CN119082229A - Production method of low oligosaccharide and low SMR glucose from wheat - Google Patents

Abstract

The invention provides a production method for preparing low oligosaccharide and low SMR glucose by wheat, which relates to the technical field of glucose production and comprises the following production steps: the wheat starch enters the top of a deodorizing purification column after pulp mixing, liquefying, saccharifying, decolorizing, filtering and ion exchange, the deodorizing purification is carried out on the sugar solution by a porous cross-linked polymer prepared by a styrene system in the deodorizing purification column, and the finished glucose is obtained after the filtration, evaporation, crystallization, separation and drying. The production method of the low-oligosaccharide and low-SMR glucose by using the wheat can remove the contents of pesticide residues, toxins, pollutants and food additives in the glucose, and simultaneously can reduce the content of the oligosaccharide, thereby increasing the taste and quality of the finished glucose, purifying the flavor and taste of the finished glucose, and recycling the deodorizing and purifying column after multiple use through regeneration, so that the material cost in production is reduced.

Description

Production method for preparing low oligosaccharide and low SMR glucose from wheat

Technical Field

The invention relates to the technical field of glucose production, in particular to a production method for preparing low-oligosaccharide and low-SMR glucose from wheat.

Background

Glucose has an important role in the field of biology, being an energy source for living cells and an intermediate product of metabolism, i.e. a main energy supply substance for organisms. The glucose is used as one of the dietary fibers with the best effect and performance, can be used for fiber reinforcement of various foods, replaces saturated fat in the foods, and improves the texture and taste of the foods. The dual standard detection is carried out on the crystalline glucose produced by taking the wheat starch as the raw material, and along with the improvement of the quality requirements of customers, in order to expand the sales market, the detection standards of SM-R, oligosaccharide and the like for the rice syrup detection standard are added on the original dual standard detection of the crystalline glucose produced by taking the wheat starch as the raw material. So that the glucose prepared from the wheat is required to meet the detection standards of edible glucose and rice syrup at the same time. Among the detection standards of rice syrup, SM-R and oligosaccharide detection are the most important, SM-R is the content of pesticide residues, toxins, pollutants and food additives in the detected glucose, the quality and safety of wheat can be reflected by the level of SM-R, the lower the value of SM-R detection is, the better the quality and safety of wheat are, and the following problems are caused when the wheat is used for producing glucose:

1. When the wheat is used for producing glucose, the production place, variety, growth environment, processing mode and the like of the wheat can influence the quality of the produced glucose, so that SM-R detection exceeds standard, the later period is difficult to adjust, the quality of the glucose produced by the wheat can be improved only by adjusting the production procedure, and meanwhile, the value of SM-R is reduced, however, the content of pesticide residues, toxins, pollutants and food additives in the glucose is difficult to completely remove by the existing method for producing the glucose by the wheat, and the SM-R detection value exceeds standard.

2. The oligosaccharide component in glucose mainly comprises maltose, sucrose, lactose and the like, so that the taste and the flavor of food can be improved, meanwhile, the oligosaccharide component can also be used as a sweetener and a nutritional supplement, different people have different absorption and utilization capacities on oligosaccharides, and some people can be allergic or intolerant to certain oligosaccharides, so that the content of the oligosaccharides in the glucose needs to be reduced to adapt to more people.

In order to solve the above problems, development of a method for producing low oligosaccharide and low SMR glucose from wheat is required.

Disclosure of Invention

Aiming at the above situation, to overcome the defects of the prior art;

The invention provides a production method for preparing low oligosaccharide and low SMR glucose by wheat, which comprises the following steps:

(1) Mixing wheat starch with water to obtain starch milk, heating the starch milk to 40-50 ℃ by a plate heat exchanger, controlling the concentration to Be 15.5-16.0Be, controlling the concentration of starch milk protein to Be less than or equal to 0.3%, controlling the fat to Be less than or equal to 0.15%, adjusting the PH to Be 5.5-6.0 by sodium hydroxide, adding high-temperature amylase, adding an enzyme preparation according to 0.2kg/t, and pumping into a feeding tank.

