JP2005225684A5 - - Google Patents

Description

Hydrogen generator

  The present invention relates to a hydrogen generator, and more particularly to a hydrogen generator that makes it possible to efficiently recover heat released from a catalyst body.

  The fuel cell system supplies a hydrogen-rich gas (reformed gas) to the anode of the fuel cell, supplies an oxidant gas to the cathode of the fuel cell, and causes these gases to react electrochemically inside the fuel cell. It generates electricity and heat at the same time.

  Here, as a method for generating the reformed gas, a hydrogen generator for producing hydrogen gas from a raw material gas (for example, natural gas or city gas) and steam by a steam reforming reaction is used. It is necessary to receive the heat of evaporation that evaporates water and the heat of reaction that promotes the reforming reaction from the high-temperature combustion gas of the heating burner, so that water and the reforming catalyst body can efficiently exchange heat with the combustion gas. However, it is an important issue from the viewpoint of effective use of thermal energy.

As a report example related to this problem, hydrogen generation in which a water evaporation part is arranged so as to cover the periphery of the cylindrical reforming part containing the reforming catalyst body in the circumferential direction with the combustion gas flow path interposed therebetween An apparatus has been proposed (see, for example, Patent Document 1). In this hydrogen generator, a high-temperature gas flowing through a combustion gas passage is covered by covering the combustion gas passage and the reforming section (reforming catalyst body) with a water evaporation section. The heat dissipation of the combustion gas and the heat dissipation of the reforming catalyst body kept at a high temperature are reduced to improve the thermal efficiency of the hydrogen generator.
JP 2003-252604 A

  However, in the conventional hydrogen generator described above, priority was given to improving the thermal efficiency of the hydrogen generator, so when the mixed gas containing the raw material gas and water vapor flows out from the water evaporation section toward the reforming section, The configuration of the mixed gas flow path is complicated by changing the flow direction from the axial direction of the water evaporation section to the circumferential direction. For example, the mixed gas supply pipe that connects the mixed gas outlet of the water evaporation section and the mixed gas inlet of the reforming section extends in the radial direction, and at the connection point between the mixed gas supply pipe and the reforming section that extends in the axial direction, It is necessary to perform piping construction such as welding, and this piping construction of the mixed gas flow path may increase the cost of the hydrogen generator and deteriorate the durability performance.

  For such a configuration, if the cylindrical water evaporation section and the reforming catalyst body are arranged side by side in the same axial direction, and the flow of the mixed gas can flow smoothly along the axial direction, Although it is possible to achieve simplification and to achieve a desirable mixed gas flow path configuration by solving the above problems, in such a mixed gas flow configuration in one direction (axial direction) It can be said that there is still room for improvement in design so that the heat released from the catalyst body is recovered as much as possible to efficiently heat the water in the water evaporation section.

  The present invention has been made in view of such circumstances, and an object of the present invention is to simplify the configuration of the mixed gas flow path and to generate hydrogen that makes it possible to efficiently recover the heat released from the catalyst body. To provide an apparatus.

A hydrogen generator according to the present invention includes a cylindrical water evaporation section through which a mixed gas of a raw material gas and water vapor flows, and a cylindrical reforming catalyst body that generates a reformed gas using the mixed gas from the water evaporation section A CO gas removal unit having a catalyst body that removes carbon monoxide gas in the reformed gas flowing out of the reforming catalyst body, a burner that generates combustion gas by combustion of combustible gas, and the combustion gas A cylindrical combustion gas flow path that flows, wherein the reforming catalyst body is provided in parallel with the central axis in an extension line of the central axis of the water evaporation section, and the CO gas removal section The combustion gas flow path is provided in parallel with the central axis inside the reforming catalyst body and the water evaporation part, and the combustion gas is provided in parallel with the water evaporation part with respect to an axis. After transferring heat to the reforming catalyst body, the water evaporation section and And it is configured so as to be transferred to the serial CO remover.

The catalyst body may be a shift catalyst body that shifts the carbon monoxide gas.

  The catalyst body may be a selective oxidation catalyst body that selectively oxidizes the carbon monoxide gas.

According to such a hydrogen generator, the mixed gas containing the raw material gas and water vapor inside the water evaporation section can flow out in one direction (in the direction of the central axis of the water evaporation section) toward the reforming catalyst body. Ru can simplify the configuration of the flow path. Also, the thermal efficiency of the hydrogen generator can be improved.

  ADVANTAGE OF THE INVENTION According to this invention, while aiming at the simplification of the structure of a mixed gas flow path, the hydrogen generator which makes it possible to collect | recover efficiently the thermal radiation of a catalyst body is obtained.

  Embodiments of the present invention will be described below with reference to the drawings. In the figure, the side marked “upper” is the upper side, the side marked “lower” is the lower side, and the vertical direction of the cylindrical hydrogen generator 10 is the axial direction. Each embodiment will be described with the direction along the circumference drawn around the first central axis 110 as the circumferential direction and the direction along the radius of the circumference as the radial direction.

(Embodiment 1)
FIG. 1 is a cross-sectional view showing the internal structure of the hydrogen generator according to Embodiment 1 of the present invention.

  The hydrogen generator 10 mainly includes a first cylindrical wall member 11 and a second cylindrical wall member made of cylindrical seamless metal (stainless steel) that share a first central axis 110 to form a double pipe. 12 and a first central axis 110 of the first and second cylindrical wall members 11, 12 formed in a cylindrical region defined by the first and second cylindrical wall members 11, 12. In a region partitioned by the first and second cylindrical wall members 11 and 12, and arranged in the direction of the first central axis 110 along the water evaporation unit 13. Between the arranged cylindrical platinum-based reforming catalyst body 14 and the lower end of the first cylindrical wall member 11 to the vicinity of the upper end inside the first cylindrical wall member 11, and between the first cylindrical wall member 11 A cylindrical third cylindrical wall member 16 forming a coaxial double tube, and an inner part of the third cylindrical wall member 16 Seamless metal (stainless steel) that forms a double pipe between the burner 15 formed at the lower central portion and the upper half of the second cylindrical wall member 12 and between the second cylindrical wall member 12 And a disc-shaped lid member 24 disposed so as to cover the entire upper surface of the cylindrical cover 22.

  In addition, the outer structure of the cylindrical cover 22 has a cylindrical modified heat insulating member 62 disposed around the cylindrical cover 22 and a cylindrical modified heat insulating member 62 disposed so as to cover at least the outer peripheral surface. Heat by the heat released from the reforming catalyst body 14 through the heat insulating member cover 61 (metal cover) and the reforming heat insulating member 62 arranged in close contact (contact) with the reforming heat insulating member cover 61 and spirally wound. It is comprised by the reforming heat exchange part 60 which consists of a water flow pipe which distribute | circulates the water to replace | exchange. In addition, this water flow pipe is comprised with the flexible stainless steel metal pipe.

  Further, as will be described in detail later, the gap between the third cylindrical wall member 16 and the first cylindrical wall member 11 is used as a first combustion gas passage 30 through which combustion gas flows, and the second The gap between the cylindrical wall member 12 and the cylindrical cover 22 is used as a reformed gas passage 45 through which the reformed gas flows.

  Here, in the present embodiment, the first central axis 110 of the reforming catalyst body 14 is made to coincide with the first central axis 110 of the water evaporation unit 13, and the mixed gas existing inside the water evaporation unit 13. The reforming catalyst bodies 14 are arranged side by side on the downstream side in the flow direction of (a gas containing raw material gas and water vapor). That is, the water evaporation unit 13 is disposed below the reforming catalyst body 14.

  Further, the reforming catalyst body 14 is supported in a boundary region between the upper end 13u of the water evaporation section 13 and the lower end 14d of the reforming catalyst body 14, and has an annular shape having a plurality of mixed gas ejection holes 43h arranged uniformly in the circumferential direction. The support member 43 is provided.

  By aligning the direction of the first central axis 110 of the water evaporation unit 13 and the reforming catalyst body 14 and arranging them side by side, the inside of the water evaporation unit 13 is directed from the water evaporation unit 13 toward the reforming catalyst body 14. Ascending mixed gas can be smoothly flowed out to the reforming catalyst body 14 in one direction (axial direction), for example, complicated gas flow paths using piping construction such as welding can be reduced, and DSS (Daily It is possible to improve the durability of the hydrogen generator 10 against a thermal cycle by Start-up & Shut-down) and to reduce the manufacturing cost of the hydrogen generator 10 by simplifying the gas flow path.

