KR101041514B1 - Highly concentrated oxygen water purifier with electrolytic oxygen generator - Google Patents

Abstract

The present invention relates to an apparatus for electrolyzing pure water to produce oxygen gas, finely granulating this oxygen gas and dissolving it in water to produce high concentration oxygen water from 50 ppm to 200 ppm in drinking water.

Description

Highly concentrated oxygen water purifier with electrolytic oxygen generator

The present invention relates to an apparatus for generating high concentration oxygen water, and more particularly, to an oxygen generator for producing oxygen with high efficiency, an oxygen dissolving agent for making oxygen produced in the oxygen generator into a supersaturated concentration state, and a high concentration oxygen having them. It relates to a water purifier.

The present invention relates to Korean Patent Application Nos. 2005-0016642 (Method for Producing Membrane Electrode Assembly Having Porous Electrode Catalyst Layer), 2005-0016639 (Method for Producing Membrane Electrode Assembly) and 2005-0016637 (Method for Producing Membrane Electrode Assembly).

Pressure swing adsorption (PSA), one of the methods of generating oxygen, is a method of separating and purifying a desired gas by changing the pressure of a supplied gas and repeating adsorption and desorption. As a technology related to such a PSA method, Korean Patent Application No. 2003-0048802 (Invention name: Oxygen water maker, Applicant: Park Moon Soo). This technology can separate oxygen from the air, but because oxygen is produced at a low concentration of about 30% purity, it is applied to water purifiers used indoors due to the relative size of the device and the noise of the compressor when raising the air pressure. There are many problems.

Another method for generating oxygen is to generate oxygen by electrolyzing water through an electrochemical method. Electrochemical oxygen generation method has the advantage that there is no noise when operating the oxygen generator. Related technologies include Korean Patent Application No. 2004-0027381 (Invention Name: Oxygen Water Maker, Applicant: Bae Joo Joo), Patent Application No. 2004-0025213 (Invention Name: Oxygen Water Purifier, Applicant: Bae Joo Joo), Patent Application No. 2005-0031092 (name of the invention: oxygen water generator capable of rapid dissolution of oxygen, Applicant: Bae Jin-joo). However, since these technologies use KOH as an electrolyte, there are practical difficulties in applying to water purifiers used as drinking water.

In addition, there are several prior arts related to the structure for dissolving the generated oxygen. For example, Korean Patent Application No. 2003-0001950 (name of the invention: oxygen water production machine, Applicant: O2plus Co., Ltd.), Patent Application No. 2005-0063057 (name of the invention: Oxygen water production apparatus and method, Applicant: Biotel), Patent Application No. 2005-0038073 (Invention name: Oxygen dissolving device and supersaturated oxygen water production device using the same, Applicant: Oxy Life Co., Ltd., Patent Application No. 2005-0038071 (Invention name: Supersaturation) Oxygen water production device, Applicant: Oxy Life Co., Patent Application No. 2005-0038072 (Invention name: Supersaturated oxygen water production device, Applicant: Oxy Life Co., Ltd.), Patent application No. 2005-0031092 (Invention) Name: Oxygen water generator capable of rapid dissolution of oxygen, Applicant: Bae Joo-joo). However, the above technologies have many components for dissolving oxygen, and also use materials harmful to the human body such as nonwoven fabrics and thus are not applicable to actual water purifiers.

Therefore, the present invention has been made to solve the problems of the prior art as described above, electrolysis only pure water to produce oxygen, high current density operation (miniaturization, light weight) is possible at the time of electrolysis, and low energy The purpose is to provide an oxygen generator having a usage amount.

In addition, the present invention has another object to provide an oxygen soluble group that easily saturates the oxygen produced in the oxygen generator in a supersaturated concentration state.

In addition, the present invention has another object to provide a high concentration oxygen water purifier to efficiently produce high concentration oxygen water by providing the oxygen generator and the oxygen dissolving group.

The oxygen generator for purified water of the present invention is capable of receiving and storing water for electrolysis and having water discharge means having a discharge line for discharging the gas generated at the time of electrolysis, and water supplied by being coupled to the water storage means. Electrolysis means includes an electrolysis means in which an emission line for generating oxygen gas and hydrogen gas and discharging the generated gas is formed, and the electrolysis means has an electrolysis cell for generating oxygen gas and hydrogen gas by electrolyzing water. The electrolysis cell is characterized in that it comprises a hydrogen ion exchange membrane and an electrode catalyst layer formed on both sides of the hydrogen ion exchange membrane and having an electrode function and a current supply function respectively having either polarity.

In addition, the oxygen generator for water purification of the present invention is to be installed in the water purification device so as to produce oxygen gas by electrolyzing pure water, supplying oxygen gas to the water purification device to generate high concentration oxygen water, water for electrolysis It is possible to receive and store the water storage means formed with a discharge line for discharging the oxygen gas or hydrogen gas generated during electrolysis, and to combine the water storage means with electrolysis of the supplied water to produce oxygen gas and hydrogen gas And electrolysis means having a discharge line for discharging oxygen gas or hydrogen gas not discharged from the discharge line of the storage means, wherein the electrolysis means includes a hydrogen ion exchange membrane and hydrogen to electrolyze water to generate oxygen gas and hydrogen gas. An electrolysis cell in which electrode catalyst layers each having both sides of the ion exchange membrane are integrally formed, and on one side of the electrode decomposition cell And a second current supply plate coupled to the other side of the electrode decomposition cell and coupled to the other side of the electrode decomposition cell to function as a current supply function having the other polarity. It is done.

