Alkaline zinc-nickel alloy wastewater treatment and recycling system

Abstract

The utility model discloses a system for treating and recycling alkaline zinc-nickel alloy wastewater, which relates to the technical field of wastewater treatment and water pollution control in the electroplating or surface treatment industry and comprises an ion exchange nickel removal system, and a nickel-containing outlet of the ion exchange nickel removal system is communicated with a nickel recovery system. A nickel-free outlet of the ion exchange nickel removal system is communicated with the electrocatalytic oxidation system, an outlet of the electrocatalytic oxidation system is communicated with the sodium sulfide zinc removal system, and an outlet of the sodium sulfide zinc removal system is communicated with the filter pressing system. Compared with a Fenton oxidation method with high medicament, equipment and maintenance cost, the cost of the electrocatalytic oxidation system is relatively low, and no secondary pollution is generated due to the fact that no medicament needs to be added; compared with an expensive metal capturing agent, the cost of nickel removal through ion exchange and zinc removal through sodium sulfide is lower, nickel exchanged through an ion exchange nickel removal system generally exists in the form of divalent nickel ions, and nickel resources can be recycled directly through a nickel recycling system.

Description

TECHNICAL FIELD

[0001] The utility model relates to electroplating or surface treatment industry wastewater treatment and water pollution control technical field, especially, relate to a kind of alkaline zinc-nickel alloy wastewater treatment and its system of resource utilization. BACKGROUND

[0002] Alkaline zinc-nickel alloy electroplating is the preferred electroplating technology of most automobile parts in recent years, in the electroplating process, in order to make nickel not to precipitate and enhance the dispersion ability of plating solution, so as to achieve good plating effect, it is often necessary to add some complexing agents, such as ethylenediamine, tartrate, triethanolamine, EDTA (ethylenediamine tetraacetic acid) and the like, which also increases the difficulty of wastewater treatment.

[0003] The conventional alkaline zinc-nickel alloy wastewater treatment method at present is Fenton oxidation method, and then metal capturing agent is added to remove zinc and nickel. Fenton oxidation method is a method for oxidizing reducing pollutants in water by using Fenton reagent. Fenton reagent is composed of hydrogen peroxide and ferrous ion Fe 2+ , which reacts under acidic conditions to generate strong oxidizing hydroxyl radicals -OH. These free radicals can react with organic matter and ultimately oxidize it to carbon dioxide and water. Since the original pH value of the wastewater is between 12 and 13, the pH value of the Fenton oxidation process reaction condition is between 3 and 4, so a lot of acid needs to be added to adjust the pH value, and the hydrogen peroxide in the Fenton reagent itself will undergo a certain decomposition reaction, so excess Fenton reagent needs to be added. In addition, the metal capturing agent added is very expensive, and the generated zinc, nickel and a large amount of iron sludge need to be handled by a special third party, so the overall cost is relatively high. Moreover, the alkaline zinc-nickel alloy wastewater contains part of the nickel resources, and the conventional wastewater treatment method cannot effectively utilize the nickel resources. If there is a solution that can treat electroplating alkaline zinc-nickel alloy wastewater at low cost and recover nickel resources from electroplating alkaline zinc-nickel alloy wastewater, the technology will have great application significance. UTILITY MODEL CONTENT

[0004] The utility model aims to provide a kind of alkaline zinc-nickel alloy wastewater treatment and its system of resource utilization, to solve the problems existing in the prior art, which can treat electroplating alkaline zinc-nickel alloy wastewater at low cost, and recover nickel resources from electroplating alkaline zinc-nickel alloy wastewater.

[0005] To achieve the above-mentioned purpose, the utility model provides the following scheme:

[0006] The system for treating and recycling alkaline zinc-nickel alloy wastewater comprises an ion exchange nickel removal system, a nickel recovery system connected to the nickel-containing outlet of the ion exchange nickel removal system, an electro-catalytic oxidation system connected to the nickel-free outlet of the ion exchange nickel removal system, a zinc removal system connected to the outlet of the electro-catalytic oxidation system, and a pressure filtration system connected to the outlet of the zinc removal system.

