JP3300896B2 - How to remove trace oxygen - Google Patents
How to remove trace oxygenInfo
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- JP3300896B2 JP3300896B2 JP25238691A JP25238691A JP3300896B2 JP 3300896 B2 JP3300896 B2 JP 3300896B2 JP 25238691 A JP25238691 A JP 25238691A JP 25238691 A JP25238691 A JP 25238691A JP 3300896 B2 JP3300896 B2 JP 3300896B2
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- Prior art keywords
- oxygen
- reaction
- adsorption tower
- catalyst
- water
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- Separation Of Gases By Adsorption (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
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Description
【０００１】[0001]
【産業上の利用分野】本発明は微量酸素の除去方法に関
し、詳しくは、ガス中に含まれる微量の酸素を水素と反
応させて水に変換し、生成した水を除去することによ
り、前記酸素を除去する方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for removing a trace amount of oxygen, and more particularly, to reacting a trace amount of oxygen contained in a gas with hydrogen to convert it into water, and removing the generated water to thereby remove the oxygen. And a method for removing the same.
【０００２】[0002]
【従来の技術】図２は、従来の一般的な酸素除去装置を
示すもので、ガス中に不純物として含まれている微量の
酸素と水素とを触媒反応により反応させて水に変換し、
生成した水を吸着除去するものである。2. Description of the Related Art FIG. 2 shows a conventional general oxygen removing apparatus, in which a very small amount of oxygen contained as an impurity in a gas is reacted with hydrogen by a catalytic reaction to convert it into water.
The generated water is adsorbed and removed.
【０００３】酸素を除去する被精製ガスは、該ガス中に
酸素との反応に必要な化学量論量より過剰な水素を含む
場合（被精製ガスが水素の場合も含む）はそのまま、水
素が不足する場合には、前工程で所定量の水素を添加さ
れた後、管１から供給される。When the gas to be purified from which oxygen is to be removed contains hydrogen in excess of the stoichiometric amount required for the reaction with oxygen (including the case where the gas to be purified is hydrogen), the hydrogen is directly converted to hydrogen. If the amount is insufficient, a predetermined amount of hydrogen is added in the previous step and then supplied from the pipe 1.
【０００４】被精製ガスは、熱交換器２で昇温した後、
さらに加熱器３で反応温度まで加熱されて反応塔４に導
入される。反応塔４内には、パラジウムや白金等の貴金
属を担体に担持させた触媒５が充填されており、該触媒
上で酸素と水素とが反応して水に変換される。このとき
の反応温度は、常温から約５００℃の範囲で行うことが
できるが、一般には１５０〜２５０℃で行われている。[0004] After the gas to be purified is heated in the heat exchanger 2,
Further, the mixture is heated to the reaction temperature by the heater 3 and introduced into the reaction tower 4. The reaction tower 4 is filled with a catalyst 5 in which a noble metal such as palladium or platinum is supported on a carrier, and oxygen and hydrogen react on the catalyst to be converted to water. The reaction temperature at this time can be in the range of room temperature to about 500 ° C, but is generally in the range of 150 to 250 ° C.
【０００５】上記反応により酸素を除去されたガスは、
管６を通って前記熱交換器２で降温した後、生成した水
を除去する吸着（乾燥）設備７に送られ、吸着工程にあ
る吸着塔で水分を除去されて精製ガスとなり管８から送
り出される。The gas from which oxygen has been removed by the above reaction is
After the temperature is lowered in the heat exchanger 2 through the pipe 6, the water is sent to an adsorption (drying) equipment 7 for removing generated water, and water is removed in an adsorption tower in an adsorption step to be purified gas to be sent out from a pipe 8. It is.
【０００６】上記吸着設備７は、複数、例えば２基の吸
着塔７ａ，７ｂを切替え可能に設けたものであって、い
わゆる温度変動吸着法により連続的にガス中の水分を除
去するものである。吸着塔内に充填される吸着剤として
は、一般にシリカゲル，アルミナゲル，ゼオライト等が
単独あるいは組み合わせて用いられる。The above-mentioned adsorption equipment 7 is provided with a plurality of, for example, two adsorption towers 7a and 7b so as to be switchable, and continuously removes moisture in a gas by a so-called temperature fluctuation adsorption method. . As the adsorbent filled in the adsorption tower, silica gel, alumina gel, zeolite, or the like is generally used alone or in combination.
