Electrochemical synergistic treatment device and method for electroplating wastewater
The electrochemical co-processing device solves the problems of low heavy metal removal rate and resource waste in traditional electroplating wastewater treatment, achieving efficient removal and resource recovery, reducing energy consumption and pollution.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- HARBIN YINGUANG PLATING CO LTD
- Filing Date
- 2026-06-16
- Publication Date
- 2026-07-31
AI Technical Summary
Traditional electroplating wastewater treatment processes cannot effectively remove highly stable complexes, resulting in low heavy metal removal rates, environmental pollution, resource waste, and the generation of high-cost hazardous waste, making it impossible to achieve metal resource recycling.
An electrochemical synergistic treatment device is adopted, which controls the pH by adjusting the adjustment component, separates impurities by the filtration component, breaks down the complex by the ozone reaction component, and recovers metals by the electrolysis component. It utilizes forced disturbance heat exchange and a membrane electrolyzer with high electrolysis efficiency to achieve efficient removal of heavy metals and resource recovery.
It achieves efficient removal and resource recovery of heavy metals, reduces system energy consumption, extends membrane module life, reduces pollution, and improves wastewater reuse rate.
Smart Images
Figure CN122482684A_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of wastewater treatment technology, specifically to an electrochemical co-treatment device and method for electroplating wastewater. Background Technology
[0002] Electroplating wastewater contains highly toxic and difficult-to-degrade heavy metal ions such as copper, nickel, and chromium, making it a key and challenging area in industrial wastewater treatment. Traditional electroplating wastewater treatment processes mainly rely on chemical precipitation, which involves adding alkaline agents such as lime and sodium hydroxide to convert heavy metal ions into insoluble hydroxides or carbonates for precipitation and removal. However, with the full implementation of environmental regulations, heavy metal emission limits have generally been tightened by more than 30%, and some regions have implemented even stricter special emission limits and mandated that the wastewater reuse rate be no less than 60%.
[0003] If electroplating wastewater is not treated with electrochemical synergy and traditional processes are still used, the ecological environment will continue to be polluted. On the one hand, electroplating wastewater contains a large amount of strong complexing agents such as EDTA, citric acid, and ammonia. The Ni-EDTA complexes formed by these complexing agents and heavy metal ions are extremely stable. Conventional chemical precipitation methods cannot effectively destroy their complex structure, resulting in low removal rates of heavy metal ions and difficulty in achieving stable effluent standards.
[0004] If traditional processes rely solely on chemical precipitation, the treated wastewater will still contain a considerable concentration of heavy metals. If discharged into rivers, this will poison aquatic life, and if it seeps into the soil, it will cause heavy metals to accumulate in crops and ultimately harm human health through the food chain. On the other hand, the traditional chemical precipitation method, which transfers heavy metals from the liquid phase to the solid phase, inevitably generates a large amount of hazardous waste electroplating sludge. This type of sludge belongs to HW17 hazardous waste, and its disposal cost is extremely high. Moreover, the traditional process only removes valuable metals from the wastewater in the form of mixed sludge, resulting in a huge waste of resources and failing to achieve the resource recycling and utilization of metals.
[0005] Therefore, it is necessary to design an electroplating wastewater treatment device that can perform electrochemical synergy and has high electrolysis efficiency. Summary of the Invention
[0006] The purpose of this invention is to provide an electrochemical co-treatment device and method for electroplating wastewater to solve the problems mentioned in the background art.
[0007] To solve the above-mentioned technical problems, the present invention provides the following technical solution: an electrochemical co-treatment device for electroplating wastewater, comprising a wastewater tank, an adjustment component for adjusting the acidity and alkalinity of the wastewater on one side of the wastewater tank, a first support frame on one side of the adjustment component, the first support frame being divided into a first layer, a second layer and a third layer from top to bottom, a filter component for filtering and separating the wastewater on the first and second layers of the first support frame, a reaction component for reacting the wastewater with ozone on one side of the filter component, a heat exchange component for electrolyzing the wastewater on the third layer of the first support frame, and an electrolysis component for exchanging heat between the electrolytic hot wastewater and the acidity and alkalinity-adjusting cold wastewater inside the heat exchange component.
[0008] According to the above technical solution, the outlet end of the wastewater tank is fixedly connected to a first outlet valve pipe. The regulating component includes a second support frame located on one side of the wastewater tank. An regulating box is fixedly connected inside the second support frame. A first water pump is fixedly connected to one side of the second support frame. The electrolysis component includes a first diaphragm electrolytic cell and a second diaphragm electrolytic cell fixedly connected inside the first support frame. The heat exchange component includes a third inlet pipe fixedly connected to the output end of the first water pump. The output end of the third inlet pipe passes through the second diaphragm electrolytic cell. The interiors of the first diaphragm electrolytic cell and the second diaphragm electrolytic cell are both divided into an anode chamber and a cathode chamber. A heat exchange tube is fixedly connected inside each anode chamber and anode plate.
[0009] According to the above technical solution, one end of the heat exchange tube inside one of the cathode chambers is fixedly connected to the output end of the third inlet pipe and the other end is fixedly connected to a first U-shaped tube. The other end of the first U-shaped tube passes through the second diaphragm electrolytic cell and is fixedly connected to the heat exchange tube inside one of the anode chambers. The other end of the heat exchange tube inside one of the anode chambers is fixedly connected to a second U-shaped tube. The output end of the second U-shaped tube passes through the first diaphragm electrolytic cell. One end of the heat exchange tube inside the other cathode chamber is fixedly connected to the output end of the second U-shaped tube.
[0010] According to the above technical solution, one end of the heat exchange tube inside the other cathode chamber is fixedly connected to a third U-shaped tube, and the other end of the third U-shaped tube passes through the first diaphragm electrolytic cell. One end of the heat exchange tube inside the other anode chamber is fixedly connected to the output end of the third U-shaped tube. The other end of the heat exchange tube inside the other anode chamber is fixedly connected to a water outlet pipe, and the output end of the water outlet pipe passes through the regulating box.
[0011] According to the above technical solution, the first U-shaped tube, the second U-shaped tube, the third U-shaped tube, and the water outlet pipe are all fixedly connected with built-in U-shaped tubes. The interiors of the first U-shaped tube, the second U-shaped tube, the third U-shaped tube, and the water outlet pipe are all separated by built-in U-shaped tubes with first partition grooves. The interior of each heat exchange tube is fixedly connected with a built-in water pipe. One end of each built-in water pipe is provided with a water inlet hole, and the other end of each built-in water pipe is provided with a closed end. Several water outlet holes are evenly provided on the outside of each built-in water pipe. The interior of each heat exchange tube is separated by built-in water pipes.
