WO2006080544A1 - 水素発生装置および方法 - Google Patents
水素発生装置および方法 Download PDFInfo
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- WO2006080544A1 WO2006080544A1 PCT/JP2006/301608 JP2006301608W WO2006080544A1 WO 2006080544 A1 WO2006080544 A1 WO 2006080544A1 JP 2006301608 W JP2006301608 W JP 2006301608W WO 2006080544 A1 WO2006080544 A1 WO 2006080544A1
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- gas
- reformer
- heat exchanger
- hydrocarbon
- reforming
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/382—Multi-step processes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
- C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1288—Evaporation of one or more of the different feed components
- C01B2203/1294—Evaporation by heat exchange with hot process stream
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
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- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Definitions
- the present invention is based on hydrogen-using devices such as fuel cells, etc., using as raw materials hydrocarbon gas such as natural gas, propane gas, gasoline, naphtha, kerosene, methanol, biogas and water and air or oxygen.
- hydrocarbon gas such as natural gas, propane gas, gasoline, naphtha, kerosene, methanol, biogas and water and air or oxygen.
- the present invention relates to a hydrogen generating apparatus and method for supplying hydrogen to hydrogen.
- Hydrogen is drawing attention as one of the leading energy sources to replace fossil fuels, but the development of social infrastructure such as hydrogen pipelines is required for its effective use.
- One way is to use natural gas, other fossil fuels, alcohol, etc., and the existing infrastructure for transportation, transportation, etc., and reform these fuels in places that require hydrogen.
- a method to produce hydrogen is being considered.
- Patent Document 1 As such a hydrogen generator as described above, for example, one shown in Patent Document 1 below is disclosed.
- This hydrogen generator introduces a mixed gas of hydrocarbon gas and steam as a raw material into the reformer, and separates and refines the hydrogen gas from the hydrogen-rich reformed gas obtained by the reforming reaction with the catalyst. It is In this hydrogen generator, since the reforming reaction is an endothermic reaction, the reformer is equipped with a burner, and the heat energy required for the reforming reaction is supplied from the outside.
- Patent Document 1 Japanese Patent Application Laid-Open Publication No. 2 0 2 5 3 3 0 7
- the present invention has been made to solve these problems, and it is an object of the present invention to provide a hydrogen generating apparatus and method that are excellent in energy efficiency and can also reduce equipment cost. Means to solve the problem
- a hydrogen generator according to the present invention is a hydrogen generator that reforms a hydrocarbon-based gas to generate a hydrogen-rich reformed gas, and the above hydrocarbon-based gas is converted to oxygen. And a reformer for burning and reforming the hydrocarbon gas by catalytic reaction with the catalyst, and between the reformed gas and the hydrocarbon-based gas in the reforming gas path provided downstream of the reformer. It is essential to provide a first heat exchanger for heating the hydrocarbon gas introduced into the reformer after heat exchange.
- the hydrogen generation method of the present invention is a hydrogen generation method for reforming a hydrocarbon-based gas to generate a hydrogen-rich reformed gas.
- the reforming process performs combustion and reforming of hydrocarbon gas by catalytic reaction with the catalyst, and heat exchange between the reforming gas and the hydrocarbon-based gas is performed downstream of the reforming process to perform the above-described reforming process.
- hydrocarbon gas is burned and reformed by catalytic reaction of the above-mentioned hydrocarbon gas with oxygen and catalyst in the reformer, and the reformed gas path provided on the downstream side of this reformer is Heat exchange between the reformed gas and the source gas is performed to heat the source gas introduced to the reformer.
- the heat energy of the reformed gas is heated by the heat of the reformed gas obtained by performing combustion and reforming instead of supplying the heat energy required for the reforming from the outside by the burner etc. It is extremely energy efficient.
- it is not necessary to provide a heating furnace equipped with a burner around the reformer and the structure of the reformer itself is simplified, and the structure for providing heat resistance and pressure resistance is also simplified. Can also be saved.
- the first heat exchanger heats a mixed gas of hydrocarbon gas and water vapor as a raw material gas
- carbonization requiring relatively large thermal energy for heating is performed. Since the hydrogen gas and the steam are heated by the first heat exchanger and then introduced into the reformer, the raw material gas can be raised to the gas temperature required for the reformer inlet.
- the third heat exchanger which heats the water by performing heat exchange between the reformed gas and water serving as steam on the downstream side of the first heat exchanger of the reformed gas passage, and
- the reformed gas whose temperature has decreased to a certain extent by heat exchange with the source gas in the first heat exchanger is further subjected to the third heat exchange.
- the third heat exchanger By exchanging heat with water, it is possible to further improve energy efficiency.
