinating process, starch hydrolyzate desalinating process is still needed to electricity
Osmotic technique improves, and while improving its salt rejection rate, reduces carbohydrate loss, reduces fouling membrane.
Summary of the invention
In view of the problems of the existing technology, it is an object of the invention to propose a kind of group for starch hydrolyzate desalination
Process is closed, the method is by realize the level desalination of starch hydrolyzate, optimizing different desalinating process organic assemblings
Operating process makes treatment process at different levels play one's part to the full, and improves desalting efficiency, while reducing the loss and film dirt of starch sugar
Dye promotes the engineering application of starch hydrolyzate electrolemma desalting technology.
To achieve this purpose, the present invention adopts the following technical scheme:
The present invention provides a kind of combined technical methods for starch hydrolyzate desalination, and the method includes following steps
It is rapid:
(1) starch hydrolyzate is successively subjected to secondary filter, ultrafiltration, obtains ultrafiltration fresh water and ultrafiltration concentrated water；
(2) the ultrafiltration fresh water for obtaining step (1) carries out electrolemma desalination, obtains primary desalination starch hydrolyzate and dense salt
Water；
(3) the primary desalination starch hydrolyzate for obtaining step (2) carries out ion exchange desalination again, obtains advanced desalination
Starch hydrolyzate.
In the present invention, the starch hydrolyzate uses secondary filter-ultrafiltration-electrolemma desalination-ion exchange group technology
Starch sugar product is produced, wherein removing solid particle, water in starch hydrolyzate after secondary filter, the ultrafiltration double-filtration
Then the impurity such as dissolubility albumen, pigment, enzyme and microbial cells carry out electrolemma desalting processing, until obtaining the de- of suitable concentration
Salt starch hydrolyzate and strong brine, primary desalination starch hydrolyzate use ion-exchange advanced desalination again, reduce ion exchange
The discharge amount of the dosage of resin and resin regeneration elution waste water.Each step level of the method for the invention is clearly demarcated, cooperates with mutually,
The efficient desalination of starch hydrolyzate can be achieved, while carbohydrate loss is few, and it is at high cost to efficiently solve resin regeneration in the prior art
And the problem that wastewater discharge is big.
It is used as currently preferred technical solution below, but not as the limitation of technical solution provided by the invention, passes through
Following technical scheme can preferably reach and realize technical purpose and beneficial effect of the invention.
As currently preferred technical solution, step (1) starch hydrolyzate is to pass through pretreated Starch Hydrolysis
Liquid, the pretreatment include plate compression, centrifugation removing protein, active carbon decoloring etc., and wherein the source of starch hydrolyzate is mainly wrapped
Include corn, potato and sweet potato etc..
As currently preferred technical solution, the temperature of step (1) described starch hydrolyzate is 40~70 DEG C, such as 40
DEG C, 45 DEG C, 50 DEG C, 55 DEG C, 60 DEG C, 65 DEG C or 70 DEG C etc., it is not limited to cited numerical value, in the numberical range other
Unlisted numerical value is equally applicable；PH value is 3.0~5.0, such as 3.0,3.5,4.0,4.5 or 5.0 etc., it is not limited to institute
The numerical value enumerated, other interior unlisted numerical value of the numberical range are equally applicable.
Preferably, in step (1) described starch hydrolyzate starch sugared content be 25~35wt%, such as 25wt%,
27wt%, 28wt%, 30wt%, 32wt%, 34wt% or 35wt% etc., it is not limited to cited numerical value, the numerical value
Other unlisted numerical value are equally applicable in range.
In the present invention, the soluble inorganic salt for including in the starch hydrolyzate mainly has SO4 2-、Cl-、Na+、K+、Ca2+With
Mg2+It is 200~1000mg/L, such as 200mg/L, 300mg/L, 400mg/L, 500mg/L, 600mg/ Deng, inorganic salts total content
L, 800mg/L or 1000mg/L etc., it is not limited to cited numerical value, other interior unlisted numerical value of the numberical range are same
Sample is applicable in.