[0012] According to the above technical solution, the inlet of the first built-in water pipe is connected to the output end of the third water inlet pipe; the output end of the first second partition groove is connected to the input end of the built-in U-shaped tube inside the first U-shaped tube; the inlet of the second built-in water pipe is connected to the output end of the built-in U-shaped tube inside the first U-shaped tube; the output end of the second second partition groove is connected to the input end of the built-in U-shaped tube inside the second U-shaped tube; the inlet of the third built-in water pipe is connected to the output end inside the second U-shaped tube; the output end of the third second partition groove is connected to the input end of the built-in U-shaped tube inside the third U-shaped tube; the inlet of the fourth built-in water pipe is connected to the output end of the built-in U-shaped tube inside the third U-shaped tube; the output end of the fourth second partition groove is connected to the input end of the built-in U-shaped tube inside the outlet pipe; and the output end of the built-in U-shaped tube inside the outlet pipe passes through the regulating box.
[0013] According to the above technical solution, the filtration assembly includes a second outlet valve pipe fixedly connected to the lower end of the regulating box, a charged nanofiltration membrane tank fixedly connected to the second layer of the first support frame, a security filter fixedly connected to the first layer of the first support frame, a second water pump fixedly connected to the outside of the charged nanofiltration membrane tank, the input end of the second water pump fixedly connected to the output end of the second outlet valve pipe, a first inlet pipe fixedly connected to the output end of the second water pump, the output end of the first inlet pipe fixedly connected to the input end of the security filter, a third outlet valve pipe fixedly connected to the output end of the security filter, the output end of the third outlet valve pipe fixedly connected to the input end of the charged nanofiltration membrane tank, a first output end and a second output end provided on the outside of the charged nanofiltration membrane tank, and a fourth outlet valve pipe fixedly connected to the first output end.
[0014] According to the above technical solution, the reaction assembly includes an ozone reaction tower fixedly connected inside the first support frame. A third water pump is fixedly connected to the outside of the ozone reaction tower. A fifth water outlet valve pipe is fixedly connected to the input end of the third water pump. The input end of the fifth water outlet valve pipe is fixedly connected to the second output end of the charged nanofiltration membrane tank. A second water inlet pipe is fixedly connected to the output end of the third water pump. The output end of the second water inlet pipe is fixedly connected to the water inlet end of the ozone reaction tower. A sixth water outlet valve pipe is fixedly connected to the water outlet end of the ozone reaction tower. An ozone generator is provided on one side of the ozone reaction tower. The gas outlet end of the ozone generator is connected to the gas inlet end pipe of the ozone reaction tower. A gas outlet pipe is provided on the upper side of the ozone reaction tower.
[0015] According to the above technical solution, an acid tank, an alkali tank, and a hydrogen peroxide tank are fixedly connected to the upper side of the second support frame in sequence. The output ends of the acid tank, alkali tank, and hydrogen peroxide tank are all fixedly connected to discharge valves. A rotary motor is fixedly connected to the center of the upper side of the second support frame. A rotary shaft is fixedly connected to the output end of the rotary motor. Four rotating blades are evenly fixedly connected to the other end of the rotary shaft. A liquid level sensor and a pH detection sensor are fixedly connected to the inner wall of the rotary motor.
[0016] According to the above technical solution, a cation exchange membrane is fixedly connected to the center of both the first diaphragm electrolytic cell and the second diaphragm electrolytic cell. An anode plate and a cathode plate are respectively provided on both sides of each cation exchange membrane. One of the anode plates and cathode plates is fixedly connected to the first diaphragm electrolytic cell, and the other anode plate and cathode plate are fixedly connected to the second diaphragm electrolytic cell. A first valve and a second valve are connected through one side of both the first diaphragm electrolytic cell and the second diaphragm electrolytic cell. The input end of each first valve is connected to the anode chamber, and the input end of each second valve is connected to the cathode chamber. A main drain pipe is fixedly connected to the input ends of both the first valve and the second valve.
[0017] Compared with the prior art, the beneficial effects achieved by the present invention are: 1. By changing the flow path of the pre-conditioned cold wastewater from the traditional axial direct flow to a forced disturbance mode of axial inlet in the central tube—radial high-pressure jet—axial outlet in the annular gap, the technical problem of low heat exchange efficiency caused by the mainstream fluid being far from the tube wall and the thermal boundary layer being too thick in traditional shell-and-tube heat exchangers is fundamentally solved. When the cold wastewater enters the interior of the built-in water pipe through the inlet hole, it does not flow smoothly forward along the tube axis, but is driven by pressure to be ejected radially at high speed from multiple outlet holes evenly opened on the tube wall in a direction close to perpendicular to the tube wall, forming a strong jet impact. This jet directly impacts and penetrates the thermal boundary layer on the inner wall of the heat exchange tube, so that the cold wastewater no longer relies on slow molecular diffusion or laminar heat conduction, but achieves efficient heat exchange through forced convection. At the same time, the radially ejected multiple jets generate violent turbulent mixing in the second partition groove, further disrupting the development of the boundary layer and making the temperature and velocity fields of the entire annular region more uniform. This dual enhancement mechanism of jet impact and turbulent mixing enables the cold wastewater to transfer heat fully and directly to the tube wall in a very short heat exchange path.
[0018] 2. Through forced disturbance, the pre-conditioned cold wastewater flows into the heat exchange tube through the inlet hole at the end of the built-in water pipe, and then is radially sprayed out through multiple evenly distributed outlet holes into the second partition groove. The sprayed cold wastewater then makes full contact with the tube wall of the heat exchange tube and flows sequentially through the cathode and anode chambers of the second diaphragm electrolytic cell and the cathode and anode chambers of the first diaphragm electrolytic cell, forming a series heat exchange cycle. This not only efficiently transfers the waste heat from electrolysis to the inlet water to preheat the wastewater, but also stably controls the temperature of the four electrode chambers within the optimal process range of ~℃. This effectively avoids the problems of insufficient heat exchange, low efficiency, and local overheating or overcooling of the electrolytic cell caused by the water flow not contacting the tube wall in the center of the tube in traditional heat exchangers. It achieves the effects of fully utilizing waste heat, reducing system energy consumption, ensuring uniform deposition of metal ions, and obtaining high-purity metal plates.
