Patent Application
20060127718
1. Field of the Invention
The present invention relates to a fuel cell, operating method of the fuel cell, sintering furnace, and power generator. More particularly, the present invention relates to a molten carbonate fuel cell, an operation method of the fuel cell, a sintering furnace equipped with the fuel cell, and a power generator, in which a gas containing a furnace exhaust gas, as a carbon dioxide source, discharged from an industrial furnace for heating materials, a mixture of the furnace exhaust gas and a gas for cathode use or a preheated gas for cathode use, which is a gas for cathode use preheated using the furnace exhaust gas as a heating source, or the preheated gas for cathode use is used as a cathode gas of the molten carbonate fuel cell, wherein, in the case in which the furnace exhaust gas or the mixed gas is used as the cathode gas, a cathode gas with a high carbon dioxide concentration can be obtained without a process for increasing the carbon dioxide concentration, and in the case in which the preheated gas for cathode use is used, the heat of the furnace exhaust gas can be effectively reclaimed and the fuel consumption can be reduced.
2. Description of Related Art
Conventionally, oxygen and carbon dioxide contained in the air have been used as the oxygen and carbon dioxide to be supplied to the cathode side of molten carbonate fuel cells. A gas with a high carbon dioxide concentration is advantageous to activate the fuel cell reaction. For this reason, carbon dioxide in the air of which the concentration is no more than 0.03 vol % has been commonly used after increasing the concentration of carbon dioxide. For example, a method of recycling exhaust gas containing carbon dioxide generated on the anode side by the electrochemical reaction during fuel cell operation is used for concentrating carbon dioxide in the gas to be supplied to the cathode side (cathode gas). However, since the fuel cell reaction is modest immediately after startup, the amount of carbon dioxide generated in the anode side is too small to sufficiently increase the carbon dioxide concentration in the gas to be supplied to the cathode side by recycling the anode exhaust gas. A method of concentrating carbon dioxide by the pressure swing adsorption (PSA) system before supplying the cathode side involves power for compressing the air, resulting in a high energy cost. In other molten carbonate fuel cells not employing the PSA system, a part of the cell fuel is burnt at the time of startup to generate heat and carbon dioxide. The generated heat is used for heating the fuel cell unit up to the operating temperature, while the carbon dioxide is supplied to the cathode side. This method also wastes energy by burning the fuel gas (e.g. Japanese Patent Application Laid-open No. 1993-89899).
Various industrial furnaces have been used for heating a wide variety of materials in various industrial fields. The industrial furnace of the type in which a fossil fuel is burnt for heating materials generates a high temperature exhaust gas (a furnace exhaust gas) containing carbon dioxide simultaneously with generation of heat by burning a fuel. In view of the recent concern over the adverse effect of high temperature exhaust gas on the environment, effective recovery and reuse of the heat possessed by the furnace exhaust gas is a subject of interest. Furthermore, the problem of the exhaust gas containing carbon dioxide is particularly highlighted in connection with the problems associated with global warming and the like in recent years. Effectively collecting the heat in exhaust gas from industrial furnaces for reuse, while reducing the amount of carbon dioxide contained therein is strongly demanded.
On the other hand, not much effort has been directed to reclaiming heat from and reducing the amount of carbon dioxide in exhaust gas from sintering furnaces for ceramics and the like, which are comparatively small industrial furnaces. The combustion gas containing carbon dioxide used for heating sintering materials in a sintering furnace is discharged as is to the atmosphere. On the contrary, for example, a method of reclaiming heat energy of exhaust gas by returning the exhaust gas discharged from a sintering furnace to the sintering furnace has been proposed (e.g. Japanese Patent Application Laid-open No. 2002-340482). This method can reclaim part of the heat energy in exhaust gas and can reduce the total amount of fuel and, therefore, can reduce the amount of carbon dioxide generated. The amount of carbon dioxide reduction, however, is limited.
The present invention has been completed in view of the problems in the molten carbonate fuel cell in the prior art whereby extra energy is required for supplying a gas with a high carbon dioxide concentration to the cathode side and the heat in exhaust gas from furnaces can be reclaimed only insufficiently. Specifically, an object of the present invention is to provide a molten carbonate fuel cell and an operation method of the fuel cell, comprising using, as a cathode gas, a furnace exhaust gas as a carbon dioxide source discharged from an industrial furnace for heating materials, a mixture (a mixed gas) of the furnace exhaust gas and a gas for cathode use or a preheated gas for cathode use, which is a gas for cathode use preheated using the furnace exhaust gas as a heating source, or the preheated gas for cathode use. When using the furnace exhaust gas or the mixed gas as the cathode gas, a gas with a high carbon dioxide concentration can be supplied to the cathode side without using extra energy, since the furnace exhaust gas containing carbon dioxide discharged from a sintering furnace can be used without any treatment for increasing the carbon dioxide concentration. When using the preheated gas for cathode use, the heat of furnace exhaust gas can be effectively reclaimed and the fuel consumption can be reduced. Another object of the present invention is to provide a sintering furnace and a power generator comprising supplying a furnace exhaust gas containing carbon dioxide discharged from a sintering furnace or the mixed gas to the cathode side of a fuel cell without any treatment for increasing the carbon dioxide concentration, thereby ensuring supplying a gas with a high carbon dioxide concentration to the cathode side without using extra energy, or supplying the preheated gas for cathode use to the cathode side of the fuel cell, thereby ensuring effective use of the furnace exhaust gas.
The above objects can be achieved in the present invention by the following fuel cell, operation method thereof, sintering furnace, and power generator.
