WO2012098924A1 - Wastewater treatment apparatus, wastewater treatment method, and wastewater treatment system - Google Patents

Abstract

A wastewater treatment apparatus (1) of the present invention is provided with: an oxidation treatment means (20) for oxidizing a metal complex-forming compound contained in wastewater (W₀) that contains at least a heavy metal and the metal complex-forming compound; an insolubilization treatment means (30) for insolubilizing the heavy metal in the oxidized wastewater (W₀); and a membrane separation means (40) for separating the insolubilized wastewater (W₀) through a membrane. In addition, a wastewater treatment method of the present invention uses the above-described wastewater treatment apparatus. The present invention is capable of providing a wastewater treatment apparatus, a wastewater treatment method and a wastewater treatment system, each of which is capable of highly treating wastewater that contains a heavy metal and a metal complex-forming compound without adding a flocculant to the wastewater, and each of which is capable of sufficiently decreasing the heavy metal concentration.

Description

Waste water treatment apparatus, treatment method, and waste water treatment system

The present invention relates to a wastewater treatment apparatus, a treatment method, and a wastewater treatment system for treating wastewater containing heavy metals.
This application claims priority based on Japanese Patent Application No. 2011-009902 filed in Japan on January 20, 2011, the contents of which are incorporated herein by reference.

Conventionally, as a method for removing heavy metals from waste water containing heavy metals such as plating waste water discharged from an electrolytic plating process, the following methods are generally used.
For example, as shown in FIG. 6, first, the waste water W ₀ once stored in the storage tank 11 is insolubilized in the insolubilization tank 31. Specifically, an insolubilizing agent such as a hydroxylating agent (alkaline agent) or a sulfiding agent is added to the waste water, and the heavy metal is made into an insolubilized material such as a hydroxide or sulfide that is hardly soluble in water. Since the insolubilized material has a small particle size, an insoluble material such as an inorganic flocculant (such as polyaluminum chloride (PAC)) or a polymer flocculant is added to the wastewater insolubilized in the agglomeration tank 71. Agglomerate. Next, the insolubilized material agglomerated in the precipitation tank 61 is settled and separated, and the supernatant liquid W ₄ is filtered with a filter 45 such as a sand filter as necessary, and the filtered water W ₁ is further passed to the pH adjustment tank 51. neutralized discharged as treated water W ₃ from Te.

In recent years, electroless plating such as electroless nickel plating has been widely performed. Electroless plating is characterized by using a reducing agent, and deposits a metal using the electrons of the reducing agent. According to this method, it is possible to plate even a non-conductive substance.
However, when treating the wastewater discharged from this electroless plating step, it is difficult to sufficiently treat the conventional method described above, and it is difficult to reduce the heavy metal concentration in the wastewater.

In electroless plating such as electroless nickel plating, this may be due to the fact that the plating solution contains a compound (for example, a chelating agent) that forms a metal complex by coordination with heavy metal. .
As described above, when treating plating wastewater, an insolubilizing treatment is performed by adding an insolubilizing agent to the wastewater. If the waste water contains a compound that forms a metal complex such as a chelating agent (hereinafter sometimes referred to as “complex-forming compound”), heavy metals such as nickel form a metal complex with the complex-forming compound, and the waste water Dissolve in. For this reason, since this metal complex leaks without being filtered with a filter, it is thought that processing efficiency falls.
Further, even when acidic zinc plating is performed, it is considered that the treatment efficiency is lowered because a large amount of ammonia is contained in the bath and the heavy metal forms ammonia and an ammine complex.

Therefore, as a method of treating wastewater containing heavy metal ions, heavy metal complexes of heavy metals and chelating agents, etc., an insolubilizing agent is generated by adding an insolubilizing agent to the wastewater, and then supplied to a membrane separation device. A separation method has been proposed (see, for example, Patent Documents 1 and 2).
In addition, as a method of removing multiple trace components such as iron, manganese, silica, and fluorine in the wastewater at once, after adding aluminum sulfate (flocculant) and oxidizing agent to the wastewater stored in the treatment tank, There has been reported a method of membrane filtration of solid matter produced by a separation membrane filter soaked in (see, for example, Patent Document 3).
Furthermore, as a method for treating waste water containing low-concentration heavy metals such as copper, a method for improving the sludge cohesiveness by performing an oxidation treatment with an oxidizing agent after an insolubilization treatment with a sulfurizing agent has been reported. (For example, refer to Patent Document 4).

Japanese Patent No. 3111508 JP-A-2-157090 JP 2010-36180 A JP 2007-69068 A

However, even in the methods described in Patent Documents 1 and 2, when a complex-forming compound is contained in the wastewater, the heavy metal to be removed forms a metal complex with the complex-forming compound, so insolubilization with an insolubilizing agent The reaction was easily inhibited, and it was difficult to obtain a sufficient treatment effect.

In the method described in Patent Document 3, since the flocculant is added, the drug cost increases. Moreover, since sludge is generated when a flocculant is added, the cost for disposal of the sludge is also increased.
Further, in the method described in Patent Document 3, since an oxidizing agent is added to the treatment tank in which the separation membrane filter is immersed, heavy metals in the wastewater are easily oxidized and easily deposited on the surface of the separation membrane filter.
When metal oxide is deposited on the membrane surface, the pores of the membrane are blocked, resulting in a problem that the membrane filtration flux is lowered. Further, when a resin separation membrane filter is used, the membrane may be deteriorated by the oxidizing agent.

In the method described in Patent Document 4, even if the coagulation of the generated sludge can be improved, when the complex forming compound is contained in the wastewater, the heavy metal forms a metal complex with the complex forming compound. The insolubilization reaction by the sulfiding agent was easily inhibited, and it was difficult to obtain a sufficient treatment effect.
In addition, in order to sufficiently reduce the concentration of heavy metals in wastewater, it is necessary to add a large amount of a sulfurizing agent and a flocculant. However, the cost of chemicals increases and the amount of sludge generated increases the disposal cost of sludge. Or

In the plating processing industry and the metal surface treatment industry, a process for cleaning the metal surface to be processed (metal surface cleaning process) is always provided.
This metal surface cleaning process includes a rinsing process for cleaning the surface with pure water or the like, and an oil cleaning process for cleaning the surface oil with water containing a cleaning component.
When wastewater discharged from the plating processing industry and the metal surface treatment industry is treated by conventional techniques (coagulation or sand filtration), if this treated water is reused in the metal surface cleaning process, the following problems occur. Arise.
(1) The SS component and the unreacted flocculant remain only by sand filtration, and these adhere to the product to be processed.
(2) Since metal ions have not been sufficiently removed, metal components adhere to the workpiece.

The present invention has been made in view of the above circumstances, and wastewater containing a compound that forms a heavy metal and a metal complex can be treated to a high degree without adding a flocculant, and the concentration of heavy metal can be sufficiently reduced. A treatment device, a treatment method, and a wastewater treatment system are provided.

