JP2016060649A - Hydrogen production system for hydrogen station - Google Patents

Abstract

PROBLEM TO BE SOLVED: To popularize a hydrogen station for a hydrogen station by reducing the number of devices composing the system to reduce the entire size of the system and reduce the cost of the system.SOLUTION: A hydrogen station for a hydrogen production system which produces hydrogen serving as fuel for a fuel cell vehicle by reforming a raw material gas in the hydrogen station comprises: a composite type reformer 1 that integrally includes a steam reforming reaction part 4 equipped with a combustor 3 and performing a steam reforming reaction, a CO shift reaction part 5 performing a CO shift reaction, a steam generation part 6 generating steam, and a preliminary reforming part 7 reforming a part of the raw material gas, and produces hydrogen from the raw material gas by the steam reforming reaction in the steam reforming reaction part 4 and the CO shift reaction in the CO shift reaction part 5 to reform the raw material gas to a reformed gas; and a hydrogen PSA apparatus 2 that is provided downstream of the composite type reformer 1 and separates and refines the hydrogen from the reformed gas.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a hydrogen production system for a hydrogen station that produces hydrogen by reforming a source gas such as city gas, propane gas, or kerosene in the hydrogen station.

  In recent years, fuel cell vehicles, which are vehicles that use hydrogen as a clean energy, have attracted attention, and the development and popularization of these fuel cell vehicles have been promoted. Along with the development and popularization of this fuel cell vehicle, the development of a hydrogen station for supplying hydrogen as a fuel to the fuel cell vehicle has also been promoted.

  As this hydrogen station, there has been known an on-site type hydrogen station that reforms a source gas in the hydrogen station to produce hydrogen and supplies the hydrogen to a fuel cell vehicle. The source gas is city gas or propane gas.

  Conventionally, as a representative example of a hydrogen production system for a hydrogen station installed in this on-site type hydrogen station, as shown in FIG. 4, one or two combustors 72 are provided, and the one or two combustors 72 are provided. A reformer 71 that performs a steam reforming reaction using thermal energy of the combustor 72 is provided, and a CO converter 73 that performs a CO shift reaction is provided downstream thereof, and the steam reforming reaction in the reformer 71 is provided. The raw material gas is reformed by the CO shift reaction in the CO converter 73 to produce hydrogen. A hydrogen PSA device 74 that separates and purifies hydrogen from the reformed gas is provided downstream of the CO converter 73.

  And as each apparatus around this reformer 71, the combustor 72, the CO converter 73, and the hydrogen PSA device 74, first, the raw material gas is divided on the upstream side of the reformer 71, and one side thereof is arranged. The fuel is supplied to one or two combustors 72 as combustion fuel, and the other side is supplied to a feed gas heater 78 through a raw material gas booster 75, a gas cooler 76, and a pressure regulating tank 77, and this feed gas heating The raw material gas is supplied from the vessel 78 to the desulfurizer 79. In the feed gas heater 78, the raw material gas is heated using the thermal energy of the exhaust gas from the reformer 71, and after heating, a part thereof is discharged as exhaust gas.

  Then, the raw material gas supplied to the desulfurizer 79 is supplied to the mixer 80, mixed with water vapor in the mixer 80, and then the raw material gas mixed with the water vapor is supplied to the raw material heater 81. In the raw material heater 81, the raw material gas is heated using the thermal energy of the exhaust gas of the reformer 71, and after heating, a part thereof is discharged as exhaust gas.

  Then, the raw material gas mixed with the water vapor supplied to the raw material heater 81 is supplied to the reformer 71.

  On the other hand, pure water is divided after passing through a pure water supply pump 82, one side thereof is supplied to a pure water heater 83, the other side is supplied to a pure water preheater 84 and a boiler 85, and pure water heating on one side is performed. Unit 83 and the other end of boiler 85 join together. Then, the pure water heater 83, the pure water preheater 84, and the boiler 85 generate water vapor. The generated water vapor is supplied to the mixer 80 and mixed with the raw material gas by the mixer 80.

  Further, combustion air is supplied to one or two combustors 72 via a combustion air fan 86.