It preferably, further include water-solubility protein, organic acid, pigment, enzyme and microorganism in step (1) described starch hydrolyzate
Thallus.
As currently preferred technical solution, step (1) starch hydrolyzate carries out precision after heat exchange cooling again
Filtering.
Preferably, the heat exchange carries out in plate-frame heat exchanger, and plate-frame heat exchanger used uses food-grade stainless steel system
It is standby to obtain.
Preferably, the starch hydrolyzate cools down through heat exchange, and temperature is reduced to 10~40 DEG C, such as 10 DEG C, 15 DEG C, 20
DEG C, 25 DEG C, 30 DEG C, 35 DEG C or 40 DEG C etc., it is not limited to cited numerical value, other unlisted numbers in the numberical range
It is worth equally applicable.
As currently preferred technical solution, step (1) described secondary filter carries out in accurate filter.
Preferably, the accurate filter includes any one in bag filter, PP cotton filter or metallic filter.
In the present invention, the accurate filter is prepared using food-grade stainless steel, and main function components are filter core or filter bag.
Preferably, the filter core aperture size of the accurate filter be 1~10 μm, such as 1 μm, 2 μm, 3 μm, 4 μm, 5 μm,
6 μm, 8 μm or 10 μm etc., it is not limited to cited numerical value, other interior unlisted numerical value of the numberical range are equally suitable
With.
Preferably, the molecular cut off of ultrafiltration membrane used in step (1) described ultrafiltration be greater than 3000Da, such as 3000Da,
4000Da, 5000Da, 8000Da, 10000Da, 50000Da or 100000Da etc., it is not limited to cited numerical value, it should
Other unlisted numerical value are equally applicable in numberical range.
In the present invention, hyperfiltration membrane assembly used in the hyperfiltration treatment meets the requirement of food-grade material, and aperture size is full
The impurity such as most of water-solubility protein, enzyme, pigment and microbial cells in foot removal starch hydrolyzate.
As currently preferred technical solution, ultrafiltration concentrated water return step (1) and starch hydrolyzate that step (1) obtains
Mixing is handled again.
Preferably, the ultrafiltration concentrated water return step (1) carries out secondary filter again.
Preferably, the secondary filter carries out in accurate filter.
Preferably, the accurate filter includes any one in bag filter, PP cotton filter or metallic filter.
Preferably, the aperture size of the filter core of the accurate filter is 0.1~10 μm, such as 0.1 μm, 0.2 μm, 0.5 μ
M, 1 μm, 2 μm, 4 μm, 6 μm, 8 μm or 10 μm etc., it is not limited to cited numerical value, other are unlisted in the numberical range
Numerical value it is equally applicable.
In the present invention, a large amount of water-solubility protein, enzyme, pigment and microbial bacteria are contained in the concentrated water that obtains after hyperfiltration treatment
The impurity such as body are filtered, the essence again to cause the continuous accumulation of impurity after avoiding it from returning to feed well using accurate filter
The components such as the shell of close filter equally use food-grade stainless steel to prepare, and main function components are filter bag or filter core, filtering
It is miscellaneous that aperture size also needs to meet most of water-solubility protein, enzyme, pigment and microbial cells etc. in removal starch hydrolyzate
The requirement of matter.
As currently preferred technical solution, step (2) the electrolemma desalination carries out in electrodialysis plant.
Preferably, the electrodialysis plant uses low permeation ion exchange membrane.
In the present invention, selected low permeation ion exchange membrane includes anion-exchange membrane and cation-exchange membrane, described low
Permeable membrane is to be modified by changing film formula with technique or progress film surface, and starch hydrolyzate electric osmose can be effectively suppressed
The leakage sugar phenomenon occurred during analysis reduces sugar loss.
