Glucose production method using diatomite to replace activated carbon

Abstract

The invention provides a glucose production method using diatomite to replace activated carbon, and relates to the technical field of glucose production, the production steps comprise: size mixing, liquefaction, saccharification, deslagging filtration, primary decoloration and filtration, primary evaporation, secondary decoloration and filtration, ion exchange, secondary evaporation, crystallization, separation and drying to obtain the finished product glucose. According to the invention, the diatomite and the active carbon are mixed, so that the efficiency of the decolorizing step is accelerated, the filtering time is shortened, the filtering quality is improved and is the same as that of pure active carbon, and the price of the diatomite is lower than that of the active carbon, so that the production cost is reduced, and the used mixed decolorizing agent is recycled again; the total utilization rate of the mixed decolorizing agent can be improved, the filtering capacity of the original decolorizing agent is improved to 80-90% from 60-70%, and meanwhile the yield and quality after production are improved.

Description

Technical Field

[0001] The invention relates to the technical field of glucose production, in particular to a method for producing glucose by replacing activated carbon with diatomaceous earth. Background Art

[0002] Glucose plays an important role in the field of biology. It is the energy source of living cells and the intermediate product of metabolism, that is, the main energy source of organisms. It is widely used in the candy manufacturing industry and the medical field. At the same time, glucose, as one of the dietary fibers with the best effects and performance, has developed rapidly in recent years and has been approved for use in many countries. It can be used to strengthen the fiber of various foods, replace saturated fat in foods, and improve the texture and taste of foods. However, due to the large fluctuations in the market price of edible glucose products in the past two years, sometimes the sales price is significantly lower than the product cost. Many glucose manufacturers are in a loss or even stopped production. The price of wheat in the domestic market is lower than that of corn. This is the advantage of using wheat starch instead of corn starch to better adapt to market competition.

[0003] The decolorization process is an important part of the glucose production process. It mainly filters, adsorbs and decolorizes the sugar solution to remove pigments, impurities, foreign matter and odors in the sugar solution. The quality of decolorization directly affects the quality of the finished glucose product. Activated carbon is the main filter material used in the decolorization process. In traditional starch sugar production, the decolorization process uses a single substance, activated carbon, for decolorization.

[0004] The following problems are also encountered in the glucose decolorization process:

[0005] 1. Due to the small particle size of activated carbon, it takes a long time to perform the decolorization step, resulting in low utilization rate, serious waste of resources, high production cost, and reduced comprehensive yield of the product. If the amount of activated carbon is increased, the filtration time will be increased, the cleaning frequency of the equipment will be increased, the labor intensity will be increased, the production of grapes will be affected, and excessive ash and other impurities in the activated carbon will be brought into the sugar solution, thereby reducing the filtration quality;

[0006] 2. The utilization rate of activated carbon after one use is very low, only about 60-70%. The filtering, adsorption and decolorization capabilities of the activated carbon are not fully utilized, and the utilization efficiency is low. At the same time, it increases the pollution to the environment and increases the environmental pressure.

[0007] 3. Because the activated carbon is too fine, it will hinder the filtration speed of the sugar solution and affect the clarity of the sugar solution.

[0008] In order to solve the above problems, it is necessary to develop a method for producing glucose by using diatomaceous earth instead of activated carbon. Summary of the invention

[0009] In view of the above situation, in order to overcome the defects of the prior art;

[0010] The present invention provides a method for producing glucose by replacing activated carbon with diatomaceous earth, comprising the following steps:

[0011] S1. Slurry preparation: wheat starch is mixed with water to obtain starch milk, the starch milk is pumped into a plate heat exchanger, the temperature is heated to 40-50°C, the concentration is controlled to be 15.5-16.0Be, starch milk protein ≤0.3%, fat ≤0.15%, the pH is adjusted to 5.5-6.0 with sodium hydroxide, high temperature amylase is added, and the enzyme preparation is added at 0.2kg / t and pumped into the feeding tank;

[0012] S2, liquefaction: the sugar solution is pumped from the feeding tank into the ejector for primary injection, the injection temperature is controlled at 100-110℃, and the sugar solution is kept under pressure for 10 minutes in the high-temperature coil. The sugar solution enters the flash tank in a tangential direction, and the sugar solution is rapidly rotated in the flash tank for vapor-liquid separation. After separation, it is cooled to room temperature and pumped into the laminar flow tank through a transfer pump. It is kept at 95℃ for 90-120 minutes, and then a secondary injection is performed. The starch milk is mixed with steam in the ejector, and the injection temperature is 135-138℃. After the secondary injection, the pH is adjusted to 4.5-4.8 with sodium hydroxide, and enzyme preparation is added at 0.3-0.35kg / t;

