WO2004048643A1 - 複極式ゼロギャップ電解セル - Google Patents
複極式ゼロギャップ電解セル Download PDFInfo
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- WO2004048643A1 WO2004048643A1 PCT/JP2003/015101 JP0315101W WO2004048643A1 WO 2004048643 A1 WO2004048643 A1 WO 2004048643A1 JP 0315101 W JP0315101 W JP 0315101W WO 2004048643 A1 WO2004048643 A1 WO 2004048643A1
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- electrolytic cell
- electrolysis
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
- C25B11/03—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form perforated or foraminous
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
- C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/052—Electrodes comprising one or more electrocatalytic coatings on a substrate
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
- C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/70—Assemblies comprising two or more cells
- C25B9/73—Assemblies comprising two or more cells of the filter-press type
- C25B9/77—Assemblies comprising two or more cells of the filter-press type having diaphragms
Definitions
- the present invention relates to a bipolar zero-gap electrolytic cell.
- the cathode chamber has a light-conductive cushion mat layer, and at least two layers in which a hydrogen-generating cathode is superimposed on the cushion mat layer above and in contact with the cation exchange membrane.
- the base material constituting the anode is a titanium expanded metal or a titanium wire mesh having an opening ratio of 25% or more and 70% or less, and the anode after coating the base material with a catalyst is used.
- the maximum difference between surface irregularities is 5 ⁇ ! 550 ⁇ m and a thickness of 0.7 mm mm2.0 mm.
- Some of these patents have an expansive pressure plate / cathode fine mesh screen.
- the strength of the mat, the strength of the mat, the shape of the anode, the concentration distribution of the electrolyte, the pressure fluctuations inside the cell, etc. are not suitable for the electrolysis cell. There are problems such as a voltage rise and breakage of the ion exchange membrane.
- JP-B 5-34434 JP-A-2000-178781, JP-A-2000-178782, JP-A-2001-64792, JP-A-2001-152380, JP-A-2001-262387
- an elastic mat is shown, and its strength, the strength of the cathode, and prevention of crushing of the mat are also disclosed.
- JP-A-10-53887 discloses an electrolytic cell using a spring.
- the local pressure was high, which could damage the membrane in contact.
- Examples of the electrolytic cell that can adopt the zero gap structure include JP-A-51-43377, JP-A-62-96688, and JP-T-61-500669 (corresponding to WO 85/2419).
- unit electrolysis cells do not have a gas-liquid separation chamber integrated with the unit electrolysis cell, and the liquid and gas are extracted to the upper part in a gas-liquid mixed phase, so vibration occurs in the unit electrolysis cell and ion exchange is performed.
- There were drawbacks such as damage to the membrane.
- JP-A-61-19789 and JP-A-63-11686 it is devised to extract gas and electrolyte downward without extracting gas and electrolyte from the upper part, but the liquid and gas are discharged in a mixed phase. As a result, it was not possible to prevent the occurrence of vibration in the unit electrolytic cell.
- a conductive dispersion or a current distribution member that can circulate the electrolyte internally is provided, but disadvantages such as the structure inside the electrolytic cell becoming complicated are provided. is there.
- Japanese Utility Model Application Laid-Open No. 59-153376 proposes a wave canceller as a measure to prevent vibrations generated in the electrolytic cell.
- this method alone does not yet provide a sufficient wave canceling effect. Vibration due to pressure fluctuation in the cell cannot be completely prevented.
- Japanese Patent Application Laid-Open Nos. 4-2818984 and 8-100286 in order to make the electrolyte in the cell uniform, a cylindrical duct capable of internally circulating the electrolyte is used.
- the gas-liquid separation chamber has a sufficiently large size to a certain extent, and a force of 5 kAZm or more that is designed to prevent vibration by devising it in a state where it is separated downward or horizontally in a gas-liquid separation state Oscillation may still occur at high current densities.
- An object of the present invention is to provide a double-electrode type open-cell gap electrolysis cell and an electrolysis method that enable stable electrolysis with a simple and reliable structure under a high current density. More specifically, an object of the present invention is to provide a zero gap structure in which an ion exchange membrane is hardly damaged when electrolysis is performed at a high current density of 4 kAZm 2 or more using a zero gap type ion exchange membrane electrolytic cell.
- the present invention provides a bipolar zero-gap electrolysis cell having an anolyte solution and a catholyte solution having a concentration distribution within a certain range, and capable of performing stable electrolysis with little fluctuation in cell internal pressure for a long period of time and an electrolysis method thereof. That is.
- Another object of the present invention in addition to the above objects, is to provide a bipolar zero-gap electrolytic cell which enables stable electrolysis for a long period of time by preventing damage to an ion exchange membrane due to gas vibration in the electrolytic cell.
- the present invention provides a bipolar zero gap electrolytic cell for electrolyzing an aqueous alkali chloride solution using a cation exchange membrane. That is, a bipolar zero-gap electrolytic cell for use in a filter-press type electrolytic cell having a plurality of bipolar electrolytic cells and a plurality of cation exchange membranes each disposed between adjacent bipolar electrolytic cells. It is.
- the electrolytic cell is formed of an anode chamber and an anode provided in the anode chamber, the anode base including titanium eta spanned metal or titanium wire mesh having an aperture ratio of 25% to 75%.
- the anode After application of the catalyst to the substrate, the anode has a maximum height difference of 5 ⁇ to 50 ⁇ on the anode surface and a thickness of 0.7 mm to 2.0 mm, and an anode chamber.
- the cathode compartment has at least two stacked layers in the cathode compartment, These layers include a conductive I "raw cushion mat layer and a layer of a cathode for hydrogen generation, and the cathode layer for hydrogen generation is adjacent to the cushion matte layer and is formed on the cation exchange membrane. And a cathode disposed in a contact area.