【０００７】上記温度変動吸着法により水分を除去する
吸着操作としては、一般に次の３工程で構成されてい
る。 常温で水分を吸着除去する吸着工程 精製ガスの一部を流しながら加熱し、水分を脱着する
加熱工程 吸着剤を常温まで冷却する冷却工程 これらの工程を、両吸着塔７ａ，７ｂについて表１に示
す順序で繰り返すことにより連続的に水分の除去処理を
行う。[0007] The adsorption operation for removing water by the temperature fluctuation adsorption method generally comprises the following three steps. Adsorption step of adsorbing and removing moisture at room temperature Heating step of heating and desorbing water while flowing a part of purified gas Cooling step of cooling adsorbent to room temperature These steps are shown in Table 1 for both adsorption towers 7a and 7b. The water removal process is continuously performed by repeating in the order shown.
【０００８】[0008]
【表１】 [Table 1]
【０００９】例えば、吸着塔７ａが吸着工程にある表１
の工程１では、入口弁１０ａから水分を含むガスが吸着
塔７ａに導入され、処理されて出口弁１１ａから管８に
送り出されるとともに、加熱器１２の弁１２ａが開かれ
て精製ガスの一部が加熱器１２に導入され、加熱されて
加熱工程にある吸着塔７ｂに供給され、吸着剤に吸着さ
れている水分を脱着して再生出口弁１３ｂを経て排気管
１４から排出される。なお、このとき他の弁１０ｂ，１
１ｂ，１２ｂ，１３ａは閉である。次の工程２では、加
熱器１２の弁１２ａが閉じられるとともにバイパス弁１
２ｂが開かれ、精製ガスの一部が常温のまま吸着塔７ｂ
に供給される。For example, Table 1 shows that the adsorption tower 7a is in the adsorption step.
In step 1, a gas containing moisture is introduced into the adsorption tower 7a from the inlet valve 10a, processed and sent out from the outlet valve 11a to the pipe 8, and the valve 12a of the heater 12 is opened to open a part of the purified gas. Is introduced into the heater 12, heated and supplied to the adsorption tower 7b in the heating step, desorbs moisture adsorbed by the adsorbent, and is discharged from the exhaust pipe 14 via the regeneration outlet valve 13b. At this time, the other valves 10b, 1
1b, 12b and 13a are closed. In the next step 2, the valve 12a of the heater 12 is closed and the bypass valve 1
2b is opened, and a part of the purified gas is kept at normal temperature in the adsorption tower 7b.
Supplied to
【００１０】上記工程２を終えると、各弁が所定の順序
で切替え開閉されて工程３及び工程４に進み、吸着塔７
ｂが吸着工程に入り、吸着塔７ａが加熱工程及び冷却工
程に入る。When the above-mentioned step 2 is completed, each valve is switched and opened and closed in a predetermined order to proceed to steps 3 and 4, where the adsorption tower 7
b enters the adsorption step, and the adsorption tower 7a enters the heating step and the cooling step.
【００１１】[0011]
【発明が解決しようとする課題】上述のように、従来の
方法では、装置を構成する要素として、触媒塔，複数の
吸着塔，触媒設備用の加熱器及び熱交換器，吸着設備用
の加熱器等が必要であり、配管が複雑で装置の大きさも
大きくなるという欠点があった。As described above, in the conventional method, the components constituting the apparatus include a catalyst tower, a plurality of adsorption towers, a heater for a catalyst facility, a heat exchanger, and a heating apparatus for an adsorption facility. However, there is a drawback that a vessel or the like is required, the piping is complicated, and the size of the apparatus is increased.
【００１２】そこで本発明は、従来法よりも簡単な装置
構成で実施することができる微量酸素の除去方法を提供
することを目的としている。Accordingly, an object of the present invention is to provide a method for removing a trace amount of oxygen, which can be performed with a simpler apparatus configuration than the conventional method.
