CN107200436B

CN107200436B - Complex electroplating wastewater treatment method, treatment system and application

Info

Publication number: CN107200436B
Application number: CN201710446986.9A
Authority: CN
Inventors: 韩全; 张恒
Original assignee: Guangdong Yeanovo Environmental Protection Co ltd
Current assignee: Guangdong Shangchen Environmental Technology Co ltd
Priority date: 2017-06-14
Filing date: 2017-06-14
Publication date: 2020-12-15
Anticipated expiration: 2037-06-14
Also published as: CN107200436A

Abstract

The invention provides a complex electroplating wastewater treatment method which is characterized by sequentially comprising the following steps: (1) pretreating the complexing electroplating wastewater to obtain pretreated water; (2) performing biochemical treatment on the pretreated water obtained in the step (1) to obtain biochemical treated water; (3) concentrating the biochemical treatment water obtained in the step (2) to obtain concentrated high-salinity concentrated water and reuse water; (4) carrying out evaporation crystallization treatment on the concentrated high-salinity concentrated water obtained in the step (3) to obtain recycled water and crystals; wherein the standard of the recycled water is as follows: the pH value is 6-8, the conductivity is less than or equal to 50, the COD is less than or equal to 30, and the turbidity is less than or equal to 1; the method has the advantages of simple operation, stable operation, low cost and high treatment efficiency, thereby achieving zero discharge or low discharge of the complexing electroplating wastewater in the electroplating production and simultaneously realizing high-purity recovery of each metal ion in the wastewater.

Description

Complex electroplating wastewater treatment method, treatment system and application

Technical Field

The invention relates to a method and a system for treating wastewater, in particular to a method and a system for treating complex electroplating wastewater.

Background

The treatment of the complex electroplating wastewater is usually carried out by a chemical precipitation method, an electrolysis method, a common ion exchange method and the like in the treatment process. However, the above treatment methods have certain limitations and cannot achieve zero emission.

The chemical precipitation method is a method frequently used for treating the complex electroplating wastewater at present, and the method needs to add a large amount of acid and alkali, and simultaneously needs to add ferrous sulfate and polyaluminium chloride, so that the salt content of the discharged water is increased, and the discharge of residual metal ions in the water still cannot reach the standard. Therefore, because the content of the controlled substances specified by the wastewater discharge standard is extremely low, excessive chemicals are required to be added to reach the discharge standard, the cost is high, and the wastewater cannot be recycled as process water. In addition, the chemical sedimentation method cannot directly recover metal ions in the wastewater, and simultaneously generates a large amount of sludge, the sludge contains a large amount of metal ions, and the sludge needs to be treated again, so that secondary pollution is caused.

The treatment process of the electrolytic method is mature and stable in operation, but because the content of controlled substances specified by the discharge standard is extremely low, the treatment method has the disadvantages of high power consumption and high treatment cost during the electrolysis of wastewater, is easy to generate toxic gas, and is difficult to treat until the wastewater reaches the standard and is discharged.

The common ion exchange method adopts organic framework ion exchange resin, can effectively remove various harmful ions in the wastewater, and can recycle water, but the treatment method needs large resin dosage, is difficult to treat regenerated liquid, consumes a large amount of acid and alkali, and has high treatment cost; in addition, during the regeneration of the resin, the resin is largely broken due to the regeneration, shrinkage and expansion of the resin, and the economic efficiency is not high. If the reverse osmosis membrane is used for concentrating and treating electroplating wastewater and simultaneously pure water is recycled, the process is only applied to the wastewater system treatment of single high-valence ions, so the use has limitation.

It can be seen that various treatment methods for complexing electroplating wastewater have many problems at present, most or all of the wastewater cannot be recycled even the existing equipment of each electroplating plant is fully utilized, and valuable metals in the wastewater cannot be effectively separated and recovered.

Disclosure of Invention

The invention aims to overcome the problems and defects in the prior art and provide a complex electroplating wastewater treatment method and a corresponding treatment system which are simple to operate, stable to operate, low in cost and high in treatment efficiency, so that zero discharge or low discharge of complex electroplating wastewater in electroplating production is achieved, high-purity recovery of metal ions in the wastewater is realized, the production water consumption in the electroplating industry is saved, the pollution of the electroplating industry to the environment is remarkably reduced, the use amount of acid and alkali is reduced, resources can be effectively saved, the production cost is reduced, the recovery of equipment investment is realized, and the clean production and sustainable development of the electroplating industry are promoted and promoted.

The purpose of the invention is realized by the following technical scheme:

the invention provides a complex electroplating wastewater treatment method which is characterized by sequentially comprising the following steps:

(1) pretreating the complexing electroplating wastewater to obtain pretreated water;

(2) performing biochemical treatment on the pretreated water obtained in the step (1) to obtain biochemical treated water;

(3) concentrating the biochemical treatment water obtained in the step (2) to obtain concentrated high-salinity concentrated water and reuse water;

(4) carrying out evaporation crystallization treatment on the concentrated high-salinity concentrated water obtained in the step (3) to obtain recycled water and crystals;

wherein the standard of the recycled water is as follows: pH 6-8, conductivity less than or equal to 50, COD less than or equal to 30 and turbidity less than or equal to 1.

Preferably, in the step (1),

the pH value of the complex electroplating wastewater is 2-6, and the complex electroplating wastewater contains copper, nickel, SS and COD;

preferably, the step of pre-treating is:

(1-1) introducing the complex electroplating wastewater into a complex breaking tank, adding sulfuric acid into the complex breaking tank until the pH value is 2-3, and then adding sodium hypochlorite until the ORP value is 300-400 mv;

(1-2) introducing the wastewater treated in the step (1-1) into a pH adjusting tank, and adding sodium hydroxide until the pH is 10-11;

(1-3) introducing the wastewater treated in the step (1-2) into a chemical reaction tank, adding a coagulant, then adding a flocculant, and stirring for 20-30 min;

(1-4) introducing the wastewater treated in the step (1-3) into a precise control efficient precipitation system;

preferably, in the step (1-1), a 10% sulfuric acid solution is added to adjust the pH; preferably, sodium hypochlorite solution with the concentration of 10 percent is added to adjust the ORP value;

preferably, in the step (1-2), a sodium hydroxide solution with the concentration of 10% is added to adjust the pH;

preferably, in the step (1-3), the coagulant is an inorganic coagulant, more preferably FeCl₃(ii) a Preferably, the flocculant is an organic flocculant, more preferably PAM; preferably, the time interval between the addition of the coagulant and the flocculant is 20-40 min;

preferably, the pH of the wastewater treated by the step (1-3) is 8-9;

preferably, in the step (1-4), the precise control efficient sedimentation system is formed by sequentially connecting a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge hopper; preferably, the wastewater treated in the step (1-3) is sequentially introduced into the water distribution system, the sedimentation treatment tank and the inclined pipe; the supernatant after the treatment enters an effluent weir to obtain pretreated water, and the obtained sludge is deposited in a sludge hopper; preferably, the pressure of the sedimentation treatment tank is 2-3 Mpa.

Preferably, in the step (2), the biochemical treatment step is: sequentially feeding the pretreated water obtained in the step (1) into an anaerobic tank, an aerobic tank and a membrane bioreactor;

preferably, the anaerobic pool comprises anaerobic bacteria; preferably, the anaerobic bacteria are selected from one or more of yeast, nitrate bacteria, clostridium or bacteroides;

preferably, the yeast, nitrate, clostridia or bacteroides are acclimatized to be salt-tolerant;

preferably, the aerobic tank contains aerobic microorganisms;

preferably, the aerobic microorganism is selected from one or more of bacillus, rhizobium, nitrobacteria or mould;

preferably, the bacillus, rhizobium, nitrifier or mould is acclimated to be salt tolerant;

preferably, the membrane bioreactor consists of a hollow fiber membrane component and a membrane pool;

preferably, the hollow fiber membrane module is located in the membrane tank;

preferably, the pore diameter of the hollow fiber membrane is 0.01-0.1 μm;

preferably, the pH after the biochemical treatment is 6 to 8.

