KR102648323B1 - Pt-Ru-Ti catalyst electrode for ballast water electrolysis - Google Patents

Abstract

The present invention relates to an electrode for electrolysis of ballast water for sterilizing ballast water, comprising at least one selected from metal mesh, metal foam, and metal plate, on which a Pt, Ru, and Ti catalyst layer is located, The catalyst layer is a ternary compound composed of Ru, Ti, and Pt, and the molar ratio of Pt:Ru in the catalyst layer is 2:8 to 8:2, and after mixing Ti, the molar ratio of (Pt:Ru) and Ti is 1:1. to 3:7, and the amount of Pt, Ru, and Ti catalyst loaded on the electrolysis electrode is 0.5 to 5 mg/cm ² .
The electrode for electrolysis of ballast water according to the present invention does not reduce chlorine oxidation efficiency even in competition with water oxidation and shows a selectivity of more than 98% for the generation of active chlorine species. In addition, since the catalyst layer is manufactured by reducing the content of precious metals, there is an advantage in securing the economic efficiency of the catalyst.

Description

Pt-Ru-Ti catalyst electrode for ballast water electrolysis}

The present invention relates to a Pt-Ru-Ti catalyst electrode for ballast water electrolysis and a manufacturing method thereof, and more specifically, to a Pt-Ru-Ti catalyst electrode for ballast water electrolysis comprising platinum, ruthenium and titanium catalyst layers. and its manufacturing method.

In general, ballast water refers to seawater filled inside a ship for safe and efficient operation. When a ship unloads its cargo, it floats on the water equal to the reduced weight, and as the center of gravity rises, the side-to-side shaking increases. Operating in this condition may lead to a rollover accident. Additionally, if a lot of cargo is loaded on only one side of the ship, water can be filled in the ballast tank on the other side to balance the left and right sides. Furthermore, ballast water is also necessary to increase the operating efficiency of ships, because the ship must be submerged to some extent so that the propeller can operate below the water surface and thus can be operated efficiently. Although ballast water is essential for ship operation, it carries the stigma of being the main cause of destruction of marine ecosystems today, and various marine organisms contained in ballast water can migrate to the coasts of other countries and disturb the ecosystem. Due to these problems, it has become mandatory to install a ballast water treatment system on new ships built after 2012 and on all ships currently in operation after 2017, and thus efficient technology for ballast water treatment is required. As general ballast water treatment technology, various treatment methods are proposed, such as electrolysis (straight-line type, side stream type), ultraviolet (UV), ozone, filter method, centrifugation, and heat treatment. The most widely adopted method recently is electrolysis. Among these, the direct electrolysis method disinfects ballast water through direct disinfection using hypochlorous acids (HClO, NaClO), OH radicals, or potential differences generated by electrolyzing seawater. It is a sterilization method. The conventional direct electrolysis method uses an electrolytic process that generates oxygen or chlorine, such as a seawater decomposition process, and uses titanium metal as a substrate. Electrode active materials (oxides of platinum group metals such as iridium (Ir) and ruthenium (Ru)) are applied to the surface of the substrate. It is common to use electrodes manufactured by depositing a catalyst layer. Catalyst layers such as oxides of platinum group metals such as iridium and ruthenium are used to induce high chlorine production and reduction reactions, and these electrodes are commonly called DSA electrodes and are currently used in various chlor-alkali industries as well as ballast water treatment. However, there is a problem of increasing process operation costs due to the high price of raw materials. Therefore, in order to develop a low-cost electrocatalytic electrode to replace these DSA electrodes, research is being conducted on binary and ternary electrodes that combine existing platinum group noble metals such as Ru and Ir with Sn, Sb, and Zr, but chlorine is still generated. There are no satisfactory results in terms of efficiency. Because the reduction potential of the chlorine generation reaction is similar to the water oxidation potential, increasing the selectivity of the chlorine generation reaction is essential for efficient process operation. Therefore, there is a need to solve the problem of reduced chlorine oxidation efficiency as the electrode operates in water, promote the chlorine generation reaction, and secure the economic feasibility of the catalyst by reducing the precious metal content.

Korean Patent Publication No. 10-2013-0130504

In order to solve the above problems, the purpose of the present invention is to provide an electrode for electrolysis of ballast water to sterilize ballast water.

