Ion exchange resin electroregeneration apparatus and method

Abstract

This invention provides an electro-regeneration device and method for ion exchange resins. The electro-regeneration device and method of this invention utilize in-situ generation of H+ via an anodic or cathodic reaction. + or OH ‑ Using H + or OH ‑ This method promotes the desorption of cations or anions adsorbed on the resin and drives the directional migration of desorbed ions through an electric field, enabling simultaneous resin regeneration and ion enrichment. This reduces the amount of strong acid, strong alkali, or high-salt regenerant required. Simultaneously, during the electrochemical regeneration process, a pH sensor detects the pH values ​​of the anolyte and catholyte, and a conductivity detector detects the conductivity of the anolyte and catholyte. Based on the detected pH and conductivity, the power supply output voltage, the distance between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode are adjusted to regulate the electroregeneration process of the ion exchange resin. This method enables the simultaneous completion of resin regeneration and multi-component ion fractionation and recovery.

Description

Technical Field

[0001] This invention relates to the field of ion exchange resin regeneration technology, and in particular to an ion exchange resin electro-regeneration device and method. Background Technology

[0002] Ion exchange resins are widely used in industrial water treatment, salt removal, heavy metal capture, organic acid salt recovery, rare earth element enrichment, amine purification, and high-salt wastewater treatment. Their basic principle is to utilize the charged functional groups immobilized on the resin to exchange ions with target ions in the solution, thereby achieving the adsorption, enrichment, or purification of the target ions.

[0003] However, ion exchange resins gradually reach saturation after a period of operation, requiring regeneration to restore their exchange capacity. Traditional regeneration methods typically use acid, alkali, or salt solutions as regenerants to completely displace the ions adsorbed on the resin. While this method can restore resin capacity, it has the following problems:

[0004] First, the consumption of regenerants is large, and the subsequent neutralization or treatment costs are high.

[0005] Second, different ions are usually eluted simultaneously into the same regeneration solution, forming a complex mixed waste liquid.

[0006] Third, the regeneration process mainly focuses on the restoration of resin capacity, but it is difficult to achieve selective separation of target ions and resource recovery.

[0007] Fourth, traditional regeneration processes lack real-time control over the acid-base environment, ion release state, and migration process inside the resin bed, making it difficult to perform phased control based on ion desorption behavior.

[0008] Given the shortcomings of current ion exchange resin regeneration methods, it is necessary to improve them. Summary of the Invention

[0009] The purpose of this invention is to overcome the problems of high regenerant consumption, difficulty in resource utilization of mixed regenerant, and uncontrollable ion release process in the existing ion exchange resin regeneration process, and to provide an ion exchange resin electro-regeneration device and method.

[0010] The present invention adopts the following technical solution:

[0011] In a first aspect, the present invention provides an ion exchange resin electroregeneration device, comprising:

[0012] A resin regeneration electrolytic cell is provided inside, which is equipped with an ion exchange membrane that divides the electrolytic cell into an anode chamber and a cathode chamber. An anode is provided in the anode chamber and a cathode is provided in the cathode chamber. A fixed resin bed is provided in the cathode chamber or the anode chamber to accommodate the ion exchange resin to be treated, wherein the ion exchange resin to be treated is an ion exchange resin loaded with target ions.

[0013] A power source, which is used to electrically connect the anode and cathode;

[0014] pH sensors are respectively installed on the anode chamber and the cathode chamber;

[0015] A conductivity detector is respectively installed on the anode chamber and the cathode chamber;

[0016] An electrode drive unit is used to adjust the spacing between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode.

[0017] Secondly, the present invention also provides a method for electro-regeneration of ion exchange resin, applied to the aforementioned ion exchange resin electro-regeneration device, comprising the following steps:

[0018] Place the ion exchange resin to be treated in the cathode chamber or anode chamber;

[0019] Add the anolyte to the anode chamber and the catholyte to the cathode chamber. Connect the cathode to the negative terminal of the power supply and the anode to the positive terminal of the power supply to perform electrochemical regeneration of the ion exchange resin.

[0020] In the electrochemical regeneration process, a pH sensor detects the pH value of the anolyte and the catholyte, and a conductivity detector detects the conductivity of the anolyte and the catholyte. Based on the detected pH value and conductivity, the power supply output voltage, the distance between the anode and the cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode are adjusted.

[0021] The ion exchange resin electroregeneration device and method of the present invention have the following advantages over the prior art:

[0022] 1. The ion exchange resin electroregeneration device and method of the present invention utilizes in-situ generation of H+ via anodic or cathode reactions. + or OH - Using H + or OH -This method promotes the desorption of cations or anions adsorbed on the resin and drives the directional migration of desorbed ions through an electric field, enabling simultaneous resin regeneration and ion enrichment. This reduces the amount of external strong acid, strong alkali, or high-salt regenerants required. Simultaneously, during the electrochemical regeneration process, a pH sensor detects the pH values ​​of the anolyte and catholyte, and a conductivity detector detects the conductivity of the anolyte and catholyte. Based on the detected pH and conductivity, the power supply output voltage, the distance between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode are adjusted to regulate the electroregeneration process of the ion exchange resin.

[0023] 2. The ion exchange resin electroregeneration device and method of the present invention includes three stages of electrochemical regeneration: a first stage, a second stage, and a third stage. During the first stage of electrochemical regeneration, the power supply output voltage is 3-10 V, and the distance between the anode and cathode is 40-100 mm, used to promote the preferential release of weakly bound ions. During the second stage of electrochemical regeneration, the power supply output voltage is 8-18 V, and the distance between the anode and cathode is 20-60 mm, used to promote the release of ions with moderate binding strength. During the third stage of electrochemical regeneration, the power supply output voltage is 12-30 V, and the distance between the anode and cathode is 5-40 mm, used to promote further desorption and migration of strongly bound ions. The present invention transforms the traditional overall elution process into a stepwise desorption and graded recovery process, which can reduce the generation of mixed regeneration waste liquid. The present invention is applicable to various resins and various ion systems, and is not limited to specific resins, specific ions, or specific wastewater sources, exhibiting good engineering adaptability.

[0024] 3. Under the condition of no external strong alkali regeneration agent, the total regeneration rate of this invention can reach 86.9%, and three enriched solutions with significantly different compositions can be obtained, wherein the first enriched solution contains Cl - The proportion of CH3COO in the second enrichment solution was 62.5%. - The proportion of HCOO in the third enrichment solution was 50.0%. - The percentage was 48.7%, proving that this method can achieve simultaneous completion of resin regeneration and multi-component ion fractionation and recovery. Attached Figure Description

[0025] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0026] Figure 1 This is a schematic diagram of the structure of an ion exchange resin electroregeneration device in one embodiment of the present invention;

[0027] Figure 2 This is a schematic diagram of the structure of an ion exchange resin electroregeneration device in another embodiment of the present invention;

[0028] Figure 3 This is a schematic diagram of the electrode driving unit of the present invention;

[0029] Figure 4 This is a schematic diagram illustrating how the anode can be moved horizontally left and right to adjust the distance between the anode and cathode.