Preferably, in the step (3), the concentration treatment step is: sequentially passing the biochemical treatment water obtained in the step (2) through a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system;

preferably, the primary nanofiltration system is formed by sequentially connecting a precision filter and a primary nanofiltration membrane;

preferably, the filter element of the precision filter is melt-blown PP cotton;

preferably, the filter element pore size of the precise microporous filter is 5 μm;

preferably, the primary nanofiltration membrane is an industrial grade high-desalination-rate nanofiltration membrane;

preferably, the aperture of the primary nanofiltration membrane is 1-2 nm;

preferably, the rejection rate of the primary nanofiltration membrane to sodium ions is 50-70%;

preferably, the rejection rate of the primary nanofiltration membrane on heavy metal ions and salts is more than 97%;

preferably, the membrane feeding pressure of the primary nanofiltration system is 1.0-1.5 Mpa;

preferably, the relative molecular mass cut-off range of the primary nanofiltration system is 150-300 daltons;

preferably, the pH of the water entering the primary nanofiltration system is 6-8;

preferably, the permeate of the primary nanofiltration system can be used as reuse water;

preferably, the concentrated solution of the primary nanofiltration system enters a primary reverse osmosis system.

Preferably, in the step (3), the first-stage reverse osmosis system is formed by sequentially connecting a precision filter and a first-stage reverse osmosis membrane;

preferably, the filter element of the precision filter is melt-blown PP cotton;

preferably, the first-stage reverse osmosis membrane is a brackish water reverse osmosis membrane;

preferably, the rejection rate of the first-stage reverse osmosis membrane on heavy metal ions and salts is more than 98 percent;

preferably, the aperture of the primary reverse osmosis membrane is 0.1-1 nm;

preferably, the membrane inlet pressure of the primary reverse osmosis system is 1.8 Mpa;

preferably, the pH of the water entering the primary reverse osmosis system is 5-6;

preferably, the primary reverse osmosis system is adjusted in pH by adding hydrochloric acid;

preferably, hydrochloric acid with the concentration of 0.2-0.5% is added to adjust the pH;

preferably, the permeate of the primary reverse osmosis system returns to the primary nanofiltration system;

preferably, the concentrate of the primary reverse osmosis system enters a secondary reverse osmosis system.

Preferably, in the step (3), the secondary reverse osmosis system is formed by sequentially connecting a precision filter and a secondary reverse osmosis membrane;

preferably, the filter element of the precision filter is melt-blown PP cotton;

preferably, the secondary reverse osmosis membrane is a seawater reverse osmosis membrane;

preferably, the rejection rate of the secondary reverse osmosis membrane on heavy metal ions and salts is more than 99.5%;

preferably, the aperture of the secondary reverse osmosis membrane is 0.1-1 nm;

preferably, the membrane inlet pressure of the secondary reverse osmosis system is 4-5 Mpa;

preferably, the pH of the water entering the secondary reverse osmosis system is 6 to 8;

preferably, the secondary reverse osmosis system is adjusted in pH by adding hydrochloric acid;

preferably, the concentration of the hydrochloric acid is 0.2-0.5%;

preferably, the permeate of the secondary reverse osmosis system returns to the primary nanofiltration system;

preferably, the concentrate of the secondary reverse osmosis system is the high salinity concentrate.

Preferably, in the step (4), the evaporative crystallization treatment step is: sequentially passing the high-salinity concentrated water obtained in the step (3) through a heat exchanger, a concentration evaporator and an evaporation crystallizer;

preferably, the operating temperature of the heat exchanger is 80-100 ℃;

preferably, the operating pressure of the heat exchanger is 0.05-0.1 MPa;

preferably, the concentration evaporator is formed by sequentially connecting a heating chamber, a separation chamber, a circulating chamber, a liquid distributor and a demister;

preferably, the evaporative crystallizer is formed by sequentially connecting a separation chamber, a salt leg, a thickener and a crystallization kettle;

preferably, the condensed water of the high-salinity concentrated water after passing through the concentration evaporator returns to the secondary reverse osmosis system;

preferably, the concentrated high-salt water passes through a concentration evaporator to obtain concentrated high-salt water;

preferably, the concentrated high-salinity concentrated water has the salinity of 30-35%;

preferably, the concentrated high-salinity concentrated water passes through an evaporative crystallizer to obtain a crystal substance and condensed water; preferably, the crystal is sodium sulfate and/or sodium chloride; preferably, the condensed water is used as reuse water.

The invention also provides a treatment system of the zinc-containing wastewater treatment method, which is characterized by comprising a pretreatment unit, a biochemical treatment unit, a concentration treatment unit and an evaporation crystallization treatment unit which are sequentially communicated.

Preferably, the pretreatment unit comprises a zinc breaking tank, a pH adjusting tank, a chemical reaction tank and a precise control efficient precipitation system which are sequentially communicated; the precise control efficient sedimentation system is formed by sequentially connecting a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge bucket.

Preferably, the biochemical treatment unit comprises an anaerobic tank, an aerobic tank and a membrane bioreactor which are communicated in sequence;

preferably, the hollow fiber membrane module is located in the membrane tank;

preferably, the pore diameter of the hollow fiber membrane is 0.01-0.1 μm.

Preferably, the concentration treatment unit comprises a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system which are communicated in sequence.

preferably, the filter element of the precision filter is melt-blown PP cotton;

preferably, the filter element pore size of the precision filter is 5 μm;

the primary nanofiltration membrane is an industrial grade high-desalination-rate nanofiltration membrane;

preferably, the aperture of the primary nanofiltration membrane is 1-2 nm;

preferably, the rejection rate of the primary nanofiltration membrane to sodium ions is 50-70%; preferably, the rejection rate of the primary nanofiltration membrane on heavy metal ions and salts is more than 97%;

preferably, the pH of the water entering the primary nanofiltration system is 6-8.

Preferably, the first-stage reverse osmosis system is formed by sequentially connecting a precision filter and a first-stage reverse osmosis membrane;

preferably, the filter element of the precision filter is melt-blown PP cotton;

preferably, the filter element pore size of the precision filter is 5 μm;

preferably, the aperture of the primary reverse osmosis membrane is 0.1-1 nm;

preferably, the concentration of the hydrochloric acid is 0.2-0.5%.

Preferably, the secondary reverse osmosis system is formed by sequentially connecting a precision filter and a secondary reverse osmosis membrane;

preferably, the filter element of the precision filter is melt-blown PP cotton;

preferably, the filter element pore size of the precision filter is 5 μm;

preferably, the aperture of the secondary reverse osmosis membrane is 0.1-1 nm;

preferably, the concentration of the hydrochloric acid is 0.2-0.5%.

Preferably, the evaporative crystallization unit comprises a heat exchanger, a concentration evaporator and an evaporative crystallizer which are communicated in sequence;

preferably, the operating temperature of the heat exchanger is 80-100 ℃;

preferably, the operating pressure of the heat exchanger is 0.05-0.1 MPa;

preferably, the evaporative crystallizer consists of a separation chamber, a salt leg, a thickener and a crystallization kettle which are connected in sequence.

