JP2009292661A - Hydrogen production apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a hydrogen production apparatus which is preheated by circulating residual heat or waste heat when the apparatus is in a halting state after cooling, and to which a heat medium from an external heat source is supplied when the apparatus is heated up and reaches hydrogen production conditions in start-up operation. <P>SOLUTION: The hydrogen production apparatus includes: an oxygen-containing hydrocarbon vaporizer 6; a steam generator 5; an oxygen-containing hydrocarbon-steam mixer 7; a mixed gas preheater 2 which preheats the mixed gas of the oxygen-containing hydrocarbon and steam; a reforming reactor 1 including a reaction tube packed with a reforming catalyst; an external heat source 21 which heats the reforming reactor 1 with a heating medium; a heat medium circulation line 37 which is isolated from the external heat source 21 and connected to at least one vessel selected from the reforming reactor 1, the mixed gas preheater 2, the steam generator 5 and the oxygen-containing hydrocarbon vaporizer 6, and through which the heating medium circulates; a circulating pump or a circulating blower 35 which is disposed in the heat medium circulation line 37 to circulate the heating medium; and a heat medium heater 36 which is disposed in the heat medium circulation line 37 to heat the heating medium. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

  The present invention relates to a hydrogen production apparatus for reforming water vapor using dimethyl ether.

  As one vision of the future society, the realization of a hydrogen energy society using hydrogen as an energy medium is attracting attention, and several promising hydrogen production methods are considered.

  The current mainstream hydrogen production method is to produce hydrogen by a steam reforming method using natural gas or liquefied petroleum gas as a raw material at a reaction temperature of 700 ° C. or more in the presence of a catalyst. In this method, since the raw material contains impurities such as sulfur, a pretreatment is required to treat the impurities. Further, since the reaction temperature is high, it is necessary to use a material having high heat resistance as the reactor structural material.

  As described above, the heat to be heated in conventional hydrogen production requires a high temperature of 700 ° C. or higher. As the heat source, the combustion heat of fossil fuel is used. For this reason, in hydrogen production by the steam reforming method, carbon dioxide is generated by fossil fuel combustion as a heat source, in addition to carbon dioxide generated by fuel reforming.

  The hydrogen produced by this hydrogen production method is characterized in that carbon dioxide, which is a global warming gas, is not generated during combustion when used as an energy source. However, at present, this hydrogen production is accompanied by carbon dioxide generation. In addition, when the heat of combustion of fossil fuel is used as the heat source, air pollutants such as sulfur oxides are simultaneously generated in addition to carbon dioxide.

  On the other hand, in steam reforming using dimethyl ether, since dimethyl ether is a synthetic fuel, impurities such as sulfur are less than natural gas and liquefied petroleum gas. In addition, hydrogen is produced at a temperature lower than that of the conventional method, that is, at a temperature of 400 ° C. or lower.

  As for the hydrogen production method using dimethyl ether, which is highly likely to reduce the environmental load, a technique related to a steam reforming catalyst used in the hydrogen production is known (for example, see Patent Document 1).

  In addition, a technology is known that uses the characteristics of dimethyl ether, which produces hydrogen at a lower temperature than natural gas, and uses an external heat source for the steam reforming heat of dimethyl ether to make a prime mover fuel (for example, Patent Documents). 2 and 3).

  Furthermore, when utilizing the characteristics of dimethyl ether that generates hydrogen at a lower temperature than the natural gas mentioned above, and when using an external heat source for the steam reforming heat of dimethyl ether, residual heat and waste that have not been used so far It is conceivable to use the waste heat that has been used as a heat source and recover the residual heat and waste heat as hydrogen.

  However, such residual heat and waste heat are not always generated constantly. For example, there is a situation in which the production facility operates only during the day or conversely during the night.

  In order to produce hydrogen by steam reforming reaction using residual heat or waste heat that is not always generated constantly, a heat medium related to the residual heat or waste heat in a cooled apparatus in a stopped state Is required to heat up the hydrogen production apparatus and raise the temperature.

  At this time, if dimethyl ether and water as raw materials are supplied without the temperature of the catalyst used for steam reforming reaching the reaction temperature, the catalyst may be contaminated with organic substances. For this reason, it takes a sufficient time until the temperature of the catalyst used for steam reforming reaches the reaction temperature, and the hydrogen production apparatus is heated and heated. Then, it takes too much time to start up and the generation time of residual heat and waste heat is limited, so there is not enough time to produce hydrogen, the amount of hydrogen production by recovering waste heat is small, and the hydrogen production facility Cannot be used effectively.

