CN112358095B - Treatment method of EDTA complex nickel wastewater - Google Patents

Treatment method of EDTA complex nickel wastewater Download PDF

Info

Publication number
CN112358095B
CN112358095B CN202011139654.4A CN202011139654A CN112358095B CN 112358095 B CN112358095 B CN 112358095B CN 202011139654 A CN202011139654 A CN 202011139654A CN 112358095 B CN112358095 B CN 112358095B
Authority
CN
China
Prior art keywords
tank
wastewater
baffle
electrolytic
treatment
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202011139654.4A
Other languages
Chinese (zh)
Other versions
CN112358095A (en
Inventor
吴文明
王俊
李海洋
查晨
王娣
贠守宝
李淑艳
杨建�
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Singapore United Technology Anhui Co ltd
Original Assignee
China Singapore United Technology Anhui Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Singapore United Technology Anhui Co ltd filed Critical China Singapore United Technology Anhui Co ltd
Priority to CN202011139654.4A priority Critical patent/CN112358095B/en
Publication of CN112358095A publication Critical patent/CN112358095A/en
Application granted granted Critical
Publication of CN112358095B publication Critical patent/CN112358095B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Abstract

The invention discloses a treatment method of EDTA complex nickel wastewater, which specifically comprises the following steps: step one, organic acid separation, step two, first complexation breaking, step three, second complexation breaking, step four, third complexation breaking, step five, flocculation precipitation, step six, chelating resin adsorption; the invention belongs to the technical field of complex heavy metal wastewater treatment, and the invention firstly separates the organic matters by acid precipitation treatment, thereby reducing the energy consumption and the medicament consumption of the subsequent treatment; the conductivity of the complex wastewater is improved by adding ferrous ions, the generation rate of hydroxyl radicals is improved by adding hydrogen peroxide, the treatment efficiency is improved, and chemicals such as sodium hypochlorite, ferrous sulfate, hydrogen peroxide and the like are all common chemical agents, so that the price of the chemical agents is low, and the wastewater treatment operation cost can be reduced; the treatment method is characterized in that the complex nickel is stably removed through three times of complex breaking treatment, the nickel discharge concentration of treated effluent is below 0.2mg/L, and the nickel removal rate is as high as 99%.

