A seawater desalination-uranium extraction cogeneration assembly device and a uranium extraction and regeneration process thereof

Abstract

The present application relates to the technical field of hollow fiber membrane, in particular to a seawater desalination-uranium extraction combined assembly device and a uranium extraction and regeneration process thereof.The present application provides a seawater desalination-uranium extraction combined assembly device, which is composed of a top cover, a rotatable bottom disc and a membrane filament assembly, and is divided into an adsorption zone, a buffer zone and a desorption regeneration zone.The process flow is as follows: seawater is adsorbed with uranium by the membrane filament assembly in series in the adsorption zone;the saturated assembly is rotated to the buffer zone and then enters the desorption regeneration zone;acid water is desorbed with uranium by the membrane filament assembly in series in the desorption regeneration zone, and the regenerated assembly is rotated back to the adsorption zone for recycling.The present application adopts a "multi-stage series progressive saturation + dynamic forward switching" mechanism to solve the continuous production bottleneck of the combined production, and realizes the integration of efficient utilization of acid water and uranium concentration through the "countercurrent concentration gradient desorption" strategy.

Description

Technical Field

[0001] This invention relates to the field of hollow fiber membrane technology, and more specifically to a seawater desalination-uranium extraction co-production component device and its uranium extraction and regeneration process. Background Technology

[0002] Hollow fiber membrane materials, with their structural advantages and separation performance, have become ideal carriers for integrating seawater desalination and uranium extraction. A previous invention patent (application number: 202311770819.1) described a methylamine oxime-modified polyacrylonitrile hollow fiber membrane for seawater uranium extraction and its preparation method. This hollow fiber membrane combines the separation function of a membrane with the specific adsorption function of uranium. However, when this membrane material is processed into common component applications, some problems still need to be solved.

[0003] Problem 1: The segmental breakdown of membrane fibers leads to low adsorption efficiency and serious waste of resources.

[0004] In existing hollow fiber membrane adsorption systems, adsorption exhibits uneven distribution under flowing seawater conditions. Because the seawater flow direction is parallel to the membrane fiber axis, seawater passes radially through the membrane fibers for filtration and adsorption, while the membrane fibers undergo adsorption and saturation breakdown sequentially along the direction perpendicular to the flow. At the inlet, the membrane fibers are first exposed to high flow velocities and high pollutant loads, leading to saturation and breakdown, while at the outlet, the membrane fibers are far from saturated. Excessively long membrane fibers cannot fully utilize the overall adsorption capacity, while shortening the fiber length can alleviate the asynchronous problem but increases the replacement frequency, further reducing system efficiency.

[0005] To maintain the effectiveness of uranium extraction from seawater, if the membrane fibers at the inlet rupture and cause uranium leakage, the entire membrane module must be replaced. The "segment-by-segment rupture" effect of the membrane fibers is similar to the "bucket effect," meaning that the overall performance of the entire system is limited by the weakest link (the shortest plank), namely the membrane fibers at the inlet. During replacement, most areas of the membrane fibers within the module are not yet saturated, resulting in significant resource waste.

[0006] The technical difficulty of solving problem 1 in the existing technology is that the inherent axial flow characteristics of the membrane fibers determine the problem of asynchronous adsorption, and the "bucket effect" in the desalination process cannot be eliminated.

[0007] Question 2: Existing membrane fiber regeneration processes are limited to desorption and are difficult to achieve efficient recycling.

[0008] Regeneration of hollow fiber membranes after adsorption saturation mainly relies on acid leaching and desorption (e.g., 0.5-2 M HCl solution) followed by water washing and neutralization. These steps can achieve a desorption rate of 80%-95%, restoring the membrane's adsorption function. However, the process consumes a large amount of water and acid, and the low uranium concentration in the desorption solution makes economic recovery difficult due to the dilution effect. Existing regeneration methods neglect recovery optimization, focusing only on the sufficiency of desorption without integrating concentration or secondary extraction steps, resulting in low overall resource utilization.

[0009] The technical difficulty of solving problem 2 in the existing technology is that the regeneration process emphasizes the use of a large amount of desorption solution for efficient desorption to restore the adsorption capacity, while the recovery process requires minimizing the amount of solvent used and the output of high uranium concentration. There is an inherent contradiction between the two, which is difficult for the existing technology to solve.

