CN214880910U - Pretreatment device and process flow for zinc-containing nickel-containing electroplating wastewater - Google Patents
Pretreatment device and process flow for zinc-containing nickel-containing electroplating wastewater Download PDFInfo
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- CN214880910U CN214880910U CN202120299837.6U CN202120299837U CN214880910U CN 214880910 U CN214880910 U CN 214880910U CN 202120299837 U CN202120299837 U CN 202120299837U CN 214880910 U CN214880910 U CN 214880910U
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Abstract
The utility model discloses a zinc-containing nickel-containing electroplating wastewater's preprocessing device and process flow, including tentatively getting rid of the electrochemistry device of the complex state nickel of aquatic, getting rid of organic additive's fenton reaction tank, once flocculation and precipitation pond, the broken complex reaction tank, the secondary coagulation and precipitation pond of complex state nickel are got rid of to the degree of depth. The device adopts the high-altitude UNICOM setting, and the water yield business turn over wherein, the medicament is added, and equipment action and instrument response detect all coordinate through control system is unified. The pretreatment device purifies through steps of electrochemical and Fenton comprehensive reaction, flocculation precipitation, M2 heavy metal chelate trapping agent complexation nickel removal and the like of the acidic electroplating wastewater containing zinc and nickel, so that the zinc and nickel heavy metals in the wastewater can reach the corresponding industrial standard.
Description
Technical Field
The utility model relates to an electroplating wastewater treatment technical field specifically is a zinc-containing nickel-containing electroplating wastewater's preprocessing device and process flow.
Background
The existing pretreatment technology of zinc-nickel-containing electroplating wastewater adopts single oxidation/complex breaking reaction, has limited removal effect on complex nickel, and is difficult to adapt to increasingly strict discharge standards. And the process is more complicated, increasing the running cost, for example:
a treatment apparatus for electroplating wastewater (CN 201820346545.1), comprising: the waste water collecting tank is used for collecting electroplating waste water to be treated; the pretreatment reaction tank is connected with the wastewater collecting tank through a first pipeline, and a plurality of groups of electrolytic material mounting seats are arranged in the pretreatment reaction tank and used for placing electrolytic materials, wherein the plurality of groups of electrolytic material mounting seats are respectively arranged in parallel; and the stirring reaction tank is connected with the pretreatment reaction tank through a second pipeline, a feed port is formed in the stirring reaction tank and used for feeding alkali-containing sludge, and a stirring device is arranged inside the stirring reaction tank and used for increasing the liquid flow inside the stirring reaction tank. And (3) pretreating through a pretreatment reaction tank, then entering a stirring reaction chamber for a second-step reaction, and finally precipitating through a precipitation tank. The pretreatment of the treatment process mainly has the following problems and disadvantages: firstly, the process only adopts a single iron-carbon micro-electrolysis process to pretreat the wastewater, and can not completely break the complex of the complex chromium and nickel, thereby affecting the subsequent flocculation and precipitation removal effect and not completely removing the nickel pollutants; secondly, the iron-carbon micro-electrolysis filler is easy to harden in the reaction process, the operation cost is increased, the treatment efficiency is influenced, the iron-carbon filler is easy to cover sediment, back washing is required to be carried out in time, and the automatic control difficulty is greatly increased.
A nickel-containing electroplating wastewater treatment system (CN201821360366. X) comprises an adjusting tank, a first pH adjusting tank, a first coagulation tank, a first flocculation tank, a first sedimentation tank, a second pH adjusting tank, an oxidation breaking tank, a third pH adjusting tank, a breaking reaction tank, a second coagulation tank, a second flocculation tank, a second sedimentation tank, a sludge tank, a temporary storage tank, a quartz sand filter, an ion exchanger and a monitoring sampling tank. The utility model discloses simple structure, it is with low costs, can reach emission standard after nickeliferous electroplating wastewater handles, prevent to discharge the back and cause the pollution to the environment. The pretreatment of the treatment process mainly has the following problems and disadvantages: : in practical engineering practice, sodium hypochlorite has a limited effect of breaking the complex of the acidic electroplating wastewater, is only limited to be used for neutral and alkaline electroplating wastewater, and is lack of application to the acidic electroplating wastewater; has certain limitations; secondly, the complex breaking reaction adopts a common heavy metal chelating agent, the removal of complex nickel is limited, the common heavy metal trapping agent is mostly a sulfur-containing compound, H2S is easily generated under an alkaline condition, and the complex breaking agent is easy to cause harm to operation operators and has certain potential safety hazard.
