Device for producing D-psicose by utilizing fructose solution

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By designing a device that utilizes fructose solution and using hollow fiber membranes and exchange resin columns to separate, desalt and decolorize enzymes and mixed solutions, the problems of heating and multi-stage decolorization in the existing D-psicose production process are solved. Low-cost, high-purity D-psicose production was achieved.

CN222349015UActive Publication Date: 2025-01-14DONGTAI HAORUI BIOTECHNOLOGY CO LTD

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Patent Information

Application Number: CN202420885778.4
Authority / Receiving Office: CN · China
Patent Type: Utility models(China)
Current Assignee / Owner
Filing Date: 2024-04-25
Publication Date: 2025-01-14
Estimated Expiration: 2034-04-25

AI Technical Summary

Technical Problem

The existing D-psicose production process requires heating to inactivate the enzyme and perform multi-stage decolorization, which increases production costs.

Method used

A device for producing D-psicose from fructose solution was designed. D-psicose 3-epimerase was added to the fructose solution for conversion, and a hollow fiber membrane was used to separate the enzyme and mixed solution. Desalination and decolorization are carried out through ceramic membrane, cation exchange resin column and anion exchange resin column, and finally the D-psicose finished product is obtained through suction filtration.

Benefits of technology

The production of D-psicose that does not require heating to inactivate enzymes and multi-stage decolorization is achieved, simplifying the process, reducing production costs, and improving product purity.

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Abstract

The utility model discloses a device for producing D-psicose by utilizing a fructose solution, and relates to the field of D-psicose production, an inlet of a first reaction kettle is respectively communicated with a D-psicose 3-epimerase tank through a pipeline, an outlet of the first reaction kettle is communicated with a hollow fiber membrane through a pipeline, and the hollow fiber membrane is communicated with a second reaction kettle through a pipeline. An outlet of the hollow fiber membrane is communicated with a second reaction kettle through a pipeline; an inlet of the second reaction kettle is communicated with a glucosamine-6-phosphate synthase tank through a pipeline; an outlet of the second reaction kettle is communicated with a cation exchange resin column, an outlet of the cation exchange resin column is communicated with an anion exchange resin column through a pipeline, an outlet of the anion exchange resin column is communicated with a first concentration tank through a pipeline, and an outlet of the first concentration tank is communicated with a suction filtration tank through a pipeline; a solid phase outlet of the suction filtration tank is communicated with a D-psicose finished product tank through a pipeline. In addition, the obtained D-psicose product is high in purity and low in production cost.

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Description

Technical Field

[0001] The utility model relates to the field of D-psicose production, in particular to a device for producing D-psicose by utilizing a fructose solution. Background Art

[0002] D-psicose is a very important rare ketohexose with a sweetness of 70% of sucrose, but its energy is almost zero, its solvent properties and taste are similar to sucrose, and it can undergo Maillard reaction. In the food and medicine industry, D-psicose is an ideal substitute for sucrose. In addition, D-psicose has the functions of inhibiting obesity, lowering blood sugar, and lowering blood lipids, and is very suitable for consumption by diabetic patients and obese people, so it has significant effects in medical treatment and health care. At present, the production of D-psicose is mainly based on the isomerization reaction of D-fructose catalyzed by isomerase. After the reaction is completed, it needs to be heated to inactivate the enzyme, and activated carbon needs to be used for multi-stage decolorization, which increases the production cost. Summary of the invention

[0003] The technical problem to be solved by the utility model is: in view of the shortcomings of the prior art, a device for producing D-psicose by using fructose solution is provided, which does not require heating to inactivate the enzyme and does not require multi-stage decolorization, and has low production cost.

[0004] In order to solve the above technical problems, the technical solution of the utility model is:

[0005] A device for producing D-psicose using a fructose solution, comprising a first reactor, wherein an inlet of the first reactor is connected to a fructose solution tank, a D-psicose 3-epimerase tank, and a buffer tank through pipelines, an outlet of the first reactor is connected to a hollow fiber membrane through a pipeline, the outlet of the hollow fiber membrane is connected to a second reactor through a pipeline, and an inlet of the second reactor is connected to a glucosamine-6-phosphate synthase tank, an ammonium chloride tank, and the buffer tank through pipelines;

[0006] The outlet of the second reactor is connected to a ceramic membrane device through a pipeline, the clear liquid outlet of the ceramic membrane device is connected to a cation exchange resin column through a pipeline, the outlet of the cation exchange resin column is connected to an anion exchange resin column through a pipeline, the outlet of the anion exchange resin column is connected to a first concentration tank through a pipeline, the outlet of the first concentration tank is connected to a suction filtration tank through a pipeline, and the solid phase outlet of the suction filtration tank is connected to a D-psicose finished product tank through a pipeline.

