JPS62216634A - Reformer for fuel - Google Patents
Reformer for fuelInfo
- Publication number
- JPS62216634A JPS62216634A JP61060073A JP6007386A JPS62216634A JP S62216634 A JPS62216634 A JP S62216634A JP 61060073 A JP61060073 A JP 61060073A JP 6007386 A JP6007386 A JP 6007386A JP S62216634 A JPS62216634 A JP S62216634A
- Authority
- JP
- Japan
- Prior art keywords
- reaction tube
- reaction
- reforming
- gas
- tube
- 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
- 239000000446 fuel Substances 0.000 title claims description 41
- 238000006243 chemical reaction Methods 0.000 claims abstract description 102
- 239000003054 catalyst Substances 0.000 claims abstract description 81
- 238000002407 reforming Methods 0.000 claims abstract description 60
- 239000007789 gas Substances 0.000 claims abstract description 35
- 239000012495 reaction gas Substances 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 7
- 230000000717 retained effect Effects 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 27
- 238000006057 reforming reaction Methods 0.000 abstract description 21
- 239000001257 hydrogen Substances 0.000 abstract description 12
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 12
- 238000012546 transfer Methods 0.000 abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 10
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 2
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 230000003197 catalytic effect Effects 0.000 abstract 2
- 239000008246 gaseous mixture Substances 0.000 abstract 2
- 238000002485 combustion reaction Methods 0.000 description 16
- 230000000694 effects Effects 0.000 description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000009792 diffusion process Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 238000010248 power generation Methods 0.000 description 5
- 238000007751 thermal spraying Methods 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000011248 coating agent Substances 0.000 description 3
- 238000000576 coating method Methods 0.000 description 3
- 239000000567 combustion gas Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- 230000035699 permeability Effects 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000000151 deposition Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000013372 meat Nutrition 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- 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
- H01M8/0625—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 in a modular combined reactor/fuel cell structure
- H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Energy (AREA)
- Manufacturing & Machinery (AREA)
- Engineering & Computer Science (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Fuel Cell (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は燃料改質器に係り、特にコンパクトで迅速な負
荷追従性が要求される燃料電池発電装置に使用されるの
に好適な燃料改質器に関する。Detailed Description of the Invention [Field of Industrial Application] The present invention relates to a fuel reformer, and particularly to a fuel reformer suitable for use in a fuel cell power generation device that is required to be compact and quick to follow load. Regarding pawns.
従来より化学工業で用いられている燃料改質器と異なり
、コンパクトで迅速な負荷追従性が要求される燃料電池
発電装置装置に使用する燃料改質器として１例えば米国
特許第４０９８５８９号に開示されたものが存在する。Unlike fuel reformers conventionally used in the chemical industry, a fuel reformer for use in a fuel cell power generation device that is compact and requires quick load followability is disclosed in U.S. Pat. No. 4,098,589, for example. There are things that exist.
この従来例では、二重管の間隙に充填された円筒状の改
質触媒層に流れる反応ガスの流れ方向に対して、燃焼ガ
スおよび改質ガスを対向流とし、改質触媒層を内外より
加熱するとともに、二重管の外側に伝熱粒子を充填する
ことにより燃焼ガスから反応ガスへの伝熱を促進する構
造となっている。In this conventional example, the combustion gas and reformed gas flow in counterflow to the flow direction of the reaction gas flowing into the cylindrical reforming catalyst layer filled in the gap between the double pipes, and the reforming catalyst layer is inserted into the reforming catalyst layer from the inside and outside. In addition to heating, the outside of the double tube is filled with heat transfer particles to promote heat transfer from the combustion gas to the reaction gas.
また、二重管式反応管内の改質触媒層の半径方向温度分
布改善と伝熱促進に関して、改質触媒層内に金属球を混
入した構造の燃料改質器（実開昭６０−８９２３４号）
や改質触媒と接触する反応管内壁面に管軸直交方向の、
あるいは管軸方向の、あるいは螺旋状の溝を形成した燃
料改質器（実開昭６０−８［１２３５号）が存在する。In addition, with regard to improving the radial temperature distribution and promoting heat transfer of the reforming catalyst layer in the double-tube reaction tube, we have developed a fuel reformer with a structure in which metal spheres are mixed in the reforming catalyst layer (Utility Model Application No. 60-89234). )
Orthogonal to the tube axis, on the inner wall surface of the reaction tube in contact with the reforming catalyst.
Alternatively, there is a fuel reformer (Utility Model Application Publication No. 1235, 1983) in which grooves are formed in the tube axis direction or in a spiral shape.
