KR102273606B1 - Fuel cell system including fuel reforming burner using high temperature combustion catalyst - Google Patents

Abstract

Disclosed is a fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst.
The present invention disclosed is a methane gas supply unit for supplying methane gas; a reforming unit reforming the methane gas supplied from the methane gas supply unit to generate hydrogen gas and supplying it; and a stack for generating electric energy through an electrochemical reaction between hydrogen supplied from the reforming unit and oxygen supplied from an oxygen supply source, wherein the reforming unit includes: a reformed fuel transfer pipe through which the reformed fuel is transferred; and a fuel reforming burner that provides a heat source to thermally reform the reformed fuel transferred to the reforming fuel transfer pipe, wherein the fuel reforming burner constitutes the lowest layer, and provides fuel gas, by-product gas, and air supplied from the supply pipe. a mixing module having a built-in mixing member for mixing; a dispersion module stacked on the top so as to communicate with the mixing module and dispersing the mixed gas mixed in the mixing module and rising; a combustion catalyst module stacked in communication with the upper part of the dispersion module and filled with a high-temperature combustion catalyst for burning the mixed gas by a catalytic reaction therein; an ignition module stacked in communication with an upper portion of the combustion catalyst module and provided with an ignition means for providing a heat source for a combustion reaction; A preheating module stacked in communication with the upper side of the ignition module and supporting the supply pipe to penetrate through the inside so that the mixed gas passing through the supply pipe is preheated by the high temperature combustion gas inside; and the reformed fuel transport pipe includes: The method further comprises: located in the preheating module to reform fuel in the reforming fuel transfer pipe by atmospheric heat in the preheating module, wherein the supply pipe includes an external supply pipe and an internal supply pipe, wherein the internal supply pipe is a preheater of the preheating module After penetrating the side horizontally, it is bent vertically downward toward the mixing member, and the end thereof further comprises positioned in the mixing barrel, wherein the external supply pipe includes: a first external supply pipe to which by-product gas and oxygen are supplied; a second external supply pipe to which fuel gas and oxygen are supplied; The first and second external supply pipes are merged into one; and a main blower is installed on the first external supply pipe to forcibly blow fuel gas, by-product gas and oxygen, and the first external supply pipe A sub blower is installed to replace the main blower, and the sub blower further comprises an auxiliary supply pipe connected to the first external supply pipe between the main blower and a second external supply pipe as a medium. .

Description

Fuel cell system including fuel reforming burner using high temperature combustion catalyst

The present invention relates to a fuel cell system, and more particularly, since the combustion temperature can be lowered in the combustion stage by preheating by the atmospheric temperature in the burner before fuel gas is burned, fuel cost can be reduced, and It relates to a fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst capable of saving energy according to the recycling of resources by recovering the reacted gas and re-injecting it into the fuel reforming burner.

A fuel cell is a power generation system that directly converts chemical energy into electrical energy through a chemical reaction with oxygen using hydrogen contained in hydrocarbon-based substances such as methanol, ethanol, and natural gas.

The polymer electrolyte membrane fuel cell (PEMFC) system is a high-efficiency, next-generation distributed power generation system that produces electricity and heat through an electrochemical reaction between hydrogen and air. Such a fuel cell system includes a fuel cell stack and a fuel processing device as main parts, and includes a fuel tank, a fuel pump, and the like as ancillary parts.

The fuel cell stack has a structure in which several to tens of unit cells composed of a membrane electrode assembly (MEA) and a separator are stacked.

The fuel processing apparatus includes a fuel reformer, a shift reactor, and a CO remover. Hydrogen generated in the fuel processing unit is supplied to the anode electrode of the PEMFC stack, meets with oxygen supplied to the cathode electrode, and undergoes an electrochemical reaction to produce electricity in the stack.

Since the reforming reaction in the fuel reformer is performed at a high temperature, the fuel processing apparatus includes a fuel reformer burner as a means for supplying necessary heat.

