KR102043423B1 - Composite metal oxide coated, electrically conductivite membrane filters for water treatment and method of fabricating the same - Google Patents

Abstract

Disclosed is an electrically conductive separation membrane for water treatment comprising: a metal filter support in a fiber yarn form; a metal oxide coating layer stacked on the support; and a composite metal oxide catalyst layer coated on nanoparticles. According to the present invention, by performing water treatment using the electrocatalytic separation membrane, decomposition of non-degradable organic matters through an electrochemical reaction and separation of particulate matters through the separation membrane can be performed at the same time. In addition, by applying the water treatment system to advanced treatment of industrial wastewater, excellent treatment efficiency can be obtained. By controlling a sheet form of the electrically conductive separation membrane, membrane fouling does not occur during a batch type continuous operation.

Description

Composite metal oxide coated, electrically conductivite membrane filters for water treatment and method of fabricating the same

The present invention relates to an electroconductive separator for water treatment coated with a composite oxide and a method of manufacturing the same, and more particularly to impregnating metal oxide nanoparticles on a fibrous metal filter support to control the pore size of the filter, and the composite metal oxide. The present invention relates to a water conductive electroconductive separator coated with a composite oxide capable of simultaneously performing sintering coating of a catalyst and performing electrochemical reactivity and filtration.

Traces of pollutants in industrial or sewage treatment water that cannot be removed by existing biological methods can cause a wide range of serious problems as new sources of water and drinking water sources. In fact, the pollution of drinking water sources and river basins related to trace harmful substances is serious both at home and abroad and in developed countries. Water pollution incidents, large and small, have been reported around major drinking water sources and river basins, and due to the development of analytical technology, the seriousness of water pollution caused by the toxic and persistent trace pollutants has emerged.

Incidents caused by hazardous chemicals such as industrial complexes continue, and analysis of pharmaceuticals, hormones, and other trace contaminants in sewage treatment, surface water, and drinking water sources shows that small to several ppb levels It is reported to have been detected. In particular, it is known that trace harmful substances of ppb level exist in sewage effluent.

Trace harmful substances include toxic substances such as 1,4-dioxane, pesticides, endocrine disruptors such as bisphenol A, pharmaceuticals and personal care products such as ibuprofen, antibiotics, and microcystins, which are toxic substances generated by eutrophication. It can be divided into Even trace levels (ppb or below) have characteristics that threaten human health. However, traditional water treatment processes do not effectively remove these trace contaminants, and the ozone oxidation process, which is equipped with a high water purification facility, is limited in treating 1,4-dioxane to an appropriate level. Moreover, the increasing demand for water shortens the cycle of water that is discharged and then reprocessed. Eventually, these factors, while gradual but without exception, result in the increase of various pollutants in the water and the lack of available water resources.

In fact, water pollution accidents caused by trace harmful substances have frequently occurred, which caused social problems and human and ecosystem risks. Therefore, waste water containing harmful substances has a high cost to rely on consignment treatment / disposal. .

However, even with the membrane bioreactor technology, which is attracting attention as the latest advanced wastewater treatment process, there is a limit in removing trace harmful substances, and it is necessary to solve the problem by removing residual trace harmful substances by applying advanced oxidation method.

Accordingly, the present inventors have attempted to effectively remove the hardly decomposable and toxic water pollutants by developing an electroconductive separator for water treatment that can simultaneously achieve membrane filtration and high oxidation while solving these problems.

Korean Patent Publication No. 10-2004-0039431 Korean Patent Publication No. 10-2011-0074178

Accordingly, the first problem to be solved by the present invention is to provide an electroconductive separator for water treatment coated with a composite oxide capable of simultaneously performing electrochemical reactivity and filtration.

The second problem to be solved by the present invention is to provide a method for producing an electroconductive separator for water treatment coated with a composite oxide capable of simultaneously performing electrochemical reactivity and filtration.

A third object of the present invention is to provide a water treatment method using an electroconductive separator coated with a composite oxide.

The present invention to solve the first problem,

Metal filter support in the form of fiber yarns;

A metal oxide coating layer laminated on the support; And

It provides an electroconductive separator for water treatment comprising; a composite metal oxide catalyst layer laminated on the metal oxide coating layer.