[0019] 3. The system uses a liquid level sensor to monitor the water level in the regulating tank in real time and triggers the start and stop of the first water pump; a pH sensor to continuously measure the pH value of the wastewater and automatically adjusts the dripping through the discharge valves of the acid and alkali tanks; and a rotary motor to drive the rotating shaft and impeller to rotate at high speed, creating a strong turbulent flow. This coordinated motion ensures that the wastewater, acid, alkali, and hydrogen peroxide are rapidly and evenly mixed in the regulating tank and maintained within the set slightly acidic pH range and pre-oxidation dosage. This not only achieves fully automatic and precise control of the influent water level and pH, but also pre-oxidizes and destroys some organic complexes in the wastewater. It effectively avoids overflow or dry pumping caused by water level fluctuations, decreased efficiency of subsequent membrane separation and electrolysis due to pH loss, and localized high or low concentrations due to uneven mixing. This achieves the effects of stabilizing pretreated water quality, extending membrane module life, and reducing the burden of subsequent ozone complex destruction. Attached Figure Description
[0020] The accompanying drawings are provided to further illustrate the invention and form part of the specification. They are used in conjunction with embodiments of the invention to explain the invention and do not constitute a limitation thereof. In the drawings: Figure 1 This is a schematic diagram of the overall structure of an electrochemical co-treatment device for electroplating wastewater according to the present invention. Figure 2 This is a schematic diagram of the structure of the filtration component, reaction component, and regulation component in this invention; Figure 3 This is a schematic diagram showing the positions of the regulating component and the electrolysis component in this invention; Figure 4 This is a schematic diagram of the structure of the adjustment component in this invention; Figure 5 This is a schematic diagram of the electrolysis assembly in this invention; Figure 6 This is a schematic diagram of the heat exchange component in this invention; Figure 7 In this invention Figure 6 An enlarged schematic diagram of area A; In the diagram: 1. Wastewater tank; 11. First outlet valve pipe; 12. First water pump; 2. Adjustment assembly; 21. Second support frame; 211. Rotary motor; 212. Rotary shaft; 213. Rotary blade; 22. Adjustment box; 23. Discharge valve; 24. Liquid level sensor; 25. pH detection sensor; 26. Acid tank; 27. Alkali tank; 28. Hydrogen peroxide tank; 3. Filter assembly; 31. Second outlet valve pipe; 32. Second water pump; 33. First inlet pipe; 34. Security filter; 35. Third outlet valve pipe; 36. Charged nanofiltration membrane tank; 37. Fourth outlet valve pipe; 4. First support frame; 5. Reaction components; 51. Second inlet pipe; 52. Gas outlet pipe; 53. Third water pump; 54. Fifth outlet valve pipe; 55. Ozone generator; 56. Ozone reaction tower; 57. Sixth outlet valve pipe; 6. Heat exchange assembly; 61. Third inlet pipe; 62. Heat exchange tube; 63. First U-shaped tube; 64. Second U-shaped tube; 65. Third U-shaped tube; 66. Outlet pipe; 67. Built-in U-shaped tube; 671. First partition groove; 68. Built-in water pipe; 681. Outlet hole; 682. Inlet hole; 683. Second partition groove; 7. Electrolysis assembly; 71. First diaphragm electrolytic cell; 711. Anode chamber; 712. Anode plate; 713. Cation exchange membrane; 714. Cathode plate; 715. Cathode chamber; 72. Second diaphragm electrolytic cell; 73. First valve; 74. Second valve; 75. Main drain pipe. Detailed Implementation
[0021] 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 embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.
[0022] Please see Figure 1-7 The present invention provides a technical solution: an electrochemical co-treatment device for electroplating wastewater, comprising a wastewater tank 1, an adjustment component 2 for adjusting the pH of the wastewater on one side of the wastewater tank 1, a first support frame 4 on one side of the adjustment component 2, the first support frame 4 being divided into a first layer, a second layer and a third layer from top to bottom, a filter component 3 for filtering and separating the wastewater on the first and second layers of the first support frame 4, a reaction component 5 for reacting the wastewater with ozone on one side of the filter component 3, a heat exchange component 6 for electrolyzing the wastewater on the third layer of the first support frame 4, and an electrolysis component 7 for exchanging heat between the electrolytic hot wastewater and the pH-adjusting cold wastewater inside the heat exchange component 6.
[0023] The wastewater tank 1 has a first outlet valve pipe 11 fixedly connected to its outlet end. The regulating assembly 2 includes a second support frame 21 located on one side of the wastewater tank 1. An regulating box 22 is fixedly connected inside the second support frame 21. A first water pump 12 is fixedly connected to one side of the second support frame 21. The input end of the first water pump 12 is fixedly connected to the output end of the first outlet valve pipe 11. The electrolysis assembly 7 includes a first diaphragm electrolysis cell 71 and a second diaphragm electrolysis cell 72 fixedly connected inside the first support frame 4. The heat exchange assembly 6 includes a third inlet pipe 61 fixedly connected to the output end of the first water pump 12. The output end of the third inlet pipe 61 passes through the second diaphragm electrolysis cell 72. The interiors of the first diaphragm electrolysis cell 71 and the second diaphragm electrolysis cell 72 are both divided into an anode chamber 711 and a cathode chamber 715. A heat exchange pipe 62 is fixedly connected inside each anode chamber 711 and the anode plate 712.
[0024] One end of the heat exchange tube 62 inside one of the cathode chambers 715 is fixedly connected to the output end of the third water inlet pipe 61, and the other end is fixedly connected to a first U-shaped tube 63. The other end of the first U-shaped tube 63 passes through the second diaphragm electrolytic cell 72 and is fixedly connected to the heat exchange tube 62 inside one of the anode chambers 711. The other end of the heat exchange tube 62 inside one of the anode chambers 711 is fixedly connected to a second U-shaped tube 64. The output end of the second U-shaped tube 64 passes through the first diaphragm electrolytic cell 71. One end of the heat exchange tube 62 inside the other cathode chamber 715 is fixedly connected to the output end of the second U-shaped tube 64.
[0025] One end of the heat exchange tube 62 inside the other cathode chamber 715 is fixedly connected to a third U-shaped tube 65, and the other end of the third U-shaped tube 65 passes through the first diaphragm electrolytic cell 71. One end of the heat exchange tube 62 inside the other anode chamber 711 is fixedly connected to the output end of the third U-shaped tube 65. The other end of the heat exchange tube 62 inside the other anode chamber 711 is fixedly connected to a water outlet pipe 66, and the output end of the water outlet pipe 66 passes through the regulating box 22.
[0026] The first U-shaped tube 63, the second U-shaped tube 64, the third U-shaped tube 65, and the outlet pipe 66 are all fixedly connected to an internal U-shaped tube 67. The interiors of the first U-shaped tube 63, the second U-shaped tube 64, the third U-shaped tube 65, and the outlet pipe 66 are all separated by a first partition groove 671 through the internal U-shaped tube 67. The interior of each heat exchange tube 62 is fixedly connected to an internal water pipe 68. One end of each internal water pipe 68 is provided with a water inlet hole 682, and the other end of each internal water pipe 68 is provided with a closed end. Several water outlet holes 681 are evenly provided on the outside of each internal water pipe 68. The interior of each heat exchange tube 62 is separated by internal water pipes 68.
[0027] The inlet 682 of the first built-in water pipe 68 is connected to the output end of the third water inlet pipe 61; the output end of the first second partition groove 683 is connected to the input end of the built-in U-shaped tube 67 inside the first U-shaped tube 63; the inlet 682 of the second built-in water pipe 68 is connected to the output end of the built-in U-shaped tube 67 inside the first U-shaped tube 63; the output end of the second second partition groove 683 is connected to the input end of the built-in U-shaped tube 67 inside the second U-shaped tube 64; and the inlet of the third built-in water pipe 68... The hole 682 is connected to the output end inside the second U-shaped tube 64. The output end of the third second partition groove 683 is connected to the input end of the U-shaped tube 67 built inside the third U-shaped tube 65. The inlet hole 682 of the fourth built-in water pipe 68 is connected to the output end of the U-shaped tube 67 built inside the third U-shaped tube 65. The output end of the fourth second partition groove 683 is connected to the input end of the U-shaped tube 67 built inside the outlet pipe 66. The output end of the U-shaped tube 67 built inside the outlet pipe 66 passes through the regulating box 22.
