JP2003238110A - Fuel treating device and its starting method - Google Patents
Fuel treating device and its starting methodInfo
- Publication number
- JP2003238110A JP2003238110A JP2002034148A JP2002034148A JP2003238110A JP 2003238110 A JP2003238110 A JP 2003238110A JP 2002034148 A JP2002034148 A JP 2002034148A JP 2002034148 A JP2002034148 A JP 2002034148A JP 2003238110 A JP2003238110 A JP 2003238110A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- fuel
- raw material
- reformer
- remover
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、燃料を加熱、改
質、ＣＯ除去する燃料処理装置とその起動方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a fuel processor for heating, reforming and removing CO and a method for starting the same.
【０００２】[0002]
【従来の技術】近年、燃料電池自動車の研究開発が活発
に行われており、特に、燃料電池としては作動温度が比
較的低い（１００℃前後）固体高分子型燃料電池（ＰＥ
ＦＣ）が有力である。また燃料としては、補給が容易で
インフラ整備の必要性が少ないメタノールが有力視され
ている。この場合、メタノールを水素に改質する改質器
が必須となる。2. Description of the Related Art In recent years, research and development of fuel cell automobiles have been actively carried out, and in particular, a polymer electrolyte fuel cell (PE) having a relatively low operating temperature (around 100 ° C.) as a fuel cell.
FC) is influential. In addition, as fuel, methanol is considered to be the most promising fuel because it can be easily replenished and there is little need for infrastructure development. In this case, a reformer for reforming methanol into hydrogen is essential.
【０００３】[0003]
【発明が解決しようとする課題】メタノールを改質する
改質器としては、例えば「メタノール改質器」（特開昭
６３−５０３０２号）が開示されている。この改質器
は、中空円筒形の反応管の内部に改質触媒を充填し、外
部から燃焼排ガスで加熱し、内部を流れる原料ガスを改
質するものである。As a reformer for reforming methanol, for example, a "methanol reformer" (JP-A-63-50302) is disclosed. In this reformer, a hollow cylindrical reaction tube is filled with a reforming catalyst and heated by combustion exhaust gas from the outside to reform a raw material gas flowing inside.
【０００４】しかし、特開昭６３−５０３０２号の「メ
タノール改質器」は、自動車用に搭載するには、（１）
大型で重く、（２）起動に時間がかかり、（３）負荷変
化への応答性が低く、（４）発生した水素含有ガス中の
ＣＯ濃度が高く、燃料電池の電極を劣化させる、等の問
題点があった。However, the "methanol reformer" disclosed in Japanese Patent Laid-Open No. 63-50302 is (1)
It is large and heavy, (2) takes a long time to start up, (3) has low responsiveness to load changes, (4) has a high CO concentration in the generated hydrogen-containing gas, and deteriorates the electrodes of the fuel cell. There was a problem.
【０００５】また、高いメタノール転化率を維持しつつ
ＣＯガスの生成を低くできる手段として、例えば、「水
素含有ガスの製造方法」（特開平６−２５６００１号、
特開平６−２７９００１号）が開示されている。この方
法は、メタノール、酸素、水を加熱した触媒に接触させ
て反応させるものであり、燃料の一部を燃焼させる部分
酸化を利用している。As a means for reducing the production of CO gas while maintaining a high methanol conversion rate, for example, "a method for producing a hydrogen-containing gas" (Japanese Patent Laid-Open No. 6-256001,
JP-A-6-279001) is disclosed. In this method, methanol, oxygen, and water are brought into contact with a heated catalyst to cause reaction, and partial oxidation in which a part of fuel is burned is used.
【０００６】しかし、特開平６−２５６００１号及び特
開平６−２７９００１号の「水素含有ガスの製造方法」
は、（５）触媒の予熱に時間がかかり、（６）ＣＯ濃度
を従来のリン酸型燃料電池には適用可能な程度（約１％
前後）まで下げることができるが、車載用に適した固体
高分子型燃料電池（ＰＥＦＣ）に適用するには依然とし
てＣＯ濃度が高い問題点があった。However, the method for producing a hydrogen-containing gas disclosed in JP-A-6-256001 and JP-A-6-279901.
(5) It takes a long time to preheat the catalyst, and (6) the CO concentration can be applied to a conventional phosphoric acid fuel cell (about 1%).
However, there is a problem that the CO concentration is still high when applied to a polymer electrolyte fuel cell (PEFC) suitable for vehicle mounting.
【０００７】更に、ＣＯ濃度が極めて低い水素含有ガス
を生成することができる「燃料改質装置」（特開平８−
１５７２０１号）が開示されている。この装置は、改質
器、選択酸化部、部分酸化部、及び制御装置を備え、選
択酸化部で一酸化炭素のみを酸化し、部分酸化部で残存
の一酸化炭素を酸化することで、ＣＯ濃度が極めて低い
（数ｐｐｍ）水素含有ガスを生成し、ＰＥＦＣへの適用
を可能にしている。Furthermore, a "fuel reformer" capable of producing a hydrogen-containing gas having an extremely low CO concentration (Japanese Patent Laid-Open No. 8-
No. 157201) is disclosed. This device is equipped with a reformer, a selective oxidation part, a partial oxidation part, and a control device. Only the carbon monoxide is oxidized in the selective oxidation part, and the remaining carbon monoxide is oxidized in the partial oxidation part. It produces a hydrogen-containing gas with a very low concentration (several ppm), which enables its application to PEFC.
【０００８】しかし、特開平８−１５７２０１号の「燃
料改質装置」は、改質器が特開昭６３−５０３０２号と
同様の間接加熱型であるため、起動に時間がかかり、負
荷変化への応答性が低い問題点があった。However, in the "fuel reformer" of Japanese Patent Laid-Open No. 8-157201, since the reformer is an indirect heating type similar to that of Japanese Patent Laid-Open No. 63-50302, it takes time to start and the load changes. There was a problem that the responsiveness was low.
【０００９】すなわち、従来の改質器はコンパクト化し
にくく、負荷応答性が低く、反応器の予熱・起動に時間
がかかり車両搭載用の燃料電池用としては不十分である
問題点があった。That is, the conventional reformer has a problem that it is difficult to make it compact, its load response is low, preheating and starting of the reactor take time, and it is insufficient for a fuel cell mounted on a vehicle.
【００１０】上述した問題点を解決するため、本発明の
出願人等は、先に、「燃料電池用改質器とその起動方
法」を創案し、出願した（特開２００１−２２６１０
６）。この発明は、図３に示すように、水蒸気を含む原
料ガスを部分酸化させその発熱で原料ガスを水素含有ガ
スに改質する燃焼・改質触媒１が充填された部分酸化改
質器２と、該部分酸化改質器の上流側と下流側に空気を
供給する上流側空気ライン４及び下流側空気ライン６
と、部分酸化改質器内の温度を検出して上流側空気ライ
ン４及び下流側空気ライン６の空気流量を制御する流量
制御器８とを備え、改質器内の上流側温度が触媒の耐熱
温度を超えないように上流側空気ラインの空気流量を制
御し、かつ改質器内の下流側温度が所定の温度範囲にな
るように下流側空気ラインの空気流量を制御するもので
ある。In order to solve the above-mentioned problems, the applicants of the present invention previously created and applied for "a reformer for a fuel cell and a starting method thereof" (Japanese Patent Laid-Open No. 2001-22610).