In order to achieve the above object, the present invention,

In the electrode for electrolysis of ballast water for sterilizing ballast water,

It includes one or more selected from metal mesh, metal foam, and metal plate, and a catalyst layer is located on top of them,
The catalyst layer is a ternary compound composed of Ru, Ti, and Pt,

The molar ratio of Pt:Ru in the catalyst layer is 2:8 to 8:2, and after mixing Ti, the molar ratio of (Pt:Ru) and Ti is 1:1 to 3:7,

An electrode for electrolysis of ballast water is provided, wherein the amount of Pt, Ru, and Ti catalyst loaded on the electrode for electrolysis is 0.5 to 5 mg/cm ² .

According to one embodiment of the present invention, the catalyst layer can be produced by firing at 400 to 900 °C.

According to another embodiment of the present invention, the catalyst layer can be produced by spray coating with an airbrush one or more selected from metal mesh, metal foam, and metal plate from which the oxide film has been removed by acid treatment.

According to another embodiment of the present invention, titanium, nickel, gold, copper, nickel alloy, and stainless steel may be used as one or more selected from the metal mesh, metal foam, and metal plate.

According to another embodiment of the present invention, a current density of 10 to 1000 mA/cm ² may be applied to the electrode for electrolysis of ballast water.

The electrode for electrolysis of ballast water according to the present invention does not reduce chlorine oxidation efficiency even in competition with water oxidation and shows a selectivity of more than 98% for the generation of active chlorine species. In addition, since the catalyst layer is manufactured by reducing the content of precious metals, there is an advantage in securing the economic efficiency of the catalyst.

Figure 1 shows an image of a two-electrode system according to an embodiment of the present invention.
Figure 2 shows a circuit model used in an experiment measuring the charge transfer resistance of an electrode according to an embodiment of the present invention.
Figure 3 shows a graph of the concentration and current efficiency of activated chlorine species generated according to an embodiment of the present invention.
Figure 4 shows durability evaluation of an electrode according to an embodiment of the present invention.
Figure 5 shows an SEM image of the electrode surface according to an embodiment of the present invention.
Figure 6 shows an EDS analysis image of an electrode according to an embodiment of the present invention.
Figure 7 shows an XRD analysis image of an electrode according to an embodiment of the present invention.

Hereinafter, the present invention will be described in more detail.

According to one aspect of the present invention, an electrode for electrolysis of ballast water for sterilizing ballast water includes at least one selected from metal mesh, metal foam, and metal plate, and the upper portion thereof includes Pt, Ru, and Ti. A catalyst layer is located, the combined molar ratio of Pt:Ru of the catalyst layer is 1:9 to 9:1, the molar ratio of (Pt:Ru):Ti is 1:1 to 3, Pt loaded on the electrolysis electrode, An electrode for electrolysis of ballast water is provided, wherein the amount of Ru and Ti catalysts is 0.5 to 5 mg/cm ² .

The electrode for ballast water electrolysis of the present invention is manufactured by coating a Pt, Ru, and Ti catalyst layer on metal mesh, metal foam, and/or metal plate, and the detailed electrode manufacturing method is as follows. The metal mesh, metal foam and/or metal plate may be titanium, nickel, gold, copper, nickel alloy, or stainless steel, but titanium and stainless steel are preferred, and titanium is most preferred.

First, the Pt, Ru and Ti metal mixture is dissolved in a citric acid solution and ethylene glycol mixture solution and then fired for 30 minutes to 1 hour and 30 minutes. Next, the obtained catalyst is placed in isopropyl alcohol and ultrasonicated for 1 to 3 hours to form particles, and then treated with strong acids such as hydrochloric acid, sulfuric acid, and nitric acid to remove the oxide film. Next, the Pt, Ru, and Ti catalysts from which the oxide film has been removed are coated on titanium mesh, titanium foam, and/or titanium plate using a spray coating method using an airbrush.

The electrode of the present invention uses a Pt-Ru-Ti electrode as a working electrode, a Saturated Calomel Electrode as a reference electrode, and a counter electrode containing platinum or titanium. Electrolysis can be performed with an electrode system, or with a two-electrode system using a Pt-Ru-Ti electrode as an anode and platinum or titanium as a cathode.

