Co-production, separation and purification system of scyllo-inositol and glucuronic acid

Abstract

The utility model relates to the technical field of scyllo-inositol, in particular to a co-production, separation and purification system for scyllo-inositol and glucuronic acid. Comprising a first filtering device, a reaction kettle, a second filtering device, a precipitation kettle, a third filtering device, a first buffer kettle, a buffer tank, a resin column, a desorption agent storage tank, a second buffer kettle, a desorption liquid storage tank, a first concentration kettle, a first crystallization kettle, a first drying device, a glucuronic acid product storage tank and a fourth filtering device which are communicated with a conversion liquid conveying pipeline, a scyllo-inositol crude product storage tank, a second concentration kettle, a second crystallization kettle, a second drying device and a scyllo-inositol product storage tank. The co-production, separation and purification system is reasonable in design, unreacted inositol can be converted into a glucuronic acid product, glucuronic acid and scyllo-inositol are conveniently separated, the yield, the yield and the purity of the two products can be improved, and economic benefits are increased for enterprises.

Description

Technical Field

[0001] The utility model relates to the technical field of scyllo-inositol, in particular to a system for the co-production and separation and purification of scyllo-inositol and glucuronic acid. Background Art

[0002] Scyllo-inositol (SI) is a diastereomer of myo-inositol (MI), which exists in plants, animals and some bacteria, but its content in nature is much lower than myo-inositol. At present, the preparation method of scyllo-inositol is to use myo-inositol as substrate, then add inositol dehydrogenase and scyllo-inositol dehydrogenase or add whole cells containing the above two enzyme genes, and obtain a liquid containing about 35% scyllo-inositol and 65% myo-inositol after reaction. The conversion rate of scyllo-inositol is less than 40%, and the utilization rate of raw materials is low, resulting in high production costs, and scyllo-inositol and myo-inositol are not easy to separate; how to effectively treat the feed liquid containing about 35% scyllo-inositol and 65% myo-inositol, on the one hand, can ensure the yield and purity of scyllo-inositol, on the other hand, can also convert myo-inositol into a by-product with high value, high purity and high yield, and can quickly and effectively separate the main product and the by-product, has become a technical problem that needs to be solved urgently; therefore, in view of the above technical problems, it is necessary to develop a co-production and separation and purification system of scyllo-inositol and glucuronic acid. Utility Model Content

[0003] The technical problem to be solved by the utility model is: in view of the deficiencies of the prior art, a system for the co-production and separation and purification of scyllo-inositol and glucuronic acid is provided, by which high-yield and high-purity scyllo-inositol and glucuronic acid products can be obtained.

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

[0005] A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid, comprising a first filter device connected to a conversion liquid delivery pipeline, wherein the liquid outlet of the first filter device is connected to a reactor, the liquid outlet of the reactor is connected to a second filter device, and the liquid outlet of the second filter device is connected to a precipitation reactor; the material outlet of the precipitation reactor is connected to a third filter device, the liquid outlet of the third filter device is connected to a first buffer reactor, and the material outlet of the third filter device is connected to a buffer tank; the liquid outlet of the first buffer reactor is connected to a liquid inlet of a resin column, the liquid inlet of the resin column is connected to a decomposing agent storage tank, and the liquid outlet of the resin column is respectively connected to the second buffer reactor and a decomposing liquid storage tank; the decomposing liquid storage tank is connected to the first concentrated liquid tank; The first concentrating kettle has a liquid outlet connected to the first crystallization kettle, the material outlet of the first crystallization kettle is connected to the first drying device, and the material outlet of the first drying device is connected to the glucuronic acid product storage tank; the liquid inlet of the buffer tank is connected to the purified water pipeline and the organic acid delivery pipeline, the material outlet of the buffer tank is connected to the fourth filtering device, the material outlet of the fourth filtering device is connected to the scyllo-inositol crude product storage tank, the scyllo-inositol crude product storage tank is connected to the hot water supply pipeline, the outlet of the scyllo-inositol crude product storage tank is connected to the second concentrating kettle, the liquid outlet of the second concentrating kettle is connected to the second crystallization kettle, the material outlet of the second crystallization kettle is connected to the second drying device, and the material outlet of the second drying device is connected to the scyllo-inositol product storage tank.