【００１３】[0013]
【課題を解決するための手段】上記した目的を達成する
ため、本発明の微量酸素の除去方法は、第１の構成とし
て、微量の酸素と、該酸素との反応に必要な化学量論量
より過剰な水素とを含むガスから酸素を除去する方法に
おいて、担体に担持させた触媒により前記酸素と水素と
を常温で反応させて水に変換し、生成した水を前記触媒
の担体に吸着させて除去するとともに、水を吸着した触
媒は加熱再生して繰り返し使用することを特徴としてい
る。In order to achieve the above object, the method for removing a trace amount of oxygen according to the present invention comprises, as a first configuration, a stoichiometric amount required for a reaction between a trace amount of oxygen and the oxygen. In a method for removing oxygen from a gas containing excess hydrogen, the catalyst supported on a carrier causes the oxygen and hydrogen to react at room temperature to be converted into water, and the generated water is adsorbed on the catalyst carrier. To remove water, and
The medium is characterized in that it is heated and regenerated and used repeatedly .
【００１４】また、本発明の第２の構成は、微量の酸素
と、該酸素との反応に必要な化学量論量より過剰な水素
とを含むガスから酸素を除去する方法において、担体に
担持させた触媒を充填した反応吸着塔を複数基設けると
ともに、反応吸着塔に前記酸素と水素とを含むガスを導
入して酸素と水素とを常温で担体に担持させた触媒によ
り反応させて水に変換し、生成した水を前記触媒の担体
に吸着させて除去する反応吸着工程と、反応吸着塔から
導出される精製ガスの一部を前記反応吸着工程を終了し
た反応吸着塔に導入するとともに該反応吸着塔を加熱し
て前記触媒の担体に吸着した水分を脱着する加熱工程
と、前記精製ガスの一部を該加熱工程を終えた反応吸着
塔に導入して該反応吸着塔を常温に冷却する冷却工程と
を、前記複数基の反応吸着塔について順次切替えて繰り
返すことにより、前記ガス中の酸素を連続的に除去する
ことを特徴としている。According to a second aspect of the present invention, there is provided a method for removing oxygen from a gas containing a trace amount of oxygen and a hydrogen in excess of a stoichiometric amount required for the reaction with the oxygen. A plurality of reaction adsorption towers filled with the reacted catalyst are provided, and the gas containing oxygen and hydrogen is introduced into the reaction adsorption tower, and oxygen and hydrogen are reacted at room temperature by a catalyst supported on a carrier to form water. Converting and adsorbing the produced water to the carrier of the catalyst and removing the water, and introducing a part of the purified gas derived from the reaction adsorption tower into the reaction adsorption tower after the reaction adsorption step. A heating step of heating the reaction adsorption tower to desorb moisture adsorbed on the catalyst carrier, and introducing a part of the purified gas into the reaction adsorption tower after the heating step to cool the reaction adsorption tower to room temperature. The cooling step of By repeating sequentially switching the adsorption tower it is characterized by the continuous removal of oxygen in the gas.
【００１５】[0015]
【作 用】上記構成によれば、触媒塔と吸着塔とを一体
化でき、乾燥工程を省略できるとともに、触媒設備用の
加熱器及び熱交換器が不要になり、装置構成を簡単なも
のとすることができる。[Operation] According to the above configuration, the catalyst tower and the adsorption tower can be integrated, the drying step can be omitted, and a heater and a heat exchanger for the catalyst equipment are not required, and the apparatus configuration can be simplified. can do.
【００１６】[0016]
【実施例】以下、本発明を、図１に示す一実施例に基づ
いて、さらに詳細に説明する。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, the present invention will be described in more detail based on one embodiment shown in FIG.
【００１７】本実施例装置は、２基の反応吸着塔を切替
え使用することにより連続して被精製ガス中の酸素を除
去できるようにしたものであり、２基の反応吸着塔２１
ａ，２１ｂと、加熱器２２と、両反応吸着塔２１ａ，２
１ｂを切替え運転するための複数の弁とから構成されて
いる。なお、被精製ガスは、前記同様に、除去すべき酸
素との反応に必要な化学量論量より過剰な水素を含むも
のである。The apparatus of this embodiment is designed so that the oxygen in the gas to be purified can be continuously removed by switching and using two reaction adsorption towers.
a, 21b, a heater 22, and both reaction adsorption columns 21a, 2
1b for switching operation. The gas to be purified contains hydrogen in excess of the stoichiometric amount necessary for the reaction with oxygen to be removed, as described above.