Description

Treatment method of EDTA complex nickel wastewater
Technical Field
The invention belongs to the technical field of complex heavy metal wastewater treatment, and particularly relates to a treatment method of EDTA complex nickel wastewater.
Background
The post-nickel plating cleaning step in the plastic and metal plating processes generates a large amount of nickel-containing wastewater, and the nickel-plating cleaning water has some unique characteristics: the method has the advantages that the nickel content is high, complexing agents such as EDTA and citric acid are high, the conductivity of the wastewater is low, the ammonia nitrogen content is high, the traditional treatment process is not applicable to nickel complexing wastewater, such as Fenton oxidation method, adsorption method and ion exchange method, the structure of beta-EDTA-Ni complex cannot be completely broken, and the discharged nickel content of effluent is not up to standard; the MVR evaporation method and the triple-effect evaporation method have the defects of high equipment cost, high energy consumption and the like;
the invention patent CN109574328A discloses a method for treating hypophosphite and complex nickel wastewater, which mainly comprises the steps of oxidizing the hypophosphite by Fenton, then removing some complexes such as sodium citrate by electrolysis, and then regulating pH to promote nickel precipitation; when the wastewater contains EDTA, beta-EDTA, heterocyclic substances and other substances with strong complexation, the Fenton medicament amount is large, the amount of sludge generated during electrolysis is large, the treatment cost is increased, and the treatment effect cannot meet the pollutant emission standard requirement of the electroplating industry;
in the literature (effective current characterization of electrochemical oxidation of organic pollutants and its stage reaction kinetics, author Li Peng), a method for degrading organic matters by destroying intermolecular structures through electrochemical oxidation-reduction is proposed. The method mainly promotes the decomposition of organic matters through high oxidation-reduction potential generated by the plate spacing in the electrocatalytic process, and the literature mentions that the oxygen evolution on the surface of the electrode is a side reaction of the oxidation of the organic matters, and the higher the oxygen evolution potential is, the oxygen evolution reaction is inhibited, so that the electric energy acts on the oxidation of the organic matters, the current efficiency is improved, and the method is also a main reason that the lead dioxide electrode has higher current efficiency. The oxygen evolution potential of the beta-PbO 2/Ti electrode prepared in the literature study is 1.79V. The method for treating the metal wastewater containing the complex compound can cause plating on the surface of the polar plate, lower oxygen evolution potential and permanent damage of the polar plate, and the effluent does not reach the standard.
Therefore, the prior art mainly focuses on the oxidation and complexation breaking treatment of metal complexing organic matters, and the oxidation process is not thorough, and the special mode is needed to be used for treatment due to the specificity of the nickel plating process wastewater.
Disclosure of Invention
The invention aims to provide a treatment method of EDTA complex nickel wastewater, which solves the technical problems of low wastewater treatment efficiency, insufficient broken collaterals and incapability of reaching emission standards of total nickel in effluent in the prior art.
The aim of the invention can be achieved by the following technical scheme:
the invention relates to a treatment method of EDTA complex nickel wastewater, which specifically comprises the following steps:
firstly, pretreating EDTA complex nickel wastewater through an active carbon filter, pumping the pretreated EDTA complex nickel wastewater into an acid separation tank of a complex nickel wastewater treatment device, regulating the pH value to 2-4, standing for 30min, carrying out acid separation of organic matters, and filtering suspended matters to obtain primary treatment wastewater;
pumping the first-stage treatment wastewater into a first electrolytic cell, pumping ferrous sulfate solution into the first electrolytic cell at a flow rate of 160-180L/h, pumping sodium hypochlorite solution into the first electrolytic cell at a flow rate of 30-40L/h, pumping hydrogen peroxide into the first electrolytic cell at a flow rate of 18-26L/h, and setting the current density of a titanium-based load lead dioxide electrode to be 10mA/cm 2 Controlling the oxidation-reduction potential to be more than 1000mv, and reacting for 1h to obtain secondary treatment wastewater;
pumping the secondary treatment wastewater into a second electrolytic cell, adding alkali into the second electrolytic cell, standing for precipitation, adjusting the pH value to 10-10.5, pumping sodium hypochlorite solution into the second electrolytic cell at a flow rate of 16L/h, controlling the oxidation-reduction potential to be more than 550mv, performing secondary decomplexing, and reacting for 20-40min to obtain tertiary treatment wastewater;
pumping the third-stage treatment wastewater into a third electrolytic cell, pumping hydrogen peroxide into the third electrolytic cell at the flow rate of 16-24L/h, controlling the oxidation-reduction potential to be more than 550mv, and carrying out third complex breaking and reaction for 10min to obtain fourth-stage treatment wastewater;
pumping the fourth-stage treatment wastewater into a coagulating sedimentation tank, adding 100mg/L flocculant into the coagulating sedimentation tank, coagulating and precipitating, and filtering by an activated carbon filter to obtain fifth-stage treatment wastewater;
and step six, regulating the pH value of the wastewater subjected to the fifth-stage treatment to be 5, and carrying out adsorption treatment by using selective chelating resin, wherein the flow speed of a chelating resin tower used for the selective chelating resin is 5BV/h, and after adsorbing free nickel, discharging or recycling the treated water.
The pH value of the EDTA complex nickel wastewater is 8, and the water inflow is 8m 3 And/h, the total complex nickel content is 20-70mg/L, the EDTA content is 50-100mg/L, the ammonia nitrogen content is 200-500mg/L, the COD content is 500-1000mg/L, and the conductivity is 6000-8000us/cm.
The concentration of ferrous sulfate is 10wt%, the concentration of sodium hypochlorite solution is 10wt%, and the concentration of hydrogen peroxide is 30wt%.
The flocculant is polyacrylamide aqueous solution with the concentration of 0.1 per mill.
The complex nickel wastewater treatment device comprises an acid separation tank, a first electrolytic tank, a second electrolytic tank, a third electrolytic tank and a coagulating sedimentation tank, wherein the first electrolytic tank, the second electrolytic tank and the third electrolytic tank are sequentially arranged;