  Further, since the water evaporation unit 13 is disposed below the reforming catalyst body 14, only the water vapor can be supplied to the reforming catalyst body 14, and the water droplets of the water evaporation unit 13 flow into the reforming catalyst body 14, so that the reforming catalyst. It is possible to prevent the medium 14 from deteriorating.

  The water evaporation unit 13 includes a first source gas pipe 40 that guides a source gas supplied from a source supply means (not shown) to a source gas inlet 40in of the water evaporation unit 13 and supply water to the water evaporation unit 13. A first connecting pipe 63 that leads to the water inlet 13in is disposed. A temperature measuring unit 64 (for example, a thermocouple) is embedded in the second cylindrical wall member 12 in the vicinity of the lower end 13d of the water evaporation unit 13, and based on the temperature detected by the temperature measuring unit 64. A control device (not shown) monitors the temperature of the water supplied to the water reservoir 38. In addition, the thickness of the reforming heat insulating member 62 and the helical pitch of the reforming heat exchange unit 60 can be set as appropriate so that the temperature of the supplied water at the water inlet 13in can be maintained near 100 ° C.

  On the other hand, the burner 15 is supplied with air supplied from a fuel gas pipe 17 and air supply means (not shown) for guiding the fuel gas recirculated as an off gas of the fuel cell (not shown) to the flame region of the burner 15. An air pipe 21 leading to 15 flame regions is arranged.

  Moreover, in order to guide the combustion gas flowing through the first combustion gas flow path 30 to the atmosphere through the combustion gas outlet 32 formed in the vicinity of the lower end of the first cylindrical wall member 11, the first cylindrical wall member A combustion gas exhaust part 33 is disposed around the vicinity of the lower end of 11, and an exhaust port pipe 34 is disposed at a predetermined position from the combustion gas exhaust part 33 so as to protrude radially outward.

  More specifically, the first cylindrical wall member 11 is formed with a combustion gas outlet 32 as an opening that is uniformly arranged in the circumferential direction, and covers the combustion gas outlet 32 so as to cover the first cylindrical wall member. 11 and a combustion gas exhaust part 33 is disposed so as to extend over the entire circumference of the first cylindrical wall member 11. A cylindrical exhaust pipe 34 is disposed so as to be connected to the combustion gas exhaust section 33 and project in the radial direction thereof.

  Further, in order to guide the reformed gas flowing through the reformed gas channel 45 to the downstream side through the reformed gas outlet 47 formed in the vicinity of the lower end of the cylindrical cover 22, A reformed gas exhaust pipe 48 is disposed so as to protrude outward in the radial direction.

  More specifically, a reformed gas outlet 47 is formed as an opening in the cylindrical cover 22, is connected to the cylindrical cover 22 so as to cover the reformed gas outlet 47, and is cylindrical so as to protrude in the radial direction thereof. The reformed gas exhaust pipe 48 is provided.

  In addition, the area | region enclosed by the 1st, 2nd cylindrical wall members 11 and 12, the support member 43, and the upper wall of the combustion gas exhaust part 33 functions as a space which encloses the mixed gas inside the water evaporation part 13. To do. Further, a region surrounded by the first and second cylindrical wall members 11 and 12, the support member 43, and the disc-like lid member 24 functions as a space for housing the reforming catalyst body 14.

  Next, the configuration of the hydrogen generator 10 related to the combustion gas path will be described in more detail.

  As shown in FIG. 1, the inner diameter of the third cylindrical wall member 16 is smaller than the inner diameter of the first cylindrical wall member 11, thereby the third cylindrical wall member 16 and the first cylindrical wall member. A first combustion gas passage 30 formed of a cylindrical gap is formed between the member 11 and the member 11. The third cylindrical wall member 16 is inserted into the first cylindrical wall member 11 from the lower end of the first cylindrical wall member 11 with a cylindrical gap at the time of assembly. Then, in a state where the third cylindrical wall member 16 is inserted into the first cylindrical wall member 11 and the directions of the first central axes 110 are aligned and fixed, the third cylindrical wall member 16 The lid member 24 closes the upper end of the first cylindrical wall member 11 so as to have an annular gap between the upper end and the upper end. This gap corresponds to the upper combustion gas inlet 31 described later.

  Further, when the third cylindrical wall member 16 is inserted, the annular flange 16a at the lower end of the third cylindrical wall member 16 is packed on the lower wall of the combustion gas exhaust part 33 via a packing (not shown). The third cylindrical wall member 16 is positioned in the axial direction by contact.

  Further, the upper end of the first cylindrical wall member 11 abuts on the lid member 24 and the lower end thereof is brought into contact with the lower wall of the combustion gas exhaust part 33 via a packing (not shown). One cylindrical wall member 11 is fixed.

  Both the first cylindrical wall member 11 and the third cylindrical wall member 16 are seamlessly extended from the vicinity of the upper end 14 u of the reforming catalyst body 14 to the vicinity of the lower end 13 d of the water evaporation section 13. Since it is a metal pipe, the first combustion gas flow path 30 is also formed from the vicinity of the upper end 14 u of the reforming catalyst body 14 to the vicinity of the lower end 13 d of the water evaporation section 13.

  Next, the configuration of the hydrogen generator 10 related to the mixed gas flow path and the reformed gas path will be described in more detail.

  As shown in FIG. 1, the mixed gas inside the water evaporation unit 13 is disposed in a boundary region between the upper end 13 u of the water evaporation unit 13 and the lower end 14 d of the reforming catalyst body 14 to support the reforming catalyst body 14. It flows out to the reforming catalyst body 14 through a plurality of mixed gas ejection holes 43 h formed in the supporting member (partition plate) 43 to be performed. Here, the mixed gas ejection holes 43 h of the support member 43 are formed as a plurality of round holes (diameter: about 1 mm) at a predetermined interval in the circumferential direction of the support member 43. As a result, the mixed gas can be supplied uniformly in the circumferential direction of the reforming catalyst body 14.

  Moreover, the outer periphery of this support member 43 is connected to the 2nd cylindrical wall member 12 as shown in FIG. 1, and the support member 43 is supported by the 2nd cylindrical wall member 12 in the cantilever state. On the other hand, there is an annular gap between the inner periphery of the support member 43 and the first cylindrical wall member 11, and the mixed gas flows from the water evaporation section 13 toward the reforming catalyst body 14 through this annular gap. Needless to say, the support member 43 can be cantilevered by the second cylindrical wall member 12, and the support member 43 may be cantilevered by the first cylindrical wall member 11. Both members may be supported by the members 11 and 12. The shape of the mixed gas ejection hole 43h is not limited to a round hole, and may be any shape such as an oval, an ellipse, or a rectangle.

  As a modification of the support member 43, instead of forming a plurality of mixed gas ejection holes 43 h in the circumferential direction of the support member 43, a mixed gas ejection hole (not shown) is provided only at one location in the circumferential direction of the support member 43. ) May be provided. By providing a single mixed gas ejection hole in this way, when the raw material gas and water vapor inside the water evaporation section 13 flow out toward the reforming catalyst body 14, the raw material gas and water vapor enter the mixed gas ejection hole. The mixed gas can be mixed and promoted to be mixed (however, a separate measure for making the mixed gas uniform in the circumferential direction and supplying it to the reforming catalyst body is necessary).

  The reformed gas released from the axial end of the reforming catalyst body 14 passes through the reformed gas inlet 44 corresponding to the annular gap between the upper end of the second cylindrical wall member 12 and the lid member 24, and passes through the reformed gas inlet 44. It flows out into the reformed gas channel 45 formed between the second cylindrical wall member 12 and the cylindrical cover 22. More specifically, the inner diameter of the second cylindrical wall member 12 is smaller than the inner diameter of the cylindrical cover 22, thereby causing a cylindrical gap between the second cylindrical wall member 12 and the cylindrical cover 22. A reformed gas flow path 45 is formed. The second cylindrical wall member 12 is inserted into the cylindrical cover 22 with a cylindrical gap at the time of assembly. In the state where the second cylindrical wall member 12 is inserted into the cylindrical cover 22 with the directions of the first central axes 110 aligned, a gap is formed between the second cylindrical wall member 12 and the upper end of the second cylindrical wall member 12. Thus, the upper end of the cylindrical cover 22 is closed by the lid member 24. Thus, an annular gap as the reformed gas inlet 44 and a cylindrical gap as the reformed gas channel 45 are formed.