The wastewater treatment apparatus of the present invention is an apparatus for treating wastewater containing at least a heavy metal and a compound that forms a metal complex by coordination with the heavy metal, and oxidizes the compound that forms the metal complex in the wastewater. An oxidation treatment means for treating, an insolubilization treatment means for insolubilizing heavy metals in the oxidized wastewater, and a membrane separation means for membrane-separating the insoluble wastewater.
Furthermore, it is preferable to provide a sedimentation separation means for sedimenting and separating heavy metals in the wastewater that has been insolubilized between the insolubilization treatment means and the membrane separation means.
Furthermore, it is preferable that the oxidation treatment step includes a means for adding at least one oxidizing agent selected from the group consisting of hypochlorous acid, chlorous acid, perchloric acid, and salts thereof.
Furthermore, it is preferable that the oxidation treatment means includes a pH adjustment means for adjusting the pH of the wastewater.

The wastewater treatment method of the present invention is a method for treating wastewater containing at least a heavy metal and a compound that forms a metal complex by coordination with the heavy metal, the compound forming the metal complex in the wastewater. And an insolubilization treatment step for insolubilizing heavy metals in the oxidized wastewater, and a membrane separation step for membrane separation of the insolubilized wastewater.
Furthermore, it is preferable to have a sedimentation separation step for separating and separating heavy metals in the wastewater that has been insolubilized between the insolubilization treatment step and the membrane separation step.
The oxidation treatment step is preferably performed by adding at least one oxidizing agent selected from the group consisting of hypochlorous acid, chlorous acid, perchloric acid, and salts thereof.
Furthermore, it is preferable that in the oxidation treatment step, an oxidizing agent is added after adjusting the pH of the wastewater to 4 or more and 8 or less.
Furthermore, it is preferable to detect the end point of the addition of the oxidizing agent to the wastewater by the redox potential.

The waste water treatment system of the present invention is characterized in that the treated water treated by the treatment apparatus of the present invention is reused in a metal surface cleaning step of plating or metal surface treatment.

According to the wastewater treatment apparatus and treatment method of the present invention, wastewater containing a compound that forms a heavy metal and a metal complex can be treated at a high level without adding a flocculant, and the heavy metal concentration can be sufficiently reduced.
The treated water obtained by the wastewater treatment apparatus and treatment method of the present invention has a very low metal content. Moreover, since a flocculant is not used for wastewater treatment, the outflow of unreacted aggregates is not mixed into the treated water.
Therefore, according to the wastewater treatment system of the present invention, the treated water treated by using the treatment apparatus and the treatment method of the present invention is circulated to the metal surface cleaning process that is a wastewater generation source, thereby affecting the product to be processed. The treated water can be used effectively without giving water.

It is a schematic block diagram which shows an example of the wastewater processing apparatus of this invention. It is a schematic block diagram which shows the other example of the wastewater processing apparatus of this invention. It is a schematic block diagram which shows the other example of the wastewater processing apparatus of this invention. It is a schematic block diagram which shows the other example of the wastewater processing apparatus of this invention. It is a graph which shows the result of a test example. It is a schematic block diagram which shows an example of the apparatus used for the process of the conventional wastewater. It is a schematic block diagram which shows an example of the wastewater treatment system of this invention. It is a schematic block diagram which shows the other example of the wastewater treatment system of this invention. It is a schematic block diagram which shows the other example of the wastewater treatment system of this invention. It is a schematic block diagram which shows the other example of the wastewater treatment system of this invention.

Hereinafter, the present invention will be described in detail.
[Wastewater treatment equipment]
FIG. 1 is a schematic configuration diagram showing an example of a wastewater treatment apparatus of the present invention. The wastewater treatment apparatus 1 in this example includes, in order from the upstream side, a storage unit 10 that temporarily stores wastewater W ₀ , an oxidation treatment unit 20, an insolubilization treatment unit 30, a membrane separation unit 40, and a pH adjustment unit 50. It comprises.
2 to 4, the same components as those in FIG. 1 are denoted by the same reference numerals, and the description thereof may be omitted.

<Waste water>
The waste water W ₀ to be treated in the present invention is, for example, a waste liquid (treated water) generated from a metal surface treatment factory such as a plating factory, and forms a metal complex by coordination with heavy metals and the heavy metals. Compounds (hereinafter referred to as “complex-forming compounds”).
Examples of heavy metals include chromium, copper, zinc, cadmium, nickel, mercury, lead, iron, and manganese. These heavy metals may be contained alone, but are usually contained in a state where a plurality of heavy metals are mixed.
On the other hand, the complex-forming compound is a compound that forms a metal complex centered on a heavy metal atom by coordination with any of the heavy metals. Examples of complex forming compounds include acidic cleaning ingredients such as citric acid, gluconic acid, oxalic acid, tartaric acid, succinic acid, cyanide and salts thereof; EDTA, ethylenediamine, triethanolamine, and ammonia (including ammonium salts), etc. And amines. In addition, since a chelate complex is also contained in a metal complex, chelating agents, such as tartaric acid and EDTA, naturally correspond to a complex formation compound.

In addition to the heavy metal and the complex forming compound, the waste water W ₀ may contain a surfactant, a Lewis acid other than the complex forming compound, and the like as a cleaning component and a pH adjusting component.

<Storage means>
The storage means 10 is a means for temporarily storing waste water W ₀ generated from a metal surface treatment factory or the like.
The storage means 10 includes a storage tank 11. The storage tank 11 is not particularly limited as long as it can store the waste water W _0.

<Oxidation treatment means>
Oxidation means 20 is a means for oxidizing the complex forming compound in the waste water W _0.
The oxidation treatment means 20 in this example includes an oxidation tank 21 that stores the waste water W ₀ sent from the storage means 10, an oxidant addition means 22 that adds an oxidant to the waste water W ₀ in the oxidation tank 21, and an oxidation tank 21. It comprises a water gauge 23 for inspecting the quality of waste water W ₀ in, and a stirring blade 24 for stirring the waste water W ₀ in the oxidation vessel 21.
The oxidizing agent adding means is not particularly limited as long as it can add an oxidizing agent, and specific examples thereof include an electromagnetic metering pump, a diaphragm pump, and a magnet pump. Among these pumps, an electromagnetic metering pump is more preferable. These pump wetted parts are made of chemical-resistant materials. Specific examples of materials having chemical resistance include PVC (vinyl chloride), PVDF (polyvinylidene fluoride), PTFE (polytetrafluoroethylene), ABS, PS (polystyrene), PE (polyethylene), PP (polypropylene), For example, ceramic.

The oxidation tank 21 is not particularly limited as long as it can store the wastewater W ₀ , but is preferably made of a material that is not easily deteriorated by the oxidizing agent.
The oxidizing agent adding means 22 is not particularly limited as long as an oxidizing agent can be added.

The water quality meter 23 inspects the water quality of the waste water W ₀ in the oxidation tank 21. By examining the water quality, it is possible to grasp the excess and deficiency of the added amount of the oxidant, and in particular, it is effective for suppressing the excessive addition of the oxidant.
Examples of the water quality meter 23 include an oxidation-reduction potentiometer and an oxidant concentration meter. Moreover, it is also possible to use a densitometer for measuring the concentration of the complex-forming compound instead of or in combination with these electrometers and densitometers. However, the densitometer for measuring the concentration of the complex-forming compound is used when treating the waste water W ₀ containing the complex-forming compound capable of measuring the concentration such as ammonia.
In addition, although the oxidation treatment means 20 of this example is provided with one water quality meter 23, it may be provided with a plurality of types of water quality meters according to the water quality inspection method.
As a specific means of the water quality meter, an oxidation-reduction potentiometer is generally used.