The treatment method of the complexing electroplating wastewater or the treatment system of the complexing electroplating wastewater provided by the invention is applied to treatment of the complexing electroplating wastewater.

In order to overcome the defects in the complex electroplating wastewater treatment in the prior art, the invention provides a treatment method of complex electroplating wastewater, which comprises the following steps:

the source analysis of the complex electroplating wastewater pollutants comprises the following steps: the complex waste water is mainly a working section of adopting complex metal to carry out electroplating in the electroplating process, mainly comprises copper salt and phosphate to form a plating solution, nickel sulfate, nickel acetate and the like are taken as main salts, hypophosphite, sodium borohydride, borane, hydrazine and the like are taken as reducing agents, and various auxiliary agents, reducing agents, potassium pyrophosphate, potassium citrate, nitrilotriacetic acid, additives and the like are added; the wastewater mainly comprises copper, nickel, SS, COD and other substances.

The method and the system for treating the complexing electroplating wastewater completely recycle the electroplating zinc-containing wastewater after treatment for production by adopting a technical route of wastewater diversion, classification treatment, wastewater recycling and resource recovery and adopting a heavy metal high-precision removal technology, a high-salinity wastewater biochemical technology, a special membrane concentration technology and a mechanical negative-pressure evaporation crystallization technology, realize zero discharge of the wastewater, improve the wastewater recycling rate to 99.67%, realize the recycling of water resources to the maximum extent, convert pollutants in the wastewater into solids for recycling, and completely realize the zero discharge of the wastewater.

The invention discloses a pretreatment process of complexing electroplating wastewater, which comprises the following steps:

the complex electroplating wastewater needs to remove phosphorus in the wastewater in a targeted manner so as to ensure that PO in the wastewater₄ ^3-The generated insoluble salt is removed, and the commonly adopted coagulants are lime, aluminum salt and iron salt. The scheme adopts an oxidant to break the complex, and the hypophosphite, metaphosphate and phosphite in the wastewater are oxidized into orthophosphate.

Independently collecting the complex electroplating wastewater into a complex electroplating wastewater regulating tank, introducing the wastewater into a complex breaking tank after the water quality and water quantity are sufficiently uniform, adding sulfuric acid into the complex breaking tank until the pH value is 2-3, and then adding sodium hypochlorite until the ORP value is 300-400 mv; then introducing the treated wastewater into a pH adjusting tank, and adding sodium hydroxide until the pH is 10-11; introducing the wastewater into a chemical reaction tank, adding a coagulant, then adding a flocculant, and stirring for 20-30 min; the coagulant is FeCl₃(ii) a The flocculant is PAM, and the time interval between coagulant addition and flocculant addition is 20-40 min; post-introduction precision control is highly efficientA sedimentation system; preferably, the precise control efficient sedimentation system is formed by sequentially connecting a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge hopper; introducing the treated wastewater into the water distribution system, the sedimentation tank treatment tank and the inclined pipe in sequence; the supernatant after the treatment enters an effluent weir to obtain pretreated water, and sludge is deposited in a sludge hopper; in order to increase the precipitation area, shorten the precipitation time and improve the precipitation efficiency, the precise control high-efficiency precipitation system has the effects of hydraulic water distribution, high-efficiency precipitation and the like, the high-efficiency precipitation flocs and the SS are efficiently precipitated, the inclined pipes are arranged in the tank at the same time, so that the precipitation particles are not interfered by the influence of steady flow, the rapid precipitation effect is achieved, the processing capacity of the precise control high-efficiency precipitation system is 3-7 times greater than that of a general precipitation tank, the sludge at the bottom of the tank is discharged into a sludge tank through the arranged static pressure sludge discharge device for further concentration, then the sludge is pumped into a sludge filter press for filter pressing, the sludge cake is retreated according to the property, about 80 percent of suspended matters and 40-70 percent of oils can be removed, and the turbidity<30NTU, COD reduction 40-60%, etc.;

the biochemical treatment process of the complexing electroplating wastewater comprises the following steps: the pretreated water sequentially enters an anaerobic tank, an aerobic tank and a membrane bioreactor; removing most of COD, ammonia nitrogen, SS and other substances in the wastewater through biodegradation of the A/O/MBR; the anaerobic process of the invention utilizes the function of anaerobic bacteria under the condition of no dissolved oxygen or under the condition of oxygen deficiency to hydrolyze and acidify organic matters, remove the organic matters in the wastewater, improve the biodegradability of the sewage and be beneficial to the subsequent aerobic treatment process; the aerobic process is that under aerobic condition, organic matter is oxidized and decomposed under the action of aerobic microbe, the concentration of organic matter is reduced, the amount of microbe is increased, the organic matter in sewage is adsorbed on the surface of active sludge and biomembrane and contacts with the surface of microbe cell, small molecular organic matter can enter microbe body through cell wall directly, and large molecular organic matter must be hydrolyzed into small molecular under the action of extracellular enzyme-hydrolase and then taken into cell body by microbe. The organic matter is finally decomposed into CO₂And H₂O; the membrane bioreactor comprises a hollow fiber membrane component anda membrane pool; preferably, the hollow fiber membrane module is located in the membrane tank; the membrane component is placed in the membrane pool, aeration is carried out in the pool, and as the aperture of the hollow fiber membrane is smaller than 0.1 micron, zoogloea and free bacteria can be completely retained in the membrane pool, so that mud-water separation is achieved, various suspended particles, bacteria, algae, turbidity and organic matters are effectively removed, and excellent effluent quality with the effluent suspended matters close to zero is ensured. The efficient interception function of the membrane bioreactor can effectively intercept nitrifying bacteria, so that the nitrification reaction is smoothly carried out, and ammonia nitrogen is effectively removed; meanwhile, macromolecular organic matters which are difficult to degrade can be intercepted, and the retention time of the macromolecular organic matters in the biochemical reaction tank is prolonged, so that the macromolecular organic matters are decomposed to the maximum extent.

The invention discloses a concentration treatment process of complexing electroplating wastewater, which comprises the following steps: the biochemical treatment water sequentially passes through a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system; in order to realize zero discharge of the complexing electroplating wastewater, the rear end of the biochemical treatment system is provided with a concentration treatment system for treating strong brine generated by the biochemical treatment system; the concentration treatment system is a process combining multi-stage concentration and nanofiltration/reverse osmosis concentration, and gradually reduces the water amount of the high-salt-content wastewater (the salt content of the obtained high-salt concentrated water is 40-60g/L) through the step-by-step concentration of the membrane, so that the investment and the operating cost of a subsequent evaporative crystallization system are reduced; the concentration treatment process reduces the concentrated brine to be treated in a subsequent evaporation crystallization system by 80 percent compared with a conventional concentration treatment system, reduces the investment cost of the whole wastewater treatment system by 20 to 30 percent, reduces the running cost of wastewater treatment by 30 to 40 percent, and improves the automation degree of the system.

