A zero-discharge treatment device and method for regenerating wastewater of a hydrogen peroxide device

Abstract

The application discloses a zero-emission treatment device and method for regenerating wastewater of a hydrogen peroxide device, which comprises a full-automatic control unit, a collecting unit, a conveying unit, a membrane concentration and purification unit, a separation unit, a low-temperature evaporation unit and a recovery unit arranged on a base. Through a full-automatic closed-loop treatment process, the application realizes water pollution control and treatment by pure physical treatment, does not add chemical agents in the whole process, eliminates palladium catalyst poisoning from the source, greatly improves the recovery rate of working liquid, reduces material loss, simultaneously eliminates explosion and VOCs pollution hidden dangers by full nitrogen inerting and negative pressure low-temperature evaporation, reduces the land occupation by miniaturizing the equipment, adds passive self-cleaning, does not need electric heating equipment to meet the explosion-proof requirement, prolongs the membrane service life by double anti-blocking, optimizes the separation efficiency of water pollution control and treatment, realizes full-automatic interlocking unattended operation, recycles all wastewater and aromatic hydrocarbon working liquid, realizes zero wastewater discharge, realizes all-round landing full-process water pollution control and treatment, and greatly reduces the environmental protection operation and maintenance cost.

Description

Technical Field

[0001] This invention relates to the field of hydrogen peroxide wastewater filtration technology, specifically to a zero-discharge treatment device and method for regenerated wastewater from a hydrogen peroxide plant. Background Technology

[0002] Hydrogen peroxide production uses a working fluid as a circulating carrier and processes such as hydrogenation, oxidation, and extraction to indirectly synthesize hydrogen peroxide solution from hydrogen and oxygen. The following wastewater is generated during hydrogen peroxide production: 1. The wastewater from the regenerated alumina bed mainly consists of: working fluid, alumina dust, and degradation products; 2. The wastewater from catalyst regeneration mainly consists of: working fluid, catalyst dust, alumina dust, and degradation products; 3. The main components of the wastewater discharged from the hydrogenation tower and oxidation tower are: working fluid and degradation products; 4. Other wastewater, mainly wastewater generated from rinsing, alkali tower, and preparation processes, has no recycling value.

[0003] Components 1, 2, and 3 in the above wastewater contain a certain amount of working fluid and are therefore valuable for recycling. This is of great significance for reducing the consumption of production equipment, alleviating the treatment load of the wastewater treatment plant, reducing treatment costs, and improving the inherent safety level of the equipment.

[0004] Currently, the following problems still exist regarding water pollution and treatment for this device: I. The existing process involves collecting all production wastewater into a unified equalization tank. The high-turbidity, high-alkalinity, and high-temperature regenerated wastewater carries emulsified working fluid. After being settled in a gravity sedimentation tank to separate the upper working fluid, the remaining wastewater is still discharged into the unified equalization tank. The wastewater contains impurities such as metal ions, sulfides, and sulfate, which can cause irreversible poisoning of the palladium catalyst. Therefore, the working fluid after sedimentation and separation is completely unusable and can only be disposed of as hazardous waste. In the working fluid cooking and regeneration process, the working fluid forms a stable emulsion with dust and water. The conventional 7-day settling time cannot achieve complete separation, and even if the settling time is extended to 30 days, the separation is still incomplete. At the same time, low-boiling-point aromatics in the working fluid continue to volatilize, requiring a large amount of activated carbon to adsorb the waste gas. This not only causes loss of working fluid materials but also brings VOCs environmental pollution. Moreover, the COD of the waste liquid is as high as tens of thousands of mg / L, putting great pressure on environmental protection. The unit price of the working fluid is as high as 100,000 yuan / ton. At present, the total circulating working fluid volume of a single 150,000-ton / year hydrogen peroxide unit is 1,000 m³, and the working fluid loss rate during the regeneration and sewage discharge process is about 1%, resulting in an annual economic loss of 1 million yuan for a single unit; there are about 200 similar units nationwide, with a total annual economic loss of over 200 million yuan. Second, the light component aromatic hydrocarbons in the working fluid in the pool continue to volatilize, which can easily accumulate inside the pool to form an explosive mixture of gases, posing an explosion risk. The sewage treatment equipment occupies too large a space, with dual safety and environmental hazards. The automation level is low, the reliance on manual labor is high, and it does not meet the requirements for the control of hazardous chemicals. Third, the existing wastewater treatment system requires a hydraulic retention time of more than 4 hours. The total volume of the flocculation tank and air flotation machine for the 150,000-ton / year capacity unit exceeds 10m³. The equipment has a large liquid holding capacity and the overall footprint exceeds the standard. The safety distance between the compression units is also a concern. At the same time, the system has multiple leakage risks, coupled with the continuous VOCs solvent volatilization problem, which simultaneously creates dual safety and environmental hazards. Fourth, the core processes of wastewater treatment (air flotation, flocculation sedimentation, and plate and frame filter press) all rely on manual visual judgment of treatment effects and manual disassembly and unloading of plates. The entire process cannot be automated without human intervention. Each wastewater treatment plant requires at least 6 on-site operators to complete the entire process of chemical preparation, process adjustment, filter press unloading, etc. On the one hand, the large fluctuations in manual operation lead to unstable wastewater treatment conditions and significant fluctuations in treatment efficiency. On the other hand, it does not meet the safety production control requirements of reducing personnel in hazardous chemical processes.

[0005] Therefore, we have made improvements to this and proposed a zero-discharge treatment device and method for wastewater regeneration from hydrogen peroxide devices. Summary of the Invention

[0006] In view of the problems in the above-mentioned or existing technologies, such as the difficulty in separating emulsions of working fluids, the inability to reuse them due to impurities, huge economic losses of materials, the safety hazards of gas explosions on site, the large footprint of wastewater treatment facilities, the high risk of leakage and VOCs pollution, the low degree of automation and high dependence on manual labor, and the failure to meet the requirements for the management of hazardous chemicals, this invention is proposed.

[0007] Therefore, the purpose of this invention is to provide a zero-discharge treatment device for wastewater regeneration from a hydrogen peroxide plant.

[0008] To solve the above-mentioned technical problems, the present invention provides the following technical solution, including: The fully automatic control unit, collection unit, conveying unit, membrane concentration and purification unit, separation unit, low-temperature evaporation unit, and recovery unit are installed on the base; The fully automatic control unit is electrically connected to the collection unit, conveying unit, membrane concentration and purification unit, separation unit, low-temperature evaporation unit, and recovery unit via signal transmission cables. The wastewater discharge outlet of the collection unit is connected to the conveying unit via a sealed metal pipeline to transport wastewater. The liquid outlet of the conveying unit is connected to the liquid inlet of the membrane concentration and purification unit. The liquid outlet of the membrane concentration and purification unit is connected to the separation unit to transport liquid centrifugation separation. The liquid outlet of the separation unit is connected to the low-temperature evaporation unit. The two discharge pipelines of the low-temperature evaporation unit are respectively connected to the recovery unit to transport high-concentration aromatics and condensed clean distillate. The fully automatic control unit is an explosion-proof PLC control cabinet; The separation unit is a centrifuge for wastewater processing; A main nitrogen pipe is also installed, from which multiple nitrogen branch pipes are connected to the collection unit, the conveying unit, the membrane concentration and purification unit, the separation unit, the low-temperature evaporation unit, and the recovery unit. The interconnected chambers form a micro-positive pressure environment of 0.01~0.03MPa. No demulsifying or flocculant chemicals are added to the entire device, and the total liquid holdup of the system is ≤0.5m³. The membrane concentration and purification unit has an integrated linkage pressure-resistant self-cleaning heating unit and a heating unit.

[0009] As a preferred embodiment of the zero-discharge treatment device and method for regenerated wastewater from the hydrogen peroxide unit of the present invention, the collection unit includes a nitrogen-sealed buffer tank for wastewater collection. A first high-temperature resistant magnetic conveying pump for introducing wastewater is installed outside the nitrogen-sealed buffer tank. A branch pipe for external connection of the alumina bed, catalyst, hydrogenation, and oxidation tower sewage discharge pipeline is installed on the first high-temperature resistant magnetic conveying pump. The outside of the nitrogen-sealed buffer tank is also connected to the outside of the conveying unit.

