Purification device for glycine desalination

Abstract

The utility model relates to the technical field of glycine desalination and purification, in particular to a glycine desalination and purification device which comprises an after-adsorption washing area, a product B enrichment area, a feeding area, a product A enrichment area and a product A repurification area which are connected in sequence, and the after-adsorption washing area, the product B enrichment area, the feeding area, the product A enrichment area and the product A repurification area are sequentially connected. The post-adsorption washing area comprises a first anion exchange resin column, a second anion exchange resin column, a third anion exchange resin column and a product B collecting tank, the discharging end of the first anion exchange resin column is connected with the second anion exchange resin column, and the discharging end of the second anion exchange resin column is connected with the third anion exchange resin column; and the discharge end of the third anion exchange resin column is connected with the product B collecting tank. Through the arrangement of the structure, the problems of poor continuity, high cost, low efficiency and large water consumption of the existing purification equipment are solved.

Description

Technical Field

[0001] This utility model relates to the field of glycine desalting and purification technology, and in particular to a glycine desalting and purification device. Background Technology

[0002] Glycine is the simplest amino acid and a component of proteins. Also known as aminoacetic acid, it is a white crystal or pale yellow crystalline powder at room temperature and pressure. Glycine is a strong electrolyte in water, highly soluble in strongly polar solvents, and practically insoluble in nonpolar solvents. By adjusting the acidity or alkalinity of the aqueous solution, glycine can be expressed in different molecular forms, exhibiting high boiling and melting points. Glycine has a unique sweet taste, which can mitigate acidic and alkaline tastes, mask the bitterness of added saccharin in food, and enhance sweetness. The uses of glycine can be mainly divided into edible and industrial applications. Industrially, glycine is primarily produced through chemical and biosynthetic processes. Chemically synthesized glycine solutions contain ammonium chloride, glycolic acid, and other colored substances generated by side reactions, in addition to glycine. Ammonium chloride is the main impurity affecting product quality; therefore, separating ammonium chloride from the glycine solution is crucial for improving product quality.

[0003] However, existing purification equipment has drawbacks such as poor continuity, high cost, low efficiency, and large water consumption. Utility Model Content

[0004] The purpose of this invention is to provide a purification device for glycine desalting, which solves the problems of poor continuity, high cost, low efficiency and large water consumption of existing purification equipment.

[0005] To achieve the above objectives, this utility model provides a purification device for glycine desalting, comprising a post-adsorption washing zone, a product B enrichment zone, a feeding zone, a product A enrichment zone, and a product A re-purification zone. The post-adsorption washing zone, the product B enrichment zone, the feeding zone, the product A enrichment zone, and the product A re-purification zone are connected sequentially. The post-adsorption washing zone includes a first anion exchange resin column, a second anion exchange resin column, a third anion exchange resin column, and a product B collection tank. The outlet end of the first anion exchange resin column is connected to the second anion exchange resin column, the outlet end of the second anion exchange resin column is connected to the third anion exchange resin column, and the outlet end of the third anion exchange resin column is connected to the product B collection tank.

[0006] The product B enrichment zone includes anion exchange resin column No. 4, anion exchange resin column No. 5, and an intermediate material tank. The discharge end of the product B collection tank is connected to the anion exchange resin column No. 4, the discharge end of the anion exchange resin column No. 4 is connected to the anion exchange resin column No. 5, and the discharge end of the anion exchange resin column No. 5 is connected to the intermediate material tank.

[0007] The feeding area includes a No. 6 anion exchange resin column, and the discharge end of the No. 6 anion exchange resin column is connected to the intermediate material pool.

[0008] The product A enrichment zone includes anion exchange resin column No. 7, anion exchange resin column No. 8, anion exchange resin column No. 9, and a product A collection tank. The discharge end of the intermediate material tank is connected to the anion exchange resin column No. 7, the discharge end of the anion exchange resin column No. 7 is connected to the anion exchange resin column No. 8, the discharge end of the anion exchange resin column No. 8 is connected to the anion exchange resin column No. 9, and the discharge end of the anion exchange resin column No. 9 is connected to the product A collection tank.

[0009] The product A repurification zone includes a No. 10 anion exchange resin column, and the outlet end of the product A collection tube is connected to the No. 10 anion exchange resin column.