  For this reason, a “fuel cell rapid start-up device” is known as means for shortening the temperature raising time at the start-up of the hydrogen production device so that it can be started quickly (see, for example, Patent Document 4). This “fuel cell rapid starter” has a reformer that supplies reformed gas to the fuel cell. The reformer includes an evaporation unit that evaporates fuel and water, a reforming unit that uses evaporated fuel and water as a reformed gas, and a CO processing unit that removes CO contained in the reformed gas. Yes. A circulation line for circulating the heat transfer medium to the evaporation unit and the CO processing unit includes a pump for circulating the heat transfer medium, a temperature regulator for adjusting the temperature of the heat transfer medium, and a tank for storing the heat transfer medium, The tank is provided with a temperature maintaining heat source.

  Further, “a fuel reforming apparatus and its starting method” is known as means for shortening the temperature raising time at the start-up of the hydrogen production apparatus so that it can be started quickly (for example, refer to Patent Document 5). This “fuel reformer and its starting method” includes a reformer that is supplied with fuel gas, water vapor, and oxygen-containing gas to generate a hydrogen-containing gas, a combustor that supplies combustion gas to the reformer, A fuel reformer having a heat medium circulation system for circulating a heat medium between a combustor and a reformer. When the temperature of the heat medium is low, an oxygen-containing gas is supplied to the reformer. A partial oxidation reaction is promoted, a heat medium is circulated between the combustor and the reformer, and the heat medium is heated by reaction heat of the partial oxidation reaction.

Further, “a fuel cell hydrogen production apparatus” is known as means for shortening the temperature rising time at the time of activation of the hydrogen production apparatus so that the hydrogen production apparatus can be activated quickly (see, for example, Patent Document 6). This “hydrogen producing apparatus for fuel cell” is a hydrogen producing apparatus for a fuel cell that uses hydrocarbon fuel as a raw material and obtains hydrogen by partial oxidation of the raw material and a steam reforming reaction. This “hydrogen producing apparatus for fuel cell” is provided with an auxiliary combustion chamber on the outer periphery of a reforming reactor that performs a steam reforming reaction, and burns auxiliary fuel in the auxiliary combustion chamber at the time of start-up, thereby Heat is supplied to the reforming reaction chamber to shorten the start-up time of the reforming reaction chamber, and to suppress heat dissipated from the outer periphery of the reforming reaction chamber in a steady state.
JP 2003-38957 A JP-A-11-106770 JP 2003-165704 A JP 2000-30724 A JP 2001-206701 A JP 2003-123819 A

  As mentioned above, when utilizing the characteristics of dimethyl ether, which produces hydrogen at a lower temperature than natural gas, and when using an external heat source for the steam reforming heat of dimethyl ether, It is conceivable to use the waste heat that has been discarded as a heat source and recover the residual heat and waste heat as hydrogen.

  However, such residual heat and waste heat are not always generated constantly. For example, there is a situation in which the production facility operates only during the day or conversely during the night. In order to produce hydrogen by steam reforming reaction using residual heat or waste heat that is not always generated constantly, a heat medium related to the residual heat or waste heat in a cooled apparatus in a stopped state It is necessary to preheat the hydrogen production apparatus, raise the temperature, and perform the start-up operation.

  However, if dimethyl ether and water as raw materials are supplied without the temperature of the catalyst used for steam reforming reaching the reaction temperature, there is a problem that the catalyst is contaminated with organic substances.

  For this reason, it takes a sufficient time until the temperature of the catalyst used for steam reforming reaches the reaction temperature, and the hydrogen production apparatus is heated and heated. Then, if it takes too long to start up, the generation time of residual heat and waste heat is limited, so there is not enough time to produce hydrogen, the amount of hydrogen production by collecting waste heat is small, and the hydrogen production facility There is a problem that cannot be used effectively.

  Therefore, as means for shortening the temperature raising time at the start-up of the hydrogen production apparatus and enabling rapid start-up, “fuel cell rapid start-up device” (see Patent Document 4), “fuel reformer and its start method” (Refer to Patent Document 5) and "hydrogen production apparatus for fuel cell" (refer to Patent Document 6).