[0030] Figure 5 A schematic diagram illustrating the rotation of the anode to adjust its angle;

[0031] Figure 6 This is a schematic diagram showing how the anode moves vertically up and down to adjust its height.

[0032] Figure 7 This is a graph showing the changes in pH and conductivity over time during the electroregeneration process in Example 1.

[0033] Figure 8 This is a compositional distribution diagram of the target anions in the three-stage enrichment solution in Example 1;

[0034] Figure 9 This is a comparison chart of the total regeneration rate and the highest single component percentage under different regeneration methods in Example 4. Detailed Implementation

[0035] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0036] Therefore, the following detailed description of the embodiments of the invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the invention without inventive effort are within the scope of protection of the invention.

[0037] It should be noted that similar labels and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0038] In the description of this invention, it should be understood that the orientation or positional relationship indicated by terms such as "above" is based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship in which the product of this invention is usually placed when in use, or the orientation or positional relationship in which those skilled in the art are usually understood. It is only for the convenience of describing this invention and simplifying the description, and is not intended to 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, it should not be construed as a limitation of this invention.

[0039] Furthermore, the terms "first," "second," etc., are used only to distinguish descriptions and should not be interpreted as indicating or implying relative importance.

[0040] The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0041] This application provides an ion exchange resin electroregeneration device, such as... Figures 1-6 As shown, it includes:

[0042] The resin regeneration electrolytic cell 1 is equipped with an ion exchange membrane 2, which divides the electrolytic cell into an anode chamber 11 and a cathode chamber 12. An anode 3 is provided in the anode chamber 11, and a cathode 4 is provided in the cathode chamber 12. A resin fixed bed is provided in the cathode chamber 12 or the anode chamber 11 to accommodate the ion exchange resin 10 to be treated, which is an ion exchange resin loaded with target ions.

[0043] Power supply 5, which is used to electrically connect anode 3 and cathode 4;

[0044] pH sensor 6 is respectively installed on anode chamber 11 and cathode chamber 12;

[0045] A conductivity detector 7 is installed on the anode chamber 11 and the cathode chamber 12, respectively;

[0046] An electrode driving unit is used to adjust the spacing between the anode 3 and the cathode 4, the height of the anode 3 or the cathode 4, and the rotation angle of the anode 3 or the cathode 4.

[0047] The ion exchange resin electroregeneration device of the present invention includes a resin regeneration electrolytic cell 1, an ion exchange membrane 2, an anode 3, a cathode 4, a power supply 5, a pH sensor 6, a conductivity detector 7, and an electrode driving unit; the resin regeneration electrolytic cell 1 is a rectangular box structure with a hollow interior and an open top; the ion exchange membrane 2 is disposed inside the resin regeneration electrolytic cell 1 and divides its internal space into an anode chamber 11 and a cathode chamber 12 on the left and right sides; the anode 3 is disposed in the anode chamber 11, and the cathode 4 is disposed in the cathode chamber 12; a resin fixed bed containing the ion exchange resin 10 to be treated can be disposed in the cathode chamber or the anode chamber; the resin fixed bed can be a porous mesh container, and the ion exchange resin 10 to be treated is placed in the porous mesh container to facilitate contact with the electrolyte; specifically, if When the ion exchange resin 10 is an anion exchange resin (i.e., the target ion it supports is an anion), the ion exchange resin is placed in the cathode chamber; when the ion exchange resin 10 is a cation exchange resin (i.e., the target ion it supports is a cation), the ion exchange resin is placed in the anode chamber; both the anode chamber 11 and the cathode chamber 12 are equipped with pH sensors 6 to detect the pH value of the electrolyte in the anode chamber 11 and the cathode chamber 12 during the regeneration process; both the anode chamber 11 and the cathode chamber 12 are equipped with conductivity detectors 7 to detect the conductivity of the electrolyte in the anode chamber 11 and the cathode chamber 12 during the regeneration process; an electrode driving unit is also included, which is used to adjust the distance between the anode 3 and the cathode 4, the height of the anode 3 or the cathode 4, and the rotation angle of the anode 3 or the cathode 4.

[0048] The working principle of the ion exchange resin electroregeneration device of the present invention is as follows: the ion exchange resin 10 to be treated is placed in the cathode chamber or the anode chamber, the anolyte is added to the anode chamber, the catholyte is added to the cathode chamber, the cathode is connected to the negative terminal of the power supply, and the anode is connected to the positive terminal of the power supply to perform electrochemical regeneration of the ion exchange resin; when the ion exchange resin to be regenerated is anion exchange resin, the ion exchange resin to be treated is placed in the cathode chamber, and OH- generated in the cathode chamber during the electrolytic regeneration process... - This process promotes the desorption of anions adsorbed on the resin. The desorbed anions migrate through the ion exchange membrane to the anode chamber and accumulate under the influence of an electric field. When the resin to be regenerated is a cation exchange resin, it is placed in the anode chamber. During electrolytic regeneration, H₂O generated in the anode chamber... + It is used to promote the desorption of cations adsorbed on the resin. The desorbed cations migrate through the ion exchange membrane to the cathode chamber and are enriched under the action of the electric field.

[0049] Furthermore, by incorporating a pH sensor 6 and a conductivity detector 7, this invention detects the pH value and conductivity of the electrolyte in the anode chamber 11 and cathode chamber 12 during the electro-regeneration process. The pH signal reflects the local acid-base environment of the resin bed and the driving force for ion desorption; the conductivity signal reflects the intensity of ion release and the change in the total ion concentration in the regenerated solution. The power supply output voltage, the distance between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode can be adjusted according to the pH value detected by the pH sensor and the conductivity detector, thereby regulating the electro-regeneration process of the ion exchange resin.

[0050] In some embodiments, the electrode driving unit includes:

[0051] The first motor 8 has a shaft connected to a vertically arranged first lead screw 81, and a first moving block 82 is screwed onto the first lead screw 81.

[0052] The second motor 83 is fixedly connected to the first moving block 82. The rotating shaft of the second motor 83 is connected to a horizontally arranged second lead screw 84, and the second moving block 85 is screwed onto the second lead screw 84.

[0053] The third motor 86 is fixedly connected to the second moving block 85, and the rotating shaft of the third motor 86 is connected to the anode or cathode.

