WO2014002472A1 - 燃料処理装置 - Google Patents
燃料処理装置 Download PDFInfo
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- WO2014002472A1 WO2014002472A1 PCT/JP2013/003944 JP2013003944W WO2014002472A1 WO 2014002472 A1 WO2014002472 A1 WO 2014002472A1 JP 2013003944 W JP2013003944 W JP 2013003944W WO 2014002472 A1 WO2014002472 A1 WO 2014002472A1
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- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
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- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
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- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
- H01M8/0675—Removal of sulfur
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- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
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- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Definitions
- the present invention relates to a fuel processing apparatus that generates hydrogen to be supplied to a fuel cell system.
- a fuel cell system such as a home cogeneration system includes a fuel processing device that generates a hydrogen-containing gas and a fuel cell that generates power using the hydrogen-containing gas generated by the fuel processing device (for example, Patent Document 1). And 2).
- the desulfurization unit 105 is preferably set and maintained at a high temperature of 250 ° C. to 300 ° C., which is the optimum temperature of the hydrodesulfurization catalyst. Further, it is preferable that the raw material gas inserted into the desulfurization section 105 is also heated to an appropriate temperature of the catalyst so that the hydrodesulfurization reaction is likely to occur. It has been proposed to preheat the raw fuel before it is supplied to the desulfurization unit with the heat of the combustion unit (see Patent Documents 4 and 5).
- the desulfurization unit 105 since the desulfurization unit 105 is disposed outside the fuel processing apparatus 100, it is easily affected by the external environment and it is difficult to maintain the temperature at the optimum temperature. If the desulfurization unit 105 is continuously operated at a temperature lower than optimum, the activity of the hydrodesulfurization catalyst is weakened, and the service life of the hydrodesulfurization catalyst is shortened. In view of the fact that the service life of the fuel processing apparatus is generally 10 years, a method for reducing the influence of temperature from the external environment has been demanded.
- Patent Document 7 discloses a reformer provided with an evaporation section so as to surround the reforming section.
- Patent Document 7 even if the amount of heat released from the reforming section can be suppressed, it has not been suggested to reduce the temperature influence from the external environment on the desulfurization section.
- Patent Document 8 discloses a fuel processing apparatus accommodated in an outer container in a state where a plurality of reactors are arranged in close contact in parallel. According to the invention disclosed in Patent Document 8, the raw material gas can be preheated with the reformed gas.
- the granular heat insulating material filled in the exterior container reduces the temperature effect from the external environment. It has not been suggested to reduce the temperature influence from the external environment on the desulfurization section. Therefore, there has been a demand for a fuel processing apparatus that is less affected by temperature from the external environment.
- a first aspect of the present invention includes a combustion unit including a heat source, a desulfurization unit that removes a sulfur component from a raw material gas, and a reforming unit that generates a hydrogen-containing gas containing hydrogen as a main component from the desulfurized raw material gas.
- the gist of the present invention is a fuel processing apparatus having a low-temperature metamorphic section having an exothermic catalyst for reducing the impurity concentration in the hydrogen-containing gas.
- the reforming section and the desulfurization section are configured to surround the combustion section, and are arranged concentrically in the order of the reforming section and the desulfurization section from the combustion section toward the outside. It further has a preheating channel that is provided at the bottom of the combustion section via a heat insulating material and communicates with the desulfurization section so that the raw material gas is preheated by the heat of the combustion section.
- FIG. 1 is a cross-sectional view of a fuel processing apparatus according to an embodiment.
- FIG. 2 is a cross-sectional view showing the relationship between the first cylinder and the second cylinder as a part of the fuel processor according to the embodiment.
- FIG. 3 is a perspective view of a part (spiral wavy slope) of the fuel processing apparatus according to the embodiment.
- FIG. 4 is a perspective view of a part (third cylinder) of the fuel processing apparatus according to the embodiment.