【００１８】反応吸着塔２１ａ，２１ｂ内には、微量の
水分を吸着することができる担体、例えばアルミナ等に
パラジウムや白金等を担持させた触媒兼吸着剤が充填さ
れており、常温で酸素と水素とを触媒反応させ、生成し
た水分を担体に吸着させて除去するようにしている。The reaction adsorption towers 21a and 21b are filled with a carrier capable of adsorbing a very small amount of water, for example, a catalyst / adsorbent in which palladium, platinum or the like is supported on alumina or the like. The catalyst reacts with hydrogen, and the generated water is adsorbed on a carrier and removed.
【００１９】また、微量の酸素とは、該酸素と水素との
反応熱により触媒兼吸着剤が常温以上、例えば４０℃以
上に昇温しない範囲であり、触媒兼吸着剤の種類やその
充填量（塔の大きさ）、被精製ガスの流速等により異な
るが、通常は１００ｐｐｍ程度以下をいう。The trace amount of oxygen refers to a range in which the temperature of the catalyst / adsorbent does not rise to above normal temperature, for example, 40 ° C. or more, due to the heat of reaction between the oxygen and hydrogen. (The size of the tower), it depends on the flow rate of the gas to be purified, etc., but usually means about 100 ppm or less.
【００２０】両反応吸着塔２１ａ，２１ｂは、次の３工
程を表２に示す順序で切り替えて運転される。 常温で酸素と水素とを反応させるとともに、生成した
水分を担体に吸着させて除去する反応吸着工程 精製ガスの一部を流しながら加熱し、水分を脱着する
加熱工程 吸着剤を常温まで冷却する冷却工程The two reaction adsorption towers 21a and 21b are operated by switching the following three steps in the order shown in Table 2. A reaction adsorption step in which oxygen and hydrogen are reacted at room temperature and the generated water is adsorbed and removed by a carrier. A heating step in which heating is performed while flowing a part of the purified gas to desorb water. Cooling to cool the adsorbent to room temperature Process
【００２１】[0021]
【表２】 [Table 2]
【００２２】例えば、反応吸着塔２１ａが反応吸着工程
にある表２の工程１では、入口管２３から導入される被
精製ガスが入口弁２４ａから反応吸着塔２１ａに導入さ
れ、処理されて出口弁２５ａから出口管２６に送り出さ
れるとともに、加熱器２２の加熱弁２２ａが開かれて精
製ガスの一部が加熱器２２に導入され、加熱されて加熱
工程にある反応吸着塔２１ｂに供給され、担体に吸着さ
れている水分を脱着して再生出口弁２７ｂを経て排気管
２８から排出される。For example, in step 1 in Table 2 in which the reaction adsorption tower 21a is in the reaction adsorption step, the gas to be purified introduced from the inlet pipe 23 is introduced into the reaction adsorption tower 21a from the inlet valve 24a, processed, and processed to the outlet valve. 25a, is sent out to the outlet pipe 26, and the heating valve 22a of the heater 22 is opened, a part of the purified gas is introduced into the heater 22, heated and supplied to the reaction adsorption tower 21b in the heating step, The water adsorbed on the gas is desorbed and discharged from the exhaust pipe 28 via the regeneration outlet valve 27b.
【００２３】この加熱再生工程は、前記のように精製ガ
スの一部を加熱してから再生工程にある反応吸着塔に導
入することにより行っても、また、反応吸着塔の内部あ
るいは外部にヒーター等を設けておいて、これにより加
熱を行いつつ精製ガスの一部を流通させることによって
行っても良い。This heating and regeneration step may be performed by heating a part of the purified gas and then introducing the purified gas into the reaction adsorption tower in the regeneration step as described above. Or the like may be provided, and a part of the purified gas may be circulated while heating by this.
【００２４】なお、このとき他の弁２２ｂ，２４ｂ，２
５ｂ，２７ａは閉である。次の工程２では、加熱器２２
の弁２２ａが閉じられるとともにバイパス弁２２ｂが開
かれ、精製ガスの一部が常温のまま反応吸着塔２１ｂに
供給される。At this time, the other valves 22b, 24b, 2
5b and 27a are closed. In the next step 2, the heater 22
Is closed and the bypass valve 22b is opened, and a part of the purified gas is supplied to the reaction adsorption tower 21b at room temperature.
