Patent Application
20130089810
The present invention relates to a gas decomposition component, an ammonia decomposition component, a power generation apparatus, and an electrochemical reaction apparatus; specifically, to a gas decomposition component that can efficiently decompose a predetermined gas, particularly, an ammonia decomposition component that can decompose ammonia, a power generation apparatus based on a gas decomposition reaction, and an electrochemical reaction apparatus.
Although ammonia is an essential compound in agriculture and industry, it is hazardous to humans and hence a large number of methods for decomposing ammonia in water and the air have been disclosed. For example, a method for removing ammonia through decomposition from water containing ammonia at a high concentration has been proposed: aqueous ammonia being sprayed is brought into contact with airflow to separate ammonia into the air and the ammonia is brought into contact with a hypobromous acid solution or sulfuric acid (Patent Literature 1). Another method has also been disclosed: ammonia is separated into the air by the same process as above and the ammonia is incinerated with a catalyst (Patent Literature 2). Another method has also been proposed: ammonia-containing wastewater is decomposed with a catalyst into nitrogen and water (Patent Literature 3). Disclosed catalysts for ammonia decomposition reactions are, for example, porous carbon particles containing a transition metal component, a manganese composition, an iron-manganese composition (Patent Literature 3); a chromium compound, a copper compound, a cobalt compound (Patent Literature 4); and platinum held in a three-dimensional network alumina structure (Patent Literature 5). Use of methods in which ammonia is decomposed by chemical reactions employing such catalysts can suppress generation of nitrogen oxides NOx. Methods have also been proposed in which manganese dioxide is used as a catalyst to thereby promote efficient thermal decomposition of ammonia at 100° C. or less (Patent Literatures 6 and 7).
In general, waste gas from semiconductor fabrication equipment contains ammonia, hydrogen, and the like. To completely remove the odor of ammonia, the amount of ammonia needs to be reduced to the ppm order. For this purpose, a method has been commonly used in which waste gas to be released from semiconductor fabrication equipment is passed through scrubbers so that water containing chemicals absorbs the hazardous gas. On the other hand, to achieve a low running cost without supply of energy, chemicals, or the like, a treatment for waste gas from semiconductor fabrication equipment has been proposed: ammonia is decomposed with a phosphoric acid fuel cell (Patent Literature 8).
As described above, ammonia can be decomposed by, for example, the method of using a chemical solution such as a neutralizing agent (PTL 1), the incineration method (PTL 2), or methods employing thermal decomposition reactions with catalysts (PTLs 3 to 7). However, these methods have problems that they require chemicals and external energy (fuel) and also require periodic replacement of the catalysts, resulting in high running costs. In addition, such an apparatus has a large size and, for example, it may be difficult to additionally install the apparatus in existing equipment in some cases.
The apparatus in which a phosphoric acid fuel cell is used to detoxify ammonia in waste gas from compound semiconductor fabrication has also a problem: since the electrolyte is liquid, the size of air-side and ammonia-side separators cannot be reduced and it is difficult to reduce the size of the apparatus.
An object of the present invention is to provide a gas decomposition component that employs an electrochemical reaction to reduce the running cost and provides a apparatus having high treatment performance; in particular, an ammonia decomposition component for ammonia; a power generation apparatus including a power generation component among the above-described decomposition components; and an electrochemical reaction apparatus.
A gas decomposition component according to the present invention is used for decomposing a gas. This component includes a cylindrical-body membrane electrode assembly (MEA) including a first electrode on an inner-surface side, a second electrode on an outer-surface side, and a solid electrolyte sandwiched between the first electrode and the second electrode; and a porous metal body that is inserted on the inner-surface side of the cylindrical-body MEA and is electrically connected to the first electrode, wherein a metal mesh sheet or metal paste is disposed between the first electrode and the porous metal body.
In the above-described configuration, the collector for the first electrode includes the metal mesh sheet or metal paste and the porous metal body. On the inner-surface side of the cylindrical-body MEA, in general, a gaseous fluid containing a gas to be detoxified such as ammonia is introduced. This gaseous fluid flows through the porous metal body. Accordingly, when the porous metal body has a low proportion of pores (porosity) and a small average pore size, though the electrical conductivity is good, the flow of the gaseous fluid is considerably hampered, resulting in an increase in the pressure loss.
When the collector is constituted by a plurality of members, it is important that the contact resistance between the members is made low. When the metal mesh sheet or metal paste is not used, the porous metal body is electrically connected to the first electrode through direct contact therebetween. The porous metal body has the shape of a sheet having a predetermined thickness; microscopically, dendritic metal forms a network structure. When the porous metal body is inserted as a first-electrode collector on the inner-surface side of the cylindrical-body MEA, the above-described sheet-shaped porous metal body is spirally wound and inserted such that the axial center of the spiral extends along the axial center of the cylindrical-body MEA. In the outer circumferential surface of the porous metal body spiral sheet, the outermost edge or the generatrix portions at predetermined positions in the spiral tend to be in contact with the inner surface of the cylinder; however, portions positioned inside relative to the above-described portions tend to be separated from the first electrode because of the shape of not a non-concentric circle but a spiral. Accordingly, a sufficiently large contact area is less likely to be achieved between the porous metal body and the first electrode. Likewise, regarding contact pressure, a sufficiently high contact pressure can be ensured in the outer edge portions, whereas the contact pressure of portions positioned inside relative to the above-described portions becomes insufficient. Accordingly, when electrical connection is established by direct contact between the porous metal body and the first electrode, the contact resistance becomes high, resulting in an increase in the electric resistance of the first-electrode collector. An increase in the electric resistance of the collector results in degradation of the electrochemical-reaction performance.
In contrast, by using the metal mesh sheet or metal paste, the contact resistance can be decreased in the following manner. (1) In the case of the metal mesh sheet, since it has the shape of a single sheet, the entire circumference of the sheet naturally comes in contact with the cylindrical inner surface of the first electrode. As a result of, for example, application of an external force for filling the cylindrical body and adjustment of increasing the amount of materials for the filling, the metal mesh sheet and the porous metal body conform to each other and protrude to the first electrode, resulting in an increase in the contact area with the first electrode. At the contact interface between the metal mesh sheet and the porous metal body, the metal dendritic structures are pressed against each other and enter each other's pores to thereby achieve contact with each other. Accordingly, a low contact resistance is maintained. (2) In the case of the metal paste, since the metal paste applied has plasticity, even in portions where the porous metal body is slightly separated from the first electrode, the metal paste fills the gaps to thereby establish electrical connection. Accordingly, low-resistance electrical connection between the first electrode and the porous metal body can be very easily established.