the acid separation device comprises an acid separation tank, a first electrolytic tank, a second electrolytic tank, a third electrolytic tank, a first pump, a second pump, a third pump, a fourth pump, a filter and a filter, wherein a water outlet pipe is arranged between the acid separation tank and the first electrolytic tank, the water outlet pipe is used for communicating the acid separation tank with the first electrolytic tank, the first pump is arranged on the water outlet pipe, a butterfly valve is arranged at the input end of the first pump, the first electrolytic tank is communicated with one side bottom of the second electrolytic tank through a pipeline, the second pump is arranged on the pipeline, the butterfly valve is respectively arranged at the input end of the second electrolytic tank and one side bottom of the third electrolytic tank through a pipeline, the third pump is respectively arranged at the output end of the third pump, the other side of the third electrolytic tank is communicated with the coagulating sedimentation tank through a pipeline, the butterfly valve is arranged at the input end of the fourth pump, and the filter is arranged at the output end of the fourth pump.
The acid precipitation separation tank comprises a separation tank body, a wastewater inlet is fixedly formed in the center of one side of the separation tank body, the wastewater inlet penetrates through the separation tank body, a first baffle is arranged inside the separation tank body, the first baffle is located on one side, close to the wastewater inlet, of the separation tank body, the first baffle is respectively fixedly connected with the side wall and the bottom surface of the separation tank body, a second baffle is arranged on one side, far away from the wastewater inlet, of the first baffle, the second baffle is located above the inside of the separation tank body, the second baffle is fixedly connected with the side wall of the separation tank body, an air inlet pipe is arranged on one side, far away from the first baffle, of the second baffle, an air inlet pipe is arranged on the inner side wall of the separation tank body, a plurality of small holes are formed in the inner side wall of the separation tank body, the second baffle is provided with a third baffle, the third baffle is located above the inner side wall of the separation tank body, one side, a slag scraping blade is arranged between the second baffle and the third baffle, the slag scraping blade is arranged on one side, the second baffle is fixedly connected with the side wall of the separation tank body, the second baffle is fixedly connected with the side wall of the fourth baffle, the second baffle is fixedly connected with the fourth baffle is arranged on one side, the side, far away from the fourth baffle is fixedly connected with the fourth baffle, the fourth baffle is arranged on one side, and the fourth baffle is fixedly connected with the side of the fourth baffle, and the fourth baffle is far away from the side, and the fourth baffle is fixedly connected with the side of the third baffle.
The first preparation tank is communicated with the first electrolytic cell through a first liquid inlet pipe, a first pressure pump is arranged on the first liquid inlet pipe, the second preparation tank is respectively communicated with the first electrolytic cell and the second electrolytic cell through a second liquid inlet pipe, a second pressure pump is arranged on the second liquid inlet pipe, the third preparation tank is respectively communicated with the first electrolytic cell and the third electrolytic cell through a third liquid inlet pipe, a third pressure pump is arranged on the third liquid inlet pipe, the fourth preparation tank is communicated with the coagulation sedimentation tank through a fourth liquid inlet pipe, and a fourth pressure pump is arranged on the fourth liquid inlet pipe.
The stirring mechanism comprises a frame, four stirring motors are fixedly arranged on the frame, the four stirring motors are respectively matched with a first preparation tank, a second preparation tank, a third preparation tank and a fourth preparation tank, the output end of each stirring motor is fixedly provided with a stirrer, and the stirrers are positioned inside the first preparation tank, the second preparation tank, the third preparation tank and the fourth preparation tank.
The first preparation tank, the second preparation tank, the third preparation tank and the fourth preparation tank are provided with water injection pipes on one side far away from the first electrolytic cell, and the water injection pipes are respectively communicated with the inside of the first preparation tank, the second preparation tank, the third preparation tank and the fourth preparation tank.
The invention has the beneficial effects that:
the invention obtains the first-stage treatment wastewater by carrying out organic acid precipitation separation on the filtered EDTA complex nickel wastewater, wherein the organic separation amount accounts for 3-5% of the volume of the EDTA complex nickel wastewater, and the organic treatment separation is carried out firstly, so that the energy consumption and the medicament use amount of the subsequent treatment can be reduced; the conductivity of the complex wastewater can be improved by adding ferrous ions into the primary treatment wastewater, the generation rate of hydroxyl radicals can be improved by adding hydrogen peroxide into the primary treatment wastewater and the tertiary treatment wastewater, so that the electrolysis and complexing breaking treatment efficiency is improved, and chemicals such as sodium hypochlorite, ferrous sulfate, hydrogen peroxide and the like are common chemical agents, the price of the chemical agents is low, and the operation cost of wastewater treatment can be reduced; meanwhile, the treatment method can realize the stable removal of the complex nickel through three times of complex breaking treatment, the nickel emission concentration of treated effluent is below 0.2mg/L, and the nickel removal rate is as high as 99%;
the complex nickel wastewater treatment device is used, and is distributed according to a wastewater treatment process, so that the structure is compact, the treatment efficiency is high, and the operation is convenient; the organic suspended matters can be efficiently separated by arranging a plurality of baffles in the acid precipitation separation tank and arranging a slag scraping blade and a slag collecting tank between the second baffle and the third baffle, and the wastewater and the suspended matters are further filtered and separated by arranging a filter cotton block between the third baffle and the fourth baffle, so that the amount of subsequent sediment is reduced, and the electrolysis energy consumption and the medicament use amount are reduced; through the setting of preparing the jar, the preparation and the use of the chemical agent of being convenient for improves waste water treatment efficiency.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed for the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a complex nickel wastewater treatment device according to the present invention;