Disclosure of Invention
An object of the utility model is to provide a zinc-containing nickeliferous electroplating wastewater's preprocessing device and process flow to solve the problem that provides among the above-mentioned background art.
In order to achieve the above object, the utility model provides a following technical scheme: a pretreatment device for zinc-containing nickel-containing electroplating wastewater comprises: an electrochemical device 1 for primarily removing complex nickel in water, a Fenton reaction tank 2 for removing organic additives, a primary flocculation sedimentation tank 3, a primary sedimentation tank 4, a complex breaking reaction tank 5 for deeply removing complex nickel and zinc, a secondary flocculation sedimentation tank 6 and a secondary sedimentation tank 7, wherein the devices are arranged in a communicated manner according to the elevation in turn, and the water inlet and outlet, the addition of medicaments, the device action and the instrument induction detection of the devices are uniformly and coordinately controlled by a control system,
a process flow of a pretreatment device for zinc-containing nickel-containing electroplating wastewater comprises the following specific steps:
firstly, acid electroplating wastewater containing zinc and nickel enters an electrochemical device 1 from a front-end regulating and collecting pool through a lift pump, wherein the electrochemical device 1 is internally provided with an electrochemical module 11, the electrochemical module 11 is formed by alternately placing a positive electrode plate and a negative electrode plate into a bracket, the positive electrode plate and the negative electrode plate are connected by corresponding positive and negative power supplies, the electrochemical device 1 can perform the actions of electrocoagulation, electrocatalytic oxidation and the like to primarily remove heavy metal ions and organic matters in the wastewater, and the electroplating wastewater enters a Fenton reaction pool 2 after reaction; the electrochemical device 1 is provided with an independent power supply for providing power for electrolysis, the electrochemical device 1 is also provided with a liquid level meter 12 and a pH meter 13, the liquid level meter 12 monitors the liquid level, and when the liquid level reaches an alarm liquid level, the lifting pump of the front-end regulation collection pool stops conveying wastewater; the electrochemical reaction condition is pH 3-4, pH meter 13 detects and adjusts the acid dosage, the sulfuric acid is dilute sulfuric acid with 10% concentration; the current density of the electrochemical device is adjusted to 10-20mA/cm by a rectifier2(ii) a The retention time of the electrochemical reaction is 0.25-0.5 h;
secondly, after the wastewater enters a Fenton reaction tank 2, adjusting the pH value to 2-3, adding 30% hydrogen peroxide solution, fully stirring the inlet water by using a paddle stirrer 21 in the Fenton reaction tank, keeping the reaction for 0.5-0.8h, monitoring and adjusting the pH value by using a pH meter 22, and after the reaction, feeding the wastewater into a primary flocculation tank 3;
thirdly, after the wastewater enters a primary flocculation tank 3, adding 20% NaOH solution, adjusting the pH value in the flocculation tank to 8-9, using ferric hydroxide as a coagulant, adding 0.01% polyacrylamide PAM solution, wherein a paddle type stirrer 31 fully and uniformly stirs the wastewater, the retention time is 10-15min, and a pH meter 32 is adopted to monitor and adjust the pH value; the pH value of the optimal precipitation of Ni is 6.9-8.9, the pH value of the optimal precipitation of Zn is 8-9, and the wastewater enters a primary sedimentation tank 4 after reaction;
fourthly, precipitating the wastewater in a primary sedimentation tank 4 to remove most suspended substances SS, heavy metals Zn and Ni, wherein the retention time is 1.5-2 h;