(2) Pumping the liquid into an ejector from a charging tank for primary injection, controlling the injection temperature to be 105-110 ℃, feeding the liquid into a high-temperature coil pipe for preserving pressure for 10 minutes, enabling the liquid glucose to enter a flash tank in a tangential direction, performing rapid rotation in the flash tank for vapor-liquid separation, cooling to room temperature after separation, pumping the liquid glucose into a laminar flow tank through a transfer pump, preserving heat for 90-120 minutes at 95 ℃, then performing secondary injection, mixing starch milk and steam in the ejector, adjusting the PH to be 4.5-4.8 by using sodium hydroxide after secondary injection, and adding an enzyme preparation according to 0.3-0.35 kg/t;

(3) Saccharifying, namely feeding the liquefied feed liquid into a saccharifying tank, preserving heat and saccharifying for 60 hours at 60-62 ℃, and detecting that DE is more than 96.5% and the oligosaccharide content is less than 0.5%;

(4) Decoloring and filtering, namely adding the lignocellulose activated carbon into the sugar solution according to 0.3Kg/t for decoloring, and filtering the decolored sugar solution through a filter.

(5) Ion exchange, namely, exchanging sugar materials by using ion exchange columns, wherein the exchange times are two groups, the sequence of each group is that cation columns are firstly passed, then anion columns are passed, cation in sugar liquid is removed by the cation columns, anion in the sugar liquid is removed by the anion columns, the temperature is 40-50 ℃, the discharge PH is controlled to be 3.8-4.0, and the conductivity is less than 100PPM.

(6) And (3) deodorizing and purifying, namely, feeding the ion-exchanged feed liquid from the upper part of a deodorizing and purifying column, controlling the temperature to be 80 ℃, and feeding the flow rate into the deodorizing and purifying column at a speed of 12M3/t for deodorizing and purifying.

(7) And (3) evaporating, namely performing twice evaporation by adopting a vacuum multi-effect countercurrent feeding method, wherein the primary evaporation concentration is controlled to be 45-50%, and the secondary evaporation concentration is controlled to be 72.0-73.5%.

(8) And (3) crystallizing, namely pumping the evaporated feed liquid into a horizontal crystallizer, mixing the feed liquid with reserved seed crystals at the feed tank temperature of 55.0-56.0 ℃, controlling the temperature of the feed liquid at 40-45 ℃ after the feed liquid is fully fed, cooling the feed liquid with warm water at 32-35 ℃ in the first 25 hours, and cooling the feed liquid to 0.3 ℃ per hour. Cooling with 18-20deg.C cold water for 25-60 hr, cooling the material per hour by 0.5 deg.C, crystallizing for 60 hr, discharging at 20-22deg.C, and retaining 30% massecuite as seed crystal of the next tank.

(9) Separating, namely conveying the crystallized material to a separator by a packing auger, separating mother liquor and washing liquor at a high speed of 1350 revolutions per hour, wherein the separation time is 25 minutes, the yield is 51.4%, and the oligosaccharide is <0.01% and SMR=0 after the mother liquor and the washing liquor are removed by separation.

(10) And (3) drying by adopting a positive pressure drying and negative pressure cooling airflow drying method, wherein the temperature of hot air is 100-110 ℃, the wind speed is 5-10m/s, the drying time is 30-40 minutes, and the finished glucose is obtained after drying.

Preferably, the decolorizing time of step (4) is 30 minutes and the decolorizing temperature is 75-80 ℃.

Preferably, the filtering in the step (4) is sequentially performed through filters with the precision of 10um, 5um, 2um and 1 um.

Preferably, the deodorizing and purifying column is filled with porous crosslinked polymer made of styrene, is a bead body with the pore size of nonpolar bead adsorption resin and the water content of 55.0-65.0%, and is regenerated after being continuously used for 70 hours, and the regeneration method comprises the following steps:

The first method is to fill the resin into the column, wash the resin with condensed water or deionized water at a flow rate of 1BV/h for one hour, and the water flow rate is preferably controlled to control the resin to be stable in the middle of the rearview mirror.

And in the second method, 4% sodium hydroxide or 4-5% saline alkali water with the volume of 2 times of resin is introduced into a deodorizing purification column at the temperature of between 75 and 80 ℃ for 1 hour at 1 BV/h, then soaked for 4 to 8 hours, and then washed with water to pH10 and the flow rate of between 5 and 8BV/h.

In the third method, 4% hydrochloric acid with the volume of 0.5-0.8 times of the resin is used for passing through a deodorizing purification column at the flow rate of 1 BV/h.

Preferably, the separation time of the step (9) is 20-25 minutes, and the yield is 50-55%.