しかし、上記各種従来例のように、触媒粒子充填層を還
流する流体を外部から加熱する場合では、反応管管壁と
触媒粒子が接触するところの粒子の空隙率は大きいため
１反応ガスの流れの乱れる程度が小さく、かつ触媒粒子
と触媒粒子間との接触に比べると、粒子の反応管管壁間
の接触点の数がかなり少ないので、反応管管壁近傍にお
ける伝熱能力が低下する問題がある。However, when the fluid flowing back through the catalyst particle packed bed is heated from the outside, as in the various conventional examples described above, the porosity of the particles where the reaction tube wall and the catalyst particles contact is large, so the flow of one reaction gas is The degree of turbulence is small, and the number of contact points between particles and the walls of the reaction tube is quite small compared to the contact between catalyst particles, so the heat transfer ability near the walls of the reaction tube is reduced. There is.
本発明はかかる問題点を解決するために１反応管管壁近
傍の伝熱能力を向上させることにより。The present invention solves these problems by improving the heat transfer ability near the wall of the reaction tube.
迅速な改質反応を行い得る燃料改質器を提供することを
目的とする。An object of the present invention is to provide a fuel reformer that can perform a rapid reforming reaction.
上記目的を達成するために１本発明は、改質触媒が充填
された反応管内に反応ガスが供結され、当該反応ガスを
改質ガスに変換してなる燃料改質器において、前記反応
管壁面に改質触媒が保持されてなることを特徴とする燃
料改質器である。In order to achieve the above object, the present invention provides a fuel reformer in which a reaction gas is connected to a reaction tube filled with a reforming catalyst and the reaction gas is converted into a reformed gas. This is a fuel reformer characterized by having a reforming catalyst held on the wall surface.
上記構成によれば、反応管管壁に保持された触媒により
、反応ガスまたは改質ガスの流れの乱れる程度が大きく
なり、反応管管壁と触媒粒子が接する部分の触媒粒子の
空隙率を小さくすることができる。さらに９反応管管壁
と触媒粒子との間の接触点の数を増加させるので５反応
管管壁近傍における伝熱能力が向上することになる。ま
た１反応管管壁に保持された触媒自身で吸熱反応が起こ
るため、一層伝熱が促進されることになる。According to the above configuration, the degree of turbulence in the flow of the reaction gas or reformed gas is increased due to the catalyst held on the reaction tube wall, and the porosity of the catalyst particles is reduced at the portion where the reaction tube wall and the catalyst particles are in contact. can do. Furthermore, since the number of contact points between the wall of the 9th reaction tube and the catalyst particles is increased, the heat transfer ability near the wall of the 5th reaction tube is improved. Furthermore, since an endothermic reaction occurs within the catalyst itself held on the wall of one reaction tube, heat transfer is further promoted.
次に、本発明に係る燃料改質器の実施例を添付図面に従
って詳説する。Next, embodiments of the fuel reformer according to the present invention will be described in detail with reference to the accompanying drawings.
第１図は、その一実施例を示す断面構成図である０本実
施例では、単管式反応管で構成される場合の燃料改質器
を示している。FIG. 1 is a cross-sectional configuration diagram showing one embodiment of the present invention. This embodiment shows a fuel reformer constructed of a single-tube reaction tube.
第１図において、燃料改質器の円筒状の反応管１の一端
にはフランジ２が設けられ、そのフランジ２に対向する
ように、反応ガス１１を導く導管３を有するフランジ４
が、パツキン７を挾んで数本のボルト５およびナツト６
により接合されている。In FIG. 1, a flange 2 is provided at one end of a cylindrical reaction tube 1 of a fuel reformer, and a flange 4 having a conduit 3 for guiding a reaction gas 11 faces the flange 2.
However, while holding the packing 7, I removed several bolts 5 and nuts 6.
It is joined by
燃料改質器の反応管１の他端には、改質ガス１２の出口
となる導管８が設けられている。A conduit 8 serving as an outlet for the reformed gas 12 is provided at the other end of the reaction tube 1 of the fuel reformer.
上記反応管１内には、改質触媒粒子９が充填されており
１反応管１の内管面に改質触媒１０が保持されている。The reaction tube 1 is filled with reforming catalyst particles 9, and a reforming catalyst 10 is held on the inner surface of each reaction tube 1.
この改質触媒１０の反応管１壁面への保持は、Ｗｊ射、
メッキ等の手段により、触媒を一面にコーティングもし
くは分散して付着保持する方法、多孔質に触媒粒子を拡
散する方法などがある。This reforming catalyst 10 is held on the wall surface of the reaction tube 1 by Wj radiation,
There are a method in which the catalyst is coated or dispersed over one surface and retained by means of plating, and a method in which the catalyst particles are diffused in a porous structure.
次に１本実施例の動作について説明する。反応ガス１１
、例えば炭化水素と水蒸気の混合ガスが導管３を介して
反応管内に供結される。なお、反応ガスとして、この他
アルコール等を用いることも可能である。Next, the operation of this embodiment will be explained. Reaction gas 11
A mixed gas of, for example, hydrocarbon and steam is connected via conduit 3 into the reaction tube. In addition, it is also possible to use alcohol or the like as the reaction gas.
