JPH01208302A - Hydrogen generator of on-site type - Google Patents
Hydrogen generator of on-site typeInfo
- Publication number
- JPH01208302A JPH01208302A JP2875188A JP2875188A JPH01208302A JP H01208302 A JPH01208302 A JP H01208302A JP 2875188 A JP2875188 A JP 2875188A JP 2875188 A JP2875188 A JP 2875188A JP H01208302 A JPH01208302 A JP H01208302A
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- fuel
- tank
- valve
- stored
- 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 102
- 239000001257 hydrogen Substances 0.000 title claims abstract description 102
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 101
- 238000010438 heat treatment Methods 0.000 claims abstract description 34
- 239000002828 fuel tank Substances 0.000 claims abstract description 17
- 238000007084 catalytic combustion reaction Methods 0.000 claims description 13
- 150000001298 alcohols Chemical class 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 238000000629 steam reforming Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 abstract description 52
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 32
- 238000000034 method Methods 0.000 abstract description 14
- 238000004904 shortening Methods 0.000 abstract description 2
- 230000003197 catalytic effect Effects 0.000 abstract 1
- 238000007796 conventional method Methods 0.000 abstract 1
- 230000000994 depressogenic effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- 238000002485 combustion reaction Methods 0.000 description 11
- 239000000498 cooling water Substances 0.000 description 10
- 239000003345 natural gas Substances 0.000 description 10
- 238000010926 purge Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000004043 responsiveness Effects 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野）
本発明は、触媒燃焼により発生する熱て炭化水素やアル
コール類を水蒸気改質して水素または水素リッチなガス
を製造するオンサイト型水素発生装置。Detailed Description of the Invention (Field of Industrial Application) The present invention is an on-site hydrogen generation system that produces hydrogen or hydrogen-rich gas by steam reforming hot hydrocarbons and alcohols generated by catalytic combustion. Device.
（従来技術）
大型水素製造プラントで製造した水素をボンベやカード
ルに詰めて水素使用場所に輸送する代りに、水素使用場
所で必要時に必要な量だけ水素を ・製造する据置
き式の水素発生装置はオンサイト型水素発生装置と呼ば
れており、この種の水素発生装置で製造した水素を使用
する装置の一例として、この水素または水素リッチなガ
スを燃料とする業務用燃料電池か挙げられる。業務用燃
料電池は大型発電所から送電線により供給される電力の
一部の代りに、ホテルや病院等のビル単位や地域単位の
需要場所て必要時に必要なだけの電力を発電するものと
して利用されている。(Prior technology) Instead of packing the hydrogen produced at a large hydrogen production plant into cylinders or cards and transporting it to the hydrogen usage site, this is a stationary hydrogen generator that produces hydrogen in the required amount at the hydrogen usage site, when it is needed. is called an on-site hydrogen generator, and an example of a device that uses hydrogen produced by this type of hydrogen generator is a commercial fuel cell that uses this hydrogen or hydrogen-rich gas as fuel. Commercial fuel cells can be used to replace a portion of the electricity supplied from large power plants via power lines, and can be used to generate the amount of electricity needed when needed by buildings such as hotels and hospitals, or by regional demand locations. has been done.
従来のオンサイト型水素発生装置のシステム構成例を第
２図に示す。原料天然ガスは、脱硫塔ｌで硫黄分が取除
かれ、原料予熱器２で予熱された後、水蒸気を混合され
てリフオー７８の反応部に供給され、ここで水素を豊富
に含むガスに改質される。リフオー７８を出た改質ガス
は、プロセスボイラ９で冷却された後、シフトコンバー
タ１０でガス中の一酸化炭素が水と反応し、二酸化炭素
と水素に転換される。続いてこのガスは原料予熱器２、
スチームスーパーヒーター７、ボイラ給水子熱器５、プ
ロセスガスクーラ１１で冷却され。FIG. 2 shows an example of the system configuration of a conventional on-site hydrogen generator. The raw natural gas has its sulfur content removed in the desulfurization tower 1, is preheated in the raw material preheater 2, is mixed with water vapor, and is supplied to the reaction section of the reflow 78, where it is converted into hydrogen-rich gas. questioned. The reformed gas that has exited the reflow 78 is cooled in the process boiler 9, and then in the shift converter 10, carbon monoxide in the gas reacts with water and is converted into carbon dioxide and hydrogen. Next, this gas is sent to the raw material preheater 2,
It is cooled by a steam super heater 7, a boiler water heater 5, and a process gas cooler 11.