- the above configuration maintains an appropriate zero gap between the anode, the ion exchange membrane, and the cathode, and allows the generation of gas to pass, reducing damage to the ion exchange membrane and fluctuations in the internal pressure of the cell. To be able to do so.
- the anode substrate contains titanium-made expanded metal, and that the metal is formed from a titanium plate by eta-spanding and then rolling.
- the thickness of the expanded metal is preferably set to 95% to 105% of the sheet thickness before the expansive processing by rolling after the expansive processing.
- the cathode for hydrogen generation is a base material selected from nickel wire mesh, nickel expanded metal and nickel perforated perforated plate with a thickness of 0.05 mm to 0.5 mm.
- the hydrogen generating cathode preferably has an electrolysis catalyst coating layer having a thickness of 50 m or less formed on the hydrogen generating cathode. According to such a structure, there is an appropriate softness, and a small number of electrodes that damage the ion exchange membrane can be easily and inexpensively manufactured.
- the electrolysis cell may further include a gas-liquid separation chamber formed integrally with a non-conducting portion above the anode and cathode chambers.
- a gas-liquid separation chamber formed integrally with a non-conducting portion above the anode and cathode chambers.
- at least one of the cylindrical duct and the baffle plate serving as the internal circulation flow path for the electrolytic solution is provided between the anode and the electrode associated with at least one partition of the cathode chamber. Is preferred.
- a partition plate is formed in the gas-liquid separation chamber.
- the installation of the gas-liquid separation chamber prevents gas vibration by extracting the generated gas from the upper part of the electrode chamber and enables more stable electrolysis. .
- FIG. 1 is a side view showing an example of a cathode that can be used in the bipolar zero-gap electrolytic cell of the present invention.
- FIG. 2 is a perspective view showing an L-shaped portion of an example of a conductive plate usable in the present invention.
- FIG. 3 is a plan view showing an example of an anode which can be used in the bipolar electrode gap electrolysis cell of the present invention and a sampling position of an electrolyte concentration.
- FIG. 4 is a side sectional view showing an example of an anode chamber that can be used in the bipolar electrode type gap electrolysis cell of the present invention.
- FIG. 5 is a side sectional view showing an anode-side gas-liquid separation chamber that can be used in the bipolar zero-gap electrolytic cell of the present invention.
- FIG. 6 is a sectional view of a bipolar zero-gap electrolytic cell according to an embodiment of the present invention.
- FIG. 7 is a partially cutaway assembly diagram showing an application example of an electrolytic cell using the cell of the present invention.
- the cathode gasket 27 and the anode chamber gasket 29 are fixed between the ion exchange membrane 28 and the anode chamber, respectively.
- FIG. 8 is a plan view showing an example of a cathode that can be used in the bipolar zero-gap electrolytic cell of the present invention and a sampling position of an electrolyte concentration.
- FIG. 9 is a cross-sectional view illustrating a bipolar poled fine-gap electrolytic cell according to another embodiment of the present invention.
- the current 4 k A / Not only is it required to be able to perform electrolysis at m 2 to 8 kA / m 2 , but also to lower the voltage to the limit.
- the present inventors have view of this situation, when improving the unit electrolytic cell, 4 k A / m 2 from a high current density such as 8 k A / m 2, significantly lower voltage than the conventional electrolytic cells Therefore, studies have been conducted with the aim of achieving stable electrolysis.
- the cation exchange membrane is pressed against the anode by the pressure of the cathode chamber, so that a gap is formed between the cathode and the cation exchange membrane.
- This part contains a large amount of bubbles in addition to the electrolyte, and has extremely high electrical resistance.
- the distance between the anode and the cathode hereinafter referred to as the interelectrode distance
- the electrolyte or gas bubbles existing between the anode and the cathode It is most effective to eliminate the effects of
- the distance between the poles was usually about 1 to 3 mm (hereinafter referred to as a fine gap).
- Several means have been proposed to reduce this gap.
- L electrolysis cells generally have an energization area of 2 m or more, and it is impossible to make the tolerance of the production accuracy almost zero by completely smoothing the anode and cathode. Therefore, simply reducing the distance between the electrodes can push the ion exchange membrane between the anode and the cathode to break, or the distance between the poles is almost the same as the thickness of the ion exchange membrane.
- the ideal zero gap cannot be obtained because there are parts that cannot be kept in a state where there is almost no gap between the anode and the membrane and between the cathode and the membrane (hereinafter referred to as zero gap).
- the anode has a relatively high rigidity in order to achieve a zero gap, has a structure that is less deformed even when the ion-exchange membrane is pressed, and has a flexible structure only on the cathode side.
- the structure is designed to absorb the unevenness due to tolerances in manufacturing accuracy and deformation of the electrodes, etc., and maintain the opening gap.
- the mouth gap structure needs to have a conductive cushion mat on the cathode side and at least two layers of hydrogen generation cathodes adjacent to this and in contact with the cation exchange membrane. is there.
- a conductive plate 3 is installed in the cathode chamber, and a conductive mat 2 It is preferable to have at least three layers in which the hydrogen generating cathode 1 having a thickness of 0.5 mm or less is superposed on the portion that contacts the cation exchange membrane.
- the conductive plate 3 transmits electricity to the cushion mat 2 and the hydrogen generating cathode 1 laminated thereon, supports the load received from them, and allows the gas generated from the cathode to pass through the partition wall 5 without any trouble.
- the shape of this conductive plate is preferably an expansive methanol punched porous plate.
