Production device of glucuronic acid

Abstract

The utility model discloses a glucuronic acid production device, and relates to the technical field of pharmacy, an inlet of a conversion kettle is respectively communicated with an inositol solution tank, an inositol oxidase tank and an ammonia water solution tank, an outlet of the conversion kettle is communicated with a ceramic membrane device, and a clear liquid outlet of the ceramic membrane device is communicated with a concentration tank; an inlet of the concentration tank is respectively communicated with a first ethanol tank and a seed crystal tank, an outlet of the concentration tank is communicated with a first filter, and a solid phase outlet of the first filter is communicated with a glucuronic acid crude product tank. In the conversion process, the pH is adjusted to 7.0-8.0 through ammonia water, solid impurities and macromolecular substances in reaction liquid can be effectively separated through the high-precision filtering characteristic of a ceramic membrane device, a clear glucuronic acid solution is obtained, the solubility of the solution can be changed by adding ethyl alcohol, glucuronic acid is promoted to be crystallized and separated out, and the purity of the glucuronic acid is improved. And the addition of the seed crystal can guide the crystallization process, so that the crystallization is more uniform and rapid, and the quality and yield of the glucuronic acid crude product are improved.

Description

TECHNICAL FIELD

[0001] The utility model relates to the field of pharmaceutical technology, specifically relates to a production device of glucuronic acid. BACKGROUND

[0002] Glucuronic acid, simply glucuronide, is a compound formed by the oxidation of the primary alcohol hydroxyl group of glucose into a carboxyl group, and is widely distributed in animals and plants. In plants, it exists in the form of arabinoglucuronide in gum arabic and other gums, and is an important component of pectin, mucus and high polysaccharides.

[0003] At present, the preparation methods of glucuronic acid mainly include polysaccharide hydrolysis method, chemical oxidation method and biological fermentation method, etc. However, the above methods all have some problems: the glucuronic acid obtained by the chemical oxidation method has low yield and low purity, and a large amount of by-products are produced, which are difficult to separate; the biological fermentation method has a complex process, and the obtained glucuronic acid has low yield and is difficult to separate; the polysaccharide hydrolysis method needs strong acid and alkali hydrolysis conditions due to the high stability of the glycosidic bond connecting the glucuronic acid, and has the problems of difficult hydrolysis, low product yield and a large amount of wastewater, which cannot meet the needs of industrialization. SUMMARY

[0004] The technical problem to be solved by the utility model is to provide a production device of glucuronic acid in view of the deficiencies of the prior art, which has a simple process, less by-products and is suitable for industrialization.

[0005] To solve the above technical problems, the technical scheme of the utility model is:

[0006] A production device of glucuronic acid, comprising a conversion kettle, the inlet of the conversion kettle is connected with an inositol solution tank, an inositol oxidase tank and an ammonia water solution tank through pipelines respectively, the outlet of the conversion kettle is connected with a ceramic membrane device through a pipeline, and the clear liquid outlet of the ceramic membrane device is connected with a concentration tank through a pipeline.

[0007] The inlet of the concentration tank is connected with a first ethanol tank and a crystal seed tank through pipelines respectively, the outlet of the concentration tank is connected with a first filter through a pipeline, and the solid phase outlet of the first filter is connected with a glucuronic acid crude product tank through a pipeline.

[0008] As an improved technical scheme, the outlet of the conversion kettle is connected with an acidification tank through a pipeline, the inlet of the acidification tank is connected with an acetic acid tank through a pipeline, and the outlet of the acidification tank is connected with the ceramic membrane device through a pipeline.

[0009] As an improved technical scheme, the thick liquid outlet of the ceramic membrane device is connected with a flocculation tank through a pipeline, and the pore size of the ceramic membrane device is 50-100 nm.

[0010] As the improved technical scheme, the clear liquid outlet of the ceramic membrane device is communicated with the first ultrafiltration membrane device through a pipeline, the clear liquid outlet of the first ultrafiltration membrane device is communicated with the thickening tank through a pipeline, and the pore size of the first ultrafiltration membrane device is 8000-10000 Da.