Specific examples of the oxidizing agent include at least one oxidizing agent selected from the group consisting of hypochlorous acid, chlorous acid, perchloric acid, and salts thereof.
Moreover, the oxidation treatment means 20 may include a pH adjustment means for adjusting the pH of the waste water. As the pH adjusting means, the same means as the pH adjusting means 50 described later can be adopted. Moreover, it is preferable to adjust pH before adding an oxidizing agent.
The pH of the waste water in the oxidation treatment means 20 is preferably 4 to 8, and more preferably 4 to 6. Thereby, the oxidizing power by an oxidizing agent can be improved without generating chlorine gas.

<Insolubilization treatment means>
The insolubilization treatment means 30 is a means for insolubilizing heavy metals in the waste water W ₀ oxidized by the oxidation treatment means 20. The insolubilization means that heavy metal ions that are liberated in the waste water W ₀ are precipitated by using a hardly soluble compound (insolubilized product). Here, the insolubilized material means a material having a very low solubility, such as a hydroxide or a sulfide.
The insolubilization treatment means 30 of this example includes an insolubilization tank 31 for storing the waste water W ₀ sent from the oxidation treatment means 20, an insolubilization agent addition means 32 for adding an insolubilization agent to the waste water W ₀ in the insolubilization tank 31, and an insolubilization tank. It comprises a water meter 33 for checking the quality of waste water W ₀ in the 31, and a stirring blade 34 for stirring the waste water W ₀ in the insolubilized tank 31.

The insolubilizing tank 31 is not particularly limited as long as it can store the wastewater W ₀ , but is preferably made of a material that is not easily deteriorated by the insolubilizing agent. Specific examples of materials that are not easily deteriorated by the insolubilizer include stainless steel, FRP, PVC (vinyl chloride), PVDF (polyvinylidene fluoride), PTFE (polytetrafluoroethylene), ABS, PS (polystyrene), and PE (polyethylene). ), PP (polypropylene), and ceramic.
As specific means of the insolubilization processing means, a storage tank, an insolubilizing agent addition means, a stirrer and a pH meter are used.
The insolubilizing agent adding means 32 is not particularly limited as long as an insolubilizing agent can be added.
As specific means for adding the insolubilizing agent, when using the hydroxide method, a sodium hydroxide solution storage tank having chemical resistance, an electromagnetic metering pump having a chemical resistance, a diaphragm pump, a magnet pump, etc. Is used. When using the sulfide method, a sodium sulfide solution storage tank having chemical resistance and an electromagnetic metering pump, diaphragm pump, or magnet pump having chemical resistance are used.

The water quality meter 33 inspects the water quality of the waste water W ₀ in the insolubilization tank 31. By examining the water quality, it is possible to grasp the excess or deficiency of the amount of the insolubilizing agent added, and it is particularly effective for suppressing the excessive addition of the insolubilizing agent.
Examples of the water quality meter 33 include a pH meter.
Although the insolubilization processing means 30 of this example includes one water quality meter 33, a plurality of types of water quality meters may be provided depending on the water quality inspection method.

<Membrane separation means>
The membrane separation unit 40 is a unit that separates the waste water W ₀ insolubilized by the insolubilization unit 30 into filtered water W ₁ and membrane separation concentrated water W ₂ .
The membrane separation means 40 in this example is a system in which pressure is applied by a pressure pump P1, and includes a filtration membrane 41.
Examples of the filtration membrane 41 include a hollow fiber membrane, a flat membrane, a tubular membrane, and a monolith type membrane. A hollow fiber membrane is preferable because of its high volume filling rate.
When a hollow fiber membrane is used as the filtration membrane 41, examples of the material include cellulose, polyolefin, polysulfone, polyvinylidene fluoride difluoride (PVDF), and polytetrafluoroethylene (PTFE). Among the materials described above, polyvinylidene fluoride difluoride (PVDF) and polytetrafluoroethylene (PTFE) are preferable as the material for the hollow fiber membrane.
When a monolithic membrane is used as the filtration membrane 41, a ceramic membrane can be used.
As a specific means of membrane separation means, a hollow fiber membrane element made of polyvinylidene difluoride is immersed in a water tank for membrane separation, and the secondary side (filtered water side) of the membrane element is connected to a filtration pump. Is used. A device provided with aeration means for cleaning the membrane surface is used below the membrane element.

The average pore diameter of the micropores formed in the filtration membrane 41 is generally 0.001 to 0.1 μm for a membrane called an ultrafiltration membrane, and 0.1 to 1 μm for an average pore size for a membrane commonly called a microfiltration membrane. In the present invention, these films are preferably used.
Since the particle diameter of the insolubilized material generated by insolubilizing heavy metal is generally 0.1 to 100 μm, the average pore diameter of the fine pores of the filtration membrane 41 is preferably 0.03 μm or more. . When the average pore diameter is less than 0.03 μm, the pressure required for membrane separation increases, and the operating energy becomes excessive. The average pore diameter of the fine pores of the filtration membrane 41 is more preferably 0.1 μm or more. On the other hand, the average pore diameter of the fine pores of the filtration membrane 41 is preferably 3 μm or less. When the average pore diameter exceeds 3 μm, the proportion of particles of insolubilized heavy metal leaking to the secondary side (in the filtrate water W ₁ ) of the filtration membrane 41 increases, and the metal concentration in the filtrate water W ₁ tends to increase. . The average pore diameter of the fine pores of the filtration membrane 41 is more preferably 10 μm or less.

The membrane separation means 40 separates the waste water W ₀ into filtered water W ₁ from which insolubilized substances have been removed and membrane separation concentrated water W ₂ from which insoluble substances have been concentrated.
Filtered water _{W 1} is transferred to a pH adjustment means which will be described later, is pH adjusted. On the other hand, membrane separation concentrated water W ₂ is typically dehydrated by the dehydration means (not shown), it is treated as industrial wastes such as dehydrated cake.

<PH adjusting means>
The pH adjusting unit 50 is a unit that adjusts the pH of the filtered water W ₁ membrane-separated by the membrane separating unit 40 to a pH suitable for discharge into a river or the like. The pH-adjusted filtered water W ₁ is treated. It is discharged as water _{W 3.}
Incidentally, the film since the sufficiently remove the insolubles by separation means 40, heavy metals and neutralize the pH of the filtered water W ₁ there is no fear of remelting.

The pH adjusting means 50 includes a pH adjusting tank 51, a pH meter (not shown), an acid addition device, and an alkali addition device (both not shown).
The pH adjusting tank 51 is not particularly limited as long as it can store the filtered water W _1. Specifically, the material of the pH adjusting tank 51 is stainless steel, FRP, PVC (vinyl chloride), PVDF (polyvinylidene fluoride), PTFE (polytetrafluoroethylene), ABS, PS (polystyrene), PE (polyethylene), Examples include PP (polypropylene) and ceramic. Further, the pH meter, the acid addition device, and the alkali addition device are not particularly limited as long as they are used for pH adjustment.
As specific means of the pH adjusting means, a storage tank, an acid addition means, an alkali addition means, a stirrer, and a pH meter are used.
As specific means of the acid addition device (acid addition means), a chemical storage tank having chemical resistance and an electromagnetic metering pump, diaphragm pump, or magnet pump having chemical resistance are used.
As specific means of the alkali addition device (alkali addition means), a chemical storage tank having chemical resistance and an electromagnetic metering pump, diaphragm pump, or magnet pump having chemical resistance are used.