(1) A fuel cell comprising a cathode, an anode, and an electrolyte layer containing molten carbonate held between the cathode and the anode, a gas containing oxygen and carbon dioxide (a cathode gas) being supplied to the cathode side and a gas containing hydrogen (an anode gas) being supplied to the anode side to generate electric power, wherein the cathode gas is a gas containing a furnace exhaust gas discharged from an industrial furnace for heating materials, a mixed gas of the furnace exhaust gas and a gas for cathode use or a preheated gas for cathode use, which is a gas for cathode use preheated using the furnace exhaust gas as a heating source, or the preheated gas for cathode use, and the carbon dioxide concentration of the cathode gas is 0.1-50 vol %.
(2) The fuel cell according to (1) above, wherein, when the cathode gas contains the furnace exhaust gas or the mixed gas, the said industrial furnace is a sintering furnace for heating materials using a combustion gas generated by burning a fuel and said furnace exhaust gas is an exhaust gas of the combustion gas (combustion exhaust gas) and/or decomposition gas produced by decomposition of organic materials contained in the heated materials (decomposition exhaust gas).
(3) The fuel cell according to (2) above, wherein the fuel is a fuel containing a hydrocarbon.
(4) The fuel cell according to (3) above, wherein the fuel containing a hydrocarbon is selected from the group consisting of town gas, liquefied natural gas, LP gas, diesel fuel oil, and heavy oil.
(5) The fuel cell according to any of (1)-(4) above, wherein the cathode gas is preheated using a catalyst combustor.
(6) The fuel cell according to (5) above, wherein the heat source of the catalyst combustor is the anode exhaust gas discharged from the anode.
(7) The fuel cell according to any of (1)-(6) above, wherein, when the cathode gas contains the preheated gas for cathode use, the preheated gas for cathode use is preheated by a heat exchanger using said furnace exhaust gas as a heat source.
(8) The fuel cell according to any of (1)-(7) above, wherein the anode gas uses hydrogen contained in a reformed gas reformed in a steam reformer installed in the industrial furnace.
(9) A method for operating a fuel cell equipped with a cathode, an anode, and an electrolyte layer containing molten carbonate held between the cathode and the anode, the method comprising supplying a gas containing oxygen and carbon dioxide (a cathode gas) to the cathode side and supplying a gas containing hydrogen (an anode gas) to the anode side to generate electric power, wherein the cathode gas is a gas containing a furnace exhaust gas discharged from an industrial furnace for heating materials, a mixed gas of the furnace exhaust gas and a gas for cathode use or a preheated gas for cathode use, which is a gas for cathode use preheated using the furnace exhaust gas as a heating source, or the preheated gas for cathode use, and the carbon dioxide concentration of the cathode gas is 0.1-50 vol %.
(10) The method according to (9) above, wherein, when the cathode gas contains the furnace exhaust gas or the mixed gas, the industrial furnace is a sintering furnace for heating materials using a combustion gas generated by burning a fuel and, the furnace exhaust gas is an exhaust gas of the combustion gas (combustion exhaust gas) and/or decomposition gas produced by decomposition of organic materials contained in the heated materials (decomposition exhaust gas).
(11) The method according to (10) above, wherein the fuel is a fuel containing a hydrocarbon.
(12) The method according to (11) above, wherein the fuel containing a hydrocarbon is selected from the group consisting of town gas, liquefied natural gas, LP gas, diesel fuel oil, and heavy oil.
(13) The method according to any of (9)-(12) above, wherein the cathode gas is preheated using a catalyst combustor.
(14) The method according to (13) above, wherein the heat source of the catalyst combustor is the anode exhaust gas discharged from the anode.
(15) The method according to any of (9)-(14) above, wherein, when the cathode gas contains the preheated gas for cathode use, the preheated gas for cathode use is preheated by a heat exchanger using the furnace exhaust gas as a heat source.
(16) The method according to any of (9)-(15) above, wherein the anode gas uses hydrogen contained in a reformed gas reformed in a steam reformer installed in the industrial furnace.
(17) A sintering furnace comprising a combustor for combusting a fuel containing hydrocarbon to generate a combustion gas, a sintering furnace main body for heating and sintering materials delivered therein by the combustion gas and discharging the combustion gas and/or decomposition gas of organic substances contained in the heated materials as a furnace exhaust gas, and the fuel cell according to any of (1)-(8) above installed so that the furnace exhaust gas discharged from the sintering furnace main body is supplied to the cathode side as the cathode gas.
(18) The sintering furnace according to (17) above, further provided with a steam reformer for a steam reforming reaction producing a reformed gas containing hydrogen and carbon dioxide from hydrocarbon introduced to the furnace and steam.
(19) The sintering furnace according to (18) above, wherein the steam reformer comprises a low temperature reforming section having a metallic reactor tube or a ceramic reactor tube for causing the steam reforming reaction to occur therein and a reforming catalyst for accelerating the steam reforming reaction packed in the reactor tube and a high temperature reforming section having a ceramic reactor tube for causing the steam reforming reaction therein.
(20) The sintering furnace according to (18) or (19) above, wherein the steam reformer is installed in the sintering furnace main body and/or the furnace exhaust gas flow channel, with the low temperature reforming section being arranged in a location heated to 600-1,000° C. and the high temperature reforming section being arranged in a location heated to 1,000-1,800° C.
(21) The sintering furnace according to any of (18)-(20) above, wherein a part or the whole of hydrogen contained in the reformed gas is used as the anode gas.
(22) The sintering furnace according to any of (18)-(21) above, further provided with a hydrogen separator for selectively separating hydrogen in the reformed gas produced in the steam reformer into a hydrogen fuel containing the hydrogen as a main component and a residual gas containing carbon dioxide by introducing the reformed gas therein.
(23) The sintering furnace according to (22) above, further provided with a carbon dioxide immobilizer for immobilizing the carbon dioxide in the residual gas which is separated by the hydrogen separator and/or the carbon dioxide contained in the anode gas (anode exhaust gas) discharged from the molten carbonate fuel cell.