FIG. 2 is a schematic diagram of the structure of the acid separation cell of the present invention;
FIG. 3 is a top view of the complex nickel wastewater treatment device of the present invention after concealing the acid separation cell;
FIG. 4 is a front view of the complex nickel wastewater treatment device of the present invention after concealing the acid separation cell.
In the drawings, the list of components represented by the various numbers is as follows:
1. an acid separation tank; 101. a separation tank body; 102. a waste water inlet; 103. a first baffle; 104. a second baffle; 105. an air inlet pipe; 106. slag scraping blades; 107. a slag collecting groove; 108. a third baffle; 109. a cotton filter block; 110. a fourth baffle; 111. a water outlet pipe; 2. a first electrolytic cell; 3. a second electrolytic cell; 4. a third electrolytic cell; 5. a coagulating sedimentation tank; 6. a first compounding tank; 7. a second compounding tank; 8. a third compounding tank; 9. a fourth compounding tank; 10. a stirring mechanism; 1001. a frame; 1002. a stirring motor; 11. and a water injection pipe.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1:
the treatment method of the EDTA complex nickel wastewater specifically comprises the following steps:
firstly, pretreating EDTA complex nickel wastewater through an active carbon filter, pumping the pretreated EDTA complex nickel wastewater into an acid precipitation separation tank 1 of a complex nickel wastewater treatment device, adjusting the pH value to 2, standing for 30min, carrying out acid precipitation separation on organic matters, and filtering suspended matters to obtain primary treatment wastewater;
pumping the first-stage treatment wastewater into a first electrolytic cell 2, pumping ferrous sulfate solution into the first electrolytic cell 2 at a flow rate of 160L/h, pumping sodium hypochlorite solution into the first electrolytic cell 2 at a flow rate of 30L/h, pumping hydrogen peroxide into the first electrolytic cell 2 at a flow rate of 18L/h, and setting the current density of a titanium-based load lead dioxide electrode to be 10mA/cm 2 Controlling the oxidation-reduction potential to 1100mv, and reacting for 1h to obtain secondary treatment wastewater;
pumping the secondary treatment wastewater into a second electrolytic cell 3, adding alkali into the second electrolytic cell 3, standing for precipitation, adjusting the pH value to 10, pumping sodium hypochlorite solution into the second electrolytic cell 3 at a flow rate of 16L/h, controlling the oxidation-reduction potential to 650mv, performing secondary decomplexing, and reacting for 20min to obtain tertiary treatment wastewater;
pumping the third-stage treatment wastewater into a third electrolytic cell 4, pumping hydrogen peroxide into the third electrolytic cell 4 at a flow rate of 16L/h, controlling the oxidation-reduction potential to be 600mv, carrying out third complex breaking, and reacting for 10min to obtain fourth-stage treatment wastewater;
pumping the fourth-stage treatment wastewater into a coagulating sedimentation tank 5, adding 100mg/L flocculant into the coagulating sedimentation tank 5, coagulating and precipitating, and filtering by an activated carbon filter to obtain fifth-stage treatment wastewater;
and step six, regulating the pH value of the wastewater subjected to the fifth-stage treatment to be 5, and carrying out adsorption treatment by using selective chelating resin, wherein the flow speed of a chelating resin tower used for the selective chelating resin is 5BV/h, and after adsorbing free nickel, discharging or recycling the treated water.
The pH value of the EDTA complex nickel wastewater is 8, and the water inflow is 8m 3 And/h, the total complex nickel content is 55mg/L, the EDTA content is 76mg/L, the ammonia nitrogen content is 350mg/L, the COD content is 640mg/L, and the conductivity is 6900us/cm.
Example 2:
the treatment method of the EDTA complex nickel wastewater specifically comprises the following steps:
firstly, pretreating EDTA complex nickel wastewater through an active carbon filter, pumping the pretreated EDTA complex nickel wastewater into an acid precipitation separation tank 1 of a complex nickel wastewater treatment device, adjusting the pH value to 3, standing for 30min, carrying out acid precipitation separation on organic matters, and filtering suspended matters to obtain primary treatment wastewater;
pumping the first-stage treatment wastewater into a first electrolytic cell 2, pumping ferrous sulfate solution into the first electrolytic cell 2 at 170L/h flow rate, pumping sodium hypochlorite solution into the first electrolytic cell 2 at 35L/h flow rate, pumping hydrogen peroxide into the first electrolytic cell 2 at 22L/h flow rate, and setting the current density of the titanium-based load lead dioxide electrode to be 10mA/cm 2 Controlling the oxidation-reduction potential to be 1200mv, and reacting for 1h to obtain secondary treatment wastewater;
pumping the secondary treatment wastewater into a second electrolytic cell 3, adding alkali into the second electrolytic cell 3, standing for precipitation, adjusting the pH value to 10.5, pumping sodium hypochlorite solution into the second electrolytic cell 3 at a flow rate of 16L/h, controlling the oxidation-reduction potential to be 700mv, performing secondary decomplexing, and reacting for 30min to obtain tertiary treatment wastewater;
pumping the third-stage treatment wastewater into a third electrolytic cell 4, pumping hydrogen peroxide into the third electrolytic cell 4 at a flow rate of 20L/h, controlling the oxidation-reduction potential to be more than 630mv, performing third complex breaking, and reacting for 10min to obtain fourth-stage treatment wastewater;
pumping the fourth-stage treatment wastewater into a coagulating sedimentation tank 5, adding 100mg/L flocculant into the coagulating sedimentation tank 5, coagulating and precipitating, and filtering by an activated carbon filter to obtain fifth-stage treatment wastewater;
and step six, regulating the pH value of the wastewater subjected to the fifth-stage treatment to be 5, and carrying out adsorption treatment by using selective chelating resin, wherein the flow speed of a chelating resin tower used for the selective chelating resin is 5BV/h, and after adsorbing free nickel, discharging or recycling the treated water.