- FIG. 5 is an enlarged cross-sectional view of a part (evaporation flow path and high-temperature transformation part) of the fuel processing apparatus according to the embodiment.
- FIG. 6 is a cross-sectional view of a main part of a fuel processor according to a modification of the embodiment.
- FIG. 1 is a cross-sectional view of a fuel processing apparatus according to an embodiment.
- FIG. 2 is a cross-sectional view showing the relationship between the first cylinder and the second cylinder as a part of the fuel
- FIG. 7 is a cross-sectional view of a main part of a fuel processor according to a modification of the embodiment.
- FIG. 8 is a cross-sectional view of a main part of a fuel processor according to a modification of the embodiment.
- FIG. 9 is a cross-sectional view of a conventional fuel processor.
- FIG. 1 is a schematic cross-sectional view of a fuel processing apparatus according to an embodiment.
- the fuel processing apparatus 1 includes a combustion unit 2 including a burner 23 as a heat source, a desulfurization unit 5 that removes a sulfur component from a raw material gas, and a hydrogen-containing gas containing hydrogen as a main component from the desulfurized raw material gas.
- the low temperature transformation part 6b Via the heat insulating material 4 so that the raw material gas is preheated by the heat of the combustion part 2 and the reforming part 3 to be generated, the low temperature transformation part 6b having a heat generation system catalyst that lowers the impurity concentration in the hydrogen-containing gas.
- a preheating channel 55 is provided at the bottom of the combustion unit 2 and communicates with the desulfurization unit 5.
- the reforming unit 3 and the desulfurization unit 5 are arranged in a circle so as to surround the combustion unit 2. Further, the reforming unit 3 and the desulfurization unit 5 are arranged concentrically in this order from the combustion unit 2 toward the outside. Further, in the fuel processing device 1, the reforming unit 3, the desulfurization unit 5, and the low temperature transformation unit 6b are arranged concentrically in that order from the combustion unit 2 toward the outside.
- the fuel processing apparatus 1 includes a combustion section cylinder 22, first to eighth cylinders 21, 32, 31, 41, 51, 61, 62, 91, and a bottom section 53. By these members, the combustion section cylinder is formed. 2 is configured to surround 2.
- the raw material gas is supplied to the desulfurization section 5 through the preheating channel 55.
- the preheating channel 55 is adjacent to the bottom of the combustion unit 2 via a heat insulating material. Therefore, the raw material gas flowing through the preheating channel 55 can be preheated before being supplied to the desulfurization unit 5. Therefore, the desulfurization reaction in the desulfurization part 5 proceeds efficiently.
- the reforming section 3 and the desulfurization section 5 are arranged concentrically from the combustion section 2 toward the outside.
- the reforming catalytic reaction in the reforming unit 3 requires a higher reaction temperature than the desulfurizing catalytic reaction in the desulfurizing unit 5. Therefore, in the fuel processing apparatus 1, a temperature suitable for the catalytic reaction is provided to the reforming unit 3 and the desulfurization unit 5.
- the combustion section cylinder 22 includes a combustion section cylinder body 22a, and a funnel-shaped inclined section 22b whose diameter widens from the upper opening of the combustion section cylinder body 22a.
- the first cylinder 21 is disposed on the outer periphery of the combustion section cylinder body 22a, and has a bottomed first cylinder body 21a in which the combustion section 2 is formed, and an opening of the first cylinder body 21a. And a funnel-shaped first inclined portion 21b whose diameter widens toward the outermost periphery.
- the upper ends of the first cylinder 21 and the combustion section cylinder 22 are joined by, for example, vacuum brazing.
- a combustion exhaust gas path 25 is formed between the first cylinder 21 and the combustion section cylinder 22.