- the opening ratio is preferably at least 40% so that hydrogen gas generated from the cathode can be extracted to the partition wall side without any trouble.
- strength when the distance between ribs 4 is 1 ⁇ 0 mm, a pressure of 3 mH 2 O can be applied to the center of the ribs and if it bends less than 0.5 mm, it can be used as a conductive plate.
- Nickel, nickel alloy, stainless steel, iron, etc. can be used for the material of corrosion resistance, but nickel is the most preferable for conductivity.
- An L-shaped portion 6 can be formed on a part of the conductive plate 3 as shown in FIG.
- the rib serves as the conductive plate, which is preferable because the material can be saved and the assembling time can be reduced.
- the cathode that has been used in the Finite Night Gap electrolytic cell can be used as it is.
- Cushion mats need to transmit electricity to the cathode between the conductive plate and the cathode for hydrogen generation, and to pass hydrogen gas generated from the cathode to the conductive plate side without resistance.
- the most important role is to apply a uniform and appropriate pressure to the cathode in contact with the ion-exchange membrane so as not to damage the membrane, thereby bringing the ion-exchange membrane into close contact with the cathode.
- the wire diameter of the cushion mat is preferably from 0.05 mm to 0.25 mm. If the wire diameter is smaller than 0.05 mm, the cushion mat will be easily crushed, and if the wire diameter is larger than 0.25 mm, the cushion mat will be strong.If used for electrolysis, the pressure will increase and the membrane performance will be affected. Exert.
- a wire diameter in the range of 0.08 mm to 0.15 mm can be used.
- the thickness of such a cushion mat can be about 3 mm to 15 mm.
- those having a size of about 5 mm to 10 mm can be used.
- a material having a known range can be used.
- those having a repulsive force S20 g / cm 2 to 400 g / cm 2 at the time of 50% compression deformation can be used. If the repulsive force at the time of 50% compression deformation is smaller than 20 g / cm 2 , it is not possible to completely press H, and if it is larger than 400 g / cm 2 , the membrane is pressed more strongly, which is not preferable.
- a material having a resilience of 30 gZcm 2 to 200 gZ cm 2 at the time of 50% compression deformation can be used.
- Such a cushion mat is used by being stacked on a conductive plate.
- This mounting method may be a commonly known method, for example, appropriately fixed by spot welding, or a resin pin or a metal wire.
- the cathode may be directly stacked on the cushion mat. Alternatively, the cathodes may be overlapped via another conductive sheet.
- a cathode that can be used for the zero gap a cathode having a small wire diameter and a small number of meshes is preferable because of its high flexibility.
- a substrate a known one can be used.
- a wire diameter of 0.1 to 0.5 mm and a mesh size of about 20 to 80 mesh may be used.
- the base material of the cathode is a punched perforated plate made of nickel metal or nickel metal with a thickness of 0.05 to 0.5 mm or a wire net made of nickel metal with an opening ratio of 20% to 70%. Can also be suitably used.
- a nickel expansed metal having a thickness of 0.1 mm to 0.2 mm or a punched perforated plate or nickel made of nickel.
- a nickel wire mesh having an aperture ratio force S of 25% to 65% can be more preferably used.
- the metal is rolled and flattened in the range of 95 to 105% of the thickness of the metal plate before processing.
- wire mesh two wires intersect at right angles, so the thickness is twice as large as the wire diameter.
- the wire mesh is rolled in the range of 95 to 105% of the wire diameter. Can also be suitably used.
- the coating of the cathode is preferably a noble metal oxide coating and thin.
- the plasma sprayed coating of nickel oxide has a thickness of 100 / ini or more, and it is hard and brittle as a zero-gap cathode that requires flexibility.
- the exchange membrane was sometimes damaged.
- the thickness of the coating layer is small, since the softness of the cathode substrate is not impaired and the ion exchange membrane is not damaged. If the coating is too thick, as described above, not only may the ion exchange membrane be damaged, but also there are problems such as an increase in the manufacturing cost of the cathode. If it is too thin, sufficient activity cannot be obtained. Therefore, the thickness of the coating layer is preferably from 0.5 ⁇ m to 50 ⁇ m, and most preferably from 1 ⁇ m to 10 ⁇ m. The coating thickness of the cathode can be measured with an optical microscope and an electron microscope by cutting a cross section of the substrate.
- the shape of the anode itself is important in addition to the requirements described above.
- the ion-exchange membrane is pressed against the anode more strongly than the conventional fin-gap electrolysis cell, so in the case of an anode using an eta-spun metal substrate, the ion-exchange membrane may be damaged at the end of the opening, or In some cases, the ion-exchange membrane digged into the opening, creating a gap between the cathode and the ion-exchange membrane, causing the voltage to rise.
- the electrodes have as planar a shape as possible.
- the apparent thickness increases about 1.5 times to 2 times before the processing. If this is used for a zero-gap electrolytic cell as it is, the above-mentioned problem will occur.
- rolling is performed by means such as a roll press to reduce the thickness from 95% to 105% of the thickness of the metal plate before expanding. Flatten Is desirable. By doing so, not only can the ion exchange membrane be prevented from being damaged, but also the voltage can be unexpectedly reduced. The reason for this is not clear, but it is expected that the current density will be uniform because the surface of the electrode and the electrode surface are in uniform contact.
- the thickness of the anode is usually preferably from 0.7 mni to 2.0 mm. If the thickness is too small, the pressure drops between the anode and cathode chambers and the pressure of the cathode, which causes the ion exchange membrane to press the anode, causing the anode to drop and the distance between the electrodes to widen. It is not preferable because it becomes high. On the other hand, if the thickness is too large, an electrochemical reaction occurs on the back side of the electrode, that is, on the side opposite to the surface in contact with the ion-exchange membrane, and the resistance is undesirably increased.
