CN212741066U - Electroplating nickel-containing wastewater treatment device - Google Patents
Electroplating nickel-containing wastewater treatment device Download PDFInfo
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- CN212741066U CN212741066U CN202020897134.9U CN202020897134U CN212741066U CN 212741066 U CN212741066 U CN 212741066U CN 202020897134 U CN202020897134 U CN 202020897134U CN 212741066 U CN212741066 U CN 212741066U
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Abstract
The utility model discloses a processing apparatus for electroplating nickel-containing wastewater. The utility model discloses a processing apparatus of nickeliferous waste water of electroplating thoughtlessly congeals device, one-level sedimentation tank, one-level fenton reaction unit, submergence formula ultrafiltration membrane reactor, second grade coagulation unit, second grade sedimentation tank, biochemical reaction pond and membrane bioreactor including consecutive preliminary treatment. Utilize the utility model provides a processing apparatus handles electroplating nickel waste water, can stably get rid of characteristic pollutant such as heavy metal, COD, ammonia nitrogen in the electroplating effluent, guarantees that electroplating effluent treatment goes out water up to standard or reaches the reuse of reclaimed water condition, and the running cost is more economical moreover.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment, in particular to a treatment device for nickel-containing electroplating wastewater.
Background
The nickel-containing wastewater in the electroplating industry refers to cleaning water generated in nickel electroplating, waste liquid discharged after pretreatment of high-concentration nickel waste liquid, comprehensive wastewater of an electroplating plant and the like. The electroplating wastewater has complex water quality components and contains a large amount of heavy metal ions and organic pollutants, particularly chemical nickel plating wastewater, and the wastewater contains a large amount of complexing agents which coexist with nickel, copper and other metal ions in a complexing way, such as citric acid, tartaric acid, sodium hypophosphite and the like, so that the heavy metal ions are difficult to effectively remove through coagulating sedimentation and can be removed only after the complexing is broken. The traditional complex breaking process mainly comprises a chemical oxidation complex breaking process, an electrochemical oxidation complex breaking process and the like, wherein the chemical oxidation complex breaking process mainly uses oxidants such as ozone, sodium hypochlorite, Fenton reagent and the like, and because the components of the chemical nickel plating wastewater are complex, the chemical nickel plating wastewater has a good removal effect, the oxidant adding amount is large, and the treatment cost is high. The stability of the electrochemical oxidation complex breaking effect is poor, and the nickel-containing wastewater is difficult to be treated in a large scale.
The electroplating nickel-containing wastewater not only contains heavy metal pollution components, but also contains a large amount of organic and nitrogen and phosphorus components, and the organic and nitrogen and phosphorus components need to be further removed. Heavy metal ions have biotoxicity, and after conventional treatment, treated effluent cannot be guaranteed to directly enter a biochemical system, so that organic matters, nitrogen, phosphorus and other pollution components are removed. Therefore, how to effectively treat the chemical nickel plating wastewater is a difficult problem.
The electroplating enterprises have large water discharge quality and water quantity fluctuation due to production property, and the stable operation pressure of the sewage treatment unit is large, so that a large-scale electroplating industrial park is built, and the wastewater of each procedure of the electroplating enterprises is classified, collected and treated in a centralized way to become the wastewater treatment trend of the electroplating industry in the future. Therefore, a large-scale electroplating wastewater treatment device which can stably operate and has low operation cost is needed at present.
SUMMERY OF THE UTILITY MODEL
The utility model discloses aim at solving one of the technical problem that exists among the above-mentioned prior art at least. Therefore, the utility model aims to provide a processing apparatus of electroplating nickeliferous waste water. The treatment device can be used for centralized treatment of nickel-containing wastewater in an electroplating industrial park.
In order to realize the purpose, the utility model adopts the technical scheme that:
the utility model provides an electroplate processing apparatus who contains nickel waste water, this processing apparatus coagulate device, one-level sedimentation tank, one-level fenton reaction unit, submergence formula ultrafiltration membrane reactor (MCR), second grade coagulation device, second grade sedimentation tank, biochemical reaction pond and Membrane Bioreactor (MBR) including consecutive preliminary treatment.
Preferably, in the device for treating nickel-containing electroplating wastewater, the pretreatment coagulation device comprises a first pH adjusting tank, a coagulant dosing tank and a first flocculant dosing tank which are connected in sequence.
