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KR20120084062A - Reformer for fuel cell with excellent effect of heat exchange - Google Patents

Reformer for fuel cell with excellent effect of heat exchange Download PDF

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KR20120084062A
KR20120084062A KR1020110005363A KR20110005363A KR20120084062A KR 20120084062 A KR20120084062 A KR 20120084062A KR 1020110005363 A KR1020110005363 A KR 1020110005363A KR 20110005363 A KR20110005363 A KR 20110005363A KR 20120084062 A KR20120084062 A KR 20120084062A
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heat exchange
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KR101240849B1 (en
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박정주
전유택
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현대하이스코 주식회사
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
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    • 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
    • C01B3/48—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 followed by reaction of water vapour with carbon monoxide
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    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
    • H01M8/04022—Heating by combustion
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0668—Removal of carbon monoxide or carbon dioxide
    • 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
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/044—Selective oxidation of carbon monoxide
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • 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
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • 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
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

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Abstract

원통형의 컴팩트한 구조를 가지면서 열교환 효과가 우수한 연료전지용 개질기에 대하여 개시한다.
본 발명에 따른 연료전지용 개질기는 중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부, CO제거부 및 ㄷ제3열교환부가 순차적으로 형성되어 있는 원통형 구조를 가지되, 상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 반응 물이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하는 것을 특징으로 한다. Disclosed is a fuel cell reformer having a cylindrical compact structure and excellent in heat exchange effect.
The reformer for a fuel cell according to the present invention includes a burner part, a high temperature reformer, a first heat exchange part, a first heat insulation part, a CO denaturation part, a second heat exchange part, a second heat insulation part, a CO removal part, and a third heat exchange part sequentially from the center. It has a cylindrical structure formed in the burner portion, the fuel and oxygen is oxidized reaction in the burner unit to generate heat to transfer to the high temperature reforming unit, the high temperature reforming unit reacts with the hydrocarbon-based fuel introduced from the first heat exchange unit The water is catalytically reacted at a first temperature by the heat transferred from the burner unit, and in the CO-denatured unit, CO generated from the high temperature reforming unit and the remaining reactant are catalytically reacted at a second temperature lower than the first temperature. In the CO removal unit, the CO and oxygen remaining in the CO modifying unit are catalytically reacted at a third temperature lower than the second temperature.

Description

열교환 효과가 우수한 연료전지용 개질기 {REFORMER FOR FUEL CELL WITH EXCELLENT EFFECT OF HEAT EXCHANGE}Reformer for fuel cell with excellent heat exchange effect {REFORMER FOR FUEL CELL WITH EXCELLENT EFFECT OF HEAT EXCHANGE}

본 발명은 연료전지용 개질기에 관한 것으로서, 보다 상세하게는 원통형 구조를 가지면서 열교환 효과가 우수하여 개질 효율을 높일 수 있는 연료전지용 개질기에 관한 것이다.
The present invention relates to a fuel cell reformer, and more particularly, to a fuel cell reformer having a cylindrical structure and having an excellent heat exchange effect, thereby improving reforming efficiency.

연료전지에 수소를 공급하기 위한 개질기는 천연가스(NG)와 같은 탄화수소계(hydrocarbon) 연료를 수소(H2)로 개질(reforming)한다. 이를 위하여, 개질기는 메탄(CH4) 등과 같은 탄화수소계 연료와 반응 물(Process H2O)이 반응하여 다량의 수소로 개질하는 고온 개질부와, 고온개질에 의하여 불가피하게 생성되는 CO를 변성시키는 CO변성부와, CO변성 이후 잔류하는 CO를 제거하는 CO제거부를 포함한다. A reformer for supplying hydrogen to a fuel cell reforms a hydrocarbon fuel such as natural gas (NG) to hydrogen (H 2 ). To this end, the reformer is a high temperature reforming unit for reacting hydrocarbon-based fuels such as methane (CH 4 ) and the like (Process H 2 O) to reform with a large amount of hydrogen, and to modify the CO inevitably generated by the high temperature reforming. CO modification portion, and CO removal portion for removing the CO remaining after the CO modification.

이들 고온개질부, CO변성부 및 CO제거부에서의 반응은 각각 촉매 반응으로, 개질기가 정상적으로 구동하기 위해서는 개질기를 구성하는 각 단위 반응기의 온도가 각 부분에 포함되는 촉매의 활성 온도에 맞추어져야 한다. The reactions in the high temperature reformer, the CO denaturation unit, and the CO removal unit are catalyzed reactions, respectively. In order for the reformer to operate normally, the temperature of each unit reactor constituting the reformer must be adjusted to the active temperature of the catalyst included in each part. .

또한, 개질기의 각 단위 반응기 촉매부에 반응 물이 기화된 상태로 공급되어야 한다. 그 이유는 촉매부에 액체 상태의 물이 접촉하면 촉매의 성능이 저하될 수 있다.
In addition, the reactants must be supplied in a vaporized state to each unit reactor catalyst part of the reformer. The reason for this is that when the water in the liquid state comes into contact with the catalyst, the performance of the catalyst may be reduced.

본 발명의 목적은 일체형의 원통형 구조를 가지면서 열교환 효과가 우수한 연료전지용 개질기를 제공하는 것이다.An object of the present invention is to provide a reformer for a fuel cell having an integral cylindrical structure and excellent in heat exchange effect.

또한, 본 발명은 물의 예열이 충분히 이루어질 수 있으며, 각 단위 촉매 반응의 온도를 쉽게 유지할 수 있는 연료전지용 개질기를 제공하는 것을 그 목적으로 한다.
In addition, an object of the present invention is to provide a reformer for a fuel cell that can be sufficiently preheated of water, and can easily maintain the temperature of each unit catalytic reaction.