- the thickness of the anode is more preferably from 0.9 mm to 1.5 mm, and even more preferably 0.9 mn! ⁇ 1.1 mm thick. In the case of wire mesh, two wires intersect at right angles, so the thickness is twice the wire diameter.
- a zero gap electrolysis cell In a zero gap electrolysis cell, the ion exchange membrane and the anode surface are in close contact during electrolysis, which may cause a local shortage of electrolyte supply.
- chlorine gas is generated on the anode side during electrolysis, and hydrogen gas is generated on the cathode side.
- electrolysis is performed by keeping the gas pressure on the cathode side higher than the gas pressure on the anode side and pressing the membrane against the anode by the gas differential pressure.
- the pressing pressure due to the mattress on the cathode side is also applied during operation, so the pressing pressure on the anode side is larger than that of the usual finite gap electrolytic cell with a gap between the anode and the cathode.
- the pressing pressure was increased, fine water bubbles were formed on the ion exchange membrane, and in some cases, the electrolysis voltage was increased.
- the anode surface is provided with irregularities so that the electrolytic solution can be easily supplied by the depressions.
- it is effective to provide appropriate irregularities on the surface by means such as plast treatment or etching treatment with an acid.
- the anode catalyst is applied to the irregularities.
- the anode catalyst enters the irregularities, and the degree of roughness is reduced from the surface roughness after etching.
- the anode catalyst is prepared by treating the surface of a titanium substrate with an acid and then applying iridium chloride, ruthenium chloride, or titanium chloride. It is formed by thermal decomposition after applying a mixed solution of tan.
- the average thickness of the catalyst layer is in the range of 1 m to 10 ⁇ m as a whole by repeating the coating and thermal decomposition processes with a catalyst thickness of 0.2 ⁇ m to 0.3 ⁇ m per time. can do.
- the thickness of the catalyst layer is determined based on the life and price of the anode. A range of 33 ⁇ is suitably selected.
- the maximum difference between the peak and valley heights must be in the range of 5 ⁇ m to 50 ⁇ m. If the unevenness is too small, the supply of the electrolyte may be insufficient locally, which is not preferable. On the other hand, if the irregularities are too large, the surface of the ion exchange membrane may be adversely damaged. Therefore, in order to use the ion exchange membrane stably, it is necessary that the maximum value of the difference between the irregularities on the surface of the anode is in the range of 5 ⁇ to 50 ⁇ . For more stable operation, the maximum value of the difference between the irregularities on the surface of the anode is more preferably from 8 / zm to 3 ° ⁇ . '
- the measurement by the non-contact type optical interference method utilizes NewwView5202 made by Zygo.
- This device is equipped with an optical microscope, an interference-type objective lens, and a CCD camera.
- a white light source is applied to the object to be measured, and the interference fringes generated according to the surface shape are vertically scanned to obtain the surface shape of the object.
- the area to be measured can be arbitrarily selected, but it is preferable to measure the area from 100 zm to 300 ⁇ m square in order to grasp the unevenness of the anode surface to some extent. it can. In particular, when measuring eta spanned metal, it is more preferable to measure a region from 50 ⁇ m to 150 / zm square.
- the difference between the maximum and minimum values of the surface irregularities is calculated as the PV value (Peak to Val ly). Is calculated.
- the inventors have found a remarkable correlation between the roughness of the anode surface according to the value and the evaluation result when those anodes are used in a zero gap electrolytic cell, and completed the present invention.
- this PV value is the maximum value of the difference between the irregularities on the anode surface.
- the aperture ratio of the anode substrate is preferably 25% or more and 70% or less.
- various methods for measuring the aperture ratio such as a method in which a sample of the electrode is copied with a copying machine, the opening is cut out and weighed, or the length and width of the opening are measured and calculated. Any method is acceptable.
- the aperture ratio is too small, the supply of the electrolytic solution to the ion-exchange membrane may be insufficient, and water bubbles may be generated, which may make it impossible to operate at a stable voltage and current efficiency. Also, if the aperture ratio is too large, the surface area of the electrode decreases, and the voltage increases, which is not preferable. Therefore, the most preferable is an aperture ratio in the range of 30% to 60%.
- a cylindrical duct and / or an internal circulation flow path for the electrolyte solution are provided between the anode chamber and the partition of the cathode chamber or the electrode and the electrode.
- a conductive plate layer is provided on the cathode side, a conductive cushion mat layer is provided thereon, and 0.5 mm is provided on the upper portion thereof and in contact with the cation exchange membrane.
- a bipolar zigzag gap electrolytic cell having at least three layers of the following cathode layers for hydrogen generation with the following thickness.
- the anode-side electrolyte concentration distribution and the cathode-side concentration distribution are easily adjusted appropriately. Furthermore, the pressure fluctuation in the cell is small, and the ion exchange membrane is hardly damaged. Therefore, stable electrolysis can be performed for a long period of time even at a high current density of about 8 kAZm 2 .
- What is required for long-term operation at a stable voltage is that the electrolyte concentration distribution in the electrolytic cell is uniform, there are no bubbles or gas stagnation in the electrolytic cell, and the electrolyte, bubbles and gas When discharging from the discharge nozzle, they do not become a mixed phase, there is no pressure fluctuation in the electrolytic cell, and no vibration occurs.
- the vibration in the cell is measured by using the Yokogawa AR1200 Analyzing Recorder to measure the pressure fluctuation in the anode cell, and the difference between the maximum pressure and the minimum pressure as the vibration of the electrolytic cell.