[0010] As a preferred embodiment of the zero-discharge treatment device and method for regenerated wastewater from the hydrogen peroxide unit of the present invention, the conveying unit is adapted to wastewater with a temperature ≤100℃ and a solid content ≥2000mg / L. The conveying unit includes a second high-temperature resistant magnetic conveying pump installed outside a nitrogen-sealed buffer tank. A main pipeline for liquid transmission is fixedly installed at the output end of the second high-temperature resistant magnetic conveying pump. An electromagnetic flow meter and a pressure transmitter are sequentially installed on the main pipeline, and the signal transmission cables of the electromagnetic flow meter and the pressure transmitter are connected to a fully automatic control unit. One end of the main pipeline is installed on the external phase of the membrane concentration and purification unit.

[0011] As a preferred embodiment of the zero-discharge treatment device and method for the hydrogen peroxide device regeneration wastewater of the present invention, the membrane concentration and purification unit includes a purification box connected to the liquid outlet of the main pipeline. The membrane concentration and purification unit also includes a catalyst transporter loaded with palladium and titanium, an ultraviolet lamp, and an ultrasonic transducer, all integrated in the water inlet area of ​​the purification chamber. The ultraviolet lamp and ultrasonic transducer are electrically connected to the fully automatic control unit via signal cables. A filter frame is fixed at an incline downstream of the inner cavity of the purification chamber. A ceramic membrane is mounted on the filter frame. The surface of the ceramic membrane is coated with a hydrophilic and oleophobic coating. The outlet of the purification chamber is connected to the centrifuge inlet of the separation unit through a sealed pipeline. The centrifuge outlet pipeline is connected to the feed end of the low-temperature evaporation unit.

[0012] As a preferred embodiment of the zero-discharge treatment device and method for the regeneration wastewater of the hydrogen peroxide unit of the present invention, the low-temperature evaporation unit includes a vacuum scraper evaporator fixedly installed at one end of the centrifuge outlet of the separation unit, and the vacuum scraper evaporator operates in the temperature range of 60~80℃. The main shaft of the vacuum scraper evaporator is fixedly equipped with an anti-static polytetrafluoroethylene scraper. The inner wall of the vacuum scraper evaporator is provided with an anti-static rod. The gas phase outlet pipeline of the vacuum scraper evaporator is connected to a two-stage shell-and-tube condenser, and the return pipeline of the two-stage shell-and-tube condenser is connected to the bottom of the vacuum scraper evaporator. At the same time, the vacuum scraper evaporator is connected to the vacuum unit pipeline and the nitrogen distribution pipeline respectively. The two independent discharge pipelines at the bottom of the vacuum scraper evaporator are installed on the external phase of the recovery unit.

[0013] As a preferred embodiment of the zero-discharge treatment device and method for the regeneration wastewater of the hydrogen peroxide unit of the present invention, the recovery unit includes a working fluid reuse tank that collects high-concentration aromatic hydrocarbons and a distillate water storage tank that collects condensed clean distillate water, respectively connected to two independent discharge pipelines at the bottom of the vacuum scraper evaporator. The working fluid reuse tank and the distillate water storage tank are respectively equipped with reflux pumps for material external transfer and reuse at the bottom. Both the working fluid reuse tank and the distillate water storage tank are equipped with liquid level detection elements, which are electrically connected to the fully automatic control unit through signal transmission cables.

[0014] As a preferred embodiment of the zero-discharge treatment device and method for the regeneration wastewater of the hydrogen peroxide device of the present invention, wherein: the inner cavity of the purification box is provided with an integrated linkage pressure-resistant self-cleaning heating unit, the heating unit is assembled on the outside of the integrated linkage pressure-resistant self-cleaning heating unit, and the heating unit and the integrated linkage pressure-resistant self-cleaning heating unit are in transmission cooperation.

[0015] As a preferred embodiment of the zero-discharge treatment device and method for regenerated wastewater from the hydrogen peroxide device of the present invention, the integrated linkage pressure-resistant self-cleaning heating unit includes a pressure-bearing support frame fixedly embedded in the inner cavity of the purification box. The pressure-bearing support frame has a coaxially arranged movable hole in the middle. A sealed bearing is provided in the movable hole. The transmission rod is rotatably inserted into the movable hole through the sealed bearing. A fluid-driven conveying wheel is fixedly provided at the top of the transmission rod. A spiral guide block is fixedly provided in the purification box above the fluid-driven conveying wheel. A wave-shaped blade scraper wheel is fixedly installed at the bottom of the transmission rod. The wave-shaped blade scraper wheel is fitted with the hydrophilic and oleophobic coating of the ceramic membrane. The transmission rod is connected to the heating unit.

[0016] As a preferred embodiment of the zero-discharge treatment device and method for the regeneration wastewater of the hydrogen peroxide device of the present invention, the heating unit includes an assembly ring fixedly sleeved on the outside of the transmission rod. The assembly ring is arranged in a ring array with multiple sets of elastic expansion members. Each set of elastic expansion members has a wave-shaped friction plate fixedly installed at its end. A ring-shaped heat-conducting ring is coaxially fixed to the inner wall of the purification box. The wave-shaped friction plate is tightly attached to the inner wall of the heat-conducting ring by the elastic force of the elastic expansion members.

[0017] Zero-discharge treatment methods for wastewater from hydrogen peroxide unit regeneration include: S1. Nitrogen gas is introduced into the collection unit, conveying unit, membrane concentration and purification unit, separation unit, low temperature evaporation unit and recovery unit through the main nitrogen pipe and nitrogen branch pipes to create a micro positive pressure environment of 0.01~0.03MPa in each chamber. No demulsifying agent or flocculant is added to the entire process. The fully automatic control unit monitors the operating conditions of the entire device. The regenerated wastewater discharged from S2, alumina bed, catalyst, hydrogenation tower, and oxidation tower is passed through a branch pipe into the nitrogen-sealed buffer tank of the collection unit for sealed temporary storage. S3. The second high-temperature magnetic conveying pump of the conveying unit transports the buffered wastewater to the membrane concentration and purification unit through the main pipeline. The electromagnetic flow meter and pressure transmitter collect the pipeline flow and pressure signals and feed them back to the fully automatic control unit. S4. Wastewater enters the purification tank. The spiral guide block gathers the wastewater fluid and impacts the fluid-driven conveyor wheel. Relying on fluid power, the transmission rod rotates without external power. The pressure support frame counteracts the high-pressure filtration impact inside the purification tank. The transmission rod drives the wave-shaped blade scraper wheel to scrape the ceramic membrane surface circumferentially. At the same time, the transmission rod is linked to the heating unit to operate. The wave-shaped friction plate rubs against the annular heat-conducting ring to generate frictional heat. Simultaneously, the catalyst transfer device, ultraviolet lamp tube, and ultrasonic transducer inside the purification tank are turned on to treat the wastewater medium in a coordinated manner. S5. The modified wastewater undergoes solid-liquid separation through an inclined ceramic membrane, and the separated liquid phase material is then introduced into the separation unit. S6. The centrifuge in the separation unit centrifuges the membrane filtered water to remove residual fine aromatic hydrocarbon impurities from the water. S7. After centrifugation, the material is sent to the vacuum scraper evaporator of the low-temperature evaporation unit. The anti-static PTFE scraper removes the material adhering to the inner wall of the evaporator. The static elimination rod eliminates the static electricity during equipment operation. The gaseous medium generated by the evaporator is passed into a two-stage shell-and-tube condenser for condensation. The condensed material flows back to the bottom of the vacuum scraper evaporator. S8. The vacuum scraper evaporator delivers high-concentration aromatic materials and condensed clean distillate water to the working fluid reuse tank and the distillate water storage tank respectively through two independent discharge pipelines. S9. The liquid level detection element inside the recycling unit collects the liquid level signal of the storage tank and transmits it to the fully automatic control unit. After the set liquid level threshold is reached, the corresponding return conveying pump is started to complete the material delivery and realize zero discharge treatment of wastewater.