- the second heat exchanger performs heat exchange between the reformed gas and the hydrocarbon-based gas on the downstream side of the first heat exchanger of the reformed gas passage to heat the hydrocarbon-based gas. If it is equipped with the raw material in the first heat exchanger The energy efficiency can be further improved by further exchanging heat with the hydrocarbon-based gas in the second heat exchanger to further lower the temperature of the reformed gas whose temperature has decreased to some extent by heat exchange with the gas.
- the pressurized vacuum pressure cussing adsorption device when the adsorption device for adsorbing the impurities in the reformed gas is provided, and the adsorption device is a pressurized vacuum pressure swing adsorption device, the pressurized vacuum pressure cussing adsorption device is in a pressurized state. Since the impurities in the reformed gas are adsorbed and the adsorbed impurities are desorbed in the vacuum state, the impurities remaining in the adsorbent after desorption are greater than in the pressure-pressure-swing type adsorption apparatus in which the desorption is performed at atmospheric pressure. It will be significantly reduced.
- the amount of purge gas can be greatly reduced in the product hydrogen gas purge after the completion of desorption, and the amount of purge gas discharged as off gas can be reduced.
- the amount of adsorption of impurities to the adsorbent is increased by performing desorption in a vacuum state, the amount of packing of the adsorbent can be reduced accordingly, so that the amount of purge gas can be further reduced and the amount of off gas can be reduced.
- the amount of adsorption of the adsorbent is not reduced, the amount of impurities adsorbed in one adsorption can be increased. As a result, the pressure cascading cycle is extended and the number of purges per hour is reduced. Can also be reduced.
- the burner for heating the reformer that can burn off the off gas is not provided, the effect of improving the processing efficiency by reducing the amount of off gas is extremely remarkable.
- combustion reaction and reforming reaction of hydrocarbon are simultaneously performed in the same reaction region by using R h modified (N i -C e 0 2 ) —P t catalyst.
- the heat energy generated in the combustion reaction is used as a heat source for the reforming reaction by simultaneously performing the exothermic reaction, the combustion reaction, and the reforming reaction, which is the endothermic reaction, in the same reaction region. It is extremely energy efficient because it can be used.
- thermal neutralization occurs because exothermic reaction and endothermic reaction occur simultaneously.
- FIG. 1 is a view showing an embodiment of a hydrogen generator to which the present invention is applied.
- FIG. 2 is a cross-sectional view showing an embodiment of a reformer to which the present invention is applied.
- FIG. 3 is a cross-sectional view showing a second example of the reformer.
- FIG. 4 is a cross-sectional view showing a third example of the above-mentioned reformer.
- FIG. 1 is a block diagram showing an example of a hydrogen generator to which the present invention is applied.
- This hydrogen generator is a hydrogen generator that reforms a hydrocarbon-based gas to generate hydrogen-rich reformed gas.
- hydrocarbon gas such as natural gas and methane, including hydrocarbon gas which is generally supplied as a social infrastructure like propane gas or city gas. it can.
- natural gas as the hydrocarbon gas is described.
- This hydrogen generation device converts the reformed gas discharged from the reformer 1 into CO by reforming the reformer 1 that reforms the natural gas by introducing natural gas, steam, and oxygen as source gases.
- a CO converter 4 and an adsorption unit 5 for adsorbing impurities in the CO-transformed reformed gas are provided.
- the hydrogen generating apparatus includes: a natural gas supply passage 22 for circulating natural gas supplied to the reformer 1; and water for supplying and circulating water for generating steam to be introduced to the reformer 1
- a supply path 23 and an oxygen supply path 24 for introducing oxygen to the reformer 1 are provided.
- the water supply path 23 is provided with a steam heater 6 for converting the supplied water into water vapor.
- the source gas supply passage 10 is connected to the reformer 1 so that a mixed gas of natural gas, steam and oxygen is introduced into the reformer 1 as a source gas.
- the reformed gas reformed by the reformer 1 flows through the reformed gas passage 25 and is introduced into the CO converter 4, and the reformed gas transformed by the CO converter 4 is a reformed gas. It flows through the channel 26 and is introduced into the adsorption device 5.
- the hydrogen gas from which the impurities are adsorbed and removed by the adsorption device 5 is supplied from the product gas passage 2 9 to a predetermined hydrogen gas using facility.
- the reformer 1 is a unit that performs a catalytic reaction of the natural gas with oxygen and steam with a reforming catalyst to burn and reform the natural gas.
- a reforming catalyst to burn and reform the natural gas.
- R h modified (N i —C e O 2 ) —P t catalyst is used for the above-mentioned reformer 1, and the combustion reaction and the reforming reaction of hydrocarbons are performed by this one type of catalyst. Are performed simultaneously in the same reaction area.