[0007] In an exemplary embodiment, the ion exchange nickel removal system comprises an ion exchange column and an acid eluent preparation tank, the ion exchange column is provided with a wastewater inlet, an acid eluent inlet, the nickel-containing outlet and the nickel-free outlet, the wastewater inlet is connected to a wastewater raw water pool, and the acid eluent inlet is connected to the acid eluent preparation tank.

[0008] In an exemplary embodiment, the ion exchange nickel removal system further comprises a multi-medium filter arranged between the wastewater raw water pool and the ion exchange column, the inlet of the multi-medium filter is connected to the wastewater raw water pool, and the outlet of the multi-medium filter is connected to the wastewater inlet of the ion exchange column.

[0009] In an exemplary embodiment, the nickel recovery system comprises a nickel eluent collection tank, an electrolytic impurity removal tank, a boric acid solution preparation tank, and a diaphragm electrodeposition tank, the electrolytic impurity removal tank is used to remove impurity metal ions in the solution, and the diaphragm electrodeposition tank is used to electrodeposition nickel ions; the inlet of the nickel eluent collection tank is connected to the nickel-containing outlet of the ion exchange column, the nickel eluent collection tank, the electrolytic impurity removal tank and the diaphragm electrodeposition tank are sequentially connected, the outlet of the boric acid solution preparation tank is connected to the inlet of the diaphragm electrodeposition tank, and the outlet of the diaphragm electrodeposition tank is connected to the inlet of the acid eluent preparation tank.

[0010] In an exemplary embodiment, the electro-catalytic oxidation system comprises an electro-catalytic oxidation tank, the inlet of the electro-catalytic oxidation tank is connected to the ion exchange nickel removal system, and the outlet of the electro-catalytic oxidation tank is connected to the zinc removal system.

[0011] In an exemplary embodiment, the electro-catalytic oxidation system is a three-dimensional electro-catalytic oxidation system, the electro-catalytic oxidation tank is a three-dimensional oxidation tank, the three-dimensional oxidation tank is provided with an electro-catalytic oxidation cathode plate, an electro-catalytic oxidation anode plate and three-dimensional electrode particles, and the electro-catalytic oxidation cathode plate and the electro-catalytic oxidation anode plate are electrically connected to a direct current power supply.

[0012] In an exemplary embodiment, the zinc removal system comprises an acid-base adjustment tank and a zinc removal reaction tank connected in sequence, the inlet of the acid-base adjustment tank is connected to the electro-catalytic oxidation system, and the outlet of the zinc removal reaction tank is connected to the pressure filtration system.

[0013] In an exemplary embodiment, the sodium sulfide zinc removal system further comprises a dilute acid preparation tank in communication with the acid-base adjustment tank, and a dilute acid lifting pump is arranged between the dilute acid preparation tank and the acid-base adjustment tank.

[0014] In an exemplary embodiment, the sodium sulfide zinc removal system further comprises a sodium sulfide solution preparation tank in communication with the sodium sulfide zinc removal reaction tank, and a sodium sulfide lifting pump is arranged between the sodium sulfide solution preparation tank and the sodium sulfide zinc removal reaction tank.

[0015] In an exemplary embodiment, the filter pressing system comprises a diaphragm pump, a filter press, an SCR treatment device and a zinc-containing sludge collecting device, the inlet of the diaphragm pump is in communication with the sodium sulfide zinc removal system, the outlet of the diaphragm pump is in communication with the inlet of the filter press, the water outlet of the filter press is in communication with the SCR treatment device, and the sludge outlet of the filter press is in communication with the zinc-containing sludge collecting device.