In addition, the oxygen dissolving device for purified water according to the present invention, the inlet for introducing the oxygen mixed water mixed with oxygen gas into the water, the decompression unit for reducing the oxygen mixed water passed through the inlet to increase the flow rate, and the decompression unit It characterized in that it comprises an outlet for discharging the oxygen mixture water passed through to return to the original pressure and flow rate.

In addition, the high-concentration oxygen water purifier according to the present invention is to store the purified water through the sedimentation filter, carbon filter, and membrane filter in the purified water storage tank and use the drinking water as a drinking water. Oxygen generator for generating oxygen by electrolysis by receiving water stored in the water, Mixer for mixing oxygen with other water branched from cold water tank to make oxygen mixed water, Circulating pump for flowing oxygen mixed water, and Circulating pump The carbon filter removes ozone contained in the oxygen mixed water supplied therethrough, and the oxygen mixed water is depressurized and the flow rate is increased to flow and then returned to the original pressure and flow rate to make supersaturated oxygen water in which oxygen is supersaturated in water. It characterized in that it comprises an oxygen dissolving discharged to the cold water tank.

The oxygen generator of the present invention electrolyzes only pure water for producing oxygen through an electrolysis cell composed of a metal-film, but has excellent performance and durability.

Oxygen dissolving device of the present invention can easily saturate oxygen to a supersaturated concentration state without a separate power through a structure that rapidly depressurizes and restores the path pressure of oxygen mixed water (water + oxygen gas) moving from the inlet to the outlet. have.

The high-concentration oxygen water purifying device of the present invention includes the oxygen generator and the oxygen dissolving agent, thereby overcoming the difficulties of using an oxygen-rich water purifier due to the limitations of the oxygen generating technology and the dissolving technology, and miniaturization and low cost. Efficient production of high concentration oxygen water is possible.

Figure 1a is a block diagram showing the configuration of the high concentration oxygen water purifier according to an embodiment of the present invention,
Figure 1b is a block diagram showing the configuration of the high concentration oxygen water purifier according to another embodiment of the present invention,
Figure 2a is a principle diagram of the electrolysis cell constituting the oxygen generator shown in Figure 1a,
Figure 2b is another principle diagram of the electrolysis cell shown in Figure 2a,
3 is an exploded view showing the configuration of the oxygen generator shown in Figure 1a,
4 is a coupling diagram of the oxygen generator shown in FIG.
FIG. 5 is a schematic diagram showing a configuration relationship of the oxygen dissolver shown in FIG. 1A;
6 is a schematic view showing another configuration of the oxygen dissolver shown in FIG.
7 is a diagram illustrating the size of the micro-bubbles that are the experimental results of the experiments and comparative examples according to the present invention.

Hereinafter, with reference to the accompanying drawings, a preferred embodiment of the oxygen generator for water purification and the oxygen dissolving device and the high concentration oxygen water purifier having them according to the present invention will be described in detail.

For reference, the structural diagram used in the drawings is for easy understanding, and the relative size or positional relationship of each element is not necessarily accurate.

Figure 1a is a block diagram showing the configuration of the high concentration oxygen water purifier according to an embodiment of the present invention. As shown in Figure 1a, the high concentration oxygen water purifier 10 is introduced into the raw water through the raw water inlet line (S1), the precipitation filter 100, the first carbon filter 200, the membrane filter 300 and the first 2 is purified after passing through the carbon filter 400 and the like, and is stored in the purified water storage tank 500 by the purified water injection line (S2). Water from the purified water storage tank 500 is introduced into the cold water tank 600 via the cold water inflow line S3 according to natural flow (gravity). That is, the water purifier 10 of this embodiment includes the configuration relationship of the above general water purifier.

In this embodiment, the water purifier 10 is supplied with cold water to the mixer M through the cold water line S4 branched from the cold water tank 600, and at the same time, oxygen generated from the electrochemical oxygen generator 700 discharges the line S5. ) Is supplied to the mixer (M), and becomes oxygen mixed water mixed with oxygen and cold water and is sucked into the circulation pump (P) along the oxygen mixed water line (S6). After passing through the circulating pump P, the water passes through a third carbon filter 800 to remove ozone that may be generated during water electrolysis, and then becomes supersaturated oxygen water in which oxygen is supersaturated in water in an oxygen dissolving unit 900. It is supplied to the cold water tank 600 along the line (S7) and circulated repeatedly. At this time, the water required for electrolysis for oxygen generation is supplied to the oxygen generator 700 through another cold water line (S8) branched from the cold water tank (600).

Figure 1b is a block diagram showing the configuration of the high concentration oxygen water purifier according to another embodiment of the present invention. As shown in FIG. 1B, the water purification device 10A of this embodiment omits the third carbon filter 800, which is installed in FIG. 1A for the purpose of removing ozone, and instead is provided in the general water purification line. It is configured similarly to the water purification device 10 of the first embodiment except that the two-carbon filter 400 is used and the oxygen dissolver 900 is inserted into the cold water tank 600. Therefore, like reference numerals refer to like elements and descriptions thereof will be omitted.

Figure 2a is a principle diagram of the electrolysis cell constituting the oxygen generator shown in Figure 1a. As shown in FIG. 2A, the electrolysis cell 721 of this embodiment produces oxygen gas by electrochemically decomposing water, and does not use a poison such as caustic carry (KOH) as an electrolyte, and an anode catalyst layer ( 721a), a hydrogen ion exchange membrane 721b, and a cathode catalyst layer 721c.