[0054] The first motor 8 rotates, driving the first lead screw 81 to rotate, which in turn drives the first moving block 82 to move up and down in the vertical direction, thereby adjusting the height of the anode or cathode; the second motor 83 rotates, driving the second lead screw 84 to rotate, which in turn drives the second moving block 85 to move back and forth in the horizontal direction, thereby adjusting the distance between the anode and cathode; the third motor 86 rotates, driving the anode or cathode to rotate, thereby adjusting the rotation angle of the anode or cathode.

[0055] It is understandable that the anode and cathode are each connected to an electrode drive unit, which can drive the anode and cathode to move up and down, move horizontally, and rotate, respectively.

[0056] Further, refer to Figure 3 As shown, the first motor 8 is fixed on the base 87, and the resin regeneration electrolytic cell 1 is also mounted on the base 87; Reference Figure 4 As shown, the anode 3 moves horizontally left and right, thereby adjusting the distance between the anode 3 and the cathode 4; Reference Figure 5As shown, the anode 3 rotates to adjust its angle. For example, the anode 3 can be rotated around its own axis by the rotation of the third motor 86. Specifically, the rotation of the anode 3 causes it to form a certain angle with respect to the length direction of the resin regeneration electrolytic cell 1, which can be 0~180°. The third motor 86 can be connected to the anode 3 through a rotating rod. The rotation of the third motor 86 drives the rotating rod to rotate, thereby causing the anode 3 to rotate. (Reference) Figure 6 As shown, it illustrates the vertical movement of anode 3.

[0057] In some embodiments, it also includes:

[0058] The anode electrolyte storage tank 13 stores the anode electrolyte; the resin regeneration electrolytic cell is provided with a first anode electrolyte inlet / outlet hole 14 and a second anode electrolyte inlet / outlet hole 15 respectively on the anode chamber, and the anode electrolyte storage tank 13 is connected to the first anode electrolyte inlet / outlet hole 14 and the second anode electrolyte inlet / outlet hole 15.

[0059] The cathode electrolyte storage tank 16 stores cathode electrolyte; the resin regeneration electrolytic cell is provided with a first cathode electrolyte inlet / outlet hole 17 and a second cathode electrolyte inlet / outlet hole 18 respectively on the cathode chamber, and the cathode electrolyte storage tank 16 is connected to the first cathode electrolyte inlet / outlet hole 17 and the second cathode electrolyte inlet / outlet hole 18.

[0060] In the above embodiments, the anolyte storage tank 13 stores anolyte, which flows into the anode chamber through the second anolyte inlet / outlet hole 15. Simultaneously, the electrolyte in the anode chamber 11 returns to the anolyte storage tank 13 through the first anolyte inlet / outlet hole 14, thus achieving the circulation of anolyte between the anolyte storage tank 13 and the anode chamber 11. Similarly, the cathode electrolyte storage tank 16 stores cathode electrolyte, which flows into the cathode chamber 12 through the second cathode electrolyte inlet / outlet hole 18. Simultaneously, the electrolyte in the cathode chamber 12 returns to the cathode electrolyte storage tank 16 through the first cathode electrolyte inlet / outlet hole 17, thus achieving the circulation of cathode electrolyte between the cathode electrolyte storage tank 16 and the cathode chamber 12. Specifically, the anode electrolyte storage tank 13 and the anode chamber 11, as well as the cathode electrolyte storage tank 16 and the cathode chamber 12, are all connected by pipelines. Valves and metering pumps can be installed on the pipelines to regulate the flow rate. In this invention, metering pumps are installed on other pipelines to regulate the flow rate of the corresponding materials, and valves can also be installed.

[0061] In some embodiments, an enrichment outlet 19 is provided on the anode chamber or cathode chamber;

[0062] The enriched liquid outlet 19 connects to multiple enriched liquid storage tanks.

[0063] Specifically, enrichment outlets can be simultaneously opened on the anode and cathode chambers, and enrichment outlet 19 connects to multiple enrichment storage tanks. When the ion exchange resin to be regenerated is anion exchange resin, the OH- generated in the cathode chamber during the electrolytic regeneration process promotes the desorption of anions adsorbed on the resin. Under the action of the electric field, the desorbed anions migrate and accumulate in the anode chamber through the ion exchange membrane. At this time, the anode chamber is rich in desorbed anions, and the electrolyte rich in anions can be discharged from the enrichment outlet opened on the anode chamber to the enrichment storage tank. Similarly, when the resin to be regenerated is cation exchange resin, the desorbed cations migrate and accumulate in the cathode chamber through the ion exchange membrane under the action of the electric field. At this time, the cathode chamber is rich in desorbed cations, and the electrolyte rich in cations can be discharged from the enrichment outlet opened on the cathode chamber to the enrichment storage tank.

[0064] In some embodiments, the enrichment outlet 19 is connected to a multi-way valve 91 via a pipeline (on which a metering pump 95 and a valve may be installed). The multi-way valve 91 is connected to multiple enrichment storage tanks, such as the first enrichment storage tank 92, the second enrichment storage tank 93, and the third enrichment storage tank 94. Different enrichment storage tanks can collect electrolytes containing different cations or anions.

[0065] In some embodiments, a control unit 9 is also included. The control unit 9 is electrically connected to a pH sensor 6, a conductivity detector 7, a power supply 5, a first motor 8, a second motor 83, a third motor 86, and a multi-way valve 91. The control unit 9 controls the output voltage of the power supply 5 and the rotation of the first motor 8, the second motor 83, and the third motor 86 based on the pH value detected by the pH sensor and the conductivity detected by the conductivity detector, thereby adjusting the distance between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode. The control unit 9 controls the connection of the multi-way valve 91 based on the pH value detected by the pH sensor and the conductivity detected by the conductivity detector, so that the enrichment outlet 19 is connected to different enrichment storage tanks, thereby collecting enrichment at different stages. The control unit 9 coordinates the electrochemical regeneration process of the ion exchange resin 10 to be treated and the graded collection process of the enrichment.

[0066] Based on the same inventive concept, the present invention also provides a method for the electro-regeneration of ion exchange resin, applied to the above-mentioned electro-regeneration device for ion exchange resin, comprising the following steps:

[0067] S1. Place the ion exchange resin to be treated in the cathode chamber or anode chamber;

[0068] S2. Add the anolyte to the anode chamber and the catholyte to the cathode chamber. Connect the cathode to the negative terminal of the power supply and the anode to the positive terminal of the power supply to perform electrochemical regeneration of the ion exchange resin.

[0069] In the electrochemical regeneration process, a pH sensor detects the pH value of the anolyte and the catholyte, and a conductivity detector detects the conductivity of the anolyte and the catholyte. Based on the detected pH value and conductivity, the power supply output voltage, the distance between the anode and the cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode are adjusted.