[0018] Beneficial effects This invention adopts a fully enclosed nitrogen-inert modular structure, employing purely physical processing without the addition of flocculants or demulsifiers. This eliminates the risk of palladium catalyst poisoning caused by metallic impurities, thus strengthening the source of water pollution control and treatment. The combination of hydrophilic and oleophobic modified ceramics with ultraviolet and ultrasonic synergistic treatment eliminates the need for prolonged settling, significantly improving separation efficiency. The working fluid recovery rate reaches 99.2%, saving millions of yuan in material losses annually for a single 150,000-ton-per-year unit. The total liquid holding capacity of the system is only 0.42 m³, reducing the footprint by 75%. This eliminates the need for large civil engineering water tanks, lowering infrastructure investment in water pollution control and treatment. Combined with negative pressure low-temperature evaporation and full-process explosion-proof PLC automatic interlocking, it eliminates the dual hazards of aromatic hydrocarbon explosions and VOCs volatilization. No six-person on-site monitoring is required. All distillate and concentrated working fluid are reused, truly achieving zero discharge of regenerated wastewater. This comprehensively meets the environmental compliance requirements for water pollution control and treatment in the chemical industry, balancing multiple needs for safety, environmental protection, and cost reduction. 2. This device is equipped with a fluid-driven passive heating component, which integrates membrane scraping, pressure protection, and friction heating by relying on the kinetic energy of the wastewater inlet. It does not require external electric heating equipment, is fully compatible with Class A explosion-proof area safety regulations, avoids the risk of electrical fire and explosion, eliminates the risk of secondary pollution, and ensures the safe and stable operation of the water pollution control and treatment system. The 55~65℃ gradient heating effectively reduces the viscosity of anthraquinone aromatics. Combined with mechanical membrane scraping and ultraviolet ultrasound, it forms a dual anti-clogging mechanism, which greatly extends the service life of the ceramic membrane. At the same time, the passive heating mode and the low-temperature evaporation at the back end form a matching temperature gradient, reducing the energy consumption of the evaporation heat source. The entire set of components is integrated inside the purification tank, without occupying additional space or increasing power consumption. It further improves the demulsification and separation effect of highly emulsified wastewater, strengthens the water pollution control and treatment capabilities of the core section, and reduces the long-term operation and maintenance costs of the equipment. 3. This invention features a fully automated closed-loop treatment process. Relying on nitrogen pressure stabilization and real-time interlocking of pressure and liquid levels in each process, it can automatically alarm and shut down in case of malfunction, constructing a fully automated, unattended water pollution control and treatment system. Wastewater undergoes multi-stage synergistic treatment, including classification and buffering, membrane purification, centrifugal impurity removal, and negative pressure evaporation, accurately separating and recovering reusable working fluid and clean distillate water, achieving closed-loop material circulation and zero wastewater discharge. The equipment adopts a centrifugal automatic closed slag discharge and storage tank level linkage pumping mode, completely eliminating all on-site manual positions for dosing, filtration, and unloading, requiring only remote monitoring from the central control unit. This meets the requirements for minimally manned management of hazardous chemical processes. The entire system can operate stably for 90 consecutive days, maintaining stable treatment indicators even under harsh conditions of high COD and high solids content in the influent, ensuring long-term, stable, and compliant industrial water pollution control and treatment effects, and exhibiting extremely strong industrial adaptability. Attached Figure Description

[0019] 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 a zero-discharge treatment device for regenerated wastewater from a hydrogen peroxide unit according to the present invention. Figure 2 This is a schematic diagram of the assembly structure of the collection unit and the conveying unit of a zero-discharge treatment device for regenerated wastewater from a hydrogen peroxide device according to the present invention. Figure 3 This is a schematic diagram of the internal structure of the membrane concentration and purification unit of a zero-discharge treatment device for regenerated wastewater from a hydrogen peroxide unit according to the present invention. Figure 4 This is a schematic diagram of the low-temperature evaporation unit structure of a zero-discharge treatment device for regenerated wastewater from a hydrogen peroxide device according to the present invention. Figure 5 This is a schematic diagram of the recovery unit structure of a zero-discharge treatment device for regenerated wastewater from a hydrogen peroxide unit according to the present invention. Figure 6 This is a schematic diagram of the heating unit assembly structure of a zero-discharge treatment device for regenerated wastewater from a hydrogen peroxide device according to the present invention. Figure 7 This is a flowchart of a zero-discharge treatment method for regeneration wastewater from a hydrogen peroxide device according to the present invention.

[0020] In the picture: 1. Fully automatic control unit; 2. Collection unit; 201. Nitrogen gas sealed buffer tank; 202. First high-temperature resistant magnetic transfer pump; 203. Diversion branch pipe; 3. Conveying unit; 301. Second high-temperature resistant magnetic conveying pump; 302. Main pipeline; 303. Electromagnetic flow meter; 304. Pressure transmitter; 4. Membrane concentration and purification unit; 401. Purification box; 402. Filter frame; 403. Ceramic membrane; 404. Hydrophilic and oleophobic coating; 405. Catalyst transfer device; 406. Ultraviolet lamp tube; 407. Ultrasonic transducer; 5. Separation unit; 6. Low-temperature evaporation unit; 601. Vacuum scraped evaporator; 602. Antistatic PTFE scraper; 603. Static eliminator rod; 604. Two-stage shell-and-tube condenser; 7. Recovery unit; 701. Working fluid reuse storage tank; 702. Distillate water storage tank; 703. Return transfer pump; 8. Integrated linkage pressure-resistant self-cleaning heating unit; 801. Pressure-bearing support frame; 802. Movable hole; 803. Transmission rod; 804. Conveying wheel; 805. Guide block; 806. Wave-shaped blade scraper wheel; 9. Heating unit; 901. Assembly ring; 902. Elastic expansion joint; 903. Corrugated friction plate; 904. Heat-conducting ring. Detailed Implementation

[0021] The preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are for illustration and explanation only and are not intended to limit the present invention.

[0022] Example 1, refer to Figures 1 to 6 ; Specifically, a zero-discharge treatment device for regeneration wastewater from a hydrogen peroxide unit is provided, comprising: The fully automatic control unit 1, collection unit 2, conveying unit 3, membrane concentration and purification unit 4, separation unit 5, low temperature evaporation unit 6, and recovery unit 7 are installed on the base; The fully automatic control unit 1 is electrically connected to the collection unit 2, the conveying unit 3, the membrane concentration and purification unit 4, the separation unit 5, the low-temperature evaporation unit 6, and the recovery unit 7 via signal transmission cables. The fully automatic control unit 1 is an explosion-proof PLC control cabinet. It is suitable for Class A explosion-proof chemical areas and has built-in multi-channel acquisition modules for temperature, pressure, liquid level, and flow. It is equipped with an audible and visual alarm module and a central control communication module. It can collect all instrument data of the entire set of equipment in real time, and automatically interlock and shut down when the threshold is exceeded. It completely replaces manual on-site duty and strengthens the whole process of water pollution control and treatment by relying on automated management and control. It solves the defects of existing sewage treatment plants that require more than 6 people to operate on-site, the unstable efficiency of manual treatment, and the large fluctuation of water pollution control and treatment effects. The wastewater discharge outlet of collection unit 2 is connected to conveying unit 3 via a sealed metal pipeline to transport wastewater. The liquid outlet of conveying unit 3 is connected to the liquid inlet of membrane concentration and purification unit 4. The liquid outlet of membrane concentration and purification unit 4 is connected to separation unit 5 to transport liquid for centrifugal separation. The liquid outlet of separation unit 5 is connected to low-temperature evaporation unit 6. The two discharge pipelines of low-temperature evaporation unit 6 are respectively connected to recovery unit 7 to transport high-concentration aromatic hydrocarbons and condensed clean distillate. Collection Unit 2 includes a nitrogen-sealed buffer tank 201 for wastewater collection. The nitrogen-sealed buffer tank 201 has a volume of 0.12 m³. Nitrogen is introduced into the tank through the main nitrogen pipe to maintain a slight positive pressure of 0.02 MPa. The entire process is sealed without any openings, eliminating the safety hazards of VOCs and explosive mixtures generated by the volatilization of aromatics in existing gravity sedimentation tanks. This fundamentally solves the problem of explosions caused by the accumulation of aromatic mixtures in open equalization tanks and sedimentation tanks. At the same time, it reduces secondary water pollution associated with waste gas and improves the front-end water pollution control and treatment capabilities. The nitrogen-sealed buffer tank 201 can withstand a maximum medium temperature of 98℃, making it suitable for high-temperature inlet conditions after the regenerated wastewater has been boiled. The nitrogen-sealed buffer tank 201 is externally equipped with a first high-temperature resistant magnetic transfer pump 202 for introducing wastewater. The first high-temperature resistant magnetic transfer pump 202 is equipped with a branch pipe 203 for connecting the external alumina bed, catalyst, hydrogenation, and oxidation tower sewage discharge pipelines. The branch pipe 203 is simultaneously connected to four types of waste generation points: the sewage discharge pipeline of the regenerated alumina bed, the sewage discharge pipeline of the regenerated catalyst, the sewage discharge pipeline of the hydrogenation tower, and the sewage discharge pipeline of the oxidation tower.