反応ガスが供結された反応管１内では、比較的大きな吸
熱反応が起きるため１反応管１の外部から加熱触媒１３
により改質触媒粒子９が充填されている部分を加熱し、
当該反応管１を約８００℃程度の温度に維持するように
する。メタンと水蒸気の混合ガスである反応ガス１１は
、導管３より反応管１内に送り込まれたのち、改質触媒
粒子９の充填層および反応管１の内壁面に付着している
改質触媒１０の表面および内部にて改質反応を起こし、
水素富化ガスに改質されていく、このとき、反応管１の
外部より熱を供結され、改質反応が持続していく。反応
ガス１１は、所定の改質触媒粒子９の充填層を通過する
と、水素富化ガスである改質ガス１２となって、導管８
より反応管１外に出ていく、この反応管１から出た水素
富化ガスは。Because a relatively large endothermic reaction occurs in the reaction tube 1 to which the reaction gas is connected, the heated catalyst 13 is heated from the outside of the reaction tube 1.
heating the part filled with reforming catalyst particles 9,
The reaction tube 1 is maintained at a temperature of about 800°C. The reaction gas 11, which is a mixed gas of methane and water vapor, is sent into the reaction tube 1 through the conduit 3, and then the reforming catalyst 11 adhering to the packed bed of reforming catalyst particles 9 and the inner wall surface of the reaction tube 1 is introduced. A modification reaction occurs on the surface and inside of the
At this time, heat is supplied from the outside of the reaction tube 1 to continue the reforming reaction. When the reaction gas 11 passes through a packed bed of predetermined reforming catalyst particles 9, it becomes a reformed gas 12, which is a hydrogen-enriched gas, and is passed through a conduit 8.
The hydrogen-enriched gas coming out of the reaction tube 1 goes out of the reaction tube 1.
例えば燃料電池発電装置においては、アノードガスとし
て利用される。For example, in a fuel cell power generation device, it is used as an anode gas.
上記本実施例では、触媒粒子が反応管壁面にコーティン
グされているために１反応流体が反応管壁面を流れる際
の流れの乱れる程度が大きくなるとともに１反応管管壁
と触媒粒子が接するところの粒子の空隙率は小さくなる
。したがって１反応管管壁と触媒粒子との間の接触点の
数が増加するため、反応管管壁近傍における伝熱能力が
向上する。さらに１１１反応管管壁コーティングされた
触媒それ自身で、吸熱反応が起こるため、加熱媒体１３
からの熱供結が一層促進し、伝熱がさらに促進される。In this example, since the catalyst particles are coated on the wall surface of the reaction tube, the degree of turbulence in the flow when one reaction fluid flows on the wall surface of the reaction tube becomes large, and the contact between the wall surface of one reaction tube and the catalyst particles increases. The porosity of the particles becomes smaller. Therefore, the number of contact points between the wall of one reaction tube and the catalyst particles is increased, so that the heat transfer ability in the vicinity of the wall of the reaction tube is improved. Furthermore, since an endothermic reaction occurs in the catalyst itself coated on the wall of the 111 reaction tube, the heating medium 13
This further promotes heat connection from the inside and further promotes heat transfer.
上記本実施例によれば、燃料改質器の反応管内壁面に改
質触媒を付着するようにしたので、燃料改質器の反応管
の軸方向の温度分布の均一化を図ることができる。すな
わち、触媒層を設けた部分で吸熱反応が起きるため、反
応管の過熱を防ぐことができ、反応管の温度分布が均一
となる。したがって、付着させる改質触媒の位置と、付
着分布状況によって、温度均一化を任意に行うことがで
き、その結果１反応管の寿命を向上させることができる
。According to this embodiment, since the reforming catalyst is attached to the inner wall surface of the reaction tube of the fuel reformer, the temperature distribution in the axial direction of the reaction tube of the fuel reformer can be made uniform. That is, since an endothermic reaction occurs in the portion where the catalyst layer is provided, overheating of the reaction tube can be prevented and the temperature distribution of the reaction tube can be made uniform. Therefore, temperature uniformity can be arbitrarily achieved depending on the position of the deposited reforming catalyst and the deposition distribution, and as a result, the life of one reaction tube can be improved.
次に１本発明の第２の実施例を説明する。第２図はその
断面構成図である０本実施例では、二重管式反応管で構
成される場合の燃料改質器を示している。Next, a second embodiment of the present invention will be described. FIG. 2 is a sectional view of the fuel reformer. In this embodiment, a fuel reformer is constructed of double-tube reaction tubes.