[0016] The utility model discloses relative to prior art has obtained following technical effect:

[0017] Through setting up ion exchange nickel removal system, nickel recovery system, electro-catalytic oxidation system, sodium sulfide zinc removal system and filter pressing system, wastewater first flows through ion exchange nickel removal system and carries out adsorption nickel removal, and the nickel element that is adsorbed flows to nickel recovery system and carries out recovery, and the liquid after adsorption that does not contain nickel element flows to electro-catalytic oxidation system and carries out oxidation, and the COD in solution is removed, and the liquid after oxidation enters sodium sulfide zinc removal system and removes zinc, and the solution after treatment enters filter pressing system and carries out filter pressing, and obtains zinc-containing sludge and waste water to be discharged.

[0018] Compared with the Fenton oxidation method with high cost of medicament, equipment and maintenance, the cost of electro-catalytic oxidation system is relatively low, and no secondary pollution is caused since no medicament is added, and compared with the expensive metal capture agent, the ion exchange nickel removal and sodium sulfide zinc removal are more inexpensive.

[0019] Moreover, the metal capture agent is usually an organic compound containing specific functional groups, and these functional groups can form stable chemical bonds or complexes with nickel ions, so as to separate nickel ions from wastewater, and the captured nickel mainly exists in the form of precipitate and cannot be directly recovered.

[0020] The other technical solutions disclosed by the utility model have the following technical advantages:

[0021] The nickel is removed by setting an ion exchange column, and then the nickel is recovered by setting an electrolytic impurity removal tank and a diaphragm electrodeposition tank, in the process of flowing through the ion exchange column, the nickel ions in the wastewater are adsorbed by the ion exchange resin, after saturation, the resin adsorbed with the nickel ions is desorbed by using dilute acid, the obtained nickel desorption solution first enters the electrolytic impurity removal tank, then enters the diaphragm electrodeposition tank for diaphragm electrodeposition after electrolysis by a small current, and a nickel plate is formed on the cathode, and the purity of the nickel can reach more than 99.5%, so that the high-purity recovery of the nickel resource is realized. BRIEF DESCRIPTION OF DRAWINGS

[0022] In order to more clearly illustrate the technical solutions of the embodiments of the present application or the prior art, the drawings needed in the embodiments will be briefly introduced as follows. Obviously, the drawings described in the following are only some embodiments of the present application, and for those skilled in the art, other drawings can be obtained from these drawings without creative labor.

[0023] Figure 1 The structural diagram of the system for treating and recycling alkaline zinc-nickel alloy wastewater is disclosed in a specific embodiment of the present application.

[0024] 1, wastewater raw water pool; 2, wastewater lifting pump; 3, multi-medium filter; 4, ion exchange column; 5, acid desorption solution preparation tank; 6, desorption solution lifting pump; 7, electro-catalytic oxidation cathode plate; 8, activated carbon three-dimensional electrode particle; 9, electro-catalytic oxidation anode plate; 10, electro-catalytic oxidation tank; 11, direct current power supply; 12, acid-base adjusting tank; 13, dilute acid preparation tank; 14, dilute acid lifting pump; 15, pH meter; 16, zinc removal reaction tank; 17, sodium sulfide solution preparation tank; 18, sodium sulfide lifting pump; 19, diaphragm pump; 20, filter press; 21, zinc-containing sludge collecting device; 22, SCR treatment device; 23, nickel desorption solution collecting tank; 24, nickel desorption solution lifting pump; 25, electrolysis cathode plate; 26, electrolytic impurity removal tank; 27, electrolysis anode plate; 28, peristaltic pump; 29, electrodeposition anode plate; 30, electrodeposition cathode plate; 31, diaphragm electrodeposition tank; 32, boric acid lifting pump; 33, boric acid solution preparation tank; 34, post-electrodeposition liquid lifting pump. DETAILED DESCRIPTION

[0025] The technical solutions in the embodiments of the present application will be described clearly and completely in combination with the drawings in the embodiments of the present application. Those skilled in the art can easily understand other advantages and effects of the present application from the content disclosed in the present description. Obviously, the described embodiments are only some embodiments of the present application, not all embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the present application.