As shown in FIG. 2A, water is decomposed into oxygen, electrons, hydrogen ions (H ⁺ ) (protons) in the anode catalyst layer 721a, and the hydrogen ions are hydrated to the cathode electrode layer 721c through the hydrogen ion exchange membrane 721b. The electrons move from the anode catalyst layer 721a to the cathode catalyst layer 721c along the external circuit 721d. The hydrogen ions (H ⁺ ) transferred to the cathode catalyst layer 721c through the hydrogen ion exchange membrane 721b react with electrons (e ⁻ ) moved along the external circuit 721d to form hydrogen gas (H ₂ ). In this case, the electrochemical reactions occurring in the electrode (anode and cathode) catalyst layers 721a and 721c, respectively, are represented by Schemes 1 and 2.

Scheme 1

Scheme 2

The hydrogen ion exchange membrane 721b is a solid polymer electrolyte and has a thickness of 50 to 200 µm. In addition, the hydrogen ion exchange membrane 721b cannot move along the inside of the anions, whereas cations, ie, hydrogen ions, must be movable, and have heat resistance against temperature and durability in an electrochemical redox atmosphere. Should have

Accordingly, the hydrogen ion exchange membrane 721b transfers ions to selectively move cations to a hydrocarbon-based or fluorocarbon-based polymer so as to satisfy such a function and requirement. It is preferable to construct a polymer structure having sulfonic, carboxylic and phosphoric acidic groups. More preferably, the polymer has a film structure having a strong acidity group of ˜SO _{3 in a} hydrocarbon-based or fluorocarbon-based polymer having excellent heat resistance and oxidation resistance. A typical hydrogen ion exchange membrane 721b of this series is "trade name NAFION" of DuPont (EI du Pont de Nemours and Company, Wilmington, Del.).

Electrode catalyst layers 721a and 721c of the electrolysis cell 721 according to this embodiment preferably have a catalyst or a polymer other than the catalyst. Here, the ion exchange resin may have a binder function of the catalyst layer. At this time, the ion exchange resin contained in the catalyst layer may be the same as or different from the ion exchange resin constituting the hydrogen ion exchange membrane 721b. In addition, when thickening a catalyst layer, you may repeat coating until it becomes a predetermined | prescribed film thickness.

The catalysts contained in the electrode catalyst layers 721a and 721c of this embodiment may be the same or different, but a metal catalyst made of a platinum group or a platinum group alloy is preferable. Here, the metal catalyst may be a metal of platinum group (platinum, ruthenium, rhodium, palladium, osmium, iridium), gold, silver, chromium, iron, titanium, manganese, cobalt, nickel, molybdenum, tungsten, aluminum, silicon, zinc, Alloys with one or more metals selected from the group consisting of tin are preferred.

The thicknesses of the electrode catalyst layers 721a and 721c and the hydrogen ion exchange membrane 721b of this embodiment are not limited, respectively, but the hydrogen ion exchange membrane 721b has a short thickness if its thickness is too thin (50 μm or less). If the thickness is 200 µm or more, the resistance increases and the voltage rises rapidly. Therefore, the thickness is preferably 50 µm to 200 µm. As the electrode catalyst layers 721a and 721c become thicker, the electrode catalyst layers 721a and 721c easily diffuse water, hydrogen or oxygen, thereby improving the characteristics of the electrolysis cell 721. However, when the thickness of the electrode catalyst layers 721a and 721c is 20 µm or more, there is a problem of catalyst loss due to the excessive use of the catalyst. When the thickness is thinner than 1 µm, the amount of catalyst present per unit area decreases and the reaction activity decreases. Since it can be, the thickness of a catalyst layer is preferably 1-15 micrometers.

The electrolysis cell 721 of this embodiment should be configured to be suitable for generation of oxygen gas, and according to a method of maintaining a gap between the anode catalyst layer 721a, the hydrogen ion exchange membrane 721b, and the cathode catalyst layer 721c, Zero-gap), finite-gap (Finite Gap), or electrode and polymer integrated (Electrode Membrane Composite (hereinafter referred to as "EMC") can be produced.

The zero gap type has a structure in which the gap between the hydrogen ion exchange membrane 721b and the electrode catalyst layers 721a and 721c is in close contact with zero (0 mm), and the finite distance type is between the hydrogen ion exchange membrane 721b and the electrode catalyst layers 721a and 721c. The interval between the two is a structure having a constant distance, and the EMC type is a structure in which the hydrogen ion exchange membrane 721b and the electrode catalyst layers 721a and 721c are integrated.

By the way, pure water has low conductivity (high resistance), so a large amount of energy must be supplied to obtain a certain amount of oxygen. From this point of view, a zero gap type or an EMC type that can reduce energy consumption is preferable.

In order to fabricate an EMC type electrolysis cell, a method of forming a catalyst layer on a hydrogen ion exchange membrane is not limited to a specific method. Specifically, for example, a method of directly depositing a catalyst on a hydrogen ion exchange membrane and a hydrogen ion of the catalyst layer Thereafter, two sets of half cells formed on the exchange membrane are prepared, and the surfaces of the respective hydrogen ion exchange membranes are faced and pressed.