A fuel reformer burner basically burns fuel gas to generate heat. At this time, the fuel gas is mainly hydrocarbon gas such as city gas mainly composed of methane gas. However, in order to improve the efficiency of the PEMFC system, the burner must be capable of not only burning fuel gas, such as hydrocarbon, but also hydrogen gas. In other words, a means for burning the hydrogen gas contained in the anode off gas (AOG) that is not reacted and discharged from the PEMFC stack must be essentially provided. The hydrogen gas utilization rate in the PEMFC stack is generally about 70 to 85%, and the remaining unreacted residual hydrogen fuel is thrown out of the stack, so there is a problem in that resources are wasted.

In addition, the conventional fuel reformer burner uses a flame burner, which has the advantage of easy fuel supply and excellent efficiency. In addition, since the emission of harmful gas is relatively small, it is widely used in various places. However, in the case of a flame burner, since it is difficult to control the flame temperature above 1,000°C, there is a disadvantage in that NOx and CO are discharged more than the standard value.

In addition, since normal gas fuel goes through the combustion process without preheating, it consumes a lot of fuel, and forced blowing is performed so that the gas fuel can reach the combustion region, so the air flow rate is irregular and the combustion efficiency is lowered due to concentrated blowing. there was.

Document 1: Registered Patent Publication No. 1015506 (2011.02.10, registered) Document 2: Registered Patent Publication No. 1305805 (2013.09.02, registered)

The present invention is to solve the problems of the prior art described above, and an object of the present invention is to recover hydrogen gas that is not used in a stack and use it as a fuel for a fuel reforming burner. An object of the present invention is to provide a fuel cell system including a fuel reforming burner using a combustion catalyst.

Another object of the present invention is that fuel cost can be reduced because the combustion temperature can be lowered in the combustion stage as the mixed gas used as fuel is preheated by the atmospheric temperature in the stove before being burned, and the temperature is increased by preheating. An object of the present invention is to provide a fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst, which is characterized in that the gas is naturally raised by the rising air flow and combusted so that constant and stable combustion is possible.

The technical problems to be achieved by the present invention are not limited to the technical problems mentioned above, and other technical problems not mentioned can be clearly understood by those of ordinary skill in the art to which the present invention belongs from the following description. There will be.

The present invention according to the above object, a methane gas supply unit for supplying methane gas; a reforming unit reforming the methane gas supplied from the methane gas supply unit to generate hydrogen gas and supplying it; and a stack for generating electric energy through an electrochemical reaction between hydrogen supplied from the reforming unit and oxygen supplied from an oxygen supply source, wherein the reforming unit includes: a reformed fuel transfer pipe through which the reformed fuel is transferred; and a fuel reforming burner that provides a heat source for thermally reforming the reformed fuel transferred to the reforming fuel transfer pipe, wherein the fuel reforming burner constitutes the lowest layer and provides fuel gas, by-product gas and air supplied from the supply pipe. a mixing module having a built-in mixing member for mixing; a dispersion module stacked on the top so as to communicate with the mixing module and dispersing the mixed gas mixed in the mixing module and rising; a combustion catalyst module stacked in communication with the upper part of the dispersion module and filled with a high-temperature combustion catalyst for burning the mixed gas by a catalytic reaction therein; an ignition module stacked in communication with an upper portion of the combustion catalyst module and provided with an ignition means for providing a heat source for a combustion reaction; A preheating module stacked in communication with the upper side of the ignition module and supporting the supply pipe to penetrate through the inside so that the mixed gas passing through the supply pipe is preheated by the high temperature combustion gas inside; and the reformed fuel transport pipe includes: The method further comprises: located in the preheating module to reform fuel in the reforming fuel transfer pipe by atmospheric heat in the preheating module, wherein the supply pipe includes an external supply pipe and an internal supply pipe, wherein the internal supply pipe is a preheater of the preheating module After penetrating the side horizontally, it is bent vertically downward toward the mixing member, and the end thereof further comprises positioned in the mixing barrel, wherein the external supply pipe includes: a first external supply pipe to which by-product gas and oxygen are supplied; a second external supply pipe to which fuel gas and oxygen are supplied; The first and second external supply pipes are merged into one; and a main blower is installed on the first external supply pipe to forcibly blow fuel gas, by-product gas and oxygen, and the first external supply pipe a sub blower for replacing the main blower is installed, the sub blower being installed between the main blower and a second external supply pipe through an auxiliary supply pipe connected to the first external supply pipe as a medium is provided

Preferably, the unreacted gas in the stack may be recovered through a supply pipe of the fuel reforming burner and recycled as fuel.