The invention relates to an evaporation crystallization treatment process of complexing electroplating wastewater, which comprises the following steps: the high-salinity concentrated water obtained by concentration treatment sequentially passes through a heat exchanger, a concentration evaporator and an evaporation crystallizer; the invention treats the waste water to the evaporation and crystallization stage and then recycles the waste water completely, thereby realizing zero discharge of the complexing electroplating waste water; the waste water firstly enters a heat exchanger in the evaporative crystallization system, and the O in the waste water is removed through heat exchange₂And CO₂Gas and waste water after heat exchange enter a concentration evaporator for evaporation concentrationAnd (3) when the salt concentration of the wastewater is 30-35%, namely before sodium sulfate and sodium chloride crystals are generated, sending the wastewater to an evaporative crystallizer to obtain crystals and condensed water, and using the condensed water as reuse water. The evaporative crystallization system utilizes mechanical temperature increasing equipment to cause negative pressure of the waste water evaporation part, so that energy can be saved, compressed waste water steam is heated and pressurized to enter the outside of a concentration evaporator, latent heat is transferred to a pipe, the pipe is condensed into condensed water, and meanwhile, salt-containing waste water in the pipe is evaporated. The evaporative crystallization system has the characteristics of small volume, small occupied area, low energy consumption and high thermal efficiency, the power consumption of one ton of waste water is 16-20kwh, the thermal efficiency is 27 times that of a single-effect flash evaporation system and 7 times that of a four-effect flash evaporation system, the evaporative crystallization system is the most advanced evaporative concentration system at present, the generated crystals can be treated or sent to related departments for purification and utilization, and the main components of the evaporative crystallization system are sodium sulfate and sodium chloride.

The advantages of the evaporative crystallization system are as follows: (1) the system adopts mixed process water supply to reduce the ton water power consumption of the same water making tonnage device by 40-50% compared with the foreign technology; (2) because the mixed process of the system supplies water, the high-salinity concentrated water passing through the concentration treatment system sequentially enters the low-temperature effect from the high-temperature effect of the evaporative crystallization system, the concentration is gradually increased, and the temperature is gradually reduced. The increase of the concentration of the high-temperature effect feed water caused by circulating feed water from low-temperature effect to high-temperature effect in foreign technologies is avoided, and the scaling and corrosion conditions of high-temperature effect are effectively reduced; (3) the high-salinity concentrated water passing through the concentration treatment system is uniformly distributed on the concentration evaporator, so that the defect that the spray head type water supply in the existing evaporative crystallization system is not uniform and is easy to block is avoided; (4) the vacuum system adopts a differential pressure air extractor, and the designed differential pressure is accurately formed among the effects, so that the system is stable and reliable in operation.

The treatment system of the complex electroplating wastewater treatment method adopts the programmable logic controller, simultaneously realizes the automatic control and monitoring of the electric and instruments, and adopts the industrial personal computer to monitor the operation process state and the operation parameters of the system. In addition, a membrane system in the system is periodically flushed by using a permeate liquid to flush pollutants and protect a membrane; and an on-line chemical cleaning system is established, so that long-term, stable and efficient operation of the system can be ensured.

At present, the conventional treatment technology related to the complexing electroplating wastewater in the prior art comprises a chemical precipitation technology, a biological treatment technology and a membrane separation technology, the conventional technology is mainly designed according to a route of standard discharge, and compared with the invention, the invention has the following defects:

(1) the system waste water reuse rate of the conventional technology is 60%, wherein water resources are not fully recycled, and the waste water is discharged after being treated, so that the load of the surrounding environment is increased;

(2) the tolerance of the microorganism to salt in the conventional biochemical treatment technology is poor, the sludge concentration is generally 3000mg/L, and the sludge concentration of the biochemical system in the technology of the invention is 7000-8000 mg/L.

(3) Heavy metal ions are not removed 100%, and environmental pollution still exists;

(4) concentrated water generated by the membrane concentration system needs to be treated again, otherwise, two layers of pollution can be caused;

(5) the conductivity of the reuse water in the conventional technology is 200-300 mu S/cm, and the conductivity of the reuse water in the technology is less than or equal to 50 mu S/cm.

The complex electroplating wastewater treatment method and the treatment system have the beneficial effects that:

(1) according to different reaction conditions of various heavy metal ions, the complexing electroplating wastewater pretreatment process adopts online monitoring instruments such as pH and ORP, automatically controls a metering pump to quantitatively feed chemicals, adds the chemicals to fully react with wastewater, and carries out solid-liquid separation treatment through a precisely controlled high-efficiency precipitation system, so that the removal rate of the heavy metal ions can reach 99.99%.

(2) The biochemical process of the complex electroplating wastewater adopts an A/O/MBR process, the system consists of a biochemical tank, a membrane component and a membrane tank, and the activated sludge can be completely retained in the membrane tank, so that various pollutants such as various suspended particles, bacteria, organic matters and the like can be retained for a long time, and can be fully removed, the quality of effluent is ensured to be excellent, and SS is almost zero. The process has high volume load and strong adaptability to water quality and water quantity, and adopts the domesticated special microorganism with salt tolerance to remove the wastewater with high salt content and hard-to-degrade COD with high efficiency and good denitrification effect.

(3) The concentration process of the complexing electroplating wastewater adopts a special membrane concentration technology to concentrate the salt in the wastewater by more than 30 times according to the technology of combining desalination concentration and fine desalination concentration, and the produced water of an advanced treatment system can be directly reused for production. The special membrane concentration technology has the characteristics of high efficiency desalination rate under high flow rate, higher mechanical strength, longer service life, capability of playing a function under lower operation pressure, good chemical stability and high cost performance.

(4) The evaporation crystallization of the complex electroplating wastewater adopts a German special vapor compression technology and comprises a distilled water heat exchanger, a concentration evaporator, a crystallizer, a centrifuge and the like, when the evaporator is used for treating the wastewater, the heat energy required by the evaporation wastewater is provided by the heat energy released when the vapor is condensed and the condensed water is cooled, and no latent heat is lost in the operation process, so that the wastewater is evaporated at low temperature and negative pressure. When the compressor compresses, the pressure and the temperature are increased, and the high enthalpy steam is used as a heat source again to fully recover the heat of the distilled water and the concentrated solution, thereby saving the energy consumption. During evaporation, the evaporation outside the pipe is adopted, so that the efficiency is high and the scale in the pipe is never accumulated.

Drawings

Embodiments of the invention are described in detail below with reference to the attached drawing figures, wherein:

FIG. 1 is a schematic view of a complex electroplating wastewater treatment system according to the present invention.

Detailed Description

The invention is illustrated below with reference to specific examples. It will be understood by those skilled in the art that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention in any way.

The experimental procedures in the following examples are conventional unless otherwise specified. The raw materials and reagent materials used in the following examples are all commercially available products unless otherwise specified.

Firstly, the source analysis of the complex electroplating wastewater pollutants of the invention is as follows: the complex waste water is mainly a working section of adopting complex metal to carry out electroplating in the electroplating process, mainly comprises copper salt and phosphate to form a plating solution, nickel sulfate, nickel acetate and the like are taken as main salts, hypophosphite, sodium borohydride, borane, hydrazine and the like are taken as reducing agents, and various auxiliary agents, reducing agents, potassium pyrophosphate, potassium citrate, nitrilotriacetic acid, additives and the like are added; the wastewater mainly comprises copper, nickel, SS, COD and other substances.

