JP3532466B2 - Air separation device - Google Patents
Air separation deviceInfo
- Publication number
- JP3532466B2 JP3532466B2 JP20685199A JP20685199A JP3532466B2 JP 3532466 B2 JP3532466 B2 JP 3532466B2 JP 20685199 A JP20685199 A JP 20685199A JP 20685199 A JP20685199 A JP 20685199A JP 3532466 B2 JP3532466 B2 JP 3532466B2
- Authority
- JP
- Japan
- Prior art keywords
- raw material
- material air
- tower
- catalyst
- air
- 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.)
- Expired - Fee Related
Links
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、空気分離装置に関
するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an air separation device.
【０００２】[0002]
【従来の技術】従来から、空気分離装置において、原料
空気中の不純物（ＣＯ・Ｈ2 等）を除去する前処理装置
として、触媒を使用した酸化反応タイプが用いられてい
る。その理由は、深冷分離方法では、ＣＯとＮ2 の沸点
が極めて近いこと、また、Ｈ2はＮ2 より沸点が低いこ
とから、ＣＯ・Ｈ2 とＮ2 との分離が困難であるからで
ある。したがって、前処理段階で、触媒によりＣＯ・Ｈ
2 とＯ2 とを反応させてそれぞれＣＯ2 ・Ｈ2 Ｏに変化
させてから、吸着塔によりＣＯ2 ・Ｈ2 Ｏを吸着除去す
る方法が採用されている。Heretofore, in an air separation unit, a processing unit prior to the removal of impurities in the feed air (CO · H 2, etc.), an oxidation reaction type using a catalyst is used. The reason is that the cryogenic separation method, the boiling point of CO and N 2 is very close, also, since the H 2 has a boiling point less than N 2, because separation of CO · H 2 and N 2 is difficult Is. Therefore, in the pretreatment stage, CO
A method is employed in which 2 and O 2 are reacted to change each to CO 2 · H 2 O, and then CO 2 · H 2 O is adsorbed and removed by an adsorption tower.
【０００３】[0003]
【発明が解決しようとする課題】通常、圧縮機による圧
縮熱を有効利用するために、圧縮機の吐出側に前処理装
置を接続している。この場合に、夏場の水分の多い時期
やＳＯX の多く含まれる環境下で運転すると、水分およ
びＳＯX は触媒毒であるため、触媒は被毒し活性が低下
する。そして、活性が低下すると、酸化反応率が低下
し、ｐｐｂオーダーでのＣＯ・Ｈ2 の除去が困難とな
る。また、水分の被毒は一次的なものであり、水分の少
ない冬場になれば、活性をある程度取り戻すものの、Ｓ
ＯX は永久的に被毒し、再活性化は難しい。Usually, a pretreatment device is connected to the discharge side of the compressor in order to effectively utilize the compression heat of the compressor. In this case, when operated in an atmosphere containing a lot of watery timing and SO X in summer, moisture and SO X because a catalyst poison, catalyst poisoning and activity decreases. When the activity decreases, the rate of oxidation reaction decreases and it becomes difficult to remove CO · H 2 on the ppb order. In addition, water poisoning is temporary, and although it regains some activity in winter when the water content is low, S
O X is permanently poisoned, reactivation is difficult.
【０００４】そこで、このような状況を打開するため
に、触媒の反応温度を高め、より活性の高い条件で運転
を行うことや、ＳＯX を反応除去する充填物を前処理段
階に設置すること等の対策が行われているが、大きな効
果が得られていない。また、最近のガスに要望される不
純物含有量は、低下の一途をたどっており、超高純度化
が強く要求されている（ｐｐｂレベル）。しかしなが
ら、現在の装置では、このような要求を長期間満足させ
ることができていないのが実情である。Therefore, in order to overcome such a situation, it is necessary to raise the reaction temperature of the catalyst to operate under conditions of higher activity and to install a packing for reacting and removing SO X in the pretreatment stage. Although measures such as these have been implemented, no major effect has been obtained. In addition, the content of impurities required for recent gases is steadily decreasing, and ultra-high purification is strongly required (ppb level). However, in the current device, such a requirement cannot be satisfied for a long period of time.