  However, the “fuel cell rapid start-up device” (see Patent Document 4) requires a heat transfer medium different from the heat source, and maintains equipment such as a tank and a pump for circulating the heat transfer medium and the temperature. There is a problem that a heat source or the like is further required and the facility becomes large.

  In the “fuel reformer and its starting method” (see Patent Document 5), when the temperature of the heat medium is low, an oxygen-containing gas is supplied to the reformer to promote the partial oxidation reaction. Therefore, there is a problem that the oxygen-containing gas supply facility is required and the facility is enlarged.

  Further, in the “hydrogen producing apparatus for fuel cell” (see Patent Document 6), an auxiliary combustion chamber is provided on the outer periphery of the reforming reactor for performing the steam reforming reaction, and a facility for supplying auxiliary fuel to the auxiliary combustion chamber is required. Thus, there is a problem that auxiliary equipment is required.

  The present invention has been made in order to solve the above-mentioned problems, and a heat medium circulation line that can be isolated from an external heat source is provided, and the cooled apparatus in a stopped state generates residual heat and waste heat via the heat medium circulation line. An object of the present invention is to provide a hydrogen production apparatus in which a heat medium from an external heat source is supplied when the hydrogen production conditions for circulating and preheating, raising the temperature and starting operation are reached.

  In order to achieve the above object, in the hydrogen production apparatus of the present invention, an oxygen-containing hydrocarbon vaporizer for converting the oxygen-containing hydrocarbon used as a raw material into a gaseous state, a water vapor generator for generating water vapor, and a vaporized gas An oxygen-containing hydrocarbon / steam mixer for mixing the oxygen-containing hydrocarbon and steam in the form of a gas, a mixed gas preheater for preheating the mixed gas of the oxygen-containing hydrocarbon and steam to a predetermined reformer supply temperature, and A reforming reactor including a reaction tube into which a mixed gas is introduced and filled with a reforming catalyst, an external heat source for heating the reforming reactor using a heat transfer medium, and the reforming reaction isolated from the external heat source A heat medium circulation line through which a heat transfer medium circulates and is connected to at least one vessel selected from a steam generator, the mixed gas preheater, the water vapor generator, and the oxygen-containing hydrocarbon vaporizer, and the heat medium circulation line Setting It is a circulation pump or circulating blower circulates the heat transfer medium, is characterized in that it has a, a heat medium heater for heating the heat transfer medium provided in the heat medium circulation line.

  In order to achieve the above object, in the hydrogen production apparatus of the present invention, an oxygen-containing hydrocarbon vaporizer for converting the oxygen-containing hydrocarbon as a raw material into a gaseous state, a steam generator for generating water vapor, and a vaporization An oxygen-containing hydrocarbon / steam mixer for mixing the gaseous oxygen-containing hydrocarbon and steam, and a mixed gas preheater for preheating the mixed gas of oxygen-containing hydrocarbon and steam to a predetermined reformer supply temperature; A reforming reactor including a reaction tube into which the mixed gas is introduced and filled with the reforming catalyst, an external heat source for heating the reforming reactor using a heat transfer medium, and the reforming reactor in parallel A heat medium circulation line provided for circulating a heat transfer medium for controlling the temperature of the reforming reactor, a circulation pump or a circulation blower provided in the heat medium circulation line for circulating the heat transfer medium, and the heat medium Provided in the circulation line It is characterized in that it has a, a heat medium heater for heating the heat transfer medium.

  According to the hydrogen production apparatus of the present invention, a heating medium circulation line that can be isolated from an external heat source is provided, and the cooled apparatus in a stopped state is preheated by circulating residual heat and waste heat through the heating medium circulation line. When the hydrogen production conditions are reached when the temperature is raised and the startup operation is reached, the heat medium from the external heat source is supplied, so that residual heat that has not been used or wasted waste heat is used as the heat source. The efficiency of hydrogen production can be improved.

  Hereinafter, an embodiment of a hydrogen production apparatus according to the present invention will be described with reference to the drawings. Here, the same or similar parts are denoted by common reference numerals, and redundant description is omitted.

  FIG. 1 is a block diagram showing the configuration of the hydrogen production apparatus according to the first embodiment of the present invention.

  First, the basic configuration of the hydrogen production apparatus will be described with reference to FIG.