(24) The sintering furnace according to any of (17)-(23) above, wherein the sintering furnace main body continuously introduces materials to be heated therein and continuously carries the heated materials therefrom.
(25) The sintering furnace according to any of (17)-(24) above, wherein the materials to be heated are ceramics.
(26) The sintering furnace according to any of (17)-(25) above, wherein the materials to be heated are honeycomb structures.
(27) A power generator comprising a fuel cell having a cathode, an anode, and an electrolyte layer containing molten carbonate held between the cathode and the anode, a cathode gas supply means for supplying a gas containing oxygen and carbon dioxide (a cathode gas) to the cathode, and an anode gas supply means for supplying a gas containing hydrogen (an anode gas) to the anode to generate electric power, wherein the cathode gas supply means has a furnace exhaust gas supply means which can supply a gas discharged from an industrial furnace for heating materials and/or a supply means for gas for cathode use which can supply the gas for cathode use to the cathode, the cathode gas supplied to the cathode by the cathode gas supply means contains the furnace exhaust gas transported via the furnace exhaust gas supply means, a mixed gas of the furnace exhaust gas and the gas for cathode use sent via the supply means for gas for cathode use or the gas for cathode use, which is preheated using the furnace exhaust gas as a heat source (preheated gas for cathode use), or the preheated gas for cathode use, and the carbon dioxide concentration of the cathode gas is 0.1-50 vol %.
(28) The power generator according to (27) above, wherein, when the cathode gas contains the furnace exhaust gas or the mixed gas, the industrial furnace is a sintering furnace for heating materials using a combustion gas generated by burning a fuel and the furnace exhaust gas is an exhaust gas of the combustion gas (combustion exhaust gas) and/or decomposition gas produced by decomposition of organic materials contained in the heated materials (decomposition exhaust gas).
(29) The power generator according to (28) above, wherein the fuel is a fuel containing a hydrocarbon.
(30) The power generator according to (29) above, wherein the fuel containing a hydrocarbon is selected from the group consisting of town gas, liquefied natural gas, LP gas, diesel fuel oil, and heavy oil.
(31) The power generator according to any of (27)-(30) above, wherein the power generator is further provided with a catalyst combustor and the gas for cathode use is preheated using the catalyst combustor.
(32) The power generator according to (31) above, wherein the heat source of the catalyst combustor is the anode exhaust gas discharged from the anode.
(33) The power generator according to any of (27)-(32) above, wherein the power generator is further provided with a heat exchanger and the preheated gas for cathode use is preheated by the heat exchanger using the furnace exhaust gas as a heat source.
(34) The power generator according to any of (27)-(33) above, wherein the power generator is provided with a steam reformer and the anode gas uses hydrogen contained in a reformed gas reformed in the steam reformer.
According to the fuel cell of the present invention, when a furnace exhaust gas or a mixed gas of the furnace exhaust gas and a gas for cathode use or a preheated gas for cathode use is used as the cathode gas, the furnace exhaust gas containing carbon dioxide discharged from a sintering furnace can be used as the cathode gas for the molten carbonate fuel cell without any processing for increasing the carbon dioxide concentration. Therefore, electric power can be generated by supplying a gas with a high carbon dioxide concentration without using extra energy. When using the preheated gas for cathode use, the heat of the furnace exhaust gas can be effectively reclaimed and the fuel consumption can be reduced. According to the fuel cell operating method of the present invention, when the furnace exhaust gas or the mixed gas is used as the cathode gas, the furnace exhaust gas containing carbon dioxide discharged from a sintering furnace can be used as the cathode gas for the molten carbonate fuel cell without any processing for increasing the carbon dioxide concentration. Therefore, electric power can be generated by supplying a gas with a high carbon dioxide concentration without using extra energy. When using the preheated gas for cathode use, the heat of the furnace exhaust gas can be effectively reclaimed and the fuel consumption can be reduced. According to the sintering furnace and power plant of the present invention, when the furnace exhaust gas or the mixed gas is used as the cathode gas, the furnace exhaust gas containing carbon dioxide discharged from a sintering furnace main body can be supplied to the cathode side of the fuel cell without any processing for increasing the carbon dioxide concentration. Therefore, electric power can be generated by supplying a gas with a high carbon dioxide concentration to the cathode side of the fuel cell without using extra energy. When using the preheated gas for cathode use as the cathode gas, the heat of the furnace exhaust gas can be effectively reclaimed and the fuel consumption can be reduced.
Embodiments of the present invention are described below referring to the drawings. However, the present invention is not limited to the following embodiments. Various modifications and improvements of design may be made as appropriate based on knowledge of a person skilled in the art without departing from the scope and spirit of the present invention.
In this manner, when the furnace exhaust gas or the mixed gas is used as the cathode gas 21 in the fuel cell 1 of this embodiment, the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) containing carbon dioxide discharged from an industrial furnace (for example, a sintering furnace) can be used as the cathode gas 21 for the furl cell 1 without any processing for increasing the carbon dioxide concentration. Therefore, electric power can be generated by supplying a gas with a high carbon dioxide concentration to the cathode 2 side without using extra energy.
In this embodiment, the industrial furnace is a facility for heating materials. For instance, the sintering furnace is a facility for heating and sintering materials using combustion gas generated by burning fuel. The fuel used in the sintering furnace is preferably a fuel containing a hydrocarbon, specifically, at least one fuel selected from the group consisting of town gas, liquefied natural gas, LP gas, diesel fuel oil, and heavy oil. The term “town gas” indicates a gas containing 70-90 vol % of methane as a main component and other hydrocarbons such as ethane, propane, and butane.
