JP2006137668A - Hydrogen producing apparatus and fuel cell generating set - Google Patents

Hydrogen producing apparatus and fuel cell generating set Download PDF

Info

Publication number
JP2006137668A
JP2006137668A JP2005336918A JP2005336918A JP2006137668A JP 2006137668 A JP2006137668 A JP 2006137668A JP 2005336918 A JP2005336918 A JP 2005336918A JP 2005336918 A JP2005336918 A JP 2005336918A JP 2006137668 A JP2006137668 A JP 2006137668A
Authority
JP
Japan
Prior art keywords
temperature
operation
gas
apparatus
unit
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
JP2005336918A
Other languages
Japanese (ja)
Other versions
JP4664808B2 (en
Inventor
Seiji Fujiwara
Yukimune Kani
Kiyoshi Taguchi
Kunihiro Ukai
Hidenobu Wakita
幸宗 可児
清 田口
英延 脇田
誠二 藤原
邦弘 鵜飼
Original Assignee
Matsushita Electric Ind Co Ltd
松下電器産業株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to JP2004014751 priority Critical
Application filed by Matsushita Electric Ind Co Ltd, 松下電器産業株式会社 filed Critical Matsushita Electric Ind Co Ltd
Priority to JP2005336918A priority patent/JP4664808B2/en
Publication of JP2006137668A publication Critical patent/JP2006137668A/en
Application granted granted Critical
Publication of JP4664808B2 publication Critical patent/JP4664808B2/en
Application status is Active legal-status Critical
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00Enabling technologies or technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/50Fuel cells

Abstract

PROBLEM TO BE SOLVED: To provide a hydrogen production apparatus capable of preventing a decrease in catalyst activity due to the stop of the apparatus and capable of stably performing good hydrogen production.
At the start of a stop operation of a hydrogen production apparatus, the temperature of a reforming reaction unit 2 is detected by a reforming temperature measuring unit 3 (step S2). In the control unit 9, the process control unit 61 compares the first to fourth reference temperatures stored in the storage unit 62 in advance with the detected temperature, and the temperature state of the apparatus at the time of stop is the first that causes water condensation. 1 state, a second state where water condensation and carbon deposition can be avoided, a third state where carbon deposition occurs, a fourth state where disproportionation reaction occurs, and a fifth state where catalytic oxidation occurs Determine whether. Then, according to the determination result, an appropriate setting is appropriately selected from the first to fifth replacement settings previously set in the control unit 9 corresponding to each of the first to fifth states, and in the apparatus according to the setting. Perform gas replacement. (Steps S3 to 11).
[Selection] Figure 5

Description

  The present invention relates to a hydrogen production apparatus that generates a hydrogen-rich gas by steam reforming a raw material containing at least carbon atoms and hydrogen atoms, and a fuel cell power generation apparatus that generates electricity and heat using the hydrogen-rich gas.

  At present, the hydrogen gas supply system is not established as a general infrastructure. For this reason, in a fuel cell power generation apparatus that is being developed and commercialized as a distributed power generation apparatus, instead of directly supplying hydrogen gas as power generation fuel to the apparatus, a hydrogen gas generation means is attached to the fuel cell, There is a configuration in which the hydrogen gas generated by the hydrogen gas generating means is supplied to the fuel cell. For example, there is a fuel cell power generation apparatus provided with a hydrogen production apparatus that generates hydrogen using raw materials supplied from existing infrastructure such as city gas and LPG.

  Many hydrogen production apparatuses produce hydrogen gas by chemically reacting raw materials such as city gas and LPG using a catalyst (specifically, steam reforming). In such a hydrogen production apparatus, when the operation and the stop of the apparatus are repeated, the possibility that the oxidation and reduction of the catalyst is repeated at a high temperature is higher than that in the case of continuous operation. There is a high possibility of decline. In particular, when the apparatus is stopped, the catalyst in the apparatus is in a high temperature state, and since the inside of the apparatus is depressurized due to the temperature drop caused by the stop, the probability that air enters the apparatus increases. When the catalyst is placed in a high-temperature oxidizing atmosphere in this way, the catalyst activity is significantly reduced due to sintering or the like.

  In order to prevent a decrease in catalytic activity caused by the shutdown of the hydrogen production apparatus, the product gas remaining inside the apparatus is replaced by using an inert gas such as nitrogen gas as a replacement gas (hereinafter referred to as in-apparatus gas replacement). Called). However, as in the case of hydrogen gas, the present situation is that the infrastructure of the inert gas is not in place, and therefore it is desired to perform the gas replacement in the apparatus without using the inert gas to prevent the catalyst activity from being lowered. As such a hydrogen production apparatus, for example, in the operation of stopping the apparatus, the supply of the raw material and water is stopped after the temperature of the catalyst is lowered, and thereby the oxidation of the catalyst is prevented even if air is mixed in the apparatus. There are some which are configured in such a manner (for example, see Patent Document 1).

Further, the temperature of the reforming reaction section is configured to be detectable, and when the apparatus is stopped, the temperature of the reforming reaction section is detected. Some are configured to prevent mixing. In such a configuration, it is possible to prevent the activity of the shift catalyst from being particularly lowered due to water vapor and oxygen by replacing the gas in the apparatus with the raw material gas (see, for example, Patent Document 2). Further, a configuration in which a mixed gas of a raw material and water vapor is circulated in the apparatus during the stop operation of the apparatus to naturally cool the catalyst, and after cooling, the gas in the apparatus is replaced with air (for example, Patent Document 3 and There are some which perform gas replacement in the apparatus with raw materials (see, for example, Patent Document 5).
JP 2000-290001 A JP 2000-95504 A JP 2002-8701 A JP 2002-93447 A JP 2002-151124 A

  By the way, the temperature state of the hydrogen production apparatus at the time of stop differs depending on the operation state of the apparatus until the stop is reached. Here, the stop time refers to the time point when the control signal for stopping operation is output from the control unit, and the period from when this signal is output until the device is completely stopped is referred to as a stop operation period.

  For example, the temperature state of the apparatus at the time of stopping differs between when the hydrogen production apparatus is stopped after being operated for a long time and when it is stopped immediately after the start of operation. Even when the apparatus is stopped immediately after the start of the operation of the hydrogen production apparatus, there are a state where the inside of the apparatus is not sufficiently heated and a state where the apparatus is heated to some extent depending on the state of the apparatus before the start of operation. . For example, when the operation of a device whose temperature has been lowered to room temperature by starting for a long time is started and the device is stopped immediately thereafter, the inside of the device is not sufficiently heated, while the operation is performed for a long time. When the apparatus held at a high temperature is temporarily stopped, and then the operation is restarted immediately and the apparatus is stopped again, the inside of the apparatus is heated to some extent and the temperature is kept high.

  As described above, the temperature state of the hydrogen production apparatus at the time of stoppage varies depending on the operation state of the apparatus until the stoppage is reached. The method does not always correspond appropriately, and if an appropriate replacement method is not performed, the catalytic activity of the reforming catalyst is reduced. For example, when the raw material and water (water vapor) are replaced with a gas having an inappropriate ratio, the catalyst is oxidized or carbon in the raw material is deposited when the temperature in the apparatus is high. Moreover, if the inside of an apparatus is low temperature, water vapor | steam will condense in an apparatus and water will produce | generate. As a result, the catalytic activity of the reforming catalyst decreases.

  The present invention solves the above-described problems, prevents a decrease in catalyst activity associated with the stoppage of the apparatus, and enables stable hydrogen production and a fuel cell including the apparatus. An object is to provide a power generator.

In order to solve the above problems, a hydrogen production apparatus according to the present invention generates a hydrogen-rich reformed gas by reacting a raw material containing an organic compound composed of at least carbon and hydrogen with steam using a catalyst. A hydrogen generation unit including a reforming reaction unit, a heating unit that heats at least the reforming reaction unit, a raw material supply unit that supplies the raw material to the hydrogen generation unit, and water that is a source of the steam A water supply unit that supplies to the hydrogen generation unit, and at least the heating unit, the raw material supply unit, and a control unit that controls the water supply unit, and heating in the heating unit is stopped at the start of the shutdown operation In the shutdown operation, a hydrogen production apparatus in which an in-apparatus gas replacement operation is performed by flowing a replacement gas for replacing the hydrogen-rich gas in the apparatus,
In the gas replacement operation in the apparatus, the raw material supplied from the raw material supply unit, the water vapor generated from the water supplied from the water supply unit, air supplied from the outside of the apparatus, and supplied from the outside of the apparatus An inert gas or a gas in which two or more of these are mixed is used as the replacement gas, and the control unit includes at least the temperature of the reforming reaction unit in the shutdown operation according to the temperature state of the apparatus. The composition of the replacement gas to be used is set in advance, and the control unit determines the temperature state of the device in the shutdown operation, and uses the replacement gas selected from the determination result and the setting. The heating unit, the raw material supply unit, and the water supply unit are controlled to perform an in-apparatus gas replacement operation.

  According to such a configuration, it is possible to perform gas replacement in the apparatus using an appropriate method according to the temperature state of the apparatus at the time of stoppage, specifically, using a replacement gas having an appropriate composition corresponding to the temperature state of the apparatus. Become. For this reason, while preventing the decrease in catalytic activity caused by carbon deposition from raw materials, water condensation from water vapor in the apparatus, high-temperature oxidation of the catalyst, etc., caused by high temperature conditions or inappropriate substitution gas composition It is possible to perform gas replacement in the apparatus quickly and efficiently using the replacement gas efficiently.

  Reforming temperature detecting means for detecting the temperature of the reforming reaction section is further provided, the control section is based on the temperature of the reforming reaction section detected by the reforming temperature detection means in the shutdown operation. You may determine the temperature state of an apparatus.

  In the control unit, the reforming reaction unit in the shutdown operation is in a state where water condensation of water vapor occurs, in a state where thermal decomposition of the raw material occurs, whether carbon monoxide and carbon dioxide. At least one reference temperature serving as a criterion for determining whether or not carbon disproportionation occurs or whether or not the catalyst is oxidized is set in advance, and when the operation is stopped, The temperature state of the apparatus may be determined by comparing the temperature of the reforming reaction section detected by the reforming temperature detecting means with the reference temperature.

  The apparatus further comprises temperature detecting means for detecting the temperature of a predetermined portion other than the reforming reaction section, and determines the temperature state of the apparatus in consideration of the temperature of the predetermined portion in the operation of stopping operation detected by the temperature detecting means. May be.

  A carbon monoxide shift section that removes carbon monoxide by a shift reaction from the hydrogen-rich gas produced in the reforming reaction section, and a post-change gas obtained from the carbon monoxide shift section is selectively oxidized and further oxidized. A carbon monoxide selective oxidation unit for removing carbon oxide, a conversion temperature detection unit for detecting the temperature of the carbon monoxide conversion unit, and a selective oxidation temperature detection unit for detecting the temperature of the carbon monoxide selective oxidation unit. The controller further includes a temperature of the carbon monoxide shifter detected by the shift temperature detector in the shutdown operation and a temperature of the carbon monoxide shifter detected by the selective oxidation temperature detector. And whether the carbon monoxide shifter and the carbon monoxide selective oxidizer in the shutdown operation are in a state where water condensation of water vapor occurs. It may determine the temperature state of the device based on the determination result of the temperature condition of the reformer.

  The control unit stores the operation state of the device before the operation stop, and in the operation stop operation, estimates the temperature state of the device in the operation stop operation from the stored operation state of the device. Also good.

  The correlation between the duration of the driving operation and the temperature state of the device is stored in the control unit in advance, and the duration of the driving operation until the start of the operation stop operation is the operation state of the device before the stop of the operation. Acquired by the control unit, and the control unit determines whether the device in the operation of stopping operation is based on the correlation stored in advance from the duration of the operation until the start of the operation of stopping operation. Whether water is condensed from water vapor, whether the raw material is thermally decomposed, whether carbon monoxide and carbon dioxide are disproportionated, or Whether or not the catalyst is oxidized may be determined.

  The controller is configured to perform the gas replacement operation in the apparatus with the replacement gas having a composition excluding the composition of only the water vapor when the temperature state of the apparatus in the shutdown operation is a state in which the water is condensed. One replacement gas setting may be stored.

  In the control unit, when the temperature state of the apparatus in the shutdown operation is a state in which condensation of the water and thermal decomposition of the raw material can be avoided, the raw material, the water vapor, the air, the inert gas, or A second replacement gas setting may be stored so that the gas replacement operation in the apparatus is performed with a mixed gas containing two or more of these.

  The controller performs the gas replacement operation in the apparatus with the replacement gas having a composition excluding the composition of only the raw material when the temperature state of the apparatus in the shutdown operation causes the thermal decomposition of the raw material. A third replacement gas setting may be stored.

  In the control unit, a fourth replacement gas setting is performed so that the gas replacement operation in the apparatus is performed with the replacement gas containing the water vapor when the temperature state of the apparatus in the shutdown operation causes the disproportionation reaction. May be stored.

  The controller is configured to perform the gas replacement operation in the apparatus with the replacement gas having a composition excluding the composition of only the air when the temperature state of the apparatus in the shutdown operation causes oxidation of the catalyst. The replacement gas setting may be stored.