【０００５】本発明は、このような事情に鑑みなされた
もので、原料空気中の水分，ＳＯXが少ない環境で、触
媒による酸化反応が効率良く行える空気分離装置の提供
をその目的とする。The present invention has been made in view of the above circumstances, and an object thereof is to provide an air separation device capable of efficiently carrying out an oxidation reaction by a catalyst in an environment in which the amount of water and SO X in the feed air is small.
【０００６】[0006]
【課題を解決するための手段】上記の目的を達成するた
め、本発明の空気分離装置は、外部より取り入れた原料
空気を圧縮する圧縮機と、この圧縮機による圧縮熱によ
って昇温した原料空気を水と熱交換させて冷却する第１
の熱交換器と、この第１の熱交換器による冷却によって
発生した凝縮水を分離する凝縮水分離器と、この凝縮水
分離器を経た原料空気中の水分をさらに吸着して除湿す
るとともに酸化イオウを代表とする触媒毒を吸着する第
１の吸着塔と、原料空気中の一酸化炭素および水素を酸
化する触媒塔と、上記第１の吸着塔を経た原料空気と触
媒塔を経た原料空気とを熱交換させて上記第１の吸着塔
を経た原料空気を昇温させるとともに上記触媒塔を経た
原料空気を降温させる第２の熱交換器と、この第２の熱
交換器を経た原料空気を加熱するヒーターと、このヒー
ターにより加熱された原料空気を上記触媒塔に導入して
原料空気中の一酸化炭素および水素を酸化させる導入路
と、上記触媒塔から取り出されたのち第２の熱交換器を
経由した原料空気を冷却水により冷却する第３の熱交換
器と、この第３の熱交換器により冷却された原料空気中
の炭酸ガスと水とを吸着して除去する第２の吸着塔と、
この第２の吸着塔を経た原料空気を超低温に冷却する主
熱交換手段と、この主熱交換手段により超低温に冷却さ
れた原料空気の一部を液化して底部に溜め窒素のみを気
体として上部側から取り出す精留塔と、この精留塔から
気体として取り出される窒素を上記主熱交換手段を経由
させその内部を通る原料空気と熱交換させることにより
温度上昇させ取り出す窒素ガス取出路とを備えたという
構成をとる。In order to achieve the above object, the air separation apparatus of the present invention is a compressor for compressing raw material air taken from the outside, and a raw material air heated by the heat of compression by the compressor. For cooling water by exchanging heat with water
Heat exchanger, a condensed water separator that separates condensed water generated by cooling by the first heat exchanger, and moisture in the raw material air that has passed through the condensed water separator is further adsorbed to dehumidify and oxidize. A first adsorption tower that adsorbs a catalyst poison represented by sulfur, a catalyst tower that oxidizes carbon monoxide and hydrogen in the raw material air, a raw material air that has passed through the first adsorption tower, and a raw material air that has passed through the catalyst tower. And a second heat exchanger for raising the temperature of the raw material air that has passed through the first adsorption tower and lowering the temperature of the raw material air that has passed through the catalyst tower, and the raw material air that has passed through the second heat exchanger. A heater for heating the catalyst, an inlet passage for introducing the raw material air heated by the heater into the catalyst tower to oxidize carbon monoxide and hydrogen in the raw material air, and a second heat after being taken out from the catalyst tower. Raw material air passed through the exchanger A third heat exchanger for cooling the coolant, a second adsorption tower for adsorbing and removing the carbon dioxide and water in the feed air which is cooled by the third heat exchanger,
Main heat exchanging means for cooling the raw material air that has passed through the second adsorption tower to an ultra low temperature, and a part of the raw material air cooled to the ultra low temperature by this main heat exchanging means is liquefied and stored in the bottom portion only nitrogen as a gas A rectification column to be taken out from the side, and a nitrogen gas take-out passage to take out nitrogen, which is taken out as a gas from this rectification tower, by raising the temperature by exchanging heat with the raw material air passing through the main heat exchange means. Take the configuration.