[0011] As the improved technical scheme, the clear liquid outlet of the first ultrafiltration membrane device is communicated with the second ultrafiltration membrane device through a pipeline, the clear liquid outlet of the second ultrafiltration membrane device is communicated with the thickening tank through a pipeline, and the pore size of the second ultrafiltration membrane device is 1000-2000 Da.

[0012] As the improved technical scheme, the clear liquid outlet of the second ultrafiltration membrane device is communicated with the cation exchange resin column through a pipeline, and the outlet of the cation exchange resin column is communicated with the thickening tank through a pipeline.

[0013] The inlet of the cation exchange resin column is respectively communicated with a dilute hydrochloric acid tank and a deionized water tank through pipelines.

[0014] As the preferred technical scheme, the outlet of the cation exchange resin column is communicated with the nanofiltration membrane device through a pipeline, the outlet of the nanofiltration membrane device is communicated with the thickening tank through a pipeline, and the pore size of the nanofiltration membrane device is 150-200 Da.

[0015] As the preferred technical scheme, the outlet of the glucose uronic acid crude product tank is communicated with the decolorizing tank through a pipeline, the inlet of the decolorizing tank is communicated with a hot ethanol tank through a pipeline, the outlet of the decolorizing tank is communicated with the second filter through a pipeline, the liquid phase outlet of the second filter is communicated with a dryer, and the outlet of the dryer is communicated with a glucose uronic acid pure product tank.

[0016] As the preferred technical scheme, the inlet of the glucose uronic acid crude product tank is communicated with the second ethanol tank through a pipeline, and the outlet of the glucose uronic acid crude product tank is communicated with the recovery tank through a pipeline.

[0017] As the preferred technical scheme, the liquid phase outlet of the first filter is communicated with the recovery tank.

[0018] Due to the adoption of the above technical scheme, the beneficial effects of the present application are:

[0019] The utility model discloses a production device of glucuronic acid, including conversion kettle, the inlet of conversion kettle is passed through pipeline communication with inositol solution jar, inositol oxidase jar and ammonia liquor solution jar respectively, the outlet of conversion kettle is passed through pipeline communication with ceramic membrane device, and the clear liquid outlet of ceramic membrane device is passed through pipeline communication with concentration jar, the inlet of concentration jar is passed through pipeline communication with first ethanol jar and crystal seed jar respectively, and the outlet of concentration jar is passed through pipeline communication with first filter, and the solid phase outlet of first filter is passed through pipeline communication with glucuronic acid crude product jar. The conversion process is adjusted to 7.0-8.0 through ammonia water, utilizes the high-precision filtering characteristics of ceramic membrane device, can effectively separate the solid impurity and macromolecular substance in reaction liquid, obtains the clear glucuronic acid solution, adds ethanol and can change the solubility of solution, promotes the crystallization of glucuronic acid and precipitates, and the addition of crystal seed can guide the crystallization process, makes the crystallization more uniform, fast, improves the quality and output of glucuronic acid crude product.

[0020] The outlet of the conversion kettle is connected to the acidification tank through a pipeline, the inlet of the acidification tank is connected to the glacial acetic acid tank through a pipeline, and the outlet of the acidification tank is connected to the ceramic membrane device through a pipeline. The addition of glacial acetic acid for acidification treatment can adjust the pH value of the reaction liquid to 4-5, optimize the reaction environment, and is conducive to the generation and separation of glucuronic acid, thereby improving the purity and yield of the product.

[0021] The concentrated liquid outlet of the ceramic membrane device is connected to the flocculation tank through a pipeline, the pore size of the ceramic membrane device is 50-100 nm, and the concentrated liquid filtered by the ceramic membrane device is subjected to flocculation filtration recovery, which can be used as organic fertilizer, thereby increasing the income and reducing the discharge of waste.

[0022] The clear liquid outlet of the ceramic membrane device is connected to the first ultrafiltration membrane device through a pipeline, the clear liquid outlet of the first ultrafiltration membrane device is connected to the concentration tank through a pipeline, the pore size of the first ultrafiltration membrane device is 8000-10000 Da, which can further remove the medium and large molecular impurities in the solution, improve the purity of the glucuronic acid solution, and provide purer raw materials for subsequent concentration and refining.