<Effect>
Processing apparatus 1 of the waste water of the present invention described above, the oxidation treatment unit 20 in this order from the upstream side, insolubilization means 30, since comprising a membrane separation means 40, the waste water W ₀ is insolubilized and membrane separation after being oxidized The That is, since the complex-forming compound in the waste water W ₀ is oxidized by the oxidation treatment means 20 before the insolubilization treatment, the insolubilization treatment in the subsequent insolubilization treatment means 30 is not easily inhibited by the complex-forming compound. Therefore, if the processing device 1 of the waste water of the present invention, the waste water W ₀ can be processed highly, it can sufficiently reduce the concentration of heavy metals in the treated water W _3.

Moreover, since the wastewater treatment apparatus 1 of the present invention can oxidize the complex-forming compound in the wastewater W ₀ by the oxidation treatment means 20, the heavy metal produced by the insolubilization treatment means 30 can be insolubilized without adding a flocculant. The particle diameter of the product can be increased. Therefore, the filtration membrane 41 of the downstream membrane separation means 40 is less likely to be blocked by the insolubilized material, and the membrane separation means 40 can be stably operated over a long period of time.

Processing apparatus 1 of the waste water of the present invention, suitable for is a device for processing waste water W ₀ containing heavy metals and complexing compounds, in particular process waste water discharged from an electroless plating process such as electroless nickel plating It is.

<Other embodiments>
The wastewater treatment apparatus of the present invention is not limited to the treatment apparatus 1 shown in FIG. For example, in the processing apparatus 1 of FIG. 1, is provided with the pH adjustment unit 50, pH of the filtered water W ₁ is as long as pH suitable for discharge into rivers or the like, may not include the pH adjustment unit 50 .
In addition, in the oxidation treatment means 20, when a chlorine-based oxidant is added from the oxidant addition means 22, an odor component such as chlorine gas or chloramine due to ammonia oxidation may be generated. Therefore, it is desirable to appropriately install gas recovery means according to the generated concentration.
Specific examples of the gas recovery means include a scrubber or an activated carbon gas purification device.

Further, the processing apparatus 1 of FIG. 1 includes the full-volume type membrane separation means 40, but may be a cross-flow type membrane separation means 40 as shown in FIG. 2.
In the wastewater treatment apparatus 2 shown in FIG. 2, a part of the membrane separation concentrated water W ₂ separated by the membrane separation means 40 is returned to the insolubilization tank 31 of the insolubilization treatment means 30 in the previous stage. A part of the concentrated water W ₂ may be returned to the oxidation tank 21 of the oxidation treatment tank 20 or the storage tank 11 of the storage means 10.

The membrane separation means 40 provided in the wastewater treatment apparatuses 1 and 2 shown in FIGS. 1 and 2 are both pressurized, but the membrane separation means 40 may be an immersion type as shown in FIG.
Membrane separation means 40 of the processor 3 of waste water shown in Figure 3, a membrane separation tank 42 for storing the waste water W ₀ sent from the insolubilization treatment unit 30, the membrane module 43 provided in the membrane separation tank 42, membrane And an aeration means 44 for cleaning. A suction pump P <b> 2 is connected to the membrane module 43, and a blower B is connected to the air diffuser 44.

Examples of the membrane module 43 include a normal membrane module used for a separation operation such as water treatment. In the membrane module 43, filtered water W ₁ and the membrane separation concentrated water W waste water W ₀ by suction filtration through pores of the filtration membrane of the waste water W ₀ of the membrane in the separation tank 42 by the suction pump P2 membrane module 43 ₂ and separated.
On the other hand, the air diffuser 44 is provided below the membrane module 43 and discharges the air supplied from the blower B into the membrane separation tank 42. Thus, continuously or intermittently diffuser air bubbles from the air diffuser means 44, through the liquid of the waste water W ₀ reaches a membrane module 43, then, is discharged from the water surface. At this time, the filtration membrane is washed.
A part of the membrane separation concentrated water W ₂ separated by the membrane separation means 40 may be returned to the insolubilization tank 31, the oxidation tank 21, and the storage tank 11.

Further, the wastewater treatment apparatus of the present invention, for example, as shown in FIG. 4, removes heavy metals in wastewater W ₀ insolubilized by the insolubilization treatment means 30 between the insolubilization treatment means 30 and the membrane separation means 40. It is preferable to provide sedimentation separation means 60 for sedimentation separation.
The sedimentation separation means 60 of the wastewater treatment apparatus 4 shown in FIG. 4 includes a sedimentation tank 61 that accumulates the wastewater W ₀ sent from the insolubilization treatment means 30.
The structure of the precipitation tank 61 is not particularly limited, and an effective surface area may be increased by installing an inclined plate inside the precipitation tank 61.
Moreover, what is necessary is just to set suitably about the volume of the sedimentation tank 61 according to the solid content density | concentration of a process target liquid, and the magnitude | size of process target particle | grains (insoluble matter of heavy metal).

The waste water W ₀ is separated into the supernatant liquid W ₄ and the precipitated concentrated water W ₅ by the sedimentation separation means 60.
The supernatant liquid W ₄ is transferred to the subsequent membrane separation means 40 and further membrane-separated into filtrate water W ₁ and membrane separation concentrated water W ₂ . The supernatant W ₄ contains fine heavy metal insolubilized material that has not been completely settled and removed by the sedimentation separation means 60, but the fine insolubilized material is removed by the membrane separation means 40.
On the other hand, precipitated the concentrate W ₅ is usually dehydrated by the dehydration means (not shown), it is treated as industrial wastes such as dehydrated cake.

If the sedimentation separation means 60 is provided between the insolubilization treatment means 30 and the membrane separation means 40 as in the wastewater treatment apparatus 4 shown in FIG. 4, it is insolubilized before the membrane separation by the membrane separation means 40. the majority of heavy metals in waste water W ₀ can be removed from the waste water W _0. Accordingly, since the amount of particles removed by the membrane separation means 40 is reduced, the burden on the membrane separation means 40 is reduced, and a more stable filtration operation can be continued.
The wastewater treatment apparatus 4 shown in FIG. 4 includes the same membrane separation means 40 as the treatment apparatus 1 shown in FIG. 1, but the membrane separation means 40 of the treatment apparatuses 2 and 3 shown in FIGS. May be the same.

As described above, the wastewater treatment apparatus of the present invention can treat wastewater to a high degree even without a coagulation means for adding a flocculant to the wastewater to coagulate the insolubilized material, and can sufficiently reduce the heavy metal concentration. If necessary, aggregating means may be provided. However, the smaller the amount of the flocculant added to the waste water by the flocculating means, the more the chemical cost can be reduced and the sludge amount generated can be reduced, so that the sludge disposal cost can be reduced. Therefore, when the target treated water quality can be achieved without the aggregation means, it is preferable not to provide the aggregation means. The target treated water quality is 0.1 mg / L or less for nickel, for example.
In the case where the aggregation means is provided, the installation location is between the insolubilization processing means and the membrane separation means, and in the case where the sedimentation separation means is provided, between the insolubilization processing means and the sedimentation separation means. Specific examples of the aggregating means include a method of adding an inorganic aggregating agent such as polyaluminum chloride or a polymer aggregating agent.