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Preferably, an exhaust pipe for exhausting combustion gas to the outside may be connected to the upper side of the preheating module.

Preferably, each of the modules may be joined by a flange joint.

Preferably, the ignition means may be any one of a spark-type ignition rod, a pilot burner, and an electric heater.

Preferably, the high-temperature combustion catalyst contains a nitrate transition metal, an alkaline earth nitrate metal and aluminum nitrate, wherein the alkaline earth nitrate metal may include at least one of calcium, strontium, barium or radium.

Preferably, the molar ratio of transition metal nitrate/alkaline earth nitrate/aluminum nitrate is (1-x)/(1-y)/11, wherein x is a number in the range of 0.1 to 0.5, and y is 0.1 to 0.5 It can be any number of ranges.

According to an embodiment of the present invention, it is possible to increase the efficiency of effective resources by recovering hydrogen gas that is not used and discarded in the stack and utilizes it as a fuel for a fuel reforming burner.

In addition, the supply pipe to which the mixed gas is supplied is configured to pass through the inside of the stove so that the mixed gas is preheated by the atmospheric temperature in the stove before combustion, so that the combustion temperature can be lowered in the combustion stage, thereby reducing fuel costs. have.

In addition, since the mixed gas whose temperature has been raised by preheating is burned while rising by the convection action, there is an advantage that consistent and stable combustion is possible compared to combustion by forced air.

It should be understood that the effects of the present invention are not limited to the above-described effects, and include all effects that can be inferred from the configuration of the invention described in the detailed description or claims of the present invention.

1 is a block diagram of a fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst according to the present invention;
2 is a detailed configuration diagram of a fuel reforming burner according to the present invention;
3 is an operation state diagram showing the flow of mixed gas in the fuel reforming burner according to the present invention by an arrow;

The present invention may be embodied in several different forms, and thus is not limited to the embodiments described herein. And in order to clearly explain the present invention in the drawings, parts irrelevant to the description are omitted, and similar reference numerals are given to similar parts throughout the specification.

Throughout the specification, when a part is said to be “connected (connected, contacted, coupled)” with another part, it is not only “directly connected” but also “indirectly connected” with another member interposed therebetween. "Including cases where In addition, when a part "includes" a certain component, this means that other components may be further provided without excluding other components unless otherwise stated.

The terms used herein are used only to describe specific embodiments, and are not intended to limit the present invention. The singular expression includes the plural expression unless the context clearly dictates otherwise. In this specification, terms such as "comprises" or "have" are intended to designate that the features, numbers, steps, operations, components, parts, or combinations thereof described in the specification exist, but one or more other features It should be understood that this does not preclude the existence or addition of numbers, steps, operations, components, parts, or combinations thereof.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a block diagram of a fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst according to the present invention.

Referring to FIG. 1 , the fuel cell system according to the present invention _{generates hydrogen gas by reforming a methane gas supply unit 200 for supplying methane gas (CH 4} ), and the methane gas supplied from the methane gas supply unit. It may be composed of a reforming unit 300 for supplying, and a stack 400 for generating electric energy through an electrochemical reaction between hydrogen supplied from the reformer and oxygen supplied from an oxygen source.

here. Considering that the reforming reaction in the reformer 300 is performed at a high temperature, the reformed fuel transfer pipe 310 through which the reformed fuel is transferred and the reformed fuel transferred to the reformed fuel transfer pipe are thermally reformed by heating. It may be composed of a fuel reforming burner 100 that provides a heat source for this purpose.

As shown in FIGS. 2 and 3 , the fuel reforming burner 100 includes a mixing module 120 , a dispersion module 130 , a combustion catalyst module 140 , an ignition module 150 , and a preheating module 160 . can do. Here, each module may be provided, for example, in the form of a square box, and each module may be stacked and coupled by a flange joint, so that the stacking configuration of the module may be changed as needed, and it is also useful when exchanging a specific module.

The mixing module 120 serves to mix fuel gas, by-product gas, and air (oxygen) supplied from the supply pipe 110 , and constitutes the lowermost layer of the fuel reforming burner 100 .

