A clavulanic acid purification and concentration system

Abstract

The utility model relates to the technical field of chemical equipment, concretely relates to a clavulanic acid purification concentration system to solve the problem of big water consumption and high energy consumption in prior art. The system includes a first ceramic membrane separation unit, a first shunt control unit, a second ultrafiltration membrane separation unit, a second shunt control unit, a third nanofiltration membrane separation unit and a third shunt control unit, and the system is also provided with a three-stage circulation loop, and the flow direction of the concentrated liquid and dialysis liquid output by the membrane separation units at all stages is controlled through the shunt control units at all stages and the multistage circulation loop to improve the purification efficiency, reduce energy consumption and production cost, and ensure the product quality stability.

Description

Technical Field

[0001] This utility model relates to the field of chemical equipment technology, and in particular to a clavulanic acid purification and concentration system. Background Technology

[0002] Clavulanic acid is an important β-lactamase inhibitor. By irreversibly inhibiting β-lactamase, clavulanic acid blocks the hydrolytic action of bacterial enzymes on β-lactam antibiotics (such as penicillin and cephalosporins), thereby protecting the activity of antibiotics, enhancing antibacterial effects, and broadening the antibacterial spectrum. It can be used to treat respiratory tract infections, urinary tract infections, and skin and soft tissue infections.

[0003] Currently, clavulanic acid is mainly produced through microbial fermentation (such as with Streptomyces strains). This involves purifying and concentrating the fermented culture, followed by extraction with organic solvents. The effectiveness of the purification process directly impacts product quality. The clavulanic acid fermentation broth purification process primarily utilizes ceramic membranes to remove bacterial cells, ultrafiltration for decolorization and impurity removal, and nanofiltration for concentration. As disclosed in the background technology of Chinese utility model patent CN206414979U, existing nanofiltration membrane concentration systems operate below 20 bar, achieving a concentration factor of approximately 10 times and a concentrate concentration of around 4%. This results in significant water consumption and increases the energy required for subsequent evaporation processes. Therefore, existing technologies require further improvement. Utility Model Content

[0004] To address the aforementioned technical problems, the purpose of this invention is to provide a clavulanic acid purification and concentration system that solves the problems of high water consumption and high energy consumption in the prior art.

[0005] To achieve the above-mentioned technical effects, the present invention adopts the following technical solution:

[0006] A clavulanic acid purification and concentration system, comprising:

[0007] The primary ceramic membrane separation unit is configured to use a primary ceramic membrane separation component with a pore size of 0.05-0.2μm to perform solid-liquid separation on the clavulanic acid fermentation broth;

[0008] A primary diversion control unit is connected to the dialysate outlet of the primary ceramic membrane separation assembly and is configured to direct the dialysate to the primary dialysis tank or an external water storage tank.

[0009] A secondary ultrafiltration membrane separation unit, starting from the primary dialysis tank, is configured to decolorize and purify the dialysate using a secondary ultrafiltration membrane separation assembly with a molecular weight cutoff of 500-5000 Daltons.

[0010] A secondary diversion control unit is connected to the dialysate outlet of the secondary ultrafiltration membrane separation assembly and is configured to guide the dialysate to a secondary dialysis tank or a crystallization tank.

[0011] The three-stage nanofiltration membrane separation unit is configured to use a three-stage nanofiltration membrane separation component with a molecular weight cutoff of ≤200 Daltons to concentrate the dialysate in stages.

[0012] The three-stage diversion control unit is connected to the dialysate outlet of the three-stage nanofiltration membrane separation assembly and is configured to guide the dialysate to the three-stage dialysis tank or an external water storage tank.

[0013] In the aforementioned system, the primary ceramic membrane separation unit utilizes a ceramic membrane with a pore size of 0.05-0.2 μm to effectively remove large particulate impurities such as bacterial cells from the fermentation broth, achieving solid-liquid separation and providing a clear dialysis solution for subsequent processing. The secondary ultrafiltration membrane separation unit uses an ultrafiltration membrane with a molecular weight cutoff of 500-5000 Daltons, which can further decolorize and remove impurities, such as proteins and polysaccharides, from the fermentation broth, improving the purity of clavulanic acid. The tertiary nanofiltration membrane separation unit uses a nanofiltration membrane with a molecular weight cutoff of ≤200 Daltons to fractionally concentrate the ultrafiltration dialysis solution, effectively concentrating clavulanic acid and increasing its concentration, thereby improving product quality and yield.