Secondly, the pretreatment process of the complexing electroplating wastewater comprises the following steps: independently collecting the complex electroplating wastewater into a complex electroplating wastewater regulating tank, introducing the wastewater into a complex breaking tank after the water quality and water quantity are sufficiently uniform, adding sulfuric acid into the complex breaking tank to reach pH 2-3 in the complex breaking tank, and then adding sodium hypochlorite until the ORP value is 300-400 mv; then introducing the treated wastewater into a pH adjusting tank, and adding sodium hydroxide until the pH is 10-11; introducing the wastewater into a chemical reaction tank, adding a coagulant, then adding a flocculant, and stirring for 20-30 min; the coagulant is FeCl₃(ii) a The flocculant is PAM, and the time interval between coagulant addition and flocculant addition is 20-40 min; then introducing a precise control efficient precipitation system; preferably, the precise control efficient sedimentation system is formed by sequentially connecting a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge hopper; introducing the treated wastewater into the water distribution system, the sedimentation treatment tank and the inclined pipe in sequence; the supernatant after the treatment enters an effluent weir to obtain pretreated water, and sludge is deposited in a sludge hopper; in order to increase the precipitation area, shorten the precipitation time and improve the precipitation efficiency, the precise control high-efficiency precipitation system has the effects of hydraulic water distribution, high-efficiency precipitation and the like, the high-efficiency precipitation flocs and the SS are efficiently precipitated, the inclined pipes are arranged in the tank at the same time, so that the precipitation particles are not interfered by the influence of steady flow, the rapid precipitation effect is achieved, the processing capacity of the precise control high-efficiency precipitation system is 3-7 times greater than that of a general precipitation tank, the sludge at the bottom of the tank is discharged into a sludge tank through the arranged static pressure sludge discharge device for further concentration, then the sludge is pumped into a sludge filter press for filter pressing, the sludge cake is retreated according to the property, about 80 percent of suspended matters and 40-70 percent of oils can be removed, and the turbidity<30NTU, COD reduction 40-60%, etc.;

thirdly, the biochemical treatment process of the complexing electroplating wastewater comprises the following steps: the pretreated water sequentially enters an anaerobic tank, an aerobic tank and a membrane bioreactor; removing by biodegradation of A/O/MBRMost of COD, ammonia nitrogen, SS and other substances in the wastewater; the anaerobic process of the invention utilizes the function of anaerobic bacteria under the condition of no dissolved oxygen or under the condition of oxygen deficiency to hydrolyze and acidify organic matters, remove the organic matters in the wastewater, improve the biodegradability of the sewage and be beneficial to the subsequent aerobic treatment process; the aerobic process is that under aerobic condition, organic matter is oxidized and decomposed under the action of aerobic microbe, the concentration of organic matter is reduced, the amount of microbe is increased, the organic matter in sewage is adsorbed on the surface of active sludge and biomembrane and contacts with the surface of microbe cell, small molecular organic matter can enter microbe body through cell wall directly, and large molecular organic matter must be hydrolyzed into small molecular under the action of extracellular enzyme-hydrolase and then taken into cell body by microbe. The organic matter is finally decomposed into CO₂And H₂O; the membrane bioreactor consists of a hollow fiber membrane component and a membrane pool; preferably, the hollow fiber membrane module is located in the membrane tank; the membrane component is placed in the membrane pool, aeration is carried out in the pool, and as the aperture of the hollow fiber membrane is smaller than 0.1 micron, zoogloea and free bacteria can be completely retained in the membrane pool, so that mud-water separation is achieved, various suspended particles, bacteria, algae, turbidity and organic matters are effectively removed, and excellent effluent quality with the effluent suspended matters close to zero is ensured. The efficient interception function of the membrane bioreactor can effectively intercept nitrifying bacteria, so that the nitrification reaction is smoothly carried out, and ammonia nitrogen is effectively removed; meanwhile, macromolecular organic matters which are difficult to degrade can be intercepted, and the retention time of the macromolecular organic matters in the biochemical reaction tank is prolonged, so that the macromolecular organic matters are decomposed to the maximum extent.

Fourthly, the concentration treatment process of the complexing electroplating wastewater comprises the following steps: the biochemical treatment water sequentially passes through a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system; in order to realize zero discharge of the complexing electroplating wastewater, the rear end of the biochemical treatment system is provided with a concentration treatment system for treating strong brine generated by the biochemical treatment system; the concentration treatment system is a process combining multi-stage concentration and nanofiltration/reverse osmosis concentration, and gradually reduces the water amount of the high-salt-content wastewater (the salt content of the obtained high-salt concentrated water is 40-60g/L) through the step-by-step concentration of the membrane, so that the investment and the operating cost of a subsequent evaporative crystallization system are reduced; the concentration treatment process reduces the concentrated brine to be treated in a subsequent evaporation crystallization system by 80 percent compared with a conventional concentration treatment system, reduces the investment cost of the whole wastewater treatment system by 20 to 30 percent, reduces the running cost of wastewater treatment by 30 to 40 percent, and improves the automation degree of the system.

Fifthly, the evaporation crystallization treatment process of the complexing electroplating wastewater comprises the following steps: the high-salinity concentrated water obtained by concentration treatment sequentially passes through a heat exchanger, a concentration evaporator and an evaporation crystallizer; the invention treats the waste water to the evaporation and crystallization stage and then recycles the waste water completely, thereby realizing zero discharge of the complexing electroplating waste water; the waste water firstly enters a heat exchanger in the evaporative crystallization system, and the O in the waste water is removed through heat exchange₂And CO₂And (3) gas and waste water after heat exchange enter a concentration evaporator for evaporation concentration, when the salt concentration of the waste water is 30-35%, namely before sodium sulfate and sodium chloride are crystallized, the waste water is sent to an evaporation crystallizer to obtain crystals and condensed water, and the condensed water is used as reuse water. The evaporative crystallization system utilizes mechanical temperature increasing equipment to cause negative pressure of the waste water evaporation part, so that energy can be saved, compressed waste water steam is heated and pressurized to enter the outside of a concentration evaporator, latent heat is transferred to a pipe, the pipe is condensed into condensed water, and meanwhile, salt-containing waste water in the pipe is evaporated. The evaporative crystallization system has the characteristics of small volume, small occupied area, low energy consumption and high thermal efficiency, the power consumption of one ton of waste water is 16-20kwh, the thermal efficiency is 27 times that of a single-effect flash evaporation system and 7 times that of a four-effect flash evaporation system, the evaporative crystallization system is the most advanced evaporative concentration system at present, the generated crystals can be treated or sent to related departments for purification and utilization, and the main components of the evaporative crystallization system are sodium sulfate and sodium chloride.

The process flow of the following embodiment of the invention comprises the following basic treatment flows: electroplating complex electroplating wastewater → pretreatment process → biochemical treatment process → anaerobic tank → aerobic tank → membrane bioreactor → pressurization → first-stage nanofiltration membrane separation → pressurization → first-stage reverse osmosis membrane separation → pressurization → second-stage reverse osmosis membrane separation, and the separated high-salinity concentrated water enters an evaporation crystallization system; in the evaporative crystallization system, condensed water generated by treating high-salinity concentrated water by a concentration evaporator can meet the water quality requirement of workshop reuse water.

Example 1

(1) The complexing electroplating wastewater is pretreated to obtain pretreated water

Firstly, taking complex electroplating wastewater, wherein the complex electroplating wastewater mainly is a working section of electroplating by adopting complex metal in the electroplating process, mainly comprises copper salt and phosphate to form a plating solution, nickel sulfate, nickel acetate and the like are taken as main salts, hypophosphite, sodium borohydride, borane, hydrazine and the like are taken as reducing agents, and various auxiliary agents, reducing agents, potassium pyrophosphate, potassium citrate, nitrilotriacetic acid, additives and the like are added; the wastewater mainly comprises copper, nickel, SS, COD and other substances.