As described above, by using a metal mesh sheet or metal paste, the overall electric resistance of the first-electrode collector can be made low. Accordingly, even when the porous metal body is disposed not continuously but discontinuously in the direction of the axial center of the cylindrical-body MEA, a collector having a sufficiently low electric resistance can be formed. As a result, by decreasing the total length of the porous metal body, the pressure loss of the gaseous fluid passing through this portion can be made low.
Although the metal mesh sheet may be any sheet such as a woven fabric, a nonwoven fabric, or a perforated sheet, it is preferably a woven fabric in view of, for example, flexibility and uniform distribution of pore size. Preferred examples of the metal material include Ni, Ni—Fe, Ni—Co, Ni—Cr, and Ni—W. The mesh sheet may have a structure in which a plated layer is composed of such a metal. For example, an Fe woven fabric plated with Ni may be used; it forms an alloy by heating, that is, Ni—Fe alloy. In bonding of such a metal or an alloy to the first electrode, a reducing atmosphere for the metal forming the mesh sheet can be relatively easily achieved without employing very strict sealing conditions. Thus, reduction bonding can be readily performed. In particular, Ni—W and the like have excellent catalysis and can promote decomposition of, for example, ammonia.
The following configuration may be employed: the metal mesh sheet is formed by perforating a single-phase or composite-phase metal sheet or by knitting metal wires into a mesh sheet, and at least a surface layer of the metal mesh sheet does not contain Cr. In this case, a metal mesh sheet that is disposed between the first electrode and the porous metal body to decrease the contact resistance can be easily obtained. When at least the outer layer does not contain Cr, inhibition of the function of the ion-conductive ceramic in the first electrode due to Cr poisoning can be suppressed.
The metal paste preferably does not contain Cr. Cr poisoning caused by the metal paste can also be suppressed.
The porous metal body may be discontinuously disposed in a direction of an axial center of the cylindrical-body MEA.
In this case, an increase in the pressure loss of the gaseous fluid can be suppressed.
A Ni-containing alloy mesh sheet or Ni paste may be disposed between the first electrode and the porous metal body. In this case, Cr poisoning is not caused and the above-described low contact resistance can be achieved with Ni, which is excellent in heat resistance and corrosion resistance. For the above-described reason, the Ni-containing alloy is preferably Ni, Ni—Fe, Ni—Co, Ni—Cr, Ni—W, or the like.
A gas decomposition component according to another embodiment of the present invention is used for decomposing a gas. This component includes a cylindrical-body MEA including a first electrode on an inner-surface side, a second electrode on an outer-surface side, and a solid electrolyte sandwiched between the first electrode and the second electrode; and a silver-paste-coated layer formed on the first electrode or the second electrode, wherein the silver-paste-coated layer is a porous body.
In the above-described configuration, in the electrode on which the silver-paste-coated layer is formed, the silver-paste-coated layer is a porous body and hence the density of contact sites among the gas component, the ion-conductive material forming the electrode, and silver particles in the silver paste can be increased. Accordingly, (1) the silver particles exhibit catalysis to promote the decomposition reaction of the gas molecules. In addition, the silver particles serve as a good electric conductor and hence the electric resistance of the collector for the electrode coated with the silver particles can be decreased and the treatment performance of the gas decomposition can be enhanced.
The following configuration may be employed: a main portion of the electrode on which the silver-paste-coated layer is formed does not contain silver particles. In this case, the main portion of the electrode does not contain silver particles and the silver-paste-coated layer can be used instead of these silver particles. Thus, the cost efficiency can be increased.
The silver-paste-coated layer may include band-shaped wires formed in a grid pattern. In this case, the silver-paste-coated layer functions as a collector and can also exhibit catalysis that promotes the decomposition reaction of gas molecules.
The silver-paste-coated layer may be formed so as to cover an entire surface of the first electrode or the second electrode. In this case, the electric conductivity of the collector can be further increased and the catalysis that promotes decomposition of gas molecules can be enhanced.
For the electrode on the entire surface of which the silver-paste-coated layer is formed, the silver-paste-coated layer only may be used as a collector. In this case, the necessity of using another gas-permeable conductive member is eliminated and the production cost can be further decreased.
In addition to the silver-paste-coated layer, a metal mesh sheet or a metal mesh sheet plated with silver may be used as a collector for the second electrode. In this case, while the gas permeability is ensured, the current-collecting capability for the cathode can be enhanced. Although the cathode often comes in contact with oxygen and the like, the catalysis of the silver-plated layer promotes decomposition of oxygen molecules to suppress oxidation of the cathode. In addition, the silver-plated layer can cause a considerable increase in the electric conductivity. Here, although the metal mesh sheet may be any sheet such as a woven fabric, a nonwoven fabric, or a perforated sheet, it is preferably a woven fabric in view of, for example, flexibility and uniform distribution of pore size. Preferred examples of the metal material include Ni, Ni—Fe, Ni—Co, Ni—Cr, and Ni—W. As described above, the mesh sheet may have the silver-plated layer as a surface layer. For example, a Ni woven fabric plated with silver may be used. In particular, Ni—W and the like have excellent catalysis and can promote decomposition of, for example, oxygen molecules.
According to the present invention, the first electrode and/or the second electrode may be a sinter containing an ion-conductive ceramic and metal chain particles mainly containing nickel (Ni). The metal chain particles denote an elongated moniliform metal substance in which metal particles are connected together. The metal is preferably Ni, Fe-containing Ni, Ni containing a trace amount of Ti, or Fe-containing Ni containing a trace amount of Ti. When the surface of Ni or the like is oxidized, the surfaces of the metal chain particles are oxidized while the contents (portions inside the surface layers) are not oxidized and have metal conductivity. Accordingly, for example, when ions moving through the solid electrolyte are anions (the ions may be cations) and (A1) the first electrode (anode) is formed so as to contain metal chain particles, in the anode, the chemical reaction between the anions moving through the solid electrolyte and gas molecules in a gaseous fluid introduced into the anode from the outside thereof is promoted (catalysis) with the oxide layers of the metal chain particles and the chemical reaction in the anode is also promoted (promotion effect due to charges) through participation of the anions. As a result of the chemical reaction, conductivity of generated electrons can be ensured in the metal portions of the metal chain particles. As a result, the electrochemical reaction accompanying giving and receiving of charges in the anode can be promoted on the whole. When the first electrode (anode) contains metal chain particles, in the anode, cations such as protons are generated and the cations move through the solid electrolyte to the cathode to thereby similarly provide the above-described promotion effect due to charges.