In the fuel cell 1 of this embodiment, the cathode gas 21 enters a cathode gas channel 5 from the cathode gas inlet port 6 and is fed to the cathode 2, where the cathode gas 21 supplies carbon dioxide and oxygen, and is discharged via a cathode exhaust gas exit port 7 as cathode exhaust gas. The anode gas 23 enters an anode gas channel 8 from an anode gas inlet port 9 and is fed to the anode 3, where the anode gas 23 supplies hydrogen, and is discharged via an anode exhaust gas exit port 10 as anode exhaust gas. Electrons produced by the reactions in the cathode 2 and anode 3 travel from the anode 3 to the cathode 2 in the direction 25 and are used as electrical energy at a load 31. When the cathode gas 21 or anode gas 23 contains foreign matters such as dust, these foreign matters are preferably removed using a filter before these gases are sent to the cathode gas channel 5 or anode gas channel 8.
Typical reactions that take place in the fuel cell (molten carbonate fuel cell) of the present invention are as follows.
(1) On the cathode side: CO2+(1/2)O2+2e−═CO32−
(2) Carbonate ions (CO32−) are transferred to the anode side through an electrolyte layer.
(3) On the anode side: H2+CO32−═H2O+CO2+2e−
(4) When the anode gas contains CO, the following reaction takes place on the anode side. CO+H2O═CO2+H2
H2 produced in this reaction is used as the anode side H2 in the reaction (3).
As a component of the mixed gas 72a other than the furnace exhaust gas, a gas for cathode use 73 or a preheated gas for cathode use 73b is usually used as mentioned above. Since the air at room temperature is usually used as the gas for cathode use 73, the use of preheated gas for cathode use 73b, for example, which has been preheated in a heat exchanger 73a using furnace exhaust gas as a heat source is more preferable for reducing the amount of anode exhaust gas 54 which is used for heating the catalyst combustor 42a and for promoting the power generation efficiency. A gas not containing the furnace exhaust gas 72, but containing only the preheated gas for cathode use 73b may be used as the cathode gas 51. Here, the anode exhaust gas 54 is the gas discharged as a part of the fuel not consumed. Therefore, reducing the amount of anode exhaust gas results in reduction of the amount of fuel. The power generation efficiency here is a value obtained by dividing the generated electric energy by the energy of input fuel. Generation of power using a smaller amount of fuel indicates promotion of the power generation efficiency. Surplus anode exhaust gas 54 contains hydrogen and the like and, therefore, can be either used as fuel for the fuel cell or removed to outside the fuel cell unit, as required. In this instance, although the heat source (fuel) for the heat exchanger 73a is preferably the furnace exhaust gas 72 in view of the heat efficiency as mentioned above, fuel may be supplied from other sources. It is preferable to burn combustible components (hydrogen and carbon monoxide) in the anode exhaust gas 54 in the catalyst combustor 42a while introducing air therein, thereby heating the air and producing carbon dioxide necessary for the cathode 42. However, since the carbon dioxide concentration may be insufficient if only the anode exhaust gas 54 is used, part of the cathode exhaust gas 52 is preferably recycled as the cathode gas 51. When the concentration of carbon dioxide supplied to the cathode 42 is insufficient, it is desirable to increase the recycling ratio of the cathode exhaust gas to maintain a constant carbon dioxide concentration.
An anode gas 53 (indicated by numeral 23 in
In the fuel cell of this embodiment, lithium-containing nickel oxide and the like can be used as the material for the cathode. As the material for the anode, aluminum-containing nickel, chromium-containing nickel, and the like can be given. As the material for the electrolyte layer, lithium aluminate (LiAlO2) impregnated with molten carbonate can be used. Although the forms of the fuel cell, cathode, anode, and electrolyte layer are not specifically limited, a laminate made from a plate-like cathode, a plate-like anode, and a plate-like electrolyte layer held between them may be put in a cylindrical fuel cell container.
As a molten carbonate, sodium carbonate, lithium carbonate, potassium carbonate, and the like may be used either individually or as a mixture.
The fuel cell reaction temperature in the fuel cell 1 of this embodiment is preferably 500-700° C. If less than 500° C., carbonate may brought into a molten state only insufficiently, resulting in reduced conductivity. If more than 700° C., not only the amount of vaporized molten carbonate increases, resulting in a decrease in the amount of electrolyte, but also the strength of stainless steel which is the material of construction of the fuel cell unit decreases, which may result in deformation of the fuel cell.
One embodiment of the method for operating the fuel cell of the present invention is described below. The operating method of the present embodiment comprises supplying the cathode gas 21 containing carbon dioxide and oxygen to the cathode 2 side and supplying the anode gas 23 containing hydrogen to the anode 3 as shown in
In the operating method of this embodiment, the carbon dioxide concentration of the cathode gas 21 is preferably 10-45 vol %, and more preferably 20-40 vol %. If the carbon dioxide concentration is less than 0.1 vol %, the fuel cell reaction occurs only modestly; if more than 50 vol %, the amount of oxygen molecule is insufficient for producing an adequate amount of carbonate ion. The cathode gas 21 either may contain only furnace exhaust gas discharged from the sintering furnace containing carbon dioxide at a high concentration and also containing oxygen (combustion exhaust gas and/or decomposition exhaust gas) or may be a mixture of the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) and a gas for cathode use or preheated gas for cathode use. When the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) and a gas for cathode use or preheated gas for cathode use are mixed (when using a mixed gas), the ratio by volume of the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) to the gas for cathode use or preheated gas for cathode use is preferably 100:0 to 1:4. Although a cathode gas 21 with a required carbon dioxide concentration can be obtained without any processing for increasing the carbon dioxide concentration such as the concentration using the PSA method, the carbon dioxide concentration may be optimized by employing any such process for increasing the carbon dioxide concentration. In such a case, the cost for the process for increasing the carbon dioxide concentration is very small due to the use of the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) with a high carbon dioxide concentration as the cathode gas 21. The above discussion is based on the presumption that a furnace exhaust gas is used as a carbon dioxide source for the cathode gas 21. When reduction of fuel consumption by effectively reclaiming the heat of the furnace exhaust gas is more important, the cathode gas 21 may not contain the furnace exhaust gas, but may consist only of preheated gas for cathode use which has been heated using the furnace exhaust gas as a heat source.
