Patent Application
20200024758
One or more embodiments of the present invention relate to a method for producing sodium hydroxide and/or chlorine, and a two-chamber type electrolytic cell for saltwater.
Sodium hydrate and chlorine are essential as industrial materials. They have conventionally been produced by a method using an ion exchange membrane electrolytic cell to electrolyze saltwater, in which a metal electrode is used as a cathode and the saltwater is electrolyzed according to the reaction given by the following equation (1).
2NaCl+2H2O→Cl2+2NaOH+H2 (11)
However, since the electrolysis of saltwater according to the above equation (I) requires huge amounts of electric power, a method in which a gas-diffusion electrode is used as a cathode to reduce oxygen (hereinafter, referred to as oxygen cathode method) has been addressed in hope of significant energy saving in recent years. In the oxygen cathode method, a reaction at the anode is oxidation of chlorine ion, which is the same as in the conventional method, and as a whole, the reaction is given by the following equation (2).
2NaCl+½O2+H2O→Cl2+2NaOH (2)
In the oxygen cathode method, a three-chamber type method, in which an electrolytic cell is divided into an anode chamber, a catholyte chamber, and a cathode gas chamber, has been employed. However, in recent years, as described in Patent Document 1, for example, a two-chamber type method has been investigated, in which an electrolytic cell is divided into an anode chamber and a cathode gas chamber by making an anode, an ion exchange membrane, and a gas-diffusion cathode attached firmly to each other to eliminate a catholyte chamber substantially. As shown in the above chemical equations, water is required for electrolyzing saltwater, and at the same time, water is also required for keeping the concentration of the generated sodium hydroxide from being too high. In the three-chamber type method, the cathode chamber has a liquid chamber to circulate aqueous sodium hydroxide, from which sufficient water is supplied. On the other hand, in the two-chamber type method, since the cathode chamber does not have a liquid chamber, water is supplied through the ion exchange membrane from the anode chamber as electro-osmosis water, which is not sufficient, and water is needed to be supplied to the cathode in some way. The Patent Document 1 discloses that the shortage of water is compensated by supplying water through the gas chamber, and specifically discloses that water is heated beforehand to 90° C. and then introduced through an inlet for oxygen gas. Patent Document 2 also discloses that humidified oxygen-containing gas is supplied to the cathode chamber, and specifically discloses that the humidified oxygen-containing gas has been prepared by bubbling oxygen into water heated to 80° C. and then is introduced to the cathode chamber.
However, the method for supplying water disclosed in the Patent Document 1 and 2 requires energy to heat water to 80° C. or 90° C. In addition, in the method disclosed in the Patent Document 1, when the temperature of the electrolytic cell becomes too high, the anolyte temperature is decreased by circulating the anolyte in an external heat exchanger and using cooling water and the like, which further requires energy for preparing the cooling water.
One or more embodiments of the present invention offer a method capable of efficiently producing sodium hydroxide and/or chlorine in such a way that water is supplied to the cathode chamber and overheating of the electrolytic cell is suppressed without extra energy other than the energy for electrolytic reaction.
One or more embodiments of the present invention include the following:
[1] A method for producing sodium hydroxide and/or chlorine by electrolyzing saltwater, comprising using a two-chamber type electrolytic cell for saltwater comprising one or more unit cells equipped with an anode chamber including an anode, a cathode chamber including a gas-diffusion cathode, and an ion exchange membrane sandwiched by the anode chamber and the cathode chamber, supplying saltwater to the anode chamber, and supplying humidified oxygen-containing gas to the cathode chamber, wherein each of the unit cells further comprises a humidifying chamber generating the humidified oxygen-containing gas that is to be supplied to the cathode chamber, the humidifying chamber is adjoined to and in heat exchange relation with the anode chamber or the cathode chamber in one of the unit cells, or the anode chamber or the cathode chamber in another of the unit cells adjacent to the one of the unit cells, and the oxygen-containing gas is humidified by generating water vapor with heat from the anode chamber or the cathode chamber.
[2] The method according to [1], wherein the humidifying chamber is adjoined to the cathode chamber, and the humidified oxygen-containing gas generated in the humidifying chamber is supplied from the humidifying chamber to the cathode chamber through at least one opening located at a partition between the humidifying chamber and the cathode chamber.
[3] The method according to [2], wherein the at least one opening located at the partition between the humidifying chamber and the cathode chamber comprises a single opening.