Note that, prior to use, the oxide layers of the metal chain particles are formed by sintering with certainty; however, during use, the oxide layers are often eliminated by the reduction reaction. Even when the oxide layers are eliminated, the above-described catalysis is not eliminated though it may reduce. In particular, Ni that contains Fe or Ti has high catalysis in spite of the absence of the oxide layers.
(A2) When the second electrode (cathode) is formed so as to contain the metal chain particles, in the cathode, the chemical reaction of gas molecules in a gaseous fluid introduced into the cathode from the outside thereof is promoted (catalysis) with the oxide layers of the metal chain particles; and electron conductivity from the external circuit is enhanced and, through participation of the electrons, the chemical reaction in the cathode is also promoted (promotion effect due to charges). Thus, anions are efficiently generated from the molecules and can be sent to the solid electrolyte.
As with (A1), in (A2), the electrochemical reaction among cations having moved through the solid electrolyte, electrons having flowed through the external circuit, and the second gaseous fluid can be promoted. Accordingly, as in the case where the anode contains the metal chain particles, the electrochemical reaction accompanying giving and receiving of charges in the cathode can be promoted on the whole. Whether the cathode is formed so as to contain the metal chain particles or not depends on the gas to be decomposed. (A3) When the anode and the cathode are formed so as to contain the metal chain particles, the above-described effects in (A1) and (A2) can be obtained.
The metal chain particles will be described in embodiments according to the present invention below.
The rates of the above-described electrochemical reactions are often limited by the speed at which ions move through the solid electrolyte or the time for which ions move through the solid electrolyte. To increase the movement speed of ions, the gas decomposition component is generally equipped with a heating unit such as a heater and heated at a high temperature such as 600° C. to 1000° C. By the heating to a high temperature, in addition to an increase in the movement speed of ions, chemical reactions accompanying giving and receiving of charges in the electrodes can be promoted.
When the ions moving through the solid electrolyte are anions, as described above, the anions are generated by the chemical reaction in the cathode and supplied. The anions are generated in the cathode through the reaction between molecules of a fluid introduced and electrons. The generated anions move through the solid electrolyte to the anode. The electrons participating in the cathode reaction move from the external circuit (including a capacitor, a power supply, and a power consumption device) connecting the anode and the cathode. When the ions moving thorough the solid electrolyte are cations, the cations are generated by the electrochemical reaction in the anode and move through the solid electrolyte to the cathode. Electrons are generated in the anode and flow through the external circuit to the cathode and participate in the electrochemical reaction in the cathode.
The electrochemical reactions may be power generation reactions of a fuel cell or may be electrolytic reactions.
The solid electrolyte may have oxygen-ion conductivity or proton conductivity.
As for oxygen-ion conductivity, a large number of solid electrolytes are known and well-proven.
When an oxygen-ion-conductive solid electrolyte is used, for example, a reaction between electrons and oxygen molecules is caused to generate oxygen ions in the cathode, the oxygen ions move through the solid electrolyte, and the predetermined electrochemical reaction can be caused in the anode. In this case, since the speed at which the oxygen ions move through the solid electrolyte is not higher than that of protons, to achieve a decomposition capacity on the practical level, for example, the following expedients are required: a sufficiently high temperature is provided and/or the thickness of the solid electrolyte is made sufficiently small.
On the other hand, as proton-conductive solid electrolytes, barium zirconate (BaZrO3) and the like are known. When a proton-conductive solid electrolyte is used, for example, ammonia is decomposed in the anode to generate protons, nitrogen molecules, and electrons; the protons move through the solid electrolyte to the cathode and react with oxygen in the cathode to generate water (H2O). Protons are smaller than oxygen ions and hence move through the solid electrolyte at a higher speed than oxygen ions. Accordingly, at a lower heating temperature, a decomposition capacity on the practical level can be achieved.
For example, when ammonia is decomposed with a cylindrical-body MEA in which an anode is disposed inside thereof and an oxygen-ion-conductive solid electrolyte is used, a reaction of generating water is caused inside the cylindrical body (in the anode). The water takes the form of water droplets at low-temperature portions near the outlet and may cause pressure loss. In contrast, when a proton-conductive solid electrolyte is used, protons, oxygen molecules, and electrons are generated in the cathode (outside). Since the outside is substantially open, even when adhesion of water droplets occurs, pressure loss is less likely to be caused.
The porous metal body may be a metal-plated body. In this case, a porous metal body having a high porosity can be obtained and the pressure loss can be suppressed. In a metal-plated porous body, the skeleton part is formed by plating with metal (Ni). Accordingly, the thickness can be easily adjusted to be small and hence a high porosity can be easily achieved.
The following configuration may be employed: a first gaseous fluid is introduced into the first electrode, a second gaseous fluid is introduced into the second electrode, and electric power is output from the first electrode and the second electrode. In this case, the gas to be decomposed is used as fuel and the gas decomposition component constitutes a fuel cell to generate electric power.
The gas decomposition component may further include a heater, wherein the electric power is supplied to the heater. In this case, gas decomposition can be performed with high energy efficiency.
An ammonia decomposition component according to the present invention includes any one of the above-described gas decomposition components, wherein a gaseous fluid containing ammonia is introduced into the first electrode and a gaseous fluid containing oxygen molecules is introduced into the second electrode.
In this case, oxygen ions generated in the second electrode (cathode) move to the first electrode (anode); the reaction between ammonia and oxygen ions is caused in the first electrode under the catalysis due to metal chain particles and the promotion effect due to ions; and electrons generated by the reaction can be rapidly moved.
The following configuration may be employed: a third gaseous fluid is introduced into the first electrode, a fourth gaseous fluid is introduced into the second electrode, and electric power is supplied through the first electrode and the second electrode. In this case, electric power is consumed to decompose the decomposition target gas. In this case, in the gas decomposition component, electrolysis of the gas in the third and fourth gaseous fluids is performed in the first electrode and the second electrode. Depending on the electrochemical relationship between a gas to be decomposed and a gaseous fluid (NH3, volatile organic compounds (VOC), air (oxygen), H2O, or the like) supplying ions participating in the electrochemical reaction, the selection between the electrolysis and the fuel cell is determined.