Preferably, in the device for treating nickel-containing electroplating wastewater, the coagulant adding pool is a polyaluminium chloride (PAC) adding pool.
Preferably, in the treatment device for nickel-containing electroplating wastewater, the first flocculating agent dosing pool is a Polyacrylamide (PAM) dosing pool.
Preferably, in the treatment device for nickel-containing electroplating wastewater, the primary Fenton reaction device comprises a second pH adjusting tank, a first ferrous sulfate dosing tank, a hydrogen peroxide dosing tank, a Fenton reaction tank, an aeration tank and a first alkali regulating tank which are connected in sequence.
Preferably, in the nickel-containing electroplating wastewater treatment device, a TOC (total organic carbon) online detection device is arranged at the water inlet end of the primary Fenton reaction device.
Preferably, in the treatment device for nickel-containing electroplating wastewater, the secondary coagulation device comprises a third pH adjusting tank, a heavy metal collector dosing tank, a second ferrous sulfate dosing tank, a second alkali adjusting tank and a second flocculant dosing tank which are connected in sequence.
Preferably, in the treatment device for nickel-containing electroplating wastewater, the heavy metal capturing agent added in the heavy metal capturing agent adding tank is a substance with chelating capacity with heavy metal ions, such as inorganic sulfide or organic sulfide; further preferably, the heavy metal trapping agent is at least one selected from the group consisting of sodium sulfide, sodium polysulfide, sodium dimethyldithiocarbamate, sodium diethyldithiocarbamate, N-bis (dithiocarboxy) diethylenetriamine ethyl polymer, and DTCR heavy metal trapping agent.
Preferably, in the treatment device for nickel-containing electroplating wastewater, the second flocculating agent dosing pool is a polyacrylamide dosing pool.
Preferably, in the nickel-containing electroplating wastewater treatment device, the biochemical reaction tank comprises an anaerobic tank and an aerobic tank which are connected in sequence.
Preferably, in the treatment device for nickel-containing electroplating wastewater, all the device units are connected in series.
Preferably, in the nickel-containing electroplating wastewater treatment device, the water inlet of the primary sedimentation tank is connected with the sludge discharge port of the immersed ultrafiltration membrane reactor.
Preferably, in the device for treating nickel-containing electroplating wastewater, a water inlet of a coagulant adding pool is connected with a sludge discharge port of the immersed ultrafiltration membrane reactor.
Preferably, in the nickel-containing electroplating wastewater treatment device, the immersed ultrafiltration membrane reactor is internally provided with a hollow fiber ultrafiltration membrane component.
Preferably, in the treatment device for nickel-containing electroplating wastewater, the first pH adjusting tank, the coagulant adding tank, the first flocculant adding tank, the second pH adjusting tank, the first ferrous sulfate adding tank, the hydrogen peroxide adding tank, the fenton reaction tank, the first alkali adjusting tank, the third pH adjusting tank, the heavy metal collector adding tank, the second ferrous sulfate adding tank, the second alkali adjusting tank and the second flocculant adding tank are all provided with stirring devices.
The utility model has the advantages that:
utilize the utility model provides a processing apparatus handles electroplating nickel waste water, can stably get rid of characteristic pollutant such as heavy metal, COD, ammonia nitrogen in the electroplating effluent, guarantees that electroplating effluent treatment goes out water up to standard or reaches the reuse of reclaimed water condition, and the running cost is more economical moreover.
Drawings
FIG. 1 is a schematic view of an apparatus for treating nickel-containing electroplating wastewater according to the present invention;
FIG. 2 is a schematic view of an apparatus for treating nickel-containing wastewater in accordance with an embodiment.
In FIG. 2, 100-pretreatment coagulation device, 110-first pH adjusting tank, 120-coagulant dosing tank, 130-first flocculant dosing tank, 200-first precipitation tank, 300-first Fenton reaction device, 310-second pH adjusting tank, 320-first ferrous sulfate dosing tank, 330-hydrogen peroxide dosing tank, 340-Fenton reaction tank, 350-aeration tank, 360-first alkali adjusting tank, 400-submerged ultrafiltration membrane reactor, 500-second coagulation device, 510-third pH adjusting tank, 520-heavy metal collector dosing tank, 530-second ferrous sulfate dosing tank, 540-second alkali adjusting tank, 550-second flocculant dosing tank, 600-second precipitation tank, 700-biochemical reaction tank, 710-anaerobic tank, 720-aerobic tank, 800-membrane bioreactor.
