Continuous production system for food-grade glycine
By constructing a continuous production system for food-grade glycine, and utilizing reaction crystallization and centrifugal separation technologies, the problems of high production costs and difficulty in meeting product quality standards in existing technologies have been solved, achieving efficient and low-cost continuous production of glycine.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-04-08
- Publication Date
- 2026-03-20
AI Technical Summary
In existing technologies, the production process of food-grade glycine is simple, resulting in high costs and difficulty in meeting product quality standards. Furthermore, the existing ammonolysis method for chloroacetic acid has problems such as difficulty in recycling catalysts, high product impurities, and the need for high-cost equipment, making continuous production impossible.
A food-grade continuous production system for glycine is adopted, including a raw material reactor, an ammoniation reactor, a mixed crystal silo, a purification vessel, and a recrystallization vessel. Combined with multiple centrifugal separation modules and circulating pumps, the system achieves direct precipitation and separation of mixed crystals through reaction crystallization, avoiding the use of membrane separation or electrodialysis devices, and constructing a purification system for glycine mixed crystals.
It enables continuous production from chloroacetic acid raw material to food-grade glycine product, reduces production costs, improves production efficiency, avoids the use of high-cost equipment, and realizes the recycling of catalysts and efficient separation of products.
Smart Images
Figure CN224009117U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to aminoacetic acid production technical field, concretely relates to a food grade aminoacetic acid continuous production system. BACKGROUND
[0002] Aminoacetic acid is the simplest amino acid, and is also a non-essential amino acid, commonly known as glycine, white monoclinic or hexagonal crystal, is used in food industry as synthetic wine, brewing products, meat processing and cool beverage formula and saccharin base agent, as food additive, aminoacetic acid can be used as condiment alone, also can cooperate with sodium glutamate, DL-alanine, citric acid etc.
[0003] In the prior art, the process of producing food grade aminoacetic acid is relatively single, and some manufacturers use industrial grade aminoacetic acid to refine and purify multiple times to obtain food grade aminoacetic acid, which greatly increases the production cost of food grade aminoacetic acid, or due to the problem of refining and purification process, the quality of the obtained aminoacetic acid product cannot meet the standard requirements of food grade aminoacetic acid. UTILITY MODEL CONTENT
[0004] The utility model provides a kind of food grade aminoacetic acid continuous production system for realizing from raw material to food grade aminoacetic acid continuous production, and greatly reduce the production cost, can at least solve one of the above technical problems.
[0005] In order to solve the above technical problems, the utility model adopts the following technical scheme: a food grade aminoacetic acid continuous production system, comprising:
[0006] The raw material reactor, the ammoniation reactor, the mixed crystal bin, the refining and purification kettle and the recrystallization kettle are connected in sequence, the raw material reactor inputs chloroacetic acid source product, and the recrystallization kettle outputs food grade aminoacetic acid product;
[0007] The distillation column is connected to the refining and purification kettle for separating and outputting ammonium chloride byproduct;
[0008] The centrifugal separation module has multiple, is connected between the remaining above-mentioned two adjacent devices except between the mixed crystal bin and the refining and purification kettle, and is also connected to the discharge port of the recrystallization kettle and the discharge port of the distillation column;
[0009] A plurality of circulating pumps are connected between the raw material reactor and the centrifugal separation module, between the ammoniation reactor and the centrifugal separation module, and between the recrystallization kettle and the centrifugal separation module, respectively.
[0010] Further, the plurality of centrifugal separation modules are a first centrifugal separation module, a second centrifugal separation module, a third centrifugal separation module, a fourth centrifugal separation module, and a fifth centrifugal separation module, respectively.
[0011] The feed inlet of the first centrifugal separation module is connected to the discharge outlet of the raw material reactor, and the discharge outlet of the first centrifugal separation module is connected to the feed inlet of the ammoniation reactor.