プロセスガスクーラム１２で水分が除去されて、コンプ
レッサー１３で昇圧され、アフタークーラー１４で再び
冷却されてＰＳＡ１５に至り、ＰＳＡで純度の高い製品
水素と不純分を多く含んだパージガスとに分離される。Moisture is removed in the process gas cooler 12, the pressure is increased by the compressor 13, and the gas is cooled again by the aftercooler 14 to reach the PSA 15, where it is separated into product hydrogen with high purity and purge gas containing many impurities.
パージガス中にはまだ可燃成分である水素や一酸化炭素
が残っているので、このパージガスはパージガスドラム
１６に一旦貯えられた後、図中燃料３と記した図示しな
い経路て送られて燃料空気予熱器１９で予熱されてリフ
オーマ８の加熱部の燃料として用いられる。Since the purge gas still contains combustible components such as hydrogen and carbon monoxide, this purge gas is temporarily stored in the purge gas drum 16 and then sent through an unillustrated path marked as fuel 3 in the figure to preheat the fuel air. The fuel is preheated in a vessel 19 and used as fuel for the heating section of the reheater 8.
他方ブロワ１７により昇圧された空気は、同じく燃料空
気予熱器１９で予熱されリフオー７８の加熱部の燃焼に
用いられる。リフオー７８の加熱部には、ＰＳＡ排ガス
のような低カロリーで圧力変動のあるガスを低ＮＯｘで
燃焼させることができ且つ燃焼部の容積の小さい触媒燃
焼方式が採用されている。リフオー７８の起動時に必要
な加熱部の燃料および負荷増加時に不足する燃料として
は、原料天然ガスが用いられる（図示燃料１）。On the other hand, the air pressurized by the blower 17 is similarly preheated by the fuel air preheater 19 and used for combustion in the heating section of the reflow 78. The heating section of the reflow 78 employs a catalytic combustion system that can burn low-calorie gas with pressure fluctuations, such as PSA exhaust gas, with low NOx and has a small volume of combustion section. Raw material natural gas is used as the fuel for the heating section that is necessary when starting the reflow 78 and the fuel that is insufficient when the load increases (fuel 1 in the figure).
リフオー７８の起動時には、燃焼用空気はスタートアッ
プヒーター１８により天然ガスのメタンの着火温度３５
０℃以上に予熱される。水は、純水装置３からポンプ４
にて送り出され、ボイラ給水子熱器５て予熱され、プロ
セスガスボイラ９と補助ボイラ６により気化されて、ス
チームスーパーヒーター７により加熱され、原料天然ガ
スと混合される。When starting up the reflow 78, the combustion air is heated to the ignition temperature of natural gas methane by the startup heater 18 at 35°C.
Preheated to 0°C or higher. Water is pumped from pure water device 3 to pump 4
The gas is sent out, preheated by the boiler feed water subheater 5, vaporized by the process gas boiler 9 and auxiliary boiler 6, heated by the steam super heater 7, and mixed with raw natural gas.
第４図は、水素または水素リッチなガスを燃料とする従
来の業務用燃料電池のシステム構成例を示す。FIG. 4 shows an example of the system configuration of a conventional commercial fuel cell that uses hydrogen or hydrogen-rich gas as fuel.
天然ガス等の原料はエジェクタ２４（または混合器）に
より水蒸気と混合されてリフオー７８の反応部に供給さ
れ、ここで水素を豊富に含むガスに改質される。このガ
スは、続いてシフトコンバーター１０に導かれ、・ガス
中の一酸化炭素が水と反応して二醜化炭素と水素に転換
される０次いてガス中に余分の水分がある場合はこれを
除去した後、燃料電池３２のアノードＡに導かれ、ここ
で約８０％の水素が消費され、残り２０％の水素を含む
アノード排ガスはりフォー７８の加熱部ＢＮＲに戻され
、改質反応に必要な燃焼熱を発生するための燃料の一部
に用いられる。リフオー７８の加熱部ＢＮＲには、前述
と同様の触媒燃焼方式が採用されている。A raw material such as natural gas is mixed with water vapor by the ejector 24 (or mixer) and supplied to the reaction section of the reflow 78, where it is reformed into a hydrogen-rich gas. This gas is then led to the shift converter 10, where the carbon monoxide in the gas reacts with water and is converted into carbon dioxide and hydrogen.Then, if there is excess moisture in the gas, it is removed. After removal, it is led to the anode A of the fuel cell 32, where about 80% of the hydrogen is consumed, and the anode exhaust gas containing the remaining 20% hydrogen is returned to the heating section BNR of the Four 78, which is necessary for the reforming reaction. It is used as part of the fuel to generate significant combustion heat. The heating part BNR of the reflow 78 employs the same catalytic combustion method as described above.
空気はブロワ１７により昇圧され、燃料電池３２のカソ
ードにおよびリフオー７８の加熱部ＢＮＲに供給される
。Air is pressurized by the blower 17 and supplied to the cathode of the fuel cell 32 and the heating section BNR of the reflow 78.
燃料電池３２のカソードＫからの排出空気およびリフオ
ー７８の加熱部ＢＮＲからの排ガスは合流して排ガス用
熱交換器３１に導かれ、循環水等によって排ガス中の水
分が凝縮するまで冷却されて排熱回収が行なわれる０回
収された水分は水タンク２９に導かれ再利用される。The exhaust air from the cathode K of the fuel cell 32 and the exhaust gas from the heating part BNR of the reflow 78 are combined and guided to the exhaust gas heat exchanger 31, where they are cooled by circulating water or the like until the moisture in the exhaust gas is condensed, and then exhausted. The recovered moisture is led to the water tank 29 and reused.
冷却水は冷却水ポンプ２７により昇圧され、燃料電池３
２の電池冷却装置に供給され、燃料電池３２からの発生
熱を奪った後、蒸気発生器２５でフラッシュされる。こ
こで冷却水の一部は水蒸気となり、エジェクタ２４に導
かれる。残りは給水ポンプ２８からの補給水と合流し、
再び冷却水ポンプ２７に導かれる。この冷却水系で発生
した余剰の熱は冷却水用熱交換器２６により温水等の系
て回収される。The pressure of the cooling water is increased by the cooling water pump 27, and the pressure is increased by the cooling water pump 27.
After being supplied to the battery cooling device No. 2 and removing the heat generated from the fuel cell 32, it is flashed at the steam generator 25. Here, a part of the cooling water becomes water vapor and is guided to the ejector 24. The remaining water is combined with makeup water from the water supply pump 28,
The cooling water is guided to the cooling water pump 27 again. Excess heat generated in the cooling water system is recovered by the cooling water heat exchanger 26 as hot water or the like.
以上述べたようなオンサイト型水素製造装置や業務用燃
料電池はリフオーマの加熱部に触媒燃焼方式を用いれば
、ＰＳＡ排ガスやアノード排ガスのような低カロリーの
ガスをリフオーマ加熱部の燃料として低ＮＯ，で 安定
に燃焼させることができ且つ燃焼部の容積も小さくでき
るものであるから、必要な場所で必要な量の水素や電力
を発生させてコストの合理化を図ろうとするオンサイト
型水素発生装置や業務用燃料電池の目的から見て、かか
る触媒燃焼方式のりフォーマ加熱部を採用することのメ
リットは大きい。The on-site hydrogen production equipment and commercial fuel cells described above can use low-calorie gases such as PSA exhaust gas and anode exhaust gas as fuel for the re-o-o-mer heating part, with low NO, if a catalytic combustion method is used in the re-o-o-o-o-o-o-o-o-o-o-o-o-ma heating part. On-site hydrogen generation equipment aims to generate the required amount of hydrogen and electricity at the required location and to rationalize costs, as it is capable of stable combustion and the volume of the combustion part can be reduced. From the viewpoint of commercial fuel cells and commercial fuel cells, there are great advantages in adopting such a catalytic combustion type glue former heating section.
（発明が解決しようとする問題点）
オンサイト型水素発生装置は、必要とする場所で必要と
する時に必要なだけの水素を製造することがてきるもの
であるから、迅速な起動および速い負荷応答性が求めら
れる。起動時間の決定要因はりフォーマの昇温時間であ
るが、前記従来技術のようにリフオーマの加熱部に触媒
燃焼方式を採用した場合、天然ガスの主成分であるメタ
ンの着火温度が３５０℃以上と高いため１着火するまて
に要する加熱時間が長くなり、起動までに時間がかかる
という問題がある。また、水素発生装置で製造した水素
または水素リッチなガスを燃料とする業務用燃料電池も
、必要とする場所て必要とする時に必要とする量の発電
をするものであるから、迅速な起動および負荷応答性が
求められる。(Problems to be Solved by the Invention) On-site hydrogen generators can produce the required amount of hydrogen at the required location and at the required time, so they can be started up quickly and loaded quickly. Responsiveness is required. The determining factor for the start-up time is the heating time of the reformer, but when a catalytic combustion method is adopted for the heating section of the reformer as in the conventional technology, the ignition temperature of methane, the main component of natural gas, is 350°C or higher. Because of the high temperature, it takes a long time to heat up for one ignition, and there is a problem that it takes a long time to start up. In addition, commercial fuel cells that use hydrogen or hydrogen-rich gas produced by a hydrogen generator as fuel can generate the required amount of power at the required location and time, so they can be started up quickly and Load responsiveness is required.
したがって、その燃料である水素発生装置のりフォーマ
の加熱部に触媒燃焼方式を採用した場合、上述と同様の
問題がある。Therefore, when a catalytic combustion method is adopted for the heating section of the fuel former of the hydrogen generator, problems similar to those described above arise.
本発明の目的は、リフオーマ加熱部に触媒燃焼方式を用
いたオンサイト型水素発生装Ｍ（それが水素を燃料とす
る燃料電池に利用される場合も含む）において上記問題
点を解決し、起動時間の短縮を図ることにある。The purpose of the present invention is to solve the above-mentioned problems in an on-site hydrogen generation system M using a catalytic combustion method in the re-former heating section (including the case where it is used in a fuel cell that uses hydrogen as fuel), and to start up the system. The purpose is to save time.
（問題点を解決するための手段）
上記目的を解決するため、本発明は、炭化水素やアルコ
ール類を水蒸気改質するために必要な熱を与えるための
触媒燃焼方式の加熱部を有するリフオーマを備えたオン
サイト型水素発生装置において、起動用燃料タンクと、
該起動用燃料タンクに上記水素発生装置で発生された水
素の一部を導入する配管と、該起動用燃料タンク中に貯
えられた水素をリフオーマの加熱部に導く配管と、これ
ら配管中に設けられた開閉弁とを設けたことを特徴とす
るものである。(Means for Solving the Problems) In order to solve the above object, the present invention provides a reformer having a catalytic combustion heating section for providing the heat necessary for steam reforming hydrocarbons and alcohols. In the on-site hydrogen generator equipped with a startup fuel tank,
A pipe for introducing a part of the hydrogen generated by the hydrogen generator into the start-up fuel tank, a pipe for guiding the hydrogen stored in the start-up fuel tank to the heating part of the reheater, and a pipe installed in these pipes. The invention is characterized in that it is provided with an on-off valve.
（作 用）
上記水素発生装置の運転中、該水素発生装置によって製
造された水素の一部を起動用燃料タンクに貯えておき、
水素発生装置の起動時には、起動用燃料タンク中に貯え
られた水素をリフオーマの加熱部に起動用燃料として供
給する。水素は約５０″Ｃで着火するので、メタンを起
動用燃料とする従来技術に比べて起動時間は大幅に短縮
される。起動後、運転状態に入った後には、水素発生装
置によって製造された水素の一部を再び起動用燃料タン
クに貯えることによって起動時に消費した水素を補って
おく、こうすることにより、起動の都度、起動用燃料タ
ンク中の水素を起動用燃料として供給することができる
。(Function) During operation of the hydrogen generator, a part of the hydrogen produced by the hydrogen generator is stored in a startup fuel tank,
When starting up the hydrogen generator, hydrogen stored in the starting fuel tank is supplied as starting fuel to the heating section of the reheater. Since hydrogen ignites at approximately 50"C, the start-up time is significantly reduced compared to conventional technology that uses methane as the start-up fuel. After start-up and operation, the hydrogen generated by the hydrogen generator is Part of the hydrogen is stored in the startup fuel tank again to replenish the hydrogen consumed during startup. By doing this, the hydrogen in the startup fuel tank can be supplied as startup fuel each time the vehicle is started. .
（実 施 例）
第１図は本発明によるオンサイト型水素発生装置の一実
施例のシステム構成を示すもので、第２図の従来例と異
なる点は、起動用燃料タンク２０と、このタンク２０に
水素発生装置により製造されたＰＳＡ１５からの水素の
一部を導入するための弁２１付き配管と、タンク２０に
貯えられた水素なりフォー７８の触媒燃焼方式の加熱部
に導くための弁２２．２３付き配管とを設けた点であり
、他の構成は第２図と同じである。(Embodiment) FIG. 1 shows the system configuration of an embodiment of the on-site hydrogen generator according to the present invention.The difference from the conventional example shown in FIG. A pipe with a valve 21 for introducing a part of the hydrogen from the PSA 15 produced by the hydrogen generator into the tank 20, and a valve 22 for guiding the hydrogen stored in the tank 20 to the heating section of the catalytic combustion system of the Four 78. .23 piping is provided, and the other configurations are the same as in FIG. 2.
運転中、製造された水素の一部は弁２１を開くことによ
って起動用燃料タンク２０に貯えられる。起動時には、
タンク２０に貯えられた水素な゛ 減圧弁２２て減圧
して、三方切換弁２３を介して図中に燃料３と記した図
示しない配管路を経てリフオーマ８の加熱部に起動用燃
料として水素を供給する。水素は約５０℃で着火するの
で、約３５０″Ｃで着火するメタンを起動用燃料とする
従来技術の場合に比べて起動時間は遥かに短かくなる。During operation, a portion of the hydrogen produced is stored in the start-up fuel tank 20 by opening the valve 21. At startup,
The pressure of the hydrogen stored in the tank 20 is reduced by the pressure reducing valve 22, and hydrogen is supplied as starting fuel to the heating section of the reheater 8 via a three-way switching valve 23 and a piping path (not shown) marked as fuel 3 in the figure. supply Since hydrogen ignites at about 50°C, the start-up time is much shorter than in the prior art, where the start-up fuel is methane, which ignites at about 350"C.
リフオー７８の加熱部の燃焼触媒で着火した後はタンク
２０からの水素の供給を絞り１図中に燃料ｌと記した天
然ガスをリフオーマ８の加熱部に供給してリフオーマの
昇温を行う、系全体の動作が立ち上がり、水素が製造さ
れ始めたら三方切換弁２３を切替え、ＰＳＡ１５のオフ
ガス（パージガス）をリフオー７８の加熱部に燃料とし
て供給し、燃料の不足分は天然ガスで補う、これによっ
て前記第２図で説明したと同様の通常の運転状態になる
。運転中、弁２１を開いて、発生した水素の余剰分を再
び起動用燃料２０に貯える。After ignition by the combustion catalyst in the heating section of the reflow 78, the hydrogen supply from the tank 20 is throttled, and natural gas, indicated as fuel l in Figure 1, is supplied to the heating section of the reflowr 8 to raise the temperature of the reflowr. When the operation of the entire system starts up and hydrogen begins to be produced, the three-way switching valve 23 is switched, the off-gas (purge gas) of the PSA 15 is supplied as fuel to the heating section of the reflow 78, and the shortage of fuel is made up with natural gas. The normal operating state is the same as that described in FIG. 2 above. During operation, the valve 21 is opened and the generated surplus hydrogen is stored again in the starting fuel 20.
なお、負荷増大時や装置の一時停止など、負荷である水
素需要装置への水素が不足する時には弁２１を開いて起
動用燃料タンク２０内の貯蔵水素を負荷である水素需要
装置に供給することかできる。この場合、タンク２０内
の水素か一起動用としては不足することが考えられるが
、−時停止が短時間であれば、リフオーマ加熱部の燃焼
触媒の温度は十分高く保たれているとみてよいので、メ
タンを主成分とする天然ガスで充分起動できる。また、
負荷が急減した時には余った製造水素をタンク２０に貯
蔵し、負荷が急増した場合には不足分の水素をタンク２
０から供給することによって、負荷追従性を改善するこ
とも可能である。Note that when there is a shortage of hydrogen to the hydrogen demand device, which is the load, such as when the load increases or when the device is temporarily stopped, the valve 21 may be opened to supply the hydrogen stored in the startup fuel tank 20 to the hydrogen demand device, which is the load. I can do it. In this case, it is possible that the hydrogen in the tank 20 is insufficient for one start, but if the - time stop is short, it can be assumed that the temperature of the combustion catalyst in the re-boomer heating section is kept sufficiently high. Therefore, natural gas, whose main component is methane, is sufficient to start the process. Also,
When the load suddenly decreases, surplus produced hydrogen is stored in tank 20, and when the load suddenly increases, the hydrogen shortage is stored in tank 2.
It is also possible to improve load followability by supplying from zero.
本実施例は、起動用燃料として水素を用いためスタート
アップヒーター１８の温度が低くなり、容量も小さくて
済むため、リフオーマ８の燃焼触媒を直接加熱すること
が容易となり、リフオーマの小型化と起動時間の短縮を
図ることができる。In this embodiment, since hydrogen is used as the startup fuel, the temperature of the startup heater 18 is low and the capacity is also small, so it is easy to directly heat the combustion catalyst of the refoomer 8, which reduces the size of the refoomer and reduces the startup time. The time can be shortened.
起動用に水素を用いるだけなら、他所からボンベやカー
ドルに詰めて運ばれた水素を用いることも考えられるが
、それでは必要な場所で製造するというオンサイト形水
素製造装置の本来の意義が薄れる。これに対し、本発明
ではオンサイト型水素発生装置で製造した水素を起動用
に用いるのでこのような欠点は生じない。If hydrogen is only used for startup, it may be possible to use hydrogen packed in cylinders or cards from elsewhere, but that would diminish the original significance of on-site hydrogen production equipment, which allows hydrogen to be produced where it is needed. On the other hand, in the present invention, such a drawback does not occur because hydrogen produced by an on-site hydrogen generator is used for startup.
第３図は、本発明によるオンサイト型水素発生装置を水
素を燃料とする業務用燃料電池システムに適用した実施
例を示すもので、第４図の従来例と異なる点は、起動用
燃料タンク２０と、水素発生装置で発生させたシフトコ
ンバータから燃料電池３２のアノードＡに導かれる水素
の一部をタンク２０に導く弁２１付き配管と、タンク２
０内に貯えられた水素をリフオー７８の触媒燃焼方式の
加熱部に導く弁２２．２３付き配管とを設けた点であり
、他の構成は第４図゛と同じである。Figure 3 shows an embodiment in which the on-site hydrogen generator according to the present invention is applied to a commercial fuel cell system using hydrogen as fuel.The difference from the conventional example in Figure 4 is that the starting fuel tank 20, a pipe with a valve 21 that guides a part of the hydrogen that is generated by the hydrogen generator to the anode A of the fuel cell 32 from the shift converter to the tank 20, and the tank 2.
The other difference is that pipes with valves 22 and 23 are provided to guide the hydrogen stored in the reflow 78 to the catalytic combustion type heating section of the reflow 78, and other configurations are the same as in FIG.
運転中、リフオー７８て製造されアノードＡに向う水素
の一部を起動用燃料タンク２０に貯えておき、その後の
起動時にはタンク２０に貯えられた水素を起動用燃料と
してリフオー７８の加熱部に導き、起動後は三方切替弁
２３を切換えて、アノード排ガスをリフオー７８の加熱
部に燃料として送って運転し運転時のり７オ一マ加熱部
の燃料不足分は天然ガスで補う、負荷変動時や一時停止
時における作動については第１図の実施例の場合と同じ
である。During operation, a part of the hydrogen produced by the reflow 78 and destined for the anode A is stored in the startup fuel tank 20, and during subsequent startup, the hydrogen stored in the tank 20 is guided to the heating section of the reflow 78 as startup fuel. After startup, the three-way switching valve 23 is switched and the anode exhaust gas is sent as fuel to the heating section of the reflow 78 during operation, and the fuel shortage in the reflow 78 heating section is supplemented with natural gas. The operation during a temporary stop is the same as in the embodiment shown in FIG.
（発明の効果）
本発明によれば、触媒燃焼方式リフオーマ加熱部の持つ
特徴、すなわち、（１）低カロリーガス、低酸素濃度で
も安定した燃焼が容易にできる。（２）燃焼部分の容積
が小さくできる、（３）圧力変動の影響がない、（４）
Ｎｏ、の発生がすくない、という特徴を生かしながら、
パイロットバーナーも水素ボンベも用いず、スタートア
ップヒーターの容量を小さくした上で起動時間を短縮で
きる。また装置の短時間停止時の水素連続供給も可能と
なり、さらに、負荷変動を吸収するバッファの役目を果
たすこともでき、システムの負荷追従性を向上させるこ
もできる。(Effects of the Invention) According to the present invention, the characteristics of the catalytic combustion type re-former heating section are as follows: (1) Stable combustion can be easily achieved even with low calorie gas and low oxygen concentration. (2) The volume of the combustion part can be reduced, (3) There is no effect of pressure fluctuations, (4)
While taking advantage of the feature that there are few No, occurrences,
It does not use a pilot burner or a hydrogen cylinder, reducing the capacity of the startup heater and shortening startup time. Furthermore, it is possible to continuously supply hydrogen when the device is stopped for a short time, and it can also serve as a buffer to absorb load fluctuations, thereby improving the load followability of the system.
第１図は本発明によるオンサイト型水素発生装置の一実
施例の概略系統図、第２図は従来のオンサイト型水素発
生装置の概略系統図、第３図は本発明によるオンサイト
型水素発生装置を用いた業務用燃料電池の概略系統図、
第４図は従来のオンサイト型水素発生装置を用いた業務
用燃料電池の概略系統図である。
ｌ・・・脱硫塔、２・・・原料予熱器、３・・・純水装
置、４・・・ポンプ、５・・・ボイラ給水子熱器、６・
・・補助ボイラ、７・・・スチームスーパーヒーター、
８−・・リフオーマ、９・・・プロセスガスボイラ、１
０・・・シフトコンバーター、ｌ ｌ−・・プロセスガ
スクーラー、１２・・・プロセスガスボイラ’ラム、１
３・・・コンプレッサー、１４−・・アフタークーラー
、１５・・・ＰＳＡ、１６−・・パージガスドラム、１
７・・・ブロワ、１８・・・スタートアップヒーター、
１９・・・燃料・空気予熱器、２０・・・起動用燃料タ
ンク、２１・・・貯蔵・供給用弁、２２−・・減圧弁、
２３・・・燃料切替弁、２４・・・エジェクタ、２５・
・・蒸気発生器、２６・・・冷却水用熱交換器、２７・
・・冷却水ポンプ、２８・・・給水ポンプ、２９−・・
水タンク、３０・・・インバータ、３１・・・排ガス用
熱交換器、３２・・・燃料電池Figure 1 is a schematic system diagram of an embodiment of an on-site hydrogen generator according to the present invention, Figure 2 is a schematic diagram of a conventional on-site hydrogen generator, and Figure 3 is an on-site hydrogen generator according to the present invention. Schematic diagram of a commercial fuel cell using a generator,
FIG. 4 is a schematic diagram of a commercial fuel cell using a conventional on-site hydrogen generator. 1... Desulfurization tower, 2... Raw material preheater, 3... Pure water device, 4... Pump, 5... Boiler feed water heater, 6...
...Auxiliary boiler, 7...Steam super heater,
8--Reformer, 9--Process gas boiler, 1
0...Shift converter, l l-...Process gas cooler, 12...Process gas boiler'ram, 1
3... Compressor, 14-... Aftercooler, 15-... PSA, 16-... Purge gas drum, 1
7... Blower, 18... Startup heater,
19... Fuel/air preheater, 20... Starting fuel tank, 21... Storage/supply valve, 22-... Pressure reducing valve,
23... Fuel switching valve, 24... Ejector, 25...
...Steam generator, 26...Cooling water heat exchanger, 27.
...Cooling water pump, 28...Water supply pump, 29-...
Water tank, 30... Inverter, 31... Exhaust gas heat exchanger, 32... Fuel cell
Claims (1)
熱を与えるための触媒燃焼方式の加熱部を有するリフォ
ーマを備えたオンサイト型水素発生装置において、起動
用燃料タンクと、該起動用燃料タンクに上記水素発生装
置で発生された水素の一部を導入する弁付き配管と、該
起動用燃料タンクに貯えられた水素をリフォーマの加熱
部に導く弁付き配管とを設けたことを特徴とするオンサ
イト型水素発生装置。In an on-site hydrogen generator equipped with a reformer having a catalytic combustion type heating section for providing the heat necessary for steam reforming hydrocarbons and alcohols, a startup fuel tank and a startup fuel tank are provided. A valved pipe for introducing a part of the hydrogen generated by the hydrogen generator, and a valved pipe for guiding the hydrogen stored in the startup fuel tank to the heating section of the reformer are provided. On-site hydrogen generator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2875188A JPH01208302A (en) | 1988-02-12 | 1988-02-12 | Hydrogen generator of on-site type |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2875188A JPH01208302A (en) | 1988-02-12 | 1988-02-12 | Hydrogen generator of on-site type |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH01208302A true JPH01208302A (en) | 1989-08-22 |
Family
ID=12257113
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2875188A Pending JPH01208302A (en) | 1988-02-12 | 1988-02-12 | Hydrogen generator of on-site type |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH01208302A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001520576A (en) * | 1997-04-15 | 2001-10-30 | インターナショナル フュエル セルズ コーポレイション | Apparatus and method for producing gas |
| WO2004014788A1 (en) * | 2002-08-09 | 2004-02-19 | Honda Giken Kogyo Kabushiki Kaisha | Hydrogen generating apparatus |
| JP2004352511A (en) * | 2003-05-26 | 2004-12-16 | Honda Motor Co Ltd | Pure hydrogen production device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6110001A (en) * | 1984-06-22 | 1986-01-17 | Mitsubishi Heavy Ind Ltd | Device for modifying fuel |
| JPS61197402A (en) * | 1985-02-27 | 1986-09-01 | Hitachi Ltd | Apparatus for reforming fuel for fuel cell |
-
1988
- 1988-02-12 JP JP2875188A patent/JPH01208302A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6110001A (en) * | 1984-06-22 | 1986-01-17 | Mitsubishi Heavy Ind Ltd | Device for modifying fuel |
| JPS61197402A (en) * | 1985-02-27 | 1986-09-01 | Hitachi Ltd | Apparatus for reforming fuel for fuel cell |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001520576A (en) * | 1997-04-15 | 2001-10-30 | インターナショナル フュエル セルズ コーポレイション | Apparatus and method for producing gas |
| WO2004014788A1 (en) * | 2002-08-09 | 2004-02-19 | Honda Giken Kogyo Kabushiki Kaisha | Hydrogen generating apparatus |
| JP2004352511A (en) * | 2003-05-26 | 2004-12-16 | Honda Motor Co Ltd | Pure hydrogen production device |
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