[0013] S3, saccharification: the liquefied liquid enters the saccharification tank and is kept at 60-62°C for saccharification for 60 hours, and the saccharification liquid is discharged;

[0014] S4, slag removal and filtration: the saccharified sugar solution is pumped into the filter for filtration at a filtration temperature of 50-60°C and a filtration rate of 16-20 ml / min;

[0015] S5, primary decolorization and filtration: put the sugar solution into the decolorization tank, add the mixed decolorizer into the sugar solution and mix evenly for 30 minutes, keep the temperature at 75-80°C, absorb the impurities such as fine protein, fat, pigment in the sugar solution, and then put it into the filter after mixing for solid-liquid separation, and discard the separated solids;

[0016] S6, primary evaporation: the sugar solution separated from the solid and liquid is pumped into the multi-effect concentrator to remove excess water from the sugar solution. The feed flow rate is 30-35m 3 / h, evaporation time 40-45min, concentration 45-50%;

[0017] S7, secondary decolorization and filtration: put the sugar solution into the decolorization tank, add the mixed decolorizer into the sugar solution at 0.3 kg / t and mix evenly for 30 minutes, keep the temperature at 70-75 ° C, and then put it into the filter after mixing for solid-liquid separation, and keep the separated solids for secondary use;

[0018] S8, ion exchange: the sugar solution after solid-liquid separation is exchanged with sugar material through ion exchange column. The exchange process is two-stage exchange. The sugar solution passes through the cation column first and then the anion column. The cations in the sugar solution are removed by the cation column, and the anions in the sugar solution are removed by the anion column. The temperature is 40-50℃, the discharge pH is controlled at 3.8-4.0, and the conductivity is less than 100PPM.

[0019] S9, secondary evaporation: pump the sugar solution into the multi-effect concentrator at a flow rate of 20-22m 3 / h, evaporation time 40-45min, control concentration at 72.0-73.5%;

[0020] S10, crystallization: the evaporated liquid is pumped into a horizontal crystallizer, the inlet temperature is 55.0-56.0°C, and mixed with the reserved crystal seeds. After the sugar liquid is full, the material temperature is controlled at 40-45°C. The material is cooled by 32-35°C warm water for the first 25 hours, and the temperature is reduced by 0.3°C per hour. The material is cooled by 18-20°C cold water for the next 25-60 hours, and the temperature is reduced by 0.5°C per hour. The crystallization time is 60 hours, and the outlet temperature is 20-22°C. When the sugar liquid is discharged from the tank, 30% of the massecuite is retained as the crystal seeds for the next tank.

[0021] S11, separation: the crystallized material is transported to a separator by an auger, and the mother liquor and the washing liquid are separated at a high speed of 1350 rpm, the separation time is 25 minutes, the yield is 50-55%, and the mother liquor and the washing liquid are removed by separation;

[0022] S12, drying: adopt positive pressure drying, negative pressure cooling airflow drying method for drying, hot air temperature is 100-110 ℃, wind speed is 5-10m / s, drying time is 30-40 minutes, and finished glucose is obtained after drying.

[0023] Preferably, the mixed decolorizing agent in step S7 is prepared by mixing 90% of a solvent and 10% of a decolorizing agent, wherein the solvent is water or sugar solution or a mixture of the two, and the decolorizing agent is a mixture of 30-50% diatomaceous earth and 50-70% activated carbon, wherein the particle size of the diatomaceous earth is 100 mesh, and the particle size of the activated carbon is 200 mesh.

[0024] Preferably, the mixed decolorizing agent in step S5 is prepared by mixing 90% of a solvent and 10% of a decolorizing agent agglomerate, wherein the solvent is water or a sugar solution or a mixture of the two, and the decolorizing agent agglomerate is a secondary utilization of the solid separated in step S7.

[0025] Preferably, the separation time of step S9 is 20-25 minutes, and the yield is 50-55%.

