JPS63310702A - Methanol reforming device - Google Patents
Methanol reforming deviceInfo
- Publication number
- JPS63310702A JPS63310702A JP62147202A JP14720287A JPS63310702A JP S63310702 A JPS63310702 A JP S63310702A JP 62147202 A JP62147202 A JP 62147202A JP 14720287 A JP14720287 A JP 14720287A JP S63310702 A JPS63310702 A JP S63310702A
- Authority
- JP
- Japan
- Prior art keywords
- air
- reactor
- burner
- partition wall
- air chamber
- 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
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000002407 reforming Methods 0.000 title abstract description 13
- 238000005192 partition Methods 0.000 claims abstract description 30
- 238000002485 combustion reaction Methods 0.000 claims abstract description 19
- 238000010438 heat treatment Methods 0.000 claims description 14
- 239000006200 vaporizer Substances 0.000 claims description 14
- 239000007789 gas Substances 0.000 abstract description 26
- 239000000446 fuel Substances 0.000 abstract description 13
- 239000000567 combustion gas Substances 0.000 abstract description 4
- 238000000034 method Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000002994 raw material Substances 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 229910002090 carbon oxide Inorganic materials 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 238000000629 steam reforming Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization 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
- H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
-
- 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)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
この発明は、メタノールを水蒸気改質して、燃料電池の
燃料ガスとなる水素を製造するためのメタノール改質器
に関する。The present invention relates to a methanol reformer for steam reforming methanol to produce hydrogen that becomes fuel gas for a fuel cell.
メタノールは、燃料電池へ供給する燃料ガスの水素源と
して、天然ガスに比べて改質温度が大幅に低く、かつ改
質工程が簡易であるという特徴を有している。
このようなメタノールを改質原料とする改質器として、
筒状の炉体と、この炉体の上部中央に設けられたバーナ
と、このバーナを囲んで前記炉体内に懸架された筒状の
隔壁と、この隔壁に囲まれた燃焼室に配置された気化器
と、前記隔壁の外側の加熱室に配置され下端部で前記気
化器に通じ上端部で改質ガスの送気口に通じる反応器と
を備えたものが知られている。
第３図はこの種の従来のメタノール改質器の一例を示す
ものである。
１は円筒状の炉体で、この炉体１の上部中央には炉内を
加熱するためのバーナ２が設けられている。４はバーナ
２の燃料供給管、５は同じく燃焼用空気供給管である。
バーナ２を囲んで、炉体１内には円筒状の隔壁３が同心
的に懸架して設けられている。この隔壁３は炉体１内を
、隔壁３でかこまれた燃焼室６と、隔壁３の外側の環状
の加熱室７とに区画しているが、燃焼室６と加熱室７と
は図示されている通り、それぞれの下部で通じている。
燃焼室６内には、バーナ２の下方に、気化器８が配置さ
れている。気化器８は、改質原料供給口９に接続された
入口端８ａかららせん状に上昇し、その後下降して出口
端８ｂに至っている。
加熱室７には、環状に配列された直立する多数の反応管
１０ａからなる反応器１０が配置されている。反応管１
０ａの下端部は中空円板状の原料ガスマニホルド１１を
介して気化器８の出口端８ｂに接続されており、また上
端部は環状中空体の改質ガスマニホルド１２を介して改
質ガス送気口１３に接続されている。反応管１０ａ内に
は触媒１４が充填されている。
炉体１の上部外側には、加熱室７を取り巻くように排気
ガスマニホルド１５が形成されている。
この排気ガスマニホルド１５は炉体１に空けられた多数
の排気穴１ａを介して加熱室７に通じ、また出口は排気
口１６に接続されている。
このように構成されたメタノール改質器では、バーナ２
による加熱の下で、改質原料供給口９から供給された改
質原料が以下のようにして改質される。
まず、バーナ２においては、燃料供給管４を通して供給
される燃料が、燃焼用空気供給管５から同時に供給され
る空気の下で燃焼する。燃料としては、定常運転下では
、図示しない燃料電池から水素を残存させて排出される
、いわゆるオフガスが用いられる。
バーナ２から生ずる高温の燃焼ガスは、矢印１７で示す
ように、燃焼室６内を下降した後、隔壁３の下端部と炉
体１の底板との間を潜り抜けてＵターンし、加熱室７内
を上昇する。そして、加熱室７の上部で排気穴１ａから
排気ガスマニホルド１５に集められ、排気口１６から機
外へ排出される。
燃焼ガスは、上記過程で気化器７および反応器１０と接
触し、熱伝達によりこれらを加熱する。
また、気化器８および反応器１０は熱輻射によっても加
熱され、気化器８はバーナ２から直接に、また反応器１
０は隔壁３からそれぞれ輻射熱を受けて加熱される。
一方、液体メタノールおよび水からなる改質原料は、矢
印１８で示すように、改質原料供給口９を通して、気化
器８に供給される。
この改質原料は、気化器８内で加熱されてガス化し、原
料ガスマニホルド１１を経て反応器１０の上端部入口に
達する。この原料ガスは、触媒１４と接触しながら反応
器１０内を上昇し、この間に次第に改質されて反応器１
０の上端出口部分で水素リッチな改質ガスとなり、改質
ガスマニホルド１２を経て改質ガス送気口１３から送出
される。
このようなメタノールの水蒸気改質反応は、次式（１）
で表される。
ＣＨ３０Ｈ＋Ｈｚ ｏ−＋ｃｏ！ ＋３Ｈｚ （１
）この反応は吸熱反応であり高温はど平衡、反応速度面
で有利であるが、３００°Ｃを超えると触媒の劣化が促
進されること、および２００〜３００ ’Ｃで平衡反応
率はほぼ１００％に達することから、この温度範囲が適
温として一般に実用されている。
ところで、上記式（１）の反応で生成した炭酸ガスは、
次のＣＯ逆変成により、−酸化炭素と水を作る。この反
応も吸熱反応である。
Ｃｏｔ ＋Ｈｚ →ＣＯ＋Ｈｚ Ｏ（２）この−酸化炭
素は燃料電池の白金系の電極触媒にとって被毒物質で、
特にメタノール改質器をリン酸型の燃料電池と組み合わ
せて用いる時は、その生成をできるだけ抑えなければな
らない。
そのためには、上記（２）式の反応が吸熱反応であるこ
とから、反応器における出口部分の改質触媒層の温度を
下げる必要があり、２５０°Ｃ以下が望ましい。Methanol, as a hydrogen source for the fuel gas supplied to the fuel cell, has the characteristics that its reforming temperature is significantly lower than that of natural gas, and the reforming process is simple. As a reformer that uses such methanol as a reforming raw material,
