CN106916864B - Method and system for making sugar - Google Patents
Method and system for making sugar Download PDFInfo
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Abstract
The invention relates to the field of sugar production, and discloses a method and a system for producing sugar, wherein the method comprises the steps of sequentially carrying out liquefaction, saccharification, decoloration and evaporation treatment on starch milk, and the method further comprises the following steps: the starch milk and the steam generated in the evaporation treatment process are subjected to primary heat exchange, and the starch milk subjected to primary heat exchange and the decolored material are subjected to secondary heat exchange, so that the temperature of the starch milk is increased. The method of the invention heats the starch milk twice by two times of heat exchange by utilizing the inherent heat in the sugar making process, improves the temperature of the starch milk before liquefaction, and thus reduces the using amount of steam during liquefaction.
Description
Technical Field
The invention relates to the field of sugar production, in particular to a method and a system for producing sugar.
Background
Corn starch is widely used as a raw material in corn deep processing industries such as feed, starch sugar and the like, and China is a large country for producing starch and starch sugar, wherein the annual yield of the starch sugar is over 600 million tons, and the production process mostly adopts a corn wet sugar making process. The wet corn sugar making process includes soaking corn grains in water, pulping, liquefying, saccharifying, decolorizing, evaporating and concentrating.
In the traditional sugar making process, a large amount of steam is needed to be used as a raw material for heating in the liquefaction process, and in winter, the temperature of the starch milk is only 20-25 ℃, and in summer, the temperature of the starch milk is 30-35 ℃, so that the steam consumption of the starch milk in the process of liquefaction in winter is greatly increased, and the cost of the sugar making process is increased.
Disclosure of Invention
The invention aims to reduce the cost of a sugar making process and provides a sugar making method and system.
In order to achieve the above object, the present invention provides a method for producing sugar, which comprises sequentially subjecting starch milk to liquefaction, saccharification, decolorization, and evaporation treatment, wherein the method further comprises: the starch milk and the steam generated in the evaporation treatment process are subjected to primary heat exchange, and the starch milk subjected to primary heat exchange and the decolored material are subjected to secondary heat exchange, so that the temperature of the starch milk is increased.
The invention also provides a system for producing sugar, which comprises a starch milk supply device, a liquefying device, a saccharifying device, a decoloring device and an evaporating device, the starch milk supply device is communicated with the liquefying device, the liquefying device is communicated with the saccharifying device, the saccharification device is communicated with the decolorization device, the decolorization device is communicated with the evaporation device, wherein the system also comprises a primary heat exchanger and a secondary heat exchanger, the primary heat exchanger is respectively connected with the material outlet of the starch milk supply device and the steam outlet of the evaporation device, is used for carrying out primary heat exchange between the starch milk provided by the starch milk supply device and the steam discharged by the evaporation device, the secondary heat exchanger is respectively connected with the material outlet of the primary heat exchanger and the material outlet of the decoloring device, the starch milk which is discharged by the primary heat exchanger and subjected to primary heat exchange is subjected to secondary heat exchange with the material discharged by the decoloring device.
The method of the invention heats the starch milk twice by two times of heat exchange by utilizing the inherent heat in the sugar making process, improves the temperature of the starch milk before liquefaction, and thus reduces the using amount of steam during liquefaction. By adopting the method, 0.03-0.04 ton of steam can be saved when 1 ton of starch milk (calculated by dry matter) is processed, and the cost can be saved by 44-59 ten thousand (the steam unit price is 210 yuan/ton) per year according to 7 ten thousand tons of starch milk (calculated by dry matter) per year of processing amount.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
FIG. 1 is a preferred embodiment of a sugar manufacturing system according to the present invention.
In the figure: a starch milk supply device 1, a primary heat exchanger 2, a secondary heat exchanger 3, a liquefying device 4, a saccharifying device 5, a decolorizing device 6, an ion exchange device 7, an evaporating device 8 and a condensed water tank 9.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The invention provides a method for preparing sugar, which comprises the steps of sequentially carrying out liquefaction, saccharification, decolorization and evaporation treatment on starch milk, wherein the method further comprises the following steps: the starch milk and the steam generated in the evaporation treatment process are subjected to primary heat exchange, and the starch milk subjected to primary heat exchange and the decolored material are subjected to secondary heat exchange, so that the temperature of the starch milk is increased.