第２図において１反応管１は、それ自身外管４１を構成
するとともに、内部に内管１４を外管４１と同軸位置に
なるように包含している。改質触媒粒子９は、外管４１
と内管１４との１１１に形成される環状の隙間に充填さ
れている。一方、外管４１および内管１４が改質触媒粒
子９と接するそれぞれの壁面には、改質触媒１０が溶射
によって付着されている。In FIG. 2, one reaction tube 1 itself constitutes an outer tube 41 and includes an inner tube 14 therein so as to be coaxial with the outer tube 41. The reforming catalyst particles 9 are inserted into the outer tube 41
An annular gap formed at 111 between the inner tube 14 and the inner tube 14 is filled. On the other hand, the reforming catalyst 10 is attached by thermal spraying to the respective wall surfaces of the outer tube 41 and the inner tube 14 in contact with the reforming catalyst particles 9.
次に１本実施例の動作について説明する。メタンと水蒸
気の混合ガスである反応ガス１１は、燃料改質器内の改
質触媒粒子９が充填された充填層に向って流入し、その
充填層内および外管４１と内管１４との管壁にそれぞれ
付着された改質触媒１０の表面および内部にて改質反応
を起こし、水素富化ガスに変わっていく。このとき、改
質反応に必要な熱量の約７５％程度が、外管４１の外部
から加熱媒体１３によって補給される。残りの約２５％
の熱量は、改質ガス１２が内管１４内を通ることによっ
て、反応ガス１１との熱交換を行うことで補われる。生
成した改質ガス１２は、内管１４を経由して燃料改質器
の系外へ導かれる。Next, the operation of this embodiment will be explained. The reaction gas 11, which is a mixed gas of methane and water vapor, flows toward the packed bed filled with reforming catalyst particles 9 in the fuel reformer, and flows into the packed bed and between the outer pipe 41 and the inner pipe 14. A reforming reaction occurs on the surface and inside of the reforming catalyst 10 attached to each tube wall, and the gas is converted into hydrogen-enriched gas. At this time, about 75% of the heat required for the reforming reaction is supplied from the outside of the outer tube 41 by the heating medium 13. The remaining approximately 25%
The amount of heat is compensated by the reformed gas 12 passing through the inner tube 14 and exchanging heat with the reaction gas 11. The generated reformed gas 12 is led out of the fuel reformer system via the inner pipe 14.
上記本実施例によれば、燃料数１ｆｔｔｏの外管の内壁
面および内管の外壁面に改質触媒を付着するようにした
ので、燃料改質器の反応管の軸方向温度分布均一化を、
付着させる改質触媒の位置と分布状況によって任意に達
成することができるという効果と、二重管の外管径は、
単管式の場合に比べて大きいので、外管の内壁面への改
質触媒の付着が容易であり、かつ内情については外壁面
への改質触媒を付着させればよいので、同じく改質触媒
の付着が容易であるという効果がある。また、溶射等に
よって触媒を付着させるときの条件を変えることで、付
着の状Ｓ（大きさ、形状）を変えられるので、反応管管
壁における反応流体の流れの乱れ具合いをさらに増加す
ることもできる。According to this embodiment, the reforming catalyst is attached to the inner wall surface of the outer tube and the outer wall surface of the inner tube, which has 1 ftto of fuel, so that the temperature distribution in the axial direction of the reaction tube of the fuel reformer can be made uniform. ,
The effect can be achieved arbitrarily depending on the position and distribution of the attached reforming catalyst, and the outer diameter of the double pipe is
Since it is larger than the single tube type, it is easy to attach the reforming catalyst to the inner wall of the outer tube. This has the effect that the catalyst can be easily attached. In addition, by changing the conditions when depositing the catalyst by thermal spraying, etc., the state of deposit S (size, shape) can be changed, so it is possible to further increase the degree of turbulence in the flow of the reaction fluid on the reaction tube wall. can.
次に、本発明の第３の実施例を第３図に従い説明する。Next, a third embodiment of the present invention will be described with reference to FIG.
第３図はその断面構成図を示したものであり、二重管式
の場合である。FIG. 3 shows a sectional view of the structure, which is a double pipe type.
本実施例では、第２図の実施例に加え、内管１４の内壁
面にも改質触媒１５を付着させた場合を示す。In this embodiment, in addition to the embodiment shown in FIG. 2, a reforming catalyst 15 is also attached to the inner wall surface of the inner tube 14.
第３図において、その動作は１反応ガス１１が燃料改質
器内の改質触媒粒子の充填層および外管４１および内管
１４の管壁に付着された改質触媒１０の表面および内部
において改質され、改質ガスとなる。この改質ガス１２
は、さらに溶射あるいは塗布等によって内管１４の内壁
面に付着された改質触媒１５と接触することにより、改
質ガス１２の一部がさらに改質触媒１５の表面および内
部において改質される。In FIG. 3, the operation is such that a reaction gas 11 is applied to the packed bed of reforming catalyst particles in the fuel reformer and to the surface and inside of the reforming catalyst 10 attached to the pipe walls of the outer pipe 41 and the inner pipe 14. It is reformed and becomes reformed gas. This reformed gas 12
Further, by contacting with the reforming catalyst 15 attached to the inner wall surface of the inner pipe 14 by thermal spraying or coating, a part of the reformed gas 12 is further reformed on the surface and inside of the reforming catalyst 15. .