- the upper end 32e of the second cylinder 32 and the upper end 21c of the first cylinder 21 are joined by, for example, vacuum brazing. Moreover, the convex part of the 1st inclination part 21b and the wavy inclination part 32b is joined without gap, for example by brazing. Therefore, the evaporation flow path 8 is configured in a space obtained by the first cylinder 21 and the second cylinder 32 contacting the first inclined portion 21b and the convex portion of the undulating inclined portion 32b.
- the first inclined portion 21b and the convex portion of the undulating inclined portion 32b are brazed to prevent a shortcut of the evaporation flow path 8 due to the reformed water. Further, it is possible to prevent the temperature in the evaporation channel 8 from changing suddenly. Conventionally, after inserting the middle cylinder between the inner cylinder and the outer cylinder, the middle cylinder is compressed in the axial direction to raise the convex portion of the middle cylinder. Thereby, the middle cylinder, the outer cylinder, and the inner cylinder are brought into close contact with each other.
- the first inclined portion 21b and the convex portion of the undulating inclined portion 32b can be brought into close contact with each other without performing such a complicated operation. Can be formed.
- the cost of the apparatus can be suppressed.
- a nickel (Ni) catalyst instead of the platinum catalyst as the reforming catalyst, the cost of the apparatus can be suppressed.
- ammonia gas may be generated when the raw material gas is reformed to hydrogen gas, there is a concern that ammonia gas is mixed in the hydrogen gas. This is because when ammonia gas is mixed in the hydrogen gas, deterioration of the members of the fuel cell and a decrease in catalyst activity are likely to occur.
- a home cogeneration system there is a possibility of giving an unpleasant feeling due to a bad odor.
- the ammonia decomposition unit 9 is provided, so that the generated ammonia gas can be decomposed even when a nickel catalyst is used as the reforming catalyst. Therefore, the problem resulting from ammonia gas is solved, and the cost of the entire fuel processing apparatus 1 can be suppressed.
- the high-temperature metamorphic part 6 a is composed of a second cylinder 32 and a third cylinder 31 disposed on the outer periphery of the second cylinder 32.
- the third cylinder 31 includes a bottomed third cylinder body 31a disposed on the outer periphery of the second cylinder body 32a, and a funnel-shaped second inclined portion 31b whose diameter widens from the opening of the third cylinder body 31a. Is provided. Via a flow path configured between the second cylindrical main body 32a and the third cylindrical main body 31a, and a flow path configured between the spiral wavy inclined portion 32b and the second inclined portion 31b, The reforming unit 3 and the high temperature transformation unit 6a communicate with each other.
- a flow path 31c as shown in FIG. 4 is formed in a part of the second inclined portion 31b of the third cylinder 31.
- the high temperature transformation part 6a is arrange
- the gas that has passed through the flow path 31c passes through the flow path 31d and the high-temperature metamorphic portion 6a, and then turns back toward the low-temperature metamorphic portion 6b.
- a copper-based catalyst can be used as the high temperature shift catalyst.
- the desulfurization unit 5 removes a sulfur component from a hydrocarbon-based source gas (hydrocarbon-based raw fuel) such as city gas supplied.
- the desulfurization section 5 is configured between a bottomed fourth cylinder 41 and a fifth cylinder 51 disposed on the outer periphery of the fourth cylinder 41, and a desulfurization catalyst is disposed thereon.
- a heat insulating material 4 is provided between the fourth cylinder 41 and the third cylinder body 31a.
- Stainless steel plates are joined to the portions corresponding to the upper and lower ends of the desulfurization section 5 by welding or the like.
- a through hole is provided in the main surface of the stainless steel plate so that gas can pass through.
- Desulfurization catalyst is not particularly limited, and various desulfurization catalysts can be used.
- a copper catalyst can be used as the desulfurization catalyst.
- the low temperature transformation part 6 b is configured between the sixth cylinder 61 and the seventh cylinder 62.
- the sixth cylinder 61 is disposed on the outer periphery of the fifth cylinder 51, and the upper end thereof is in contact with the second inclined portion 31b.
