JPH02160601A - Production of hydrogen by methanol reforming and apparatus therefor - Google Patents
Production of hydrogen by methanol reforming and apparatus thereforInfo
- Publication number
- JPH02160601A JPH02160601A JP63317215A JP31721588A JPH02160601A JP H02160601 A JPH02160601 A JP H02160601A JP 63317215 A JP63317215 A JP 63317215A JP 31721588 A JP31721588 A JP 31721588A JP H02160601 A JPH02160601 A JP H02160601A
- Authority
- JP
- Japan
- Prior art keywords
- methanol
- water
- hydrogen
- gas
- reforming
- 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
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 189
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 39
- 239000001257 hydrogen Substances 0.000 title claims abstract description 39
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 238000002407 reforming Methods 0.000 title claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000007789 gas Substances 0.000 claims abstract description 30
- 239000000567 combustion gas Substances 0.000 claims abstract description 15
- 238000000746 purification Methods 0.000 claims abstract description 14
- 238000000034 method Methods 0.000 claims abstract description 13
- 238000007084 catalytic combustion reaction Methods 0.000 claims abstract description 5
- 230000003197 catalytic effect Effects 0.000 claims description 21
- 239000000446 fuel Substances 0.000 claims description 12
- 239000003054 catalyst Substances 0.000 claims description 10
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- 150000002431 hydrogen Chemical class 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 238000001704 evaporation Methods 0.000 abstract description 3
- 230000008020 evaporation Effects 0.000 abstract description 3
- 238000000629 steam reforming Methods 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 description 5
- 239000006200 vaporizer Substances 0.000 description 5
- 238000001556 precipitation Methods 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 208000036366 Sensation of pressure Diseases 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
- B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
- B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (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、メタノールと水とを原料とするメタノール改
質装置と、水素精製装置とを組み合わせて、高純度水素
を製造する方法およびその装置に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention provides a method and apparatus for producing high-purity hydrogen by combining a methanol reformer using methanol and water as raw materials and a hydrogen purification device. It is related to.
従来、メタノール改質による水素製造方式として、第２
図に示すような熱媒循環加熱方式が知られている。この
方式は、メタノールと純水とを混合して予熱器１に供給
し、ついで気化器２で蒸発させた後、改質装置３に供給
して水蒸気改質するものである。そして、熱媒を熱媒加
熱炉４と改質装置３との間で循環ポンプ５により循環し
ている。Conventionally, the second method of hydrogen production by methanol reforming was
A heating medium circulation heating method as shown in the figure is known. In this method, methanol and pure water are mixed and supplied to a preheater 1, then evaporated in a vaporizer 2, and then supplied to a reformer 3 for steam reforming. The heat medium is circulated between the heat medium heating furnace 4 and the reformer 3 by a circulation pump 5.
改質装置３からの粗水素（−例として、Ｈ８７５％）は
、分離タンク６で水分が除去された後、水素精製装置７
に導入されて、高純度水素が得られる。Crude hydrogen (for example, H875%) from the reformer 3 is dehydrated in a separation tank 6, and then transferred to a hydrogen purifier 7.
high purity hydrogen is obtained.
水素精製装置７からのオフガスは（−例として、Ｈ８４
５％、Ｃ０，５０％）、オフガスタンク８を経て、熱媒
加熱炉４に燃料として供給される。１０は冷却器、１１
はメタノールポンプ、１２は純水ポンプである。The off-gas from the hydrogen purification device 7 is (for example, H84
5%, C0, 50%), and is supplied as fuel to the heat medium heating furnace 4 through the off-gas tank 8. 10 is a cooler, 11
is a methanol pump, and 12 is a pure water pump.
また従来、実開昭６２−１７０７２８号公報には、メタ
ノールと純水とを混合して気化器に供給して蒸発させた
後、改質器に供給し、一方、水素精製装置からのオフガ
スを触媒燃焼器で燃焼させ、この燃焼ガスを気化器の熱
源とするようにしたメタノール改質水素製造装置が開示
されている。Conventionally, in Japanese Utility Model Application Publication No. 62-170728, methanol and pure water are mixed and supplied to a vaporizer for evaporation, and then supplied to a reformer, while off-gas from a hydrogen purification device is A methanol reformed hydrogen production apparatus is disclosed in which combustion is performed in a catalytic combustor and the combustion gas is used as a heat source for a vaporizer.