Preferably, step (2) the electrolemma desalination multistage is carried out continuously, such as two-stage, three-level, level Four, Pyatyi or six grades
Enter next stage circulation concentration Deng, the concentrated water that every grade of desalination obtains.
Preferably, after step (2) the electrolemma desalination, the salt rejection rate of starch hydrolyzate reaches 80% or more, such as 80%,
82%, 84%, 86%, 88%, 90%, 92%, 94% or 95% etc., it is not limited to cited numerical value, the numerical value model
Other unlisted numerical value are equally applicable in enclosing.
Preferably, the conductivity of step (2) described strong brine is not more than 8000 μ S/cm, such as 8000 μ S/cm, 7500 μ S/
Cm, 7000 μ S/cm, 6500 μ S/cm, 6000 μ S/cm, 5500 μ S/cm, 5000 μ S/cm or 4000 μ S/cm etc., but simultaneously not only limit
It is equally applicable in other unlisted numerical value in cited numerical value, the numberical range.
In the present invention, electrolemma desalination processes multistage is carried out continuously, in order to reduce the discharge amount of concentrated water, every grade of electrodialysis process
The concentrated water obtained afterwards enters next stage recycling, and salt content is continuously improved, but its salt content is unsuitable excessively high, otherwise can be due to
Salinity is excessively high and ion is caused reversely to spread, and increases the salt content in starch hydrolyzate instead, therefore strong brine needs to control
System in a certain range, is measured in the present invention with conductivity.
Preferably, step (2) described strong brine is discharged into Sewage Disposal and is focused on.
As currently preferred technical solution, step (3) ion exchange is carried out using ion exchange resin.
Preferably, the conductivity for the primary desalination starch hydrolyzate that step (2) obtains is 40~80 μ S/cm, such as 40 μ S/
Cm, 45 μ S/cm, 50 μ S/cm, 55 μ S/cm, 60 μ S/cm, 65 μ S/cm, 70 μ S/cm, 75 μ S/cm or 80 μ S/cm etc., but not
It is only limitted to cited numerical value, other unlisted numerical value are equally applicable in the numberical range.
In the present invention, the series of electrolemma desalination is also required to control, and the conductivity of gained starch hydrolyzate is unsuitable too low, no
It will cause the concentration gradient of film two sides salt is excessive, concentration polarization, which occurs, drastically reduces desalting efficiency instead.
Preferably, after step (3) described ion exchange, the conductivity of the starch hydrolyzate of advanced desalination is not more than 5 μ S/
Cm, such as 5 μ S/cm, 4 μ S/cm, 3 μ S/cm, 2 μ S/cm, 1 μ S/cm or 0.5 μ S/cm etc., it is not limited to cited number
Value, other interior unlisted numerical value of the numberical range are equally applicable.
In the present invention, according to the requirement of final starch hydrolyzate salt content, after electromembrane treatment using ion exchange resin into
Row advanced desalination can greatly extend resin regeneration compared with using ion exchange resin desalination completely in the prior art at this time
Period, when resin regeneration required acid, alkali amount can also reduce, reduce cost, while avoiding generating a large amount of high-concentration waste waters.
As currently preferred technical solution, after step (3) described ion exchange, the starch hydrolyzate of advanced desalination into
Row is concentrated by evaporation, and obtains starch sugar product.
Preferably, described be concentrated by evaporation uses multi-effect evaporator and/or MVR evaporator.
Preferably, the volume of the starch sugar product after the evaporation and concentration is starch hydrolyzate volume before being concentrated by evaporation
50% hereinafter, such as 50%, 45%, 40%, 35%, 30%, 25% or 20%, it is not limited to cited numerical value,
Other unlisted numerical value are equally applicable in the numberical range.
In the present invention, starch sugar concentration increases in starch hydrolyzate after evaporation and concentration, can after starch sugar concentration is concentrated 2 times
Starch sugar product is obtained, can get crystallization sugar product after removing 95% or more moisture.