The pH value of the EDTA complex nickel wastewater is 8, and the water inflow is 8m 3 And/h, the total complex nickel content is 58mg/L, the EDTA content is 85mg/L, the ammonia nitrogen content is 350mg/L, the COD content is 860mg/L, and the conductivity is 7200us/cm.
Example 3:
the treatment method of the EDTA complex nickel wastewater specifically comprises the following steps:
firstly, pretreating EDTA complex nickel wastewater through an active carbon filter, pumping the pretreated EDTA complex nickel wastewater into an acid precipitation separation tank 1 of a complex nickel wastewater treatment device, adjusting the pH value to 4, standing for 30min, carrying out acid precipitation separation on organic matters, and filtering suspended matters to obtain primary treatment wastewater;
pumping the first-stage treatment wastewater into a first electrolytic cell 2, pumping ferrous sulfate solution into the first electrolytic cell 2 at a flow rate of 180L/h, pumping sodium hypochlorite solution into the first electrolytic cell 2 at a flow rate of 40L/h, pumping hydrogen peroxide into the first electrolytic cell 2 at a flow rate of 26L/h, and setting the current density of a titanium-based load lead dioxide electrode to be 10mA/cm 2 Controlling the oxidation-reduction potential to be 1200mv, and reacting for 1h to obtain secondary treatment wastewater;
pumping the secondary treatment wastewater into a second electrolytic cell 3, adding alkali into the second electrolytic cell 3, standing for precipitation, adjusting the pH value to 10.5, pumping sodium hypochlorite solution into the second electrolytic cell 3 at a flow rate of 16L/h, controlling the oxidation-reduction potential to 650mv, performing secondary decomplexing, and reacting for 40min to obtain tertiary treatment wastewater;
pumping the third-stage treatment wastewater into a third electrolytic cell 4, pumping hydrogen peroxide into the third electrolytic cell 4 at the flow rate of 24L/h, controlling the oxidation-reduction potential to be more than 600mv, carrying out third complex breaking, and reacting for 10min to obtain fourth-stage treatment wastewater;
pumping the fourth-stage treatment wastewater into a coagulating sedimentation tank 5, adding 100mg/L flocculant into the coagulating sedimentation tank 5, coagulating and precipitating, and filtering by an activated carbon filter to obtain fifth-stage treatment wastewater;
and step six, regulating the pH value of the wastewater subjected to the fifth-stage treatment to be 5, and carrying out adsorption treatment by using selective chelating resin, wherein the flow speed of a chelating resin tower used for the selective chelating resin is 5BV/h, and after adsorbing free nickel, discharging or recycling the treated water.
The pH value of the EDTA complex nickel wastewater is 8, and the water inflow is 8m 3 And/h, the total complex nickel content is 70mg/L, the EDTA content is 100mg/L, the ammonia nitrogen content is 500mg/L, the COD content is 1000mg/L, and the conductivity is 8000us/cm.
The concentration of ferrous sulfate is 10wt%, the concentration of sodium hypochlorite solution is 10wt%, and the concentration of hydrogen peroxide is 30wt%.
The flocculant is polyacrylamide aqueous solution with the concentration of 0.1 per mill.
Referring to fig. 1-4, the complex nickel wastewater treatment device in the foregoing embodiment includes an acid separation tank 1, a first electrolytic tank 2, a second electrolytic tank 3, a third electrolytic tank 4 and a coagulating sedimentation tank 5, where the first electrolytic tank 2, the second electrolytic tank 3 and the third electrolytic tank 4 are sequentially arranged, the acid separation tank 1 is disposed on one side of the first electrolytic tank 2, the second electrolytic tank 3 and the third electrolytic tank 4, the coagulating sedimentation tank 5 is disposed on one side of the third electrolytic tank 4 away from the acid separation tank 1, a first preparation tank 6, a second preparation tank 7, a third preparation tank 8 and a fourth preparation tank 9 are disposed on one side of the first electrolytic tank 2 away from the second electrolytic tank 3, and a stirring mechanism 10 is disposed above the first preparation tank 6, the second preparation tank 7, the third preparation tank 8 and the fourth preparation tank 9;
the acid separation device is characterized in that a water outlet pipe 111 is arranged between the acid separation tank 1 and the first electrolytic tank 2, the water outlet pipe 111 is used for communicating the acid separation tank 1 with the first electrolytic tank 2, a first pump is arranged on the water outlet pipe 111, a butterfly valve is arranged at the input end of the first pump, the first electrolytic tank 2 is communicated with one side bottom end of the second electrolytic tank 3 through a pipeline, a second pump is arranged on the pipeline, butterfly valves are respectively arranged at the input end and the output end of the second pump, the second electrolytic tank 3 is communicated with one side bottom end of the third electrolytic tank 4 through a pipeline, a third pump is arranged on the pipeline, butterfly valves are respectively arranged at the input end and the output end of the third pump, the other side of the third electrolytic tank 4 is communicated with the coagulating sedimentation tank 5 through a pipeline, a fourth pump is arranged on the pipeline, a butterfly valve is arranged at the input end of the fourth pump, and a filter is arranged at the output end.
The acid separation tank 1 comprises a separation tank body 101, a wastewater inlet 102 is fixedly arranged in the center of one side of the separation tank body 101, the wastewater inlet 102 penetrates through the separation tank body 101, a first baffle 103 is arranged in the separation tank body 101, the first baffle 103 is positioned at one side, close to the wastewater inlet 102, of the separation tank body 101, the first baffle 103 is fixedly connected with the side wall and the bottom surface of the separation tank body 101 respectively, a second baffle 104 is arranged at one side, far away from the wastewater inlet 102, of the first baffle 103, and is positioned above the inside of the separation tank body 101, the second baffle 104 is fixedly connected with the side wall of the separation tank body 101, an air inlet pipe 105 is arranged at one side, far away from the first baffle 103, of the second baffle 104, the air inlet 105 is positioned at the bottom end inside the separation tank body 101, the air inlet 105 penetrates through the side wall of the separation tank body 101, one end of the air inlet 105 is closed, the other end of the air inlet 105 is communicated with an air pump, the air inlet pipe 105 is provided with a plurality of small holes which are uniformly distributed on the pipe wall inside the separating tank body 101, one side of the second baffle 104, which is far away from the first baffle 103, is provided with a