Compared with the prior art, the invention provides a production method for preparing low oligosaccharide and low SMR glucose from wheat, which has the following beneficial effects:

The porous cross-linked polymer prepared from styrene can play a role in filtering and adsorbing sugar liquid, is nonpolar bead adsorption resin, has good adsorption capacity and high-efficiency elution rate for organic matters and organic pigments in the sugar liquid, is suitable for removing peculiar smell and improving taste in the sugar liquid, can remove pesticide residues, toxins, pollutants and food additives in glucose after being filtered by a deodorizing and purifying column, can reduce the content of oligosaccharide, thereby increasing the taste and quality of finished glucose, purifying the flavor and taste of the finished glucose product, meeting the requirements of customers on quality, expanding the sales market, and reducing the material cost in production by recycling the deodorizing and purifying column after multiple use.

Detailed Description

The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.

Example 1:

the method comprises the following steps:

(1) Mixing wheat starch with water to obtain starch milk, heating the starch milk to 40 ℃ by a plate heat exchanger, wherein the concentration is 15Be, the concentration of starch milk protein is 0.35%, the concentration of fat is 0.2%, regulating the pH value to 5.8 by sodium hydroxide, adding high-temperature amylase, adding an enzyme preparation according to 0.2kg/t, and pumping into a feeding tank.

(2) Pumping the liquid into an ejector from a charging tank for primary injection, controlling the injection temperature to be 105 ℃, feeding a high-temperature coil pipe for preserving pressure for 10 minutes, enabling sugar liquid to enter a flash tank in a tangential direction, performing rapid rotation in the flash tank for gas-liquid separation, cooling to room temperature after separation, pumping the liquid into a laminar flow tank through a transfer pump, preserving heat for 100 minutes at 95 ℃, then performing secondary injection, mixing starch milk and steam in the ejector, adjusting the PH to 4.7 by using sodium hydroxide after the secondary injection, and adding an enzyme preparation according to 0.3 kg/t;

(3) Saccharifying, namely feeding the liquefied feed liquid into a saccharifying tank, and saccharifying at 60 ℃ for 60 hours;

(4) Decoloring and filtering, namely adding the lignocellulose activated carbon into the sugar solution according to 0.3Kg/t for decoloring, wherein the decoloring time is 30 minutes, the decoloring temperature is 78 ℃, and filtering the decolored sugar solution through a filter.

(5) And (3) ion exchange, namely, exchanging sugar materials by using ion exchange columns, wherein the exchange times are two groups, the sequence of each group is that the sugar liquid passes through a cation column and then an anion column, cations in the sugar liquid are removed by the cation column, anions in the sugar liquid are removed by the anion column, the temperature is 45 ℃, and the discharge PH is controlled to be 3.9.

(6) And (3) deodorizing and purifying, namely, feeding the ion-exchanged feed liquid from the upper part of a deodorizing and purifying column, controlling the temperature to be 80 ℃, and feeding the flow rate into the deodorizing and purifying column at a speed of 12M3/t for deodorizing and purifying.

(7) And (3) evaporating, namely performing twice evaporation by adopting a vacuum multi-effect countercurrent feeding method, wherein the primary evaporation concentration is controlled to be 45%, and the secondary evaporation concentration is controlled to be 72.5%.

(8) And (3) crystallizing, namely pumping the evaporated feed liquid into a horizontal crystallizer, mixing the feed liquid with reserved seed crystals at the feed tank temperature of 55.0 ℃, controlling the temperature of the feed liquid at 40 ℃ after the feed liquid is fully fed, cooling the feed liquid with warm water at 32 ℃ for the first 25 hours, and cooling the feed liquid to 0.3 ℃ per hour. Cooling with 18 deg.c cold water for the next 35 hr, material cooling by 0.5 deg.c every hr, crystallizing for 60 hr, discharging at 20 deg.c, and maintaining 30% massecuite as seed crystal for the next tank.

(9) And separating, namely conveying the crystallized material to a separator by a packing auger, and separating mother liquor and washing liquor at a high speed of 1350 revolutions per hour for 25 minutes.

(10) And (3) drying by adopting a positive pressure drying and negative pressure cooling airflow drying method, wherein the temperature of hot air is 100 ℃, the wind speed is 5m/s, the drying time is 30 minutes, and the finished glucose is obtained after drying.