[Wastewater treatment method]
The wastewater treatment method of the present invention includes an oxidation treatment step for oxidizing a complex-forming compound in wastewater, an insolubilization treatment step for insolubilizing heavy metals in the oxidized wastewater, and membrane separation for membrane separation of the insoluble wastewater. Process.
Hereinafter, an example of the wastewater treatment method of the present invention will be specifically described using the wastewater treatment apparatus 1 shown in FIG.

<Oxidation process>
First, the waste water W ₀ is temporarily stored in the storage tank 11 of the storage means 10.
Next, the waste water W ₀ stored in the storage tank 11 is transferred to the oxidation tank 21 of the oxidation treatment means 20, and an oxidizing agent is added to oxidize the complex-forming compound in the waste water W ₀ .

Examples of the oxidizing agent used in the oxidation treatment step include hypochlorous acid, chlorous acid, perchloric acid or a salt thereof, and hydrogen peroxide. Among these, hypochlorous acid, chlorous acid, perchloric acid or a salt thereof, or a mixed solution thereof is preferable, and a sodium hypochlorite solution is particularly preferable from the viewpoints of handleability and availability.
If hypochlorous acid, chlorous acid, perchloric acid or a salt thereof, or a mixed solution thereof is used as an oxidizing agent, the oxidation reaction easily proceeds quickly, and the overall processing speed can be increased. Moreover, since these have high decomposition efficiency of complex-forming compounds having a chelating action such as EDTA and tartaric acid, they can prevent the inhibition of aggregation of insolubilized products by the complex-forming compounds in the insolubilization treatment step described later, and more insolubilization treatment Can be done efficiently.

In particular, when sodium hypochlorite or a solution thereof is used as an oxidizing agent, the particle size of the heavy metal insolubilized product produced in the insolubilizing treatment step tends to increase. When the particle size of the insolubilized material is larger, it is possible to suppress clogging of the pores of the filtration membrane in the membrane separation step described later, and the membrane flux can be maintained high.
Furthermore, when the waste water W ₀ is waste water containing nickel as a heavy metal such as electroless nickel plating waste water, dissolved nickel ions are converted into nickel oxyhydroxide (NiO (OH) by adding an oxidizing agent such as sodium hypochlorite. )) Oxidized. Since nickel oxyhydroxide generally has a lower solubility than nickel hydroxide (Ni (OH) ₂ ), sodium hypochlorite or a solution thereof is an oxidizing agent when performing advanced wastewater treatment. Is particularly preferred.

The addition of the oxidizing agent to the waste water W ₀ is a purpose to be oxidizing the complex forming compound contained in the wastewater W _0, adding an excess oxidizing agent becomes excessive consumption of chemicals. Moreover, when an oxidizing agent is added excessively, there exists a possibility that the filtration membrane used at the membrane separation process mentioned later may be oxidized with the remaining oxidizing agent. In addition, when an oxidizing agent is excessively added, the amount of sludge that is finally generated tends to increase.
From the above, when the oxidation treatment process that all oxidized complex forming compound contained in the wastewater W _0, it is desirable to stop the addition of the oxidizing agent to the waste water W _0, to control the excessive addition Good.
Examples of the method for detecting the end point of the addition of the oxidizing agent include a method of monitoring the oxidation-reduction potential using the water quality meter 23, monitoring the oxidizing agent concentration, or monitoring the concentration of the complex-forming compound.

<Monitoring of redox potential>
If the complex-forming compound remains in the wastewater W ₀ , the added oxidizing agent is consumed by the redox reaction with the complex-forming compound. While the oxidizing agent is consumed by the oxidation of the complex-forming compound, the redox potential of the wastewater W ₀ is low, and when all the complex-forming compounds capable of oxidative decomposition are oxidized and the oxidizing agent remains, the redox potential of the waste water W ₀ is Get higher.
Therefore, if the oxidation-reduction potential of the wastewater W ₀ in the oxidation tank 21 is monitored by the water quality meter (oxidation-reduction potentiometer) 23, the complex-forming compound capable of being oxidized and decomposed in the wastewater W ₀ when the oxidation-reduction potential increases. Can be easily determined to be all oxidized, and the addition of the oxidizing agent may be stopped at this point.

<Monitoring of oxidant concentration>
If the complex-forming compound remains in the wastewater W ₀ , the added oxidizing agent is consumed. That is, in the process of continuously adding the oxidizing agent, the oxidizing agent concentration is low and remains substantially constant while the complex-forming compound to be oxidized remains.
Therefore, if the concentration of the oxidizing agent in the oxidation tank 21 is monitored by the water quality meter (oxidizing agent concentration meter) 23, all the complex-forming compounds capable of oxidative decomposition in the wastewater W ₀ are oxidized when the oxidizing agent concentration increases. It can be easily determined that the oxidant has been added, and the addition of the oxidizing agent may be stopped at this point.
When hypochlorous acid, chlorous acid, perchloric acid, or a salt thereof is used as the oxidant, the oxidant concentration can also be obtained by measuring the residual chlorine concentration.

<Monitoring the concentration of complex-forming compounds>
If the complex-forming compound in the waste water W ₀ is a substance that can be monitored by a water quality meter such as ammonia, the substance is continuously monitored, and the addition of the oxidizing agent is stopped when the concentration of the complex-forming compound is sufficiently reduced do it.

Among the above-described methods for detecting the end point of addition of the oxidizing agent, the oxidation-reduction potential meter used as the water quality meter 23 is preferably monitored by the oxidation-reduction potential because it is easy to use. The redox potential can be monitored continuously (continuous measurement), while the oxidant and complexing compound concentrations can be monitored batchwise (samples taken at regular intervals). Therefore, the oxidation-reduction potential monitoring can detect the oxidant addition end point more instantaneously than other methods.

When the end point of the addition of the oxidizing agent is detected by monitoring the oxidation-reduction potential, the following is preferable.
That is, it is preferable to measure in advance the oxidation-reduction potential at the timing when the oxidant concentration increases (the addition of oxidant becomes excessive). Thereby, since the value of the oxidation-reduction potential measured in advance can be used as a criterion, it is possible to more easily determine the timing of stopping the addition of the oxidizing agent.

Note that it is difficult to determine whether or not the addition amount of the oxidizing agent is insufficient in the monitoring of the oxidation-reduction potential or the monitoring of the oxidizing agent concentration. In such a case, the amount of oxidant necessary to oxidize all the complex-forming compounds is predicted from the concentration of the complex-forming compounds in the wastewater W ₀ , and a larger amount of oxidant than the predicted amount is required. Added. Then, if it is determined that the oxidizing agent is excessive by monitoring the oxidation-reduction potential or monitoring the oxidizing agent concentration, the addition of the oxidizing agent may be stopped or the addition amount may be reduced.

Moreover, the oxidation treatment process may include a pH adjustment process for adjusting the pH of the wastewater. As the pH adjusting means, the same means as in the pH adjusting step described later can be adopted. Moreover, it is preferable to adjust pH before adding an oxidizing agent.
The pH of the waste water in the oxidation treatment step is preferably 4 to 8, and more preferably 4 to 6. Thereby, the oxidizing power by an oxidizing agent can be improved without generating chlorine gas.