- the seventh cylinder 62 is disposed on the outer periphery of the sixth cylinder 61, and the upper end thereof is in contact with the second inclined portion 31b.
- Stainless steel plates are joined to the portions corresponding to the upper end and the lower end of the low temperature transformation part 6b by welding or the like. A through hole is provided in the main surface of the stainless steel plate so that gas can pass through.
- the low temperature shift section 6b includes a low temperature shift catalyst as an exothermic catalyst.
- the ammonia decomposing unit 9 includes an ammonia decomposing catalyst as an exothermic catalyst.
- a copper-based catalyst can be used as the low temperature shift catalyst and ammonia decomposition catalyst.
- the selective oxidation unit 10 removes remaining carbon monoxide from the gas subjected to the transformation treatment in the high temperature transformation unit 6a and the low temperature transformation unit 6b. Specifically, in the selective oxidation unit 10, carbon monoxide remaining in the gas subjected to the transformation treatment at a reaction temperature of about 100 ° C. to 200 ° C. by the catalytic action of ruthenium or the like is added to oxygen in the added air. Oxidized by.
- the shape of the preheating channel 55 is not limited to a radial shape as long as the supplied raw material gas can be preheated.
- an inverted frustoconical preheating recess 153 d may be provided in a part of the preheating channel 55. It is preferable that the center axis in the gravitational direction of the combustion unit 2 passes through the center of the bottom surface and the top surface of the inverted truncated cone constituting the preheating recess 153d.
- the raw material gas supplied from the supply port is preheated by the preheating recess 153d and then inserted into the desulfurization unit 5. Therefore, even if the supply amount of the raw material gas suddenly increases or the supply is temporarily interrupted and the supply amount of the raw material gas changes, the raw material gas preheated to a desired temperature is desulfurized. Easy to supply to part 5.
- a part of the preheating channel 55 may be a spiral channel 253d.
- the spiral flow path 253 d is formed in a spiral shape around the central axis of the combustion unit 2 in the gravity direction.
- the source gas is preheated while flowing in the circumferential direction, so that the source gas is preheated more reliably.
- variation in the temperature of the source gas can be reduced.
- the raw material gas can be preheated without increasing the size of the fuel processing apparatus 1.
- the material used for the combustion part cylinder 22, the first cylinder to the eighth cylinder 21, 32, 31, 41, 51, 61, 62, 91, and the bottom part 53 constituting the fuel processing apparatus 1 can be molded. There is no particular limitation as long as it can withstand the temperature to which each member is exposed. Although various materials can be used, for example, stainless steel can be used.
- the fuel processing apparatus 1 can be manufactured by fitting, for example, cylinders formed of stainless steel plates into a cylindrical shape. Between the cylinders, each catalyst unit (the reforming unit 3, the desulfurization unit 5, the high temperature conversion unit 6a, the low temperature conversion unit 6b, the ammonia decomposition unit 9, the selective oxidation unit 10, etc.) constitutes the combustion unit 2.
- the reforming section 3 and the desulfurization section 5 are arranged concentrically around the combustion section 2.
- an evaporating flow path 8 that is inclined outward from the upper end of the reforming unit 3 is disposed above the desulfurization unit 5 and the low temperature transformation unit 6b. Thereby, the evaporation flow path 8 can be arrange
- piping for connection with an external device is arranged on the bottom and side of the fuel processing device 1. Therefore, when assembling the apparatus by fitting each cylinder, the pipe for connection with the external apparatus and each catalyst part do not interfere. Thus, the fuel processing apparatus 1 can be easily manufactured by fitting each cylinder.
- a temperature region of 600 ° C., a temperature region of 250 ° C. to 300 ° C., a temperature region of 300 ° C., a temperature region of 200 ° C., and a temperature region of 150 ° C. are configured.
- the reforming unit 3 is in the temperature region of 600 ° C.