[0010] Question 3: The huge volume of seawater to be treated and the need for frequent replacement of saturated membrane fiber modules restrict continuous production.

[0011] Seawater desalination has a huge production capacity, but the membrane fiber adsorption capacity is limited, resulting in a short saturation period and frequent component replacements, interrupting production continuity. This has become a bottleneck problem for cogeneration processes. Existing systems are feasible on a laboratory scale, but when scaled up industrially, the large number of membrane modules and high replacement costs make replacements difficult. Summary of the Invention

[0012] Based on the above problems and their technical difficulties, the following inventive concept is proposed:

[0013] To address issue 1, a "multi-stage series progressive saturation + dynamic forward switching" mechanism is adopted to avoid the "bucket effect" caused by uneven adsorption along the axial direction of a single membrane filament.

[0014] By designing a perforated connection method, hollow fiber membrane modules are connected in series to achieve a multi-stage adsorption system. Seawater flows sequentially through the series-connected membrane modules in a single direction, with the uranium adsorption capacity of the hollow fiber membranes in each module decreasing progressively. When the first-stage membrane module reaches adsorption saturation, it automatically enters the desorption and regeneration zone; subsequent membrane modules move forward in sequence to fill the gap, taking over the adsorption task of the previous stage until saturation. This series configuration effectively extends the overall breakdown time of the hollow fiber membrane system, overcomes the "bucket effect" limitation, and significantly improves adsorption efficiency and resource utilization.

[0015] Regarding question 2: The "countercurrent concentration gradient desorption" strategy achieves integrated efficient utilization of acid and uranium enrichment, resolving the contradiction between regeneration and recycling.

[0016] The desorption module consists of multiple hollow fiber membrane modules connected in series, with the flow direction of the desorption acid opposite to that of the seawater. The first-stage desorption module has already undergone desorption as a subsequent module in the previous multi-stage desorption cycle, and its uranium residue is the lowest among the desorption modules at the current stage. The uranium residue in subsequent modules increases sequentially. When the acid enters the first-stage module, because the acid does not contain uranium, the concentration difference between the acid and the uranium residue on the membrane surface is the largest, resulting in the strongest driving force and ensuring complete uranium removal in this module. Subsequently, the acid carrying low-concentration uranium flows sequentially through subsequent desorption modules, with the uranium removal efficiency decreasing at each stage. By controlling the acid dosage and the multi-stage desorption process, the final effluent is a high-concentration uranium solution, significantly improving uranium recovery efficiency. The acid gradually enriches uranium during multiple desorption processes, achieving uranium recovery from low to high concentrations; simultaneously, each membrane module undergoes multiple desorption cycles, efficiently completing membrane fiber regeneration.

[0017] Regarding question 3: Constructing a "multi-module + cyclic rotation switching" framework to achieve parallel adsorption and regeneration, eliminating replacement interruptions, has become a key breakthrough for continuous co-production.

[0018] The design incorporates multiple independent module arrays, with some connected in series as adsorption channels (for seawater treatment) and others as regeneration channels (for uranium desorption). A rotating mechanism periodically switches module positions, allowing saturated modules to be seamlessly transferred and regenerated, with new modules immediately filling the gap. The two channels operate in parallel with physical isolation, completely resolving the bottleneck.

[0019] The technical problem to be solved by the present invention is how to provide an extraction and regeneration process and apparatus based on seawater uranium extraction components.

[0020] Based on the above-mentioned inventive concept, this invention fully utilizes the synergistic effect between the various components and processes, which complement and interact with each other to form a whole, rather than a simple combination, thus systematically solving the above-mentioned technical problems.

[0021] To achieve the objectives of this invention, the following technical solution is adopted:

[0022] A seawater desalination-uranium extraction co-production unit consists of three parts: a top cover, a chassis, and a membrane fiber assembly. It is divided into an adsorption zone, a buffer zone, and a desorption / regeneration zone. The corresponding inlet, groove, pipeline, membrane fiber assembly, and outlet of each zone constitute the seawater circuit, acid water circuit, and clean water circuit, respectively. Different membrane fiber assemblies can be connected to the adsorption zone, buffer zone, and desorption / regeneration zone by rotating the chassis.

[0023] The top cover is equipped with seawater inlet, seawater outlet, acid water inlet, acid water outlet, clean water inlet, and clean water outlet; each of these is also equipped with a groove.