Detailed Description
The embodiments of the present invention will be described in detail below, and the embodiments described with reference to the drawings are exemplary only for the purpose of explaining the present invention, and should not be construed as limiting the present invention. As will be apparent to those skilled in the art,
in the description of the present invention, it is to be understood that the terms "upper", "lower", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention.
If the first and second are described for the purpose of distinguishing technical features, they are not to be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated or implicitly indicating the precedence of the technical features indicated.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The starting materials, reagents or apparatus used in the examples and comparative examples were obtained from conventional commercial sources or can be obtained by a method of the prior art, unless otherwise specified. Unless otherwise indicated, the testing or testing methods are conventional in the art.
As shown in figure 1, the treatment device for nickel-containing electroplating wastewater comprises a pretreatment coagulation device, a primary sedimentation tank, a primary Fenton reaction device, an immersed ultrafiltration membrane reactor, a secondary coagulation device, a secondary sedimentation tank, a biochemical reaction tank and a membrane bioreactor which are connected in sequence. The sludge discharge port of the immersed ultrafiltration membrane reactor is also connected with the water inlet of the primary sedimentation tank.
An electroplating nickel-containing wastewater treatment device according to an embodiment of the utility model is described below with reference to fig. 2.
As shown in fig. 2, the nickel-containing electroplating wastewater treatment device according to the embodiment of the present invention comprises a pretreatment coagulation device 100, a primary sedimentation tank 200, a primary fenton reaction device 300, an immersed ultrafiltration membrane reactor 400, a secondary coagulation device 500, a secondary sedimentation tank 600, a biochemical reaction tank 700, and a membrane bioreactor 800.
According to the utility model discloses electroplating nickeliferous effluent treatment plant, preliminary treatment coagulation device 100 is including consecutive first pH equalizing basin 110, coagulant dosing tank 120 and first flocculating agent dosing tank 130.
According to the utility model discloses electroplating nickeliferous effluent treatment plant, one-level fenton reaction unit 300 is including consecutive second pH equalizing basin 310, first ferrous sulfate dosing tank 320, hydrogen peroxide solution dosing tank 330, fenton reaction tank 340, aeration tank 350 and first alkali regulation pond 360. And a TOC online detection device is arranged at the water inlet end of the primary Fenton reaction device, namely a water inlet pipeline of the second pH adjusting tank, and is in linkage control with the addition of Fenton reagents (ferrous sulfate and hydrogen peroxide). The TOC on-line detection device can be an ORP meter and is also called an oxidation-reduction potential on-line analyzer.
According to the utility model discloses electroplating nickel effluent treatment plant, second grade coagulation system 500 is including consecutive third pH equalizing basin 510, heavy metal collector pond 520, ferrous sulfate pond 530, the alkali pond 540 is transferred to the second and the second flocculating agent pond 550 that adds.
According to the utility model discloses electroplating nickeliferous effluent treatment plant, biochemical reaction pond 700 is including consecutive anaerobism pond 710 and good oxygen pond 720.
According to the utility model discloses electroplating nickeliferous effluent treatment plant, the mud discharging port of submergence formula ultrafiltration membrane reactor 400 links to each other with the water inlet of one-level sedimentation tank 200.
According to the utility model discloses electroplating nickeliferous effluent treatment plant, the mud discharging port of submergence formula ultrafiltration membrane reactor 400 still links to each other with the water inlet of coagulant dosing tank 120.
As shown in fig. 2, in an embodiment of an apparatus for treating nickel-containing electroplating wastewater, a first pH adjusting tank 110, a coagulant adding tank 120, a first flocculant adding tank 130, a primary sedimentation tank 200, a second pH adjusting tank 310, a first ferrous sulfate adding tank 320, a hydrogen peroxide adding tank 330, a fenton reaction tank 340, an aeration tank 350, a first alkali adjusting tank 360, a submerged ultrafiltration membrane reactor 400, a third pH adjusting tank 510, a heavy metal collector adding tank 520, a second ferrous sulfate adding tank 530, a second alkali adjusting tank 540, a second flocculant adding tank 550, a secondary sedimentation tank 600, an anaerobic tank 710, an aerobic tank 720 and a membrane bioreactor 800 are connected in sequence.
