Treatment system for preparing high-purity glucose from starch milk
By combining tubular ultrafiltration membranes, plate and frame pressing, and membrane separation and purification systems, the problems of low glucose purity and unstable processing in traditional methods have been solved, achieving the production of high-purity glucose and reducing costs and resource consumption.
Patent Information
- Application Number
- CN202423240619.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-27
- Publication Date
- 2026-01-02
- Estimated Expiration
- 2034-12-27
AI Technical Summary
In existing technologies, traditional plate and frame pressing systems require a large amount of filter aids and are costly when processing saccharified liquids, while membrane separation technology suffers from short membrane life and severe pollution, resulting in unstable glucose purity and quality.
A combination of tubular ultrafiltration membrane separation system, plate and frame pressing system, and membrane separation and purification system is used, along with an ion exchange system. Suspended proteins are removed by tubular ultrafiltration membrane, solid residue is removed by plate and frame pressing, soluble proteins are removed by decolorization tank, inorganic salts and trace proteins are removed by ion exchange system, and finally high-purity glucose is obtained by membrane separation and purification system.
This method achieves a glucose purity of over 99.5%, reduces labor and resource consumption, improves processing stability and glucose purity, and lowers costs.
Smart Images
Figure CN223752818U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to starch lactose production technical field, especially a kind of starch lactose high-purity glucose processing system. BACKGROUND
[0002] In the glucose production process, starch lactose is subjected to saccharification reaction and generates saccharification liquor containing a large amount of saccharifying protein. The presence of saccharifying protein affects the purity and quality of glucose, so it is necessary to clarify and remove protein from the saccharification liquor. The traditional treatment method mainly uses a plate and frame pressing system to remove saccharifying protein by adding a large amount of diatomite and activated carbon and other filter aids. This method not only has high cost, but also needs a large amount of manual participation, and the treatment effect is unstable. Direct use of traditional membrane separation technology for purification still has some problems, such as short service life of the membrane and serious membrane pollution.
[0003] Therefore, we propose a starch lactose high-purity glucose processing system to solve the above problems. UTILITY MODEL CONTENTS
[0004] The utility model aims at solving the shortcomings in the prior art and proposes a starch lactose high-purity glucose processing system.
[0005] In order to achieve the above-mentioned purpose, the utility model adopts the following technical scheme:
[0006] A starch lactose high-purity glucose processing system includes a saccharification liquor storage tank, the saccharification liquor storage tank is connected with a tubular ultrafiltration membrane separation system and a plate and frame pressing system and a membrane separation purification system, the saccharification liquor storage tank is connected with a decolorizing tank through the tubular ultrafiltration membrane separation system, the decolorizing tank is connected with an ion exchange system clear liquid tank, and the ion exchange system clear liquid tank is connected with the membrane separation purification system.
[0007] Preferably, the tubular ultrafiltration membrane separation system includes a tubular ultrafiltration membrane separation assembly and a water inlet pump, the water inlet end of the water inlet pump is connected with the saccharification liquor storage tank, the water outlet end of the water inlet pump is connected to the water inlet end of the tubular ultrafiltration membrane separation assembly, and the water outlet end of the tubular ultrafiltration membrane separation assembly is connected to the decolorizing tank.
[0008] Preferably, the plate and frame pressing system includes a tubular membrane thick liquid tank, a plate and frame feed pump, a diaphragm filter press, a pressing water tank and a pressing pump, the thick water end of the tubular ultrafiltration membrane separation assembly is connected to the tubular membrane thick liquid tank, the water inlet end of the diaphragm filter press is connected to the plate and frame feed pump, the inlet end of the plate and frame feed pump is connected to the outlet end of the thick liquid storage tank, the pressing clear liquid water outlet end of the diaphragm filter press is connected to the saccharification liquor storage tank, and the water outlet end of the pressing water tank is connected to the water inlet end of the diaphragm filter press through the pressing pump.