According to a preferred embodiment of the invention, the primary heat exchange process raises the temperature of the starch milk by 10-20 ℃; and/or the temperature of the starch milk is increased by 15-20 ℃ in the secondary heat exchange process.
The heat exchange with the steam generated in the evaporation treatment process and the decolored material is carried out in sequence, so that the temperature of the starch milk can be increased by 25-40 ℃, and meanwhile, the decolored material after the heat exchange can be cooled to the required temperature, such as 45-50 ℃, so as to be convenient for subsequent operations, such as ion exchange treatment.
In a preferred embodiment of the invention, the steam generated during the evaporation process is condensed (to form condensed water) and then subjected to a primary heat exchange with the starch milk. The condensed water of the steam and the starch milk are subjected to primary heat exchange, so that the defect that the steam is difficult to enter a primary heat exchange process due to the negative pressure of the steam when the steam is directly used for primary heat exchange can be avoided.
In the present invention, there is no particular requirement for the specific operation of the heat exchange as long as heat can be transferred in the above manner. In general, the heat exchange can be effected by means of heat exchangers, which can be any of the commonly used heat exchangers and are commercially available, for example, the spiral flat tube heat exchanger of Brown corporation, usa.
In the present invention, the starch milk may be prepared from a starchy material, and various conventional methods known to those skilled in the art may be used to obtain the starch milk, for example, by pulverizing the starchy material and mixing the pulverized product with water. Wherein, the concentration of the starch milk is not particularly limited, and the dry matter content in the starch milk is preferably 35 to 40 weight percent.
According to the invention, the starchy material can be various starchy materials which are known in the art and can be used for enzymolysis and fermentation, and can be selected from one or more of corn, potatoes, wheat and sorghum.
In the present invention, the conditions for the liquefaction, saccharification and decolorization are not particularly limited, and may be conventionally selected in the art. Preferably, the liquefaction conditions include: the liquefaction temperature is 110-120 ℃, and the liquefaction time is 2-2.5 h; and/or, the conditions of saccharification comprise: the saccharification temperature is 60-70 ℃, and the saccharification time is 36-48 h; and/or, the decolorizing conditions comprise: the decolorizing temperature is 65-75 deg.C, and decolorizing time is 15-30 min; and/or, the conditions of the evaporation treatment include: the temperature of the evaporation treatment is 100-110 ℃.
In the present invention, the time for the evaporation is not particularly limited, but preferably, the time for the evaporation is such that the volume of the material after the evaporation treatment is 0.6 to 0.7 times the volume of the material before the evaporation treatment.
In the present invention, the liquefaction may be carried out in a conventional manner, for example, the starch slurry may be liquefied by contacting a mixture of starch milk and amylase with steam, the amount of amylase used for the liquefaction being conventionally selected in the art, preferably 400-450g of amylase per ton of dry matter in starch milk, wherein the amylase used for the liquefaction may be an amylase conventionally used in the art, such as α -amylase, β -amylase and isoamylase, or a high temperature resistant amylase.
In the present invention, the saccharification process is performed to convert the starch milk into monosaccharide as much as possible. In the present invention, the saccharification is carried out in a conventional manner, for example, the way of saccharification may be: adding the obtained liquefied liquid into a saccharification device, adding saccharifying enzyme and stirring.
The saccharifying enzyme acts on non-reducing end of starch molecule, takes glucose as unit, and acts on α -1, 4-glycosidic bond in starch molecule to generate glucose, the product of saccharifying enzyme acting on amylopectin contains glucose and oligosaccharide with α -1, 6-glycosidic bond, and the product of saccharifying enzyme acting on amylose is almost all glucose.