[0026] The utility model discloses a kind of alkaline zinc nickel alloy wastewater treatment and its system of resource, to solve the problems existing in prior art, both can low-cost treatment electroplating alkaline zinc nickel alloy wastewater, electroplating alkaline zinc nickel alloy wastewater in nickel resource can be recycled.

[0027] In order to make the above-mentioned purpose, features and advantages of the utility model more obvious and easy to understand, the utility model is further explained in detail below with reference to the drawings and specific embodiments.

[0028] Please refer to Figure 1 The embodiment provides a kind of alkaline zinc nickel alloy wastewater treatment and its system of resource, including ion exchange nickel removal system, the nickel outlet of ion exchange nickel removal system is connected with nickel recovery system, the nickel-free outlet of ion exchange nickel removal system is connected with electrocatalytic oxidation system, the outlet of electrocatalytic oxidation system is connected with zinc removal system of zinc sulfide, the outlet of zinc removal system of zinc sulfide is connected with filter pressing system.

[0029] The working principle of the embodiment is as follows:

[0030] By setting ion exchange nickel removal system, nickel recovery system, electrocatalytic oxidation system, zinc removal system of zinc sulfide and filter pressing system, alkaline zinc nickel alloy wastewater first flows through ion exchange nickel removal system for adsorption and nickel removal, the adsorbed nickel element flows to nickel recovery system for recovery, and the adsorbed liquid without nickel element flows to electrocatalytic oxidation system for oxidation, removes COD in the solution, and the oxidized liquid enters zinc removal system of zinc sulfide for zinc removal, and the treated solution enters filter pressing system for filter pressing, to obtain sludge and waste water to be discharged.

[0031] Compared with the Fenton oxidation method with high cost of reagents and equipment depreciation and maintenance cost, the cost of electrocatalytic oxidation system is relatively low, and no reagents need to be added, which will not cause secondary pollution; compared with expensive metal capture agent, ion exchange nickel removal and zinc removal by zinc sulfide are more cost-effective. Moreover, metal capture agents are usually organic compounds containing specific functional groups, which can form stable chemical bonds or complexes with nickel ions, thereby separating nickel ions from wastewater. The captured nickel mainly exists in the form of precipitate and cannot be directly recycled. The nickel exchanged by the ion exchange nickel removal system usually exists in the form of divalent nickel ions, which can be directly recycled by the nickel recovery system.

[0032] Specifically, the ion exchange nickel removal system includes an ion exchange column 4 and an acid elution liquid preparation tank 5. The ion exchange column 4 is provided with a wastewater inlet, an acid elution liquid inlet, a nickel-containing outlet, and a nickel-free outlet. The wastewater inlet is used to communicate with the wastewater raw water pool 1. The acid elution liquid inlet communicates with the acid elution liquid preparation tank 5. The nickel-containing outlet communicates with the nickel recovery system. The nickel-free outlet communicates with the electrocatalytic oxidation system.

[0033] Furthermore, the ion exchange nickel removal system also includes a multi-media filter 3 installed between the wastewater raw water tank 1 and the ion exchange column 4. The inlet of the multi-media filter 3 is connected to the wastewater raw water tank 1, and the outlet is connected to the wastewater inlet of the ion exchange column 4.

[0034] Wastewater raw water tank 1 includes an inlet and an outlet. The inlet is used to receive alkaline zinc-nickel alloy wastewater, and the outlet is connected to a wastewater lift pump 2. The wastewater lift pump 2 pumps the alkaline zinc-nickel alloy wastewater to a multi-media filter 3 for filtration to remove particulate matter and suspended solids from the wastewater. The alkaline zinc-nickel alloy wastewater from the multi-media filter 3 passes through an ion exchange column 4 to adsorb nickel metal ions from the wastewater. The adsorbed liquid, which does not contain nickel, then flows to an electrocatalytic oxidation system for oxidation. The adsorbed nickel is subsequently recovered through a nickel recovery system.