[0028] The specific explanation based on the above structure is as follows: After opening the first outlet valve pipe 11 of the wastewater tank 1, the entire heat exchange cycle is immediately started. First, the first water pump 12 draws out the pre-conditioned cold wastewater to be treated from the wastewater tank 1. This cold wastewater is sent through the third inlet pipe 61 into the heat exchange tube 62 installed inside the cathode chamber 715 of the second diaphragm electrolytic cell 72. Under normal circumstances, when ordinary pre-conditioned cold wastewater flows inside the pipe for heat exchange, the mainstream part located in the center of the pipe never comes into contact with the pipe wall, resulting in insufficient heat exchange and low efficiency. This design is precisely to overcome this defect. In the heat exchange tube 62, the pre-conditioned cold wastewater passes through the end of the built-in water pipe 68. The water flows into the interior of the built-in water pipe 68 through the inlet hole 682, and then flows forward along the axial direction of the built-in water pipe 68. It is then radially sprayed out through multiple outlet holes 681 evenly distributed on the pipe wall and enters the second partition groove 683 formed by the inner wall of the built-in water pipe 68 and the heat exchange tube 62. During this process, the sprayed pre-conditioned cold wastewater comes into full contact with the pipe wall of the heat exchange tube 62, thus completely solving the problem of low heat exchange efficiency in traditional heat exchangers where the intermediate water source cannot contact the pipe wall. At this time, the pre-conditioned cold wastewater completes the first heat exchange with the electrolyte in the cathode chamber 715. Heat is transferred from the electrolyte to the cold wastewater, so that the temperature of the electrolytic cell is initially controlled.
[0029] Next, the pre-conditioned cold wastewater, after completing the first stage of heat exchange, leaves the cathode chamber 715 heat exchange tube 62 and flows into the first U-shaped tube 63. Inside the first U-shaped tube 63, the built-in U-shaped tube 67 guides the flow direction. At the same time, the first partition groove 671 is filled with a special gas that can block heat loss. This gas effectively isolates the pre-conditioned cold wastewater from the outer tube wall, so that the pre-conditioned cold wastewater only flows inside the built-in U-shaped tube 67. The advantage of this design is that it can effectively prevent the pre-conditioned cold wastewater, which has already absorbed a certain amount of heat, from directly contacting the outer pipe wall, which is too cold. This avoids the phenomenon of a significant drop in the temperature of the pre-conditioned cold wastewater due to excessive heat dissipation, ensuring the stability and efficiency of the subsequent heat exchange process. After being guided by the built-in U-shaped tube 67, the pre-conditioned cold wastewater smoothly enters the heat exchange tube 62 in the anode chamber 711 of the second diaphragm electrolytic cell 72, and then passes through the heat exchange path of the inner tube inlet-outlet hole 681 spraying and the outer ring second partition groove 683 to carry out a second heat exchange with the electrolyte in the anode chamber 711, thus removing a large amount of excess heat generated by the oxygen evolution overpotential and Joule heating in the anode chamber 711.
[0030] Subsequently, the pre-conditioned cold wastewater enters the heat exchange tube 62 in the cathode chamber 715 of the first diaphragm electrolytic cell 71 through the second U-shaped tube 64 to complete the third heat exchange, and then enters the heat exchange tube 62 in the anode chamber 711 of the first diaphragm electrolytic cell 71 through the third U-shaped tube 65 to complete the fourth heat exchange. By this time, the pre-conditioned cold wastewater has flowed through the heat exchange tubes 62 of a total of four electrode chambers in the two diaphragm electrolytic cells, and has absorbed the heat of each chamber evenly.
[0031] Finally, the pre-conditioned cold wastewater, after completing all four heat exchanges, returns to the regulating tank 22 through the outlet pipe 66 and its internal built-in U-shaped pipe 67, thus forming a complete series heat exchange cycle. This process achieves precise temperature control of the four electrode chambers in the two diaphragm electrolyzers, keeping the electrolyzer temperature stable within the optimal process range of 30-40℃. This ensures efficient electrodeposition and recovery of heavy metal ions while making full use of the waste heat from electrolysis, achieving the effects of energy saving, consumption reduction, and stable operation.
[0032] Furthermore, proper preheating facilitates the uniform reduction of metal ions on the cathode surface, inhibiting dendrite growth and hydrogen bubble inclusion. When the temperature is too low, a concentration gradient is easily formed near the cathode due to rapid ion consumption, leading to intensified concentration polarization. The deposited metal layer may be loose, porous, and prone to impurities. Preheated wastewater entering the electrolyzer, combined with the heat generated by the electrolysis process itself, can maintain a uniform temperature field in the cathode area, thereby obtaining a metal plate with a smooth surface and high purity. Temperature increase also has a positive effect on membrane separation. In the range of 20-30℃, the flux of nanofiltration membranes increases with increasing temperature. After preheating, the wastewater entering the membrane unit can improve the membrane water production rate, reduce concentration polarization, and reduce membrane fouling tendency, thus providing the electrolyzer with cleaner and more stable ionized wastewater.
[0033] An acid tank 26, an alkali tank 27, and a hydrogen peroxide tank 28 are sequentially fixedly connected to the upper side of the second support frame 21. A discharge valve 23 is fixedly connected to the output ends of the acid tank 26, the alkali tank 27, and the hydrogen peroxide tank 28. A rotary motor 211 is fixedly connected to the center of the upper side of the second support frame 21. A rotary shaft 212 is fixedly connected to the output end of the rotary motor 211. Four rotating blades 213 are evenly fixedly connected to the other end of the rotary shaft 212. A liquid level sensor 24 and a pH detection sensor 25 are fixedly connected to the inner wall of the rotary motor 211.
[0034] The specific explanation based on the above structure is as follows: The pH detection sensor 25 is based on potentiometric analysis. It indirectly determines the pH value of a solution by measuring the potential difference between a pair of electrodes. Its core component is a composite electrode integrating a glass electrode and a reference electrode. The glass electrode tip has a special glass membrane that is particularly sensitive to hydrogen ions. When it is immersed in the solution to be tested, a potential difference is generated inside and outside the membrane due to the difference in hydrogen ion concentration. The reference electrode provides a constant potential that is not affected by the pH of the solution. The measurement circuit formed by the two will output a weak millivolt-level signal. The magnitude of this signal strictly follows the Nernst equation, that is, it is linearly related to the pH value of the solution. After receiving this signal, the transmitter, in conjunction with the built-in temperature sensor, performs high-impedance amplification, signal processing, and temperature compensation, automatically calculates and displays the real-time pH value.