  In the reformer 71, the reformed gas is reformed by the steam reforming reaction from the raw material gas mixed with the supplied steam, and the reformed gas reformed in the reformer 71 is After pure water is heated by the pure water heater 83, the pure water is cooled to an optimum temperature for the CO shift reaction and supplied to the CO converter 73.

  In the CO converter 73, the supplied reformed gas undergoes a CO shift reaction to obtain a reformed gas, and the hydrogen gas is converted from the raw material gas by the steam reforming reaction in the reformer 71 and the CO shift reaction in the CO converter 73. To produce reformed gas.

  Further, on the downstream side of the CO converter 73, the reformed gas produced by reforming hydrogen from the raw material gas is supplied to the condensed water separation tank 88 through the boiler 85, the pure water preheater 84, and the condenser 87. In the condensed water separation tank 88, the condensed water is separated, and the condensed water is discharged as a waste liquid.

  Then, the reformed gas is supplied from the condensed water separation tank 88 to the hydrogen PSA device 74, and the hydrogen PSA device 74 separates and purifies hydrogen from the reformed gas to take out high purity hydrogen. Thereby, hydrogen used as a fuel for the fuel cell vehicle is produced.

  Further, the impurity gas separated by the hydrogen PSA device 74 is collected in an off-gas tank 89 and stored therein, and this impurity gas is supplied to one or two combustors 72 as combustion fuel.

  In such a hydrogen production system for a hydrogen station, the number of devices constituting this system is about 20.

  In such a conventional hydrogen production system for a hydrogen station, since the number of devices constituting the system is about 20, the number of devices is considerably large, and therefore the size of the entire system is large. In addition, since the number of devices is large, the price of the system is very expensive.

  In such a conventional hydrogen production system for a hydrogen station, the number of devices constituting the system is large, the size of the entire system is large, and the price is also very expensive. There was a problem that the hydrogen station did not spread well in the hydrogen station where the hydrogen production system would be installed.

  Accordingly, the present invention provides a hydrogen production system for a hydrogen station by greatly reducing the number of devices constituting the system, reducing the overall size of the system, and reducing the price of the system. It is an object of the present invention to provide a hydrogen production system for a hydrogen station that can be widely used.

  A first invention is a hydrogen production system for a hydrogen station that reforms a raw material gas in a hydrogen station to produce hydrogen as fuel for a fuel cell vehicle. The hydrogen production system for a hydrogen station includes a combustor and performs a steam reforming reaction. A steam reforming reaction part to be performed, a CO shift reaction part to perform a CO shift reaction, and a steam generation part to generate steam are integrally provided, and by a steam reforming reaction in the steam reforming reaction part and a CO shift reaction in the CO shift reaction part A hydrogen station that has a combined reformer that produces hydrogen from a raw material gas and reforms it into a reformed gas, and a hydrogen PSA device that separates and purifies hydrogen from the reformed gas downstream of the combined reformer Hydrogen production system.

  The second invention is the composite reformer according to the first invention, wherein the combined reformer is upstream of the steam reforming reaction section and adjacent to the CO shift reaction section, and the heat from the CO shift reaction section is obtained. This is a hydrogen production system for a hydrogen station that includes a pre-reformer that absorbs and reforms part of the raw material gas by this heat.

  According to a third invention, in the first or second invention, in the composite reformer, the overall shape is made substantially cylindrical, and the entire periphery is covered with a high-performance special heat insulating material, and the center This is a hydrogen production system for a hydrogen station equipped with a combustor.

  According to a fourth aspect of the present invention, in the first to third aspects, a mixer is provided on the upstream side of the composite reformer, and water vapor generated in the steam generator of the composite reformer is supplied to the mixer. Here, the hydrogen production system for the hydrogen station is configured such that the raw material gas mixed with the water vapor is supplied to the combined reformer after the water vapor is mixed with the raw material gas.