In the invention, the specific operation of decoloring can be a conventional decoloring method adopted in the sugar making process, and if the primary decoloring effect is not good, secondary decoloring can be carried out, and a person skilled in the art can select and judge the conventional decoloring method, so that the detailed description is omitted.
In the present invention, the evaporation process is a concentration process of the material, and can be performed by a conventional method in the art, which is not described herein again.
According to a preferred embodiment of the present invention, the method may further include: after the decolorization and before the evaporation treatment, subjecting the material to an ion exchange treatment; the ion exchange treatment comprises a regeneration process, and the condensate water obtained after the heat exchange between the steam generated in the evaporation treatment process and the starch milk is used for eluting the regenerant in the regeneration process.
The ion exchange treatment process generally adopts ion exchange resin. The sugar solution still contains part of inorganic salt and organic impurities after being decolored, so that the sugar solution is refined by adopting ion exchange resin to play roles of ion exchange and adsorption. The ion exchange resin has a strong ability to remove proteins, amino acids, hydroxymethylfurfural, colored substances, and the like, compared with activated carbon. The ion exchange treatment includes a regeneration process, the regeneration process is the regeneration of ion exchange resin, generally, acid or alkali is used as a regenerant to perform the regeneration treatment on the ion exchange resin, and the specific implementation mode is a conventional choice in the field and is not described herein again.
As shown in fig. 1, the present invention further provides a sugar manufacturing system, which comprises a starch milk supply device 1, a liquefaction device 4, a saccharification device 5, a decolorization device 6 and an evaporation device 8, wherein the starch milk supply device 1 is communicated with the liquefaction device 4, the liquefaction device 4 is communicated with the saccharification device 5, the saccharification device 5 is communicated with the decolorization device 6, and the decolorization device 6 is communicated with the evaporation device 8, the sugar manufacturing system is characterized in that the system further comprises a primary heat exchanger 2 and a secondary heat exchanger 3, the primary heat exchanger 2 is respectively connected with a material outlet of the starch milk supply device 1 and a steam outlet of the evaporation device 8, and is used for performing primary heat exchange between the starch milk supplied by the starch milk supply device 1 and the steam discharged by the evaporation device 8, the secondary heat exchanger 3 is respectively connected with a material outlet of the primary heat exchanger 2 and a material outlet of the decolorization device 6, used for carrying out secondary heat exchange on the starch milk which is discharged by the primary heat exchanger 2 and is subjected to primary heat exchange and the material discharged by the decolorization device 6.
According to a preferred embodiment of the invention, the system further comprises an ion exchange device 7, said ion exchange device 7 being located on the line between the secondary heat exchanger 3 and the evaporation device 8.
In the invention, in order to fully utilize water resources and save energy consumption, the condensed water outlet of the primary heat exchanger 2 is communicated with the ion exchange device 7. And the condensed water discharged from the condensed water outlet is used for eluting the regenerant used in the ion exchange regeneration process.
According to another preferred embodiment of the invention, the system further comprises a condensate tank 9, said condensate tank 9 being located on the line between the evaporation device 8 and the primary heat exchanger 2. The condensed water tank 9 is used for condensing the steam discharged by the evaporation device 8, and the condensed water formed after the steam condensation is used for carrying out primary heat exchange with the starch milk.
The present invention will be described in detail below by way of examples. The temperatures in the following examples and comparative examples (except for the temperature change caused by heat exchange) were provided by consuming steam.
In the following examples and comparative examples, the starchy material used was corn material having an average particle size of 10 μm obtained by pulverizing corn (moisture content of 13 wt%); the heat exchange is carried out by means of a tube and tube heat exchanger (Brown company, USA), and the specific operation is shown in the specification; the decoloring step is as follows: 0.5g/100g of activated carbon (specific surface area 1000 m) of sugar solution was added to the sugar solution2The grain size is less than 50 mu m), stirring in a water bath, decoloring and filtering to remove active carbon; cation exchange resin used for ion exchange is 732 strong-acid cation exchange resin, anion exchange resin is D311 weak-base anion exchange resin, feed liquid sequentially passes through an ion exchange resin filter bed formed by connecting cation-anion-cation-anion in series, and the flow rate of the feed liquid is controlled to be 2 BV/h; the light transmittance is measured according to standard QB/T2319-1997 by using a spectrum SP-752 ultraviolet-visible spectrophotometer (Shanghai spectrometer Co., Ltd.), and the higher the light transmittance is, the lower the turbidity of the sugar solution is, and the purer the sugar solution is.
