KR19980087769A - Electrolytic Device and Electrolytic Method - Google Patents

Abstract

The present invention relates to an electrolytic device and an electrolytic method for electrolyzing water. When the electrolyte concentration is lowered, the electrolytic voltage is lowered, so that the electrolyzed water with less odor of chlorine gas can be used for sterilization, cleaning, surface treatment, or promotion of plant growth. It is about the technology of obtaining.

To this end, the present invention is an electrolytic apparatus characterized by having an anode chamber separated by a diaphragm, an anode electrode attached to the diaphragm, and an fluoride cation exchange membrane used for the diaphragm provided on the anode electrode. .

Description

Electrolytic Device and Electrolytic Method

The present invention relates to an electrolytic device and an electrolytic method, and to an electrolytic device and an electrolytic method for producing water that can be used for sterilization, cleaning, surface treatment, or promoting plant growth.

In general, electrolysing saline produces an oxidizing liquid having acidity on the anode electrode side and a reducing solution having alkalinity on the cathode electrode side.

Such an electrolytic device has the structure shown in FIG. In Fig. 6, 21 is an anode chamber, 22 is an anode electrode, 23 is a cathode chamber, 24 is a cathode electrode, and 25 is a separator in which the anode chamber 21 and the cathode chamber 23 are separated. In the conventional electrolytic apparatus having a two-chamber electrolytic cell having an anode chamber 21 and a cathode chamber 23 separated by the diaphragm 25, when the voltage is applied between the anode electrode 22 and the cathode electrode 24, the electrolysis is performed. When the electrolyte concentration such as salt was low, the electrolytic voltage had to be increased. In addition, the lower the electrolytic voltage was forced to increase the saline concentration.

By the way, it is proposed to use the acidic oxidized water obtained by electrolysis of the saline solution on the anode electrode 22 as sterilization (disinfection) water in a hospital, etc. This is caused by the following reaction on the anode electrode side, resulting in chlorine gas (Cl ₂ ), It is thought that this is because it produces chlorine compounds such as hypochlorite ions (ClO ⁻ ) and these active species exert bactericidal action.

_{^{2Cl - - 2e - → Cl 2}} (1)

2Na ⁺ + 2e ⁺ → 2Na (2)

_{^{2Na + + 2H 2 O → 2Na}} + + H 2 + 2OH - (3)

^{_{2H 2 O + 2e - → H}} 2 + 2OH - (4)

In addition, part of the chlorine gas (Cl ₂ ) produced in the formula (1) is dissolved in water to produce chloric acid.

Cl ₂ + H ₂ O → HClO + HCl (5)

Therefore, when the brine concentration is increased, the oxidation reaction of chlorine ions increases, the amount of chlorine gas (Cl ₂ ) is increased, and when the chlorine smell is strong, problems such as corrosion of the device and deterioration of the working environment are generated. . Due to the above problem, high saline concentrations should be avoided. However, lowering the saline concentration means increasing the electrolytic voltage.

Alkaline reduced water obtained on the cathode electrode by electrolysis of saline promotes the growth and enzymatic reaction of organisms. However, when oxidized water is produced as sterilized water, when it is produced as a by-product, the hydrogen ion concentration (pH) is about 12 and the oxidation reduction potential (ORP) is weak according to the reaction formulas (2) to (4). Alkaline reduced water in which a high concentration of sodium chloride (NaCl) is dissolved at -850 mV is obtained. Such alkaline reduced water adversely affects plant growth due to very high hydrogen ion concentration (pH) and high concentration of sodium chloride (NaCl). Therefore, even in the above case, it can be seen that the lower the NaCl concentration.

The problem to be solved by the present invention is to solve the above problems, chlorine which can be used for sterilization, cleaning, surface treatment or plant growth promotion by enabling electrolysis at low electrolytic voltage even when the electrolyte concentration is low. It is an object of the present invention to provide a technique for obtaining an electrolytic water with a low smell.

1 is a schematic diagram of an actual form of a first type of electrolytic apparatus according to the present invention,

2 is a schematic diagram of an actual form of a second type of electrolytic apparatus according to the present invention;

3 is a schematic diagram of an actual form of a third type of electrolytic apparatus according to the present invention;

4 is a schematic diagram of an actual form of a fourth type of electrolytic apparatus according to the present invention;

5 is a schematic diagram of an actual form of a fifth type of electrolytic apparatus according to the present invention;

6 is a schematic diagram of a conventional electrolytic apparatus.