In this manner, when the furnace exhaust gas or the mixed gas is used as the cathode gas 21 in the operating method of the fuel cell of this embodiment, the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) containing carbon dioxide discharged from a sintering furnace can be used as the cathode gas for the furl cell without any processing for increasing the carbon dioxide concentration. Therefore, electric power can be generated by supplying a gas with a high carbon dioxide concentration to the cathode side without using extra energy.
The other constitutions, use conditions, and the like in the operating method of the fuel cell of this embodiment are the same as those of the fuel cell of the present invention that have already been discussed. The same effects can be obtained by employing such constitutions, use conditions, and the like in operating the fuel cell of this embodiment.
Next, the sintering furnace of the present invention equipped with the above fuel cell (hereinafter simply referred to from time to time as “sintering furnace”) will be described. As shown in
In this manner, when using the sintering furnace of the present invention in which the sintering furnace main body is equipped with the fuel cell, the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) containing carbon dioxide discharged from the sintering furnace main body is supplied to the cathode side of the fuel cell without any processing for increasing the carbon dioxide concentration. Therefore, electric power can be generated by supplying a gas with a high carbon dioxide concentration to the cathode side without using an extra energy and, in addition, the furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) generated in the sintering furnace main body can be effectively used. Moreover, the amount of carbon dioxide discharged to the atmosphere can be reduced by immobilizing carbon dioxide contained in the anode exhaust gas of the fuel cell using a carbon dioxide immobilizer and the like.
In the sintering furnace of this embodiment, the fuel cell is equipped with a cathode 42, an anode 43, and an electrolyte layer 44 containing molten carbonate held between the cathode 42 and anode 43. A gas containing oxygen and carbon dioxide (a cathode gas 51) is supplied to the cathode 42 side and a gas containing hydrogen (an anode gas 53) is supplied to the anode 43 side to generate electric power. The constitutions, use conditions, and the like of the fuel cell are the same as those of the above-described fuel cell, and the same effects can be obtained by employing such constitutions, use conditions, and the like.
In the sintering furnace 100 of this embodiment shown in
In the sintering furnace 100 of this embodiment shown in
As shown in
In this manner, a part of the combustion heat generated in the sintering furnace main body 61 is recovered in the steam reformer 63 to produce hydrogen-containing reformed gas 82, which is used as the anode gas 53 as is or from which the hydrogen is separated by the hydrogen separator 64 to be used as the anode gas 53. The remaining gas components after having been used as the anode gas 53 are discharged as an anode exhaust gas 54. Since the anode exhaust gas 54 contains carbon dioxide, this gas may be either mixed with the cathode gas 51 or supplied to the carbon dioxide immobilizer 65 to cause the carbon dioxide to be absorbed. The furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) 72 discharged from the sintering furnace main body 61 is preferably used for supplying heat to the steam reformer 63, following which the gas is preferably used as the cathode gas 51. After having been used as the cathode gas 51, the remaining gas is discharged as a cathode exhaust gas 52.
The carbon dioxide immobilizer 65 is designed to allow sodium hydroxide as an immobilizer 88 for immobilizing carbon dioxide to be introduced therein, causing the immobilizer 88 to come in contact with a residual gas 84 thereby causing the immobilizer 88 to absorb carbon dioxide contained in the residual gas 84 to produce sodium carbonate, and discharging a waste fluid 89 containing the sodium carbonate outside. Any material that can react with or absorb carbon dioxide can be used as the immobilizer 88 without any specific limitations. For example, NaOH, Mg(OH)2, and the like can be used.
The sintering furnace 100 of this embodiment is preferably designed so that the steam reforming reaction is caused to occur in the steam reformer 63, which is installed in the sintering furnace main body 61 and in the passage of the furnace exhaust gas (combustion gas and/or decomposition exhaust gas) 72, by heating the material to be reformed 81 flowing in the steam reformer 63 with the combustion gas (furnace exhaust gas) and/or the radiant heat from the sintered material, sintering jigs, and furnace wall (the wall of exhaust gas (combustion gas and/or decomposition exhaust gas) passage) heated by the combustion gas. The resulting reformed gas 82 is supplied to the hydrogen separator 64 and separated into hydrogen fuel 83 and residual gas 84. The hydrogen fuel 83 (hydrogen fuel for anode 86) is preferably used as the anode gas 53. In this manner, high purity hydrogen can be used for the fuel cell. The reformed gas 82 may also be directly supplied to the anode 43 side as a reformed gas for anode use 82a. As the anode gas 53 supplied to the fuel cell 41, a hydrogen-containing gas for anode use 87 supplied by a hydrogen supply means (not shown) can be used. As the hydrogen supply means, a steam reforming hydrogen generator, hydrogen gas holder, hydrogen cylinder, and the like can be used.
The heat of the combustion gas can be used for the endothermic reaction of reforming raw materials in the steam reformer. In this manner, part of the heat possessed by the combustion gas which is otherwise discharged outside can be effectively recovered.
