JPH07118887A - Bielectrode-type electrolytic cell - Google Patents

Abstract

PURPOSE: To enable excellent performance, easy operation and manufacture and management at a low cost by energizing partition walls, anodes and cathodes, forming electric conduction plates to multiple layers and disposing current distribution frames between these electric conduction plates and the electrodes.

CONSTITUTION: A unit electrolytic cell 1 is provided with electrolyte inflow ports 6 and 15, products outlets 7 and 16 and slopes for prohibiting the stagnation of gases at an inside end. The one side thereof is provided with frame walls 2 and 11 and the partition walls 3, 12 are fixed thereto. These walls and the anodes 5 and the cathodes 4 are energized between each other. The electric conduction plates 4 and 13 of the prescribed size to uniformly maintain the current density and the concn. distribution of the electrolyte in the unit electrolytic cell 1 are formed to the multiple layers. The respective unit electrolytic cells are electrically connected by many conductive medium bodies 20 positioned between the electrodes 5 and 14. The electrode current distribution frames 32 for decreasing the locally high current density and maintaining the specified current density are disposed between the conductive medium bodies 20 and the electrodes 5 and 14. The respectively unit electrolytic cells are continuously arrayed by coupling loads 23 and the partition walls 3 and 12 are energized by the many metallic plates 20 of a spring type subjected to explosive welding across these walls.

COPYRIGHT: (C)1995,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a bipolar electrode electrolytic cell composed of a large number of unit electrolytic cells. Specifically, a spring-shaped metal plate was obtained by the explosive welding connection method so as to be compatible with the electrolysis production of chlorine and alkali metal hydroxide that electrolyzes an aqueous solution of alkali chloride. The electrolytic cell. Inside each electrolysis chamber of a large number of unit cells connected in series, there is a multi-layered electric conduction plate to maintain uniform current density and electrolyte concentration, and cation exchange between electrodes. In order to protect the membrane, we have installed a current distribution frame that makes the current uniform.
Furthermore, it has a sloping frame wall to protect the cation exchange membrane from the stagnation of chlorine gas.

[0002]

2. Description of the Related Art A conventional electrolytic cell is obtained by directly welding an electrode (1 mm thick) and an electric conductive plate (2 mm thick). In such a method, welding is very difficult and the welding state becomes very poor.
Due to the poor welding condition, the electrodes are not uniform and the deviation of the current density is increased in the thin film in the electrolytic cell. The non-uniformity of current density in the electrolytic cell reduces the electrolytic cell voltage and reduces the performance of the electrolytic cell.

Not only is the performance of the electrolytic cell reduced, but it also affects the stability of the electrolytic cell system. The pressure inside the electrolytic cell is 0.5 kg /
When the area reaches about cm ² , heat is locally generated by the electrode and the electric conductive plate being dropped, and this heat causes fatal damage to the membrane, resulting in stability problems of the electrolytic cell system.

A large number of unit electrolytic cells having a cation exchange membrane inserted therein are connected between the anode chamber and the cathode chamber, and the unit electrolytic cell at one end is connected to the anode side and the cathode of the unit electrolytic cell at the other end is low. A number of prior patents have been filed for a bipolar electrode cell that is supplied with a high-current power source and produces an alkali metal such as chlorine and potassium hydroxide using a cation exchange membrane as a separation membrane.

Particularly, as a prior patent for the electrical connection between the unit electrolytic cells and the unit electrolytic cells constituting the bipolar electrode electrolytic cell,
An electrolytic cell using the explosive-welding method for a partition wall in which the material of one unit electrolytic cell is titanium and the entire partition wall in which the material of the other electrolytic cell is iron (US Pat. No. 4,111,779).
No.), an electrolytic cell in which a plate on which a node is formed is inserted between partition walls and electrically connected (European Patent No. 0172495),
An electrolytic cell (German Patent No. 2551234) in which each unit electrolytic cell formed of a plastic material is electrically connected by means of fixing bolts and nuts, and a connecting portion made of ultrasonic welding or titanium-copper-stainless steel And an electrolytic cell (Japanese Patent Laid-Open No. 54-90079).