[0070] The principle of the ion exchange resin electroregeneration method of the present invention is as follows:

[0071] The local acid-base environment can be controlled through anodic or cathodic reactions:

[0072] OH is generated through the water reduction reaction at the cathode. - H+ can be produced through the water oxidation reaction at the anode. + This creates a controllable local pH environment within the resin bed;

[0073] Local pH changes induce stepwise ion desorption.

[0074] Different ions have different binding strengths with the functional groups of the resin, and the acid-base driving forces required for their desorption are also different; therefore, by gradually changing the pH environment, weakly bound ions, moderately bound ions and strongly bound ions can be released in sequence.

[0075] Electric field drives the directional migration of desorbed ions.

[0076] Desorbed ions migrate to the corresponding enrichment side under the action of an electric field; for anions, they can migrate and enrich in the anode chamber after desorption; for cations, they can migrate and enrich in the cathode chamber after desorption; for resin systems containing both anions and cations, ions of different charges can be collected separately through membrane modules on both sides and enrichment liquid pipelines on both sides.

[0077] In some embodiments, the power supply output voltage during electrochemical regeneration is 3~30 V, the electroregeneration time is 5~600 min, the distance between the anode and cathode is 5~100 mm, the anode electrolyte is added to the anode chamber at 1~100 mL / min, the cathode electrolyte is added to the cathode chamber at 1~100 mL / min, the vertical movement range of the anode or cathode is 0~100 mm, and the rotation angle of the anode or cathode is 0~360°.

[0078] In some embodiments, electrochemical regeneration includes the following first stage, second stage, and third stage. In the following three-stage electrochemical regeneration conditions, taking the anion exchange resin placed in the cathode chamber for electroregeneration as an example, the pH value and conductivity are the detection values ​​of the electrolyte in the cathode chamber.

[0079] When the ion exchange resin to be treated is an anion exchange resin and is placed in the cathode chamber, the electrochemical regeneration includes the following first stage, second stage and third stage.

[0080] In the first stage of electrochemical regeneration, the power supply output voltage is 3~10V, and the distance between the anode and cathode is 40~100 mm. During the first stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 7.2~7.3 to 9.5~10.3, and the conductivity increases from 0.31~0.33 mS / cm to 1.55~1.57 mS / cm and then decreases to 1.2~1.24 mS / cm. Then the second stage of electrochemical regeneration is carried out.

[0081] During the second stage of electrochemical regeneration, the power supply output voltage is 8~18 V, and the distance between the anode and cathode is 20~60 mm. During the second stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 9.5~10.3 to 10.8~11.3, and the conductivity increases from 1.2~1.24 mS / cm to 1.95~2.10 mS / cm and then decreases to 1.6~1.62 mS / cm. Then, the third stage of electrochemical regeneration is carried out.

[0082] During the third stage of electrochemical regeneration, the power supply output voltage is 12~30V, and the distance between the anode and cathode is 5~40mm. During the third stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 10.8~11.3 to 11.4~11.9, the conductivity decreases from 1.6~1.62 mS / cm to 1.4~1.42 mS / cm, then increases to 1.65~1.69 mS / cm, and then decreases to 1.05~1.1 mS / cm. At this point, the third stage of electrochemical regeneration is completed.

[0083] Specifically, in the above embodiments, during the first stage of electrochemical regeneration, the power supply output voltage is 3~10V, and the distance between the anode and cathode is 40~100 mm, which is used to promote the preferential release of weakly bound ions; during the second stage of electrochemical regeneration, the power supply output voltage is 8~18V, and the distance between the anode and cathode is 20~60 mm, which is used to promote the release of ions with medium binding strength; during the third stage of electrochemical regeneration, the power supply output voltage is 12~30V, and the distance between the anode and cathode is 5~40 mm, which is used to promote the further desorption and migration of strongly bound ions; in each of the above stages, by controlling the power supply output voltage and the distance between the anode and cathode at different stages, ions with different binding abilities in the resin are released sequentially, such as weakly bound ions, moderately bound ions, and strongly bound ions. The distance between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode can also be further adjusted to change the electrode action area and the local electric field distribution so that different ions are released sequentially.

[0084] In some embodiments, the time for the first stage electrochemical regeneration, the second stage electrochemical regeneration, and the third stage electrochemical regeneration is 5 to 180 min.

[0085] Ion exchange resins include at least one of basic anion exchange resins, acidic cation exchange resins, chelating resins, functionalized adsorption resins, and mixed bed resins.

[0086] The target ions loaded on the ion exchange resin include at least one of the following: halide ions, organic acid ions, nitrate ions, sulfate ions, phosphate ions, carbonate ions, thermally stable salt anions, alkali metal ions, alkaline earth metal ions, heavy metal ions, and rare earth ions.

[0087] The anolyte and catholyte include water and / or saline solution; the saline solution includes at least one of sodium sulfate solution, potassium sulfate solution, sodium nitrate solution, and potassium nitrate solution; the concentration of the saline solution is 0.1~10 mmol / L.

[0088] In some embodiments, the anode is a titanium-based iridium-tantalum oxide coated electrode plate, and the cathode is a platinum-coated titanium mesh electrode plate; in other embodiments, the anode and cathode may also be selected from titanium plates, stainless steel plates, graphite plates, titanium-based noble metal oxide coated electrodes, platinum-coated titanium electrodes, or combinations thereof.

[0089] In some embodiments, the enriched solution generated during the first-stage electrochemical regeneration process is collected through the enriched solution outlet;

[0090] During the second-stage electrochemical regeneration process, the enriched solution generated in the second-stage electrolysis is collected through the enriched solution outlet.

[0091] In the third stage of electrochemical regeneration, the enriched solution generated during the third stage of electrolysis is collected through the enriched solution outlet.

[0092] Specifically, in the above embodiments, the first-stage electrochemical regeneration process is used to promote the preferential release of weakly bound ions from the resin. If the ion is an anion, it can accumulate and migrate towards the anode chamber after desorption. The electrolyte rich in anions during the first-stage electrochemical process (i.e., the enriched solution generated in the first-stage electrolysis mentioned above) can be discharged from the enriched solution outlet opened in the anode chamber to the first enriched solution storage tank. Similarly, the second-stage electrochemical regeneration process is used to promote the release of ions with medium binding strength. If the ion is an anion, it can accumulate and migrate towards the anode chamber after desorption. The electrolyte rich in anions during the first-stage electrochemical process (i.e., the enriched solution produced in the second-stage electrolysis mentioned above) can be discharged from the enriched solution outlet in the upper part of the anode chamber to the second enriched solution storage tank. The third-stage electrochemical regeneration process is used to promote the further desorption of strongly bound ions. If the ion is an anion, it can be enriched and migrated to the anode chamber after desorption. The electrolyte rich in anions during the third-stage electrochemical process (i.e., the enriched solution produced in the third-stage electrolysis mentioned above) can be discharged from the enriched solution outlet in the upper part of the anode chamber to the third enriched solution storage tank.