[4] The method according to [2], wherein the at least one opening located at the partition between the humidifying chamber and the cathode chamber comprises a plurality of openings.
[5] The method according to [1], wherein the humidified oxygen-containing gas generated in the humidifying chamber is supplied from the humidifying chamber to the cathode chamber through at least one flow path located outside the humidifying chamber and the cathode chamber.
[6] The method according to [5], wherein the at least one flow path located outside the humidifying chamber and the cathode chamber comprises a single flow path.
[7] The method according to [5], wherein the at least one flow path located outside the humidifying chamber and the cathode chamber comprises a plurality of flow paths.
[8] The method according to any one of [1] to [7], wherein the unit cells are connected with each other in the electrolytic cell, and the unit cells are arranged such that the sequence of the anode chamber, the cathode chamber, and the humidifying chamber is repeated.
[9] A two-chamber type electrolytic cell for saltwater, comprising one or more unit cells equipped with an anode chamber, a cathode chamber, and an ion exchange membrane sandwiched by the anode chamber and the cathode chamber, wherein the anode chamber includes an anode, and is equipped with an inlet for saltwater as a starting material, an outlet for electrolyzed saltwater, and an outlet for chlorine, the cathode chamber includes a gas-diffusion cathode, and is equipped with an inlet for humidified oxygen-containing gas and an outlet for electrolytic reactant, each of the unit cells further comprises a humidifying chamber generating oxygen-containing gas that is to be supplied to the cathode chamber, and the humidifying chamber is adjoined to and in heat exchange contact with the anode chamber or the cathode chamber in one of the unit cells, or the anode chamber or the cathode chamber in another of the unit cells adjacent to the one of the unit cells, and is equipped with an inlet for the oxygen-containing gas.
[10] The electrolytic cell according to [9], wherein the unit cells are connected with each other in the electrolytic cell, and the unit cells are arranged such that the sequence of the anode chamber, the cathode chamber, and the humidifying chamber is repeated.
According to one or more embodiments of the present invention, since the humidifying chamber is adjoined to and in heat exchange relation with the anode chamber or the cathode chamber, the oxygen-containing gas can be humidified with heat from the anode chamber or the cathode chamber, and overheating of the electrolytic cell can be suppressed.
Hereinafter, a two-chamber type electrolytic cell for saltwater and a method for producing sodium hydroxide and/or chlorine using the electrolytic cell according to one or more embodiments of the present invention will be described with reference to the drawings. The present invention, however, is not limited by the following drawings and can be altered in design within a scope in compliance with the intent described above and below.
The unit cell 1 according to one or more embodiments of the present invention is equipped with a humidifying chamber 5 separated from the cathode chamber 4 by a partition 6, and the humidifying chamber 5 is in heat exchange relation with the cathode chamber 4. The partition 6 exemplified in the drawing has a planar shape as shown in
In one or more embodiments, water in the humidifying chamber 5 may be in communication with the outside, or may not be in communication with the outside. In cases where the water is in communication with the outside, a line can be further provided to introduce water from the outside to the humidifying chamber and to discharge heated water to the outside (not shown in the figures). In the case where the water is introduced from the outside, the flow rate and the temperature of the water can be accordingly determined such that the water temperature in the humidifying chamber satisfies the predetermined condition (for example, 80° C. or higher). However, in either case, whether the water is introduced or not introduced from the outside, the only heat produced by electrolytic reaction may be used to heat the water up to the predetermined temperature in view of energy efficiency.