  Whether the reforming reaction unit is in a state where the reforming reaction unit is in a state where water is condensed from water vapor or not is in a state where thermal decomposition of the raw material occurs. A second reference temperature that is higher than the first reference temperature, which is a determination criterion for the first, and a third reference temperature that is higher than the second reference temperature, which is a determination criterion for determining whether or not the disproportionation reaction occurs. And a fourth reference temperature higher than the third temperature, which is a criterion for determining whether or not the catalyst is oxidized, are set in advance and detected in the stop operation. If the temperature of the reforming reaction section is lower than the first reference temperature, the raw material is used as the replacement gas based on the first replacement gas setting, and the second reference temperature is higher than the first reference temperature. If below the reference temperature, based on the second replacement gas setting If the raw material is the replacement gas, and if the temperature is equal to or higher than the second reference temperature and lower than the third reference temperature, the water vapor is set as the replacement gas based on the third replacement gas setting, and the third reference temperature is set. If the temperature is higher than the temperature and lower than the fourth reference temperature, the ratio S / C of the water molecule S to the carbon atom C derived from the raw material including the raw material and the water vapor is 2 based on the fourth replacement gas setting. The above mixed gas is used as the replacement gas, and if the temperature is equal to or higher than the fourth reference temperature, the raw material and the water vapor supplied at the same supply amount as in the hydrogen generation operation based on the fifth replacement gas setting The gas replacement operation in the apparatus may be performed using the mixed gas as the replacement gas.

  Based on the correlation between the duration of the operation and the temperature of the reforming reaction unit, the control unit determines whether or not the reforming reaction unit in a shutdown operation is in a state where water is condensed from water vapor. A first reference time serving as a determination criterion, a second reference time longer than the first reference time serving as a determination criterion regarding whether or not the raw material is thermally decomposed, and the unevenness. A third reference time that is longer than the second reference time, which is a criterion for determining whether or not the oxidation reaction occurs, and the first criterion that is a criterion for determining whether or not the catalyst is oxidized. A fourth reference time longer than the reference time of 3 is set in advance, and the duration of the operation is less than the first reference time, based on the first replacement gas setting The raw material is the replacement gas, and the first reference time or more and before If the second reference time is less than the second reference time, the source gas is used as the replacement gas based on the second replacement gas setting. If the second reference time is longer than the second reference time and less than the third reference time, the third Based on the replacement gas setting, the steam is used as the replacement gas, and the raw material, the water vapor, and the water vapor are converted based on the fourth replacement gas setting if the replacement gas is equal to or longer than the third reference time and less than the fourth reference time. The replacement gas is a mixed gas in which the ratio S / C of water molecules S to carbon atoms C derived from the raw material is 2 or more, and if it is the fourth reference temperature or higher, the fifth replacement gas is set. Based on this, the in-apparatus gas replacement operation may be performed using the mixed gas of the raw material and the water vapor supplied at the same supply amount as in the hydrogen generation operation as the replacement gas.

  The control unit may control the in-device gas replacement operation in accordance with a change in the temperature state of the device accompanying the stop in the in-device gas replacement operation during the operation stop operation. For example, the control unit may determine a temperature state of the device during the operation of stopping the operation, and select an appropriate setting of the replacement gas from the determination result.

  A fuel cell power generation device according to the present invention includes a hydrogen production device having the above-described configuration, and a hydrogen rich gas generated by the hydrogen production device is supplied as a raw material and oxygen is supplied as an oxidant to oxidize the hydrogen rich gas. And a fuel cell that generates heat and electricity.

  According to such a configuration, good hydrogen production is stably performed in the hydrogen production apparatus, so that it is possible to stably supply the hydrogen-rich gas as a raw material to the fuel cell. Therefore, it is possible to realize a cogeneration apparatus that is highly reliable and excellent in economy and energy saving.

  The hydrogen production apparatus of the present invention also includes a reforming reaction section that reforms a raw material to generate a hydrogen-rich reformed gas, a reformed gas passage through which the reformed gas flows, and combustion fuel mixed with air. And heating the reforming reaction section by heating, a reformed gas flow path separated from the reformed gas flow path and a post-combustion gas flow path through which a post-combustion gas generated by the combustion flows, and an oxidizing atmosphere A reforming reaction temperature measuring instrument having a sheath tube having an oxide film formed on its surface and a heat detection element disposed in the sheath tube, and detecting the temperature of the reforming reaction section by the heat detection element; , And the sheath tube of the reforming reaction temperature measuring device is disposed in contact with the partition wall.

  A recess is formed in the partition so as to be recessed when viewed from the gas flow path side after combustion, and the sheath tube of the reforming reaction temperature measuring device is accommodated in the recess so as to contact the wall of the recess. Also good.

  According to the hydrogen production apparatus according to the present invention, it is possible to realize a hydrogen production apparatus that can prevent a decrease in catalytic activity due to the stoppage of the apparatus and can stably perform good hydrogen production. In addition, according to the fuel cell power generation apparatus according to the present invention including such a hydrogen production apparatus, it is possible to stably perform a reliable and favorable cogeneration operation.

  Embodiments of the present invention will be described below with reference to the drawings.

(Embodiment 1)
FIG. 1 is a block diagram schematically showing the configuration of the hydrogen production apparatus according to Embodiment 1 of the invention. FIG. 2 is a cross-sectional view schematically showing the configuration of the reforming reaction unit in FIG. FIG. 3 is a block diagram schematically showing the configuration of the control unit in FIG.

  As shown in FIG. 1, the hydrogen production apparatus 100 includes a hydrogen generation unit 1 including a preheating unit 8 and a reforming reaction unit 2, a raw material supply unit 6, a water supply unit 7, a combustion unit 4, and a control unit. 9 as a main component.

  The raw material supply unit 6 is connected to the preheating unit 8 of the hydrogen generation unit 1 through the raw material flow path a. The water supply unit 7 is connected to the preheating unit 8 of the hydrogen generation unit 1 through the water channel b. Further, the preheating unit 8 is connected to the reforming reaction unit 2 via the mixed raw material flow path c. In addition, here, the reforming reaction section 2 in the hydrogen generating section 1 is transferred to the preheating section 8 so that heat generated by the combustion of the combustion fuel in the combustion section 4 is transferred in the order of the reforming reaction section 2 and the preheating section 8. It is arrange | positioned rather than the upstream of the heat-transfer path | route of combustion heat. Further, a reforming temperature measuring unit 3 for measuring the temperature of the reforming reaction unit 2 is disposed at an appropriate position of the hydrogen generating unit 1. The combustion unit 4 includes a combustion fan 5 for supplying air, and a post-combustion gas flow path g for discharging a post-combustion gas generated along with combustion. The combustion unit 4 is connected to a combustion fuel flow path f that supplies part of the raw material supplied from the raw material supply unit 6 to the combustion unit 4 as combustion fuel. The control unit 9 is configured to be able to control the raw material supply unit 6, the water supply unit 7, the combustion unit 4, and the combustion fan 5, and to transmit temperature information detected by the reforming temperature measurement unit 3. It is configured. The controller 9 controls each operation of starting, operating, and stopping the hydrogen production apparatus.

  As shown in FIG. 2, the reforming reaction unit 2 includes a cylindrical main body 30. In addition, although illustration is abbreviate | omitted here, since the reforming reaction part 2 becomes high temperature, in order to prevent the thermal radiation to the exterior, the outer wall of the main body 30 is covered with the heat insulating material. A plurality of cylindrical bodies having different diameters are concentrically disposed inside the main body 30, whereby the internal space of the main body 30 is radially divided by each cylindrical body and is extended in the axial direction. An annular gap 31 is formed. Here, a cylindrical peripheral wall that divides the inside of the main body 30 in the radial direction is referred to as a vertical wall 32. A disc-like or hollow disc-like lateral wall 33 arranged concentrically with the vertical wall 32 is arranged at a predetermined end in the axial direction of the vertical wall 32.

  Due to the gap 31 formed by the vertical wall 32 and the horizontal wall 33, the downstream passage g1 of the double-combusted gas passage g is formed inside the main body 30 from the radially outer peripheral side toward the center. A reformed gas channel d, a reforming catalyst housing portion e, and an upstream channel g2 of the post-combustion gas channel g are formed.

  The downstream flow path g1 and the upstream flow path g2 of the post-combustion gas flow path g formed in the main body axial direction communicate with each other at the bottom of the main body 30. Further, the upstream flow path g2 of the post-combustion gas flow path g is formed along the upper surface and the side surface of the radiant cylinder 40 of the combustion section 4 described later, and communicates with the inside of the cylinder through the ejection hole of the radiant cylinder 40. Further, the end of the downstream flow path g1 is formed so that the combustion gas can be taken out of the reforming reaction section 2.

  A reforming catalyst layer 20 is formed by filling the reforming catalyst housing portion e with the reforming catalyst. Here, a catalyst prepared by supporting a ruthenium catalyst on an alumina carrier is used as a reforming catalyst. The reforming catalyst layer 20 is disposed along the upper surface and the side surface of the radiant cylinder 40 of the combustion section 4 via the upstream flow path g2 of the post-combustion gas flow path g. The central part of the upper end of the reforming catalyst layer 20 faces the mixed raw material flow path c communicating with the preheating part 8 (see FIG. 1), and the lower end faces the reformed gas flow path d. A reforming temperature measuring unit 3 is disposed at the upstream end of the reformed gas channel d serving as a reformed gas inlet. Here, the reforming temperature measuring unit 3 includes a thermocouple as a temperature detecting means, and this thermocouple is arranged in a gas collecting portion that has flowed through the reforming catalyst layer 20. The reforming temperature measurement unit 3 is not limited to the arrangement position as long as the temperature change of the reforming catalyst layer 20 can be measured relatively quickly and in the atmosphere. Here, the temperature of the gas after flowing through the reforming catalyst layer 20 is set as the temperature of the reforming reaction unit 2, and the temperature state of the reforming reaction unit 2 is grasped by the temperature detected by the reforming temperature measuring unit 3. The Here, in the present invention (in the claims and the specification), “detecting the temperature” includes both the case of detecting the temperature directly and the case of detecting the temperature indirectly. Detecting the temperature directly means detecting a physical quantity called temperature, for example, when detecting the temperature of a certain detection target with a thermocouple or thermistor. On the other hand, indirectly detecting the temperature means detecting a physical quantity or time other than the temperature related to the temperature to be detected, for example, the pressure inside the reforming reaction unit or the operation time of the reforming reaction unit. This is the case when detecting.

  A radiation tube 40 is inserted concentrically with the vertical wall 32 at the center of the main body 30 of the reforming reaction unit 2. The upper end of the radiant cylinder 40 communicates with the upstream flow path g2 of the post-combustion gas flow path g, and a burner 41 having a fuel outlet 41a is disposed at the lower end of the radiant cylinder 40. The internal space of the radiation tube 40 constitutes a combustion space 44 where a flame 42 is formed. Further, a flow path 43 of air sent from the combustion fan 5 (see FIG. 1) is formed so as to surround the burner 41, and this air flow path 43 communicates with the combustion space 44 through the air jet 43a. . The burner 41 is connected to the raw material supply unit 6 (see FIG. 1) via a combustion fuel flow path f. Thus, here, the combustion section 4 is configured by the radiation tube 40, the burner 41, and the air flow path 43, and air is supplied to the air flow path 43 by the sirocco fan as the combustion fan 5. The rotation speed of the sirocco fan is controlled by the control unit 9, and thereby the amount of air supplied to the combustion unit 4 is adjusted. The reforming reaction unit 2 is heated by the combustion of the combustion fuel in the combustion unit 4, and here, the temperature of the reforming reaction unit 2 is carbonized such as methane, ethane, propane or the like supplied to the reforming reaction unit 2 as a raw material. The heating amount is controlled by the control unit 9 so that about 85 to 95% of the hydrogen-based raw material becomes a temperature at which steam reforming is possible, for example, about 650 to 700 ° C.

  The raw material supply unit 6 (see FIG. 1) supplies hydrocarbon raw materials such as natural gas and LPG, naphtha raw materials, alcohol raw materials such as methanol, etc. to the hydrogen generation unit 1 through the raw material flow path a. It is configured. Here, the raw material supply unit 6 is configured so that natural gas containing a hydrocarbon-based organic compound (specifically, mainly methane) and supplied from existing infrastructure is used as a raw material. Although not shown, the raw material supply unit 6 includes a booster that increases the supply pressure of the raw material, and includes a desulfurization unit that reduces the sulfur component in the raw material. It has a zeolite adsorbent that removes odor components.

  Although not shown here, the water supply unit 7 (see FIG. 1) includes an ion exchanger and a plunger pump. For example, after the supplied tap water is processed by the ion exchanger, the plan The jar pump is pressurized and supplied to the hydrogen generator 1.

  As shown in FIG. 3, the control unit 9 is configured by a computer such as a microcomputer, and includes a processing control unit (CPU) 61, a storage unit (internal memory) 62 configured by a semiconductor memory, and an operation input unit 63. And a display unit 64 and a clock unit 65. In the control unit 9, the processing units 61 to 65 control the supply amount of raw materials and water, the combustion amount in the combustion unit 4, the output of the combustion fan 5, and the like. In particular, when the apparatus is stopped, the temperature state of the apparatus is grasped based on the temperature of the reforming reaction section 2 detected by the reforming temperature measuring section 3 when the apparatus is stopped, and the temperature state of the apparatus is supported. The composition of the replacement gas is adjusted by controlling the raw material supply unit 6 and the water supply unit 7 so as to perform the in-apparatus gas replacement operation. Details of the gas replacement operation in the apparatus will be described later.

  Next, the operation of the hydrogen production apparatus will be described. The operation of the hydrogen production apparatus is actually performed after the operation start control signal is output and the operation stop control signal is output, and after the operation stop control signal is output. It is divided into a stop operation (operation stop operation) that is carried out until the motor stops. In the operation operation, the start-up operation and the hydrogen generation operation of the device are performed, and in the stop operation, the gas replacement operation in the device is performed.