- the desulfurization unit 5 is in the temperature region of 250 ° C. to 300 ° C.
- the high temperature transformation unit 6a is in the temperature region of 300 ° C.
- the ammonia decomposition unit 9 are 200 ° C.
- the selective oxidation unit 10 can be disposed in a temperature region of 150 ° C. in the temperature region.
- each catalyst part is arrange
- the ammonia decomposition part 9 and the selective oxidation part 10 which are disposed outside the apparatus also achieve a heat insulating effect. That is, according to the fuel processing apparatus 1, heat radiation can be prevented, and the thickness of the heat insulating material disposed on the outer periphery of the apparatus can be made thinner than before, so that the apparatus can be downsized.
- the high temperature shift catalyst in the high temperature shift section 6a disposed along the evaporation flow path 8 and disposing the low temperature shift catalyst in the low temperature shift section 6b, temperature unevenness can be effectively prevented. This is because the heat generated by the catalytic reaction in the high temperature transformation section 6a is efficiently absorbed by the evaporation flow path 8 so that the catalytic reaction can proceed more efficiently.
- the catalyst addition amount can also be reduced by improving the reaction efficiency of the catalyst.
- a fuel processing apparatus 1 as shown in FIG. 1 is prepared.
- a raw material gas containing methane such as a hydrocarbon-based fuel such as LPG gas or city gas is supplied from a raw material gas supply port provided in the cylinder 53b of the bottom 53.
- the raw material gas is supplied to the desulfurization unit 5 through the preheating channel 55.
- the source gas is heated (preheated).
- the sulfur component contained in the raw material gas reacts with the hydrodesulfurization catalyst stored in the desulfurization section 5 to remove the sulfur component contained in the raw material gas.
- the desulfurized source gas is supplied from the desulfurized source gas discharge port arranged in the bottom main body 53a to the evaporation channel 8 via a pipe (not shown).
- the reforming water is supplied to the evaporation channel 8 and heated to evaporate.
- the desulfurized source gas and the evaporated improved water are mixed while passing through the evaporation flow path 8 to obtain a mixed gas.
- the obtained mixed gas is supplied to the reforming unit 3 filled with the reforming catalyst.
- a hydrogen-containing gas is generated from the mixed gas by the reforming reaction.
- the gas reformed from the raw material gas into the hydrogen-containing gas in the reforming unit 3 is transformed from the lower end of the reforming unit 3 through the channel 35 along the evaporation channel 8 shown in FIG. To the unit 6a. And it is made to react with the high temperature transformation catalyst with which the high temperature transformation part 6a was filled. The transformed gas that has passed through the lower end of the high temperature transformation section 6a is sent to the low temperature transformation section 6b.
- the low temperature transformation part 6b In the low temperature transformation part 6b, the gas transformed at high temperature is transformed again, and carbon monoxide is reduced from the hydrogen-containing gas. Then, the low-temperature transformed gas that has passed through the low-temperature transformation unit 6b is sent to an ammonia decomposition unit 9 as an arbitrary device. Note that the low temperature transformation portion 6b and the high temperature transformation portion 6a may be integrally molded continuously.
- ammonia decomposition In the ammonia decomposition part 9, the remaining ammonia gas is removed from the hydrogen-containing gas.
- the gas that has passed through the ammonia decomposition section 9 is sent to the selective oxidation section 10 provided along the evaporation flow path 8 via the flow path 95.
- the carbon monoxide gas remaining in the gas is further removed. Since the selective oxidation unit 10 with an exothermic reaction is disposed adjacent to the evaporation channel 8; heat generated by the catalytic reaction in the selective oxidation unit 10 is efficiently absorbed into the evaporation channel 8. Therefore, the temperature of the selective oxidation unit 10 is controlled to an appropriate temperature, and the catalytic reaction proceeds efficiently.
- a hydrogen-containing gas can be obtained.