The steam reformer 63 used in the sintering furnace 100 of this embodiment is not specifically limited. Any instrument that can be installed in the sintering furnace main body 61 and in the passage of the furnace exhaust gas (combustion gas and/or decomposition exhaust gas) 72 and can allow a steam reforming reaction to occur using given heat can be used. At a temperature of less than 1000° C., such an instrument may be a reaction tube made of a metal or ceramic packed with a reforming catalyst, for example. At 1000° C. or more, a ceramic reaction tube can be used. As the steam reformer 63 comprising the above combination, a unit having a low temperature reforming section having a metallic reactor tube or a ceramic reactor tube for causing the steam reforming reaction to occur therein and a reforming catalyst for accelerating the steam reforming reaction packed in the reactor tube, and a high temperature reforming section having a ceramic reactor tube for causing the steam reforming reaction to occur therein can be given. In the above unit, the steam reformer 63 is preferably installed in the sintering furnace main body 61 and/or the furnace exhaust gas (combustion gas and/or decomposition exhaust gas) 72 flow channel, with the low temperature reforming section being arranged in the location heated to 600-1,000° C. and the high temperature reforming section being arranged in the location heated to 1,000-1,800° C. The metallic reaction tube is suitable for use at temperatures below 1,000° C. because of the heat resistance temperature that is not sufficiently high. However, the tube allows the reaction to occur efficiently due to the reforming catalyst for accelerating the steam reforming reaction packed therein. The ceramic reaction tube can allow the steam reforming reaction to occur efficiently without using a reforming catalyst, because the ceramic reaction tube can be used at a high temperature of 1000° C. or more. It is possible to use the ceramic reaction tube at temperatures below 1000° C. by packing the reforming catalyst therein.
In
The raw material to be reformed 81 supplied to the steam reformer 63 is preferably a mixture obtained by feeding hydrocarbons and steam respectively from a hydrocarbon supply means (not shown) and a steam supply means (not shown) to a mixer (not shown). Any commonly used hydrocarbon supply means can be used without specific limitations. For example, when using a town gas, hydrocarbons can be supplied from the existing gas piping. If no piping is available, a gas tank may be installed to supply hydrocarbons by piping from the tank. Other hydrocarbons such as liquefied petroleum gas and kerosene can also be supplied by installing piping in the same manner or may be supplied via piping from the locations of a storage means such as a tank, a cylinder, and the like. In this instance, liquid hydrocarbon materials are gasified by heating before feeding to the reformer. If necessary, the raw material gas pressure may be increased using a pressure pump. This is an effective way of carrying out the reaction because the reaction amount can be increased by increasing the raw material gas pressure. Any commonly used steam supply means can be used without specific limitations. For example, a commonly used boiler, an exhaust heat recovery boiler utilizing exhaust heat from a furnace or other heat sources, and the like can be mentioned.
As the material for the ceramic rector tube in the steam reformer 63, at least one ceramic selected from the group consisting of silicon nitride, silicon carbide, aluminum nitride, aluminum oxide, and zirconium oxide is preferably used. The use of such ceramics with high heat resistance ensures a steam reforming reaction at a high temperature. As examples of the material for the metallic reactor tube, SUS309, SUS310, SCH22CF (HK40), SCH24CF (H.P.), HA230, and the like can be given.
When the reactor tube is corroded by the atmosphere in the sintering furnace 100, the reactor tube is inserted into a hole bored through a heat-resistant brick so that heat is transferred to the reactor tube through the brick. Since the heat-resistant brick shuts out the corrosive gas in this configuration, the reactor tube is protected from corrosion.
As the reforming catalyst used in the steam reformer 63, a nickel catalyst, for example, Synetix catalyst manufactured by Johnson Matthey Co., is preferably used. As other effective catalysts, a nickel catalyst, a copper catalyst, a transition metal catalyst, a platinum catalyst, and the like can be given. As a preferable example of the steam reforming reaction using a nickel-containing catalyst, the ICI method in which a mixture of hydrogen (4 mols) and carbon dioxide (1 mol) is produced from methane (1 mol) and water (2 mol) by an endothermic reaction under the conditions of a temperature of 700-950° C. and pressure of 1.01×105 to 40.52×105 (N/m2) in the presence of a nickel-containing catalyst can be given.
The reaction rate of hydrocarbons and water (the ratio of the amount of hydrogen actually produced to the theoretical amount of hydrogen to be produced) in the steam reformer 63 is preferably 50 mol % or more. If less than 50 mol %, the fuel consumption may increase. The reaction rate of hydrocarbons and water is preferably as high as possible.
The hydrogen content in the reformed gas produced in the steam reformer 63 is preferably 10-80 mol %, and the carbon dioxide content is preferably 1-20 mol %.
As the hydrocarbon used as the raw material for the steam reforming reaction in the steam reformer 63, methane, ethane, propane, butane, and the like can be given. Of these, methane is preferable.
When a ceramic reactor tube 24 is used for the steam reforming reaction, hydrocarbons and water is preferably reacted at 1,000-1,800° C. to produce hydrogen and carbon dioxide.
In the sintering furnace 100 of this embodiment shown in
The hydrogen separator 64 may be integrally formed with the steam reformer 63 so that hydrogen generated in the steam reformer 63 may be selectively separated by the hydrogen separator 64 installed in the steam reformer 63 to be sent out from the steam reformer 63 for used as the hydrogen fuel 83. As the method for installing the hydrogen separator 64 in the steam reformer 63, a method of arranging a cylindrical hydrogen separator film in the steam reformer 63 and packing the cylinder with a reforming catalyst can be mentioned. In this case, since the hydrogen separator film functions as the hydrogen separator 64, the hydrogen separator 64 in effect is arranged in the steam reformer 63. Using this system, the raw material to be reformed 81 introduced into the hydrogen separator film cylinder is converted into hydrogen by the reaction catalyzed by the reforming catalyst packed in the hydrogen separator film cylinder and the generated hydrogen can be transported outside the cylinder through the hydrogen separator film. The hydrogen flowing out is used as the hydrogen fuel 83.