Explanation of symbols for main parts of the drawings

1, 10, 11: diaphragm,

2a, 12a: the anode chamber,

2b, 12b: cathode chamber,

12c: middle room,

1a, 10a: fluorine-based cation exchange membrane,

3a, 13a: anode electrode,

3b, 13b: cathode electrode,

1Ob: anion exchange membrane,

11b anion exchange membrane.

The above object is an electrolytic device having an anode chamber separated by a diaphragm, wherein the anode chamber is provided with an anode electrode in close contact with the diaphragm, and a fluorine-based cation exchange membrane is used for the diaphragm in close contact with the anode electrode. It is solved by an electrolytic device characterized in that.

In addition, an anode chamber, a cathode chamber, and an intermediate chamber are provided between the anode chamber and the cathode chamber, and the anode chamber and the intermediate chamber are separated by a diaphragm, and the anode chamber is in close contact with the diaphragm to A node electrode is provided, and the diaphragm provided in close contact with the anode electrode has a fluorine-based cation exchange membrane.

In addition, the conductivity of the electrolytic apparatus is solved by an electrolytic method, characterized in that the electrolysis by supplying water of 60000 Pa / cm or less. In particular, in the case of using a two-chamber electrolytic cell comprising an anode chamber and a cathode chamber, water having a conductivity of 60000 mW / cm or less is supplied to the cathode chamber, and water containing an oxidizing substance is supplied to the anode chamber by electrolysis. , The cathode chamber is solved by an electrolytic method, characterized in that to produce water containing a reducing substance.

Alternatively, in the case of using a three-chamber electrolytic cell consisting of an anode chamber, a cathode chamber, and an intermediate chamber, water having a conductivity of 60000 mW / cm or less is supplied to the intermediate chamber, and water containing an oxidizing substance is supplied to the anode chamber by electrolysis. In the cathode chamber is solved by an electrolytic method, characterized in that to produce water containing a reducing substance.

In addition, when a fluorine-based cation exchange membrane is provided in close contact with the anode electrode, it is not yet fully understood why the electrolytic water is obtained at a low electrolytic voltage even when the electrolyte concentration is low. ^It is thought that this is because dissociation of ⁺ ) occurs and conductivity increases in the exchange membrane. As a result, electrolysis of water occurs easily at the contact point of the fluorine-based cation exchange membrane and the anode electrode, and it is considered that the anion does not necessarily move to the anode electrode.

In the case where an anion exchange membrane is provided on the side opposite to the anode electrode of the fluorine-based cation exchange membrane, the membrane separated in order to form an anode chamber is particularly used as a diaphragm in which a fluorine-based cation exchange membrane and an anion exchange membrane are stacked. Alternatively, when the fluorine-based cation exchange membrane is installed in close contact with the anode electrode, electrolytic water with a low chlorine odor that can be used for sterilization, cleaning, surface treatment, or promoting plant growth at a lower voltage can be obtained even when the electrolyte concentration is lowered. Can be.

Chloride ions in the electrolytic water obtained in enoic served side (Cl ^-) If you want to increase the anion concentration such as is leaving drilled fine hole (Pin Hole) the cation exchange membrane of a fluorine-containing chloride ions (Cl ^-) anion, such as is not lack Hainaut You will be taken to the room. If a hole is drilled with a predetermined precision according to the required use, an anode electrolyte solution having an anion such as chloride ion (Cl ⁻ ) at a desired concentration can be obtained.

When controlling the cation concentration of sodium ions (Na ⁺ ) and the like in the electrolyzed water obtained from the cathode chamber side, it is particularly preferable to use a cation exchange membrane and an anion exchange membrane together as a separation membrane to form the cathode chamber. In the case where a fluorine-based cation exchange membrane is used on the anode chamber side, it is not necessary even on the cathode chamber side. However, in order to control the cation concentration to lower the electrolytic voltage, it is preferable to provide an anion exchange membrane in close contact with the cathode electrode.

In order to increase the cation concentration of the electrolyzed water obtained from the cathode chamber side, when a pin hole is drilled in the anion exchange membrane, the cation moves to the cathode chamber without being deficient. Depending on the required use, if the hole is drilled with a predetermined precision, a cathode electrolyte having a cation of a desired concentration can be obtained.