A cylindrical furnace body, a burner provided at the center of the upper part of the furnace body, a cylindrical partition wall surrounding the burner and suspended within the furnace body, and a combustion chamber surrounded by the partition wall. A reactor is known that includes a vaporizer and a reactor that is arranged in a heating chamber outside the partition wall and communicates with the vaporizer at its lower end and communicates with the reformed gas inlet at its upper end. FIG. 3 shows an example of this type of conventional methanol reformer. Reference numeral 1 denotes a cylindrical furnace body, and a burner 2 for heating the inside of the furnace is provided at the upper center of the furnace body 1. 4 is a fuel supply pipe for the burner 2, and 5 is a combustion air supply pipe. A cylindrical partition wall 3 is provided in the furnace body 1 surrounding the burner 2 and suspended concentrically. The partition wall 3 divides the inside of the furnace body 1 into a combustion chamber 6 surrounded by the partition wall 3 and an annular heating chamber 7 outside the partition wall 3, but the combustion chamber 6 and the heating chamber 7 are not shown in the figure. As shown, they are connected at the bottom of each. A carburetor 8 is arranged in the combustion chamber 6 below the burner 2 . The vaporizer 8 spirally rises from an inlet end 8a connected to a reforming material supply port 9, and then descends to an outlet end 8b. A reactor 10 consisting of a large number of upright reaction tubes 10a arranged in an annular shape is arranged in the heating chamber 7. reaction tube 1
The lower end of 0a is connected to the outlet end 8b of the vaporizer 8 via a hollow disk-shaped raw material gas manifold 11, and the upper end is connected to the reformed gas manifold 12 via an annular hollow reformed gas manifold. It is connected to the air port 13. A catalyst 14 is filled in the reaction tube 10a. An exhaust gas manifold 15 is formed outside the upper part of the furnace body 1 so as to surround the heating chamber 7 . This exhaust gas manifold 15 communicates with the heating chamber 7 through a large number of exhaust holes 1a formed in the furnace body 1, and its outlet is connected to an exhaust port 16. In the methanol reformer configured in this way, burner 2
Under heating, the reforming raw material supplied from the reforming raw material supply port 9 is reformed in the following manner. First, in the burner 2, fuel supplied through the fuel supply pipe 4 is combusted under air simultaneously supplied from the combustion air supply pipe 5. As the fuel, so-called off-gas, which is discharged from a fuel cell (not shown) with hydrogen remaining therein, is used during steady operation. The high-temperature combustion gas generated from the burner 2 descends in the combustion chamber 6 as shown by the arrow 17, passes between the lower end of the partition wall 3 and the bottom plate of the furnace body 1, makes a U-turn, and enters the heating chamber. Rise within 7. Then, the gas is collected in the exhaust gas manifold 15 through the exhaust hole 1a in the upper part of the heating chamber 7, and is discharged outside the machine through the exhaust port 16. The combustion gases come into contact with the vaporizer 7 and the reactor 10 during the above process and heat them by heat transfer. The vaporizer 8 and the reactor 10 are also heated by thermal radiation, with the vaporizer 8 being heated directly from the burner 2 and the reactor 1
0 receives radiant heat from the partition wall 3 and is heated. On the other hand, the reforming raw material consisting of liquid methanol and water is supplied to the vaporizer 8 through the reforming raw material supply port 9, as shown by an arrow 18. This reformed raw material is heated and gasified in the vaporizer 8, and reaches the upper end inlet of the reactor 10 via the raw material gas manifold 11. This raw material gas rises in the reactor 10 while contacting the catalyst 14, and is gradually reformed during this time.