6). As shown in FIG. 3, the present invention includes a partial oxidation reformer 2 filled with a combustion / reforming catalyst 1 that partially oxidizes a raw material gas containing water vapor and reforms the raw material gas into a hydrogen-containing gas by its heat generation. An upstream air line 4 and a downstream air line 6 for supplying air to the upstream side and the downstream side of the partial oxidation reformer.
And a flow rate controller 8 that detects the temperature in the partial oxidation reformer and controls the air flow rate in the upstream air line 4 and the downstream air line 6, and the upstream temperature in the reformer is set to the catalyst temperature. The air flow rate of the upstream air line is controlled so as not to exceed the heat resistant temperature, and the air flow rate of the downstream air line is controlled so that the downstream temperature in the reformer falls within a predetermined temperature range.
【００１１】この発明により、燃焼・改質触媒１が充填
された部分酸化改質器１２に空気ライン４、６から空気
を供給するので、触媒の作用により水蒸気を含む原料ガ
スの一部が直ちに部分酸化し、その発熱で燃焼・改質触
媒を直接加熱するので、間接加熱式のように大型の熱交
換器が不要となり、短時間に加熱でき、燃料電池の急速
な負荷変化に容易に追従できるようになった。According to the present invention, since air is supplied from the air lines 4 and 6 to the partial oxidation reformer 12 filled with the combustion / reforming catalyst 1, a part of the raw material gas containing steam is immediately discharged by the action of the catalyst. Partial oxidation directly heats the combustion / reforming catalyst due to the heat generated, eliminating the need for a large heat exchanger as in the indirect heating type, heating in a short time, and easily following the rapid load change of the fuel cell. I can do it now.
【００１２】しかし、特開２００１−２２６１０６の場
合でも、燃料として液体燃料（例えばメタノール）を用
いる場合、燃料の加熱に熱交換器・蒸発器を用い、加熱
・蒸発させるため、装置が大きくなり、かつ起動に時間
がかかっていた。また、部分酸化改質器内でも部分酸化
により加熱するため、原料ガスの供給温度は反応温度よ
り低くする必要があり、改質反応が入口付近では十分に
進行せず、触媒が十分に利用できていなかった。However, even in the case of Japanese Patent Laid-Open No. 2001-226106, when a liquid fuel (for example, methanol) is used as the fuel, a heat exchanger / evaporator is used for heating the fuel to heat and evaporate, so that the device becomes large, And it took a long time to start. In addition, since the partial oxidation reformer also heats by partial oxidation, the feed temperature of the raw material gas must be lower than the reaction temperature, and the reforming reaction does not proceed sufficiently near the inlet and the catalyst can be used sufficiently. Didn't.
【００１３】また、これらの問題点を解決するために、
特開平７−２１５７０２号、特開２００１−１５３３１
３等が提案されている。Further, in order to solve these problems,
JP-A-7-215702, JP-A-2001-15331
3rd grade is proposed.
【００１４】特開平７−２１５７０２号の「燃料改質装
置」は、燃料噴射ノズルからの燃料を完全燃焼させる工
程と、燃料気化用コイルからの燃料を部分酸化反応させ
る工程とを備え、装置の前段部において、バーナとして
理論空燃比で完全燃焼させ、この熱で触媒床と反応ガス
の加熱を行い、触媒床においては、部分酸化によりＣＯ
が発生し、このＣＯと完全燃焼により生成した水蒸気に
より水素へのシフト反応が行われるものである。The "fuel reformer" of Japanese Patent Laid-Open No. 7-215702 has a step of completely burning the fuel from the fuel injection nozzle and a step of partially oxidizing the fuel from the fuel vaporizing coil, and the In the front stage, the burner is completely burned at the stoichiometric air-fuel ratio, and the heat heats the catalyst bed and the reaction gas.
Is generated, and the shift reaction to hydrogen is performed by the CO and steam generated by complete combustion.
【００１５】しかし、この装置では、前段部において完
全燃焼させるため、空燃比を非常に大きく（１４．５以
上に）設定するため、下流部に大量の酸素が残留し、こ
れを部分酸化により完全に消費する必要がある。また、
その結果大量のＣＯが発生するため、ＣＯ濃度を従来の
リン酸型燃料電池には適用可能な程度（約１％前後）ま
で下げることが困難である。またこのＣＯと燃焼により
生成した水蒸気のみを反応させるため、改質反応の制御
が困難である等の問題点があった。[0015] However, in this apparatus, since the air-fuel ratio is set to a very large value (14.5 or more) in order to completely burn the fuel in the former stage, a large amount of oxygen remains in the downstream portion, which is completely oxidized by partial oxidation. Need to consume. Also,
As a result, a large amount of CO is generated, and it is difficult to reduce the CO concentration to a level applicable to the conventional phosphoric acid fuel cell (about 1%). Further, there is a problem that it is difficult to control the reforming reaction because only the steam produced by combustion reacts with the CO.
【００１６】また、特開２００１−１５３３１３の「部
分酸化バーナ」は、燃焼空間壁の内壁にセラミック部材
を設け、燃焼空間の下流側に、液体燃料を気化させる機
構を備える熱交換器を配設し、熱交換器で気化した燃料
ガスを燃焼空間で燃焼させるものである。Further, in the "partial oxidation burner" of Japanese Patent Laid-Open No. 2001-153313, a ceramic member is provided on the inner wall of the combustion space wall, and a heat exchanger having a mechanism for vaporizing liquid fuel is arranged downstream of the combustion space. However, the fuel gas vaporized by the heat exchanger is burned in the combustion space.
【００１７】この装置は、低い空気比でも火炎を安定化
させることができるが、セラミック部材や熱交換器が十
分加熱されるまで、安定燃焼が困難であり、その結果起
動時間がかかる。また、排ガス温度を低減するために熱
交換器を用いるため、装置構造が複雑かつ大型となり、
かつその温度制御が困難である問題点があった。Although this device can stabilize the flame even at a low air ratio, stable combustion is difficult until the ceramic member and the heat exchanger are sufficiently heated, and as a result, it takes a long starting time. Further, since the heat exchanger is used to reduce the exhaust gas temperature, the device structure becomes complicated and large,
In addition, there is a problem that the temperature control is difficult.
【００１８】本発明は上述した種々の問題点を解決する
ために創案されたものである。すなわち、本発明の目的
は、燃料として液体燃料を用いる場合でも、短時間で起
動でき、かつ容易に小型化ができる燃料処理装置とその
起動方法を提供することにある。The present invention was created to solve the above-mentioned various problems. That is, an object of the present invention is to provide a fuel processing apparatus and a starting method thereof which can be started in a short time and can be easily downsized even when a liquid fuel is used as the fuel.