[0012] The feed inlet of the second centrifugal separation module is connected to the discharge outlet of the ammoniation reactor, the discharge outlet of the second centrifugal separation module is connected to the feed inlet of the mixed crystal bin, and the discharge outlet of the mixed crystal bin is connected to the feed inlet of the refining purification kettle.
[0013] The feed inlet of the third centrifugal separation module is connected to the discharge outlet of the refining purification kettle, and the discharge outlet of the third centrifugal separation module is connected to the feed inlets of the recrystallization kettle and the distillation column, respectively.
[0014] The feed inlet of the fourth centrifugal separation module is connected to the discharge outlet of the recrystallization kettle, and the discharge outlet of the fourth centrifugal separation module is connected to obtain a food-grade aminoacetic acid product.
[0015] The feed inlet of the fifth centrifugal separation module is connected to the discharge outlet of the distillation column, and the discharge outlet of the fifth centrifugal separation module is connected to obtain an ammonium chloride byproduct.
[0016] Further, the plurality of circulating pumps are a first circulating pump, a second circulating pump, and a third circulating pump, respectively.
[0017] The first circulating pump is connected between the liquid inlet of the raw material reactor and the liquid outlet of the first centrifugal separation module.
[0018] The second circulating pump is connected between the liquid inlet of the ammoniation reactor and the liquid outlet of the second centrifugal separation module.
[0019] The third circulating pump is connected between the liquid inlet of the recrystallization kettle and the liquid outlet of the fourth centrifugal separation module.
[0020] Further, the liquid outlets of the distillation column and the fifth centrifugal separation module are connected to the liquid inlet of the refining purification kettle, respectively.
[0021] Further, the centrifugal separation module is a filter centrifuge.
[0022] Furthermore, the circulating pump is selected as a diaphragm metering pump.
[0023] Furthermore, the distillation column is selected as a vacuum distillation column.
[0024] The beneficial effects of this utility model are reflected in:
[0025] 1. This utility model achieves continuous production from chloroacetic acid raw material to food-grade glycine product without adding an alcohol precipitation vessel or relying on membrane separation or electrodialysis devices, thereby improving production efficiency and significantly reducing production costs.
[0026] 2. This utility model utilizes a reaction crystallization method, which allows the mixed crystals of glycine obtained after the ammoniation reaction to precipitate directly from the reaction system without the need for a separate alcohol precipitation vessel. The mixed crystals can be separated from the mother liquor (containing catalyst) by a centrifugal separation device, and catalytic recycling can be achieved, saving resources and promoting green production.
[0027] 3. This utility model constructs a purification system for mixed crystal matching of glycine. It does not rely on membrane separation devices or electrodialysis devices. The mixed crystals only need to pass through a purification kettle and a recrystallization kettle to obtain food-grade glycine products, which is more efficient and more economical. Attached Figure Description
[0028] The accompanying drawings, which are provided to further illustrate this application and form part of this application, illustrate exemplary embodiments of this application and are used to explain this application, but do not constitute an undue limitation of this application.
[0029] Figure 1 This is a schematic diagram of the overall structure of the continuous production device according to an embodiment of the present invention.
[0030] The components in the attached diagram are labeled as follows: 1. Raw material reactor; 2. Ammoniation reactor; 3. Purification vessel; 4. Recrystallization vessel; 5. Distillation column; 6. Mixed crystal silo; 7. First centrifugal separation module; 8. Second centrifugal separation module; 9. Third centrifugal separation module; 10. Fourth centrifugal separation module; 11. Fifth centrifugal separation module; 12. First circulation pump; 13. Second circulation pump; 14. Third circulation pump. Detailed Implementation
[0031] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only a part of the embodiments of the present utility model, and not all of them. Unless otherwise specified, the embodiments and features in the embodiments of this application can be combined with each other. Based on the embodiments of the present utility model, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present utility model.