FIG. 2B is another principle diagram of the electrolysis cell shown in FIG. 2A, illustrating that water is supplied to the cathode catalyst layer 721c of the electrolysis cell 721. As shown in FIG. 2B, the water supplied to the cathode catalyst layer 721c moves to the anode catalyst layer 721a by diffusion (indicated by H ₂ Oa in FIG. 2B). Water transferred to the anode catalyst layer 721a is decomposed into oxygen, electrons, and hydrogen ions by the reaction equation 1, and the hydrogen ions are hydrated to move to the cathode catalyst layer 721c through the hydrogen ion exchange membrane 721b (H in FIG. 2C). Shown as ₂ Oc). That is, part of the water moved to the anode catalyst layer 721a moves back to the cathode catalyst layer 721c. At this time, the amount of water (H ₂ Oa) moving from the cathode catalyst layer 721c to the anode catalyst layer 721a is determined by the concentration gradient related to water in the hydrogen ion exchange membrane 721b, and the anode catalyst layer 721a. ), The amount of water (H ₂ Oc) and hydrogen ions moving from the cathode catalyst layer 721c to the cathode catalyst layer 721c is determined by the current supplied to the electrolysis cell 721. In the case of using the electrolysis cell 721, there is an advantage that there is no moisture in the oxygen discharged.

3 is an exploded view showing the configuration of the oxygen generator shown in Figure 1a, Figure 4 is a coupling diagram of the oxygen generator shown in FIG. As shown in Figures 3 and 4, the oxygen generator 700 of this embodiment is composed of a water storage means 710 for storing water, and an electrolysis means 720 for electrolyzing the water.

The water storage unit 710 may include a water storage unit 711 for storing water, a cover 712 covering an upper portion of the water storage unit 711, and a lower portion of the water storage unit 711. Consists of a connecting portion 713 to connect and integrate with the top of. Here, the cover 712 is formed with a cold water line (S8) for supplying cold water from the cold water tank 600 shown in Figure 1a, and a discharge line (S5) for moving the oxygen gas generated in the oxygen generator 700, respectively. . At this time, it is preferable to have a water level control unit 714 such as a level sensor or a plotter for adjusting the water level of the water storage means 710 at the end of the cold water line (S8).

In addition, the water storage means 710 has a cation exchange resin layer 715 filled with a cation exchange resin in the water storage unit 711. Here, the cation exchange resin layer 715 serves to remove the hardness components (particularly calcium and magnesium components as cations) present in the water supplied through the cold water line S8. If the hardness components are not removed, these components may accumulate in the hydrogen ion exchange membrane 721b of the electrolysis cell 721 in the electrolysis means 720 to shorten the lifespan. In addition, a support layer 716 supporting the cation exchange resin is formed at the bottom of the cation exchange resin layer 715.

The electrolysis means 720 is composed of an electrolysis cell 721 and its related components, the upper module 722, the lower module 723 and the like.

The upper module 722 has a connecting portion 724 for connecting with the connecting portion 713 of the water storage means 710, a fixing pin 725 for connecting and fixing the lower module 723, and the like. Accordingly, holes are formed in the upper and lower modules 722 and 723, the electrolysis cell 721, and related components, through which the fixing pin 725 can be inserted. In addition, the lower module 723 is provided with a discharge line (S9) for discharging the gas generated during electrolysis.

In addition, the electrolysis means 720 includes an electrolysis cell 721 and related components, and includes first and second current supply plates 726 and 727 disposed above and below the electrolysis cell 721, respectively. And a pair of gaskets 728. In this case, connection terminals 729 are formed on the first and second current supply plates 726 and 727 to receive current from an external power source (not shown) through the connection terminals 729.

The electrolysis cell 721 according to this embodiment is manufactured in the EMC type as described above with reference to FIG. 2A, but may be configured as a zero-gap type.

That is, when the electrolysis cell is configured in the EMC type as shown in FIG. 3, the EMC type electrolysis cell 721, the first current supply plate 726 having the polarity on one side, and the polarity on the other side are formed. 2 has a current supply plate 727. Here, the first and second current supply plates 726 and 727 receive current from an external power source from the respective connection terminals 729.

At this time, the movement path of the current (electron flow) is as follows. When a current is applied from the external power source to the connection terminal 729 of the first current supply plate 726 having one side polarity, the first current supply plate 726, the EMC electrolysis cell 721, and the reverse polarity It moves to an external power source via the second current supply plate 727 and the connection terminal 729 of the second current supply plate 727. Here, a gasket 728 is provided outside the first and second current supply plates 726 and 727 to prevent leakage of water and the generated gas. In addition, the first and second current supply plates 726 and 727 preferably have a porous structure to facilitate the inflow and outflow of water and generated gas.

By the way, when the electrolysis cell is configured in a zero-gap type, as shown in FIG. 2A, the hydrogen ion exchange membrane 721b, the electrode having the polarity of the anode, and the anode catalyst layer 721a having the current supply function ( A first current supply plate), an electrode having a polarity of the cathode, and a cathode catalyst layer 721c (second current supply plate) having a current supply function. At this time, the movement path of the current (electron flow) and the structure, material, and assembly method of the first and second current supply plates are the same as those of the aforementioned EMC type electrolysis cell.

Oxygen generator 700 is composed of acrylic resin, acetal resin, PVC (polyvinylchloride) resin, CPVC (chlorinated PVC) resin, PVDF (polyvinylidene difluoride) resin, Teflon (or PTFE, polytetrafluoroethylene) resin, fluoropolymer resin It is possible to molded products made of polymer materials such as acrylonitrile-butadiene-styrene (ABS) resin, and ABS is suitable in consideration of non-toxicity of human body and price.

Cation exchange resins filled in the cation exchange resin layer 715 include strong acid types, weak acid types, and chelating types of polystyrene divinylbenzene crosslinked resins. Preferred cation exchange resins are strong acid types polystyrene divinylbenzene crosslinked exchange resins.