[0023] The clear liquid outlet of the first ultrafiltration membrane device is connected to the second ultrafiltration membrane device through a pipeline, the clear liquid outlet of the second ultrafiltration membrane device is connected to the concentration tank through a pipeline, and the pore size of the second ultrafiltration membrane device is 1000-2000 Da. The solution can be filtered more finely, the small molecular impurities are removed, the purity of the glucuronic acid solution is further improved, and the production demand of higher quality is met.

[0024] The clarified liquid outlet of the second ultrafiltration membrane device is connected to a cation exchange resin column via a pipeline, and the outlet of the cation exchange resin column is connected to the concentration tank via a pipeline. Through the cation exchange resin column, cationic impurities such as metal ions in the solution can be removed, further purifying the glucuronic acid solution and improving the purity and quality of the product.

[0025] The inlet of the cation exchange resin column is connected to a dilute hydrochloric acid tank and a deionized water tank via pipelines. Before desalination, the resin is regenerated with 3-5% dilute hydrochloric acid and then washed with deionized water until it is neutral to improve the adsorption efficiency of the resin and the purity of the target product.

[0026] The outlet of the cation exchange resin column is connected to a nanofiltration membrane device via a pipeline, and the outlet of the nanofiltration membrane device is connected to the concentration tank via a pipeline. The nanofiltration membrane device has a pore size of 150-200 Da. This allows for deep filtration of the solution, removing smaller molecules of impurities and salts, further improving the purity of the glucuronic acid solution, and ensuring the high quality of the final product.

[0027] The outlet of the crude glucuronic acid tank is connected to a decolorizing tank via a pipeline. The inlet of the decolorizing tank is connected to a hot ethanol tank via a pipeline. The outlet of the decolorizing tank is connected to a second filter via a pipeline. The liquid phase outlet of the second filter is connected to a dryer. The outlet of the dryer is connected to a pure glucuronic acid tank. Utilizing the solubility and decolorizing properties of hot ethanol, impurities such as pigments in the crude product can be effectively removed, improving the color and purity of the product and resulting in a higher quality pure glucuronic acid.

[0028] The inlet of the crude glucuronic acid tank is connected to a second ethanol tank via a pipeline, and the outlet of the crude glucuronic acid tank is connected to a recovery tank via a pipeline, which can further wash the crude product and improve its purity; the outlet is connected to the recovery tank, which can recover unreacted raw materials and solvents, reduce production costs, and realize the recycling of resources.

[0029] The liquid phase outlet of the first filter is connected to the recovery tank, and after treatment, it can be reused in the production process, improving the utilization rate of raw materials, reducing production costs, and reducing waste emissions. Attached Figure Description

[0030] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0031] Figure 1 This is a structural schematic diagram of an embodiment of the present utility model;

[0032] The equipment includes: 1. Conversion vessel; 2. Inositol solution tank; 3. Inositol oxidase tank; 4. Ammonia solution tank; 5. Ceramic membrane device; 6. Concentration tank; 7. First ethanol tank; 8. Seed crystal tank; 9. First filter; 10. Crude glucuronic acid tank; 11. Acidification tank; 12. Glacial acetic acid tank; 13. Flocculation tank; 14. First ultrafiltration membrane device; 15. Second ultrafiltration membrane device; 16. Cation exchange resin column; 17. Dilute hydrochloric acid tank; 18. Deionized water tank; 19. Nanofiltration membrane device; 20. Decolorization tank; 21. Hot ethanol tank; 22. Second filter; 23. Dryer; 24. Pure glucuronic acid tank; 25. Second ethanol tank; 26. Recovery tank. Detailed Implementation

[0033] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0034] like Figure 1 As shown, a glucuronic acid production apparatus includes a conversion vessel 1. The inlet of the conversion vessel 1 is connected via pipes to an inositol solution tank 2, an inositol oxidase tank 3, and an ammonia solution tank 4. The outlet of the conversion vessel 1 is connected via pipes to a ceramic membrane device 5. The clear liquid outlet of the ceramic membrane device 5 is connected via pipes to a concentration tank 6. The inlet of the concentration tank 6 is connected via pipes to a first ethanol tank 7 and a seed crystal tank 8. The outlet of the concentration tank 6 is connected via pipes to a first filter 9. The solid phase outlet of the first filter 9 is connected via pipes to a crude glucuronic acid tank 10. During the conversion process, the pH is adjusted to 7.0-8.0 with ammonia. Utilizing the high-precision filtration characteristics of the ceramic membrane device 5, solid impurities and macromolecules in the reaction solution can be effectively separated to obtain a clear glucuronic acid solution. The addition of ethanol can change the solubility of the solution, promoting the crystallization of glucuronic acid. The addition of seed crystals can guide the crystallization process, making the crystallization more uniform and faster, thereby improving the quality and yield of the crude glucuronic acid.