[0032] It should be noted that if the embodiments of this utility model involve descriptions such as "first" or "second," these descriptions are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first" or "second" may explicitly or implicitly include at least one of those features. Furthermore, the meaning of "and / or" throughout the text includes three parallel solutions; for example, "A and / or B" includes solution A, solution B, or a solution where A and B are simultaneously satisfied. Additionally, "multiple" refers to two or more. Moreover, the technical solutions of the various embodiments can be combined with each other, but this must be based on the ability of those skilled in the art to implement them. When the combination of technical solutions is contradictory or impossible to implement, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection claimed by this utility model.
[0033] See Figure 1 This utility model provides a continuous production system for food-grade glycine, comprising:
[0034] The raw material reactor 1, ammoniation reactor 2, mixed crystal silo 6, purification vessel 3 and recrystallization vessel 4 are connected in sequence. The raw material reactor 1 inputs chloroacetic acid source product and the recrystallization vessel 4 outputs food-grade glycine product.
[0035] Distillation column 5, which is connected to the purification vessel 3, is used to separate and output ammonium chloride byproduct;
[0036] Centrifugal separation modules, comprising multiple modules, are respectively connected between the other two adjacent devices mentioned above, except for the mixed crystal hopper 6 and the purification vessel 3, and are also connected to the outlet of the recrystallization vessel 4 and the outlet of the distillation column 5.
[0037] Multiple circulating pumps are connected between the raw material reactor 1 and the centrifugal separation module, between the ammoniation reactor 2 and the centrifugal separation module, and between the recrystallization kettle 4 and the centrifugal separation module.
[0038] See Figure 1In this embodiment, the plurality of centrifugal separation modules are respectively a first centrifugal separation module 7, a second centrifugal separation module 8, a third centrifugal separation module 9, a fourth centrifugal separation module 10 and a fifth centrifugal separation module 11;
[0039] The inlet of the first centrifugal separation module 7 is connected to the outlet of the raw material reactor 1, and the outlet of the first centrifugal separation module 7 is connected to the inlet of the ammoniation reactor 2.
[0040] The inlet of the second centrifugal separation module 8 is connected to the outlet of the ammoniation reactor 2, the outlet of the second centrifugal separation module 8 is connected to the inlet of the mixed crystal silo 6, and the outlet of the mixed crystal silo 6 is connected to the inlet of the purification vessel 3.
[0041] The feed inlet of the third centrifugal separation module 9 is connected to the discharge outlet of the purification vessel 3, and the discharge outlet of the third centrifugal separation module 9 is connected to the feed inlets of the recrystallization vessel 4 and the distillation column 5 respectively.
[0042] The feed inlet of the fourth centrifugal separation module 10 is connected to the discharge outlet of the recrystallization kettle 4, and the discharge outlet of the fourth centrifugal separation module 10 separates and obtains food-grade aminoacetic acid product.
[0043] The feed inlet of the fifth centrifugal separation module 11 is connected to the discharge outlet of the distillation column 5, and the discharge outlet of the fifth centrifugal separation module 11 separates and obtains ammonium chloride byproduct.
[0044] See Figure 1 In this embodiment, the plurality of circulating pumps are a first circulating pump 12, a second circulating pump 13 and a third circulating pump 14;
[0045] The first circulating pump 12 is connected between the inlet of the raw material reactor 1 and the outlet of the first centrifugal separation module 7;
[0046] The second circulating pump 13 is connected between the inlet of the ammoniation reactor 2 and the outlet of the second centrifugal separation module 8;
[0047] The third circulating pump 14 is connected between the liquid inlet of the recrystallization kettle 4 and the liquid outlet of the fourth centrifugal separation module 10.
[0048] See Figure 1 In this embodiment, the outlet of the distillation column 5 and the outlet of the fifth centrifugal separation module 11 are respectively connected to the inlet of the purification vessel 3.
[0049] In this embodiment, the centrifugal separation module is a filter centrifuge.
[0050] In this embodiment, the circulating pump is a diaphragm metering pump.
[0051] In this embodiment, the distillation column 5 is a vacuum distillation column.