[0009] Preferably, the water production end of the decoloring tank is connected with an ion exchange feed pump, the water outlet end of the ion exchange feed pump is connected with an ion exchange system, the water production end of the ion exchange system is connected with an ion exchange system clear liquid tank, and the clear liquid generated by the ion exchange system enters the ion exchange system clear liquid tank.
[0010] Preferably, the membrane separation and purification system comprises a membrane separation and purification system feed pump, a membrane separation and purification system membrane group and a finished product collection tank, the water inlet end of the membrane separation and purification system feed pump is connected with the water outlet end of the ion exchange system clear liquid tank, the outlet end of the ion exchange system clear liquid tank enters the membrane separation and purification assembly through the membrane separation and purification system feed pump, the membrane separation and purification assembly is connected with the finished product collection tank, and the clear liquid obtained by the membrane separation and purification assembly enters the finished product collection tank.
[0011] Preferably, the diaphragm filter press is made of stainless steel, and the diaphragm filter press is provided with a plurality of filter plates.
[0012] Preferably, the tubular ultrafiltration membrane separation assembly obtains tubular ultrafiltration membrane clear liquid, the decoloring tank can stir and adsorb the tubular ultrafiltration membrane clear liquid, and decoloring clear liquid is obtained.
[0013] Compared with the prior art, the beneficial effects of the utility model are as follows:
[0014] The present application can completely solve the problem that a large amount of diatomite and activated carbon is added when the sugar solution is pressed by the plate and frame pressing system, improve the purity of glucose to more than 99.5%, reduce the participation of manual work, and improve the stability of the product. BRIEF DESCRIPTION OF DRAWINGS
[0015] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings needed in the embodiments or the prior art description will be briefly introduced as follows, and obviously, other drawings can also be obtained by those skilled in the art without creative labor on the basis of these drawings.
[0016] Figure 1 The present application is a structural schematic diagram.
[0017] In the figure: 1, saccharification liquid storage tank; 2, water inlet pump; 3, tubular ultrafiltration membrane separation assembly; 4, tubular membrane concentrated liquid tank; 5, plate and frame feed pump; 6, diaphragm filter press; 7, squeezing water tank; 8, squeezing pump; 9, decoloring tank; 10, ion exchange feed pump; 11, ion exchange system; 12, ion exchange system clear liquid tank; 13, membrane separation purification system feed pump; 14, membrane separation purification assembly; 15, finished product collection tank; 101, tubular ultrafiltration membrane separation system; 201, plate and frame squeezing system; 301, membrane separation purification system. DETAILED DESCRIPTION
[0018] The technical solutions in the embodiments of the utility model will be clearly and completely described below with reference to the drawings in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, rather than all the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the utility model.
[0019] In the description of the utility model, it should be understood that the terms "opening", "upper", "lower", "thickness", "top", "middle", "length", "inner", "periphery" and the like indicate the orientation or positional relationship, which are only for the convenience of describing the utility model and simplifying the description, and do not indicate or imply that the components or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the utility model.
[0020] Reference Figure 1 A starch milk high-purity glucose treatment system, comprising saccharification liquid storage tank 1, tubular ultrafiltration membrane separation system 101 and decoloring tank 9, ion exchange system 11, plate and frame squeezing system 201, membrane separation purification system 301 connected in sequence; the saccharification liquid storage tank 1 is connected to the decoloring tank 9 through the water production end of the tubular ultrafiltration membrane separation assembly 3, the concentrated water end of the tubular ultrafiltration membrane separation assembly 3 is connected to the tubular membrane concentrated liquid tank 4, the plate and frame squeezing system 201 returns the squeezing clear liquid to the saccharification liquid storage tank 1, the discharge end of the decoloring tank 9 is connected to the ion exchange system 11, and the discharge of the ion exchange system 11 is connected to the membrane separation purification system 301.