【００２５】上記反応吸着塔２１ａの反応吸着工程は、
常温、例えば０〜４０℃程度（担体としての吸着剤又は
反応容器中に充填する吸着剤の水分吸着量が著しく低下
しない温度範囲）で行われ、被精製ガス中の酸素と水素
とを触媒反応させて水に変換するとともに、該生成した
水を触媒を担持する担体に吸着させて除去する。この反
応吸着工程は、水分を吸着する担体が破過する前に終了
し、工程３に進む。The reaction adsorption step of the reaction adsorption tower 21a includes:
The reaction is carried out at room temperature, for example, at about 0 to 40 ° C. (a temperature range in which the amount of water adsorbed by the adsorbent as a carrier or the adsorbent to be charged into the reaction vessel does not significantly decrease), and the catalytic reaction between oxygen and hydrogen in the gas to be purified Then, the water is converted into water, and the generated water is adsorbed and removed by a carrier supporting a catalyst. This reaction adsorption step is completed before the carrier that adsorbs moisture breaks through, and proceeds to step 3.
【００２６】工程３では、入口弁２４ａ，出口弁２５ａ
が閉じて反応吸着塔２１ｂ側の入口弁２４ｂ及び出口弁
２５ｂが開き、反応吸着塔２１ｂが反応吸着工程に入る
とともに、加熱器２２の加熱弁２２ａが開かれて反応吸
着塔２１ｂから導出された精製ガスの一部が加熱器２２
に導入され、加熱されて反応吸着塔２１ｂに供給され、
反応吸着塔２１ａが加熱工程に入る。In step 3, the inlet valve 24a and the outlet valve 25a
Is closed, the inlet valve 24b and the outlet valve 25b on the side of the reaction adsorption tower 21b are opened, the reaction adsorption tower 21b enters the reaction adsorption step, and the heating valve 22a of the heater 22 is opened to be drawn out of the reaction adsorption tower 21b. A part of the purified gas is supplied to the heater 22
And heated and supplied to the reaction adsorption tower 21b,
The reaction adsorption tower 21a enters a heating step.
【００２７】反応吸着塔２１ａ内の担体に吸着された水
分が十分に脱着された後、工程４に移り、加熱器２２の
弁２２ａが閉じられるとともにバイパス弁２２ｂが開か
れ、精製ガスの一部が常温のまま反応吸着塔２１ａに供
給され、反応吸着塔２１ａが冷却工程となる。そして、
工程４が終了すると各弁が切替え開閉されて前記工程１
に戻る。After the water adsorbed on the carrier in the reaction adsorption tower 21a is sufficiently desorbed, the process proceeds to step 4, where the valve 22a of the heater 22 is closed and the bypass valve 22b is opened, and a part of the purified gas is removed. Is supplied to the reaction adsorption tower 21a at a normal temperature, and the reaction adsorption tower 21a becomes a cooling step. And
When Step 4 is completed, each valve is switched and opened and closed, and Step 1 is performed.
Return to
【００２８】本実施例装置は、上記のようにして両反応
吸着塔２１ａ，２１ｂを切替えることにより連続して酸
素除去処理を行うことができる。なお、触媒の種類や充
填量、反応吸着塔の切替え時間等は、被精製ガス中に含
まれる酸素量や処理量に応じて適宜設定されるものであ
る。また、反応吸着塔の設置数は、処理を連続で行う必
要が無ければ１基でも良く、必要に応じて３基以上を切
替えるようにしても良い。さらに、生成した水分を吸着
除去するために、上記反応吸着塔に触媒とともに吸着剤
（乾燥剤）を充填しておくこともできる。この場合、両
者を層別に分けて充填しても良く、混合して充填しても
良い。The apparatus of this embodiment can continuously perform the oxygen removal treatment by switching the two reaction adsorption towers 21a and 21b as described above. The type and amount of the catalyst, the switching time of the reaction adsorption tower, and the like are appropriately set according to the amount of oxygen contained in the gas to be purified and the amount of processing. The number of the reaction adsorption towers may be one if there is no need to perform the treatment continuously, and three or more may be switched as needed. Furthermore, in order to adsorb and remove the generated water, the reaction adsorption tower may be filled with an adsorbent (drying agent) together with a catalyst. In this case, both may be filled separately for each layer, or may be mixed and filled.