Example 2:

the method comprises the following steps:

Mixing wheat starch with water to obtain starch milk, heating the starch milk to 40 ℃ by a plate heat exchanger, wherein the concentration is 16Be, the concentration of starch milk protein is 0.37%, the concentration of fat is 0.24%, regulating the pH value to 6.0 by sodium hydroxide, adding high-temperature amylase, adding an enzyme preparation according to 0.2kg/t, and pumping into a feeding tank.

The remaining steps and addition amounts of liquefaction, saccharification, decolorization and filtration, ion exchange, deodorization purification, evaporation, crystallization, separation and drying remain the same as in example 1.

Example 2 differs from example 1 in that the concentration of starch milk, the parameters of starch milk protein and fat are changed, while the parameters of PH are changed, keeping the remaining steps and parameters unchanged.

Example 3:

the method comprises the following steps:

Mixing wheat starch with water to obtain starch milk, heating the starch milk to 40 ℃ by a plate heat exchanger, adjusting pH to 5.8 by sodium hydroxide, adding high-temperature amylase, adding enzyme preparation at 0.25kg/t, and pumping into a feeding tank, wherein the concentration is 15.6Be, the concentration of starch milk protein is 0.28%, and the fat is 0.19%.

The remaining steps and addition amounts of liquefaction, saccharification, decolorization and filtration, ion exchange, deodorization purification, evaporation, crystallization, separation and drying remain the same as in example 1.

Example 3 differs from example 1 in that the concentration of starch milk, the parameters of starch milk protein and fat are changed, the amount of enzyme preparation added is increased, and the remaining steps and parameters are kept unchanged.

Comparative example:

the steps and the addition amounts of the pulping, liquefying, saccharifying, decolorizing and filtering, ion exchange, evaporating, crystallizing, separating and drying in the steps remain the same as those of example 1, and the deodorizing and purifying steps between the ion exchange and evaporating steps are reduced.

Example 4 differs from example 1 in that the steps of deodorizing and purifying are removed, and the remaining steps and parameters are kept unchanged.

Comparative analyses of example 1, example 2, example 3 and comparative example were performed as follows:

Under the same parameters, SM-R detection before deodorization and purification, SM-R detection after finished products, outer oligosaccharide detection before deodorization and purification and outer oligosaccharide detection after deodorization and purification are respectively compared in example 1, example 2, example 3 and comparative example.

Table 1 comparison of parameters

Examples 1,2,3 and comparative examples although SM-R was detected after ion exchange, examples 1,2 and 3 were added with a deodorizing and purifying step in the production steps, and after the deodorizing and purifying step, the finished product was not detected by SM-R, whereas comparative examples were not added with a deodorizing and purifying step, and both after ion exchange and after the finished product, SM-R was detected, and the content of exooligosaccharide was high.

Therefore, the deodorizing and purifying step between the ion exchange and evaporation steps can filter and adsorb the sugar solution by using the deodorizing and purifying column of the macroporous adsorption resin made of the styrene, remove the contents of pesticide residues, toxins, pollutants and food additives in the glucose, and is suitable for removing peculiar smell in the sugar solution and improving the taste and the quality, so that the SM-R is not detected during the detection of a finished product, and the content of external oligosaccharides can be reduced.

Claims (5)

1. The production method for preparing low oligosaccharide and low SMR glucose from wheat is characterized by comprising the following steps:

(1) Mixing wheat starch with water to obtain starch milk, heating the starch milk to 40-50 ℃ by a plate heat exchanger, controlling the concentration to Be 15.5-16.0Be, controlling the concentration of starch milk protein to Be less than or equal to 0.3%, controlling the fat to Be less than or equal to 0.15%, adjusting the PH to Be 5.5-6.0 by sodium hydroxide, adding high-temperature amylase, adding an enzyme preparation according to 0.2kg/t, and pumping into a feeding tank.

(2) Pumping the liquid into an ejector from a charging tank for primary injection, controlling the injection temperature to be 105-110 ℃, feeding the liquid into a high-temperature coil pipe for preserving pressure for 10 minutes, enabling the liquid glucose to enter a flash tank in a tangential direction, performing rapid rotation in the flash tank for vapor-liquid separation, cooling to room temperature after separation, pumping the liquid glucose into a laminar flow tank through a transfer pump, preserving heat for 90-120 minutes at 95 ℃, then performing secondary injection, mixing starch milk and steam in the ejector, adjusting the PH to be 4.5-4.8 by using sodium hydroxide after secondary injection, and adding an enzyme preparation according to 0.3-0.35 kg/t;

(3) Saccharifying, namely feeding the liquefied feed liquid into a saccharifying tank, preserving heat and saccharifying for 60 hours at 60-62 ℃, and detecting that DE is more than 96.5% and the oligosaccharide content is less than 0.5%;

(4) Decoloring and filtering, namely adding the lignocellulose activated carbon into the sugar solution according to 0.3Kg/t for decoloring, and filtering the decolored sugar solution through a filter.