[0021] The tubular ultrafiltration membrane separation system 101 comprises a tubular ultrafiltration membrane separation assembly 3, a water inlet pump 2, and the water inlet pump 2 is connected to the saccharification liquid storage tank 1; the water outlet end of the water inlet pump 2 is connected to the water inlet end of the tubular ultrafiltration membrane separation assembly 3; the water production end of the tubular ultrafiltration membrane separation assembly 3 is connected to the decoloring tank 9; and the concentrated water end of the tubular ultrafiltration membrane separation assembly 3 is connected to the tubular membrane concentrated liquid tank 4.
[0022] The pipe type ultrafiltration membrane separation system 101 selects a large channel 6-8 mm anti-pollution filter membrane, and the material selects PEK material resistant to pH value of 13 or above, to ensure that the flux is restored after heavy pollution by increasing the amount of reagent, rapid cleaning, the molecular weight cut-off is 0.01-0.1 μm. The pipe type ultrafiltration membrane device in the treatment of saccharification liquid, the flow rate is 3-4 m / s, the temperature is 60-70℃, the saccharification liquid recovery rate is controlled to be greater than 99.5%, and only a small amount of sugar liquid is discharged outside the system with the squeezing residue. The clear liquid after the pipe type ultrafiltration membrane treatment has light transmittance of 95%-98% detected at 420 nm absorbance. The ultrafiltration membrane device adopts a series connection, parallel connection or series-parallel combination mode, and adopts full automatic control, and the ultrafiltration water and concentrated water adopt a regulating valve to control the recovery rate.
[0023] The plate and frame squeezing system 201 includes a pipe membrane thick liquid tank 4, a plate and frame feed pump 5, a diaphragm filter press 6, a squeezing water tank 7 and a squeezing pump 8. The water inlet end of the diaphragm filter press 6 is connected to the plate and frame feed pump 5, the inlet end of the plate and frame feed pump 5 is connected to the outlet end of the pipe membrane thick liquid tank 4, the squeezing clear liquid water outlet end of the diaphragm filter press 6 is connected to the saccharification liquid storage tank 1, the squeezing residue is transported outside, and the water outlet end of the squeezing water tank 7 is connected to the water inlet end of the diaphragm filter press 6 through the squeezing pump 8. The squeezing water returns to the squeezing water tank 7.
[0024] The diaphragm filter press 6 is made of stainless steel, the filter plate adopts a pure polypropylene feed diaphragm filter plate, the food-grade filter cloth is made of polypropylene or polyester, the filtering precision is at least 3-5 microns, and the squeezing pressure is 0.2-0.5 MPa. The pipe type ultrafiltration thick liquid containing a relatively high amount of suspended protein passes through the diaphragm filter press 6, the filtrate enters the saccharification liquid storage tank 1 again, and the squeezing pump 8 rapidly extrudes the suspended protein in the diaphragm filter press 6 by using the circulating water of the squeezing water tank 7 to form filter cake containing a relatively low amount of sugar liquid.
[0025] The pipe type ultrafiltration membrane separation assembly 3 obtains pipe type ultrafiltration membrane clear liquid, the inside of the decolorization tank 9 can stir and adsorb the pipe type ultrafiltration membrane clear liquid, and decolorized clear liquid is obtained. The water outlet end of the decolorization tank 9 is connected with an ion exchange feed pump 10, the water outlet end of the ion exchange feed pump 10 is connected with an ion exchange system 11, the water outlet end of the ion exchange system 11 is connected with an ion exchange system clear liquid tank 12, and the clear liquid generated by the ion exchange system 11 enters the ion exchange system clear liquid tank 12.
[0026] For the above example, those skilled in the art should know that, in the implementation of the above technical solutions, the soluble protein content of the starch lactose glucose saccharification liquid is 0.05-0.08 g / L, the light transmittance detected at 420 nm absorbance is 70%-85%, the sugar liquid concentration is 36%-40%, and the saccharification liquid contains about 5%-7% of suspended protein.