The mixing module 120 may include a mixing barrel 121 and a mixing member 122 installed on the inner bottom surface of the mixing barrel. Here, the mixing member 122 may be shaped like a steel wool brush in which iron threads are tangled. In this case, the fuel gas discharged from the supply pipe 110 is mixed and dispersed while passing through the irregular flow path of the iron scrubber.

In the mixing module 120 , an undescribed reference numeral 123 denotes a drain valve for draining the condensed water accumulated in the mixing barrel 121 to the outside, and 124 denotes a mixed gas in the mixing barrel 121 to the outside in an emergency It is an air vent valve for exhaust to the

The dispersing module 130 serves to disperse the mixed gas that is mixed in the mixing module and rises while being stacked on top to communicate with the mixing module 120. In this embodiment, the dispersing module 130 ) may be composed of a distribution tube 131 and a mesh-shaped distribution member 132 installed in the distribution tube.

The combustion catalyst module 140 is stacked in communication with the upper portion of the dispersion module 130 , and a high-temperature combustion catalyst 141 for burning the mixed gas by a catalytic reaction may be filled therein.

The volume of the combustion catalyst module 140 is variable depending on the filling amount of the high-temperature combustion catalyst, but 100 to 500 liters is appropriate. As a result of the experiment, the thermal efficiency of the combustion catalyst module 140 can be 90% or more, the amount of CO discharged from the combustion catalyst module is 20 ppm or less, and the amount of NOx discharged from the combustion catalyst module 140 is 20 ppm or less, and by-products The treatment efficiency of gas and harmful gas is more than 99%.

The high-temperature combustion catalyst 141 may have a granular shape, that is, a pellet shape, but a cylindrical shape, a cylindrical shape, a spherical shape, a hexahedral shape, etc. may also be applied. All of these may form pores, and when the pores are formed, the fuel gas is not biased to a specific part and passes through it uniformly because the fuel gas is not prevented from spreading and the differential pressure is not applied.

Preferably, the size of the pellet is appropriate 2 ~ 5mm If the size of the pellets is larger than this range, the pores between the pellets and the pellets become large, the combustion efficiency is lowered, whereas if the size of the pellets is smaller than this range, the pores are The size range must be adhered to because the small size reduces the passage rate of the combustion gas, so that the ignition spark of the combustion catalyst module 140 flashes back to the dispersion module 130 .

On the other hand, the high-temperature combustion catalyst 141 can be mass-produced by the following process.

A metal precursor solution containing a nitrate transition metal, an alkali earth metal nitrate and aluminum nitrate is prepared. The molar ratio of transition metal nitrate/alkaline earth nitrate/aluminum nitrate is (1-x)/(1-y)/11, wherein x is a number in the range of 0.1 to 0.5, and y can be in the range of 0.1 to 0.5 have. The nitrate transition metal may include at least one of manganese, cobalt, iron, and chromium. The alkaline earth metal nitrate may include at least one of calcium, strontium, barium, and radium. Preparing the metal precursor solution may be dissolving a transition metal nitrate, an alkaline earth metal nitrate and aluminum nitrate in distilled water.

A precipitation solution is prepared. Preparing the precipitation solution may be stirring the urea in distilled water. The concentration of urea in the precipitation solution may be 12 times the concentration of the metal precursor in the metal precursor solution.

When the mixed solution is prepared by mixing the metal precursor solution and the precipitation solution, the temperature of the mixed solution is raised to 90 ~ 100 ℃, and maintained for 10 ~ 48 hours to cause the precipitation reaction. A homogeneous solution precipitation method may be used for the precipitation reaction of the mixed solution.

A precipitate slurry formed by the precipitation reaction is filtered and separated from the mixed solution. The mixed solution separated by filtration of the precipitate slurry can be recycled to prepare a precipitation solution. The sediment slurry is washed with water.

Drying is performed to remove moisture in the washed sediment slurry. Drying the washed sediment slurry may be drying at a temperature in the range of 100 ~ 150 ℃.