<Insolubilization process>
In the insolubilization treatment step, the oxidized waste water W ₀ is transferred to the insolubilization tank 31 of the insolubilization treatment means 30, and an insolubilizing agent is added to insolubilize heavy metals in the waste water W ₀ .
As the insolubilization method, there are a hydroxide method using a hydroxylating agent and a sulfide method using a sulfiding agent. In the case of the sulfide method, hydrogen sulfide may be generated, and therefore the hydroxide method is preferable as the insolubilization treatment.

The hydroxide method is a method in which a hydroxylating agent (hydroxide ion) and a target metal are reacted and precipitated as a metal hydroxide having low solubility.
As the hydroxylating agent, sodium hydroxide, sodium carbonate, calcium hydroxide, magnesium hydroxide and the like are used. Sodium hydroxide is more preferable because sludge generation is reduced.

On the other hand, the sulfide method is a method in which a sulfiding agent (sulfide ion) and a target metal are reacted and precipitated as a metal sulfide having low solubility.
Examples of the sulfiding agent include sodium sulfide and hydrogen sulfide.

When insolubilization is performed by a hydroxide method, heavy metals have different pH ranges where the solubility is lowest depending on each metal species. Therefore, in order to increase the removal rate of heavy metals, an insolubilizing agent (hydroxylating agent) is added until the pH reaches the lowest solubility.
At that time, the addition amount of the insolubilizing agent is controlled by measuring the pH of the waste water W ₀ in the insolubilizing tank 31 by the water quality meter 33.
However, the composition and concentration of heavy metals in waste water W ₀ to be supplied to the waste water treatment apparatus, if you are found to be constant at all times, can also be controlled by a certain amount injected insolubilizing agent .

Moreover, even if it is the same heavy metal, the pH area | region where solubility becomes the lowest may differ with the other components to coexist. Therefore, in practice, it is desirable to control the pH by conducting a preliminary test using the waste water W ₀ to be treated and adding an insolubilizing agent so as to be in the most suitable pH range. The pre-test is a test for determining pH conditions that can achieve the target treated water quality with the least amount of insolubilizer used.

<Membrane separation process>
In the membrane separation step, the waste water W ₀ that has been insolubilized is transferred to the membrane separation means 40, and the filtered water W _{1 from} which the insoluble matter has been removed by the filtration membrane 41 and the membrane separation concentrated water W ₂ in which the insoluble matter has been concentrated. Membrane separation.
Filtered water W ₁ may be pH adjusted by the pH adjustment step described below as required. On the other hand, membrane separation concentrated water W ₂ is usually dehydrated, it is treated as industrial wastes such as dehydrated cake.

<PH adjustment step>
In pH adjustment step, transferring the filtered water _{W 1} to pH adjustment tank 51 of the pH adjusting means 50, the pH of the filtered water _{W 1} is adjusted to pH suitable for discharge into rivers. In particular, when the hydroxide method is used in the insolubilization treatment step, the filtered water W ₁ is usually alkaline, so it is preferable to neutralize it. The filtered water W ₁ whose pH has been adjusted is discharged as treated water W ₃ .
In the pH adjustment step, acids such as hydrochloric acid, sulfuric acid, and carbon dioxide are used as a pH adjuster for neutralization. When an excessive amount of acid is added in the pH adjustment step, an alkali such as sodium hydroxide, sodium carbonate, calcium hydroxide, and magnesium hydroxide is added as a pH adjuster, and the pH is adjusted to be in a neutral region. Readjust.
Incidentally, since the sufficiently remove the insolubles by membrane separation process, heavy metals and neutralize the pH of the filtered water W ₁ there is no possibility to re-dissolve.

<Effect>
According to the wastewater treatment method of the present invention described above, the oxidation treatment step is performed before the insolubilization treatment step, and the complex forming compound in the wastewater is oxidized, so that the insolubilization treatment in the insolubilization treatment step is performed by the complex forming compound. Hard to be disturbed. Therefore, wastewater can be treated at a high level and the heavy metal concentration in the treated water can be sufficiently reduced.

By the way, generally, when the hydroxide method is used in the insolubilization process, the particles of the insolubilized heavy metal produced therefrom are fine and the sedimentation rate tends to be very slow. Further, if fine particles are filtered in the membrane separation step, the pores of the membrane are easily blocked, and it is difficult to continue membrane filtration stably for a long period of time.
However, in the wastewater treatment method of the present invention, the complex-forming compound in the wastewater is oxidized by the oxidation treatment step before the insolubilization treatment step, so that it is generated by the insolubilization treatment step without adding a flocculant. The particle size of the heavy metal insolubilized material can be increased. Therefore, in the membrane separation step performed after the insolubilization treatment step, the filtration membrane is hardly clogged with the insolubilized material, and the membrane separation step can be performed stably over a long period of time.

The wastewater treatment method of the present invention is a method for treating wastewater containing heavy metals and complex-forming compounds, and is particularly suitable for treating wastewater discharged from an electroless plating step such as electroless nickel plating.

<Other embodiments>
The wastewater treatment method of the present invention is not limited to the method described above. For example, in the above-described method, it performs the pH adjustment step after the membrane separation step, if the pH at which the pH of the filtered water W ₁ is suitable for discharge into rivers or the like, pH adjustment step may not be performed.

In the above-described method, the oxidant addition method is exemplified as the oxidation treatment method in the oxidation treatment step. However, for example, an ozone oxidation method, a photocatalyst method, or a biological oxidation method may be used. However, from the viewpoint of simplicity of control and reaction rate, an oxidizing agent addition method is preferable as the oxidation treatment method. The ozone oxidation method is a method of oxidizing and decomposing organic substances using the oxidizing power of ozone generated from an ozone generator or the like. The photocatalytic method is a method of oxidizing and decomposing organic substances using an oxidizing power generated when a photocatalyst such as titanium dioxide is irradiated with ultraviolet rays. The biological oxidation method is a method of oxidizing and decomposing organic substances using an oxidizing action by microorganisms, such as an activated sludge method.
In addition, when an oxidizing agent addition method using a chlorine-based oxidizing agent is adopted as an oxidation treatment method, odorous components such as chlorine gas or chloramine due to ammonia oxidation are generated, so gas recovery can be performed according to the generated concentration. It is desirable to do it.

Further, in the above-described method, the method using the whole-volume type membrane separation means 40 as shown in FIG. 1 is exemplified as the membrane separation method in the membrane separation step, but for example, a cross-flow type membrane as shown in FIG. Separation means 40 or immersion type membrane separation means 40 may be used.
The full-volume type membrane separation means 40 shown in FIG. 1 and the cross-flow type membrane separation means 40 shown in FIG. 2 employ a pressure type, and the primary side of the membrane is high with the filtration membrane 41 sealed in a container. Can be pressurized with pressure. Therefore, the membrane can be separated with a high permeation flux, and the required membrane area can be reduced. However, when the insolubilized substance concentration (turbidity concentration) of the liquid to be treated is high, the filtration membrane 41 tends to be clogged. Therefore, it is preferable to carry out when the insolubilized substance concentration of the liquid to be treated is low.
On the other hand, the submerged membrane separation means 40 shown in FIG. 3 performs filtration by immersing the membrane module 43 in the liquid to be treated and setting the secondary side of the membrane to a negative pressure. Therefore, although the permeation flux is lower than that of the pressurization type, membrane separation can be performed without clogging the filtration membrane even if the concentration of insolubilized material is high.