【００１９】[0019]
【課題を解決するための手段】本発明によれば、燃料を
燃焼させて高温ガスを発生させる過濃燃焼バーナ（１
２）と、燃料と水の混合原料を蒸発させて加熱する蒸発
加熱装置（１４）と、混合原料を水素含有ガスに改質す
る改質器（１６）と、一酸化炭素を選択的に除去するＣ
Ｏ除去器（１８）とを備えた一体型の燃料処理装置であ
って、前記蒸発加熱装置（１４）は、改質器（１６）を
出たガスとＣＯ除去器（１８）を出たガスを液体状態の
混合原料で冷却する液体原料チャンバ（１５）を有し、
前記改質器（１６）は、改質触媒を外部からの高温ガス
で間接加熱するガス加熱管（１６ａ）を内蔵し、前記Ｃ
Ｏ除去器（１８）は、ＣＯ除去触媒を外部からの高温ガ
スで間接加熱するガス加熱管（１８ａ）を内蔵する、こ
とを特徴とする燃料処理装置が提供される。According to the present invention, a rich combustion burner (1) for burning a fuel to generate a high temperature gas is provided.
2), an evaporation heating device (14) for evaporating and heating a mixed raw material of fuel and water, a reformer (16) for reforming the mixed raw material into a hydrogen-containing gas, and selectively removing carbon monoxide. To do C
An integrated fuel processor comprising an O remover (18), wherein the evaporative heating device (14) is a gas leaving the reformer (16) and a gas leaving the CO remover (18). A liquid raw material chamber (15) for cooling the mixed raw material in a liquid state,
The reformer (16) has a built-in gas heating pipe (16a) for indirectly heating the reforming catalyst with a high temperature gas from the outside.
There is provided a fuel processing device, characterized in that the O remover (18) has a built-in gas heating pipe (18a) for indirectly heating the CO removing catalyst with a high temperature gas from the outside.
【００２０】上記本発明の構成によれば、過濃燃焼バー
ナ（１２）で燃料を燃焼させて高温ガスを発生させるの
で、燃料として液体燃料を用いる場合でも、短時間で着
火し、例えば１０００℃以上の高温ガスを短時間（数秒
程度）で発生することができる。また、蒸発加熱装置
（１４）で燃料と水の混合原料を蒸発させて加熱するの
で、温度制御が容易にできる。According to the above-mentioned structure of the present invention, since the fuel is burned by the rich combustion burner (12) to generate high temperature gas, even when a liquid fuel is used as the fuel, it ignites in a short time, for example, 1000 ° C. The above high-temperature gas can be generated in a short time (about several seconds). Further, since the mixed raw material of fuel and water is evaporated and heated by the evaporation heating device (14), temperature control can be easily performed.
【００２１】さらに加熱された混合原料を一体に形成さ
れた改質器（１６）とＣＯ除去器（１８）に直接供給で
きるので、放熱ロスを最小限度に抑えて、改質とＣＯ除
去ができ、燃料電池にそのまま供給して発電に用いるこ
とができる。Further, since the heated mixed raw material can be directly supplied to the reformer (16) and the CO remover (18) which are integrally formed, the heat loss can be suppressed to the minimum and the reforming and the CO can be removed. It can be directly supplied to the fuel cell and used for power generation.
【００２２】また、蒸発加熱装置（１４）は、改質器
（１６）を出たガスとＣＯ除去器（１８）を出たガスを
液体状態の混合原料で冷却する液体原料チャンバ（１
５）を有するので、別の熱交換器なしで、改質器を出た
ガスとＣＯ除去器を出たガスとを冷却でき、全体を容易
に小型化ができる。The evaporative heating device (14) cools the gas discharged from the reformer (16) and the gas discharged from the CO remover (18) with a liquid mixed raw material chamber (1).
Since 5) is provided, the gas exiting the reformer and the gas exiting the CO remover can be cooled without a separate heat exchanger, and the overall size can be easily reduced.
【００２３】さらに、改質器（１６）は、改質触媒を外
部からの高温ガスでは間接加熱するガス加熱管（１６
ａ）を内蔵し、ＣＯ除去器（１８）は、ＣＯ除去触媒を
外部からの高温ガスでは間接加熱するガス加熱管（１８
ａ）を内蔵するので、別の熱交換器なしで、改質器とＣ
Ｏ除去器を加熱でき、全体を容易に小型化ができる。Further, the reformer (16) includes a gas heating pipe (16) for indirectly heating the reforming catalyst with a high temperature gas from the outside.
a), and the CO remover (18) includes a gas heating pipe (18) for indirectly heating the CO removing catalyst with a high temperature gas from the outside.
Since a) is built-in, there is no need for a separate heat exchanger and the reformer and C
The O 2 remover can be heated, and the overall size can be easily reduced.
【００２４】従って、着火、燃焼、加熱、改質、ＣＯ除
去を短時間にできるので、燃料電池の起動が短時間でで
きる。Therefore, since ignition, combustion, heating, reforming and CO removal can be performed in a short time, the fuel cell can be started in a short time.
【００２５】本発明の好ましい実施形態によれば、前記
改質器（１６）とＣＯ除去器（１８）は、過濃燃焼バー
ナ（１２）を囲んで連続して形成されており、前記液体
原料チャンバ（１５）は、ＣＯ除去器（１８）とその前
後の空洞部（１７ａ、１７ｂ）を囲み、該空洞部との熱
交換により、改質器（１６）を出たガスとＣＯ除去器
（１８）を出たガスを液体状態の混合原料で冷却する。According to a preferred embodiment of the present invention, the reformer (16) and the CO remover (18) are continuously formed so as to surround the rich combustion burner (12), and the liquid raw material is used. The chamber (15) surrounds the CO remover (18) and the cavities (17a, 17b) before and after the CO eliminator, and heat exchange with the cavities allows the gas and CO remover (gas leaving the reformer (16)) to be removed. The gas discharged from 18) is cooled with the mixed raw material in a liquid state.
【００２６】この構成により、過濃燃焼バーナ（１２）
からの伝熱で改質器（１６）とＣＯ除去器（１８）を加
熱でき、放熱ロスを最小限度に抑えることができる。ま
た、液体原料チャンバ（１５）とＣＯ除去器（１８）の
前後の空洞部（１７ａ、１７ｂ）との熱交換により、改
質器（１６）を出たガスとＣＯ除去器（１８）を出たガ
スを液体状態の混合原料で冷却でき、かつ全体を容易に
小型化ができる。With this configuration, the rich combustion burner (12)
The reformer (16) and the CO remover (18) can be heated by the heat transfer from, and the heat radiation loss can be suppressed to the minimum. In addition, heat exchange between the liquid source chamber (15) and the cavities (17a, 17b) before and after the CO remover (18) causes the gas leaving the reformer (16) and the CO remover (18) to exit. The gas can be cooled with the mixed raw material in a liquid state, and the whole can be easily downsized.