- a fuel cell system partially including the fuel processing apparatus 1 described in the embodiment can be manufactured.
- a frustoconical space defined by the inclined portion 22 b and the lid portion 24 is formed above the combustion portion 2.
- the reforming water can be preheated using the heat of the combustion section 2.
- warmed reformed water it is possible to prevent heat from being released from the fuel processing apparatus 1. This provides a fuel processor that is less affected by temperature from the external environment and that has a higher reaction efficiency of the catalyst.
- the improved water is not sufficiently heated in the evaporation flow path 8 and does not evaporate in the evaporation flow path, so that the water may wet the surface of the reforming catalyst.
- the contact area between the catalyst and the gas is reduced, and the catalytic activity may be reduced.
- the catalyst deteriorates due to getting wet with water, and there is a possibility that the reforming of the raw material gas is hindered.
- the improved water is sufficiently heated and easily evaporated, thereby solving the conventional problems and efficiently reforming the raw material gas into hydrogen gas.
- a fuel processing apparatus that is less affected by the temperature from the external environment and can preheat the raw material gas. Moreover, according to this invention, the fuel processing apparatus with high reaction efficiency of a catalyst is provided.
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Abstract
Description
図1は、実施形態に係る燃料処理装置の概略断面図である。実施形態に係る燃料処理装置1は、熱源としてのバーナ23を備える燃焼部2と、原料ガスから硫黄成分を取り除く脱硫部5と、脱硫された原料ガスから水素を主成分とする水素含有ガスを生成する改質部3と、水素含有ガス中の不純物濃度を低下させる発熱系触媒を備える低温変成部6bと、燃焼部2の熱により原料ガスが予熱されるように、断熱材4を介して燃焼部2の底部に設けられ、脱硫部5に連通する予熱流路55とを有する。
燃焼部2は、燃料処理装置1の熱源としてバーナ23を作動させることにより、燃料処理装置1全体に熱を供給する。燃焼部2は、燃焼部円筒22と、燃焼部円筒22の外周に配置された第一円筒21と、燃焼部円筒22の上部に配置された、バーナ23を備える蓋部24とから形成されている。
蒸発流路8は、脱硫部5で脱硫された原料ガスと、改質水を蒸発して得られる水蒸気とを混合し、混合ガスを生成する。改質部3は、蒸発流路8と連通し、蒸発流路8で生成された混合ガスから、水素を主成分とする水素含有ガスを生成する。具体的には、原料ガスがメタンを主成分とする天然ガスである場合、改質部3では、燃焼部2による例えば600℃程度の加熱下でメタンと水蒸気とが下記の反応式にて改質反応する。そして、水素と一酸化炭素と、二酸化炭素とを含むガスに改質処理される。