The hydrogen separation efficiency for separating hydrogen from reformed gas 82 using the hydrogen separator 64, in terms of (the residual amount of hydrogen in reformed gas 82: the amount of separated hydrogen), is preferably 50:50 to 1:99 (volume ratio). If less than 50:50 (volume ratio), the fuel may not be used efficiently. Although a high separation efficiency is desirable, the efficiency of 1:99 (volume ratio) is sufficient as a recovery rate of hydrogen for fuel. A higher separation efficiency may involve a cost increase.
In the sintering furnace 100 of this embodiment shown in
When a sodium hydroxide-containing substance (solution) such as the sodium hydroxide aqueous solution mentioned above is used as an immobilizing agent 88, sodium carbonate can be produced in the carbon dioxide immobilizer 65. The waste fluid 89 discharged from the carbon dioxide immobilizer 65 can be removed as a sodium carbonate-containing solution. The carbon dioxide immobilizer 65 can thus be used as a sodium carbonate production means. The carbon dioxide immobilizer 65 will now be discussed in more detail taking the case in which the carbon dioxide immobilizer 65 is used as a sodium carbonate production means.
There are no specific limitations to the structure of the container used as the carbon dioxide immobilizer 65 insofar as the container can hold an aqueous solution of sodium hydroxide to be reacted with carbon dioxide to produce sodium carbonate therein. For example, a cylindrical container having at least one introductory pipe for introducing the residual gas and sodium hydroxide and an exit for discharging the waste fluid (hereinafter referred to from time to time as “sodium carbonate-containing solution”) can be used. The shape of the container is not specifically limited. A circular cylinder, a polygonal cylinder such as a cylinder having a square base (including a box-type), a cylinder having a base with any other shape (including a box-type), and the like can be given. As required, the carbon dioxide immobilizer 65 may be equipped with a stirrer and jacket or coil for heating and cooling. Either a batch type or a semi-batch-type carbon dioxide immobilizer 65 can be used. The batch-type carbon dioxide immobilizer 65 uses one container of the above-mentioned type to react carbon dioxide with sodium hydroxide, while feeding the residual gas. When almost all sodium hydroxide has reacted, the residual gas flow is stopped and the resulting solution containing sodium carbonate is removed, whereupon sodium hydroxide is again charged to the container and feeding of the residual gas is resumed. In the semi-batch-type carbon dioxide immobilizer, two or more containers of the above-mentioned type are used. When almost all the sodium hydroxide has reacted in one of the containers, the residual gas flow is switched to another container, in which production of sodium carbonate is started, while the sodium carbonate-containing solution in the container in which almost all sodium hydroxide has reacted is discharged.
As the method for producing sodium carbonate by immobilizing carbon dioxide, a method of circulating a sodium hydroxide aqueous solution used as the immobilizing agent 88 and feeding the residual gas 84 to the circulated sodium hydroxide aqueous solution to react sodium hydroxide with carbon dioxide can be given. As the method for circulating the sodium hydroxide aqueous solution (which may also contain sodium carbonate that has been produced in the reaction), a method of discharging the sodium hydroxide aqueous solution from the container via piping and returning the discharged solution to the container can be used. In this instance, the carbon dioxide immobilizer 65 may be continuously operated by continuously feeding sodium hydroxide to the circulating system of sodium hydroxide and sodium carbonate-containing aqueous solution produced by the reaction and continuously removing a portion of the circulating sodium carbonate-containing aqueous solution from the system as a sodium carbonate-containing aqueous solution (waste fluid) 89.
When the carbon dioxide immobilizer 65 is used as a sodium carbonate production means, the carbon dioxide content in the residual gas 84 after separating hydrogen from a reformed gas 82 using the hydrogen separator 64 is preferably 15 to 99.9 wt %, and more preferably 60 wt % or more. If less than 15 wt %, impurities in the residual gas 84 increase, making it difficult to obtain high purity sodium carbonate by purifying the sodium carbonate-containing waste fluid 89 discharged from the carbon dioxide immobilizer 65.
When the residual gas 84 contains a large amount of carbon monoxide produced in the steam reformer 64 as a by-product, a carbon monoxide converter may be installed to feed the residual gas 84 thereto. A carbon monoxide converter in which the residual gas 84 controlled at a temperature of 350-360° C. is caused to come in contact with an Fe—Cr-based catalyst to convert the carbon monoxide is preferably used. In this carbon monoxide converter, the carbon monoxide is reacted with water to produce carbon dioxide and hydrogen. The carbon monoxide converter can reduce the carbon monoxide content in the residual gas 84 by converting the carbon monoxide in the residual gas 84 into carbon dioxide. The residual gas 84 with a reduced carbon monoxide content is fed to the carbon dioxide immobilizer 65. Since hydrogen is produced in addition to carbon dioxide in the carbon monoxide converter, the residual gas 84 removed from the carbon monoxide converter may be processed in a hydrogen separator to collect hydrogen, which can be used by mixing with the anode gas 53. In this instance, either a separate hydrogen separator may be installed to charge the residual gas 84 thereinto or the hydrogen separator 64 may be used, in which case a portion of the residual gas 84 may be extracted and charged into the hydrogen separator 64 together with the reformed gas 82, thus circulating a portion of the residual gas 84. The residual gas 84 with an increased carbon dioxide content as a result of carbon monoxide conversion (or the residual gas 84 removed from the hydrogen separator, when processed by the hydrogen separator) is sent to the carbon dioxide immobilizer 65.