A power generation apparatus according to the present invention includes any one of the above-described gas decomposition components that outputs electric power and a power-supply part that supplies the electric power to another electric apparatus. In this case, a gas decomposition component regarded as a power generation apparatus can be used to generate electric power with, for example, a combination of gases from which only emission gas placing no load on the global environment is generated.
An electrochemical reaction apparatus according to the present invention is used for fluid (gas or liquid) and includes any one of the above-described gas decomposition components. In this case, the component will be used not only in gas detoxification but also as, for example, electrodes serving as bases of apparatuses, in fuel cells and in original electrochemical reaction apparatuses employing gas decomposition, to thereby contribute to, for example, enhancement of the efficiency of electrochemical reactions, size reduction of apparatuses, and low running costs.
A gas decomposition component according to the present invention has high treatment performance and can be operated at low running cost. In particular, as a result of employing, as the first-electrode collector, the combination of the metal mesh sheet or metal paste and the porous metal body, while the electric resistance is decreased, the total length of the porous metal body can be decreased and the pressure loss of the gaseous fluid passing on the inner-surface side of the cylindrical MEA can be made low.
A gas decomposition component according to another embodiment of the present invention has high treatment performance and can be operated at low running cost. In particular, the silver-paste-coated layer is formed on the first electrode or the second electrode and it is a porous body. Accordingly, while the electric resistance is decreased, the gas decomposition reaction in the electrode can be promoted and hence a gas decomposition component and the like that have a small size and high cost efficiency can be obtained.
In the ammonia decomposition component 10, an anode (first electrode) 2 is disposed so as to cover the inner surface of a cylindrical solid electrolyte 1; a cathode (second electrode) 5 is disposed so as to cover the outer surface of the cylindrical solid electrolyte 1; thus, a cylindrical MEA 7 (1, 2, 5) is formed. The anode 2 may be referred to as a fuel electrode. The cathode 5 may be referred to as an air electrode. In general, the cylindrical body may have a winding shape such as a spiral shape or a serpentine shape; in
<Anode Collector 11>: Ni Mesh Sheet 11a/Porous Metal Body 11s/Central Conductive Rod 11k
A Ni mesh sheet 11a is in contact with the anode 2 disposed on the inner-surface side of the cylindrical MEA 7, to conduct electricity through a porous metal body 11s to a central conductive rod 11k. The porous metal body 11s is preferably a metal-plated body, which can be formed so as to have a high porosity, such as Celmet (registered trademark: Sumitomo Electric Industries, Ltd.) for the purpose of decreasing the pressure loss of an ammonia-containing gaseous fluid described below. On the inner-surface side of the cylindrical MEA, it is important that, while the overall electric resistance of the collector 11 formed of a plurality of members is made low, the pressure loss in the introduction of a gaseous fluid on the anode side is made low.
<Cathode Collector 12>: Silver-Paste-Coated Wiring 12g+Ni Mesh Sheet 12a
A Ni mesh sheet 12a is in contact with the outer surface of the cylindrical MEA 7 to conduct electricity to the external wiring. Silver-paste-coated wiring 12g contains silver serving as a catalyst for promoting decomposition of oxygen gas into oxygen ions in the cathode 5 and also contributes to a decrease in the electric resistance of the cathode collector 12. The cathode 5 may be formed so as to contain silver. However, the silver-paste-coated wiring 12g having predetermined properties in the cathode collector 12 allows passing of oxygen molecules therethrough and contact of silver particles with the cathode 5. Thus, catalysis similar to that provided by silver particles contained in the cathode 5 is exhibited. In addition, this is less expensive than the case where the cathode 5 is formed so as to contain silver particles.
While the ammonia-containing gaseous fluid passes through pores in the Ni mesh sheet 11a and the porous metal 11s, it also comes into contact with the anode 2, resulting in an ammonia decomposition reaction described below. Oxygen ions O2− are generated by an oxygen gas decomposition reaction in the cathode and pass through the solid electrolyte 1 to reach the anode 2. That is, this is an electrochemical reaction in the case where oxygen ions, which are anions, move through the solid electrolyte.
(Anode reaction): 2NH3+3O2−→N2+3H2O+6e−
Specifically, a portion of ammonia reacts: 2NH3→N2+3H2. These 3H2 react with the oxygen ions 3O2− to generate 3H2O.
The air, in particular, oxygen gas is passed through a space S and introduced into the cathode 5. Oxygen ions dissociated from oxygen molecules in the cathode 5 are sent to the solid electrolyte 1 toward the anode 2. The cathode reaction is as follows.
(Cathode reaction): O2+4e−→2O2−
As a result of the electrochemical reaction, electric power is generated; a potential difference is generated between the anode 2 and the cathode 5; current I flows from the cathode collector 12 to the anode collector 11. When a load, such as a heater 41 for heating the gas decomposition component 10, is connected between the cathode collector 12 and the anode collector 11, electric power for the heater 41 can be supplied. This supply of electric power to the heater 41 may be a partial supply. Rather, in most cases, the amount of supply from the self power generation is equal to or lower than half of the overall electric power required for the heater.
As has already been described, the key point of the gas decomposition component above is that, in the anode 2 disposed on the inner-surface side of the cylindrical MEA, while the electric resistance of the anode collector 11 is made low, the pressure loss in the gaseous fluid passing through the anode collector 11 is made low. On the cathode side, although the air does not pass through the cylinder, the key point is that the density of contact points between the air and the cathode is made high and the resistance of the cathode collector 12 is also made low.
The above-described electrochemical reaction is one in which oxygen ions, which are anions, move through the solid electrolyte 1. In another desirable embodiment according to the present invention, for example, the solid electrolyte 1 is composed of barium zirconate (BaZrO3) and a reaction is caused in which protons are generated in the anode 2 and moved through the solid electrolyte 1 to the cathode 5.
When a proton-conductive solid electrolyte 1 is used, for example, in the case of decomposing ammonia, ammonia is decomposed in the anode 2 to generate protons, nitrogen molecules, and electrons; the protons are moved through the solid electrolyte 1 to the cathode 5; and, in the cathode 5, the protons react with oxygen to generate water (H2O). Since protons are smaller than oxygen ions, they move through the solid electrolyte at a higher speed than oxygen ions. Accordingly, while the heating temperature can be decreased, the decomposition capacity on the practical level can be achieved.
In addition, the solid electrolyte I can be easily formed so as to have a thickness providing a sufficient strength.