The efficiency of the chlorine oxidation reaction of the electrode manufactured by the above manufacturing method is measured by measuring the production rate of active chlorine species by applying a current density of 10 to 1000 mA/cm ² to the electrode, preferably 60 to 1000 mA/cm ² , more preferably is 80 to 1000 mA/cm ² , more preferably 80 to 800 mA/cm ² , and the efficiency of generating active chlorine species may be affected by the Pt and Ru molar ratio combination, catalyst amount, calcination temperature, and presence or absence of Ti mixing. The molar ratio of Pt and Ru in the Pt-Ru-Ti catalyst layer may be 1:9 to 9:1, and is preferably 2:8 to 8:2. Under firing conditions of 500°C, the efficiency is the best at a molar ratio of 8:2, but it is possible to achieve excellent efficiency with electrodes under other molar ratio conditions through changes in firing temperature. The molar ratio of the electrode is selected considering both efficiency and precious metal content. A catalyst having a molar ratio of Pt and Ru of 0:10 to 1:9 or 9:1 has a low rate of active chlorine species production and cannot function properly as an electrode.

After mixing Ti, the molar ratio of (Pt:Ru):Ti may be 3:7 to 7:3, but preferably the molar ratio of (Pt:Ru):Ti is 1:1 to 3. Increasing the Ti content can reduce the precious metal content, thereby securing the economic feasibility of the electrode and maintaining the function of the electrode stably. Mixing Ti maintains the function of the electrode stably with an active chlorine species generation efficiency of 92 to 100% of the Pt-Ru-Ti electrode regardless of the sintering temperature. Preferably, the molar ratio of (Pt:Ru):Ti is 1: When 1 to 3, it has a selectivity of 98 to 100% for generating active chlorine species.

In addition, after mixing Ti, when the molar ratio of (Pt:Ru):Ti is 1:1 to 3, the charge transfer resistance is It has the lowest and largest electrochemical active area, and the charge transfer resistance (R _ct ) of the electrode of the present invention is 30 to 40, and the electrochemical surface area is 5 to 7 mF/cm ² . At this time, the firing temperature is 450 to 550°C, most preferably 500°C.

The amount of Pt, Ru, and Ti catalyst loaded on the electrode for electrolysis is 0.5 to 5 mg/cm ² , preferably 0.8 to 4 mg/cm ² . When the catalyst amount is less than 0.5 mg/cm ² , the active chlorine species production rate of the electrode is significantly reduced and it cannot function as an electrode for electrolysis of ballast water. When the catalyst amount is more than 5 mg/cm ² , the catalyst amount is adjusted to 0.5 to 5 mg/cm . ² The production rate of active chlorine species does not increase significantly compared to when used, and the cost of electrode manufacturing actually increases.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the attached drawings. Meanwhile, illustrations and detailed descriptions of the configuration and its operations and effects that can be easily seen by those with ordinary knowledge in the relevant technical field will be simplified or omitted and will be explained in detail focusing on parts related to the present invention.

<Example>

Example 1 - Electrode Fabrication

(1) Fabrication of Pt-Ru electrode

Pt and Ru were dissolved in a mixed solution of citric acid aqueous solution and ethylene glycol at a molar ratio of 0:10 to 9:1 and then fired for 1 hour. At this time, the obtained catalyst was placed in isopropyl alcohol and ultrasonicated for 2 hours to form particles, and then spray-coated using an airbrush on a titanium mesh from which the oxide film was removed by acid treatment. At this time, in order to evaluate the durability of the electrodes, some electrodes were separately spray coated and heat treated at 300°C for 6 hours. Then, the coated electrode was dried and fabrication was completed.

(2) Fabrication of Pt-Ru-Ti electrode

The ratio of Pt-Ru-Ti was 0.6:2.4:7 (mol %), and it was dissolved in a mixed solution of citric acid and ethylene glycol and fired for 1 hour. At this time, the obtained catalyst was placed in isopropyl alcohol and ultrasonicated for 2 hours to form particles, and then coated with an airbrush on a titanium mesh from which the oxide film was removed by acid treatment. Then, the coated electrode was dried and fabrication was completed.

Example 2 - Performance analysis of electrodes

To observe chlorine oxidation of the electrode manufactured in Example 1, an electrolysis experiment was conducted using a two-electrode system in 0.137 M and 0.5 M NaCl aqueous solutions and artificial seawater. A Pt-Ru or Pt-Ru-Ti electrode was used as the anode, and platinum or titanium was used as the cathode (see Figure 1). As a performance analysis experiment of the electrode, active chlorine species generation efficiency and potential, electrochemical active area, and charge transfer resistance were measured according to the Pt-Ru combination ratio, calcination temperature, and catalyst amount. The current density applied to the electrode is 80 mA/cm ² , and the performance analysis method is as follows:

(1) Generation of active chlorine species

The experimental device was configured with a two-electrode system, and electrolysis experiments were conducted in 0.137 M, 0.5 M, and 0.941 M NaCl aqueous solutions or artificial seawater. Hach is a method of calculating concentration by extracting a certain amount of sample from the electrolyte over time during an electrolysis experiment and measuring the absorbance of the color generated by the reaction between active chlorine species and DPD reagent (N,N-diethyl-p-phenylenediamine). The amount of active chlorine species generated during the reaction was measured using the method and the Faraday efficiency was calculated. When calculating efficiency, multiply by 2 because 2 electrons are required to produce active chlorine species:

[Equation 1]

Faradaic Efficiency(%)=

Q is the amount of charge (C) flowing during the electrochemical reaction, F is Faraday's constant (96485 C/mol), and n is the number of moles of active chlorine species generated (mol).

(2) Measurement of electrochemically active area of electrode

The activity of the manufactured electrode was confirmed by calculating ECSA (ElectroChemical Surface Area) through cyclic voltamogram (CV). CV was 0.85-0.95 V vs. 0.5 M NaCl. The SCE range was measured from 20 to 100 mV/s.

(3) Measurement of charge transfer resistance of electrode

Resistance during electrochemical reaction was measured using impedance spectroscopy (EIS). Measurements and calculations were made at 10 mV intervals from 0.01 to 50000 Hz (1.1 V vs. SCE) in 0.5 M NaCl. The circuit model used is shown in Figure 2.

Example 3 - Evaluation of durability of electrodes

A voltage measurement experiment was conducted for 500 hours in 0.941 M NaCl by applying a current density of 800 mA/cm ² to the electrode under the condition of Pt:Ru:Ti=0.6:2.4:7.

Example 4 - Evaluation of physical properties of electrode

(1) SEM analysis

For SEM (Scanning Electron Microscope) analysis, images of the electrode surface were taken by applying an accelerating voltage of 5.0 kV using Su-8230 (Hitachi) equipment.

(2) EDS analysis

Element mapping was performed using OXFORD's Ultim Extreme equipment attached to the SEM.

(3) XRD analysis

Observation was made by applying Cu-Kα radiation (40 kV, 30 mA) with a wavelength of 1.5406 Å using EMPYREAN equipment from Panalytical.

<Results and Evaluation>

Active chlorine species production efficiency according to molar ratio of Pt-Ru

0.137 M NaCl 0.5 M NaCl Pt:Ru molar ratio Active chlorine species production efficiency Pt:Ru molar ratio Active chlorine species production efficiency 0:10 32.34% 0:10 54.84% 1:9 39.37% 2:8 47.80% 2:8 67.49% 3:7 49.21% 4:6 54.83% 4:6 71.71% 5:5 59.06% 6:4 64.7% 6:4 80.15% 7:3 54.84% 8:2 71.71% 8:2 90% 9:1 36.56% 9:1 81.55%

Table 1 shows the active chlorine species generation efficiency of electrodes manufactured according to the molar ratio of Pt and Ru at a sintering temperature of 400°C. Referring to Table 1, the ratio of Pt-Ru with the highest production efficiency for active chlorine species was 8:2, and the ratio with the lowest potential when the same current density was applied was 2:8.

Active chlorine species generation efficiency according to calcination temperature

0.137 M NaCl 0.5 M NaCl Pt:Ru
molar ratio firing temperature
(℃) Active chlorine species production efficiency Pt:Ru
molar ratio firing temperature
(℃) Active chlorine species production efficiency 8:2 400 80.15% 8:2 400 90% 500 100% 500 100% 600 80.15% 600 91.4% 2:8 400 46.40% 2:8 400 67.49% 500 67.49% 500 84.37% 600 77.33% 600 95.62% 700 78.74% 700 92.80% 800 91.40% 800 95.62% 900 75.93% 900 90%

Table 2 shows the efficiency and potential of active chlorine species according to calcination temperature. Referring to Table 2, the molar ratio of Pt:Ru was fixed at 8:2 or 2:8 and the production efficiency of active chlorine species was measured in the temperature range of 400 to 900 ℃. When the molar ratio was 8:2, the calcination temperature was 500 ℃. It was confirmed that the production efficiency of active chlorine species was 100% regardless of the molar concentration of the NaCl solution. In addition, when the molar ratio was 2:8, the 0.137 M NaCl aqueous solution showed the highest active chlorine species generation efficiency at 91.40% at a calcination temperature of 800 ℃, and the 0.5 M NaCl aqueous solution showed the highest activity at 600 ℃, 95.62%. It was confirmed that the chlorine species production efficiency was shown.