상기 목적을 달성하기 위한 본 발명의 실시예에 따른 연료전지용 개질기는 중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부 및 CO제거부가 순차적으로 형성되어 있는 원통형 구조를 가지되, 상기 CO변성부 하부에는 CO변성부 하부 열교환부가 형성되어 있으며, 상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 기화된 상태의 반응 물(Process H2O)이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하며, 외부에서 공급되는 물이 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO변성부, CO변성부 하부 열교환부, 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되는 것을 특징으로 한다.
The reformer for a fuel cell according to an embodiment of the present invention for achieving the above object is a burner part, a high temperature reforming part, a first heat exchange part, a first heat insulating part, a CO modifying part, a second heat exchange part, a second heat insulating part, and the like from the center. The CO removal unit has a cylindrical structure that is formed sequentially, the lower portion of the CO modified portion is formed under the CO modified portion heat exchanger, the burner portion is fuel and oxygen is oxidized to generate heat to transfer to the high temperature reforming unit. In the high temperature reforming unit, the hydrocarbon-based fuel introduced from the first heat exchange unit and the reactant in a vaporized state (Process H 2 O) are catalytically reacted at a first temperature by the heat transferred from the burner unit, and the CO In the modified portion, the CO generated in the high temperature reforming portion and the remaining reactant are catalytically reacted at a second temperature lower than the first temperature, and in the CO removal portion, The flow is catalyzed by CO and oxygen at a third temperature lower than the second temperature, and water supplied from outside is exchanged in the second heat exchange part and the first heat exchange part in the CO modifying part, the CO modifying part, and the lower heat exchange part, And it is characterized in that the high temperature reforming unit is introduced into the reaction water in the high temperature reforming unit in a vaporized state through sequential heat exchange.

상기 목적을 달성하기 위한 본 발명의 다른 실시예에 따른 연료전지용 개질기는 중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부, CO제거부 및 제3열교환부가 순차적으로 형성되어 있는 원통형 구조를 가지되, 상기 CO변성부 하부에는 CO변성부 하부 열교환부가 형성되어 있으며, 상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 반응 물이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하며, 외부에서 공급되는 물이 상기 제3열교환부, 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO제거부, 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되는 것을 특징으로 한다.
The reformer for a fuel cell according to another embodiment of the present invention for achieving the above object is a burner part, a high temperature reforming part, a first heat exchange part, a first heat insulating part, a CO modification part, a second heat exchange part, a second heat insulating part from the center. , The CO removal part and the third heat exchange part has a cylindrical structure formed sequentially, the CO heat exchanger lower heat exchanger is formed below the CO modification, the burner unit is the heat generated by the oxidation reaction of fuel and oxygen And the hydrocarbon-based fuel and reactants introduced from the first heat exchange unit are catalytically reacted at a first temperature by the heat transferred from the burner unit, and the CO-modified unit is used for the high temperature reforming unit. CO generated in the high temperature reforming unit and the remaining reactant are catalytically reacted at a second temperature lower than the first temperature, and in the CO removal unit, CO and oxygen are catalytically reacted at a third temperature lower than the second temperature, and water supplied from the outside is removed from the third heat exchange part, the second heat exchange part, and the first heat exchange part by the CO removal part and the CO modification. Part, characterized in that it is introduced into the high temperature reforming unit as a reactant in a vaporized state through the heat exchange unit and the heat exchanger and the lower portion of the CO modification portion sequential heat exchange.

상기 목적을 달성하기 위한 본 발명의 또 다른 실시예에 따른 연료전지용 개질기는 중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부, CO제거부 및 제3열교환부가 순차적으로 형성되어 있는 원통형 구조를 가지되, 상기 CO변성부 하부에는 CO변성부 하부 열교환부가 형성되어 있으며, 상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 반응 물이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하며, 외부에서 공급되는 물의 양이 상대적으로 많을 경우, 상기 물은 상기 제3열교환부로 공급되어, 상기 제3열교환부, 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO제거부, 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되고, 외부에서 공급되는 물의 양이 상대적으로 적을 경우, 상기 물은 상기 제2열교환부로 공급되어, 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되는 것을 특징으로 한다.
A reformer for a fuel cell according to another embodiment of the present invention for achieving the above object is a burner part, a high temperature reforming part, a first heat exchange part, a first heat insulating part, a CO modification part, a second heat exchange part, a second heat insulating part from the center. Part, a CO remover and a third heat exchanger having a cylindrical structure sequentially formed, the CO-denatured lower portion is formed under the heat exchanger CO-modified portion, the burner portion in the fuel and oxygen is oxidized reaction heat Generated and delivered to the high temperature reforming unit, wherein the hydrocarbon-based fuel and reactant introduced from the first heat exchange unit are catalytically reacted at a first temperature by the heat transferred from the burner unit, and in the CO modified unit, The CO generated in the high temperature reforming unit and the remaining reactant are catalytically reacted at a second temperature lower than the first temperature, and in the CO removal unit, the CO reactant remains in the CO modifying unit. Is catalytically reacted at a third temperature at which CO and oxygen are lower than the second temperature, and when the amount of water supplied from the outside is relatively large, the water is supplied to the third heat exchange part to supply the third heat exchange part and the third heat exchange part. In the heat exchange unit and the first heat exchange unit, the CO removal unit, the CO modification unit, the CO modification unit, the lower heat exchange unit, and the high temperature reforming unit in a vaporized state through sequential heat exchange with the high temperature reforming unit, When the amount of water supplied from the outside is relatively small, the water is supplied to the second heat exchange part, so that the CO-modified part, the CO-denatured bottom heat exchange part, and the high temperature are supplied from the second heat exchange part and the first heat exchange part. Characterized in that the high temperature reforming unit is introduced into the reaction water in a vaporized state through a sequential heat exchange with the reforming unit.

본 발명에 따른 연료전지용 개질기는 원통형의 컴팩트한 구조로서, 중앙의 버너부로부터 발생되는 열이 바깥쪽의 고온 개질부로 쉽게 전달될 수 있다. 따라서, 본 발명에 따른 연료전지용 개질기는 열교환 효과가 우수하여 열 손실을 방지할 수 있으며, 이에 따라 개질 효율이 상승할 수 있다. The reformer for a fuel cell according to the present invention has a cylindrical compact structure, and heat generated from a central burner portion can be easily transferred to an outer high temperature reformer. Therefore, the reformer for a fuel cell according to the present invention can prevent heat loss due to the excellent heat exchange effect, thereby improving the reforming efficiency.

또한, 본 발명에 따른 연료전지용 개질기는 외부로부터 공급되는 물이 CO 제거부 또는 CO변성부와의 열교환을 통하여 미리 예열됨으로써 CO제거부 또는 CO변성부의 온도 상승을 방지할 수 있다. 따라서, 발열반응이 이루어지는 CO제거부 및 CO변성부의 촉매 활성화 온도를 계속해서 유지할 수 있는 장점이 있다. In addition, the reformer for a fuel cell according to the present invention may prevent the temperature increase of the CO removal unit or the CO modification unit by preheating the water supplied from the outside through heat exchange with the CO removal unit or the CO modification unit. Therefore, there is an advantage that can continuously maintain the catalyst activation temperature of the CO removal unit and the CO-modified unit in which the exothermic reaction takes place.