  A round bar 46 is disposed in a gap defined by the second cylindrical wall member 12 and the cylindrical cover 22. More specifically, a flexible round bar 46 is spirally wound around the second cylindrical wall member 12, and the round bar 46 is arranged on the second cylindrical wall member 12 and the cylindrical cover 22. A reformed gas spiral channel 45 </ b> A (reformed gas circumferential direction moving means) is formed in the reformed gas channel 45.

  The cylindrical cover 22 is a seamless stainless steel metal pipe that extends from the vicinity of the upper end 14u of the reforming catalyst body 14 to the vicinity of the lower end 14d.

  Furthermore, the configuration of the hydrogen generator 10 related to the supply water path flowing through the reforming heat exchange unit 60 will be described in more detail.

  A cylindrical modified heat insulating member 62 made of aluminum oxide, silicon oxide, titanium oxide or the like is disposed so as to cover the entire circumference of the cylindrical cover 22, and at least the entire circumference of the modified heat insulating member 62 (here, Further, a metal modified heat insulating member cover 61 is disposed so as to cover the outer peripheral surface and the upper end surface of the modified heat insulating member 62.

  Further, the water flow pipes constituting the reforming heat exchanging unit 60 are arranged in close contact with and spirally around the reforming heat insulating member cover 61.

  As a result, the reforming heat insulating member cover 61 is uniformly heated by the heat of the reforming catalyst body 14 kept at a high temperature via the reforming gas flow path 45, the cylindrical cover 22, and the reforming heat insulating member 62. The water flowing through the reforming heat exchanging unit 60 can be heated by the reforming heat insulating member cover 61 that has been made. Thus, since the reforming heat insulating member cover 61 can be heated using almost the entire amount of the heat released from the reforming catalyst body 14, the heat radiation of the reforming catalyst body 14 can be used as the evaporation heat of the water supplied to the water evaporation section 13 without waste. Can be used effectively.

  Further, a first connection pipe 63 that connects the reforming heat exchanging section outlet 60out and the water inlet 13in of the reforming heat exchanging section 60 is formed by extending the water pipe constituting the reforming heat exchanging section 60. Yes. As a result, the first connecting pipe 63 and the reforming heat exchanger 60 can be shared, and the number of parts can be reduced.

  Here, the water inlet 13in is disposed above the water reservoir 38 so as to avoid the water reservoir 38 formed in an annular shape in the vicinity of the lower end 14d of the water evaporator 14. In addition, the source gas inlet 40in is disposed at the same position as or higher than the water inlet 13in. By doing so, the water inlet 13in and the raw material gas inlet 40in are prevented from being immersed in the water reservoir 38, and the water flowing in the reforming heat exchanger 60 is obstructed by the water reservoir 38. The raw material gas flowing through the first raw material gas pipe 40 can be smoothly introduced into the water evaporation unit 13 without being obstructed by the water reservoir 38. Inflow.

  Further, the reforming heat exchange section outlet 60out is located above the water inlet 13in, and the first connecting pipe 63 that connects the reforming heat exchange section outlet 60out and the water inlet 13in has a first length in the longitudinal direction. The connecting pipes are arranged with a downward slope. By doing so, even if water vapor is generated inside the first connection pipe 63, this water vapor can be quickly discharged to the water evaporation section 13, and the water inlet caused by the water vapor in the middle of the first connection pipe 63. Water discharge pulsation in the vicinity of 13 inches can be suppressed.

  The circulation operation of the combustion gas, mixed gas, reformed gas, and heated water of the hydrogen generator 10 configured as described above will be described in order.

  The fuel gas supplied from the fuel gas inlet port 17in connected to the passage (not shown) of the fuel gas (for example, the off gas of the fuel cell) is guided to the fuel gas pipe 17. Thereafter, the fuel gas rises in the direction of the burner 15 through the fuel gas pipe 17. Subsequently, the flow of the fuel gas is blocked by the fuel gas pipe lid 18 that seals the downstream end of the fuel gas pipe 17, and from there, the fuel gas is in the vicinity of the fuel gas pipe lid 18, and the fuel gas The fuel gas is ejected from a plurality of fuel gas ejection holes 19 provided on the side surface of the pipe 17 to the flame region of the burner 15.

  On the other hand, combustion air supplied from an air inlet port 21in connected to an air supply means (not shown) rises in the direction of the burner 15 through the air pipe 21 and in the vicinity of the downstream end of the fuel gas pipe 17. It is provided around the fuel gas pipe 17 and supplied to the inside of an air buffer 23 formed of an annular hollow body that is recessed in a substantially central shape. Then, the air in the air buffer 23 is ejected from the plurality of air ejection holes 20 formed on the inner surface of the concave concave portion to the flame region of the burner 15. In this way, the combustible gas concentration in the mixed gas containing the fuel gas and the air guided to the flame region of the burner 15 is maintained at the combustible concentration, and the combustible gas is burned, and a high-temperature combustion gas is generated inside the burner 15.

  The combustion gas is released to the outside (in the atmosphere) through the third cylindrical wall member 16 and the inside of the first combustion gas flow path 30 through a path indicated by a dotted line shown in FIG.

  The combustion gas generated in the burner 15 rises inside the third cylindrical wall member 16, and a gap corresponding to the annular upper combustion gas inlet 31 corresponding to the upper end of the third cylindrical wall member 16. The rise is blocked by the lid member 24 arranged at a distance. The blocked combustion gas diffuses along the lid member 24 in the radial direction of the lid member 24 from there, and is guided to the cylindrical first combustion gas passage 30 through the upper combustion gas inlet 31. . Thereafter, the combustion gas gives reaction heat for a reforming reaction (endothermic reaction) by heat exchange from the combustion gas to the reforming catalyst body 14 while being guided downward through the first combustion gas passage 30. After that, evaporating heat is given to the water inside the water evaporation section 13 by heat exchange from the combustion gas. Here, the upper half part of the third cylindrical wall member also functions as a combustion cylinder, and gives heat to the reforming catalyst body 14 by its thermal radiation. The combustion gas that has exchanged heat with the water inside the water evaporation section 13 flows into the combustion gas exhaust section 33 from the combustion gas outlet 32. The inflowing combustion gas passes through the inside of the combustion gas exhaust portion 33 and is discharged to the outside from the exhaust pipe 34.

  Further, the mixed gas containing the raw material gas and the water vapor flows out from the water evaporation section 13 to the reforming catalyst body 14 as follows.

  The source gas supplied to the source gas inlet 40in connected to the source supply means is led to the water evaporation unit 13 through the first source gas pipe 40 and heated water supplied to the water inlet 13in connected to the reforming heat exchange unit 60. Is guided to the water evaporation unit 13 through the first connection pipe 63. Then, a predetermined amount of supply water is stored in the water reservoir 38 of the water evaporation unit 13, and this supply water generates heat of evaporation from the combustion gas by heat exchange with the combustion gas via the first cylindrical wall member 11. Received and evaporated to steam. The vapor thus evaporated is mixed with the raw material gas in the water evaporation section 13 and rises in the axial direction of the water evaporation section 13, and a plurality of mixed gas ejection holes formed in the support member (partition plate) 43 described above. It flows out to the reforming catalyst body 14 through 43h. The mixed gas is reformed into a hydrogen-rich reformed gas by a reforming reaction while passing through the reforming catalyst body 14.

  The reformed gas flows out from the reforming catalyst body 14 through the reformed gas channel 45 to the downstream side, as indicated by a thin one-dot chain line shown in FIG.

  More specifically, the reformed gas generated by reforming the mixed gas as described above in the reforming catalyst body 14 rises inside the reforming catalyst body 14 and is prevented from rising by the lid member 24. . The reformed gas that has been blocked diffuses along the lid member 24 in the radial direction of the lid member 24, and is guided to the reformed gas channel 45 through the reformed gas inlet 44. Thereafter, the reformed gas is moved in the circumferential direction of the reforming catalyst body 14 along the second round bar 46 (bar-shaped member) while being guided downward through the reformed gas spiral channel 45A.

  Thus, the reformed gas flowing through the reformed gas channel 45 flows out to the reformed gas exhaust pipe 48 through the reformed gas outlet 47. The outflowed reformed gas flows out downstream through the reformed gas exhaust pipe 48.