[0035] The principle of the liquid level sensor 24 is that it is responsible for monitoring the water level and converting it into an electrical signal. It mainly works in two ways: contact and non-contact. In complex environments such as electroplating wastewater, the most commonly used sensors are float-type sensors based on Archimedes' principle and ultrasonic sensors using the transmit-reflect-receive mode. The float-type liquid level switch uses a float with a built-in magnet to rise and fall with the liquid level, triggering the internal reed switch to close or open, thereby outputting a switch signal. The ultrasonic liquid level gauge is installed on the top of the container. It emits ultrasonic pulses to the liquid surface and calculates the time it takes for the echo to return to accurately measure the distance and thus determine the liquid level.
[0036] The preheated electroplating wastewater is pumped from the wastewater tank 1 by the first water pump 12 and sent to the regulating tank 22. The liquid level sensor 24 monitors the water level of the wastewater in the tank in real time. When the water level reaches the set high limit, the first water pump 12 stops pumping and automatically closes the first outlet valve pipe 11 to prevent overflow. When the water level drops to the low limit, water inlet is triggered. The pH detection sensor 25 continuously measures the pH value of the wastewater and determines whether acid or alkali needs to be added based on the pH value of the wastewater.
[0037] Acid tank 26 and alkali tank 27 store dilute sulfuric acid and sodium hydroxide solutions, respectively. The pH value fed back by the pH sensor 25 is compared with the set target pH range. If the measured pH is higher than the upper limit of the target, the discharge valve 23 of acid tank 26 will automatically open and add acid solution to the regulating tank 22. If the measured pH is lower than the lower limit of the target, the discharge valve 23 of alkali tank 27 will open and add alkali solution to the tank. The opening time of the discharge valve 23 can be automatically adjusted until the wastewater reaches the set slightly acidic requirement.
[0038] The hydrogen peroxide tank 28 stores a certain concentration of hydrogen peroxide solution. According to the process settings, the discharge valve 23 at the outlet of the hydrogen peroxide tank 28 is controlled to slowly inject hydrogen peroxide into the regulating tank 22 in proportion. The addition of hydrogen peroxide can preliminarily oxidize some organic complexes in the wastewater at room temperature, destroy their structure, reduce the burden of subsequent ozone catalytic oxidation, and also help to regulate the oxidation-reduction potential of the wastewater.
[0039] To ensure that the added acid, alkali, hydrogen peroxide and wastewater are fully and evenly mixed, and to avoid local concentrations that are too high or too low, the motor is started by controlling the motor to rotate the rotating shaft 212. The rotating shaft 212 drives the rotating blade 213 to rotate at a certain speed, forming strong turbulence in the tank, which quickly stirs and mixes the wastewater, acid, alkali and hydrogen peroxide evenly.
[0040] The filter assembly 3 includes a second outlet valve pipe 31 fixedly connected to the lower end of the regulating box 22, a charged nanofiltration membrane tank 36 fixedly connected to the second layer of the first support frame 4, a security filter 34 fixedly connected to the first layer of the first support frame 4, a second water pump 32 fixedly connected to the outside of the charged nanofiltration membrane tank 36, the input end of the second water pump 32 fixedly connected to the output end of the second outlet valve pipe 31, the output end of the second water pump 32 fixedly connected to a first inlet pipe 33, the output end of the first inlet pipe 33 fixedly connected to the input end of the security filter 34, the output end of the security filter 34 fixedly connected to a third outlet valve pipe 35, the output end of the third outlet valve pipe 35 fixedly connected to the input end of the charged nanofiltration membrane tank 36, a first output end and a second output end provided on the outside of the charged nanofiltration membrane tank 36, and a fourth outlet valve pipe 37 fixedly connected to the first output end.
[0041] The reaction assembly 5 includes an ozone reaction tower 56 fixedly connected inside the first support frame 4. A third water pump 53 is fixedly connected to the outside of the ozone reaction tower 56. A fifth water outlet valve pipe 54 is fixedly connected to the input end of the third water pump 53. The input end of the fifth water outlet valve pipe 54 is fixedly connected to the second output end of the charged nanofiltration membrane tank 36. A second water inlet pipe 51 is fixedly connected to the output end of the third water pump 53. The output end of the second water inlet pipe 51 is fixedly connected to the water inlet end of the ozone reaction tower 56. A sixth water outlet valve pipe 57 is fixedly connected to the water outlet end of the ozone reaction tower 56. An ozone generator 55 is provided on one side of the ozone reaction tower 56. The gas outlet end of the ozone generator 55 is connected to the gas inlet end pipe of the ozone reaction tower 56. A gas outlet pipe 52 is provided on the upper side of the ozone reaction tower 56.
[0042] A cation exchange membrane 713 is fixedly connected to the center of both the first diaphragm electrolytic cell 71 and the second diaphragm electrolytic cell 72. An anode plate 712 and a cathode plate 714 are respectively provided on both sides of each cation exchange membrane 713. One anode plate 712 and cathode plate 714 are fixedly connected to the first diaphragm electrolytic cell 71, and the other anode plate 712 and cathode plate 714 are fixedly connected to the second diaphragm electrolytic cell 72. A first valve 73 and a second valve 74 are connected through one side of both the first diaphragm electrolytic cell 71 and the second diaphragm electrolytic cell 72. The input end of each first valve 73 is connected to the anode chamber 711, and the input end of each second valve 74 is connected to the cathode chamber 715. A main drain pipe 75 is fixedly connected to the input ends of both the first valve 73 and the second valve 74.
[0043] The specific explanation based on the above structure is as follows: After adjustment and compatibility, the electroplating wastewater first flows out from the second outlet valve pipe 31 at the lower end of the regulating tank 22, is drawn and pressurized by the second water pump 32, and is sent into the interior of the security filter 34 through the first inlet pipe 33. The security filter 34 is equipped with a filter element of a certain precision. Its core function is to intercept the residual suspended particles, silt, colloids and possible microorganisms and other mechanical impurities in the wastewater, and prevent these impurities from causing physical damage or chemical pollution to the subsequent high-precision charged nanofiltration membrane, thereby effectively extending the service life of the nanofiltration membrane and ensuring its separation performance. After the fine filtration of the security filter 34, the large particulate impurities in the wastewater are completely removed, and the effluent enters the interior of the charged nanofiltration membrane tank 36 through the third outlet valve pipe 35.
[0044] The charged nanofiltration membrane tank 36 is the core equipment of the entire separation process. It integrates a negatively charged nanofiltration membrane module with a specific molecular weight cutoff value. Utilizing the electrostatic repulsion effect between the surface charge and ions, it can accurately separate different components in the wastewater. Under operating pressure, water molecules and positively charged free metal ions can pass through the membrane layer to become permeate, while larger molecular weight or complexed heavy metals encapsulated by organic complexing agents, as well as large organic molecules, are retained by the membrane to form a concentrate. Through this dual sieving effect of charge and pore size, the charged nanofiltration membrane tank 36 accurately separates the wastewater into two streams. The first output is the permeate containing free metal ions, which is directly sent to the subsequent first diaphragm electrolytic cell 71 for electrolytic recovery via the fourth outlet valve pipe 37. The second output is the concentrate containing complexed heavy metals encapsulated by organic complexing agents, which enters the reaction assembly 5 via the fifth outlet valve pipe 54 for further processing.