The hydrogen-rich reformed gas becomes a hydrogen-rich reformed gas at the upper end exit portion of the reformed gas, and is sent out from the reformed gas inlet 13 via the reformed gas manifold 12. The steam reforming reaction of methanol is expressed by the following equation (1):
It is expressed as CH30H+Hz o-+co! +3Hz (1
) This reaction is an endothermic reaction, and a high temperature is advantageous in terms of equilibrium and reaction rate. %, this temperature range is generally used as an appropriate temperature. By the way, the carbon dioxide gas generated by the reaction of formula (1) above is
The following CO reverse transformation produces -carbon oxide and water. This reaction is also an endothermic reaction. Cot +Hz →CO+Hz O(2) This -carbon oxide is a poisonous substance for platinum-based electrode catalysts in fuel cells.
Particularly when a methanol reformer is used in combination with a phosphoric acid fuel cell, its production must be suppressed as much as possible. To this end, since the reaction of formula (2) above is an endothermic reaction, it is necessary to lower the temperature of the reforming catalyst layer at the exit portion of the reactor, preferably 250°C or less.
ところが、第３図のような従来の構成の改質器では、隔
壁３の上部がバーナ２の直下の高温に曝されているため
にこの部分が高温となり、その結果、反応器１０の上部
は隔壁３の上部からの輻射熱で加熱され改質触媒層の温
度が上昇してしまい、改質ガス中での一酸化炭素の濃度
を下げることが困難であった。
また、バーナ直下の温度を下げようとして燃焼用空気の
量を増加させると、気化器８内での気化が不安定となり
、安定した改質ガスが得られなくなったり、燃焼生成物
中に未燃燐分が増えたりする問題があった。
この発明は、このような問題点を解決しようとするもの
であって、バーナの安定した燃焼を保ったまま、隔壁か
ら反応器上部への熱輻射を減らし、反応器内に最適な温
度分布をつくることによって、燃料電池に良質の改質ガ
スを供給することのできるメタノール改質器を提供する
ことを目的とするものである。However, in a reformer with a conventional configuration as shown in FIG. The temperature of the reforming catalyst layer increases due to heating by radiant heat from the upper part of the partition wall 3, making it difficult to lower the concentration of carbon monoxide in the reformed gas. Additionally, if the amount of combustion air is increased in an attempt to lower the temperature directly below the burner, the vaporization within the vaporizer 8 will become unstable, making it impossible to obtain stable reformed gas, or causing unburned gas to be present in the combustion products. There was a problem with increased phosphorus content. This invention aims to solve these problems by reducing heat radiation from the partition wall to the upper part of the reactor while maintaining stable combustion in the burner, thereby creating an optimal temperature distribution within the reactor. The purpose of this invention is to provide a methanol reformer that can supply high-quality reformed gas to a fuel cell.
この発明は、筒状の炉体と、この炉体の上部中央に設け
られたバーナと、このバーナを囲んで前記炉体内に懸架
された筒状の隔壁と、この隔壁に囲まれた燃焼室に配置
されたの気化器と、前記隔壁の外側の加熱室に配置され
下端部で前記気化器に通じ上端部で改質ガスの送気口に
通じる反応器とを備えたメタノール改質器において、前
記バーナと前記反応器との間に空気室を形成し、この空
気室に前記バーナに供給される空気の一部を流すように
するのである。This invention includes a cylindrical furnace body, a burner provided at the center of the upper part of the furnace body, a cylindrical partition wall surrounding the burner and suspended within the furnace body, and a combustion chamber surrounded by the partition wall. A methanol reformer comprising: a vaporizer disposed in the partition wall; and a reactor disposed in a heating chamber outside the partition wall, the reactor having a lower end communicating with the vaporizer and an upper end communicating with a reformed gas supply port. An air chamber is formed between the burner and the reactor, and a part of the air supplied to the burner flows through the air chamber.