fifthly, the wastewater enters a complex breaking reaction tank 5 after passing through a primary sedimentation tank 4, the pH value of the wastewater is kept at about 8-9, and a HMC-M2 high-efficiency heavy metal remover produced by Zhanqing environmental protection technology ltd is added, wherein the remover chelates ionic or complex nickel ions in the wastewater into insoluble groups, so that the purpose of separating the heavy metal ions from the wastewater is achieved, and the remover does not contain sulfur compounds; wherein the paddle type stirrer 51 is fully and uniformly stirred, the retention time is 15-20min, and the pH meter 52 is adopted for pH monitoring and adjustment;
sixthly, the wastewater enters a secondary coagulation and flocculation tank 6 after being reacted in a complex breaking reaction tank 5, wherein the tank is divided into two grids, the first grid is a coagulation tank, and the second grid is a flocculation tank; in the first grid, pH monitoring is carried out through a pH meter 62 to regulate the wastewater to be 8-9, and a polyaluminium chloride PAC solution with the concentration of 15% is added to generate small-particle water-insoluble colloidal groups in the water; and adding a polyacrylamide PAM solution with the concentration of 0.01% into the second cell, reacting to generate large-particle sediment, sealing the first cell and the second cell by adopting partition walls, connecting the first cell and the second cell by a perforated tracery wall at the bottom of the partition walls, respectively installing a paddle stirrer/frame stirrer 61 in the two tanks, fully and uniformly stirring, keeping the time for 10-15min, and fully reflecting and then entering a subsequent secondary sedimentation tank 7.
And seventhly, precipitating the wastewater in a secondary sedimentation tank 7 to basically remove suspended matters SS and heavy metal Ni, wherein the retention time is 1.5-2h, and discharging supernatant after precipitation to a subsequent reaction unit.
Furthermore, the electrochemical device 1 adopts the technologies of electrolyzing at a power frequency of 50 Hz, automatically changing the phase of the cathode and the anode of the polar plate configured by the electric control cabinet, adjusting the voltage and the current by the trigger plate and the like, so that the service life of the electrochemical device is prolonged.
Compared with the prior art, the beneficial effects of the utility model are that: the utility model discloses preprocessing device carries out "electrochemistry + fenton method" comprehensive reaction processing to zinciferous nickeliferous acid electroplating wastewater, produces a series of effects such as electric flocculation and electro-oxidation reduction in the electrochemical module reaction unit, makes organic additive pollutant and complex state heavy metal take place direct electrochemical reaction or indirect electrochemical reaction and obtain the conversion on the electrode;
adding a small amount of acidity regulator and hydrogen peroxide agent, and utilizing the catalytic action of Fe2+ ions generated by an electrochemical module to decompose H2O2 to generate hydroxyl radical OH < - >, wherein the hydroxyl radical OH < - > can convert nickel in a complex state into nickel in a free state, iron hydroxide generated by the reaction can be used as a coagulant, and then adding an alkalinity regulator and a flocculating agent in the subsequent reaction to precipitate the nickel and zinc in a zinc and nickel precipitation zone to primarily remove zinc and nickel pollutants;
and then the HMC-M2 high-efficiency remover is added to carry out deep complex breaking purification on the complex nickel, the HMC-M2 has special strong efficiency, the chelating groups on the branches and chains can chelate heavy metals to form stable insoluble substances to precipitate, a reaction bridge is built with nickel ions in the groups to generate specific chelating groups of the HMC-M2 and the nickel ions, and the precipitate is generated through the coagulation and flocculation agent added subsequently, so that the zinc-nickel heavy metals in the wastewater can reach the corresponding industrial discharge standard after being removed, and the subsequent treatment reaction is facilitated.