上記本実施例によれば、第２図の実施例の効果に加えて
、改質ガスがさらに内管の内壁に保持した改質触媒と接
触し、実質的にガスと改質触媒との接触時間が長くなる
ので、改質率を平衡時の改質率、すなわち最大の改質率
に近づけることができる。しかも、その効果をほとんど
圧力損失の増加なしに実現できることになる。According to the present embodiment described above, in addition to the effects of the embodiment shown in FIG. Since the time becomes longer, the reforming rate can be brought closer to the reforming rate at equilibrium, that is, the maximum reforming rate. Moreover, this effect can be achieved with almost no increase in pressure loss.
次に、本発明の第４の実施例を第４図に従い説明する。Next, a fourth embodiment of the present invention will be described with reference to FIG.
第４図はその断面構成図を示したものであり、単管の反
応管の場合を示している。FIG. 4 shows a cross-sectional configuration diagram thereof, and shows the case of a single reaction tube.
第４図において、反応管１の内壁面には改質触媒１０が
、外壁面には燃焼触媒１６がそれぞれ溶射もしくは塗布
等の手段によって付着されている。In FIG. 4, a reforming catalyst 10 is attached to the inner wall surface of the reaction tube 1, and a combustion catalyst 16 is attached to the outer wall surface by thermal spraying, coating, or the like.
反応管１の内部に導入された反応ガス１１は、改質触媒
１０の表面および内部にて改質反応を起こし、水素に富
んだ改質ガス１２となって反応管１から放出される。一
方、反応管１の外部には１反応管１を取り囲むように、
空気と可燃ガスの混合燃料ガス１７が送り込まれ、その
混合燃料ガス１７は燃焼触媒１６の表面および内部にて
燃焼し。The reaction gas 11 introduced into the reaction tube 1 undergoes a reforming reaction on the surface and inside of the reforming catalyst 10, and is released from the reaction tube 1 as hydrogen-rich reformed gas 12. On the other hand, on the outside of the reaction tube 1, so as to surround the reaction tube 1,
A mixed fuel gas 17 of air and combustible gas is fed, and the mixed fuel gas 17 burns on the surface and inside of the combustion catalyst 16.
燃焼ガス１３となって反応管１より離れる。以上の経過
において、燃焼触媒１６での燃焼反応による発熱台が１
反応管１の管壁を通して、改質触媒１０での改質反応の
吸熱台を充当される。なお。It becomes combustion gas 13 and leaves the reaction tube 1. In the above process, the number of heating units due to the combustion reaction in the combustion catalyst 16 is 1.
It passes through the tube wall of the reaction tube 1 and serves as an endothermic table for the reforming reaction in the reforming catalyst 10. In addition.
反応管１内には、改質触媒粒子が充填されていてよい。The reaction tube 1 may be filled with reforming catalyst particles.
本実施例によれば、前記各実施例の効果に加え。According to this embodiment, in addition to the effects of each of the embodiments described above.
燃焼反応による熱の発生する位置と、改質反応によって
熱の吸収される位置との距離を最短にできるので、燃料
改質器の熱効率が向上し、また、燃焼触媒による燃焼と
したため、騒音およびＮＯｘ等が少なくできるという効
果がある。The distance between the location where heat is generated by the combustion reaction and the location where heat is absorbed by the reforming reaction can be minimized, improving the thermal efficiency of the fuel reformer.In addition, since combustion is performed using a combustion catalyst, noise and This has the effect of reducing NOx, etc.
次に１本発明の第５の実施例について説明する。Next, a fifth embodiment of the present invention will be described.
第５図はその断面構成図を示したものであり、単管式の
燃料改質器の場合を示す。FIG. 5 shows a cross-sectional configuration diagram thereof, and shows the case of a single-tube fuel reformer.
第５図において、反応管１はガス透過性材料で構成され
ている。ガス透過性材料で構成することにより、例えば
水素分子を容易に透過する一方で、酸素分子を透過しに
くいようにすることができる。In FIG. 5, the reaction tube 1 is constructed of a gas-permeable material. By using a gas-permeable material, it is possible to easily allow hydrogen molecules to pass through, while making it difficult for oxygen molecules to pass through, for example.
ガス透過性材料としては、所定の大きさの孔を数多く有
するセラミックス等がある。Examples of gas permeable materials include ceramics having many pores of a predetermined size.