In the case of using the device configured as described above, electrolyte concentration such as chloride ion (Cl ⁻ ) is lowered on the electrode surface, and electrolysis of water occurs first. As a result, the species of the electrolytic product contributing to the redox potential (ORP) changes. That is, in the low concentration region of sodium chloride (NaCl), in addition to chlorine oxidation, ozone (O ₃ ), hydrogen peroxide (H ₂ O ₂ ), etc., which are oxidative decomposition species of water, are produced by the following reaction, and the active species is hypochlorite ion. (ClO ^-) by acting with the anion of the oxidation reaction product and the like increase the sterilizing effect.

[Anode reaction]

^{_{2H 2 O - 4e - → 4H}} + + O 2 (6)

^{_{2H 2 O - 2e - → H}} 2 O + 2H + (7)

_{H 2 O + O 2 - 2e} - → O 3 + 2H + (8)

In addition, ozone (O ₃ ), hydrogen peroxide (H ₂ O ₂ ), etc., oxidize bacteria and return to oxygen and water. Therefore, the electrolyzed water of the anode in which the electrolyte is delivered at low concentration is excellent also in the environment.

Also in the reduction reaction, hydrogen gas, hydroxide ions, and the like are generated according to the following equation.

[Cathode reaction]

^{_{2H 2 O + 2e - → H}} 2 + 2OH - (9)

_{^{2H + + 2e - → H 2}} (10)

^{_{H 2 O + e - → OH}} - + H (11)

^{H + + e - → H (} 12)

The electrolytic device according to the present invention is an electrolytic device having an anode chamber separated by a diaphragm, and the anode chamber is provided with an anode electrode in close contact with the membrane, and the membrane installed in close contact with the anode electrode has a fluorine-based cation exchange membrane. It is used. In particular, an electrolytic apparatus having an anode chamber and a cathode chamber, wherein the anode chamber and the cathode chamber are separated by a diaphragm, and the anode chamber is provided in close contact with the diaphragm and an anode electrode is provided. Fluorine-based cation exchange membranes are used for the diaphragm attached to the anode electrode.

In addition, an electrolytic cell having a three-chamber electrolytic cell having an anode chamber and a cathode chamber, an intermediate chamber provided between the anode chamber and the cathode chamber, and wherein the anode chamber and the intermediate chamber, the cathode chamber and the intermediate chamber are separated by a diaphragm, respectively. The device is an anode chamber in which an anode electrode is provided in close contact with the diaphragm, and a fluorine-based cation exchange membrane is used in the diaphragm provided in close contact with the anode electrode. In the above electrolytic apparatus, an anion exchange membrane is provided on the side opposite to the anode electrode of the fluorine-based cation exchange membrane. Moreover, in the electrolytic apparatus provided with a 3-chamber electrolytic cell, the thing in which the cation exchange membrane and the anion exchange membrane overlapped the separator which separated the cathode chamber and the intermediate chamber is used. In addition, a hole is drilled through the fluorine-based cation exchange membrane. In addition, holes are formed in the anion exchange membrane of the diaphragm which separated the cathode chamber and the intermediate chamber.

In the electrolytic method according to the present invention, electrolysis is performed by supplying water having a conductivity of 60000 Pa / cm or less (lower limit value of 0.05 Pa / cm) to the electrolytic apparatus. In particular, in the case of using a two-chamber electrolytic cell consisting of an anode chamber and a cathode chamber, water having a conductivity of 60000 mW / cm or less (lower limit 0.05 mW / cm) is supplied to the cathode chamber and electrolytically supplied to the anode chamber. Water containing an oxidizing substance produces water containing a reducing substance in the cathode chamber. In addition, in the case of using a three-chamber electrolytic cell comprising an anode chamber, a cathode chamber and an intermediate chamber, the anode chamber is supplied with electrolysis of 60000 kW / cm or less (lower limit 0.05 kW / cm) to the intermediate chamber by electrolysis. Water containing oxidizing material in the cathode chamber and water containing reducing material in the cathode chamber.

It will be described below in detail as follows.

1 shows the actual form of the electrolytic apparatus type 1 according to the present invention.