【０００７】すなわち、本発明の空気分離装置は、圧縮
機と主熱交換手段の間に、第１の熱交換器と凝縮水分離
器と第１の吸着塔と第２の熱交換器とヒーターと触媒塔
と第３の熱交換器と第２の吸着塔とを備えている。そし
て、第１の熱交換器により、圧縮機による圧縮熱によっ
て昇温した原料空気を水（例えば、３２℃以下の冷却
水）と熱交換させて冷却し、ついで凝縮水分離器によ
り、第１の熱交換器による冷却によって発生した凝縮水
を分離し、つぎに第１の吸着塔により、凝縮水分離器を
経た原料空気中の水分をさらに吸着して除湿するととも
に酸化イオウを代表とする触媒毒を吸着し、つぎに第２
の熱交換器により、第１の吸着塔を経た原料空気を触媒
塔を経た原料空気と熱交換させて昇温させ、つぎにヒー
ターにより、第２の熱交換器により昇温された原料空気
をさらに（第２の熱交換器の温端温度差分）加熱し、つ
ぎに触媒塔により、ヒーターを経た原料空気中の一酸化
炭素および水素を酸化し、つぎに第２の熱交換器によ
り、触媒塔を経た原料空気を第１の吸着塔を経た原料空
気と熱交換させて降温させ、つぎに第３の熱交換器によ
り第２の熱交換器により降温された原料空気を冷却水に
よりさらに冷却し、つぎに第２の吸着塔により、第３の
熱交換器により降温された原料空気中の炭酸ガスと水と
を吸着して除去したのち、精製ガスとして主熱交換手
段，精留塔に導入するようにしている。That is, in the air separation apparatus of the present invention, the first heat exchanger, the condensed water separator, the first adsorption tower, the second heat exchanger, and the heater are provided between the compressor and the main heat exchange means. And a catalyst tower, a third heat exchanger, and a second adsorption tower. Then, the first heat exchanger exchanges heat with the water (for example, cooling water having a temperature of 32 ° C. or less) of the raw material air that has been heated by the heat of compression by the compressor to cool the raw material air. Condensed water generated by cooling by the heat exchanger is separated, and then the first adsorption tower further adsorbs moisture in the raw material air that has passed through the condensed water separator to dehumidify it and a catalyst represented by sulfur oxide. Adsorb the poison, then the second
Heat exchange of the raw material air that has passed through the first adsorption tower with the raw material air that has passed through the catalyst tower to raise the temperature, and then by the heater, the raw material air that has been raised in temperature by the second heat exchanger. Further heating (difference in the temperature of the second heat exchanger), then the catalyst tower oxidizes carbon monoxide and hydrogen in the feed air that has passed through the heater, and then the second heat exchanger conducts the catalyst. The raw material air that has passed through the tower is heat-exchanged with the raw material air that has passed through the first adsorption tower to lower the temperature, and then the raw material air that has been cooled by the second heat exchanger by the third heat exchanger is further cooled by cooling water. Then, the second adsorption tower adsorbs and removes carbon dioxide gas and water in the raw material air whose temperature has been lowered by the third heat exchanger, and then the purified gas is supplied to the main heat exchange means and the rectification tower. I am trying to introduce it.