In order to remove moisture remaining in the dried sediment slurry, calcination is performed at 1,000 ~ 1,500 °C. The calcined sediment slurry has a hexaaluminate structure, and may have a specific surface area in the range of ^{5 to 150 m 2 /g.}

Unlike other precipitation methods, the homogeneous solution precipitation method applied to the method for manufacturing a high-temperature combustion catalyst according to the present invention is simple and easy to design for mass production. The co-precipitation method, which is widely used as a general catalyst preparation method, uses a _{basic material such as sodium carbonate (Na 2} CO ₃ ) or sodium hydroxide (NaOH) as a precipitation agent for synthesizing the catalyst, and an acidic material such as metal nitrate is used as a metal precursor do. The salt produced in the acid neutralization reaction of these two substances is used as a catalyst. In this process, pH control is one of the important factors that determine the properties and performance of the catalyst. However, it is a relatively difficult and demanding process to adjust the pH adjustment rate. Due to this process, it is relatively difficult to manufacture a catalyst of the same quality in large quantities and repeatedly.

The homogeneous solution precipitation method used in the method for producing a high-temperature combustion catalyst according to the present invention can produce a high-temperature combustion catalyst of the same quality in large quantities and repeatedly while solving the pH control problem. The urea used is decomposed into ammonia (NH3) and carbon dioxide (CO2) between 90 and 100°C and reacts with metal precursors. At this time, the precipitation reaction appears uniformly throughout the solution, and the pH is naturally maintained at 7. In the co-precipitation method using sodium hydroxide or the like as a precipitating agent, the precipitation reaction occurs locally only at the place where the precipitating agent is input, and instantaneously at the site However, since high pH appears, strong stirring is required, and it is difficult to ensure uniformity, so it is difficult to produce a catalyst of the same quality. On the other hand, since the homogeneous solution precipitation method can solve this problem, it is possible to relatively simply produce a high-temperature combustion catalyst of the same quality.

In the filtration and washing process, in the case of the co-precipitation method using sodium hydroxide as a precipitating agent, impurities such as sodium (Na) or nitrate remaining in the precipitate slurry are removed, and these impurities are removed only by dissolving them with a large amount of distilled water. Since these impurities act as a cause of deterioration of the properties and performance of the catalyst, the filtration and washing process must be strictly carried out. At this time, the amount of distilled water used is 3 to 4 times higher than that of distilled water used when synthesizing the catalyst. On the other hand, impurities generated in the homogeneous solution precipitation method are ammonium nitrate (NH ₄ NO ₃ ) or unreacted elements, and these impurities It dissolves well in a small amount of distilled water, so it is easy to remove, and it can also be removed by heat. Therefore, the homogeneous solution precipitation method hardly exhibits deterioration in properties and performance of the catalyst due to impurities compared to the general co-precipitation method, and the process cost may be low due to the simplicity of the process.

In addition, after the precipitation reaction is completed, most of the wastewater generated in the filtration process is unreacted urea, so it can be reused as a precipitation solution serving as a precipitating agent. Of the precipitation solution used in excess in the precipitation reaction, only the urea equal to the precursor concentration is used in the precipitation reaction, and the remaining elements remain. The reason for using an excess of urea is to smoothly advance the precipitation reaction rate toward the forward reaction. Only a part of the solution is used and the rest comes out as the filtrate. If only the theoretical amount of urea used is added to the filtrate, it can be recycled as a precipitation solution.

In addition, the water washing process is also simpler than the conventional co-precipitation method. The reason is that the impurities remaining in the sediment after the filtration process remain in the form of ammonium nitrate produced after the reaction. Ammonium nitrate also has high solubility, and can be sufficiently removed by using only 1/2 of the distilled water used for the reaction, drying and calcination It can also be completely removed in the process. In addition, a small amount of wastewater generated here can also be reused. Therefore, the method for manufacturing a high-temperature combustion catalyst according to an embodiment of the present invention can be said to be a pollution-free manufacturing method with almost no waste liquid to be discarded.

In the drying and calcining process, drying of the sediment slurry is performed at about 100° C. for 10 hours or more to remove residual moisture. In addition, in the calcination process, a high-temperature combustion catalyst capable of maintaining performance and durability even at a high temperature can be manufactured by maintaining the calcination at 1,000° C. or higher for about 1 hour or more.

Hereinafter, a method for producing a high-temperature combustion catalyst according to the present invention will be described in more detail.