As shown in FIG. 1, the diaphragm 1 which consists of an ion exchange membrane is provided in an electrolytic cell, and the anode chamber 2a and the cathode chamber 2b are comprised. Therefore, there are no intermediate chambers in the two-chamber type like the three-chamber type.

The diaphragm 1 overlaps the fluorine-based cation exchange membrane 1a and the anion exchange membrane 1b. The fluorine-based cation exchange membrane 1a is in contact with the anode chamber 2a. An anode electrode 3a is provided in close contact with the diaphragm (fluorine-based cation exchange membrane 1a) in the anode chamber 2a. 3b is a cathode electrode, and the cathode electrode 3b may be in close contact with the anion exchange membrane 1b, or may be spaced apart from the anion exchange membrane 1b as shown in FIG. In this example, it fell 5 mm from the diaphragm.

Pure water having a conductivity of about 1 kW / cm was flowed into the anode chamber 2a, and 2 l of saline solution in which 200 g / l of salt was dissolved was added to the cathode chamber 2b. When the electrolytic current 9A flowed between the anode electrode 3a and the cathode electrode 3b, the electrolytic voltage was 16V and electrolysis was performed. As a result, the hydrogen ion concentration (pH) of the anode electrolyte flowing out from the drainage port of the anode chamber 2a was 4.1, and the redox potential (ORP) was 1100 mV (vs, silver (Ag) / silver chloride (AgCl)).

The residual chlorine concentration was 2 ppm. In addition, E. coli and P. aeruginosa were collected for the investigation of the antibacterial activity of the anode electrolyte, and the bacterial concentration was 10 ⁷ / cc, and 1cc of the bacterial solution was mixed with 10cc of the anode electrolyte. After that, the mixed solution was smeared on a standard agar medium and cultured at 30 ° C. for 24 hours. In this experiment, it can be determined that the anode electrolyte is excellent for sterilization.

In addition, in the apparatus of FIG. 1, when the anode electrode 3a is 5 mm away from the fluorine-based cation exchange membrane 1a, an electrolytic voltage of 500 V or more is required, and electrolysis at low voltage is impossible.

2 shows the actual form of the electrolytic apparatus type 2 according to the present invention.

This actual form is a three-chamber form with an anode thread, a cathode thread and an intermediate thread. As shown in Fig. 2, diaphragms 10 and 11 made of ion exchange membranes are provided in the electrolytic cell, and are composed of an anode chamber 12a, an intermediate chamber 12c, and a cathode chamber 12b. In the diaphragm 10 which separated the anode chamber 12a and the intermediate chamber 12c, the fluorine-type cation exchange membrane 10a and the anion exchange membrane 10b overlapped. The fluorine-based cation exchange membrane 10a is in contact with the anode chamber 12a.

The diaphragm 11 which separated the cathode chamber 12b and the intermediate chamber 12c is a cation exchange membrane, and the anode chamber 12a is provided with an anode electrode in close contact with the diaphragm 10 (fluorine-based cation exchange membrane 10a). In the cathode chamber 12b, a cathode electrode 13b was provided in close contact with the diaphragm (anion exchange membrane) 11, and a glass bead was filled in the intermediate chamber 12c. Pure water (conductivity of 1.0 kW / cm) of about 1 L / min was supplied to the anode chamber 12a and the cathode chamber 12b, and the saline solution of saturated concentration was supplied to the intermediate chamber 12c.

When the electrolytic current 9A flowed between the anode electrode 13a and the cathode electrode 13b, the electrolytic voltage became 14V and electrolysis was performed. The hydrogen ion concentration (pH) of the anode electrolyte collected from the drainage port of the anode chamber 12a was 4.05, and the redox potential (ORP) was 1090 mV. In addition, the residual chlorine concentration was 2 ppm. In addition, E. coli and P. aeruginosa were collected to check the antimicrobial activity of the anode electrolyte, and the bacterial concentration was 10 ⁷ / cc, and 1cc of the bacterial solution was mixed with 10cc of the electrolyte solution. After that, the mixture was incubated for 24 hours at 30 ℃ in standard agar medium (標準 寒 天 培 地), the number of bacteria was significantly reduced. In this experiment, it can be seen that the anode electrolyte is excellent for sterilization.