Furthermore, the wastewater treatment method of the present invention uses, for example, the treatment device 4 shown in FIG. 4 to settle and separate heavy metals in the insolubilized wastewater W ₀ between the insolubilization treatment step and the membrane separation step. It is preferable to have.
The sedimentation process, transferred to waste water W ₀ which is insolubilized on the precipitation layer 61 of the settling device 60, to precipitate the insoluble matter of heavy metals, is separated into a supernatant and W ₄ and precipitation concentrated water W _5.
The supernatant W ₄ is transferred to a membrane separation step, and further membrane-separated into filtered water W ₁ and membrane separation concentrated water W ₂ . Although the supernatant W ₄ there is insolubilized of fine heavy metal that has not been completely settled removed by sedimentation separation step, fine insolubles by membrane separation step is removed.
On the other hand, precipitated the concentrate W ₅ is usually dehydrated, it is treated as industrial wastes such as dehydrated cake.

If a sedimentation separation step is performed between the insolubilization treatment step and the membrane separation step, most of the heavy metals in the insolubilized wastewater can be removed from the wastewater before membrane separation in the membrane separation step. Therefore, since the amount of particles to be removed in the membrane separation step is reduced, the burden on the filtration membrane is reduced, and more stable filtration operation can be continued.

As described above, when the hydroxide method is used in the insolubilization process step, the heavy metal insolubilized particles produced therefrom are fine and the sedimentation rate tends to be very slow. Therefore, it took a long time for precipitation, and it was necessary to enlarge the precipitation tank.
However, in the wastewater treatment method of the present invention, the complex-forming compound in the wastewater is oxidized by the oxidation treatment step before the insolubilization treatment step, so that it is generated by the insolubilization treatment step without adding a flocculant. The particle diameter of the heavy metal insolubilized material can be increased, and the sedimentation rate can be increased. Therefore, heavy metals can be precipitated in a short time in the sedimentation separation step, and therefore there is no need to increase the size of the precipitation tank.

As described above, the wastewater treatment method of the present invention can treat wastewater to a high degree without adding a flocculant and can sufficiently reduce the concentration of heavy metals. Good. However, the smaller the amount of the flocculant added, the lower the cost of chemicals and the amount of sludge that can be generated, so that the disposal cost of sludge can also be reduced. Therefore, it is preferable not to add the flocculant when the target treated water quality can be achieved without adding the flocculant. The target treated water quality is 0.1 mg / L or less for nickel, for example.
In addition, when adding a flocculant, the timing of addition of a flocculant is between an insolubilization treatment process and a membrane separation process, and when performing a sedimentation separation process, it is between an insolubilization treatment process and a sedimentation separation process.

[Wastewater treatment system]
FIG. 7 is a schematic configuration diagram showing an example of the wastewater treatment system of the present invention. The wastewater treatment system in FIG. 7 is a system that reuses treated water obtained from the wastewater treatment apparatus shown in FIG. 1 in a process for cleaning the metal surface of a product to be processed (metal surface cleaning process). The metal surface cleaning step includes an oil cleaning tank for cleaning the object to be processed before plating, and a primary cleaning tank and a secondary cleaning tank for cleaning the object to be processed after plating. Waste water generated in each washing tank is temporarily stored in the storage means 10 and then processed by the waste water treatment apparatus. The obtained treated water is reused in the metal surface cleaning step. Treated water may be used either before or after plating.
As shown in FIGS. 8 to 10, a system for reusing treated water obtained using the wastewater treatment apparatus of FIGS. 2 to 4 may be used.

Hereinafter, the present invention will be specifically described by way of examples, but the present invention is not limited thereto.

[Example 1]
As waste water, nickel-containing waste water discharged from the electroless nickel plating process was used. The nickel concentration in the wastewater was 6.5 mg / L. Further, this wastewater contained ammonia as a complex-forming compound. The concentration of ammonia was 3.8 mg / L as ammonia nitrogen (NH ₃ —N) concentration.
0.5 mL of sodium hypochlorite solution (effective chlorine concentration: 12% by mass) was added as an oxidizing agent to 500 mL of the nickel-containing waste water, and the mixture was stirred for 15 minutes to oxidize ammonia (oxidation process).
Thereafter, a sodium hydroxide solution adjusted to 0.1 mol / L as an insolubilizing agent was added to the oxidized wastewater to adjust the pH to 10 and stirred for 30 minutes to produce an insolubilized nickel product (insolubilized). Processing step).
Next, the insolubilized waste water was membrane-separated into filtered water and membrane-separated concentrated water using a hollow fiber membrane made of polyvinylidene fluoride (Mitsubishi Rayon Co., Ltd., “STELLAPORE SADF”, nominal pore size 0.4 μm) ( Membrane separation step).
The concentration of nickel (Ni) and ammonia nitrogen (NH ₃ —N) in the obtained filtered water was measured. The results are shown in Table 1.
Moreover, particle distribution was measured about the insolubilized material of nickel produced | generated by the insolubilization process process. The measurement was performed using a laser diffraction / scattering particle size distribution measuring apparatus (“LA-920” manufactured by Horiba, Ltd.), and the particle size was measured based on the volume and the frequency distribution was measured. Table 1 shows the mode diameter of the insolubilized material (particle diameter having the largest appearance ratio).

[Example 2]
An oxidation treatment process was performed in the same manner as in Example 1.
To the nickel-containing wastewater after the oxidation treatment step, 2.5 mL of a sodium sulfide nonahydrate aqueous solution adjusted to 0.1 mol / L as an insolubilizing agent was added and stirred for 30 minutes to form an insolubilized nickel (insolubilized) Processing step).
Subsequently, the membrane separation step was performed in the same manner as in Example 1, the concentrations of nickel and ammonia nitrogen in the filtered water were measured, and the particle distribution of the nickel insolubilized material was measured. These results are shown in Table 1.

[Example 3]
In the membrane separation step, an oxidation treatment step and an insolubilization treatment step were performed in the same manner as in Example 1 except that a polyethylene porous hollow fiber membrane (manufactured by Mitsubishi Rayon Co., Ltd., fractional pore size 0.03 μm) was used as the filtration membrane. The membrane separation process was performed, and the concentration of nickel in the filtered water was measured. The results are shown in Table 1.

[Example 4]
Example, except that polyaluminum chloride was added as an inorganic flocculant between the insolubilization step and the membrane separation step so that the flocculant concentration in the wastewater was 300 mg / L and gently stirred for 15 minutes. The oxidation treatment process, the insolubilization treatment process, and the membrane separation process were performed in the same manner as in Example 1, and the nickel concentration in the filtrate was measured. The results are shown in Table 1.

[Comparative Example 1]
Except for not performing the oxidation treatment step, the insolubilization treatment step and the membrane separation step were carried out in the same manner as in Example 1, the concentration of nickel and ammonia nitrogen in the filtrate was measured, and the particle distribution of the nickel insolubilized product was determined. It was measured. These results are shown in Table 1.

[Comparative Example 2]
Except for not performing the oxidation treatment step, the insolubilization treatment step and the membrane separation step were carried out in the same manner as in Example 2, the concentration of nickel and ammonia nitrogen in the filtered water was measured, and the particle distribution of the nickel insolubilized product was determined. It was measured. These results are shown in Table 1.

[Comparative Example 3]
Except that the insolubilization treatment step was not performed, the oxidation treatment step and the membrane separation step were performed in the same manner as in Example 1, and the concentrations of nickel and ammonia nitrogen in the filtered water were measured. These results are shown in Table 1.