The present invention to solve the second problem,

Placing the first metal oxide powder in a solvent to homogenize the slurry;

Dropping the slurry onto a first metal filter, drying the coating layer and evaporating the solvent;

Firing the first metal filter including the first metal oxide to generate a first metal oxide coating layer on the first metal filter;

Adding a second metal hydrate and a first metal oxide powder to deionized water to form a composite metal oxide; And

It provides a method for producing an electroconductive separator for water treatment comprising the step of electrospinning the complex metal oxide solution on the first metal oxide coating layer.

The present invention to solve the third problem,

Metal filter support in the form of fiber yarns;

A metal oxide coating layer laminated on the support; And

It provides a water treatment system using an electroconductive separator for water treatment, including; a composite metal oxide catalyst layer laminated on the metal oxide coating layer.

By proceeding the water treatment using the electroconductive separator according to the present invention can provide a water treatment system capable of simultaneously performing decomposition of the hardly decomposable organic matter through the electrochemical reaction and separation of the particulate matter through the separator. Through such a water treatment system, it is possible to obtain an excellent treatment efficiency by applying to the advanced treatment of industrial wastewater, and to prevent membrane contamination during batch and continuous operation by controlling the sheet type of the electroconductive separator.

1 illustrates a water treatment system using an electroconductive separator according to an embodiment of the present invention.
2 illustrates a method of manufacturing an electroconductive separator according to an embodiment of the present invention.
Figure 3 shows the layer structure (a) and surface photograph (b, c, d) of the electroconductive separator according to an embodiment of the present invention, XRD photograph (e, f) and pore distribution characteristics (g) of the electroconductive separator It is shown.
Figure 4 shows the processing efficiency (a) and membrane permeation pressure change (b) of the single sheet type and double sheet type electroconductive membrane reactor according to one embodiment of the present invention.
FIG. 5 illustrates chromaticity removal rate (a), 1,4-dioxane removal rate (b), and change in membrane permeation pressure (c) of an electroconductive membrane reactor according to current density according to an embodiment of the present invention.
Figure 6 is a (a) chromaticity removal rate, (b) chemical oxygen demand removal, (c) total organic carbon removal rate, (d) 1,4-dioxane according to the continuous operation of the electroconductive membrane reactor according to an embodiment of the present invention The removal rate, (e) turbidity removal rate, and (f) membrane permeation pressure change are shown.
Figure 7 briefly illustrates a process generated in the process of using a water treatment system using an electroconductive separator according to an embodiment of the present invention.

Hereinafter, the present invention will be described in more detail with reference to the accompanying drawings.

The present invention is a fiber filter metal filter support; A metal oxide coating layer laminated on the support; And a composite metal oxide catalyst laminated on the metal oxide coating layer.

The metal oxide of the present invention is a transition metal comprising TiO ₂ , V ₂ O ₅ , MnO ₂ , Fe ₂ O ₃ , Fe ₃ O ₄ , Co ₃ O ₄ , NiO, Cu ₂ O, ZnO, ZrO ₂ , WO ₃ oxide; Alkaline earth metal oxides including MgO; And 3A / 4A group metal oxide including Al ₂ O ₃ and SnO ₂ .

Composite metal oxides include transition metal oxides including Ti, Co, Ru, Ta, Ir, W; And 3A / 4A group metal oxides including Sn, Pb, Sb, and Bi.

In the electroconductive separator for water treatment according to an embodiment of the present invention, the metal filter is a titanium filter, the metal oxide is titanium oxide, and the composite metal oxide is a complex oxide of ruthenium oxide and titanium oxide.

Specifically, the composite metal oxide is preferably xRuO ₂ -yTiO ₂ , where x is 0.6 to 0.9 and y is 0.1 to 0.4. More preferably, the composite metal oxide coated on both surfaces of the TiO ₂ / Ti filter is a 0.8RuO ₂ -0.2TiO ₂ catalyst.

1 illustrates a water treatment system using an electroconductive separator according to an embodiment of the present invention. Referring to FIG. 1, a separator reactor apparatus for forming a single or double sheet-type electroconductive separator, installing in a reactor, and performing water treatment while applying a current is shown.

The electroconductive separator according to the present invention extracts the treated water through the separator by a pressure reducing pump in batch and continuous experiments, circulates the treated water back to the reactor in the case of batch operation, and treats the treated water in the continuous operation. Collect it in a water tank and drain it. Preferably it can be treated at a membrane permeation flow rate of 10 to 100 L / m ² -h.