[0045] The third water pump 53 draws the concentrated liquid from the fifth outlet valve pipe 54 and sends it to the inlet of the ozone reaction tower 56 through the second inlet pipe 51. Simultaneously, the ozone generator 55 on one side of the ozone reaction tower 56 starts operating. The ozone generator 55 typically employs dielectric barrier discharge technology, using air or pure oxygen as a gas source, and generates a high concentration of ozone gas through high-voltage ionization. This equipment stably delivers ozone to the inlet of the ozone reaction tower 56 through pipelines, providing sufficient oxidant for the subsequent catalytic oxidation reaction. The ozone reaction tower 56 is a vertical closed reactor, pre-filled with granular metal oxide catalysts to form a fixed-bed catalyst layer. Wastewater enters from the top of the ozone reaction tower 56 and flows downwards through the catalyst bed. Ozone enters from the bottom of the ozone reaction tower 56, contacting the wastewater counter-currently and dispersing evenly. Under the action of the active sites on the catalyst surface, the ozone rapidly decomposes to produce oxygen. The highly reactive hydroxyl radicals can non-selectively attack the molecular structure of organic complexing agents such as citric acid, oxidizing and breaking them, thereby completely releasing the previously locked heavy metal ions into a free state. This complex-breaking process can also degrade some COD, greatly improving the electrolytic properties of wastewater. The remaining tail gas after the reaction (mainly containing unreacted ozone, oxygen, and possible gaseous products) is discharged from the outlet pipe 52 at the top of the ozone reaction tower 56. In actual engineering, the outlet pipe 52 is usually connected to a tail gas destroyer (such as activated carbon adsorption or heating catalytic decomposition device) to decompose the residual ozone into oxygen before safe discharge, avoiding secondary pollution to the atmospheric environment. After sufficient complex-breaking treatment, the heavy metal ions in the wastewater have been completely converted into a free state and sent from the outlet of the ozone reaction tower 56 into the second diaphragm electrolytic cell 72 through the sixth outlet valve pipe 57.
[0046] The two electrolytic cells have identical internal structures, ensuring the consistency and stability of the processing technology. Each electrolytic cell has a cation exchange membrane 713 fixed at its center. This membrane is selectively permeable, allowing only positively charged cations to pass through while blocking negatively charged anions and neutral or large organic molecules. The cation exchange membrane 713 tightly divides the cell into two independent working areas: an anode chamber 711 and a cathode chamber 715. An anode plate 712 and a cathode plate 714 are fixed in each chamber, respectively. The anode plate 712 uses a titanium-based noble metal oxide coated electrode, which has excellent corrosion resistance and a low oxygen evolution overpotential, enabling long-term stable operation under acidic conditions. The cathode plate 714 uses copper... The substrate, either a plate or a stainless steel plate, is used as the base for the reduction deposition of metal ions. It is required to have a smooth surface, good conductivity, and easy peeling of the deposited metal layer. The second diaphragm electrolytic cell 72 receives the broken-complex wastewater from the sixth outlet valve pipe 57 (which also enters its anode chamber 711), while the first diaphragm electrolytic cell 71 receives the ionized permeate from the fourth outlet valve pipe 37 (which directly enters its anode chamber 711). Under the electric field driven by the DC power supply, the oxidation reaction of water occurs in the anode chambers 711 of both electrolytic cells. The generated oxygen escapes from the solution, and the generated hydrogen ions keep the anode chambers 711 acidic. This helps to maintain the metal ions in a stable free state and prevents them from hydrolyzing and precipitating.
[0047] Meanwhile, under the influence of the electric field, the metal cations in the anode chamber 711 migrate directionally through the cation exchange membrane 713 to the cathode chamber 715. Anions and any residual organic molecules in the solution are effectively blocked by the cation exchange membrane 713 in the anode chamber 711, preventing them from entering the cathode chamber 715. This ensures the high purity of the cathode product. The metal cations that migrate to the cathode chamber 715 gain electrons on the surface of the cathode plate 714, are reduced to metal atoms, and are deposited layer by layer. As the electrolysis time increases, a dense, flat, and high-purity metal plate gradually forms on the cathode plate 714. After electrolysis, the effluent from the anode chambers 711 of the two electrolytic cells is discharged through the corresponding first valve 73, and the effluent from the cathode chamber 715 is discharged through the second valve 74. All effluent is ultimately collected in the main drain pipe 75 and sent to the subsequent advanced treatment system. This achieves efficient recovery of heavy metals from electroplating wastewater and preliminary purification of the effluent, laying a solid foundation for subsequent zero discharge and resource utilization.
[0048] A method for operating an electrochemical co-treatment device for electroplating wastewater includes the following steps: S1: Wastewater tank 1 stores electroplating wastewater. The electroplating wastewater passes through heat exchange component 6 and electrolysis component 7, where it exchanges heat with pre-conditioned cold wastewater and electrolytic hot wastewater, and the heated electroplating wastewater is then transported to the conditioning component 2.
[0049] S11: After opening the first outlet valve pipe 11 of the wastewater tank 1, the entire heat exchange cycle is started. First, the first water pump 12 draws out the pre-conditioned cold wastewater to be treated from the wastewater tank 1. The cold wastewater is sent through the third inlet pipe 61 into the heat exchange tube 62 set inside the cathode chamber 715 of the second diaphragm electrolytic cell 72. Under normal circumstances, when ordinary pre-conditioned cold wastewater flows inside the pipe for heat exchange, the mainstream part located in the center of the pipe can never contact the pipe wall, resulting in insufficient heat exchange and low efficiency. This design is precisely to overcome this defect in the heat exchange tube 62.
[0050] S12: The pre-conditioned cold wastewater flows into the interior of the built-in water pipe 68 through the inlet hole 682 at the end of the built-in water pipe 68, then flows forward along the axial direction of the built-in water pipe 68, and is radially sprayed out through multiple outlet holes 681 evenly distributed on the pipe wall, entering the second partition groove 683 formed by the inner wall of the built-in water pipe 68 and the heat exchange tube 62. During this process, the sprayed pre-conditioned cold wastewater directly contacts the pipe wall of the heat exchange tube 62, thus completely solving the problem of low heat exchange efficiency due to the intermediate water source not contacting the pipe wall in traditional heat exchangers. At this time, the pre-conditioned cold wastewater completes the first heat exchange with the electrolyte in the cathode chamber 715, and the heat is transferred from the electrolyte to the cold wastewater, so that the temperature of the electrolytic cell is initially controlled.