[0007] As an improved technical solution, the clear liquid outlet of the ceramic membrane device is connected to an ultrafiltration membrane device through a pipeline, and the clear liquid outlet of the ultrafiltration membrane device is connected to the cation exchange resin column through a pipeline.

[0008] As an improved technical solution, the filtration pore size of the ceramic membrane is 20-100 nm.

[0009] As an improved technical solution, the molecular weight cutoff of the ultrafiltration membrane device is 5000-10000Da.

[0010] As an improved technical solution, the outlet of the anion exchange resin column is connected to a nanofiltration membrane device through a pipeline, and the concentrated liquid outlet of the nanofiltration membrane device is connected to the first concentration tank through a pipeline.

[0011] As an improved technical solution, the filtration pore size of the nanofiltration membrane device is 150-300Da.

[0012] As a preferred technical solution, the inlet of the suction filtration tank is connected to an ethanol tank through a pipeline.

[0013] As a preferred technical solution, the inlet of the cation exchange resin column is connected to a hydrochloric acid solution tank through a pipeline, the outlet of the cation exchange resin column is connected to a second concentration tank through a pipeline, the outlet of the second concentration tank is connected to a first filter through a pipeline, and the solid phase outlet of the first filter is connected to a crude glucosamine hydrochloride tank through a pipeline.

[0014] As a preferred technical solution, the outlet of the cation exchange resin column is connected to a collection liquid tank through a pipeline.

[0015] As a preferred technical solution, the outlet of the crude glucosamine hydrochloride tank is connected to a purification tank via a pipeline, the inlet of the purification tank is connected to a purified water tank and an activated carbon tank via pipelines, respectively, the outlet of the purification tank is connected to a second filter via a pipeline, the outlet of the second filter is connected to a dryer via a pipeline, and the outlet of the dryer is connected to a finished glucosamine phosphate tank.

[0016] Due to the adoption of the above technical solution, the beneficial effects of the utility model are:

[0017] The utility model discloses a device for producing D-psicose by utilizing a fructose solution, comprising a first reactor, wherein an inlet of the first reactor is respectively connected with a fructose solution tank, a D-psicose 3-epimerase tank and a buffer tank through pipelines, an outlet of the first reactor is respectively connected with a hollow fiber membrane through a pipeline, the outlet of the hollow fiber membrane is connected with a second reactor through a pipeline, and an inlet of the second reactor is respectively connected with a glucosamine-6-phosphate synthase tank, an ammonium chloride tank and the buffer tank through pipelines; an outlet of the second reactor is connected with a ceramic membrane device through a pipeline, a clear liquid outlet of the ceramic membrane device is connected with a cation exchange resin column through a pipeline, an outlet of the cation exchange resin column is connected with an anion exchange resin column through a pipeline, an outlet of the anion exchange resin column is connected with a first concentration tank through a pipeline, an outlet of the first concentration tank is connected with a suction filtration tank through a pipeline, and a solid phase outlet of the suction filtration tank is connected with a D-psicose finished product tank through a pipeline. D-psicose 3-epimerase is added to a fructose solution for conversion to obtain a mixed solution containing fructose and psicose, which is then passed through a hollow fiber membrane to separate the enzyme from the mixed solution, and the mixed solution is passed through a ceramic membrane, a cation exchange resin column, and an anion exchange resin column, and then heat concentrated, cooled, and filtered to obtain D-psicose. There is no need to heat to inactivate the enzyme, and desalting and decolorizing are achieved through the cation exchange resin column and the anion exchange resin column, and there is no need for decolorization using multi-stage activated carbon, which simplifies the production process. In addition, the obtained D-psicose product has high purity and low production cost.