[0024] The chassis has two concentric parallel pipes that connect to the inlet and outlet of each membrane fiber module, with a total of 6-12 membrane fiber modules. The chassis and the 6-12 membrane fiber modules are connected by a connecting pipe. The buffer zone contains 1 membrane fiber module; the adsorption zone contains 3-5 membrane fiber modules; and the desorption and regeneration zone contains 2-6 membrane fiber modules, one of which is a clean water washing membrane fiber module.

[0025] The top cover and the chassis are connected by a central fixed shaft. The contact surface between the bottom of the top cover and the top of the chassis is sealed and can rotate around the fixed shaft.

[0026] A uranium extraction and regeneration process for a seawater desalination-uranium extraction co-production unit includes the following components:

[0027] Adsorption process: Seawater enters through the seawater inlet of the top cover adsorption zone, flows through 3-5 membrane fiber modules connected in series via the matching of the top cover connecting groove and the bottom platen orifice, with a flux of 20-70 L / (m²). 2 ·h), the area of ​​each membrane fiber module is 5-80m² 2 Each membrane fiber module has a height of 0.5-2m and an adsorption time of 1-30 days;

[0028] Desorption and regeneration: Acidic water with pH=1-5 flows through 1-5 membrane fiber modules connected in series, with a volume of 3-50L and a desorption time of 1-3 days. The volume of clean water is 3-50L, and the rinsing time is 1-3 days. The pH of the rinsed clean water is adjusted to the pH required for the acidic water and used as acidic water. The volumes of acidic water and clean water are 3-50L, which are the volumes entering through the acidic water inlet and the clean water inlet, respectively.

[0029] Rotation switching: After adsorption is complete, rotate the chassis clockwise by 360° divided by the number of holes on the inner side of the chassis center; the membrane fiber assembly is switched sequentially.

[0030] Technical Notes:

[0031] 1. After rotation, the membrane fiber assembly, which has been rinsed with clean water in the desorption and regeneration zone, enters the adsorption zone; the membrane fiber assembly connected to the seawater inlet rotates to the buffer zone; the membrane fiber assembly in the buffer zone enters the desorption and regeneration zone and is connected to the acid water outlet; the rotation is repeated in the above manner.

[0032] 2. The adsorption zone membrane fiber module consists of multiple membrane fiber modules connected in series. Their uranium adsorption capacity decreases sequentially along the direction of the coastal water flow. Through rotation, the membrane fiber module whose uranium adsorption capacity is closest to saturation first enters the buffer zone. After the membrane fiber module in the regeneration and desorption zone enters the adsorption zone, the uranium adsorption capacity of the membrane fiber module continues to decrease sequentially along the direction of the coastal water flow, achieving single-fiber saturation and single-fiber desorption.

[0033] like Figure 7 and Figure 8As shown, in the breakdown performance test of the membrane fiber modules, the breakdown time of a single membrane fiber in modules with 1, 2, and 3 tandem membrane fibers increases sequentially, while the adsorption capacity of uranium per unit volume in modules with 3 and 4 tandem membrane fibers is basically the same. Moreover, the filtration pressure increases significantly with the increase of the number of membrane fibers in the tandem membrane module. Therefore, modules with 3 tandem membrane fibers have the best adsorption effect.

[0034] 3. The membrane fiber module in the desorption and regeneration zone consists of multiple membrane fiber modules connected in series. The uranium content in the acid water increases sequentially along the acid water flow direction, and the uranium concentration in the acid water flowing out of the acid water outlet is the highest. By rotating, the amount of uranium remaining on the membrane fiber after desorption is sequentially reduced in a clockwise direction (rotation direction).

[0035] The "countercurrent concentration gradient desorption" strategy can significantly improve acid washing efficiency. As the concentration of uranium in the acid water gradually increases along the flow direction, the desorption capacity of the acid water gradually decreases. Conversely, along the reverse flow direction, the uranium residue in the membrane fiber assembly decreases sequentially, making desorption increasingly difficult. This design fully utilizes the concentration gradient principle, allowing the high-concentration acid water with strong elution capacity to preferentially treat membrane fibers with low uranium residue and difficult desorption, thus improving membrane fiber regeneration. Simultaneously, the high-concentration uranium acid water treats membrane fibers with high uranium residue, further increasing the uranium concentration in the acid water, enhancing its usability, and reducing production costs.