- the reformer 1 has a double structure of an inner cylinder 34 and an outer case 33, and the reforming catalyst 31 is disposed in the inner cylinder 34, In one reaction zone in the inner cylinder 34, combustion reaction and reforming reaction of hydrocarbons are simultaneously performed in the same reaction zone.
- the heat energy generated by the combustion reaction can be used as a heat source for the reforming reaction. Energy efficiency improves. Furthermore, since the exothermic reaction and the endothermic reaction occur simultaneously in the reaction area, thermal neutralization occurs. For example, compared with the case where the catalytic combustion reaction is independently performed in the reformer 1, the reaction area Since the temperature rise of the heat exchanger can be considerably suppressed and the heat resistant material to be used for the reformer 1 can be selected and the heat resistant structure of the reformer 1 itself does not have to be so high temperature specification, the equipment cost can be reduced. The details of the reformer 1 will be described later.
- the reformed gas connecting the reformer 1 and the CO converter 4 downstream of the above reformer 1 The first heat exchanger 3 for heating the source gas introduced into the reformer 1 by heat exchange between the reformed gas and the source gas flowing through the source gas supply path 10 is provided in the path 25. ing.
- the first heat exchanger 3 heats a mixed gas of natural gas and water vapor as a source gas.
- the heat energy required for reforming is not supplied from the outside by a burner or the like, but the raw material to be introduced into the reformer 1 by the heat of the reformed gas obtained by performing combustion and reforming. Because the gas is heated, it is extremely energy efficient. In addition, it is not necessary to provide a heating device with a burner around the reformer 1, and the structure of the reformer 1 itself is simplified, and the structure for providing heat resistance and pressure resistance is also simplified. Can also be saved.
- the hydrocarbon gas and the steam which require relatively large heat energy to heat the mixed gas of the hydrocarbon gas and the steam are heated to the first heat exchanger 3 Since the raw material gas is heated and introduced into the reformer 1, the raw material gas can be raised to the gas temperature required for the inlet of the reformer 1.
- the first heat exchanger 3 is disposed on the upstream side closest to the reformer 1 as compared with other heat exchangers described later. As a result, since the raw material gas that must be heated to the highest temperature immediately before being introduced into the reformer 1 is heated by the first heat exchanger 3 on the most upstream side, the raw material gas is heated to a sufficiently high temperature. It can be introduced into the reformer 1 and the source gas can be raised to the gas temperature required at the inlet of the reformer 1.
- the raw material gas supply passage 10 is provided with a raw material heater 2 for heating the raw material gas introduced into the reformer 1.
- a raw material heater 2 for heating the raw material gas introduced into the reformer 1.
- the heat exchange between the natural gas flowing through the natural gas supply passage 22 and the reformed gas is performed downstream of the first heat exchanger 3 of the reformed gas passage 25 to heat the natural gas.
- 2 Heat exchanger 9 is provided. In this way, the heat of the reformed gas whose temperature has dropped to a certain extent by heat exchange with the source gas in the first heat exchanger 3 is further heat exchanged with the natural gas in the second heat exchanger 9. Energy efficiency can be further improved.
- a third heat exchanger 11 is provided to heat the water by heat exchange with gas.
- the temperature of the reformed gas is lowered to a certain extent by the heat exchange with the raw material gas in the first heat exchanger 3 and the heat exchange with the natural gas by the second heat exchanger 9.
- energy efficiency can be further improved.
- a preheating heater 8 for further preheating the natural gas heated by the second heat exchanger 9 and a preheating heater 8 are provided downstream of the second heat exchanger 9 of the natural gas supply passage 22 described above.
- a desulfurizer 7 is provided to remove sulfur additives from natural gas.
- the desulfurizer 7 is not particularly limited, and may be one that physically adsorbs to an adsorbent, or may be one that performs hydrodesulfurization.
- a steam heater water vapor generating device that uses the water heated by the third heat exchanger 1 1 as a steam downstream of the third heat exchanger 1 1 of the water supply passage 23.
- a natural gas supply passage 2 extending from the tip of the steam supply passage 2 3 a extending from the steam heater 6 and the desulfurizer 7 The tip end of 2 joins the source gas supply path 10 and is connected to the first heat exchanger 3.
- a pure water apparatus 12 for converting the supplied tap water into pure water, and a pure water pump 13 for pumping the pure water discharged from the pure water apparatus 12 to the water supply path 23 Is provided.
- the natural gas supply passage 22 is provided with a compressor 19 for pressure-feeding the natural gas supplied from the supply source.