1. Preparation of metal precursor solution

Manganese (Mn), barium (Ba), and aluminum as metal precursors, manganese nitrate in the form of nitrate (Mn(NO ₃ ) ₂ .6H ₂ O), barium nitrate (Ba(NO ₃ ) ₂ ), aluminum nitrate (Al( NO ₃ ) ₃ 9H ₂ O) reagents were used Manganese/aluminum/barium, which is a component ratio of the high-temperature combustion catalyst, is dissolved in distilled water at a molar ratio of 1/10/1.

2. Preparation of urea solution

Urea is also stirred in distilled water to prepare a urea solution. The concentration of the urea solution is about 12 times that of the metal precursor.

3. Mix

The metal precursor solution and the urea solution of the same volume prepared previously are mixed in a synthesis reactor to form a mixed solution.

4. Precipitation reaction

The temperature of the synthesis reactor is raised to about 95 °C, and the mixed solution is maintained with vigorous stirring for 24 hours or more.

5. Filtration

A filtration process is performed to remove ammonium nitrate and a small amount of unreacted urea, impurities, and water, which are metal precursors, remaining in the precipitated slurry by this homogeneous solution precipitation method. After installing a filter in the Buchner funnel, the sediment slurry is introduced to separate the sediment slurry and waste liquid filtered through the filter. And the waste liquid is reused with urea (if the metal precursor concentration is 1 M, urea In addition, it can be recycled as a urea solution by adding 1 M).

6. wash

After separating the waste liquid, ammonium nitrate remaining in the sediment slurry is removed by passing a small amount of distilled water through the sediment slurry. In addition, the waste liquid generated here can also be stored and then put back into the water washing process when manufacturing a high-temperature combustion catalyst.

7. Drying and firing

In order to completely remove moisture remaining in the sediment slurry from which impurities and water have been removed, a drying process is performed in a drying oven at about 100° C. for about 10 hours or more. Thereafter, in order to prepare a high-temperature combustion catalyst, which is a final product, the dried precipitate slurry is heated to 1,200° C. at a temperature increase rate of about 3° C./min and maintained for the next about 6 hours.

The high-temperature combustion catalyst serves to cause the decomposition/combustion reaction of the harmful gas at the same time as the combustion reaction of the fuel gas. In particular, the combustion reaction and the decomposition reaction occur at the same time in the part corresponding to the active point of the high-temperature combustion catalyst, and since this reaction is a strong exothermic reaction, a large amount of heat is generated. For example, when the harmful gas is toluene, about 9,665 kcal of heat is generated when an amount of 1 kg is treated in a high-temperature combustion catalyst. In addition, when the fuel gas is LNG, about 10,200 kcal of heat is also generated when an amount of ^{1Nm 3 is burned in a high-temperature combustion catalyst.} This is the same as the sum of the heat of fuel gas and noxious gas as fuel gas and noxious gas are simultaneously processed in a high-temperature combustion catalyst. Therefore, the higher the concentration of the harmful gas, the less the amount of fuel gas is input, so that it has the advantage of being able to save fuel.

The optimum condition for increasing the catalyst efficiency in the combustion catalyst module 140 is when the space velocity (GHSV) of the mixed gas for the combustion catalyst module is 1,000 to 30,000 h ^-1 , the combustion catalyst module 140 ) has a volume of 1 to 15 liters, the density of the high-temperature combustion catalyst 141 is 0.5-1 g/ml, and the porosity of the high-temperature combustion catalyst 141 (the ratio of space volume to the total volume of high-temperature combustion catalyst) is 0.3 It is preferable to set it as ~ 0.5%. Accordingly, the pressure drop rate on the discharge side of the combustion catalyst module 140 can be maintained within 20%.

Table 1 below compares and measures the THC concentration before and after the process gas passes through the combustion catalyst module.

Here, methane was used as the fuel gas, and total hydro-carbon (THC), a VOCS type, was used as the harmful gas.

In Table 1, the THC treatment efficiency was consistently shown at an average of 995% or more, indicating that it was significantly superior to the existing air environment purification systems (RTO system, activated carbon adsorption treatment system, etc.).