[0023] The first high-temperature magnetic transfer pump 202 is used to collect the four types of recyclable wastewater containing working fluid into the nitrogen-sealed buffer tank 201. The wastewater from rinsing and alkali tower that has no recycling value is diverted separately and does not enter the nitrogen-sealed buffer tank 201. This avoids the introduction of metal ions, sulfides, and sulfate impurities into the recyclable working fluid by the wastewater, prevents irreversible poisoning of the palladium catalyst, and simplifies the difficulty of subsequent water pollution control and treatment processes. The nitrogen-sealed buffer tank 201 is also externally connected to the external of the transfer unit 3. The conveying unit 3 is suitable for wastewater with a temperature ≤100℃ and a solid content ≥2000mg / L. The conveying unit 3 includes a second high-temperature resistant magnetic conveying pump 301 installed outside the nitrogen-sealed buffer tank 201. The second high-temperature resistant magnetic conveying pump 301 has a medium tolerance temperature of 0~100℃, no risk of mechanical seal leakage, and eliminates water pollution caused by pipeline leakage. It strengthens the water pollution control and treatment defense line in the conveying process and is suitable for conveying high-turbidity emulsified wastewater with a solid content of 2200~5000mg / L. The output end of the second high-temperature magnetic transfer pump 301 is fixedly installed with a main liquid transmission pipeline 302. An electromagnetic flowmeter 303 and a pressure transmitter 304 are sequentially installed on the main pipeline 302. The electromagnetic flowmeter 303 measures the wastewater feed flow rate in real time, maintaining a stable daily feed of 52 tons under the operating conditions of a single 150,000-ton / year hydrogen peroxide unit, meeting the unit's processing load. The pressure transmitter 304 monitors the pipeline pressure of the main pipeline 302 in real time. When the pipeline is blocked and the pressure exceeds 0.4 MPa, the explosion-proof PLC control cabinet automatically triggers an audible and visual alarm and shuts down the unit, avoiding the risk of sudden water pollution caused by pipeline overpressure leakage and ensuring continuous and stable water pollution control and treatment operation. The signal transmission cables of the electromagnetic flowmeter 303 and the pressure transmitter 304 are connected to the fully automatic control unit 1. One end of the main pipeline 302 is installed externally to the membrane concentration and purification unit 4. The membrane concentration and purification unit 4 includes a purification tank 401 connected to the outlet of the main pipeline 302, with a total volume of 0.15 m³. The membrane concentration and purification unit 4 also includes a palladium and titanium supported catalyst transporter 405, an ultraviolet lamp 406, and an ultrasonic transducer 407 integrated in the water inlet area of ​​the purification chamber 401. The ultraviolet lamp 406 and the ultrasonic transducer 407 are electrically connected to the fully automatic control unit 1 via signal cables. During use, the internally integrated palladium-titanium composite catalyst transporter 405, the 254nm wavelength ultraviolet lamp 406, and the 28kHz ultrasonic transducer 407 operate synchronously. A filter frame 402 is fixed at an incline downstream of the inner cavity of the purification box 401. A ceramic membrane 403 is mounted on the filter frame 402. The substrate of the ceramic membrane 403 is porous alumina ceramic with an average pore diameter of 0.1μm. A hydrophilic and oleophobic coating 404 is provided on the surface of the ceramic membrane 403. The hydrophilic and oleophobic coating 404 is a silica hydrophilic modified coating, which is applied by an impregnation high-temperature sintering process and has a coating thickness of 5~10μm. The palladium-titanium composite catalyst transport component 405 uses porous alumina filler as its carrier, with a palladium loading of 0.3% by mass and a titanium loading of 1.2% by mass. The palladium-titanium catalyst on the palladium-titanium composite catalyst transport component 405 is made of the same material as the catalyst in the hydrogen peroxide production system, and will not introduce foreign metal impurities such as iron, aluminum, and silicon to contaminate the working fluid. Unlike the traditional process of adding aluminum salts and iron salts as demulsifiers, it completely eliminates catalyst poisoning caused by impurities. The recovered working fluid can be recycled and reused normally, reducing pollutant production from the source and optimizing the water pollution control and treatment effect of the core process section. The ultraviolet light generated by the UV lamp tube 406 can break down large molecular degradation products in wastewater, reducing material viscosity. Continuous ultrasonic vibration peels away organic matter and dust particles adsorbed on the surface of the ceramic membrane 403. The ceramic membrane 403 is loaded with a hydrophilic and oleophobic coating 404. Aqueous phase penetrates the membrane pores, while emulsified working fluid and dust accumulate on the concentrate side for demulsification, achieving purely physical separation. No demulsifiers or flocculants are added throughout the process, eliminating secondary water pollution and significantly reducing the pressure on downstream water pollution control and treatment. The ceramic membrane 403 achieves a concentration ratio of up to 100:1 and can operate continuously for 365 days without permanent membrane clogging or failure. It solves the shortcomings of traditional organic membranes and ordinary ceramic filters, which are prone to clogging and failure, and cannot completely demulsify even after 30 days of static separation. It completely replaces the multi-day static settling process in gravity sedimentation tanks, eliminating the loss of aromatics due to long-term static volatilization, saving a large amount of activated carbon for waste gas adsorption, significantly reducing the difficulty of treating high-COD wastewater of tens of thousands of mg / L, and significantly improving the efficiency of water pollution control and treatment for high-concentration organic wastewater. Separation unit 5 is a closed tubular fine separator for wastewater processing. Its processing capacity matches the discharge flow rate of the front-end membrane concentration and purification unit 4. The outlet of the purification box 401 is connected to the centrifuge inlet of separation unit 5 through a closed pipeline. Centrifugal force enhances solid-liquid stratification, separating alumina, catalyst inorganic dust impurities. Impurities are periodically and automatically discharged in a closed system, preventing sludge discharge and secondary water and soil pollution. This completes the solid-liquid synergistic water pollution control and treatment system, eliminating the need for manual plate disassembly and unloading. The centrifuge chamber is connected to a nitrogen distribution pipeline to maintain a slightly positive pressure sealed environment, preventing the volatilization and leakage of aromatic hydrocarbons. This eliminates the need for manual unloading and chemical preparation in traditional filter presses. The entire unit does not require continuous on-site human supervision, solving the pain points of existing air flotation and plate and frame filter press processes that rely on manual visual judgment, frequent plate disassembly and unloading, large staffing, large fluctuations in processing conditions, and unstable water pollution control and treatment effects. The centrifuge discharge pipeline is connected to the feed end of the low-temperature evaporation unit 6. The low-temperature evaporation unit 6 includes a vacuum scraper evaporator 601 fixedly installed at one end of the centrifuge outlet of the separation unit 5. The vacuum scraper evaporator 601 operates in a temperature range of 60~80℃, with a vacuum degree of -0.07~-0.09MPa, and a stable evaporation temperature control of 70℃. The negative pressure lowers the boiling point of aromatics. An anti-static PTFE scraper 602 is fixedly installed on the main shaft of the vacuum scraper evaporator 601. Static elimination rods 603 are provided on the inner wall of the vacuum scraper evaporator 601. These, along with the anti-static PTFE scraper 602 continuously scraping away material from the cylinder wall and the static elimination rods 603 eliminating static electricity from material friction, combined with a slight positive pressure of nitrogen to isolate air, completely avoids the risk of explosion during atmospheric pressure evaporation of aromatics. The gas phase outlet pipe of the vacuum scraper evaporator 601 is connected to a two-stage shell-and-tube condenser 604, and the return pipe of the two-stage shell-and-tube condenser 604 is connected to the bottom of the vacuum scraper evaporator 601. The vacuum unit pipeline and nitrogen distribution pipeline are connected respectively. The gaseous aromatic vapor enters the two-stage shell and tube condenser 604 for condensation. The uncondensed light components are returned to the evaporator for secondary evaporation. There is no direct discharge of aromatic waste gas. This solves the problems of aromatic volatilization pollution and high cost of activated carbon adsorption materials in the existing process. It also reduces the secondary wastewater caused by waste gas scrubbing and comprehensively improves the end-of-pipe water pollution control and treatment chain. The vacuum scraper evaporator 601 has two independent discharge pipelines at the bottom and is installed on the external phase of the recovery unit 7. The recovery unit 7 includes two independent discharge pipelines that are respectively connected to the bottom of the vacuum scraper evaporator 601, a working fluid reuse storage tank 701 for collecting high-concentration aromatic hydrocarbons, and a distillate water storage tank 702 for collecting condensed clean distillate water. The working fluid reuse storage tank 701 and the distillate water storage tank 702 are respectively equipped with a reflux transfer pump 703 for material external transfer and reuse at the bottom. The working fluid reuse storage tank 701 stores the high-purity working fluid after separation and purification, and then directly transports it back to the hydrogen peroxide hydrogenation oxidation process for recycling via the reflux transfer pump 703. A single 150,000-ton / year unit reduces working fluid loss by 1 million yuan per year, and 200 units nationwide can reduce material economic losses by about 200 million yuan per year, while simultaneously reducing the total amount of pollutant emissions and improving the overall benefits of water pollution control and treatment throughout the plant. Distillate water storage tank 702 collects condensed clean water, which can be reused in the equipment flushing and alkali preparation processes. The entire unit has no external wastewater discharge, achieving zero discharge and realizing the goal of closed-loop water pollution control and treatment. Both the working fluid recycling tank 701 and the distillate water storage tank 702 are equipped with liquid level detection elements. The liquid level detection elements are electrically connected to the fully automatic control unit 1 via signal cables. The liquid level detection elements upload the liquid level to the explosion-proof PLC control cabinet in real time. When the liquid level is high, the return transfer pump 703 is automatically started by interlocking. When the liquid level is low, the pump is automatically stopped. The entire process is automated material transfer, preventing overflow and sewage discharge from causing sudden water pollution. A main nitrogen pipeline is also installed, from which multiple nitrogen branch pipelines connect to collection unit 2, conveying unit 3, membrane concentration and purification unit 4, separation unit 5, low-temperature evaporation unit 6, and recovery unit 7. These interconnected chambers create a slightly positive pressure environment of 0.01~0.03MPa. The entire system does not require the addition of demulsifying or flocculant chemicals, resulting in no chemical waste. This simplifies water pollution control and treatment operation and maintenance. The main nitrogen pipeline is equipped with a nitrogen pressure regulating valve and a slightly positive pressure transmitter, while each unit's nitrogen branch pipeline has an independent flow-limiting valve. When the pressure in the chamber is below 0.01MPa, nitrogen is automatically replenished; when the pressure is above 0.03MPa, the explosion-proof vent valve opens, and a low-pressure nitrogen alarm interlock is included. The total liquid holding capacity of the entire device is 0.42 m³, which is far lower than the liquid holding capacity of more than 10 m³ of traditional flocculation and flotation tanks. It eliminates the need to build large civil engineering sedimentation tanks, reducing the equipment footprint by more than 75%. The modular integration of the device into an integrated base ensures that the equipment spacing meets chemical safety standards. This solves the shortcomings of traditional water treatment facilities, such as large liquid holding capacity, excessive land occupation, reduced safety spacing of devices, and multiple leakage points, which can easily lead to non-point source water pollution in the plant area. It strengthens the hardware foundation for water pollution control and treatment throughout the entire process. The entire process is sealed with nitrogen micro-positive pressure to isolate air, with no VOCs volatilization and no chemical reagents added. The recovered working fluid is free of foreign impurities and will not cause palladium catalyst poisoning. At the same time, it can also significantly reduce the cost of chemicals, activated carbon, and manual operation and maintenance of wastewater treatment plants, and reduce the investment in water pollution control and treatment operations. The device described in this application can stably treat high-temperature emulsified wastewater from hydrogen peroxide regeneration for 90 consecutive days. The influent temperature is 92℃, the solid content of the wastewater is 2800mg / L, and the influent COD is 126000mg / L. After membrane concentration and purification, centrifugal separation, and vacuum low-temperature evaporation, the working solution recovery rate is 99.2%, and the COD of the distillate is less than 50mg / L, which can be completely reused. The entire process requires no on-site human operation, relying solely on remote monitoring from the central control unit. It eliminates issues such as explosions, excessive VOCs, and catalyst poisoning. It implements integrated water pollution control and treatment across the entire process from wastewater generation, separation, evaporation, and reuse, resolving all the shortcomings of existing technologies in one go, including low separation efficiency, significant safety hazards, high operating costs, large footprint, inability to automate or operate unmanned, inability to achieve zero wastewater discharge, and poor water pollution control and treatment effects.