In addition, the conductivity of the anode electrolyte obtained by supplying tap water (hydrogen ion concentration (pH) = 7.56, conductivity = 320 mW / cm) instead of pure water and electrolytic current at 9 A was 360 mW / cm and hydrogen ion concentration. (pH) was 5.5 and the redox potential (ORP) was 1020 mV. The chlorine odor was not felt, but the residual chlorine concentration was 2.5 ppm.

In this way, the generation of chlorine gas to the anode electrolyte was almost eliminated in the electrolysis of both pure water and tap water, and the generation of ozone (O ₃ ) was observed. In other words, it was found that active oxygen is generated in the anode electrolyte.

In the apparatus of FIG. 2, 5% lactic acid solution was added to the intermediate chamber 12c, and about 1 liter / min of pure water (conductivity of 1.0 mA / cm) was supplied to the anode chamber 12a and the cathode chamber 12b. When the electrolysis was carried out under the condition of 20 V, an anode electrolyte solution having a hydrogen ion concentration (pH) of 4.89 and a redox potential (ORP) of -450 mV was obtained. When the oxide film of magnetite (Fe ₃ O ₄ ) in the anode electrolyte was immersed in water after 5 minutes of iron, the oxide film on the surface was removed cleanly. That is, it can be seen that the anode electrolyte can also be used for dissolution removal such as an oxide film.

In addition, in the apparatus of FIG. 2 for comparison, the anode electrode 13a was placed 5 mm apart from the fluorine-based cation exchange membrane 10a. In this case, an electrolytic voltage of 500 V or more was required for electrolysis.

In addition, in the apparatus of FIG. 2 for comparison, a cation exchange membrane which is not a fluorine substance is used instead of the fluorine cation exchange membrane 10a, and the amount of pure water (conductivity 1.0 kV / cm) is applied to the anode chamber 12a and the cathode chamber 12b. In addition, when electrolyzed with saturated salt solution in the middle chamber 12c, the electrolytic voltage was required to be 300V or more, and the electrolysis to a low voltage became difficult.

In the comparative apparatus of FIG. 2, a nonwoven fabric made of a fluorine resin was used instead of the fluorine cation exchange membrane 10a, and about 1 liter / min of pure water (conductivity 1.0 kW / cm) was supplied to the anode chamber 12a and the cathode chamber 12b. In addition, electrolysis was performed even at a relatively low voltage when electrolyzing with saturated salt solution of saturated concentration in the intermediate chamber 12c. However, the hydrogen ion concentration (pH) of the electrolyte obtained at this time was 2.7, the redox potential (ORP) was 1160 mV, the conductivity was 950 mW / cm, the residual chlorine concentration was 80 ppm, and the smell of chlorine caused the generation of chlorine gas. It was confirmed.

In the apparatus of FIG. 2, electrolysis was performed with the same specification using what drilled 500 holes (Pin Hole: 0.1 mm) in the fluorine-type cation exchange membrane 10a. In other words, about 1 liter / min of tap water (conductivity of 320 ㎲ / cm) is supplied to the anode chamber 12a and the cathode chamber 12b, and the saturated salt solution of saturated concentration is added to the middle chamber 12c, and the electrolytic current is 9A and the electrolytic voltage is 14.5. Electrolysis was initiated at V, and an anode electrolyte having a hydrogen ion concentration (pH) of 3.1, a redox potential (ORP) of 1130 mV), and a conductivity of 430 Pa / cm was obtained. This anode electrolyte showed antimicrobial activity against E. coli, P. aeruginosa, and B. subtilis, and in particular, had higher antimicrobial activity than that of the above-mentioned actual form. In addition, the residual chlorine concentration of the anode electrolyte was 150 to 200 ppm, and the amount of chlorine gas generated at the time of electrolysis was very small, and ozone (O ₃ ) was more generated. This shows that this oxide directly chloride ion (Cl ^{- -)} on the anode electrode 13a is not a chloride ion is oxidized by the active oxygen generated in the oxidation of water (Cl).

Therefore, the generation of chlorine gas was suppressed by electrolysis despite the increase of the residual chlorine concentration contained in the anode electrolyte by controlling the size and number of holes drilled in the fluorine-based cation exchange membrane 10a. In addition, the anode electrolyte had a high residual chlorine concentration but a low chloride ion (Cl ⁻ ) concentration, and thus did not promote corrosion of materials such as stainless steel (SUS304).

