JPH09129257A - Power generating system - Google Patents
Power generating systemInfo
- Publication number
- JPH09129257A JPH09129257A JP7283331A JP28333195A JPH09129257A JP H09129257 A JPH09129257 A JP H09129257A JP 7283331 A JP7283331 A JP 7283331A JP 28333195 A JP28333195 A JP 28333195A JP H09129257 A JPH09129257 A JP H09129257A
- Authority
- JP
- Japan
- Prior art keywords
- fuel
- reforming
- solid electrolyte
- electrode
- cell
- 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.)
- Pending
Links
- 239000000446 fuel Substances 0.000 claims abstract description 81
- 239000003054 catalyst Substances 0.000 claims abstract description 29
- 238000002407 reforming Methods 0.000 claims abstract description 28
- 239000007784 solid electrolyte Substances 0.000 claims abstract description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 10
- 239000012528 membrane Substances 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000006057 reforming reaction Methods 0.000 abstract description 11
- 230000008021 deposition Effects 0.000 abstract description 4
- 229910052759 nickel Inorganic materials 0.000 abstract description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 abstract 2
- 238000002485 combustion reaction Methods 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 52
- 239000007789 gas Substances 0.000 description 23
- 238000010248 power generation Methods 0.000 description 19
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- -1 oxygen ion Chemical class 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000020169 heat generation Effects 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 229910052573 porcelain Inorganic materials 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 229910018279 LaSrMnO Inorganic materials 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000036647 reaction Effects 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
-
- 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
- H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
- H01M8/2465—Details of groupings of fuel cells
- H01M8/247—Arrangements for tightening a stack, for accommodation of a stack in a tank or for assembling different tanks
-
- 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
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fuel Cell (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】この発明は、内部改質固体電
解質形燃料電池を用いた発電装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a power generator using an internal reforming solid oxide fuel cell.
【０００２】[0002]
【従来の技術】周知の如く、固体電解質形燃料電池で
は、電極を設けた酸素イオン導電性固体電解質を８００
℃から１０００℃の高温にして、この固体電解質を隔壁
として、一方に燃料ガスを、もう一方に空気を供給し、
固体電解質の両面に設けた電極において電気化学的反応
を進行させて外部に電力を取り出す。As is well known, in a solid oxide fuel cell, an oxygen ion conductive solid electrolyte provided with electrodes is used.
C. to 1000.degree. C., the solid electrolyte is used as a partition wall, the fuel gas is supplied to one side, and the air is supplied to the other side.
Electrochemical reactions are caused to proceed in electrodes provided on both sides of the solid electrolyte to take out electric power to the outside.
【０００３】燃料ガスとしては、メタンを主成分とした
天然ガス、アルコール類や石炭ガス化ガスを用いる。メ
タンを主成分とした天然ガス、アルコール類燃料ガスを
使用する場合には、水蒸気と反応させて燃料電池の使用
に適する燃料ガスを生成する。その方法としては、燃料
電池供給前に燃料と水蒸気を反応させて水素と一酸化炭
素の混合物に変化させるが、この反応は吸熱反応である
ため熱入力を必要とする。As the fuel gas, natural gas containing methane as a main component, alcohols or coal gasification gas is used. When natural gas or alcohol fuel gas containing methane as a main component is used, it is reacted with water vapor to generate a fuel gas suitable for use in a fuel cell. As a method for this, the fuel and water vapor are reacted with each other to change into a mixture of hydrogen and carbon monoxide before the fuel cell is supplied, but this reaction is an endothermic reaction and requires heat input.
【０００４】その方法として、電池発電装置から発生し
た熱を供給することが考えられるが、発電装置から熱を
供給するために熱移動時の熱損失を最小限にする必要が
ある。そのためには熱交換機の構造や配管が複雑にな
り、熱効率が低下する懸念がある。そこで、改質反応を
燃料電池内部で行うことにより、電池発熱をそのまま改
質反応に供給できるため、発電設備の構造が簡略化さ
れ、熱効率も高くすることができる。As a method therefor, it is conceivable to supply the heat generated from the battery power generator, but in order to supply the heat from the power generator, it is necessary to minimize the heat loss during heat transfer. For this reason, the structure and piping of the heat exchanger become complicated, and there is a concern that the thermal efficiency will decrease. Therefore, by carrying out the reforming reaction inside the fuel cell, the heat of the cell can be directly supplied to the reforming reaction, so that the structure of the power generation facility can be simplified and the thermal efficiency can be increased.