Table 2 below compares the conventional combustion catalyst and the high-temperature combustion catalyst according to the present invention. In terms of treatment efficiency, the present invention is superior to the conventional treatment system, and the operating temperature is higher than that of the conventional combustion catalyst. This is possible. Therefore, it is advantageous in poisoning to tar, fine dust, sulfur compounds and chlorine compounds, and there is an advantage in that the maintenance cost is low because a low-cost transition metal-based high-temperature combustion catalyst is used.

The ignition module 150 is stacked in communication with the upper portion of the combustion catalyst module 140, and an ignition means 151 for providing a heat source for the combustion reaction is provided. Here, the ignition means may be any one of a spark-type ignition rod, a pilot burner, and an electric heater. Among them, when an electric heater is applied during preheating, initial flame does not occur at all.

On the other hand, an observation window (not shown) through which the combustion state in the combustion catalyst module 140 can be visually confirmed may be provided on one side of the ignition module 150 .

The preheating module 160 is a core component of the fuel reforming burner, and is stacked on the upper side of the ignition module 150, and supports the supply pipe 110 to penetrate through the supply pipe 116 by the high temperature combustion gas inside. It serves to preheat the mixed gas passing through. An exhaust pipe 170 for exhausting combustion gas to the outside may be connected to the upper side of the preheating module 160 .

Here, the reformed fuel conveying pipe 310 is located in the preheating module 160, and the fuel in the reformed fuel conveying pipe is reformed by heat exchange action by atmospheric heat in the preheating module, and in order to increase reforming efficiency, the reformed fuel conveying pipe In 310, the heat exchange time and area were extended by taking the shape of a zigzag bent tube.

A sampling valve 171 for sampling a part of the exhaust gas in order to measure a component of the exhaust gas discharged through the exhaust pipe may be installed on one side of the exhaust pipe 170 .

Here, the supply pipe 116 may be composed of an external supply pipe 111 located outside the preheating module 160 and an internal supply pipe 112 located inside the preheating module 160, and the internal supply pipe ( After horizontally passing through the side of the preheating tube 161 of the preheating module 160 , the 112 is installed to be bent vertically downward toward the mixing member 122 .

In the supply pipe 110 , as the internal supply pipe 112 passes through the preheating module 160 , the fuel gas passing through the internal supply pipe is heat-exchanged by the high-temperature combustion gas in the preheating module to be preheated to a high temperature. Because it is preheated to a high temperature before combustion, the combustion temperature can be lowered in the combustion stage, so fuel cost can be reduced. There is an advantage that

Meanwhile, the external supply pipe 111 includes a first external supply pipe 111a to which byproduct gas and oxygen are supplied, a second external supply pipe 111b to which fuel gas and oxygen are supplied, and the first and second external supply pipes into one. It may be composed of a merge pipe (111c) to be merged.

In addition, a main blower 113 for forcibly blowing fuel gas, by-product gas and oxygen may be installed on the first external supply pipe 111a.

In addition, a sub blower 114 for replacing the main blower 113 may be installed in the first external supply pipe 111a via the auxiliary supply pipe 111d. Accordingly, when the main blower 113 cannot be used due to a malfunction or repair, the sub blower 114 may be operated to blow fuel gas or the like through the auxiliary supply pipe 111d.

Unexplained reference numeral 111e denotes an emergency discharge valve for discharging by-product gas and oxygen supplied through the first external supply pipe 111a to the outside in an emergency, and 111f denotes an emergency by blocking the second external supply pipe 111b. It is a shut-off valve that stops the supply of fuel gas and oxygen.

Meanwhile, unreacted gas in the stack 400 may be recovered through the supply pipe 110 of the fuel reforming burner 100 and recycled as fuel. In particular, the recovery pipe 500 from which the unreacted gas is recovered is connected to the supply pipe 110 in the preheating module 160, so that it is preheated together with the fuel gas passing through the supply pipe, and is transferred to the mixing module 120. It is supplied and used as fuel for fuel reforming burners.

The above description of the present invention is for illustration, and those of ordinary skill in the art to which the present invention pertains can understand that it can be easily modified into other specific forms without changing the technical spirit or essential features of the present invention. will be. Therefore, it should be understood that the embodiments described above are illustrative in all respects and not restrictive. For example, each component described as a single type may be implemented in a distributed manner, and likewise components described as distributed may be implemented in a combined form.