- the denatured gas passage 26 through which the reformed gas discharged from the CO shift converter 4 is circulated is water that is pumped by the pure water pump 13 and circulated through the water supply passage 23 and the transformed gas passage 26
- a fourth heat exchanger 14 and a fifth heat exchanger 15 are provided to heat the water by heat exchange with the reformed gas flowing therethrough.
- a pure water heater 16 for heating pure water is provided on the downstream side of the fifth heat exchanger 15 and on the upstream side of the fourth heat exchanger 14. Then, the water sent in by the pure water pump 13 is preheated by the fifth heat exchanger 15, the pure water heater 16, the fourth heat exchanger 14, and then the third heat exchanger 1 described above. It will be introduced to 1.
- a sixth heat exchanger 17 is provided which heats the natural gas by heat exchange with the reformed gas flowing through the gas passage 26.
- the natural gas fed by the compressor 19 is preheated by the sixth heat exchanger 17 and then introduced into the second heat exchanger 9.
- the heat of the reformed gas discharged from the CO converter 4 is used to preheat the supplied water and natural gas, thereby further improving the thermal efficiency.
- a gas-liquid separator 18 is provided to separate and remove water vapor remaining in the reformed gas. The water separated and removed by the gas-liquid separator 18 is drained from the drainage channel 27.
- the adsorption apparatus 5 which adsorbs CO and C 0 2 is impurities of the reformed gas.
- the above adsorption device is a pressure swing type adsorption device in which a first adsorption tower 20a and a second adsorption tower 20b, each of which is filled with an adsorbent, exist in parallel. While letting the quality gas flow and adsorb the impurities to the adsorbent, the other adsorption tower is evacuated by a vacuum pump 21 to carry out vacuum desorption to desorb the impurity gas adsorbed on the adsorbent. It is a suction vacuum pressure swing type adsorption device. In the example shown, there are two adsorption towers, but three or more adsorption towers may be used.
- the adsorption device 5 of the pressurized vacuum pressure swing type adsorbs the impurities in the reformed gas in the pressurized state and desorbs the adsorbed impurities in the vacuum state, the desorption is performed at the atmospheric pressure.
- the amount of impurities remaining in the adsorbent after desorption is significantly reduced as compared to the pressure swing type adsorption device performed.
- the amount of purge gas can be greatly reduced in the product hydrogen gas purge after desorption, and the amount of purge gas discharged as off gas can be reduced.
- the amount of adsorption of impurities to the adsorbent can be increased, and the amount of packing of the adsorbent can be reduced accordingly, so the amount of purge gas can be further reduced and the amount of off gas can be reduced. Becomes possible. Furthermore, if the amount of adsorbent loading is not reduced, the amount of impurities adsorbed per adsorption can be increased, thereby extending the pressure swing cycle and reducing the number of purges per hour. The amount of off-gas can also be reduced. In the present invention, since the burner for heating the reformer which can burn off the off gas is not provided, the processing efficiency is improved by reducing the amount of off gas. The effect is very remarkable.
- the reformer 1 reforms the raw material gas introduced from the upstream end and discharges the reformed gas to the downstream end, as shown in FIG.
- the reforming catalyst 31 is disposed inside.
- the upper side of the figure is the upstream side, and the lower side is the downstream side.
- the outer case 33 has a bottomed cylindrical shape, and a disc-like flange 3 6 a is formed so as to project around the periphery of the upper end portion.
- a plate-like flange 36b is disposed on the upper side of the flange 36a, and the flange 36b is disposed so that the cylindrical introduction cylinder 35 is substantially concentric with the outer case. It is done.
- the introduction cylinder 35 is set to have substantially the same diameter as the inner cylinder 3 4 housed inside with a smaller diameter than the outer case 3 3, and is joined and fixed to the flange 3 6 b. It also protrudes upstream.
- the upstream end opening of the introduction cylinder 35 is covered with a flange 36c, and the source gas supply passage 10 is connected to the flange 36c, and natural gas is introduced into the internal space of the introduction cylinder 35
- the source gas which is a mixture of water vapor and oxygen, is supplied.
- a reformed gas passage 25 through which the reformed gas flows is connected to the bottom of the outer case, and the reformed gas passage 25 is provided with a first heat exchanger 3 and a second heat exchanger 9. (The third heat exchanger 11 is not shown).
- a support cylinder 3 8 in which the inner cylinder 34 is fitted is provided so as to protrude in the inward direction.
- a large number of flow holes 3 2 a are formed in the upper portion of the support cylinder 3 8 so that the catalyst 3 1 is placed.
- a medium 32 is provided.