또한, 본 발명에 따른 연료전지용 개질기는 연료전지에서 요구되는 전기 생산량에 따라 물의 공급 위치를 조절할 수 있어 연료전지의 구동 효율을 높일 수 있는 장점이 있다.
In addition, the reformer for a fuel cell according to the present invention has an advantage of increasing the driving efficiency of the fuel cell by adjusting the supply position of water according to the amount of electricity required by the fuel cell.

도 1은 본 발명의 실시예에 따른 연료전지용 개질기의 단면도를 나타낸 것으로서, 제2열교환부로 물이 공급되는 예를 나타낸 것이다.
도 2는 본 발명의 다른 실시예에 따른 연료전지용 개질기의 단면도를 나타낸 것으로서, 제3열교환부로 물이 공급되는 예를 나타낸 것이다.
도 3은 본 발명의 또 다른 실시예에 따른 연료전지용 개질기의 단면도를 나타낸 것으로서, 물의 공급량에 따라 제2열교환부 혹은 제3열교환부로 물이 공급되는 예를 나타낸 것이다. 1 is a cross-sectional view of a reformer for a fuel cell according to an exemplary embodiment of the present invention, and illustrates an example in which water is supplied to a second heat exchanger.
Figure 2 shows a cross-sectional view of a reformer for a fuel cell according to another embodiment of the present invention, showing an example in which water is supplied to the third heat exchange unit.
Figure 3 shows a cross-sectional view of a reformer for a fuel cell according to another embodiment of the present invention, showing an example in which water is supplied to the second heat exchange unit or the third heat exchange unit in accordance with the supply amount of water.

본 발명의 이점 및 특징, 그리고 그것들을 달성하는 방법은 상세하게 후술되어 있는 실시예들 및 도면을 참조하면 명확해질 것이다. BRIEF DESCRIPTION OF THE DRAWINGS The advantages and features of the present invention, and how to accomplish them, will become apparent with reference to the embodiments and drawings described in detail below.

그러나, 본 발명은 이하에서 개시되는 실시예들에 한정되는 것이 아니라 서로 다른 다양한 형태로 구현될 수 있으며, 단지 본 실시예들은 본 발명의 개시가 완전하도록 하며, 본 발명이 속하는 기술분야에서 통상의 지식을 가진 자에게 발명의 범주를 완전하게 알려주기 위해 제공되는 것이며, 본 발명은 청구항의 범주에 의해 정의될 뿐이다.However, it is to be understood that the present invention is not limited to the disclosed embodiments, but may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. It is intended that the disclosure of the present invention be limited only by the terms of the appended claims.

이하에서는, 본 발명에 따른 열교환 효과가 우수한 연료전지용 개질기 에 대하여 상세히 설명한다.
Hereinafter, a reformer for a fuel cell having excellent heat exchange effect according to the present invention will be described in detail.

도 1은 본 발명의 실시예에 따른 연료전지용 개질기의 단면도를 나타낸 것으로서, 제2열교환부로 물이 공급되는 예를 나타낸 것이다. 1 is a cross-sectional view of a reformer for a fuel cell according to an exemplary embodiment of the present invention, and illustrates an example in which water is supplied to a second heat exchanger.

도 1을 참조하면, 도시된 연료전지용 개질기는 중앙으로부터 버너부(101), 고온 개질부(110), 제1열교환부(141), 제1단열부(151), CO변성부(120), 제2열교환부(142), 제2단열부(152) 및 CO제거부(130)가 순차적으로 형성되어 있는 원통형 구조를 가진다.
Referring to FIG. 1, the fuel cell reformer illustrated includes a burner unit 101, a high temperature reformer 110, a first heat exchanger 141, a first insulation unit 151, a CO modified unit 120, The second heat exchange part 142, the second heat insulating part 152, and the CO removal part 130 have a cylindrical structure sequentially formed.

버너부(101)는 연료와 산소가 산화 반응하여 열을 발생시켜, 고온 개질부(110)에서 이루어지는 고온 개질 반응에 필요한 대략 700℃ 정도의 제1온도를 제공한다. The burner unit 101 generates heat by oxidizing the fuel and oxygen, thereby providing a first temperature of about 700 ° C. required for the high temperature reforming reaction of the high temperature reforming unit 110.

고온 개질부(110)는 버너부(101) 외측에 형성된다. 고온 개질부(110)는 외측의 제1열교환부(141)로부터 투입되는 탄화수소계 연료(NG)와 기화된 상태의 반응 물(Process H2O)이 700 ~ 750℃ 정도의 제1온도에서 촉매 반응하여 수소를 생성한다.The high temperature reforming unit 110 is formed outside the burner unit 101. The high temperature reforming unit 110 is a hydrocarbon-based fuel (NG) introduced from the outer first heat exchange unit 141 and the reaction product (Process H 2 O) in the vaporized state of the catalyst at a first temperature of about 700 ~ 750 ℃ React to produce hydrogen.

예를 들어, 탄화수소계 원료(NG)가 메탄(CH4)이라고 하면, 메탄이 촉매(catalyst)를 통하여 과량의 반응 물과 반응하여, 부피%로 대략 70% 정도의 수소(H2)를 생성한다. 이때, 대략 10% 정도의 CO가 함께 생성된다.For example, if the hydrocarbon-based raw material (NG) is methane (CH 4 ), the methane reacts with an excess of reactant through a catalyst to generate approximately 70% of hydrogen (H 2 ) by volume. do. At this time, approximately 10% of CO is generated together.

본 발명의 경우, 원통형 개질기의 중앙 부분에 구비되는 버너부(101)로부터 발생되는 열이 버너부(101) 바깥쪽에 인접한 고온 개질부(110)로 쉽게 전달될 수 있어서, 열 손실을 최소화할 수 있다.
In the case of the present invention, the heat generated from the burner portion 101 provided in the central portion of the cylindrical reformer can be easily transferred to the high temperature reforming portion 110 adjacent to the burner portion 101 outside, thereby minimizing heat loss. have.

제1열교환부(141)는 고온 개질부(110) 외측에 형성된다. 제1열교환부(141)에는 탄화수소계 연료(NG)와 기체 상태의 물(H2O(g))이 투입된다. 또한, 제1열교환부(141)에 공급된 물은 고온 개질부(110)와 열교환을 통하여 고온 기화된 상태가 된다. The first heat exchange part 141 is formed outside the high temperature reforming part 110. The hydrocarbon-based fuel NG and gaseous water H 2 O (g) are introduced into the first heat exchanger 141. In addition, the water supplied to the first heat exchanger 141 is in a high temperature vaporized state through heat exchange with the high temperature reformer 110.