【０００５】[0005]
【発明が解決しようとする課題】上述したように、メタ
ンを主成分とした天然ガス、アルコール類燃料ガスを水
蒸気と反応させて改質する場合には、燃料電池内部で改
質した方が熱効率が高くなる。燃料電池の燃料極には一
般にＮｉ，Ｃｏなどの金属酸化物等を使用しているが、
これらの金属酸化物等は改質反応に活性が高い。従っ
て、セルに直接燃料と水蒸気を供給すれば、改質反応が
進行すると同時に、生成した水素や一酸化炭素による発
電が同時に行える。しかしながら、燃料極において直接
的な改質反応を行うと、その条件によっては電極上に炭
素析出が生じるため、電池反応を阻害する恐れがある。As described above, when the natural gas containing methane as a main component and the alcohol fuel gas are reformed by reacting with the steam, it is better to reform inside the fuel cell. Becomes higher. Metal oxides such as Ni and Co are generally used for the fuel electrode of the fuel cell.
These metal oxides and the like are highly active in the reforming reaction. Therefore, if the fuel and steam are directly supplied to the cell, the reforming reaction proceeds, and at the same time, the generated hydrogen and carbon monoxide can generate electric power. However, if a direct reforming reaction is performed in the fuel electrode, carbon deposition may occur on the electrode depending on the conditions, which may hinder the cell reaction.
【０００６】この発明はこうした事情を考慮してなされ
たもので、固体電解質電気化学セル内部で改質を行う際
に、電池に燃料極以外の箇所で改質反応を進行させ、燃
料極に炭素析出が生じないようにしながら、なおかつ電
池発熱部を燃料改質時の吸熱分に置き換えて、ジュール
全体の発電効率を向上しえる発電装置を提供することを
目的とする。The present invention has been made in consideration of the above circumstances. When reforming is performed inside the solid electrolyte electrochemical cell, the reforming reaction proceeds at a position other than the fuel electrode in the cell, and the carbon is fed to the fuel electrode. An object of the present invention is to provide a power generation device capable of improving the power generation efficiency of the entire joule by preventing the precipitation from occurring and at the same time replacing the heat generation part of the battery with the heat absorption amount at the time of fuel reforming.
【０００７】[0007]
【課題を解決するための手段】この発明は、複数の単位
セルから構成される管状の内部改質型固体電解質燃料電
池と、この燃料電池の内側に配置された、改質される前
の燃料が供給されて燃料の改質が行われる燃料供給管と
を具備することを特徴とする発電装置である。The present invention relates to a tubular internal reforming solid electrolyte fuel cell composed of a plurality of unit cells, and a fuel before reforming, which is arranged inside the fuel cell. And a fuel supply pipe for reforming the fuel.
【０００８】この発明において、前記燃料電池として
は、例えば、酸素イオン導電性の固体電解質膜と、この
固体電解質膜の一方の側に設けられた空気極と、前記固
体電解質膜の他方の側に設けられた燃料極とから構成さ
れ、作動温度が８００℃〜１０００℃である構成のもの
が挙げられる。In the present invention, the fuel cell may be, for example, an oxygen ion conductive solid electrolyte membrane, an air electrode provided on one side of the solid electrolyte membrane, and an air electrode on the other side of the solid electrolyte membrane. An example of such a structure is that the operating temperature is 800 ° C. to 1000 ° C., which is composed of the provided fuel electrode.