Independently collecting the complex electroplating wastewater into a complex electroplating wastewater regulating tank, introducing the wastewater into a complex breaking tank after the water quality and water quantity are sufficiently uniform, adding a sulfuric acid solution with the concentration of 10% into the complex breaking tank until the pH value is 2-3, and then adding a sodium hypochlorite solution with the concentration of 10% until the ORP value is 300-400 mv; then introducing the treated wastewater into a pH adjusting tank, and adding a 10% sodium hydroxide solution until the pH is 10-11; then the wastewater is led into a chemical reaction tank, and coagulant FeCl is added₃Then adding flocculant PAM, and stirring for 20-30 min; the time interval between the addition of the coagulant and the flocculant is 20-40 min; then introducing a precise control efficient precipitation system; preferably, the precise control efficient sedimentation system is formed by sequentially connecting a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge hopper; introducing the treated wastewater into the water distribution system, the sedimentation treatment tank and the inclined pipe in sequence; the supernatant after the treatment enters an effluent weir to obtain pretreated water, and sludge is deposited in a sludge hopper; above-mentioned high-efficient sedimentation system of accurate control shortens the settling time in order to increase the area of deposiing, improves precipitation efficiency, through the high-efficient sedimentation system's of accurate control hydraulic power water distribution, high-efficient effect such as subside, high-efficient precipitate floc and SS, sets up simultaneously in the pond the pipe chute makes the sunken granule not receive the interference that the stationary flow influences, reaches quick precipitation effect, accurate controlThe processing capacity of the high-efficiency sedimentation system is 3-7 times greater than that of a common sedimentation tank, sludge at the bottom of the sedimentation tank is discharged into a sludge tank through a static pressure sludge discharge device for further concentration, then the sludge is pumped into a sludge press filter for press filtration, and sludge cakes are reprocessed according to properties, so that about 80% of suspended matters and 40-70% of oils can be removed, and the turbidity of effluent is enabled to be<30NTU, COD reduction 40-60%, etc.;

(2) performing biochemical treatment on the pretreated water to obtain biochemical treated water

The pretreated water sequentially enters an anaerobic tank, an aerobic tank and a membrane bioreactor; wherein, the anaerobic pool contains anaerobic bacteria, and the aerobic pool contains aerobic microorganisms; the oxygen microorganism is selected from one or more of bacillus, rhizobium, nitrobacteria or mould; the bacillus, the rhizobium, the nitrobacteria or the mould is domesticated to enable the bacillus, the rhizobium, the nitrobacteria or the mould to have salt tolerance; the anaerobic pool comprises anaerobic bacteria; preferably, the anaerobic bacteria are selected from one or more of yeast, nitrate bacteria, clostridium or bacteroides, and the yeast, nitrate bacteria, clostridium or bacteroides are acclimatized to have salt tolerance; then enters a membrane bioreactor which consists of a hollow fiber membrane (the aperture of the hollow fiber membrane is 0.01-0.1 mu m) component and a membrane pool; the membrane assembly is placed in a membrane tank, aeration is carried out in the membrane tank, the pH value after biochemical treatment is 6-8, and most of substances such as COD, ammonia nitrogen, SS and the like in the wastewater can be removed; the anaerobic process of the invention utilizes the function of anaerobic bacteria under the condition of no dissolved oxygen or under the condition of oxygen deficiency to hydrolyze and acidify organic matters, remove the organic matters in the wastewater, improve the biodegradability of the sewage and be beneficial to the subsequent aerobic treatment process; the aerobic process is that under aerobic condition, organic matter is oxidized and decomposed under the action of aerobic microbe, the concentration of organic matter is reduced, the amount of microbe is increased, the organic matter in sewage is adsorbed on the surface of active sludge and biomembrane and contacts with the surface of microbe cell, small molecular organic matter can enter microbe body through cell wall directly, and large molecular organic matter must be hydrolyzed into small molecular under the action of extracellular enzyme-hydrolase and then taken into cell body by microbe. The organic matter is finally decomposed into CO₂And H₂O; the membrane bioreactor comprises a hollow fiber membrane component and a membrane pool, wherein the membrane component is placed in the membrane pool, aeration is carried out in the membrane pool, and as the pore diameter of the hollow fiber membrane is smaller than 0.1 micron, zoogloea and free bacteria can be completely retained in the membrane pool, so that mud-water separation is achieved, various suspended particles, bacteria, algae, turbidity and organic matters are effectively removed, and the excellent effluent quality with the effluent suspended matters close to zero is ensured. The efficient interception function of the membrane bioreactor can effectively intercept nitrifying bacteria, so that the nitrification reaction is smoothly carried out, and ammonia nitrogen is effectively removed; meanwhile, macromolecular organic matters which are difficult to degrade can be intercepted, and the retention time of the macromolecular organic matters in the biochemical reaction tank is prolonged, so that the macromolecular organic matters are decomposed to the maximum extent.

(3) Concentrating the biochemical treatment water to obtain high-salinity concentrated water and reuse water

The biochemical treatment water sequentially passes through a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system; the primary nanofiltration system is formed by sequentially connecting a precision filter and a primary nanofiltration membrane, wherein a filter element of the precision filter is melt-blown PP cotton, the aperture of the precision microporous filter is 5 mu m, the aperture of the primary nanofiltration membrane is 1nm, when water to be treated passes through the primary nanofiltration membrane, the rejection rate of sodium ions is 50%, and the rejection rate of heavy metal ions and salt is 98%; then passing through a primary nanofiltration system, wherein the pH is 6-8, and the membrane inlet pressure is 1.5 Mpa; the relative molecular mass interception range of the primary nanofiltration system is 300 daltons; the permeate of the primary nanofiltration system can be used as reuse water for continuous use through ion exchange;

the concentrated solution of the treated water passing through the primary nanofiltration system enters a primary reverse osmosis system, the primary reverse osmosis system is formed by sequentially connecting a precision filter and a primary reverse osmosis membrane (a brackish water reverse osmosis membrane with the aperture of 0.1-1nm), the membrane inlet pressure of the primary reverse osmosis system is 1.8Mpa, the pH is adjusted to 5-6 by 0.2% hydrochloric acid, and the rejection rate of heavy metal ions and salt is 99% by the primary reverse osmosis membrane; the permeate of the treated water passing through the primary reverse osmosis system returns to the primary nanofiltration system, and the concentrated solution enters the secondary reverse osmosis system. The secondary reverse osmosis system is formed by sequentially connecting a precision filter and a secondary reverse osmosis membrane (a seawater reverse osmosis membrane with the aperture of 0.1-1 nm); the membrane inlet pressure of the secondary reverse osmosis system is 5Mpa, the pH value is adjusted to 6-8 by 0.2% hydrochloric acid, and the rejection rate of heavy metal ions and salt is 99.9% by the secondary reverse osmosis membrane; and the permeate of the treated water passing through the secondary reverse osmosis system returns to the primary nanofiltration system, the concentrated solution is high-salt concentrated water, and the salt content of the high-salt concentrated water is 40 g/L.

In order to realize zero discharge of the complexing electroplating wastewater, the rear end of the biochemical treatment system is provided with a concentration treatment system for treating strong brine generated by the biochemical treatment system; the concentration treatment system is a process combining multi-stage concentration and nanofiltration/reverse osmosis concentration, and gradually reduces the water amount of the high-salt-content wastewater (the salt content of the obtained high-salt concentrated water is 40g/L) through the step-by-step concentration of the membrane, so that the investment and the operating cost of a subsequent evaporative crystallization system are reduced; the concentration treatment process reduces the concentrated brine to be treated in a subsequent evaporation crystallization system by 80 percent compared with a conventional concentration treatment system, reduces the investment cost of the whole wastewater treatment system by 30 percent, reduces the running cost of wastewater treatment by 40 percent, and improves the automation degree of the system. The concentration treatment process of the complexing electroplating wastewater is characterized in that the complexing electroplating wastewater is pre-concentrated by a primary nanofiltration system, the permeate of the primary nanofiltration system can be used as reuse water after ion exchange, and the concentrated solution of the primary nanofiltration system enters a primary reverse osmosis system; the permeate of the primary reverse osmosis system returns to the primary nanofiltration system, and the concentrated solution of the primary reverse osmosis system enters the secondary reverse osmosis system; and the permeate of the secondary reverse osmosis system returns to the primary nanofiltration system, and the concentrated solution of the secondary reverse osmosis system is the high-salinity concentrated water.