[0036] Beneficial effects:

[0037] 1. By utilizing the "multi-stage series progressive saturation + dynamic forward switching" mechanism, the overall breakdown time of the hollow fiber membrane system is effectively extended, overcoming the "bucket effect" limitation and significantly improving adsorption efficiency and resource utilization.

[0038] 2. By adopting the "countercurrent concentration gradient desorption" strategy, the efficient utilization of acid water and uranium enrichment are integrated, effectively resolving the contradiction between regeneration and recycling.

[0039] 3. A framework of "multi-module array + cyclic rotation switching" was successfully constructed, realizing the spatiotemporal parallelism of adsorption and regeneration, eliminating replacement interruptions, and solving the technical bottleneck of continuous co-production. Attached Figure Description

[0040] Figure 1 : Longitudinal cross-sectional view of the device described in Example 2.

[0041] Figure 2 : A cross-sectional view of the upper part of the top cover (1) of the device described in Example 2 along the AB tangent.

[0042] Figure 3 Example 2: Sectional diagram of the upper part of the device top cover (1) along the AB tangent.

[0043] Figure 4: Cross-sectional view of the lower part of the top cover (1) of the device described in Example 2 along the CD tangent.

[0044] Figure 5 : Cross-sectional view of the chassis (2) of the device described in Example 2 along the EF tangent.

[0045] Figure 6 : Cross-sectional view of the device described in Example 2 along the GH tangent.

[0046] Figure 7 Breakdown curves of 1-4 tandem membrane fiber modules.

[0047] Figure 8 : Uranium adsorption capacity per unit volume of 1-4 tandem membrane fiber modules. Detailed Implementation

[0048] The present invention will now be described in detail with reference to specific embodiments. These embodiments will help those skilled in the art to further understand the present invention, but do not limit the invention in any way. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention. These all fall within the scope of protection of the present invention.

[0049] Example 1

[0050] A seawater desalination-uranium extraction co-production unit consists of three parts: a top cover (1), a chassis (2), and a membrane fiber assembly (3). It is divided into an adsorption zone, a buffer zone, and a desorption regeneration zone. The corresponding inlet, groove, pipeline, membrane fiber assembly (3), and outlet of each zone constitute a seawater circuit, an acid water circuit, and a clean water circuit, respectively. By rotating the chassis (2), different membrane fiber assemblies (3) can be connected to the adsorption zone, the buffer zone, and the desorption regeneration zone.

[0051] The top cover (1) is equipped with a seawater inlet (1-1), a seawater outlet (1-2), an acid water inlet (1-3), an acid water outlet (1-4), a clean water inlet (1-5), and a clean water outlet (1-6); the top cover (1) is also equipped with a groove (1-7);

[0052] The chassis (2) is provided with two concentric parallel pipes, which are connected to the inlet and outlet of each membrane fiber assembly (3), and there are a total of 6-12 membrane fiber assemblies (3); the chassis (2) and the 6-12 membrane fiber assemblies (3) are connected by a connecting pipe; the buffer zone contains 1 membrane fiber assembly (3); the adsorption zone contains 3-5 membrane fiber assemblies (3); the desorption and regeneration zone contains 2-6 membrane fiber assemblies (3), of which 1 is a clean water washing membrane fiber assembly (3);

[0053] The top cover (1) and the chassis (2) are connected by a central fixed shaft (1-8). The bottom of the top cover (1) and the top of the chassis (2) are sealed and can rotate around the fixed shaft (1-8).

[0054] A uranium extraction and regeneration process for a seawater desalination-uranium extraction co-production unit includes the following components:

[0055] Adsorption process: Seawater enters from the seawater inlet (1-1) of the adsorption zone of the top cover (1), flows through the matching of the connecting groove of the top cover (1) and the orifice of the chassis (2), and flows through 3-5 membrane fiber modules (3) connected in series, with a flux of 20-70 L / (m²). 2 ·h), the area of ​​each membrane fiber module (3) is 5-80m² 2 Each membrane fiber module (3) has a height of 0.5-2m and an adsorption time of 1-30 days;

[0056] Desorption and regeneration: Acidic water with pH=1-5 flows through 1-5 membrane fiber modules (3) connected in series, with a volume of 3-50L and a desorption time of 1-3 days. The volume of clean water is 3-50L, and the cleaning time is 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The volume of acidic water is 3-50L and the volume of clean water is 3-50L, which are the volumes entering the acidic water inlet (1-3) and the clean water inlet (1-5).