[0035] When the resin in the ion exchange column 4 is saturated with adsorption, dilute acid provided by the acid elution solution preparation tank 5 is used for elution and regeneration. The specific process is as follows: dilute acid of appropriate concentration is prepared in the acid elution solution preparation tank 5 and pumped into the ion exchange column 4 through the elution solution booster pump 6 to elute the saturated resin. The resulting nickel elution solution enters the nickel recovery system from the nickel-containing outlet.

[0036] The nickel recovery system includes a nickel stripping solution collection tank 23, an electrolytic impurity removal tank 26, a boric acid solution preparation tank 33, and a diaphragm electrowinning tank 31. The electrolytic impurity removal tank 26 is used to remove impurity metal ions from the solution, and the diaphragm electrowinning tank 31 is used to electrowinicate nickel ions. The inlet of the nickel stripping solution collection tank 23 is connected to the nickel-containing outlet of the ion exchange column 4. The nickel stripping solution collection tank 23, the electrolytic impurity removal tank 26, and the diaphragm electrowinning tank 31 are connected in sequence. The outlet of the boric acid solution preparation tank 33 is connected to the inlet of the diaphragm electrowinning tank 31, and the outlet of the diaphragm electrowinning tank 31 is connected to the inlet of the acid stripping solution preparation tank 5.

[0037] The collected nickel stripping solution is pumped into the electrolytic purification tank 26 via a booster pump. The electrolytic purification tank 26 is equipped with an electrolytic cathode plate 25 and an electrolytic anode plate 27. In this embodiment, the electrolytic cathode plate 25 is made of stainless steel, and the electrolytic anode plate 27 is made of titanium-based lead dioxide. Both are electrically connected to a DC power supply 11 with a current density of 2.5 A / m. 2 This is to remove trace amounts of impurity metal ions, such as copper and zinc ions, from the solution.

[0038] The solution in the electrolytic purification tank 26 is pumped into the diaphragm electrodeposition tank 31 by the peristaltic pump 28. The diaphragm electrodeposition tank 31 is equipped with an electrodeposition anode plate 29 and an electrodeposition cathode plate 30. In this embodiment, the electrodeposition anode plate 29 is a titanium-based lead dioxide anode plate, and the electrodeposition cathode plate 30 is a foamed nickel cathode plate. Both are connected to the DC power supply 11 with a current density of 220 A / m. 2The solution enters the diaphragm electrodeposition tank 31 to carry out diaphragm electrodeposition, and the nickel ions in the solution are deposited on the cathode to form a nickel plate. The boric acid solution in the boric acid solution preparation tank 33 is pumped into the diaphragm electrodeposition tank 31 through the boric acid lifting pump 32. The boric acid solution can be used as a buffer and an equalizer to adjust the pH value of the electrodeposition solution, improve the deposition efficiency, make the uniformity of the electrodeposited nickel layer better, effectively inhibit oxidation, prevent ohmic reaction, thereby reduce the generation of oxides, and obviously improve the corrosion resistance of the deposited nickel layer. The post-electrodeposition solution is pumped into the acid elution solution preparation tank 5 through the post-electrodeposition solution lifting pump 34 for recycling as an elution solution.

[0039] The ion exchange column 4 is arranged to remove nickel, and the electrolytic impurity removal tank 26 and the diaphragm electrodeposition tank 31 are arranged to recover nickel. During the process of flowing through the ion exchange column 4, the ion exchange resin is used to adsorb the nickel ions in the wastewater. After the adsorption is saturated, the resin adsorbed with the nickel ions is eluted with dilute acid to obtain a nickel elution solution. The nickel elution solution first enters the electrolytic impurity removal tank 26, is subjected to low-current electrolysis, and then enters the diaphragm electrodeposition tank 31 to carry out diaphragm electrodeposition. A nickel plate is formed on the cathode, and the purity of the nickel can reach more than 99.5%, realizing high-purity recovery of nickel resources.