[0018] The clear liquid outlet of the ceramic membrane device of the utility model is connected to the ultrafiltration membrane device through a pipeline, and the clear liquid outlet of the ultrafiltration membrane device is connected to the cation exchange resin column through a pipeline. The feed liquid is further filtered and impurities are removed by the ultrafiltration membrane, thereby improving the purity of the product.

[0019] The outlet of the anion exchange resin column is connected to a nanofiltration membrane device through a pipeline, and the concentrated liquid outlet of the nanofiltration membrane device is connected to the first concentration tank through a pipeline. The permeate is initially concentrated by the nanofiltration membrane device, which reduces the energy consumption during subsequent heating and concentration, and also reduces the subsequent concentration time and shortens the process cycle.

[0020] The filtration pore size of the ceramic membrane is 20-100 nm, the molecular weight cutoff of the ultrafiltration membrane device is 5000-10000 Da, and the filtration pore size of the nanofiltration membrane device is 150-300 Da, so the interception and filtration effects are better.

[0021] The inlet of the suction filtration tank is connected to an ethanol tank through a pipeline. The crude D-psicose product is washed with ethanol, and the obtained D-psicose product has higher purity.

[0022] The inlet of the cation exchange resin column is connected to a hydrochloric acid solution tank through a pipeline, the outlet of the cation exchange resin column is connected to a second concentration tank through a pipeline, the outlet of the second concentration tank is connected to a first filter through a pipeline, and the solid phase outlet of the first filter is connected to a crude glucosamine hydrochloride tank through a pipeline. The glucosamine hydrochloride adsorbed on the cation exchange resin column is parsed by a hydrochloric acid solution, and the effluent with a pH of 2-3 is collected and concentrated and filtered to obtain a crude glucosamine hydrochloride tank. The separation of the target product is achieved without the need for simulating a moving bed, and the separation of D-psicose and glucosamine hydrochloride under the same substrate condition is also achieved. Compared with the traditional enzymatic process, it has the advantages of saving time and economic cost, and does not require enzyme inactivation and multi-stage decolorization, and the product purity is high and the by-products are few.

[0023] The outlet of the cation exchange resin column is connected to a liquid collection tank through a pipeline, and the effluent with a pH value less than 2 is used for preparing a hydrochloric acid solution, thereby avoiding waste and saving raw materials.

[0024] The outlet of the crude glucosamine hydrochloride tank is connected to a purification tank through a pipeline, the inlet of the purification tank is connected to a purified water tank and an activated carbon tank through pipelines, the outlet of the purification tank is connected to a second filter through a pipeline, the outlet of the second filter is connected to a dryer through a pipeline, and the outlet of the dryer is connected to a finished glucosamine phosphate tank. The purity of the glucosamine hydrochloride product is improved by re-dissolving and decolorizing the crude glucosamine hydrochloride and then re-crystallizing it. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] The utility model is further described below in conjunction with the accompanying drawings and embodiments.

[0026] Figure 1 It is a structural schematic diagram of an embodiment of the utility model;

[0027] Wherein: 1. first reactor; 2. fructose solution tank; 3. D-psicose 3-isomerase tank; 4. buffer tank; 5. hollow fiber membrane; 6. second reactor; 7. glucosamine-6-phosphate synthase tank; 8. ammonium chloride tank; 9. ceramic membrane device; 10. cation exchange resin column; 11. anion exchange resin column; 12. first concentration tank; 13. suction filtration tank; 14. D-psicose finished product tank; 15. ultrafiltration membrane device; 16. nanofiltration membrane device; 17. ethanol tank; 18. hydrochloric acid solution tank; 19. second concentration tank; 20. first filter; 21. glucosamine hydrochloride crude product tank; 22. collection liquid tank; 23. purification tank; 24. purified water tank; 25. activated carbon tank; 26. second filter; 27. dryer; 28. glucosamine phosphate finished product tank. DETAILED DESCRIPTION

[0028] The present invention is further described below in conjunction with the accompanying drawings and embodiments.