In the above unit cell 1, saltwater as a starting material is supplied from the inlet 3h for saltwater to the anode chamber 3, and at the same time, oxygen-containing gas is bubbled from an inlet 5a for oxygen-containing gas into water stored in the humidifying chamber 5 to generate the humidified oxygen-containing gas (oxygen concentration may be, for example, 90% or more in some embodiments, and 93% or more in another embodiment). By supplying the humidified oxygen-containing gas to the cathode chamber 4 and applying an electrical current, chlorine is generated art the anode 3a and sodium hydroxide is generated at the gas-diffusion cathode 4a. With progression of the electrolytic reaction of saltwater, heat generated at the cathode is conducted to the humidifying chamber 5, which can heat the water stored in the humidifying chamber 5 and facilitate vaporization of the water in the humidifying chamber 5. The following supply of the oxygen-containing gas to the humidifying chamber 5 by means like bubbling can generate oxygen-containing gas including water vapor with an amount approximately equal to the saturation amount at the water temperature in the humidifying chamber. Therefore, without using extra energy other than the energy for electrolytic reaction, the efficiency of humidifying the oxygen-containing gas can be improved. Moreover, in the case where oxygen-containing gas that contains highly concentrated water vapor is supplied from a humidifier located outside the electrolytic cell, which is disclosed in the Patent Document 1, enough amount of water vapor cannot be supplied because of water condensation in a pipe during being supplied. Additionally, especially in an electrolytic cell having some unit cells, each of the unit cells may be supplied with a different amount of water because the degree of water condensation may vary in each of the unit cells. On the contrary, in one or more embodiments of the present invention, since each of the unit cells is equipped with the humidifying chamber, enough amount of water can be supplied to each of the unit cells without variation of the water amount. Furthermore, by conducting heat of the cathode chamber to the humidifying chamber, overheating of the unit cells, that is, overheating of the electrolytic cell, can be prevented without extra energy for cooling.
In the example of
In one or more embodiments, chlorine generated in the anode chamber 3 is discharged from the outlet 3c along with saltwater after electrolyzation. Sodium hydroxide generated in the cathode chamber 4 is transformed into aqueous sodium hydroxide having a concentration of about 32.0% to 34.0% with electro-osmotic water from the anode chamber 3 or moisture in the oxygen-containing gas transferred to the cathode chamber, which runs down the cathode chamber under its weight and is discharged along with exhaust gas of the oxygen-containing gas from an outlet 4g for electrolytic reactant. As described above, since enough amount of water can be supplied to the cathode in one or more embodiments of the present invention, the concentration of the aqueous sodium hydroxide can be kept from being too high, and as a result, damage of the gas-diffusion cathode 4a and the ion exchange membrane 2 can be prevented.
In one or more embodiments, the partition 6 in the unit cell 1 may have at least one opening 7 having various shapes, as long as the partition 6 allows the humidified oxygen-containing gas to be communicated from the humidifying chamber 5 to the cathode chamber 4 through an upper side of the partition 6. For example, as shown in
Moreover, in one or more embodiments, the partition 6 may not have the at least one opening 7, as long as the humidified oxygen-containing gas is allowed to be communicated from the humidifying chamber 5 to the cathode chamber 4. For example, the humidified oxygen-containing gas may be supplied to the cathode chamber 4 through an external flow path such as a connecting pipe 8 as shown in
In the case where the aforementioned B-type unit cell is used, connecting the humidifying chamber 5 and the cathode chamber 4 by the connecting pipe 8 as described above enables the humidified oxygen-containing gas to be supplied from the humidifying chamber 5 to the cathode chamber 4. In addition, in the case where more than one B-type cell is placed next to each other, to enable the oxygen-containing gas to be supplied from the humidifying chamber 5 to the cathode chamber 4 of the adjacent unit cell, the opening 7 may be formed at the boundary of the humidifying chamber 5 and the cathode chamber 4 of the adjacent unit cell, or the connecting pipe 8 may be connected to the humidifying chamber 5 and the cathode chamber 4 of the adjacent unit cell.
In the unit cell as described above (including both the A-type unit cell and the B-type unit cell; the same applies hereafter), the anode 3a is not particularly limited, as long as it is an insoluble anode used for electrolysis of saltwater. For example, the anode may be such that coating of metal oxide including ruthenium oxide, titanium oxide, iridium oxide, or platinum-group metal oxides is applied on a base substance having a mesh structure such as expanded metal or fine mesh composed of metal including titanium.
In one or more embodiments, the ion exchange membrane 2 is not particularly limited as long as it can be used for electrolysis of saltwater, and for example, it can be exemplified by a cation exchange membrane of perfluorocarbon-type, in which the ion exchange group is carboxyl acid and/or sulfonic acid.
In one or more embodiments, the gas-diffusion cathode 4a is not particularly limited as long as it can be used for electrolysis of saltwater by the oxygen cathode method, and it is exemplified by a sheet-like triple-layer electrode in which a base material such as metal mesh-like material, carbon cloth, and/or hydrophobic resin is used, a reactive layer supported by a hydrophile catalyst is jointed on one side of the base material, and a water-shedding gas-diffusion layer is jointed on the other side of the base material. The catalyst can be exemplified by silver, platinum, gold, metal oxides, and carbon. The gas-diffusion cathode may be permeable to liquid, or may not permeable to liquid.