As the treated water is discharged, inflow water is continuously injected into the reactor using an inflow pump and a water gauge. While operating under constant velocity transmembrane conditions, changes in transmembrane pressure can be measured with a pressure sensor, data can be continuously collected using a data recorder, and the degree of membrane contamination can be evaluated. Preferably the current per reactor volume is applied in the range of 0.1 to 2.0 A / L. The larger the current, the higher the processing efficiency, and the smaller the current, the lower the processing efficiency. Therefore, it is preferable to adjust the operating conditions as appropriate within the numerical range.

In the electroconductive separator reactor of the present invention, an electroconductive separator may be used as an electrode of a positive electrode or a negative electrode. When an electric current is applied to the positive electrode and the negative electrode, a reactive oxidant is generated, and the reactive oxidant can decompose contaminants present in the influent and can remove particulate matter by filtration of the separator.

In an embodiment of the present invention, a composite oxide separator electrode may be used as an anode, and stainless steel may be used as the cathode. The structure of the composite oxide separator anode may be a single sheet module (b of FIG. 1) made of one sheet, or may have a double sheet module (c of FIG. 1) made of two sheets.

According to another embodiment of the present invention, the method comprises the steps of: putting a first metal oxide powder in a solvent to homogenize the slurry; Dropping the slurry onto a first metal filter, drying the coating layer and evaporating the solvent; Firing the first metal filter including the first metal oxide to generate a first metal oxide coating layer on the first metal filter; Adding a second metal hydrate and a first metal oxide powder to deionized water to form a composite metal oxide; And electrospinning the complex metal oxide solution on the first metal oxide coating layer.

According to one embodiment of the invention, the step of homogenizing the slurry into the TiO ₂ powder in an alcohol solution; Dropping the slurry onto a Ti filter, drying the coating layer and evaporating the solvent; And firing the Ti filter containing the TiO ₂ to produce a TiO ₂ / Ti to form a TiO ₂ coating layer on the Ti; Adding ruthenium (III) chloride hydrate and TiO ₂ powder to deionized water to form a composite metal oxide; And electrospinning the complex metal oxide solution on the TiO ₂ / Ti filter.

In the method for preparing an electroconductive separator for water treatment according to the present invention, an oxide and an electrocatalyst may be coated by using a drop casting procedure and an electrospinning procedure.

First, the drop casting process will be described, whereby metal fiber yarns are formed by electrospinning. It is preferable to apply a well dispersed metal oxide nanoparticle solution on the metal fiber yarn support layer thus formed. The metal oxide nanoparticle solution is placed in an alcohol solution to homogenize the slurry, the slurry is applied to the metal filter and dried by evaporating the solvent to form a coating layer.

The content of the metal oxide nanoparticles to be applied can be used by adjusting in the range of 0.01 to 50 mg / cm ² . When the content of the metal oxide nanoparticles applied is less than 0.01 mg / cm ² , the content is too small to be undesirable to form a metal oxide. In addition, when the content of the metal oxide nanoparticles to be applied exceeds 50 mg / cm ^{2 It} is not preferable because the content of the metal oxide nanoparticles is too large to properly achieve a coating.

The metal filter coated with the metal oxide nanoparticles is fired to generate a metal oxide coating layer on the metal filter. After the coating of the metal oxide nanoparticles, the separator may be obtained through sintering and heat treatment at a temperature of 300 to 700 ° C. in order to form a stable coating layer after drying.

The electroconductive separator of the present invention is composed of three layers, by impregnating a metal oxide on a metal fiber yarn support to control the size of the pores, and to prepare a separator by coating a complex oxide catalyst having an electroactivity on top of the metal oxide. . It is preferable that the pore size of the electrospun fiber yarn is 3 to 30 µm. Here, the pore size of the fiber yarn refers to a two-dimensional shape of a space in which a plurality of fiber yarns are formed alternately, not pores on the surface of the fiber yarn. Referring to b of FIG. 3, spaces are generated as the metal fiber yarns are alternately arranged, and each space is formed in various shapes. That is, it is preferable that the space | interval between a fiber yarn and a fiber yarn is 3-30 micrometers. This size may be undesirable for use as a separator for water treatment, but through the impregnation of the metal oxide nanoparticles, the pore size, ie, the spacing between the fiber yarns on which the metal oxide coating layer is laminated, may be reduced to 10 μm or less, more preferably. 3 to 5 μm.