【０００９】この発明において、供給される燃料として
は、例えば改質可能な炭素系燃料に水蒸気を添加したも
のが挙げられ、また燃料電池の内側に配置された燃料供
給管内部に改質触媒を充填することができる。In the present invention, the fuel to be supplied may be, for example, a reformable carbon-based fuel to which steam is added, and a reforming catalyst is provided inside the fuel supply pipe arranged inside the fuel cell. Can be filled.
【００１０】この発明においては、上述のように構成さ
れるため、燃料極に炭素析出などの損失を与えることな
く、改質ガスによる発電を行うことができる。そのた
め、セル発熱分を改質反応に供給することができるの
で、熱効率が向上し、モジュール全体の発熱効率も向上
することができる。Since the present invention is constructed as described above, power generation by the reformed gas can be performed without giving a loss such as carbon deposition to the fuel electrode. Therefore, the heat generated by the cells can be supplied to the reforming reaction, so that the thermal efficiency can be improved and the heat generating efficiency of the entire module can also be improved.
【００１１】[0011]
【発明の実施の形態】以下、本発明の一実施例を図１及
び図２を参照して説明する。ここで、図１はこの発明の
実施例１に係る発電装置の説明図、図２は図１の発電装
置を構成する燃料電池の単位セルの拡大図である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS One embodiment of the present invention will be described below with reference to FIGS. Here, FIG. 1 is an explanatory view of a power generator according to Embodiment 1 of the present invention, and FIG. 2 is an enlarged view of a unit cell of a fuel cell constituting the power generator of FIG.
【００１２】図中の符番１は、側板２と天板３と底板４
とからなる発電装置本体である。この発電装置本体１内
は、上部管板５及び下部管板６により供給ヘッダ７，燃
料排出ヘッダ８及び発電室９に仕切られている。前記天
板２には、前記供給ヘッダ７に燃料と水蒸気を送給する
燃料入口管10が設けられている。前記天板２と上部管板
５には、前記燃料排出ヘッダ８からの排ガスが発電装置
本体１の外部へ排出する排ガス管11が設けられている。Reference numeral 1 in the drawing is a side plate 2, a top plate 3 and a bottom plate 4.
It is the main body of the power generator. The inside of the power generator main body 1 is divided into a supply header 7, a fuel discharge header 8 and a power generation chamber 9 by an upper tube plate 5 and a lower tube plate 6. The top plate 2 is provided with a fuel inlet pipe 10 for feeding fuel and steam to the supply header 7. The top plate 2 and the upper tube plate 5 are provided with an exhaust gas pipe 11 through which exhaust gas from the fuel exhaust header 8 is exhausted to the outside of the power generator body 1.
【００１３】前記発電室９の内壁には断熱材12が設けら
れ、発電室９の略中心には前記燃料排出ヘッダ８と連通
する管状の内部改質型固体電解質燃料電池13が下部管板
６に支持されて設けられている。前記燃料電池13は複数
の単位セル14から構成されている。ここで、単位セル14
は、酸素イオン導電性の固体電解質膜15と、この固体電
解質膜15の一方の側に設けられた空気極16と、前記固体
電解質膜15の他方の側に設けられた燃料極16とから構成
されている。前記空気極16はＬａ系のペロブスカイト型
酸化物で、例えばＬａＳｒＭｎＯ3 ，ＬａＳｒＣｏＯ3
が使用される。前記燃料極16はＮｉＯとＹＳＺ（Ｙ2 Ｏ
3 安定化ＺｒＯ2 ）の混合物で、組成の範囲は重量割合
でＮｉＯ：ＹＳＺ＝５：５〜８：２である。A heat insulating material 12 is provided on the inner wall of the power generation chamber 9, and a tubular internal reforming type solid electrolyte fuel cell 13 communicating with the fuel discharge header 8 is provided in the lower tube sheet 6 at substantially the center of the power generation chamber 9. It is supported and provided by. The fuel cell 13 is composed of a plurality of unit cells 14. Where the unit cell 14
Is composed of an oxygen ion conductive solid electrolyte membrane 15, an air electrode 16 provided on one side of the solid electrolyte membrane 15, and a fuel electrode 16 provided on the other side of the solid electrolyte membrane 15. Has been done. The air electrode 16 is a La-based perovskite type oxide, such as LaSrMnO 3 or LaSrCoO 3.