For example, when ammonia is decomposed with a cylindrical-body MEA, an anode is disposed inside the cylindrical-body MEA, and an oxygen-ion-conductive solid electrolyte is used, a reaction generating water occurs inside the cylindrical body (in the anode). The water takes the form of water droplets at low-temperature portions near the outlet of the cylindrical-body MEA and may cause pressure loss. In contrast, when a proton-conductive solid electrolyte is used, protons, oxygen molecules, and electrons react in the cathode (outside) to generate water. Since the outside is substantially open, even when water droplets adhere to low-temperature portions near the outlet, pressure loss is less likely to be caused.
The Ni mesh sheet 11a in the anode collector 11 in
When a metal-plated body is inserted as a first-electrode collector on the inner-surface side of the cylindrical-body MEA, the above-described sheet-shaped metal-plated body is spirally wound and the metal-plated body is inserted such that the axial center of the spiral extends along the axial center of the cylindrical-body MEA. In the outer circumferential surface of the spiral sheet, the outermost edge or the generatrix portions at predetermined positions in the spiral tend to be in contact with the inner surface of the cylinder; however, portions positioned inside relative to the above-described portions tend to be separated from the first electrode because of the shape of not a non-concentric circle but a spiral. Accordingly, a sufficiently large contact area is less likely to be achieved between the porous metal body and the first electrode. Likewise, regarding contact pressure, a sufficiently high contact pressure can be ensured in the predetermined generatrix portions, whereas the contact pressure of portions positioned inside relative to the above-described portions becomes insufficient. Accordingly, when electrical connection is established by direct contact between the porous metal body and the first electrode, the contact resistance becomes high, resulting in an increase in the electric resistance of the first-electrode collector. An increase in the electric resistance of the collector results in degradation of the electrochemical-reaction performance. To make matters worse, in order to increase the contact area, the porous metal body 11s is conventionally arranged continuously over the entire length of the anode 2. This arrangement of the porous metal body 11s continuously over the entire length results in an increase in the pressure loss of the introduced gaseous fluid.
In contrast, by using the metal mesh sheet 11a, in particular, a Ni mesh sheet, the contact resistance can be decreased in the following manner. Specifically, since the Ni mesh sheet 11a has the shape of a single sheet, the entire circumference of the Ni mesh sheet 11a naturally comes in contact with the cylindrical inner surface of the first electrode.
As a result of, for example, application of an external force (compressive) for filling the cylindrical body and adjustment of increasing the amount of materials for the filling, the metal mesh sheet 11a and the metal-plated body 11s conform to each other and protrude to the anode 2, resulting in an increase in the contact area with the anode 2. At the contact interface between the metal mesh sheet 11a and the metal-plated body 11s, the metal dendritic structures are pressed against each other and enter each other's pores to thereby achieve contact with each other. Accordingly, a low contact resistance is maintained.
As described above, even when a metal-plated body Celmet (registered trademark) is used as the porous metal body 11 is, the absence of a Ni mesh sheet results in a relatively high contact resistance: the electric resistance between the cathode collector 12 and the anode collector 11 of the gas decomposition component 10 is, for example, about 4 to about 7Ω. By inserting the Ni mesh sheet 11a into this structure, the electric resistance can be decreased to about 1Ω or less, that is, decreased by a factor of about 4 or more.
From the above-described configuration in which the Ni mesh sheet 11a is used in the anode collector 11, the following findings have been revealed.
(F1) By disposing the Ni mesh sheet 11a, it will suffice that the porous metal body 11s is discontinuously disposed inside the cylindrical MEA. Thus, in the configuration illustrated in
(F2) As a result of discontinuously arranging the porous metal body 11s at intervals, pressure loss in the flow of the ammonia-containing gaseous fluid can be considerably decreased. As a result, for example, a sufficiently large amount of an ammonia-containing gaseous fluid discharged from a waste-gas unit of semiconductor fabrication equipment can be extracted without application of a large pressure difference and the electric-power cost required for extracting the gaseous fluid can be reduced.
In addition, the requirements for parts of the piping system and the gas decomposition component in view of the pressure difference can be relaxed. Thus, the cost efficiency can be enhanced and the risk of accidents due to large pressure difference or the like can also be reduced.
The material of the metal mesh sheet will be described. The metal material is not limited to Ni. Although the metal mesh sheet may be any sheet such as a woven fabric, a nonwoven fabric, or a perforated sheet, it is preferably a woven fabric in view of, for example, flexibility and uniform distribution of pore size. Preferred examples of the metal material include Ni, Ni—Fe, Ni—Co, Ni—Cr, and Ni—W. The mesh sheet may have a structure in which a plated layer is composed of such a metal or an alloy. For example, an Fe woven fabric plated with Ni may be used; it forms an alloy by heating, that is, Ni—Fe alloy. In bonding of such a metal or an alloy to the first electrode, a reducing atmosphere for the metal forming the mesh sheet can be relatively easily achieved without employing very strict sealing conditions. Thus, reduction bonding to the first electrode can be readily performed. In particular, Ni—W and the like have excellent catalysis and can promote decomposition of, for example, ammonia.
Conventionally, in general, silver particles are disposed in the cathode 5 so that catalysis by the silver particles is used to increase the decomposition rate of oxygen molecules. However, in the structure including the cathode 5 containing silver particles, the cost of the cathode 5 becomes high, resulting in a decrease in cost efficiency. Instead of forming the cathode 5 so as to contain silver particles, silver-particle wiring can be formed in the form of a silver-paste-coated layer on the outer surface of the cathode 5.
In the silver paste, it is important that the silver paste is dried or sintered so as to provide a porous structure having a high porosity.
The amount of oxygen molecules O2 supplied to the cathode 5 is preferably maximized. In addition, silver particles contained in silver paste have catalysis that promotes the cathode reaction in the cathode 5 (refer to
In addition, since the silver-paste-coated wiring 12g containing silver particles have a high conductivity, together with the Ni mesh sheet 12a, it decreases the electric resistance of the cathode collector 12. Accordingly, as described above, the silver-paste-coated wiring 12g is preferably continuously disposed in a grid pattern (in the generatrix direction and in the circular direction). The Ni mesh sheet 12a on the outer side is wound so as to be in contact with and electrically connected to the silver-paste-coated wiring 12g.
In summary, by using the silver-paste-coated wiring 12g that is porous, (1) the cathode reaction can be promoted and (2) the electric resistance of the cathode collector 12 can be decreased.