제1단열부(151)는 제1열교환부(141) 외측에 형성된다. 제1단열부(151)는 제1열교환부(141)와 CO변성부(120)의 열교환을 차단하여, CO변성부(120)의 온도가 CO변성부(120) 내 촉매의 활성화 온도보다 상승하는 것을 방지한다.
The first heat insulating part 151 is formed outside the first heat exchange part 141. The first heat insulating part 151 blocks the heat exchange between the first heat exchange part 141 and the CO modifying part 120 so that the temperature of the CO modifying part 120 rises above the activation temperature of the catalyst in the CO modifying part 120. Prevent it.

CO변성부(120)는 제1단열부(151) 외측에 형성된다. CO변성부(120)에서는 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기의 제1온도보다 낮은 200 ~ 250℃ 정도의 제2온도에서 다음과 같은 촉매 반응하여, 고온 개질 반응에 의하여 불가피하게 발생하는 CO(일산화탄소)을 변성시킨다. The CO modification part 120 is formed outside the first insulation part 151. In the CO modifying unit 120, the CO generated from the high temperature reforming unit and the remaining reactant are catalytically reacted as follows at a second temperature of about 200 to 250 ° C. lower than the first temperature, thereby making it unavoidable by the high temperature reforming reaction. To denature carbon monoxide (CO).

CO변성부 : CO + H2O → H2 +CO2 CO modified part: CO + H 2 O → H 2 + CO 2

CO변성부(120)에서의 반응온도인 제2온도는 고온 개질부(110)의 결과물에 해당하는 가스들이 제1열교환부(141)의 물과 열교환에 의하여 온도가 하강함으로써 확보될 수 있다. 또한, CO변성부 하부 열교환부(121)에 의하여 고온 개질부의 가스는 액상의 물과 열교환하여 상기 CO변성부의 촉매층 활성 온도에 확실하게 맞출 수 있다.
The second temperature, which is the reaction temperature in the CO modifying unit 120, may be ensured by reducing the temperature of the gases corresponding to the result of the high temperature reforming unit 110 by heat exchange with water of the first heat exchanger 141. In addition, the gas of the high-temperature reforming unit may be heat-exchanged with the liquid water by the CO-modifying unit lower heat exchanger 121 to reliably match the catalyst layer active temperature of the CO-modifying unit.

제2열교환부(142)는 CO변성부(120) 외측에 형성된다. 본 실시예에서는 외부의 물이 제2열교환부(142)를 통하여 공급된다. 제2열교환부(142)에 공급된 물은 CO변성부(120), CO변성부 하부 열교환부(121)와 열교환을 통하여 미리 예열된다. The second heat exchange part 142 is formed outside the CO modification part 120. In the present embodiment, external water is supplied through the second heat exchanger 142. The water supplied to the second heat exchange part 142 is preheated in advance through heat exchange with the CO modifying part 120 and the CO modifying part lower heat exchange part 121.

이에 따라, 본 실시예에서는 외부에서 공급되는 물이 제2열교환부(142) 및 제1열교환부(141)에서 CO변성부(120), CO변성부 하부 열교환부(121) 및 고온 개질부(110)와 순차적인 열교환을 통하여 기화된 상태로 고온 개질부(110)에 반응 물로 투입된다. Accordingly, in the present embodiment, the water supplied from the outside is CO-modified part 120, CO-modified part lower heat exchanger 121, and high-temperature reforming part in the second heat exchange part 142 and the first heat exchange part 141. 110 is introduced into the hot reformer 110 as a reactant in a vaporized state through sequential heat exchange.

한편, CO변성부(120)에서의 반응은 발열 반응이므로, CO변성부(120)의 온도가 촉매 활성화 온도 이상으로 상승할 수 있다. 그러나, 상기의 제2열교환부(142)에 공급된 물과 CO변성부(120)의 열교환에 의하여 CO변성부(120)의 온도 상승이 방지될 수 있다.
On the other hand, since the reaction in the CO modifying unit 120 is an exothermic reaction, the temperature of the CO modifying unit 120 may rise above the catalyst activation temperature. However, the temperature rise of the CO-modified part 120 may be prevented by heat exchange between the water supplied to the second heat exchange part 142 and the CO-modified part 120.

제2단열부(152)는 제2열교환부(142) 외측에 형성된다. 제2단열부(152)는 제2열교환부(142)와 CO제거부(130)의 열교환을 차단하여, CO제거부(130)의 온도가 CO제거부(130) 내 촉매의 활성화 온도보다 상승하는 것을 방지한다. The second heat insulating part 152 is formed outside the second heat exchange part 142. The second heat insulating part 152 blocks heat exchange between the second heat exchange part 142 and the CO removing part 130, so that the temperature of the CO removing part 130 rises above the activation temperature of the catalyst in the CO removing part 130. Prevent it.

한편, 버너부(101) 운전에 의해 생성되는 버너 폐가스가 배출되도록, 제2열교환부(142) 외측에는 버너 폐가스부(160)가 형성될 수 있다. 이 경우, 제2단열부(152)는 버너 폐가스부(160) 외측에 형성되며, 버너 폐가스부(160)와 CO제거부(130)의 열교환을 차단한다. Meanwhile, the burner waste gas unit 160 may be formed outside the second heat exchange unit 142 so that the burner waste gas generated by the burner unit 101 operation is discharged. In this case, the second insulation unit 152 is formed outside the burner waste gas unit 160 and blocks heat exchange between the burner waste gas unit 160 and the CO removal unit 130.

또한, 제2열교환부(142)에 공급되는 물은 CO변성부(120), CO변성부 하부 열교환부(121) 외에 버너 폐가스부(160)와도 열교환하면서 예열된다.
In addition, the water supplied to the second heat exchange part 142 is preheated while heat-exchanging with the burner waste gas part 160 in addition to the CO modification part 120 and the CO modification part lower heat exchange part 121.

CO제거부(130)는 제2단열부(152) 외측에 형성된다. CO제거부(130)에서는 CO 변성부(120)에서의 CO 변성 반응 후에 잔류하는 CO와 산소가 제2온도보다 낮은 100 ~ 140℃ 정도의 제3온도에서 다음과 같은 촉매 반응하여, CO의 농도를 ppm 단위로 낮춘다. The CO removal unit 130 is formed outside the second insulation unit 152. In the CO removal unit 130, the CO and oxygen remaining after the CO modification reaction in the CO modification unit 120 are catalytically reacted as follows at a third temperature of about 100 to 140 ° C. lower than the second temperature, thereby providing a concentration of CO. Lower in ppm.