上記ガス透過性材料よりなる反応管１の内壁面には、改
質触媒１０が溶射等の手段によって付着されている。前
記反応管１の外部には１反応管１を取り囲むように予熱
された空気１８が供結されている。一方、反応管１の内
部に導入された反応ガス１１は、改質触媒１０の表面お
よび内部にて改質反応を受け、水素に富んだ改質ガス１
２となって１反応管１から取り出される。A reforming catalyst 10 is attached to the inner wall surface of the reaction tube 1 made of the gas permeable material by means such as thermal spraying. Preheated air 18 is connected to the outside of the reaction tube 1 so as to surround the reaction tube 1 . On the other hand, the reaction gas 11 introduced into the reaction tube 1 undergoes a reforming reaction on the surface and inside of the reforming catalyst 10, and the hydrogen-rich reformed gas 1
2 and taken out from 1 reaction tube 1.
上記反応管１の管壁の内壁面から所定の肉Ｊ！メ部分で
は、水素分子を容易に透過し、かつ酸素分子は透過され
にくいような構造となっている。すなわち、上記したよ
うに、所定の大きさをもつ多数の孔が１反応管１に設け
られているからである。A predetermined amount of meat J! from the inner wall surface of the tube wall of the reaction tube 1! The main part has a structure that allows hydrogen molecules to pass through easily and oxygen molecules to hardly pass through. That is, as described above, one reaction tube 1 is provided with a large number of holes having a predetermined size.
ガス選択透過性のある多孔質性材料の使用によって、改
質反応の結果得られた水素１９の一部が、多孔質の改質
触媒１０およびそのガス選択透過性のある反応管１の管
壁内部を、反応管１の外側方向へ透過する。By using a porous material having gas selective permeability, a part of the hydrogen 19 obtained as a result of the reforming reaction is transferred to the porous reforming catalyst 10 and the tube wall of the reaction tube 1 having gas selective permeability. The inside of the reaction tube 1 is transmitted toward the outside.
一方、ガス選択透過性を有する反応管管壁部分以外の反
応管管壁は、酸素分子を容易に透過する大きさの孔が、
数多く占めている。これにより、改質反応で得られた水
＃Ｊ１９の一部と、空気１８中の酸素とが、多孔質の反
応管１の内部で接触し。On the other hand, the reaction tube wall other than the reaction tube wall portion having gas selective permeability has pores large enough to allow oxygen molecules to pass through easily.
It occupies a large number. As a result, a part of water #J19 obtained by the reforming reaction and oxygen in the air 18 come into contact inside the porous reaction tube 1.
燃焼反応を起こす。その結果、改質反応による吸熱台の
熱を連続的かつ直接的に補給することができる。反応管
１内には、改質触媒粒子が充填されていてよい。Causes a combustion reaction. As a result, the heat of the heat absorption table due to the reforming reaction can be continuously and directly replenished. The reaction tube 1 may be filled with reforming catalyst particles.
上記本実施例によれば、多孔質の反応管内部で燃焼反応
を起こさせ、その燃焼熱を改質反応の吸熱台に当てる構
成としたため、燃料改質器の熱効率を向上することがで
きる。According to this embodiment, the combustion reaction is caused inside the porous reaction tube, and the heat of combustion is applied to the heat absorption table for the reforming reaction, so that the thermal efficiency of the fuel reformer can be improved.
次に、本発明の第６の実施例について説明する。Next, a sixth embodiment of the present invention will be described.
第６図はその断面構成図を示したものであり、単管式の
燃料改質器の場合である。FIG. 6 shows a cross-sectional configuration diagram of the fuel reformer, which is a single-tube type fuel reformer.
第６図において、前記第５図の実施例で説明したガス透
過性材料よりなる反応管１の内壁面に付着させた改質触
媒１０を、その反応管１の内壁面から適当な肉厚部分ま
でに拡散させて保持している。改質触媒（Ｎｉ）の拡散
は、セラミックにニッケルを拡散させることにより実現
することができる。In FIG. 6, the reforming catalyst 10 attached to the inner wall surface of the reaction tube 1 made of the gas-permeable material explained in the embodiment of FIG. It has been diffused and maintained. Diffusion of the reforming catalyst (Ni) can be achieved by diffusing nickel into ceramic.
上記反応管１の外部には１反応管１を取り囲むように、
予熱された空気１８が送り込まれている。On the outside of the reaction tube 1, so as to surround the reaction tube 1,
Preheated air 18 is being fed.
反応ガス１１は、前記改質触媒１０の拡散部分２０にお
いて改質反応を受け、水素に富んだ改質ガス１２となっ
て１反応管１から排出される。改質反応の結果得られた
水素１９の一部が、反応管１の管壁内で空気１８中の酸
素と接触し、燃焼反応を起こすことにより、改質反応に
よる吸熱台の熱を連続的かつ直接的に補給する。The reaction gas 11 undergoes a reforming reaction in the diffusion section 20 of the reforming catalyst 10, becomes hydrogen-rich reformed gas 12, and is discharged from one reaction tube 1. A part of the hydrogen 19 obtained as a result of the reforming reaction comes into contact with oxygen in the air 18 within the wall of the reaction tube 1 and causes a combustion reaction, thereby continuously dissipating the heat in the heat absorbing table due to the reforming reaction. and supply directly.