[0006] As an improved technical solution, the first filtering device is a ceramic membrane filtering device with a pore size of 20-100 nm.

[0007] As an improved technical solution, the reaction kettle comprises a kettle body, a jacket is arranged on the outside of the kettle body, and a pH sensor and an anchor stirrer are arranged on the inside of the kettle body.

[0008] As an improved technical solution, the precipitation kettle comprises a kettle body, the top of which is provided with a feed inlet, an additive inlet and an organic acid inlet, and the interior of the kettle body is provided with a pH sensor and a plurality of stirring blades.

[0009] As an improved technical solution, the second filtering device is a nanofiltration membrane filtering device, and the third filtering device and the fourth filtering device are both plate and frame filters.

[0010] As an improved technical solution, the first drying device and the second drying device are vacuum drying ovens.

[0011] After adopting the above technical solution, the beneficial effects of the utility model are:

[0012] The co-production and separation and purification system of scyllo-inositol and glucuronic acid comprises a first filtering device connected to a conversion liquid conveying pipeline, the liquid outlet of the first filtering device is connected to a reactor, the liquid outlet of the reactor is connected to a second filtering device, the liquid outlet of the second filtering device is connected to a precipitation reactor; the material outlet of the precipitation reactor is connected to a third filtering device, the liquid outlet of the third filtering device is connected to a first buffer reactor, the material outlet of the third filtering device is connected to a buffer tank; the liquid outlet of the first buffer reactor is connected to a liquid inlet of a resin column, the liquid inlet of the resin column is connected to a decomposing agent storage tank, the liquid outlet of the resin column is connected to the second buffer reactor and a decomposing liquid storage tank respectively; the decomposing liquid storage tank is connected to the first The concentration kettle, the liquid outlet of the first concentration kettle is connected to the first crystallization kettle, the material outlet of the first crystallization kettle is connected to the first drying device, and the material outlet of the first drying device is connected to the glucuronic acid product storage tank; the liquid inlet of the buffer tank is connected to the purified water pipeline and the organic acid delivery pipeline, the material outlet of the buffer tank is connected to the fourth filtering device, the material outlet of the fourth filtering device is connected to the scyllo-inositol crude product storage tank, the scyllo-inositol crude product storage tank is connected to the hot water supply pipeline, the outlet of the scyllo-inositol crude product storage tank is connected to the second concentration kettle, the liquid outlet of the second concentration kettle is connected to the second crystallization kettle, the material outlet of the second crystallization kettle is connected to the second drying device, and the material outlet of the second drying device is connected to the scyllo-inositol product storage tank. In actual production, the conversion liquid containing about 35% scyllo-inositol and 65% myo-inositol enters the interior of the first filtering device along the conversion liquid conveying pipeline under the action of the conveying pump, and the filtered filtrate enters the interior of the reactor, and then fully reacts with the whole cells containing inositol oxidase, and inositol is converted into glucuronic acid. The filtrate (containing scyllo-inositol and glucuronic acid) collected after filtration by the second filtering device enters the precipitation kettle and then adds boric acid to adjust the pH to alkaline. After the reaction, scyllo-inositol-diboric acid-disodium salt complex (existing in the form of precipitate) and scyllo-inositol are obtained, and then filtered by the third filtering device, and the filtrate enters The collected precipitate enters the first buffer kettle, and the collected precipitate enters the buffer tank. The feed liquid in the first buffer kettle enters the resin column under the action of the delivery pump, and is adsorbed by the resin through glucuronic acid. The effluent after the feeding is completed enters the second buffer kettle, and then the resin column is analyzed by a decomposing agent. The collected analytical liquid enters the analytical liquid storage tank, and the analytical liquid in the analytical liquid storage tank enters the first concentrating kettle. The concentrated liquid enters the first crystallization kettle again. The feed liquid after cooling and crystallization is then filtered to extract the mother liquor, and the collected crystals are dried by the first drying device. The obtained glucuronic acid product is collected in the glucuronic acid storage tank.The precipitate in the buffer tank is added with water and organic acid to adjust the pH to acidic. The precipitate is dissolved and cooled before entering the fourth filter device. The solid collected after filtration enters the scyllo-inositol crude product storage tank, and hot water and decolorizer are added for stirring. The decolorized liquid collected after suction filtration enters the second concentration kettle, and the concentrated liquid enters the second crystallization kettle after concentration. The crystal liquid after cooling and crystallization is then filtered to extract the mother liquor, and the crystal enters the second drying device for drying. The obtained scyllo-inositol product is stored in the scyllo-inositol storage tank. The above-mentioned co-production and separation and purification system is reasonably designed, which can convert unreacted inositol into glucuronic acid product, and glucuronic acid and scyllo-inositol are convenient to separate, and the output, yield and purity of the two products can be improved, which increases the economic benefits for the enterprise.