Metal oxides include transition metal oxides including TiO ₂ , V ₂ O ₅ , MnO ₂ , Fe ₂ O ₃ , Fe ₃ O ₄ , Co ₃ O ₄ , NiO, Cu ₂ O, ZnO, ZrO ₂ , WO ₃ ; Alkaline earth metal oxides including MgO; And 3A / 4A group metal oxide including Al ₂ O ₃ and SnO ₂ . Preferably the metal filter is a titanium (Ti) filter and the metal oxide is titanium oxide (TiO ₂ ).

Composite metal oxides include transition metal oxides including Ti, Co, Ru, Ta, Ir, W; And

It may be a mixed metal oxide of two or more selected from the group consisting of; Group 3A / 4A metal oxide including Sn, Pb, Sb, Bi. Preferably the composite metal oxide is a composite oxide of ruthenium oxide and titanium oxide.

In the present invention, the electrically conductive separator is preferably coated with a complex oxide of ruthenium oxide and titanium oxide on both sides of the metal oxide / metal filter (TiO ₂ / Ti filter). Specifically, xRuO ₂ -yTiO ₂ is preferable, where x is 0.6 to 0.9 and y is 0.1 to 0.4. Most preferably the active composite metal oxide coated on both sides of the TiO ₂ / Ti filter is a 0.8RuO ₂ -0.2TiO ₂ catalyst.

In the case of the electroconductive separator of the present invention, it may be a single sheet type or a double sheet type. In the case of the single sheet type, the membrane is continuously blocked, causing membrane fouling and the membrane permeation pressure may increase over time. In the case of the double sheet type, the membrane permeation pressure can be stabilized with little contamination of the separation membrane. This means that the treated water passes through the membrane surface and is collected in the internal void space between the membrane, thereby preventing clogging due to particulate matter or filtration resistance. It is not so big that there is very little fouling. In view of membrane fouling control, it can be said that a double sheet type membrane structure is preferable.

In the case of using the electroconductive separator of the present invention, the removal rate increases as the applied current density increases. This allows large dissolved organics (eg humic materials) with negatively charged functional groups (such as carboxyl groups and phenol groups) to be adsorbed on the anode surface by high current densities. Complexes can be formed with trace organics.

Figure 7 briefly illustrates a process generated in the process of using a water treatment system using an electroconductive separator according to an embodiment of the present invention.

When the current is applied to the electroconductive separator of the present invention, these macromolecules are decomposed by the electrochemical reaction, and the 1,4-dioxane is moved to the liquid phase as the 1,4-dioxane is separated from the electrode surface. Although the concentration of the liquid phase is slightly increased, it may be stabilized again and decomposed slowly over time.

The electroconductive separator according to the present invention exhibits a very stable level regardless of the current density at a membrane permeation pressure of 4 kPa or less, preferably 3 to 4 kPa.

The electroconductive separator according to the present invention has excellent chromaticity removal rate, chemical oxygen demand removal rate, total organic carbon removal rate, 1,4-dioxane removal rate, turbidity removal rate, and overall stable effect by continuous operation. According to the present invention, the electroconductive separator may exhibit an excellent effect that almost no fouling occurs in the case of the positive electrode.

In addition, the chromaticity decreases rapidly at the initial stage of operation, indicating a stable removal rate of 90% or more during continuous operation, and the chemical oxygen demand may exhibit a stable removal rate at about 80%. Total organic carbon can represent about 50% removal.

Example

Hereinafter, the present invention will be described in more detail with reference to Examples. These examples are only for illustrating the present invention in more detail, it will be apparent to those skilled in the art that the scope of the present invention is not limited by these examples in accordance with the gist of the present invention. .

Preparation of Composite Oxide Membranes

2 illustrates a method of manufacturing an electrocatalyst membrane according to an embodiment of the present invention. Referring to Figure 2, an electrocatalyst filter was prepared using drop casting (step 1) and electrospinning coating technique (step 2). The exposed Ti filter (7.5 cm wide, 6.5 cm long, 0.5 mm thick) was washed with a detergent solution, sonicated for 15 minutes and then at 90 ° C. in an alkaline solution (5% NaOH) and an acid solution (10% oxalic acid). After treating for 1 hour, rinsed with distilled water and dried before coating. TiO ₂ particles were loaded into the basic filter using a drop casting method.