In the apparatus shown in FIG. 2, 500 holes (Pin Holes: 0.1 mm diameter) drilled through the fluorine-based cation exchange membrane 10a were used, and about 1 liter / min of pure water (conductivity of 1.0 kPa) was applied to the anode chamber 12a and the cathode chamber 12b. / cm), and when saturated brine is added to the intermediate chamber 12c for electrolysis, the electrolysis is carried out under the conditions of an electrolytic current of 9A and an electrolytic voltage of 14.5V, and the hydrogen ion concentration (pH) is 2.6, and the redox potential ( ORP) was obtained at an anode electrolyte of 200 ppm at 1160 mV, conductivity of 430 kW / cm, and residual chlorine concentration of 150. The glass substrate for hard disk cleaned with this anode electrolyte and the glass substrate for hard disk cleaned with ordinary pure water were exposed for one week at 80 ° C saturation temperature. After virtue of pure water, the glass substrate for hard disks has a surface of several micrometers and the surface flatness is reduced by moisture in the air, whereas the glass substrate for hard disks cleaned with an anode electrolyte is used. It was found that the surface was not soiled by the moisture in the air and the surface flatness was also excellent.

Figure 3 shows another form of the electrolytic apparatus according to the present invention. This actual embodiment uses the cathodic exchange membrane 11a and the anion exchange membrane 11b to overlap the cathode chamber 12b and the intermediate chamber 12c in the separator 11, as well as the cation exchange membrane 11a. The cathode electrode 13b is provided in close contact with the anion exchange membrane 11b. Since the other configurations are basically the same as those of the actual type of the second type, the same parts are denoted by the same reference numerals and detailed description thereof will be omitted.

Then, pure water (conductivity of 1.0 mW / cm) of about 1 L / min was supplied to the anode chamber 12a and the cathode chamber 12b, and a saturated salt solution was placed in the intermediate chamber 12c, and the anode electrode 13a and the cathode electrode 13b were placed. When 7 A of electrolytic currents flowed, electrolysis voltage became 30V and electrolysis was performed. This electrolyte solution also has the characteristics of the same specifications as in the actual embodiment of the present invention. For example, the cathode electrolyzed water had a conductivity of 250 mA / cm, a hydrogen ion concentration (pH) of 10.5, and a redox potential (ORP) of -810 mV.

In the apparatus shown in Fig. 3, 500 holes (diameter 1 mm) bored through the fluorine-based cation exchange membrane 10a and the anion exchange membrane 11b were used, and tap water (conductivity 320) of about 1 liter / min was applied to the anode chamber 12a and the cathode chamber 12b. Cm / cm), and saturated salt solution was added to the intermediate chamber 12c, and electrolysis was carried out under the condition of an electrolytic current of 9A and an electrolytic voltage of 16.5V. This electrolyte solution also has the characteristics of the same specifications as in the actual embodiment of the present invention. For example, the cathode electrolytic water had a conductivity of 390 kW / cm, a hydrogen ion concentration (pH) of 11.1, and a redox potential (ORP) of -870 mV.

When the fluorine-based cation exchange membrane 10a was removed for comparison, an electrolytic voltage of 100 V or more was required to obtain an electrolytic current 5A, and electrolysis to a low voltage was not possible.

In the apparatus of Fig. 3, the cation exchange resin is filled as a solid electrolyte in the intermediate chamber 12c, and about 0.5 L / min of ultrapure water (resistance of 18 mA) is supplied to the anode chamber 12a and the cathode chamber 12b, and the electrolytic current 5A, Electrolysis was performed under the conditions of an electrolytic voltage of 35V. This electrolyte solution also has the same characteristics as the actual form of the invention. For example, the conductivity was 2 kV / cm, the hydrogen ion concentration (pH) was 9.051, and the redox potential (ORP) was -690 mV.

Figure 4 shows another actual form of the electrolytic apparatus according to the present invention. This actual form removes the anion exchange membrane 10b leaving only the fluorine-based cation exchange membrane 10a in the apparatus of FIG. Since the other configurations are basically the same as those of the second actual form, the same parts will be denoted by the same reference numerals and detailed description thereof will be omitted.