CO제거부 : CO + 1/2O2 → CO2 CO removal part: CO + 1 / 2O 2 → CO 2

CO제거부(130)에서의 반응온도인 제3온도는 CO변성부(120)의 결과물에 해당하는 가스들이 제2열교환부(142)의 물과 열교환에 의하여 온도가 하강함으로써 확보될 수 있다.
The third temperature, which is the reaction temperature in the CO removal unit 130, may be secured by reducing the temperatures of the gases corresponding to the result of the CO modification unit 120 by heat exchange with water of the second heat exchange unit 142.

도 2는 본 발명의 다른 실시예에 따른 연료전지용 개질기의 단면도를 나타낸 것으로서, 제3열교환부로 물이 공급되는 예를 나타낸 것이다. Figure 2 shows a cross-sectional view of a reformer for a fuel cell according to another embodiment of the present invention, showing an example in which water is supplied to the third heat exchange unit.

도 2를 참조하면, 도시된 연료전지용 개질기는 중앙으로부터 버너부(101), 고온 개질부(110), 제1열교환부(141), 제1단열부(151), CO변성부(120), 제2열교환부(142), 제2단열부(152), CO제거부(130) 및 제3열교환부(143)가 순차적으로 형성되어 있는 원통형 구조로 이루어진다. 또한, 상기 CO변성부(120) 하부에는 CO변성부 하부 열교환부(121)가 형성되어 있다. 또한, 제2열교환부(142)의 외측에는 버너 폐가스부(160)가 형성될 수 있다.
Referring to FIG. 2, the reformer for a fuel cell illustrated includes a burner unit 101, a high temperature reformer 110, a first heat exchange unit 141, a first insulation unit 151, a CO modification unit 120, The second heat exchange part 142, the second heat insulation part 152, the CO removal part 130, and the third heat exchange part 143 are formed in a cylindrical structure sequentially formed. In addition, a CO heat exchanger lower heat exchanger 121 is formed under the CO modifying unit 120. In addition, a burner waste gas unit 160 may be formed outside the second heat exchange unit 142.

버너부(101)에서는 연료와 산소가 산화 반응하여 열을 발생시켜 고온 개질부(110)로 전달한다. 고온 개질부(110)에서는 제1열교환부(141)로부터 투입되는 탄화수소계 연료와 기화된 상태의 반응 물이 버너부(101)에서 전달된 열에 의하여 700 ~ 750℃ 정도의 제1온도에서 촉매 반응한다. In the burner unit 101, fuel and oxygen are oxidized to generate heat and are transferred to the high temperature reformer 110. In the high temperature reforming unit 110, the hydrocarbon-based fuel introduced from the first heat exchange unit 141 and the reactant in a vaporized state are catalyzed at a first temperature of about 700 to 750 ° C. by the heat transferred from the burner unit 101. do.

CO변성부(120)에서는 고온 개질부(110)에서 발생되는 CO와 잔류하는 반응 물이 200 ~ 250℃ 정도의 제2온도에서 촉매 반응한다. CO제거부(130)에서는 CO변성부(120)에서 잔류하는 CO와 산소가 100 ~ 140℃ 정도의 제3온도에서 촉매 반응한다.
In the CO modifying unit 120, the CO generated from the high temperature reforming unit 110 and the remaining reactant are catalytically reacted at a second temperature of about 200 to 250 ° C. In the CO removal unit 130, the CO and oxygen remaining in the CO modification unit 120 are catalytically reacted at a third temperature of about 100 to 140 ° C.

본 실시예에서는 외부의 물이 CO제거부(130) 외측에 형성되는 제3열교환부(143)를 통하여 개질기 내부로 공급된다. 그 결과, 외부에서 공급되는 물은 제3열교환부(143), 제2열교환부(142) 및 제1열교환부(141)에서 CO제거부(130), CO변성부(120), CO변성부 하부 열교환부(121) 및 고온 개질부(110)와 순차적인 열교환을 통하여 기화된 상태로 고온 개질부(110)에 반응 물로 투입된다. 또한, 제2열교환부(142) 외측에 버너 폐가스부(160)가 형성되는 경우, 제2열교환부(142)에 공급되는 물은 CO변성부(120), CO변성부 하부 열교환부(121)와의 열교환 뿐만 아니라, 버너 폐가스부(160)와의 추가적인 열교환에 의하여 예열될 수 있다. In the present embodiment, external water is supplied into the reformer through the third heat exchanger 143 formed outside the CO remover 130. As a result, the water supplied from the outside is removed from the third heat exchanger 143, the second heat exchanger 142 and the first heat exchanger 141, the CO removal unit 130, CO denaturation unit 120, CO modification unit The lower heat exchanger 121 and the high temperature reformer 110 are introduced into the hot reformer 110 as a reactant in a vaporized state through sequential heat exchange. In addition, when the burner waste gas unit 160 is formed outside the second heat exchange unit 142, the water supplied to the second heat exchange unit 142 is CO-modified unit 120 and CO-denatured unit lower heat exchanger 121. In addition to heat exchange with the burner, it may be preheated by additional heat exchange with the burner waste gas unit 160.

통상, 기화된 상태의 반응 물의 온도가 높을 수록 고온 개질부(110)에서의 개질 효율이 향상되므로, 본 실시예의 경우, 물의 예열을 충분히 확보할 수 있어 고온 개질의 효율을 향상시킬 수 있다. In general, since the reforming efficiency in the high temperature reforming unit 110 is improved as the temperature of the reactant in the vaporized state increases, in this embodiment, sufficient preheating of water may be ensured, thereby improving the efficiency of high temperature reforming.

또한, 제3열교환부(143) 및 제2열교환부(142)에서의 열교환을 통하여 CO제거부(130) 및 CO변성부(120)의 온도가 각각에 구비되는 촉매의 활성 온도보다 상승하는 것을 방지할 수 있다.
In addition, through the heat exchange in the third heat exchanger 143 and the second heat exchanger 142, the temperature of the CO removal unit 130 and the CO denaturation unit 120 rises above the active temperature of the catalyst provided in each. It can prevent.