  According to the present invention, in a combined reformer, a plurality of devices such as a steam reforming reaction unit, a CO shift reaction unit, a steam generation unit, and a preliminary reforming unit are integrated and integrated. By miniaturizing this, in the hydrogen production system for the hydrogen station, the number of devices constituting the system can be greatly reduced, thereby reducing the overall size of the system. In addition, the cost of the system can be reduced, and a hydrogen station for supplying hydrogen as fuel to the fuel cell vehicle can be promoted.

  In the combined reformer, the pre-reformer is adjacent to the CO shift reaction unit and absorbs heat from the CO shift reaction unit. Can be efficiently absorbed, and a part of the raw material gas can be favorably modified.

  Furthermore, in the combined reformer, a combustor is provided at the center, and the entire periphery is covered with a high-performance special heat insulating material, thereby suppressing the loss of heat energy and improving the heat energy efficiency. Therefore, it is possible to efficiently perform the work of producing hydrogen from the raw material gas and reforming it into the reformed gas. In addition, the high-performance special heat insulating material can be reduced in weight and size, and the combined reformer can be reduced in weight and size.

  Further, by providing the composite reformer with a steam generating section for generating steam mixed with the raw material gas, the steam generating section uses the combustor provided in the composite reformer to generate steam. Can be efficient.

It is explanatory drawing which shows the hydrogen production system for hydrogen stations of this invention. It is sectional drawing which shows the structure of the composite reformer of the hydrogen production system for hydrogen stations of this invention. It is a perspective view which shows a part of compound type reformer of the hydrogen production system for hydrogen stations of this invention. It is explanatory drawing which shows the conventional hydrogen production system for hydrogen stations.

  An embodiment of a hydrogen production system for a hydrogen station of the present invention will be described. This hydrogen production system for hydrogen stations is a new energy / industrial technology development organization (NEDO) fuel cell and hydrogen field "Hydrogen utilization technology research and development project / low cost equipment for fuel cell vehicles and hydrogen stations."・ Research and development has been adopted in the “R & D on systems, etc.” project.

  As shown in FIG. 1, a combustor 3 is provided, and a steam reforming reaction unit 4 that performs a steam reforming reaction, a CO shift reaction unit 5 that performs a CO shift reaction, and a steam generation unit 6 that generates steam are integrated. The combined reformer 1 is provided that generates hydrogen from the raw material gas by the steam reforming reaction in the steam reforming reaction section 4 and the CO shift reaction in the CO shift reaction section 5 to reform the reformed gas. Further, in this combined reformer 1, upstream of the steam reforming reaction section 4 and adjacent to the CO shift reaction section 5, the heat from the CO shift reaction section 5 is absorbed, and this heat A pre-reformer 7 for reforming a part of the raw material gas by the minute is provided.

  A hydrogen PSA device 2 for separating and purifying hydrogen from the reformed gas is provided downstream of the combined reformer 1.

  The source gas is city gas or propane gas, or kerosene, specifically vaporized kerosene.

  Further, each device around the combined reformer 1 and the hydrogen PSA device 2 will be described. First, on the upstream side of the composite reformer 1, the raw material gas is divided, one side thereof is supplied as a combustion fuel to the combustor 3 of the composite reformer 1, and the other side is provided with the raw material gas booster 11. Then, it is supplied to the desulfurizer 12 and supplied from the desulfurizer 12 to the mixer 13. The supplied raw material gas is mixed with water vapor in the mixer 13, and then the raw material gas mixed with the water vapor is supplied to the combined reformer 1. When kerosene is used as the raw material gas, although not shown, kerosene is supplied to the mixer using a kerosene supply pump and vaporized with water vapor in the mixer to obtain vaporized kerosene. Moreover, since this kerosene uses the desulfurized kerosene, the desulfurizer 12 becomes unnecessary.

  On the other hand, the pure water required for the steam reforming reaction is supplied to the pure water preheating / condenser 15 through the pure water supply pump 14, and is preheated by the pure water preheating / condenser 15 and combined with the preheated pure water. Supplied to the steam generator 6 of the mold reformer 1. Then, steam is generated in the steam generating section 6, and the generated steam is supplied to the mixer 13 and mixed with the raw material gas by the mixer 13.