[0010] This invention relates to a purification device for glycine desalting. The device comprises a post-adsorption washing zone, a product B enrichment zone, a feeding zone, a product A enrichment zone, and a product A re-purification zone, connected sequentially. The post-adsorption washing zone includes a first anion exchange resin column, a second anion exchange resin column, a third anion exchange resin column, and a product B collection tank. The outlet end of the first anion exchange resin column is connected to the second anion exchange resin column, the outlet end of the second anion exchange resin column is connected to the third anion exchange resin column, and the outlet end of the third anion exchange resin column is connected to the product B collection tank. Each resin column uses DTF-NH4. + The resin is designed to process 3 × 10⁻⁴ m³. 3 The system operates at a rate of 1.5 m / h, with each resin column containing 450 ml of liquid. The liquid flow direction within the resin column is opposite to the column's rotation direction. The system advances one unit position at a time, significantly improving product precision and purification efficiency of glycine production. Each anion exchange resin column is pre-adsorbed with glycine. The feed to the post-adsorption washing zone is pure water, designed with a feed rate of 1.38 × 10⁻³ m / s. 3 / h, three anion exchange resin columns are connected in series in the same direction as the liquid flow. When each resin column leaves the area, the residual product B on the cation resin will be thoroughly cleaned to improve the product recovery rate. Attached Figure Description

[0011] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0012] Figure 1 This is a schematic diagram of the purification device for glycine desalting according to this utility model.

[0013] 1-Anion exchange resin column No. 1, 2-Anion exchange resin column No. 2, 3-Anion exchange resin column No. 3, 4-Product B collection tank, 5-Anion exchange resin column No. 4, 6-Anion exchange resin column No. 5, 7-Intermediate material tank, 8-Anion exchange resin column No. 6, 9-Anion exchange resin column No. 7, 10-Anion exchange resin column No. 8, 11-Anion exchange resin column No. 9, 12-Product A collection tank, 13-Anion exchange resin column No. 10. Detailed Implementation

[0014] The embodiments of this utility model are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain this utility model, and should not be construed as limiting this utility model.

[0015] Please see Figure 1 This utility model provides a purification device for glycine desalting, including an adsorption washing zone, a product B enrichment zone, a feeding zone, a product A enrichment zone, and a product A repurification zone. The adsorption washing zone, the product B enrichment zone, the feeding zone, the product A enrichment zone, and the product A repurification zone are connected sequentially. The adsorption washing zone includes a first anion exchange resin column 1, a second anion exchange resin column 2, a third anion exchange resin column 3, and a product B collection tank 4. The outlet end of the first anion exchange resin column 1 is connected to the second anion exchange resin column 2, the outlet end of the second anion exchange resin column 2 is connected to the third anion exchange resin column 3, and the outlet end of the third anion exchange resin column 3 is connected to the product B collection tank 4.

[0016] In this embodiment, each resin column uses DTF-NH4. + The resin is designed to process 3 × 10⁻⁴ m³. 3The system operates at a rate of 1.5 m / h, with each resin column containing 450 ml of liquid. The liquid flow direction within the resin column is opposite to the column's rotation direction. The system advances one unit position at a time, significantly improving product precision and purification efficiency of glycine production. Each anion exchange resin column is pre-adsorbed with glycine. The feed to the post-adsorption washing zone is pure water, designed with a feed rate of 1.38 × 10⁻³ m / s. 3 / h, three anion exchange resin columns are connected in series in the same direction as the liquid flow. When each resin column leaves the area, the residual product B on the cation resin will be thoroughly cleaned to improve the product recovery rate.

[0017] Furthermore, the product B enrichment zone includes anion exchange resin column 5 (number four), anion exchange resin column 6 (number five), and an intermediate material tank 7. The discharge end of the product B collection tank 4 is connected to the anion exchange resin column 5 (number four), the discharge end of the anion exchange resin column 5 (number four) is connected to the anion exchange resin column 6 (number five), and the discharge end of the anion exchange resin column 6 (number five) is connected to the intermediate material tank 7.

[0018] In this embodiment, the product B enrichment zone feed is connected to the product B collection tank 4, and the designed feed rate is 1.02 × 10⁻³ m / s. 3 / h, the remaining small amount of product A in the resin column corresponding to this area is pushed into the intermediate material tank 7, while the anion exchange resin that is about to be transferred to the product B enrichment zone adsorbs product B to a saturated state, so as to make full use of it.

[0019] Furthermore, the feeding area includes a No. 6 anion exchange resin column 8, and the discharge end of the No. 6 anion exchange resin column 8 is connected to the intermediate material tank 7.