CH4+H2O→CO+3H2 …[化1]
CH4+2H2O→CO2+4H2 …[化2]
高温変成部6aは、改質部3にて改質生成された水素含有ガスに含まれる一酸化炭素濃度を低減する。具体的には、高温変成部6aにおいて、次式に示されるようにして、水素含有ガス中の一酸化炭素と水蒸気とが反応して、二酸化炭素と水素が生成される。
CO+H2O→CO2+H2 …[化3]
脱硫部5は、供給される都市ガスなどの炭化水素系の原料ガス(炭化水素系の原燃料)から硫黄成分を除去する。
低温変成部6bは、第六円筒61と第七円筒62との間に構成されている。第六円筒61は、第五円筒51の外周に配置されており、その上端は第二傾斜部31bと接している。第七円筒62は、第六円筒61の外周に配置されており、その上端が第二傾斜部31bと接している。低温変成部6bの上端よび下端に対応する部分には、ステンレス板がそれぞれ溶接などにより接合されている。ステンレス板の主面には貫通孔が設けられ、ガスが通り抜けられるようにされている。
選択酸化部10は、高温変成部6aおよび低温変成部6bにおいて変成処理されたガス中から、残留する一酸化炭素を除去する。具体的には、選択酸化部10においては、ルテニウム等の触媒作用によって、100℃~200℃程度の反応温度で変成処理されたガス中に残留する一酸化炭素が、添加された空気中の酸素によって酸化される。
予熱流路55は、第1円筒41と有底の円筒53bとの間に構成されている。有底の円筒53bの、燃焼部2の重力方向の中心軸に対応する部分に、原料ガス取り込み口が形成されていることが好ましい。また、予熱流路55は、燃焼部の重力方向の中心軸を中心にして放射状に構成されている。そのため、原料ガス取り込み口から予熱流路55に供給された原料ガスは、燃焼部2からの熱によって予熱される。そして予熱(例えば、250℃程度にまで加熱)された原料ガスが、脱硫部5に供給される。そのため、脱硫部5での脱硫が効率よく進行する。
次に、燃料処理方法の説明を通じて、原料ガスが水素含有ガスに処理される過程(ガスの流れ)を説明する。
まず、図1に示すような燃料処理装置1を用意する。次に底部53の円筒53bに設けられた原料ガス供給口から、LPGガスや都市ガス等の炭化水素系燃料などのメタンを含む原料ガスを供給する。原料ガスは、予熱流路55を通って脱硫部5に供給される。予熱流路55において、原料ガスは加熱(予熱)される。原料ガス中に含有される硫黄成分は、脱硫部5に納められた水添脱硫触媒と反応して、原料ガス中に含有される硫黄成分が取り除かれる。
脱硫された原料ガスを、底部本体53aに配置された脱硫済原料ガス排出口から、配管(図示せず)を介して、蒸発流路8に供給する。一方で、改質水を蒸発流路8に供給し加熱して蒸発させる。そして、脱硫された原料ガスと蒸発した改良水を、蒸発流路8を通過させながら混合させて、混合ガスを得る。得られた混合ガスを、改質触媒が充填された改質部3に供給する。改質反応によって、混合ガスから水素含有ガスを生成させる。
改質部3で原料ガスから水素含有ガスに改質されたガスを、改質部3の下端から、流路35を介して、図5に示す蒸発流路8に沿って設けられた高温変成部6aに供給する。そして、高温変成部6aに充填された高温変成触媒で反応させる。高温変成部6aの下端を通過した変成されたガスを、低温変成部6bに送る。
低温変成部6bにおいて、高温変成されたガスを再度変成させ、水素含有ガス中から一酸化炭素を低減させる。そして低温変成部6bを通過した低温変成されたガスを、任意の装置としてのアンモニア分解部9に送る。なお、低温変成部6bおよび高温変成部6aは、連続して一体に成形してもよい。
アンモニア分解部9において、水素含有ガス中から、残存するアンモニアガスを除去する。アンモニア分解部9を通過したガスを、流路95を介して、蒸発流路8に沿って設けられた選択酸化部10に送る。なお、水素含有ガスからアンモニアを除去する必要がない場合は、アンモニア分解部9の位置にも、低温変成部6bと同様の変成触媒を充填しておくことが好ましい。熱が装置の外部に放出することを防止するためである。
選択酸化部10において、ガス中に残存する一酸化炭素ガスをさらに除去する。発熱反応を伴う選択酸化部10は、蒸発流路8に隣接して配置されるので;選択酸化部10での触媒反応により生じた熱が、効率よく蒸発流路8に吸収される。そのため、選択酸化部10の温度が適温に制御され、触媒反応が効率よく進行する。
上記のように、本発明を、実施形態を参照して説明したが、この開示の一部をなす論述及び図面はこの発明を限定するものであると理解すべきではない。この開示から当業者には様々な代替実施の形態、実施例及び運用技術が明らかとなろう。
2 燃焼部
3 改質部
5 脱硫部
6a 高温変成部
6b 低温変成部
8 蒸発流路
9 アンモニア分解部
10 選択酸化部
23 バーナ
22 燃焼部円筒
21 第一円筒