The utility model discloses the electrochemistry device polar plate is packed to change conveniently for the iron carbon, and the polar plate consumption is less than the iron carbon packing, and the high-efficient remover of HMC-M2 is effectual to the broken of nickel and twines, and does not contain harmful substance such as sulphide, and the security performance is good, the utility model has the advantages of degree of automation is high, and the technology combination is simple, handles high-efficient up to standard, is applicable to the preliminary treatment of the nickeliferous zinciferous waste water of acidity.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Referring to fig. 1, the utility model provides a zinc-containing nickel-containing electroplating wastewater pretreatment device, which comprises: the electrochemical device for removing the complex nickel in water primarily comprises an electrochemical device 1 for removing the complex nickel in water primarily, a Fenton reaction tank 2 for removing organic additives, a primary flocculation tank 3, a primary sedimentation tank 4, a complex breaking reaction tank 5 for removing the complex nickel and zinc deeply, a secondary coagulation flocculation tank 6 and a secondary sedimentation tank 7. In each device, an electrochemical device 1 is communicated with a Fenton reaction tank 2 according to an elevation pipeline; the Fenton reaction tank 2 is communicated with the primary flocculation tank 3, and the complex breaking reaction tank 5 is communicated with the secondary flocculation tank 6 through a perforated tracery wall at the bottom of the partition wall; the primary sedimentation tank 4 is provided with a water inlet pipe on a partition wall and is communicated with a water outlet hole of the primary flocculation tank 3 according to the elevation, a water outlet weir is arranged at the water outlet end inwards, and the water outlet weir is communicated with the collateral breaking reaction tank 5 according to the elevation through a perforated wall of the partition wall; the secondary sedimentation tank 7 is provided with a water inlet pipe on the partition wall to be communicated with the water outlet hole of the secondary flocculation tank 6 according to the elevation, the water outlet end is internally provided with a water outlet weir, and the water outlet weir is communicated with the subsequent reaction tank according to the elevation through a perforated wall of the partition wall and a pipeline. The water inlet and outlet of each device, the addition of the medicament, the device action and the instrument induction detection are all coordinately controlled by a control system in a unified way,
a process flow of a pretreatment device for zinc-containing nickel-containing electroplating wastewater comprises the following specific steps:
firstly, acid electroplating wastewater containing zinc and nickel enters an electrochemical device 1 from a front-end regulating and collecting pool through a lift pump, wherein the electrochemical device 1 is internally provided with an electrochemical module 11, the electrochemical module 11 is formed by alternately placing a positive electrode plate and a negative electrode plate into a bracket, the positive electrode plate and the negative electrode plate are connected by corresponding positive and negative power supplies, the electrochemical device 1 can perform the actions of electrocoagulation, electrocatalytic oxidation and the like to primarily remove heavy metal ions and organic matters in the wastewater, and the electroplating wastewater enters a Fenton reaction pool 2 after reaction; the electrochemical device 1 is provided with an independent power supply for providing power for electrolysis, the electrochemical device 1 is also provided with a liquid level meter 12 and a pH meter 13, the liquid level meter 12 monitors the liquid level, and when the liquid level reaches an alarm liquid level, the lifting pump of the front-end regulation collection pool stops conveying wastewater; the electrochemical reaction condition is pH 3-4, pH meter 13 detects and adjusts the acid dosage, the sulfuric acid is dilute sulfuric acid with 10% concentration; the current density of the electrochemical device is adjusted to 10-20mA/cm by a rectifier2(ii) a The retention time of the electrochemical reaction is 0.25-0.5 h;
secondly, after the wastewater enters a Fenton reaction tank 2, adjusting the pH value to 2-3, adding 30% hydrogen peroxide solution, fully stirring the inlet water by using a paddle stirrer 21 in the Fenton reaction tank, keeping the reaction for 0.5-0.8h, monitoring and adjusting the pH value by using a pH meter 22, and after the reaction, feeding the wastewater into a primary flocculation tank 3;