[0040] The nickel-free outlet of the ion exchange nickel removal system is connected to an electro-catalytic oxidation system, which includes an electro-catalytic oxidation tank 10. The electro-catalytic oxidation tank 10 is provided with an electro-catalytic cathode plate and an electro-catalytic anode plate electrically connected to a direct current power supply 11. The inlet of the electro-catalytic oxidation tank 10 is connected to the nickel-free outlet of the ion exchange nickel removal system, and the outlet of the electro-catalytic oxidation tank 10 is connected to a zinc removal system.

[0041] As a preferred scheme of the embodiment, the electro-catalytic oxidation system is a three-dimensional electro-catalytic oxidation system, and the electro-catalytic oxidation tank 10 is a three-dimensional oxidation tank. The three-dimensional oxidation tank is provided with an electro-catalytic oxidation cathode plate 7, an electro-catalytic oxidation anode plate 9, and three-dimensional electrode particles 8. The electro-catalytic oxidation cathode plate 7 and the electro-catalytic oxidation anode plate 9 are electrically connected to the direct current power supply 11. The electro-catalytic oxidation cathode plate 7 and the electro-catalytic oxidation anode plate 9 can specifically adopt graphene electrode plates, and the three-dimensional electrode particles 8 adopt activated carbon particles.

[0042] The electro-catalytic oxidation technology includes two-dimensional electrochemical oxidation technology and three-dimensional electro-catalytic oxidation technology (Three Dimensional Electrolysis, TDE). Two-dimensional electro-catalytic oxidation refers to that a large number of hydroxyl radicals are generated on the surface of the anode under the action of an electric field, and the original ecological oxygen reacts with the pollutants in the solution to form small-molecule inorganic substances, so that the wastewater is harmless. Three-dimensional electro-catalytic oxidation is to fill granular working electrode materials between the electrodes of the traditional two-dimensional electrolytic tank and make the surface of the filled particles charged to become a new pole, so that the electrochemical reaction can be intensified on the surface of the filled particle electrode materials.

[0043] Compared with the two-dimensional electrochemical oxidation technology, the three-dimensional electro-catalytic oxidation system effectively increases the electrode area, improves the current efficiency and mass transfer rate by filling the three-dimensional electrode particles 8, so as to degrade the pollutants more quickly.

[0044] The sodium sulfide zinc removal system comprises the acid-base adjusting tank 12 and the sodium sulfide zinc removal reaction tank 16 connected in sequence, the inlet of the acid-base adjusting tank 12 is communicated with the electro-catalytic oxidation system, and the outlet of the sodium sulfide zinc removal reaction tank 16 is communicated with the filter pressing system.

[0045] The oxidized solution after the removal of COD by the electro-catalytic oxidation system needs to be adjusted in pH value by the acid-base adjusting tank 12 before the zinc removal reaction, the acid-base adjusting tank 12 is provided with a dilute acid preparation tank 13 for providing the dilute acid for adjusting the pH value of the acid-base adjusting tank 12, and the dilute acid solution is pumped into the acid-base adjusting tank 12 by a dilute acid lifting pump 14, and the acid-base adjusting tank 12 is also provided with a pH meter 15 for monitoring the pH value of the solution in the acid-base adjusting tank 12 in real time, and the pH value control range is 9.0-10.0.

[0046] The solution with the adjusted pH value flows into the sodium sulfide zinc removal reaction tank 16, the sodium sulfide zinc removal reaction tank 16 is provided with a sodium sulfide solution preparation tank 17 for providing the sodium sulfide solution for the zinc removal reaction of the sodium sulfide zinc removal reaction tank 16, and the sodium sulfide solution is pumped into the sodium sulfide zinc removal reaction tank 16 by a sodium sulfide lifting pump 18.

[0047] The filter pressing system comprises a diaphragm pump 19, a filter press 20, an SCR treatment device 22 and a zinc-containing sludge collecting device 21, the inlet of the diaphragm pump 19 is communicated with the sodium sulfide zinc removal system, the outlet of the diaphragm pump 19 is communicated with the inlet of the filter press 20, the water outlet of the filter press 20 is communicated with the SCR treatment device 22, and the sludge outlet of the filter press 20 is communicated with the zinc-containing sludge collecting device 21.