Example 1
Adding water into starchy raw materials to prepare starch milk with the dry matter content of 35 wt% (at the temperature of 25 ℃), and sequentially carrying out liquefaction, saccharification, decolorization, ion exchange and evaporation treatment, wherein the specific operation is as follows:
performing primary heat exchange on steam generated in the evaporation treatment process (forming condensed water, the temperature is 58 ℃, and the flow is 25 tons/hour) and starch milk, wherein the temperature of the starch milk subjected to the primary heat exchange is 35 ℃, performing secondary heat exchange on the starch milk subjected to the primary heat exchange and a decolored material (the temperature is 65 ℃, and the flow is 41 tons/hour), and the temperature of the starch milk subjected to the secondary heat exchange is 55 ℃;
adding calcium hydroxide into the starch milk subjected to secondary heat exchange to adjust the pH value to 6.0, adding α -amylase (adding α -amylase of 420g per ton of dry matter), stirring uniformly, pumping into a liquefying device by a pump, wherein the liquefying temperature is 110 ℃, and the liquefying time is 2.5 hours;
adding liquefied liquid into saccharifying device, adding saccharifying enzyme (4060 composite saccharifying enzyme produced by Jenenaceae, 550g saccharifying enzyme is added per ton dry matter) at 60 deg.C and pH of 4.4, and stirring for 48 hr;
the saccharified liquid obtained after saccharification is contacted with activated carbon for decolorization (the temperature for decolorization is 65 ℃ and the time for decolorization is 30min), the decolorized material and the starch milk subjected to primary heat exchange are subjected to secondary heat exchange, the temperature of the decolorized material subjected to secondary heat exchange is 47 ℃, the decolorized material subjected to secondary heat exchange is subjected to ion exchange, the material subjected to ion exchange is subjected to evaporation treatment (the temperature is 100 ℃), steam formed by the evaporation treatment is condensed and then subjected to primary heat exchange with the starch milk, and condensed water (the temperature is 45 ℃) discharged after the primary heat exchange enters an ion exchange process for cleaning ion exchange resin. When the volume of the material after evaporation treatment is 0.6 times of the volume of the material before evaporation treatment, the evaporation is stopped to obtain sugar liquid, and the light transmittance of the sugar liquid is 99%.
In this process, steam consumption was 0.32 ton/ton starch milk (dry matter basis).
Example 2
Adding water into starchy raw materials to prepare starch milk with the dry matter content of 40 wt% (at the temperature of 25 ℃), and sequentially carrying out liquefaction, saccharification, decolorization, ion exchange and evaporation treatment, wherein the specific operation is as follows:
performing primary heat exchange on steam generated in the evaporation treatment process (forming condensed water, the temperature is 65 ℃, and the flow rate is 26 tons/hour) and starch milk, wherein the temperature of the starch milk subjected to the primary heat exchange is 45 ℃, performing secondary heat exchange on the starch milk subjected to the primary heat exchange and a decolored material (the temperature is 75 ℃, and the flow rate is 45 tons/hour), and the temperature of the starch milk subjected to the secondary heat exchange is 60 ℃;
adding calcium hydroxide into starch milk subjected to secondary heat exchange to adjust pH to 6.0, adding α -amylase (adding α -amylase of 420g per ton of dry matter), stirring uniformly, pumping into a liquefying device by a pump, wherein the liquefying temperature is 120 ℃, and the liquefying time is 2 h;
adding liquefied liquid into saccharifying device, adding saccharifying enzyme (4060 composite saccharifying enzyme produced by Jenenaceae, 550g saccharifying enzyme is added per ton dry matter) at 70 deg.C and pH of 4.4, and stirring for 36 hr;
the saccharified liquid obtained after saccharification is contacted with activated carbon for decolorization (the temperature for decolorization is 75 ℃ and the time for decolorization is 15min), the decolorized material and the starch milk subjected to primary heat exchange are subjected to secondary heat exchange, the temperature of the decolorized material subjected to secondary heat exchange is 50 ℃, the decolorized material subjected to secondary heat exchange is subjected to ion exchange, the material subjected to ion exchange is subjected to evaporation treatment (the temperature is 110 ℃), steam formed by the evaporation treatment is condensed and then subjected to primary heat exchange with the starch milk, and condensed water (the temperature is 47 ℃) discharged after the primary heat exchange enters an ion exchange process for cleaning ion exchange resin. When the volume of the material after evaporation treatment is 0.6 times of the volume of the material before evaporation treatment, the evaporation is stopped to obtain sugar liquid, and the light transmittance of the sugar liquid is 98%.