  Further, the supply water flowing inside the reforming heat exchange unit 60 flows into the water evaporation unit 13 as shown by a two-dot chain line shown in FIG.

  The water at room temperature (about 20 ° C.) supplied to the reforming heat exchanging unit 60 via the reforming heat exchanging unit inlet 60 in by the water supply means (shown in the figure) spirals around the reforming heat insulating member cover 61. During the period of flow, the heat is released by the heat released from the reforming catalyst body 14. Thereafter, the heated water that has passed through the first connection pipe 63 from the reforming heat exchange section outlet 60out is supplied to the water evaporation section 13 through the water inlet 13in, and a water pool section is formed inside the water evaporation section 13 by this heating water. 38 is formed. Further, the temperature is optimized by the reforming heat exchanging portion 60 and the reforming heat insulating member 62 so that the temperature of water at the water inlet 13in is about 100 ° C.

  According to such a hydrogen generator 10, since the first, second, and third cylindrical wall members 11, 12, and 16 and the cylindrical cover 22 are all simple cylindrical shapes, the hydrogen generator 10 Durability performance is improved. In particular, for these first, second, and third cylindrical wall members 11, 12, 16 and the cylindrical cover 22, seamless stainless steel metal pipes that have no joints such as welds in the middle of the piping are used. Therefore, it is possible to eliminate the influence on the weld due to the thermal cycle based on the DSS operation in which the start and stop are performed every day.

  Further, the entire circumferential surface from the upper end 14u to the lower end 14d of the reforming catalyst body 14 can be brought into contact with the combustion gas flowing through the first combustion gas flow path 30 via the first cylindrical wall member 11, The reaction heat necessary for the reforming reaction can be efficiently given to the reforming catalyst body 14 from the combustion gas, and the entire surface in the circumferential direction from the upper end 13u to the lower end 13d of the water evaporation section 13 is It is possible to make contact with the combustion gas flowing through the first combustion gas passage 30 via the cylindrical wall member 11, and to efficiently give evaporation heat from the combustion gas to the water inside the water evaporation section 13. Is possible.

  In addition, since the first combustion gas channel 30 can be disposed inside the first cylindrical wall member 11, heat radiation of the combustion gas flowing through the first combustion gas channel 30 can be suppressed.

  Further, since the reformed gas is moved in the circumferential direction of the reforming catalyst body 14, the unevenness of the reformed gas flow in the circumferential direction can be suppressed, and the heat release of the reforming catalyst body 14 kept at a high temperature is spread over the entire circumferential direction. Can be prevented evenly.

  In addition, according to the reforming heat exchange section 60 and the first connection pipe 63 as described above, after the water flowing through the reforming heat exchange section 60 is heated by the heat released from the reforming catalyst body 14, Since the heated water is supplied to the water evaporation unit 14, the heat radiation of the high temperature reforming catalyst body 14 can be used as the evaporation heat of the supply water to the water evaporation unit 13, and the heat dissipation of the reforming catalyst body 14 can be efficiently recovered. Thus, the thermal efficiency of the hydrogen generator 10 can be improved.

  In addition, since almost the entire contact surface between the reforming heat insulating member 62 and the outside (atmosphere) is covered with the metal reforming heat insulating member cover 61, the heat conducted from the reforming catalyst body 14 to the reforming heat insulating member 62. Can be suppressed, and the thermal efficiency of the hydrogen generator 10 can be improved.

  In addition, although the example which distribute | circulates only water to the reforming heat exchange part 60 was demonstrated so far, it is not restricted to this, For example, as shown to sectional drawing (FIG. 2) explaining the modification about source gas supply, The second source gas pipe 65 may be connected to the reforming heat exchange unit 60 on the upstream side of the reforming heat exchange unit inlet 60in, and the source gas may be circulated through the reforming heat exchange unit 60 together with water. However, in this case, the first raw material gas pipe 40 connected to the water evaporation section 13 shown in FIG. 1 is unnecessary, and is removed.

  If it carries out like this, source gas can also be heated simultaneously with water, and it will become possible to perform the temperature rise of the mixed gas containing the water vapor | steam inside the water evaporation part 13 and source gas more smoothly.

(Embodiment 2)
FIG. 3 is a cross-sectional view showing the internal structure of the hydrogen generator according to Embodiment 2 of the present invention.

  The main difference between FIG. 3 and FIG. 1 (Embodiment 1) is that the shift catalyst body 74 removes carbon monoxide gas (CO gas) contained in the reformed gas flowing out from the reformed catalyst body 14. And in place of the reforming heat exchanger 60 (FIG. 1) for recovering the heat released from the reforming catalyst body 14, a shift heat exchanger 70 for recovering the heat released from the shift catalyst body 74 is provided. is there.

  Hereinafter, the configuration of the third embodiment will be described focusing on this difference, and the description of the same configuration and operation as those in FIG. 1 will be omitted.

  The peripheral structure of the shift catalyst body 74 of the hydrogen generator 10 is mainly made of a cylindrical seamless metal that forms a double pipe by sharing a second central axis direction 120 extending in parallel with the first central axis 110 ( A stainless-made shift catalyst inner tube 73, a cylindrical seamless metal (stainless steel) shift catalyst outer tube 71 (metal cover) covering the outer peripheral surface of the shift catalyst inner tube 73, and a shift catalyst inner tube 73 A cylindrical platinum-based shift catalyst body 74 that is disposed and removes CO gas in the reformed gas by a shift reaction, and is disposed in close contact (contact) with the shift catalyst body outer tube 71 and spirally wound, and the shift catalyst body A transformation heat exchanging unit 70 including a water flow pipe that circulates water to be heat exchanged by heat released from 74 is provided. This water flow pipe is composed of a flexible stainless steel metal pipe.

  Further, in order to optimize heat exchange between the shift catalyst body 74 and the feed water flowing through the shift heat exchanger 70, a cylindrical shift heat insulating member 72 is disposed in a region defined by the shift catalyst inner and outer pipes 73 and 71. ing. Here, the CO gas removal unit 100 is configured by the shift catalyst body 74, the shift catalyst inner pipe 73, and the shift catalyst outer pipe 71.

  According to such a configuration, the water flow pipe constituting the shift heat exchange unit 70 is wound in close contact with the periphery of the shift catalyst outer tube 71 in a spiral manner. The transformation catalyst body outer tube 71 can be uniformly heated by the heat of the transformation catalyst body 74 maintained. Then, the water flowing through the shift heat exchanger 70 can be heated by the heated shift catalyst outer tube 71. Thus, the conversion catalyst body outer tube 71 can be heated using almost the entire amount of the heat released from the conversion catalyst body 74, so that the heat release from the conversion catalyst body 74 can be effectively utilized as the evaporation heat of the supplied water to the water evaporation section 13 without waste. Can do.

  Further, both ends of the shift catalyst body 74 in the axial direction of the shift catalyst body 74 disposed inside the shift catalyst body pipe 73 are disk-shaped first and second shift transitions having a large number of punch holes 76h and 77h for the flow of reformed gas. It is supported by catalyst body punch metals 76 and 77.

In addition, the interior in the vicinity of the upper end of the shift catalyst internal pipe 73 is connected to the reformed gas outlet 47 via the reformed gas exhaust pipe 48. Further, the shift heat exchanger outlet 70out of the shift heat exchanger 70 is The water inlet 13in is connected via a second connection pipe 75 (second connection member) formed by extending a water flow pipe constituting the metamorphic heat exchange section 70. As a result, it is possible to share the members of the second connecting pipe 75 and the shift heat exchanger 70.

  In addition, the water inlet 13in is disposed above the water reservoir 38 so as to avoid the annular water reservoir 38 formed in the vicinity of the lower end 14d of the water evaporator 14, and the source gas inlet 40in It is disposed at the same position as or higher than the inlet 13in. By doing so, the water inlet 13in and the raw material gas inlet 40in are prevented from being immersed in the water reservoir 38, and the water flowing inside the reforming heat exchanger 60 is obstructed by the water reservoir 38. And can smoothly flow out into the water evaporating unit 13, and the source gas flowing through the first source gas pipe 40 can smoothly enter the water evaporating unit 13 without being obstructed by the water reservoir 38. It can leak.

  Further, the second connection pipe extends over the entire length in the longitudinal direction of the second connection pipe 75 in which the transformation heat exchange section outlet 70out is located above the water inlet 13in and connects the transformation heat exchange section outlet 70out and the water inlet 13in. 75 is arranged with a downward slope.