[0052] It should be noted that the specific models or types of production equipment or devices involved in this application, such as the centrifugal separation module, circulating pump or distillation column mentioned above, are not specifically limited, and all are implemented using existing technology.
[0053] Hereinafter, this application will combine the above-described embodiments and Figure 1 The production process of food-grade glycine is described in detail:
[0054] The chloroacetic acid source product, namely chloroacetic acid and the reaction solvent, are added to the raw material reactor 1. Ammonia gas is introduced and the reaction is carried out at a set temperature to generate ammonium chloroacetate. The ammonium chloroacetate will crystallize and precipitate in the reaction solvent. After the reaction is completed, the reaction liquid is fed from the outlet of the raw material reactor 1 to the inlet of the first centrifugal separation module 7. After the centrifugal separation operation, the centrifugal filtrate obtained is fed from the outlet of the first centrifugal separation module 7 through the first circulation pump 12 back to the raw material reactor 1 for recycling. The separated ammonium chloroacetate is fed from the outlet of the first centrifugal separation module 7 to the ammoniation reactor 2.
[0055] The catalyst and reaction solvent are added to the ammoniation reactor 2, and ammonia gas is introduced. At a set temperature, ammonium chloroacetate and ammonia gas undergo an ammoniation reaction under the action of the catalyst. The generated glycine and ammonium chloride will crystallize out completely in this reaction system. After the reaction is completed, the reaction liquid containing mixed crystals is input from the outlet of the ammoniation reactor 2 to the second centrifugal separation module 8. After centrifugation, the obtained centrifugal filtrate is input from the outlet of the second centrifugal separation module 8 through the second circulation pump 13 into the ammoniation reactor 2 for recycling. The separated glycine mixed crystals are input from the outlet of the second centrifugal separation module 8 to the mixed crystal silo 6. The glycine mixed crystals in the mixed crystal silo 6 are input into the purification vessel 3.
[0056] The purification solvent is added to the purification vessel 3. At a set temperature, the glycine mixed crystals are purified. In the designed purification solvent, ammonium chloride dissolves while glycine remains insoluble. The solution containing glycine crystals is fed into the third centrifugal separation module 9 through the outlet of the purification vessel 3. After centrifugation, the resulting centrifugal filtrate is fed into the distillation column 5 for distillation. The light component solvent obtained by distillation is fed into the purification vessel 3 through the outlet at the top of the distillation column 5 for recycling. The heavy component is fed into the fifth centrifugal separation module 11 through the outlet at the bottom of the distillation column 5. After centrifugation, the resulting centrifugal filtrate is returned to the purification vessel 3 for recycling, while ammonium chloride byproduct is separated.
[0057] A saturated solution of glycine is added to the recrystallization vessel 4. The glycine crystals separated by the third centrifugal separation module 9 enter the recrystallization vessel 4. At a set temperature, a small amount of ammonium chloride in the glycine crystals dissolves in the solution of the recrystallization vessel 4, while the glycine recrystallizes and precipitates out. After recrystallization, the slurry is fed into the fourth centrifugal separation module 10 through the outlet of the recrystallization vessel 4. After centrifugation, the centrifugal filtrate is returned to the recrystallization vessel 4 for recycling via the third circulation pump 14, while food-grade glycine product is obtained.
[0058] In summary, this utility model provides a continuous production system for food-grade glycine without adding an alcohol precipitation vessel or relying on membrane separation or electrodialysis devices, achieving continuous production from chloroacetic acid raw material to food-grade glycine product, thereby improving production efficiency and significantly reducing production costs.
[0059] Specifically, by using the reaction crystallization method, the glycine mixed crystals obtained after the amination reaction can be directly precipitated from the reaction system without the need for a separate alcohol precipitation vessel. The mixed crystals can be separated from the mother liquor (containing the catalyst) by a centrifugal separation device, and catalytic recycling can be achieved. In addition, a purification system matching the glycine mixed crystals can be constructed. Without relying on membrane separation devices or electrodialysis devices, the mixed crystals can be purified and recrystallized to obtain food-grade glycine products.