Then, the cation exchange resin was filled with a solid electrolyte in the intermediate chamber 12c, and about 0.5 liter / min of tap water (conductivity of 320 kW / cm) was supplied to the anode chamber 12a and the cathode chamber 12b. When the supply was made and an electrolytic current 5A flowed between the anode electrode 13a and the cathode electrode 13b, the electrolytic voltage was 25V and electrolysis was performed. This electrolyte solution also has the characteristics of the same specifications as in the actual embodiment of the present invention. For example, the anode electrolytic water has a conductivity of 390 kW / cm, a hydrogen ion concentration (pH) of 7.0, and a redox potential (ORP) of 960 mV, and the cathode electrolytic water has a conductivity of 350 kW / cm and a hydrogen ion. The concentration (pH) was 9.65 and the redox potential (ORP) was -620 mV.

Figure 5 shows another practical form of the electrolytic apparatus according to the present invention. This actual form removes the anion exchange membrane 10b, leaving only the fluorine-based cation exchange membrane 10a in the apparatus of FIG. 2, filling the intermediate chamber 12c with the cation exchange resin as a solid electrolyte, and passing the water passed through the intermediate chamber 12c to the anode chamber 12a. It was to supply. Since the other configurations are basically the same as those of the actual type of the second type, the same parts will be denoted by the same reference numerals and detailed description thereof will be omitted. In addition, 4 in FIG. 5 is a three-chamber electrolytic cell, 5 is a softener, 6 is a cathodic seal liquid tank, and 7 is an anode seal liquid tank.

Then, about 0.5 liter / min of tap water (conductivity of 320 kW / cm) was supplied to the cathode chamber 12b, and electrolysis was performed under the condition of an electrolytic current of 5A and an electrolytic voltage of 20V. This electrolyte solution also has the same characteristics as the actual form of the invention. For example, the anode electrolytic water has a conductivity of 430 kW / cm, a hydrogen ion concentration (pH) of 3.55, and a redox potential (ORP) of 1120 mV), and the cathode electrolytic water has a conductivity of 450 kW / cm and hydrogen. The ion concentration (pH) was 10.02 and the redox potential (ORP) was -750 mV.

As described above, even when electrolysis is carried out by lowering the concentration of the electrolyte by the electrolytic apparatus and the electrolytic method according to the present invention, the electrolytic voltage can be lowered to obtain electrolytic water with less chlorine generation. It can be applied in various fields such as agriculture, food, beauty, sterilization field and semiconductor process, cleaning and surface treatment, plant growth promotion and organic method.

Claims (9)

The anode chamber separated by the diaphragm is installed, The anode chamber is provided in close contact with the diaphragm and an anode electrode is provided. And an fluorine-based cation exchange membrane is used for the diaphragm provided in close contact with the anode electrode. An anode chamber, a cathode chamber, an intermediate chamber provided between the anode chamber and the cathode chamber, The anode chamber and the intermediate chamber are separated by a diaphragm, The anode chamber is provided in close contact with the diaphragm and an anode electrode is provided. An electrolytic apparatus, wherein a fluorine-based cation exchange membrane is used for the diaphragm provided in close contact with the anode chamber electrode. The electrolytic apparatus according to claim 1 or 2, wherein an anion exchange membrane is provided on the side opposite to the anode electrode of the fluorine-based cation exchange membrane. The electrolytic apparatus according to claim 2 or 3, wherein a cation exchange membrane and an anion exchange membrane are used together in a septum separating the cathode chamber and the intermediate chamber. The electrolytic apparatus according to claim 1, wherein a hole is formed in the cation exchange membrane. The electrolytic apparatus according to claim 3 or 4, wherein a hole is formed in the anion exchange membrane. The electrolytic method according to claim 1, wherein the electrolytic apparatus is supplied with electrolytic water having a conductivity of 60000 Pa / cm or less. In the case of using the electrolytic apparatus in the form of a two-chamber electrolytic cell composed of an anode chamber and a cathode chamber according to claim 7, water having a conductivity of 60000 mW / cm or less is supplied to the cathode chamber, and an oxidizing substance is supplied to the anode chamber by electrolysis. An electrolytic method characterized by producing water containing a reducing substance in the cathode chamber. In the case of using a three-chamber electrolytic cell type electrolytic apparatus composed of an anode chamber, a cathode chamber and an intermediate chamber, water having a conductivity of 60000 mW / cm or less is supplied to the intermediate chamber, and the oxidative property is supplied to the anode chamber by electrolysis. The water containing a substance produces | generates the water containing a reducing substance in a cathode chamber.