- the anode and cathode are in close contact with the ion exchange membrane Mass transfer to the ion exchange membrane is likely to be inhibited. If the mass transfer to the ion-exchange membrane is hindered, adverse effects will occur, such as formation of water bubbles in the ion-exchange membrane, an increase in voltage, and a decrease in current efficiency. Therefore, it is important to promote the mass transfer to the ion exchange membrane and keep the concentration distribution of the electrolyte in the cell uniform.
- the concentration distribution on the anode side and the tendency of the current efficiency of the ion exchange membrane to decrease are correlated, and the lower the current efficiency, the greater the concentration distribution. This tendency was particularly remarkable when the current density was high and when there was a gap.
- the concentration was measured at nine sampling positions 13 indicated by black circles in Fig. 3, and the value obtained by subtracting the minimum concentration from the maximum concentration was taken as the concentration difference. From 4 kAZ m or more to 8 kA / m 2 or less, it was found that when this concentration difference was 0.5 N or more, the current efficiency was significantly reduced. Therefore, at a current density of 4 k ⁇ / ⁇ or more and 8 k ⁇ or less in the zero-gap electrolytic cell, it is preferable that at least the salt water concentration difference be 0.5 N or less.
- the electrolytic cell has a plate that can circulate inside the electrolytic cell and can supply the electrolyte uniformly in the horizontal direction. Is one of the structures suitable for the anode side of a zero gap cell.
- the saturated salt water supplied uniformly in the horizontal direction by the anolyte distributor 14 is circulated in the vertical direction of the electrolytic cell by the baffle plate 9, and the concentration distribution is uniform throughout the cell. Is obtained.
- the concentration distribution can be adjusted with higher accuracy. In this way, the zero gap electrolysis cell can be electrolyzed with stable performance.
- the concentration distribution on the cathode side and the increasing tendency of the voltage of the ion-exchange membrane were correlated, and the larger the concentration distribution, the greater the voltage increase. This tendency was particularly remarkable when the current density was high and when the gear was zero.
- the concentrations were measured at nine sampling positions 13 similar to those in the anode chamber, and the value obtained by subtracting the minimum concentration from the maximum concentration among them was defined as the concentration difference.
- eight / ⁇ ! ⁇ In 8 k AZM 2 or less from the following, when the density difference is greater than 2%, found that decrease in current efficiency is remarkably. Therefore, at a current density of 4 kA / m 2 or more and 8 kA / m 2 or less in the zero gap electrolytic cell, it is preferable that at least the difference in the concentration of the aluminum alloy be 2% or less.
- an electrolytic cell that can supply an electrolytic solution uniformly in the horizontal direction is one of the preferred structures for the cathode side of a zero gap cell.
- the electrolytic solution uniformly supplied in the horizontal direction by the catholyte distributor 23 is circulated in the upward and downward directions of the cell due to the difference between the supply voltage and the concentration in the cathode chamber.
- a uniform concentration distribution is obtained throughout the cell.
- the concentration distribution can be adjusted with higher accuracy by appropriately adjusting the supply flow rate using such an electrolytic cell. In this way, the zero gap electrolysis cell can be electrolyzed at a stable voltage.
- the pressure difference between the anode chamber and the cathode chamber fluctuates.
- the anode and the cathode are always kept in close contact with each other through the ion exchange membrane using a cushion mat. Therefore, if there is a change in the differential pressure, the adhesion may fluctuate and the electrode may rub the ion exchange membrane. Since the ion-exchange membrane is made of resin and has a coating on its surface to prevent gas adhesion, if the electrode rubs the ion-exchange membrane, the coating layer of the ion-exchange membrane may peel off, The ion exchange resin itself may be scraped off.
- a partition plate 20 is provided in the gas-liquid separation chamber 7, and a porous plate 19 for removing air bubbles is provided above the partition plate 20. It is effective to provide.
- a double-pole zero-gap electrolytic cell 30 according to an embodiment of the present invention having the same anode structure and cathode structure as in FIGS. 3 and 8 and having the same cross-sectional structure as in FIG. 6, is arranged in series.
- An anode unit cell and a cathode unit cell were arranged at the other end, and a current lead plate 28 was attached thereto, thereby assembling the electrolytic cell shown in FIG.
- the bipolar-type gap electrolysis cell 30 has a width of 24.0 mni and a height of 1280 mm, and has an anode chamber, a cathode chamber, and a gas-liquid separation chamber 7.
- the anode compartment and the cathode compartment are each formed by a pan-shaped partition wall 5 and arranged back to back.
- the anode chamber and the cathode chamber are combined by inserting a frame member 22 into a bent portion 18 provided above the partition wall 5.
- Each gas-liquid separation chamber is defined above each electrode chamber by fixing an L-shaped partition member 16 having a height H to the partition wall 5.
- Gas-liquid cross-sectional area of the separation chamber anode 2 7 cm 2, 1 is the cross-sectional area of the cathode side of the gas-liquid separation chamber 5 In cm z , only the anode-side gas-liquid separation chamber had the same structure as that in FIG. That is, a titanium partition plate 20 having a width W of the passage B of the anode-side gas-liquid separation chamber of 5 mm, a height H 'of 50 mm, and a plate thickness of lmm is provided, and the height from the upper end to the upper end of the gas-liquid separation chamber vertically.
- the aperture ratio 5 9%, c anode side gas-liquid separation chamber of holes 15 fitted with a perforated plate 19 of titanium E box pan dead metal thickness 1 mm can be of oval width 5 mm, length 22 mm With a pitch of 37.5 mm. .