Sodium carbonate produced in the carbon dioxide immobilizer 65 is discharged from the carbon dioxide immobilizer 65 as a waste fluid (a sodium carbonate-containing solution) 89, which is preferably purified in a sodium carbonate purification step (not shown) and removed as high purity sodium carbonate. For this purpose, the sodium carbonate content in the components excluding water from the sodium carbonate-containing solution 89 produced in the carbon dioxide immobilizer 65 is preferably 80-99.9 wt %, and more preferably 95 wt % or more. If less than 80 wt %, it may be difficult to increase the purity of the sodium carbonate obtained by the purification in the sodium carbonate purification step (not shown).
To increase the purity of sodium carbonate obtained by the purification in this manner, it is desirable to use sodium hydroxide with a high purity in the reaction with carbon dioxide using the carbon dioxide immobilizer 65. Specifically, the sodium hydroxide content in the components excluding water from the immobilizing agent 88 (the total amount of immobilizing agent 88, when the immobilizing agent 88 does not contain water) added to the carbon dioxide immobilizer 65 is preferably 80-99.9 wt %, and more preferably 95 wt % or more. If less than 80 wt %, it is difficult to increase the purity of the sodium hydroxide obtained by the purification. As the immobilizing agent 88, an aqueous solution of sodium hydroxide may be used as mentioned above, or molten sodium hydroxide may also be used. When an aqueous solution of sodium hydroxide is used as the immobilizing agent 88, the sodium hydroxide content in the aqueous solution is preferably 30-95 wt %. If less than 30%, carbon dioxide may not efficiently react due to the too low concentration of sodium hydroxide, resulting in a high carbon dioxide concentration of the gas discharged from the carbon dioxide immobilizer. If more than 95 wt %, fluidity of the aqueous solution of sodium hydroxide is impaired due to the high viscosity of the solution, which may result in difficulty in efficient reaction with carbon dioxide.
The purity of sodium carbonate obtained by purification of the sodium carbonate-containing solution 68 discharged from the carbon dioxide immobilizer 65 using a purification step (not shown) is preferably 98-99.9 wt %, and more preferably 99.0 wt % or more. Sodium carbonate with a purity of 98 wt % or more can be used in a field requiring high purity sodium carbonate such as optical glass, medical supplies, and the like. The purity of sodium carbonate as high as possible is preferable. The concentration of sodium carbonate in the total aqueous solution of sodium carbonate 89 is preferably of 60-95 wt %. If less than 60 wt %, it may be difficult to efficiently produce sodium carbonate crystals due to the low sodium carbonate concentration. If more than 95 wt %, fluidity may be impaired due to too high a concentration of the slurry of sodium carbonate crystals obtained by crystallization of the sodium carbonate.
As the purification method for the sodium carbonate-containing solution 89 discharged from the carbon dioxide immobilizer 65, a method of causing sodium carbonate crystals to deposit and separating the deposited sodium carbonate crystals from the mother liquor is preferably used. Sodium carbonate is preferably purified by a purification step (not shown) provided with a crystallizer (not shown) to deposit sodium carbonate crystals from the sodium carbonate-containing solution 89, and a filter (not shown) to separate the sodium carbonate crystals produced in the crystallizer from the mother liquor.
Next, the power generator of the present invention equipped with the above fuel cell will be described.
In the embodiment, when the cathode gas 151 is the furnace exhaust gas 172 or the mixed gas 172a, the industrial furnace is preferably a sintering furnace 100a for heating materials using a combustion gas generated by burning a fuel 171 and the furnace exhaust gas 172 is preferably an exhaust gas of the combustion gas (combustion exhaust gas) and/or decomposition gas produced by decomposition of organic materials contained in the heated materials (decomposition exhaust gas).
The fuel 171 is preferably a fuel containing a hydrocarbon.
The hydrocarbon-containing fuel 171 is preferably at least one fuel selected from the group consisting of town gas, liquefied natural gas, LP gas, diesel fuel oil, and heavy oil.
The power generator is preferably further provided with a catalyst combustor 142a and the cathode gas 151 is preferably preheated using the catalyst combustor 142a.
The heat source of the catalyst combustor 142a is preferably the anode exhaust gas 154 discharged from the anode 143.
The power generator is preferably further provided with a heat exchanger 173a and the preheated gas for cathode use 173 is preferably preheated by the heat exchanger 173a using the furnace exhaust gas 172 as a heat source.
Preferably, the power generator is further provided with a steam reformer 163 and the anode gas 153 uses hydrogen contained in the reformed gas 182 reformed in the steam reformer 163.
The other constitutions, use conditions, and the like of the power generator are the same as those of the fuel cell, the operating method of the fuel cell, and the sintering furnace that have already been discussed. For example, although not shown in
The fuel cell, operation method of the fuel cell, sintering furnace, and power generator of the present invention, in which a gas containing a furnace exhaust gas (combustion exhaust gas and/or decomposition exhaust gas) discharged from sintering furnaces in which ceramics and the like are sintered in the ceramic industry, a mixture of the furnace exhaust gas and a gas for cathode use or a preheated gas for cathode use, which is a gas for cathode use preheated using the furnace exhaust gas as a heating source, or the preheated gas for cathode use is used as a cathode gas, can supply a gas with a high carbon dioxide concentration to the cathode without a process for concentrating the carbon dioxide in the air and can effectively reclaim the heat of furnace exhaust gas, thereby reducing the fuel consumption. Therefore, the fuel cell, operation method of the fuel cell, sintering furnace, and power generator of the present invention are effectively used in the manufacture of molten carbonate fuel cells and power generators, as well as various industrial fields in which the molten carbonate fuel cell, sintering furnace, and power generator are used.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2004-359363 | Dec 2004 | JP | national |
| 2005-293545 | Oct 2005 | JP | national |
| Number | Date | Country | |
|---|---|---|---|
| 60675582 | Apr 2005 | US |