[0048] The solution after the zinc removal reaction is pumped into the filter press 20 by the diaphragm pump 19, the solution obtained after the pressure filtration of the filter press 20 enters the SCR (selective catalytic reduction technology) treatment device, and the zinc-containing sludge obtained enters the zinc sludge collecting device, waiting for subsequent treatment.

[0049] In the description of the utility model, it is understood that the orientation or positional relationship indicated by the terms "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like is the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the utility model, and does not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the utility model. In addition, the terms "first", "second", "third" and the like are only for the purpose of description, and cannot be understood as indicating or implying relative importance. Therefore, the features limited by "first", "second" and the like can be explicitly or implicitly included one or more features. In the description of the utility model, unless otherwise specified, the meaning of "a plurality of" is two or more.

[0050] In the description of the utility model, unless otherwise specified and limited, the terms "mounting", "connection" and "connection" should be understood broadly, for example, it can be fixed connection, can also be detachable connection, or integral connection, can be mechanical connection, can also be electrical connection, can be direct connection, can also be indirectly connected through an intermediate medium, and can be the communication between two elements. For ordinary skilled in the art, the specific meaning of the above terms in the application can be understood according to the specific circumstances.

[0051] If the utility model discloses or involves mutually fixed and connected parts or structural parts, unless otherwise stated, the fixed connection can be understood as: detachable fixed connection (for example, connected by using bolts or screws), and can also be understood as: non-detachable fixed connection (for example, riveting, welding), of course, the mutually fixed connection can also be replaced by integral structure (for example, manufactured by integral forming process) (except that integral forming process is obviously unavailable).

[0052] In addition, the terms used to indicate the positional relationship or shape in any technical solution disclosed by the utility model include the approximate, similar or close state or shape unless otherwise stated.

[0053] Any component provided by the utility model can be assembled by a plurality of individual components, or can be a single component manufactured by integral forming process.

[0054] It should be understood that the structure, proportion, size and the like shown in the drawings of the present application are only used to illustrate the content disclosed in the present application, to enable those skilled in the art to understand and read, and are not used to limit the implementation conditions of the present application, and therefore do not have technical significance. Any modification of structure, change of proportion relationship or adjustment of size, without affecting the effects and purposes of the present application, should still fall within the scope of the technical content disclosed in the present application.

[0055] It should be further noted that the same reference signs in the embodiments of the present application represent the same component or the same part.

[0056] Any adaptive changes according to actual needs are within the scope of the present application.

[0057] It should be noted that for those skilled in the art, it is obvious that the present application is not limited to the details of the above exemplary embodiments, and the present application can be implemented in other specific forms without departing from the spirit or basic characteristics of the present application. Therefore, from any point of view, the embodiments should be regarded as exemplary and non-limiting, and the scope of the present application is defined by the appended claims rather than the above description, and therefore all changes falling within the meaning and scope of the equivalent elements of the claims are intended to be included in the present application. Any reference signs in the claims should not be regarded as limiting the claims.

[0058] The principles and implementation modes of the present application are described by applying specific examples in the present application, and the above embodiment descriptions are only used to help understand the method and core idea of the present application; at the same time, for those skilled in the art, according to the idea of the present application, there will be changes in specific implementation modes and application scope. In conclusion, the content of the present application should not be understood as a limitation of the present application.

Claims

1. A system for treating and recycling alkaline zinc-nickel alloy wastewater, characterized in that it comprises the following steps: The system comprises an ion exchange nickel removal system, a nickel recovery system, an electro-catalytic oxidation system, a zinc removal system and a pressure filtration system. ​ 2. The system for alkaline zinc nickel alloy wastewater treatment and its reclamation according to claim 1, characterized in that: The ion exchange nickel removal system comprises an ion exchange column and an acid elution solution preparation tank, the ion exchange column is provided with a wastewater inlet, an acid elution solution inlet, a nickel-containing outlet and a nickel-free outlet, the wastewater inlet is connected with a wastewater raw water pool, and the acid elution solution inlet is connected with the acid elution solution preparation tank.