この発明によれば、バーナと反応器との間に形成された
空気室を流れる空気によって、反応器上部とバーナとの
間に断熱層が形成され、バーナから隔壁を通して反応器
上部に加わる輻射熱が減少する。According to this invention, a heat insulating layer is formed between the upper part of the reactor and the burner by the air flowing through the air chamber formed between the burner and the reactor, and radiant heat is applied from the burner to the upper part of the reactor through the partition wall. Decrease.
以下、第１図および第２図に基づいて、この発明の詳細
な説明する。なお、第１図において、第３図の従来例と
同一の部分には同一の符号を付は説明を省略する。
第１図において、燃焼室６にはバーナ２と反応器１０と
の間に、空気室１９が形成されている。
この空気室１９は、円筒状の隔壁３の内側に、バーナ２
を囲むようにして円筒状の短い隔壁２０を設けることに
よって、隔壁３と隔壁２０との間に環状に形成される。
バーナ２の上部には炉体１の天板１ｂとの間に中空円板
状の空気マニホルド２１が設けられている。バーナ２に
図示しない燃料電池からオフガスを供給する燃料供給管
４は、空気マニホルド２１の中心部を貫通してバーナ２
に接続されている。
燃焼用空気供給管５から供給された空気は、空気マニホ
ルド２１に入り、空気供給口２２を経てバーナ２に供給
される。
空気マニホルド２１に入った空気の一部は、隔壁２０に
空けられた空気分岐口２３を通して、矢印２４で示すよ
うに空気室１９に注入される。この空気は空気室３内を
下降して流れ、やがて燃焼ガスと合流する。
空気室３は、その内部を常に流れる新鮮な外部空気によ
り、バーナ２と反応器１０との間に断熱層を形成する。
したがって、反応器１０の上部は、バーナ２の直下の高
温の直接的な影響を免れることができる。
燃焼に必要な空気量と空気室１９に流す空気量との比は
、空気供給口２２と空気分岐口２３との開口比できめら
れる。
第２図の（Ａ）と（Ｂ）に、この発明の改質器と従来の
改質器について、反応器１０の触媒層中の軸方向の温度
分布の実測結果をそれぞれ示す。
第２図（Ａ）から分かる通り、この発明の改質器では、
反応器上部の温度上昇が抑えられ、反応器の入口直後か
ら出口部分に至るまで、約２２０°Ｃに保たれている。
これに対して、第２図（Ｂ）の従来の改質器では、反応
器の途中から出口にかけて温度上昇し、出口付近で約２
７０°Ｃに達している。水素が豊富となる反応器の後半
部分で温度上昇することは、−酸化炭素の生成を抑制す
る上で不利である。Hereinafter, the present invention will be explained in detail based on FIGS. 1 and 2. In FIG. 1, the same parts as those in the conventional example shown in FIG. 3 are designated by the same reference numerals, and the explanation thereof will be omitted. In FIG. 1, an air chamber 19 is formed in the combustion chamber 6 between the burner 2 and the reactor 10. This air chamber 19 has a burner 2 inside the cylindrical partition wall 3.
By providing a short cylindrical partition wall 20 to surround the partition wall 3 and the partition wall 20, an annular shape is formed between the partition wall 3 and the partition wall 20. An air manifold 21 in the shape of a hollow disk is provided at the upper part of the burner 2 between it and the top plate 1b of the furnace body 1. A fuel supply pipe 4 that supplies off gas from a fuel cell (not shown) to the burner 2 passes through the center of the air manifold 21 and is connected to the burner 2.