[0051] S13: Next, the pre-conditioned wastewater, after completing the first stage of heat exchange, leaves the cathode chamber 715 heat exchange tube 62 and flows into the first U-shaped tube 63. Inside the first U-shaped tube 63, an internal U-shaped tube 67 guides the flow. Simultaneously, the first partition groove 671 contains a special gas that prevents heat loss. This gas effectively separates the pre-conditioned wastewater from the outer tube wall, ensuring that the pre-conditioned wastewater flows only within the internal U-shaped tube 67. This design effectively prevents the pre-conditioned wastewater, which has already absorbed some heat, from directly contacting the excessively cold outer tube wall, thus avoiding a significant drop in temperature due to excessive heat dissipation and ensuring the stability and efficiency of subsequent heat exchange processes.
[0052] S14: After being guided by the built-in U-shaped tube 67, the pre-conditioned cold wastewater smoothly enters the heat exchange tube 62 in the anode chamber 711 of the second diaphragm electrolyzer 72, and then passes through the heat exchange path of the inner tube inlet-outlet hole 681 spraying out of the outer ring second partition groove 683, and performs a second heat exchange with the electrolyte in the anode chamber 711, carrying away a large amount of excess heat generated by the oxygen evolution overpotential and Joule heating in the anode chamber 711.
[0053] S15: Subsequently, the pre-conditioned cold wastewater enters the heat exchange tube 62 in the cathode chamber 715 of the first diaphragm electrolytic cell 71 via the second U-shaped tube 64 to complete the third heat exchange. Then, it enters the heat exchange tube 62 in the anode chamber 711 of the first diaphragm electrolytic cell 71 via the third U-shaped tube 65 to complete the fourth heat exchange. By this point, the pre-conditioned cold wastewater has flowed through the heat exchange tubes 62 of the four electrode chambers in the two diaphragm electrolytic cells in sequence, absorbing the heat of each chamber evenly. Finally, after completing all four heat exchanges, the pre-conditioned cold wastewater returns to the regulating tank 22 via the outlet pipe 66 and its internal built-in U-shaped tube 67, thus forming a complete series heat exchange cycle.
[0054] S2: Adjusting component 2 adjusts the pH of the internal electroplating wastewater, adds hydrogen peroxide and stirs it, and then sends it into the filter component 3.
[0055] S21: The preheated electroplating wastewater is pumped from the wastewater tank 1 by the first water pump 12 and sent to the regulating tank 22. The liquid level sensor 24 monitors the water level of the wastewater in the tank in real time. When the water level reaches the set high limit, the first water pump 12 stops pumping and automatically closes the first outlet valve pipe 11 to prevent overflow. When the water level drops to the low limit, the water inlet is triggered to replenish the water. The pH detection sensor 25 continuously measures the pH value of the wastewater and determines whether acid or alkali needs to be added based on the pH value of the wastewater.
[0056] S22: Acid tank 26 and alkali tank 27 store dilute sulfuric acid and sodium hydroxide solutions respectively. The pH value fed back by the pH sensor 25 is compared with the set target pH range. If the measured pH is higher than the upper limit of the target, the discharge valve 23 of acid tank 26 will open automatically to add acid solution to the regulating tank 22. If the measured pH is lower than the lower limit of the target, the discharge valve 23 of alkali tank 27 will open to add alkali solution to the tank. The opening time of the discharge valve 23 can be automatically adjusted until the wastewater reaches the set slightly acidic requirement.
[0057] S23: The hydrogen peroxide tank 28 stores a certain concentration of hydrogen peroxide solution. According to the process settings, the discharge valve 23 at the outlet of the hydrogen peroxide tank 28 is controlled to slowly inject hydrogen peroxide into the regulating tank 22 in proportion. The addition of hydrogen peroxide can preliminarily oxidize some organic complexes in the wastewater at room temperature, destroy their structure, reduce the burden of subsequent ozone catalytic oxidation, and also help to regulate the oxidation-reduction potential of the wastewater.
[0058] S24: To ensure that the added acid, alkali, and hydrogen peroxide are thoroughly and evenly mixed with the wastewater, and to avoid local concentrations that are too high or too low, the motor is started. The motor output drives the rotating shaft 212 to rotate, and the rotating shaft 212 drives the rotating blade 213 to rotate at a certain speed, creating strong turbulence in the tank, which rapidly and evenly mixes the wastewater, acid, alkali, and hydrogen peroxide. S3: Filter component 3 filters suspended particles and separates wastewater into ionic heavy metal wastewater and complexed heavy metal wastewater.
[0059] S4: Ionic heavy metal wastewater is sent into the electrolysis unit 7, while complexed heavy metal wastewater is sent into the reaction unit 5. The reaction unit 5 reacts the complexed heavy metal wastewater with ozone and catalyst to release metal ions into a free state, and then sends the free metal ion solution after the reaction into the electrolysis unit 7.
[0060] S5: Electrolysis unit 7 electrolyzes free metal ion solutions and ionic heavy metal wastewater to collect high-purity metal elements and discharge the remaining wastewater.
[0061] S51: The second diaphragm electrolyzer 72 receives the broken-complex wastewater from the sixth outlet valve pipe 57 (which also enters its anode chamber 711), and the first diaphragm electrolyzer 71 receives the ionized permeate from the fourth outlet valve pipe 37 (which directly enters its anode chamber 711). Under the electric field driven by the DC power supply, the oxidation reaction of water occurs in the anode chamber 711 of both electrolyzers. The generated oxygen escapes from the solution, and the generated hydrogen ions keep the anode chamber 711 in an acidic environment. This is beneficial to maintain the metal ions in a stable free state and prevent their hydrolysis and precipitation.
[0062] S52: Simultaneously, under the influence of the electric field, the metal cations in the anode chamber 711 migrate directionally through the cation exchange membrane 713 to the cathode chamber 715. Meanwhile, the anions in the solution and any residual organic molecules are effectively blocked by the cation exchange membrane 713 in the anode chamber 711 and cannot enter the cathode chamber 715, thus ensuring the high purity of the cathode product. The metal cations that migrate to the cathode chamber 715 gain electrons on the surface of the cathode plate 714, are reduced to metal atoms, and are deposited layer by layer. As the electrolysis time increases, a dense, flat, and high-purity metal plate is gradually formed on the cathode plate 714. After electrolysis, the effluent from the anode chamber 711 of the two electrolytic cells is discharged through the corresponding first valve 73, and the effluent from the cathode chamber 715 is discharged through the second valve 74. All the effluent is finally collected in the main drain pipe 75 and sent to the subsequent advanced treatment system.
[0063] It should be noted that, in this document, relational terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such process, method, article, or apparatus.
[0064] Finally, it should be noted that the above descriptions are merely preferred embodiments of the present invention and are not intended to limit the present invention. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.