- a baffle plate 9 is provided only on the anode side, a titanium baffle plate with a width W2 of passage D of 10 mm, a height H2 of 500 mm and a plate thickness of 1 mm is provided, and a gap W2 'between the partition wall 5 and the plate bottom is 3 mm. And The height S vertically from the top of the baffle plate to the top of the electrode chamber was 40 mm.
- the anolyte distributor 14 is a rectangular pipe with a length of 220 cm and a cross-sectional area of 4 cm 2 and having 24 holes of 1.5 mm in diameter at equal intervals. It was mounted horizontally at a position of 50 mm, and one end was joined to Ronozunore 12 on the anode side. The pressure loss of this distributor was about 2 mm ⁇ H 2 ⁇ when saturated brine was supplied at a feed rate of 150 L / Hr equivalent to 4 kA / m 2 .
- the catholyte distributor 23 those having 24 equally spaced square pipe holes 2 mm diameter with a cross-sectional area of 3. 5 cm 2 in the length of 220 cm, 50 mm from the cathode chamber bottom of the electrolytic cell It was mounted horizontally at one position, and one end was joined to the cathode-side insertion Ronozunore 24. Pressure loss of this distributor was filed at about 12 mm ⁇ H 2 0 upon applying in 4KAZ m corresponding alkali supply amount 300 L / Hr.
- a nickel-expanded metal having a thickness of 1.2 mm, a horizontal length of the opening of 8 mm, and a vertical length of 5 mm was used as the conductive f raw plate 3, and the cushion mat 2 had a thickness of 0.1 mm.
- Approximately 3 ⁇ coated, covered with a 40-mesh nickel mesh with a wire diameter of 0.15 mm and around the cathode was fixed to a conductive plate by spot welding at about 60 places to form a three-layer structure.
- the structure on the anode side was the same as in FIGS. 3 and 4 and provided with an anolyte distributor 14 and a baffle plate 9.
- a partition plate 2 ° and a porous plate 19 for eliminating bubbles were provided in the anode-side gas-liquid separation chamber as shown in FIG. No such partition plate or perforated plate for eliminating bubbles was provided in the gas-liquid separation chamber on the cathode side.
- a 1 mm titanium plate is subjected to an expansive process, which is rolled to a thickness of 1 ⁇ 0.05 mm by a roll press process, and is attached to the rib 22.
- the opening of the expansive metal before the roll press was applied with a pitch of 6 mm (width) ⁇ 3 mm (length) and a feed pitch of 1 mm.
- the aperture ratio of the metal was 40% as measured by copying with a copy machine. This was etched with sulfuric acid, and the maximum difference in height between peaks and valleys (irregularities) on the surface was 30 ⁇ m.
- the maximum value of the difference between the irregularities on the anode surface was measured using NewView 5022 manufactured by Zygo.
- a cation exchange membrane ACIP LEX (registered trademark) F4401 was sandwiched via a gasket to assemble an electrolytic cell.
- a 300 g / L salt solution is supplied to the anode compartment side of this electrolytic cell so that the outlet salt solution concentration becomes 200 g ZL as an anolyte solution, and the outlet aqueous sodium hydroxide concentration becomes 32% by weight on the cathode compartment side.
- dilute caustic soda electrolysis temperature 90 ° C, 0. 14MP a absolute pressure during electrolysis, and electrolysis 360 days in a range of current density 4 k AZm 2 ⁇ 6 k a / m 2.
- the anolyte and catholyte concentration distributions in the electrolysis cell during electrolysis are shown in Figs. 3 and 8. It was measured at the position of the pulling point 13. That is, at a position 150 mm, 600 mm, and 1000 mm below the upper end of the current-carrying part in the cell, 9, 100 mm inside from the cell center and both ends of the cell were measured. Table 1 shows the difference between the maximum density and the minimum density among the nine points as the density difference.
- Table 1 shows the measurement results of voltage, current efficiency, vibration and concentration distribution in the electrolytic cell during electrolysis. From these results, the voltage rise was only 3 OmV even at 6 kA / m 2 , and the current efficiency was reduced by only about 1%.
- the vibration in the electrolysis cell is also 5 cm or less at the water column, and the concentration difference is 0.31 N to 0.35 N on the anode side and 0.6% to 0.3 N on the cathode side.
- the electrolytic cell was disassembled and the ion exchange membrane was taken out and examined. It was found that there was no water bubbles and the operation could be continued for a longer time.
- An electrolytic cell was formed using the same bipolar electrode cell except that the anode used in Application Example 1 was changed. That is, as an anode, a titanium plate 1 mm obtained by Ekusupando processed, those opening ratio is 30%, by etching with sulfuric acid, the maximum value of unevenness difference on the surface is about 8 ⁇ , Ru0 2 , the maximum value of unevenness difference after applying the coatings based on I r 0 2, T I_ ⁇ 2 is 3 mu m, an anode thickness of 1. was 8 mm.
- Table 2 shows the results of the same measurement as in application example 1 with the same operation. The results show that the voltage rise was 150 kV at 6 kA / m "and the current efficiency declined by 2 to 3%. The vibration in the electrolytic cell was less than 5 cm at a water column even at 6 kA / m.
- the concentration difference was 0.31N to 0.35N on the anode side and 0.6% to 0.8 ⁇ % on the cathode side.
- the electrolytic cell was disassembled and the ion-exchange membrane was taken out and examined.
- the ion-exchange membrane had fine water bubbles and an ion-exchange membrane with small pinholes.
- An electrolytic cell was formed using the same bipolar electrolytic cell except that the hydrogen generation cathode used in Application Example 1 was changed. That is, a 14-mesh nickel wire gauze with a wire diameter of 0.4 mm (cathode thickness 0.8 mm) coated with a coating of about 250 ⁇ m mainly composed of nickel oxide was used as the cathode for hydrogen generation.