- the inner cylinder 34 is fixed to the outer case 3 3 at the upstream end of the source gas. That is, the upstream end of the inner cylinder 34 is welded, joined and fixed to the downstream end of the introduction cylinder 35. In this state, the catalyst 31 is placed on the catalyst seat 32, and the downstream end of the inner cylinder 34 opposite to the fixed end is inserted so as to be externally fitted to the support cylinder 38. There is.
- the inner cylinder 34, the catalyst seat 32 and the support cylinder 38 are not fixed, and the inner cylinder 34 can slide relative to the catalyst seat 32 and the support cylinder 38. It has become Furthermore, the fixed end of the inner cylinder 34 and the downstream end on the opposite side are not fixed to the outer case 33 with a predetermined gap 40 between the outer case 33 and the lower case.
- a heat insulating material (not shown) is filled in the heat insulating space 37 between the inner cylinder 34 and the outer case 33.
- the outer case 33, the introduction cylinder 35, and the flanges 36a, 36b, and 36c are made of stainless steel having a thickness that can withstand a predetermined pressure in order to have a pressure resistant structure.
- a heat resistant alloy such as Inconel is used for the inner cylinder 34 so as to withstand the high temperature of the reforming reaction.
- the source gas supplied from the source gas supply path 10 is reformed in contact with the catalyst 31 in the inner cylinder 34 to obtain the reformed gas obtained. It passes from the inner cylinder 34 to the circulation hole 32a and the support cylinder 38 and is sent to the reformed gas passage 25.
- an R h modified (N i CC e O 2 ) —P t catalyst is used, and this one type of catalyst can be used to carry out the combustion reaction and the reforming reaction of hydrocarbons.
- the same combustion reaction and reforming reaction of hydrocarbons in one reaction zone of cylinder 34 It takes place simultaneously in the reaction zone.
- the reformer 1 includes an inner cylinder 3 4 having a catalyst disposed therein and reforming the raw material gas introduced from the upstream end to discharge the reformed gas to the downstream end, and the predetermined inner cylinder 3 4 and the inner cylinder 3 4. Since the outer case 3 3 containing the inner cylinder 3 4 is provided with the adiabatic space 3 7 separated, even if the reformed gas flows and the inside of the inner cylinder 3 4 becomes hot, Since the outer case 3 3 is present via the adiabatic space 3 7, the outer case 3 3 does not become so hot compared to the inner cylinder 3 4. Therefore, it is possible to use high temperature resistant materials only for the inner cylinder 34, and to use relatively inexpensive materials such as stainless steel for the outer case 33, significantly reducing the equipment cost. It becomes possible. In addition, the pressure resistance structure of the outer case 33 eliminates the need to consider the pressure resistance of the inner cylinder 34. Therefore, the thickness of the inner cylinder 34 formed of a relatively expensive high-temperature resistant material can be reduced. Equipment cost can be further reduced.
- the inner cylinder 34 is fixed to the outer case 3 3 at the upstream end of the source gas, and the end opposite to the fixed end has a predetermined gap 40 with the outer case 3 3. Since the inner cylinder 34 is not fixed to the outer case 33, the temperature of the inner cylinder 34 becomes high and thermally expands, and a large difference in thermal expansion occurs with the outer case 3 3 whose temperature rise is suppressed. The thermal expansion difference between the inner cylinder 3 4 and the outer case 3 3 is absorbed by the predetermined gap 40 between the outer case 3 3 and the inner cylinder 3 4. Therefore, stress concentration between the high temperature inner cylinder 3 4 and the relatively low temperature outer case 3 3 does not occur, and it is possible to cause the tearing fatigue failure in the repeated start and stop as in the prior art. It will be gone.
- the fixed end of the inner cylinder 34 is the upstream end, it is possible to prevent damage to the joint portion at the fixed end of the inner cylinder 34 in advance. That is, the end opposite to the fixed end of the inner cylinder 34 fixed to the outer case 33 is 200
- the flow of the raw material gas is disturbed in the portion of the predetermined gap 40 between the end and the outer case 33, and vibration is generated in the inner cylinder 34 itself.
- stress is applied to the fixed end, and the joint portion is easily damaged.
- the predetermined gap 40 on the downstream side with the fixed end as the upstream end, the flow of the raw material gas is made smooth and the inner cylinder 3 The vibration of 4 is prevented, and the stress applied to the fixed end is greatly reduced to prevent damage to the joint.
- the support cylinder 38 provided in the outer case 33 is inserted into the inner cylinder 34 at the end opposite to the fixed end of the inner cylinder 34. It functions as a slip prevention member that prevents slippage of the end of the cylinder 34. For this reason, damage to the joint at the fixed end of the inner cylinder 34 can be prevented in advance. That is, if the end opposite to the fixed end of the inner cylinder 34 fixed to the outer case 33 is a free end, the inner cylinder will be exposed when an external force is applied to the reformer 1 itself.