As currently preferred technical solution, the described method comprises the following steps:
(1) its temperature will be made to be reduced to 10~40 DEG C from 40~70 DEG C by the heat exchange cooling of pretreated starch hydrolyzate,
Then secondary filter, ultrafiltration are successively carried out, obtains ultrafiltration fresh water and ultrafiltration concentrated water, the ultrafiltration concentrated water returns and starch hydrolyzate
Mixing is handled again；
(2) the ultrafiltration fresh water for obtaining step (1) carries out multistage continuous electrolemma desalination, the electric osmose in electrodialysis plant
Analysis apparatus uses low permeation ion exchange membrane, obtains primary desalination starch hydrolyzate and strong brine, the strong brine is discharged into dirt
Water treatment station is focused on；
(3) the desalination starch hydrolyzate for obtaining step (2) carries out ion exchange desalination again, obtained advanced desalination
The conductivity of starch hydrolyzate is not more than 5 μ S/cm, is then evaporated and is concentrated to get starch sugar product.
Compared with prior art, the present invention at least has the advantages that
(1) organic assembling and synergistic effect of the method for the invention by different desalinating process, especially electrolemma desalination
The salt rejection rate of starch hydrolyzate can be made to reach 80% or more, then finally make the electricity of starch hydrolyzate by ion exchange depth desalination
Conductance is not higher than 5 μ S/cm, realizes the efficient desalination of starch hydrolyzate；
(2) generation of fouling membrane phenomenon when the method for the invention can either significantly slow electromembrane treatment, and greatly prolong
The regeneration period of resin is grown, so as to largely save the acid, alkali and softened water etc. for resin regeneration, being greatly lowered can be high
The discharge amount of concentration organic wastewater；
(3) combination desalination process of the present invention is applicable to the desalting processing of separate sources starch hydrolyzate, has suitable
Answer the advantages that range is wide, impact resistance is strong, low energy consumption, required equipment scale is small and system run all right is high.
Detailed description of the invention
Fig. 1 is the process flow chart for the starch hydrolyzate desalination combined technical method that the embodiment of the present invention 1 provides.
Specific embodiment
In order to better illustrate the present invention, be easy to understand technical solution, below the present invention is described in more detail.But it is following
Embodiment be only simple example of the invention, represent or limit the scope of the present invention, the present invention protect model
It encloses and is subject to claims.
Specific embodiment of the invention part provides a kind of combined technical method for starch hydrolyzate desalination, described
Method the following steps are included:
(1) starch hydrolyzate is successively subjected to secondary filter, ultrafiltration, obtains ultrafiltration fresh water and ultrafiltration concentrated water；
(2) the ultrafiltration fresh water for obtaining step (1) carries out electrolemma desalination, obtains primary desalination starch hydrolyzate and dense salt
Water；
(3) the desalination starch hydrolyzate for obtaining step (2) carries out ion exchange desalination again, obtains the shallow lake of advanced desalination
Powder hydrolyzate.
The following are typical but non-limiting embodiments of the invention:
Embodiment 1:
Present embodiments provide a kind of combined technical method for starch hydrolyzate desalination, the process flow of the method
Figure is as shown in Figure 1, comprising the following steps:
(1) will be cooled down by pretreated cornstarch hydrolyzate using plate-frame heat exchanger, the cornstarch water
The temperature for solving liquid is 65 DEG C, pH value 3.7, and wherein starch sugared content is 31wt%, and inorganic salt content 450mg/L also contains
The impurity such as a small amount of water-solubility protein, organic acid, pigment, enzyme and microbial cells, the temperature of cornstarch hydrolyzate is after cooling
30℃；
(2) starch hydrolyzate after step (1) cooling is subjected to secondary filter, the secondary filter using accurate filter
The filter core aperture size of device is 5 μm, then carries out ultrafiltration, and the molecular cut off of hyperfiltration membrane assembly used is greater than 10000Da, obtains
Ultrafiltration fresh water and ultrafiltration concentrated water, the ultrafiltration concentrated water return step (1) filter removal ultrafiltration concentrated water using accurate filter again
In the impurity such as suspended matter after continue with, the filter core aperture size of accurate filter used is 2 μm；
(3) the ultrafiltration fresh water for obtaining step (2) carries out the continuous electrolemma desalination of Pyatyi, the electric osmose in electrodialysis plant
Analysis apparatus uses low permeation ion exchange membrane, obtains desalination starch hydrolyzate and recycles the strong brine being concentrated to get, until dense salt
When the conductivity of water is about 8000 μ S/cm, discharges it into Sewage Disposal and focused on；
(4) the desalination starch hydrolyzate for obtaining step (3) carries out advanced desalination using ion exchange resin, then uses
Multi-effect evaporator is concentrated, and obtains starch sugar product after 2 times of concentration.