The silver-paste-coated wiring 12g may be formed so as to have the shape of bands in a grid pattern as illustrated in
When the Ni mesh sheet 12a is not omitted, in addition to the silver-paste-coated layer 12g, a metal mesh sheet or a metal mesh sheet plated with silver can be used as a collector for the cathode 5. In this case, while the gas permeability is ensured, the current-collecting capability for the cathode can be enhanced. Although the cathode often comes in contact with oxygen and the like, the catalysis of the silver-plated layer promotes decomposition of oxygen molecules to suppress oxidation of the cathode. The silver-plated layer can promote decomposition of oxygen molecules as in the case where the cathode 5 is formed so as to contain silver particles.
In addition, the silver-plated layer can cause a considerable increase in the electric conductivity. The metal mesh sheet having the silver-plated layer provides such effects and hence plays an important role.
Here, although the metal mesh sheet for the cathode 5 may be any sheet such as a woven fabric, a nonwoven fabric, or a perforated sheet, it is preferably a woven fabric in view of, for example, flexibility and uniform distribution of pore size. Preferred examples of the metal material include Ni, Ni—Fe, Ni—Co, Ni—Cr, and Ni—W. The mesh sheet may have a silver-plated layer as a surface layer. For example, a Ni woven fabric plated with silver may be used. In particular, Ni—W and the like have excellent catalysis and can promote decomposition of, for example, oxygen molecules.
The present embodiment has a feature that the MEA 7 is cylindrical and the anode collector 11 includes the central conductive rod 11k. The central conductive rod 11k is preferably formed of a metal such that at least the surface layer does not contain Cr. For example, a Ni conductive rod 11k is preferably used. This is because, when stainless steel containing Cr is employed, during the use, Cr poisoning inhibits the function of ceramic in the anode 2, such as gadolia-doped ceria (GDC). Although the diameter of the central conductive rod 11k is not particularly limited, it is preferably about 1/9 to about ⅓ of the inner diameter of the cylindrical solid electrolyte 1. For example, when the inner diameter is 18 mm, the diameter is preferably about 2 to about 6 mm. When the diameter is excessively large, the maximum gas flow rate becomes low. When the diameter is excessively small, the electric resistance becomes high, leading to a decrease in the voltage at the time of electric power generation. The porous metal body 11s having the shape of a sheet (Celmet sheet) is spirally tightly wound around the central conductive rod 11k to keep the spiral state of the porous metal body 11s. Alternatively, a start-of-winding portion of the sheet is welded to the central conductive rod 11k by resistance welding and then the sheet is spirally tightly wound to keep the spiral state. Accordingly, the electric resistance at the interface between the porous metal body 11s and the central conductive rod 11k is low. The advantages provided by use of the central conductive rod 11k are as follows.
(E1) The overall electric resistance from the anode 2 to the external wiring can be decreased. That is, a decrease in the electric resistance of the anode collector 11 is achieved.
(E2) The drawback of using the existing cylindrical MEA is that the external terminal of a collector on the inner-surface side cannot be converged to a simple and small structure. For current collection on the inner-surface side of the cylindrical MEA, a porous metal body is indispensable; an end portion of the porous metal body is less likely to be converged and a terminal portion having a small size cannot be formed. For example, when an end of the porous metal is extended to achieve electrical connection with the outside, the size of the gas decomposition component itself becomes large and the commercial value of the component is considerably degraded.
In addition, in view of pressure loss, the extension of the porous metal body is not preferable.
Furthermore, since an ammonia-containing gaseous fluid is introduced into the inside of the cylindrical MEA 7, it is important to establish, in a highly airtight manner, connection between the gaseous-fluid transfer passage and the cylindrical MEA 7 and connection between the anode collector 11 and the external wiring. At an end of the cylindrical MEA 7, both of a connection portion of the anode collector to the external wiring and a connection portion to the gaseous-fluid transfer passage are provided.
The central conductive rod 11k can be easily processed by threading, grooving, or the like. Since the central conductive rod 11k is a solid rod, it does not deform by an external stress to a degree and can stably maintain its shape. As a result, the connection portion between the anode collector 12 and the external wiring can be formed so as to have a simple and small structure.
(E3) To efficiently operate the gas decomposition component 10, it needs to be heated to 600° C. to 1000° C. The position where the heater 41 for the heating can be disposed is outside the air passage. The heat propagates from the outside to the inside of the cylindrical MEA 7 and end portions of the cylindrical MEA 7 naturally have a high temperature. To connect the external wiring and the gaseous-fluid transfer passage to such a high-temperature end portion in a highly airtight manner, in view of the above-described high temperature, a special heat-resistant resin is required. In addition, for example, corrosion caused by gas tends to proceed as the temperature increases. Accordingly, in view of corrosion resistance, a special material may be required. As a result, usable resins may be limited to very expensive resins.
In contrast, when the central conductive rod 11k is used, it is disposed at a position farthest from the heater-41-side outside and can be easily extended in the axial direction. Accordingly, at an extension position at a relatively low temperature, the electrical connection to the external wiring and the connection to the gaseous-fluid transfer passage can be achieved in a highly airtight manner. As a result, the necessity of using special resins has been eliminated and a resin having heat resistance and corrosion resistance on the ordinary level can be used. Thus, the cost efficiency can be increased and the durability can be enhanced.
In the body portion 31 of the tubular joint 30, a conductive penetration part 37c that penetrates the body portion 31 in an airtight manner is provided. To ensure the airtightness, for example, a sealing resin 38 is applied. The conductive penetration part 37c is preferably a cylindrical rod threaded for screwing a nut 39 for the purpose of ensuring electrical connection with the external wire 11e. To the intra-tube end of the conductive penetration part 37c, a conductive lead 37b is connected. Another end of the conductive lead 37b is connected to a connection plate 37a.
Electrical connection between the connection plate 37a and a tip portion 35 of the central conductive rod 11k is established by using a connection tool such as a screwdriver and tightening a screw 34 with the screwdriver inserted into a protrusion hole portion 31a of the tubular joint 30. By tightening the screw 34 with the screwdriver, the electric resistance (contact resistance) in the electrical connection between the tip portion 35 and the connection plate 37a can be substantially eliminated.
By winding an external wire 12e around the outer circumference of an end portion of the Ni mesh sheet 12a of the cathode collector 12, connection to the outside can be established. Since the cathode 5 is positioned on the outer-surface side of the cylindrical MEA 7, the establishment of the connection is less difficult than that from the anode collector 11 to the outside.
The gaseous-fluid transfer passage 45 is preferably an elastically deformable tube composed of, for example, a resin. The tube 45 is engaged around the outer circumference of the protrusion hole portion 31a and fastened with a fastener 47. As a result, a connection that is highly airtight can be obtained.