- a 14-mesh nickel wire gauze with a wire diameter of 0.4 mm (cathode thickness 0.8 mm) coated with a coating of about 250 ⁇ m mainly composed of nickel oxide was used as the cathode for hydrogen generation.
- Table 2 shows the results of the same measurement as in application example 1 with the same operation. From this result, the voltage is high from the beginning, the rise is 6 kA / m 2 and 8 OmV, and the decrease in current efficiency is 2% to 3. /. There was also. Vibrations in the electrolytic cell is at less than 5 cm in water column even 6 kAZm 2, density difference anode side 0. 31N ⁇ 0. 35 N, a cathode side was 6% to 0. 8% 0.1.
- An electrolytic cell was formed using the same bipolar electrode cell except that the anode used in Application Example 1 was changed.
- Table 4 shows the measurement results of the voltage, current efficiency, vibration and concentration distribution in the electrolysis cell during electrolysis. From this result, the voltage rise was only 3 OmV even at 8 kA / m 2 , and the current efficiency decline was only about 0.9%. Vibration in the electrolytic cell is also 10 cm at the water column The concentration difference is 0.39N ⁇ 0.47N on the anode side and 1.2% ⁇ on the cathode side: L.
- the electrolytic cell was disassembled, and the ion exchange membrane was taken out and examined. It was found that there was no water bubble and the operation could be continued longer.
- Electrolysis was performed in the range of 7 kA / m 2 to 8 kAZm 2 using the same electrolytic cell as in Application Example 1.
- Table 4 shows the measurement results of the voltage, current efficiency, vibration and concentration distribution in the electrolysis cell during electrolysis. From these results, the rise in voltage was 9 OmV at 8 kA / m 2 , and the decrease in current efficiency was 3.3%.
- the vibration in the electrolytic cell was less than 5 cm at the water column, and the concentration difference was 0.6N to 0.7N on the anode side and 1.5% to 2.1% on the cathode side.
- the electrolytic cell was disassembled and the ion exchange membrane was taken out and examined. As a result, many water bubbles with a diameter of 1 mm to 10 mm were formed throughout the ion exchange membrane.
- the cross-sectional view of the bipolar electrolysis cell has the structure shown in Fig. 9 and is equipped with an exponential metal thickness of 1.8 mm as the anode, and a plasma sprayed nickel-sputtered metal with a thickness of 250 mm as the cathode.
- An electrolytic cell was prepared, which had a coating containing nickel oxide as the main component and was used for one year with a distance between electrodes of 2 mm. The anode of this electrolytic cell was removed, and a new anode was used. Was installed. Further, the coating of the cathode was scraped off with a brush to expose the nickel background and used as a conductive plate. Further, the same cushion mat and the cathode for hydrogen generation as in Application Example 1 were attached in exactly the same manner.
- the electrolytic cell was disassembled, and the ion exchange membrane was taken out and examined. As a result, there was no water bubble and the operation was possible for a longer time.
- a gas-liquid separation chamber is provided on each of the non-conducting part above the anode chamber and the non-conducting part above the cathode chamber so as to be integrated with the cathode chamber or the cathode chamber.
- a cylindrical duct and / or baffle plate that serves as an internal circulation channel for the electrolyte It has at least one conductive plate on the cathode side, a conductive cushion mat on the top, and at least 3 layers of a hydrogen cathode for use on the top and in contact with the cation exchange membrane.
- Such a zero-gap electrolytic cell can also be manufactured by modifying the electrolytic cell previously used in the fine-gap.
- a gas-liquid separation chamber is provided integrally with the anode chamber or the cathode chamber at each of the non-conducting part at the upper part of the anode chamber and the non-conducting part at the upper part of the cathode chamber. Between them, there is a case where an electrolytic cell having a cylindrical duct or baffle plate that serves as an internal circulation flow path for the electrolytic solution, which was previously used as a fine night gap, is modified into a zero gap electrolytic cell.
- the structure of the anode and the anode chamber should be improved as described above, and the cathode chamber should be remodeled so that a conductive plate, a cushion mat, and a cathode could be attached to form a zero-gap electrolytic cell.
- the cathode used in the fine-gap can be used as it is as a conductive plate, and a zero-gap electrolytic cell can be obtained by simply laminating a cushion mat and a new cathode.
- the cathode, cushion mat, and conductive plate can be removed from the Zeguchi Gap electrolytic cell, and a new cathode can be used to use it as a fine night gap.