As a prior patent for the structure of the electric conduction plate provided inside the electrolytic cell, particularly between the electrode and the partition wall of the electrolysis chamber, an electrolytic cell having an electric conduction plate having a large number of openings formed in a single plate (European Patent No. 220659), an electrolytic cell having an electric conductive plate composed of a single plate having a space on both sides
(US Pat. No. 4,389,289) and an electrolytic cell (US Pat. No. 4,417,960) having an electrically conductive plate in the form of a skeleton.

On the other hand, as a prior patent for the form of the bipolar wall of the bipolar type electrolytic cell, an electrolytic cell (S.OGAWA) in which the bipolar electrode wall is made by explosive welding connection so that the anode chamber and the cathode chamber cannot be separated from each other. , CHEM.AGE, INDIA,
31, 1980, 441; MOTANI, ibid, 3
1, 1980, 457), an electrolytic cell in which a bipolar wall is made by explosive welding connection to separate an anode chamber and an anode chamber (US Pat. No. 4,568,434), an anode chamber and a cathode chamber can be separated, and an explosion occurs. An electrolytic cell having a bipolar wall that is not welded (J. OF ELECTROCHEMISTRY 1
2, 1982, 631).

[0008] Furthermore, when operating the electrolytic cell at an internal pressure higher than the atmospheric pressure, the size of the bubbles of chlorine gas is reduced and the voltage of the electrolytic cell can be reduced (US Pat. No. 4,105,515). No.)

As an electrolytic cell, it has to satisfy the conditions such as excellent performance, easy operation, and the fact that it can be manufactured and managed at a low cost, but the conventional electrolytic cell largely satisfies all the above conditions. I haven't been able to. The electrolytic cell having the excellent partition having the explosion-welded joints has a problem that the manufacturing cost is increased because it requires a long time and personnel for the explosive-welded joints. Further, an electrolytic cell having a partition wall which is not explosion-welded has a merit that the cost for manufacturing and maintaining is low, but has a problem that the performance of the electrolytic cell is low. When the unit electrolytic cell is made of a plastic material, the partition wall of the electrolytic cell must be made thick in consideration of mechanical strength. For this reason, it is not possible to make a thin and small electrolytic cell, and it is limited to a large electrolytic cell, and when a problem occurs in one of the unit electrolytic cells during operation of the electrolytic cell in which many unit electrolytic cells are continuously connected, After stopping the operation of all the unit electrolytic cells that are directly connected to each other, it is necessary to check the problems, so that there is a problem that workability is deteriorated.

[0010]

SUMMARY OF THE INVENTION An object of the present invention is to provide a sufficient machine by forming the anode chamber partition wall and the cathode chamber partition wall of each unit electrolytic cell constituting the bipolar electrode cell by titanium and nickel materials, respectively. (EN) Provided is a bipolar electrode type electrolytic cell which is provided with an appropriate strength and whose size and shape can be freely selected according to working conditions.

Another object of the present invention is to connect a plurality of unit electrolytic cells constituting a bipolar electrode electrolytic cell by a connecting method using bolts and nuts, and to form a large number of springs made of explosive-welded copper and nickel materials. By connecting using a metal plate of a mold so that it can be energized, it is possible to easily replace only the unit cell where problems have been exposed even when all the unit cells are in operation, and to perform explosive welding connection inside each cell. An object of the present invention is to provide a bipolar electrode electrolytic cell capable of improving workability by reducing the working time required for assembling and disassembling the electrolytic cell by forming a non-polar electrode partition.

Further, according to the present invention, an electric conduction plate formed in multiple layers is provided in each electrolysis chamber of the unit electrolytic cell in order to keep the current density and the electrolyte concentration uniform, and the cation exchange membrane is protected by the stagnation of chlorine gas. Therefore, it is an object to provide a bipolar electrode electrolytic cell having an inclined frame wall and having excellent performance.

[0013]

In order to achieve the above-mentioned object, the present invention is characterized in that the anode chamber partition wall and the anode and the cathode chamber partition wall and the cathode are electrically energized, and the current density in the unit electrolytic cell is increased. In order to keep the concentration distribution of the electrolyte and electrolyte uniform, a plurality of electric conduction plates of a predetermined size are formed, and a current distribution frame for maintaining a constant current density is provided between the electric conduction plate and the electrode. is there. Another feature of the present invention is that it is designed to be energized by a large number of explosion-welded metal plates installed between the anode chamber partition wall and the cathode chamber partition wall, and the electrolyte flows into each unit electrolytic cell by the connecting means. The inflow port and the product outlet are formed on the lower and upper sides of the electrolytic cell so that the product flows out, and the inner end face is provided with an inclined surface to prevent the gas from stagnating.