  First, in the operation of the hydrogen production apparatus, a control signal for starting operation is output from the process control unit 61 of the control unit 9 to start the apparatus. Specifically, the combustion fuel is supplied to the burner 41 of the combustion unit 4 at a predetermined supply amount via the combustion fuel flow path f, and the combustion fan 5 is supplied to the combustion space 44 of the combustion unit 4 at a predetermined supply amount. Air is supplied. Here, the air supply amount is 1.5 times the theoretical air amount necessary for complete combustion of methane. The combustion fuel and air are reacted to form a flame 42 in the combustion space 44, and the reforming reaction section 2 and the preheating section 8 are heated by the combustion heat and the heat of the gas after combustion. At the time of heating, the temperature of the reforming reaction unit 2 is always detected by the reforming temperature measuring unit 3, and information on the detected temperature is transmitted to the process control unit 61 of the control unit 9. Here, the operation in which the combustion in the combustion unit 4 is started and the reforming reaction unit 2 and the preheating unit 8 are preheated is referred to as a start-up operation.

  After heating the reforming reaction unit 2 and the preheating unit 8 as described above to increase the temperature of the reforming reaction unit 2 (more specifically, the reforming catalyst layer 20) and the preheating unit 8, the preheating unit 8 The raw material is supplied from the raw material supply unit 6 and the water is supplied from the water supply unit 7. The supplied water evaporates in the preheating unit 8 to become steam, and the steam and the raw material are mixed and supplied to the reforming reaction unit 2 through the mixed raw material flow path c. In the reforming reaction section 2, the raw material is steam reformed by the reforming reaction to generate a reformed gas, that is, a hydrogen rich gas (hereinafter simply referred to as hydrogen gas). The produced hydrogen gas is taken out of the hydrogen production apparatus through the reformed gas flow path d. Here, the operation in which the raw material and water vapor are supplied to the reforming reaction unit 2 and hydrogen gas is generated by the reforming reaction is referred to as a hydrogen generating operation.

  During the hydrogen generation operation, the temperature detected by the reforming temperature measuring unit 3 is about 650 ° C. so that about 85 to 95% of the raw material (specifically methane) supplied to the reforming reaction unit 2 is reformed. The heating amount of the combustion unit 4 is controlled by the control unit 9 so as to be held. Further, the ratio of water molecules to carbon atoms in the mixed gas of the raw material and steam supplied to the reforming reaction section 2 (this is referred to as the steam / carbon ratio and expressed as S / C) is 3, that is, In the mixed gas supplied to the mass reaction unit 2, S / C is set so that the number of water molecules is 3 mol per mol of carbon atoms. Accordingly, the theoretical amount of water for 1 mol of methane is 2 mol, whereas 3 mol of water is supplied here. Such S / C is input by a user while confirming a desired value (here, 3) on the operation input unit 63 of the control unit 9 on the display unit 64, and the input value is stored by the processing control unit 61. The settings are stored in the unit 62. Further, in such an operation of the hydrogen production apparatus, the process control unit 61 of the control unit 9 acquires the temperature of the reforming reaction unit 2 by the reforming temperature measuring unit 3 and grasps the temperature state of the reforming reaction unit 2. Then, according to the temperature state, the supply amount of the raw material, water and air, the combustion amount of the combustion fuel in the combustion section 4 and the like are controlled.

  Next, the stop operation of the hydrogen production apparatus will be described. Here, the time when the operation stop control signal is output is referred to as the start of the stop operation, and the period from the start of the stop operation to the actual stop of the device is referred to as the stop operation period.

  As described above in the conventional problem, the catalytic activity of the reforming catalyst constituting the reforming catalyst layer 20 decreases when sintering, oxidation, or the like occurs under the influence of temperature. In particular, during the stop operation period of the apparatus, the reforming catalyst is easily oxidized at a high temperature, so that the catalytic activity is likely to decrease. For example, in the hydrogen production apparatus during the stop operation period, the reforming catalyst is easily oxidized at a high temperature because the probability that air is mixed into the apparatus from the outside due to the volume shrinkage of the internal gas accompanying the temperature decrease of the apparatus is increased. The tendency for the catalytic activity to decrease increases.

  FIG. 4 is a diagram showing the relationship between the oxidation temperature of the reforming catalyst and the specific surface area of the reforming catalyst. Here, the catalyst specific surface area is a relative ratio of the surface area after oxidation to the surface area before oxidation of the Ru metal constituting the reforming catalyst, and specifically, the carbon monoxide adsorption amount of the Ru metal before and after oxidation. Is the ratio. When the Ru metal is oxidized, it has a smaller surface area than before oxidation due to sintering. Here, there is a correlation between the catalyst activity and the catalyst surface area. Since the catalyst activity decreases as the surface area decreases, the decrease in the catalyst specific surface area indicates a decrease in the catalyst activity.

  As shown in FIG. 4, in the reforming catalyst, it is clear that the catalyst specific surface area decreases as the oxidation temperature increases, and thus the catalyst activity decreases as the oxidation temperature increases. This is because sintering is more likely to occur at higher temperature oxidation. For example, in the hydrogen generation operation, the reforming catalyst is maintained at about 650 ° C. as described above, but if the reforming catalyst is placed in an oxidizing atmosphere at this high temperature as the apparatus is stopped, the reforming catalyst is modified by sintering. The activity of the catalyst is significantly reduced.

  In order to suppress such a decrease in the catalyst activity, it is necessary to avoid the inside of the apparatus from becoming an oxidizing atmosphere during the stop operation period in which the reforming catalyst is at a high temperature, and to quickly lower the temperature of the reforming catalyst. is there. Therefore, in the stop operation of the apparatus, it is necessary to avoid as much as possible the gas replacement operation in the apparatus under the condition that an oxidizing atmosphere is generated when the reforming catalyst is at a high temperature. In addition, if the reforming catalyst is at a high temperature, there is a high possibility that carbon deposition will occur due to thermal decomposition of the raw material or disproportionation reaction of carbon monoxide and carbon dioxide. It is desirable to avoid as much as possible.

  On the other hand, when the temperature of the reforming catalyst is low, for example, when the apparatus is stopped immediately after the start-up operation of the apparatus is started, the above-described reduction in catalytic activity or carbon deposition due to oxidation is unlikely to occur. Therefore, it is possible to perform the gas replacement operation in the apparatus under conditions rich in raw materials. However, in this case, since the reforming catalyst is at a low temperature, if the water vapor content in the replacement gas used for the gas replacement operation in the apparatus is large, the water vapor condenses on the reforming catalyst to produce water (hereinafter referred to as this). Is called water condensation), which can reduce the catalytic activity. Therefore, in this case, it is desired that the water vapor content in the replacement gas is small.

  As described above, in order to prevent the catalytic activity of the reforming catalyst from being lowered, it is necessary to perform gas replacement in the apparatus by an appropriate method in accordance with the temperature state of the apparatus in the stop operation. Therefore, in the present embodiment, the following method is used to select and implement an appropriate in-device gas replacement method corresponding to the temperature state of the device as appropriate, and to stop the device without reducing the catalytic activity of the reforming catalyst. .

  The details of the gas replacement operation in the apparatus will be described below with reference to FIG.

  FIG. 5 is a flowchart schematically showing the contents of the stop operation program stored in the control unit 9. The outline of the gas replacement operation in the apparatus will be described. First, a control signal for stopping operation is output from the processing control unit 61 of the control unit 9 to shift from the operation operation to the stop operation. The supply of fuel and air is stopped (step S1). At the time of this transition, that is, at the start of the shutdown operation, the temperature of the reforming reaction unit 2 is detected by the reforming temperature measuring unit 3, and the temperature information is acquired by the processing control unit 61 of the control unit 9 (step S2). . And the process control part 61 compares the 1st-4th reference temperature used as the criteria set beforehand by the memory | storage part 62, and the acquired temperature of the reforming reaction part 2, and based on the comparison result Then, it is determined whether the temperature state of the reforming reaction unit 2 at the start of the stop operation is one of first to fifth states described later. Then, according to the determination result, an appropriate setting is selected from first to fifth replacement settings, which will be described later, stored in advance in the storage unit 62, and a replacement gas having a composition according to the setting is stored in the apparatus. The raw material supply from the raw material supply unit 6 and the water supply from the water supply unit 7 are controlled so as to be supplied, and the gas replacement operation in the apparatus is performed (steps S3 to S11).

  Specifically, in the above determination in the processing control unit 61, the temperature state of the reforming reaction unit 2 is the first state where water condensation occurs, water condensation and carbon derived from the raw material (here, the raw material is assumed to be methane alone). In the second state in which precipitation due to thermal decomposition can be avoided, in the third state in which the thermal decomposition proceeds and carbon deposition occurs, and the disproportionation reaction of carbon monoxide and carbon dioxide proceeds. The determination is made in five parts: a fourth state in which precipitation occurs and a fifth state in which the reforming catalyst is oxidized. Here, the reference temperature for determining whether or not the reforming reaction unit 2 is in the first state is the first reference temperature, and the reference temperature for determining whether or not the reforming reaction unit 2 is in the second state is The second reference temperature is used, the reference temperature for determining whether the state is the third state is the third reference temperature, and the reference temperature for determining whether the state is the fourth state is the first reference temperature. The reference temperature is 4. In this case, the first reference temperature is 100 ° C., the second reference temperature is 300 ° C., the third reference temperature is 400 ° C., and the fourth reference temperature is 500 ° C. Such first to fourth reference temperatures are stored and set in the storage unit 62 by inputting each numerical value to the operation input unit 63 while confirming with the display unit 64 in the control unit 9.

  Further, the storage unit 62 of the control unit 9 does not cause water condensation in the reforming reaction unit 2, does not precipitate carbon derived from the raw material or disproportionation reaction, and contains the reforming catalyst. The composition of the replacement gas used for the gas replacement operation in the apparatus is set in advance according to the temperature state of the reforming reaction unit 2 so as not to oxidize. Here, if the reforming reaction unit 2 is in the first state in which water condensation occurs, it is set to perform gas replacement in the apparatus using the raw material as a replacement gas (hereinafter referred to as the first replacement setting), In the second state in which water condensation and deposition of carbon derived from the raw material can be avoided, gas replacement in the apparatus is performed using the raw material as a replacement gas (hereinafter referred to as a second replacement setting). In addition, in the third state in which the carbon deposition occurs, it is set to perform gas replacement in the apparatus using water vapor as a replacement gas (hereinafter referred to as the third replacement setting). In the fourth state in which carbon precipitation occurs due to the leveling reaction, gas replacement in the apparatus is performed using a mixed gas of a raw material having a high water vapor content and water vapor as a replacement gas (hereinafter referred to as the fourth replacement). Called the setting), and the reforming catalyst is oxidized In the fifth state, the raw material and water vapor are supplied at the same supply amount as in the hydrogen generation operation, and the gas in the apparatus is replaced by using the mixed gas as a replacement gas (hereinafter referred to as the first state). 5 is called the replacement setting).

  As shown in FIG. 5, the control unit 9 first compares the temperature of the reforming reaction unit 2 at the start of the operation stop operation acquired in step S <b> 2 with the fourth reference temperature (500 ° C.). Thus, the reforming reaction unit 2 determines whether or not catalytic oxidation occurs (fifth state) (step S3). If the detected temperature is equal to or higher than the fourth reference temperature, it is determined that catalytic oxidation occurs in the reforming reaction unit 2 (that is, the fifth state), and therefore the fifth replacement setting is selected. Thereby, the raw material supply unit 6 and the water supply unit 7 are controlled so that the raw material and water are supplied to the hydrogen generation unit 1 with the same supply amount as in the hydrogen generation operation, and a mixed gas of the raw material and water vapor is supplied. The When this mixed gas is supplied to the reforming reaction section 2, the reforming reaction, which is an endothermic reaction, proceeds in the high temperature reforming reaction section 2 in the same way as during the hydrogen generation operation, thereby quickly lowering the catalyst temperature. (Step S4).

  On the other hand, when the detected temperature is lower than the fourth reference temperature (500 ° C.), a comparison with the third reference temperature (400 ° C.) is further performed, and the reforming reaction unit 2 causes a disproportionation reaction. It is determined whether or not it is in a state (ie, a fourth state) (step S5). If the detected temperature of the reforming reaction unit 2 is equal to or higher than the third reference temperature (that is, 400 ° C. or higher and lower than 500 ° C.), the catalyst is hardly oxidized but the carbon is precipitated by the disproportionation reaction (fourth state). ) And the fourth replacement setting is selected according to the determination result. When the reforming reaction section 2 is in the fourth state, carbon replacement may occur due to disproportionation reaction if gas replacement in the apparatus is performed with only the raw material or a mixed gas having a low water vapor content. According to the replacement setting of 4, the control unit 9 controls the water supply amount from the water supply unit 7 and the raw material supply amount from the raw material supply unit 6 so that the S / C of the replacement gas becomes 2 or more (that is, the water vapor content becomes high). Since it is adjusted, it becomes possible to prevent carbon deposition due to the disproportionation reaction (step S6).

  In addition, when the detected temperature is lower than the third reference temperature (400 ° C.), the comparison is made with the second reference temperature (300 ° C.), and the reforming reaction unit 2 thermally decomposes the carbon derived from the raw material. It is determined whether or not it is in a state of being deposited (ie, a third state) (step S7). If the detected temperature of the reforming reaction section 2 is not less than the third reference temperature (ie, not less than 300 ° C. and less than 400 ° C.), the disproportionation reaction is unlikely to occur but the carbon derived from the raw material is precipitated (third state). And the third replacement setting is selected according to the determination result. Thereby, water is supplied from the water supply part 7 and the inside of the apparatus is replaced with water vapor (step S8).