【０００８】このように、本発明では、凝縮水分離器に
より凝縮水を分離するときに、原料空気中の水分、およ
び凝縮水に溶け込んだ原料空気中の大半のＳＯX を除去
することができ、また、第１の吸着塔によりさらに水分
およびＳＯX を除去することができる。したがって、触
媒塔に原料空気を導入する前に、原料空気中の水分・Ｓ
ＯX をほとんど除去することができる。その結果、反応
環境がドライになり、つぎの効果が得られる。すなわ
ち、触媒の反応率が高くなり、このため、ガスの精製度
が良くなり、高純度のガスが得られる。しかも、触媒毒
の水分がないため、ガスの精製度が良くなり、高純度の
ガスが得られるとともに、触媒が長寿命になる。しか
も、触媒が水分により膨脹しないため、触媒が粉化しに
くくなり、長寿命になる。また、反応環境に触媒毒であ
るＳＯX がなく、つぎの効果が得られる。すなわち、触
媒の反応率が高くなり、このため、ガスの精製度が良く
なり、高純度のガスが得られるとともに、触媒が長寿命
になる。また、上記の効果から、従来の仕様を満足させ
る装置を設計した場合に、触媒の反応温度を低下させる
ことができ、つぎの効果が得られる。すなわち、触媒本
体（貴金属等）が酸化しにくくなるため、触媒の寿命が
長くなる。しかも、触媒本体の加熱温度が低くなるた
め、触媒が粉化しにくくなり、長寿命になる。しかも、
第２の熱交換器の熱交換量が少なくなるため、第２の熱
交換器を小さくすることができ、低コストになる。しか
も、触媒の充填量を少なくすることができるため、触媒
量を減らすことができ、低コストになる。しかも、触媒
量を減らすことができるため、触媒塔が小さくなり、低
コストになる。さらに、第２の熱交換器の熱交換量が少
ないこと、触媒の充填量が少ないこと、および、触媒量
が減少することから、放熱が少なくなり、ヒーターを小
さくすることができて低コストになるうえ、消費電力が
減って省エネになる。このように、本発明によれば、高
純度化，低コスト化，省エネ化を実現することができ
る。As described above, according to the present invention, when the condensed water is separated by the condensed water separator, the water in the raw material air and most of the SO X in the raw material air dissolved in the condensed water can be removed. Further, water and SO X can be further removed by the first adsorption tower. Therefore, before introducing the raw material air into the catalyst tower, the water content of the raw material air
Most of O x can be removed. As a result, the reaction environment becomes dry, and the following effects are obtained. That is, the reaction rate of the catalyst is increased, and thus the purification degree of the gas is improved and a high-purity gas is obtained. Moreover, since there is no water that is a catalyst poison, the degree of purification of the gas is improved, high-purity gas is obtained, and the catalyst has a long life. Moreover, since the catalyst does not expand due to water, it becomes difficult for the catalyst to be pulverized and the life becomes long. In addition, since the reaction environment does not contain SO X which is a catalyst poison, the following effects can be obtained. That is, the reaction rate of the catalyst becomes high, so that the degree of purification of gas is improved, high-purity gas is obtained, and the catalyst has a long life. Further, from the above effects, the reaction temperature of the catalyst can be lowered when the device that meets the conventional specifications is designed, and the following effects can be obtained. That is, the catalyst body (noble metal or the like) is less likely to be oxidized, so that the life of the catalyst is extended. Moreover, since the heating temperature of the catalyst body is lowered, the catalyst is less likely to be pulverized and the life is extended. Moreover,
Since the amount of heat exchange of the second heat exchanger is small, the size of the second heat exchanger can be made small and the cost can be reduced. Moreover, since the filling amount of the catalyst can be reduced, the amount of the catalyst can be reduced and the cost can be reduced. Moreover, since the amount of catalyst can be reduced, the size of the catalyst column becomes smaller and the cost becomes lower. Further, since the heat exchange amount of the second heat exchanger is small, the catalyst filling amount is small, and the catalyst amount is reduced, the heat radiation is reduced, and the heater can be made smaller and the cost can be reduced. In addition, it consumes less power and saves energy. As described above, according to the present invention, high purity, low cost, and energy saving can be realized.