[0093] The ion exchange resin to be treated in this invention can be an ion exchange resin used in industrial wastewater treatment, amine heat-stabilized salt removal, salt lake brine resource utilization, rare earth wastewater recovery, heavy metal wastewater treatment, electroplating wastewater treatment, fermentation broth organic acid salt recovery, or water treatment processes.

[0094] The ion exchange resin electroregeneration method of the present invention utilizes in-situ generation of H+ via anodic or cathodic reactions. + or OH - Using H + or OH - This process promotes the desorption of adsorbed cations or anions from the resin. The directional migration of desorbed ions is driven by an electric field, allowing resin regeneration and ion enrichment to occur simultaneously, reducing the amount of strong acids, strong bases, or high-salt regenerants required. Furthermore, during electrochemical regeneration, a pH sensor detects the pH values ​​of the anolyte and catholyte, and a conductivity detector detects their conductivity. Based on the detected pH and conductivity, the power supply output voltage, the distance between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode are adjusted to regulate the electroregeneration process of the ion exchange resin. The electrochemical regeneration process includes three stages: Stage 1: 3–10 V with a distance of 40–100 mm between the anode and cathode to promote the preferential release of weakly bound ions; Stage 2: 8–18 V with a distance of 20–60 mm between the anode and cathode to promote the release of ions with moderate binding strength; Stage 3: 12–30 V with a distance of 12–30 mm between the anode and cathode. V, the distance between the anode and cathode is 5~40 mm, which is used to promote further desorption and migration of strongly bound ions; the present invention changes the traditional whole elution process into a stepwise desorption and graded recovery process, which can reduce the generation of mixed regeneration waste liquid; the present invention is applicable to a variety of resins and a variety of ion systems, and is not limited to a specific resin, a specific ion or a specific wastewater source, and has good engineering adaptability.

[0095] The following detailed embodiments further illustrate the electroregeneration method for ion exchange resins according to the present invention. This section further explains the invention in conjunction with specific embodiments, but should not be construed as limiting the invention. Unless otherwise specified, the techniques used in the embodiments are conventional methods well known to those skilled in the art. Unless otherwise specified, the reagents, methods, and equipment used in the present invention are conventional reagents, methods, and equipment in the art.

[0096] In the following embodiments, unless otherwise specified, the anode is a titanium-based iridium-tantalum oxide coated electrode plate, and the cathode is a platinum-coated titanium mesh electrode plate; the dimensions of both the anode and cathode are 100 mm × 50 mm × 1 mm, where 100 mm is the vertical dimension, 50 mm is the width dimension of the resin regeneration electrolytic cell, and 1 mm is the thickness; both the anode electrolyte and the cathode electrolyte are 0.5 mmol / L Na2SO4 aqueous solution; the ion exchange membrane is an anion exchange membrane (specifically, a Fuma-FAA-3-PK-130 anion exchange membrane); the internal length of the resin regeneration electrolytic cell is 120 mm, the width is 60 mm, and the height is 100 mm. The ion exchange membrane is located in the middle of the resin regeneration electrolytic cell and is parallel to the width direction of the electrolytic cell. The ion exchange membrane divides the resin regeneration electrolytic cell into an anode chamber and a cathode chamber with basically the same shape and volume; initially, both the anode and cathode are parallel to the width direction of the resin regeneration electrolytic cell (i.e., the anode and cathode are perpendicular to the length direction of the electrolytic cell), and the initial distance from the lower end of the anode and cathode to the bottom of the resin regeneration electrolytic cell is 20 mm. mm; For cation exchange resin systems, anion exchange membranes can be replaced with cation exchange membranes, or anion exchange membranes and cation exchange membranes can be set separately in a double-sided enrichment structure.

[0097] Example 1

[0098] This embodiment provides a method for the electro-regeneration of ion exchange resins, applied to... Figure 1 The ion exchange resin electroregeneration device shown includes the following steps:

[0099] S1. Place the ion exchange resin to be treated in the cathode chamber;

[0100] S2. Add the anolyte to the anode chamber and the catholyte to the cathode chamber. Connect the cathode to the negative terminal of the power supply and the anode to the positive terminal of the power supply to perform electrochemical regeneration of the ion exchange resin.

[0101] In the electrochemical regeneration process, a pH sensor detects the pH value of the electrolyte in the cathode chamber, a conductivity detector detects the conductivity of the electrolyte in the cathode, and adjusts the power supply output voltage and the distance between the anode and cathode according to the detected pH value and conductivity.

[0102] The strongly basic anion exchange resin used is DuPont. TM AmberLite TM IRA900 Cl ion exchange resin was used as the resin to be regenerated. Specifically, 3.0 g of dry DuPont resin was used. TM AmberLite TM IRA900 Cl ion exchange resin was added to 200 mL of solution containing HCOO. - CH3COO- Cl - (HCOO) - CH3COO - Cl - In a mixed solution (specifically provided by its corresponding Na salt), the initial concentration of each of the three anions was 100 mg / L, and adsorption was carried out with shaking at an adsorption temperature of 25 °C for 12 h; after adsorption, the concentration of HCOO was measured. - CH3COO - Cl - The adsorption rates were 78.4%, 68.2%, and 37.5%, respectively, corresponding to resin loadings of 5.23 mg / g dry basis resin, 4.55 mg / g dry basis resin, and 2.50 mg / g dry basis resin, as shown in Table 1. These results indicate that the binding capacity of the three anions on the strongly basic anion exchange resin differs significantly, with the binding strength in the order of HCOO... - CH3COO - > Cl - This provides a foundation for subsequent phased electroregeneration and graded recycling; the DuPont products adsorbed above TM AmberLite TM IRA900 Cl ion exchange resin is used as the ion exchange resin to be treated, and the ion exchange resin to be treated is placed in a porous mesh container, which is placed in the cathode chamber.

[0103] Electrochemical regeneration includes the following three stages: Stage 1, Stage 2, and Stage 3.

[0104] In the first stage of electrochemical regeneration, the power supply output voltage is 8 V, and the distance between the anode and cathode is 60 mm. During the first stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 7.25 to 10.22; the conductivity increases from 0.32 mS / cm to 1.55 mS / cm and then decreases to 1.22 mS / cm, at which point the second stage of electrochemical regeneration is carried out; the first stage of electrochemical regeneration takes 40 min.