In the present embodiment, after step (3) electrolemma desalination, for the salt rejection rate of starch hydrolyzate up to 85%, conductivity is down to 50 μ
S/cm or so, the conductivity of starch hydrolyzate is only 3 μ S/cm after step (4) ion exchange.
Embodiment 2:
A kind of combined technical method for starch hydrolyzate desalination is present embodiments provided, the method includes following steps
It is rapid:
(1) will be cooled down by pretreated cornstarch hydrolyzate using plate-frame heat exchanger, the cornstarch water
The temperature for solving liquid is 40 DEG C, pH value 3.0, and wherein starch sugared content is 25wt%, and inorganic salt content 200mg/L also contains
The impurity such as a small amount of water-solubility protein, organic acid, pigment, enzyme and microbial cells, the temperature of cornstarch hydrolyzate is after cooling
10℃；
(2) starch hydrolyzate after step (1) cooling is subjected to secondary filter, the secondary filter using accurate filter
The filter core aperture size of device is 8 μm, then carries out ultrafiltration, and the molecular cut off of hyperfiltration membrane assembly used is greater than 5000Da, obtains
Ultrafiltration fresh water and ultrafiltration concentrated water, the ultrafiltration concentrated water return step (1) filter removal ultrafiltration concentrated water using accurate filter again
In the impurity such as suspended matter after continue with, the filter core aperture size of accurate filter used is 4 μm；
(3) the ultrafiltration fresh water for obtaining step (2) carries out the continuous electrolemma desalination of three-level, the electric osmose in electrodialysis plant
Analysis apparatus uses low permeation ion exchange membrane, obtains desalination starch hydrolyzate and recycles the strong brine being concentrated to get, until dense salt
When the conductivity of water is about 6000 μ S/cm, discharges it into Sewage Disposal and focused on；
(4) the desalination starch hydrolyzate for obtaining step (3) carries out advanced desalination using ion exchange resin, then uses
MVR evaporator is concentrated, and obtains starch sugar product after 3 times of concentration.
In the present embodiment, after step (3) electrolemma desalination, for the salt rejection rate of starch hydrolyzate up to 90%, conductivity is down to 40 μ
S/cm or so, the conductivity of starch hydrolyzate is only 1.8 μ S/cm after step (4) ion exchange.