[0014] Furthermore, the external water storage tank is connected to the primary ceramic membrane separation unit via a pipeline.

[0015] Preferably, the external water storage tank is configured as follows:

[0016] Recovery of dialysate with a potency of <100 μg / ml and a transmittance of ≥10% from the primary ceramic membrane separation unit;

[0017] Recovery of dialysate with a potency ≥10μg / ml and transmittance ≥40% from a three-stage nanofiltration membrane separation unit;

[0018] This method enables the recycling of low-concentration clavulanic acid aqueous solutions, reducing production costs, water consumption, and consequently energy consumption in subsequent evaporation processes.

[0019] Furthermore, the system also includes a three-level loop, which includes:

[0020] A primary circulation loop is connected to the primary ceramic membrane separation unit and configured to return the concentrate output from the primary ceramic membrane separation unit to the upstream of the primary ceramic membrane separation unit;

[0021] A secondary circulation loop is connected to the secondary ultrafiltration membrane separation unit and configured to return the concentrate output from the secondary ultrafiltration membrane separation unit to the upstream of the secondary ultrafiltration membrane separation unit;

[0022] A three-stage circulation loop is connected to the three-stage nanofiltration membrane separation assembly and configured to return the concentrate output by the three-stage nanofiltration membrane separation assembly to the upstream of the three-stage nanofiltration membrane separation assembly.

[0023] Preferably, the output end of the primary circulation loop is connected to the primary raw material tank; the output end of the secondary circulation loop is connected to the secondary raw material tank; and the output end of the tertiary circulation loop is located in the tertiary raw material tank. This multi-stage circulation loop setup ensures the full processing and recycling of the concentrate throughout the system, improving purification and concentration efficiency. Simultaneously, the output end of each circulation loop is also connected to the corresponding raw material tank, ensuring sufficient raw material supply to each processing unit and maintaining stable system operation.

[0024] Furthermore, heat exchange devices are installed in the primary, secondary, and tertiary circulation loops. These heat exchange devices effectively utilize the heat generated by the concentrate during the circulation process, enabling energy recovery and reuse. By preheating or cooling the concentrate through the heat exchange devices, its temperature is brought closer to the optimal operating temperature range of each processing unit, improving the efficiency and effectiveness of the membrane separation process. At the same time, it reduces the system's energy consumption, achieving the goal of energy saving and consumption reduction, improving the overall energy utilization efficiency of the system, and reducing production costs.

[0025] Furthermore, the primary ceramic membrane separation unit includes a primary feed tank, the primary ceramic membrane separation component is located downstream of the primary feed tank, and the concentrate outlet of the primary ceramic membrane separation component is connected to the primary feed tank through the primary circulation loop.

[0026] Furthermore, the secondary ultrafiltration membrane separation unit includes a secondary feed tank located between the primary dialysis tank and the secondary ultrafiltration membrane separation assembly, and the output end of the secondary circulation loop is connected to the secondary feed tank.

[0027] Furthermore, the three-stage nanofiltration membrane separation unit includes a three-stage feed tank located between the two-stage dialysis tank and the three-stage nanofiltration membrane separation assembly, and the output end of the three-stage circulation loop is connected to the three-stage feed tank.

[0028] Furthermore, in this system, to achieve precise control of the dialysate flow direction, the primary diversion control unit, the secondary diversion control unit, and the tertiary diversion control unit all include:

[0029] A hydrometer is installed on each level of the diversion control unit and is used to detect the dialysate. It can monitor the specific gravity and other mass parameters of the dialysate in real time.

[0030] The diversion valve assembly, linked to the hydrometer, controls the liquid flow direction. This diversion valve assembly can automatically control the operation of the diversion valve assembly according to the set indicators, ensuring that only dialysate that meets the quality requirements can enter the next processing stage, thereby improving the quality and stability of the final product.

[0031] Compared with the prior art, the beneficial effects of this utility model are as follows:

[0032] First, the clavulanic acid purification and concentration system provided by this utility model achieves efficient graded separation and concentration. Specifically, it achieves the gradual purification and concentration of clavulanic acid fermentation broth through the synergistic effect of a primary ceramic membrane separation unit, a secondary ultrafiltration membrane separation unit, and a tertiary nanofiltration membrane separation unit.