[0027] For the above example, those skilled in the art should know that, in the implementation of the above technical solutions, the saccharification liquid is clarified by using the tubular ultrafiltration membrane separation system 101 to remove suspended proteins; the tubular ultrafiltration membrane separation assembly 3 selects high-temperature alkali-resistant tubular ultrafiltration membrane with a pore size of 0.01-0.1 μm; after the tubular ultrafiltration membrane separation system 101 processes the saccharification liquid, the clear liquid has a 420 nm absorbance detection transmittance of 95%-98%; the tubular ultrafiltration membrane separation system 101 is resistant to temperatures of 60-70°C, and the tubular ultrafiltration membrane separation assembly 3 is resistant to an alkali concentration of up to 4%; the flow rate of the system is preferably 3-5 m / s; and the clear liquid recovery rate is greater than 99.5%.
[0028] For the above example, those skilled in the art should know that, in the implementation of the above technical solutions, the concentrated liquid after the tubular ultrafiltration membrane separation system 101 processes is sent to the plate-and-frame pressing system 201, which selects a diaphragm filter press with a pressing pressure of 0.2-0.5 Mpa. After the plate-and-frame pressing system 201 processes the tubular ultrafiltration concentrated liquid, sugar residue is formed.
[0029] For the above example, those skilled in the art should know that, in the implementation of the above technical solutions, the clear liquid produced by the tubular ultrafiltration membrane separation system 101 enters the decolorizing tank 9 to remove soluble proteins and colored substances. The decolorizing tank 9 uses activated carbon powder with a specific surface area of 500-1200 m2 / g. After the decolorizing tank 9 processes the clear liquid from the tubular ultrafiltration membrane separation system 101, the soluble protein content is 0.01-0.02 g / L, and the colority is 20%-38%.
[0030] For the above example, those skilled in the art should know that, in the implementation of the above technical solutions, the decolorized clear liquid enters the ion exchange system 11, which selects cation and anion exchange resins to further adsorb and remove inorganic salts and other trace proteins and other impurities in the sugar liquid, producing a glucose solution with a concentration of 34%-41%, a pH of 3.7-4.9, an electrical conductivity of 32-110 μS / cm, and a glucose content of 94.5% or more.
[0031] The clear liquid produced by the ion exchange system 11 enters the ion exchange system clear liquid tank 12, and the outlet end of the ion exchange system clear liquid tank 12 enters the membrane separation purification assembly 14 through the membrane separation purification system feed pump 13, and the obtained clear liquid enters the finished product collection tank 15.
[0032] For the above example, those skilled in the art should know that when implementing the above technical solutions, the ion exchange system 11 produces an ion-exchanged glucose solution with a concentration of 34%-41%, a pH of 3.7-4.9, a conductivity of 32-110 μS / cm, and a glucose content of 94.5% or more into the membrane separation and purification system 301. The membrane separation and purification system 301 utilizes a spiral nanofiltration membrane with a molecular weight cutoff of 200-700 Da. The operating pressure of the membrane separation and purification system 301 is preferably 2.0-3.5 MPa, and the temperature is controlled below 55°C. The membrane separation and purification system produces a clear solution with a glucose purity of 99.5% or more, and a glucose recovery rate of 50% or more. The device is fully automated.
[0033] In the utility model, the working principle of the device is as follows:
[0034] The saccharified liquid after starch lactosaccharification and liquefaction is stored in the saccharified liquid storage tank 1. The obtained saccharified liquid is sent to the tubular ultrafiltration membrane separation system 101 to obtain tubular ultrafiltration concentrated liquid and tubular ultrafiltration clear liquid. The obtained ultrafiltration concentrated liquid is sent to the plate and frame pressing system 201 to obtain protein-containing sugar residue solids; the obtained tubular ultrafiltration clear liquid is sent to the decolorization tank 9 to obtain decolorized clear liquid. The obtained decolorized clear liquid is sent to the ion exchange system 11 to obtain ion-exchanged clear liquid; the ion-exchanged clear liquid obtained in the above step is sent to the membrane separation and purification system 301 to obtain purified clear liquid and purified concentrated liquid. The purified clear liquid obtained in the above step is sent to the finished product collection tank 15.