Is used. The fuel electrode 16 is made of NiO and YSZ (Y 2 O
3 Stabilized ZrO 2 ) in the composition range by weight ratio of NiO: YSZ = 5: 5-8: 2.
【００１４】前記燃料電池13の下端にはセルキャップ17
が設けられている。前記燃料電池13の内側には、上端が
前記供給ヘッダ７に連通しかつ下端が燃料電池13の底部
の領域と開放状態にある燃料供給管18が前記上部管板５
に支持されて設けられている。この燃料供給管18のガス
入口部分には、改質反応用の触媒層19が充填されてい
る。ここで、炭素系ガスと水蒸気がこの触媒層19を通過
する際に改質反応を行い、水素と一酸化炭素の混合ガス
を電池に供給する。前記触媒層19の温度は、６００℃〜
８００℃になるようにモジュール内部の熱バランスをと
る。前記底板４には、発電室９に空気を導入する空気導
入管20，発電室９から空気を排出する空気排出管21が夫
々設けられている。A cell cap 17 is provided at the lower end of the fuel cell 13.
Is provided. Inside the fuel cell 13, a fuel supply pipe 18 having an upper end communicating with the supply header 7 and a lower end in an open state with a region of the bottom of the fuel cell 13 is provided in the upper tube sheet 5.
It is supported and provided. The gas inlet portion of the fuel supply pipe 18 is filled with a catalyst layer 19 for reforming reaction. Here, when the carbon-based gas and the steam pass through the catalyst layer 19, a reforming reaction is performed and a mixed gas of hydrogen and carbon monoxide is supplied to the battery. The temperature of the catalyst layer 19 is 600 ° C.
Balance the heat inside the module to 800 ° C. The bottom plate 4 is provided with an air introduction pipe 20 for introducing air into the power generation chamber 9 and an air discharge pipe 21 for discharging air from the power generation chamber 9.
【００１５】図３は、触媒の改質効果試験を実施するた
めの装置の説明図である。この装置は実際の燃料電池１
本を模擬した緻密管31の内部にＳＵＳ製燃料供給管（φ
８×φ６）32を設置したものである。なお、図中の符番
33は前記緻密管31を収納する磁製管、符番34は前記磁製
管33の外周部に配置された電気炉を示す。この燃料供給
管32の一部に改質触媒を充填し、メタン（０．０８〜
０．１６Ｎｌ／min ）及び水蒸気（０．２４〜０．４９
Ｎｌ／min ）を水蒸気／炭素のモル比で３になるように
混合したガスを燃料供給管32に供給した。触媒層温度は
約８００℃に維持し、ガス流量および触媒量を変化させ
て、触媒層を通過した後のガス組成をガスクロマトグラ
フィーで分析した。FIG. 3 is an explanatory view of an apparatus for carrying out a catalyst reforming effect test. This device is a real fuel cell 1
Inside the dense pipe 31 simulating a book, the SUS fuel supply pipe (φ
8 × φ6) 32 is installed. Note that the numbers in the figure
Reference numeral 34 indicates a porcelain tube that houses the dense tube 31, and reference numeral 34 indicates an electric furnace arranged on the outer peripheral portion of the porcelain tube 33. A part of the fuel supply pipe 32 is filled with a reforming catalyst, and methane (0.08 ~
0.16 Nl / min) and steam (0.24 to 0.49)
Gas mixed with Nl / min) so that the molar ratio of steam / carbon was 3 was supplied to the fuel supply pipe 32. The catalyst layer temperature was maintained at about 800 ° C., the gas flow rate and the catalyst amount were changed, and the gas composition after passing through the catalyst layer was analyzed by gas chromatography.