[0026] Preferably, in step S6, after the sugar solution enters the multi-effect concentrator, five-effect vacuum evaporation is performed in sequence, and the pressure and temperature of the five-effect vacuum evaporation are: first-effect vacuum: 0.025Mpa, temperature: 78°C; second-effect vacuum: -0.042Mpa, temperature: 72°C; third-effect vacuum: -0.058Mpa, temperature: 65°C; fourth-effect vacuum: -0.072Mpa, temperature: 60°C; fifth-effect vacuum: -0.092Mpa, temperature: 55°C.

[0027] Preferably, in step S9, after the sugar solution enters the multi-effect concentrator, five-effect vacuum evaporation is performed in sequence, and the pressure and temperature of the five-effect vacuum evaporation are: first-effect vacuum: 0.025Mpa, temperature: 95°C; second-effect vacuum: -0.042Mpa, temperature: 86°C; third-effect vacuum: -0.058Mpa, temperature: 75°C; fourth-effect vacuum: -0.072Mpa, temperature: 68°C; fifth-effect vacuum: -0.092Mpa, temperature: 58°C.

[0028] Preferably, after the sugar solution enters the filter, it is filtered through 10um, 5um, 2um, and 1um filters in sequence.

[0029] Compared with the prior art, the present invention provides a method for producing glucose by using diatomaceous earth instead of activated carbon, which has the following beneficial effects:

[0030] 1. The particle size of diatomaceous earth in the mixed decolorizer is larger than that of activated carbon, so that activated carbon can adsorb smaller proteins and diatomaceous earth can adsorb larger proteins. The larger particle size can increase the flow rate of the sugar solution, thereby speeding up the decolorization process and reducing production time. At the same time, activated carbon has the ability to decolorize, adsorb and filter, and can comprehensively filter the sugar solution, while diatomaceous earth only has the ability to adsorb and filter. Pigments are impurities such as organic matter and organic acids produced during the saccharification process, and account for a small proportion. After diatomaceous earth and activated carbon are mixed, the two interact with each other and complement each other. The mixed diatomaceous earth and activated carbon can enhance the capacity of the mixed decolorizer, enhance the overall filtration capacity of the decolorization process, and improve the quality of filtration. At the same time, the price of diatomaceous earth is lower than that of activated carbon, thereby reducing production costs.

[0031] 2. The mixed decolorizing agent after the secondary decolorization is recycled and used again in the primary decolorization step, which can improve the utilization rate of the mixed decolorizing agent. The second decolorization process can reuse the decolorization and adsorption functions that were not fully utilized once. The forced decolorization and adsorption are performed again by increasing the material temperature so that the mixed decolorizing agent can be adsorbed and filtered again. The mixed decolorizing agent can utilize the powerful surface area and specific surface area and the pore sizes of different sizes generated after activation. The larger pore size adsorbs the larger protein, the smaller pore size adsorbs the smaller protein, and the tiny pore size adsorbs the tiny protein. Through the secondary decolorization, the tiny protein is first adsorbed and then the fine protein is adsorbed, which improves the utilization rate of the mixed decolorizing agent. Compared with the original single decolorizing agent, the utilization efficiency of the mixed decolorizing agent is increased from 60-70% to 80-90%. DETAILED DESCRIPTION

[0032] The following will be combined with the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0033] Embodiment 1:

[0034] In this embodiment, the secondary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorizing agent, wherein the solvent is sugar solution and the decolorizing agent is composed of 30% diatomaceous earth and 70% activated carbon;

[0035] The primary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorization agent agglomerates, wherein the solvent is sugar solution and the decolorization agent agglomerates are solids separated from the secondary decolorization and filtration steps for reuse.

[0036] A method for producing glucose comprises the following steps:

[0037] S1. Slurry preparation: wheat starch is mixed with water to obtain starch milk, the starch milk is pumped into a plate heat exchanger, the temperature is heated to 45°C, the concentration is controlled to be 15.8Be, starch milk protein is 0.28%, fat is 0.14%, the pH is adjusted to 5.5 with sodium hydroxide, high temperature amylase is added, and enzyme preparation is added at 0.2kg / t and pumped into the feeding tank;

[0038] S2, liquefaction: the sugar solution is pumped from the feeding tank into the ejector for primary injection, the injection temperature is controlled at 108°C, and the sugar solution enters the high-temperature coil for 10 minutes of pressure maintenance. The sugar solution enters the flash tank in a tangential direction, and the sugar solution is rapidly rotated in the flash tank for vapor-liquid separation. After separation, it is cooled to room temperature and pumped into the laminar flow tank through the transfer pump. It is kept at 95°C for 100 minutes, and then a secondary injection is performed. The starch milk is mixed with steam in the ejector. The injection temperature is 135°C. After the secondary injection, the pH is adjusted to 4.7 with sodium hydroxide, and an enzyme preparation is added at 0.3kg / t;