  In addition, when the detected temperature is lower than the second reference temperature (300 ° C.), the comparison is made with the first reference temperature (100 ° C.), and the reforming reaction unit 2 performs water condensation and carbon derived from the raw material. It is determined whether or not it is in a state in which precipitation of (a second state) can be avoided (step S9). If the detected temperature of the reforming reaction unit 2 is equal to or higher than the first reference temperature (ie, 100 ° C. or higher and lower than 300 ° C.), the apparatus can avoid water condensation and raw material-derived carbon deposition (second state). And the second replacement setting is selected according to the determination result. Thereby, a raw material is supplied from the raw material supply part 6, and the inside of an apparatus is substituted with a raw material (step S10). On the other hand, when the detected temperature is lower than the first reference temperature (100 ° C.), it is determined that the apparatus is in a state that causes water condensation (that is, the first state), and the first replacement is performed according to the determination result. A setting is selected. Then, the raw material is supplied from the raw material supply unit 6, and the inside of the apparatus is replaced with the raw material (step S11).

  By the way, when the gas replacement operation in the apparatus is performed according to the temperature of the reforming reaction unit 2 at the start of the stop operation as described above, the temperature of the apparatus decreases with the passage of time from the start of the stop operation. . For this reason, according to the temperature fall of an apparatus, it is necessary to change the gas seed | species (specifically gas composition) used by substitution operation in an apparatus at any time. Therefore, here, also in the stop operation after the start of the stop operation, the control unit 9 determines the temperature state of the apparatus based on the first to fourth reference temperatures from the detected temperature of the reforming reaction unit 2. According to the determination, the setting of the replacement gas is appropriately selected and the setting is switched to appropriately change the type of the replacement gas.

  For example, when the detected temperature of the reforming reaction unit 2 at the start of the stop operation is lower than the first reference temperature (100 ° C.), the inside of the apparatus is replaced with the raw material as described above (step S9, 11) Water condensation does not occur even if the temperature of the apparatus decreases. Therefore, in this case, after supplying the raw material for a predetermined time and ventilating an amount of the raw material that can sufficiently replace the inside of the apparatus, the raw material supply unit 6 is controlled to stop the aeration of the raw material and the stop operation is finished ( Steps S12 and 13). Even when the detected temperature at the start of the stop operation is equal to or higher than the first reference temperature and lower than the second reference temperature (100 ° C. or higher and lower than 300 ° C.), the inside of the apparatus is replaced with the raw material as described above. (Steps S9 and S10) Water condensation does not occur even when the temperature of the apparatus is lowered. Therefore, after supplying the raw material for a predetermined time and ventilating an amount of raw material that can sufficiently replace the inside of the apparatus, the raw material supply unit 6 Is controlled to stop the aeration of the raw material and the stopping operation is terminated (steps S12 and S13).

  On the other hand, when the detected temperature of the reforming reaction unit 2 at the start of the stop operation is equal to or higher than the second reference temperature and lower than the third reference temperature (300 ° C. or higher and lower than 400 ° C.), the steam is used as described above. The replacement is performed by aeration. However, in such a replacement using water vapor, if the temperature of the apparatus decreases and becomes lower than the first reference temperature (100 ° C.), water condensation may occur in the apparatus. Therefore, here, when the temperature of the reforming reaction unit 2 in the gas replacement operation in the apparatus is detected by the reforming temperature measuring unit 3 and the detected temperature becomes lower than the second reference temperature (300 ° C.) (step S15), The supply of water from the water supply unit 7 to the hydrogen generation unit 1 is stopped to stop the flow of water vapor, and the raw material supply unit 6 is controlled to allow a sufficient amount of raw material to be substituted in the apparatus to be aerated for a predetermined time. Thereafter, the raw material supply unit 6 is controlled to stop the aeration of the raw material, and the stop operation is finished (steps S14, 12, 13).

  Further, when the detected temperature of the reforming reaction unit 2 at the start of the stop operation is equal to or higher than the third reference temperature and lower than the fourth reference temperature (400 ° C. or higher and lower than 500 ° C.), as described above, Since the replacement is performed by the mixed gas with the raw material, the temperature of the reforming reaction section 2 is lower than the second reference temperature (300 ° C.) in order to prevent the occurrence of water condensation due to the temperature drop, as in the above case. If it becomes (step S16), the water supply from the water supply part 7 to the hydrogen production | generation part 1 will be stopped, the ventilation | gas_flowing of water vapor | steam will be stopped, and the raw material of the quantity which can fully replace the inside of an apparatus will be aerated for a predetermined time. Thereafter, the raw material supply unit 6 is controlled to stop the aeration of the raw material, and the stop operation is finished (steps S14, 12, 13).

  Further, when the detected temperature at the start of the stop operation is higher than the fourth reference temperature (500 ° C.), as described above, the temperature of the apparatus decreases and becomes lower than the fourth reference temperature (500 ° C.). Water and raw material are supplied to perform replacement with a mixed gas (step S4). When the temperature becomes lower than the fourth reference temperature, the raw material supply unit 6 is controlled to stop the supply of the raw material and allow only water vapor to flow (step S4). S17, 18). Further, when the temperature of the reforming reaction unit 2 becomes lower than the second reference temperature (300 ° C.), the water supply unit 7 is controlled to stop the water supply and the raw material supply unit 6 is controlled to recycle the raw material. An amount of raw material that can be supplied and sufficiently replaced in the apparatus is aerated for a predetermined time. Thereafter, the raw material supply unit 6 is controlled to stop the aeration of the raw material, and the stopping operation is finished (steps S19, 14, 12, 13).

  In this way, by appropriately changing the replacement gas used for the replacement operation in the apparatus according to the temperature decrease of the apparatus with the passage of time, it is possible to prevent the occurrence of water condensation and carbon deposition of the raw material regardless of the temperature decrease. It is possible to perform a stop operation promptly.

  As described above, according to the hydrogen production apparatus of the present embodiment, the temperature of the reforming reaction unit 2 at the start of the apparatus stop operation and the temperature change of the reforming reaction unit 2 during the stop operation are appropriate. It is possible to replace the gas in the equipment using a new replacement gas, so that the replacement gas is efficiently and effectively used, and the flow of the reforming catalyst due to temperature, the oxidation, etc. Problems such as road blockages can be reliably avoided. Accordingly, it is possible to prevent the catalytic activity of the reforming catalyst from being lowered, and as a result, it is possible to stably perform good hydrogen generation.

  As an example, when a series of operations of operation and stop of the hydrogen production apparatus was repeated by the above method, even after the operation was repeated about 200 times, the reforming catalyst did not show a large decrease in catalytic activity. It was.

  The setting of the replacement gas composition and the setting of the reference temperature are not limited to the above as long as they are appropriately set in consideration of the temperature state of the apparatus in the stop operation.

  For example, when the temperature state of the apparatus at the start of the shutdown operation is the second state, only water vapor may be used as the replacement gas, or a mixed gas of the raw material and water vapor may be used as the replacement gas. . When using a replacement gas containing water vapor in this way, the supply of water vapor is stopped and the replacement gas is changed to a raw material when the temperature of the apparatus drops below 100 ° C. during the stop operation period. Further, when the temperature state of the apparatus at the start of the stop operation is the third state, a mixed gas of the raw material and water vapor may be used as the replacement gas. Further, when the temperature state of the apparatus at the start of the stop operation is the fourth state and the fifth state, only water vapor may be used as the replacement gas. When the temperature state of the apparatus at the start of the stop operation is the fifth state, the catalyst temperature can be quickly lowered by the endothermic reaction as described above by supplying the raw material together with the water vapor. Therefore, it is desirable to supply a mixed gas of water vapor and raw material as a replacement gas as described above. Thereby, sintering due to catalytic oxidation can be reliably prevented.

  Further, in addition to water vapor and raw materials, an inert gas such as nitrogen gas or air may be supplied from the outside of the apparatus and used as a replacement gas. Specifically, a configuration in which a nitrogen cylinder and an air supply pump are provided May be included in the hydrogen production apparatus. By using the inert gas in combination with the raw material and water vapor to replace the gas in the apparatus, the amount of the inert gas used can be greatly reduced compared to the case of replacing with the inert gas alone as in the prior art. . Further, by using air alone or in combination with the raw material or water vapor as a replacement gas, it is possible to reduce the supply amount of the raw material and water in the stop operation of the apparatus. For example, when the temperature state of the apparatus at the start of the stop operation is the first state, a mixed gas of raw material and an inert gas or air may be used as a replacement gas. In addition, when the temperature state of the apparatus at the start of the stop operation is the second to fifth states, the apparatus is a mixed gas containing two or more of raw materials, water vapor, inert gas, and air at an appropriate ratio. An inner replacement operation may be performed.

  As a modification of the present embodiment, for example, a flow path closing valve is provided in the vicinity of the outlet (extraction port) of the reformed gas flow path d of the hydrogen production apparatus, and the supply of the raw material is stopped when the stop operation is terminated. In addition, the flow path closing valve may be closed and the replacement gas may be sealed in the stopped apparatus.

(Embodiment 2)
The hydrogen production apparatus according to Embodiment 2 of the present invention has the same apparatus configuration as that of Embodiment 1. In such a hydrogen production apparatus of the present embodiment, the gas replacement method in the apparatus is appropriately selected according to the temperature state of the apparatus at the start of the stop operation as in the first embodiment. Whereas the temperature state of the apparatus is determined by detecting the temperature of the reforming reaction unit 2 at the start of the stop operation, in the present embodiment, the apparatus is operated based on the operation operation time before the start of the stop operation. The temperature state is determined.

  The temperature in the apparatus of the hydrogen production apparatus often depends on the operation operation time. For example, when operating under a certain condition, the temperature in the apparatus increases as the operation time increases.

  FIG. 6 is a diagram illustrating the relationship between the operation operation time and the temperature of the reforming reaction unit 2. As shown in FIG. 6, the temperature of the reforming reaction unit 2 increases as the operation operation time increases, and the temperature of the reforming reaction unit 2 is 100 from the start of operation (at the start-up) to 8 minutes later (period A). 8 to 15 minutes (Period B) is 100 ° C. or more and less than 300 ° C., and 15 to 18 minutes later (Period C) is 300 ° C. or more and less than 400 ° C., 18 From minute to 22 minutes (period D) is 400 ° C. or higher and lower than 500 ° C., and after 22 minutes (period E) is 500 ° C. or higher.

  Thus, since there is a correlation between the temperature of the reforming reaction unit 2 and the operation operation time of the apparatus, here, based on the operation operation time until the start of the stop operation of the apparatus is reached. The temperature state of the apparatus at the start of the stop operation is determined, an appropriate replacement setting is selected according to the determination result, and the apparatus gas replacement operation is performed. Hereinafter, the stop operation in the present embodiment will be described in accordance with a stop operation program stored in the control unit 9.

  FIG. 7 is a flowchart schematically showing the contents of the stop operation program stored in the control unit 9. As shown in FIG. 7, the clock unit 65 of the control unit 9 starts from the time when the device starts (that is, when the start control signal is output) until the time when the device stops (that is, when the stop control signal is output). Is measured as the driving operation time, and the measurement result is transmitted to the control unit 9 at the start of the stop operation of the apparatus, and the processing control unit 61 acquires it (steps S21 and S22). On the other hand, the storage unit 62 of the control unit 9 stores correlation data between the operation time shown in FIG. 6 and the temperature of the reforming reaction unit 2 in advance. At the start of the stop operation, the process control unit 61 compares the acquired driving operation time with the correlation data, and determines whether the device is in the first to fifth states. Based on the determination result, an appropriate setting is selected from the first to fifth replacement settings, and the in-device gas replacement operation is performed (steps S23 to S31).

  Specifically, first, it is determined whether or not the driving operation time is less than 22 minutes (step S23), and when the driving operation time is 22 minutes or more, based on the data stored in the storage unit 62. Therefore, the process control unit 61 estimates that the temperature of the reforming reaction unit 2 is 500 ° C. or higher, and thus determines that the reforming reaction unit 2 is in a state where the reforming catalyst is oxidized (fifth state). . Therefore, in this case, the fifth replacement setting is selected, and the raw material and water are supplied to the hydrogen generator 1 at the same supply amount as in the hydrogen generation operation, and the replacement operation is performed by the mixed gas of the raw material and water vapor. Implemented (step S24).

  If the driving operation time is less than 22 minutes, it is further determined whether or not it is less than 18 minutes (step S25). When the operation time is 18 minutes or more and less than 22 minutes, the process control unit 61 estimates that the temperature of the reforming reaction unit 2 is 400 ° C. or more and less than 500 ° C. Therefore, the reforming reaction unit 2 is revised. It is determined that the catalyst is not oxidized but the disproportionation reaction occurs (that is, the fourth state). Therefore, in this case, the fourth replacement setting is selected, and the replacement operation is performed using the mixed gas of the raw material having S / C of 2 or more and water vapor as the replacement gas (step S26).

  If the driving operation time is less than 18 minutes, it is further determined whether or not it is less than 15 minutes (step S27). When the operation time is 15 minutes or more and less than 18 minutes, the process control unit 61 estimates that the temperature of the reforming reaction unit 2 is 300 ° C. or more and less than 400 ° C. Although the homogenization reaction does not occur, it is determined that the carbon derived from the raw material is deposited by thermal decomposition (that is, the third state). Accordingly, in this case, the third replacement setting is selected, and a replacement operation is performed using water vapor as a replacement gas (step S28).