[0013] Since the first filtering device is a ceramic membrane filtering device with a pore size of 20-100 nm, bacterial cells can be effectively removed by the ceramic membrane filtering device.

[0014] The reactor includes a reactor body, a jacket is provided on the outside of the reactor body, and a pH sensor and an anchor stirrer are provided inside the reactor body. The filtered liquid enters the reactor body, the heat medium in the jacket is used to provide the temperature required for the reaction, the pH of the feed liquid is detected by the pH sensor, and the feed liquid is fully contacted and reacted with the whole cells containing inositol oxidase by the anchor stirrer, thereby promoting the conversion of inositol.

[0015] Since the precipitation kettle includes a kettle body, a feed port, an auxiliary agent inlet and an alkali solution inlet are arranged on the top of the kettle body, and a pH sensor and a plurality of stirring blades are arranged inside the kettle body. The filtrate filtered by the second filtering device enters the kettle body, boric acid is added from the auxiliary agent inlet, and then alkali solution is added from the alkali solution inlet to adjust the pH, the pH of the feed solution is detected by the pH sensor, and a plurality of stirring blades are used to make the filtrate fully contact and react with the boric acid to form a scyllo-inositol-diboric acid-disodium salt complex in the form of a precipitate. The kettle body of the above structure is reasonably designed and can promote the formation of the scyllo-inositol-diboric acid-disodium salt complex. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 This is a schematic diagram of the structure of a utility model system for the co-production and separation and purification of scyllo-inositol and glucuronic acid;

[0017] Among them, 1-conversion liquid delivery pipeline, 2-first filtering device, 3-reaction kettle, 4-second filtering device, 5-precipitation kettle, 6-first buffer kettle, 7-buffer tank, 8-resin column, 9-analyzer storage tank, 10-second buffer kettle, 11-analyzer storage tank, 12-first concentration kettle, 13-first crystallization kettle, 14-first drying device, 15-glucuronic acid product storage tank, 16-purified water pipeline, 17-organic acid delivery pipeline, 18-fourth filtering device, 19-scyllo-inositol crude product storage tank, 20-hot water supply pipeline, 21-second crystallization kettle, 22-second drying device, 23-scyllo-inositol product storage tank. DETAILED DESCRIPTION

[0018] In order to make the purpose, technical solution and advantages of the utility model more clear, the utility model is further described in detail in combination with the embodiments below. It should be understood that the specific embodiments described here are only used to explain the utility model, and are not used to limit the utility model.