  The combustion air is supplied to the air heater 17 via the combustion air fan 16, and the combustion air is supplied from the air heater 17 to the combustor 3 of the combined reformer 1.

  Then, in the combined reformer 1, hydrogen is produced from the raw material gas mixed with the supplied steam, through the preliminary reforming section 7, the steam reforming reaction section 4, and the CO shift reaction section 5, and reformed. Reform to gas. The point that the hydrogen is generated from the raw material gas in the composite reformer 1 and reformed into the reformed gas and the structure thereof will be described later.

  Then, on the downstream side of the composite reformer 1, the exhaust gas emitted from the combustor 3 of the composite reformer 1 is heated as the combustion air by the air heater 17 and then discharged as exhaust gas.

  Further, the reformed gas produced by reforming hydrogen from the raw material gas in the combined reformer 1 preheats pure water at the pure water preheated portion above the pure water preheater / condenser 15. Further, the water in the reformed gas is condensed at the lower part of the pure water preheating / condenser 15 and supplied to the condensed water separation tank 18. In the condensed water separation tank 18, the condensed water is separated and the condensed water is discharged as a waste liquid.

  Then, the reformed gas is supplied from the condensed water separation tank 18 to the hydrogen PSA device 2, and in the hydrogen PSA device 2, hydrogen is separated and purified from the reformed gas, and high-purity hydrogen is taken out. It is trying to produce hydrogen as a fuel.

This hydrogen PSA apparatus 2 uses gas separation technology by PSA (Pressure Swing Adsorption) method, and hydrogen separation and purification by PSA method repeats pressurization and depressurization in a plurality of containers filled with an adsorbent. A method for separating and purifying hydrogen that obtains high-purity hydrogen (H ₂ ) by adsorbing and desorbing an impurity gas containing carbon monoxide (CO) and carbon dioxide (CO ₂ ) on an adsorbent It is.

  Further, the impurity gas separated by the hydrogen PSA device 2 is collected in an off-gas tank 19 and stored therein, and this impurity gas is supplied to the combustor 3 of the combined reformer 1 as a combustion fuel.

  Next, the point and structure of producing hydrogen from the raw material gas and reforming it into reformed gas in the combined reformer will be described.

  First, as shown in FIGS. 2 and 3, the combined reformer 1 includes a first cylindrical body 21 having a vertically-oriented cylindrical shape at the upper part and a vertically-oriented cylinder having a larger diameter than the first cylindrical body 21 at the lower part. The entire shape of the first cylindrical body 21 and the second cylindrical body 22 is covered with a high-performance special heat insulating material 23.

As this high-performance special heat insulating material 23, a fine porous structure heat insulating material is used, and this fine porous structure heat insulating material has a thermal conductivity of 0.0045 W / m · K and a very low heat conductivity. Moreover, the density is as small as 400 kg / m ³ . Considering that the thermal conductivity of a ceramic fiber heat insulating material, which is generally said to have excellent heat insulating performance, is 0.14 W / m · K, the heat conductivity of this microporous heat insulating material is very small. Recognize. Thereby, in the high performance special heat insulating material 23 using this fine porous structure heat insulating material, the heat insulating performance is very excellent, and the loss of heat energy can be suppressed as much as possible. In addition, since the thermal conductivity is very small and the density is also small as described above, the weight and size can be reduced here.

The upper first cylindrical body 21 includes a pre-reforming portion 7 and a CO shift reaction portion 5, and the lower second cylindrical body 22 includes a steam reforming reaction portion 4 and a steam generation portion 6. Is provided. Inside the first cylindrical body 21, an inner cylinder 31 is provided on the inner side and an outer cylinder 32 is provided on the outer side to form an annular first space. Further, inside the second cylindrical body 22, a special heat insulating wall 25 is further provided on the inner surface of the high performance special heat insulating material 23 at the upper, lower and side portions to form a circular indoor space. Inside, an inner cylinder 41 and an outer cylinder 42 having the same diameter as the inner cylinder 31 and the outer cylinder 32 of the first cylinder 21 and a bottom lid 43 are provided to form an annular second space. The special heat insulating wall 25 provided on the inner surface of the upper part, the lower part, and the side part in the second cylindrical body 22 is made of a high alumina polycrystalline fiber heat insulating material. The fibrous heat insulating material has a thermal conductivity of 0.18 W / m · K and a density of 400 kg / m ³ . A commonly used plastic refractory has a thermal conductivity of 0.986 W / m · K and a density of 2700 kg / m ^3, and therefore, high alumina with lower thermal conductivity and density than this plastic refractory. In the special heat insulation wall 25 using the polycrystalline fiber heat insulating material, the weight reduction and size reduction can be achieved here.