32 第二円筒
31 第三円筒
41 第四円筒
51 第五円筒
61 第六円筒
62 第七円筒
91 第八円筒
53 底部
55 予熱流路
153d 予熱窪部
253d 螺旋状流路
Claims (8)
- 熱源を備える燃焼部と、
原料ガスから硫黄成分を取り除く脱硫部と、
脱硫された前記原料ガスから水素を主成分とする水素含有ガスを生成する改質部と、
前記水素含有ガス中の不純物濃度を低下させる発熱系触媒を備える低温変成部とを有し、
前記改質部および前記脱硫部は、前記燃焼部を取り囲むように構成され、前記燃焼部から外側に向かって、前記改質部、前記脱硫部の順に同心円状に配置され、
前記燃焼部の熱により前記原料ガスが予熱されるように、断熱材を介して前記燃焼部の底部に設けられ、前記脱硫部に連通する予熱流路を更に有する、
燃料処理装置。 - 前記予熱流路の一部に、前記燃焼部の重力方向の中心軸を中心にして、中心から外側にいくほど径が拡がる逆円錐台状の予熱窪部を備える、請求項1に記載の燃料処理装置。
- 前記予熱窪部の大径側の径方向の端部で、前記予熱窪部よりも細径の前記予熱流路と連通している、請求項2に記載の燃料処理装置。
- 前記予熱流路は、前記燃焼部の重力方向の中心軸を中心にして放射状に形成されている、請求項1に記載の燃料処理装置。
- 前記予熱流路は、前記燃焼部の重力方向の中心軸を中心にして螺旋状に形成されている、請求項1に記載の燃料処理装置。
- 前記予熱流路は、前記燃焼部の重力方向の中心軸に対応する部分に原料ガス取り込み口を備えている、請求項1に記載の燃料処理装置。
- 前記予熱流路が、前記燃焼部の底部と、前記燃焼部の側部の一部を覆うように配置されている、請求項1に記載の燃料処理装置。
- 前記改質部、前記脱硫部、前記低温変成部は、前記燃焼部を取り囲むように構成され、前記燃焼部から外側に向かって、前記改質部、前記脱硫部、前記低温変成部の順に同心円状に配置されている、請求項1に記載の燃料処理装置。
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JP2015187981A (ja) * | 2014-03-14 | 2015-10-29 | パナソニック株式会社 | 燃料電池システム |
US20160204453A1 (en) * | 2015-01-09 | 2016-07-14 | Honda Motor Co., Ltd. | Fuel cell module |
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JP5483787B1 (ja) * | 2012-06-25 | 2014-05-07 | パナソニック株式会社 | 燃料処理装置 |
CN115504434B (zh) * | 2022-11-09 | 2023-08-01 | 常州创氢能源科技有限公司 | 自热式重整制氢反应器 |
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- 2013-06-24 WO PCT/JP2013/003944 patent/WO2014002472A1/ja active Application Filing
- 2013-06-24 US US14/404,624 patent/US9144781B2/en not_active Expired - Fee Related
- 2013-06-24 JP JP2013546120A patent/JP5427326B1/ja not_active Expired - Fee Related
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JP2015151312A (ja) * | 2014-02-17 | 2015-08-24 | パナソニックIpマネジメント株式会社 | 水素生成装置及びそれを用いた燃料電池システム |
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Also Published As
Publication number | Publication date |
---|---|
EP2735541B1 (en) | 2016-03-09 |
US9144781B2 (en) | 2015-09-29 |
JP5427326B1 (ja) | 2014-02-26 |
JPWO2014002472A1 (ja) | 2016-05-30 |
EP2735541A1 (en) | 2014-05-28 |
US20150118129A1 (en) | 2015-04-30 |
EP2735541A4 (en) | 2015-01-14 |
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