Suitable materials for the current supply plate 726 are titanium, tantalum, or the like, and in order to impart conductivity, platinum is preferably coated by a method such as pyrolysis or electroplating.

Hereinafter, the operation process of the oxygen generator 700 configured as described above is as follows.

1A to 4, when cold water is supplied along the cold water line S8 of the cold water tank 600 to the inside of the oxygen generator 700 of this embodiment, cation exchange water installed in the oxygen generator 700 is provided. The strata 715 removes the hardness present in the cold water. Deionized water from which hardness is removed undergoes an electrochemical reaction in the electrolysis cell 721 in the electrolysis means 720.

As a method of operating the oxygen generator 700, first, the (+) pole of the current supply source is connected to the first current supply plate 726 and the (-) of the current supply source is connected to the second current supply plate 727 on the other side. ), And second, connecting the (-) pole of the current source to the first current supply plate 726 and the (+) pole of the current source to the second current supply plate 727 on the other side. There are two ways to do this.

As in the first method, when the positive pole of the current source is connected to the first current supply plate 726 and the negative pole of the current source is connected to the second current supply plate 727 on the other side, water storage is performed. Oxygen is discharged along the discharge line S5 formed in the cover 712 of the means 710, and hydrogen and water are discharged along the discharge line S9 formed in the lower module 723 of the electrolysis means 720. .

However, as in the second method, when connecting the negative pole of the current source to the first current supply plate 726 and the positive pole of the current source to the second current supply plate 727 on the other side, Hydrogen is discharged along the discharge line S5 formed on the cover 712 of the water storage means 710, and oxygen is discharged along the discharge line S9 formed on the lower module 723 of the electrolysis means 720. .

The operating current density of the electrolysis cell is preferably operated at a DC voltage of 2 to 5 Volt at 0.01 to 2.0 A / cm ² . Current density is 0.01A / cm ² Below, the amount of current supplied per unit area is small and the device becomes large, and the current density is 2.0A / cm ² In the above, the voltage rises to 5 V or more, and the amount of ozone generated in addition to oxygen becomes large, and the suitability of drinking water is inferior. More preferably, the current density is 0.1 to 1.0 A / cm ² and the DC voltage is 2 to 4 Volt.

FIG. 5 is a schematic view showing a configuration relationship of the oxygen dissolver shown in FIG. 1A. The oxygen dissolver 900 shown in FIG. 5 has a structure capable of generating an oxygen water concentration of up to 100 ppm, and includes an inlet 910, a taper 920, and an outlet 930. Here, the tapered portion 920 has a tapered shape so that the diameter thereof becomes smaller toward the discharge portion 930. Therefore, the mixed oxygen and water is introduced into the inlet 910, the pressure is reduced while passing through the tapered portion 920 and the velocity of oxygen is increased, the speed is increased, and then the pressure is passed through the outlet 930 It grows to a state. Since the velocity of sound decreases in the flow of bubbles, the flow velocity of the bubbles mixed is faster than the velocity of sound, so that a shock wave is generated in the discharge portion 930 and the bubbles are refined.

Inlet 910 and outlet 930 is suitable for the pipe diameter (D) of 0.5mm ~ 16mm, 1mm ~ 10mm tube is most preferable when considering the installation space in the water purifier.

The most influential factor in the micro bubble is the ratio (Dt / D) of the diameter D of the inlet 910 and the outlet 930 and the diameter Dt of the taper 920. It is preferable that ratio is 0.01-0.8. When the ratio (Dt / D) of the diameter (D) of the inlet part 910 and the outlet part 930 and the diameter Dt of the taper part 920 is 0.01 or less, the driving power of the pump is increased rapidly. The size of the bubble is increased to 1mm, so the melting capacity is drastically reduced.

In addition, bubble refinement is influenced by the distance L between the tapered portion 920 and the discharge portion 930. The preferred distance L is within 100 mm, and bubbles are coalesced again at 100 mm or more.

In addition, the size and number of bubbles associated with oxygen dissolution are largely determined by the amount of water supplied and the flow rate of oxygen. When the ratio of the water supply unit (ml / min) and the oxygen supply unit ml / min is a void rate (void fraction = oxygen supply (ml / min) / water supply (ml / min) * 100), the void rate It is preferable that it is 0.01-10. Here, when the void ratio is 0.01 or less, bubbles having a large bubble size of 0.35 mm are generated, and the dissolution capacity is drastically reduced.

In addition, the oxygen dissolver may be composed of an inlet, a valve and a discharge. That is, fine bubbles can be formed by using a valve instead of the tapered portion. In the case of using a valve, a pipe having a diameter of 0.5 mm to 16 mm is suitable, and the void ratio is preferably 0.01 to 30. Here, when the void ratio is 0.01 or less, bubbles having a large bubble size of 0.4 mm are generated, so that the dissolution capacity is drastically reduced, and at 30 or more, there is a disadvantage in that the cost and power cost increase due to the increase in the pump capacity. The size of the fine bubbles can be easily adjusted by adjusting the opening and closing rate of the valve.

6 is a schematic view showing another configuration of the oxygen dissolving unit shown in FIG. The oxygen dissolver 900a shown in FIG. 6 is composed of an inlet 910a, an orifice 920a, and an outlet 930a. The principle of making oxygen into micro bubbles is a pressure as shown in FIG. Through the process of decompression and pressurization of the bubble is refined. The inlet 910a and the outlet 930a are suitable for pipes having a diameter D of 0.5 mm to 16 mm, and most preferably 1 mm to 10 mm when considering an installation space in a water purifier.