- the inner cylinder 34 is an outer case at either one of the upstream end and the downstream end of the source gas. If it is fixed to 3 3, it is the meaning included in the present invention.
- FIG. 3 is a second example of the reformer 1 to which the present invention is applied.
- the catalyst seat 32 is fixed to the inside of the inner cylinder 34 by welding, and the catalyst 31 is placed.
- the outer case 33 is formed in a cylindrical shape, and the downstream end of the inner cylinder 34 largely opens into the first heat exchanger 3.
- an inward projecting disc-like member 39 is attached to a portion near the downstream end of the outer case 33.
- the disc-like member 39 functions as a slip prevention member.
- the other parts are the same as the first example, and the same reference numerals are given to the same parts.
- the hydrogen generation device described above generates hydrogen, for example, as follows.
- the natural gas supplied as the raw material is compressed by the compressor 19 and circulated through the natural gas supply passage 22, and the sixth heat exchanger 17 changes the circulation through the modified gas passage 26.
- the heat is exchanged with the quality gas and heated, and the second heat exchanger 9 exchanges heat with the reformed gas flowing through the reformed gas passage 25 and is heated.
- the sulfur additive is heated by the preheating heater 8 and the sulfur additive is removed by the desulfurizer 7 and introduced into the raw material gas supply passage 10.
- the tap water supplied as a raw material is made pure water by the pure water device 12 and then pressure-fed by the pure water pump 13 to flow through the water supply path 23.
- the fifth heat exchanger 15 and the fourth heat exchanger 14 exchange heat with the reformed gas flowing through the modified gas passage 26 and heat it, and it is also heated by the pure water heater 16
- the third heat exchanger 11 exchanges heat with the reformed gas flowing through the reformed gas passage 25 and is heated, and is steamed by the steam heater 6 and passes through the steam supply passage 23a to supply the raw material gas Road 10 will be introduced.
- the natural gas and the steam introduced into the source gas supply passage 10 become mixed gas while flowing through the source gas passage, and heat exchange with the reformed gas flowing through the reformed gas passage 25 in the first heat exchanger 3 is performed. And heated.
- the oxygen supplied to the oxygen supply passage 24 is further introduced into the source gas supply passage 10, and a mixed gas of natural gas, steam and oxygen is supplied to the reformer 1 as a source gas.
- the combustion reaction and the reforming reaction of hydrocarbons are carried out in one reaction region in the inner cylinder 34 by the R h modification (N i -C e 0 2 ) —P t catalyst.
- the hydrogen combustion reaction and the reforming reaction occur simultaneously in the same reaction zone.
- the reaction is expressed as a whole by the following equation (1), but in fact, as shown by the equations (2) to (4), It is a sequential reaction that the CO 2 and H 2 O generated in the reaction further cause a reforming reaction with CH 4 and convert it to CO and H 2 .
- CO 2 and 2 H 2 O can also be supplied to the system.
- the supply amount of O 2 can be reduced according to the supply amount of CO 2 and 2 H 2 0.
- the reaction temperature is suitably about 350-800 ° C, preferably about 400-750 ° C.
- the reaction temperature is compensated in part by reaction with CH 4 and 0 2, the shortage will be externally heated.
- the reaction pressure may be normal pressure under which normal pressure is employed.
- composition of the reformed gas obtained by this reforming step is approximately 70% H 2 + 15% CO + 15% C 0 2 on a dry basis, with the balance being impurities.
- This reforming process is an exothermic reaction on the catalyst, and the temperature of the reformed gas at the outlet is about 70 ° C. to 800 ° C.
- the R h modified (N i -C e O 2 ) -P t catalyst has, for example, an appropriate porosity.
- the catalyst is obtained by loading Rh on the surface of the alumina support, followed by loading Pt, and co-loading Ni and CeO 2 .
- the selection of the material and shape of the carrier, the presence or absence of the formation of the coating, and the selection of the material can be carried out various variations.
- Rh is carried out by impregnating an aqueous solution of a water-soluble salt of Rh, followed by drying, calcination, and hydrogen reduction. Further, Pt is supported by impregnating an aqueous solution of a water-soluble salt of Pt, followed by drying, calcination, and hydrogen reduction. Simultaneous loading of N i and C e 0 2 after impregnating a mixed aqueous solution of water-soluble salts of water-soluble salts and C e of N i, drying, calcination is carried out by hydrogen reduction.
- the procedure exemplified above yields the desired R h modified (N i —C e O 2 ) —P t catalyst.
- the composition of each component is a weight ratio.
- R h: N i: C e O 2 : P t (0.05-0.5): (3. 0-1 0. 0): (2. 0-8. 0): (0.