The treatment device of the embodiment is used for treating nickel-containing electroplating wastewater, the nickel-containing electroplating wastewater firstly enters a pretreatment coagulation device, sodium hydroxide is added into a first pH adjusting tank of the pretreatment coagulation device to adjust the pH value of the wastewater to 7-8, 100-800 mg/L PAC solution is added into a coagulant adding tank, and 2-5 mg/L PAM is added into a first flocculant adding tank for precipitation. Suspended matters, colloids and partial heavy metals in the nickel-containing electroplating wastewater are removed by coagulation, and flocs generated by pretreatment coagulation can further adsorb partial heavy metals.
Electroplating nickeliferous waste water is treated by a pretreatment coagulation device and then enters a primary sedimentation tank for mud-water separation, and effluent of the primary sedimentation tank enters a primary Fenton reaction device. And adjusting the pH of the wastewater to about 3.5 in a second pH adjusting tank, then sequentially entering a first ferrous sulfate dosing tank and a hydrogen peroxide dosing tank, and controlling and dosing Fenton reagents (ferrous sulfate and hydrogen peroxide) according to the TOC concentration of the primary precipitated effluent. The mass ratio of the ferrous sulfate to the TOC is (2.5-3.3): 1, the mass ratio of hydrogen peroxide to TOC is (2.5-4): 1. and after finishing adding the Fenton reagent, feeding the obtained product into a Fenton reaction tank for reaction, feeding the obtained product into an aeration tank for aeration, and then feeding the obtained product into a first alkali regulation tank for regulating the pH value to 7.5-8.5.
The effluent of the first-stage Fenton reaction device enters an MCR reactor, and a hollow fiber ultrafiltration membrane component is arranged in the MCR reactor. The concentration of the mud-water mixture in the MCR reactor is controlled to be 4000 mg/L-7000 mg/L, the higher concentration of the mud-water mixture is beneficial to removing heavy metals through sludge adsorption, and the MCR can completely separate mud from water, so that the heavy metals are prevented from entering the next process unit along with sludge. A continuous sludge discharge pipeline is arranged at the bottom of the MCR reactor and is connected to a primary sedimentation tank or a coagulant dosing tank to discharge sludge generated by a primary Fenton reaction device, and the iron sludge discharged by the MCR reactor still has the adsorption and removal effects in the primary sedimentation tank or the coagulant dosing tank. The mud-water mixture can be refluxed according to 0.8-1.2 times of the yield of the iron mud produced by Fenton.
Effluent of the MCR reactor enters a secondary coagulation device, the pH of wastewater is adjusted to be 7.5-8.5 in a third pH adjusting tank, and then the wastewater sequentially enters a heavy metal trapping agent dosing tank, a second ferrous sulfate dosing tank, a second alkali adjusting tank and a second flocculating agent dosing tank. And respectively adding the heavy metal trapping agent, the ferrous sulfate and the PAM into the heavy metal trapping agent adding pool, the second ferrous sulfate adding pool and the second flocculating agent adding pool for coagulating sedimentation. Wherein the dosage of the heavy metal trapping agent is 100 mg/L-300 mg/L, the dosage of the ferrous sulfate is 50 mg/L-200 mg/L, and the dosage of the polyacrylamide is 1 mg/L-5 mg/L. The complex nickel in the wastewater treated by the primary Fenton reaction device is converted into an ionic state and can be removed by a heavy metal trapping agent and coagulation. And the pH value of the wastewater is adjusted to 7-8 by the second alkali adjusting tank. The heavy metal trapping agent is a substance with chelating capacity with heavy metal ions, such as inorganic sulfide or organic sulfide.
And the effluent of the secondary coagulation device enters a biochemical reaction tank after mud-water separation in a secondary sedimentation tank. The traditional AO process is carried out through an anaerobic pool and an aerobic pool of a biochemical reaction pool. The aerobic tank is provided with a mud-water mixture reflux denitrification denitrogenation with 3 times of water inlet flow.
The effluent of the biochemical reaction tank enters an MBR (membrane bioreactor) for enhanced biochemical treatment, and the active sludge concentration of the wastewater is controlled to be 5000-8000 mg/L in the MBR. The MBR has 3 times of the slurry mixture of the inflow flow and flows back to the aerobic tank, and the high biomass of the biochemical system is ensured.