【０００９】また、本発明では、反応温度が２５０℃以
上である場合に、ＣＨ4 が酸化反応し、ＣＨ4 の除去が
可能となる。従来の方式では、２５０℃以上であって
も、ＣＨ4 が酸化反応せず、最低でも３５０℃程度は必
要であった。これは、反応環境に水が存在したため、反
応率が低下していたことが原因であった。また、従来の
ＴＳＡ方式の吸着塔では、ＣＨ4 を吸着除去することが
できないため、後段のコールドボックスにて処理してい
た。本発明でも、後段の処理設備を外すことはできない
が、安全性は数段向上する。Further, according to the present invention, when the reaction temperature is 250 ° C. or higher, CH 4 undergoes an oxidation reaction and CH 4 can be removed. In the conventional method, CH 4 does not undergo an oxidation reaction even at 250 ° C. or higher, and at least about 350 ° C. is required. This was because water was present in the reaction environment and the reaction rate was reduced. Further, in the conventional TSA type adsorption tower, CH 4 cannot be adsorbed and removed, so that it is treated in the cold box in the latter stage. Even in the present invention, it is not possible to remove the processing equipment in the subsequent stage, but the safety is improved by several steps.
【００１０】また、本発明において、触媒塔に用いる触
媒がパラジウム等の貴金属触媒および銅系触媒である場
合には、原料空気中の一酸化炭素および水素を効果的に
酸化させることができる。Further, in the present invention, when the catalyst used in the catalyst tower is a noble metal catalyst such as palladium and a copper-based catalyst, carbon monoxide and hydrogen in the feed air can be effectively oxidized.
【００１１】[0011]
【発明の実施の形態】つぎに、本発明の実施の形態を図
面にもとづいて詳しく説明する。BEST MODE FOR CARRYING OUT THE INVENTION Next, embodiments of the present invention will be described in detail with reference to the drawings.
【００１２】図１は本発明の空気分離装置の前処理装置
の一実施の形態を示すフローシートである。この実施の
形態では、Ａは原空圧縮機であり、図２に示すように、
外部より取り入れた原料空気を清浄化するフィルター１
と、第１圧縮機２と、第１圧縮機２を経た原料空気を冷
却水（３２℃以下）により４０℃以下に冷却するインタ
ークーラー３と、第２圧縮機４と、第２圧縮機４を経た
原料空気と再生ガス（精留塔４１〔図６参照〕で発生し
た排ガス）とを熱交換させて原料空気を降温させるとと
もに再生ガスを昇温（３０→１１０℃）させる排熱回収
器５と、排熱回収器５を経た原料空気を冷却水（３２℃
以下）により４０℃以下に冷却するアフタークーラー６
とを備えている。図において、８は再生ガスを排熱回収
器５に供給するパイプ（放出パイプ５４〔図６参照〕に
接続している）であり、９は排熱回収器５を経た再生ガ
スを後述する第２吸着ユニットＥの第２再生ヒーター２
７に供給するパイプである。FIG. 1 is a flow sheet showing an embodiment of a pretreatment device for an air separation device of the present invention. In this embodiment, A is an original air compressor, and as shown in FIG.
Filter 1 for cleaning the raw material air taken in from the outside
A first compressor 2, an intercooler 3 that cools the raw material air that has passed through the first compressor 2 to 40 ° C. or less with cooling water (32 ° C. or less), a second compressor 4, and a second compressor 4. Exhaust heat recovery unit 5 that heats the raw material air that has passed through and the regeneration gas (exhaust gas generated in the rectification column 41 [see FIG. 6]) to lower the temperature of the raw material air and raise the temperature of the regeneration gas (30 → 110 ° C.) And the raw material air that has passed through the exhaust heat recovery unit 5 is cooled with water (32 ° C.
After cooler 6 to cool below 40 ℃ by
It has and. In the figure, 8 is a pipe (connected to the discharge pipe 54 [see FIG. 6]) for supplying the regenerated gas to the exhaust heat recovery device 5, and 9 is a first part of the regenerated gas that has passed through the exhaust heat recovery device 5. 2 Second regeneration heater 2 of adsorption unit E
It is a pipe to supply to 7.