The scope of the present invention is indicated by the following claims, and all changes or modifications derived from the meaning and scope of the claims and their equivalent concepts should be construed as being included in the scope of the present invention.

100: fuel reforming burner 110: supply pipe
120: mixed module 130: distributed module
140: combustion catalyst module 150: ignition module
160: preheating module 170: exhaust pipe
200: methane gas supply unit 300: reforming unit
310: reformed fuel transfer pipe 400: stack
500: recovery tube

Claims (10)

Methane gas supply unit for supplying methane gas; a reforming unit reforming the methane gas supplied from the methane gas supply unit to generate hydrogen gas and supplying it; and a stack for generating electric energy through an electrochemical reaction between hydrogen supplied from the reforming unit and oxygen supplied from an oxygen source.
The reforming unit includes a reformed fuel transfer pipe through which the reformed fuel is transferred; It consists of a fuel reforming burner that provides a heat source to thermally reform the reformed fuel transferred to the reformed fuel transfer pipe,
The fuel reforming burner,
a mixing module constituting the lowermost layer and having a built-in mixing member to mix fuel gas, by-product gas, and air supplied from the supply pipe;
a dispersion module stacked on the top so as to communicate with the mixing module and dispersing the mixed gas mixed in the mixing module and rising;
a combustion catalyst module stacked in communication with the upper part of the dispersion module and filled with a high-temperature combustion catalyst for burning the mixed gas by a catalytic reaction therein;
an ignition module stacked in communication with an upper portion of the combustion catalyst module and provided with an ignition means for providing a heat source for a combustion reaction;
A preheating module stacked in communication with the upper side of the ignition module and supporting the supply pipe to pass through the inside so that the mixed gas passing through the supply pipe is preheated by the high temperature combustion gas inside;
The reformed fuel transfer pipe is located in the preheating module, and the method further comprises reforming the fuel in the reforming fuel transferring pipe by atmospheric heat in the preheating module,
The supply pipe is composed of an external supply pipe and an internal supply pipe, wherein the internal supply pipe horizontally passes through the side of the preheater of the preheating module, and then is bent vertically downward toward the mixing member, and the end thereof is located in the mixing barrel. including more,
The external supply pipe,
a first external supply pipe to which by-product gas and oxygen are supplied;
a second external supply pipe to which fuel gas and oxygen are supplied;
It consists of; a merge pipe in which the first and second external supply pipes are merged into one;
Further comprising a main blower installed on the first external supply pipe for forcibly blowing fuel gas, by-product gas and oxygen,
A sub blower for replacing the main blower is installed in the first external supply pipe, and the sub blower is installed between the main blower and the second external supply pipe through an auxiliary supply pipe connected to the first external supply pipe as a medium. A fuel cell system comprising a fuel reforming burner using a high-temperature combustion catalyst.
The method according to claim 1,
The fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst, characterized in that the unreacted gas in the stack is recovered through a supply pipe of the fuel reforming burner and recycled as fuel.
delete delete delete The method according to claim 1,
A fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst, characterized in that an exhaust pipe for exhausting combustion gas to the outside is connected to the upper side of the preheating module.
The method according to claim 1,
The fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst, characterized in that each module is coupled by a flange joint.
The method according to claim 1,
The ignition means is a fuel cell system including a fuel reforming burner using a high-temperature combustion catalyst, characterized in that any one of a spark-type ignition rod, a pilot burner, and an electric heater.
The method according to claim 1,
The high-temperature combustion catalyst contains a nitrate transition metal, an alkaline earth nitrate metal and aluminum nitrate, wherein the alkaline earth nitrate metal includes at least one of calcium, strontium, barium or radium. A fuel reforming burner using a high-temperature combustion catalyst A fuel cell system comprising.
10. The method of claim 9,
The molar ratio of transition metal nitrate/alkaline earth nitrate/aluminum nitrate is (1-x)/(1-y)/11, wherein x is a number in the range of 0.1 to 0.5, and y is a number in the range of 0.1 to 0.5 A fuel cell system comprising a fuel reforming burner using a high-temperature combustion catalyst, characterized in that.

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