[0029] like Figure 1 As shown, a device for producing D-psicose using a fructose solution comprises a first reactor 1, wherein the inlet of the first reactor 1 is connected to a fructose solution tank 2, a D-psicose 3-epimerase tank 3 and a buffer tank 4 through pipelines, respectively; the outlet of the first reactor 1 is connected to a hollow fiber membrane 5 through a pipeline, the outlet of the hollow fiber membrane 5 is connected to a second reactor 6 through a pipeline, and the inlet of the second reactor 6 is connected to a glucosamine-6-phosphate synthase tank 7, an ammonium chloride tank 8 and the buffer tank 4 through pipelines, respectively; the outlet of the second reactor 6 is connected to a ceramic membrane device 9 through a pipeline, the clear liquid outlet of the ceramic membrane device 9 is connected to a cation exchange resin column 10 through a pipeline, the outlet of the cation exchange resin column 10 is connected to an anion exchange resin column 11 through a pipeline, the outlet of the anion exchange resin column 11 is connected to a first concentration tank 12 through a pipeline, the outlet of the first concentration tank 12 is connected to a suction filtration tank 13 through a pipeline, and the solid phase outlet of the suction filtration tank 13 is connected to a D-psicose finished product tank 14 through a pipeline. D-psicose 3-epimerase is added to the fructose solution for conversion to obtain a mixed solution containing fructose and psicose, which enters the hollow fiber membrane 5 to separate the enzyme and the mixed solution, and the mixed solution enters the ceramic membrane, the cation exchange resin column 10, and the anion exchange resin column 11, and then is thermally concentrated, cooled, and filtered to obtain D-psicose. There is no need to heat to inactivate the enzyme, and desalting and decolorization are achieved by the cation exchange resin column 10 and the anion exchange resin column 11, and multi-stage activated carbon decolorization is not required, which simplifies the production process. In addition, the obtained D-psicose product has high purity and low production cost.

[0030] The clear liquid outlet of the ceramic membrane device 9 is connected to the ultrafiltration membrane device 15 through a pipeline, and the clear liquid outlet of the ultrafiltration membrane device 15 is connected to the cation exchange resin column 10 through a pipeline. The feed liquid is further filtered and impurities are removed by the ultrafiltration membrane, thereby improving the purity of the product.

[0031] The outlet of the anion exchange resin column 11 is connected to the nanofiltration membrane device 16 through a pipeline, and the concentrated liquid outlet of the nanofiltration membrane device 16 is connected to the first concentration tank 12 through a pipeline. The nanofiltration membrane device 16 performs preliminary concentration on the permeate, which reduces the energy consumption during subsequent heating and concentration, and also reduces the subsequent concentration time and shortens the process cycle.

[0032] The filtration pore size of the ceramic membrane device 9 is 20-100 nm, the molecular weight cutoff of the ultrafiltration membrane device 15 is 5000-10000 Da, and the filtration pore size of the nanofiltration membrane device 16 is 150-300 Da, so the interception and filtration effects are better.

[0033] The inlet of the suction filtration tank 13 is connected to the ethanol tank 17 through a pipeline. The crude D-psicose is washed with ethanol, and the obtained D-psicose product has higher purity.

[0034] The inlet of the cation exchange resin column 10 is connected to the hydrochloric acid solution tank 18 through a pipeline, the outlet of the cation exchange resin column 10 is connected to the second concentration tank 19 through a pipeline, the outlet of the second concentration tank 19 is connected to the first filter 20 through a pipeline, and the solid phase outlet of the first filter 20 is connected to the glucosamine hydrochloride crude product tank 21 through a pipeline. The glucosamine hydrochloride adsorbed on the cation exchange resin column 10 is analyzed by the hydrochloric acid solution, and the effluent with a pH of 2-3 is collected and concentrated and filtered to obtain the glucosamine hydrochloride crude product tank 21. The separation of the target product is achieved without the need for simulating a moving bed, and the separation of D-psicose and glucosamine hydrochloride under the same substrate condition is also achieved. Compared with the traditional enzymatic process, it has the advantages of saving time and economic cost, and does not require enzyme inactivation and multi-stage decolorization, and the product purity is high and the by-products are small.

[0035] The outlet of the cation exchange resin column 10 is connected to a liquid collection tank 22 through a pipeline, and the effluent with a pH value less than 2 is used for preparing a hydrochloric acid solution, thereby avoiding waste and saving raw materials.