〔発明が解決しようとする課題］
しかし、上記の従来技術においては、メタノールを気化
させる際の温度が高くなるので、炭素の析出が起こり易
いという不都合がある。また、負荷変動があると、気化
器内の気液平衡状態が変化し、一定した原料ガス（水・
メタノール混合ガス）が得られず、安定な運転が難しい
という不都合がある。[Problems to be Solved by the Invention] However, in the above-mentioned conventional technology, since the temperature when vaporizing methanol becomes high, there is a disadvantage that carbon precipitation tends to occur. In addition, if there is a load fluctuation, the gas-liquid equilibrium state in the vaporizer changes, and the raw material gas (water, water, etc.) remains constant.
There is a disadvantage that stable operation is difficult because methanol mixed gas) cannot be obtained.
本発明は上記の点に鑑みなされたもので、触媒燃焼方式
と、メタノールと水との別供給方法との採用により、気
化器における炭素の析出を防止するとともに、コンパク
トで熱効率の優れたメタノール改質による水素製造方法
およびその装置を提供することを目的とするものである
。The present invention was developed in view of the above points, and by adopting a catalytic combustion method and a separate supply method for methanol and water, it prevents carbon precipitation in the vaporizer, and is compact and has excellent thermal efficiency. The purpose of the present invention is to provide a hydrogen production method and an apparatus for the same.
〔課題を解決するための手段］
上記の目的を達成するために、本発明のメタノール改質
によ、る水素製造方法は、第１図に示すように、メタノ
ールを気化させて水蒸気改質した後、水素精製して高純
度水素を製造する方法において、メタノールと水とをそ
れぞれ別個の蒸発器１５．１８に供給し、水素精製の際
に発生するオフガスを触媒燃焼させて得た燃焼ガスを、
まず水の蒸発に用い、ついでメタノール改質に用いた後
、メタノールの蒸発に用いるものである。[Means for Solving the Problems] In order to achieve the above object, the method for producing hydrogen by methanol reforming of the present invention involves vaporizing methanol and reforming it with steam, as shown in Fig. 1. After that, in the method of producing high-purity hydrogen by hydrogen purification, methanol and water are each supplied to separate evaporators 15.18, and the combustion gas obtained by catalytic combustion of the off-gas generated during hydrogen purification is ,
It is first used to evaporate water, then used to reform methanol, and then used to evaporate methanol.
本発明の方法において、水素精製の際に発生するオフガ
スを、一旦オフガス貯蔵タンク２１に溜めた後、このオ
フガスを触媒燃焼器２２へ燃料として供給し、このオフ
ガス供給量をオフガス貯蔵タンク２１の容積または圧力
が一定になるように制御するとともに、触媒燃焼器２２
の温度を補助燃料として供給するメタノール量によって
制御するのが望ましい。In the method of the present invention, after the off-gas generated during hydrogen purification is temporarily stored in the off-gas storage tank 21, this off-gas is supplied to the catalytic combustor 22 as fuel, and the amount of off-gas supplied is equal to the volume of the off-gas storage tank 21. Alternatively, the pressure is controlled to be constant, and the catalytic combustor 22
It is desirable to control the temperature of the fuel by controlling the amount of methanol supplied as auxiliary fuel.
そして、本発明のメタノール改質による水素製造装置は
、第１図に示すように、メタノール改質装置３と水素精
製装置７とを組み合わせた高純度水素製造装置において
、メタノールタンク１３をメタノールポンプ１４、メタ
ノール予熱器３４およびメタノール蒸発器１５を介して
改質装置３に接続するとともに、水タンク１６を水ポン
プ１７、水予熱器３５および水蒸発器１８を介して改質
装置３に接続し、水素精製装置７のオフガス出口をオフ
ガス貯蔵タンク２１を介して触媒燃焼器２２に接続し、
この触媒燃焼器２２の燃焼ガス出口を水蒸発器１８を介
して改質装置３に接続し、この改質装置３の燃焼ガス出
口をメタノール蒸発器１５に接続したものである。As shown in FIG. 1, the hydrogen production device by methanol reforming of the present invention is a high-purity hydrogen production device that combines a methanol reformer 3 and a hydrogen purification device 7. , is connected to the reformer 3 via the methanol preheater 34 and the methanol evaporator 15, and the water tank 16 is connected to the reformer 3 via the water pump 17, the water preheater 35 and the water evaporator 18, Connecting the off-gas outlet of the hydrogen purification device 7 to the catalytic combustor 22 via the off-gas storage tank 21,
A combustion gas outlet of this catalytic combustor 22 is connected to a reformer 3 via a water evaporator 18, and a combustion gas outlet of this reformer 3 is connected to a methanol evaporator 15.