  As shown in FIG. 1, the hydrogen production apparatus includes an oxygen-containing hydrocarbon vaporizer 6 that converts the oxygen-containing hydrocarbon 12 that is the introduced raw material into a gaseous state. Moreover, it has the water vapor generator 5 which introduce | transduces the water 11 used as a raw material, and generates the water vapor | steam 17. FIG. The vaporized gaseous oxygen-containing hydrocarbon 12 and water vapor 17 are introduced into the oxygen-containing hydrocarbon / steam mixer 7 and mixed to form an oxygen-containing hydrocarbon / steam mixed gas 13. This mixed gas comprising the oxygen-containing hydrocarbon / steam mixed gas 13 is introduced into the mixed gas preheater 2 in order to preheat to a predetermined reformer supply temperature. The oxygen-containing hydrocarbon / steam mixed gas 14 preheated by the mixed gas preheater 2 is introduced into the reforming reactor 1 having a reaction tube filled with a reforming catalyst. The reformed gas 15 reformed in the reforming reactor 1 recovers heat from the reformed gas 15 and preheats the water preheater 3 and the oxygen-containing hydrocarbon 12 for preheating the raw water 11. Is introduced into the oxygen-containing hydrocarbon preheater 4 and led out as reformed gas 16 to the next process.

  Next, the heat medium circulation line 37 of the hydrogen production apparatus according to the present embodiment will be described with reference to FIG.

  As shown in FIG. 1, the heat medium circulation line 37 of the hydrogen production apparatus is connected to at least one container of the reforming reactor 1, the mixed gas preheater 2, the steam generator 5, and the oxygen-containing hydrocarbon vaporizer 6. And a heat transfer medium that can heat these containers is circulated. Here, the heat-medium circulation line 37 shows the example connected to all the containers of the reforming reactor 1, the mixed gas preheater 2, the steam generator 5, and the oxygen-containing hydrocarbon vaporizer 6.

  This heat transfer medium is introduced into the heat medium circulation line 37 from the external heat source 21 via the external heat source inlet isolation valve 31. The heat exchange medium subjected to heat exchange is led to the external heat source 22 via the external heat source outlet isolation valve 32.

  In the present embodiment configured as described above, the oxygen-containing hydrocarbon 12 is converted into a gas via the oxygen-containing hydrocarbon preheater 4 and the oxygen-containing hydrocarbon vaporizer 6, and the oxygen-containing hydrocarbon / steam mixer. 7 is supplied. Further, the water 11 is converted into steam via the water preheater 3 and the steam generator 5, supplied to the oxygen-containing hydrocarbon / steam mixer 7, and mixed with the oxygen-containing hydrocarbon 12.

  The oxygen-containing hydrocarbon / steam mixed gas 13 that has passed through the oxygen-containing hydrocarbon / steam mixer 7 is preheated to a predetermined reformer supply temperature by the mixed gas preheater 2. The preheated oxygen-containing hydrocarbon / steam mixed gas 14 is supplied to the reforming reactor 1.

  In the reforming reactor 1, when the oxygen-containing hydrocarbon / steam mixed gas 13 as a raw material gas passes through the reforming catalyst layer filled in the reforming reactor, the hydrogen-rich reforming by the steam reforming reaction is performed. It becomes the quality gas 15 and is led out from the reforming reactor 1. This reformed gas 15 exchanges heat with water 11 and oxygen-containing hydrocarbon 12 which are raw materials in the water preheater 3 and the oxygen-containing hydrocarbon preheater 4, respectively, and is discharged as a reformed gas 16 to the next process.

  The heat transfer medium from the external heat source 21 first exchanges heat with the process gas in the mixed gas preheater 2 after exchanging heat necessary for the steam reforming reaction in the reforming reactor 1, and then generates steam. Heat is exchanged with water 11 in the vessel 5, and heat exchange with the raw material oxygen-containing hydrocarbon 12 is carried out with the oxygen-containing hydrocarbon vaporizer 6.

  As described above, residual heat that has not been used until now and waste heat that has been discarded are used as a heat source, and it is considered that these residual heat and waste heat are recovered as hydrogen. These residual heat and waste heat are not always generated constantly. For example, there may be circumstances such as operating only during the day when the production facility is operating, or conversely operating only at night.

  In order to produce hydrogen by a steam reforming reaction using residual heat or waste heat that is not always generated constantly, the residual heat or waste heat is introduced into a cooled apparatus in a stopped state. In addition, a start-up operation for heating and heating the hydrogen production apparatus is required.