[0020] In this embodiment, glycine is added to the No. 6 anion exchange resin column 8. In the feeding zone, part of product B is adsorbed by the resin, and the remaining product B is mixed with product A and enters the intermediate material tank 7 from the discharge port. The designed feeding rate is 3×10-4 m3 / h.

[0021] Furthermore, the product A enrichment zone includes anion exchange resin column 9 (No. 7), anion exchange resin column 10 (No. 8), anion exchange resin column 11 (No. 9), and product A collection tank 12. The discharge end of the intermediate material tank is connected to anion exchange resin column 9 (No. 7), the discharge end of anion exchange resin column 9 (No. 7) is connected to anion exchange resin column 10 (No. 8), the discharge end of anion exchange resin column 10 (No. 8) is connected to anion exchange resin column 11 (No. 9), and the discharge end of anion exchange resin column 11 (No. 9) is connected to product A collection tank 12.

[0022] In this embodiment, the feed to the product A enrichment zone is a mixture of products A and B from the intermediate feed tank 7, and the designed feed rate is 1.26 × 10⁻³ m. 3 / h, after the mixed product enters the enrichment zone of product A, product B is completely adsorbed by the No. 7 anion exchange resin column 9, the No. 8 anion exchange resin column 10 and the No. 9 anion exchange resin column 11, and the remaining product A enters the A collection tank through the discharge port.

[0023] Furthermore, the product A repurification zone includes a No. 10 anion exchange resin column 13, and the outlet end of the product A collection tube is connected to the No. 10 anion exchange resin column 13.

[0024] In this embodiment, the product A re-purification zone is connected to the product A collection tank 12, and the product A re-purification zone is a reverse feed zone. While re-purifying product A in the product A collection tank 12, the product A re-purification zone simultaneously pushes out all the pure water that was originally filling the resin column newly entering this functional zone, preventing it from entering the product A collection tank 12 and diluting product A. The product A re-purification zone is designed to have a feed rate of 6 × 10⁻⁴ m³ / s. 3 / h.

[0025] The above-disclosed embodiments are merely preferred embodiments of the present utility model and should not be construed as limiting the scope of the present utility model. Those skilled in the art can understand that implementing all or part of the above-described embodiments and making equivalent changes in accordance with the claims of the present utility model are still within the scope of the utility model.

Claims

1. A purification apparatus for desalting glycine, characterized in that, It includes an adsorption washing zone, a product B enrichment zone, a feeding zone, a product A enrichment zone, and a product A repurification zone, wherein the adsorption washing zone, the product B enrichment zone, the feeding zone, the product A enrichment zone, and the product A repurification zone are connected in sequence; The post-adsorption washing zone includes a No. 1 anion exchange resin column, a No. 2 anion exchange resin column, a No. 3 anion exchange resin column, and a product B collection tank. The discharge end of the No. 1 anion exchange resin column is connected to the No. 2 anion exchange resin column, the discharge end of the No. 2 anion exchange resin column is connected to the No. 3 anion exchange resin column, and the discharge end of the No. 3 anion exchange resin column is connected to the product B collection tank.

2. The purification apparatus for glycine desalting as described in claim 1, characterized in that, The product B enrichment zone includes anion exchange resin column No. 4, anion exchange resin column No. 5, and an intermediate material tank. The discharge end of the product B collection tank is connected to the anion exchange resin column No. 4, the discharge end of the anion exchange resin column No. 4 is connected to the anion exchange resin column No. 5, and the discharge end of the anion exchange resin column No. 5 is connected to the intermediate material tank.

3. The purification apparatus for glycine desalting as described in claim 2, characterized in that, The feeding area includes a No. 6 anion exchange resin column, and the discharge end of the No. 6 anion exchange resin column is connected to the intermediate material tank.

4. The purification apparatus for glycine desalting as described in claim 3, characterized in that, The product A enrichment zone includes anion exchange resin column No. 7, anion exchange resin column No. 8, anion exchange resin column No. 9, and a product A collection tank. The discharge end of the intermediate material tank is connected to the anion exchange resin column No. 7, the discharge end of the anion exchange resin column No. 7 is connected to the anion exchange resin column No. 8, the discharge end of the anion exchange resin column No. 8 is connected to the anion exchange resin column No. 9, and the discharge end of the anion exchange resin column No. 9 is connected to the product A collection tank.

5. The purification apparatus for glycine desalting as described in claim 4, characterized in that, The product A repurification zone includes a No. 10 anion exchange resin column, and the outlet end of the product A collection tube is connected to the No. 10 anion exchange resin column.

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