[0057] Rotation switching: After adsorption is completed, rotate the base (2) clockwise by an angle of 360° divided by the number of holes on the inner side of the center of the base (2); the membrane fiber assembly (3) is switched in sequence.

[0058] Example 2

[0059] This embodiment is basically the same as Embodiment 1, except that:

[0060] The chassis (2) is provided with two concentric parallel pipes, which are connected to the inlet and outlet of each membrane fiber assembly (3) respectively, and a total of 8 membrane fiber assemblies (3) are distributed. The chassis (2) and the 8 membrane fiber assemblies (3) are connected by a connecting pipe. The buffer zone contains 1 membrane fiber assembly (3), the adsorption zone contains 3 membrane fiber assemblies (3), and the desorption and regeneration zone contains 4 membrane fiber assemblies (3).

[0061] Technical specifications: as attached Figure 7 As shown, based on previous studies, the unit adsorption efficiency of more than three membrane filaments connected in series was not significantly improved, but a greater mass transfer driving force was required.

[0062] Example 3

[0063] This embodiment is basically the same as embodiment 2, except that:

[0064] An extraction and regeneration process based on seawater uranium extraction components includes the following parts:

[0065] Adsorption process: Seawater enters from the seawater inlet (1-1) of the adsorption zone of the top cover (1), flows through the matching of the connecting groove of the top cover (1) and the orifice of the chassis (2), and flows through the three membrane fiber modules (3) connected in series, with a flux of 20 L / (m²). 2 ·h), each membrane fiber module (3) has an area of ​​5m². 2 Each membrane fiber assembly (3) has a height of 0.5m and an adsorption time of 1-30 days.

[0066] Technical Description: The low height of the membrane fiber module facilitates timely replacement after adsorption saturation; the low flux facilitates the membrane fiber module reaching uranium adsorption saturation.

[0067] Example 4

[0068] This embodiment is basically the same as embodiment 3, except that:

[0069] Desorption and regeneration: Acidic water with pH=1 flows through three membrane fiber modules (3) connected in series, with a volume of 3L and a desorption time of 1-3 days. The volume of clean water is 3L, with a cleaning time of 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The 3L volume of acidic water and the 3L volume of clean water are the volumes entering the acidic water inlet (1-3) and the clean water inlet (1-5).

[0070] Technical Note: The small volume of acidic water helps to increase the value of acid recovery.

[0071] Example 5

[0072] This embodiment is basically the same as Embodiment 1, except that:

[0073] The chassis (2) is provided with two concentric parallel pipes, which are connected to the inlet and outlet of each membrane fiber assembly (3), and there are a total of 10 membrane fiber assemblies (3). The chassis (2) and the 10 membrane fiber assemblies (3) are connected by a connecting pipe. The buffer zone contains 1 membrane fiber assembly (3), the adsorption zone contains 3 membrane fiber assemblies (3), and the desorption and regeneration zone contains 6 membrane fiber assemblies (3).

[0074] Technical Note: Multiple tandem desorption methods are beneficial for increasing the concentration of uranium in acidic water and thus increasing the value of uranium recovery.

[0075] Example 6

[0076] This embodiment is basically the same as embodiment 5, except that:

[0077] Adsorption process: Seawater enters from the seawater inlet (1-1) of the adsorption zone of the top cover (1), flows through the matching of the connecting groove of the top cover (1) and the orifice of the chassis (2), and flows through the three membrane fiber modules (3) connected in series, with a flux of 21-40 L / (m²).2 ·h), each membrane fiber module (3) has an area of ​​5m². 2 Each membrane fiber assembly (3) is 1m high and has an adsorption time of 1-30 days.

[0078] Technical Note: Increasing the aspect ratio of the membrane fibers and accelerating the flow rate are beneficial to improving adsorption efficiency.

[0079] Example 7

[0080] This embodiment is basically the same as embodiment 6, except that:

[0081] Desorption and regeneration: Acidic water with pH=3 flows through 5 membrane fiber modules (3) connected in series, with a volume of 3-50L and a desorption time of 1-3 days. The volume of clean water is 3-50L, and the cleaning time is 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The volume of acidic water (3-50L) and clean water (3-50L) are the volumes entering the acidic water inlet (1-3) and the clean water inlet (1-5).