  The combustor 3 is provided at the center of the composite reformer 1. This includes a combustor 3 extending from the center upper part of the first cylinder 21 to the center upper part in the indoor space of the second cylinder 22, and the combustor 3 is disposed at the center upper part of the first cylinder 21. A main body 51 is disposed, and combustion fuel is supplied to the combustor main body 51 and fuel air is supplied. The combustor main body 51 is connected to a burner chamber 52 provided at the center upper portion in the indoor space of the second cylindrical body 22 through the inner cylinder 31 of the first cylindrical body 21, and combustion is performed in the burner chamber 52. I do. The heat energy generated by the combustion in the burner chamber 52 is transmitted to the steam reforming reaction section 4, the CO shift reaction section 5, the steam generation section 6, and the preliminary reforming section 7.

  In the first cylindrical body 21, an inner inner intermediate tube 33 and an outer outer intermediate tube 34 are provided concentrically in an annular first space formed between the inner tube 31 and the outer tube 32. The annular space formed between the inner cylinder 31 and the inner intermediate cylinder 33 and the annular space formed between the outer intermediate cylinder 34 and the outer cylinder 32 have substantially the same cross-sectional area. A pre-reformer 7 is provided in each of the annular space formed between the inner cylinder 31 and the inner intermediate cylinder 33 and the annular space formed between the outer intermediate cylinder 34 and the outer cylinder 32. The pre-reformer 7 has a heat transfer particle layer (endothermic reaction) 7a in the upper half of which is in the form of particles and a pre-reformation reaction catalyst layer (endothermic reaction) 7b in the lower half of which is a pellet type. To.

  The CO shift reaction section 5 is provided in an annular space formed between the inner intermediate cylinder 33 and the outer intermediate cylinder 34 of the first cylindrical body 21. As this CO shift reaction part 5, the upper half here is a pellet type low temperature CO shift reaction catalyst layer (exothermic reaction) 5a and the lower half is a pellet type high temperature CO shift reaction catalyst layer (exothermic reaction). 5b.

  As described above, the first cylindrical body 21 includes the CO shift reaction portion 5 in the annular space formed between the inner intermediate cylinder 33 and the outer intermediate cylinder 34 in the first space, and the inner cylinder 31 and the inner side. By providing the pre-reformer 7 in the annular space formed between the intermediate cylinders 33 and the annular space formed between the outer intermediate cylinder 34 and the outer cylinder 32, the pre-reformer 7 is subjected to CO shift reaction. Provided to be adjacent to part 5.

  Further, in the first cylindrical body 21, a raw material gas inlet 26 is provided at an upper portion thereof, and the raw material gas mixed with the water vapor supplied from the mixer 13 flows in. Further, a reformed gas discharge port 27 is provided in the upper part, and reformed reformed gas is produced by producing hydrogen from the raw material gas on the downstream side of the combined reformer 1.

  In the second cylindrical body 22, the inner inner intermediate tube 44 and the outer outer intermediate tube 45 are concentrically formed in an annular second space formed between the inner tube 41, the outer tube 42, and the bottom cover 43. Provided. The inner intermediate cylinder 44 and the outer intermediate cylinder 45 are stopped halfway without reaching the bottom lid 43. The steam reforming reaction section 4 is provided in each of an annular space formed between the inner cylinder 41 and the inner intermediate cylinder 44 and an annular space formed between the outer intermediate cylinder 45 and the outer cylinder 42. The steam reforming reaction section 4 is a pellet type reforming reaction catalyst layer (endothermic reaction) 4a.