The bipolar electrode electrolytic cell of the present invention will be further described with reference to the drawings. FIG. 1 is a cross-sectional view showing a continuous arrangement of unit electrolytic cells 1 formed of an anode chamber 10, a cathode chamber 19 and a cation exchange membrane 21 interposed therebetween. The anode chamber includes an anode chamber frame wall 2, an anode chamber partition wall 3 fixed to one side of the anode chamber partition wall 3, and an anode chamber partition wall 3 and an anode 5 welded to an electric conduction plate 4 which will be described later so as to be electrically connected to each other. It has the electric conduction plate 4 formed in multiple layers between. Similar to the anode chamber 10, the cathode chamber 19 includes a frame wall 11 of the cathode chamber, a cathode chamber partition wall 12 fixed to one side of the frame wall 11, and the cathode chamber partition wall 12 and the cathode 14 welded to the electric conductive plate 13 to each other. To be able to conduct
An electric conduction plate 13 formed in multiple layers is provided between them. Passages 8 and 1 of the electric conduction plates 4 and 13 formed in this multilayer
7 allows electrolyte and products to pass through.

The anode chamber frame wall 2 and the cathode chamber frame wall 11 are formed so as to be symmetrical with respect to the cation exchange membrane 21. Electrolyte inlets 6 and 15 are connected to one side of the lower part of the unit electrolytic cell 1 so that the electrolyte flows into the inside of the unit electrolytic cell 1, and an outlet 7 through which a product flows out to one side of the opposite upper side, 16 are connected so as to communicate with each other.

Electrolyte inlet 6,15 and product outlet 7,16
Are connected to the supply heads 22 and 22 'and the outlet heads 23 and 23' located at the lower and upper portions of the unit electrolytic cell 1 through flexible hoses 27 and 28 connected to them, respectively.

Generally, when there is no inclined surface at the inner ends of the anode chamber frame wall 2 and the cathode chamber frame wall 11, hydroxide ions that move to the anode chamber 10 in the cathode chamber 19 during electrolysis of salt water, and the anode chamber 1
Chlorine stagnation in 0 diffuses into the cation exchange membrane 21 and reacts in the cation exchange membrane 21 according to the following equation to generate crystals, so that the cation exchange membrane 2
The performance of 1 deteriorates. 2NaOH + Cl ₂ → NaCl + NaOCl + H ₂ O

In order to prevent such damage of the thin film, that is, at the inner ends of the anode chamber frame wall 2 and the cathode chamber frame wall 11, a gas generated from an electrolysis product (for example, an electrolytic cell during electrolysis of salt water) is used. An inclined surface having an inclination angle of 5 ° or more was formed to protect the cation exchange membrane 21 from chlorine gas that stagnates at the inner end portion of the. The thicknesses of the anode chamber frame wall 2 and the cathode chamber frame wall 11 are not particularly limited as long as the electrolyte inlets 6 and 15 and the product outlets 7 and 16 can be installed, but the thickness is usually 10 mm to 50 mm. Economically, the thickness of 40 mm is most preferable. Further, the anode chamber frame wall 2 and the cathode chamber frame wall 11
As the material of the above, metals such as iron, nickel and titanium, which have chemical resistance to the electrolyte and products, and polyethylene,
Plastics such as polypropylene, vinyl chloride resin, and fluorine resin are used, and it is preferable to use metal in consideration of price, leakage of electrolytic solution, and mechanical strength of the electrolytic cell. For example, in electrolysis of salt water, it is most desirable to use titanium for the material of the anode chamber frame wall 2 and nickel for the material of the cathode chamber frame wall 11.

The electric conduction plates 4 and 13 are welded to the partition walls 3 and 12, and the active anode 5 and the active cathode 14 are connected to the electric conduction plates 4 and 13.
And the electric current is supplied to the active anode 5 from the anode partition wall 3. The electric conductive plates 4 and 13 affect the current density distribution and the electrolyte concentration distribution of the electrolytic cell, and these have the property of mutual exchange (Trade-Off).