First, TiO ₂ powder (480 mg) was added to 5 mL of 2-propanol and sonicated for 30 minutes to homogenize the slurry. A small portion of the slurry was dropped onto the Ti filter (both sides) as evenly as possible using a pipette, and the coating layer was dried at 60 ° C. for 10 minutes to evaporate the solvent. This coating procedure was repeated until all TiO ₂ slurries were used. Finally, the Ti filter containing TiO ₂ was calcined at 550 ° C. for 30 minutes in a muffle furnace to produce a firm TiO ₂ coating layer on the Ti filter (TiO ₂ / Ti).

Electrospin coating method (ESR200, eS-robot®, NanoNC, Korea) was used to deposit the active composite metal oxide catalyst on both sides of the TiO ₂ / Ti filter. 1.449 g of ruthenium (III) chloride hydrate and 0.139 g of TiO ₂ powder were added to 100 mL of deionized water at a molar ratio of 8: 2 to prepare a composite metal oxide (0.8 RuO ₂ -0.2 TiO ₂ ). A total of 4 mL of 2 mL of this solution was mixed into a 10 mL volume syringe and then dispensed at a constant flow rate of 54 μL / min using a syringe pump. A voltage of 17 kV was applied to spray the composite metal oxide solution onto an exposed TiO ₂ / Ti filter placed in a 15 cm collector under the syringe tip. After the electrospinning process, the filter specimen was calcined at 550 ° C. for 10 hours in air to prepare a composite oxide separator.

Evaluation and Results

Figure 3 shows the layer structure and surface and pore distribution characteristics of the electrocatalyst membrane according to an embodiment of the present invention. Referring to FIG. 3, the separator is composed of three layers, and the metal oxide (TiO ₂ ) is impregnated on a metal (Ti) fiber support to adjust the size of pores, and the composite oxide having electrical activity on the top thereof. The catalyst is coated.

(B) a metal (Ti) of a fiber yarn surface pictures, Fig. 3 (c) is that the surface of photo-impregnated metal oxide (TiO ₂₎ on the four metal fibers, (d) of Fig. 3 in FIG. 3 at the top The surface photograph of the composite metal oxide catalyst is illustrated. 3 (g) shows the pore size of the electroconductive separator. 3 (e) and 3 (f) show XRD analysis photographs of the electroconductive separator, and it can be seen that RuO ₂ is coated on the surface of the finally formed separator.

Referring to (g) of FIG. 3, the metal fiber yarn may have a pore size of 3-30 μm, which may not be suitable for use as a separator for water treatment, but the pore size may be 10 μm or less (average porosity) through metal oxide impregnation. 4 μm), and it was confirmed that it was suitable as an electroconductive separator for water treatment.

Figure 4 shows the treatment efficiency (a) and the membrane permeation pressure change (b) of the single sheet type and double sheet type electrochemical membrane reactors according to one embodiment of the present invention.

Referring to the treatment efficiency (a) of the electrochemical membrane reactor of FIG. 4, color removal was hardly achieved when electricity was not applied, but both single and double sheet separators showed very effective color removal rates when electricity was applied. It was. In particular, the double sheet exhibited a higher removal efficiency than the single sheet, which may be due to the increased surface area with relative electroactivity due to the use of the double sheet.

Referring to the membrane permeation characteristic (b) of Figure 4, in the case of a single sheet-type membrane can be seen that the membrane is continuously blocked membrane fouling and the membrane permeation pressure increases linearly with time. On the other hand, in the case of the double sheet type, the contamination of the separator hardly occurred and showed a stable membrane penetration pressure. It can be seen that membrane contamination hardly occurs even when electricity is not applied.

Membrane contamination is more likely to occur in the single sheet type than in the double sheet type. If particulate matter enters the inside of the filter, membrane fouling is accelerated as the treated water accumulates on the side of the 0.5 mm thick membrane filter. In the case of permeation at the end of the filter, it has a long catchment length, thereby increasing resistance due to filtration.