third baffle 108, the third baffle 108 is positioned above the inside of the separating tank body 101, the third baffle 108 is fixedly connected with the side wall of the separating tank body 101, a slag scraping blade 106 is arranged between the second baffle 104 and the third baffle 108, two ends of the slag scraping blade 106 are rotationally connected with the side wall of the separating tank body 101, one end of the slag scraping blade 106 is fixedly connected with the output end of a driving motor, a slag collecting groove 107 is fixedly arranged above one side, which is close to the second baffle 104, of the third baffle 108, the edge of the slag collecting groove 107 is matched with the slag scraping blade 106, one side, which is far away from the second baffle 104, of the third baffle 108 is provided with a fourth baffle 110, the fourth baffle 110 is respectively fixedly connected with the side wall and the bottom surface of the separating tank body 101, a filter cotton block 109 is arranged between the fourth baffle 110 and the third baffle 108, and a water outlet pipe 111 is arranged on one side of the fourth baffle 110 away from the third baffle 108.
The first preparation tank 6 is communicated with the first electrolytic cell 2 through a first liquid inlet pipe, a first pressure pump is arranged on the first liquid inlet pipe, the second preparation tank 7 is respectively communicated with the first electrolytic cell 2 and the second electrolytic cell 3 through a second liquid inlet pipe, a second pressure pump is arranged on the second liquid inlet pipe, the third preparation tank 8 is respectively communicated with the first electrolytic cell 2 and the third electrolytic cell 4 through a third liquid inlet pipe, a third pressure pump is arranged on the third liquid inlet pipe, the fourth preparation tank 9 is communicated with the coagulation sedimentation tank 5 through a fourth liquid inlet pipe, and a fourth pressure pump is arranged on the fourth liquid inlet pipe.
The stirring mechanism 10 comprises a frame 1001, four stirring motors 1002 are fixedly arranged on the frame 1001, the four stirring motors 1002 are respectively matched with a first preparation tank 6, a second preparation tank 7, a third preparation tank 8 and a fourth preparation tank 9, the output end of the stirring motor 1002 is fixedly provided with a stirrer, and the stirrer is positioned inside the first preparation tank 6, the second preparation tank 7, the third preparation tank 8 and the fourth preparation tank 9.
The first preparation tank 6, the second preparation tank 7, the third preparation tank 8 and the fourth preparation tank 9 are provided with water injection pipes 11 at one side far away from the first electrolytic cell 2, and the water injection pipes 11 are respectively communicated with the inside of the first preparation tank 6, the second preparation tank 7, the third preparation tank 8 and the fourth preparation tank 9.
The working principle of the invention is as follows:
when in use, filtered EDTA complex nickel wastewater is injected into the separating tank body 101 from the wastewater inlet 102, the pH of the wastewater is adjusted by adding acid between the second baffle 104 and the third baffle 108, air is introduced into the air inlet pipe 105 after the wastewater is subjected to acid precipitation, separation and standing, suspended matters float on the upper layer, the slag scraping blade 106 is rotated, the suspended matters on the upper layer are separated into the slag collecting tank 107, the first-stage treatment wastewater is obtained through filtration of the filter cotton block 109, and the first-stage treatment wastewater is pumped into the first electrolytic tank 2 through the water outlet pipe 111 and the first pump;
ferrous sulfate, sodium hypochlorite, hydrogen peroxide and flocculant are respectively added into a first preparation tank 6, a second preparation tank 7, a third preparation tank 8 and a fourth preparation tank 9, water is respectively added into the first preparation tank 6, the second preparation tank 7, the third preparation tank 8 and the fourth preparation tank 9 through water injection pipes 11, and reagents with required concentration are respectively prepared, and a stirring motor 1002 is started for stirring; the first pressure pump is opened, ferrous sulfate solution is added into the first electrolytic cell 2 through the first liquid inlet pipe, the second pressure pump is opened, sodium hypochlorite solution is added into the first electrolytic cell 2 through the second liquid inlet pipe, the third pressure pump is opened, hydrogen peroxide is added into the first electrolytic cell 2 through the third liquid inlet pipe, the titanium-based load lead dioxide electrode of the first electrolytic cell 2 is electrified to perform first complexing breaking, the titanium-based load lead dioxide electrode is connected with a rectifier, passivation of polar plates can be prevented, and secondary treatment wastewater is obtained after the reaction is completed; pumping the secondary treatment wastewater into a second electrolytic cell 3 through a second pump, adding alkali to adjust pH, controlling a water pipe switch on a second liquid inlet pipe, adding sodium hypochlorite solution into the second electrolytic cell 3, electrifying an electrode of the second electrolytic cell 3, performing secondary complex breaking, and obtaining tertiary treatment wastewater after the reaction is completed; pumping the third-stage treated wastewater into a third electrolytic cell 4 through a third pump, controlling a water pipe switch on a third liquid inlet pipe, adding hydrogen peroxide into the third electrolytic cell 4, electrifying an electrode of the third electrolytic cell 4, carrying out third complex breaking, and obtaining fourth-stage treated wastewater after the reaction is completed; pumping the fourth-stage treatment wastewater into a coagulating sedimentation tank 5 through a fourth pump, opening a fourth pressure pump, adding a flocculating agent into the coagulating sedimentation tank 5 through a fourth liquid inlet pipe, and obtaining fifth-stage treatment wastewater after coagulating sedimentation is completed; and (3) regulating the pH value of the wastewater subjected to the fifth-stage treatment, and then introducing the wastewater subjected to the fifth-stage treatment into a chelating resin tower, and adsorbing free nickel in the wastewater subjected to the fifth-stage treatment, thereby completing the wastewater treatment flow of all EDTA complex nickel wastewater.
The foregoing is merely illustrative and explanatory of the principles of the invention, as various modifications and additions may be made to the specific embodiments described, or similar thereto, by those skilled in the art, without departing from the principles of the invention or beyond the scope of the appended claims.