The electrolytic cell of the present invention allows a large amount of contact between the partition wall and the electrode to make the current density uniform on the active electrode surface in the electrolytic cell, and at the same time, to make the concentration of the electrolytic solution uniform in the electrolytic cell. The electric conduction plates 4 and 13 of the passages 8 and 17 are provided at optimum sizes and positions. Any material may be used as the material for the electric conduction plates 4 and 13 as long as it has excellent chemical resistance and electric conductivity to electrolytes and products. For example, in electrolysis of salt water, the electric conduction plate 4 of the anode chamber 10 is made of titanium. The electric conduction plate 13 of the cathode chamber 19 is preferably made of nickel. When the electric conduction plates 4 and 13 are coated with a platinum group oxide, electric conductivity is further improved. Electrically conductive plates 4, 13 and electrodes 5, 14
A current distribution frame 32 for equalizing the current density on the electrode surface is present between them, and this induces a current partially entering through the electric conduction plate so as to have a uniform distribution over the entire electrode surface. .

As the material of the conduction medium 20 provided to reduce the electric contact resistance between the anode partition wall 3 and the cathode partition wall 12, a metal such as copper, nickel, titanium or an alloy thereof is used. During electrolysis of salt water, the anode partition wall 3 and the cathode partition wall 12 are metals different from each other, and therefore a copper-nickel dual alloy is used to induce a current in these metals. The structure of the conduction medium 20 is in the form of a spring support so that when the unit cells are combined with the coupling load 29, the adjacent unit cells are sufficiently brought into close contact with each other and the current is well conducted to the respective unit cells. Has become.

The anode partition wall 3 and the cathode partition wall 12 must be thick enough to support the internal pressure of the electrolytic cell and to weld the electrically conductive plates 4 and 13. A thickness of 1-3 mm is appropriate from the mechanical strength and economical aspects of the electrolytic cell. The material of the partition wall is preferably the same as the material of the frame walls 2 and 11. The partition walls 3 and 12 and the frame walls 2 and 11 are connected by welding and bonding.

The material of the anode 5 is a titanium material and a platinum group metal oxide coated thereon. As the platinum group oxide, an iridium compound, ruthenium oxide, titanium oxide, zirconium oxide or the like is used, and a mixture of the above platinum group compounds for improving performance may be used.

Gases such as chlorine gas and oxygen gas are generated at the anode 5, so that the gas existing between the anode 5 and the cation exchange membrane 21 interrupts the current and raises the electrolysis voltage. Therefore, an electrode is formed in the same shape as a porous plate having an opening of 40% so that the generated gas is released to the rear surface of the anode 5 to prevent the electrolytic current from being cut off by the gas and to lower the electrolytic voltage. keep.

A perforated flat metal and an expanded metal electrode are used for the porous plate. The use of expanded metal is preferred for electrolysis of brine. The shape is selected in terms of metal consumption and cost. Distance between the anode 5 and the anode chamber partition wall 3
(D of FIG. 1) promotes the release of the gas generated at the anode 5 to the rear surface of the anode 5, so that the gas accumulation between the electrodes 5 and 14 and the cation exchange membrane 21 is alleviated to a low voltage. , If possible, it is required to be large.

Iron, nickel, or an alloy thereof is used as the material of the cathode 14. The metal is used as the cathode material so as to improve the performance, and the cathode is coated with Raney nickel, nickel oxide or the like. And
The structure of the cathode 14 may be the same as that of the above-described anode 5, and the distance between the cathode 14 and the cathode chamber partition 12 (D in FIG. 1) is preferably large for the same reason as in the case of the anode 5.
However, a minimum distance of 20 mm is required in the cathode chamber 19. This is because when D'is manufactured to be smaller than this minimum distance, the size of the gas generated at the cathode 14 when combined is 20 mm or more, so that a gas space is formed in the electrolytic cell and the electrolytic current is instantaneously generated. Is interrupted and the electrolysis voltage is increased, which is not preferable.

Gaskets 9 and 18 are provided at both ends of the cation exchange membrane 21 in order to prevent leakage of the electrolyte solution in the unit electrolytic cell. The gasket preferably has a surface as flat as possible, and a material having a chemical resistance to the electrolyte and the product may be used as the material. For example, in the case of electrolytic decomposition of salt water, ethylene-propylene rubber, chloropropylene rubber, butyl rubber, fluorine rubber and the like are preferably used. However, in terms of price and performance, gasket 9 is fluorine rubber and gasket 19 is ethylene-propylene rubber. Is preferred. The gasket shape and size shall be set under the same conditions as the electrolyte frame wall.