Abbreviations in Table 1 are as follows.
· NaClO: sodium hypochlorite · NaOH: Sodium hydroxide · _Na 2 S: sodium sulfide

As is clear from Table 1, in Examples 1 to 3, the nickel concentration in the filtered water was low, and nickel could be sufficiently removed. Moreover, from the results of Examples 1 and 2, it was shown that ammonia, which is a complex-forming compound that forms a metal complex with respect to nickel, was decomposed because the concentration of ammonia nitrogen in the filtered water was low. Furthermore, the particle diameter of the insolubilized material showed large values of 8.8 μm and 10 μm, respectively.
In addition, also in Example 4 to which a flocculant was added, the nickel concentration in the filtered water was a low value, and nickel could be sufficiently removed. However, the amount of sludge was larger than in Examples 1 to 3.
In Examples 3 and 4, as in Examples 1 and 2, it was easily estimated that ammonia was decomposed, so the concentration of ammonia nitrogen in the filtered water was not measured. Further, in Examples 3 and 4, as in Examples 1 and 2, it was easily estimated that the particle diameter of the insolubilized material showed a large value, and therefore the particle diameter of the insolubilized material was not measured.

On the other hand, in Comparative Examples 1 and 2 where the oxidation treatment step was not performed, the nickel concentration in the filtered water was higher than in Examples 1 and 2, and nickel could not be sufficiently removed. In addition, the concentration of ammonia nitrogen in the filtered water was high, indicating that the complex forming ammonia was not sufficiently decomposed. Furthermore, the particle diameter of the insolubilized material was 3.9 μm and 5.1 μm, respectively, and the particle diameter was smaller than those of Examples 1 and 2.
Moreover, in the case of the comparative example 3 which did not perform the insolubilization process process, the nickel density | concentration in filtered water was still higher than the comparative examples 1 and 2, and nickel could hardly be removed. Further, the concentration of ammonia nitrogen in the filtered water was the same as the concentration of ammonia nitrogen in the waste water, indicating that the complex forming compound ammonia was not decomposed. In Comparative Example 3, as in Comparative Examples 1 and 2, it was easily estimated that the particle size of the insolubilized material showed a small value, so the particle size of the insolubilized material was not measured.

[Test Example 1]
As waste water, nickel-containing waste water discharged from the electroless nickel process and having a nickel concentration of 1900 mg / L and an ammonia nitrogen (NH ₃ -N) concentration of 820 mg / L was used.
A sodium hypochlorite solution (effective chlorine concentration: 12% by mass) was added as an oxidizing agent from 500 mL to 50 mL of the nickel-containing wastewater.
After adding each amount of sodium hypochlorite solution and stirring for 5 minutes, the free residual chlorine concentration, ammonia nitrogen (NH ₃ -N) concentration, redox potential and pH of the wastewater were measured. These results are shown in Table 2 and FIG.
The oxidation-reduction potential of the wastewater was measured using a portable ORP meter (manufactured by Toa DKK Corporation, “RM-30P”).

As is clear from Table 2 and FIG. 5, ammonia in the wastewater was decomposed as sodium hypochlorite was added.
In addition, when the amount of sodium hypochlorite added was 5 mL to 20 mL, the oxidation-reduction potential remained constant at approximately 630 mV, and during that period, the free residual chlorine concentration also remained at a low concentration of 1.5 mg / L or less. .
However, when the amount of sodium hypochlorite added reached 30 mL, the oxidation-reduction potential rose rapidly to 1113 mV, and the free residual chlorine concentration also increased to 16 mg / L.
From these results, in the case of the wastewater used in Test Example 1, the oxidation-reduction potential of the wastewater is measured in the oxidation treatment step, and the addition of sodium hypochlorite is stopped when the oxidation-reduction potential reaches 650 mV. Thus, the free residual chlorine concentration can be reduced to 30 mg / L or less, and excessive addition of an oxidizing agent (sodium hypochlorite) can be easily suppressed.

According to the wastewater treatment apparatus and treatment method of the present invention, wastewater containing a compound that forms a heavy metal and a metal complex can be treated at a high level without adding a flocculant, and the heavy metal concentration can be sufficiently reduced.
The treated water obtained by the wastewater treatment apparatus and treatment method of the present invention has a very low metal content. Moreover, since a flocculant is not used for wastewater treatment, the outflow of unreacted aggregates is not mixed into the treated water.
Therefore, according to the wastewater treatment system of the present invention, the treated water treated by using the treatment apparatus and the treatment method of the present invention is circulated to the metal surface cleaning process that is a wastewater generation source, thereby affecting the product to be processed. The treated water can be used effectively without giving water.

1, 2, 3, 4 Wastewater treatment apparatus 10 Storage means 20 Oxidation treatment means 23, 33 Water quality meter 30 Insolubilization treatment means 40 Membrane separation means 50 pH adjustment means 60 Sedimentation separation means W ₀ Waste water W ₁ Filtration water W ₂ Membrane separation Concentrated water W ₃ Treated water W ₄ Supernatant W ₅ Precipitated concentrated water

Claims (10)

1. An apparatus for treating wastewater comprising at least a heavy metal and a compound that forms a metal complex by coordination with the heavy metal,
   Wastewater comprising oxidation treatment means for oxidizing the compound forming the metal complex in wastewater, insolubilization treatment means for insolubilizing heavy metals in the oxidized wastewater, and membrane separation means for membrane separation of the insoluble wastewater Processing equipment.
2. The wastewater treatment apparatus according to claim 1, further comprising a sedimentation separation unit that settles and separates heavy metals in the insolubilized wastewater between the insolubilization treatment unit and the membrane separation unit.
3. The wastewater according to claim 1 or 2, wherein the oxidation treatment step comprises means for adding at least one oxidizing agent selected from the group consisting of hypochlorous acid, chlorous acid, perchloric acid, and salts thereof. Processing equipment.
4. The wastewater treatment apparatus according to claim 1 or 2, wherein the oxidation treatment means includes pH adjustment means for adjusting the pH of the wastewater.
5. A method for treating wastewater comprising at least a heavy metal and a compound that forms a metal complex by coordination with the heavy metal,
   Wastewater having an oxidation treatment step for oxidizing the compound forming the metal complex in the wastewater, an insolubilization treatment step for insolubilizing the heavy metal in the wastewater subjected to oxidation treatment, and a membrane separation step for membrane separation of the insoluble wastewater Processing method.
6. The wastewater treatment method according to claim 5, further comprising a sedimentation separation step of separating and separating heavy metals in the insolubilized wastewater between the insolubilization treatment step and the membrane separation step.
7. The wastewater according to claim 5 or 6, wherein the oxidation treatment step is performed by adding at least one oxidizing agent selected from the group consisting of hypochlorous acid, chlorous acid, perchloric acid, and salts thereof. Processing method.
8. The treatment method according to claim 7, wherein in the oxidation treatment step, an oxidizing agent is added after adjusting the pH of the wastewater to 4 or more and 8 or less.
9. The wastewater treatment method according to claim 7 or 8, wherein an end point of addition of the oxidizing agent to the wastewater is detected by a redox potential.
10. A wastewater treatment system, wherein the treated water treated by the treatment apparatus according to any one of claims 1 to 4 is reused in a metal surface cleaning step of plating or metal surface treatment.

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