[0082] Technical Description: A high pH level helps reduce the aging effects of high-concentration acid on the membrane fiber assembly, and the uranium desorption effect is improved by connecting multiple membrane fiber assemblies in series.

[0083] Example 8

[0084] This embodiment is basically the same as embodiment 7, except that:

[0085] Desorption and regeneration: Acidic water with pH=3 flows through 5 membrane fiber modules (3) connected in series, with a volume of 3L and a desorption time of 1-3 days. The volume of clean water is 10L, with a cleaning time of 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The volume of acidic water is 3L and the volume of clean water is 10L, which are the volumes entering the acidic water inlet (1-3) and the clean water inlet (1-5).

[0086] Technical Description: This method reduces acid water consumption and increases the uranium concentration in the acid solution by connecting multiple membrane fiber modules in series, thereby enhancing its usability. A 10L volume of clean water connected in series with multiple modules also improves regeneration efficiency.

Claims

1. A uranium extraction and regeneration process for a seawater desalination-uranium extraction co-production unit, comprising the following steps: Adsorption process: Seawater enters from the seawater inlet (1-1) of the adsorption zone of the top cover (1), and flows through 3-5 membrane fiber modules (3) connected in series, matching the top cover (1) connecting groove and the bottom plate (2) orifice. The uranium adsorption capacity of the membrane fiber module (3) decreases sequentially along the direction of the coastal water flow. The flux of the membrane fiber module (3) is 20-70 L / (m³). 2 ·h), the area of ​​each membrane fiber module (3) is 5-80m² 2 Each membrane fiber module (3) has a height of 0.5-2m and an adsorption time of 1-30 days. By rotating, the membrane fiber module (3) with the uranium adsorption amount that is closest to saturation first enters the buffer zone. After the membrane fiber module (3) in the regeneration and desorption zone enters the adsorption zone, the uranium adsorption amount of the membrane fiber module (3) still decreases sequentially along the coastal water direction. Desorption and regeneration: Acidic water with pH=1-5 flows through 1-5 membrane fiber modules (3) connected in series, with a volume of 3-50L and a desorption time of 1-3 days. The uranium content in the acidic water increases sequentially along the flow direction of the acidic water. The concentration of uranium in the acidic water flowing out of the acidic water outlet (1-4) is the highest. By rotating, the amount of uranium remaining on the membrane fiber after desorption of the membrane fiber module (3) decreases sequentially in a clockwise direction. The volume of clean water is 3-50L, and the cleaning time is 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The volume of acidic water is 3-50L and the volume of clean water is 3-50L, which are the volumes entering through the acidic water inlet (1-3) and the clean water inlet (1-5). Rotation switching: After adsorption is completed, rotate the chassis (2) clockwise by an angle of 360° divided by the number of holes on the inner side of the center of the chassis (2); the membrane fiber assembly (3) after being cleaned with water in the desorption regeneration zone enters the adsorption zone; the membrane fiber assembly (3) connected to the seawater inlet (1-1) rotates to the buffer zone; the membrane fiber assembly (3) in the buffer zone enters the desorption regeneration zone and is connected to the acid water outlet (1-4); rotate in sequence in the above manner.

2. The uranium extraction and regeneration process of a seawater desalination-uranium extraction co-production unit as described in claim 1, characterized in that: Adsorption process: Seawater enters from the seawater inlet (1-1) of the adsorption zone of the top cover (1), flows through the matching of the connecting groove of the top cover (1) and the orifice of the chassis (2), and flows through the three membrane fiber modules (3) connected in series, with a flux of 20 L / (m²). 2 ·h), each membrane fiber module (3) has an area of ​​5m². 2 Each membrane fiber assembly (3) has a height of 0.5m and an adsorption time of 1-30 days.

3. The uranium extraction and regeneration process of a seawater desalination-uranium extraction co-production unit as described in claim 2, characterized in that: Desorption and regeneration: Acidic water with pH=1 flows through three membrane fiber modules (3) connected in series, with a volume of 3L and a desorption time of 1-3 days. The volume of clean water is 3L, with a cleaning time of 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The 3L volume of acidic water and the 3L volume of clean water are the volumes entering the acidic water inlet (1-3) and the clean water inlet (1-5).