  By doing so, even if water vapor is generated inside the second connection pipe 75, this water vapor can be quickly discharged to the water evaporation section 13, and the water inlet caused by the water vapor in the middle of the second connection pipe 75. Water discharge pulsation in the vicinity of 13 inches can be suppressed.

  In such a configuration, the reformed gas flowing out from the reformed gas outlet 47 circulates inside the shift catalyst body 74 as shown by a thin dashed-dotted path shown in FIG.

  The reformed gas guided from the reformed gas exhaust pipe 48 to the inside of the shift catalyst body pipe 73 is directed downward by the upper lid of the shift catalyst body pipe 73 to punch the first shift catalyst body punch metal 76. It passes through the hole 76 h and flows into the shift catalyst body 74. Then, during the period in which the reformed gas passes through the inside of the shift catalyst body 74, a shift reaction (exothermic reaction) that generates carbon dioxide gas and hydrogen gas from the CO gas and water contained in the reformed gas by the shift catalyst body 74. ) To remove CO gas. Thereafter, the reformed gas after the removal of the CO gas flows out downstream through the shift exhaust pipe 78 via the punch holes 77h of the second shift catalyst body punch metal 77.

  On the other hand, the water flowing in from the shift heat exchanger inlet 70in flows through the shift heat exchanger 70 like a two-dot chain path shown in FIG.

  A period in which water at room temperature (about 20 ° C.) supplied to the shift heat exchanger 70 via the shift heat exchanger inlet 70 in by the water supply means (shown) flows spirally around the shift catalyst outer tube 71. It is heated by the heat released from the shift catalyst body 74. Thereafter, the heated water that has passed through the second connection pipe 75 from the transformation heat exchanger outlet 70out is supplied to the water evaporator 13 through the water inlet 13in, and the water reservoir 38 is provided inside the water evaporator 13 by this heated water. Is formed. The temperature of the water at the water inlet 13in is optimized by the shift heat exchanger 70, the shift heat insulation member 72, and the like so that the temperature of the water is about 100 ° C.

  In this way, the CO gas that poisons the catalyst body of the fuel cell can be removed and the heat released from the shift catalyst body 14 can be recovered. That is, since the temperature of the shift catalyst body 74 during the shift reaction is maintained at about 300 ° C. to 350 ° C., after the water flowing through the shift heat exchanger 70 is heated by the heat release of the shift catalyst body 74, Heated water can be supplied to the inside of the water evaporation section 13 through the connection pipe 75. Therefore, the heat release of the shift catalyst body 74 can be effectively utilized as the heat of evaporation of the feed water supplied to the water evaporation section 13, the heat release of the shift catalyst body 14 can be recovered, and the thermal efficiency of the hydrogen generator 10 can be improved.

  In addition, since almost the entire contact surface between the shift heat insulating member 72 and the outside (atmosphere) is covered by the metal shift catalyst body outer tube 71, the heat conducted from the shift catalyst body 14 to the shift heat insulating member 62 is released to the atmosphere. Therefore, the thermal efficiency of the hydrogen generator 10 can be improved.

  Here, in the second embodiment, an example in which heated water flowing through the shift heat exchanger 70 is supplied to the water evaporator 13 for supplying the reformed catalyst body 14 with the mixed gas containing the raw material gas and the water vapor. As described above, this heated water may be supplied to a water evaporation section (not shown) that generates water vapor for shift reaction in the shift catalyst body 74.

  In addition, although the example which distribute | circulates only water to the transformation heat exchange part 70 was demonstrated so far, it is not restricted to this, For example, as shown in sectional drawing (FIG. 4) explaining the modification about raw material gas supply, a transformation is carried out. A third source gas pipe 79 may be connected to the shift heat exchanger 70 upstream of the heat exchanger inlet 70in, and the source gas may be circulated through the shift heat exchanger 70 together with water. However, in this case, the first raw material gas pipe 40 connected to the water evaporation section 13 shown in FIG. 3 is unnecessary, and is removed.

  If it carries out like this, source gas can also be heated simultaneously with water, and it will become possible to perform the temperature rise of the mixed gas containing the water vapor | steam inside the water evaporation part 13 and source gas more smoothly.

(Embodiment 3)
FIG. 5 is a cross-sectional view showing the internal structure of the hydrogen generator according to Embodiment 3 of the present invention.

  In the third embodiment, both the reforming heat exchanging unit 60 (the first embodiment; FIG. 1) and the transformation heat exchanging unit 70 (the second embodiment; FIG. 3) are provided. The reforming heat exchange part outlet 60out and the transformation heat exchange part inlet 70in of the transformation heat exchange part 70 are connected to each other by a third connection pipe 80 (third connection member).

  Here, the hydrogen generation apparatus 10 other than the case where the reforming and transformation heat exchange units 60 and 70 are connected to each other by the third connecting pipe 80 and the supply water is allowed to flow inside the reforming and transformation heat exchange units 60 and 70. The configuration of is the same as that described in the first embodiment or the second embodiment, and the distribution operation of the combustion gas and the distribution operation of the reformed gas are the same as those described in the first embodiment or the second embodiment. Since they are the same, their description is omitted.

  The reforming heat exchange section 60 is constituted by a water pipe made of a metal pipe spirally wound in the circumferential direction around the reforming heat insulating member cover 61, and the water pipe is extended to form a third connection. A pipe 80 is formed, and further, the water passage pipe is extended to form a shift heat exchanging portion 70 spirally wound around the shift catalyst outer pipe 71 in the circumferential direction, and the water flow pipe is further extended. Thus, the second connection pipe 75 is formed. This makes it possible to share the members of the reforming heat exchange unit 60, the third connection pipe 80, the transformation heat exchange unit 70, and the second connection pipe 75.

  Here, the feed water flowing inside the reforming heat exchange unit 60 flows into the shift heat exchange unit 70 as indicated by a two-dot chain line shown in FIG. 5, and the feed water flowing inside the shift heat exchange unit 70 is 5 flows into the water evaporation section 13 as indicated by a two-dot chain line shown in FIG.

  The water at room temperature (about 20 ° C.) supplied to the reforming heat exchanger 60 via the reforming heat exchanger inlet 60 in by a water supply means (not shown) spirals around the reforming heat insulating member cover 61. The heat is released by the heat released from the reforming catalyst body 14. And the heating water which passed through the 3rd connection pipe 80 from the reforming heat exchange part outlet 60out is supplied to the transformation heat exchange part 70 via the transformation heat exchange part inlet 70in. Subsequently, the heated water supplied to the shift heat exchanger 70 is heated again by the heat released from the shift catalyst body 74 while spirally flowing around the shift catalyst body outer pipe 71, and then the second water. The water is supplied from the water inlet 13in to the inside of the water evaporation part 13 through the connecting pipe 75, and the water reservoir part 38 is formed inside the water evaporation part 13 by this heated water. Further, the temperature of water at the water inlet 13in is optimized by the reforming heat exchange section 60, the reforming heat insulating member 62, the shift heat exchanging section 70, the shift heat insulating member 72, and the like so that the temperature of the water becomes about 100 ° C.

  In this way, while the supply water flows through the inside of the reforming heat exchanger 60, the inside feed water can be heated by the heat released from the reforming catalyst body 14, and the inside of the shift heat exchanger 70 is supplied to the feed water. Since the feed water in the inside can be heated by the heat released from the shift catalyst body 74 during the circulation, the heat radiation of both the catalyst bodies 14 and 74 is effectively utilized as the evaporation heat of the feed water to the water evaporation section 13. The thermal efficiency of the hydrogen generator 10 can be improved.

  As in the first and second embodiments, the raw material gas may be flowed together with the feed water flowing through the reforming heat exchange unit 60 and the modified heat exchange unit 70.

(Embodiment 4)
FIG. 6 is a cross-sectional view showing the internal structure of the hydrogen generator according to Embodiment 4 of the present invention.

  In the first to third embodiments, the burner 15 is inserted into the interior of the first cylindrical wall member 11 from the bottom to the top so that the flame of the burner 15 is directed upward (the upper side in FIG. 1). However, in the fourth embodiment, the burner 15 is arranged at the upper end of the first cylindrical wall member 11 with its direction reversed 180 ° so that the flame of the burner 15 is directed downward.

  In the first to third embodiments, a CO gas removing unit 100 which will be described in detail later is provided in a region surrounded by the water evaporation unit 13 and housing the burner 15.