[0039] S3, saccharification: the liquefied liquid enters the saccharification tank and is kept at 61°C for saccharification for 60 hours, and the material is discharged after saccharification;

[0040] S4, slag removal and filtration: the saccharified sugar solution is pumped into the filter for filtration at a filtration temperature of 55°C and a filtration rate of 20 ml / min;

[0041] S5, primary decolorization and filtration: put the sugar solution into the decolorization tank, add the mixed decolorizer into the sugar solution and mix evenly for 30 minutes, keep the temperature at 75°C, absorb the impurities such as fine protein, fat, pigment in the sugar solution, and then put it into the filter after mixing for solid-liquid separation, and discard the separated solid;

[0042] S6, primary evaporation: the sugar solution separated from the solid and liquid is pumped into the multi-effect concentrator to remove excess water from the sugar solution. The feed flow rate is 30m 3 / h, evaporation time 40min, concentration 45%;

[0043] S7, secondary decolorization and filtration: the sugar solution is pumped into a decolorization tank, and the mixed decolorizer is added into the sugar solution at a rate of 0.3 kg / t for uniform mixing, and the mixture is mixed for 30 minutes, and the temperature is maintained at 70°C. After mixing, the mixture is pumped into a filter for solid-liquid separation, and the separated solid is retained for secondary utilization;

[0044] S8, ion exchange: the sugar solution after solid-liquid separation is exchanged with sugar material by ion exchange column. The exchange process is two-stage exchange. The sugar solution passes through the cation column first and then the anion column. The cations in the sugar solution are removed by the cation column, and the anions in the sugar solution are removed by the anion column. The temperature is 40°C and the discharge pH is controlled at 4.0.

[0045] S9, secondary evaporation: pump the sugar solution into the multi-effect concentrator at a flow rate of 20m 3 / h, evaporation time 45min, concentration controlled at 72.0%;

[0046] S10, crystallization: the evaporated liquid is pumped into a horizontal crystallizer, the inlet temperature is 55.0°C, and it is mixed with the reserved crystal seeds. After the sugar liquid is full, the material temperature is controlled at 45°C. The material is cooled by 32°C warm water for the first 25 hours, and the temperature drops by 0.3°C per hour. The material is cooled by 20°C cold water for the next 25 hours, and the temperature drops by 0.5°C per hour. The crystallization time is 60 hours, and the outlet temperature is 22°C. When the sugar liquid is out of the tank, 30% of the massecuite is retained as the crystal seeds for the next tank.

[0047] S11, separation: the crystallized material is transported to a separator by an auger, and the mother liquor and the washing liquid are separated at a high speed of 1350 rpm, the separation time is 25 minutes, the yield is 54%, and the mother liquor and the washing liquid are removed by separation;

[0048] S12, drying: adopt positive pressure drying, negative pressure cooling airflow drying method for drying, hot air temperature is 100 ℃, wind speed is 10m / s, drying time is 30 minutes, and finished glucose is obtained after drying.

[0049] Embodiment 2:

[0050] In this embodiment, the secondary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorizing agent, wherein the solvent is sugar solution and the decolorizing agent is composed of 40% diatomaceous earth and 60% activated carbon;

[0051] The primary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorization agent agglomerates, wherein the solvent is sugar solution and the decolorization agent agglomerates are solids separated in the secondary decolorization and filtration steps.

[0052] The difference between Example 2 and Example 1 is that the ratio of the decolorizing agent in the secondary decolorization and filtration steps is changed, and the other production steps and parameters are consistent with Example 1.

[0053] Embodiment 3:

[0054] In this embodiment, the secondary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorizing agent, wherein the solvent is sugar solution and the decolorizing agent is composed of 50% diatomaceous earth and 50% activated carbon;

[0055] The primary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorization agent agglomerates, wherein the solvent is sugar solution and the decolorization agent agglomerates are solids separated in the secondary decolorization and filtration steps.

[0056] The difference between Example 3 and Example 1 is that the ratio of the decolorizing agent in the secondary decolorization and filtration steps is changed, and the other production steps and parameters are consistent with Example 1.