Claims (8)

  1. A treatment method of EDTA complex nickel wastewater is characterized by comprising the following steps: the method comprises the steps that a nickel complexing wastewater treatment device is adopted, the nickel complexing wastewater treatment device comprises an acid separation tank (1), a first electrolytic tank (2), a second electrolytic tank (3), a third electrolytic tank (4) and a coagulating sedimentation tank (5), the first electrolytic tank (2), the second electrolytic tank (3) and the third electrolytic tank (4) are sequentially arranged, the acid separation tank (1) is arranged on one side of the first electrolytic tank (2), one side of the second electrolytic tank (3) and one side of the third electrolytic tank (4) far away from the acid separation tank (1), the coagulating sedimentation tank (5) is arranged on one side of the third electrolytic tank (4) far away from the acid separation tank (1), a first preparation tank (6), a second preparation tank (7), a third preparation tank (8) and a fourth preparation tank (9) are arranged on one side of the first preparation tank (6), the second preparation tank (7), the third preparation tank (8) and the fourth preparation tank (9) are provided with a stirring mechanism (10);
    the acid separation tank (1) comprises a separation tank body (101), a wastewater inlet (102) is fixedly arranged in the center of one side of the separation tank body (101), the wastewater inlet (102) penetrates through the separation tank body (101), a first baffle (103) is arranged in one side, close to the wastewater inlet (102), of the separation tank body (101), the first baffle (103) is fixedly connected with the side wall and the bottom surface of the separation tank body (101) respectively, a second baffle (104) is arranged on one side, far away from the wastewater inlet (102), of the first baffle (103), the second baffle (104) is arranged above the inside of the separation tank body (101), the second baffle (104) is fixedly connected with the side wall of the separation tank body (101), an air inlet pipe (105) is arranged on one side, far away from the first baffle (103), of the second baffle (104) and is provided with an air inlet pipe (105), the air inlet pipe (105) is arranged at the bottom end, close to the side wall of the separation tank body (101), one end of the air inlet pipe (105) is communicated with the air inlet pipe (101), the air inlet pipe (105) is uniformly distributed on the side, far away from the first baffle (103), the third baffle (108) is positioned above the inside of the separation tank body (101), the third baffle (108) is fixedly connected with the side wall of the separation tank body (101), a slag scraping blade (106) is arranged between the second baffle (104) and the third baffle (108), two ends of the slag scraping blade (106) are rotationally connected with the side wall of the separation tank body (101), one end of the slag scraping blade (106) is fixedly connected with the output end of the driving motor, a slag collecting groove (107) is fixedly arranged above one side, close to the second baffle (104), of the third baffle (108), the edge of the slag collecting groove (107) is matched with the slag scraping blade (106), a fourth baffle (110) is arranged on one side, far away from the second baffle (104), of the third baffle (108), the fourth baffle (110) is fixedly connected with the side wall and the bottom surface of the separation tank body (101), cotton filtering blocks (109) are arranged between the fourth baffle (110) and the third baffle (108), and a water outlet pipe (111) is arranged on one side, far away from the third baffle (108);
    the method specifically comprises the following steps:
    firstly, pretreating EDTA complex nickel wastewater through an active carbon filter, pumping the pretreated EDTA complex nickel wastewater into an acid precipitation separation tank (1) of a complex nickel wastewater treatment device, regulating the pH value to 2-4, standing for 30min, carrying out acid precipitation separation on organic matters, and filtering suspended matters to obtain primary treatment wastewater;
    pumping the primary treatment wastewater into a first electrolytic cell (2), pumping ferrous sulfate solution into the first electrolytic cell (2) at a flow rate of 160-180L/h, pumping sodium hypochlorite solution into the first electrolytic cell (2) at a flow rate of 30-40L/h, pumping hydrogen peroxide into the first electrolytic cell (2) at a flow rate of 18-26L/h, setting the current density of a titanium-based lead dioxide electrode to be 10mA/cm < 2 >, controlling the oxidation-reduction potential to be more than 1000mv, and reacting for 1h to obtain secondary treatment wastewater;
    pumping the secondary treatment wastewater into a second electrolytic cell (3), adding alkali into the second electrolytic cell (3), standing for precipitation, adjusting the pH value to 10-10.5, pumping sodium hypochlorite solution into the second electrolytic cell (3) at a flow rate of 16L/h, controlling the oxidation-reduction potential to be more than 550mv, performing secondary complexing breaking, and reacting for 20-40min to obtain tertiary treatment wastewater;
    pumping the third-stage treatment wastewater into a third electrolytic cell (4), pumping hydrogen peroxide into the third electrolytic cell (4) at the flow rate of 16-24L/h, controlling the oxidation-reduction potential to be more than 550mv, and carrying out third complexation breaking for 10min to obtain fourth-stage treatment wastewater;
    pumping the fourth-stage treatment wastewater into a coagulating sedimentation tank (5), adding 100mg/L flocculant into the coagulating sedimentation tank (5), coagulating and precipitating, and filtering by an activated carbon filter to obtain fifth-stage treatment wastewater;
    and step six, regulating the pH value of the wastewater subjected to the fifth-stage treatment to be 5, and carrying out adsorption treatment by using selective chelating resin, wherein the flow speed of a chelating resin tower used for the selective chelating resin is 5BV/h, and after adsorbing free nickel, discharging or recycling the treated water.
  2. 2. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the pH value of the EDTA complex nickel wastewater is 8, the water inflow is 8m3/h, the total complex nickel content is 20-70mg/L, the EDTA content is 50-100mg/L, the ammonia nitrogen content is 200-500mg/L, the COD content is 500-1000mg/L, and the conductivity is 6000-8000us/cm.
  3. 3. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the concentration of ferrous sulfate is 10wt%, the concentration of sodium hypochlorite solution is 10wt%, and the concentration of hydrogen peroxide is 30wt%.
  4. 4. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the flocculant is polyacrylamide aqueous solution with the concentration of 0.1 per mill.
  5. 5. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the acid separation device comprises an acid separation tank (1) and a first electrolytic tank (2), wherein a water outlet pipe (111) is arranged between the acid separation tank (1) and the first electrolytic tank (2), the water outlet pipe (111) is communicated with the acid separation tank (1) and the first electrolytic tank (2), a first pump is arranged on the water outlet pipe (111), a butterfly valve is arranged at the input end of the first pump, the first electrolytic tank (2) is communicated with one side bottom end of a second electrolytic tank (3) through a pipeline, a second pump is arranged on the pipeline, butterfly valves are respectively arranged at the input end and the output end of the second pump, the second electrolytic tank (3) is communicated with one side bottom end of a third electrolytic tank (4) through a pipeline, a butterfly valve is respectively arranged at the input end and the output end of the third pump, a fourth pump is arranged on the pipeline, a butterfly valve is arranged at the input end of the fourth pump, and a filter is arranged at the output end.
  6. 6. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the first preparation tank (6) is communicated with the first electrolytic tank (2) through a first liquid inlet pipe, a first pressure pump is arranged on the first liquid inlet pipe, the second preparation tank (7) is respectively communicated with the first electrolytic tank (2) and the second electrolytic tank (3) through a second liquid inlet pipe, a second pressure pump is arranged on the second liquid inlet pipe, the third preparation tank (8) is respectively communicated with the first electrolytic tank (2) and the third electrolytic tank (4) through a third liquid inlet pipe, a third pressure pump is arranged on the third liquid inlet pipe, the fourth preparation tank (9) is communicated with the coagulating sedimentation tank (5) through a fourth liquid inlet pipe, and a fourth pressure pump is arranged on the fourth liquid inlet pipe.
  7. 7. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the stirring mechanism (10) comprises a frame (1001), four stirring motors (1002) are fixedly arranged on the frame (1001), the four stirring motors (1002) are respectively matched with a first preparation tank (6), a second preparation tank (7), a third preparation tank (8) and a fourth preparation tank (9), a stirrer is fixedly arranged at the output end of the stirring motor (1002), and the stirrer is positioned inside the first preparation tank (6), the second preparation tank (7), the third preparation tank (8) and the fourth preparation tank (9).
  8. 8. The method for treating EDTA-complexed nickel wastewater according to claim 1, wherein: the first preparation tank (6), the second preparation tank (7), the third preparation tank (8) and the fourth preparation tank (9) are provided with a water injection pipe (11) on one side far away from the first electrolytic cell (2), and the water injection pipe (11) is respectively communicated with the inside of the first preparation tank (6), the second preparation tank (7), the third preparation tank (8) and the fourth preparation tank (9).
CN202011139654.4A 2020-10-22 2020-10-22 Treatment method of EDTA complex nickel wastewater Active CN112358095B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202011139654.4A CN112358095B (en) 2020-10-22 2020-10-22 Treatment method of EDTA complex nickel wastewater