The ratio Do / D of the diameter D of the inlet part 910a and the outlet part 930a and the diameter Do of the orifice part 920a is preferably 0.01 to 0.8. When the ratio (Do / D) is less than 0.01, the driving power of the pump is increased rapidly. At 0.8 or more, the size of the generated bubbles is increased to 1 mm, and the dissolution capacity is drastically reduced. The size and number of bubbles related to oxygen dissolution are largely determined by the amount of water supplied and the flow rate of oxygen, and the void ratio is preferably 0.01-20. Here, when the void ratio is 20 or more, the cost and power ratio increase as the capacity of the pump increases, and in 0.01 or less, a bubble having a large bubble size of 1 mm is generated and the melting capacity is drastically reduced.

[ Inventive Example  One]

Inventive Example 1 produced and evaluated the EMC type electrolysis cell by manufacturing the half cell 2 tank in which the catalyst layer was formed on the hydrogen-ion exchange membrane, and crimping by facing the surface of each hydrogen-ion exchange membrane side.

end. Configuration and operation of the experimental device

(1) electrolysis cell

(A) EMC production

Pt black was used as the cathode catalyst, and Pt black and IrO ₂ were used as the cathode catalyst. The electrode layer was made by mixing an electrode catalyst, Nafion ionomer (Aldrich, USA), and PTFE binder (Aldrich, USA) in an iso-propyl-alcohol solution. The mixed slurry was uniformly mixed for 30 minutes under ultrasonic conditions, and then poured into a mold of 5 X 5 cm and dried in a forced convective oven at 30 ° C. for 4 hours to form an anode and a cathode electrode catalyst layer.

Nafion 117 (Dupont, USA) was used as the hydrogen ion exchange membrane. The hydrogen ion exchange membrane was boiled in 3 wt.% H ₂ O ₂ solution for 1 hour and immediately boiled in 0.5MH ₂ SO ₄ solution for 1 hour. It was then stored in boiling pure water for 1 hour, and this was repeated twice to completely remove H ₂ SO ₄ .

In order to prepare the EMC, the cathode electrode catalyst layer, the solid polymer electrolyte, and the cathode electrode catalyst layer were hot pressed together at 120 ° C. under a pressure of 100 kgfcm ⁻² for 7 minutes. MEA was measured by swelling in DI water for 24 hours prior to electrochemical measurements.

(B) First and second current supply plates

After platinum plating the porous titanium, the positive pole of the current source is connected to the first current supply plate, and the negative pole of the current source is connected to the second current supply plate.

(2) electrode active area: 7cm ²

(3) Applied current: 3A (current density 0.45A / cm ² )

I. Performance measurement

Measure the flow voltage (CV, Cell Voltage, unit is Voltage) and the flow rate of oxygen according to the amount of current with a flow meter.

All. Experiment result

Table 1 shows the experimental results obtained through the experimental system, and the results of measuring the voltage and oxygen generation according to the current. The experimental results are shown by the data of Inventive Example 1.

[ Inventive Example  2]

Inventive Example 2 is prepared by evaluating the EMC-type electrolysis cell through the method of depositing the catalyst directly on the hydrogen ion exchange membrane.

end. Configuration and operation of the experimental device

(1) electrolysis cell

(A) EMC production

Pt was used as the cathode catalyst and Pt-Ir was used as the cathode catalyst. First, the hydrogen ion exchange membrane was pretreated as in Inventive Example 1.

The pretreated hydrogen ion exchange membrane was placed in a mixed solution of methanol and water containing 5 mM pt (NH ₃ ) ₄ Cl ₂ (tetra-amineplatinum chloride hydrate, 98%) in a volume ratio of 1: 3 for 40 minutes. Allow platinum ions to diffuse and adsorb into the membrane. Then, NaBH ₄ was added to a solution of PH 13 preheated to 50 ° C. to form a 1 mM reducing solution. After removing the platinum solution in the adsorption process, 60 ml of reducing solution was filled instead. After 2 hours of reduction through this process, the hydrogen ion exchange membrane is impregnated with 0.5 M H ₂ SO ₄ for 2 hours and ultrapure water for 1 hour and then stored. After the reduction process, an EMC type electrolysis cell (hereinafter referred to as Pt-M-Pt) having a Pt electrode catalyst layer is manufactured.

Again, Pt-M-Pt masks one side and then coats Ir or Ru on the other side. Methanol containing 5mM IrCl ₄ (Iridium chloride) or 5mM RuCl ₄ (Ruthenium chloride) and water were mixed in a volume ratio of 1: 3, and then the washed membrane was added to the mixed solution for 40 minutes to iridium. It is allowed to diffuse and adsorb into the membrane. Then, NaBH ₄ was added to a solution of PH 13 preheated to 50 ° C. to form a 1 mM reducing solution, followed by removing the platinum solution from the adsorption process, followed by filling with 60 ml of reducing solution. After 2 hours of reduction, the membrane is immersed in 0.5M H ₂ SO ₄ for 2 hours and ultrapure water for 1 hour and then stored.

(B) First and second current supply plates

After platinum plating the porous titanium, the positive pole of the current source is connected to the first current supply plate, and the negative pole of the current source is connected to the second current supply plate on the other side.

(3) electrode active area: 7cm ²

(4) Applied current: 3A (current density 0.45A / cm ² )

I. Performance measurement

Measure the flow voltage (CV, Cell Voltage, unit is Voltage) and the flow rate of oxygen according to the amount of current with a flow meter.