도 3은 본 발명의 또 다른 실시예에 따른 연료전지용 개질기의 단면도를 나타낸 것으로서, 물의 공급량에 따라 제2열교환부 혹은 제3열교환부로 물이 공급되는 예를 나타낸 것이다. Figure 3 shows a cross-sectional view of a reformer for a fuel cell according to another embodiment of the present invention, showing an example in which water is supplied to the second heat exchange unit or the third heat exchange unit in accordance with the supply amount of water.

도 3을 참조하면, 도시된 연료전지용 개질기는 도 2에 도시된 개질기와 거의 동일한 원통형 구조를 갖는다. 보다 구체적으로 도 3에 도시된 연료전지용 개질기에는 중앙으로부터 버너부(101), 고온 개질부(110), 제1열교환부(141), 제1단열부(151), CO변성부(120), 제2열교환부(142), 제2단열부(152), CO제거부(130) 및 제3열교환부(143)가 순차적으로 형성되어 있다. 또한, 제2열교환부(142)의 외측에는 버너 폐가스부(160)가 형성될 수 있다. Referring to FIG. 3, the illustrated reformer for a fuel cell has a cylindrical structure that is substantially the same as the reformer illustrated in FIG. 2. More specifically, the fuel cell reformer illustrated in FIG. 3 includes a burner unit 101, a high temperature reformer 110, a first heat exchanger 141, a first insulation unit 151, a CO modified unit 120, The second heat exchanger 142, the second insulation 152, the CO removal unit 130, and the third heat exchanger 143 are sequentially formed. In addition, a burner waste gas unit 160 may be formed outside the second heat exchange unit 142.

버너부(101)에서는 연료와 산소가 산화 반응하여 열을 발생시켜 고온 개질부(110)로 전달한다. In the burner unit 101, fuel and oxygen are oxidized to generate heat and are transferred to the high temperature reformer 110.

고온 개질부(110)에서는 제1열교환부(141)로부터 투입되는 탄화수소계 연료(NG)와 기화된 상태의 반응 물이 버너부(101)에서 전달된 열에 의하여 700 ~ 750℃ 정도의 제1온도에서 촉매 반응한다. In the high temperature reforming unit 110, the hydrocarbon-based fuel NG introduced from the first heat exchange unit 141 and the reactant in a vaporized state are firstly heated at about 700 to 750 ° C. by the heat transferred from the burner unit 101. Catalytic reaction at

CO변성부(120)에서는 고온 개질부(110)에서 발생되는 CO와 잔류하는 반응 물이 200 ~ 250℃ 정도의 제2온도에서 촉매 반응한다. In the CO modifying unit 120, the CO generated from the high temperature reforming unit 110 and the remaining reactant are catalytically reacted at a second temperature of about 200 to 250 ° C.

CO제거부(130)에서는 CO변성부(120)에서 잔류하는 CO와 산소가 100 ~ 140℃ 정도의 제3온도에서 촉매 반응한다.
In the CO removal unit 130, the CO and oxygen remaining in the CO modification unit 120 are catalytically reacted at a third temperature of about 100 to 140 ° C.

본 실시예에서는 개질기 내부로 공급되는 물의 양에 따라 물의 공급 위치가 조절될 수 있다. In this embodiment, the supply position of the water may be adjusted according to the amount of water supplied into the reformer.

개질기 내부로 공급되는 물의 양이 상대적으로 많을 경우, 예열 구간이 짧을 경우 충분히 예열되기 어렵다. 반대로, 개질기 내부로 공급되는 물의 양이 상대적으로 적을 경우, 예열 구간이 길 경우 필요 이상의 예열이 발생할 수 있다. If the amount of water supplied into the reformer is relatively large, it is difficult to sufficiently preheat the preheating section. On the contrary, when the amount of water supplied into the reformer is relatively small, a longer preheating period may cause more preheating than necessary.

이에 본 발명에서는 외부에서 공급되는 물의 양이 상대적으로 많을 경우, 공급되는 물이 충분히 예열될 수 있도록 제3열교환부(143)로 투입되며, 반대로, 외부에서 공급되는 물의 양이 상대적으로 적을 경우, 공급되는 물이 필요 이상으로 예열되지 않도록 제2열교환부(142)로 투입될 수 있다. In the present invention, when the amount of water supplied from the outside is relatively large, the water is supplied to the third heat exchanger 143 so that the water supplied is sufficiently preheated. On the contrary, when the amount of water supplied from the outside is relatively small, The supplied water may be introduced into the second heat exchanger 142 so as not to be preheated more than necessary.

외부에서 공급되는 물의 양이 상대적으로 많아서, 공급되는 물이 제3열교환부(143)로 투입되는 경우, 제3열교환부(143)로 투입된 물은 제3열교환부(143), 제2열교환부(142) 및 제1열교환부(141)에서 CO제거부(130), CO변성부(120), CO변성부 하부 열교환부(121) 및 고온 개질부(110)와 순차적인 열교환을 통하여 기화된 상태로 고온 개질부(110)에 반응 물로 투입된다. Since the amount of water supplied from the outside is relatively large, and the supplied water is introduced into the third heat exchange part 143, the water introduced into the third heat exchange part 143 is the third heat exchange part 143 and the second heat exchange part. 142 and the first heat exchanger 141 is evaporated through sequential heat exchange with the CO removal unit 130, the CO modification unit 120, the CO modification unit lower heat exchanger 121 and the high temperature reforming unit 110. Into the high temperature reforming unit 110 as a reaction water.

이와 반대로, 외부에서 공급되는 물의 양이 상대적으로 적어서, 공급되는 물이 제2열교환부(142)로 투입되는 경우, 제2열교환부(142)로 투입된 물은 제2열교환부(142) 및 제1열교환부(141)에서 CO변성부(120), CO변성부 하부 열교환부(121) 및 고온 개질부(110)와 순차적인 열교환을 통하여 기화된 상태로 고온 개질부(110)에 기화된 상태의 반응 물로 투입된다. On the contrary, when the amount of water supplied from the outside is relatively small, and the supplied water is introduced into the second heat exchanger 142, the water introduced into the second heat exchanger 142 may include the second heat exchanger 142 and the second heat exchanger 142. In the heat exchange part 141, the CO-modified part 120, the CO-modified part, the heat exchange part 121, and the high-temperature reformed part 110 in a vaporized state through evaporation through sequential heat exchange. Is injected into the reaction water.