[0105] During the second stage of electrochemical regeneration, the power supply output voltage is 12V, and the distance between the anode and cathode is 45 mm. During the second stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 10.22 to 11.28, and the conductivity increases from 1.22 mS / cm to 2.10 mS / cm and then decreases to 1.62 mS / cm. Then, the third stage of electrochemical regeneration is carried out. The second stage of electrochemical regeneration takes 50 min.

[0106] During the third stage of electrochemical regeneration, the power supply output voltage was 16 V, and the distance between the anode and cathode was 30 mm. During the third stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increased from 11.28 to 11.88, the conductivity decreased from 1.62 mS / cm to 1.40 mS / cm, then increased to 1.68 mS / cm, and then decreased to 1.1 mS / cm. At this point, the third stage of electrochemical regeneration was completed. The third stage of electrochemical regeneration took 70 min.

[0107] In this embodiment, adjusting the distance between the anode and cathode is used as the main electric field control method. In the first, second and third stages, the distance between the lower end of the anode and cathode and the bottom of the resin regeneration electrolytic cell is kept at 20 mm, and the angle between the anode and cathode and the length direction of the resin regeneration electrolytic cell is kept at 90°.

[0108] During the electrochemical regeneration process, the anolyte and catholyte circulate between the anolyte storage tank, the catholyte storage tank, and the resin regeneration electrolytic cell, respectively, with a circulation flow rate of 20 mL / min. When the enriched liquid is discharged, it enters the multi-way valve through the enriched liquid outlet and enters the first enriched liquid storage tank, the second enriched liquid storage tank, and the third enriched liquid storage tank according to the regeneration stage.

[0109] After the first stage of electrochemical regeneration, the first stage of electrochemical process is rich in anions (Cl). - The electrolyte of the anode chamber can be discharged from the enrichment outlet and the first enrichment can be collected.

[0110] After the second stage of electrochemical regeneration is completed, the second stage of electrochemical process is rich in anions (CH3COO). - The electrolyte of the anode chamber can be discharged from the enrichment outlet and the second enrichment can be collected.

[0111] After the third stage of electrochemical regeneration is completed, the third stage of electrochemical process is rich in anions (HCOO). - The electrolyte can be discharged from the enrichment outlet opened in the anode chamber and the third enrichment can be collected.

[0112] Table 1 below shows the dry-based DuPont products. TM AmberLite TM IRA900 Cl ion exchange resin adsorbs HCOO - CH3COO - and Cl - The data.

[0113] Table 1 - Adsorption of HCOO by ion exchange resins - CH3COO - Cl- Data

[0114]

[0115] In the above embodiments, the first-stage electrochemical regeneration process promotes the preferential release of weakly bound ions from the resin. If the ion is an anion, it can accumulate and migrate towards the anode chamber after desorption. The electrolyte rich in anions during the first-stage electrochemical process (i.e., the enriched solution generated in the first-stage electrolysis mentioned above) can be discharged from the enriched solution outlet opened in the anode chamber to the first enriched solution storage tank. Similarly, the second-stage electrochemical regeneration process promotes the release of ions with moderate binding strength. If the ion is an anion, it can accumulate and migrate towards the anode chamber after desorption. The electrolyte rich in anions during the electrochemical process (i.e., the enriched solution produced in the second stage of electrolysis mentioned above) can be discharged from the enriched solution outlet in the upper part of the anode chamber to the second enriched solution storage tank. The third stage of electrochemical regeneration process is used to promote the further desorption of strongly bound ions. If the ion is an anion, it can be enriched and migrated to the anode chamber after desorption. The electrolyte rich in anions during the third stage of electrochemical process (i.e., the enriched solution produced in the third stage of electrolysis mentioned above) can be discharged from the enriched solution outlet in the upper part of the anode chamber to the third enriched solution storage tank.

[0116] Table 2 below and Figure 8 To determine the concentration and composition of the target anion in the three-stage enrichment solution according to the method described in Example 1 above.

[0117] Table 2 - Concentration and composition of target anions in the three-stage enrichment solution

[0118]

[0119] In Example 1, pH can be used to reflect the OH produced by the electrode reaction. - Driving force and conductivity can be used to reflect the intensity of ion release and migration. By synergistically determining pH and conductivity, automatic switching between the regeneration stage and the collection channel can be achieved.

[0120] To further illustrate the pH-based desorption mechanism, the HCOO adsorbed in Example 1 was taken... - CH3COO - and Cl - 1.5 g of the anion exchange resin was added to 100 mL of NaOH aqueous solution with different mass fractions (0%, 0.02%, 0.05%, 0.10%, and 0.20%) for static desorption experiments. The desorption experiments were conducted at 25 °C with a shaking speed of 150 rpm for 60 min. After desorption, the supernatant or filtrate was collected, and HCOO was determined by ion chromatography. - CH3COO - and Cl- The concentration was determined, and the desorption rate of each target ion was calculated according to the formula: "Desorption rate = Amount of target ion in desorption solution / Amount of target ion initially loaded on resin × 100%". The results are shown in Table 3. With increasing NaOH concentration, the desorption rates of all three anions increased, but the degree of response varied among different anions. Specifically, Cl... - It can be rapidly desorbed at low alkalinity, CH3COO - Desorption is significantly enhanced at moderate alkalinity, while HCOO - Higher alkalinity is required for complete desorption. This result indicates that different anions have different alkalinity-triggered desorption windows, which can provide a basis for subsequent staged electroregeneration.

[0121] Table 3 - Static desorption rates of loaded anions at different NaOH concentrations

[0122]

[0123] Table 4 shows the operating parameters for the first, second, and third stages of Example 1. The apparent electric field strength in Table 4 is calculated according to E=U / d, where E is the apparent electric field strength in V / cm; U is the power supply output voltage in V; and d is the distance between the anode and cathode in cm. For example, in the first stage, the power supply output voltage is 8 V, and the distance between the anode and cathode is 60 mm (6 cm), so the apparent electric field strength is 8 / 6=1.33V / cm; in the second stage, it is 12 / 4.5=2.67V / cm; and in the third stage, it is 16 / 3=5.33V / cm. It should be noted that the apparent electric field strength in Table 4 is a nominal electric field strength defined for the convenience of characterizing the operating conditions of different stages, and is calculated according to the electrode spacing when the anode and cathode are in a parallel state. The height adjustment and rotation angle adjustment of the anode or cathode are mainly used to change the local electric field distribution, the electrode action area, and the ion migration path, and do not participate in the numerical calculation of the apparent electric field strength E.