(5) Ion exchange, namely, exchanging sugar materials by using ion exchange columns, wherein the exchange times are two groups, the sequence of each group is that cation columns are firstly passed, then anion columns are passed, cation in sugar liquid is removed by the cation columns, anion in the sugar liquid is removed by the anion columns, the temperature is 40-50 ℃, the discharge PH is controlled to be 3.8-4.0, and the conductivity is less than 100PPM.

(6) And (3) deodorizing and purifying, namely, feeding the ion-exchanged feed liquid from the upper part of a deodorizing and purifying column, controlling the temperature to be 80 ℃, and feeding the flow rate into the deodorizing and purifying column at a speed of 12M3/t for deodorizing and purifying.

(7) And (3) evaporating, namely performing twice evaporation by adopting a vacuum multi-effect countercurrent feeding method, wherein the primary evaporation concentration is controlled to be 45-50%, and the secondary evaporation concentration is controlled to be 72.0-73.5%.

(8) And (3) crystallization: feeding the evaporated feed liquid into a horizontal crystallizer, mixing the feed liquid with reserved seed crystals at a feed tank temperature of 55.0-56.0 ℃, controlling the temperature of the feed liquid at 40-45 ℃ after the feed liquid is fully fed, cooling the feed liquid with warm water at 32-35 ℃ in the first 25 hours, cooling the feed liquid to 0.3 ℃ per hour, cooling the feed liquid with cold water at 18-20 ℃ in the last 25-60 hours, cooling the feed liquid to 0.5 ℃ per hour, crystallizing for 60 hours, discharging the feed liquid at a tank temperature of 20-22 ℃, and keeping 30% massecuite as seed crystals of the next tank when discharging the feed liquid.

(9) Separating, namely conveying the crystallized material to a separator by a screw conveyor, separating mother liquor and washing liquor at a high speed of 1350 revolutions per hour, wherein the separation time is 25 minutes, the yield is 50-55%, and separating to remove the mother liquor and the washing liquor, wherein the oligosaccharide is less than 0.01%, and the SMR=0.

(10) And (3) drying by adopting a positive pressure drying and negative pressure cooling airflow drying method, wherein the temperature of hot air is 100-110 ℃, the wind speed is 5-10m/s, the drying time is 30-40 minutes, and the finished glucose is obtained after drying.

2. The method for producing low oligosaccharides and low SMR glucose by wheat as claimed in claim 1, wherein said decoloring time in said step (4) is 30 minutes and the decoloring temperature is 75 to 80 ℃.

3. The method for producing low oligosaccharides and low SMR glucose from wheat as set forth in claim 1, wherein said filtering in step (4) is performed by sequentially passing through filters having an accuracy of 10um, 5um, 2um, 1 um.

4. The method for producing low oligosaccharides and low SMR glucose from wheat according to claim 1, wherein said deodorizing and purifying column is filled with a porous crosslinked polymer made of styrene, is a porous bead body of nonpolar bead adsorption resin, has a water content of 55.0 to 65.0%, and is regenerated after being continuously used for 70 hours, and the regeneration method comprises:

The first method is to fill the resin into the column, wash the resin with condensed water or deionized water at a flow rate of 1BV/h for one hour, and the water flow rate is preferably controlled to control the resin to be stable in the middle of the rearview mirror.

And in the second method, 4% sodium hydroxide or 4-5% saline alkali water with the volume of 2 times of resin is introduced into a deodorizing purification column at the temperature of between 75 and 80 ℃ for 1 hour at 1 BV/h, then soaked for 4 to 8 hours, and then washed with water to pH10 and the flow rate of between 5 and 8BV/h.

In the third method, 4% hydrochloric acid with the volume of 0.5-0.8 times of the resin is used for passing through a deodorizing purification column at the flow rate of 1 BV/h.

5. The method for producing low oligosaccharides and low SMR glucose by wheat as claimed in claim 1, wherein said separation time in said step (9) is 20 to 25 minutes, and the yield is 50 to 55%.