In one or more embodiments, in the cathode chamber 4, absence of liquid between the ion exchange membrane 2 and the gas-diffusion cathode 4a makes it impossible for current to flow therebetween. While liquid can be retained between the ion exchange membrane 2 and the gas-diffusion cathode 4 by capillary action if the ion exchange membrane 2 and the gas-diffusion cathode 4 are closely attached to each other, the liquid retention layer 4b may be placed between the ion exchange membrane 2 and the gas-diffusion cathode 4a to retain liquid more certainly. The liquid retention layer 4b enables liquid such as aqueous sodium hydroxide to be uniformly retained between the ion exchange membrane 2 and the gas-diffusion cathode 4a to prevent an increase in current density and voltage. Hydrophilicity and corrosion resistance are required for the liquid retention layer because the liquid retention layer needs to retain aqueous sodium hydroxide (having a concentration of about 30% and temperature of about 80° C. to 90° C.) generated by electrolytic reaction. Therefore, carbon materials such as carbon fibers and a porous structure composed of resin may be used.
An advantage of the two-chamber type method according to one or more embodiments of the present invention is that voltage can be made small due to small electric resistance between the electrodes since the anode, the ion exchange membrane, and the cathode are adjoined to each other. To closely attach the gas-diffusion cathode 4a to the ion exchange membrane 2 (if necessary, through the liquid retention layer 4b), the cushion material 4d may be placed in a compressed state to generate reactive force, which is utilized to closely attach the gas-diffusion cathode 4a to the ion exchange membrane 2. In the two-chamber type method according to one or more embodiments of the present invention, separated by the ion exchange membrane, liquid, pressure exerted by saltwater is applied to the anode chamber, and gas pressure is applied to the cathode chamber. The reactive force of the cushion material 4d is designed in conformity with the difference between the liquid pressure and the gas pressure. Since the deeper the depth of the saltwater is, the larger the liquid pressure is, making the reactive force of the cushion material at the lower side larger than at the upper side of the cathode chamber enables pressure applied to the ion exchange membrane or the anode electrode to be uniform. As such a cushion material 4d, a coiled material or a waved mat material can be used. Since the coiled material has elasticity in the diametrical direction and generates the reactive force in the diametrical direction, the coil axis can be placed parallel to the back board of the cathode gas chamber, and the reactive force of the cushion material can be designed to be larger at the lower side than at the upper side by selecting the wire diameter of the coil, the diameter of the coil material, and the laying density of the coil. As to the waved mat material, waved demister mesh in which metal wires are stocking stitched can be used, and the reactive force of the cushion material can be designed to be larger at the lower side than at the upper side by selecting the diameter of the wires, the number of the wires, and the number of the lamination layers of the mat material.
In one or more embodiments, the gas-diffusion cathode support 4c can be placed between the cushion material 4d and the gas-diffusion cathode 4a, if necessary. The gas-diffusion cathode support 4c receives the reactive force of the cushion material 4d to allow the force to be uniformed and transmits the uniformed force to the gas-diffusion cathode 4a and the liquid retention layer 4b, and farther, the ion exchange membrane 2. As the gas-diffusion cathode support 4c, mesh materials such as a woven metal wire can be used.
Since both the cushion material 4d and the gas-diffusion cathode support 4c are placed in the cathode chamber, which is in a high corrosive environment because of high temperatures and the existence of highly concentrated oxygen and highly concentrated sodium hydroxide, nickel or nickel alloy whose nickel content is 20% by weight or more, and silver plating thereof may be used in one or more embodiments.
As the material for the walls constituting the anode chamber 3, titanium or titanium alloy whose titanium content is 20% by weight or more may be used in one or more embodiments. As the material for the walls constituting the cathode chamber 4 and the humidifying chamber 5, nickel or nickel alloy whose nickel content is 20% by weight or more, and silver plating thereof may be used.