[0024] Example 2, see Figures 3 and 6 in the instruction manual; Based on Example 1, an integrated linkage pressure-resistant self-cleaning heating unit 8 and a heating unit 9 adapted to deep water pollution control and treatment are added; to address the issues of high viscosity anthraquinone aromatics in hydrogen peroxide regeneration wastewater, high pressure conditions of membrane filtration, and the prohibition of electric heating in Class A explosion-proof areas, this invention overcomes the shortcomings of traditional processes, such as the inability to raise the temperature on-site to reduce the viscosity of the medium, incomplete separation increasing the load on subsequent water pollution control and treatment, and the explosion hazard posed by the addition of electric heating. The medium can be heated without external power supply, which further improves the demulsification and separation efficiency of emulsified wastewater, reduces the volatilization and leaching of pollutants caused by long-term static placement at the front end, and reduces the pressure on the entire water pollution control and treatment system; it relies on the kinetic energy of the wastewater itself to achieve non-electric drive, and simultaneously completes the triple functions of membrane cavity pressure protection, continuous self-cleaning of membrane surface, and passive heating of medium. The heating range can be matched with the process parameters of the downstream low-temperature evaporation unit 6 to form a gradient heating process and reduce the energy consumption of the evaporation section; The purification chamber 401 has an integrated linkage pressure-resistant self-cleaning heating unit 8 inside. The heating unit 9 is mounted on the outside of the integrated linkage pressure-resistant self-cleaning heating unit 8. The heating unit 9 is in transmission cooperation with the integrated linkage pressure-resistant self-cleaning heating unit 8. The integrated linkage pressure-resistant self-cleaning heating unit 8 includes a pressure-bearing support frame 801 that is fixedly embedded in the inner cavity of the purification box 401; The pressure support frame 801 adopts a thickened 316L stainless steel one-piece molded structure and is welded and fixed to the inner wall of the purification tank 401. It can withstand the fluid impact load generated by membrane concentration and high-pressure filtration, prevent the filter frame 402 and ceramic membrane 403 components from being deflected and deformed under pressure, prevent membrane leakage from causing separation failure and pollutant penetration, and ensure the stable operation of water pollution control and treatment in the membrane section. The pressure support frame 801 has a coaxially arranged movable hole 802 in the middle, and a sealed bearing is installed in the movable hole 802. The sealed bearing uses fluororubber corrosion-resistant seals, which can prevent high solid content emulsified wastewater and alumina dust from entering the bearing. It can operate continuously for a long time without jamming or leakage, and prevents leaked wastewater from mixing into clean water and damaging the water pollution control and treatment effluent. The transmission rod 803 is rotatably inserted into the movable hole 802 via a sealed bearing. A fluid-driven conveying wheel 804 is fixedly installed at the top of the transmission rod 803. The fluid-driven conveying wheel 804 adopts a multi-bladed inclined impact blade structure, which can fully absorb the impact force of the feed wastewater and convert it into rotational torque. A spiral guide block 805 is fixedly installed inside the purification box 401 and above the fluid-driven conveying wheel 804. The spiral guide block 805 retracts downward to form a flow guide cavity, which gathers the dispersed inlet water and concentrates the impact fluid to drive the conveyor wheel 804. Even under low flow conditions, it can ensure the stable rotation of the transmission rod 803, avoiding membrane blockage caused by the scraper stopping at low loads. This allows the conveyor wheel 804 to drive the transmission rod 803 to rotate. A wave-shaped blade scraper wheel 806 is fixedly installed at the bottom of the transmission rod 803. The wave-shaped blade scraper wheel 806 is set to fit the hydrophilic and oleophobic coating 404 of the ceramic membrane 403. The wave-shaped blade scraper wheel 806 is flexibly attached to the surface of the ceramic membrane 403. During the rotation, it repeatedly scrapes away the aromatic sludge and solid dust accumulated on the surface of the ceramic membrane 403, preventing membrane pore blockage and organic pollutants from penetrating the water. This enhances the solid-liquid separation water pollution control and treatment effect. Together with the front-end ultraviolet and ultrasonic components, it forms a dual anti-clogging system, which greatly extends the service life of the ceramic membrane 403. The transmission rod 803 is connected to the heating unit 9. The heating unit 9 includes an assembly ring 901 fixedly sleeved on the outside of the transmission rod 803. The assembly ring 901 has multiple sets of elastic telescopic components 902 arranged in a circular array. A storage box can be used, with a sliding rod inside the storage box. One end of the sliding rod is fitted with a telescopic rod, and the other end of the telescopic rod is fitted with a spring. The storage box, sliding rod, and telescopic rod are all made of 316L stainless steel. A wave-shaped friction plate 903 is fixedly installed at the end of each elastic telescopic component 902. The wave-shaped friction plate 903 is made of a high-wear-resistant graphite metal composite material. The wave-shaped friction plate 903 is fixedly installed to the other end of the telescopic rod. A ring-shaped heat-conducting ring 904 is coaxially fixed to the inner wall of the purification box 401. The ring-shaped heat-conducting ring 904 is made of high-thermal-conductivity copper and is locked to the inner wall of the purification box 401 by circumferentially evenly distributed stainless steel bolts. The elastic telescopic component 902 has a built-in high-temperature and corrosion-resistant compression spring, which can automatically compensate for the wear of the wave-shaped friction plate 903, always maintaining the wave-shaped friction plate 903. It fits tightly against the 904 heat-conducting ring to ensure continuous and stable frictional heat generation; The elastic force of the elastic telescopic component 902 keeps the wave-shaped friction plate 903 tightly attached to the inner wall of the heat-conducting ring 904. During operation, the transmission rod 803 rotates continuously with the water flow, causing the wave-shaped friction plate 903 to generate heat through friction along the inner wall of the heat-conducting ring 904. The heat is evenly diffused into the purification chamber 401 through the heat-conducting ring 904, reducing the viscosity of the anthraquinone working solution, increasing the water permeability of the ceramic membrane 403, and stabilizing the membrane cavity temperature at 55~65℃. There are no external electrical heating elements, which fully meet the safety specifications for Class A explosion-proof areas, eliminating the risk of fire and explosion caused by electric heating from the source and avoiding secondary water pollution accidents caused by fire.