  If the driving operation time is less than 15 minutes, it is further determined whether or not it is less than 8 minutes (step S29). If the operation time is 8 minutes or more and less than 15 minutes, the process control unit 61 estimates that the temperature of the reforming reaction unit 2 is 100 ° C. or more and less than 300 ° C. It is determined that this is a state in which condensation and precipitation of raw material-derived carbon can be avoided (that is, the second state). Therefore, in this case, the second replacement setting is selected, and the replacement operation is performed using the raw material as the replacement gas (step S30).

  When the operation time is less than 8 minutes, the process control unit 61 estimates that the temperature of the reforming reaction unit 2 is less than 100 ° C., and thus the reforming reaction unit 2 is in a state where water is condensed ( That is, it is determined that the first state). Therefore, in this case, the first replacement setting is selected, and the replacement operation is performed using the raw material as the replacement gas (step S31).

  Here, also in the present embodiment, as in the case of the first embodiment, the replacement gas type is changed in accordance with the temperature drop of the reforming reaction unit 2 during the in-device replacement operation.

  Specifically, when it is determined that the reforming reaction unit 2 at the start of the stop operation is in the first state, the inside of the apparatus is replaced with the raw material as described above (steps S29 and 31). Even if the temperature of the apparatus decreases, water condensation does not occur. Therefore, in this case, after supplying the raw material for a predetermined time and ventilating an amount of the raw material that can sufficiently replace the inside of the apparatus, the raw material supply unit 6 is controlled to stop the aeration of the raw material and the stop operation is finished ( Steps S32 and 33). Even when it is determined that the reforming reaction unit 2 at the start of the stop operation is in the second state, the inside of the apparatus is replaced with the raw material (steps S29 and S30), so even if the temperature of the apparatus decreases. Water condensation does not occur. Therefore, as in the case described above, after a sufficient amount of source gas has been ventilated for a predetermined time, the source gas supply unit 6 is controlled to stop aeration of the source gas. The operation is finished (steps S32 and S33).

  In addition, when it is determined that the reforming reaction unit 2 at the start of the stop operation is in the third state, the interior of the apparatus is replaced with water vapor as described above (steps S27 and S28). If the temperature is lowered to below 100 ° C., water condensation may occur. Therefore, here, when the temperature of the reforming reaction unit 2 detected by the reforming temperature measuring unit 3 becomes less than 300 ° C. (step S34), the water supply unit 7 is controlled to stop the flow of water vapor and the inside of the apparatus. An amount of the raw material that can sufficiently replace is aerated for a predetermined time. Thereafter, the raw material supply unit 6 is controlled to stop the aeration of the raw material, and the stop operation is finished (steps S35, 32, 33).

  Further, when it is determined that the reforming reaction unit 2 at the start of the stop operation is in the fourth state, the inside of the apparatus is replaced with the mixed gas of water vapor and the raw material as described above (step S25). , 26) As in the above case, in order to prevent the occurrence of water condensation, when the temperature of the apparatus drops below 300 ° C. (step S36), the water supply unit 7 is controlled to supply water. Stop the flow of water vapor and stop a sufficient amount of raw material to replace the inside of the apparatus for a predetermined time. Thereafter, the raw material supply unit 6 is controlled to stop the aeration of the raw material, and the stop operation is finished (steps S35, 32, 33).

  Further, when it is determined that the reforming reaction unit 2 at the start of the stop operation is in the fifth state, the temperature of the reforming reaction unit 2 detected by the reforming temperature measuring unit 3 is less than 500 ° C. If it becomes (step S37), the raw material supply part 6 is controlled, supply of a raw material is stopped, and only water vapor | steam is ventilated as substitution gas (step S38). When the temperature of the reforming reaction unit 2 becomes less than 300 ° C. (step S39), the water supply unit 7 is controlled to stop the supply of water, stop the supply of water vapor, and sufficiently replace the inside of the apparatus. The raw material is aerated for a predetermined time, and thereafter, the raw material supply unit 6 is controlled to stop the aeration of the raw material, and the stopping operation is ended (steps S35, 32, 33).

  As described above, according to the hydrogen production apparatus of the present embodiment, the same effects as those of the first embodiment can be obtained.

  In the present embodiment, the temperature state of the apparatus may vary depending on the start-up conditions and operating conditions of the apparatus even during the same operation operation time. For this reason, it is preferable to use in combination with the control based on the operation duration time, as well as to grasp the temperature state of the apparatus based on the temperature of the reforming reaction unit 2 as in the first embodiment. Thereby, it becomes possible to improve the determination accuracy of the temperature state of the apparatus.

  By the way, the hydrogen production apparatus according to the present invention can be used for various applications, and may have other configurations as appropriate according to the applications. For example, in a hydrogen production apparatus that generates hydrogen to be supplied to a fuel cell power generation apparatus, it is necessary to generate hydrogen with a reduced concentration of carbon monoxide. Part and a carbon monoxide selective oxidation part are provided. Hereinafter, the hydrogen production apparatus having such a configuration will be described as an example.

(Embodiment 3)
FIG. 8 is a schematic diagram showing the configuration of the hydrogen production apparatus according to Embodiment 3 of the present invention. As shown in FIG. 8, the hydrogen production apparatus of the present embodiment has the same apparatus configuration as the hydrogen production apparatus of the first embodiment, but differs from the first embodiment in the following points.

  In the hydrogen production apparatus 100 ′ of the present embodiment, a carbon monoxide conversion unit 10 and a carbon monoxide selective oxidation unit 11 are further arranged in this order on the downstream side of the hydrogen generation unit 1. Specifically, for example, in the hydrogen production apparatus in which the reforming reaction unit 2 has a cylindrical shape as shown in FIG. 2, the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 generate heat generated in the combustion unit 4. Is disposed downstream of the reforming reaction section 2 in the heat transfer path. Due to the heating by the combustion unit 4, the temperatures of the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 during the operation are about 200 ° C. to 250 ° C. and about 100 ° C. to 150 ° C.

  The carbon monoxide shifter 10 includes a platinum group shift catalyst. The carbon monoxide selective oxidation unit 11 includes a platinum group oxidation catalyst. The gas inlet of the carbon monoxide shifter 10 is connected to a reformed gas takeout pipe 12 that communicates with the reformed gas flow path d of the reformed gas reaction unit 2 of the hydrogen generator 1, and the gas of the carbon monoxide shifter 10. The outlet is connected to the gas inlet of the carbon monoxide selective oxidation unit 11 by a post-transform gas extraction pipe 13. An air supply pipe 14 for introducing air is connected to the post-transform gas extraction pipe 13, and the air used for the oxidation reaction in the carbon monoxide selective oxidation unit 11 through the air supply pipe 14 is carbon monoxide selection. It is supplied to the oxidation unit 11. A hydrogen gas extraction pipe 15 is connected to the gas outlet of the carbon monoxide selective oxidation unit 11.

  Further, the carbon monoxide shift unit 10 and the carbon monoxide selective oxidation unit 11 are respectively provided with a shift temperature measurement unit 16 and a selective oxidation temperature measurement unit 17, which are specifically composed of thermocouples. Has been. The shift temperature measuring unit 16 is arranged to detect the temperature in the shift catalyst and / or the carbon monoxide shift unit 10 (atmosphere temperature or component temperature), and the selective oxidation temperature measuring unit 17 is an oxidation catalyst. And / or a temperature in the carbon monoxide selective oxidation unit 11 (atmosphere temperature or temperature of the constituent member) is detected. Further, the temperature information of the carbon monoxide shifter 10 and the carbon monoxide shifter 11 detected by the shift temperature measurement unit 16 and the selective oxidation temperature measurement unit 17 is transmitted to the control unit 9.

  In the hydrogen production apparatus 100 ′ having such a configuration, the reformed gas generated in the reforming reaction unit 2 as in Embodiment 1 is transferred from the hydrogen generating unit 1 to the carbon monoxide conversion unit 10 through the reformed gas take-out pipe 12. To be supplied. In the carbon monoxide shifter 10, the reforming reaction of the reformed gas is performed using the shift catalyst, and the concentration of carbon monoxide in the reformed gas is reduced. Further, the gas obtained in the carbon monoxide shifter 10, that is, the gas after shift, is supplied to the carbon monoxide selective oxidizer 11 through the post-shift gas extraction pipe 13. At this time, air is supplied to the carbon monoxide selective oxidation unit 11 together with the post-transformation gas through the air supply pipe 14 connected to the post-transformation gas extraction pipe 13. In the carbon monoxide selective oxidation unit 11, an oxidation reaction of the post-modification gas is performed using air and an oxidation catalyst, thereby further reducing the carbon monoxide concentration in the post-modification gas. Thus, the hydrogen gas having a reduced carbon monoxide concentration is taken out of the apparatus through the hydrogen gas take-out pipe 15.

  By the way, in the above-described first embodiment, the temperature of the reforming reaction unit 2 at the start of the stop operation of the apparatus is detected by the reforming temperature measuring unit 3, and the temperature state of the apparatus is detected by the control unit 9 based on this detected temperature. However, in the hydrogen production apparatus of the present embodiment, not only the reforming temperature measuring unit 3 detects the temperature of the reforming reaction unit 2 but also the transformation temperature measuring unit 16 at the start of the stop operation. While detecting the temperature of the carbon monoxide conversion unit 10, the selective oxidation temperature measurement unit 17 detects the temperature of the carbon monoxide selective oxidation unit 11. Then, the control unit 9 determines the temperature state of the apparatus based on the detected temperatures of the reforming reaction unit 2, the carbon monoxide conversion unit 10, and the carbon monoxide selective oxidation unit 11, and the temperature of the apparatus is determined according to the determination result. The replacement operation is performed by setting the replacement gas according to the state. According to such a configuration of the present embodiment, the following effects are exhibited.

  As described above, the temperature state of the apparatus at the start of the stop operation is not only different depending on the operating state before the apparatus is stopped, but also in each part constituting the apparatus depending on the configuration, arrangement, and the like. For example, FIG. 9 is a diagram showing detected temperatures in the reforming temperature measuring unit 3, the transformation temperature measuring unit 16, and the selective oxidation temperature measuring unit 17 when the apparatus is started and operated from a sufficiently cooled state. It is. As shown in FIG. 9, since the apparatus is in a sufficiently cooled state before the start-up here, the reforming reaction is detected by the reforming temperature measuring unit 3, the transformation temperature measuring unit 16, and the selective oxidation temperature measuring unit 17. The temperature of the section 2, the carbon monoxide shift section 10, and the carbon monoxide selective oxidation section 11 is about room temperature. When the apparatus is started from such a cold state, the reforming reaction section 2 is located upstream of the heat transfer path of the combustion section 4 relative to the carbon monoxide shift section 10 and the carbon monoxide selective oxidation section 11 due to the apparatus configuration. Therefore, the reforming reaction section 2 is preferentially heated by the heat of the combustion section 4 over the other two, and the temperature rises quickly. Therefore, the temperature of the reforming reaction unit 2 becomes high even if the elapsed time from the start of activation is short. On the other hand, the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 are located downstream of the reforming reaction unit 2 in the heat transfer path of the combustion unit 4. The rise is moderate.

  On the other hand, FIG. 10 shows each detection in the reforming temperature measurement unit 3, the modification temperature measurement unit 16, and the selective oxidation temperature measurement unit 17 when the apparatus is once stopped after a long time operation and then restarted immediately after that. It is a figure which shows temperature. When the apparatus is once stopped after operating for a long time, the temperature in the reforming reaction section 2 kept at a high temperature during the operation rapidly decreases with the stop. On the other hand, in the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 in which the operating temperature is kept lower than that of the reforming reaction unit 2, the temperature rapidly decreases as in the reforming reaction unit 2. Rather, it is heated by receiving heat radiation from the reforming reaction unit 2, and the temperature becomes higher than that of the reforming reaction unit 2. When the operation is resumed after the stop, the reforming reaction unit 2 is preferentially heated by the heat of the combustion unit 4 over the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11, and the temperature rises quickly. On the other hand, the temperature of the carbon monoxide shifter 10 and the carbon monoxide selective oxidizer 11 is moderately higher than that of the reforming reactor 2, but in this case, the temperature at the time of restarting operation is compared as described above. Since the temperature is high, the temperature rises more quickly than in the case shown in FIG.

  Next, consider the case where, for example, the apparatus is stopped after 10 minutes have elapsed since the start of the operation in each of the operating situations shown in FIGS. 9 and 10. As shown in FIGS. 9 and 10, in the case of FIG. 9 in the state cooled to room temperature, the temperature of the reforming reaction unit 2 at the start of the stop operation of the apparatus is about 200 ° C., whereas FIG. In this case, the temperature of the reforming reaction unit 2 at the start of the stop operation is about 600 ° C. In the carbon monoxide shifter 10 and the carbon monoxide selective oxidizer 11, the temperature at the start of the stop operation in the case of FIG. 9 is about room temperature, whereas the start of the stop operation in the case of FIG. The temperature at the time is about 200 ° C. for the carbon monoxide shift section 10 and about 150 ° C. for the carbon monoxide selective oxidation section 11.