【００１６】改質用触媒としては、Ａｌ2 Ｏ3 やＭｇＡ
ｌ2 Ｏ4 を担体として、これらにＮｉを担持させたもの
が使用されるが、本実施例では25wt％Ｎｉ−75wt％Ｍｇ
Ａｌ2 Ｏ4 を使用した。その結果、図４のように触媒重
量／ガス流量をパラメータとしたメタン改質率曲線が得
られた。同図より、電池作動時の燃料利用率から供給す
るメタン／水蒸気量を決定すれば、任意のメタン改質率
にするために必要な触媒量が算出できる。例として、メ
タン利用率が８０％、改質率３０％で発電する場合、電
池１本あたり約０．１１ｇの触媒が必要であることが分
かる。As the reforming catalyst, Al 2 O 3 or MgA is used.
Although 1 2 O 4 is used as a carrier and Ni is supported on these, 25 wt% Ni-75 wt% Mg is used in this embodiment.
Al 2 O 4 was used. As a result, a methane reforming rate curve with the catalyst weight / gas flow rate as a parameter was obtained as shown in FIG. From the figure, if the amount of supplied methane / steam is determined from the fuel utilization rate when the cell is operating, the amount of catalyst required to achieve an arbitrary methane reforming rate can be calculated. As an example, when generating electricity with a methane utilization rate of 80% and a reforming rate of 30%, it can be seen that about 0.11 g of catalyst is required for each battery.
【００１７】なお、上記メタン改質率，メタン利用率η
の定義及び触媒量の算出方法は下記の通りである。 i)メタン改質率ｘ ｘ＝出口未反応メタン量（Ｎｌ／min ）／入口供給メタ
ン量（Ｎｌ／min ） ii) メタン利用率η：供給したメタンガスのうち発電に
供されたメタンガス量で定義。The above methane reforming rate and methane utilization rate η
And the calculation method of the catalyst amount are as follows. i) Methane reforming rate x x = Outlet unreacted methane amount (Nl / min) / Inlet supply methane amount (Nl / min) ii) Methane utilization rate η: Defined by the amount of methane gas supplied to power generation out of the supplied methane gas .
【００１８】 η＝Ｖｅ（ＣＨ4 ）／Ｖｉｎ（ＣＨ4 ） …(1) ここで、Ｖｅ（ＣＨ4 ）は発電に使用されたメタンガス
量（Ｎｌ／min ）、Ｖｉｎ（ＣＨ4 ）は投入したメタン
ガス量（Ｎｌ／min ）を示す。Η = Ve (CH 4 ) / Vin (CH 4 ) (1) Here, Ve (CH 4 ) is the amount of methane gas used for power generation (Nl / min), and Vin (CH 4 ) is input. The amount of methane gas (Nl / min) is shown.
【００１９】Ｖｅ（ＣＨ4 ）は次式の８電子反応を用い
て発電時の電流値（Ｉ）から計算した。 ＣＨ4 ＋４Ｏ2-＝ＣＯ2 ＋２Ｈ2 Ｏ＋８ｅ- …(2) Ｖｅ（ＣＨ4 ）［Ｎｌ／min ］＝２２．４１４［Ｎｌ／ｍｏｌ］×Ｉ［Ｃ／se c ］×６０［sec ／min ］×１５／（８×９６４８５［Ｃ／ｍｏｌ］）…(3) 但し、 Ｉ：電流 ［Ａ］＝［Ｃ／sec ］ １５：セル数 ［−］ ８：反応電子数［−］ 96485：ファラデー定数［−］ iii)触媒量の算出方法 図４の横軸は触媒量（ｇ）を一定にして、供給ガス量
（Ｎｌ／min ）を変化させた時の試験結果から算出し
た。ＳＯＦＣでは改質率が３０％以上であれば安定した
発電が期待できるが、この場合の触媒量／ガス量は図４
より０．３４５ｇ（Ｎｌ／min ）である。従って、供給
ガス量（メタン＋水蒸気）が判れば、必要触媒量が得ら
れる。Ve (CH 4 ) was calculated from the current value (I) during power generation using the 8-electron reaction of the following equation. CH 4 + 4O 2− = CO 2 + 2H 2 O + 8e − (2) Ve (CH 4 ) [Nl / min] = 22.414 [Nl / mol] × I [C / se c] × 60 [sec / min] × 15 / (8 × 96485 [C / mol]) (3) However, I: current [A] = [C / sec] 15: number of cells [−] 8: number of reaction electrons [−] 96485: Faraday constant [−] Iii) Calculation method of catalyst amount The horizontal axis of FIG. 4 was calculated from the test results when the catalyst amount (g) was kept constant and the supply gas amount (Nl / min) was changed. In SOFC, stable power generation can be expected if the reforming rate is 30% or more, but the catalyst amount / gas amount in this case is shown in FIG.