(4) Carrying out evaporation crystallization treatment on the high-salinity concentrated water to obtain recycled water and crystals

Sequentially passing the high-salinity concentrated water through a heat exchanger, a concentration evaporator and an evaporation crystallizer; the operating temperature of the heat exchanger is 80-100 ℃; the operating pressure of the heat exchanger is 0.05-0.1 MPa; the concentration evaporator is formed by sequentially connecting a heating chamber, a separation chamber, a circulating chamber, a liquid distributor and a demister; the evaporative crystallizer is formed by sequentially connecting a separation chamber, salt legs, a thickener and a crystallization kettle; the condensed water of the high-salinity concentrated water after passing through the concentration evaporator returns to the secondary reverse osmosis system; the concentrated solution obtained after the high-salt concentrated water passes through a concentration evaporator is concentrated high-salt concentrated water, and the salt content is 40-60 g/L; the concentrated high-salinity concentrated water passes through an evaporative crystallizer to obtain a crystal and condensed water; the obtained crystal is sodium sulfate and/or sodium chloride; and the condensed water is returned to the workshop as reuse water for continuous use.

Wherein, the concentration evaporator is composed of a plurality of evaporators connected in series, low-temperature (about 90 ℃) heating steam is introduced into the first effect to heat feed liquid therein, so that the feed liquid generates almost equivalent evaporation with the temperature lower than that of the steam. The steam produced is introduced into the second effect as heating steam, causing the feed liquid of the second effect to evaporate at a lower temperature than the first effect. This process is repeated until the final effect. The first effect condensate water returns to the heat source, other effect condensate water is collected and then output as desalted water, and one part of steam is input and can evaporate multiple times of water to be output. Meanwhile, the feed liquid is sequentially concentrated from the first effect to the last effect, and the feed liquid is supersaturated at the last effect and crystallized and separated out. Thereby realizing the solid-liquid separation of the feed liquid.

The technical parameters of the evaporative crystallization system for treating concentrated water are as follows:

(1) the desalted water has a salt content (TDS) of less than 10ppm

(2) Consumption of steam for desalting per ton is (1/effect number)/90% t/t

(3) The electric power consumption of the desalinated water is 2-4 kwh/t

Compared with the prior art, the method for treating the complexing electroplating wastewater improves the reuse rate of the wastewater to 99.67 percent, can greatly reduce the treatment cost, reduce the generation amount of solid waste and the recycling of metal ions in the wastewater, and thoroughly realizes the zero discharge of the wastewater.

In conclusion, the above description of the embodiments of the present invention is not intended to limit the present invention, and those skilled in the art can make various changes or modifications according to the present invention without departing from the spirit of the present invention, which falls within the scope of the appended claims.

Claims

1. A complex electroplating wastewater treatment method is characterized by comprising the following steps in sequence:

wherein, in the step (1), the step of preprocessing is:

(1-1) introducing the complex electroplating wastewater into a complex breaking pool, adding a 10% sulfuric acid solution into the complex breaking pool to adjust the pH value to 2-3, and then adding a 10% sodium hypochlorite solution to adjust the ORP value to 300-400 mv;

(1-2) introducing the wastewater treated in the step (1-1) into a pH adjusting tank, and adding a 10% sodium hydroxide solution to adjust the pH to 10-11;

(1-3) introducing the wastewater treated in the step (1-2) into a chemical reaction tank, and adding a coagulant FeCl₃Adding a flocculating agent PAM after 20-40min, and stirring for 20-30 min;

(1-4) introducing the wastewater treated in the step (1-3) into a precise control efficient precipitation system; the precise control efficient sedimentation system comprises a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge hopper; wherein the wastewater treated in the step (1-3) is sequentially introduced into the water distribution system, the sedimentation treatment tank and the inclined pipe; the supernatant after the treatment enters an effluent weir to obtain pretreated water, and the obtained sludge is deposited in a sludge hopper; the pressure of the sedimentation treatment tank is 2-3 Mpa;

in the step (2), the biochemical treatment step is: sequentially feeding the pretreated water obtained in the step (1) into an anaerobic tank, an aerobic tank and a membrane bioreactor; the membrane bioreactor consists of a hollow fiber membrane component and a membrane pool, wherein the hollow fiber membrane component is positioned in the membrane pool, and the aperture of the hollow fiber membrane is 0.01-0.1 mu m;

in the step (3), the concentration treatment step is: sequentially passing the biochemical treatment water obtained in the step (2) through a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system; wherein the content of the first and second substances,

the primary nanofiltration system is formed by sequentially connecting a precision filter and a primary nanofiltration membrane, wherein a filter element of the precision filter is melt-blown PP cotton, and the aperture of the filter element is 5 mu m; the primary nanofiltration membrane is an industrial grade high-desalination-rate nanofiltration membrane, and the aperture of the primary nanofiltration membrane is 1-2 nm; the membrane inlet pressure of the primary nanofiltration system is 1.0-1.5 Mpa; the concentrated solution of the primary nanofiltration system enters a primary reverse osmosis system;

the primary reverse osmosis system is formed by sequentially connecting a precision filter and a primary reverse osmosis membrane, wherein a filter element of the precision filter is melt-blown PP cotton, and the aperture of the filter element is 5 mu m; the first-stage reverse osmosis membrane is a brackish water reverse osmosis membrane, and the aperture of the first-stage reverse osmosis membrane is 0.1-1 nm; the membrane inlet pressure of the primary reverse osmosis system is 1.8 Mpa; the permeate of the first-stage reverse osmosis system returns to the first-stage nanofiltration system; the concentrated solution of the first-stage reverse osmosis system enters a second-stage reverse osmosis system;

the secondary reverse osmosis system is formed by sequentially connecting a precision filter and a secondary reverse osmosis membrane, wherein a filter element of the precision filter is melt-blown PP cotton, and the aperture of the filter element is 5 mu m; the secondary reverse osmosis membrane is a seawater reverse osmosis membrane, and the aperture of the secondary reverse osmosis membrane is 0.1-1 nm; the membrane inlet pressure of the secondary reverse osmosis system is 4-5 Mpa; the permeate of the secondary reverse osmosis system returns to the primary nanofiltration system; the concentrated solution of the secondary reverse osmosis system is the high-salinity concentrated water;

in the step (4), the evaporative crystallization treatment step is: sequentially passing the high-salinity concentrated water obtained in the step (3) through a heat exchanger, a concentration evaporator and an evaporation crystallizer, wherein the operating temperature of the heat exchanger is 80-100 ℃; the operating pressure of the heat exchanger is 0.05-0.1 MPa; the condensed water of the high-salinity concentrated water after passing through the concentration evaporator returns to the secondary reverse osmosis system;

wherein the standard of the recycled water is as follows: pH is 6-8, conductivity is less than or equal to 50 mu S/cm, COD is less than or equal to 30mg/L, and turbidity is less than or equal to 1 NTU.

2. The treatment method according to claim 1, wherein in the step (1), the pH of the complex electroplating wastewater is 2-6, and the complex electroplating wastewater contains copper, nickel, SS and COD.

3. The treatment method according to claim 1, wherein the pH of the wastewater treated in the step (1-3) is 8 to 9.

4. The process of claim 1, wherein in step (2), the anaerobic pond contains anaerobic bacteria; the anaerobic bacteria are selected from one or more of yeast, clostridium and bacteroides.