[0036] The outlet of the crude glucosamine hydrochloride tank 21 is connected to a purification tank 23 through a pipeline, the inlet of the purification tank 23 is connected to a purified water tank 24 and an activated carbon tank 25 through pipelines, the outlet of the purification tank 23 is connected to a second filter 26 through a pipeline, the outlet of the second filter 26 is connected to a dryer 27 through a pipeline, and the outlet of the dryer 27 is connected to a finished glucosamine phosphate tank 28. The purity of the glucosamine hydrochloride product is improved by re-dissolving and decolorizing the crude glucosamine hydrochloride and then re-crystallizing it.

[0037] It should be understood that these embodiments are only used to illustrate the present invention and are not used to limit the scope of the present invention. In addition, it should be understood that after reading the content taught by the present invention, those skilled in the art can make various changes or modifications to the present invention, and these equivalent forms also fall within the scope defined by the claims attached to this application.

Claims

1. A device for producing D-psicose using a fructose solution, characterized in that: The invention comprises a first reactor, wherein the inlet of the first reactor is connected to a fructose solution tank, a D-psicose 3-epimerase tank and a buffer tank through pipelines, the outlet of the first reactor is connected to a hollow fiber membrane through a pipeline, the outlet of the hollow fiber membrane is connected to a second reactor through a pipeline, and the inlet of the second reactor is connected to a glucosamine-6-phosphate synthase tank, an ammonium chloride tank and the buffer tank through pipelines; The outlet of the second reactor is connected to a ceramic membrane device through a pipeline, the clear liquid outlet of the ceramic membrane device is connected to a cation exchange resin column through a pipeline, the outlet of the cation exchange resin column is connected to an anion exchange resin column through a pipeline, the outlet of the anion exchange resin column is connected to a first concentration tank through a pipeline, the outlet of the first concentration tank is connected to a suction filtration tank through a pipeline, and the solid phase outlet of the suction filtration tank is connected to a D-psicose finished product tank through a pipeline.

2. The device for producing D-psicose using fructose solution according to claim 1, characterized in that: The clear liquid outlet of the ceramic membrane device is connected to the ultrafiltration membrane device through a pipeline, and the clear liquid outlet of the ultrafiltration membrane device is connected to the cation exchange resin column through a pipeline.

3. The device for producing D-psicose using fructose solution according to claim 2, characterized in that: The filtration pore size of the ceramic membrane is 20-100 nm.

4. The device for producing D-psicose using fructose solution according to claim 2, characterized in that: The molecular weight cut-off of the ultrafiltration membrane device is 5000-10000Da.

5. The device for producing D-psicose using fructose solution according to claim 1, characterized in that: The outlet of the anion exchange resin column is connected to a nanofiltration membrane device through a pipeline, and the concentrated liquid outlet of the nanofiltration membrane device is connected to the first concentration tank through a pipeline.

6. The device for producing D-psicose using fructose solution according to claim 5, characterized in that: The filtration pore size of the nanofiltration membrane device is 150-300Da.

7. The device for producing D-psicose using fructose solution according to claim 1, characterized in that: The inlet of the suction filtration tank is connected with an ethanol tank through a pipeline.

8. The device for producing D-psicose using fructose solution according to claim 1, characterized in that: The inlet of the cation exchange resin column is connected to a hydrochloric acid solution tank through a pipeline, the outlet of the cation exchange resin column is connected to a second concentration tank through a pipeline, the outlet of the second concentration tank is connected to a first filter through a pipeline, and the solid phase outlet of the first filter is connected to a glucosamine hydrochloride crude product tank through a pipeline.

9. The device for producing D-psicose using fructose solution according to claim 8, characterized in that: The outlet of the cation exchange resin column is connected to a collection liquid tank through a pipeline.

10. The device for producing D-psicose using fructose solution according to claim 8, characterized in that: The outlet of the crude glucosamine hydrochloride tank is connected to a purification tank via a pipeline, the inlet of the purification tank is connected to a purified water tank and an activated carbon tank via pipelines, respectively, the outlet of the purification tank is connected to a second filter via a pipeline, the outlet of the second filter is connected to a dryer via a pipeline, and the outlet of the dryer is connected to a finished glucosamine phosphate tank.