4. The uranium extraction and regeneration process of a seawater desalination-uranium extraction co-production unit as described in claim 1, characterized in that: Adsorption process: Seawater enters from the seawater inlet (1-1) of the adsorption zone of the top cover (1), flows through the matching of the connecting groove of the top cover (1) and the orifice of the chassis (2), and flows through the three membrane fiber modules (3) connected in series, with a flux of 21-40 L / (m²). 2 ·h), each membrane fiber module (3) has an area of ​​5m². 2 Each membrane fiber assembly (3) is 1m high and has an adsorption time of 1-30 days.

5. The uranium extraction and regeneration process of a seawater desalination-uranium extraction co-production unit as described in claim 4, characterized in that: Desorption and regeneration: Acidic water with pH=3 flows through 5 membrane fiber modules (3) connected in series, with a volume of 3-50L and a desorption time of 1-3 days. The volume of clean water is 3-50L, and the cleaning time is 1-3 days. The pH of the clean water after cleaning is adjusted to the pH required for the acidic water and used as acidic water. The volume of acidic water (3-50L) and clean water (3-50L) are the volumes entering the acidic water inlet (1-3) and the clean water inlet (1-5).

6. The apparatus corresponding to the uranium extraction and regeneration process of the seawater desalination-uranium extraction co-production unit as described in claim 1, characterized in that: A seawater desalination-uranium extraction co-production unit consists of three parts: a top cover (1), a chassis (2), and a membrane fiber assembly (3). It is divided into an adsorption zone, a buffer zone, and a desorption / regeneration zone. The corresponding inlets, grooves, pipelines, membrane fiber assemblies (3), and outlets of each zone constitute a seawater circuit, an acid water circuit, and a clean water circuit, respectively. Different membrane fiber assemblies (3) can be connected to the adsorption zone, buffer zone, and desorption / regeneration zone by rotating the chassis (2). The top cover (1) is equipped with a seawater inlet (1-1), a seawater outlet (1-2), an acid water inlet (1-3), an acid water outlet (1-4), a clean water inlet (1-5), and a clean water outlet (1-6). The top cover (1) is equipped with a seawater inlet (1-1), a seawater outlet (1-2), a acid water inlet (1-3), an acid water outlet (1-4), a clean water inlet (1-5), and a clean water outlet (1-6). The base (2) has two concentric parallel pipes that connect to the inlet and outlet of each membrane fiber assembly (3), and there are a total of 6-12 membrane fiber assemblies (3). The base (2) and the 6-12 membrane fiber assemblies (3) are connected by a connecting pipe. The buffer zone contains 1 membrane fiber assembly (3). The adsorption zone contains 3-5 membrane fiber assemblies (3). The desorption and regeneration zone contains 2-6 membrane fiber assemblies (3), of which 1 is a clean water washing membrane fiber assembly (3). The top cover (1) and the base (2) are connected by a central fixed shaft (1-8). The contact surface between the bottom of the top cover (1) and the top of the base (2) is sealed and can rotate around the fixed shaft (1-8).

7. The seawater desalination-uranium extraction co-production assembly device as described in claim 6, characterized in that: The chassis (2) is provided with two concentric parallel pipes, which are connected to the inlet and outlet of each membrane fiber assembly (3), and there are a total of 8 membrane fiber assemblies (3). The chassis (2) and the 8 membrane fiber assemblies (3) are connected by a connecting pipe. The buffer zone contains 1 membrane fiber assembly (3), the adsorption zone contains 3 membrane fiber assemblies (3), and the desorption and regeneration zone contains 4 membrane fiber assemblies (3).

8. The seawater desalination-uranium extraction co-production assembly device as described in claim 6, characterized in that: The chassis (2) is provided with two concentric parallel pipes, which are connected to the inlet and outlet of each membrane fiber assembly (3), and there are a total of 10 membrane fiber assemblies (3). The chassis (2) and the 10 membrane fiber assemblies (3) are connected by a connecting pipe. The buffer zone contains 1 membrane fiber assembly (3), the adsorption zone contains 3 membrane fiber assemblies (3), and the desorption and regeneration zone contains 6 membrane fiber assemblies (3).

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