5. The process of claim 4, wherein the yeast, Clostridium or Bacteroides is acclimatized to be salt tolerant.

6. The treatment method according to claim 1, wherein in the step (2), the aerobic tank contains aerobic microorganisms; the aerobic microorganism is selected from one or more of bacillus, rhizobium, nitrobacteria and mould.

7. The method of claim 6, wherein the bacillus, rhizobium, nitrifier or mold is acclimated to provide salt tolerance.

8. The treatment method according to claim 1, wherein the post-biochemical treatment has a pH of 6 to 8.

9. The process of claim 1, wherein in the step (3), the rejection rate of the primary nanofiltration membrane on sodium ions is 50-70%.

10. The process of claim 1, wherein in the step (3), the rejection rate of the primary nanofiltration membrane on heavy metal ions and salts is more than 97%.

11. The process as claimed in claim 1, wherein in the step (3), the relative molecular mass cut-off range of the primary nanofiltration system is 150-300 daltons.

12. The process according to claim 1, wherein in the step (3), the permeate of the primary nanofiltration system is used as reuse water.

13. The process of claim 1 wherein in step (3) the primary reverse osmosis membrane has a rejection rate of > 98% for heavy metal ions and salts.

14. The process of claim 1 wherein in step (3) the pH of the water entering the primary reverse osmosis system is between 5 and 6.

15. The process of claim 1 wherein in step (3) the primary reverse osmosis system is adjusted for pH by the addition of hydrochloric acid.

16. The treatment process according to claim 15, wherein in the step (3), the pH is adjusted by adding hydrochloric acid having a concentration of 0.2 to 0.5%.

17. The process of claim 1 wherein in step (3) the secondary reverse osmosis membrane has a rejection rate of > 99.5% for heavy metal ions and salts.

18. The process of claim 1 wherein in step (3) the pH of the water entering the secondary reverse osmosis system is from 6 to 8.

19. The process of claim 1 wherein in step (3) the secondary reverse osmosis system is adjusted for pH by the addition of hydrochloric acid.

20. The process according to claim 19, characterized in that the concentration of hydrochloric acid is between 0.2 and 0.5%.

21. The process of claim 1, wherein in the step (4), the concentration evaporator comprises a heating chamber, a separation chamber, a circulation chamber, a liquid distributor and a demister which are connected in sequence.

22. The process according to claim 1, wherein in the step (4), the evaporative crystallizer consists of a separation chamber, a salt leg, a thickener and a crystallization kettle which are connected in sequence.

23. The process of claim 1, wherein in step (4), the concentrated high-salinity water is obtained after the high-salinity water passes through a concentration evaporator.

24. The process of claim 23, wherein the concentrated high salinity concentrate has a salinity of 30-35%.

25. The process of claim 23, wherein the concentrated high salinity concentrated water is passed through an evaporative crystallizer to obtain a crystallized product and condensed water.

26. The process of claim 25, wherein the crystalline material is sodium sulfate and/or sodium chloride; the condensed water is used as reuse water.

27. A treatment system for implementing the complex electroplating wastewater treatment method according to any one of claims 1 to 26, wherein the system comprises a pretreatment unit, a biochemical treatment unit, a concentration treatment unit and an evaporation crystallization treatment unit which are sequentially communicated;

the pretreatment unit comprises a collateral breaking pool, a pH adjusting pool, a chemical reaction pool and a precise control efficient precipitation system which are sequentially communicated; the precise control efficient sedimentation system comprises a water distribution system, a sedimentation treatment tank, an inclined pipe, a water outlet weir and a sludge hopper;

the biochemical treatment unit comprises an anaerobic tank, an aerobic tank and a membrane bioreactor which are communicated in sequence; wherein the membrane bioreactor consists of a hollow fiber membrane component and a membrane pool; the hollow fiber membrane module is positioned in the membrane pool; the aperture of the hollow fiber membrane is 0.01-0.1 μm;

the concentration treatment unit comprises a primary nanofiltration system, a primary reverse osmosis system and a secondary reverse osmosis system which are sequentially communicated; the primary nanofiltration system is formed by sequentially connecting a precision filter and a primary nanofiltration membrane; wherein the filter element of the precision filter is melt-blown PP cotton; the aperture of the filter element of the precision filter is 5 mu m; the primary nanofiltration membrane is an industrial grade high-desalination-rate nanofiltration membrane; the aperture of the primary nanofiltration membrane is 1-2 nm;

the first-stage reverse osmosis system is formed by sequentially connecting a precision filter and a first-stage reverse osmosis membrane; wherein the filter element of the precision filter is melt-blown PP cotton, and the aperture of the filter element is 5 mu m; the first-stage reverse osmosis membrane is a brackish water reverse osmosis membrane, and the aperture of the first-stage reverse osmosis membrane is 0.1-1 nm;

the secondary reverse osmosis system is formed by sequentially connecting a precision filter and a secondary reverse osmosis membrane; wherein the filter element of the precision filter is melt-blown PP cotton, and the aperture of the filter element is 5 mu m; the secondary reverse osmosis membrane is a seawater reverse osmosis membrane, and the aperture of the secondary reverse osmosis membrane is 0.1-1 nm;

the evaporative crystallization unit comprises a heat exchanger, a concentration evaporator and an evaporative crystallizer which are sequentially communicated.

28. The treatment system of claim 27, wherein the rejection rate of the primary nanofiltration membrane for sodium ions is 50-70%; the rejection rate of the first-stage nanofiltration membrane on heavy metal ions and salts is more than 97%.

29. The process system of claim 27, wherein the primary nanofiltration system has a membrane inlet pressure of 1.0 to 1.5 Mpa.

30. The treatment system as claimed in claim 27, wherein the relative molecular mass cut-off of the primary nanofiltration system is in the range of 150-300 daltons.

31. The treatment system of claim 27, wherein the primary reverse osmosis membrane has a rejection rate of > 98% for heavy metal ions and salts.

32. The treatment system of claim 27 wherein the primary reverse osmosis system has a membrane inlet pressure of 1.8 Mpa.

33. The treatment system of claim 27 wherein the pH of the water entering the primary reverse osmosis system is between 5 and 6.

34. The treatment system of claim 27 wherein the primary reverse osmosis system has a pH adjusted by the addition of hydrochloric acid.

35. The treatment system of claim 34, wherein the hydrochloric acid has a concentration of 0.2-0.5%.

36. The treatment system of claim 27, wherein the secondary reverse osmosis membrane has a rejection rate of > 99.5% for heavy metal ions and salts.

37. The treatment system of claim 27, wherein the secondary reverse osmosis system has a membrane inlet pressure of 4 to 5 Mpa.

38. The treatment system of claim 27 wherein the pH of the water entering the secondary reverse osmosis system is between 6 and 8.

39. The treatment system of claim 27 wherein the secondary reverse osmosis system has a pH adjusted by the addition of hydrochloric acid.

40. The treatment system of claim 39, wherein the hydrochloric acid has a concentration of 0.2-0.5%.

41. The treatment system of claim 27, wherein the operating temperature of the heat exchanger is 80-100 ℃; the operating pressure is 0.05-0.1 MPa.

42. The processing system of claim 27, wherein the concentration evaporator comprises a heating chamber, a separation chamber, a circulation chamber, a liquid distributor and a demister which are connected in sequence.

43. The processing system of claim 27, wherein the evaporative crystallizer is composed of a separation chamber, a salt leg, a thickener and a crystallization kettle which are connected in sequence.

44. Use of the treatment method of any one of claims 1 to 26 or the treatment system of any one of claims 27 to 43 for treating complex electroplating wastewater.