  Hereinafter, the structure regarding the burner 15 and the CO gas removal part 100 is demonstrated.

  First, the structure of the burner 15 facing down the flame will be described.

  According to FIG. 6, as compared with FIG. 1 (Embodiment 1), the lid member 24 is removed, and the combustion cylinder 50 is inserted into the third cylindrical wall member 16 from its upper end. The lower end 50A of the combustion cylinder 50 is positioned near the center in the axial direction of the first cylindrical wall member 11 (third cylindrical wall member 16) (in the vicinity of the lower end 14d of the reforming catalyst body 14). Here, the annular flange 50S provided at the upper end 50B of the combustion cylinder 50 is brought into contact with the upper ends of the first cylindrical wall member 11 and the cylindrical cover 22 to position the combustion cylinder 50 in the axial direction. Yes. In addition, the upper end of the hydrogen generator 10 surrounded by the cylindrical cover 22 is covered by the flange 50S except for the inner region of the combustion cylinder 50, and the flange 50S serves as the lid member 24 in the first embodiment. (Role as a lid member provided above the first, second, and third cylindrical wall members 11, 12, and 16). And the burner 15 is connected to this collar part 50S.

  Further, the disc-shaped partition member 51 opposes the lower end 50A of the combustion cylinder 50 in the vicinity of the lower end 50A of the combustion cylinder 50, blocks the lower side of the combustion cylinder 50, and covers the inside of the third cylindrical wall member 16. It is arranged to partition.

  The cylindrical gap between the combustion cylinder 50 and the third cylindrical wall member 16 is used as the second combustion gas flow path 53, and the third cylindrical wall member 16 and the first cylindrical wall member are used. A cylindrical gap between 11 is used as the first combustion gas flow path 30.

  More specifically, the inner diameter of the combustion cylinder 50 is smaller than the inner diameter of the third cylindrical wall member 16, whereby a first cylindrical gap is formed between the combustion cylinder 50 and the third cylindrical wall member 16. A second combustion gas passage 53 is formed. The combustion cylinder 50 is inserted into the inside thereof from the upper end of the third cylindrical wall member 16 with a cylindrical gap at the time of assembly. In a state where the combustion cylinder 50 is inserted into the third cylindrical wall member 16 with the directions of the first central axes 110 aligned, an annular gap is provided between the combustion cylinder 50 and the lower end 50A of the combustion cylinder 50. A disc-shaped partition member 51 is arranged. This gap corresponds to the lower combustion gas inlet 52. Note that the configuration of the first combustion gas channel 30 is the same as that of the first embodiment, and thus detailed description thereof is omitted.

  In this way, as shown in FIG. 6, the combustion gas flow path is formed by the third cylindrical wall member 16 inserted in the region between the combustion cylinder 50 and the first cylindrical wall member 11 so that the second combustion gas flow. From the passage 53 toward the first combustion gas passage 30, it is bent in a U shape with the upper combustion gas inlet 31 as a boundary.

  Next, the configuration of the CO gas removal unit 100 housed in the region surrounded by the water evaporation unit 13 will be described.

  According to FIG. 6, a cylindrical CO gas removing portion 100 is disposed in the third cylindrical wall member 16 from the lower end thereof so that both the first central axes 110 coincide with each other.

  The CO gas removing unit 100 mainly includes a cylindrical CO gas removing unit inner pipe 93 that forms a double pipe by sharing the first central axis 110 and a cylindrical CO gas removing unit that covers the CO gas removing unit inner pipe 93. Supports the axially opposite ends of the outer / outer tube 92, the cylindrical CO gas removing unit catalyst body 98 disposed in the region defined by the inner and outer tubes 93 and 92, and the cylindrical CO gas removing unit catalyst body 98. In addition, annular first and second CO gas removal unit punch metals 96 and 97 having a large number of punch holes 96h and 97h, and CO gas removal unit upper and lower lids 95 that block both axial ends of the CO gas removal unit outer tube 92 , 94. And the inner pipe 93 has penetrated the center part of the CO gas removal part lower cover 94 to the up-down direction.

  Further, between the partition member 51 and the CO gas removing unit upper cover 95 (the end wall of the CO gas removing unit), a disk-shaped first CO gas removing unit heat insulating member 90 covers the surface of the CO gas removing unit upper cover 95. A cylindrical second CO gas removal unit heat insulating member 91 is packed between the CO gas removal unit outer tube 92 (the surrounding wall of the CO gas removal unit) and the third cylindrical wall member 16 so as to cover the cover. The CO gas removal unit outer tube 92 is packed so as to cover the outer peripheral surface. In this way, the first CO gas removal unit heat insulating member 90 prevents the CO gas removal unit 100 from being overheated by the high-temperature (about 1000 ° C.) combustion gas inside the burner 15. Further, by changing the heat insulation condition of the second CO gas removal unit heat insulation member 91, the amount of heat transferred by heat exchange between the first combustion gas flow path 30 and the cylindrical CO gas removal unit catalyst body 98 can be reduced. The cylindrical CO gas removing unit catalyst body 98 can be appropriately controlled and can be maintained at a desired temperature.

  Further, the lower end of the shift catalyst internal pipe 73 and the vicinity of the lower end of the CO gas removal section outer pipe 92 are connected by the shift exhaust pipe 78, and the reformed gas flowing out of the shift catalyst internal pipe 73 is converted into CO through the shift exhaust pipe 78. The gas can be introduced into the gas removal portion outer tube 92.

  Here, the operation of the hydrogen generator 10 configured as described above will be described.

  Note that the operation of supplying the fuel gas and air to the burner 15 is the same as that of the first embodiment, and therefore the description thereof is omitted.

  The combustible gas concentration in the mixed gas containing the fuel gas and air guided to the flame region of the burner 15 is maintained at the combustible concentration, and the combustible gas is burned to generate a high-temperature combustion gas.

  The combustion gas generated by the combustion descends inside the combustion cylinder 50, and the combustion gas passes through the lower combustion gas inlet 52 as shown by the dotted line in FIG. It is formed between the third cylindrical wall member 16 and the first cylindrical wall member 11 through the second combustion gas channel 53 and the upper combustion gas inlet 31 formed between the wall members 16. The first combustion gas passage 30 is circulated.

  More specifically, the combustion gas generated in the burner 15 descends inside the combustion cylinder 50 and is prevented from descending by a partition member 51 arranged with a gap from the lower end 50A of the combustion cylinder 50. The blocked combustion gas diffuses along the partition member 51 in the radial direction of the partition member 51, passes through the annular lower combustion gas inlet 52, and is formed into a cylindrical second combustion gas flow channel 53. Led inside. Thereafter, while the high-temperature combustion gas is guided upward through the second combustion gas flow channel 53, the first cylindrical wall member 11 and the first combustion gas flow channel 30 with respect to the reforming catalyst body 14. In addition, reaction heat for the endothermic reforming reaction supplied from the combustion gas is given through the third cylindrical wall member 16 (for example, the heat is improved by radiant heat transfer of the third cylindrical wall member 16 heated by the combustion gas). The catalyst body 14 is heated.) The combustion gas rising in the second combustion gas flow channel 53 is blocked from rising by the flange portion 50 </ b> S arranged at a distance from the upper end of the third cylindrical wall member 16. The blocked combustion gas diffuses along the flange 50S in the radial direction of the flange 50S from there, passes through the annular upper combustion gas inlet 31, and the cylindrical first combustion gas flow path 30. Led inside.

  That is, the first and second combustion gas passages 30 and 53 are provided, and the combustion gas is raised from the vicinity of the lower end 14d of the reforming catalyst body toward the vicinity of the upper end 14u in the second combustion gas passage 53. At the same time, the combustion gas is lowered in the first combustion gas flow path 30 from the vicinity of the upper end 14u of the reforming catalyst body toward the vicinity of the lower end 14d.

  Thereafter, the combustion gas that has flowed into the first combustion gas flow path 30 is released to the outside (atmosphere) of the hydrogen generator 10 through the same path as described in the first embodiment.

  As described above, by forming the flame of the burner 15 downward, the combustion product (for example, metal oxide) generated on the surface of the burner 15 or the combustion cylinder 50 that has been heated and dropped is partitioned. It can be deposited on the member 51, and the combustion product can prevent the air ejection hole 20 and the fuel gas ejection hole 19 of the burner 15 from being blocked.