The cation exchange membrane 21 is the anode 5 of the anode chamber 10.
And the cathode 14 of the cathode chamber 19 are installed. A fluorine-containing resin having a cation exchanger is used as the cation exchange membrane. As the cation exchanger, a sulfo group membrane form, a carboxyl group membrane form, or a composite membrane in which these are combined is used. When a composite film is used, the sulfo group film is located on the side facing the anode 5, and the carboxyl group film is located on the side facing the cathode 14.

In the production of the electrolytic cell, the internal pressure of each unit electrolytic cell 1 is maintained above atmospheric pressure (0.2-2 kg / m ² ). The pressure change in the unit electrolytic cell 1 is adjusted by a control valve (not shown) provided in the outlet head 23.

2 and 3 are plan views of an electrolysis chamber which constitutes a unit electrolysis cell. The electric conduction plates 4 and 13 of the anode chamber 10 and the cathode chamber 19 are provided at the same position. The position of the electric conduction plate 4 along the I direction shown in FIG. 2 influences the current density distribution of the electrolytic cell, so it is necessary to install the electric conduction plate 4 at a narrow interval, but from the viewpoint of economical efficiency and electrolyte concentration distribution. 200-5
It is installed at intervals of 00 mm, more preferably at intervals of 300 mm. FIG. 3 shows another embodiment relating to the electrolysis chamber of the bipolar electrolyzer of the present invention, in which the adjacent electroconductive plates 4 ′ and 13 ′ are installed so as to be staggered so that the concentration distribution of the electrolyte is It becomes more uniform.

FIG. 4 is a side view of the anode chamber and the cathode chamber forming the unit electrolytic cell. The unit size B of the electric conductive plate 4 along the II direction marked in FIG. 2 is 100-500 mm, especially 200-.
Most preferably, it is 400 mm.

When the ratio of the unit size B of the electric conductive plate 4 and the interval A of each electric conductive plate 4 is expressed by the area ratio (A / (A + B) × 100), it is 60-80%, preferably 70%. Is. If it is less than 60%, the current density becomes non-uniform and 80%
The above is not preferable because the electrolyte concentration becomes non-uniform.

FIGS. 4A, 4B, 4C and 4D show the structure of the explosion-welded metal plate for electrically connecting the unit electrolytic cells of the present invention. The metal plate 20 is nickel 3
It is formed from 0 and the copper plate 31. This is a structure in which a copper plate 31 having a predetermined shape is connected to one end and a center or both ends of a copper plate 31 which is explosion-welded as a structure having a predetermined size and shape. In order to electrically connect the unit electrolytic cells, the metal plate 20 is positioned between the partition walls of the adjacent unit electrolytic cells 1 ′, and the nickel plate 30 of the metal plate 20 is welded to the cathode chamber partition wall 12 of the unit electrolytic cell 1. After that, the distorted copper plate 31 ′, which is compressed to the unit electrolytic cell 1 by a predetermined external force and welded to the metal plate 20, is brought into close contact with the copper plate 31 ′ that is explosion-welded to the nickel 30 of the adjacent unit electrolytic cell 1 ′. To be electrically connected to.

As shown in FIG. 4 (A), the metal plate 20 joined by explosion welding described above has a length of 100 mm and a length of 28.
A copper plate 31 having a length of 5 mm and a thickness of 1 mm and a nickel plate 30 having a length of 100 mm, a length of 28.5 mm, and a thickness of 2 mm are explosively welded together, and one side of the copper plate 31 has a width of 10 mm.
A copper plate 31 'having a length of 0 mm, a length of 240 mm, and a thickness of 1 mm was welded so as to be bonded by 1 mm, and then bent in a V shape at the center which is a 120 mm length. (A) is the copper plate 3 on both sides of the copper plate 31 of the metal plate 20 which is explosion-welded as described above.
1'was welded and bent at a predetermined position. (C)
Is a plurality of copper plates 31 ′ that are bent and bent in a diamond shape at the central point of the copper plate 31 of the metal plate 20 joined by explosion welding, and (D) is the copper plate 31 of the metal plate 20 joined by explosion welding.
A flat copper plate 31 'is welded to one side of the.