Is 0.345 g (Nl / min). Therefore, if the supply gas amount (methane + steam) is known, the required catalyst amount can be obtained.
【００２０】運転条件として燃料利用率が８０％、水蒸
気／メタン＝３を想定する。この場合の供給メタン流量
Ｖｉｎ（ＣＨ4 ）は式(1) から求めるが、その際、Ｖｅ
（ＣＨ4 ）は式(3) において電流値が０．２Ａ／cm2 相
当の電流値（約２．５Ａ）を用いて求める。即ち、 Ｖｅ（ＣＨ4 ）＝０．０６５（Ｎｌ／min ） Ｖｉｎ（ＣＨ4 ）＝０．０６５／０．８＝０．０８１
（Ｎｌ／min ） ガス量（メタン＋水蒸気）は、 ０．０８１＋０．０８１×３＝０．３２４ 触媒量／ガス量は０．３４５ｇ（Ｎｌ／min ）であるか
ら、必要触媒量は、 ０．３４５×０．３２４＝０．１１（ｇ） このように、上記実施例に係る発電装置においては、固
体電解質燃料電池の内側に設置した燃料供給管18に触媒
層19を設け、６００℃〜８００℃に維持することによ
り、炭素系燃料と水蒸気の混合ガス及び一酸化炭素に改
質し、発電用燃料として供給することが可能である。ま
た、モジュール内部で吸熱反応である改質を行うため電
池発熱を有効に利用することができ、モジュール全体の
熱効率および発電効率を向上できる。As the operating conditions, it is assumed that the fuel utilization rate is 80% and steam / methane = 3. In this case, the supplied methane flow rate Vin (CH 4 ) is obtained from the equation (1).
(CH 4 ) is obtained by using the current value (about 2.5 A) corresponding to the current value of 0.2 A / cm 2 in the equation (3). That is, Ve (CH 4 ) = 0.065 (Nl / min) Vin (CH 4 ) = 0.065 / 0.8 = 0.081
(Nl / min) Gas amount (methane + steam) is 0.081 + 0.081 × 3 = 0.324 Catalyst amount / gas amount is 0.345 g (Nl / min), so the required catalyst amount is 345 × 0.324 = 0.11 (g) As described above, in the power generation device according to the above-described embodiment, the catalyst layer 19 is provided on the fuel supply pipe 18 installed inside the solid electrolyte fuel cell, and the temperature is 600 ° C. to 800 ° C. By maintaining the temperature at 0 ° C., it is possible to reform to a mixed gas of carbon-based fuel and water vapor and carbon monoxide, and supply it as fuel for power generation. Further, since the reforming, which is an endothermic reaction, is performed inside the module, the heat generation of the battery can be effectively used, and the thermal efficiency and power generation efficiency of the entire module can be improved.
【００２１】[0021]
【発明の効果】以上詳述したようにこの発明によれば、
固体電解質電気化学セル内部で改質を行う際に、電池に
燃料極以外の箇所で改質反応を進行させ、燃料極に炭素
析出が生じないようにしながら、なおかつ電池発熱部を
燃料改質時の吸熱分に置き換えて、ジュール全体の発電
効率を向上しえる発電装置を提供できる。As described in detail above, according to the present invention,
When performing reforming inside the solid electrolyte electrochemical cell, the reforming reaction proceeds at a location other than the fuel electrode in the cell to prevent carbon deposition on the fuel electrode, while It is possible to provide a power generation device capable of improving the power generation efficiency of the entire Joule by replacing the heat absorption with
【図１】この発明の一実施例に係る発電装置の説明図。FIG. 1 is an explanatory diagram of a power generator according to an embodiment of the present invention.