  When the apparatus is stopped 10 minutes after the start of starting and the temperature state of the apparatus is determined according to the temperature of the reforming reaction section 2 as in the first embodiment, in the case of FIG. Therefore, the temperature state of the apparatus is determined to be the second state (that is, a state where water condensation and carbon deposition can be avoided). Here, for example, if the second replacement setting is made so that the mixed gas of the raw material and water vapor is used as the replacement gas when the apparatus is in the second state, the determination result based on the temperature of the reforming reaction unit 2 Accordingly, the gas substitution in the apparatus is performed by the second substitution setting, that is, the mixed gas. However, as described above, the temperatures of the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 at this time are less than 100 ° C. In the carbon monoxide shifter 10 and the carbon monoxide selective oxidizer 11, the water vapor in the replacement gas is condensed to produce water. For this reason, even though the replacement setting is selected based on the temperature detected by the reforming temperature measuring unit 3 at the start of the stop operation, water condensation in the carbon monoxide shifter 10 and the carbon monoxide selective oxidizing unit 11 is performed. The catalytic activity may be reduced.

  On the other hand, in the case of FIG. 10, since the temperature of the reforming reaction unit 2 is about 600 ° C., the temperature state of the apparatus is determined to be the fifth state (that is, the state where the oxidation reaction of the reforming catalyst occurs). Here, for example, when the fifth replacement setting is made so that the mixed gas of the raw material and water vapor is used as the replacement gas when the apparatus is in the fifth state, the raw material and water vapor are mixed according to the fifth replacement setting. The gas in the apparatus is replaced by the mixed gas. At this time, since the temperatures of the carbon monoxide shifter 10 and the carbon monoxide selective oxidizer 11 are higher than 100 ° C., condensed water is generated from the water vapor in the replacement gas. There is nothing.

  As described above, the temperature states of the reforming reaction unit 2, the carbon monoxide conversion unit 10, and the carbon monoxide selective oxidation unit 11 are different from each other depending on the operation state before the apparatus is stopped, and in particular, the carbon monoxide conversion unit 10. In addition, the temperature state of the carbon monoxide selective oxidation unit 11 is more greatly affected by the operating state before the apparatus is stopped because the temperature rise accompanying heating by the combustion unit 4 is more gradual than that of the reforming reaction unit 2. Therefore, in order to prevent the decrease in the catalyst activity more reliably, not only the temperature state of the apparatus is determined based on the temperature of the reforming reaction section 2 at the start of the stop operation of the apparatus, but also the carbon monoxide conversion section 10 In addition, it is preferable to comprehensively consider the temperature of the carbon monoxide selective oxidation unit 11 and grasp the temperature state of the apparatus more accurately.

  In the present embodiment, in addition to the reforming temperature measuring unit 3 that detects the temperature of the reforming reaction unit 2, a conversion temperature measuring unit 16 that detects the temperature of the carbon monoxide conversion unit 10, and a carbon monoxide selective oxidation unit. 11 and a selective oxidation temperature measuring unit 17 for detecting the temperature of the apparatus 11, and at the start of the operation of stopping the apparatus, the temperatures of the reforming reaction unit 2, the carbon monoxide conversion unit 10, and the carbon monoxide selective oxidation unit 11 are set. These are detected by the reforming temperature measuring unit 3, the transformation temperature measuring unit 16, and the selective oxidation temperature measuring unit 17, respectively. The detected temperature information is transmitted to the process control unit 61 of the control unit 9. And the process control part 61 which acquired these temperatures determines the temperature state of an apparatus as follows.

  That is, in the method for determining the temperature state of the apparatus in the present embodiment, the process control unit 61 first performs the reforming temperature measurement unit 3 at the start of the stop operation, similarly to the method of the first embodiment of FIG. Based on the detected temperature of the reforming reaction unit 2, the temperature state of the apparatus at the start of the stop operation is determined from the first to fifth states by comparison with the first to fourth reference temperatures. . Further, here, in addition to the determination based on the temperature of the reforming reaction unit 2, the temperature of the carbon monoxide conversion unit 10 at the start of the stop operation detected by the conversion temperature measurement unit 16 and the selective oxidation temperature measurement unit 17 are detected. It is determined whether or not the temperature of the carbon monoxide selective oxidation unit 11 at the start of the stopped operation is less than 100 ° C. When at least one of the carbon monoxide shifter 10 and the carbon monoxide selective oxidizer 11 is less than 100 ° C., the gas does not contain water vapor even if the temperature of the reforming reaction unit 2 is 100 ° C. or higher. Gas replacement in the apparatus is performed using On the other hand, when the temperature of the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 is 100 ° C. or higher, a gas containing water vapor is used according to the substitution setting selected based on the temperature of the reforming reaction unit 2. To replace the gas in the equipment.

  In the present embodiment, as described above in the first embodiment, according to the temperature change of the reforming reaction unit 2, the carbon monoxide conversion unit 10, and the carbon monoxide selective oxidation unit 11 during the stop operation, Change the replacement gas type by selecting the optimal replacement setting as appropriate.

  According to the present embodiment, the temperature state of the apparatus at the start of the operation for stopping operation can be grasped more accurately, so that a more appropriate in-apparatus gas replacement operation can be performed. Specifically, the gas replacement operation in the apparatus can be performed while preventing water condensation in the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 as well as the reforming reaction unit 2. For example, as an example of the present embodiment, the apparatus is operated under each situation in FIGS. 9 and 10, and the apparatus is stopped after 10 minutes from the start of starting, and the gas replacement operation in the apparatus is performed by the above method. At the same time, when a series of operations for starting up the apparatus again was repeated about 100 times, the reforming catalyst did not show a significant decrease in catalytic activity, and stable and good hydrogen production was possible. .

(Embodiment 4)
The hydrogen production apparatus according to Embodiment 4 of the present invention has the same configuration as the hydrogen production apparatus of Embodiment 3, and is detected by the reforming temperature measurement unit 3 in the same manner as in Embodiment 1. The temperature state of the apparatus is determined based on the temperature of the reforming reaction unit 2, but here, data related to the operation status of the apparatus before the operation stop, specifically, the operation operation time before the stop and the start-up Data such as the temperature of each part during operation and operation (hereinafter referred to as operation data) is stored in the storage unit 62 of the control unit 9, and in the determination of the temperature state of the device at the start of the stop operation The temperature state of the apparatus is determined in consideration of the operation data together with the temperature of the reforming reaction unit 2.

  If the temperature state of the apparatus is determined only by the temperature of the reforming reaction unit 2 at the start of the stop operation, as described above in the third embodiment, the temperature state of the carbon monoxide shifter 10 and the carbon monoxide selective oxidation unit 11 Is not reflected, there is a case where an appropriate gas replacement operation in the apparatus cannot be performed. By the way, as shown in FIG. 9 and FIG. 10 described above, the temperatures of the carbon monoxide conversion unit 10 and the carbon monoxide selective oxidation unit 11 at the start of the stop operation are the operation history of the operation and stop of the apparatus, and before the stop. It depends on the operating time. Therefore, in the present embodiment, the operation history of operation and stop of the apparatus and the operation operation time before the stop are stored in the storage unit 62 of the control unit 9 as operation data of the apparatus, and when the temperature state of the apparatus is determined, the reforming is performed. The determination is performed in consideration of this operation data together with the temperature of the reaction unit 2. Thus, by considering the operation history of the operation and stop of the apparatus and the operation operation time before the stop, the carbon monoxide shifter 10 and the carbon monoxide selective oxidation at the start of the stop operation without directly measuring the temperature. The state other than the reforming reaction unit 2 such as the unit 11 can be estimated, and therefore the temperature state of the apparatus can be comprehensively determined in consideration of the temperature of each unit. Therefore, the gas replacement operation in the apparatus is performed in consideration of the temperature state of the apparatus that is not reflected in the temperature detected by the reforming temperature measuring unit 3, such as the temperature state of the carbon monoxide shifter 10 or the carbon monoxide selective oxidizer 11 here. Therefore, as in the case of the third embodiment, it is possible to perform more appropriate in-apparatus gas replacement.

(Embodiment 5)
FIG. 11 is a schematic block diagram showing the configuration of the fuel cell power generator according to Embodiment 5 of the present invention. As shown in FIG. 11, the fuel cell power generation device according to the present embodiment includes a hydrogen production device 100 ′ according to the third embodiment, a polymer electrolyte fuel cell (hereinafter simply referred to as a fuel cell) 101, and water recovery. The apparatus 102, the blower 103, and the control apparatus 9 are provided as main components. The control device 9 controls the hydrogen production device 100 ′, the fuel cell 101, the water recovery device 102, and the blower 103. Here, a control signal for stopping the fuel cell power generation device is output to the control device 9. This is the time when the stop operation of the fuel cell power generation device is started, and the state where the operations of all the components 100 ′, 101, 102, 103 are stopped is the stop of the fuel cell power generation device. The start of the stop operation of the fuel cell power generation apparatus corresponds to the start of the stop operation of the hydrogen production apparatus 100 ′.

  The hydrogen production apparatus 100 ′ is connected to the fuel cell 101 through a power generation fuel pipe 104 and a fuel off gas pipe 105. The fuel cell 101 is connected to the blower 103 via the air pipe 106 and is connected to the water recovery apparatus 102 via the water recovery pipe 107. The water recovery apparatus 102 is further connected to the water supply unit 7 of the hydrogen production apparatus 100 ′ through a water recovery pipe 107.

  When the fuel cell power generator is in operation, first, hydrogen gas is generated in the hydrogen production apparatus 100 ′ as described above. The generated hydrogen gas is supplied to the fuel electrode side of the fuel cell 101 through the power generation fuel pipe 104 as power generation fuel. On the other hand, air is supplied from the blower 103 to the air electrode side of the fuel cell 101 via the air pipe 106. In the fuel cell 101, the supplied hydrogen gas and air react (hereinafter referred to as a power generation reaction) to generate power, and heat is generated along with this power generation reaction. Although illustration is omitted here, the electric energy obtained by the fuel cell 101 is supplied to the power load terminal and used for various purposes, while the heat energy generated in response to the power generation reaction is used for heat recovery. It collect | recovers by a means, and is supplied to a heat load terminal after that, and is utilized for various uses. As the heat recovery means, for example, a hot water recovery device or the like is used.

  Water generated by the power generation reaction in the fuel cell 101 is recovered by the water recovery device 102 through the water recovery pipe 107, and part or all of the water is further supplied through the water recovery device 107 to the water supply unit 7 of the hydrogen production device 100 ′. Sent to. On the other hand, unused hydrogen gas (so-called off gas) that has not been used for the power generation reaction is taken out of the fuel cell 101 and supplied as combustion fuel to the combustion unit 4 of the hydrogen production apparatus 100 ′ through the fuel off gas pipe 105.

  In the fuel cell power generation device according to the present embodiment, hydrogen gas can be efficiently and stably produced in the hydrogen production device 100 ′, so that hydrogen gas can be stably supplied to the fuel cell 101. It becomes possible. Therefore, in the fuel cell 101, it is possible to stably generate electric power energy and thermal energy, and it is possible to realize a cogeneration apparatus that is excellent in energy saving and economy.

(Embodiment 6)
FIG. 12 is a schematic cross-sectional view showing the configuration of the main part of the reforming reaction section of the hydrogen production apparatus according to Embodiment 6 of the present invention, and FIG. 13 is an enlarged view of the reforming temperature measuring section of FIG. It is an expanded sectional view. 12 and 13, the same reference numerals as those in FIG. 2 denote the same or corresponding parts.

  As shown in FIGS. 12 and 13, in this embodiment, the reforming temperature measuring unit 3 determines the temperature of the reforming reaction unit 2 as a partition wall between the reformed gas channel d and the post-combustion gas channel g. (Horizontal wall) It is comprised so that it may detect via 33a. In addition, the hydrogen production apparatus 100 is configured such that the interior is not purged with a replacement gas or is finally purged with air when stopped. Other points are the same as in the first embodiment.

  Specifically, as shown in FIG. 13, the partition wall 33a between the reformed gas flow path d and the post-combustion gas flow path g is recessed as viewed from the post-combustion gas flow path g and the reformed gas. A cylindrical recess 33c protruding into the flow path d is formed. In addition, a through hole 33d is formed in a portion of the outer wall (lateral wall) 33b of the post-combustion gas flow channel that faces the concave portion 33c.

On the other hand, the reforming temperature measuring unit 3 has a cylindrical sheath tube 51 whose one end is open and the other end is closed. A flange 51a is formed at one end of the sheath tube 51 (hereinafter referred to as an open end). Inside the sheath tube 51, a thermocouple 54 is inserted such that the tip 54a contacts the bottom 51b of the sheath tube 51. Furthermore, the sheath tube 51 is filled with a powdery filler 54 so as to fill the space between the thermocouple 54 and the tube wall. The filler 54 is for preventing the movement of the thermocouple, and is made of a thermally conductive and electrically insulating material such as magnesium oxide (MgO 2 ). And the open end of the sheath pipe | tube 51 is sealed by the cover plate 52 fitted to the flange 51a. The lid plate 52 is joined to the flange 51a of the sheath tube 51 by an appropriate means such as welding. Further, a through hole is formed in the lid plate 52, and the thermocouple 54 is led out of the sheath tube 51 through the through hole.

  The sheath tube 51 of the reforming temperature measuring unit 3 is fitted into the recess 33c of the partition wall 33a through the through hole 33d of the outer wall 33b of the post-combustion gas flow path g with the bottom 51b first (upward). ing. The bottom 51b (tip portion) of the sheath tube 51 is in contact with the bottom (partition wall 33a) of the recess 33c. The sheath tube 51 is fixed to the outer wall 33b by fixing the flange 51a to the outer wall 33b of the gas flow path g after combustion with an appropriate fixing tool such as a screw. The flange 51a is fixed to the outer wall 33 such that the packing 55 is sandwiched between the flange 51a and the outer wall 33b of the post-combustion gas flow path g, so that the space between the post-combustion gas flow path g and the outside is sealed. .