本発明の装置において、触媒燃焼器２２内の入口部に白
金担持触媒を充填し、触媒燃焼器２２内の入口部より後
流部にパラジウム担持触媒を充填するのが望ましい。In the apparatus of the present invention, it is desirable that the inlet portion of the catalytic combustor 22 is filled with a supported platinum catalyst, and the portion downstream of the inlet portion of the catalytic combustor 22 is filled with a supported palladium catalyst.
（作 用）
メタノールと水とをそれぞれ別個の蒸発器１５．１８に
供給し、触媒燃焼器２２で発生した比較的高温（約５５
０″Ｃ前後）の燃焼ガスを直接熱源として、まず水の蒸
発に用い、続いて改質装置３でメタノール改質反応熱と
して用いた後、比較的低温（約２５０″Ｃ前後）でメタ
ノール（沸点が水より低い）を蒸発させる。このように
して、加熱用燃焼ガス温度レベルに適した熱の有効利用
を図り、全体の熱効率を向上させ、かつ、炭素の析出を
防止する。(Function) Methanol and water are supplied to separate evaporators 15 and 18, respectively, and the relatively high temperature (approximately 55
Using the combustion gas at a temperature of around 0"C as a direct heat source, it is first used to evaporate water, then used as the heat of the methanol reforming reaction in the reformer 3, and then converted to methanol (around 250"C) at a relatively low temperature (around 250"C). evaporate (boiling point lower than water). In this way, it is possible to effectively utilize heat appropriate to the temperature level of the heating combustion gas, improve overall thermal efficiency, and prevent carbon precipitation.
以下、図面を参照して本発明の好適な実施例を詳細に説
明する。ただしこの実施例に記載されている構成機器の
形状、その相対配置などは、とくに特定的な記載がない
限りは、本発明の範囲をそれらのみに限定する趣旨のも
のではなく、単なる説明例にすぎない。Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings. However, unless there is a specific description, the shapes of the components described in this example, their relative positions, etc. are not intended to limit the scope of the present invention to these, but are merely illustrative examples. Only.
第１図は本発明のメタノール改質による水素製造装置の
一例を示している。３ばメタノール改質装置、７は水素
精製装置で、−例として、圧力揺動吸着型（ｐｒｅｓｓ
ｕｒｅ ｓｗｉｎｇ ａｄｓｏｒｐｔｉｏｎＳＰＳＡ型
）のものが用いられる。そして、メタノールタンク１３
はメタノールポンプ１４、メタノール予熱器３４および
メタノール蒸発器１５を介して改質装置３に接続され、
水タンク１６は水ポンプ１７、水予熱器３５および水蒸
発器１８を介して改質装置３に接続されている。水素精
製装置７のオフガス出口２０はオフガス貯蔵タンク２１
を介して触媒燃焼器２２に接続され、この触媒燃焼器の
燃焼ガス出口２３は水蒸発器１８を介して改質装置３に
接続され、さらに、この改質装置の燃焼ガス出口２４ば
メタノール蒸発器１５に接続されている。FIG. 1 shows an example of an apparatus for producing hydrogen by methanol reforming according to the present invention. 3 is a methanol reformer, and 7 is a hydrogen purification device, for example, a pressure swing adsorption type (press
ure swing advertising (SPSA type) is used. And methanol tank 13
is connected to the reformer 3 via a methanol pump 14, a methanol preheater 34 and a methanol evaporator 15,
The water tank 16 is connected to the reformer 3 via a water pump 17, a water preheater 35, and a water evaporator 18. The off-gas outlet 20 of the hydrogen purification device 7 is connected to the off-gas storage tank 21
The combustion gas outlet 23 of this catalytic combustor is connected to the reformer 3 through a water evaporator 18, and the combustion gas outlet 24 of this reformer is connected to a methanol evaporator. 15.