In the process of sugar production, the consumption of steam is 0.31 ton/ton starch milk (based on dry matter).
Example 3
Adding water into starchy raw materials to prepare starch milk with the dry matter content of 37 wt% (at the temperature of 25 ℃), and sequentially carrying out liquefaction, saccharification, decolorization, ion exchange and evaporation treatment, wherein the specific operation is as follows:
performing primary heat exchange on steam generated in the evaporation treatment process (forming condensed water, the temperature is 68 ℃, and the flow is 24 tons/hour) and starch milk, wherein the temperature of the starch milk subjected to the primary heat exchange is 40 ℃, performing secondary heat exchange on the starch milk subjected to the primary heat exchange and a decolored material (the temperature is 70 ℃, and the flow is 43 tons/hour), and the temperature of the starch milk subjected to the secondary heat exchange is 57 ℃;
adding calcium hydroxide into the starch milk subjected to secondary heat exchange to adjust the pH value to 6.0, adding α -amylase (adding α -amylase of 420g per ton of dry matter), stirring uniformly, pumping into a liquefying device by a pump, wherein the liquefying temperature is 115 ℃, and the liquefying time is 2.2 hours;
adding liquefied liquid into saccharifying device, adding saccharifying enzyme (4060 composite saccharifying enzyme produced by Jenenaceae, 550g saccharifying enzyme is added per ton dry matter) at 65 deg.C and pH of 4.4, and stirring for 40 hr;
the saccharified liquid obtained after saccharification is contacted with activated carbon for decolorization (the temperature for decolorization is 70 ℃, and the time for decolorization is 20min), the decolorized material and the starch milk subjected to primary heat exchange are subjected to secondary heat exchange, the temperature of the decolorized material subjected to secondary heat exchange is 45 ℃, the decolorized material subjected to secondary heat exchange is subjected to ion exchange, the material subjected to ion exchange is subjected to evaporation treatment (the temperature is 105 ℃), steam formed by the evaporation treatment is condensed and then subjected to primary heat exchange with the starch milk, and condensed water (the temperature is 46 ℃) discharged after the primary heat exchange enters an ion exchange process for cleaning ion exchange resin. When the volume of the material after evaporation treatment is 0.7 times of the volume of the material before evaporation treatment, the evaporation is stopped to obtain sugar liquid, and the light transmittance of the sugar liquid is 98.5%.
In the process of sugar production, the consumption of steam is 0.315 ton/ton starch milk (based on dry matter).