【図２】図１の発電装置の一構成である燃料電池の単位
セルの拡大図。FIG. 2 is an enlarged view of a unit cell of a fuel cell which is one configuration of the power generator of FIG.
【図３】燃料供給管触媒充填による改質特性試験装置の
説明図。FIG. 3 is an explanatory view of a reforming characteristic test device by filling a fuel supply pipe catalyst.
【図４】メタン改質率と触媒重量／ガス流量との関係を
示す特性図。FIG. 4 is a characteristic diagram showing the relationship between methane reforming rate and catalyst weight / gas flow rate.
１…発電装置本体、 ２…側板、３…天板、
４…底板、５…上部管板、 ６…下部管板、７…供
給ヘッダ、 ８…燃料排出ヘッダ、９…発電室、
10…燃料入口管、11…排ガス管、 12…断熱
材、13…燃料電池、 14…単位セル、15…固体電解
質膜、 16…空気極、17…燃料極、 18…燃料供
給管、19…触媒層、 20…空気入口管、21…空気
排出管。1 ... Power generator main body, 2 ... Side plate, 3 ... Top plate,
4 ... Bottom plate, 5 ... Upper tube plate, 6 ... Lower tube plate, 7 ... Supply header, 8 ... Fuel discharge header, 9 ... Power generation chamber,
10 ... Fuel inlet pipe, 11 ... Exhaust gas pipe, 12 ... Thermal insulation material, 13 ... Fuel cell, 14 ... Unit cell, 15 ... Solid electrolyte membrane, 16 ... Air electrode, 17 ... Fuel electrode, 18 ... Fuel supply pipe, 19 ... Catalyst layer, 20 ... Air inlet pipe, 21 ... Air exhaust pipe.
Claims (3)
部改質型固体電解質燃料電池と、この燃料電池の内側に
配置された、改質される前の燃料が供給されて燃料の改
質が行われる燃料供給管とを具備することを特徴とする
発電装置。1. A tubular internal reforming solid electrolyte fuel cell composed of a plurality of unit cells, and a fuel before reforming, which is arranged inside the fuel cell, is supplied to reform the fuel. And a fuel supply pipe for performing the above.
体電解質膜と、この固体電解質膜の一方の側に設けられ
た空気極と、前記固体電解質膜の他方の側に設けられた
燃料極とから構成され、作動温度が８００℃〜１０００
℃であることを特徴とする請求項１記載の発電装置。2. The fuel cell comprises an oxygen ion conductive solid electrolyte membrane, an air electrode provided on one side of the solid electrolyte membrane, and a fuel electrode provided on the other side of the solid electrolyte membrane. And an operating temperature of 800 ° C to 1000
2. The power generator according to claim 1, wherein the temperature is in degrees Celsius.
に水蒸気を添加したもので、燃料電池の内側に配置され
た燃料供給管内部に改質触媒が充填されていることを特
徴とする請求項１記載の発電装置。3. A fuel to be supplied is a reformable carbon-based fuel to which steam is added, and a reforming catalyst is filled in a fuel supply pipe arranged inside a fuel cell. The power generator according to claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7283331A JPH09129257A (en) | 1995-10-31 | 1995-10-31 | Power generating system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7283331A JPH09129257A (en) | 1995-10-31 | 1995-10-31 | Power generating system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09129257A true JPH09129257A (en) | 1997-05-16 |
Family
ID=17664098
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7283331A Pending JPH09129257A (en) | 1995-10-31 | 1995-10-31 | Power generating system |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09129257A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998021776A1 (en) * | 1996-11-12 | 1998-05-22 | Forschungszentrum Jülich GmbH | Fuel cell with integrated reformer |
-
1995
- 1995-10-31 JP JP7283331A patent/JPH09129257A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998021776A1 (en) * | 1996-11-12 | 1998-05-22 | Forschungszentrum Jülich GmbH | Fuel cell with integrated reformer |
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