触媒燃焼器２２内に充填される燃料触媒としては、Ｐ
ｔＳＰｄｚ Ｒｕ５ｔｓ Ｃｏ１１４、ＮｔＯｌＭｎＯ
ｔなどをアルミナ、シリカ、チタニアなど一般に用いら
れている触媒担体に担持させた酸化触媒が用いられる。The fuel catalyst filled in the catalytic combustor 22 is P
tSPdz Ru5ts Co114, NtOlMnO
An oxidation catalyst in which T is supported on a commonly used catalyst carrier such as alumina, silica, or titania is used.
この場合、触媒燃焼器２２内の入口部に白金担持触媒を
充填し、触媒燃焼器２２内の入口部より後流部にパラジ
ウム担持触媒を充填することにより、メタノールを燃料
とした冷起動が可能となり、かつ、高温化でのオフガス
の安定燃焼を可能とす２５は冷却器、２６は気水分離器
、２７は補助燃料ポンプ、２８は空気送風機、３０．３
１は調節弁、３２は圧力指示調節計、３３は温度指示調
節計である。In this case, by filling the inlet of the catalytic combustor 22 with a platinum-supported catalyst and filling the downstream part of the catalytic combustor 22 with a palladium-supported catalyst, cold startup using methanol as fuel is possible. 25 is a cooler, 26 is a steam separator, 27 is an auxiliary fuel pump, 28 is an air blower, 30.3
1 is a control valve, 32 is a pressure indicating regulator, and 33 is a temperature indicating regulator.
上記のように構成された装置において、水を水蒸発器１
８に供給するとともに、触媒燃焼器２２からの高温燃焼
ガスで蒸発させた後、この燃焼ガスを改質装置３に導入
して改質用熱源とする。改質装置３からの燃焼ガスはメ
タノール蒸発器１５に導入されて、メタノールを蒸発さ
せ、蒸発したメタノールは改質装置３に送られて次式に
より水蒸気改質される。In the apparatus configured as described above, water is transferred to the water evaporator 1.
After being evaporated with high-temperature combustion gas from the catalytic combustor 22, this combustion gas is introduced into the reformer 3 and used as a heat source for reforming. The combustion gas from the reformer 3 is introduced into the methanol evaporator 15 to evaporate methanol, and the evaporated methanol is sent to the reformer 3 where it is steam reformed according to the following equation.
ＣＨコＯＩＩ＋ＨｚＯ→Ｃｏｔ＋３Ｈ。CH CoOII+HzO→Cot+3H.
Ｃｏｔ ＋ Ｈｚ →ＣＯ＋ＩＩｔＯ水素精製装置７
のオフガスは、一旦、オフガス貯蔵タンク２１に溜めら
れた後、触媒燃焼器２２へ燃料として供給される。そし
て、このオフガス供給量をオフガス貯蔵タンク２１の容
積または圧力が一定になるように、圧力指示調節計３２
、調節弁３０により制御するとともに、触媒燃焼器２２
の温度を補助燃料として供給するメタノール量によって
、温度指示調節計３３、調節弁３１を作動させて制御す
る。Cot + Hz → CO + IItO hydrogen purifier 7
The off-gas is once stored in the off-gas storage tank 21 and then supplied to the catalytic combustor 22 as fuel. Then, the pressure indicating controller 32 controls the off-gas supply amount so that the volume or pressure of the off-gas storage tank 21 is constant.
, a control valve 30, and a catalytic combustor 22.
The temperature is controlled by operating the temperature indicator controller 33 and control valve 31 depending on the amount of methanol supplied as auxiliary fuel.
本発明は上記のように構成されているので、つぎのよう
な効果を奏する。Since the present invention is configured as described above, it has the following effects.
（１）水とメタノールとをそれぞれ別々に供給し、別個
の蒸発器を設けているので、低レベルのエネルギーを効
率よく回収・利用することができる。(1) Since water and methanol are supplied separately and separate evaporators are provided, low-level energy can be efficiently recovered and utilized.
（２）高温ゾーン（約５００”Ｃ以上）の排熱は、原料
水の気化にしか使用されないので、メタノールの分解に
伴う炭素の析出を防止することができる。(2) Since the exhaust heat from the high temperature zone (approximately 500"C or higher) is used only for vaporizing the raw water, it is possible to prevent the precipitation of carbon accompanying the decomposition of methanol.