FIG. 5 shows a frame installed between the electric conductive plate and the electrode according to the present invention to provide a uniform current density to the electrode. The current flowing into the cathode frame wall 11 is the electric conduction plate 13
The current distribution frame 32 relaxes the current distribution in advance at this time, and prevents the local current density from being distributed in the film. Further, by covering a part of the inside of the electrolytic cell, the region where the gas coalesces and stagnates in the electrolytic cell is isolated from the film, and the film is protected from the influence of blistering.

To explain this in more detail, the current distribution frame
(4-5 mm) easily induces welding so that the electric current received by the electric conductive plate is uniformly distributed on the electrode surface. The size (a) of the electrically conductive plate is appropriate so as not to prevent the release of the gas released at the electrode, and this is designed based on the maximum size of the gas generated in the electrolytic cell. A suitable size can be 1-10 mm, with 4 mm being most preferred. The space (b) is formed so as to match the space between the electrically conductive plates.

In the existing electrolytic cell, an inclined frame is installed at each corner to protect the membrane to suppress the stagnation of chlorine gas in the electrolytic cell, and chlorine diffuses into the membrane to react with caustic soda.
It prevents the formation of deadly crystals in the film.
However, such a method induces an increase in the manufacturing cost of the electrolytic cell. According to the present invention, the current distribution frame covers the corner where chlorine is stagnant in the electrolytic cell, and it is not necessary to round the corner of the electrolytic cell.

[0038]

EXAMPLE A bipolar electrode type electrolytic cell having the structure shown in FIG. 1 was prepared. The size of each part is as follows. Width of anode chamber (D): 50 mm Width of cathode chamber (D '): 35 mm Vertical length of electrolysis cell: 1000 mm Horizontal length of electrolysis cell: 2000 mm Distance between electroconductive plates in electrolysis cell: 300 mm Length of electroconductive plate (B ) (See FIG. 4): 200 mm Distance between electric conductive plates (A) (See FIG. 4): 50 mm Arrangement between adjacent electric conductive plates: Formed in the form of FIG. Anode: Numerically stable electrode (material is titanium, coating is ruthenium-titanium oxide) Cathode: Active electrode (material is iron, coating is Raney nickel)

A current distribution frame as shown in FIG. 6 was set between the electric conductive plate and the electrodes. A cation exchange membrane of Napion 90209 manufactured by DuPont, USA was provided between the unit electrolytic cells. The material of the gasket provided between the electrolytic cells was 1 mm thick fluoropolymer Teflon in the anode chamber and 2 mm thick ethylene-propylene rubber in the cathode chamber.

Salt water having a concentration of 300 g / L and adjusted to pH 4 with hydrochloric acid was supplied to the anode chamber, and water was supplied to the lower portion of the cathode chamber. The operating conditions for electrolysis are as follows. Temperature: 90 ° C. Current density: 3.0 kA / ² anode chamber outlet concentration: 200 g / L cathode compartment sodium hydroxide concentration: 30% anode chamber pressure: 1.5 kg / cm ² cathode chamber pressure: 1.6 kg / cm ² above operating conditions When operated at, the cell voltage is 3.32V,
The current efficiency was 97%.

[0041]

Example 2 An electrolytic cell having the same structure as in Example 1 was prepared except that the adjacent electroconductive plates in the electrolysis chamber were arranged so as to be staggered (see FIG. 3). When operated under the same conditions as in Example 1, the cell voltage was 3.2 V and the current efficiency was 97.5%.

[0042]

As described above, the bipolar electrode electrolytic cell of the present invention is
It consists of a cathode chamber, a cation exchange membrane, and an anode chamber, and a large number of unit electrolytic cells connected by fastening means are continuously arranged by a coupling load that is not explosive welding, thus shortening the assembly and disassembly time of the electrolytic cell. it can. The labor cost is significantly reduced, and the performance of the electrolytic cell is improved by forming a large number of electrically conductive plates inside the electrolytic cell and an inclined surface at the inner end. Further, the bipolar electrode electrolytic cell of the present invention, of course, electrolyzes an alkali metal chloride to produce chlorine and an alkali metal,
It can also be used for other electrolysis such as water electrolysis.

[Brief description of drawings]

FIG. 1 is a cross-sectional view showing a continuous arrangement of unit electrolytic cells constituting a bipolar electrode electrolytic cell according to the present invention.

FIG. 2 is a plan view of an electrolysis chamber forming a unit electrolysis cell.

FIG. 3 is a plan view of another electrolyte forming a unit electrolytic cell.