3. The system for alkaline zinc nickel alloy wastewater treatment and its reclamation according to claim 2, characterized in that: The ion exchange nickel removal system further comprises a multi-medium filter arranged between the wastewater raw water pool and the ion exchange column, the inlet of the multi-medium filter is connected with the wastewater raw water pool, and the outlet of the multi-medium filter is connected with the wastewater inlet of the ion exchange column.

4. The system for wastewater treatment and its valorization of alkaline zinc-nickel alloys according to claim 2, characterized in that: The nickel recovery system comprises a nickel elution solution collection tank, an electrolytic impurity removal tank, a boric acid solution preparation tank and a diaphragm electrodeposition tank, the electrolytic impurity removal tank is used for removing impurity metal ions in the solution, and the diaphragm electrodeposition tank is used for electrodeposition of nickel ions; the inlet of the nickel elution solution collection tank is connected with the nickel-containing outlet of the ion exchange column, the nickel elution solution collection tank, the electrolytic impurity removal tank and the diaphragm electrodeposition tank are sequentially connected, the outlet of the boric acid solution preparation tank is connected with the inlet of the diaphragm electrodeposition tank, and the outlet of the diaphragm electrodeposition tank is connected with the inlet of the acid elution solution preparation tank.

5. The system for wastewater treatment and its valorization of alkaline zinc-nickel alloys according to claim 1, characterized in that: The electro-catalytic oxidation system comprises an electro-catalytic oxidation tank, the inlet of the electro-catalytic oxidation tank is connected with the ion exchange nickel removal system, and the outlet of the electro-catalytic oxidation tank is connected with the zinc removal system.

6. The system for alkaline zinc nickel alloy wastewater treatment and its valorization according to claim 5, characterized in that: The electro-catalytic oxidation system is a three-dimensional electro-catalytic oxidation system, the electro-catalytic oxidation tank is a three-dimensional oxidation tank, the three-dimensional oxidation tank is provided with an electro-catalytic oxidation cathode plate, an electro-catalytic oxidation anode plate and three-dimensional electrode particles, and the electro-catalytic oxidation cathode plate and the electro-catalytic oxidation anode plate are electrically connected with a direct-current power supply.

7. The system for wastewater treatment and its valorization of alkaline zinc-nickel alloys according to claim 1, characterized in that: The zinc removal system comprises an acid-alkali adjusting tank and a zinc removal reaction tank which are sequentially connected, the inlet of the acid-alkali adjusting tank is connected with the electro-catalytic oxidation system, and the outlet of the zinc removal reaction tank is connected with the pressure filtration system.

8. The system for alkaline zinc nickel alloy wastewater treatment and its valorization according to claim 7, characterized by the fact that: The zinc removal system further comprises a dilute acid preparation tank connected with the acid-alkali adjusting tank, and a dilute acid lifting pump is arranged between the dilute acid preparation tank and the acid-alkali adjusting tank.

9. The system for alkaline zinc nickel alloy wastewater treatment and its valorization according to claim 7, characterized in that: The zinc removal system further comprises a sodium sulfide solution preparation tank connected with the zinc removal reaction tank, and a sodium sulfide lifting pump is arranged between the sodium sulfide solution preparation tank and the zinc removal reaction tank.

10. The system for treatment and recycling of alkaline zinc nickel alloy wastewater as claimed in claim 1 wherein: The pressure filtration system comprises a diaphragm pump, a pressure filter, an SCR treatment device and a zinc-containing sludge collection device, the inlet of the diaphragm pump is connected with the zinc removal system, the outlet of the diaphragm pump is connected with the inlet of the pressure filter, the water outlet of the pressure filter is connected with the SCR treatment device, and the sludge outlet of the pressure filter is connected with the zinc-containing sludge collection device.

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