  At this time, if the oxygen-containing hydrocarbon 12 and water 11 which are raw materials are supplied without the temperature of the catalyst used for steam reforming reaching the reaction temperature, problems such as contamination of the catalyst with organic substances occur. It is necessary to heat and raise the temperature of the hydrogen production apparatus by taking a sufficient time until the temperature of the catalyst used for reforming reaches the reaction temperature. On the other hand, if it takes too much time to start up, the generation time of residual heat and waste heat is limited, so there is not enough time to produce hydrogen, the amount of hydrogen production by collecting waste heat is small, hydrogen production facilities There is a concern that it cannot be used effectively.

  As a countermeasure, in the present embodiment, the reforming reactor 1, the mixed gas preheater 2, the steam generator 5, and the oxygen-containing hydrocarbon vaporizer 6 constituting the hydrogen production apparatus are connected by a heat medium circulation line 37. The heat transfer medium is circulated through the heat medium circulation line 37. The heat transfer medium is introduced from the external heat sources 21 and 22 and can be isolated via the heat medium circulation line inlet valve 33 and the heat medium circulation line outlet valve 34. The heat medium circulation line 37 can be isolated from the external heat sources 21 and 22 via the external heat source inlet isolation valve 31 and the external heat source outlet isolation valve 32. The heat medium circulation line 37 is provided with a heat medium circulation line inlet valve 33, a heat medium circulation line outlet valve 34, a circulation pump or blower 35, and a heat medium heater 36. The heat medium circulation line inlet valve 33 and the heat medium circulation line outlet valve 34 are opened, and the circulation pump or blower 35 and the heat medium heater 36 are operated to circulate the heat transfer medium in the heat medium circulation line 37. .

  Next, examples of the hydrogen production apparatus according to this embodiment will be described.

A test apparatus having the configuration shown in this figure was prototyped, and a hydrogen production test was conducted using 350 ° C. exhaust gas from the private power generation facility as an external heat source and dimethyl ether (DME) as an oxygen-containing hydrocarbon. This test apparatus has a hydrogen production flow rate of ³ Nm ³ / h. The in-house power generation equipment installed in connection with the test apparatus was started and stopped every day.

  The temperature condition of the catalyst layer in the reforming reactor 1 for hydrogen production is 300 ° C. When the test equipment is stopped the same day as the private power generation equipment is shut down, the temperature of the entire test equipment gradually decreases at night, and when the equipment is started the next day along with the start of the private power generation equipment. The temperature dropped to about 150 ° C. In this state, when the exhaust gas from the private power generation facility was introduced into the test apparatus and the temperature of the test apparatus was increased, it took about 3 hours for the temperature of the catalyst layer in the reforming reactor 1 to reach 300 ° C. In addition, when starting over the weekend, the temperature of the test apparatus has dropped to about 50 ° C., so it takes about 5 hours for the temperature of the catalyst layer in the reforming reactor to reach 300 ° C. did.

  On the other hand, a hydrogen production test was performed using a test apparatus having a heat medium circulation line 37 that can be isolated from the external heat sources 21 and 22 via the external heat source inlet isolation valve 31 and the external heat source outlet isolation valve 32.

  When starting the test apparatus, the external heat source inlet isolation valve 31 and the external heat source outlet isolation valve 32 shown in FIG. 1 are closed, the heat medium circulation line inlet valve 33 and the heat medium circulation line outlet valve 34 are opened, the circulation blower 35, the heat The medium heater 36 was driven, and the temperature of the test apparatus composed of the reforming reactor 1, the mixed gas preheater 2, the steam generator 5, and the oxygen-containing hydrocarbon vaporizer 6 was raised.

  Under the condition of the heat output of the heat medium heater 36 of 10 kW, the temperature of the catalyst layer in the reforming reactor 1 reached 300 ° C. in about 1 hour. When the cooled apparatus in the stopped state is heated, the temperature is raised and the hydrogen production conditions for starting operation are reached, supply of the heat medium from the external heat source 21 is started. That is, the external heat source inlet isolation valve 31 and the external heat source outlet isolation valve 32 are opened, the heat medium circulation line inlet valve 33 and the heat medium circulation line outlet valve 34 are closed, the circulation blower 35 and the heat medium heater 36 are stopped, Hydrogen could be generated using the exhaust gas from the private power generation facility as the external heat source 21.