thirdly, after the wastewater enters a primary flocculation tank 3, adding 20% NaOH solution, adjusting the pH value in the flocculation tank to 8-9, using ferric hydroxide as a coagulant, adding 0.01% polyacrylamide PAM solution, wherein a paddle type stirrer 31 fully and uniformly stirs the wastewater, the retention time is 10-15min, and a pH meter 32 is adopted to monitor and adjust the pH value; the pH value of the optimal precipitation of Ni is 6.9-8.9, the pH value of the optimal precipitation of Zn is 8-9, and the wastewater enters a primary sedimentation tank 4 after reaction;
fourthly, precipitating the wastewater in a primary sedimentation tank 4 to remove most suspended substances SS, heavy metals Zn and Ni, wherein the retention time is 1.5-2 h;
fifthly, after the wastewater passes through a primary sedimentation tank 4, the wastewater enters a complex breaking reaction tank 5, the pH value of the wastewater is kept at about 8-9, and an efficient HMC-M2 remover produced by Zhanqing environmental protection technology ltd is added, wherein the remover chelates ionic or complex nickel ions in the wastewater into insoluble groups, so that the purpose of separating heavy metal ions from the wastewater is achieved; wherein the paddle type stirrer 51 is fully and uniformly stirred, the retention time is 15-20min, and the pH meter 52 is adopted for pH monitoring and adjustment;
sixthly, the wastewater enters a secondary coagulation and flocculation tank 6 after being reacted in a complex breaking reaction tank 5, wherein the tank is divided into two grids, the first grid is a coagulation tank, and the second grid is a flocculation tank; in the first grid, pH monitoring is carried out through a pH meter 62 to regulate the wastewater to be 8-9, and a polyaluminium chloride PAC solution with the concentration of 15% is added to generate small-particle water-insoluble colloidal groups in the water; and adding a polyacrylamide PAM solution with the concentration of 0.01% into the second cell, reacting to generate large-particle sediment, sealing the first cell and the second cell by adopting partition walls, connecting the first cell and the second cell by a perforated tracery wall at the bottom of the partition walls, respectively installing a paddle stirrer/frame stirrer 61 in the two tanks, fully and uniformly stirring, keeping the time for 10-15min, and fully reflecting and then entering a subsequent secondary sedimentation tank 7.
And seventhly, precipitating the wastewater in a secondary sedimentation tank 7 to basically remove suspended matters SS and heavy metal Ni, wherein the retention time is 1.5-2h, and discharging supernatant after precipitation to a subsequent reaction unit.
Furthermore, the electrochemical device 1 adopts the technologies of electrolyzing at a power frequency of 50 Hz, automatically changing the phase of the cathode and the anode of the polar plate configured by the electric control cabinet, adjusting the voltage and the current by the trigger plate and the like, so that the service life of the electrochemical device is prolonged.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (2)
1. A pretreatment device for zinc-containing nickel-containing electroplating wastewater is characterized by comprising: the electrochemical device (1) of complex state nickel in the preliminary aquatic of getting rid of, get rid of fenton reaction tank (2) of organic additive, primary flocculation and precipitation pond (3), primary sedimentation tank (4), the broken complex reaction tank (5) of complex state nickel and zinc are got rid of to the degree of depth, secondary coagulating and flocculation and precipitation pond (6), secondary sedimentation tank (7), above-mentioned each equipment adopts height UNICOM's setting in proper order, and the business turn over of each equipment water yield, the joining of medicament, equipment action and instrument response detect by the unified coordinated control of control system.
2. The pretreatment device for zinc-containing and nickel-containing electroplating wastewater according to claim 1, wherein an electrochemical module (11) is installed in the electrochemical device (1), the electrochemical module (11) is formed by alternately placing positive and negative electrode plates into a support, and the positive and negative electrode plates are connected by corresponding positive and negative power supplies.
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| CN112645530A (en) * | 2021-02-03 | 2021-04-13 | 湖南惟创环境科技有限公司 | Pretreatment device and process flow for zinc-containing nickel-containing electroplating wastewater |
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Address after: 410000 room 406, building A4, Jinghuan community, 126 Xing'an Road, Yuhua District, Changsha City, Hunan Province Patentee after: Weichuang Environmental Technology Co.,Ltd. Address before: 410000 room 406, building A4, Jinghuan community, 126 Xing'an Road, Yuhua District, Changsha City, Hunan Province Patentee before: HUNAN WEICHUANG ENVIRONMENT TECHNOLOGY CO.,LTD. |
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