In one or more embodiments of the present invention, more than one of the aforementioned unit cells (the A-type unit cells or the B-type unit cells) may be placed next to each other to compose the electrolytic cell. In this case, each of the unit cells may be connected in parallel electrically to compose a monopolar electrolytic cell, or each of the unit cells may be connected in series electrically to compose a bipolar electrolytic cell. Hereinafter, the monopolar electrolytic cell and the bipolar electrolytic cell will be explained referring to an example in which more than one of the A-type unit cells having the aforementioned opening 7 for the means of communication of the oxygen-containing gas between the humidifying chamber 5 and the cathode chamber 4 are placed next to each other. The following example may be applied to another example in which the connecting pipe 8 is used or in which more than one of the B-type cells are placed next to each other.
Moreover, in the case where more than one of the B-type unit cells (having the sequence of the humidifying chamber, the anode chamber, and the cathode chamber) are arranged regularly without alternately reversing the sequence of each of the unit cells to compose a bipolar electrolytic cell such as the example shown in
The present application claims priority based on Japanese Patent Application No. 2017-068057 filed on Mar. 30, 2017. All the contents described in Japanese Patent Application No. 2017-068057 filed on Mar. 30, 2017 are incorporated herein by reference.
Hereinafter, one or more embodiments of the present invention are more specifically described with reference to examples. The present invention, however, is not limited by the following examples but can also be absolutely carried out with appropriate changes to the examples within a scope in compliance with the intent described above and later, and all the changes are to be encompassed within a technical scope of the present invention.
Five of the unit cells shown in
Saltwater having a concentration of 218 g/L and a temperature of 53.8° C. was supplied to the anode chamber at the rate of 183 L/m2/h. Water was stored in the humidifying chamber, to which 1.5 times the theoretical requisite moles of oxygen-containing gas (corresponds to “oxygen-containing gas supplied to electrolytic cell” shown in the below table 1) having a temperature of 25° C. and a concentration of 93.0% was supplied by bubbling. The temperature of the humidifying chamber was 84.0° C., and therefore, at the time when being supplied to the cathode chamber, the temperature of the humidified oxygen-containing gas was about 84.0° C. The saltwater was electrolyzed at the current density of 5.65 kA/m2, and each value was measured after ten days of the electrolyzation.
Except not having the humidifying chamber in a unit cell, five of the same unit cells as Example 1 having the same material of the anode electrode, the cathode electrode, the ion exchange membrane, etc. and the same size of the cathode chamber, the anode chamber, etc. were arranged such that the sequence of the anode chamber, and the cathode chamber is repeated in this sequence, and were connected to each other in series electrically to compose a conventional bipolar two-chamber type electrolytic cell for saltwater (not shown in the figures).
Saltwater having a concentration of 219 g/L, and a temperature of 51.4° C. was supplied to the anode chamber at the rate of 183 μm2/h. The cathode chamber of each of the unit cells was connected to a humidifier prepared outside the electrolytic cell. In the humidifier, 1.5 times the theoretical requisite moles of oxygen-containing gas having a concentration of 93.0% was bubbled into the water (25° C.) in the humidifier to generate humidified oxygen-containing gas having a temperature of 25° C., which was supplied to the cathode chamber at the same temperature. The saltwater was electrolyzed at the current density of 5.65 kA/m2, and each value was measured after ten days of the electrolyzation. Being different from Example 1, Comparative Example 1 did not have the humidifying chamber in the unit cell and the humidified oxygen-containing gas was supplied from the external humidifier, and therefore, the meaning of “oxygen-containing gas supplied to electrolytic cell” and “oxygen-containing gas supplied to cathode chamber” shown in the below table 1 are identical in meaning (the same applies to the following Comparative Examples 2 to 4).
In the same manner as in Comparative Example 1 except that the water temperature of the external humidifier in Comparative Example 1 was altered to 84° C., and that humidified oxygen-containing gas generated at 84° C. was supplied to the cathode chamber at the same temperature (heat input rate to the humidifier was about 5.2 MJ/m2/h), each value was measured after ten days of the electrolyzation.
With the same composition as in Comparative Example 2, additionally, heat-retention around the pipe connecting the humidifier and the anode chamber of each of the unit cells was improved to prevent the temperature of the humidified oxygen-containing gas from decreasing, and each value was measured after ten days of the electrolyzation. The heat input rate to the humidifier was about 5.2 MJ/m2/h, which was the same as in Comparative Example 2.
The same electrolytic cell as in Example 1 was operated for 300 days, after which each value was measured.
The same electrolytic cell as in Comparative Example 1 was operated for 300 days, after which each value was measured.