It is connected to the. Air supplied from the combustion air supply pipe 5 enters the air manifold 21 and is supplied to the burner 2 via the air supply port 22. A portion of the air that has entered the air manifold 21 is injected into the air chamber 19 as shown by arrow 24 through an air branch port 23 formed in the partition wall 20 . This air flows downward within the air chamber 3 and eventually merges with the combustion gas. The air chamber 3 forms a thermal insulation layer between the burner 2 and the reactor 10 with fresh external air constantly flowing inside it. Therefore, the upper part of the reactor 10 can be avoided from the direct influence of the high temperature immediately below the burner 2. The ratio between the amount of air required for combustion and the amount of air flowing into the air chamber 19 is determined by the opening ratio of the air supply port 22 and the air branch port 23. FIGS. 2A and 2B show actual measurement results of the temperature distribution in the axial direction in the catalyst layer of the reactor 10 for the reformer of the present invention and the conventional reformer, respectively. As can be seen from FIG. 2(A), in the reformer of this invention,
The temperature rise in the upper part of the reactor is suppressed, and the temperature is maintained at approximately 220°C from immediately after the inlet to the outlet of the reactor. On the other hand, in the conventional reformer shown in Figure 2 (B), the temperature increases from the middle of the reactor to the exit, and the temperature rises by about
The temperature has reached 70°C. An increase in temperature in the latter half of the reactor, which is enriched with hydrogen, is disadvantageous in suppressing the formation of -carbon oxides.
この発明は、バーナと反応器との間に空気室を形成し、
この空気室に前記バーナに送気される空気の一部を流す
ようにしたので、燃焼室から隔壁を通して反応器上部に
加わる輻射熱が減少し、反応器上部の温度上昇が抑止さ
れる。その結果、触煤層中の軸方向の温度分布を適正に
保ことができ、改質ガス中の一酸化濃度を低減させるこ
とができる。This invention forms an air chamber between the burner and the reactor,
Since a part of the air sent to the burner is made to flow into this air chamber, the radiant heat applied from the combustion chamber to the upper part of the reactor through the partition wall is reduced, and the temperature rise in the upper part of the reactor is suppressed. As a result, the axial temperature distribution in the soot layer can be maintained appropriately, and the monoxide concentration in the reformed gas can be reduced.
第１図はこの発明の実施例の断面図、第２図の（Ａ）お
よび（Ｂ）はそれぞれこの発明および従来の改質器の触
媒層中の軸方向の温度分布図、第３図は従来の改質器の
断面図である。
１：炉体、２：バーナ、３：隔壁、６：燃焼室、７：加
熱室、８：気化器、［０：反応器、１４：触媒、１９：
空気室。FIG. 1 is a sectional view of an embodiment of the present invention, FIG. 2 (A) and (B) are temperature distribution diagrams in the axial direction in the catalyst layer of the present invention and a conventional reformer, respectively. FIG. 2 is a cross-sectional view of a conventional reformer. 1: Furnace body, 2: Burner, 3: Partition wall, 6: Combustion chamber, 7: Heating chamber, 8: Vaporizer, [0: Reactor, 14: Catalyst, 19:
air chamber.
Claims (1)
ーナと、このバーナを囲んで前記炉体内に懸架された筒
状の隔壁と、この隔壁に囲まれた燃焼室に配置された気
化器と、前記隔壁の外側の加熱室に配置され下端部で前
記気化器に通じ上端部で改質ガスの送気口に通じる反応
器とを備えたメタノール改質器において、前記バーナと
前記反応器との間に空気室を形成し、この空気室に前記
バーナに供給される空気の一部を流すようにしたことを
特徴とするメタノール改質器。1) A cylindrical furnace body, a burner provided at the center of the upper part of the furnace body, a cylindrical partition wall surrounding the burner and suspended within the furnace body, and a combustion chamber surrounded by the partition wall. a reactor disposed in a heating chamber outside the partition wall, the reactor having a lower end communicating with the vaporizer and an upper end communicating with a reformed gas inlet; A methanol reformer, characterized in that an air chamber is formed between the reactor and the reactor, and a part of the air supplied to the burner flows through the air chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62147202A JPS63310702A (en) | 1987-06-13 | 1987-06-13 | Methanol reforming device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62147202A JPS63310702A (en) | 1987-06-13 | 1987-06-13 | Methanol reforming device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63310702A true JPS63310702A (en) | 1988-12-19 |
Family
ID=15424868
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62147202A Pending JPS63310702A (en) | 1987-06-13 | 1987-06-13 | Methanol reforming device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63310702A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0277421U (en) * | 1988-11-26 | 1990-06-14 | ||
| JP2021121995A (en) * | 2020-01-31 | 2021-08-26 | 京セラ株式会社 | Modification unit and fuel cell device |
-
1987
- 1987-06-13 JP JP62147202A patent/JPS63310702A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0277421U (en) * | 1988-11-26 | 1990-06-14 | ||
| JP2021121995A (en) * | 2020-01-31 | 2021-08-26 | 京セラ株式会社 | Modification unit and fuel cell device |
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