Embodiment 3:
A kind of combined technical method for starch hydrolyzate desalination is present embodiments provided, the method includes following steps
It is rapid:
(1) will be cooled down by pretreated cornstarch hydrolyzate using plate-frame heat exchanger, the cornstarch water
The temperature for solving liquid is 70 DEG C, pH value 5.0, and wherein starch sugared content is 35wt%, and inorganic salt content 1000mg/L also contains
The impurity such as a small amount of water-solubility protein, organic acid, pigment, enzyme and microbial cells, the temperature of cornstarch hydrolyzate is after cooling
40℃；
(2) starch hydrolyzate after step (1) cooling is subjected to secondary filter, the secondary filter using accurate filter
The filter core aperture size of device is 1 μm, then carries out ultrafiltration, and the molecular cut off of hyperfiltration membrane assembly used is greater than 3000Da, obtains
Ultrafiltration fresh water and ultrafiltration concentrated water, the ultrafiltration concentrated water return step (1) filter removal ultrafiltration concentrated water using accurate filter again
In the impurity such as suspended matter after continue with, the filter core aperture size of accurate filter used is 0.2 μm；
(3) the ultrafiltration fresh water for obtaining step (2) carries out six grades of continuous electrolemma desalinations, the electric osmose in electrodialysis plant
Analysis apparatus uses low permeation ion exchange membrane, obtains desalination starch hydrolyzate and recycles the strong brine being concentrated to get, until dense salt
When the conductivity of water is about 8000 μ S/cm, discharges it into Sewage Disposal and focused on；
(4) the desalination starch hydrolyzate for obtaining step (3) carries out advanced desalination using ion exchange resin, then uses
MVR evaporator is concentrated, and obtains starch sugar product after 1 times of concentration.
In the present embodiment, after step (3) electrolemma desalination, for the salt rejection rate of starch hydrolyzate up to 80%, conductivity is down to 80 μ
S/cm or so, the conductivity of starch hydrolyzate is only 5 μ S/cm after step (4) ion exchange.
Embodiment 4:
A kind of combined technical method for starch hydrolyzate desalination is present embodiments provided, the method includes following steps
It is rapid:
Step (1), step (2) and step (4) are same as Example 1；
(3) the ultrafiltration fresh water for obtaining step (2) carries out seven grades of continuous electrolemma desalinations, the electric osmose in electrodialysis plant
Analysis apparatus uses low permeation ion exchange membrane, obtains desalination starch hydrolyzate and recycles the strong brine being concentrated to get, is arranged
Enter Sewage Disposal to be focused on.
In the present embodiment, since electrolemma desalination processes progress series is on the high side, so that the conductivity of desalination starch hydrolyzate is low
In 40 μ S/cm, and the conductivity for recycling the strong brine being concentrated to get is higher than 8000 μ S/cm, the concentration and infiltration of permeable membrane two sides
Differing greatly for pressure, due to concentration polarization and reverse osmosis double action, can cause reduction and the unit desalination energy of desalting efficiency
Consumption increases.
Comparative example 1:
This comparative example provides a kind of method for starch hydrolyzate desalination, the described method comprises the following steps:
Step (1) is identical as step (1) in embodiment 1；
(2) starch hydrolyzate after step (1) cooling is entered into ion exchange resin bed and carries out desalination, respectively by level-one yin
Ion exchange resin bed, level-one cation exchange resin bed and level-one mixed bed are used in series, until ion exchange resin absorption is full
It is regenerated with rear using the acid, alkali and softened water of mass fraction 4.2wt%, until the desalination for reaching starch hydrolyzate is wanted
It asks.
In this comparative example, since only with ion exchange resin desalination, resin is easy adsorption saturation and needs often to regenerate,
And acid, alkali number needed for resin regeneration are larger, while can generate high concentrated organic wastewater, starch sugar product per ton generates waste water about
2.2 ton；Since dopant species are more in starch hydrolyzate, the load of ion exchange resin is larger, and regeneration frequently, can also be such that it makes
It is reduced with the service life.
The technical indicator of starch sugar hydrolyzate desalting processing identical in embodiment 1 and comparative example 1 is compared, it is known that reach
99% or more essentially identical salt rejection rate, acid, alkali and water consumption, sugar loss, wastewater discharge and COD content, power consumption etc.