In
Hereinafter, the configuration of components will be described.
The metal of the metal chain particles 21 is preferably nickel (Ni) or iron (Fe)-containing Ni. More preferably, the metal contains Ti in a trace amount, about 2 to about 10000 ppm.
(1) Ni itself has catalysis that promotes decomposition of ammonia. When Ni contains a trace amount of Fe or Ti, the catalysis can be further enhanced. When such Ni is oxidized to form nickel oxide, the catalysis due to the elemental metals can be further enhanced. Note that the decomposition reaction of ammonia (anode reaction) is a reduction reaction; in the product to be used, Ni chain particles have oxide layers formed by sintering or the like; as a result of use of the product, the metal chain particles in the anode are also reduced and the oxide layers are eliminated. However, Ni itself certainly has catalysis. In addition, to compensate for the lack of the oxide layers, Ni may contain Fe or Ti to compensate for the degradation of the catalysis.
In addition to the catalysis, in the anode, oxygen ions are used in the decomposition reaction. Specifically, the decomposition is performed in the electrochemical reaction. In the anode reaction 2NH3+3O2−→N2+3H2O+6e−, oxygen ions contribute to a considerable increase in the decomposition rate of ammonia. (3) In the anode reaction, free electrons e− are generated. When electrons e− remain in the anode 2, the occurrence of the anode reaction is inhibited. The metal chain particles 21 have the shape of an elongated string; a content 21a covered with an oxide layer 21b is composed of a metal (Ni) serving as a good conductor. Electrons e− smoothly flow in the longitudinal direction of the string-shaped metal chain particles. Accordingly, electrons e− do not remain in the anode 2 and pass through the contents 21a of the metal chain particles 21 to the outside. The metal chain particles 21 considerably facilitate passage of electrons e−. In summary, features in an embodiment of the present invention are the following (e1), (e2), and (e3) in the anode.
(e1) promotion of decomposition reaction by nickel chain particles, Fe-containing nickel chains, or Fe- and Ti-containing nickel chain particles (high catalysis)
(e2) promotion of decomposition by oxygen ions (promotion of decomposition in electrochemical reaction)
(e3) establishment of conduction of electrons with string-shaped good conductor of metal chain particles (high electron conductivity)
These (e1), (e2), and (e3) considerably promote the anode reaction.
By simply increasing the temperature and contacting with a catalyst a gas to be decomposed, decomposition of this gas proceeds. This is disclosed in literatures and well known as described above. However, as described above, in a component constituting a fuel cell, oxygen ions supplied from the cathode 5 and through the ion-conductive solid electrolyte 1 are used in the reaction and the resultant electrons are conducted to the outside; thus, the rate of the decomposition reaction is considerably increased. A big feature of the present invention is the functions (e1), (e2), and (e3) above and a configuration providing these functions.
In the above description, the case where the solid electrolyte 1 is oxygen-ion conductive is described. Alternatively, the solid electrolyte 1 may be proton (H+)-conductive. In this case, the ion-conductive ceramic 22 in the anode 2 may be a proton-conductive ceramic, for example, barium zirconate.
When the oxygen-ion-conductive metal oxide (ceramic) in the anode 2 is SSZ, a SSZ raw-material powder has an average particle size of about 0.5 μm to about 50 μm. The mixing ratio (mol ratio) of the metal chain particles 21 whose surfaces are oxidized to SSZ 22 is in the range of 0.1 to 10. The mixture is sintered by, for example, being held in the air atmosphere at a temperature in the range of 1000° C. to 1600° C. for 30 to 180 minutes. The production method will be described below, in particular, in conjunction with the production method of the cylindrical MEA 7.
The metal chain particles 21 are preferably produced by a reduction precipitation process. This reduction precipitation process for the metal chain particles 21 is described in detail in, for example, Japanese Unexamined Patent Application Publication No. 2004-332047. The reduction precipitation process described herein employs trivalent titanium (Ti) ions as a reducing agent and precipitated metal particles (such as Ni particles) contain a trace amount of Ti. Accordingly, quantitative analysis in terms of Ti content allows identification that the particles are produced by a reduction precipitation process employing trivalent titanium ions. By changing the type of metal ions coexistent with the trivalent titanium ions, desired metal particles can be obtained; to obtain Ni particles, Ni ions are used together with the trivalent titanium ions; addition of a trace amount of Fe ions results in the formation of Ni chain particles containing a trace amount of Fe.
To form chain particles, the metal needs to be a ferromagnetic metal and also satisfy a predetermined size or more. Since Ni and Fe are ferromagnetic metals, metal chain particles can be easily formed. The requirement in terms of size needs to be satisfied during the process in which a ferromagnetic metal forms magnetic domains to cause bonding together through magnetic force and, in this bonding state, metal precipitation and subsequent growth of a metal layer are achieved to cause integration as a metal body. After metal particles having a predetermined size or more are bonded together through magnetic force, the metal precipitation continues: for example, neck portions at the boundaries between bonded metal particles grow thicker together with the other portions of the metal particles.
The metal chain particles 21 contained in the anode 2 preferably have an average diameter D of 5 nm or more and 500 nm or less, and an average length L of 0.5 μm or more and 1000 μm or less. The ratio of the average length L to the average diameter D is preferably 3 or more. Note that the metal chain particles 21 may have dimensions that do not satisfy these ranges.
The importance of the surface oxidation treatment slightly diminishes for the anode 2 because reduction is to be caused.
Hereinafter, such surface oxidation processes will be described. Three processes are preferred: (i) thermal oxidation by vapor-phase process, (ii) electrolytic oxidation, and (iii) chemical oxidation. In (i), a treatment is preferably performed in the air at 500° C. to 700° C. for 1 to 30 minutes; this is the simplest process; however, control of the thickness of the oxide film is less likely to be achieved. In (ii), the surface oxidation is achieved by anodic oxidation through application of an electric potential of about 3 V with respect to a standard hydrogen electrode; this process has a feature that the thickness of the oxide film can be controlled by changing the amount of electricity in accordance with a surface area; however, for a large area, a uniform oxide film is less likely to be formed. In (iii), the surface oxidation is achieved by immersion for about 1 to about 5 minutes in a solution in which an oxidizing agent such as nitric acid is dissolved; the thickness of the oxide film can be controlled by changing time, temperature, or the type of the oxidizing agent; however, washing the agent off is cumbersome. Although all these processes are preferred, (i) and (iii) are more preferred.