[0057] Comparative Example:

[0058] In this embodiment, the secondary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorizing agent, wherein the solvent is sugar solution and the decolorizing agent is composed of 100% activated carbon;

[0059] The primary decolorization and filtration is made by mixing 90% of solvent and 10% of decolorization agent agglomerates, wherein the solvent is sugar solution and the decolorization agent agglomerates are solids separated in the secondary decolorization and filtration steps.

[0060] The difference between the comparative example and Example 1 is that the components of the decolorizing agent in the secondary decolorization and filtration steps are all changed to activated carbon, and the other production steps and parameters are consistent with Example 1.

[0061] The production tests of each group of Example 1, Example 2, Example 3 and the comparative example were repeated twice, and the comparison was the average data of the two productions.

[0062] The following comparative analysis is performed on the data of Example 1, Example 2, Example 3 and the comparative example, which are the average production data of two times:

[0063] Under the same parameters, the transmittance, chromaticity, clarity and filtration rate of a glucose production method using diatomaceous earth instead of activated carbon were compared.

[0064] Table 1 Comparison of glucose parameters

[0065]

[0066] By comparing the experimental data in Table 1, it can be understood that the transmittance value, chromaticity and clarity of Example 1 in Example 1, Example 2 and Example 3 can reach or exceed the quality standard of the comparative example, and at the same time, it is shown that the filtration rate of Example 1, Example 2 and Example 3 containing diatomaceous earth is faster than that of the comparative example of pure activated carbon, which proves that the filtration, adsorption and decolorization capabilities of the mixed decolorant mixed with diatomaceous earth and the decolorant made of pure activated carbon on the sugar solution can reach or exceed the decolorant made of pure activated carbon.

[0067] It can be seen that the filtration speed can be increased by adding a certain proportion of activated carbon to the decolorizer. At the same time, the mixed decolorizer made by using diatomaceous earth to replace a part of the activated carbon can maximize the role and function of both, which not only increases the filtration speed and increases the output, but also improves the quality of the product and significantly reduces the production cost.

Claims

1. A method for producing glucose by using diatomaceous earth instead of activated carbon, characterized in that: The following steps are involved: S1. Slurry preparation: wheat starch is mixed with water to obtain starch milk, which is pumped into a plate heat exchanger, heated to 40-50°C, with a concentration of 15.5-16.0Be, starch milk protein ≤ 0.3%, fat ≤ 0.15%, pH adjusted to 5.5-6.0 with sodium hydroxide, high temperature amylase added, and enzyme preparation added at 0.2kg / t and pumped into the feeding tank; S2, liquefaction: the sugar solution is pumped from the feeding tank into the ejector for primary injection, the injection temperature is controlled at 100-110℃, and the sugar solution is kept under pressure for 10 minutes in the high-temperature coil. The sugar solution enters the flash tank in a tangential direction, and the sugar solution is rapidly rotated in the flash tank for vapor-liquid separation. After separation, it is cooled to room temperature and pumped into the laminar flow tank through a transfer pump. It is kept at 95℃ for 90-120 minutes, and then a secondary injection is performed. The starch milk is mixed with steam in the ejector, and the injection temperature is 135-138℃. After the secondary injection, the pH is adjusted to 4.5-4.8 with sodium hydroxide, and enzyme preparation is added at 0.3-0.35kg / t; S3, saccharification: the liquefied liquid enters the saccharification tank and is kept at 60-62°C for saccharification for 60 hours, and the saccharification liquid is discharged; S4, slag removal and filtration: the saccharified sugar solution is pumped into the filter for filtration at a filtration temperature of 50-60°C and a filtration rate of 16-20 ml / min; S5, primary decolorization and filtration: put the sugar solution into the decolorization tank, add the mixed decolorizer into the sugar solution and mix evenly for 30 minutes, keep the temperature at 75-80°C, absorb the impurities such as fine protein, fat, pigment in the sugar solution, and then put it into the filter after mixing for solid-liquid separation, and discard the separated solids; S6, primary evaporation: the sugar solution separated from the solid and liquid is pumped into the multi-effect concentrator to remove excess water from the sugar solution. The feed flow rate is 30-35m 3 / h, evaporation time 40-45min, concentration 45-50%; S7, secondary decolorization and filtration: put the sugar solution into the decolorization tank, add the mixed decolorizer into the sugar solution at 0.3 kg / t and mix evenly for 30 minutes, keep the temperature at 70-75 ° C, and then put it into the filter after mixing for solid-liquid separation, and keep the separated solids for secondary use; S8, ion exchange: the sugar solution after solid-liquid separation is exchanged with sugar material through ion exchange column. The exchange process is two-stage exchange. The sugar solution passes through the cation column first and then the anion column. The cations in the sugar solution are removed by the cation column, and the anions in the sugar solution are removed by the anion column. The temperature is 40-50℃, the discharge pH is controlled at 3.8-4.0, and the conductivity is less than 100PPM. S9, secondary evaporation: pump the sugar solution into the multi-effect concentrator at a flow rate of 20-22m 3 / h, evaporation time 40-45min, control concentration at 72.0-73.5%; S10, crystallization: the evaporated liquid is pumped into a horizontal crystallizer, the inlet temperature is 55.0-56.0°C, and mixed with the reserved crystal seeds. After the sugar liquid is full, the material temperature is controlled at 40-45°C. The material is cooled by 32-35°C warm water for the first 25 hours, and the temperature is reduced by 0.3°C per hour. The material is cooled by 18-20°C cold water for the next 25-60 hours, and the temperature is reduced by 0.5°C per hour. The crystallization time is 60 hours, and the outlet temperature is 20-22°C. When the sugar liquid is discharged from the tank, 30% of the massecuite is retained as the crystal seeds for the next tank. S11, separation: the crystallized material is transported to a separator by an auger, and the mother liquor and the washing liquid are separated at a high speed of 1350 rpm, the separation time is 25 minutes, the yield is 50-55%, and the mother liquor and the washing liquid are removed by separation; S12, drying: adopt positive pressure drying, negative pressure cooling airflow drying method for drying, hot air temperature is 100-110 ℃, wind speed is 5-10m / s, drying time is 30-40 minutes, and finished glucose is obtained after drying.