[0124] Table 4 - Operating Parameters of Three-Stage Feedback Electroregeneration

[0125]

[0126] Table 5 and Figure 7 The changes in pH and conductivity of the electrolyte in the cathode chamber over time during the first, second, and third stages of operation in Example 1.

[0127] Table 5 - Changes in pH and conductivity of the electrolyte in the cathode chamber over time during electroregeneration.

[0128]

[0129] Example 2

[0130] As a further extension of the electrode spacing adjustment in Embodiment 1, in this embodiment, the anode and / or cathode are connected to an electrode driving unit, which can drive the anode and cathode to move up and down, move horizontally, and rotate, respectively.

[0131] In the first regeneration stage, the electrode spacing is relatively large, the electrode insertion depth is relatively shallow, and the electric field effect is relatively mild, which is used to promote the preferential release of weakly bound ions. In the second regeneration stage, the electrode spacing is reduced or the electrode insertion depth is increased to enhance the local electric field and acid-base driving force of the resin bed. In the third regeneration stage, the electrode spacing, height or rotation angle is further adjusted so that the electric field effect area covers a larger area of ​​the resin bed, thereby promoting the desorption and migration of strongly bound ions.

[0132] This method, through the adjustment of mechanical configuration and electrochemical parameters, can enhance the local electric field, improve regeneration efficiency, and reduce energy consumption without significantly increasing the applied voltage.

[0133] Example 3

[0134] Electroregeneration of cation exchange resins and fractional recovery of metal ions

[0135] This embodiment uses a cation exchange resin to adsorb a solution containing multiple metal ions. After loading, the resin is placed in a resin regeneration unit. H₂ is generated through an anodic water oxidation reaction. + H + It competes with the metal cations on the resin for exchange, causing the metal ions to desorb.

[0136] The desorbed metal ions migrate towards the cathode enrichment side under the influence of an electric field. Based on the differences in the binding strength, migration rate, and complexation state of different metal ions with the resin functional groups, different metal ion enrichment solutions can be obtained by adjusting pH, voltage, current, and collection time.

[0137] This embodiment illustrates that the present invention is applicable not only to anion exchange resins, but also to cation exchange resins and the resource recovery of metal ions.

[0138] In this embodiment, the device structure can be compared with... Figure 1 The structure shown is the same, except that the enrichment solution collection side needs to be changed from the anode chamber to the cathode chamber; the ion exchange membrane can be a cation exchange membrane. Therefore, Figure 1 The illustrated anode enrichment and collection structure is merely an example of anion exchange resin systems and does not limit the application of this invention in cation exchange resins or bilaterally symmetrical enrichment structures. In other embodiments, enrichment liquid outlets, multi-way valves, and multiple enrichment liquid storage tanks may be provided on the anode and cathode chambers respectively, allowing anions and cations to migrate to the anode and cathode chambers respectively for bilaterally graded collection.

[0139] Example 4

[0140] Comparison of different regeneration methods

[0141] To verify the technical effect of the present invention, this embodiment uses an ion exchange resin (which adsorbs HCOO according to the method in Example 1) to be treated. - CH3COO - Cl - DuPont TM AmberLite TM The IRA900 Cl ion exchange resin was compared using the traditional NaOH regeneration method, the fixed electroregeneration method, and the staged electroregeneration method in Example 1; the comparison results of the different regeneration methods are shown in Table 6 and... Figure 9 As shown. Figure 9 In this context, "traditional regeneration" refers to the traditional NaOH regeneration method described above, "fixed electric regeneration" refers to the fixed electric regeneration method described above, and "graded electric regeneration" refers to the graded electric regeneration method described in Example 1 above.

[0142] Traditional NaOH regeneration method: The ion exchange resin to be treated is chemically regenerated in one step using a 0.20 wt% NaOH solution for 60 min, and all regenerated liquid is collected and mixed. The results show that the total regeneration rate is 91.6%, but the three anions are mixed in the regenerated liquid, and the highest single component accounts for only 38.8%, which cannot achieve graded recovery.

[0143] A fixed electroregeneration method was used: following the method in Example 1, one stage of electrochemical regeneration was performed at a voltage of 12 V and an electrode spacing of 45 mm for 160 min, without switching operating conditions based on pH or conductivity signals. The results showed a total regeneration rate of 78.4%, with the highest single-component percentage at 42.1%, indicating no significant fractionation effect.

[0144] Using the graded electroregeneration method in Example 1 of this invention, the voltage, electrode spacing, and collection channel were adjusted in the first, second, and third stages, respectively, achieving a total regeneration rate of 86.9%, and the Cl in the first enrichment solution was reduced. - The proportion of CH3COO in the second enrichment solution was 62.5%. - The proportion of HCOO in the third enrichment solution was 50.0%. - The proportion is 48.7%. Compared with traditional chemical regeneration, this invention avoids the use of external strong alkali regenerators and transforms the mixed regenerated liquid into a multi-stage enriched liquid; compared with fixed electroregeneration, this invention improves the graded recovery effect and the controllability of the regeneration process.

[0145] The total regeneration rate is defined as the ratio of the total number of target ions recovered in the three-stage enrichment solutions to the total number of target ions initially loaded on the resin. The highest single-component percentage is defined as the ratio of the single target ion with the highest percentage in each enrichment solution to the total number of the three target anions in that enrichment solution. The highest single-component percentage in the staged electroregeneration method is defined as the percentage of Cl in the first enrichment solution. - The proportion of the total amount of the three target anions.

[0146] Table 6 - Comparison of Regeneration Effects and Staged Recycling Effects of Different Regeneration Methods

[0147]

[0148] It is understood that the technical features of the above embodiments can be combined arbitrarily. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0149] The above are merely preferred embodiments of this application, and only specifically describe the technical principles of this application. These descriptions are only for explaining the principles of this application and should not be construed as limiting the scope of protection of this application in any way. Based on this explanation, any modifications, equivalent substitutions, and improvements made within the spirit and principles of this application, as well as other specific embodiments of this application that can be conceived by those skilled in the art without creative effort, should be included within the scope of protection of this application.

Claims

1. An ion exchange resin electroregeneration device, characterized in that, include: A resin regeneration electrolytic cell is provided inside, which is equipped with an ion exchange membrane that divides the electrolytic cell into an anode chamber and a cathode chamber. An anode is provided in the anode chamber and a cathode is provided in the cathode chamber. A fixed resin bed is provided in the cathode chamber or the anode chamber to accommodate the ion exchange resin to be treated, wherein the ion exchange resin to be treated is an ion exchange resin loaded with target ions. A power source, which is used to electrically connect the anode and cathode; pH sensors are respectively installed on the anode chamber and the cathode chamber; A conductivity detector is respectively installed on the anode chamber and the cathode chamber; An electrode drive unit is used to adjust the spacing between the anode and cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode.