[0019] A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid, such as Figure 1 As shown, it includes a first filtering device 2 (a ceramic membrane filtering device with a pore size of 20-100nm) connected to a conversion liquid conveying pipeline 1, the liquid outlet of the first filtering device 2 is connected to a reactor 3, the liquid outlet of the reactor 3 is connected to a second filtering device 4 (nanofiltration membrane device), and the liquid outlet of the second filtering device 4 is connected to a precipitation reactor 4; the material outlet of the precipitation reactor 4 is connected to a third filtering device 5, the liquid outlet of the third filtering device 5 (plate and frame filter) is connected to a first buffer reactor 6, and the material outlet of the third filtering device 5 is connected to a buffer tank 7; the liquid outlet of the first buffer reactor 6 is connected to the liquid inlet of a resin column 8, the liquid inlet of the resin column 8 is connected to a decomposing agent storage tank 9, and the liquid outlet of the resin column 8 is respectively connected to a second buffer reactor 10 and a decomposing liquid storage tank 11; the decomposing liquid storage tank 11 is connected to a first concentration reactor 12, and the first concentration reactor 12 is ... second buffer reactor 10. The liquid outlet is connected to the first crystallization kettle 13, the material outlet of the first crystallization kettle 13 is connected to the first drying device 14 (vacuum drying oven), and the material outlet of the first drying device 14 is connected to the glucuronic acid product storage tank 15; the liquid inlet of the buffer tank 7 is connected to the purified water pipeline 16 and the organic acid delivery pipeline 17, the material outlet of the buffer tank 7 is connected to the fourth filtering device 18 (plate and frame filter), the material outlet of the fourth filtering device 18 is connected to the scyllo-inositol crude product storage tank 19, the scyllo-inositol crude product storage tank 19 is connected to the hot water supply pipeline 20, the outlet of the scyllo-inositol crude product storage tank 19 is connected to the second concentrating kettle 21, the liquid outlet of the second concentrating kettle 21 is connected to the second crystallization kettle 22, the material outlet of the second crystallization kettle 22 is connected to the second drying device 23 (vacuum drying oven), and the material outlet of the second drying device 23 is connected to the scyllo-inositol product storage tank 24.

[0020] In actual production, the conversion liquid containing about 35% scyllo-inositol and 65% myo-inositol enters the interior of the first filtering device along the conversion liquid conveying pipeline under the action of the conveying pump, and the filtered filtrate enters the interior of the reactor, and then fully reacts with the whole cells containing inositol oxidase, and inositol is converted into glucuronic acid. The filtrate (containing scyllo-inositol and glucuronic acid) collected after filtration by the second filtering device enters the precipitation kettle and then adds boric acid to adjust the pH to alkaline. After the reaction, scyllo-inositol-diboric acid-disodium salt complex (existing in the form of precipitate) and scyllo-inositol are obtained, and then filtered by the third filtering device, and the filtrate enters the first The collected precipitate enters the buffer kettle, and the feed liquid in the first buffer kettle enters the resin column under the action of the delivery pump, and is adsorbed by the resin through glucuronic acid. The effluent after the feeding is completed enters the second buffer kettle, and then the resin column is analyzed by an analytical agent. The collected analytical liquid enters the analytical liquid storage tank, and the analytical liquid in the analytical liquid storage tank enters the first concentrating kettle. The concentrated liquid enters the first crystallization kettle again. The feed liquid after cooling and crystallization is discharged from the liquid outlet through the filter screen by a suction pump, and the collected crystals are dried by the first drying device. The obtained glucuronic acid product is collected in the glucuronic acid storage tank. Water and organic acid are added to the precipitate in the buffer tank to adjust the pH to acidic. The precipitate is dissolved and cooled before entering the fourth filter device. The solid collected after filtration enters the scyllo-inositol crude product storage tank, hot water and decolorizer are added for stirring, and then the decolorized liquid passes through the filter under the action of the suction pump and is discharged from the liquid outlet and enters the second concentrator. The concentrated liquid enters the second crystallization kettle. The crystal feed liquid after cooling and crystallization is filtered to extract the mother liquor, and the crystal enters the second drying device for drying. The obtained scyllo-inositol product is stored in the scyllo-inositol storage tank.