[0033] Meanwhile, the system's multi-stage diversion control units allow for flexible adjustment of the dialysate flow direction based on actual production needs. In the primary diversion control unit, the dialysate can be directed to the primary dialysis tank for further processing, or temporarily stored in an external water tank depending on its quality. Similarly, the secondary and tertiary diversion control units also possess this function, ensuring that dialysate at different stages is properly treated and recycled. Furthermore, the external water tank can recover dialysate with lower potency but meeting certain transmittance requirements, and use it as a washing solvent for the primary ceramic membrane separation unit, achieving water recycling, reducing production costs, decreasing water consumption, and consequently reducing energy consumption in subsequent evaporation processes.

[0034] Furthermore, the three-stage circulation loop design, including primary, secondary, and tertiary circulation loops, allows the concentrated liquid output from each membrane separation unit to be returned to the corresponding upstream feed tank, ensuring full treatment and recycling of the fermentation broth throughout the system and improving purification and concentration efficiency. Simultaneously, the output of each circulation loop is connected to the corresponding feed tank, ensuring sufficient raw material supply to each processing unit, maintaining stable system operation, avoiding production interruptions due to insufficient raw materials, and improving production continuity and stability.

[0035] Finally, precise diversion control and quality monitoring: The interconnected design of the hydrometers and diversion valve assemblies in each diversion control unit enables real-time monitoring of quality parameters such as the specific gravity of the dialysate. Based on set parameters, the system automatically controls the diversion valve assembly, achieving precise control of the dialysate flow direction. This ensures that only dialysate meeting quality requirements proceeds to the next processing stage, thereby improving the quality and stability of the final product, reducing the generation of defective products, and lowering production costs. Attached Figure Description

[0036] Figure 1 A schematic diagram of the overall structure of a clavulanic acid purification and concentration system provided by this utility model;

[0037] The attached figures are labeled as follows: 01, valve; 02, heat exchanger; 03, hydrometer; 04, external water storage tank; 101, primary feed tank; 102, primary feed pump; 103, primary ceramic membrane separation assembly; 104, primary dialysis tank; 105, primary circulation loop; 201, secondary feed tank; 202, secondary feed pump; 203, secondary ultrafiltration membrane separation assembly; 204, secondary dialysis tank; 205, secondary circulation loop; 206, crystallization tank; 301, tertiary feed tank; 302, tertiary feed pump; 303, tertiary nanofiltration membrane separation assembly; 304, tertiary dialysis tank; 305, tertiary circulation loop. Detailed Implementation

[0038] The embodiments of the present invention will now be described in detail with reference to the accompanying drawings. These embodiments are merely illustrative of the present invention and should not be construed as limiting the scope of protection of the present invention.

[0039] Unless otherwise specified, in this utility model, terms such as "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," "x-direction," "y-direction," and "z-direction" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, the terms used to describe orientation or positional relationships in this utility model are for illustrative purposes only and should not be construed as limiting this patent. For those skilled in the art, the specific meaning of the above terms can be understood in conjunction with the accompanying drawings and according to the specific circumstances.

[0040] This embodiment provides a clavulanic acid purification and concentration system. Through reasonable equipment configuration and optimized operation process, this clavulanic acid purification and concentration system and process achieve efficient purification and concentration of clavulanic acid fermentation broth, improving product quality while reducing production costs, and has significant practical value. The equipment structure and process flow of this clavulanic acid purification and concentration system are closely linked to achieve efficient purification and concentration.

[0041] Please see Figure 1 The clavulanic acid purification and concentration system comprises key components such as multi-stage separation units, multi-stage diversion control units, circulation loops, external water storage tank 04, heat exchange device 02, hydrometer 03, and multi-stage raw material tanks. The multi-stage separation units include a first-stage ceramic membrane separation unit, a second-stage ultrafiltration membrane separation unit, and a third-stage nanofiltration membrane separation unit connected in sequence. Specifically:

[0042] First, the clavulanic acid purification and concentration system includes an external water tank 04, which is used to supply washing solvent to the primary ceramic membrane separation unit and recover the low-efficiency, high-transmittance dialysate diverted from each stage of the membrane separation unit, thereby realizing solvent recycling and reducing production costs.