【００２７】また、本発明によれば、燃料を燃焼させて
高温ガスを発生させる過濃燃焼ステップ（Ａ）と、燃料
と水の混合原料を蒸発させて加熱する蒸発加熱ステップ
（Ｂ）と、加熱された混合原料を水素含有ガスに改質す
る改質ステップ（Ｃ）と、を備え、起動時と定常運転時
とで、混合原料の蒸発量を変化させて、蒸発加熱室にお
ける混合原料の温度を制御し、かつ改質触媒及びＣＯ除
去触媒を外部からの高温ガスにより加熱する、ことを特
徴とする燃料処理装置の起動方法が提供される。Further, according to the present invention, a rich combustion step (A) of combusting the fuel to generate a high temperature gas, and an evaporative heating step (B) of evaporating and heating the mixed raw material of fuel and water, A reforming step (C) for reforming the heated mixed raw material into a hydrogen-containing gas, and changing the evaporation amount of the mixed raw material between the start-up and the steady operation to change the mixed raw material in the evaporation heating chamber. There is provided a method for starting a fuel processing apparatus, which comprises controlling a temperature and heating a reforming catalyst and a CO removal catalyst with a high temperature gas from the outside.
【００２８】この起動方法により、過濃燃焼ステップ
（Ａ）で燃料を燃焼させて高温ガスを発生させるので、
燃料として液体燃料を用いる場合でも、短時間で着火
し、例えば１０００℃以上の高温ガスを短時間（数秒程
度）で発生することができる。According to this starting method, the fuel is burned in the rich combustion step (A) to generate high temperature gas.
Even when a liquid fuel is used as the fuel, it is possible to ignite in a short time and generate a high temperature gas of 1000 ° C. or higher in a short time (about several seconds).
【００２９】また、蒸発加熱ステップ（Ｂ）で燃料と水
の混合原料を蒸発させて加熱するので、温度制御が容易
にできる。さらに改質ステップ（Ｃ）において、混合ガ
スの保有する熱で下流側に位置する改質触媒を直接及び
間接に加熱することができるので、別の熱交換器なし
で、改質器とＣＯ除去器を加熱でき、全体を容易に小型
化ができる。また、更に、着火、燃焼、加熱、改質、Ｃ
Ｏ除去を短時間にできるので、燃料電池の起動が短時間
でできる。Further, since the mixed raw material of fuel and water is vaporized and heated in the evaporation heating step (B), temperature control can be facilitated. Further, in the reforming step (C), the heat of the mixed gas can directly and indirectly heat the reforming catalyst located on the downstream side, so that the reformer and CO removal can be performed without another heat exchanger. The vessel can be heated and the whole can be easily miniaturized. In addition, ignition, combustion, heating, reforming, C
Since O can be removed in a short time, the fuel cell can be started in a short time.
【００３０】更に、起動時と定常運転時とで、起動時と
定常運転時とで、混合原料の蒸発量を変化させて、改質
器の入口ガス温度が触媒の耐熱温度を超えないように蒸
発加熱室における混合原料の温度を制御し、かつ改質触
媒及びＣＯ除去触媒を外部からの高温ガスにより加熱す
るので、一層速い起動ができるばかりでなく、触媒の加
熱を防止して触媒寿命を延ばし、高温におけるＣＯの発
生を抑制することができる。Further, the evaporation amount of the mixed raw material is changed between the startup and the steady operation so that the inlet gas temperature of the reformer does not exceed the heat resistant temperature of the catalyst. Since the temperature of the mixed raw material in the evaporative heating chamber is controlled and the reforming catalyst and the CO removal catalyst are heated by the high temperature gas from the outside, not only can the start-up be faster, but the heating of the catalyst can be prevented to extend the catalyst life. It can be extended and the generation of CO at high temperature can be suppressed.
【００３１】[0031]
【発明の実施の形態】以下、本発明の好ましい実施形態
を図面を参照して説明する。なお、各図において共通す
る部分には同一の符号を付して使用する。BEST MODE FOR CARRYING OUT THE INVENTION Preferred embodiments of the present invention will be described below with reference to the drawings. In addition, in each figure, the same parts are denoted by the same reference numerals.
【００３２】図１は、本発明による燃料処理装置の全体
概念図であり、図２はその具体的構成図である。燃料処
理装置１０は、図１に破線で囲む過濃燃焼バーナ１２、
蒸発加熱装置１４、改質器１６、及びＣＯ除去器１８か
らなる。また図２に示すように、この燃料処理装置１０
はこれらの構成機器が一体化された一体型の装置であ
る。また、燃料処理装置１０の外部には、固体高分子型
燃料電池２０（ＰＥＦＣ）と補助バーナ２２が発電用と
加熱用に設置されている。FIG. 1 is an overall conceptual view of a fuel processing apparatus according to the present invention, and FIG. 2 is a concrete configuration diagram thereof. The fuel processor 10 includes a rich combustion burner 12 surrounded by a broken line in FIG.
It is composed of an evaporative heating device 14, a reformer 16, and a CO remover 18. Further, as shown in FIG.
Is an integrated device in which these components are integrated. Further, outside the fuel processor 10, a polymer electrolyte fuel cell 20 (PEFC) and an auxiliary burner 22 are installed for power generation and heating.
【００３３】過濃燃焼バーナ１２は、燃焼室１２ａと燃
料噴射器１２ｂを有し、燃料を燃焼させて高温ガスを発
生させる燃焼器（プリバーナ）である。この燃焼器は、
燃料を燃空比１以上で燃焼させるのがよい。なお燃空比
１以上の燃焼とは、燃料と空気の当量比が１以上である
ことを意味し、燃焼後の高温ガスが酸素を含まない還元
状態となるものをいう。この過濃燃焼バーナ１２は、図
２に示すように、燃料処理装置１０の中心部分に設けら
れ、高温Ｔ１（例えば１０００℃以上）の燃焼ガスを発
生する。The rich combustion burner 12 has a combustion chamber 12a and a fuel injector 12b, and is a combustor (preburner) that burns fuel to generate high-temperature gas. This combustor
It is preferable to burn the fuel at a fuel-air ratio of 1 or more. Note that combustion with a fuel-air ratio of 1 or more means that the equivalence ratio of fuel and air is 1 or more, and means that the high temperature gas after combustion is in a reduced state containing no oxygen. As shown in FIG. 2, the rich combustion burner 12 is provided in the central portion of the fuel processing device 10 and generates combustion gas of high temperature T1 (for example, 1000 ° C. or higher).
【００３４】過濃燃焼バーナ１２の燃料は、好ましくは
改質原料と同じメタノール、メタン、ガソリン（ナフ
サ）、その他の炭化水素化合物である。またこの燃料と
水を混合した混合原料をそのまま燃焼させてもよい。The fuel for the rich combustion burner 12 is preferably the same methanol, methane, gasoline (naphtha), or other hydrocarbon compound as the reforming raw material. Further, the mixed raw material obtained by mixing the fuel and water may be burned as it is.