All. Experiment result

Table 1 shows the experimental results obtained through the experimental system, and the results of measuring the voltage and oxygen generation according to the current. The experimental results are shown by the data of invention example 2.

[ Inventive Example  3]

Inventive Example 3 is an experimental example of a zero gap type electrolysis cell.

end. Configuration and operation of the experimental device

(1) Electrolysis cell type: zero-gap

(A) Electrode: An electrode plated with platinum on titanium. The positive electrode of the current source is connected to the first current supply plate, and the negative electrode of the current source is connected to the second current supply plate.

(B) Ion-exchange membrane: US Dupont Nafion 117

(C) Spacing between electrodes: physical zero gap

(2) electrode active area: 7cm ²

(3) Applied current: 3A (current density 0.45A / cm ² )

I. Performance measurement

Measure the flow voltage (CV, Cell Voltage, unit is Voltage) and the flow rate of oxygen according to the amount of current with a flow meter.

All. Experiment result

Table 1 shows the results of measuring the voltage and oxygen generation amount according to the current as the data of the invention example 3.

[ Inventive Example  4]

Inventive Example 4 is the same as the configuration of Inventive Example 2, except that the first current supply plate is connected with the negative pole of the current supply source, and the other second current supply plate is connected with the positive pole of the current supply source to provide the current amount. According to the flow rate of the flow voltage (CV, cell voltage, unit is Voltage) and the generation of oxygen was measured. In Table 1, the results of measuring the voltage and oxygen generation amount according to the current are shown as data of Inventive Example 4.

[ Comparative example  One]

In Comparative Example 1, a finite-gap electrolytic cell was constructed and compared.

end. Configuration and operation of the experimental device

(1) Electrolysis cell type: finite distance type

(A) Electrode: An electrode plated with platinum on titanium. The positive electrode of the current source is connected to the first current supply plate, and the negative electrode of the current source is connected to the other second current supply plate.

(B) Ion-exchange membrane: US Dupont Nafion 117

(C) Spacing between electrodes: 2mm

(2) electrode active area: 7cm ²

(3) Applied current: 3A (current density 0.45A / cm ² )

I. Performance measurement

Measure the flow voltage (CV, Cell Voltage, unit is Voltage) and the flow rate of oxygen according to the amount of current with a flow meter.

All. Experiment result

Table 1 shows the results of measuring the voltage and oxygen generation amount according to the current as the data of Comparative Example 1.

[ Inventive Example  5]

Inventive Example 5 relates to the oxygen dissolving agent of this invention.

end. Configuration and operation of the experimental device

The experimental apparatus constitutes an oxygen dissolver as shown in FIG. 5. DO (dissolved oxygen) meter is installed after the oxygen dissolver. At this time, the main specifications of the oxygen dissolver are as follows.

(1) Inlet diameter: 6 mm (0.25 inch)

(2) Tapered part diameter: 0.5mm

(3) outlet diameter: 6mm (0.25 inch)

(4) Ratio (Dt / D): 0.08

(5) void fraction: 0.2 (oxygen supply amount: 2ml / min, water supply amount: 1000ml / min)

(6) Distance between tapered part and discharge part (L): 50mm

I. Performance measurement

The size of the fine bubbles was measured by installing a camera at the rear end of the oxygen dissolver, and the oxygen solubility was measured using a dissolved oxygen concentration meter.

All. Experiment result

Table 2 shows the size and dissolved oxygen rate (%) of the micro-bubbles measured through the experimental system, and the size of the micro-bubble in FIG. Experimental results are shown in Inventive Example 5.

[ Inventive Example  6]

Inventive Example 6 relates to the oxygen-dissolving agent of this invention.

end. Configuration and operation of the experimental device

The experimental apparatus constitutes an oxygen dissolver in a structure similar to that of FIG. 5. DO (dissolved oxygen) meter is installed after the oxygen dissolver. At this time, the main specifications of the dissolver are as follows.

(1) Inlet and outlet diameters: 6 mm (0.25 inch)

(2) Valve part diameter: 6mm

(3) Ratio (Dt / D): 0.08

(4) void fraction: 0.2 (oxygen supply: 2ml / min, water supply: 1000ml / min)

(5) Distance between valve part and outlet part (L): 50mm

I. Performance measurement

The size and dissolved oxygen of the microbubbles were measured by adjusting the opening and closing rate of the valve. The size of the fine bubbles was measured by installing a camera at the rear end of the dissolver, and the oxygen solubility was measured using a dissolved oxygen concentration meter.

All. Experiment result

Table 2 shows the size and dissolved oxygen rate (%) of the micro-bubbles measured through the experimental system, and the size of the micro-bubble in FIG. Experimental results are shown in Inventive Example 6.

[ Inventive Example  7]

Inventive Example 7 relates to the oxygen dissolving agent of this invention.

end. Configuration and operation of the experimental device

The experimental apparatus constitutes an oxygen dissolver as shown in FIG. 6. DO (dissolved oxygen) meter is installed after the oxygen dissolver. At this time, the main specifications of the dissolver are as follows.

(1) Inlet diameter: 6 mm (0.25 inch)

(2) Orifice part diameter: 0.5mm

(3) Outlet diameter: 6 mm (0.25 inch)

(4) Ratio (Do / D): 0.08

(5) void fraction: 0.2 (oxygen supply amount: 2ml / min, water supply amount: 1000ml / min)

I. Performance measurement

The size of the fine bubbles was measured by installing a camera at the rear end of the oxygen dissolver, and the oxygen solubility was measured using a dissolved oxygen concentration meter.