[0043] In this system, the primary ceramic membrane separation unit includes a primary raw material tank 101, a primary feed pump 102, and a primary ceramic membrane separation component 103. The primary raw material tank 101 is connected to an external water storage tank 04 and is equipped with a clavulanic acid fermentation broth inlet. The primary ceramic membrane separation unit uses the primary ceramic membrane separation component 103 with a pore size of 0.05-0.2μm to perform preliminary solid-liquid separation on the clavulanic acid fermentation broth, removing mycelia and suspended solids from the clavulanic acid fermentation broth to produce a preliminarily clarified dialysate.

[0044] To achieve the objective of this invention, the dialysis solution obtained by the primary ceramic membrane separation component 103 needs to undergo fractionation treatment, including:

[0045] The resulting dialysate 1 (potency ≥ 20000 μg / ml, transmittance ≥ 10%) enters the secondary ultrafiltration membrane separation unit for decolorization; the resulting dialysate 2 (100 μg / ml ≤ potency < 20000 μg / ml, transmittance ≥ 10%) enters the secondary ultrafiltration membrane separation unit for further processing; and the resulting dialysate 3 (potency < 100 μg / ml, transmittance ≥ 10%) is returned to the external water storage tank 04 for recycling as clavulanic acid washing solution.

[0046] To achieve the aforementioned functions, the system also includes a primary diversion control unit and a primary circulation loop 105. The primary diversion control unit directs the dialysate to the secondary ultrafiltration membrane separation unit or the external water storage tank 04 for reuse based on the dialysate quality parameters. The primary circulation loop 105 returns the concentrate separated by the primary ceramic membrane separation component 103 to the primary feed tank 101, enhancing the separation effect and ensuring system stability. Specifically, the primary ceramic membrane separation component 103 includes a primary dialysate outlet and a primary concentrate outlet. The primary circulation loop 105 is connected to the primary concentrate outlet to return the concentrate, while the primary dialysate outlet is connected to the primary diversion control unit. The primary diversion control unit is equipped with a hydrometer 03. After detection by the hydrometer 03, the liquid from the primary dialysate outlet is divided into two streams: one stream connects to the primary dialysis tank 104 via valve 01 and a pipeline, and the other stream connects to the external water storage tank 04 via valve 01 and a pipeline.

[0047] In this embodiment, a heat exchange device 02 is installed on the primary circulation loop 105, and the primary dialysis tank 104 is connected to the secondary raw material tank 201 through a pipeline.

[0048] In this system, the secondary ultrafiltration membrane separation unit uses an ultrafiltration membrane with a molecular weight cutoff of 500-5000 Daltons to decolorize dialysate 1 and dialysate 2 after treatment by the primary ceramic membrane separation component 103. Specifically, the secondary ultrafiltration membrane separation unit includes a secondary feed tank 201, a secondary feed pump 202, and a secondary ultrafiltration membrane separation component 203 connected in sequence by pipelines. The secondary diversion control unit directs the dialysate to the secondary dialysis tank 204 or the crystallization tank 206 via a diversion valve assembly, depending on the dialysate quality.

[0049] The secondary ultrafiltration membrane separation component 203 includes a secondary dialysate outlet and a secondary concentrate outlet. The secondary concentrate outlet is connected to the secondary feed tank 201 via a secondary circulation loop 205. The secondary dialysate outlet is connected to a secondary diversion control unit, which is equipped with a hydrometer 03. After detection by the hydrometer 03, the liquid is divided into two streams: the generated dialysate 4 (potency ≥ 20000 μg / ml, transmittance ≥ 40%) is fed into the crystallization tank 206 for evaporation and crystallization, while the generated dialysate 5 (potency < 20000 μg / ml, transmittance ≥ 40%) enters the secondary dialysis tank 204 for further input to the next stage for nanofiltration concentration. The secondary circulation loop 205 returns the concentrate to the secondary feed tank 201 to ensure thorough treatment of the dialysate. The secondary circulation loop 205 is equipped with a heat exchange device 02, similar to the primary circulation loop 105.