The measurement results of the Examples and the Comparative Examples are shown in Table 1 and Table 2. Table 2 shows both the average value of five of the unit cells and the difference between the average value and each value of five of the unit cells in the concentration of generated sodium hydroxide and current efficiency.
+0%
In Example 1, due to the reaction heat, the temperature of the humidifying chamber was equivalent to the temperature of the anode chamber, and the concentration of generated sodium hydroxide was 32.2%, not too high, which shows that enough amount of water vapor was supplied (Table 1). In addition, variation in the concentration of generated sodium hydroxide and in current efficiency in each of five unit cells could be made small, which shows that the variation in the amount of the water vapor supplied to the anode chamber of each of the unit cells was small (Table 2). Moreover, Example 2, in which the electrolyzation was operated longer than in Example 1, showed good current efficiency of 96.3% even after 300 days, as well as good results in other values almost the same as in Example 1. Since enough amount of water vapor could be supplied in Example 2, low concentration of generated sodium hydroxide could be maintained, and since damage of the gas-diffusion cathode was prevented in Example 2, the difference in voltage of the gas-diffusion cathode after 300 days of electryzation was as small as 45 mV on average. The differences in voltage of the gas-diffusion cathode in each of the unit sells were 78 mV, 15 mV, 45 mV, 33 mV, and 54 mV respectively.
On the other hand, in Comparative Example 1, in which humidified oxygen-containing gas was supplied from the external humidifier, since the temperature of the external humidifier was 25.0° C., the pressure of water vapor in the gas was low, and the concentration of generated sodium hydroxide was as high as 34.6% which shows that the supplied amount of water vapor was insufficient (Table 1).
Comparative Example 2 was an example in which the temperature of the external humidifier was altered to 84° C. to increase the water vapor pressure in the oxygen-containing gas, which required energy to raise water temperature in the external humidifier. The average concentration of generated sodium hydroxide was 32.2% which means that enough amount of water vapor could be supplied on the average, however, as shown in Table 2, the variation in both the concentration of sodium hydroxide and current efficiency of each unit cell became large. The reason of this is considered that water was condensed in the process where the oxygen-containing gas was supplied from the external humidifier to the cathode chamber of each of the unit cells, and the degree of the condensation was different in each of the unit cells. In addition, since the oxygen-containing gas of high temperature was supplied from outside the electrolytic cell, the saltwater supplied to the anode electrode was required to have a low temperature to prevent the electrolytic cell from overheating (while the temperature of the supplied saltwater in Example 1 was 0.53.8° C., which is within the usual range of the temperature in saltwater electrolysis plants, the temperature of the supplied saltwater in Comparative Example 2 was 47.0° C.), and thus, extra energy was required for cooling the supplied saltwater.
Comparative Example 3 was an example in which heat-retention of the pipe from the external humidifier in Comparative Example 2 was improved, and required extra energy for heating in the external humidifier, which is the same as in Comparative Example 2. In Comparative Example 3, water condensation was suppressed in the pipes, and as a result, the variations in the concentration of the generated sodium hydroxide and the current efficiency of each of the unit cells could be made small, however, extra energy for cooling the supplied saltwater was required in the same manner as in Comparative Example 2.
Comparative Example 4 was an example in which the electrolytic cell was operated for 300 days in the same condition as in Comparative Example 1, and the difference in the voltage of the gas-diffusion cathode after 300 days of electrolyzation was 108 mV on average of five of the unit cells, which was much higher than in Example 2, and current efficiency was 96.0%, which was lower than in Example 2. The reason of this is considered that as the same as in Comparative Example 1, the concentration of generated sodium hydroxide was 34.6% in Comparative Example 4, which was 2% or higher than the concentration of sodium hydroxide of 32.2% in Examples 1 and 2, and as a result, the gas-diffusion cathode was damaged. The differences in voltage of the gas-diffusion cathode in each of the unit sells were 123 mV, 66 mV, 114 mV, 108 mV, and 129 mV respectively.
Although the disclosure has been described with respect to only a limited number of embodiments, those skilled in the art, having benefit of this disclosure, will appreciate that various other embodiments may be devised without departing from the scope of the present invention. Accordingly, the scope of the invention should be limited only by the attached claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2017-068057 | Mar 2017 | JP | national |
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/JP2018/010870 | Mar 2018 | US |
| Child | 16587369 | US |