Comparative example 1
Starch milk with a dry matter content of 35 wt% (temperature 25 ℃) was prepared by adding water to the starchy material, and the following specific operations were performed in sequence of liquefaction, saccharification, decolorization, ion exchange and evaporation (the sequence of heat exchange was different from example 1):
performing primary heat exchange on the starch milk and a decolored material (the temperature is 65 ℃ and the flow is 41 tons/hour), performing secondary heat exchange on the starch milk after condensing steam generated in the evaporation treatment process (forming condensed water, the temperature is 58 ℃ and the flow is 25 tons/hour) and the starch milk, wherein the temperature of the starch milk subjected to the secondary heat exchange is 47 ℃;
adding calcium hydroxide into the starch milk subjected to secondary heat exchange to adjust the pH value to 6.0, adding α -amylase (adding α -amylase of 420g per ton of dry matter), stirring uniformly, pumping into a liquefying device by a pump, wherein the liquefying temperature is 110 ℃, and the liquefying time is 2.5 hours;
adding liquefied liquid into saccharifying device, adding saccharifying enzyme (4060 composite saccharifying enzyme produced by Jenenaceae, 550g saccharifying enzyme is added per ton dry matter) at 60 deg.C and pH of 4.4, and stirring for 48 hr;
the saccharification liquid obtained after saccharification is contacted with activated carbon for decolorization (the temperature for decolorization is 65 ℃ and the time for decolorization is 30min), the decolorized material and starch milk are subjected to primary heat exchange, the temperature of the decolorized material subjected to the primary heat exchange is 42 ℃, the decolorized material subjected to the primary heat exchange is subjected to ion exchange, the material subjected to ion exchange is subjected to evaporation treatment (the temperature is 100 ℃), steam formed by evaporation treatment is condensed and then subjected to secondary heat exchange with the starch milk subjected to the primary heat exchange, and condensed water (the temperature is 53 ℃) discharged after the secondary heat exchange enters an ion exchange process for cleaning ion exchange resin. When the volume of the material after evaporation treatment is 0.6 times of the volume of the material before evaporation treatment, the evaporation is stopped to obtain sugar liquid, and the light transmittance of the sugar liquid is 81%.
In this process, steam consumption was 0.33 ton/ton starch milk (dry matter basis).
Comparative example 2
Adding water into starchy raw materials to prepare starch milk with the dry matter content of 35 wt% (at the temperature of 25 ℃), and sequentially carrying out liquefaction, saccharification, decolorization, ion exchange and evaporation treatment, wherein the specific operation is as follows (the step of heat exchange is not included):
adding calcium hydroxide to adjust pH to 6.0, adding α -amylase (α -amylase of 420g is added to each ton of dry matter), stirring, pumping into a liquefying device at 110 deg.C for 2.5 hr;
adding liquefied liquid into saccharifying device, adding saccharifying enzyme (4060 composite saccharifying enzyme produced by Jenenaceae, 550g saccharifying enzyme is added per ton dry matter) at 60 deg.C and pH of 4.4, and stirring for 48 hr;
and (3) contacting the saccharified liquid obtained after saccharification with activated carbon for decolorization (the temperature for decolorization is 65 ℃, and the time for decolorization is 30min), carrying out ion exchange on the decolorized material (the temperature is 65 ℃), then carrying out evaporation treatment on the ion-exchanged material (the temperature is 100 ℃), and stopping evaporation when the volume of the evaporated material is 0.6 times of the volume of the material before evaporation treatment to obtain a sugar liquid, wherein the light transmittance of the sugar liquid is 74%.
In the process of sugar production, the consumption of steam is 0.35 ton/ton starch milk (based on dry matter).