- the hydrogen reduction treatment in each step in the above may be omitted, and in actual use, the catalyst 31 may be used by hydrogen reduction at high temperature. Even when the hydrogen reduction treatment is carried out at each stage, the catalyst 31 can be used after reduction at a high temperature by hydrogen.
- a CO selective oxidizer may be provided on the downstream side of the CO transformer 4 to oxidize the remaining CO after the CO conversion step into CO 2 . That is, CO and O 2 in air are reacted to CO 2 as shown in the following reaction formula.
- the residual CO content will be 10 ppm or less, and the composition of the reformed gas will be approximately 7 7% H 2 + 2 3% C 0 2 + residual impurities, and hydrogen gas for fuel cells etc. It is supplied to the use facilities.
- the hydrogen generating apparatus and method described above are capable of reforming the thermal energy generated by the combustion reaction by simultaneously performing the combustion reaction which is the exothermic reaction and the reforming reaction which is the endothermic reaction in the same reaction region. Because it can be used as a heat source for the reaction, it is extremely energy efficient. Furthermore, since the exothermic reaction and the endothermic reaction occur simultaneously in the reaction area, thermal neutralization occurs. For example, compared with the case where the catalytic combustion reaction is independently performed in the reformer 1, the reaction area Since the temperature rise of the heat exchanger is considerably suppressed and the heat resistant material used for the reformer 1 is not required to have the heat resistant structure of the reformer 1 itself so as to have a high temperature specification, equipment cost can also be saved.
- the outer case 33 exists through the adiabatic space 37, so the inner cylinder 3 4
- the outer case 3 3 does not get so hot compared to. Therefore, it is possible to use high temperature resistant materials only for the inner cylinder 34, and to use relatively inexpensive materials such as stainless steel for the outer case 33, It is possible to significantly reduce the cost.
- the pressure resistance structure of the outer case 33 eliminates the need to consider the pressure resistance of the inner cylinder 34. Therefore, the thickness of the inner cylinder 34 formed of a relatively expensive high-temperature resistant material can be reduced. Equipment cost can be further reduced.
- the temperature difference between the inner cylinder 34 and the outer casing 33 is large even if the temperature of the inner cylinder 34 becomes large due to the thermal expansion of the outer casing 33, the temperature rise is suppressed.
- the thermal expansion difference of the source 33 is absorbed at the predetermined gap 40 between the outer case 3 3 and the inner cylinder 3 4. Therefore, stress concentration between the high temperature inner cylinder 34 and the relatively low temperature outer case 3 3 does not occur, and creep fatigue breakage occurs in the repeated start and stop as in the conventional problem. There is no such thing.
- FIG. 4 is a third example of the reformer 1 to which the present invention is applied.
- reheat so-called “thermal” reforming is carried out, and the combustion reaction of hydrocarbons and the above-mentioned R h modified (N i -C e O 2 ) catalyst or the like are obtained.
- R h modified (N i -C e O 2 ) catalyst or the like are obtained.
- a combustion catalyst 41 is disposed upstream of the source gas as a catalyst, and a reforming catalyst 42 is disposed downstream thereof.
- the thermal energy required for the reforming reaction in the reforming catalyst 42 is compensated by the combustion energy obtained by burning the raw material gas by the combustion catalyst 4 1.
- the fuel gas has the following reaction.
- the reaction at this time is an exothermic reaction, which has the advantage of generating hydrogen required by the fuel cell.
- the steam generated by the reaction of (2) Then, hydrogen is generated by the reforming reaction of the following formula.
- the present invention can be applied not only to hydrogen generators for household fuel cells, but also to hydrogen generators for automobiles, plants and other fuel cells, and for hydrogen gas utilization equipment other than fuel cells.
- the present invention can also be applied to a hydrogen generator for supplying hydrogen gas.