Compared with the case where the temperature of the test apparatus is raised using only the exhaust gas from the private power generation facility, the time for raising the temperature to the hydrogen production conditions can be reduced by 2 hours, and more hydrogen can be produced accordingly. In the case of this test apparatus, 3Nm ³ / h × 2h = 6Nm ³ of hydrogen can be produced.

Since the combustion energy of hydrogen is 286 kJ / mol and the volume of 1 mol of gas in a standard state is 0.02241 m ³ / mol, the energy held by 6 Nm ³ of hydrogen is expressed by the following equation (1): E = 7.66 × 10 ⁴ kJ.

E = 286 kJ / mol × [1 / (0.02241 m ³ / mol)] × 6 Nm ³
= 7.66 × 10 ⁴ kJ (1)
The energy E = 7.66 × 10 ⁴ kJ possessed by the generated 6Nm ³ hydrogen is sufficiently larger than the thermal energy 10 kW × 1 h = 3.6 × 10 ⁴ kJ used for the temperature increase of the test apparatus. It was confirmed that this example was effective.

  Note that here, a hydrogen production test was performed using dimethyl ether (DME) as the oxygen-containing hydrocarbon, but methanol can be used as the oxygen-containing hydrocarbon.

  According to the present embodiment, the cooled reforming reactor 1, the mixed gas preheater 2, the steam generator 5, the oxygen-containing hydrocarbon vaporizer 6, and the like in the stopped state are connected to the heat medium circulation line 37. It can be used to preheat by circulating the residual heat and waste heat in the system. When the hydrogen production apparatus reaches the hydrogen production conditions when the temperature rises and starts up, supply of the heat medium from the external heat source 21 is started. Thus, it is possible to efficiently produce hydrogen from waste heat that has been discarded so far and residual heat that has not been effectively used, and the startup time of the hydrogen production apparatus can be shortened. Moreover, the amount of hydrogen production can be increased stably. Further, the product hydrogen purity can be stably improved.

  FIG. 2 is a block diagram showing the configuration of the hydrogen production apparatus according to the second embodiment of the present invention. Parts that are the same as or similar to those in FIG.

  As shown in FIG. 2, in the hydrogen production apparatus according to the present embodiment, between the outlet and the inlet of the reforming reactor 1, it is in parallel with the reforming reactor 1 in order to heat the reforming reactor 1. Thus, a heat medium line 40 is provided. A circulation pump or blower 38 that circulates the heat transfer medium and a heat medium heater 39 that heats the heat transfer medium are installed in the heat medium line 40.

  In the reforming reactor 1, when hydrogen is produced by the steam reforming reaction using the oxygen-containing hydrocarbon 12 as a raw material, the amount of hydrogen produced and the components of the produced gas are determined by the reforming catalyst layer in the reforming reactor 1. This temperature control is important because it is affected by temperature.

  In the present embodiment configured as described above, the temperature of the reforming catalyst layer in the reforming reactor 1 is monitored. When the temperature is lower than the predetermined temperature, the circulation pump installed in parallel with the reforming reactor 1 Alternatively, the temperature of the reforming catalyst layer in the reforming reactor 1 can be maintained at a predetermined temperature by driving the blower 38 and the heat medium heater 39. When the reforming reactor 1 is started and the temperature of the entire apparatus is low, the circulation pump or blower 38 and the heat medium heater 39 are driven to set the temperature of the reforming catalyst layer in the reforming reactor 1. If the heat transfer medium is supplied from the external heat source 21 while maintaining the predetermined temperature, the reforming reactor 1 can be started up in a short time.

  According to the present embodiment, by operating the circulation pump or blower 38 and the heat medium heater 39 that are interposed in the heat medium circulation line 40 provided in parallel with the reforming reactor 1, If the heat transfer medium is supplied from the external heat source 21 while maintaining the temperature of the reforming catalyst layer at a predetermined temperature, the reforming reactor 1 can be started up in a short time. Thus, it is possible to efficiently produce hydrogen from waste heat that has been discarded so far and residual heat that has not been effectively used, and the startup time of the hydrogen production apparatus can be shortened. Moreover, the amount of hydrogen production can be increased stably. Further, the product hydrogen purity can be stably improved.