On the other hand, in the case of the double sheet type, the treated water passes through the membrane surface and is collected in the internal empty space between the membrane and the membrane, so that no membrane fouling phenomenon is observed because of no clogging due to particulate matter or filtration resistance. In terms of membrane fouling control, it can be seen that the double sheet type membrane structure is excellent.

5 shows chromaticity removal (a), 1,4-dioxane removal (b) and change in membrane permeation pressure (c) according to current density in accordance with one embodiment of the present invention. Referring to FIG. 5, in the case of chromaticity, the current was hardly removed when current was not applied. However, even when only 0.3 A / L was applied, the chromaticity was rapidly removed.

On the other hand, in the case of 1,4-dioxane (b), the removal rate tends to be largely dependent on the current density. That is, the removal rate tended to increase as the current density increased. On the other hand, when 1.0 A / L was applied, the current density was rapidly removed and tended to increase somewhat. This means that large dissolved organic materials (eg humic materials) with negatively charged functional groups (eg carboxyl, phenolic groups) in the waste water can be adsorbed on the anode surface by high current densities, which are also traces of 1,4-dioxane. Complexes with organics can be formed.

When the current is applied, these macromolecules are decomposed by the electrochemical reaction and fall off the electrode surface, and the liquid phase concentration of 1,4-dioxane in the initial stage of the reaction is slightly increased due to the movement of 1,4-dioxane into the liquid phase. It is assumed to show a phenomenon. However, as time passed, it was stabilized again and gradually degraded. Batch experiments showed greater than 90% 1,4-dioxane removal.

On the other hand, the membrane permeation pressure (c) was maintained at a very stable level regardless of the current density at 4 kPa or less. That is, it can be seen that the clogging phenomenon of the membrane filter hardly occurs when the double sheet type membrane structure is provided.

Figure 6 shows the efficiency according to the continuous operation of the electrochemical membrane reactor according to one embodiment of the present invention. Specifically, (a) chromaticity removal rate, (b) chemical oxygen demand removal rate, (c) total organic carbon removal rate, (d) 1,4-dioxane removal rate, (e) turbidity removal rate, and (f) membrane permeation pressure change are shown. do.

Referring to FIG. 6, chromaticity (a) rapidly decreased at the beginning of operation, indicating stable removal rate of 90% or more during continuous operation, and chemical oxygen demand (b) showed stable removal rate at about 80% level.

On the other hand, total organic carbon (c) showed a removal rate of about 50%. This tendency shows that things like chromatic reactive groups are removed very easily by electrochemical reactions, and oxidation of hardly decomposable organic matter occurs to some extent, but about 50% is completely mineralized to CO ₂ . Increasing the amount of current applied from 1.1 A / L to 1.59 A / L showed no significant change in removal rate. On the other hand, in the case of 1,4-dioxane (d) having high hardly decomposability, it showed a tendency to be gradually removed over time. It can be seen that up to about 70% is removed at 1.1 A / L, and when the current is increased from 1.1 A / L to 1.59 A / L, it is further removed up to 95%.

However, all of the 1,4-dioxanes decomposed in this way are not mineralized and present as intermediate by-products. Thus, TOC removal rate (e) is not significantly increased. Turbidity, which indicates the removal rate of particulate matter, was removed very high by more than 90% at the beginning of the reaction, similar to chromaticity, and showed a stable level during continuous operation. That is, it can be seen that the particulate matter in the wastewater is effectively removed by the electroconductive separator.

On the other hand, the membrane permeability (f) was maintained at the 3-5 kPa level. The slight increase in the operating time of 54 h seems to be the effect of some organic or particulate matter attached by electrical attraction as the current density increases during the operation, and the level is very small at 1 kPa, The permeation pressure decreased again and remained stable. Overall, the membrane anode of the double sheet structure exhibited an excellent effect that little fouling of the membrane occurred.

So far I looked at the center of the preferred embodiment for the present invention. Those skilled in the art will appreciate that the present invention can be implemented in a modified form without departing from the essential features of the present invention. Therefore, the disclosed embodiments should be considered in descriptive sense only and not for purposes of limitation. The scope of the present invention is shown in the claims rather than the foregoing description, and all differences within the scope will be construed as being included in the present invention.