[0050] In this embodiment, the three-stage nanofiltration membrane separation unit includes a three-stage raw material tank 301, a three-stage feed pump 302, and a three-stage nanofiltration membrane separation assembly 303 connected in sequence by pipelines. The nanofiltration membrane separation pore size in the three-stage nanofiltration membrane separation assembly 303 is ≤200 Daltons. The three-stage nanofiltration membrane separation assembly 303 includes a three-stage dialysate outlet and a three-stage concentrate outlet. The three-stage dialysate outlet is connected to a three-stage diversion control unit. The three-stage diversion control unit is equipped with a hydrometer 03. The three-stage diversion control unit distributes the dialysate to the three-stage dialysis tank 304 or the external water storage tank 04 according to the dialysate index. Specifically, in this process, dialysate with a potency <10μg / ml can be input into the three-stage dialysis tank 304, while dialysate with a potency ≥10μg / ml is input into the external water storage tank 04. The dialysate in the external water storage tank 04 can be used for ceramic membrane washing filtration.

[0051] The outlet of the third-stage concentrate is connected to the third-stage circulation loop 305, which causes a portion of the concentrate to flow back to the third-stage feed tank 301, optimizing the concentration effect. The heat exchange device 02 effectively reduces energy consumption. The hydrometer 03 is installed at the dialysate outlet of each membrane separation unit to monitor key parameters such as dialysate specific gravity in real time and provide feedback to the diversion control unit, providing a basis for diversion decisions.

[0052] Each raw material tank serves as a temporary storage device for raw materials before each separation unit, storing the dialysate to be processed and then stably transporting it to the corresponding separation unit via a pumping device, ensuring the continuity of the process flow. The diversion valve assembly is closely linked with the hydrometer 03, automatically regulating the dialysate flow direction based on dialysate parameter signals to control product quality.

[0053] In the clavulanic acid purification and concentration process, the fermentation broth first enters the primary feed tank 101 for temporary storage, and is then pumped to the primary ceramic membrane separation unit for solid-liquid separation. The resulting dialysate is precisely distributed by the primary diversion control unit, with part entering the primary dialysis tank 104 and part entering the external water storage tank 04 for recycling. The dialysate in the primary dialysis tank 104 further flows into the secondary feed tank 201, and then undergoes further decolorization and impurity removal by the secondary ultrafiltration membrane separation unit to improve purity. The dialysate separated by the secondary ultrafiltration membrane separation unit is partially sent to the secondary dialysis tank 204 and partially sent to the crystallization tank 206 under the action of the secondary diversion control unit. The dialysate in the secondary dialysis tank 204 is further transported to the tertiary feed tank 301 in the next process, and then enters the tertiary nanofiltration membrane separation unit for fractional concentration to further increase the clavulanic acid concentration. After tertiary diversion control separation, the tertiary diversion control unit rationally distributes it to the tertiary dialysis tank 304 or the external water storage tank 04 according to the dialysate indicators.

[0054] During the above process, the external water storage tank 04 continuously supplies washing solvent to the primary ceramic membrane separation unit and recovers the dialysate from each stage, achieving solvent recycling. The heat exchange device 02 preheats or cools the concentrates at each stage, precisely controlling the temperature to match the optimal operating temperature range of each membrane separation unit, thereby enhancing membrane separation efficiency and reducing energy consumption. The hydrometer 03 monitors key parameters of the dialysate in real time, closely linking with the diversion valve group. Based on preset quality standards, it automatically controls the dialysate flow direction, intercepts unqualified products, and releases qualified products, ensuring stable and reliable clavulanic acid product quality.

[0055] The above embodiments are only used to illustrate the technical solutions of this utility model and are not intended to limit it. Although this utility model has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can be made to the technical solutions of this utility model without departing from the spirit and scope of the technical solutions of this utility model, and all such modifications and substitutions should be covered within the scope of the claims of this utility model. Technologies, shapes, and structural parts not described in detail in this utility model are all known technologies.