【００３５】蒸発加熱装置１４は、燃焼室１２ａの下流
側に連結された蒸発加熱室１４ａと、燃焼室１２ａまた
は蒸発加熱室１４ａに混合原料を噴霧する原料噴霧口１
４ｂとを備え、燃焼室１２ａで発生した高温ガスにより
燃料と水の混合原料を蒸発させて所望の温度Ｔ２に加熱
する。The evaporative heating device 14 includes an evaporative heating chamber 14a connected to the downstream side of the combustion chamber 12a, and a raw material spray port 1 for spraying a mixed raw material into the combustion chamber 12a or the evaporative heating chamber 14a.
4b, and the high temperature gas generated in the combustion chamber 12a evaporates the mixed raw material of fuel and water to heat it to a desired temperature T2.
【００３６】混合原料は、メタノール、メタン、ガソリ
ン（ナフサ）、その他の炭化水素化合物と水との混合体
である。水の混合比率は、改質器１６に供給される混合
ガス中の水蒸気と炭化水素化合物の比率（Ｓ／Ｃ）が改
質に適した値（例えば、Ｓ／Ｃ＝１．５前後）に設定す
る。The mixed raw material is a mixture of water with methanol, methane, gasoline (naphtha) and other hydrocarbon compounds. As for the mixing ratio of water, the ratio (S / C) of steam and hydrocarbon compounds in the mixed gas supplied to the reformer 16 becomes a value suitable for reforming (for example, S / C = about 1.5). Set.
【００３７】従って、過濃燃焼バーナ１２と蒸発加熱装
置１４により、酸素を含まない高温ガス（温度Ｔ１）を
発生させ、発生した高温ガスにより燃料と水の混合原料
を蒸発させて所望の温度Ｔ２まで加熱する。Therefore, the rich combustion burner 12 and the evaporative heating device 14 generate a high temperature gas (temperature T1) containing no oxygen, and the generated high temperature gas evaporates the mixed raw material of fuel and water to obtain a desired temperature T2. Heat up to.
【００３８】改質器１６とＣＯ除去器１８は、過濃燃焼
バーナ１２と蒸発加熱装置１４を囲む中空のリング状に
形成されている。このリング形状は、円形リングでも矩
形リングでもよい。また、改質器１６とＣＯ除去器１８
は、連続して一体に形成されており、蒸発加熱装置１４
を出たガスが、図２で閉じた右端部で反転してリング状
のフィルタ１４ｃに入り、フィルタ１４ｃを通って改質
器１６に流入し、第１空洞部１７ａを通過してＣＯ除去
器１８に入り、更に第２空洞部１７ｂを通過して外部の
燃料電池２０に供給される。The reformer 16 and the CO remover 18 are formed in the shape of a hollow ring surrounding the rich combustion burner 12 and the evaporative heating device 14. The ring shape may be circular or rectangular. In addition, the reformer 16 and the CO remover 18
Are continuously and integrally formed, and the evaporation heating device 14
The gas that has exited is inverted at the right end closed in FIG. 2, enters the ring-shaped filter 14c, flows into the reformer 16 through the filter 14c, passes through the first cavity 17a, and passes through the CO remover. Then, the fuel enters into the fuel cell 18 and further passes through the second cavity 17b to be supplied to the external fuel cell 20.
【００３９】改質器１６には、水蒸気を含む原料ガスを
水素含有ガスに改質する改質触媒１６ｂが充填されてい
る。改質触媒１６ｂには、例えば、銅−亜鉛系、貴金属
系、ニッケル、ニッケル合金、その他の改質触媒を用い
ることができる。銅−亜鉛系の改質触媒の耐熱温度は例
えば約４００℃であり、最適使用温度は約２５０〜３５
０℃である。The reformer 16 is filled with a reforming catalyst 16b for reforming a raw material gas containing steam into a hydrogen-containing gas. As the reforming catalyst 16b, for example, a copper-zinc-based, noble metal-based, nickel, nickel alloy, or other reforming catalyst can be used. The heat-resistant temperature of the copper-zinc based reforming catalyst is, for example, about 400 ° C., and the optimum use temperature is about 250 to 35.
It is 0 ° C.
【００４０】ＣＯ除去器１８には、一酸化炭素を選択的
に除去するＣＯ除去触媒１８ｂが充填されている。ＣＯ
除去触媒１８ｂにも、例えば、銅−亜鉛系、貴金属系、
ニッケル、ニッケル合金、その他の周知の触媒を用いる
ことができる。銅−亜鉛系のＣＯ除去触媒の耐熱温度は
例えば約４００℃であり、最適使用温度は約２００〜３
００℃である。The CO remover 18 is filled with a CO removing catalyst 18b for selectively removing carbon monoxide. CO
The removal catalyst 18b also includes, for example, a copper-zinc system, a noble metal system,
Nickel, nickel alloys, and other known catalysts can be used. The heat-resistant temperature of the copper-zinc-based CO removal catalyst is, for example, about 400 ° C., and the optimum use temperature is about 200 to 3
It is 00 ° C.
【００４１】図１において蒸発加熱装置１４は、改質器
１６及びＣＯ除去器１８と過濃燃焼バーナ１２の間に隔
壁を介して密着して設けられたドーナツ状の液体原料チ
ャンバ１５を有する。この液体原料チャンバ１５は、Ｃ
Ｏ除去器１８とその前後の第１、第２の空洞部１７ａ，
１７ｂを囲み、空洞部１７ａ，１７ｂとの熱交換によ
り、改質器１６を出たガスとＣＯ除去器１８を出たガス
を液体状態の混合原料で所望の温度Ｔ３，Ｔ４まで冷却
する。この冷却により液体状態の混合原料は加熱され、
蒸発加熱室１４ａとの隔壁に設けられた原料噴霧口１４
ｂから内部に噴霧されて蒸発する。In FIG. 1, the evaporative heating device 14 has a doughnut-shaped liquid raw material chamber 15 provided in close contact with the reformer 16 and the CO remover 18 and the rich combustion burner 12 via a partition wall. The liquid source chamber 15 is
O remover 18 and first and second hollow portions 17a before and after it,
The gas exiting the reformer 16 and the gas exiting the CO remover 18 are cooled to a desired temperature T3, T4 with a mixed raw material in a liquid state by surrounding the 17b and exchanging heat with the cavities 17a, 17b. This cooling heats the mixed raw material in the liquid state,
Raw material spray port 14 provided on the partition wall with the evaporation heating chamber 14a
It is sprayed inside from b and evaporates.
【００４２】また上述した改質器１６は、改質触媒１６
ｂを外部からの高温ガスで間接加熱するガス加熱管１６
ａを内蔵し、ＣＯ除去器１８も、ＣＯ除去触媒１８ｂを
外部からの高温ガスで間接加熱するガス加熱管１８ａを
内蔵する。これらのガス加熱管１６ａ，１８ａには、補
助バーナ２２で発生した高温ガスが必要時に供給され
る。なお。ＣＯ除去器１８は通常は冷却をし、起動時又
は液体で冷却されすぎるときに加熱する。The above-mentioned reformer 16 includes the reforming catalyst 16
Gas heating pipe 16 for indirectly heating b with a high temperature gas from the outside
The CO removing device 18 also includes a gas heating pipe 18a for indirectly heating the CO removing catalyst 18b with a high temperature gas from the outside. The high-temperature gas generated in the auxiliary burner 22 is supplied to these gas heating pipes 16a and 18a when necessary. Incidentally. The CO scavenger 18 normally provides cooling and heats at start-up or when overcooled by liquid.