  And the annular space formed between the inner cylinder 41 provided with the steam reforming reaction part 4 and the inner intermediate cylinder 44 in the second space of the second cylindrical body 22 and the outer side provided with the steam reforming reaction part 4 The annular space formed between the intermediate cylinder 45 and the outer cylinder 42 is an annular space formed between the inner cylinder 31 provided with the preliminary reforming portion 7 in the first space of the first cylinder 21 and the inner intermediate cylinder 33. The space communicates with an annular space formed between the outer intermediate cylinder 34 and the outer cylinder 32 provided with the preliminary reforming section 7. In addition, the annular space formed between the inner intermediate cylinder 44 and the outer intermediate cylinder 45 in the second space of the second cylindrical body 22 is an inner side provided with the CO shift reaction unit 5 in the first space of the first cylindrical body 21. It communicates with an annular space formed between the intermediate cylinder 33 and the outer intermediate cylinder 34.

  In the second cylindrical body 22, an annular heat insulating cylinder 55 is provided on the side of the circular indoor space, and a part of the heat insulating cylinder 55 is opened. And the annular space is formed between the special heat insulation wall 25 and the heat insulation cylinder 55 of the side part in indoor space, and the steam generation part 6 is provided in this annular space. The steam generating unit 6 arranges a pipe 56 in a spiral shape, and passes pure water through the pipe 56, thereby converting pure water into steam by combustion in a burner chamber 52 provided at the upper center of the indoor space. Thus, water vapor is generated. And the water vapor | steam generate | occur | produced in this steam generation part 6 is supplied to the mixer 13 provided in the upstream of the said composite reformer 1, and it mixes with raw material gas here.

  In the second cylindrical body 22, an exhaust gas discharge port 28 is provided at a side portion thereof, and exhaust gas is discharged to the downstream side of the combined reformer 1.

  The point that hydrogen is produced from the raw material gas in the composite reformer 1 having such a structure and reformed to the reformed gas will be described. First, the raw material gas mixed with water vapor is placed on the upper portion of the first cylindrical body 21. It flows into the first space of the first cylindrical body 21 from the provided raw material gas inlet 26.

  The raw material gas mixed with the flowing water vapor is the heat transfer particles of the pre-reformer 7 provided in the annular space formed between the inner cylinder 31 and the inner intermediate cylinder 33 in the first space of the first cylindrical body 21. Layer 7a and pre-reforming reaction catalyst layer 7b, and heat transfer particle layer 7a and pre-reforming reaction catalyst layer 7b of pre-reforming section 7 provided in an annular space formed between outer intermediate cylinder 34 and outer cylinder 32. Flowing. When this raw material gas flows through the heat transfer particle layer 7 a of the pre-reformer 7, it absorbs the heat heated in the low-temperature CO shift reaction catalyst layer 5 a of the adjacent CO shift reaction unit 5 and the temperature rises. And when flowing through the pre-reforming reaction catalyst layer 7b of the pre-reforming part 7, the heat component further heated by the high-temperature CO shift reaction catalyst layer 5b of the adjacent CO shift reaction part 5 is efficiently absorbed, and further The temperature rises. A part of the raw material gas is reformed by efficiently absorbing the heat and increasing the temperature.

The partially reformed source gas is an inner cylinder in the second space of the second cylindrical body 22 that communicates with the heat transfer particle layer 7a and the pre-reformation reaction catalyst layer 7b of the pre-reformer 7 in the first space. In the annular space formed between the outer intermediate cylinder 45 and the outer cylinder 42, the reforming reaction catalyst layer 4 a of the steam reforming reaction section 4 provided in the annular space formed between the inner intermediate cylinder 44 and the inner intermediate cylinder 44. It flows through the reforming reaction catalyst layer 4a of the steam reforming reaction section 4 provided. The reformed raw material gas flows through the reforming reaction catalyst layer 4a of the steam reforming reaction section, and is subjected to a steam reforming reaction accompanied with a rapid endothermic reaction caused by combustion in the burner chamber 52 of the combustor 3. Thus, hydrogen (H ₂ ) and carbon monoxide (CO) are reformed to form a reformed gas.