All. Experiment result

Table 2 shows the size and dissolved oxygen rate (%) of the micro-bubbles measured through the experimental system, and the size of the micro-bubble in FIG. Experimental results are shown as invention example 7.

Comparative Example 2 A straight pipe (straight pipe)

1. Experimental method

end. Configuration and operation of the experimental device

The experimental apparatus constitutes an oxygen dissolver with straight tubes. DO (dissolved oxygen) meter is installed after the oxygen dissolver. At this time, the main specifications of the dissolver are as follows.

(1) Straight pipe diameter: 6mm (0.25inch)

(2) void fraction: 0.2 (oxygen supply: 2ml / min, water supply: 1000ml / min)

I. Performance measurement

The size of the fine bubbles was measured by installing a camera at the rear end of the oxygen dissolver, and the oxygen solubility was measured using a dissolved oxygen concentration meter.

All. Experiment result

Table 2 shows the size and dissolved oxygen rate (%) of the micro-bubbles measured through the experimental system, and the size of the micro-bubble in FIG. Experimental results are shown in Comparative Example 2.

As can be seen from the above experimental results, the oxygen generator of the present invention has electrolytic performance and durability higher than that of the anode, membrane, and cathode, which are general electrolysis cells, which are comparative examples of the electrolysis cell composed of metal-film. It can be seen that excellent. In addition, the oxygen dissolved in the present invention is a structure that passes through a straight hole or a micro hole of the general form through a structure that rapidly reduces the pressure of the path that the fluid flows from the upstream inlet pipe to the lower inlet pipe and recovers again. Compared to easy, it can be possible to refine the bubble without a separate power.

Therefore, the present invention overcomes the problems that it is difficult to use an oxygen-rich water purifier due to the limitations of oxygen generation technology and dissolution technology, and can be miniaturized and efficiently produce high concentration oxygen water at low cost.

In the above description, the technical details of the oxygen generator for water purification and the oxygen dissolving device of the present invention and the high concentration oxygen water purifying apparatus having the same have been described together with the accompanying drawings, which are illustrative of the best embodiments of the present invention. It is not.

In addition, it is obvious that any person skilled in the art can make various modifications and imitations within the scope of the appended claims without departing from the scope of the technical idea of the present invention.

10: oxygen water purification device 100: sedimentation filter
200: first carbon filter 300: membrane filter
400: second carbon filter 500: purified water storage tank
600: cold water tank 700: oxygen generator
800: third carbon filter 900: oxygen dissolver

Claims (10)

delete As an oxygen generator for water purification, which is installed in the water purification device to electrolyze pure water to produce oxygen gas, and to supply the oxygen gas to the water purification device to generate high concentration oxygen water.
It is possible to receive and store water for electrolysis, and water storage means having a discharge line for discharging oxygen gas or hydrogen gas generated during electrolysis, and oxygen gas by electrolyzing water supplied by being coupled to the water storage means. And electrolysis means for generating hydrogen gas and having a discharge line for discharging oxygen gas or hydrogen gas not discharged from the discharge line of the water storage means.
The electrolysis means includes an electrolysis cell in which a hydrogen ion exchange membrane and an electrode catalyst layer respectively formed on both sides of the hydrogen ion exchange membrane are integrally formed to electrolyze water to generate oxygen gas and hydrogen gas, and on one side of the electrode decomposition cell. A first current supply plate coupled to function as a current supply having one polarity, and a second current supply plate coupled to the other side of the electrode decomposition cell to function as a current supply having a polarity of the other; Oxygen generator for water purification, characterized in that. The method according to claim 2,
The hydrogen ion exchange membrane has a thickness of 50 ~ 200㎛ and the oxygen generator for water purification, characterized in that it has a strong acidic group of ~ SO ₃ form in the polymer of a hydrocarbon-based material or a fluorocarbon-based material. The method according to claim 2,
The electrode catalyst layer has a thickness of 1 to 15㎛ oxygen generator for water purification. The method according to claim 2,
The electrode catalyst layer is made of platinum group metals (platinum, ruthenium, rhodium, palladium, osmium, iridium), gold, silver, chromium, iron, titanium, manganese, cobalt, nickel, molybdenum, tungsten, aluminum, silicon, zinc and tin Oxygen generator for water purification, characterized in that consisting of an alloy with one or more metals selected from the group consisting of. The method according to claim 2,
The water storage means is an oxygen generator for water purification, further comprising a cation exchange resin layer for removing the hardness component present in the water to be supplied. The method of claim 6,
The cation exchange resin layer is an oxygen generator for water purification, characterized in that the polystyrene divinylbenzene cross-linked resin of the strong acid type (weak acid type) or chelate type (chelating type) is formed. delete delete In the water purification device using the raw water flowing through the sedimentation filter, carbon filter, membrane filter to store the purified water in the purified water storage tank, the drinking water,
An oxygen generator that flows from the purified water storage tank to receive water stored in the cold water tank and electrolyzes the oxygen to generate oxygen; a mixer for mixing oxygen with other water branched from the cold water tank to form an oxygen mixed water; and the oxygen A circulating pump for flowing the mixed water, a carbon filter for removing ozone contained in the oxygen mixed water supplied through the circulating pump, and depressurizing and increasing the flow rate of the oxygen mixed water, followed by the original pressure and It includes an oxygen dissolving unit to return to the flow rate to make the supersaturated oxygen water supersaturated in the water and discharged to the cold water tank,
The oxygen generator is a high concentration oxygen water purifier, characterized in that configured as described in any one of claims 2 to 6.

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