【００２９】このように、従来の触媒反応塔と吸着塔と
を一体構成とした反応吸着塔を用いることにより、反応
工程の後に切替え使用する複数の吸着器からなる乾燥工
程を省略することができ、例えば、従来触媒反応塔１基
と吸着塔２基とで構成していた装置を反応吸着塔２基で
構成することが可能となり、装置の小型化が図れるとと
もに装置コストを低減できる。As described above, by using the conventional reaction and adsorption tower in which the catalytic reaction tower and the adsorption tower are integrated, the drying step including a plurality of adsorbers that are switched after the reaction step can be omitted. For example, an apparatus which has conventionally been constituted by one catalytic reaction tower and two adsorption towers can be constituted by two reaction adsorption towers, whereby the size of the apparatus can be reduced and the apparatus cost can be reduced.
【００３０】［実験例］ 実験例１ 水の電気分解により製造した水素中に含まれる約５ｐｐ
ｍの酸素を下記の条件で除去する実験を行った。なお、
触媒としては、パラジウムをアルミナに担持させたもの
を用いた。その結果、水素中の酸素を０．１ｐｐｍ以下
にすることができた。 ガス流量 １００Ｎｍ3 ／ｈ 触媒充填量 ６リットル 反応吸着塔切替え時間 ９６時間 実験例２ 圧力変動吸着式の窒素製造装置により製造された窒素中
に含まれる約５０ｐｐｍの酸素を下記の条件で除去する
実験を行った。なお、触媒としては、パラジウムをアル
ミナに担持させたものを用いた。その結果、窒素中の酸
素を０．１ｐｐｍ以下にすることができた。 ガス流量 １００Ｎｍ3 ／ｈ 触媒充填量 ３０リットル 反応吸着塔切替え時間 ４８時間EXPERIMENTAL EXAMPLE Experimental Example 1 About 5 pp contained in hydrogen produced by electrolysis of water
An experiment was conducted in which m oxygen was removed under the following conditions. In addition,
As the catalyst, palladium supported on alumina was used. As a result, oxygen in hydrogen could be reduced to 0.1 ppm or less. Gas flow rate 100 Nm 3 / h Catalyst filling amount 6 liter Reaction adsorption tower switching time 96 hours Experimental example 2 An experiment to remove approximately 50 ppm of oxygen contained in nitrogen produced by a pressure fluctuation adsorption type nitrogen production device under the following conditions. Was done. The catalyst used was palladium supported on alumina. As a result, oxygen in nitrogen could be reduced to 0.1 ppm or less. Gas flow rate 100Nm 3 / h Catalyst filling amount 30 liters Reaction adsorption tower switching time 48 hours
【００３１】[0031]
【発明の効果】以上説明したように、本発明の微量酸素
の除去方法は、被精製ガス中の酸素と水素とを触媒反応
により水に変換するとともに、生成した水を触媒の担体
で吸着除去するとともに、水を吸着した触媒は加熱再生
して繰り返し使用するようにしたから、従来の触媒塔と
吸着塔とを一体化することができ、通常設けられている
乾燥工程を省略することができるので、装置構成を簡単
にでき、小型化と低コスト化とを図ることができる。As described above, the method for removing a trace amount of oxygen according to the present invention converts oxygen and hydrogen in a gas to be purified into water by a catalytic reaction, and adsorbs and removes generated water by a catalyst carrier. At the same time, the water-adsorbed catalyst is heated and regenerated.
The conventional catalyst tower and adsorption tower can be integrated, and the drying step normally provided can be omitted, so that the apparatus configuration can be simplified and the size can be reduced. And cost reduction.
【図１】 本発明の一実施例を示す系統図である。FIG. 1 is a system diagram showing one embodiment of the present invention.
【図２】 従来の酸素除去装置の一例を示す系統図であ
る。FIG. 2 is a system diagram showing an example of a conventional oxygen removing device.