【００４３】上述した改質器１６は、混合原料ガスを水
素を含む改質ガス（水素含有ガス）に改質し、このガス
をＣＯ除去器１８に供給する。The above-mentioned reformer 16 reforms the mixed raw material gas into a reformed gas containing hydrogen (hydrogen-containing gas), and supplies this gas to the CO remover 18.
【００４４】またＣＯ除去器１８の上流側にはＣＯの選
択除去反応に必要な量の空気が供給できるようになって
おり、このＣＯ選択除去反応により、約２００〜３００
℃の最適使用温度を保持しながら改質器１６から供給さ
れた改質ガス（水素含有ガス）中のＣＯ濃度を低減す
る。Further, the amount of air required for the selective CO removal reaction can be supplied to the upstream side of the CO remover 18, and the CO selective removal reaction causes about 200 to 300
The CO concentration in the reformed gas (hydrogen-containing gas) supplied from the reformer 16 is reduced while maintaining the optimum use temperature of ° C.
【００４５】ＣＯ除去器１８を出た水素含有ガスは燃料
電池２０に供給され、ここで水素含有ガスと空気により
電気化学的に発電する。燃料電池２０を出た可燃性ガス
を含むアノード排ガスは、過濃燃焼バーナ１２と補助バ
ーナ２２に供給され可燃成分を燃焼させる。起動時には
主として補助バーナ２２で燃焼し、この燃焼熱を燃料、
改質器の間接加熱等に用いるのがよい。また、定常時に
はＮ2、ＣＯ2の発生を抑えるために別の燃焼器で燃焼さ
せてもよい。The hydrogen-containing gas discharged from the CO remover 18 is supplied to the fuel cell 20, where the hydrogen-containing gas and air are electrochemically generated. The anode exhaust gas containing the combustible gas that has left the fuel cell 20 is supplied to the rich combustion burner 12 and the auxiliary burner 22 to burn the combustible components. At the time of start-up, it burns mainly in the auxiliary burner 22, and this combustion heat is used as fuel,
It is preferably used for indirect heating of the reformer. Further, in a steady state, the combustion may be performed in another combustor in order to suppress the generation of N 2 and CO 2 .
【００４６】上述した燃料処理装置を用いた本発明の起
動方法は、過濃燃焼ステップ（Ａ）、蒸発加熱ステップ
（Ｂ）及び改質ステップ（Ｃ）からなる。過濃燃焼ステ
ップ（Ａ）では燃料を燃焼させて酸素を含まない高温ガ
スを発生させる。この燃焼は、燃料を燃空比１以上で行
うのがよい。蒸発加熱ステップ（Ｂ）では、燃料と水の
混合原料を蒸発させて加熱する。この温度は、起動時と
定常運転時とで、混合原料の蒸発量を変化させて、蒸発
加熱室における混合原料の温度を制御し、かつ改質触媒
及びＣＯ除去触媒を外部からの高温ガスにより加熱す
る。更に改質ステップ（Ｃ）では、加熱された混合原料
を水素含有ガスに改質する。The start-up method of the present invention using the above-mentioned fuel processor comprises a rich combustion step (A), an evaporative heating step (B) and a reforming step (C). In the rich combustion step (A), the fuel is burned to generate a high temperature gas containing no oxygen. This combustion is preferably performed with fuel having a fuel-air ratio of 1 or more. In the evaporation heating step (B), the mixed raw material of fuel and water is evaporated and heated. This temperature changes the evaporation amount of the mixed raw material at the time of startup and steady operation to control the temperature of the mixed raw material in the evaporation heating chamber, and the reforming catalyst and the CO removal catalyst by a high temperature gas from the outside. To heat. Further, in the reforming step (C), the heated mixed raw material is reformed into a hydrogen-containing gas.
【００４７】上述した本発明の構成によれば、過濃燃焼
バーナ１２で燃料を燃焼させて酸素を含まない高温ガス
を発生させるので、燃料として液体燃料（例えばメタノ
ール）を用いる場合でも、短時間で着火し、高温ガスを
短時間（数秒程度）で発生することができる。この高温
ガスは、メタノールと水の混合燃料を使用し、改質に適
したＳ／Ｃ＝１．５とした場合、燃空比１で約１６７０
Ｋ、燃空比１．１で約１４７０Ｋであり、約１２００℃
の高温（Ｔ１）を混合燃料を直接燃焼させた場合でも得
られることが試算により確認された。According to the above-described structure of the present invention, the fuel is burned by the rich combustion burner 12 to generate a high-temperature gas that does not contain oxygen. Therefore, even when a liquid fuel (for example, methanol) is used as the fuel, The high temperature gas can be ignited in a short time (about several seconds). This high-temperature gas uses a mixed fuel of methanol and water, and when the S / C ratio is 1.5, which is suitable for reforming, the fuel-air ratio is about 1670.
K, fuel-air ratio 1.1, about 1470K, about 1200 ℃
It was confirmed by trial calculation that the high temperature (T1) of (1) was obtained even when the mixed fuel was directly burned.
【００４８】また、蒸発加熱装置１４で燃料と水の混合
原料を蒸発させて所望の温度Ｔ２に加熱するので、温度
制御が容易にできる。蒸発加熱室１４ａにおける混合原
料ガスの温度（Ｔ２）は、起動時には昇温を速めるため
できるだけ高く（例えば８００℃程度）に設定し、定常
時には３５０℃前後に設定するのがよい。この結果、起
動時及び定常時において、改質器１６の上流側に流入す
る混合原料ガスの温度（Ｔ２）を触媒の耐熱温度を超え
ない温度（例えば３５０℃以下）に設定することができ
る。Further, since the mixed raw material of fuel and water is evaporated by the evaporation heating device 14 and heated to the desired temperature T2, the temperature control can be easily performed. The temperature (T2) of the mixed raw material gas in the evaporation heating chamber 14a is preferably set as high as possible (for example, about 800 ° C.) at the time of start-up to accelerate the temperature rise, and is set to about 350 ° C. at the steady state. As a result, the temperature (T2) of the mixed raw material gas flowing into the upstream side of the reformer 16 can be set to a temperature that does not exceed the heat resistant temperature of the catalyst (for example, 350 ° C. or less) at the time of startup and steady state.