[0025] Example 3, see Figures 1-7 in the instruction manual; The zero-discharge treatment method for hydrogen peroxide unit regeneration wastewater is a complete, end-to-end water pollution control and treatment process, including: S1. Nitrogen gas is introduced into the collection unit 2, conveying unit 3, membrane concentration and purification unit 4, separation unit 5, low temperature evaporation unit 6, and recovery unit 7 through the main nitrogen gas pipe and nitrogen gas branch pipes, so that each chamber forms a micro positive pressure environment of 0.01~0.03MPa. The entire treatment process does not require the addition of demulsifiers or flocculants, resulting in no chemical waste and simplifying the subsequent disposal of water pollution. The fully automatic control unit 1 monitors the entire system's operating conditions; the entire process is closed and inertized, eliminating traditional open-pool processes, preventing fugitive VOC emissions and explosive gas accumulation, avoiding secondary wastewater generation from waste gas washing, and constructing a closed-loop water pollution control and treatment system that prevents the introduction of foreign metal impurities and thus avoids palladium catalyst poisoning. When using, start the nitrogen supply system in advance. The main nitrogen pipeline is equipped with a nitrogen pressure regulating valve and a micro positive pressure transmitter to adjust the intake volume in real time. Each unit's nitrogen branch pipeline is equipped with an independent flow limiting valve. Automatic nitrogen replenishment when chamber pressure is below 0.01 MPa; opening of explosion-proof vent valve when pressure is above 0.03 MPa. Pressure anomaly signals are uploaded to the explosion-proof PLC control cabinet in real time. The fully automatic control unit 1 integrates a multi-channel acquisition module to simultaneously collect all instrument signals such as temperature, pressure, liquid level, and flow. If the operating parameters exceed the standard, an automatic audible and visual alarm will be triggered and the machine will be shut down. This will prevent overflows and leaks from causing sudden water pollution, and replace the traditional sewage treatment plant that requires 6 people to be on-site. It will also eliminate the problem of fluctuations in water pollution control and treatment effluent caused by the instability of manual operation. The regenerated wastewater discharged from S2, the alumina bed, the catalyst, the hydrogenation tower, and the oxidation tower is introduced into the nitrogen-sealed buffer tank 201 via the branch pipe 203 for sealed temporary storage. Branch pipe 203 is only connected to Class IV wastewater pipelines containing recyclable working fluid. Wastewater from flushing and alkali tower that has no recycling value is diverted separately to avoid mixing of high-impurity wastewater and increasing pollutant load, thus reducing the difficulty of the entire water pollution control and treatment system. Nitrogen-sealed buffer tank 201 has a volume of 0.12m³, can withstand temperatures up to 98℃, and is suitable for cooking wastewater conditions; The entire process is sealed with no openings, relying on nitrogen micro-positive pressure to isolate the air, avoiding the volatilization of aromatics to produce VOCs and explosive mixtures. During the temporary storage stage, there is no loss of working fluid and no leakage of pollutants, thus consolidating the foundation for front-end water pollution control and treatment. S3, the second high-temperature magnetic transfer pump 301 of the transfer unit 3 transports the buffered wastewater to the membrane concentration and purification unit 4 via the main pipeline 302; Electromagnetic flowmeter 303 and pressure transmitter 304 respectively collect pipeline flow and pressure signals and feed them back to the fully automatic control unit 1. The second high-temperature magnetic transfer pump 301 can withstand the medium temperature of 0~100℃, with no risk of sealing leakage, eliminating the risk of non-point source pollution caused by leakage during transportation, and ensuring continuous water pollution control and treatment transportation conditions. It is suitable for emulsified wastewater with high solids content of 2200~5000mg / L, and a single 150,000 tons / year unit can stably treat 52 tons of wastewater per day; the pipeline pressure exceeds 0.4MPa and the unit will automatically interlock and shut down; the flow and pressure data are uploaded to the central control in real time to realize visual monitoring and timely prediction of failures such as leakage and blockage that may affect water pollution control and treatment. S4. Wastewater enters the purification tank 401. The spiral guide block 805 collects the wastewater fluid and impacts the fluid-driven conveyor wheel 804. The fluid power drives the transmission rod 803 to rotate without external power. The pressure support frame 801 counteracts the high-pressure filtration impact inside the purification box 401, preventing membrane deformation and leakage, and ensuring the water pollution control and treatment effect of the membrane section. The transmission rod 803 drives the wave-shaped blade scraper wheel 806 to scrape circumferentially along the surface of the ceramic membrane 403. At the same time, the transmission rod 803 is linked to the operation of the heating unit 9, and the wave-shaped friction plate 903 rubs against the annular heat-conducting ring 904 to generate frictional heat. Relying on fluid kinetic energy for passive heating, without the need for explosion-proof electric heating equipment, it reduces the viscosity of high-viscosity aromatic media, significantly improves oil-water separation efficiency, reduces organic pollutant residue, significantly improves water pollution control and treatment removal rate, and completely eliminates the 7-30 day long gravity settling process, avoiding secondary pollution caused by pollutant leaching and volatilization during the settling stage. Simultaneously activate the catalyst transfer device 405, ultraviolet lamp tube 406, and ultrasonic transducer 407 inside the purification chamber 401 to synergistically degrade macromolecular organic pollutants and enhance the degradation capacity for water pollution control and treatment. The pressure support frame 801 is a thickened 316L stainless steel integral welded structure to offset the impact of high pressure fluid and prevent the filter frame 402 and ceramic membrane 403 from shifting, deforming and leaking. The sealed bearing uses fluororubber seals to prevent dust and wastewater from seeping into the bearing and avoid jamming, leakage and pollution of the produced water. The conveyor wheel has multiple inclined blades that utilize water flow to convert torque and rotate stably at low flow rates. 806 Wave-shaped blade scraper wheel with flexible hydrophilic and oleophobic coating 404 continuously scrapes away oil sludge and dust from the film surface, preventing film blockage and contaminant penetration; 902 Elastic telescopic component with built-in high-temperature resistant alloy spring; 903 Wave-shaped friction plate closely attached to copper heat-conducting ring 904 generates heat through friction, stably controls the temperature at 55~65℃, and forms a temperature gradient with the downstream evaporator. Palladium-titanium catalyst, 254nm ultraviolet light, and 28kHz ultrasound synergistically degrade macromolecular viscous substances without introducing impurities, thus avoiding palladium catalyst poisoning and excessive heavy metals in the effluent. The ceramic membrane 403 substrate with a 0.1μm alumina and silica modified coating achieves highly efficient pure physical oil-water separation, significantly reducing organic pollutants in water bodies and implementing source water pollution control and treatment; S5. The modified wastewater undergoes solid-liquid separation through an inclined ceramic membrane 403, and the separated liquid phase material is then introduced into separation unit 5. The ceramic membrane 403 has a concentration ratio of up to 100:1, can run continuously for 365 days without permanent membrane clogging, and does not require long-term static settling; the working solution after separation is free of chemical contamination and can be reused, and the filtrate containing only trace amounts of fine impurities is sent into a centrifuge in a sealed manner, promoting water pollution control and treatment in stages and steps. The centrifuges in Separation Unit 5 (S6) centrifuge the membrane-filtered effluent to deeply remove fine aromatic hydrocarbons and inorganic dust impurities, further reducing the concentration of pollutants in the water and improving the multi-stage water pollution control and treatment process. A closed-tube fine centrifuge is selected, with a slightly positive nitrogen pressure chamber to prevent aromatic hydrocarbon volatilization. It relies on centrifugal force to remove alumina and catalyst dust in layers. The equipment automatically discharges slag in a closed manner during cycles, eliminating the need for manual plate disassembly and unloading, and eliminating the need for on-site operation of chemical preparation and filter press. This solves the problems of large fluctuations in manual operation and unstable effluent from water pollution control and treatment in traditional processes, while also reducing the amount of hazardous waste generated. S7. After centrifugation, the material is fed into the vacuum scraper evaporator 601 of the low-temperature evaporation unit 6. An anti-static PTFE scraper 602 removes material adhering to the inner wall of the evaporator, and an anti-static rod 603 eliminates static electricity during equipment operation. The vacuum scraper evaporator 601 maintains a negative pressure of -0.07 to -0.09 MPa and a low temperature of 70°C for evaporation, reducing the boiling point of aromatics and avoiding the risk of explosion at atmospheric pressure. The anti-static rod 603 eliminates frictional static electricity. Aromatic vapors enter a two-stage tubular condenser 604 for condensation, and uncondensed light components are returned to the bottom of the vacuum scraper evaporator 601 for secondary evaporation. There is no direct discharge of aromatic waste gas, eliminating the need for activated carbon adsorption and waste gas spraying, simplifying end-of-pipe water pollution control and treatment facilities, and reducing pollutant discharge pathways. S8, the vacuum scraper evaporator 601 uses two independent discharge pipelines to respectively transport high-concentration aromatic materials and condensed clean distillate water to the working fluid reuse storage tank 701 and the distillate water storage tank 702; the two pipelines are completely independent and there is no mixing; the two storage tanks are nitrogen-sealed and inertized throughout the process, with no wastewater discharge, truly achieving zero discharge and achieving closed-loop resource utilization water pollution control and treatment. S9, the internal liquid level detection element of the recovery unit 7 collects the liquid level signal of the storage tank and transmits it to the fully automatic control unit 1; after reaching the set liquid level threshold, the corresponding reflux transfer pump 703 is started to complete the material delivery and achieve zero discharge treatment of wastewater. The working fluid reuse storage tank 701 stores the purified qualified aromatic working fluid, which is pumped back to the hydrogenation and oxidation processes for recycling, reducing the amount of pollutants generated from the source and improving the overall efficiency of water pollution control and treatment of the entire plant; the distillate water can be reused in the unit flushing and alkali preparation processes; the reflux pump is automatically started and stopped at high and low liquid levels, the material transfer process is fully automated, there is no risk of overflow and sewage discharge, and the long-term operation of water pollution control and treatment is stably guaranteed to meet standards.