  The sheath tube 51 and the lid member 52 are made of a material having thermal conductivity, corrosion resistance, and heat resistance. These characteristics are basically required as a material for a temperature measuring device used in a corrosive atmosphere. Further, the sheath tube 51 and the lid member 52 are characterized by forming an oxide film functioning as a protective film against corrosion on the surface in an oxidizing atmosphere as a feature characterizing the present invention. Specifically, in the present embodiment, the sheath tube 51 and the lid member 52 are made of stainless steel, and a stainless steel oxide film is formed on the surface thereof in an oxidizing atmosphere.

  Next, the operation of the reforming temperature measuring unit 3 configured as described above will be described.

  Referring to FIGS. 2 and 13, for example, the sheath tube 51 of the reforming temperature measurement unit 3 of the present embodiment is connected to the reformed gas flow path d and the post-combustion similarly to the first embodiment (see FIG. 2). If it is assumed that a partition wall (vertical wall) between the gas channel g and the gas channel g is attached so as to penetrate the partition wall 33, the sheath tube 51 is positioned in the reformed gas channel d. In the present embodiment, the reformed gas flow path d becomes an oxidizing atmosphere when the hydrogen production apparatus stops, due to the intrusion of air or the inclusion of a replacement gas made of air. In this case, an oxide film is formed on the surface of the sheath tube 51. On the other hand, during operation of the hydrogen production apparatus, the reformed gas flow path d is filled with hydrogen-rich gas. Then, the reformed gas flow path d becomes a reducing atmosphere, and the oxide film on the surface of the sheath tube 51 is reduced to iron (not stainless steel). Then, when the reformed gas flow path d becomes an oxidizing atmosphere due to the stoppage of the operation of the next hydrogen production apparatus, this iron is oxidized to become so-called iron rust, and thereby the sheath tube 51 is corroded. And corrosion progresses by the repetition of the oxidation reduction of the sheath pipe | tube 51 accompanying the repetition of a driving | operation and stop of such a hydrogen production apparatus.

  On the other hand, in the present embodiment, the sheath tube 51 is positioned in the post-combustion gas flow path g. The post-combustion gas flow path g becomes an oxidizing atmosphere when air enters when the hydrogen production apparatus is stopped. On the other hand, when the hydrogen production apparatus is in operation, the post-combustion gas is filled. This post-combustion gas contains air that was supplied for the combustion of the fuel gas and was not consumed for the combustion of the fuel gas. The rear gas flow path g becomes an oxidizing atmosphere. That is, the post-combustion gas flow path g is always in an oxidizing atmosphere. Therefore, even if the operation and stop of the hydrogen production apparatus are repeated, corrosion due to the above mechanism can be prevented. The reforming temperature measuring unit 3 is configured such that the tip (bottom) 51b of the sheath tube 51 is in contact with the partition wall 33a (more precisely, the recess 33c) that partitions the reformed gas flow path d, and the tip 54a of the thermocouple 54 is Since it is in contact with the tip 51b of the sheath tube 51, the temperature of the reforming reaction unit 2 can be accurately detected. In this case, if necessary, the temperature detected by the thermocouple 54 may be corrected as appropriate, so that the temperature of the reforming reaction unit 2 can be detected more accurately.

  As described above, according to the present embodiment, the hydrogen production apparatus of the reforming temperature measurement unit 3 having the sheath tube 51 on which the oxide film is formed in the oxidizing atmosphere is repeatedly operated and stopped. Corrosion can be prevented.

  In the first to fifth embodiments, the temperature of a required part of the hydrogen production apparatus such as the reforming reaction unit 2 is directly detected, but this may be detected indirectly by detecting the pressure or the like, for example.

  INDUSTRIAL APPLICATION This invention is useful as a hydrogen production apparatus which can prevent the fall of the catalyst activity which arises with the stop operation | movement of an apparatus, and even if it operates and stops an apparatus frequently, catalyst activity falls. It is useful as a hydrogen production device that does not have any problems. Such a hydrogen production apparatus can be used for, for example, a fuel cell power generation apparatus, thereby realizing a cogeneration apparatus excellent in economy and energy saving.

It is a typical block diagram which shows the structure of the hydrogen production apparatus which concerns on Embodiment 1 of this invention. It is typical sectional drawing which shows the structure of the principal part of the reforming reaction part of FIG. It is a block diagram which shows the structure of the control part of FIG. It is a figure which shows the relationship between oxidation temperature and the specific surface area of the Ru metal catalyst of a reforming reaction part. It is a flowchart which shows roughly the content of the stop operation | movement program stored in the control part of FIG. It is a figure which shows the relationship between the operation time memorize | stored in the control part of the hydrogen production apparatus which concerns on Embodiment 2 of this invention, and the temperature of a reforming reaction part. It is a flowchart which shows roughly the content of the stop operation | movement program stored in the control part of the hydrogen production apparatus which concerns on Embodiment 2 of this invention. It is a typical block diagram which shows the structure of the hydrogen production apparatus which concerns on Embodiment 3 of this invention. It is a figure which shows the temperature change of the reforming reaction part, the carbon monoxide transformation part, and the carbon monoxide selective oxidation part at the time of making it start from the state which temperature fell enough. It is a figure which shows the temperature change of the modification | reformation part, carbon monoxide conversion part, and carbon monoxide selective oxidation part at the time of having stopped once after driving | running for a long time, and restarting immediately. It is a typical block diagram which shows the structure of the fuel cell power generation apparatus which concerns on Embodiment 5 of this invention. It is typical sectional drawing which shows the structure of the principal part of the reforming reaction part of the hydrogen production apparatus which concerns on Embodiment 6 of this invention. It is a partial expanded sectional view which expands and shows the reforming temperature measurement part of FIG.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Hydrogen production part 2 Reforming reaction part 3 Reforming temperature measurement part 4 Combustion part 5 Combustion fan 6 Raw material supply part 7 Water supply part 8 Preheating part 9 Control part 10 Carbon monoxide conversion part 11 Carbon monoxide selective oxidation part 16 Modification Temperature measurement unit 17 Selective oxidation temperature measurement unit 20 Reforming catalyst layer 30 Main body 31 Gap 32 Vertical wall 33 Horizontal wall 40 Radiation tube 41 Burner 42 Flame 43 Air flow path 44 Combustion space 51 Sheath tube 51a Flange 51b Bottom 52 Lid material 53 Filling Material 54 Thermocouple 54a Tip 55 Packing 61 Processing Control Unit 62 Storage Unit 63 Operation Input Unit 64 Display Unit 65 Clock Unit 100, 100 ′ Hydrogen Production Device 101 Fuel Cell 102 Water Recovery Device 103 Blower
c Mixed raw material flow path d Reformed gas flow path e Reformed catalyst accommodating part g Post-combustion gas flow path

Claims (17)

  1. A hydrogen generation unit including a reforming reaction unit that generates a hydrogen-rich reformed gas by reacting a raw material containing an organic compound composed of at least carbon and hydrogen with water vapor using a catalyst;
    A heating unit for heating at least the reforming reaction unit;
    A raw material supply unit for supplying the raw material to the hydrogen generation unit;
    A water supply unit for supplying water as a source of the water vapor to the hydrogen generation unit;
    A control unit that controls at least the heating unit, the raw material supply unit, and the water supply unit,
    At the start of the shutdown operation, heating in the heating unit is stopped, and in the shutdown operation, a replacement gas for replacing the hydrogen-rich gas in the device is passed to perform the gas replacement operation in the device. A hydrogen production device,
    In the gas replacement operation in the apparatus, the raw material supplied from the raw material supply unit, the water vapor generated from the water supplied from the water supply unit, air supplied from the outside of the apparatus, and supplied from the outside of the apparatus An inert gas or a gas obtained by mixing two or more of these is used as the replacement gas,
    In the control unit, the composition of the replacement gas used in accordance with the temperature state of the apparatus including at least the temperature of the reforming reaction unit in the shutdown operation is preset,
    The control unit determines the temperature state of the apparatus in the shutdown operation, and performs the gas replacement operation in the apparatus using the replacement gas selected from the determination result and the setting, and the heating unit and the raw material A hydrogen production apparatus characterized by controlling a supply unit and the water supply unit.
  2. It further comprises a reforming temperature detecting means for detecting the temperature of the reforming reaction section,
    2. The hydrogen production apparatus according to claim 1, wherein the control unit determines a temperature state of the apparatus based on a temperature of the reforming reaction unit detected by the reforming temperature detecting unit in the operation of stopping operation.
  3. In the control unit, the reforming reaction unit in the shutdown operation is in a state where water condensation of water vapor occurs, in a state where thermal decomposition of the raw material occurs, whether carbon monoxide and carbon dioxide. At least one reference temperature is set in advance as a criterion for determining whether or not carbon disproportionation occurs or whether or not oxidation of the catalyst occurs.
    The hydrogen production apparatus according to claim 2, wherein the temperature state of the apparatus is determined by comparing the temperature of the reforming reaction section detected by the reforming temperature detecting means with the reference temperature when the operation is stopped.
  4.   The apparatus further comprises temperature detecting means for detecting the temperature of a predetermined portion other than the reforming reaction section, and determines the temperature state of the apparatus in consideration of the temperature of the predetermined portion in the operation of stopping operation detected by the temperature detecting means. The hydrogen production apparatus according to claim 2.
  5. A carbon monoxide shifter that removes carbon monoxide by a shift reaction from the hydrogen-rich gas produced in the reforming reaction block;
    A carbon monoxide selective oxidation unit that selectively oxidizes the post-transformation gas obtained from the carbon monoxide conversion unit to further remove carbon monoxide;
    A transformation temperature detection means for detecting the temperature of the carbon monoxide transformation section;
    And a selective oxidation temperature detection means for detecting the temperature of the carbon monoxide selective oxidation unit,
    The controller is based on the temperature of the carbon monoxide shifter detected by the shift temperature detector in the shutdown operation and the temperature of the carbon monoxide shifter detected by the selective oxidation temperature detector. Determining whether the carbon monoxide conversion unit and the carbon monoxide selective oxidation unit in the shutdown operation are in a state where water condensation of water vapor occurs, and the determination result and the temperature state of the reforming reaction unit The hydrogen production apparatus according to claim 4, wherein the temperature state of the apparatus is determined based on the determination result.
  6.   The control unit stores an operation state of the device before the operation stop operation, and in the operation stop operation, estimates a temperature state of the device in the operation stop operation from the stored operation state of the device. Item 2. The hydrogen production apparatus according to Item 1.
  7. The correlation between the duration of the driving operation and the temperature state of the device is stored in the control unit in advance, and the duration of the driving operation until the start of the driving stop operation is the operating state of the device before the driving stop operation. Obtained by the control unit,
    The control unit causes the apparatus in the driving operation to condense water from water vapor based on the correlation stored in advance from the acquired duration of the driving operation until the start of the operation of stopping the operation. Whether it is in a state, whether it is a state in which thermal decomposition of the raw material occurs, whether it is a state in which a disproportionation reaction of carbon monoxide and carbon dioxide occurs, or a state in which oxidation of the catalyst occurs The hydrogen production apparatus according to claim 6, wherein it is determined whether or not.
  8.   The controller is configured to perform the gas replacement operation in the apparatus with the replacement gas having a composition excluding the composition of only water vapor when the temperature state of the apparatus in the shutdown operation is a state in which the water is condensed. The hydrogen production apparatus according to claim 3, wherein one replacement gas setting is stored.
  9.   In the control unit, when the temperature state of the apparatus in the shutdown operation is a state in which condensation of the water and thermal decomposition of the raw material can be avoided, the raw material, the water vapor, the air, the inert gas, or The hydrogen production apparatus according to claim 3, wherein a second replacement gas setting is stored so that the gas replacement operation in the apparatus is performed with the mixed gas containing two or more of these.
  10.   The control unit performs the gas replacement operation in the apparatus with the replacement gas having a composition excluding the composition of only the raw material when the temperature state of the apparatus in the shutdown operation causes the thermal decomposition of the raw material. The hydrogen production apparatus according to claim 3, wherein the third replacement gas setting is stored.
  11.   The control unit includes a fourth replacement gas so as to perform the gas replacement operation in the apparatus with the replacement gas containing the water vapor when the temperature state of the apparatus in the shutdown operation causes the disproportionation reaction. The hydrogen production apparatus according to claim 3, wherein the setting is stored.
  12.   The controller is configured to perform the gas replacement operation in the apparatus with the replacement gas having a composition excluding the composition of only the air when the temperature state of the apparatus in the shutdown operation causes oxidation of the catalyst. The hydrogen production apparatus according to claim 3, wherein a fifth replacement gas setting is stored.
  13. In the control unit,
    The first reference temperature, which is a criterion for determining whether or not the reforming reaction section is in a state where water is condensed from steam, and the criterion for determining whether or not thermal decomposition of the raw material occurs A second reference temperature that is higher than the first reference temperature, a third reference temperature that is higher than the second reference temperature that is a criterion for determining whether or not the disproportionation reaction occurs, and A fourth reference temperature higher than the third temperature, which is a criterion for determining whether or not the catalyst is oxidized, is set in advance;
    If the temperature of the reforming reaction part detected in the shutdown operation is less than the first reference temperature, the raw material is the replacement gas based on the first replacement gas setting,
    If the temperature is equal to or higher than the first reference temperature and lower than the second reference temperature, the raw material is used as the replacement gas based on the second replacement gas setting.
    If the temperature is equal to or higher than the second reference temperature and lower than the third reference temperature, the water vapor is used as the replacement gas based on the third replacement gas setting.
    If the temperature is equal to or higher than the third reference temperature and lower than the fourth reference temperature, the ratio of water molecules S to carbon atoms C derived from the raw material including the raw material and the water vapor based on the fourth replacement gas setting A mixed gas having S / C of 2 or more is used as the replacement gas,
    If the temperature is equal to or higher than the fourth reference temperature, the mixed gas of the raw material and the water vapor supplied at the same supply amount as in the hydrogen generating operation based on the fifth replacement gas setting is used as the replacement gas, The hydrogen production apparatus according to claim 8, wherein the gas replacement operation in the apparatus is performed.
  14. Based on the correlation between the duration of the operation and the temperature of the reforming reaction unit, the control unit determines whether or not the reforming reaction unit in a shutdown operation is in a state where water is condensed from water vapor. A first reference time serving as a determination criterion, a second reference time longer than the first reference time serving as a determination criterion regarding whether or not the raw material is thermally decomposed, and the unevenness. A third reference time that is longer than the second reference time, which is a criterion for determining whether or not the oxidation reaction occurs, and the first criterion that is a criterion for determining whether or not the catalyst is oxidized. A fourth reference time longer than the reference time of 3 is preset,
    The duration of the operation is
    If it is less than the first reference time, the raw material is the replacement gas based on the first replacement gas setting,
    If it is not less than the first reference time and less than the second reference time, the raw material is the replacement gas based on the second replacement gas setting,
    If it is not less than the second reference time and less than the third reference time, the water vapor is used as the replacement gas based on the third replacement gas setting,
    If it is more than the third reference time and less than the fourth reference time, the ratio of water molecules S to carbon atoms C derived from the raw material including the raw material and the water vapor based on the fourth replacement gas setting A mixed gas having S / C of 2 or more is used as the replacement gas,
    If the temperature is equal to or higher than the fourth reference temperature, the mixed gas of the raw material and the water vapor supplied at the same supply amount as in the hydrogen generating operation based on the fifth replacement gas setting is used as the replacement gas, The hydrogen production apparatus according to claim 8, wherein the gas replacement operation in the apparatus is performed.
  15.   2. The hydrogen production according to claim 1, wherein the control unit controls the gas replacement operation in the apparatus according to a change in a temperature state of the apparatus in the operation stop operation in the gas replacement operation in the apparatus in the operation stop operation. apparatus.
  16.   The hydrogen production apparatus according to claim 15, wherein the control unit determines a temperature state of the apparatus during the shutdown operation and selects an appropriate setting of the replacement gas from the determination result.
  17.   2. The hydrogen production apparatus according to claim 1, and a fuel that is supplied with a hydrogen-rich gas produced by the hydrogen production apparatus as a raw material and is supplied with oxygen as an oxidant to generate heat and electricity by the oxidation of the hydrogen-rich gas. A fuel cell power generator comprising the battery.
JP2005336918A 2004-01-22 2005-11-22 Hydrogen production apparatus and fuel cell power generation apparatus Active JP4664808B2 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2004014751 2004-01-22
JP2005336918A JP4664808B2 (en) 2004-01-22 2005-11-22 Hydrogen production apparatus and fuel cell power generation apparatus