- Such a modification is significantly cheaper than making a new electrolytic cell, and can be easily modified, so there is a great advantage for the user.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
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EP03811931.9A EP1577424B1 (en) | 2002-11-27 | 2003-11-26 | Bipolar zero-gap electrolytic cell |
US10/535,249 US7323090B2 (en) | 2002-11-27 | 2003-11-26 | Bipolar zero-gap type electrolytic cell |
ES03811931.9T ES2533254T3 (es) | 2002-11-27 | 2003-11-26 | Célula electrolítica bipolar, sin intersticios |
AU2003302453A AU2003302453A1 (en) | 2002-11-27 | 2003-11-26 | Bipolar zero-gap electrolytic cell |
JP2004555055A JP4453973B2 (ja) | 2002-11-27 | 2003-11-26 | 複極式ゼロギャップ電解セル |
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JP2002344467 | 2002-11-27 | ||
JP2002-344467 | 2002-11-27 |
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WO2004048643A1 true WO2004048643A1 (ja) | 2004-06-10 |
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US (1) | US7323090B2 (ja) |
EP (2) | EP2039806B1 (ja) |
JP (2) | JP4453973B2 (ja) |
KR (1) | KR100583332B1 (ja) |
CN (2) | CN101220482B (ja) |
AU (1) | AU2003302453A1 (ja) |
ES (2) | ES2547403T3 (ja) |
TW (1) | TWI255865B (ja) |
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- 2003-11-26 AU AU2003302453A patent/AU2003302453A1/en not_active Abandoned
- 2003-11-26 TW TW092133228A patent/TWI255865B/zh not_active IP Right Cessation
- 2003-11-26 JP JP2004555055A patent/JP4453973B2/ja not_active Expired - Lifetime
- 2003-11-26 WO PCT/JP2003/015101 patent/WO2004048643A1/ja active IP Right Grant
- 2003-11-26 ES ES09150367.2T patent/ES2547403T3/es not_active Expired - Lifetime
- 2003-11-26 KR KR1020057005168A patent/KR100583332B1/ko active IP Right Grant
- 2003-11-26 EP EP03811931.9A patent/EP1577424B1/en not_active Expired - Lifetime
- 2003-11-26 US US10/535,249 patent/US7323090B2/en active Active
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JP2008013821A (ja) * | 2006-07-06 | 2008-01-24 | 炳霖 ▲楊▼ | 電気分解を利用した燃焼ガス発生装置及び車載用燃焼ガス発生装置 |
JP2010144206A (ja) * | 2008-12-18 | 2010-07-01 | National Institute Of Advanced Industrial Science & Technology | 水素発生方法及び水素発生装置 |
WO2010122785A1 (ja) * | 2009-04-21 | 2010-10-28 | 東ソー株式会社 | イオン交換膜法電解槽 |
US9476130B2 (en) | 2010-12-28 | 2016-10-25 | Tosoh Corporation | Electrolytic cell |
WO2013141211A1 (ja) | 2012-03-19 | 2013-09-26 | 旭化成ケミカルズ株式会社 | 電解セル及び電解槽 |
US9506157B2 (en) | 2012-03-19 | 2016-11-29 | Asahi Kasei Kabushiki Kaisha | Electrolysis cell and electrolysis tank |
US9683300B2 (en) | 2012-06-18 | 2017-06-20 | Asahi Kasei Kabushiki Kaisha | Bipolar alkaline water electrolysis unit and electrolytic cell |
JP2014009385A (ja) * | 2012-06-29 | 2014-01-20 | Asahi Kasei Chemicals Corp | 電解セル及び電解槽 |
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JP2018104756A (ja) * | 2016-12-26 | 2018-07-05 | 株式会社イープラン | 電解槽 |
WO2018168863A1 (ja) | 2017-03-13 | 2018-09-20 | 旭化成株式会社 | 電解セル及び電解槽 |
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JP2018165379A (ja) * | 2017-03-28 | 2018-10-25 | 高砂熱学工業株式会社 | 水電解方法、水電解装置、水電解システム、水電解・燃料電池運転方法、水電解・燃料電池装置及び水電解・燃料電池システム |
JP2020535314A (ja) * | 2017-09-29 | 2020-12-03 | ティッセンクルップ・ウーデ・クロリンエンジニアズ ゲー エム ベー ハー | 電解装置 |
JP7055864B2 (ja) | 2017-09-29 | 2022-04-18 | ティッセンクルップ・ウーデ・クロリンエンジニアズ ゲー エム ベー ハー | 電解装置 |
US11608561B2 (en) | 2017-09-29 | 2023-03-21 | Thyssenkrupp Uhde Chlorine Engineers Gmbh | Electrolysis device |
WO2019172750A1 (en) | 2018-03-05 | 2019-09-12 | Nederlandse Organisatie Voor Toegepastnatuurwetenschappelijk Onderzoek Tno | Method for electrochemically reducing carbon dioxide |
JP2022537986A (ja) * | 2019-06-18 | 2022-08-31 | ティッセンクルップ・ウーデ・クロリンエンジニアズ ゲー エム ベー ハー | 電解用電極および電解装置 |
JP7236568B2 (ja) | 2019-06-18 | 2023-03-09 | ティッセンクルップ・ウーデ・クロリンエンジニアズ ゲー エム ベー ハー | 電解用電極および電解装置 |
CN111044584A (zh) * | 2019-12-23 | 2020-04-21 | 浙江大学 | 一种动态测量金属材料氢陷阱参数的装置及方法 |
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Also Published As
Publication number | Publication date |
---|---|
AU2003302453A1 (en) | 2004-06-18 |
KR100583332B1 (ko) | 2006-05-26 |
KR20050052516A (ko) | 2005-06-02 |
US20060042935A1 (en) | 2006-03-02 |
ES2533254T3 (es) | 2015-04-08 |
EP2039806A1 (en) | 2009-03-25 |
CN100507087C (zh) | 2009-07-01 |
EP1577424A4 (en) | 2005-12-14 |
JP4453973B2 (ja) | 2010-04-21 |
CN1717507A (zh) | 2006-01-04 |
JP5047265B2 (ja) | 2012-10-10 |
CN101220482A (zh) | 2008-07-16 |
TW200409834A (en) | 2004-06-16 |
EP1577424B1 (en) | 2015-03-11 |
US7323090B2 (en) | 2008-01-29 |
TWI255865B (en) | 2006-06-01 |
EP1577424A1 (en) | 2005-09-21 |
JP2010111947A (ja) | 2010-05-20 |
JPWO2004048643A1 (ja) | 2006-03-23 |
ES2547403T3 (es) | 2015-10-06 |
EP2039806B1 (en) | 2015-08-19 |
CN101220482B (zh) | 2011-02-09 |
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