【００４９】さらに加熱された混合原料を一体に形成さ
れた改質器１６とＣＯ除去器１８に直接供給できるの
で、放熱ロスを最小限度に抑えて、改質とＣＯ除去がで
き、燃料電池にそのまま供給して発電に用いることがで
きる。また、蒸発加熱装置１４は、改質器１６を出たガ
スとＣＯ除去器１８を出たガスを液体状態の混合原料で
所望の温度Ｔ３，Ｔ４まで冷却する液体原料チャンバ１
５を有するので、別の熱交換器なしで、改質器を出たガ
スとＣＯ除去器を出たガスとを所望の温度Ｔ３，Ｔ４ま
で冷却でき、全体を容易に小型化ができる。Further, since the heated mixed raw material can be directly supplied to the reformer 16 and the CO remover 18 which are integrally formed, the heat dissipation loss can be suppressed to the minimum and the reforming and the CO can be removed and the fuel cell can be used. It can be supplied as it is and used for power generation. Further, the evaporative heating device 14 cools the gas discharged from the reformer 16 and the gas discharged from the CO remover 18 with a mixed raw material in a liquid state to desired temperatures T3 and T4, respectively.
5, the gas discharged from the reformer and the gas discharged from the CO remover can be cooled to desired temperatures T3 and T4 without using a separate heat exchanger, and the entire size can be easily reduced.
【００５０】さらに、改質器１６は、改質触媒を外部か
らの高温ガスでは間接加熱するガス加熱管１６ａを内蔵
し、ＣＯ除去器１８は、ＣＯ除去触媒を外部からの高温
ガスでは間接加熱するガス加熱管１８ａを内蔵するの
で、別の熱交換器なしで、改質器とＣＯ除去器を加熱で
き、全体を容易に小型化ができる。従って、着火、燃
焼、加熱、改質、ＣＯ除去を短時間にできるので、燃料
電池の起動が短時間でできる。Further, the reformer 16 has a built-in gas heating pipe 16a for indirectly heating the reforming catalyst with a high temperature gas from the outside, and the CO remover 18 indirectly heating the CO removing catalyst with a high temperature gas from the outside. Since the gas heating pipe 18a for heating is built in, the reformer and the CO remover can be heated without a separate heat exchanger, and the overall size can be easily reduced. Therefore, since ignition, combustion, heating, reforming, and CO removal can be performed in a short time, the fuel cell can be started in a short time.
【００５１】また、改質器１６とＣＯ除去器１８は、過
濃燃焼バーナ１２を囲んで連続して形成されており、過
濃燃焼バーナ１２からの伝熱で改質器１６とＣＯ除去器
１８を加熱でき、放熱ロスを最小限度に抑えることがで
きる。The reformer 16 and the CO remover 18 are continuously formed so as to surround the rich combustion burner 12, and heat is transferred from the rich combustion burner 12 to the reformer 16 and the CO remover. 18 can be heated and the heat dissipation loss can be suppressed to the minimum.
【００５２】さらに、液体原料チャンバ１５は、ＣＯ除
去器１８とその前後の空洞部１７ａ，１７ｂを囲んで構
成されているので、液体原料チャンバ１５とＣＯ除去器
１８の前後の空洞部１７ａ，１７ｂとの熱交換により、
改質器１６を出たガス（温度Ｔ３）とＣＯ除去器１８を
出たガス（温度Ｔ４）を液体状態の混合原料で所望の温
度（例えば約１８０℃と約１００℃前後）まで冷却で
き、かつ全体を容易に小型化ができる。Further, since the liquid source chamber 15 is constituted by surrounding the CO remover 18 and the cavity portions 17a, 17b before and after it, the liquid source chamber 15 and the cavity portions 17a, 17b before and after the CO remover 18 are formed. By heat exchange with
The gas discharged from the reformer 16 (temperature T3) and the gas discharged from the CO remover 18 (temperature T4) can be cooled to a desired temperature (for example, about 180 ° C. and about 100 ° C.) with a mixed raw material in a liquid state, Moreover, the whole can be easily miniaturized.
【００５３】また、本発明の起動方法により、過濃燃焼
ステップ（Ａ）で燃料を燃焼させて高温ガスを発生させ
るので、燃料として液体燃料を用いる場合でも、短時間
で着火し、例えば１０００℃以上の高温ガスを短時間
（数秒程度）で発生することができる。Further, according to the starting method of the present invention, the high temperature gas is generated by burning the fuel in the rich combustion step (A). Therefore, even when the liquid fuel is used as the fuel, it ignites in a short time, for example, 1000 ° C. The above high-temperature gas can be generated in a short time (about several seconds).
【００５４】また、蒸発加熱ステップ（Ｂ）で燃料と水
の混合原料を蒸発させて所望の温度Ｔ２に加熱するの
で、温度制御が容易にできる。さらに改質ステップ
（Ｃ）において、混合ガスの保有する熱で下流側に位置
する改質触媒を直接及び間接に加熱することができるの
で、別の熱交換器なしで、改質器とＣＯ除去器を所望の
温度Ｔ２に加熱でき、全体を容易に小型化ができる。ま
た、更に、着火、燃焼、加熱、改質、ＣＯ除去を短時間
にできるので、燃料電池の起動が短時間でできる。Further, since the mixed raw material of fuel and water is evaporated and heated to the desired temperature T2 in the evaporation heating step (B), temperature control can be facilitated. Further, in the reforming step (C), the heat of the mixed gas can directly and indirectly heat the reforming catalyst located on the downstream side, so that the reformer and CO removal can be performed without another heat exchanger. The vessel can be heated to a desired temperature T2, and the whole can be easily downsized. Further, since ignition, combustion, heating, reforming, and CO removal can be performed in a short time, the fuel cell can be started in a short time.
【００５５】更に、起動時と定常運転時とで、起動時と
定常運転時とで、混合原料の蒸発量を変化させて、改質
器の入口ガス温度が触媒の耐熱温度を超えないように蒸
発加熱室における混合原料の温度を制御し、かつ改質触
媒及びＣＯ除去触媒を外部からの高温ガスにより加熱す
るので、一層速い起動ができるばかりでなく、触媒の加
熱を防止して触媒寿命を延ばし、高温におけるＣＯの発
生を抑制することができる。Further, the evaporation amount of the mixed raw material is changed between the start-up and the steady operation and the start-up and the steady operation so that the inlet gas temperature of the reformer does not exceed the heat resistant temperature of the catalyst. Since the temperature of the mixed raw material in the evaporative heating chamber is controlled and the reforming catalyst and the CO removal catalyst are heated by the high temperature gas from the outside, not only can the start-up be faster, but the heating of the catalyst can be prevented to extend the catalyst life. It can be extended and the generation of CO at high temperature can be suppressed.
【００５６】なお、本発明は上述した実施形態に限定さ
れず、本発明の要旨を逸脱しない範囲で種々に変更でき
ることは勿論である。The present invention is not limited to the above-mentioned embodiments, and it goes without saying that various modifications can be made without departing from the gist of the present invention.