FIG. 4 is a side view of an anode chamber and a cathode chamber forming a unit electrolytic cell.

FIG. 5 shows a structure of explosion-welded metal plates for electrically connecting the unit electrolytic cells.

FIG. 6 is a structure of a frame provided between an electrode and an electric conduction plate for maintaining a uniform current distribution.

[Explanation of symbols]

1: unit electrolytic cell, 2, 11: frame wall, 3: anode compartment partition wall, 1
2: Cathode chamber partition wall, 4, 13: Electric conductive plate, 5: Anode, 1
4: cathode, 6, 15: electrolyte inlet, 7, 16: product flow outlet, 8, 17: passage, 9, 18: gasket, 1
0: Anode chamber, 19: Cathode chamber, 20: Conducting medium, 21:
Cation exchange membrane, 22: supply head, 23: outlet head, 27, 28: hose, 29: binding load, 30: copper-nickel steel plate, 31: copper plate, 32: electrode current distribution frame

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Shin Ho-chul Taejeong, Yousung, Shinsung Dong 119, Taerim Tule Apartment 110-707 (72) Inventor Han Jung-hee Taejong, Tong, Tae-dong 330- 15th (72) Inventor Chae Junsung 331-2nd Suns Apartment B-407 Sansdong, Mapog, Seoul, South Korea

Claims (10)

[Claims] 1. A bipolar electrode type electrolytic cell comprising a large number of unit electrolytic cells composed of an anode chamber, a cation exchange membrane and a cathode chamber, wherein an electrolyte flows into the unit electrolytic cell 1 by a connecting means to produce a product. Electrolyte inlets 6 and 15 and product outlets 7 and 16 are provided at the upper and lower portions so as to flow out, and an inclined surface is formed at the inner end of the unit electrolytic cell 1 to prevent gas from stagnating. The partition walls 3 and 12 are fixed to the side walls, respectively, and the partition walls 3 and 12 and the anode 5 and the cathode 14 are electrically connected to each other so that the current density in the unit electrolytic cell 1 and the concentration distribution of the electrolyte are In order to maintain the uniformity, a plurality of electrically conductive plates 4 and 13 having a certain size are provided, and each unit electrolytic cell 1 is electrically connected by a large number of electrically conductive mediators 20 located between both partition walls 3 and 12. Are electrically connected, and the conductive medium 20 and the electrodes 5, 1 The unit electrolyzers in which the electrode current distribution frames 32 are installed in order to reduce the locally high current density are continuously arranged by the coupling load 23, and the explosion between the anode chamber partition wall 3 and the cathode chamber partition wall 12 occurs. A bipolar electrode type electrolytic cell, which is energized by a large number of metal plates 20 welded together. 2. The multipolar electrolytic cell according to claim 1, wherein adjacent electric conductive plates 4 and 13 are installed so as to be staggered from each other. 3. The unit size of the electrically conductive plates 4 and 13 is 2.
The bipolar electrode cell according to claim 1 or 2, which has a length of 00 mm. 4. The bipolar electrode electrolytic cell according to claim 1, wherein an inclined surface is formed at an angle of 5 ° at the inner ends of the frame walls 2 and 11. 5. The internal pressure of the unit electrolytic cell 1 is 0.2-2 kg / c.
The bipolar electrode according to claim 1, which is maintained at m ² . 6. A bipolar electrode cell according to claim 1, wherein the minimum distance D between the cathode 14 and the cathode chamber partition wall 12 is at least 20 mm. 7. A copper plate 3 which is V-shaped on one side of a copper plate 31 of a copper-nickel plate to which the metal plate 20 is explosion-welded.
1'is welded.
The described bipolar electrode electrolytic cell. 8. A copper plate 31 in which the metal plate 20 is a copper-nickel plate.
8. The bipolar electrode type electrolytic cell according to claim 7, wherein a plurality of V-shaped copper plates 31 'are welded on both sides of the bipolar plate. 9. A copper plate 31 in which the metal plate 20 is a copper-nickel plate.
The bipolar electrolytic cell according to claim 7, wherein flat copper 31 'is welded to one side of the one side. 10. A copper plate 3 in which the metal plate 20 is a copper-nickel plate.
8. The bipolar electrode type electrolytic cell according to claim 7, wherein a diamond-shaped copper plate 31 'is welded to the center of 1.