Index is following (to produce per year in terms of 100,000 tons of starch sugars):
Acid consumption 412t/a (film process 112t/a, ion exchange 300t/a), quantity of alkali consumption 490t/a in embodiment 1
(film process 115t/a, ion exchange 375t/a), 10,000 m of water consumption tap water3/ a, softened water 1~20,000 m3/ a, and comparative example 1
Middle acid consumption 1200t/a, quantity of alkali consumption 1490t/a, 80,000 m of softened water3/a；
Sugared loss late is lower than 0.2% in embodiment 1, and sugared loss late reaches 1~2% in comparative example 1；
Wastewater discharge 5~70,000 m in embodiment 13/ a, waste water COD content < 5000mg/L, and waste water is arranged in comparative example 1
High-volume 220,000 m3/ a, 7000~10000mg/L of waste water COD content；
2~3kWh of starch sugar power consumption per ton in embodiment 1, and 3~4kWh of starch sugar power consumption per ton in comparative example 1.
It follows that organic assembling and synergistic effect of the present invention by different desalinating process, especially electrolemma desalination and
The cooperation of ion exchange desalination realizes the efficient desalination of starch hydrolyzate, finally makes the conductivity of starch hydrolyzate not higher than 5
μS/cm；The method can not only significantly slow fouling membrane, and largely save acid, alkali and the softened water for being used for resin regeneration
Deng high concentrated organic wastewater discharge amount is greatly lowered.It present invention can be suitably applied to the desalting processing of separate sources liquid glucose, energy consumption
Low, stability is strong, wide adaptation range.
The Applicant declares that the present invention is explained by the above embodiments method detailed of the invention, but the present invention not office
Be limited to above-mentioned method detailed, that is, do not mean that the invention must rely on the above detailed methods to implement.Technical field
Technical staff it will be clearly understood that any improvement in the present invention, equivalence replacement and auxiliary element to each raw material of product of the present invention
Addition, selection of concrete mode etc., all of which fall within the scope of protection and disclosure of the present invention.
Claims (10)
1. a kind of combined technical method for starch hydrolyzate desalination, which is characterized in that the described method comprises the following steps:
(1) starch hydrolyzate is successively subjected to secondary filter, ultrafiltration, obtains ultrafiltration fresh water and ultrafiltration concentrated water；
(2) the ultrafiltration fresh water for obtaining step (1) carries out electrolemma desalination, obtains primary desalination starch hydrolyzate and strong brine；
(3) the primary desalination starch hydrolyzate for obtaining step (2) carries out ion exchange desalination again, obtains the shallow lake of advanced desalination
Powder hydrolyzate.
2. combined technical method according to claim 1, which is characterized in that the temperature of step (1) described starch hydrolyzate
Be 3.0~5.0 for 40~70 DEG C, pH value, wherein starch sugared content be 25~35wt%, inorganic salt content be 200~
1000mg/L；
It preferably, further include water-solubility protein, organic acid, pigment, enzyme and microbial bacteria in step (1) described starch hydrolyzate
Body.
3. the combined technical method of starch hydrolyzate desalination according to claim 1 or 2, which is characterized in that step (1) institute
It states starch hydrolyzate and carries out secondary filter again after heat exchange cooling；
Preferably, the heat exchange carries out in plate-frame heat exchanger；
Preferably, the starch hydrolyzate cools down through heat exchange, and temperature is reduced to 10~40 DEG C.
4. the combined technical method of starch hydrolyzate desalination according to claim 1-3, which is characterized in that step
(1) secondary filter carries out in accurate filter；
Preferably, the accurate filter includes any one in bag filter, PP cotton filter or metallic filter；
Preferably, the filter core aperture size of the accurate filter is 1~10 μm.
5. the combined technical method of starch hydrolyzate desalination according to claim 1-4, which is characterized in that step
(1) molecular cut off of ultrafiltration membrane used in the ultrafiltration is greater than 3000Da.
6. the combined technical method of starch hydrolyzate desalination according to claim 1-5, which is characterized in that step
(1) the ultrafiltration concentrated water return step (1) obtained is handled again；
Preferably, the ultrafiltration concentrated water return step (1) carries out secondary filter again；
Preferably, the secondary filter carries out in accurate filter；
Preferably, the accurate filter includes any one in bag filter, PP cotton filter or metallic filter；
Preferably, the aperture size of the filter core of the accurate filter is 0.1~10 μm.