  In addition, as the external heat source 21, hydrogen can be efficiently produced using heat generated in a power plant, heat generated in a waste incineration facility, or heat generated in other industries. In addition, heat medium generated by heat exchange with heat generated at power plants, heat generated at waste incineration facilities, or heat generated at other industries may be used, or power plants, waste incineration facilities or other industries may be used. Similar effects can be obtained even if waste heat or residual heat generated in the above is utilized.

  The embodiments of the present invention have been described above. However, the present invention is not limited to the embodiments described above, and departs from the gist of the present invention by combining the configurations of the embodiments. Various modifications can be made without departing from the scope.

The block diagram which shows the structure of the hydrogen production apparatus of the 1st Embodiment of this invention. The block diagram which shows the structure of the hydrogen production apparatus of the 2nd Embodiment of this invention.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 ... Reforming reactor, 2 ... Mixed gas preheater, 3 ... Water preheater, 4 ... Oxygen containing hydrocarbon preheater, 5 ... Steam generator, 6 ... Oxygen containing hydrocarbon vaporizer, 7 ... Oxygen containing hydrocarbon -Steam mixer, 11 ... Water, 12 ... Oxygen-containing hydrocarbon, 13 ... Oxygen-containing hydrocarbon / steam gas mixture, 14 ... Preheated oxygen-containing hydrocarbon / steam gas mixture, 15 ... Reformed gas, 16 ... Kai Gas ... 17 ... Steam, 21 ... External heat source, 22 ... External heat source, 31 ... External heat source inlet isolation valve, 32 ... External heat source outlet isolation valve, 33 ... Heat medium circulation line inlet valve, 34 ... Heat medium circulation line outlet valve 35, 38 ... circulation pump or blower, 36, 39 ... heating medium heater, 37, 40 ... heating medium circulation line.

Claims (6)

An oxygen-containing hydrocarbon vaporizer for gasifying the oxygen-containing hydrocarbon as a raw material;
A steam generator for generating steam;
An oxygen-containing hydrocarbon / steam mixer that mixes the vaporized gaseous oxygen-containing hydrocarbon with steam;
A mixed gas preheater for preheating the mixed gas of oxygen-containing hydrocarbon and steam to a predetermined reformer supply temperature;
A reforming reactor including a reaction tube introduced with the mixed gas and filled with a reforming catalyst;
An external heat source for heating the reforming reactor using a heat transfer medium;
Heat that is isolated from the external heat source and connected to at least one vessel selected from the reforming reactor, the mixed gas preheater, the steam generator, and the oxygen-containing hydrocarbon vaporizer and circulated through the heat transfer medium Medium circulation line,
A circulation pump or a circulation blower provided in the heat medium circulation line and circulating the heat transfer medium;
A heat medium heater provided in the heat medium circulation line for heating the heat transfer medium;
The hydrogen production apparatus characterized by having. An oxygen-containing hydrocarbon vaporizer for gasifying the oxygen-containing hydrocarbon as a raw material;
A steam generator for generating steam;
An oxygen-containing hydrocarbon / steam mixer that mixes the vaporized gaseous oxygen-containing hydrocarbon with steam;
A mixed gas preheater for preheating the mixed gas of oxygen-containing hydrocarbon and steam to a predetermined reformer supply temperature;
A reforming reactor including a reaction tube introduced with the mixed gas and filled with a reforming catalyst;
An external heat source for heating the reforming reactor using a heat transfer medium;
A heat medium circulation line that is provided in parallel with the reforming reactor and in which a heat transfer medium for controlling the temperature of the reforming reactor circulates;
A circulation pump or a circulation blower provided in the heat medium circulation line and circulating the heat transfer medium;
A heat medium heater provided in the heat medium circulation line for heating the heat transfer medium;
The hydrogen production apparatus characterized by having.   The hydrogen production apparatus according to claim 1 or 2, wherein the oxygen-containing hydrocarbon is composed of at least one selected from dimethyl ether and methanol.   The hydrogen according to any one of claims 1 to 3, wherein the external heat source uses heat generated in a power plant, heat generated in a waste incineration facility, or heat generated in other industries. Manufacturing equipment.   The external heat source uses a heat medium formed by heat exchange with heat generated in a power plant, heat generated in a waste incineration facility, or heat generated in other industries. The hydrogen production apparatus according to any one of 1 to 3.   The hydrogen production apparatus according to claim 1, wherein the external heat source uses waste heat or residual heat generated in a power plant, a waste incineration facility, or other industries.

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