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- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
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- Fuel Cell (AREA)
Description
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KR1020077018208A KR101241848B1 (ko) | 2005-01-28 | 2006-01-25 | 수소 발생 장치 및 방법 |
CN2006800035540A CN101111452B (zh) | 2005-01-28 | 2006-01-25 | 氢产生装置及方法 |
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JP2005020910A JP5165832B2 (ja) | 2005-01-28 | 2005-01-28 | 水素発生装置および方法 |
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KR (1) | KR101241848B1 (ja) |
CN (1) | CN101111452B (ja) |
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JP5400425B2 (ja) * | 2009-03-03 | 2014-01-29 | Jx日鉱日石エネルギー株式会社 | 水素製造装置及び燃料電池システム |
KR101394346B1 (ko) * | 2012-02-29 | 2014-05-14 | 성균관대학교산학협력단 | 수소 생산용 개질부를 구비하는 열광전변환장치 |
KR101487835B1 (ko) | 2014-03-13 | 2015-01-30 | 성균관대학교산학협력단 | 수소 생산용 개질부를 구비하는 열광전변환장치 |
CN104609368B (zh) * | 2015-01-30 | 2016-06-22 | 山东益丰生化环保股份有限公司 | 一种将石油炼厂解析废气转化成制氢工艺原料气的方法 |
CN104609369B (zh) * | 2015-01-30 | 2015-11-18 | 山东益丰生化环保股份有限公司 | 一种将石油炼厂解析废气转化成制氢工艺原料气的方法 |
CN106556668B (zh) * | 2015-09-30 | 2020-07-10 | 中国石油化工股份有限公司 | 移动式烃类蒸汽转化制氢催化剂测试平台及测试方法 |
TWI617508B (zh) * | 2016-11-21 | 2018-03-11 | Huang Heng Xin | 沼氣觸媒熱電共生機及其操作方法 |
JP6944349B2 (ja) * | 2017-11-09 | 2021-10-06 | エア・ウォーター株式会社 | 水素発生装置 |
KR102094646B1 (ko) | 2019-10-14 | 2020-03-30 | 주식회사 트리신 | 수소탈황을 구비한 고효율 스팀 리포밍 수소 제조 장치 |
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JPH05253436A (ja) * | 1992-03-16 | 1993-10-05 | Mitsui Eng & Shipbuild Co Ltd | Ch4を含まないcoガスの製造方法 |
JP2002293510A (ja) * | 2001-03-28 | 2002-10-09 | Osaka Gas Co Ltd | 一酸化炭素転化器 |
JP2003212508A (ja) * | 2002-01-24 | 2003-07-30 | Honda Motor Co Ltd | 改質システムの水供給制御方法 |
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US4909808A (en) * | 1987-10-14 | 1990-03-20 | The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration | Steam reformer with catalytic combustor |
JP2001151502A (ja) * | 1999-11-26 | 2001-06-05 | Daikin Ind Ltd | 燃料改質装置 |
US6485853B1 (en) * | 2000-06-27 | 2002-11-26 | General Motors Corporation | Fuel cell system having thermally integrated, isothermal co-cleansing subsystem |
JP2002050386A (ja) * | 2000-08-04 | 2002-02-15 | Babcock Hitachi Kk | 燃料電池用水素製造装置 |
JP4968984B2 (ja) * | 2001-01-12 | 2012-07-04 | 三洋電機株式会社 | 燃料電池用改質装置 |
JP2002274805A (ja) * | 2001-01-12 | 2002-09-25 | Toyota Motor Corp | 改質原料を冷媒として利用した熱交換器を有する改質器の制御 |
JP2003103171A (ja) * | 2001-09-28 | 2003-04-08 | Nippon Oil Corp | オートサーマルリフォーミング用触媒および方法、水素製造装置ならびに燃料電池システム |
US20030192251A1 (en) * | 2002-04-12 | 2003-10-16 | Edlund David J. | Steam reforming fuel processor |
JP4175921B2 (ja) * | 2003-03-12 | 2008-11-05 | 東京瓦斯株式会社 | 水素製造装置における熱回収システム |
-
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- 2005-01-28 JP JP2005020910A patent/JP5165832B2/ja active Active
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2006
- 2006-01-24 TW TW095102682A patent/TWI394710B/zh active
- 2006-01-25 KR KR1020077018208A patent/KR101241848B1/ko active IP Right Grant
- 2006-01-25 CN CN2006800035540A patent/CN101111452B/zh active Active
- 2006-01-25 WO PCT/JP2006/301608 patent/WO2006080544A1/ja not_active Application Discontinuation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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JPH05253436A (ja) * | 1992-03-16 | 1993-10-05 | Mitsui Eng & Shipbuild Co Ltd | Ch4を含まないcoガスの製造方法 |
JP2002293510A (ja) * | 2001-03-28 | 2002-10-09 | Osaka Gas Co Ltd | 一酸化炭素転化器 |
JP2003212508A (ja) * | 2002-01-24 | 2003-07-30 | Honda Motor Co Ltd | 改質システムの水供給制御方法 |
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JP5165832B2 (ja) | 2013-03-21 |
KR20070099644A (ko) | 2007-10-09 |
CN101111452B (zh) | 2012-09-05 |
TW200633926A (en) | 2006-10-01 |
KR101241848B1 (ko) | 2013-03-11 |
CN101111452A (zh) | 2008-01-23 |
TWI394710B (zh) | 2013-05-01 |
JP2006206382A (ja) | 2006-08-10 |
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