The effluent water passing through the MBR can reach the discharge Standard of electroplating pollutants (GB 21900-2008), and can also be used as reclaimed water for recycling and feeding, and is directly subjected to a reverse osmosis process unit without pretreatment such as coagulation. The sludge generated in the first-stage sedimentation tank and the second-stage sedimentation tank can be discharged and treated.
Application examples
The treatment device of the embodiment is adopted to treat the electroplating nickel-containing wastewater. The nickel-containing wastewater in a certain electroplating industrial park is taken for water quality analysis and detection, and the water quality is shown in table 1.
TABLE 1 analysis result of water quality of nickel-containing raw water for electroplating
The method comprises the following steps: taking the wastewater to carry out coagulation experiments, adding sodium hydroxide to adjust the pH of the wastewater to 7.5 under the stirring condition, adding 10% PAC solution of 300mg/L, and adding 4mg/L PAM to carry out precipitation after carrying out coagulation reaction for 15 min.
Step two: taking the supernatant obtained after the precipitation in the step one, further performing a Fenton reaction, adjusting the pH value of the Fenton reaction to be 3.5, measuring the TOC of the supernatant to be 87mg/L, adding 261mg/L of ferrous sulfate (calculated by ferrous ions) according to the ratio of the ferrous sulfate to the TOC of 3:1 (the actual added weight of the ferrous sulfate heptahydrate is 261 multiplied by 278/56-1295.7 mg/L) according to the ferrous ions), and adding hydrogen peroxide (calculated by pure H)2O2Metering) and TOC ratio of 2.7:1, adding 235mg/L hydrogen peroxide for 30min of Fenton reaction, aerating for 20min after the Fenton reaction is finished, continuing aeration until pH is 8, and filtering Fenton effluent by using a 0.45-micrometer filter membrane to measure COD: 84mg/L and the nickel content is 1.1 mg/L.
Step three: and (3) carrying out sludge-water separation on the mixture of the sludge and water obtained in the step two Fenton by MCR, adjusting the pH value of the effluent to be 8, adding 200mg/L of heavy metal trapping agent, carrying out stirring reaction for 15min, adding 100mg/L of ferrous sulfate, carrying out stirring reaction for 15min, adding 2mg/L of PAM (polyacrylamide) for precipitation after adjusting the pH value to be 7.5 by adding sodium hydroxide.
Step four: and (4) taking the water precipitated in the step three, and allowing the water to enter an A/O + MBR reactor for biochemical experiments, wherein the total biochemical retention time is 26 h. Adding carbon source and sodium phosphate according to the detected total nitrogen concentration, controlling the sludge concentration of the membrane tank to be 5000mg/L, continuously running for one week, and detecting the water quality as shown in the following table 2.
TABLE 2 analysis of effluent quality
According to the test result of table 2, through adopting the utility model discloses a processing apparatus handles electroplating nickel-containing waste water, goes out water quality of water and can reach the one-level A emission standard of "electroplating pollutants emission standard" (GB 21900-.
Taking fenton sludge which is not added with PAM for precipitation after Fenton in the step two of the application example, mixing and stirring the amount of iron sludge generated by adding ferrous sulfate in the Fenton reaction with the supernatant liquid precipitated in the step one for 10min, namely taking the supernatant liquid in the step one, adding Fenton iron sludge generated in the step two according to 500mg/L for stirring and adsorption, precipitating and taking the supernatant liquid after adsorption reaction for 10min, and comparing the supernatant liquid after adsorption reaction with the supernatant liquid in the step one, wherein COD is removed by about 15-20mg/L, and other pollutants are removed by about 3% -11%, which indicates that the Fenton iron sludge still has strong adsorption when flowing back to the primary sedimentation tank.
Application comparative example 1
Taking the same nickel-containing wastewater of an electroplating industrial park to directly carry out a Fenton experiment, adding 300mg/L ferrous sulfate (calculated by ferrous ions), adding 300mg/L hydrogen peroxide, adjusting the pH value of the Fenton reaction to be 3.5, carrying out the Fenton reaction for 30min, aerating for 20min, adjusting the pH value to be 8 by using sodium hydroxide, and taking the supernatant to detect COD: 113mg/L and the nickel content is 2.6 mg/L. The COD concentration and the nickel concentration of the supernatant are higher than those of the second step in the embodiment, which shows that the direct Fenton pretreatment of the nickel-containing wastewater not only has high Fenton reagent consumption, but also has poor pollutant removal effect.