Claims (14)

A metal filter support in the form of a fiber yarn having a spacing between 3 and 30 μm between metal fiber yarns;
A metal oxide coating layer laminated on the support; And
It includes; a composite metal oxide catalyst laminated on the metal oxide coating layer,
The spacing between the fiber yarn laminated the metal oxide coating layer is 3 ~ 10 μm,
Electroconductive separator for water treatment used as anode.
The method of claim 1,
The metal oxide may be a transition metal oxide including TiO ₂ , V ₂ O ₅ , MnO ₂ , Fe ₂ O ₃ , Fe ₃ O ₄ , Co ₃ O ₄ , NiO, Cu ₂ O, ZnO, ZrO ₂ , WO ₃ ;
Alkaline earth metal oxides including MgO; And
An electroconductive separator for water treatment, characterized in that any one selected from the group consisting of Al ₂ O ₃ , Group 3A / 4A metal oxide containing SnO ₂ .
The method of claim 1,
The composite metal oxide is
Transition metal oxides including Ti, Co, Ru, Ta, Ir, W; And
An electroconductive separator for water treatment, characterized in that at least two mixed metal oxides selected from the group consisting of Group 3A / 4A metal oxides including Sn, Pb, Sb, and Bi.
The method of claim 3,
An electroconductive separator for water treatment, wherein the composite metal oxide is xRuO ₂ -yTiO ₂ .
Here, x is 0.6 to 0.9 and y is 0.1 to 0.4.
The method of claim 1,
Electrolytic separator for water treatment, characterized in that the separator is a single sheet or a double layer sheet.
The method of claim 1,
The metal filter is a titanium filter, the metal oxide is titanium oxide,
The composite metal oxide is an electroconductive separator for water treatment, characterized in that the composite oxide of ruthenium oxide and titanium oxide.
The method of claim 4, wherein
The separator is an electroconductive separator for water treatment, characterized in that the active composite metal oxide coated on both sides of the TiO ₂ / Ti filter is 0.8RuO ₂ -0.2TiO ₂ catalyst.
Placing the first metal oxide powder in a solvent to homogenize the slurry;
Dropping the slurry onto a first metal filter having a spacing between 3 and 30 μm between metal fiber yarns, drying the coating layer and evaporating the solvent;
Firing the first metal filter including the first metal oxide to generate a first metal oxide coating layer on the first metal filter to adjust the spacing between the fiber yarns on which the metal oxide coating layer is laminated to 3 to 10 μm;
Adding a second metal hydrate and a first metal oxide powder to deionized water to form a composite metal oxide; And
Comprising; electrospinning a complex metal oxide solution on the first metal oxide coating layer;
Method for producing a conductive membrane for water treatment used as a positive electrode.
delete The method of claim 8,
The metal oxide may be a transition metal oxide including TiO ₂ , V ₂ O ₅ , MnO ₂ , Fe ₂ O ₃ , Fe ₃ O ₄ , Co ₃ O ₄ , NiO, Cu ₂ O, ZnO, ZrO ₂ , WO ₃ ;
Alkaline earth metal oxides including MgO; And
Method for producing an electroconductive separator for water treatment, characterized in that any one selected from the group consisting of; Al ₂ O ₃ , Group 3A / 4A metal oxide containing SnO ₂ .
The method of claim 8,
The composite metal oxide is
Transition metal oxides including Ti, Co, Ru, Ta, Ir, W; And
Method for producing an electroconductive separator for water treatment, characterized in that at least two mixed metal oxide selected from the group consisting of; 3A / 4A group metal oxide containing Sn, Pb, Sb, Bi.
The method of claim 8,
Wherein the first metal filter is a titanium filter, the metal oxide is titanium oxide, and the composite metal oxide is a complex oxide of ruthenium oxide and titanium oxide.
The method of claim 8,
The separator is a method for producing an electroconductive separator for water treatment, characterized in that the composite metal oxide coated on both sides of the TiO ₂ / Ti filter is 0.8RuO ₂ -0.2TiO ₂ catalyst.
A metal filter support in the form of a fiber yarn having a spacing between 3 and 30 μm between metal fiber yarns;
A metal oxide coating layer laminated on the support; And
It includes; a composite metal oxide catalyst laminated on the metal oxide coating layer,
The spacing between the fiber yarn laminated the metal oxide coating layer is 3 ~ 10μm,
Water treatment system using electroconductive separator used for water treatment.

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