물론, 제2열교환부(142) 외측에 버너 폐가스부(160)가 형성되는 경우, 제2열교환부(142)에 공급되는 물은 CO변성부(120), CO변성부 하부 열교환부(121)와의 열교환 뿐만 아니라, 버너 폐가스부(160)와의 추가적인 열교환에 의하여 예열될 수 있다. Of course, when the burner waste gas unit 160 is formed outside the second heat exchange unit 142, the water supplied to the second heat exchange unit 142 is CO-modified unit 120 and CO-denatured unit lower heat exchanger 121. In addition to heat exchange with the burner, it may be preheated by additional heat exchange with the burner waste gas unit 160.

개질기 내로 투입되는 물의 양은 연료전지 스택에서 요구되는 전기 생산량과 비례 관계에 있다. 즉, 전기 생산량이 많을 경우 개질기 내에 상대적으로 많은 양의 물이 투입되어야 하며, 전기 생산량이 적을 경우 개질기 내에 상대적으로 적은 양의 물이 투입되어도 된다.The amount of water introduced into the reformer is proportional to the electricity production required in the fuel cell stack. In other words, when the amount of electricity is produced, a relatively large amount of water must be added to the reformer. When the amount of electricity is produced, a relatively small amount of water may be added to the reformer.

이에 따라 연료전지 스택에서의 전기 생산량이 많을 경우, 제3열교환부(143)을 통하여 물이 공급되며, 연료전지 스택에서의 전기 생산량이 적을 경우, 제2열교환부(143)을 통하여 물이 공급될 수 있다.
Accordingly, when the amount of electricity produced in the fuel cell stack is large, water is supplied through the third heat exchanger 143, and when the amount of electricity produced in the fuel cell stack is low, water is supplied through the second heat exchanger 143. Can be.

상술한 바와 같이, 본 발명에 따른 연료전지용 개질기는 컴팩트한 원통형 구조를 가질 수 있으며, 또한 버너부에서 발생되는 열이 고온 개질부 등 외측 방향으로 효율적으로 전달될 수 있다. As described above, the reformer for a fuel cell according to the present invention may have a compact cylindrical structure, and heat generated in the burner portion may be efficiently transferred to the outside direction such as a high temperature reformer.

또한, 본 발명에 따른 연료전지용 개질기는 물의 충분한 예열이 가능하며, 아울러 CO변성부 등의 온도 상승을 방지할 수 있다. In addition, the reformer for a fuel cell according to the present invention is capable of sufficient preheating of water, and can also prevent the temperature rise of the CO-modified part and the like.

또한, 본 발명에 따른 연료전지용 개질기는 연료전지 스택에서의 전기 생산량에 따라 물 공급 위치를 조절할 수 있어 개질 효율을 향상시킬 수 있다.
In addition, the reformer for a fuel cell according to the present invention can adjust the water supply position according to the amount of electricity produced in the fuel cell stack can improve the reforming efficiency.

이상 첨부된 도면을 참조하여 본 발명의 실시예들을 설명하였으나, 본 발명은 상기 실시예들에 한정되는 것이 아니라 서로 다른 다양한 형태로 변형될 수 있으며, 본 발명이 속하는 기술 분야에서 통상의 지식을 가진 자는 본 발명의 기술적 사상이나 필수적인 특징을 변경하지 않고서 다른 구체적인 형태로 실시될 수 있다는 것을 이해할 수 있을 것이다. 그러므로 이상에서 기술한 실시예들은 모든 면에서 예시적인 것이며 한정적이 아닌 것으로 이해해야만 한다.
While the present invention has been described in connection with what is presently considered to be practical exemplary embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, It will be understood by those skilled in the art that the present invention may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. It is therefore to be understood that the above-described embodiments are illustrative in all aspects and not restrictive.

101 : 버너부 110 : 고온 개질부
120 : CO변성부 121 : CO변성부 하부 열교환부
130 : CO제거부 141 : 제1열교환부
142 : 제2열교환부 143 : 제3열교환부
151 : 제1단열부 152 : 제2단열부
160 : 버너 폐가스부101: burner unit 110: high temperature reforming unit
120: CO modified portion 121: CO modified portion lower heat exchanger
130: CO removal unit 141: the first heat exchange unit
142: second heat exchanger 143: third heat exchanger
151: first insulating portion 152: second insulating portion
160: burner waste gas unit

Claims (7)