上記反応管１に拡散された改質触媒は、コーティングさ
れている場合に比べて、その耐剥離性が向上する。また
、内部に拡散した触媒部分で１反応ガスがかかる部分に
拡散することにより、その部分において改質反応が起こ
る。The reforming catalyst diffused into the reaction tube 1 has improved peeling resistance compared to a case where the reforming catalyst is coated. Furthermore, when one reaction gas diffuses into the catalyst portion that has diffused into the interior, a reforming reaction occurs in that portion.
上記本実施例によれば、第５図で説明した実施例におけ
る効果に加え、発熱部と吸熱部の位置がさらに近いため
、燃料改質器の熱効率が一層向上する。また１反応管管
壁における温度分布の差が小さくなり１反応管の寿命が
長くなる。According to this embodiment, in addition to the effects of the embodiment described in FIG. 5, the heat generating part and the heat absorbing part are located closer to each other, so that the thermal efficiency of the fuel reformer is further improved. Furthermore, the difference in temperature distribution on the wall of one reaction tube becomes smaller, and the life of one reaction tube becomes longer.
次に、本発明の第７の実施例について説明する。Next, a seventh embodiment of the present invention will be described.
第７図はその断面構成図を示したものであり、単管式の
燃料改質器である場合を示す。FIG. 7 shows a cross-sectional configuration diagram thereof, and shows the case where it is a single-tube fuel reformer.
第７図では、第６図で説明した実施例に加えて。In addition to the embodiment described in FIG. 6, FIG.
ガス透過性材料よりなる反応管１の外壁面から、適当な
肉厚部分までに燃焼触媒１６を拡散させて保持したこと
を特徴とする。It is characterized in that the combustion catalyst 16 is diffused and held from the outer wall surface of the reaction tube 1 made of a gas-permeable material to an appropriate wall thickness.
反応管１の外部には１反応管１を取り囲むように、予熱
された空気１８が送り込まれており、空気１８は、前記
燃焼触媒１６（例えばＬａ−βＡＱｚＯｓを担体にし、
プラチナをコーティングしたもの）の拡散部分２１に入
っていく。一方。Preheated air 18 is fed into the outside of the reaction tube 1 so as to surround the reaction tube 1.
(coated with platinum) into the diffusion section 21. on the other hand.
反応ガス１１は、改質触媒１０の拡散部分２０において
改質反応を受け、水素に富んだ改質ガス１２となって、
反応１から取り出される。その場合、改質反応の結果得
られた水：Ａ１９の一部が。The reaction gas 11 undergoes a reforming reaction in the diffusion section 20 of the reforming catalyst 10 and becomes a hydrogen-rich reformed gas 12.
Taken from reaction 1. In that case, part of the water: A19 obtained as a result of the reforming reaction.
反応管１の管壁内に保持した燃焼触媒１６の拡散部分２
１において、空気１８中の酸素と接触し。Diffusion portion 2 of combustion catalyst 16 held within the tube wall of reaction tube 1
1, in contact with oxygen in the air 18.
燃焼反応を起こす、その結果、改質反応に必要な吸熱部
の熱を連続的かつ直接的に供結することができる。A combustion reaction occurs, and as a result, the heat of the endothermic part necessary for the reforming reaction can be continuously and directly connected.
、 上記本実施例によれば、第６図で説明した実施例に
おける効果に加え、燃焼触媒を用いたことにより、可燃
性ガス濃度が低くても、改質反応に必要な熱量を供結す
ることができる。また１反応管管壁内での燃焼温度を低
下させることができるため１反応管の寿命を一層向上さ
せることができる。According to this embodiment, in addition to the effects of the embodiment described in FIG. be able to. Furthermore, since the combustion temperature within the wall of one reaction tube can be lowered, the life of one reaction tube can be further improved.
上記第１図〜第７図に説明した燃料改質器は。The fuel reformer illustrated in FIGS. 1 to 7 above is as follows.
例えば燃料電池発電装置に用いることができる。For example, it can be used in a fuel cell power generation device.
燃料電池発電装置に用いることにより、負荷追従性が優
れ、改質効率が高くなるものである。By using it in a fuel cell power generation device, it has excellent load followability and high reforming efficiency.
以上説明したように１本発明に係る燃料改質器によれば
、改質触媒を反応管壁面に保持させたため１反応管管壁
近傍における伝熱能力が向上し、迅速な改質反応を行う
ことができる。As explained above, according to the fuel reformer according to the present invention, since the reforming catalyst is held on the wall surface of the reaction tube, the heat transfer ability in the vicinity of the wall of the reaction tube is improved, and a rapid reforming reaction is performed. be able to.