  Further, since the burner 15 is inverted 180 ° and installed above the reforming catalyst body 14, access to the burner 15 at the time of maintenance work becomes easy, and maintenance workability of the burner 15 is improved.

  Further, the combustion gas flow is divided into first and second combustion gas flow paths 30 and 53 and the combustion gas is raised along the axial direction of the reforming catalyst body 14 and then lowered. By adopting the path, the heat transfer characteristic of the combustion gas with respect to the axial direction of the reforming catalyst body 14 (temperature gradient of the reforming catalyst body 14) can be improved.

  Specifically, the temperature of the combustion gas is highest immediately after flowing out of the combustion cylinder 50 (in the vicinity of the lower combustion gas inlet 52), and thereafter, the reaction heat necessary for the reforming reaction is converted from the combustion gas to the reforming catalyst body. As the gas passes through the first and second combustion gas passages 30 and 53 while being supplied to the fuel gas 14, the temperature of the combustion gas decreases. As an example of the change in the combustion gas temperature, the temperature of the combustion gas is 1000 ° C. at the lower combustion gas inlet 52, and the temperature of the combustion gas is 800 ° C. at the upper combustion gas inlet 31. Under such conditions, the first combustion gas passage 30 may be omitted, and the reaction heat necessary for the reforming reaction may be given to the reforming catalyst body 14 only by the second combustion gas passage 53. Assuming that the temperature difference (200 ° C.) between the combustion gases at the upper and lower combustion gas inlets 31 and 52 is directly reflected in the temperature difference between the upper end 14 u and the lower end 14 d of the reforming catalyst body 14. A temperature gradient is caused in the axial direction due to the temperature difference of the combustion gas.

  On the other hand, the first and second combustion gas passages 30 and 53 are provided as in the second embodiment, and the combustion gas is transferred from the lower end 14d of the reforming catalyst body to the upper end in the second combustion gas passage 53. In the second combustion gas channel 53 described above, the combustion gas is lowered toward the lower end 14d from the upper end 14u of the reforming catalyst body in the first combustion gas channel 30. The generated axial temperature gradient with respect to the reforming catalyst body 14 can be offset by the axial temperature gradient with respect to the reforming catalyst body 14 generated in the first combustion gas path 30. That is, in the vicinity of the lower end 14d of the reforming catalyst body 14, the temperature of the combustion gas flowing through the second combustion gas passage 53 is on the high temperature side, while the temperature of the combustion gas flowing through the first combustion gas passage 30 is high. Is on the low temperature side. On the other hand, in the vicinity of the upper end 14u of the reforming catalyst body 14, the temperature of the combustion gas flowing through the second combustion gas channel 53 is on the low temperature side, while the first combustion gas channel 30 The temperature of the combustion gas flowing through is on the high temperature side. Therefore, the combustion gas flowing through the first combustion gas flow channel 30 is made uniform by the difference in the temperature of the combustion gas flowing through both flow channels 53 and 30, and the lower end 14d of the reforming catalyst body 14 having a lower temperature than that of the first embodiment. Therefore, the amount of heat transferred to the upper end 14u having a high temperature is reduced, and the temperature gradient in the axial direction of the entire reforming catalyst body 14 can be made small and uniform. Therefore, it becomes easy to set the reforming catalyst body 14 in a desired temperature range (for example, 550 ° C. to 650 ° C.), and the entire reforming catalyst body 14 can be used effectively. Durability can be improved by reducing the amount and preventing the high temperature of the local reforming catalyst body 14.

  Further, the reformed gas flows inside the CO gas removing unit 100 through a path indicated by a thin one-dot chain line shown in FIG. Note that the operation of the reformed gas upstream of the shift catalyst body 74 is the same as that already described, and thus the description thereof is omitted.

  In order to remove the CO gas in the reformed gas flowing out from the shift catalyst body 74 to the shift exhaust pipe 78, the reformed gas is guided into the inner pipe 92 of the CO gas removal section, and the flow direction is directed upward. It is done. Thereafter, the reformed gas passes through the punch hole 97h of the second CO gas removal unit punch metal 97 and passes through the inside of the cylindrical CO gas removal unit catalyst body 98 upward. The contained CO gas is removed. After that, the reformed gas after passing through the punch hole 96h of the first CO gas removal unit punch metal 96 is directed downward by the CO gas removal unit upper lid 95, and the inside of the CO gas removal unit inner pipe 93 Flows downward and flows downstream.

  The cylindrical CO gas removal section catalyst body 98 may be the shift catalyst for the shift reaction already described (however, the temperature conditions are different), and a small amount of oxygen gas (the oxygen gas inflow path is illustrated in FIG. (Not shown) may be a platinum-based CO selective oxidation catalyst body in which CO gas in the reformed gas is converted into carbon dioxide gas by mixing with reformed gas.

  According to such a hydrogen generator 10, the CO gas removing unit 100 can be accommodated by effectively using the region surrounded by the water evaporation unit 13, and the configuration of the hydrogen generator 10 can be simplified.

  Further, when a shift catalyst body is used as the cylindrical CO gas removal portion catalyst body 98, the catalyst body temperature is maintained at 150 to 200 ° C, and when a CO selective oxidation catalyst body is used, the catalyst body temperature is maintained at 100 to 150 ° C. Is done. Therefore, depending on the temperature conditions of the water evaporation section 13 and the cylindrical CO gas removal section catalyst body 98, it may be possible to promote the evaporation of the water evaporation section 13 by the heat radiation of the cylindrical CO gas removal section catalyst body 98. In some cases, the temperature rise of the cylindrical CO gas removal unit catalyst body 98 can be maintained by heat radiation from the water evaporation unit 13, and the CO gas removal unit catalyst body 98 is improved so as to increase the thermal efficiency of the hydrogen generator 10. The type, the thickness of the CO gas removing portion heat insulating member 91, and the like can be selected as appropriate.

  Note that the reformed gas that has flowed out of the shift exhaust pipe 78 from the CO gas removal unit 100 is first guided to the CO gas removal unit inner pipe 93 and flows upward, and then around the CO gas removal unit inner pipe 93. You may let the inside of the installed cylindrical CO gas removal part catalyst body 98 pass below. Depending on the temperature conditions of the catalyst bodies of the water evaporation section 13 and the CO gas removal section 100, this may make it easier to optimize heat exchange between the water evaporation section 13 and the CO gas removal section catalyst body 98.

  As described above, in the fourth embodiment, the configuration of the CO gas removing unit 100, the peripheral configuration thereof, and the operation of the reformed gas flowing through the CO gas removing unit 100 have been described. explain.

[First modification]
The first modification is arranged inside the CO gas removal unit inner pipe 93 instead of the cylindrical CO gas removal unit catalyst body 98 arranged in the region partitioned by the CO gas removal unit inner and outer pipes 93 and 92. A cylindrical CO gas removing part catalyst body 99 is provided. That is, as shown in FIG. 7 which is a cross-sectional view of the internal structure of the first modification of the hydrogen generator, the columnar CO gas removal unit catalyst body 99 is disposed inside the CO gas removal unit inner pipe 93, and Disc-shaped third and fourth CO gas removal unit punch metals 101 and 102 having a large number of punch holes 101h and 102h are arranged so as to support both axial ends of the columnar CO gas removal unit catalyst body 99. Yes.

  Here, the reformed gas flowing out from the modified exhaust pipe 78 is guided downstream through a path illustrated by a thin one-dot chain line shown in FIG.

  In order to remove the CO gas in the reformed gas flowing out from the shift exhaust pipe 78, the reformed gas is guided to the inside of the CO gas removing unit inner pipe 92, and the flow direction is directed upward. Thereafter, the rising of the reformed gas is blocked by the upper cover 95 of the CO gas removing unit, the direction of the reformed gas is directed downward, and passes through the punch hole 101h of the CO gas removing unit punch metal 101. The CO gas removal unit inner pipe 93 flows downward. Then, the CO gas contained in the reformed gas is removed while the reformed gas passes through the inside of the columnar CO gas removal portion catalyst body 99 downward. Subsequently, the reformed gas after the removal of the CO gas flows out downstream through the punch hole 102h of the fourth CO gas removal portion punch metal 102.

  The columnar CO gas removal part catalyst body 99 may be the shift catalyst for the shift reaction already described (however, the temperature conditions are different), and a small amount of oxygen gas (the oxygen gas inflow path is illustrated in FIG. (Not shown) may be a platinum-based CO selective oxidation catalyst body in which CO gas in the reformed gas is converted into carbon dioxide gas by mixing with reformed gas.