The oxide layer desirably has a thickness in the range of 1 nm to 100 nm, more preferably 10 nm to 50 nm. Note that the thickness may be out of such ranges. When the thickness of the oxide film is excessively small, catalysis is not sufficiently provided; in addition, metalization may be caused even in a slightly reducing atmosphere. On the other hand, when the thickness of the oxide film is excessively large, catalysis is sufficiently maintained; however, electron conductivity is degraded at the interface, resulting in degradation of electric power generation performance.
The cathode 5 is a sinter mainly composed of an oxygen-ion-conductive ceramic 52. In this case, preferred examples of the oxygen-ion-conductive ceramic 52 include LSM (lanthanum strontium manganite), lanthanum strontium cobaltite (LSC), and samarium strontium cobaltite (SSC).
In the cathode 5 according to the present embodiment, Ag particles are disposed in the form of the silver-paste-coated wiring 12g. In this form, the Ag particles exhibit catalysis that considerably promotes the cathode reaction: O2+4e−→2O2−. As a result, the cathode reaction can proceed at a very high rate. The Ag particles preferably have an average size of 10 nm to 100 nm.
In the above description, the case where the solid electrolyte 1 is oxygen-ion conductive is described. Alternatively, the solid electrolyte 1 may be proton (H+)-conductive. In this case, the ion-conductive ceramic 52 in the cathode 5 may be a proton-conductive ceramic, preferably barium zirconate or the like.
SSZ having an average size of about 0.5 μm to about 50 μm is preferably used. Sintering conditions are holding in the air atmosphere at a temperature in the range of 1000° C. to 1600° C. for about 30 to about 180 minutes.
Although the electrolyte 1 may be a solid oxide, molten carbonate, phosphoric acid, a solid polymer, or the like, the solid oxide is preferred because it can be used in a small size and easily handled. Preferred examples of the solid oxide 1 include oxygen-ion-conductive oxides such as SSZ, YSZ, SDC, LSGM, and GDC. Alternatively, as described above, proton-conductive barium zirconate may be used.
The porous metal body 11s, which is an important component of the collector for the anode 2 is preferably a metal-plated body. The porous metal body 11 is preferably a metal-plated porous body, in particular, a Ni-plated porous body, that is, Celmet (registered trademark) described above. The Ni-plated porous body can be formed so as to have a high porosity of, for example, 0.6 or more and 0.98 or less; thus, it can function as a component of the collector for the anode 2 serving as an inner-surface-side electrode and can also have very high gas permeability. When the porosity is less than 0.6, the pressure loss becomes high; when forced circulation employing a pump or the like is performed, the energy efficiency decreases and, for example, bending deformation is caused in ion-conductive members and the like, which is not preferable. To reduce the pressure loss and to suppress damage to ion-conductive members, the porosity is preferably 0.8 or more, more preferably 0.9 or more. On the other hand, when the porosity is more than 0.98, the electric conductivity becomes low and the current-collecting capability is degraded.
Referring to
The heater 41, which is a heating unit, may be disposed so as to bind together all the cylindrical MEAs 7 arranged in parallel. In such a configuration in which all the structures are bound together, size reduction can be achieved.
As described above, in spite of using a metal-plated body Celmet (registered trademark) as the porous metal body 11s, the contact resistance is relatively high: the electric resistance between a cathode collector 12 and the anode collector 11 of the gas decomposition component 10 is, for example, about 6Ω. In this structure, by additionally forming the Ni paste layer 11g, the electric resistance can be decreased to about 2Ω, that is, decreased by a factor of about 3. This effect of reducing electric resistance is equivalent to that of the Ni mesh sheet 11a.
Selection between the Ni paste layer 11g and the Ni mesh sheet 11a is preferably determined in consideration of, for example, cost efficiency and ease of production.
(Another Gas Decomposition Component)
Table I describes examples of other gas decomposition reactions to which a gas decomposition component according to the present invention can be applied. A gas decomposition reaction R1 is an ammonia/oxygen decomposition reaction described in the first and third embodiments. In addition, a gas decomposition component according to the present invention can be applied to all the gas decomposition reactions R2 to R8: specifically, ammonia/water, ammonia/NOx, hydrogen/oxygen/, ammonia/carbon dioxide, VOC (volatile organic compounds)/oxygen, VOC/NOx, water/NOx, and the like. In any of the reactions, the first electrode is not limited to an anode and may be a cathode. This cathode and the other electrode are made to constitute a pair.
Table I merely describes several examples of a large number of electrochemical reactions. A gas decomposition component according to the present invention is also applicable to a large number of other reactions. For example, the reaction examples in Table I are limited to examples in which oxygen-ion-conductive solid electrolytes are employed. However, as described above, reaction examples in which proton (H+)-conductive solid electrolytes are employed are also major embodiments of the present invention. Even when a proton-conductive solid electrolyte is employed, in the combinations of gases described in Table I, the gas molecules can be finally decomposed, though the ion species passing through the solid electrolyte is proton. For example, in the reaction (R1), in the case of a proton-conductive solid electrolyte, ammonia (NH3) is decomposed in the anode into nitrogen molecules, protons, and electrons; the protons move through the solid electrolyte to the cathode; the electrons move through the external circuit to the cathode; and, in the cathode, oxygen molecules, the electrons, and the protons generate water molecules. In view of the respect that ammonia is finally combined with oxygen molecules and decomposed, this case is the same as the case where an oxygen-ion solid electrolyte is employed.
The above-described electrochemical reactions are gas decomposition reactions intended for gas detoxification. There are also gas decomposition components whose main purpose is not gas detoxification. A gas decomposition component according to the present invention is also applicable to such electrochemical reaction apparatuses, such as fuel cells.
Embodiments of the present invention have been described so far. However, embodiments of the present invention disclosed above are given by way of illustration, and the scope of the present invention is not limited to these embodiments. The scope of the present invention is indicated by Claims and embraces all the modifications within the meaning and range of equivalency of the Claims.
A gas decomposition component according to the present invention can provide a apparatus in which an electrochemical reaction is used to reduce the running cost and high treatment performance can be achieved. In particular, an ammonia decomposition component having a cylindrical MEA for ammonia is small but has high treatment performance and also has high durability even in high-temperature use for ensuring treatment capacity.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2010-130552 | Jun 2010 | JP | national |
| 2010-130553 | Jun 2010 | JP | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/JP2011/062888 | 6/6/2011 | WO | 00 | 12/5/2012 |