第１図〜第７図は本発明の各実施例を示す断面構成図で
ある。
■・・・反応管、９・・・改質触媒粒子、１０・・・改
質触媒（コーティング）、１６・・・燃焼触媒。FIGS. 1 to 7 are cross-sectional configuration diagrams showing each embodiment of the present invention. ■... Reaction tube, 9... Reforming catalyst particles, 10... Reforming catalyst (coating), 16... Combustion catalyst.
Claims (1)
れ、当該反応ガスを改質ガスに変換してなる燃料改質器
において、前記反応管壁面に改質触媒が保持されてなる
ことを特徴とする燃料改質器。 ２、特許請求の範囲第１項において、前記反応管壁に改
質触媒を拡散させることにより、当該反応管壁面に改質
触媒が保持されてなることを特徴とする燃料改質器。 ３、特許請求の範囲第１項または第２項において、前記
反応管はガス透過性材料で構成されてなることを特徴と
する燃料改質器。[Scope of Claims] 1. In a fuel reformer in which a reaction gas is connected to a reaction tube filled with a reforming catalyst and the reaction gas is converted into a reformed gas, reforming is carried out on the wall surface of the reaction tube. A fuel reformer characterized by retaining a catalyst. 2. The fuel reformer according to claim 1, wherein the reforming catalyst is retained on the wall surface of the reaction tube by diffusing the reforming catalyst into the wall of the reaction tube. 3. A fuel reformer according to claim 1 or 2, wherein the reaction tube is made of a gas-permeable material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61060073A JPH0722694B2 (en) | 1986-03-18 | 1986-03-18 | Fuel reformer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61060073A JPH0722694B2 (en) | 1986-03-18 | 1986-03-18 | Fuel reformer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62216634A true JPS62216634A (en) | 1987-09-24 |
| JPH0722694B2 JPH0722694B2 (en) | 1995-03-15 |
Family
ID=13131540
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61060073A Expired - Lifetime JPH0722694B2 (en) | 1986-03-18 | 1986-03-18 | Fuel reformer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0722694B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0263545A (en) * | 1988-08-30 | 1990-03-02 | Toshiaki Kabe | Reaction tube |
| US5167865A (en) * | 1989-10-02 | 1992-12-01 | Mitsubishi Petrochemical Engineering Company Limited | Apparatus and method for preparing reformed gas by means of electroless plating |
| US7060118B1 (en) | 1998-07-21 | 2006-06-13 | Haldor Topse A/S | Synthesis gas production by steam reforming |
| US7087192B2 (en) | 2002-09-26 | 2006-08-08 | Haldor Topsoe A/S | Process for the preparation of synthesis gas |
| US7090789B2 (en) | 2003-02-05 | 2006-08-15 | Haldor Topsoe A/S | Process and catalyst for treatment of synthesis gas |
| US7094363B2 (en) | 2002-09-26 | 2006-08-22 | Haldor Topsoe A/S | Process for the preparation of a synthesis gas |
| US7241401B2 (en) | 2002-09-26 | 2007-07-10 | Haldor Topsoe A/S | Process for the production of synthesis gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4884808A (en) * | 1972-02-05 | 1973-11-10 | ||
| JPS4946719A (en) * | 1972-09-08 | 1974-05-04 |
-
1986
- 1986-03-18 JP JP61060073A patent/JPH0722694B2/en not_active Expired - Lifetime
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4884808A (en) * | 1972-02-05 | 1973-11-10 | ||
| JPS4946719A (en) * | 1972-09-08 | 1974-05-04 |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0263545A (en) * | 1988-08-30 | 1990-03-02 | Toshiaki Kabe | Reaction tube |
| US5167865A (en) * | 1989-10-02 | 1992-12-01 | Mitsubishi Petrochemical Engineering Company Limited | Apparatus and method for preparing reformed gas by means of electroless plating |
| US7060118B1 (en) | 1998-07-21 | 2006-06-13 | Haldor Topse A/S | Synthesis gas production by steam reforming |
| US7087192B2 (en) | 2002-09-26 | 2006-08-08 | Haldor Topsoe A/S | Process for the preparation of synthesis gas |
| US7094363B2 (en) | 2002-09-26 | 2006-08-22 | Haldor Topsoe A/S | Process for the preparation of a synthesis gas |
| US7241401B2 (en) | 2002-09-26 | 2007-07-10 | Haldor Topsoe A/S | Process for the production of synthesis gas |
| US7547332B2 (en) | 2002-09-26 | 2009-06-16 | Haldor Topsoe A/S | Apparatus for the preparation of synthesis gas |
| US7717971B2 (en) | 2002-09-26 | 2010-05-18 | Haldor Topsoe A/S | Process for the production of synthesis gas |
| US7090789B2 (en) | 2003-02-05 | 2006-08-15 | Haldor Topsoe A/S | Process and catalyst for treatment of synthesis gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0722694B2 (en) | 1995-03-15 |
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