Claims
1. An electrochemical co-treatment device for electroplating wastewater, comprising a wastewater tank (1), characterized in that, The wastewater tank (1) is provided with an adjustment component (2) for adjusting the acidity and alkalinity of the wastewater on one side. The adjustment component (2) is provided with a first support frame (4) on one side. The first support frame (4) is divided into a first layer, a second layer and a third layer from top to bottom. The first layer and the second layer of the first support frame (4) are provided with a filter component (3) for filtering and separating the wastewater. The filter component (3) is provided with a reaction component (5) for reacting the wastewater with ozone on one side. The third layer of the first support frame (4) is provided with a heat exchange component (6) for electrolyzing the wastewater. The heat exchange component (6) is provided with an electrolysis component (7) for exchanging heat between the electrolyzed hot wastewater and the acidity and alkalinity-adjusting cold wastewater. The wastewater tank (1) is fixedly connected to a first outlet valve pipe (11) at its outlet end. The regulating component (2) includes a second support frame (21) located on one side of the wastewater tank (1). An regulating box (22) is fixedly connected inside the second support frame (21). A first water pump (12) is fixedly connected to one side of the second support frame (21). The electrolysis component (7) includes a first diaphragm electrolysis cell (71) and a second diaphragm electrolysis cell (72) fixedly connected inside the first support frame (4). The heat exchange component (6) includes a third inlet pipe (61) fixedly connected to the output end of the first water pump (12). The output end of the third inlet pipe (61) passes through the second diaphragm electrolysis cell (72). The interiors of the first diaphragm electrolysis cell (71) and the second diaphragm electrolysis cell (72) are divided into an anode chamber (711) and a cathode chamber (715). A heat exchange tube (62) is fixedly connected inside each anode chamber (711) and anode plate (712).
2. The electrochemical co-treatment device for electroplating wastewater according to claim 1, characterized in that, One end of the heat exchange tube (62) inside one of the cathode chambers (715) is fixedly connected to the output end of the third water inlet pipe (61), and the other end is fixedly connected to a first U-shaped tube (63). The other end of the first U-shaped tube (63) passes through the second diaphragm electrolytic cell (72) and is fixedly connected to the heat exchange tube (62) inside one of the anode chambers (711).
3. The electrochemical co-treatment device for electroplating wastewater according to claim 2, characterized in that, One of the heat exchange tubes (62) inside the anode chamber (711) is fixedly connected to the other end of a second U-shaped tube (64), the output end of the second U-shaped tube (64) passes through the first diaphragm electrolytic cell (71), and one end of the heat exchange tube (62) inside the cathode chamber (715) is fixedly connected to the output end of the second U-shaped tube (64).
4. The electrochemical co-treatment device for electroplating wastewater according to claim 3, characterized in that, One end of the heat exchange tube (62) inside the other cathode chamber (715) is fixedly connected to a third U-shaped tube (65), the other end of which passes through the first diaphragm electrolytic cell (71). One end of the heat exchange tube (62) inside the other anode chamber (711) is fixedly connected to the output end of the third U-shaped tube (65). The other end of the heat exchange tube (62) inside the other anode chamber (711) is fixedly connected to a water outlet pipe (66), the output end of which passes through the regulating box (22).
5. The electrochemical co-treatment device for electroplating wastewater according to claim 4, characterized in that, The first U-shaped tube (63), the second U-shaped tube (64), the third U-shaped tube (65) and the outlet tube (66) are all fixedly connected with built-in U-shaped tubes (67). The interior of the first U-shaped tube (63), the second U-shaped tube (64), the third U-shaped tube (65) and the outlet tube (66) are all separated by built-in U-shaped tubes (67) with first partition grooves (671). The interior of each heat exchange tube (62) is fixedly connected with a built-in water pipe (68). One end of each built-in water pipe (68) is provided with a water inlet hole (682). The other end of each built-in water pipe (68) is provided with a closed end. Several water outlet holes (681) are evenly provided on the outside of each built-in water pipe (68). The interior of each heat exchange tube (62) is separated by built-in water pipes (68).
6. The electrochemical co-treatment device for electroplating wastewater according to claim 1, characterized in that, The filter assembly (3) includes a second outlet valve pipe (31) fixedly connected to the lower end of the regulating box (22), a charged nanofiltration membrane barrel (36) fixedly connected to the second layer of the first support frame (4), a security filter (34) fixedly connected to the first layer of the first support frame (4), a second water pump (32) fixedly connected to the outside of the charged nanofiltration membrane barrel (36), the input end of the second water pump (32) fixedly connected to the output end of the second outlet valve pipe (31), and the output end of the second water pump (32) fixedly connected to the first inlet pipe (33).
7. The electrochemical co-treatment device for electroplating wastewater according to claim 6, characterized in that, The output end of the first inlet pipe (33) is fixedly connected to the input end of the security filter (34). The output end of the security filter (34) is fixedly connected to the third outlet valve pipe (35). The output end of the third outlet valve pipe (35) is fixedly connected to the input end of the charged nanofiltration membrane tank (36). The outside of the charged nanofiltration membrane tank (36) is provided with a first output end and a second output end. The first output end is fixedly connected to the fourth outlet valve pipe (37).
8. The electrochemical co-treatment device for electroplating wastewater according to claim 7, characterized in that, The reaction assembly (5) includes an ozone reaction tower (56) fixedly connected inside the first support frame (4). A third water pump (53) is fixedly connected to the outside of the ozone reaction tower (56). A fifth water outlet valve pipe (54) is fixedly connected to the input end of the third water pump (53). The input end of the fifth water outlet valve pipe (54) is fixedly connected to the second output end of the charged nanofiltration membrane tank (36). A second water inlet pipe (51) is fixedly connected to the output end of the third water pump (53). The output end of the second water inlet pipe (51) is fixedly connected to the water inlet end of the ozone reaction tower (56).
9. The electrochemical co-treatment device for electroplating wastewater according to claim 8, characterized in that, The outlet end of the ozone reaction tower (56) is fixedly connected to a sixth outlet valve pipe (57). An ozone generator (55) is provided on one side of the ozone reaction tower (56). The outlet end of the ozone generator (55) is connected to the inlet end pipe of the ozone reaction tower (56). An outlet pipe (52) is provided on the upper side of the ozone reaction tower (56).
10. A method for operating an electrochemical co-treatment device for electroplating wastewater, using one of the methods described in any one of claims 1-9, characterized in that, Includes the following steps: S1: The wastewater tank (1) stores electroplating wastewater. The electroplating wastewater passes through the heat exchange component (6) and the electrolysis component (7). The pre-conditioned cold wastewater and the electrolytic hot wastewater exchange heat, and the electroplating wastewater with increased temperature is transported to the conditioning component (2). S2: The regulating component (2) adjusts the pH of the internal electroplating wastewater, adds hydrogen peroxide and stirs it, and sends it into the filter component (3); S3: The filter assembly (3) filters suspended particles and separates wastewater into ionic heavy metal wastewater and complexed heavy metal wastewater; S4: Ionic heavy metal wastewater is sent into the electrolysis unit (7), while complexed heavy metal wastewater is sent into the reaction unit (5). The reaction unit (5) reacts the complexed heavy metal wastewater with ozone and catalyst to release metal ions into free state, and sends the free metal ion solution after the reaction into the electrolysis unit (7). S5: Electrolysis component (7) electrolyzes free metal ion solution and ionic heavy metal wastewater to collect high-purity metal elements and discharge the remaining wastewater.