  Depending on the temperature conditions of the catalyst bodies of the water evaporation section 13 and the CO gas removal section 100, it is more likely that the columnar CO gas removal section catalyst body 99 is disposed inside the CO gas removal section inner pipe 93 and the water evaporation section 13 and CO In some cases, it is easy to optimize heat exchange with the gas removal portion catalyst body 99.

  The reformed gas that has flowed out of the shift exhaust pipe 78 from the CO gas removal unit 100 is first guided to the CO gas removal unit inner pipe 93 and directed upward in the columnar CO gas removal unit catalyst body 99. Then, the periphery of the CO gas removal unit inner pipe 93 may be passed downward. Depending on the temperature conditions of the catalyst bodies of the water evaporation section 13 and the CO gas removal section 100, this may make it easier to optimize the heat exchange between the water evaporation section 13 and the CO gas removal section catalyst body 99.

[Second modification]
In the second modification, the second CO gas removing portion heat insulating member 91 shown in FIG. 6 is eliminated, and the lower end 16d in the axial direction of the third cylindrical wall member 16 is connected to the first CO gas removing portion heat insulating member. It matches with the lower surface of 90.

  That is, as shown in FIG. 8 which is a cross-sectional view of the internal structure of the second modification of the hydrogen generator 10, the combustion gas flow path is bordered by the axial lower end 16d of the third cylindrical wall member 16. The first combustion gas flow path 30 and the CO gas removal portion outer tube 92 formed in the region partitioned by the third cylindrical wall member 16 and the first cylindrical wall member 11 and the first cylindrical wall The third combustion gas flow path 103 formed in a region partitioned by the member 11 is divided into a structure. Note that the lower end of the third combustion gas channel 103 is closed by a hollow disk-shaped gas channel sealing lid 85.

  With such a combustion gas flow path, it is possible to reduce the number of parts such as a heat insulating member.

(Embodiment 5)
FIG. 9 is a cross-sectional view showing the internal structure of the hydrogen generator according to Embodiment 5 of the present invention.

  The hydrogen generator 10 reverses the direction of the burner 15 by 180 ° so that the flame of the burner 15 is directed downward as shown in the fourth embodiment (FIG. 6) of the burner 15 shown in the third embodiment (FIG. 5). The CO gas removal unit 100 and its peripheral members shown in FIG. 6 are placed inside the water evaporation unit shown in FIG. 5 after being placed above the first cylindrical wall member 11. is there. The configuration of the hydrogen generator 10, the distribution operation of the combustion gas, the distribution operation of the reformed gas, and the distribution operation of the feed water to the water evaporation unit 13 have already been described, and description thereof will be omitted.

  According to the hydrogen generator 10 of FIG. 9, it is possible to recover the heat released from both the reforming catalyst body 14 and the shift catalyst body 74 as the evaporation heat of the feed water flowing into the water evaporation section 13. Since the CO gas removal unit 100 is disposed inside the water evaporation unit and heat exchange between the CO gas removal unit 100 and the water evaporation unit 13 can be performed efficiently, the thermal efficiency of the hydrogen generator 10 is maximized. be able to.

  The hydrogen generation apparatus according to the present invention can be applied to applications such as a domestic fuel cell power generation apparatus that performs DSS operation while simplifying the configuration of the gas flow path and efficiently recovering the heat radiation of the catalyst body. .

It is sectional drawing which shows the internal structure of the hydrogen generator which concerns on Embodiment 1 of this invention. FIG. 6 is a cross-sectional view illustrating a modified example of source gas supply in the first embodiment. It is sectional drawing which shows the internal structure of the hydrogen generator which concerns on Embodiment 2 of this invention. Sectional drawing explaining the modification about source gas supply in Embodiment 2 It is sectional drawing which shows the internal structure of the hydrogen generator which concerns on Embodiment 3 of this invention. It is sectional drawing which shows the internal structure of the hydrogen generator which concerns on Embodiment 4 of this invention. It is sectional drawing explaining the 1st modification of the hydrogen generator which concerns on Embodiment 4 of this invention. It is sectional drawing explaining the 2nd modification of the hydrogen generator which concerns on Embodiment 4 of this invention. It is sectional drawing which shows the internal structure of the hydrogen generator which concerns on Embodiment 5 of this invention.

Explanation of symbols

DESCRIPTION OF SYMBOLS 10 Hydrogen generator 11 1st cylindrical wall member 12 2nd cylindrical wall member 13 Water evaporation part 13in Water inlet 14 Reforming catalyst body 15 Burner 16 Third cylindrical wall member 17 Fuel gas piping 17in Fuel gas inlet Port 18 Fuel gas pipe lid 19 Fuel gas jet hole 20 Air jet hole 21 Air pipe 21 in Air inlet port 22 Cylindrical cover 23 Air buffer 24 Lid member 27 Heat insulating member 30 First combustion gas flow path 31 Upper combustion gas inlet 32 Combustion gas outlet 33 Combustion gas exhaust part 34 Exhaust outlet pipe 38 Reservoir part 40 First raw material gas pipe 40in Raw material gas inlet 43 Support member 43h Mixed gas injection hole 44 Reformed gas inlet 45 Reformed gas flow path 45A Gas gas spiral channel 46 Round bar 47 Reformed gas outlet 48 Reformed gas exhaust pipe 50 Combustion cylinder 50A Lower end 50B of combustion cylinder Upper end 50S of combustion cylinder 1 Partition member 52 Lower combustion gas inlet 53 Second combustion gas flow path 60 Reforming heat exchange section 60in Reforming heat exchange section inlet 60out Reforming heat exchange section outlet 61 Reforming heat insulating member cover 62 Reforming heat insulating member 63 One connecting pipe 64 Temperature measuring means 65 Second raw material gas pipe 70 Metamorphic heat exchanging section 70 in Metamorphic heat exchanging section inlet 70 out Metamorphic heat exchanging section outlet 71 Metamorphic catalyst outer pipe 72 Metamorphic heat insulating member 73 Metacatalytic inner pipe 74 Metacatalytic body 75 Second connection pipe 76 First shift catalyst body punch metal 76h First shift catalyst body punch metal punch hole 77 Second shift catalyst body punch metal 77h Second shift catalyst body punch metal punch hole 78 Exhaust pipe 79 Third source gas pipe 80 Third connection pipe 85 Gas flow path sealing lid 90 First CO gas removal part heat insulation member 91 Second CO gas removal part heat insulation part Material 92 CO gas removal portion outer tube 93 CO gas removal portion inner tube 94 CO gas removal portion lower cover 95 CO gas removal portion upper cover 96 First CO gas removal portion punch metal 96h Punch hole 97 of first CO gas removal portion punch metal Second CO gas removal part punch metal 97h Punch hole 98 of the second CO gas removal part punch metal Cylindrical CO gas removal part catalyst body 99 Columnar CO gas removal part catalyst body 100 CO gas removal part 101 Third CO Gas removal part punch metal 101h Third CO gas removal part punch metal punch hole 102 Fourth CO gas removal part punch metal 102h Fourth CO gas removal part punch metal punch hole 103 Third combustion gas flow path 110 First central axis 120 Second central axis

Claims (3)

A cylindrical water evaporation section through which a mixed gas of raw material gas and water vapor flows, a cylindrical reforming catalyst body that generates reformed gas using the mixed gas from the water evaporation section, and an outflow from the reforming catalyst body CO gas removing section having a catalyst body for removing carbon monoxide gas in the reformed gas to be burned, a burner for generating combustion gas by combustion of combustible gas, and a cylindrical combustion gas flow path through which the combustion gas flows And comprising
The reforming catalyst body is provided in parallel with the central axis in an extension line of the central axis of the water evaporation section,
The CO gas removal unit is provided in parallel with the water evaporation unit with respect to the central axis,
The combustion gas flow path is provided in parallel to the central axis inside the reforming catalyst body and the water evaporation section, and after the combustion gas has transferred heat to the reforming catalyst body, the water evaporation section And a hydrogen generator configured to transfer heat to the CO removal unit The hydrogen generator according to claim 1 , wherein the catalyst body is a shift catalyst body that shifts the carbon monoxide gas . The catalyst body, the hydrogen generating apparatus according to claim 1 wherein a carbon monoxide selective oxidation catalyst body for selective oxidation.