（３）オフガス貯蔵タンクの圧力または内容積を一定に
保つ制御方法、およびメタノール補助燃料による触媒燃
焼器制御方法を行う場合は、特別なオフガス過不足対策
を必要としない。(3) When performing a control method for keeping the pressure or internal volume of an off-gas storage tank constant and a method for controlling a catalytic combustor using methanol auxiliary fuel, no special measures against excess or deficiency of off-gas are required.
第１図は本発明のメタノール改質による水素製造装置の
一例を示すフローシート、第２図は従来の装置のフロー
シートである。FIG. 1 is a flow sheet showing an example of an apparatus for producing hydrogen by methanol reforming according to the present invention, and FIG. 2 is a flow sheet for a conventional apparatus.
Claims (1)
製して高純度水素を製造する方法において、メタノール
と水とをそれぞれ別個の蒸発器に供給し、水素精製の際
に発生するオフガスを触媒燃焼させて得た燃焼ガスを、
まず水の蒸発に用い、ついでメタノール改質に用いた後
、メタノールの蒸発に用いることを特徴とするメタノー
ル改質による水素製造方法。 ２ 水素精製の際に発生するオフガスを、一旦オフガス
貯蔵タンクに溜めた後、このオフガスを触媒燃焼器へ燃
料として供給し、このオフガス供給量をオフガス貯蔵タ
ンクの容積または圧力が一定になるように制御するとと
もに、触媒燃焼器の温度を補助燃料として供給するメタ
ノール量によって制御することを特徴とする請求項１記
載のメタノール改質による水素製造方法。 ３ メタノール改質装置（３）と水素精製装置（７）と
を組み合わせた高純度水素製造装置において、メタノー
ルタンク（１３）をメタノールポンプ（１４）、メタノ
ール予熱器（３４）およびメタノール蒸発器（１５）を
介して改質装置（３）に接続するとともに、水タンク（
１６）を水ポンプ（１７）、水予熱器（３５）および水
蒸発器（１８）を介して改質装置（３）に接続し、水素
精製装置（７）のオフガス出口をオフガス貯蔵タンク（
２１）を介して触媒燃焼器（２２）に接続し、この触媒
燃焼器（２２）の燃焼ガス出口を水蒸発器（１８）を介
して改質装置（３）に接続し、この改質装置（３）の燃
焼ガス出口をメタノール蒸発器（１５）に接続したこと
を特徴とするメタノール改質による水素製造装置。 ４ 触媒燃焼器（２２）内の入口部に白金担持触媒を充
填し、触媒燃焼器（２２）内の入口部より後流部にパラ
ジウム担持触媒を充填したことを特徴とする請求項３記
載のメタノール改質による水素製造装置。[Claims] 1. In a method of vaporizing methanol and reforming it with steam and then purifying it to produce high-purity hydrogen, methanol and water are each supplied to separate evaporators, and during hydrogen purification, The combustion gas obtained by catalytic combustion of the generated off-gas,
A method for producing hydrogen by reforming methanol, characterized in that it is first used to evaporate water, then used to reform methanol, and then used to evaporate methanol. 2 After the off-gas generated during hydrogen purification is temporarily stored in an off-gas storage tank, this off-gas is supplied as fuel to a catalytic combustor, and the amount of off-gas supplied is controlled so that the volume or pressure of the off-gas storage tank is constant. 2. The method for producing hydrogen by reforming methanol according to claim 1, wherein the temperature of the catalytic combustor is controlled by the amount of methanol supplied as auxiliary fuel. 3 In a high-purity hydrogen production device that combines a methanol reformer (3) and a hydrogen purification device (7), a methanol tank (13) is connected to a methanol pump (14), a methanol preheater (34), and a methanol evaporator (15). ) is connected to the reformer (3) via the water tank (
16) is connected to the reformer (3) via the water pump (17), water preheater (35) and water evaporator (18), and the off-gas outlet of the hydrogen purifier (7) is connected to the off-gas storage tank (
21) to a catalytic combustor (22), the combustion gas outlet of this catalytic combustor (22) is connected to a reformer (3) via a water evaporator (18), and this reformer A hydrogen production device by methanol reforming, characterized in that the combustion gas outlet of (3) is connected to a methanol evaporator (15). 4. The catalyst according to claim 3, characterized in that the inlet portion of the catalytic combustor (22) is filled with a supported platinum catalyst, and the portion downstream of the inlet portion of the catalytic combustor (22) is filled with a supported palladium catalyst. Hydrogen production equipment using methanol reforming.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63317215A JPH0733241B2 (en) | 1988-12-15 | 1988-12-15 | Method and apparatus for producing hydrogen by reforming methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63317215A JPH0733241B2 (en) | 1988-12-15 | 1988-12-15 | Method and apparatus for producing hydrogen by reforming methanol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02160601A true JPH02160601A (en) | 1990-06-20 |