Comparative application example 2
Taking the same nickel-containing wastewater of the electroplating industrial park to carry out a two-stage coagulation experiment, namely, firstly carrying out a first-stage coagulation experiment according to the first step of the embodiment, adding 10% PAC of 300mg/L to carry out coagulation, carrying out coagulating sedimentation to obtain a supernatant, then adding 10% PAC of 300mg/L to carry out a second-stage coagulation experiment, carrying out TOC determination on the coagulated water, wherein the TOC concentration is 79mg/L, namely, only about 8mg/L of TOC is removed by the second-stage coagulation, and the removal efficiency of pollutants by the second-stage coagulation is low. And further removing residual metal nickel from the supernatant after the secondary coagulating sedimentation by using a heavy metal trapping agent, wherein the optimal nickel content of effluent is 2.3mg/L, the effluent containing nickel exceeds the standard and cannot enter a biochemical process for treatment, and the using amount of the heavy metal trapping agent is large.
The treatment device provided by the utility model adds coagulation pretreatment before the Fenton process, greatly reduces the load of the Fenton process, saves the addition of Fenton agent for complexation breaking; the Fenton process is a stable complex breaking process and a process for removing organic matters and phosphates, the Fenton and the MCR reactor are combined to play a role in direct oxidation removal and also play a role in adsorption of high-concentration sludge in the MCR reactor, heavy metal loss caused by sludge running in a sedimentation tank to downstream is reduced, and heavy metal pollutants are stably removed; the high-concentration iron mud intercepted by the MCR reactor has an adsorption effect, can further adsorb and remove pollutants by returning the discharged mud to the primary sedimentation tank, and can continuously and intensively treat the nickel-containing electroplating wastewater in the electroplating industrial park by combining biochemical strengthening treatment, and the wastewater reaches the discharge standard or is further recycled.
While embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the above-described embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.
Claims (10)
1. The utility model provides an electroplate processing apparatus who contains nickel waste water which characterized in that: the treatment device comprises a pretreatment coagulation device, a primary sedimentation tank, a primary Fenton reaction device, an immersed ultrafiltration membrane reactor, a secondary coagulation device, a secondary sedimentation tank, a biochemical reaction tank and a membrane bioreactor which are sequentially connected.
2. The apparatus for treating nickel-containing electroplating wastewater according to claim 1, wherein: the pretreatment coagulation device comprises a first pH adjusting tank, a coagulant dosing tank and a first flocculant dosing tank which are connected in sequence.
3. The apparatus for treating nickel-containing electroplating wastewater according to claim 2, wherein: the coagulant dosing tank is a polyaluminium chloride dosing tank.
4. The apparatus for treating nickel-containing electroplating wastewater according to claim 2, wherein: the first flocculating agent dosing pool is a polyacrylamide dosing pool.
5. The apparatus for treating nickel-containing electroplating wastewater according to claim 1, wherein: the first-stage Fenton reaction device comprises a second pH adjusting tank, a first ferrous sulfate dosing tank, a hydrogen peroxide dosing tank, a Fenton reaction tank, an aeration tank and a first alkali regulation tank which are sequentially connected.
6. The apparatus for treating nickel-containing electroplating wastewater according to claim 1, wherein: the second-stage coagulation device comprises a third pH adjusting tank, a heavy metal trapping agent dosing tank, a second ferrous sulfate dosing tank, a second alkali adjusting tank and a second flocculating agent dosing tank which are sequentially connected.
7. The apparatus for treating nickel-containing electroplating wastewater according to claim 6, wherein: the second flocculating agent dosing pool is a polyacrylamide dosing pool.
8. The apparatus for treating nickel-containing electroplating wastewater according to claim 1, wherein: the biochemical reaction tank comprises an anaerobic tank and an aerobic tank which are connected in sequence.
9. The apparatus for treating nickel-containing electroplating wastewater according to claim 1, wherein: and the water inlet of the primary sedimentation tank is connected with the sludge discharge port of the immersed ultrafiltration membrane reactor.
10. The apparatus for treating nickel-containing electroplating wastewater according to claim 2, wherein: and a water inlet of the coagulant adding tank is connected with a sludge discharge port of the immersed ultrafiltration membrane reactor.
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