Claims

1. A clavulanic acid purification and concentration system, characterized in that, include: The primary ceramic membrane separation unit is configured to use a primary ceramic membrane separation component (103) with a pore size of 0.05-0.2μm to perform solid-liquid separation of clavulanic acid fermentation broth; A primary diversion control unit is connected to the dialysate outlet of the primary ceramic membrane separation assembly (103) and is configured to direct the dialysate to the primary dialysis tank (104) or an external water storage tank (04). A secondary ultrafiltration membrane separation unit, starting from the primary dialysis vessel (104), is configured to decolorize and purify the dialysate using a secondary ultrafiltration membrane separation assembly (203) with a molecular weight cutoff of 500-5000 Daltons; A secondary diversion control unit is connected to the dialysate outlet of the secondary ultrafiltration membrane separation assembly (203) and is configured to direct the dialysate to the secondary dialysis tank (204) or the crystallization tank (206); The three-stage nanofiltration membrane separation unit is configured to use a three-stage nanofiltration membrane separation component (303) with a molecular weight cutoff of ≤200 Daltons to perform fractional concentration of the dialysate; The three-stage diversion control unit is connected to the dialysate outlet of the three-stage nanofiltration membrane separation assembly (303) and is configured to direct the dialysate to the three-stage dialysis tank (304) or an external water storage tank (04).

2. The clavulanic acid purification and concentration system as described in claim 1, characterized in that: The external water storage tank (04) is connected to the primary ceramic membrane separation unit via a pipeline.

3. The clavulanic acid purification and concentration system as described in claim 1, characterized in that: The external water storage tank (04) is configured as follows: Recovery of dialysate with a potency of <100 μg / ml and a transmittance of ≥10% from the primary ceramic membrane separation unit; Dialysate with a potency ≥10μg / ml and transmittance ≥40% was recovered from the three-stage nanofiltration membrane separation unit.

4. The clavulanic acid purification and concentration system as described in claim 1, characterized in that, It also includes a three-stage loop (305), which comprises: A primary circulation loop (105) is connected to the primary ceramic membrane separation unit (103) and configured to return the concentrate output by the primary ceramic membrane separation unit (103) to the upstream of the primary ceramic membrane separation unit (103); A secondary circulation loop (205) is connected to the secondary ultrafiltration membrane separation unit (203) and configured to return the concentrate output by the secondary ultrafiltration membrane separation unit (203) to the upstream of the secondary ultrafiltration membrane separation unit (203); A three-stage circulation loop (305) is connected to the three-stage nanofiltration membrane separation assembly (303) and configured to return the concentrate output by the three-stage nanofiltration membrane separation assembly (303) to the upstream of the three-stage nanofiltration membrane separation assembly (303).

5. The clavulanic acid purification and concentration system as described in claim 4, characterized in that: The output end of the primary circulation loop (105) is connected to the primary raw material tank (101); The output end of the secondary circulation loop (205) is connected to the secondary raw material tank (201); The output end of the three-stage circulation loop (305) is located in the three-stage raw material tank (301).

6. The clavulanic acid purification and concentration system as described in claim 4, characterized in that: Heat exchange devices (02) are provided on the primary circulation loop (105), the secondary circulation loop (205) and the tertiary circulation loop (305).

7. The clavulanic acid purification and concentration system as described in claim 4, characterized in that: The primary ceramic membrane separation unit includes a primary raw material tank (101), and the primary ceramic membrane separation component (103) is located downstream of the primary raw material tank (101). The concentrate outlet of the primary ceramic membrane separation component (103) is connected to the primary raw material tank (101) through the primary circulation loop (105).

8. The clavulanic acid purification and concentration system as described in claim 4, characterized in that: The secondary ultrafiltration membrane separation unit includes a secondary feed tank (201) located between the primary dialysis tank (104) and the secondary ultrafiltration membrane separation assembly (203), and the output end of the secondary circulation loop (205) is connected to the secondary feed tank (201).

9. A clavulanic acid purification and concentration system as described in claim 4, characterized in that: The three-stage nanofiltration membrane separation unit includes a three-stage feed tank (301) located between the two-stage dialysis tank (204) and the three-stage nanofiltration membrane separation assembly (303), and the output end of the three-stage circulation loop (305) is connected to the three-stage feed tank (301).

10. A clavulanic acid purification and concentration system as described in claim 1, characterized in that, The primary, secondary, and tertiary shunt control units all include: A hydrometer (03) is installed on each level of the diversion control unit and is used to detect the dialysate; The diversion valve assembly is linked with the hydrometer (03) and controls the liquid flow direction.

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