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202011139654.4A CN112358095B (en) 2020-10-22 2020-10-22 Treatment method of EDTA complex nickel wastewater

Publications (2)

Publication Number Publication Date
CN112358095A CN112358095A (en) 2021-02-12
CN112358095B true CN112358095B (en) 2023-08-29

Family

ID=74511617

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202011139654.4A Active CN112358095B (en) 2020-10-22 2020-10-22 Treatment method of EDTA complex nickel wastewater

Country Status (1)

Country Link
CN (1) CN112358095B (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112960829B (en) * 2021-02-20 2022-08-23 成都明天高新产业有限责任公司 Process for treating copper-containing wastewater generated in production of printed circuit boards
CN113955883A (en) * 2021-09-30 2022-01-21 苏州仕净科技股份有限公司 Treatment process of high-COD high-complex nickel wastewater

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5904832A (en) * 1996-12-20 1999-05-18 Huron Tech Canada, Inc. Regeneration of active carbon and polymeric adsorbents
CN107055965A (en) * 2017-05-10 2017-08-18 深圳市凯宏膜环保科技有限公司 A kind of circuit board PCB wastewater treatments integration MBR film integrated system equipment
CN207608469U (en) * 2017-12-06 2018-07-13 佛山市三水三丰包装材料有限公司 A kind of corrugated paper printing sewage treatment equipment
CN209307172U (en) * 2018-11-16 2019-08-27 珠海市海绿环保科技有限公司 A kind of printing printing ink wastewater treatment system

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5904832A (en) * 1996-12-20 1999-05-18 Huron Tech Canada, Inc. Regeneration of active carbon and polymeric adsorbents
CN107055965A (en) * 2017-05-10 2017-08-18 深圳市凯宏膜环保科技有限公司 A kind of circuit board PCB wastewater treatments integration MBR film integrated system equipment
CN207608469U (en) * 2017-12-06 2018-07-13 佛山市三水三丰包装材料有限公司 A kind of corrugated paper printing sewage treatment equipment
CN209307172U (en) * 2018-11-16 2019-08-27 珠海市海绿环保科技有限公司 A kind of printing printing ink wastewater treatment system

Also Published As

Publication number Publication date
CN112358095A (en) 2021-02-12

Similar Documents

Publication Publication Date Title
CN104386874B (en) A kind of wiring board industry high-concentration waste liquor treating process
CN206142964U (en) Integration high concentration sewage advanced oxidation treatment equipment
CN111410345A (en) Method and system for treating comprehensive wastewater generated by anodic oxidation process
CN112358095B (en) Treatment method of EDTA complex nickel wastewater
CN105540947A (en) Method and system for processing drilling wastewater
CN101781001A (en) Method for processing effluent by two-stage electrolysis and device thereof
CN109019959A (en) A kind of processing unit of strong complex state heavy metal wastewater thereby and its discharge and reuse technology
CN107857401B (en) Landfill leachate nanofiltration concentrate treatment combination device
CN110921785B (en) Electric filtration catalysis persulfate water treatment equipment and method for treating water by using same
CN104129875A (en) Cyanated wastewater treatment method
CN210176671U (en) High-salt high-concentration degradation-resistant organic wastewater treatment equipment
CN110668617A (en) Method for treating industrial wastewater difficult to degrade
CN101549920A (en) Method for recovering nickel salts in nickel-electroplating waste water
CN104030500B (en) A kind of Processes and apparatus removing nickel ion in section aluminum waste water
CN211056864U (en) Recycling equipment for treating nickel-containing wastewater
CN205099523U (en) Heavy metal wastewater handles and recovery system
CN104211232A (en) Method for coal ash and scrap iron combined treatment of dyeing and printing wastewater
CN106477807A (en) Electroplating wastewater processing medicament and processing method
CN207109133U (en) The quick clean online plating solution negative pressure evaporation equipment for reclaiming of electronickelling production line
CN212403790U (en) System for treating comprehensive wastewater generated by anodic oxidation process
CN105174567A (en) Heavy metal wastewater treatment and recovery system and method
CN210559900U (en) Chemical nickel waste water electrocatalytic oxidation treatment system
CN213803052U (en) Cleaning system for iron-manganese scaling of electrodialysis system
CN105347580B (en) A kind of method of suitable polymer flooding water processing standard discharge
CN108545871A (en) A kind of circuit-board industry chemical nickel waste water treatment system and its processing method

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant