JPH04164802A - Hydrogen production apparatus and starting thereof - Google Patents
Hydrogen production apparatus and starting thereofInfo
- Publication number
- JPH04164802A JPH04164802A JP90291036A JP29103690A JPH04164802A JP H04164802 A JPH04164802 A JP H04164802A JP 90291036 A JP90291036 A JP 90291036A JP 29103690 A JP29103690 A JP 29103690A JP H04164802 A JPH04164802 A JP H04164802A
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- methanol
- gas
- fuel
- temperature
- 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
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 71
- 239000001257 hydrogen Substances 0.000 title claims abstract description 70
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 238000004519 manufacturing process Methods 0.000 title claims description 17
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 111
- 239000000446 fuel Substances 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 37
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000000746 purification Methods 0.000 claims abstract description 14
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 12
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 12
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 12
- 239000003345 natural gas Substances 0.000 claims abstract description 12
- 238000000629 steam reforming Methods 0.000 claims abstract 2
- 230000003197 catalytic effect Effects 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 9
- 238000001651 catalytic steam reforming of methanol Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 claims 1
- 238000002485 combustion reaction Methods 0.000 abstract description 11
- 239000003054 catalyst Substances 0.000 abstract description 8
- 238000002407 reforming Methods 0.000 abstract description 7
- 238000007084 catalytic combustion reaction Methods 0.000 abstract description 6
- 239000000567 combustion gas Substances 0.000 abstract description 4
- 239000006200 vaporizer Substances 0.000 abstract description 4
- 230000008016 vaporization Effects 0.000 abstract description 3
- 238000009834 vaporization Methods 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract 1
- 230000001590 oxidative effect Effects 0.000 abstract 1
- 238000000926 separation method Methods 0.000 abstract 1
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 4
- 239000003063 flame retardant Substances 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 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
- 239000002131 composite material Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野］
本発明は、メタノールと水蒸気とを原料とするメタノー
ル改質器と、水素製精製置置とを組み合わせて、高純度
水素を製造する水素製造装置の起動方法及び装置に関す
るものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention provides a hydrogen production device that produces high-purity hydrogen by combining a methanol reformer that uses methanol and steam as raw materials and a hydrogen purification unit. The present invention relates to a method and device for starting the system.
従来、メタノール改質による水素製造方式として、例え
ば、特開平２−１６０６０１号公報に記載された方式が
知られている。この方式は、第３図に示すように、改質
器１０と、発生した改質ガスから水素を分離・精製する
水素製精製置置１２と、改質ガスから水素を分離した後
の可燃性成分を含むオフガスを貯蔵するオフガスタンク
１４と、このオフガスタンク１４からのオフガスを主燃
料とし、メタノールを補助燃料とする触媒燃焼器１６と
を備え、改質器１０の加熱源として、触媒燃焼によって
得られる燃焼ガスを利用するものである。BACKGROUND ART Conventionally, as a hydrogen production method by methanol reforming, for example, a method described in JP-A-2-160601 is known. As shown in Figure 3, this system consists of a reformer 10, a hydrogen purification unit 12 that separates and purifies hydrogen from the generated reformed gas, and combustible components after hydrogen is separated from the reformed gas. and a catalytic combustor 16 that uses the off-gas from the off-gas tank 14 as a main fuel and methanol as an auxiliary fuel. This system uses the combustion gas produced by the combustion engine.
そして、触媒燃焼器１６を起動する場合は、改質用メタ
ノールの一部を燃焼用メタノールとして混合気化器１８
で気化させた後、触媒燃焼器１６で燃焼させ、装置が安
定化すると、オフガスに切り替えていた。２０は送風機
、２２は空気予熱器、２４はメタノールポンプである。When starting the catalytic combustor 16, a part of the reforming methanol is converted into combustion methanol to the mixture vaporizer 18.
After vaporizing it in the catalytic combustor 16, it was combusted in the catalytic combustor 16, and when the device became stable, it was switched to off-gas. 20 is a blower, 22 is an air preheater, and 24 is a methanol pump.
〔発明が解決しようとする課Ｂ］
上記のように、従来は、改質用メタノールの一部を燃焼
用メタノールとして気化させた後、触媒燃焼器で燃焼さ
せ、起動時の熱源、あるいは、通常運転時にオフガスを
燃料として用いる場合に不足する熱量の補助燃料として
いた。[Problem B to be solved by the invention] As mentioned above, in the past, a part of methanol for reforming was vaporized as methanol for combustion, and then combusted in a catalytic combustor. It was used as an auxiliary fuel to compensate for the lack of heat when using off-gas as fuel during operation.
一方、天然ガス・ＬＰＧ等の安価で一般的な低級炭化水
素系燃料を使用した方が経済的に有利である。On the other hand, it is economically advantageous to use inexpensive and common lower hydrocarbon fuels such as natural gas and LPG.
しかし、触媒燃焼器でこれらの燃料を着火させるために
は、２００〜４００℃の高温まで昇温する必要があり、
その起動方法に問題があった。つまり、このような燃料
を使用する場合は、バーナー燃焼によるのが一般的であ
り、触媒燃焼ではオフガス等の低カロリー燃料を安定燃
焼できるが、バーナー燃焼では失火トラブルが起こると
いう不具合があ本発明は上記の点に鑑みなされたもので
、触媒燃焼器の冷起動・室温着火を行うために、助燃用
メタノール、又は水素製精製置置７発生する水素の一部
を貯蔵していたものを用い、天然ガス・ＬＰＧ等の高温
でなければ触媒燃焼不能な低級炭化水素系燃料（難燃性
ガス）の燃焼開始温度まで昇温した後、これらの燃料に
切り替えて水素製造装置を起動する方法及び装置を提供
することを目的とするものである。However, in order to ignite these fuels in a catalytic combustor, it is necessary to raise the temperature to a high temperature of 200 to 400 degrees Celsius.
There was a problem with the startup method. In other words, when using such fuel, burner combustion is generally used. Catalytic combustion allows stable combustion of low-calorie fuels such as off-gas, but burner combustion has the disadvantage of causing misfire problems. was created in view of the above points, and in order to perform cold start and room temperature ignition of the catalytic combustor, methanol for auxiliary combustion or a portion of the hydrogen generated in the hydrogen refining station 7 is used, A method and device for starting a hydrogen production device by increasing the temperature of lower hydrocarbon fuels (flame-retardant gases) such as natural gas and LPG, which cannot be catalytically combusted unless they are at high temperatures, to the combustion start temperature, and then switching to these fuels. The purpose is to provide the following.
〔課題を解決するための手段及び作用〕上記の目的を達
成するために、本発明の水素製造装置の起動装置は、第
１図を参照して説明すれば、メタノールのスチームリフ
ォーミング反応により水素を含む改質ガスを発生する改
質器１ｏと、発生した改質ガスから水素を分離・精製す
る水素製精製置置１２と、改質ガスから水素を分離した
後の可燃性成分を含むオフガスを貯蔵するオフガスタン
ク１４と、このオフガスタンク１４からのオフガスを主
燃料とし、メタノールを補助燃料とする触媒燃焼器１６
とを備えた水素製造装置において、
触媒燃焼器１６に、天然ガス・ＬＰＧ等の低級炭化水素
系燃料ライン２６を接続したことを特徴としている。[Means and effects for solving the problem] In order to achieve the above object, the starting device for the hydrogen production apparatus of the present invention will be described with reference to FIG. A reformer 1o that generates a reformed gas containing combustible components, a hydrogen purification unit 12 that separates and purifies hydrogen from the generated reformed gas, and an off-gas containing combustible components after separating hydrogen from the reformed gas. An off-gas tank 14 for storing and a catalytic combustor 16 that uses the off-gas from the off-gas tank 14 as main fuel and methanol as auxiliary fuel.
The hydrogen production apparatus is characterized in that a lower hydrocarbon fuel line 26 such as natural gas or LPG is connected to the catalytic combustor 16.
そして、水素製造装置を起動するに際しては、触ＩＩＸ
燃焼器１６にメタノールを供給して常温で着火した後、
天然ガス・ＬＰＧ等の高温でなければ触媒燃焼不能な低
級炭化水素系燃料の着火温度以上に昇温し、この低級炭
化水素系燃料に切り替える。When starting up the hydrogen production equipment,
After methanol is supplied to the combustor 16 and ignited at room temperature,
The temperature is raised above the ignition temperature of a lower hydrocarbon fuel such as natural gas or LPG, which cannot be catalytically combusted unless the temperature is high, and the fuel is switched to the lower hydrocarbon fuel.
また、本発明の装置は、第２図を参照して説明すれば、
第１図に示す装置におけるメタノールの代りに、水素を
触媒燃焼器１６に供給できるように、水素製精製置置１
２の水素出口に水素の一部を貯蔵する水素貯蔵タンク２
８を設け、この水素貯蔵タンク２８と触媒燃焼器１６と
を水素ライン３０を介して接続したことを特徴としてい
る。Further, the device of the present invention will be described with reference to FIG.
In order to supply hydrogen to the catalytic combustor 16 instead of methanol in the apparatus shown in FIG.
Hydrogen storage tank 2 that stores a portion of hydrogen at the hydrogen outlet of No. 2
8 is provided, and this hydrogen storage tank 28 and the catalytic combustor 16 are connected via a hydrogen line 30.
そして、水素製造装置を起動するに際しては、メタノー
ルの代りに、水素製精製置置１２から発生する水素の一
部を用い、この水素を触媒燃焼器１６に供給して常温で
着火した後、天然ガス・ＬＰＧ等の燃料の着火温度以上
に昇温し、この燃料に切り替えた後、装置が安定化すれ
ば、オフガスに切り替える。Then, when starting up the hydrogen production equipment, a part of the hydrogen generated from the hydrogen purification unit 12 is used instead of methanol, and after supplying this hydrogen to the catalytic combustor 16 and igniting it at room temperature, natural gas・After increasing the temperature to above the ignition temperature of fuel such as LPG and switching to this fuel, if the device becomes stable, switch to off-gas.
〔実 施 例］
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。[Embodiments] 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 embodiment, their relative positions, etc. are not intended to limit the scope of the present invention to these, but are merely illustrative examples. Only.
実施例１
第１図は、本例の水素製造語！の起動装置を示している
０本例は、メタノール着火後、天然ガス・ＬＰＧ等の難
燃性ガスにき切り替える方式である。Example 1 Figure 1 shows the hydrogen production example of this example! In this example, after methanol is ignited, it is switched to a flame-retardant gas such as natural gas or LPG.
すなわち、メタノールと予熱空気とを混合気化器１８に
供給してメタノールを気化させた後、触媒燃焼器１６で
常温着火し、メタノール燃焼により昇温し、天然ガス・
ＬＰＧ等の難燃性ガスの着火温度以上になった時点で、
燃料をライン２６により難燃性ガスに切り替え、改質器
１０、水素製精製置置１２が安定化すると、オフガスに
切り替える。That is, after methanol and preheated air are supplied to the mixture vaporizer 18 to vaporize the methanol, it is ignited at room temperature in the catalytic combustor 16, the temperature is raised by methanol combustion, and natural gas and
When the temperature reaches or exceeds the ignition temperature of flame-retardant gas such as LPG,
The fuel is switched to a flame-retardant gas via the line 26, and when the reformer 10 and the hydrogen purification equipment 12 are stabilized, the fuel is switched to off-gas.
水素製精製置置としては、−例として、圧力揺動吸着型
（ｐｒｅｓｓｕｒｅ ｓｗｉｎｇ ａｄｓｏｒｐｔｉｏ
ｎ、、ｐｓＡ型）のものが用いられる。As a hydrogen purification system, for example, a pressure swing adsorption type
psA type) is used.
また、触媒燃焼器１６内に充填される燃焼触媒としては
、Ｐｔ、 Ｐｄ、 Ｒｕｎｇ、ＣＯ３Ｏ４、ＮｉＯ２Ｍ
ｎ０１等をアルミナ、シリカ、チタニア等一般に用いら
れている触媒担体に担持させた酸化触媒が用いられる。In addition, the combustion catalyst filled in the catalytic combustor 16 includes Pt, Pd, Rung, CO3O4, NiO2M.
An oxidation catalyst in which n01 or the like is supported on a commonly used catalyst carrier such as alumina, silica, or titania is used.
また、改質触媒としては、ＣｕＯ１ＺｎＯ，＾１．０２
、Ｃｒ！０１、ＬａｚＯｚ等からなる複合酸化物を還元
したもの、あるいは、酸化ジルコニウム、酸化マグネシ
ウム、酸化珪素、酸化アルミニウムからなる群より選ば
れた酸化物を主成分とする耐熱性無機質からなる多孔質
の触媒担体に、Ｃｕ、 Ｚｎ、 Ｐｄ、 Ｐｔ５Ｒｈ等
を担持して形成した触媒が用いられる。In addition, as a reforming catalyst, CuO1ZnO,^1.02
,Cr! 01. A porous catalyst made of a heat-resistant inorganic material whose main component is a reduced composite oxide such as LazOz, or an oxide selected from the group consisting of zirconium oxide, magnesium oxide, silicon oxide, and aluminum oxide. A catalyst formed by supporting Cu, Zn, Pd, Pt5Rh, etc. on a carrier is used.
改質器１０には、蒸発したメタノール及び水蒸気が供給
され、触媒燃焼器１６からの燃焼ガスにより間接的に加
熱されて、次式により水蒸気改質される。Evaporated methanol and steam are supplied to the reformer 10, heated indirectly by combustion gas from the catalytic combustor 16, and steam-reformed according to the following equation.
ＣＨ，ＯＨ＋ ＨＩＯ→Ｃｏ、 ＋３０ｚＣｏｔ 十Ｈ
１Ｃｏ ＋ ）ＩｚＯ
実施例２
本例は、第２図に示すように、水素製精製置置１２から
発生する水素の一部を水素貯蔵タンク２８に貯蔵してお
き、これを起動時の着火燃料とする方式である。CH, OH+ HIO→Co, +30zCot 10H
1Co + )IzO Example 2 In this example, as shown in FIG. 2, a part of the hydrogen generated from the hydrogen purification equipment 12 is stored in the hydrogen storage tank 28, and this is used as ignition fuel at startup. This is a method to do so.
本例では、メタノールを着火燃料とする代りに、室温で
の着火性がメタノールよりも良好な水素を使用する。貯
蔵する水素は、製品水素の一部、又は水素製精製置置１
２起動直後の水素とする。なお、水素製精製置置起動直
後の水素は、性状が安定しなので、従来は放出されてい
た。In this example, instead of using methanol as the ignition fuel, hydrogen, which has better ignitability at room temperature than methanol, is used. The hydrogen to be stored is a part of the product hydrogen or the hydrogen purification plant 1.
2 Hydrogen immediately after startup. In addition, since the properties of hydrogen immediately after starting up the hydrogen refining station are stable, conventionally it was released.
また、水素貯蔵タンク２８に水素吸蔵合金を充填し、タ
ンク容量のコンパクト化を図るようにするのが望ましい
、水素吸蔵合金は、０８、ｃｏ、 ＣＯ！。Further, it is desirable to fill the hydrogen storage tank 28 with a hydrogen storage alloy to make the tank capacity more compact. .
Ｈ，Ｏ等が含まれると、吸蔵能力の低下が起こるが、本
例では、水素製精製置置で精製した高純度の水素を使用
するので、このような問題は生じない。If H, O, etc. are included, the storage capacity will be reduced, but in this example, such a problem does not occur because high purity hydrogen purified by a hydrogen purification unit is used.
他の構成は実施例１の場合と同様である。The other configurations are the same as in the first embodiment.
本発明は上記のように構成されているので、っぎのよう
な効果を奏する。Since the present invention is configured as described above, it achieves the following effects.
（１）請求項１．３では、従来のメタノールを補助燃料
とする以外に、カロリー当りの単価の安い天然ガス・Ｌ
ＰＧ等の一般的な燃料の使用が可能となり、経済性が向
上する（因みに、天然ガスの単位ｋｃａｌ当りの価格は
メタノールの約２である）。(1) In claim 1.3, in addition to using conventional methanol as an auxiliary fuel, natural gas, which has a low unit price per calorie,
It becomes possible to use common fuels such as PG, improving economic efficiency (incidentally, the price per unit kcal of natural gas is about 2 times that of methanol).
（２）請求項２．４では、カロリー当りの単価の安い天
然ガス・ＬＰＧ等の一般的な燃料の使用が可能となる上
に、メタノールを気化させるために必要であった電気ヒ
ーターや補助燃料用メタノールの気化器等の付帯設備が
省略でき、しかも、メタノール気化温度までの予熱に要
する時間、電力の節約が可能となる。(2) Claim 2.4 allows the use of general fuels such as natural gas and LPG, which have a low unit price per calorie, and also enables the use of electric heaters and auxiliary fuels that were necessary to vaporize methanol. Incidental equipment such as a vaporizer for methanol can be omitted, and the time and power required for preheating to the methanol vaporization temperature can be saved.
第１図は本発明の水素製造装置の起動方法を実施する装
置の一例を示すフローシート、第２図は本発明の方法を
実施する装置の他の例を示すフロ−シート、第３図は従
来の水素製造装置を示すフローシートである。FIG. 1 is a flow sheet showing an example of an apparatus for carrying out the method for starting up a hydrogen production apparatus of the present invention, FIG. 2 is a flow sheet showing another example of an apparatus for carrying out the method of the present invention, and FIG. It is a flow sheet showing a conventional hydrogen production device.
Claims (1)
素を含む改質ガスを発生する改質器（１０）と、発生し
た改質ガスから水素を分離・精製する水素精製装置（１
２）と、改質ガスから水素を分離した後の可燃性成分を
含むオフガスを貯蔵するオフガスタンク（１４）と、こ
のオフガスタンク（１４）からのオフガスを主燃料とし
、メタノールを補助燃料とする触媒燃焼器（１６）とを
備えた水素製造装置を起動するに際し、 触媒燃焼器（１６）にメタノールを供給して常温で着火
した後、天然ガス・ＬＰＧ等の高温でなければ触媒燃焼
不能な低級炭化水素系燃料の着火温度以上に昇温し、こ
の低級炭化水素系燃料に切り替えることを特徴とする水
素製造装置の起動方法。 ２ メタノールの代りに、水素製精製置（１２）から発
生する水素の一部を用いることを特徴とする請求項１記
載の水素製造装置の起動方法。 ３ メタノールのスチームリフォーミング反応により水
素を含む改質ガスを発生する改質器（１０）と、発生し
た改質ガスから水素を分離・精製する水素精製装置（１
２）と、改質ガスから水素を分離した後の可燃性成分を
含むオフガスを貯蔵するオフガスタンク（１４）と、こ
のオフガスタンク（１４）からのオフガスを主燃料とし
、メタノールを補助燃料とする触媒燃焼器（１６）とを
備えた水素製造装置において、 触媒燃焼器（１６）に、天然ガス・ＬＰＧ等の低級炭化
水素系燃料ライン（２６）を接続したことを特徴とする
水素製造装置の起動装置。 ４ メタノールの代りに水素を触媒燃焼器（１６）に供
給できるように、水素精製装置（１２）の水素出口に水
素の一部を貯蔵する水素貯蔵タンク（２８）を設け、こ
の水素貯蔵タンク（２８）と触媒燃焼器（１６）とを水
素ライン（３０）を介して接続したことを特徴とする請
求項３記載の水素製造装置の起動装置。[Scope of Claims] 1. A reformer (10) that generates a reformed gas containing hydrogen through a steam reforming reaction of methanol, and a hydrogen purification device (10) that separates and purifies hydrogen from the generated reformed gas.
2), an off-gas tank (14) that stores off-gas containing combustible components after hydrogen is separated from the reformed gas, and the off-gas from this off-gas tank (14) is used as the main fuel, and methanol is used as the auxiliary fuel. When starting up a hydrogen production device equipped with a catalytic combustor (16), methanol is supplied to the catalytic combustor (16) and ignited at room temperature. A method for starting a hydrogen production device characterized by raising the temperature of a lower hydrocarbon fuel to a temperature higher than the ignition temperature and switching to the lower hydrocarbon fuel. 2. The method for starting up a hydrogen production device according to claim 1, characterized in that a part of hydrogen generated from the hydrogen production plant (12) is used instead of methanol. 3 A reformer (10) that generates reformed gas containing hydrogen through a methanol steam reforming reaction, and a hydrogen purification device (10) that separates and purifies hydrogen from the generated reformed gas.
2), an off-gas tank (14) that stores off-gas containing combustible components after hydrogen is separated from the reformed gas, and the off-gas from this off-gas tank (14) is used as the main fuel, and methanol is used as the auxiliary fuel. A hydrogen production device equipped with a catalytic combustor (16), characterized in that a lower hydrocarbon fuel line (26) such as natural gas or LPG is connected to the catalytic combustor (16). Starting device. 4. In order to supply hydrogen to the catalytic combustor (16) instead of methanol, a hydrogen storage tank (28) for storing a portion of hydrogen is provided at the hydrogen outlet of the hydrogen purification device (12). 4. The starting device for a hydrogen production device according to claim 3, wherein the catalytic combustor (16) and the catalytic combustor (28) are connected via a hydrogen line (30).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP90291036A JPH04164802A (en) | 1990-10-29 | 1990-10-29 | Hydrogen production apparatus and starting thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP90291036A JPH04164802A (en) | 1990-10-29 | 1990-10-29 | Hydrogen production apparatus and starting thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04164802A true JPH04164802A (en) | 1992-06-10 |
Family
ID=17763614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP90291036A Pending JPH04164802A (en) | 1990-10-29 | 1990-10-29 | Hydrogen production apparatus and starting thereof |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04164802A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0831055A2 (en) * | 1996-09-24 | 1998-03-25 | Daimler-Benz Aktiengesellschaft | Central heating apparatus for a gas generating system |
| EP0936182A3 (en) * | 1998-02-13 | 2000-02-23 | Haldor Topsoe A/S | Method of soot-free start-up of autothermal reformers |
| US6586125B2 (en) | 2000-04-12 | 2003-07-01 | Toyota Jidosha Kabushiki Kaisha | Combustion heating device, fuel reforming apparatus including combustion heating device, and fuel cell system |
| JP2004352511A (en) * | 2003-05-26 | 2004-12-16 | Honda Motor Co Ltd | Pure hydrogen production device |
| JP2005509582A (en) * | 2001-11-22 | 2005-04-14 | レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Hydrogen production apparatus and method of using the same |
| US7501456B2 (en) | 2006-04-27 | 2009-03-10 | Compactgtl Plc | Process for preparing liquid hydrocarbons |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61197402A (en) * | 1985-02-27 | 1986-09-01 | Hitachi Ltd | Apparatus for reforming fuel for fuel cell |
| JPH02160601A (en) * | 1988-12-15 | 1990-06-20 | Kawasaki Heavy Ind Ltd | Production of hydrogen by methanol reforming and apparatus therefor |
-
1990
- 1990-10-29 JP JP90291036A patent/JPH04164802A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61197402A (en) * | 1985-02-27 | 1986-09-01 | Hitachi Ltd | Apparatus for reforming fuel for fuel cell |
| JPH02160601A (en) * | 1988-12-15 | 1990-06-20 | Kawasaki Heavy Ind Ltd | Production of hydrogen by methanol reforming and apparatus therefor |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0831055A2 (en) * | 1996-09-24 | 1998-03-25 | Daimler-Benz Aktiengesellschaft | Central heating apparatus for a gas generating system |
| EP0831055A3 (en) * | 1996-09-24 | 1999-01-20 | dbb fuel cell engines GmbH | Central heating apparatus for a gas generating system |
| US6187066B1 (en) | 1996-09-24 | 2001-02-13 | Daimlerchrysler Ag | Central heating device for a gas-generating system |
| EP0936182A3 (en) * | 1998-02-13 | 2000-02-23 | Haldor Topsoe A/S | Method of soot-free start-up of autothermal reformers |
| US6586125B2 (en) | 2000-04-12 | 2003-07-01 | Toyota Jidosha Kabushiki Kaisha | Combustion heating device, fuel reforming apparatus including combustion heating device, and fuel cell system |
| JP2005509582A (en) * | 2001-11-22 | 2005-04-14 | レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Hydrogen production apparatus and method of using the same |
| JP2004352511A (en) * | 2003-05-26 | 2004-12-16 | Honda Motor Co Ltd | Pure hydrogen production device |
| US7501456B2 (en) | 2006-04-27 | 2009-03-10 | Compactgtl Plc | Process for preparing liquid hydrocarbons |
| TWI405718B (en) * | 2006-04-27 | 2013-08-21 | Compactgtl Ltd | Process for preparing liquid hydrocarbons |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8061120B2 (en) | Catalytic EGR oxidizer for IC engines and gas turbines | |
| US8397509B2 (en) | Catalytic engine | |
| US6767530B2 (en) | Method for producing hydrogen | |
| EP2004544B1 (en) | Fuel steam reformer system and reformer startup process | |
| US7438734B2 (en) | Direct water vaporization for fuel processor startup and transients | |
| JP2003502812A (en) | Method for providing a pure hydrogen stream for a fuel cell | |
| US8163046B2 (en) | Start-up process for a unit for producing highly thermally-integrated hydrogen by reforming a hydrocarbon feedstock | |
| JP2010513835A (en) | Hybrid combustor for fuel processing applications | |
| EP1358694A2 (en) | Process for air enrichment in producing hydrogen for use with fuel cells | |
| KR20070061883A (en) | A process for the catalytic partial oxidation of a liquid hydrocarbonaceous fuel | |
| JP2003529014A (en) | Multi-stage combustion for fuel processing for use with fuel cells | |
| JPH04164802A (en) | Hydrogen production apparatus and starting thereof | |
| JP3771357B2 (en) | Hydrogen production method | |
| JP3813391B2 (en) | Solid polymer fuel cell power generator and method of operating the same | |
| KR101832136B1 (en) | High Efficient compact steam reforming reactor using regenerative burner | |
| EP0207620B1 (en) | Energy recovery | |
| JPH0733241B2 (en) | Method and apparatus for producing hydrogen by reforming methanol | |
| JPS6232227A (en) | Method of recovering energy from low heating value fuel gas | |
| JP2000191304A (en) | Liquid fuel evaporator and reformer for fuel cell using the same | |
| JPS63129002A (en) | Internal heating fuel reformer | |
| JP4116731B2 (en) | Hydrogen generator and operation method thereof | |
| JPH0725521B2 (en) | Fuel reforming method for fuel cell | |
| JP2002042851A (en) | Fuel cell system | |
| JPH04268108A (en) | Multiple-stage catalytic combustion apparatus with built-in start-up means | |
| JPH01186761A (en) | Power generation device of fuel cell |