[0060] It should be understood that the examples and embodiments described herein are for illustrative purposes only and are not intended to limit the present invention. Those skilled in the art can make various modifications or changes based on them. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.
Claims
1. A continuous production system for food-grade glycine, characterized in that, include: The raw material reactor (1), ammoniation reactor (2), mixed crystal silo (6), purification vessel (3) and recrystallization vessel (4) are connected in sequence. The raw material reactor (1) inputs chloroacetic acid source product and the recrystallization vessel (4) outputs food-grade glycine product. A distillation column (5) is connected to the purification vessel (3) for separating and outputting ammonium chloride byproducts; Centrifugal separation module, having multiple centrifugal separation modules, are respectively connected between the other two adjacent devices mentioned above, except between the mixed crystal silo (6) and the purification vessel (3), and are also connected to the outlet of the recrystallization vessel (4) and the outlet of the distillation column (5); The circulating pumps are of multiple types and are respectively connected between the raw material reactor (1) and the centrifugal separation module, between the ammoniation reactor (2) and the centrifugal separation module, and between the recrystallization kettle (4) and the centrifugal separation module.
2. The food-grade glycine continuous production system as described in claim 1, characterized in that, The plurality of centrifugal separation modules are respectively a first centrifugal separation module (7), a second centrifugal separation module (8), a third centrifugal separation module (9), a fourth centrifugal separation module (10) and a fifth centrifugal separation module (11); The inlet of the first centrifugal separation module (7) is connected to the outlet of the raw material reactor (1), and the outlet of the first centrifugal separation module (7) is connected to the inlet of the ammoniation reactor (2). The inlet of the second centrifugal separation module (8) is connected to the outlet of the ammoniation reactor (2), the outlet of the second centrifugal separation module (8) is connected to the inlet of the mixed crystal silo (6), and the outlet of the mixed crystal silo (6) is connected to the inlet of the purification vessel (3). The feed inlet of the third centrifugal separation module (9) is connected to the discharge outlet of the purification vessel (3), and the discharge outlet of the third centrifugal separation module (9) is connected to the feed inlets of the recrystallization vessel (4) and the distillation column (5), respectively. The feed inlet of the fourth centrifugal separation module (10) is connected to the discharge outlet of the recrystallization kettle (4), and the discharge outlet of the fourth centrifugal separation module (10) separates and obtains food-grade aminoacetic acid product. The feed inlet of the fifth centrifugal separation module (11) is connected to the discharge outlet of the distillation column (5), and the discharge outlet of the fifth centrifugal separation module (11) separates and obtains ammonium chloride by-product.
3. The food-grade glycine continuous production system as described in claim 2, characterized in that, The plurality of circulating pumps are a first circulating pump (12), a second circulating pump (13), and a third circulating pump (14); The first circulating pump (12) is connected between the inlet of the raw material reactor (1) and the outlet of the first centrifugal separation module (7); The second circulating pump (13) is connected between the inlet of the ammoniation reactor (2) and the outlet of the second centrifugal separation module (8); The third circulating pump (14) is connected between the liquid inlet of the recrystallization vessel (4) and the liquid outlet of the fourth centrifugal separation module (10).
4. The food-grade glycine continuous production system as described in claim 2, characterized in that, The outlet of the distillation column (5) and the outlet of the fifth centrifugal separation module (11) are respectively connected to the inlet of the purification vessel (3).
5. The food-grade glycine continuous production system as described in claim 1, characterized in that, The centrifugal separation module is a filter centrifuge.
6. The food-grade glycine continuous production system as described in claim 1, characterized in that, The circulating pump is a diaphragm metering pump.
7. The food-grade glycine continuous production system as described in claim 1, characterized in that, The distillation column (5) is a vacuum distillation column.