[0035] The outlet of the conversion reactor 1 is connected to an acidification tank 11 via a pipeline. The inlet of the acidification tank 11 is connected to a glacial acetic acid tank 12 via a pipeline. The outlet of the acidification tank 11 is connected to the ceramic membrane device 5 via a pipeline. Adding glacial acetic acid for acidification treatment can adjust the pH value of the reaction solution to 4-5, optimize the reaction environment, facilitate the formation and separation of glucuronic acid, and improve the purity and yield of the product.

[0036] The concentrated liquid outlet of the ceramic membrane device 5 is connected to the flocculation tank 13 via a pipeline. The pore size of the ceramic membrane device 5 is 50-100nm. The concentrated liquid filtered by the ceramic membrane device 5 is recycled by flocculation filtration and can be used as organic fertilizer, increasing income and reducing waste emissions.

[0037] The clear liquid outlet of the ceramic membrane device 5 is communicated with a first ultrafiltration membrane device 14 through a pipeline, the clear liquid outlet of the first ultrafiltration membrane device 14 is communicated with the concentration tank 6 through a pipeline, and the pore size of the first ultrafiltration membrane device 14 is 8000-10000 Da, which can further remove macromolecular impurities in the solution and improve the purity of the glucuronic acid solution, so as to provide purer raw materials for subsequent concentration and refining.

[0038] The clear liquid outlet of the first ultrafiltration membrane device 14 is communicated with a second ultrafiltration membrane device 15 through a pipeline, the clear liquid outlet of the second ultrafiltration membrane device 15 is communicated with the concentration tank 6 through a pipeline, and the pore size of the second ultrafiltration membrane device 15 is 1000-2000 Da. The solution can be filtered more finely to remove small molecular impurities and further improve the purity of the glucuronic acid solution to meet higher quality production requirements.

[0039] The clear liquid outlet of the second ultrafiltration membrane device 15 is communicated with a cation exchange resin column 16 through a pipeline, and the outlet of the cation exchange resin column 16 is communicated with the concentration tank 6 through a pipeline. Through the cation exchange resin column 16, metal ions and other cation impurities in the solution can be removed, the glucuronic acid solution is further purified, and the purity and quality of the product are improved.

[0040] The inlet of the cation exchange resin column 16 is respectively communicated with a dilute hydrochloric acid tank 17 and a deionized water tank 18 through pipelines. Before desalination, 3-5% dilute hydrochloric acid is used to regenerate the resin, and deionized water is used to wash the resin to neutral to improve the adsorption efficiency of the resin and the purity of the target product.

[0041] The outlet of the cation exchange resin column 16 is communicated with a nanofiltration membrane device 19 through a pipeline, the outlet of the nanofiltration membrane device 19 is communicated with the concentration tank 6 through a pipeline, and the pore size of the nanofiltration membrane device 19 is 150-200 Da. The solution can be deeply filtered to retain smaller molecular impurities and salts, further improve the purity of the glucuronic acid solution, and ensure the high quality of the final product.

[0042] The outlet of the glucuronic acid crude product tank 10 is communicated with a decolorizing tank 20 through a pipeline, the inlet of the decolorizing tank 20 is communicated with a hot ethanol tank 21 through a pipeline, the outlet of the decolorizing tank 20 is communicated with a second filter 22 through a pipeline, the liquid phase outlet of the second filter 22 is communicated with a dryer 23, and the outlet of the dryer 23 is communicated with a glucuronic acid pure product tank 24. The solubility and decolorization of hot ethanol can effectively remove impurities such as pigments in the crude product, improve the color and purity of the product, and make the quality of the glucuronic acid pure product better.