２１ａ，２１ｂ…反応吸着塔 ２２…加熱器 ２２
ａ…加熱弁 ２２ｂ…バイパス弁 ２３…入口管 ２４ａ，２４
ｂ…入口弁 ２５ａ，２５ｂ…出口弁 ２６…出口管 ２７ａ，
２７ｂ…再生出口弁 ２８…排気管21a, 21b ... reaction adsorption tower 22 ... heater 22
a: heating valve 22b: bypass valve 23: inlet pipe 24a, 24
b: Inlet valve 25a, 25b ... Outlet valve 26 ... Outlet pipe 27a,
27b: regeneration outlet valve 28: exhaust pipe
Claims (2)
学量論量より過剰な水素とを含むガスから酸素を除去す
る方法において、担体に担持させた触媒により前記酸素
と水素とを常温で反応させて水に変換し、生成した水を
前記触媒の担体に吸着させて除去するとともに、水を吸
着した触媒は加熱再生して繰り返し使用することを特徴
とする微量酸素の除去方法。1. A method for removing oxygen from a gas containing a trace amount of oxygen and a hydrogen in excess of a stoichiometric amount required for the reaction with the oxygen, the method comprising the steps of: intake was reacted at room temperature into a water, thereby removing by adsorbing water produced in the carrier of the catalyst, water
A method for removing a trace amount of oxygen, wherein the attached catalyst is heated and regenerated for repeated use .
化学量論量より過剰な水素とを含むガスから酸素を除去
する方法において、担体に担持させた触媒を充填した反
応吸着塔を複数基設けるとともに、反応吸着塔に前記酸
素と水素とを含むガスを導入して酸素と水素とを常温で
担体に担持させた触媒により反応させて水に変換し、生
成した水を前記触媒の担体に吸着させて除去する反応吸
着工程と、反応吸着塔から導出される精製ガスの一部を
前記反応吸着工程を終了した反応吸着塔に導入するとと
もに該反応吸着塔を加熱して前記触媒の担体に吸着した
水分を脱着する加熱工程と、前記精製ガスの一部を該加
熱工程を終えた反応吸着塔に導入して該反応吸着塔を常
温に冷却する冷却工程とを、前記複数基の反応吸着塔に
ついて順次切替えて繰り返すことにより、前記ガス中の
酸素を連続的に除去することを特徴とする微量酸素の除
去方法。2. A method for removing oxygen from a gas containing a trace amount of oxygen and a hydrogen in excess of a stoichiometric amount required for the reaction with the oxygen, the reaction adsorption column being filled with a catalyst supported on a carrier. And a gas containing oxygen and hydrogen is introduced into the reaction adsorption tower, oxygen and hydrogen are reacted with a catalyst supported on a carrier at room temperature to be converted into water, and the generated water is converted into water by the catalyst. A reaction adsorption step of adsorbing and removing the catalyst on the carrier, and introducing a part of the purified gas derived from the reaction adsorption tower into the reaction adsorption tower after the reaction adsorption step, and heating the reaction adsorption tower to form the catalyst. A heating step of desorbing water adsorbed on the carrier of the carrier, and a cooling step of introducing a part of the purified gas into the reaction adsorption tower after the heating step and cooling the reaction adsorption tower to normal temperature, Sequentially switch the reaction adsorption tower A method for removing trace amounts of oxygen, wherein oxygen in the gas is continuously removed by repeating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25238691A JP3300896B2 (en) | 1991-09-30 | 1991-09-30 | How to remove trace oxygen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25238691A JP3300896B2 (en) | 1991-09-30 | 1991-09-30 | How to remove trace oxygen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0592123A JPH0592123A (en) | 1993-04-16 |
| JP3300896B2 true JP3300896B2 (en) | 2002-07-08 |
Family
ID=17236603
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25238691A Expired - Lifetime JP3300896B2 (en) | 1991-09-30 | 1991-09-30 | How to remove trace oxygen |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3300896B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1997048640A1 (en) * | 1996-06-20 | 1997-12-24 | Ultraclean Technology Research Institute | Moisture generation method and moisture generator |
| JP3634115B2 (en) * | 1997-05-23 | 2005-03-30 | 大陽日酸株式会社 | Gas purification method and apparatus |
| KR100777672B1 (en) * | 2005-12-20 | 2007-11-28 | 코아텍주식회사 | Hydrogen Gas Scrubber System |
| KR101869461B1 (en) * | 2015-12-10 | 2018-06-20 | 동국대학교 산학협력단 | Method for removing oxygen in methane mixture gas by using oxygen catalyst, perovskite type oxygen removing catalyst used in the same, and land fill gas refine device applying land fill gas mathane direct converting technology using the same |
-
1991
- 1991-09-30 JP JP25238691A patent/JP3300896B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0592123A (en) | 1993-04-16 |
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