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP2005336918A JP4664808B2 (en) 2004-01-22 2005-11-22 Hydrogen production apparatus and fuel cell power generation apparatus

Related Child Applications (1)

Application Number Title Priority Date Filing Date
JP2004343300 Division

Publications (2)

Publication Number Publication Date
JP2006137668A true JP2006137668A (en) 2006-06-01
JP4664808B2 JP4664808B2 (en) 2011-04-06

Family

ID=36618717

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2005336918A Active JP4664808B2 (en) 2004-01-22 2005-11-22 Hydrogen production apparatus and fuel cell power generation apparatus

Country Status (1)

Country Link
JP (1) JP4664808B2 (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2007323972A (en) * 2006-06-01 2007-12-13 Ebara Ballard Corp Fuel treating device and fuel cell system
JP2008251398A (en) * 2007-03-30 2008-10-16 Casio Comput Co Ltd Reactor, power generation device, and shutdown method for reactor
JP2015528432A (en) * 2012-08-30 2015-09-28 エレメント・ワン・コーポレーション hydrogen generation assembly
US9616389B2 (en) 2012-08-30 2017-04-11 Element 1 Corp. Hydrogen generation assemblies and hydrogen purification devices
US9656215B2 (en) 2011-07-07 2017-05-23 Element 1 Corp. Hydrogen generation assemblies and hydrogen purification devices

Citations (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000095504A (en) * 1998-09-22 2000-04-04 Matsushita Electric Works Ltd Reformer
JP2000290001A (en) * 1999-04-05 2000-10-17 Matsushita Electric Ind Co Ltd Operation of hydrogen generation device
WO2000063114A1 (en) * 1999-04-20 2000-10-26 Tokyo Gas Co., Ltd. Single-pipe cylindrical reformer and operation method therefor
JP2002008701A (en) * 2000-06-21 2002-01-11 Tokyo Gas Co Ltd Method for starting and stopping solid polymer fuel cell
JP2002093447A (en) * 2000-09-14 2002-03-29 Tokyo Gas Co Ltd Method for starting and stopping reformer for solid high polymer type fuel cell
JP2002151124A (en) * 2000-11-14 2002-05-24 Tokyo Gas Co Ltd Stopping method of reformer for solid polymer fuel cell
JP2002179401A (en) * 2000-12-11 2002-06-26 Toyota Motor Corp Method of stopping operation of gaseous hydrogen production system
WO2002090249A1 (en) * 2001-05-07 2002-11-14 Matsushita Electric Industrial Co., Ltd. Hydrogen formation apparatus
EP1271679A1 (en) * 2000-03-28 2003-01-02 Matsushita Electric Industrial Co., Ltd. Device for producing hydrogen and method of operating the same
JP2003176105A (en) * 2001-10-03 2003-06-24 Matsushita Electric Ind Co Ltd Hydrogen production apparatus, fuel cell system and method of operating hydrogen production apparatus
JP2003300704A (en) * 2002-02-08 2003-10-21 Nissan Motor Co Ltd Fuel reforming system and fuel cell system
JP2004006217A (en) * 2002-04-12 2004-01-08 Sekisui Chem Co Ltd Fuel cell cogeneration system
JP2004002154A (en) * 2002-03-26 2004-01-08 Matsushita Electric Ind Co Ltd Hydrogen generating apparatus and fuel cell system equipped with the same
JP2004137108A (en) * 2002-10-17 2004-05-13 Nippon Chem Plant Consultant:Kk Method of stopping operation of vapor reforming system
JP2005044684A (en) * 2003-07-24 2005-02-17 Matsushita Electric Ind Co Ltd Fuel cell power generation apparatus
JP2005162580A (en) * 2003-12-05 2005-06-23 Matsushita Electric Ind Co Ltd Hydrogen generator, operation stopping method for hydrogen generator, and fuel cell power generating unit

Patent Citations (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000095504A (en) * 1998-09-22 2000-04-04 Matsushita Electric Works Ltd Reformer
JP2000290001A (en) * 1999-04-05 2000-10-17 Matsushita Electric Ind Co Ltd Operation of hydrogen generation device
WO2000063114A1 (en) * 1999-04-20 2000-10-26 Tokyo Gas Co., Ltd. Single-pipe cylindrical reformer and operation method therefor
EP1271679A1 (en) * 2000-03-28 2003-01-02 Matsushita Electric Industrial Co., Ltd. Device for producing hydrogen and method of operating the same
JP2002008701A (en) * 2000-06-21 2002-01-11 Tokyo Gas Co Ltd Method for starting and stopping solid polymer fuel cell
JP2002093447A (en) * 2000-09-14 2002-03-29 Tokyo Gas Co Ltd Method for starting and stopping reformer for solid high polymer type fuel cell
JP2002151124A (en) * 2000-11-14 2002-05-24 Tokyo Gas Co Ltd Stopping method of reformer for solid polymer fuel cell
JP2002179401A (en) * 2000-12-11 2002-06-26 Toyota Motor Corp Method of stopping operation of gaseous hydrogen production system
WO2002090249A1 (en) * 2001-05-07 2002-11-14 Matsushita Electric Industrial Co., Ltd. Hydrogen formation apparatus
JP2003176105A (en) * 2001-10-03 2003-06-24 Matsushita Electric Ind Co Ltd Hydrogen production apparatus, fuel cell system and method of operating hydrogen production apparatus
JP2003300704A (en) * 2002-02-08 2003-10-21 Nissan Motor Co Ltd Fuel reforming system and fuel cell system
JP2004002154A (en) * 2002-03-26 2004-01-08 Matsushita Electric Ind Co Ltd Hydrogen generating apparatus and fuel cell system equipped with the same
JP2004006217A (en) * 2002-04-12 2004-01-08 Sekisui Chem Co Ltd Fuel cell cogeneration system
JP2004137108A (en) * 2002-10-17 2004-05-13 Nippon Chem Plant Consultant:Kk Method of stopping operation of vapor reforming system
JP2005044684A (en) * 2003-07-24 2005-02-17 Matsushita Electric Ind Co Ltd Fuel cell power generation apparatus
JP2005162580A (en) * 2003-12-05 2005-06-23 Matsushita Electric Ind Co Ltd Hydrogen generator, operation stopping method for hydrogen generator, and fuel cell power generating unit

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2007323972A (en) * 2006-06-01 2007-12-13 Ebara Ballard Corp Fuel treating device and fuel cell system
JP2008251398A (en) * 2007-03-30 2008-10-16 Casio Comput Co Ltd Reactor, power generation device, and shutdown method for reactor
US9656215B2 (en) 2011-07-07 2017-05-23 Element 1 Corp. Hydrogen generation assemblies and hydrogen purification devices
US10391458B2 (en) 2011-07-07 2019-08-27 Element 1 Corp. Hydrogen generation assemblies and hydrogen purification devices
JP2015528432A (en) * 2012-08-30 2015-09-28 エレメント・ワン・コーポレーション hydrogen generation assembly
US9616389B2 (en) 2012-08-30 2017-04-11 Element 1 Corp. Hydrogen generation assemblies and hydrogen purification devices
US9914641B2 (en) 2012-08-30 2018-03-13 Element 1 Corp. Hydrogen generation assemblies
US10166506B2 (en) 2012-08-30 2019-01-01 Element 1 Corp. Hydrogen generation assemblies and hydrogen purification devices

Also Published As

Publication number Publication date
JP4664808B2 (en) 2011-04-06

Similar Documents

Publication Publication Date Title
US7189371B2 (en) Fuel reforming system
JP4130603B2 (en) Operation method of hydrogen production system
US7452391B2 (en) Feedforward control processes for variable output hydrogen generators
US20050191535A1 (en) Apparatus and method for controlling a fuel cell system
US6797420B2 (en) Power generation device and operation method therefor
US20050132649A1 (en) Hydrogen generator, method of shutting down operation of hydrogen generator, and fuel cell system
JP4724029B2 (en) Method for shutting down reformer
EP1840997A1 (en) Method of starting solid oxide fuel cell system
DE19727589B4 (en) Apparatus and method for starting the hydrogen-rich gas generating apparatus
US20040126288A1 (en) Hydrogen generator for fuel cell
KR20020048382A (en) Fuel reforming system
JP2006523603A (en) Method and apparatus for rapid heating of fuel reforming reactants
JP4619753B2 (en) Fuel cell operation control method and system therefor
US8038748B2 (en) Hydrogen-producing fuel processing assemblies, heating assemblies, and methods of operating the same
EP1316529A1 (en) Hydrogen generator
EP2173000A1 (en) Fuel battery system and its activating method
US7838161B2 (en) Reformer and fuel cell system using the same
US7354566B2 (en) Fuel gas production method and apparatus
EP1396473A1 (en) HYDROGEN FORMATION APPARATUS&amp;comma; FUEL CELL SYSTEM AND METHOD FOR CONTROLLING HYDROGEN FORMATION APPARATUS
US20050129997A1 (en) Hydrogen generator, method of operating hydrogen generator, and fuel cell system
DE10106803B4 (en) A reformer control apparatus and method for controlling a reformer
JP2008204655A (en) Reformer system, fuel cell system, and its operation method
DE69935884T2 (en) Reformer control apparatus and method of controlling a reformer using a controller
EP1160902B1 (en) Fuel cell system
US20090317671A1 (en) Hydrogen generator and fuel cell system including the same

Legal Events

Date Code Title Description
A621 Written request for application examination

Free format text: JAPANESE INTERMEDIATE CODE: A621

Effective date: 20070726

A131 Notification of reasons for refusal

Free format text: JAPANESE INTERMEDIATE CODE: A131

Effective date: 20101005

A521 Written amendment

Free format text: JAPANESE INTERMEDIATE CODE: A523

Effective date: 20101119

TRDD Decision of grant or rejection written
A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

Effective date: 20101214

A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

A61 First payment of annual fees (during grant procedure)

Free format text: JAPANESE INTERMEDIATE CODE: A61

Effective date: 20110107

R150 Certificate of patent or registration of utility model

Ref document number: 4664808

Country of ref document: JP

Free format text: JAPANESE INTERMEDIATE CODE: R150

Free format text: JAPANESE INTERMEDIATE CODE: R150

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20140114

Year of fee payment: 3