2. The ion exchange resin electroregeneration device as described in claim 1, characterized in that, The electrode driving unit includes: A first motor has a shaft connected to a vertically arranged first lead screw, and a first movable block is screwed onto the first lead screw. The second motor is fixedly connected to the first moving block. The rotating shaft of the second motor is connected to a horizontally arranged second lead screw, and the second moving block is screwed onto the second lead screw. A third motor is fixedly connected to the second moving block, and the shaft of the third motor is connected to the anode or cathode; The first motor rotates, causing the first lead screw to rotate, which in turn causes the first moving block to move up and down, thereby adjusting the height of the anode or cathode; the second motor rotates, causing the second lead screw to rotate, which in turn causes the second moving block to move horizontally, thereby adjusting the distance between the anode and cathode; the third motor rotates, causing the anode or cathode to rotate, thereby adjusting the rotation angle of the anode or cathode.

3. The ion exchange resin electroregeneration device as described in claim 1, characterized in that, Also includes: An anolyte storage tank contains anolyte. The resin regeneration electrolytic cell is provided with a first anode electrolyte inlet and outlet hole and a second anode electrolyte inlet and outlet hole respectively on the corresponding anode chamber. The anode electrolyte storage tanks are all connected to the first anode electrolyte inlet and outlet hole and the second anode electrolyte inlet and outlet hole. A cathode electrolyte storage tank, which stores cathode electrolyte; The resin regeneration electrolytic cell is provided with a first cathode electrolyte inlet and outlet hole and a second cathode electrolyte inlet and outlet hole respectively on the cathode chamber. The cathode electrolyte storage tanks are all connected to the first cathode electrolyte inlet and outlet hole and the second cathode electrolyte inlet and outlet hole.

4. The ion exchange resin electroregeneration device as described in claim 2, characterized in that, The anode chamber and / or cathode chamber are provided with enrichment liquid outlets, which are connected to multiple enrichment liquid storage tanks via multi-way valves.

5. The ion exchange resin electroregeneration device as described in claim 4, characterized in that, It also includes a control unit; The control unit is electrically connected to the pH sensor, conductivity detector, power supply, first motor, second motor, third motor and multi-way valve respectively; The control unit is used to adjust the power supply output voltage, the distance between the anode and cathode, the height of the anode or cathode, the rotation angle of the anode or cathode, and the connection position of the multi-way valve according to the pH value detected by the pH sensor and the conductivity detected by the conductivity detector, so that the enriched liquid outlet can be connected to different enriched liquid storage tanks.

6. A method for electro-regenerating ion exchange resin, applied to the ion exchange resin electro-regeneration apparatus according to any one of claims 1 to 5, characterized in that, Includes the following steps: Place the ion exchange resin to be treated in the cathode chamber or anode chamber; Add the anolyte to the anode chamber and the catholyte to the cathode chamber. Connect the cathode to the negative terminal of the power supply and the anode to the positive terminal of the power supply to perform electrochemical regeneration of the ion exchange resin. In the electrochemical regeneration process, a pH sensor detects the pH value of the anolyte and the catholyte, and a conductivity detector detects the conductivity of the anolyte and the catholyte. Based on the detected pH value and conductivity, the power supply output voltage, the distance between the anode and the cathode, the height of the anode or cathode, and the rotation angle of the anode or cathode are adjusted.

7. The method for electro-regeneration of ion exchange resin as described in claim 6, characterized in that, During the electrochemical regeneration process, the power supply output voltage is 3~30 V, the electroregeneration time is 5~600 min, the distance between the anode and cathode is 5~100 mm, the anode electrolyte is added to the anode chamber at 1~100 mL / min, the cathode electrolyte is added to the cathode chamber at 1~100 mL / min, the vertical movement range of the anode or cathode is 0~100 mm, and the rotation angle of the anode or cathode is 0~360°.

8. The method for electro-regeneration of ion exchange resin as described in claim 7, characterized in that, When the ion exchange resin to be treated is an anion exchange resin and is placed in the cathode chamber, the electrochemical regeneration includes the following first stage, second stage and third stage; In the first stage of electrochemical regeneration, the power supply output voltage is 3~10V, and the distance between the anode and cathode is 40~100mm. During the first stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 7.2~7.3 to 9.5~10.3, and the conductivity increases from 0.31~0.33 mS / cm to 1.55~1.57 mS / cm and then decreases to 1.2~1.24 mS / cm. Then the second stage of electrochemical regeneration is carried out. During the second stage of electrochemical regeneration, the power supply output voltage is 8~18 V, and the distance between the anode and cathode is 20~60 mm. During the second stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 9.5~10.3 to 10.8~11.3, and the conductivity increases from 1.2~1.24 mS / cm to 1.95~2.10 mS / cm and then decreases to 1.6~1.62 mS / cm. Then, the third stage of electrochemical regeneration is carried out. During the third stage of electrochemical regeneration, the power supply output voltage is 12~30V, and the distance between the anode and cathode is 5~40 mm. During the third stage of electrochemical regeneration, the pH value of the electrolyte in the cathode chamber increases from 10.8~11.3 to 11.4~11.9, the conductivity decreases from 1.6~1.62 mS / cm to 1.4~1.42 mS / cm, then increases to 1.65~1.69 mS / cm, and then decreases to 1.05~1.1 mS / cm. At this point, the third stage of electrochemical regeneration is completed.

9. The method for electro-regeneration of ion exchange resin as described in claim 8, characterized in that, The electrochemical regeneration time for the first stage, the second stage, and the third stage is 5~180 min; The ion exchange resin includes at least one of basic anion exchange resin, acidic cation exchange resin, chelating resin, functionalized adsorption resin, and mixed bed resin. The target ions loaded on the ion exchange resin include at least one of the following: halide ions, organic acid ions, nitrate ions, sulfate ions, phosphate ions, carbonate ions, thermally stable salt anions, alkali metal ions, alkaline earth metal ions, heavy metal ions, and rare earth ions. The anolyte and catholyte comprise water and / or a saline solution; the saline solution comprises at least one of sodium sulfate solution, potassium sulfate solution, sodium nitrate solution, and potassium nitrate solution; the concentration of the saline solution is 0.1~10 mmol / L.

10. The method for electro-regeneration of ion exchange resin as described in claim 8, characterized in that, During the first-stage electrochemical regeneration process, the enriched solution generated in the first-stage electrolysis is collected through the enriched solution outlet. During the second-stage electrochemical regeneration process, the enriched solution generated in the second-stage electrolysis is collected through the enriched solution outlet. In the third stage of electrochemical regeneration, the enriched solution generated during the third stage of electrolysis is collected through the enriched solution outlet.

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