Active chlorine species generation efficiency according to catalyst amount

Pt:Ru=8:2 Pt:Ru=2:8 electrolyte Catalytic amount
(mg/cm ² ) Active chlorine species production efficiency electrolyte Catalytic amount
(mg/cm ² ) Active chlorine species production efficiency 0.137M
NaCl 3.33 100% 0.137M
NaCl 3.33 91.40% 2.50 100% 2.50 90% 1.67 100% 1.67 70.30% 0.83 100% 0.83 66.09% 0.5M
NaCl 3.33 100% 0.5M
NaCl 3.33 95.62% 0.83 97.02% 0.83 100%

Table 3 shows the production efficiency and potential of active chlorine species according to the amount of catalyst when the molar ratio of Pt-Ru and calcination temperature are fixed. Referring to Table 3, when the molar ratio of Pt-Ru was 8:2, the active chlorine species production efficiency was 100% in 0.137 M NaCl aqueous solution, regardless of the catalyst amount, and 3.33 mg/cm ² in 0.5 M NaCl aqueous solution. It was confirmed that the active chlorine species production efficiency was 100%. In addition, when the molar ratio of Pt-Ru was 2:8, the production efficiency of active chlorine species increased as the amount of catalyst added increased in the 0.137 M NaCl aqueous solution, reaching the highest level of 91.40% at 3.33 mg/cm ² , while the 0.5 M NaCl aqueous solution In fact, it was confirmed that the active chlorine species production efficiency was 100% when the catalyst amount was reduced to 0.83 mg/cm ² .

Observation of electrode performance according to Ti ratio after Ti mixing

0.137 M NaCl 0.5 M NaCl (Pt:Ru):Ti molar ratio Active chlorine species production efficiency (Pt:Ru):Ti molar ratio Active chlorine species production efficiency 1:9 83% 1:9 85.77% 2:8 85.77% 2:8 91.397% 3:7 98.43% 3:7 100%

Table 4 shows electrode performance evaluation according to Ti ratio after Ti mixing. Referring to Table 4, it was confirmed that when the (Pt:Ru):Ti molar ratio was 3:7, the active chlorine species generation efficiency was over 98%, showing the best performance.

Observation of electrode performance after Ti mixing

0.137 M NaCl 0.5 M NaCl Pt:Ru:Ti molar ratio firing temperature
(℃) Active chlorine species production efficiency Pt:Ru:Ti molar ratio firing temperature
(℃) Active chlorine species production efficiency 0.6:2.4:7 400 92.80% 0.6:2.4:7 400 94.21% 500 98.43% 500 100% 600 99.83% 600 100% 700 97.02% 700 94.21% 800 94.21% 800 92.80% 900 98.43% 900 100%

Table 5 shows the performance evaluation of the ternary electrode after mixing Ti. Referring to Table 5, it can be seen that (Pt:Ru):Ti was combined at a molar ratio of 3:7, and the ratio of Pt:Ru combined with Ti was set at 2:8, and the existing Pt:Ru = 2: It was confirmed that superior performance was shown regardless of the firing temperature compared to the electrode manufactured with a molar ratio of 8.

Observation of electrode properties after Ti mixing

Pt:Ru:Ti molar ratio Firing temperature (℃) EIS ECSA R _s R _ct C _dl (mF/cm ² ) 0.6:2.4:7 400 6.358 69.63 0.81 500 6.182 35.71 5.745 600 5.884 95.92 4.385 700 6.450 259.6 0.63 800 4.771 333.2 1.875 900 3.719 427.9 0.685

Table 6 shows the observed characteristics of the three-way electrode after mixing Ti. Referring to Table 6, the lowest charge transfer resistance and the largest electrochemical active area were observed at the firing temperature of 500°C, which showed the best performance in the active chlorine species experiment. This shows that the firing temperature of 500°C is an excellent manufacturing condition. there was.

Observation of electrode performance according to catalyst amount after mixing Ti

0.137 M NaCl 0.5 M NaCl Catalyst amount (mg/cm ² ) Active chlorine species production efficiency Catalytic amount (mg/cm ² ) Active chlorine species production efficiency 3.33 98.43% 3.33 100% 0.83 100% 0.83 100%

Table 7 shows the performance evaluation of the three-way electrode according to the amount of catalyst after mixing Ti. As a result of observing the electrode performance according to the catalyst amount by fixing the molar ratio of Pt:Ru:Ti = 0.6:2.4:7 and the calcination temperature at 500 ℃, it was confirmed that excellent performance was shown regardless of the catalyst amount. Figure 3 shows a graph of the concentration and current efficiency of activated chlorine species produced according to an embodiment of the present invention. Referring to Figure 3, the current efficiency is more than 95%, which means that the Pt-Ru-Ti catalyst shows a selectivity of more than 95% for the generation of active chlorine species.