Then, the reformed reformed gas is reversed in the second space of the second cylindrical body 22, flows through an annular space formed between the inner intermediate cylinder 44 and the outer intermediate cylinder 45, and communicates with the first space. The high temperature CO shift reaction catalyst layer 5b and the low temperature CO shift reaction catalyst layer 5a of the CO shift reaction section 5 provided in the annular space formed between the inner intermediate cylinder 33 and the outer intermediate cylinder 34 in the first space of the cylindrical body 21 are provided. Flowing. When this reformed reformed gas flows through the high temperature CO shift reaction catalyst layer 5b and the low temperature CO shift reaction catalyst layer 5a of the CO shift reaction section 5, the CO shift reaction (CO + H ₂ O → CO accompanying the heat generation here). ₂ + H ₂ ) converts carbon monoxide (CO) to hydrogen (H ₂ ) and carbon dioxide (CO ₂ ). In this way, hydrogen is produced from the raw material gas and reformed into a reformed gas.

  Then, the reformed gas produced by reforming hydrogen from the raw material gas flows into the upper portion of the first space of the first cylindrical body 21, and the combined reformer from the reformed gas discharge port 27 provided here. 1 is discharged to the downstream side.

  In the combined reformer 1 having such a structure, a combustor 3 is provided at the center thereof, a steam reforming reaction unit 4 that performs a steam reforming reaction, and a CO shift reaction unit 5 that performs a CO shift reaction. The steam reforming unit 4, the CO shift reaction, and the steam generating unit 6 for generating steam and the pre-reforming unit 7 for reforming a part of the raw material gas are integrated and integrated. The heat energy is transmitted from only one combustor 3 to each of the part 5, the steam generation part 6, and the pre-reformation part 7, thereby making it very efficient.

  In addition, the combined reformer 1 is an extremely compact unit comprising a combustor 3, a steam reforming reaction unit 4, a CO shift reaction unit 5, a steam generation unit 6, and a preliminary reforming unit 7. The structure can also be reduced in size.

  In addition, the entire periphery of the composite reformer 1 is covered with the high-performance special heat insulating material 23 using the fine porous structure heat insulating material, thereby suppressing the loss of heat energy and improving the heat energy efficiency. As a result, the composite reformer 1 can efficiently perform the operation of producing hydrogen from the raw material gas and reforming it into the reformed gas. Further, by using the fine porous structure heat insulating material for the high performance special heat insulating material 23, the high performance special heat insulating material 23 can be reduced in weight and size. And with the weight reduction and size reduction in this high-performance special heat insulating material 23, the weight reduction and size reduction in the special heat insulation wall 25 provided in the inside of the second cylindrical body 22 further reduce the weight of the composite reformer 1. Miniaturization can be achieved.

As described above, in the combined reformer 1 of the hydrogen production system for the hydrogen station, a plurality of devices provided separately in the conventional hydrogen production system for the hydrogen station are combined into one, and the weight reduction and size reduction are achieved. Accordingly, in the hydrogen production system for the hydrogen station, the number of devices constituting the system can be greatly reduced, which is half of the number of the devices constituting the conventional hydrogen production system for hydrogen stations. It can be about 10 groups. In addition, the overall size of the hydrogen production system for the hydrogen station can be reduced, which is less than half the size of the conventional hydrogen production system for the hydrogen station, with a width of about 3 m, a depth of about 2.5 m, and a high Can be made extremely small, with a total volume of about 22.5 m ³ . The price of the hydrogen production system for the hydrogen station can be reduced by reducing the number of devices constituting the system.

  In the hydrogen production system for a hydrogen station, the steam reforming reaction section 4, the CO shift reaction section 5, the steam generating section 6 and the pre-reforming section 7 that require large heat energy are used as a combustor. Since the combined reformer 1 with 3 is provided as one unit, it is possible to eliminate the need for a large amount of heat energy in other equipment, and thus a large amount of heat energy when starting up the system. Only the combined reformer 1 can perform the temperature raising operation to generate the system, and the system startup time can be greatly shortened compared to the conventional one. Specifically, Conventionally, what took 4 to 5 hours can be made within one hour, enabling high-speed start-up in a hydrogen production system for a hydrogen station.