| JPH0733241B2 JPH0733241B2 (en) | 1995-04-12 |
Family
ID=18085755
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63317215A Expired - Fee Related JPH0733241B2 (en) | 1988-12-15 | 1988-12-15 | Method and apparatus for producing hydrogen by reforming methanol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0733241B2 (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04164802A (en) * | 1990-10-29 | 1992-06-10 | Kawasaki Heavy Ind Ltd | Hydrogen production apparatus and starting thereof |
| US6096286A (en) * | 1997-10-20 | 2000-08-01 | Dbb Fuel Cell Engines Gmbh | System for steam reformation of a hydrocarbon and operating method therefor |
| CN1064022C (en) * | 1997-06-20 | 2001-04-04 | 中国科学院山西煤炭化学研究所 | Process for preparing high-purity hydrogen by converting methanol aqueous vapour |
| JP2001223017A (en) * | 2000-02-09 | 2001-08-17 | Toyota Motor Corp | Fuel gas generating system for fuel cell |
| JP2004352511A (en) * | 2003-05-26 | 2004-12-16 | Honda Motor Co Ltd | Pure hydrogen production device |
| US6838063B2 (en) | 2000-10-06 | 2005-01-04 | Denso Corporation | Hydrogen supply device |
| US6919055B2 (en) | 2000-08-30 | 2005-07-19 | Denso Corporation | Hydrogen supply device |
| JP2006282460A (en) * | 2005-03-31 | 2006-10-19 | Osaka Gas Co Ltd | Apparatus for producing hydrogen |
| JP2007063066A (en) * | 2005-08-31 | 2007-03-15 | Toshiba Corp | Method and equipment for producing hydrogen |
| CN110513686A (en) * | 2019-08-02 | 2019-11-29 | 武汉船用电力推进装置研究所（中国船舶重工集团公司第七一二研究所） | A kind of hydrogen catalytic combustion heating plant of no premix |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63230501A (en) * | 1987-03-19 | 1988-09-27 | Mitsubishi Heavy Ind Ltd | Methanol reformer for fuel cell |
-
1988
- 1988-12-15 JP JP63317215A patent/JPH0733241B2/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63230501A (en) * | 1987-03-19 | 1988-09-27 | Mitsubishi Heavy Ind Ltd | Methanol reformer for fuel cell |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04164802A (en) * | 1990-10-29 | 1992-06-10 | Kawasaki Heavy Ind Ltd | Hydrogen production apparatus and starting thereof |
| CN1064022C (en) * | 1997-06-20 | 2001-04-04 | 中国科学院山西煤炭化学研究所 | Process for preparing high-purity hydrogen by converting methanol aqueous vapour |
| US6096286A (en) * | 1997-10-20 | 2000-08-01 | Dbb Fuel Cell Engines Gmbh | System for steam reformation of a hydrocarbon and operating method therefor |
| JP2001223017A (en) * | 2000-02-09 | 2001-08-17 | Toyota Motor Corp | Fuel gas generating system for fuel cell |
| US6919055B2 (en) | 2000-08-30 | 2005-07-19 | Denso Corporation | Hydrogen supply device |
| US6838063B2 (en) | 2000-10-06 | 2005-01-04 | Denso Corporation | Hydrogen supply device |
| JP2004352511A (en) * | 2003-05-26 | 2004-12-16 | Honda Motor Co Ltd | Pure hydrogen production device |
| JP2006282460A (en) * | 2005-03-31 | 2006-10-19 | Osaka Gas Co Ltd | Apparatus for producing hydrogen |
| JP2007063066A (en) * | 2005-08-31 | 2007-03-15 | Toshiba Corp | Method and equipment for producing hydrogen |
| CN110513686A (en) * | 2019-08-02 | 2019-11-29 | 武汉船用电力推进装置研究所（中国船舶重工集团公司第七一二研究所） | A kind of hydrogen catalytic combustion heating plant of no premix |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0733241B2 (en) | 1995-04-12 |
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