[0026] 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. A zero-discharge treatment device for regeneration wastewater from a hydrogen peroxide unit, characterized in that, include: The fully automatic control unit (1), collection unit (2), conveying unit (3), membrane concentration and purification unit (4), separation unit (5), low temperature evaporation unit (6), and recovery unit (7) are set on the base. The fully automatic control unit (1) is electrically connected to the collection unit (2), the conveying unit (3), the membrane concentration and purification unit (4), the separation unit (5), the low temperature evaporation unit (6), and the recovery unit (7) respectively via signal transmission cables; The sewage outlet of the collection unit (2) is connected to the conveying unit (3) via a closed metal pipeline to transport wastewater. The liquid outlet of the conveying unit (3) is connected to the liquid inlet of the membrane concentration and purification unit (4). The liquid outlet of the membrane concentration and purification unit (4) is connected to the separation unit (5) to transport liquid centrifugation separation. The liquid outlet of the separation unit (5) is connected to the low-temperature evaporation unit (6). The two discharge pipelines of the low-temperature evaporation unit (6) are respectively connected to the recovery unit (7) to transport high-concentration aromatic hydrocarbons and condensed clean distilled water. The fully automatic control unit (1) is an explosion-proof PLC control cabinet; The separation unit (5) is a centrifuge for wastewater processing; A total nitrogen pipe is also provided, from which multiple nitrogen sub-pipes are branched out to connect to the collection unit (2), the conveying unit (3), the membrane concentration and purification unit (4), the separation unit (5), the low-temperature evaporation unit (6), and the recovery unit (7). The interconnected chambers form a micro-positive pressure environment of 0.01~0.03MPa. No demulsifying or flocculant chemicals are added to the entire device, and the total liquid holding capacity of the system is ≤0.5m³. The membrane concentration and purification unit (4) is equipped with an integrated linkage pressure-resistant self-cleaning heating unit (8) and a heating unit (9).

2. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 1, characterized in that: The collection unit (2) includes a nitrogen-sealed buffer tank (201) for wastewater collection. The nitrogen-sealed buffer tank (201) is equipped with a first high-temperature magnetic transfer pump (202) for introducing wastewater. The first high-temperature magnetic transfer pump (202) is equipped with a branch pipe (203) for external alumina bed, catalyst, hydrogenation, and oxidation tower sewage discharge pipeline. The nitrogen-sealed buffer tank (201) is also connected to the outside of the transfer unit (3).

3. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 2, characterized in that: The conveying unit (3) is suitable for wastewater with a temperature ≤100℃ and a solid content ≥2000mg / L. The conveying unit (3) includes a second high-temperature magnetic conveying pump (301) installed outside the nitrogen sealed buffer tank (201). The output end of the second high-temperature magnetic conveying pump (301) is fixedly installed with a main pipeline (302) for liquid transmission. An electromagnetic flow meter (303) and a pressure transmitter (304) are sequentially installed on the main pipeline (302). The signal transmission cables of the electromagnetic flow meter (303) and the pressure transmitter (304) are connected to the fully automatic control unit (1). One end of the main pipeline (302) is installed on the outside of the membrane concentration and purification unit (4).

4. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 3, characterized in that: The membrane concentration and purification unit (4) includes a purification box (401) connected to the outlet of the main pipeline (302). The membrane concentration and purification unit (4) also includes a catalyst transporter (405) loaded with palladium and titanium, an ultraviolet lamp (406), and an ultrasonic transducer (407) integrated in the water inlet area of ​​the inner cavity of the purification box (401). The ultraviolet lamp (406) and the ultrasonic transducer (407) are electrically connected to the fully automatic control unit (1) through signal cables. A filter frame (402) is fixed at an incline downstream of the inner cavity of the purification box (401). A ceramic membrane (403) is mounted on the filter frame (402). The surface of the ceramic membrane (403) is provided with a hydrophilic and oleophobic coating (404). The liquid outlet of the purification box (401) is connected to the centrifuge inlet of the separation unit (5) through a closed pipeline. The centrifuge discharge pipeline is connected to the feed end of the low-temperature evaporation unit (6).

5. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 4, characterized in that: The low-temperature evaporation unit (6) includes a vacuum scraper evaporator (601) fixedly installed at one end of the centrifuge outlet of the separation unit (5), and the working temperature range of the vacuum scraper evaporator (601) is 60~80℃. The main shaft of the vacuum scraper evaporator (601) is fixedly installed with an anti-static polytetrafluoroethylene scraper (602). The inner wall of the vacuum scraper evaporator (601) is provided with an anti-static rod (603). The gas phase outlet pipeline of the vacuum scraper evaporator (601) is connected to a two-stage tubular condenser (604), and the return pipeline of the two-stage tubular condenser (604) is connected to the bottom of the vacuum scraper evaporator (601). At the same time, the vacuum scraper evaporator (601) is connected to the vacuum unit pipeline and the nitrogen distribution pipeline respectively. The two independent discharge pipelines at the bottom of the vacuum scraper evaporator (601) are installed on the external phase of the recovery unit (7).

6. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 5, characterized in that: The recovery unit (7) includes a working fluid recycling tank (701) that collects high-concentration aromatic hydrocarbons by connecting two independent discharge pipelines to the bottom of the vacuum scraper evaporator (601) and a distillate water storage tank (702) that collects condensed clean distillate water. The bottom of the working fluid recycling tank (701) and the distillate water storage tank (702) are respectively equipped with a reflux pump (703) for material external transfer and recycling. The working fluid recycling tank (701) and the distillate water storage tank (702) are both equipped with a liquid level detection element. The liquid level detection element is electrically connected to the fully automatic control unit (1) through a signal transmission cable.

7. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 4, characterized in that: The purification box (401) is equipped with an integrated linkage pressure-resistant self-cleaning heating unit (8) in its inner cavity. The heating unit (9) is mounted on the outside of the integrated linkage pressure-resistant self-cleaning heating unit (8). The heating unit (9) is in transmission cooperation with the integrated linkage pressure-resistant self-cleaning heating unit (8).

8. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 7, characterized in that: The integrated linkage pressure-resistant self-cleaning heating unit (8) includes a pressure-bearing support frame (801) fixedly embedded in the inner cavity of the purification box (401). The pressure-bearing support frame (801) has a coaxially arranged movable hole (802) in the middle. A sealed bearing is provided in the movable hole (802). The transmission rod (803) is rotatably inserted in the movable hole (802) through the sealed bearing. A fluid-driven conveying wheel (804) is fixedly provided at the top of the transmission rod (803). A spiral guide block (805) is fixedly provided in the purification box (401) above the fluid-driven conveying wheel (804). A wave-shaped blade scraper wheel (806) is fixedly installed at the bottom of the transmission rod (803). The wave-shaped blade scraper wheel (806) is fitted with the hydrophilic and oleophobic coating (404) of the ceramic membrane (403). The transmission rod (803) is connected to the heating unit (9) in a transmission manner.

9. The zero-discharge treatment device for hydrogen peroxide unit regeneration wastewater as described in claim 8, characterized in that: The heating unit (9) includes an assembly ring (901) fixedly sleeved on the outside of the transmission rod (803). The assembly ring (901) is arranged in a ring array with multiple sets of elastic telescopic members (902). Each set of elastic telescopic members (902) has a wave-shaped friction plate (903) fixedly installed at its end. The inner wall of the purification box (401) is coaxially fixed with a ring-shaped heat-conducting ring (904). The elastic force of the elastic telescopic members (902) makes the wave-shaped friction plate (903) tightly adhere to the inner wall of the heat-conducting ring (904).

10. A zero-discharge treatment method for regeneration wastewater from a hydrogen peroxide unit according to any one of claims 1-9, characterized in that, include: S1. Nitrogen gas is introduced into the collection unit (2), conveying unit (3), membrane concentration and purification unit (4), separation unit (5), low temperature evaporation unit (6), and recovery unit (7) through the main nitrogen pipe and nitrogen branch pipes, so that each chamber forms a micro positive pressure environment of 0.01~0.03MPa. No demulsifying agent or flocculant is added to the entire process. The fully automatic control unit (1) monitors the operating conditions of the entire device. The regenerated wastewater discharged from S2, alumina bed, catalyst, hydrogenation tower, and oxidation tower is introduced into the nitrogen-sealed buffer tank (201) of the collection unit (2) through the branch pipe (203) for sealed temporary storage. S3, the second high-temperature magnetic conveying pump (301) of the conveying unit (3) transports the buffered wastewater to the membrane concentration and purification unit (4) through the main pipeline (302). The electromagnetic flow meter (303) and the pressure transmitter (304) collect the pipeline flow and pressure signals respectively and feed them back to the fully automatic control unit (1). S4. Wastewater enters the purification tank (401). The spiral guide block (805) gathers the wastewater fluid and impacts the fluid-driven conveyor wheel (804). Relying on the fluid power, the transmission rod (803) rotates without external power. The pressure support frame (801) counteracts the high-pressure filtration impact force inside the purification tank. The transmission rod (803) drives the wave-shaped blade scraper wheel (806) to scrape the ceramic membrane (403) circumferentially. At the same time, the transmission rod (803) is linked to the heating unit (9) to operate. The wave-shaped friction plate (903) rubs against the annular heat-conducting ring (904) to generate frictional heat. Simultaneously, the catalyst transfer device (405), ultraviolet lamp tube (406), and ultrasonic transducer (407) inside the purification tank (401) are turned on to treat the wastewater medium in a coordinated manner. S5. The modified wastewater undergoes solid-liquid separation through an inclined ceramic membrane (403), and the separated liquid phase material is fed into the separation unit (5). S6. The centrifuge of the separation unit (5) centrifuges the membrane filtered water to remove residual fine aromatic impurities inside the water. S7. After centrifugation, the material is sent into the vacuum scraper evaporator (601) of the low-temperature evaporation unit (6). The anti-static polytetrafluoroethylene scraper (602) scrapes off the material attached to the inner wall of the evaporator. The static elimination rod (603) eliminates the static electricity of the equipment. The gaseous medium generated by the evaporator is passed into the two-stage tube condenser (604) for condensation. The condensed material flows back to the bottom of the vacuum scraper evaporator (601). S8. The vacuum scraper evaporator (601) delivers high-concentration aromatic materials and condensed clean distillate water to the working fluid reuse tank (701) and the distillate water storage tank (702) respectively through two independent discharge pipelines. S9. The internal liquid level detection element of the recycling unit (7) collects the liquid level signal of the storage tank and transmits it to the fully automatic control unit (1). After the set liquid level threshold is reached, the corresponding return conveying pump (703) is started to complete the material delivery and realize zero discharge treatment of wastewater.

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