[0035] The above is only a preferred specific embodiment of the utility model, but the protection scope of the utility model is not limited to this, any person skilled in the art in the utility model disclosed technical range, according to the utility model technical scheme and the utility model concept, equivalent replacement or change, all should be covered in the protection scope of the utility model.
Claims
1. A starch milk high purity glucose processing system comprising a saccharified liquid storage tank (1), characterized by, The saccharification liquid storage tank (1) is connected with a tubular ultrafiltration membrane separation system (101), a plate and frame squeezing system (201) and a membrane separation and purification system (301), the saccharification liquid storage tank (1) is connected with a decoloring tank (9) through the tubular ultrafiltration membrane separation system (101), the decoloring tank (9) is connected with an ion exchange system clear liquid tank (12), and the ion exchange system clear liquid tank (12) is connected with the membrane separation and purification system (301).
2. A high purity glucose processing system for starch dairy products according to claim 1, characterized in that, The tubular ultrafiltration membrane separation system (101) comprises a tubular ultrafiltration membrane separation assembly (3) and a water inlet pump (2), the water inlet end of the water inlet pump (2) is connected with the saccharification liquid storage tank (1), the water outlet end of the water inlet pump (2) is connected to the water inlet end of the tubular ultrafiltration membrane separation assembly (3), and the water outlet end of the tubular ultrafiltration membrane separation assembly (3) is connected to the decoloring tank (9).
3. A high purity glucose processing system for starch dairy products according to claim 1, characterized in that, The plate and frame squeezing system (201) comprises a tubular membrane concentrated liquid tank (4), a plate and frame feed pump (5), a diaphragm filter press (6), a squeezing water tank (7) and a squeezing pump (8), the concentrated water end of the tubular ultrafiltration membrane separation assembly (3) is connected to the tubular membrane concentrated liquid tank (4), the water inlet end of the diaphragm filter press (6) is connected to the plate and frame feed pump (5), the inlet end of the plate and frame feed pump (5) is connected to the outlet end of the tubular membrane concentrated liquid tank (4), the squeezing clear liquid water outlet end of the diaphragm filter press (6) is connected to the saccharification liquid storage tank (1), and the water outlet end of the squeezing water tank (7) is connected to the water inlet end of the diaphragm filter press (6) through the squeezing pump (8).
4. The high purity glucose processing system of claim 1, wherein, The water outlet end of the decoloring tank (9) is connected with an ion exchange feed pump (10), the water outlet end of the ion exchange feed pump (10) is connected with an ion exchange system (11), the water outlet end of the ion exchange system (11) is connected with an ion exchange system clear liquid tank (12), and the clear liquid generated by the ion exchange system (11) enters the ion exchange system clear liquid tank (12).
5. A high purity glucose processing system for starch dairy products according to claim 4, characterized in that, The membrane separation and purification system (301) comprises a membrane separation and purification system feed pump (13), a membrane separation and purification assembly (14) and a finished product collection tank (15), the water inlet end of the membrane separation and purification system feed pump (13) is connected with the water outlet end of the ion exchange system clear liquid tank (12), the outlet end of the ion exchange system clear liquid tank (12) enters the membrane separation and purification assembly (14) through the membrane separation and purification system feed pump (13), the water outlet end of the membrane separation and purification assembly (14) is connected with the finished product collection tank (15), and the clear liquid obtained by the membrane separation and purification assembly (14) enters the finished product collection tank (15).
6. A high purity glucose processing system for starch dairy products according to claim 3, characterized in that, The diaphragm filter press (6) is made of stainless steel, and the diaphragm filter press (6) is provided with a plurality of filter plates.
7. A high purity glucose processing system for starch dairy products according to claim 2, characterized in that, The tubular ultrafiltration membrane separation assembly (3) obtains tubular ultrafiltration membrane clear liquid, the inside of the decoloring tank (9) can stir and adsorb the tubular ultrafiltration membrane clear liquid, and decoloring clear liquid is obtained.