[0043] The inlet of the crude glucuronic acid tank 10 is communicated with the second ethanol tank 25 through a pipeline, and the outlet of the crude glucuronic acid tank 10 is communicated to the recovery tank 26 through a pipeline, so that the crude product can be further washed to improve the purity; the outlet is communicated to the recovery tank 26, so that the unreacted raw materials and solvents can be recovered, the production cost is reduced, and the recycling of resources is realized.

[0044] The liquid phase outlet of the first filter 9 is communicated to the recovery tank 26, so that the treated product can be used in the production process again, the utilization rate of raw materials is improved, the production cost is reduced, and the emission of waste is reduced.

[0045] It should be understood that the above embodiments are only used for illustrating the present application and are not used for limiting the scope of the present application. In addition, it should be understood that after reading the content of the present application, those skilled in the art can make various modifications or changes to the present application, and these equivalent forms also fall within the scope defined by the appended claims of the present application.

Claims

1. A device for producing glucuronic acid, comprising a conversion tank, characterized by: The inlet of the conversion kettle is communicated with the inositol solution tank, the inositol oxidase tank and the ammonia solution tank respectively through pipelines, the outlet of the conversion kettle is communicated with the ceramic membrane device through a pipeline, and the clear liquid outlet of the ceramic membrane device is communicated with the concentration tank through a pipeline; The inlet of the concentration tank is communicated with the first ethanol tank and the seed tank respectively through pipelines, the outlet of the concentration tank is communicated with the first filter through a pipeline, and the solid phase outlet of the first filter is communicated with the crude glucuronic acid tank through a pipeline.

2. The apparatus for producing glucuronic acid according to claim 1, wherein: The outlet of the conversion kettle is communicated with the acidification tank, the inlet of the acidification tank is communicated with the glacial acetic acid tank through a pipeline, and the outlet of the acidification tank is communicated with the ceramic membrane device through a pipeline.

3. The apparatus for producing glucuronic acid according to claim 2, wherein: The thick liquid outlet of the ceramic membrane device is communicated with the flocculation tank through a pipeline, and the pore size of the ceramic membrane device is 50-100 nm.

4. The apparatus for producing glucuronic acid according to claim 3, wherein: The clear liquid outlet of the ceramic membrane device is communicated with the first ultrafiltration membrane device through a pipeline, the clear liquid outlet of the first ultrafiltration membrane device is communicated with the concentration tank through a pipeline, and the pore size of the first ultrafiltration membrane device is 8000-10000 Da.

5. The apparatus for producing glucuronic acid according to claim 4, wherein: The clear liquid outlet of the first ultrafiltration membrane device is communicated with the second ultrafiltration membrane device through a pipeline, the clear liquid outlet of the second ultrafiltration membrane device is communicated with the concentration tank through a pipeline, and the pore size of the second ultrafiltration membrane device is 1000-2000 Da.

6. The apparatus for producing glucuronic acid according to claim 5, wherein: The clear liquid outlet of the second ultrafiltration membrane device is communicated with the cation exchange resin column through a pipeline, and the outlet of the cation exchange resin column is communicated with the concentration tank through a pipeline. The inlet of the cation exchange resin column is communicated with the dilute hydrochloric acid tank and the deionized water tank respectively through pipelines.

7. The apparatus for producing glucuronic acid according to claim 6, wherein: The outlet of the cation exchange resin column is communicated with the nanofiltration membrane device, the outlet of the nanofiltration membrane device is communicated with the concentration tank through a pipeline, and the pore size of the nanofiltration membrane device is 150-200 Da.

8. The apparatus for producing glucuronic acid according to claim 1, wherein: The outlet of the crude glucuronic acid tank is communicated with the decolorization tank, the inlet of the decolorization tank is communicated with the hot ethanol tank through a pipeline, the outlet of the decolorization tank is communicated with the second filter through a pipeline, the liquid phase outlet of the second filter is communicated with the dryer, and the outlet of the dryer is communicated with the pure glucuronic acid tank.

9. The apparatus for producing glucuronic acid according to claim 8, wherein: The inlet of the crude glucuronic acid tank is communicated with the second ethanol tank through a pipeline, and the outlet of the crude glucuronic acid tank is communicated with the recovery tank through a pipeline.

10. The apparatus for producing glucuronic acid according to claim 9, wherein: The liquid phase outlet of the first filter is communicated with the recovery tank.

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