[0021] The reaction kettle 3 includes a kettle body, a jacket is provided on the outside of the kettle body, and a pH sensor and an anchor stirrer are provided inside the kettle body. The filtered liquid enters the kettle body, and the heat medium in the jacket is used to provide the temperature required for the reaction. The pH of the feed liquid is detected by the pH sensor, and the feed liquid is fully contacted and reacted with the whole cells containing inositol oxidase through the anchor stirrer to promote the conversion of inositol.

[0022] The precipitation kettle 4 includes a kettle body, a feed port, an auxiliary agent inlet and an alkali solution inlet are arranged on the top of the kettle body, and a pH sensor and a plurality of stirring blades are arranged inside the kettle body. The filtrate filtered by the second filtering device enters the kettle body, boric acid is added from the auxiliary agent inlet, and then alkali solution is added from the alkali solution inlet to adjust the pH, the pH of the feed solution is detected by the pH sensor, and a plurality of stirring blades are used to make the filtrate fully contact and react with boric acid to form a scyllo-inositol-diboric acid-disodium salt complex in the form of a precipitate. The kettle body of the above structure is reasonably designed and can promote the formation of the scyllo-inositol-diboric acid-disodium salt complex.

[0023] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid, characterized in that: The invention comprises a first filtering device connected to a conversion liquid conveying pipeline, wherein the liquid outlet of the first filtering device is connected to a reaction kettle, the liquid outlet of the reaction kettle is connected to a second filtering device, and the liquid outlet of the second filtering device is connected to a precipitation kettle; the material outlet of the precipitation kettle is connected to a third filtering device, the liquid outlet of the third filtering device is connected to a first buffer kettle, and the material outlet of the third filtering device is connected to a buffer tank; the liquid outlet of the first buffer kettle is connected to a liquid inlet of a resin column, the liquid inlet of the resin column is connected to a decomposing agent storage tank, and the liquid outlet of the resin column is respectively connected to a second buffer kettle and a decomposing liquid storage tank; the decomposing liquid storage tank is connected to a first concentration kettle, and the first concentration kettle is connected to a second buffer kettle. The liquid outlet is connected to the first crystallization kettle, the material outlet of the first crystallization kettle is connected to the first drying device, and the material outlet of the first drying device is connected to the glucuronic acid product storage tank; the liquid inlet of the buffer tank is connected to the purified water pipeline and the organic acid delivery pipeline, the material outlet of the buffer tank is connected to the fourth filtering device, the material outlet of the fourth filtering device is connected to the scabryo-inositol crude product storage tank, the scabryo-inositol crude product storage tank is connected to the hot water supply pipeline, the outlet of the scabryo-inositol crude product storage tank is connected to the second concentrating kettle, the liquid outlet of the second concentrating kettle is connected to the second crystallization kettle, the material outlet of the second crystallization kettle is connected to the second drying device, and the material outlet of the second drying device is connected to the scabryo-inositol product storage tank.

2. A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid according to claim 1, characterized in that: The first filtering device is a ceramic membrane filtering device with a pore size of 20-100 nm.

3. A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid according to claim 1, characterized in that: The reaction kettle comprises a kettle body, a jacket is arranged on the outside of the kettle body, and a pH sensor and an anchor stirrer are arranged on the inside of the kettle body.

4. A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid according to claim 1, characterized in that: The precipitation kettle comprises a kettle body, a feed inlet, an auxiliary agent inlet and an organic acid inlet are arranged on the top of the kettle body, and a pH sensor and a plurality of stirring blades are arranged inside the kettle body.

5. A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid according to claim 1, characterized in that: The second filtering device is a nanofiltration membrane filtering device, and the third filtering device and the fourth filtering device are both plate and frame filters.

6. A system for the co-production and separation and purification of scyllo-inositol and glucuronic acid according to claim 1, characterized in that: The first drying device and the second drying device are vacuum drying ovens.

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