  In the above-described embodiment, the hydrogen production system for the hydrogen station is used. However, the hydrogen production system can be used for other purposes other than the hydrogen station, and for example, hydrogen production is required. It can also be used as a facility for producing hydrogen in a chemical factory or a semiconductor manufacturing factory.

  DESCRIPTION OF SYMBOLS 1 ... Composite reformer, 2 ... Hydrogen PSA apparatus, 3 ... Combustor, 4 ... Steam reforming reaction part, 4a ... Reforming reaction catalyst layer, 5 ... CO shift reaction part, 5a ... Low temperature CO shift reaction catalyst Layers, 5b ... high temperature CO shift reaction catalyst layer, 6 ... steam generating part, 7 ... pre-reforming part, 7a ... heat transfer particle layer, 7b ... pre-reforming reaction catalyst layer, 11 ... raw material gas booster, 12 ... desulfurization 13 ... mixer, 14 ... pure water supply pump, 15 ... pure water preheat / condenser, 16 ... combustion air fan, 17 ... air heater, 18 ... condensate separation tank, 19 ... off gas tank, 21 ... 1st cylindrical body, 22 ... 2nd cylindrical body, 23 ... High performance special heat insulating material, 25 ... Special heat insulation wall, 26 ... Raw material gas inlet, 27 ... Reformed gas outlet, 28 ... Exhaust gas outlet, 31 ... Inner cylinder, 32 ... outer cylinder, 33 ... inner intermediate cylinder, 34 ... outer intermediate cylinder, 41 ... inner cylinder, 42 ... outer cylinder, DESCRIPTION OF SYMBOLS 3 ... Bottom cover, 44 ... Inner intermediate cylinder, 45 ... Outer intermediate cylinder, 51 ... Combustor main body, 52 ... Burner chamber, 55 ... Thermal insulation cylinder, 56 ... Pipe, 71 ... Reformer, 72 ... Combustor, 73 ... CO converter, 74 ... Hydrogen PSA device, 75 ... Raw material gas booster, 76 ... Gas cooler, 77 ... Pressure regulator, 78 ... Feed gas heater, 79 ... Desulfurizer, 80 ... Mixer, 81 ... Raw material heating 82 ... Pure water supply pump, 83 ... Pure water heater, 84 ... Pure water preheater, 85 ... Boiler, 86 ... Combustion air fan, 87 ... Condenser, 88 ... Condensate separation tank, 89 ... Off-gas tank

Claims (4)

In a hydrogen production system for a hydrogen station that reforms the raw material gas in the hydrogen station to produce hydrogen as fuel for a fuel cell vehicle,
A steam reforming reaction section that performs a steam reforming reaction, a CO shift reaction section that performs a CO shift reaction, and a steam generation section that generates steam are provided integrally with the combustor, and the steam reforming in the steam reforming reaction section A combined reformer that creates hydrogen from the raw material gas by the CO shift reaction in the reaction and CO shift reaction section and reforms it into a reformed gas,
A hydrogen production system for a hydrogen station, characterized in that a hydrogen PSA device for separating and purifying hydrogen from reformed gas is provided downstream of the combined reformer.   In the combined reformer, upstream of the steam reforming reaction section and adjacent to the CO shift reaction section, the heat from the CO shift reaction section is absorbed, and one of the raw material gas is absorbed by this heat. 2. The hydrogen production system for a hydrogen station according to claim 1, further comprising a pre-reformer for reforming the part.   2. The composite reformer according to claim 1, wherein the overall shape is substantially cylindrical, the entire periphery is covered with a high performance special heat insulating material, and a combustor is provided at the center thereof. Or the hydrogen production system for hydrogen stations of 2.   A mixer is provided on the upstream side of the composite reformer, and the steam generated in the steam generator of the composite reformer is supplied to the mixer, where the steam is mixed with the raw material gas, 4. The hydrogen production system for a hydrogen station according to claim 1, wherein the mixed raw material gas is supplied to the combined reformer.

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