Efficiency of active chlorine species production in artificial seawater

Pt:Ru = 8:2 (500℃) Pt:Ru = 2:8 (600℃) Pt:Ru:Ti = 0.6:2.4:7 (500℃) Catalytic amount
(mg/cm ² ) Active chlorine species production efficiency Catalytic amount
(mg/cm ² ) Active chlorine species production efficiency Catalytic amount
(mg/cm ² ) Active chlorine species production efficiency 3.33 90.00% 3.33 95.62% 3.33 91.40% 0.83 90.00% 0.83 92.80% 0.83 91.40%

Table 8 shows the production efficiency of active chlorine species in artificial seawater of the manufactured electrode. Referring to Table 8, although the efficiency was slightly reduced compared to the NaCl solution condition of similar concentration due to the influence of various ions contained in artificial seawater, it was confirmed that excellent performance of more than 90% was shown even in artificial seawater.

Durability evaluation of Pt-Ru-Ti electrode

Figure 4 shows durability evaluation of an electrode according to an embodiment of the present invention. Referring to Figure 4, it was observed that the electrode without heat treatment was damaged in 14 hours and the voltage increased significantly, but the heat treatment electrode showed no significant increase in voltage over 500 hours, confirming that it had strong durability. .

In addition, before and after the durability evaluation experiment, an active chlorine species generation experiment was performed by applying a current density of 80 mA/cm ² in a 0.941 M NaCl aqueous solution, and the results were compared to evaluate whether the electrode was damaged during the durability evaluation. Table 9 shows the results of comparing the active chlorine species generation efficiency of the electrode before and after the durability evaluation experiment. After the durability evaluation, it was confirmed that the efficiency of the electrode decreased slightly, but it was confirmed that the efficiency was still maintained at a high level.

0.941 M NaCl Pt-Ru-Ti Active chlorine species production efficiency as-synthesized 97% used 90%

Evaluation of physical properties of Pt-Ru-Ti electrode

Figure 5 shows an SEM image of the electrode surface according to an embodiment of the present invention. Referring to Figure 5, it was confirmed that the Pt-Ru-Ti catalyst was formed in the form of nanoparticles on the titanium substrate. Figure 6 shows an EDS analysis image of an electrode according to an embodiment of the present invention. Referring to FIG. 6, it was found that the Pt-Ru-Ti catalyst on the titanium substrate was evenly distributed throughout the electrode, with each element not being localized. Figure 7 shows an XRD analysis image of an electrode according to an embodiment of the present invention. Referring to Figure 7, the peaks of RuO ₂ , TiO ₂ and Pt appeared, which shows that Ru and Ti exist in the form of oxides and Pt in the form of metals, and also that RuO ₂ , TiO ₂ and metal Pt exist in the form of metals. It can be confirmed that it is composed by mixing.

The foregoing has described, rather broadly, the features and technical advantages of the present invention to enable a better understanding of the claims described below. Those skilled in the art to which the present invention pertains will understand that the present invention can be implemented in other specific forms without changing its technical idea or essential features. Therefore, the embodiments described above should be understood in all respects as illustrative and not restrictive. The scope of the present invention is indicated by the claims described below rather than the detailed description above, and all changes or modified forms derived from the claims and their equivalent concepts should be construed as being included in the scope of the present invention.

Claims (5)

In the electrode for electrolysis of ballast water for sterilizing ballast water,
A catalyst layer is located on top of one or more selected from metal mesh, metal foam, and metal plate,
The catalyst layer is a ternary compound formed of Ru, Ti, and Pt,
The molar ratio of Pt:Ru:Ti is 0.6:2.4:7,
An electrode for electrolysis of ballast water, characterized in that the amount of Pt, Ru and Ti catalyst loaded on the electrode is 0.83 mg/cm ² .
According to clause 1,
An electrode for electrolysis of ballast water, wherein the catalyst layer is formed by sintering Ru, Ti, and Pt at 500°C.
According to clause 1,
An electrode for electrolysis of ballast water, wherein at least one selected from the metal mesh, metal foam, and metal plate is titanium, nickel, gold, copper, nickel alloy, and stainless steel.
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