As can be seen from the results of the above examples and comparative examples, the method for manufacturing sugar of the present invention can effectively reduce the consumption of steam in the sugar manufacturing process, thereby effectively reducing the sugar manufacturing cost. Moreover, the light transmittance of the finally obtained sugar solution is determined to be 98-99%. As can be seen from comparison of the results of comparative example 1 and example 1, not only the steam consumption is increased but also the light transmittance of the sugar solution is deteriorated after the sequence of the primary heat exchange and the secondary heat exchange is changed; as can be seen from the comparison of the results of comparative example 2 and example 1, in comparative example 2, the direct ion exchange affects the refining effect of sugar due to the excessively high temperature of the decolorized material. In conclusion, the heat exchange by the method can ensure better sugar making effect and save the steam consumption.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (7)
1. A method for preparing sugar, which comprises the steps of sequentially liquefying, saccharifying, decoloring and evaporating starch milk, and is characterized by further comprising the following steps: performing primary heat exchange between the starch milk and steam generated in the evaporation treatment process, and performing secondary heat exchange between the starch milk subjected to primary heat exchange and the decolorized material to increase the temperature of the starch milk;
wherein the temperature of the starch milk is increased by 10-20 ℃ in the primary heat exchange process;
and/or the temperature of the starch milk is increased by 15-20 ℃ in the secondary heat exchange process;
wherein, the steam generated in the evaporation treatment process is condensed and then carries out primary heat exchange with the starch milk;
after the decolorization and before the evaporation treatment, subjecting the material to an ion exchange treatment; the ion exchange treatment comprises a regeneration process, and the condensate water obtained after the heat exchange between the steam generated in the evaporation treatment process and the starch milk is used for eluting the regenerant in the regeneration process.
2. The method of claim 1, wherein the conditions of liquefaction comprise: the liquefaction temperature is 110-120 ℃, and the liquefaction time is 2-2.5 h;
and/or, the conditions of saccharification comprise: the saccharification temperature is 60-70 ℃, and the saccharification time is 36-48 h;
and/or, the decolorizing conditions comprise: the decolorizing temperature is 65-75 deg.C, and decolorizing time is 15-30 min;
and/or, the conditions of the evaporation treatment include: the temperature of the evaporation treatment is 100-110 ℃.
3. The process according to claim 1, wherein the dry matter content of the starch milk is 35-40 wt%.
4. A system for preparing sugar comprises a starch milk supply device (1), a liquefying device (4), a saccharifying device (5), a decoloring device (6) and an evaporating device (8), wherein the starch milk supply device (1) is communicated with the liquefying device (4), the liquefying device (4) is communicated with the saccharifying device (5), the saccharifying device (5) is communicated with the decoloring device (6), and the decoloring device (6) is communicated with the evaporating device (8), and the system is characterized by further comprising a primary heat exchanger (2) and a secondary heat exchanger (3), wherein the primary heat exchanger (2) is respectively connected with a material outlet of the starch milk supply device (1) and a steam outlet of the evaporating device (8) and is used for carrying out primary heat exchange on the starch milk provided by the starch milk supply device (1) and steam discharged by the evaporating device (8), and the secondary heat exchanger (3) is respectively connected with a material outlet of the primary heat exchanger (2) and a material outlet of the decoloring device (6) and is used for performing secondary heat exchange on the starch milk discharged by the primary heat exchanger (2) and discharged by the decoloring device (6).
5. A system according to claim 4, wherein the system further comprises an ion exchange device (7), said ion exchange device (7) being located on the line between the secondary heat exchanger (3) and the evaporation device (8).
6. A system according to claim 5, wherein the condensed water outlet of the primary heat exchanger (2) is in communication with the ion exchange device (7).
7. A system according to any one of claims 4-6, wherein the system further comprises a condensate tank (9), the condensate tank (9) being located on a line between the evaporation device (8) and the primary heat exchanger (2).
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| CN102329834A (en) * | 2011-09-29 | 2012-01-25 | 赵建安 | End-efficiency juice steam recovery method in starch sugar production |
| CN202144496U (en) * | 2011-05-30 | 2012-02-15 | 河南巨龙生物工程股份有限公司 | Glucose production equipment with starch milk preheating system |
| CN105316374A (en) * | 2014-07-11 | 2016-02-10 | 武汉中粮食品科技有限公司 | Sugar making method |
| 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202144496U (en) * | 2011-05-30 | 2012-02-15 | 河南巨龙生物工程股份有限公司 | Glucose production equipment with starch milk preheating system |
| CN102329834A (en) * | 2011-09-29 | 2012-01-25 | 赵建安 | End-efficiency juice steam recovery method in starch sugar production |
| CN105316374A (en) * | 2014-07-11 | 2016-02-10 | 武汉中粮食品科技有限公司 | Sugar making method |
| 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 |
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