중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부 및 CO제거부가 순차적으로 형성되어 있는 원통형 구조를 가지되,
상기 CO변성부 하부에는 CO변성부 하부 열교환부가 형성되어 있으며,
상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 기화된 상태의 반응 물(Process H2O)이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하며,
외부에서 공급되는 물이 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되는 것을 특징으로 하는 연료전지용 개질기.
It has a cylindrical structure in which a burner part, a high temperature reforming part, a first heat exchange part, a first heat insulation part, a CO denaturation part, a second heat exchange part, a second heat insulation part and a CO removal part are sequentially formed from the center,
A CO heat exchanger lower heat exchanger is formed under the CO modified part,
In the burner unit, fuel and oxygen are oxidized to generate heat, and transfer heat to the high temperature reforming unit. In the high temperature reforming unit, hydrocarbon-based fuel introduced from the first heat exchange unit and reactant in a vaporized state (Process H 2 O) ) Is catalytically reacted at a first temperature by the heat transferred from the burner unit, and in the CO-denatured unit, CO generated from the high temperature reforming unit and the remaining reactant are catalyzed at a second temperature lower than the first temperature. In the CO removal unit, the CO and oxygen remaining in the CO modification unit are catalytically reacted at a third temperature lower than the second temperature,
Water supplied from the outside reacts with the high temperature reforming unit in a vaporized state through sequential heat exchange with the CO modifying unit, the CO modifying unit lower heat exchanger, and the high temperature reforming unit in the second heat exchanger and the first heat exchanger. A reformer for a fuel cell, which is introduced into water.
중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부, CO제거부 및 제3열교환부가 순차적으로 형성되어 있는 원통형 구조를 가지되,
상기 CO변성부 하부에는 CO변성부 하부 열교환부가 형성되어 있으며,
상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 반응 물이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하며,
외부에서 공급되는 물이 상기 제3열교환부, 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO제거부, 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되는 것을 특징으로 하는 연료전지용 개질기.
It has a cylindrical structure in which a burner part, a high temperature reforming part, a first heat exchange part, a first heat insulation part, a CO denaturation part, a second heat exchange part, a second heat insulation part, a CO removal part and a third heat exchange part are sequentially formed from the center. Be,
A CO heat exchanger lower heat exchanger is formed under the CO modified part,
In the burner unit, fuel and oxygen are oxidized to generate heat and are transferred to the high temperature reforming unit. In the high temperature reforming unit, hydrocarbon-based fuel and reactant introduced from the first heat exchange unit are transferred by the heat transferred from the burner unit. Catalytic reaction at a first temperature, in the CO-denatured portion, the CO generated from the high temperature reforming portion and the remaining reactant catalyzes at a second temperature lower than the first temperature, the CO-denatured portion in the CO removal portion CO and oxygen remaining in the catalytic reaction at a third temperature lower than the second temperature,
Water supplied from the outside performs sequential heat exchange with the CO removal unit, the CO modification unit, the CO modification unit, the lower heat exchange unit, and the high temperature reforming unit in the third heat exchange unit, the second heat exchange unit, and the first heat exchange unit. A reformer for a fuel cell, characterized in that the high temperature reforming unit is injected into the reactant in a vaporized state.
중앙으로부터 버너부, 고온 개질부, 제1열교환부, 제1단열부, CO변성부, 제2열교환부, 제2단열부, CO제거부 및 제3열교환부가 순차적으로 형성되어 있는 원통형 구조를 가지되,
상기 CO변성부 하부에는 CO변성부 하부 열교환부가 형성되어 있으며,
상기 버너부에서는 연료와 산소가 산화 반응하여 열을 발생시켜 상기 고온 개질부로 전달하고, 상기 고온 개질부에서는 상기 제1열교환부로부터 투입되는 탄화수소계 연료와 반응 물이 상기 버너부에서 전달된 열에 의하여 제1온도에서 촉매 반응하고, 상기 CO변성부에서는 상기 고온 개질부에서 발생되는 CO와 잔류하는 반응 물이 상기 제1온도보다 낮은 제2온도에서 촉매 반응하고, 상기 CO제거부에서는 상기 CO변성부에서 잔류하는 CO와 산소가 상기 제2온도보다 낮은 제3온도에서 촉매 반응하며,
외부에서 공급되는 물의 양이 상대적으로 많을 경우, 상기 물은 상기 제3열교환부로 투입되어, 상기 제3열교환부, 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO제거부, 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되고,
외부에서 공급되는 물의 양이 상대적으로 적을 경우, 상기 물은 상기 제2열교환부로 투입되어, 상기 제2열교환부 및 상기 제1열교환부에서 상기 CO변성부, CO변성부 하부 열교환부 및 상기 고온 개질부와 순차적인 열교환을 통하여 기화된 상태로 상기 고온 개질부에 반응 물로 투입되는 것을 특징으로 하는 연료전지용 개질기.
It has a cylindrical structure in which a burner part, a high temperature reforming part, a first heat exchange part, a first heat insulation part, a CO denaturation part, a second heat exchange part, a second heat insulation part, a CO removal part and a third heat exchange part are sequentially formed from the center. Be,
A CO heat exchanger lower heat exchanger is formed under the CO modified part,
In the burner unit, fuel and oxygen are oxidized to generate heat and are transferred to the high temperature reforming unit. In the high temperature reforming unit, hydrocarbon-based fuel and reactant introduced from the first heat exchange unit are transferred by the heat transferred from the burner unit. Catalytic reaction at a first temperature, in the CO-denatured portion, the CO generated from the high temperature reforming portion and the remaining reactant catalyzes at a second temperature lower than the first temperature, the CO-denatured portion in the CO removal portion CO and oxygen remaining in the catalytic reaction at a third temperature lower than the second temperature,
When the amount of water supplied from the outside is relatively large, the water is introduced into the third heat exchanger, and the third heat exchanger, the second heat exchanger, and the first heat exchanger remove the CO and CO denatured parts. The CO-modified part is exchanged into the high-temperature reforming unit as a reactant in a vaporized state through heat exchange with the lower heat exchanger and the high-temperature reforming unit,
When the amount of water supplied from the outside is relatively small, the water is introduced into the second heat exchange part, so that the CO-modified part, the CO-denatured bottom heat exchange part, and the high temperature reforming part of the second heat exchange part and the first heat exchange part. A reformer for a fuel cell, characterized in that the high temperature reforming unit is introduced into the reactant in a vaporized state through sequential heat exchange with the unit.
제1항 내지 제3항 중 어느 하나의 항에 있어서,
상기 개질기는
상기 버너부 운전에 의해 생성되는 버너 폐가스가 배출되도록, 상기 제2열교환부 외측에 형성되는 버너 폐가스 배출부를 더 포함하는 것을 특징으로 하는 연료전지용 개질기.
4. The method according to any one of claims 1 to 3,
The reformer
And a burner waste gas discharge unit formed outside the second heat exchange unit so that burner waste gas generated by the burner unit operation is discharged.
제4항에 있어서,
상기 제2열교환부에 투입되는 물은 상기 CO변성부, 상기 CO 변성부 하부 열교환부 및 상기 버너 폐가스부와의 열교환하는 것을 특징으로 하는 연료전지용 개질기.
The method of claim 4, wherein
The water introduced into the second heat exchange part is heat-exchanged with the CO-modified part, the CO-modified part lower heat exchange part, and the burner waste gas part.
제1항 내지 제3항 중 어느 하나의 항에 있어서,
상기 개질기는
상기 고온 개질부의 결과물이 상기 제1열교환부의 물과 열교환에 의하여 온도가 상기 제2온도로 하강하여, 상기 CO변성부로 공급되고,
상기 CO변성부의 결과물이 상기 제2열교환부의 물과 열교환에 의하여 온도가 상기 제3온도로 하강하여, 상기 CO제거부로 공급되는 것을 특징으로 하는 연료전지용 개질기.
4. The method according to any one of claims 1 to 3,
The reformer
As a result of the high temperature reforming unit, the temperature is lowered to the second temperature by heat exchange with water of the first heat exchange unit, and is supplied to the CO-modifying unit,
A reformer for a fuel cell, wherein the resultant product of the CO-modifying unit is lowered to the third temperature by heat exchange with water of the second heat-exchanging unit and supplied to the CO removing unit.
제1항 내지 제3항 중 어느 하나의 항에 있어서,
상기 제1온도는 700 ~ 750℃이고, 상기 제2온도는 200 ~ 250℃이며, 상기 제3온도는 100 ~ 140℃인 것을 특징으로 하는 연료전지용 개질기.4. The method according to any one of claims 1 to 3,
The first temperature is 700 ~ 750 ℃, the second temperature is 200 ~ 250 ℃, the third temperature is a reformer for a fuel cell, characterized in that 100 ~ 140 ℃.
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