7. the combined technical method of starch hydrolyzate desalination according to claim 1-6, which is characterized in that step
(2) the electrolemma desalination carries out in electrodialysis plant；
Preferably, the electrodialysis plant uses low permeation ion exchange membrane；
Preferably, step (2) the electrolemma desalination multistage is carried out continuously, obtained concentrated water circulation concentration；
Preferably, after step (2) the electrolemma desalination, the salt rejection rate of starch hydrolyzate reaches 80% or more；
Preferably, the conductivity of step (2) described strong brine is not more than 8000 μ S/cm；
Preferably, it is focused on after step (2) the strong brine discharge.
8. the combined technical method of starch hydrolyzate desalination according to claim 1-7, which is characterized in that step
(3) ion exchange is carried out using ion exchange resin；
Preferably, the conductivity for the primary desalination starch hydrolyzate that step (2) obtains is 40~80 μ S/cm；
Preferably, after step (3) described ion exchange, the conductivity of the starch hydrolyzate of advanced desalination is not more than 5 μ S/cm.
9. the combined technical method of starch hydrolyzate desalination according to claim 1-8, which is characterized in that step
(3) after the ion exchange, the starch hydrolyzate of advanced desalination is evaporated concentration, obtains starch sugar product；
Preferably, described be concentrated by evaporation uses multi-effect evaporator and/or MVR evaporator；
Preferably, the volume of the starch sugar product after the evaporation and concentration be 50% of starch hydrolyzate volume before being concentrated by evaporation with
Under.
10. the combined technical method of -9 described in any item starch hydrolyzate desalinations according to claim 1, which is characterized in that institute
State method the following steps are included:
(1) starch hydrolyzate is exchanged heat and is cooled down, its temperature is made to be reduced to 10~40 DEG C from 40~70 DEG C, then successively carried out accurate
Filtering, ultrafiltration, obtain ultrafiltration fresh water and ultrafiltration concentrated water, and the ultrafiltration concentrated water return carries out secondary filter again；
(2) the ultrafiltration fresh water for obtaining step (1) carries out multistage continuous electrolemma desalination, the electrodialysis dress in electrodialysis plant
It sets using low permeation ion exchange membrane, primary desalination starch hydrolyzate and strong brine is obtained, after the strong brine discharge at concentration
Reason；
(3) the primary desalination starch hydrolyzate for obtaining step (2) carries out desalination again, the shallow lake of advanced desalination using ion exchange
The conductivity of powder hydrolyzate is not more than 5 μ S/cm, is then evaporated and is concentrated to get starch sugar product.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102492782A (en) * | 2011-12-16 | 2012-06-13 | 长春大成新资源集团有限公司 | Desalting method for syrup and production method for glucose syrup |
| CN105771663A (en) * | 2015-12-30 | 2016-07-20 | 中国科学院过程工程研究所 | Electrodialysis device and method for desalination of starch sugar hydrolysate |
| CN108676926A (en) * | 2018-06-01 | 2018-10-19 | 广西科技师范学院 | A kind of production method of white granulated sugar |
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2019
- 2019-03-27 CN CN201910237174.2A patent/CN109761434A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102492782A (en) * | 2011-12-16 | 2012-06-13 | 长春大成新资源集团有限公司 | Desalting method for syrup and production method for glucose syrup |
| CN105771663A (en) * | 2015-12-30 | 2016-07-20 | 中国科学院过程工程研究所 | Electrodialysis device and method for desalination of starch sugar hydrolysate |
| CN108676926A (en) * | 2018-06-01 | 2018-10-19 | 广西科技师范学院 | A kind of production method of white granulated sugar |
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| Title |
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| 质量技术监督行业职业技能鉴定指导中心: "《化学检验》", 30 September 2009, 北京：中国计量出版社 * |
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