2. A method for producing glucose by using diatomaceous earth instead of activated carbon according to claim 1, characterized in that: The mixed decolorizing agent in step S7 is prepared by mixing 90% of a solvent and 10% of a decolorizing agent, wherein the solvent is water or a sugar solution or a mixture of the two, and the decolorizing agent is a mixture of 30-50% diatomaceous earth and 50-70% activated carbon, wherein the particle size of the diatomaceous earth is 100 meshes, and the particle size of the activated carbon is 200 meshes.

3. The method for producing glucose by using diatomaceous earth instead of activated carbon according to claim 1, characterized in that: The mixed decolorizing agent in step S5 is prepared by mixing 90% of a solvent and 10% of a decolorizing agent agglomerate, wherein the solvent is water or a sugar solution or a mixture of the two, and the decolorizing agent agglomerate is a secondary utilization of the solid separated in step S7.

4. The method for producing glucose by using diatomaceous earth instead of activated carbon according to claim 1, characterized in that: The separation time of step S9 is 20-25 minutes, and the yield is 50-55%.

5. The method for producing glucose by using diatomaceous earth instead of activated carbon according to claim 1, characterized in that: In step S6, after the sugar solution enters the multi-effect concentrator, it is subjected to five-effect vacuum evaporation in sequence. The pressure and temperature of the five-effect vacuum evaporation are as follows: first-effect vacuum: 0.025Mpa, temperature: 78°C; second-effect vacuum: -0.042Mpa, temperature: 72°C; third-effect vacuum: -0.058Mpa, temperature: 65°C; fourth-effect vacuum: -0.072Mpa, temperature: 60°C; fifth-effect vacuum: -0.092Mpa, temperature: 55°C.

6. The method for producing glucose by using diatomaceous earth instead of activated carbon according to claim 1, characterized in that: In step S9, after the sugar solution enters the multi-effect concentrator, it is subjected to five-effect vacuum evaporation in sequence. The pressure and temperature of the five-effect vacuum evaporation are as follows: first-effect vacuum: 0.025Mpa, temperature: 95°C; second-effect vacuum: -0.042Mpa, temperature: 86°C; third-effect vacuum: -0.058Mpa, temperature: 75°C; fourth-effect vacuum: -0.072Mpa, temperature: 68°C; fifth-effect vacuum: -0.092Mpa, temperature: 58°C.

7. The method for producing glucose by using diatomaceous earth instead of activated carbon according to claim 1, characterized in that: After the sugar solution enters the filter, it is filtered through 10um, 5um, 2um, and 1um filters in sequence.

Images