【００５７】[0057]
【発明の効果】上述したように、本発明の燃料処理装置
とその起動方法は、燃料として液体燃料（例えばメタノ
ール）を用いる場合でも、短時間で起動でき、かつ容易
に小型化ができる、等の優れた効果を有する。As described above, the fuel processing apparatus and its starting method of the present invention can be started in a short time and can be easily downsized even when a liquid fuel (for example, methanol) is used as the fuel. Has the excellent effect of.
【図１】本発明による燃料処理装置の全体概念図であ
る。FIG. 1 is an overall conceptual diagram of a fuel processor according to the present invention.
【図２】本発明による燃料処理装置の具体的構成図であ
る。FIG. 2 is a specific configuration diagram of a fuel processing device according to the present invention.
【図３】従来の燃料処理装置の構成図である。FIG. 3 is a configuration diagram of a conventional fuel processing device.
１ 燃焼・改質触媒、２ 部分酸化改質器、４ 上流側
空気ライン、６ 下流側空気ライン、８ 流量制御器、
１０ 燃料処理装置、１２ 過濃燃焼バーナ、１２ａ
燃焼室、１２ｂ 燃料噴射器、１４ 蒸発加熱装置、１
４ａ 蒸発加熱室、１４ｂ 原料噴霧口、１４ｃ フィ
ルタ、１５ 液体原料チャンバ、１６ 改質器、１６ａ
ガス加熱管、１６ｂ 改質触媒、１７ａ 第１空洞
部、１７ｂ 第２空洞部、１８ ＣＯ除去器、１８ａ
ガス加熱管、１８ｂ ＣＯ除去触媒、２０ 燃料電池
（ＰＥＦＣ）、２２ 補助バーナ1 combustion / reforming catalyst, 2 partial oxidation reformer, 4 upstream air line, 6 downstream air line, 8 flow controller,
10 fuel processor, 12 rich burner, 12a
Combustion chamber, 12b Fuel injector, 14 Evaporative heating device, 1
4a Evaporative heating chamber, 14b Raw material spray port, 14c Filter, 15 Liquid raw material chamber, 16 Reformer, 16a
Gas heating pipe, 16b reforming catalyst, 17a first cavity, 17b second cavity, 18 CO remover, 18a
Gas heating tube, 18b CO removal catalyst, 20 fuel cell (PEFC), 22 auxiliary burner
Claims (3)
過濃燃焼バーナ（１２）と、燃料と水の混合原料を蒸発
させて加熱する蒸発加熱装置（１４）と、混合原料を水
素含有ガスに改質する改質器（１６）と、一酸化炭素を
選択的に除去するＣＯ除去器（１８）とを備えた一体型
の燃料処理装置であって、 前記蒸発加熱装置（１４）は、改質器（１６）を出たガ
スとＣＯ除去器（１８）を出たガスを液体状態の混合原
料で冷却する液体原料チャンバ（１５）を有し、 前記改質器（１６）は、改質触媒を外部からの高温ガス
で間接加熱するガス加熱管（１６ａ）を内蔵し、前記Ｃ
Ｏ除去器（１８）は、ＣＯ除去触媒を外部からの高温ガ
スで間接加熱するガス加熱管（１８ａ）を内蔵する、こ
とを特徴とする燃料処理装置。1. A rich combustion burner (12) for combusting a fuel to generate a high temperature gas, an evaporation heating device (14) for evaporating and heating a mixed raw material of fuel and water, and a hydrogen-containing gas for the mixed raw material. An integrated fuel treatment device comprising a reformer (16) for reforming into carbon dioxide and a CO remover (18) for selectively removing carbon monoxide, wherein the evaporation heating device (14) comprises: There is a liquid raw material chamber (15) for cooling the gas discharged from the reformer (16) and the gas discharged from the CO remover (18) with a mixed raw material in a liquid state, and the reformer (16) is A gas heating pipe (16a) for indirectly heating the high quality catalyst with a high temperature gas from the outside,
The O remover (18) has a built-in gas heating pipe (18a) that indirectly heats a CO removal catalyst with a high temperature gas from the outside.
８）は、過濃燃焼バーナ（１２）を囲んで連続して形成
されており、 前記液体原料チャンバ（１５）は、ＣＯ除去器（１８）
とその前後の空洞部（１７ａ、１７ｂ）を囲み、該空洞
部との熱交換により、改質器（１６）を出たガスとＣＯ
除去器（１８）を出たガスを液体状態の混合原料で冷却
する、ことを特徴とする請求項１に記載の燃料処理装
置。2. The reformer (16) and CO remover (1)
8) is formed continuously around the rich combustion burner (12), and the liquid raw material chamber (15) is a CO remover (18).
And the cavities (17a, 17b) in front of and behind it, and the gas and CO that have left the reformer (16) by heat exchange with the cavities.
The fuel processing device according to claim 1, wherein the gas discharged from the remover (18) is cooled by the mixed raw material in a liquid state.
過濃燃焼ステップ（Ａ）と、燃料と水の混合原料を蒸発
させて加熱する蒸発加熱ステップ（Ｂ）と、加熱された
混合原料を水素含有ガスに改質する改質ステップ（Ｃ）
と、を備え、 起動時と定常運転時とで、混合原料の蒸発量を変化させ
て、蒸発加熱室における混合原料の温度を制御し、かつ
改質触媒及びＣＯ除去触媒を外部からの高温ガスにより
加熱する、ことを特徴とする燃料処理装置の起動方法。3. A rich combustion step (A) of combusting a fuel to generate a high temperature gas, an evaporation heating step (B) of evaporating and heating a mixed raw material of fuel and water, and a heated mixed raw material. Reforming step (C) for reforming to hydrogen-containing gas
The temperature of the mixed raw material in the evaporation heating chamber is controlled by changing the evaporation amount of the mixed raw material at the time of start-up and at the time of steady operation, and the reforming catalyst and the CO removal catalyst are supplied from the high temperature gas from the outside. A method for starting a fuel processing apparatus, comprising:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002034148A JP4000860B2 (en) | 2002-02-12 | 2002-02-12 | Fuel processing apparatus and starting method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002034148A JP4000860B2 (en) | 2002-02-12 | 2002-02-12 | Fuel processing apparatus and starting method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2003238110A true JP2003238110A (en) | 2003-08-27 |
| JP4000860B2 JP4000860B2 (en) | 2007-10-31 |
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ID=27776738
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2002034148A Expired - Fee Related JP4000860B2 (en) | 2002-02-12 | 2002-02-12 | Fuel processing apparatus and starting method thereof |
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| Country | Link |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009059667A (en) * | 2007-09-03 | 2009-03-19 | Honda Motor Co Ltd | Fuel cell system, and operation method thereof |
-
2002
- 2002-02-12 JP JP2002034148A patent/JP4000860B2/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009059667A (en) * | 2007-09-03 | 2009-03-19 | Honda Motor Co Ltd | Fuel cell system, and operation method thereof |
| US8557457B2 (en) | 2007-09-03 | 2013-10-15 | Honda Motor Co., Ltd. | Fuel cell system and method of operating the fuel cell system |
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| Publication number | Publication date |
|---|---|
| JP4000860B2 (en) | 2007-10-31 |
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