【００１３】Ｂは原空冷却器ユニットであり、図２に示
すように、アフタークーラー６を経た原料空気を冷却水
（３２℃以下）により３４℃以下に冷却する第１原空冷
却器（第１の熱交換器）１０と、第１原空冷却器１０に
よる冷却によって発生した凝縮水（この凝縮水には、圧
縮機２，４による圧縮によって、大気中のＳＯX の大半
が溶け込んでいる）を分離するミストセパレーター１１
と、後述する空気処理設備Ｄの原空熱交換器２０（第２
の熱交換器）で降温した原料空気を冷却水（３２℃以
下）により３４℃以下に冷却する第２原空冷却器１２と
を備えている。図において、７は原空圧縮機Ａのインタ
ークーラー３，アフタークーラー６および原空冷却器ユ
ニットＢの第１原空冷却器１０，第２原空冷却器１２に
冷却水（３２℃以下）を供給するパイプであり、１３は
ミストセパレーター１１を経た原料空気を後述する第１
吸着ユニットＣの第１吸着塔１５もしくは第２吸着塔１
６に供給するパイプであり、２３は原空熱交換器２０を
経た原料空気を第２原空冷却器１２に供給するパイプで
あり、２４は第２原空冷却器１２を経た原料空気を後述
する第２吸着ユニットＥの第１吸着塔２５もしくは第２
吸着塔２６に供給するパイプである。Reference numeral B denotes an original air cooler unit, and as shown in FIG. 2, a first original air cooler (first air cooler for cooling the raw material air having passed through the aftercooler 6 to 34 ° C. or less with cooling water (32 ° C. or less). No. 1 heat exchanger) 10 and condensed water generated by cooling by the first original air cooler 10 (most of SO X in the atmosphere is dissolved in this condensed water by compression by the compressors 2 and 4) ) Separating mist separator 11
And the raw air heat exchanger 20 of the air treatment facility D (second
The second raw air cooler 12 for cooling the raw material air whose temperature has been reduced by the heat exchanger (1) to 34 ° C. or lower with the cooling water (32 ° C. or lower). In the figure, reference numeral 7 supplies cooling water (32 ° C. or less) to the intercooler 3 and aftercooler 6 of the raw air compressor A and the first raw air cooler 10 and the second raw air cooler 12 of the raw air cooler unit B. Is a pipe, and 13 is a first air which will be described later with respect to the raw material air that has passed through the mist separator 11.
The first adsorption tower 15 or the second adsorption tower 1 of the adsorption unit C
6, a pipe 23 supplies the raw material air that has passed through the raw air heat exchanger 20 to the second raw air cooler 12, and 24 denotes the raw material air that has passed through the second raw air cooler 12 described below. The first adsorption tower 25 or the second adsorption unit E of the second adsorption unit E
It is a pipe that supplies the adsorption tower 26.
【００１４】Ｃは第１吸着ユニットであり、図３に示す
ように、ＴＳＡ吸着方式による２塔交互切替式の第１吸
着塔１５，第２吸着塔１６と、第１再生ヒーター１７と
を備えている。上記両吸着塔１５，１６には、水分の吸
着容量が大きい合成ゼオライトが充填されており、精製
工程では、ミストセパレーター１１を経た原料空気中の
水分を露点−７０℃以下まで、ＣＯ2 を０〜５００ｐｐ
ｍ程度に吸着除去する。また、ミストセパレーター１１
による凝縮水分離時に一部残っていたＳＯX も水分とと
もに吸着されるか、もしくは合成ゼオライト等と反応し
て除去される。一方、第１再生ヒーター１７では、第２
吸着ユニットＥの第１吸着塔２５もしくは第２吸着塔２
６を経た再生ガスを１７０℃程度に加熱する。図におい
て、１８は第１吸着ユニットＣの第１吸着塔１５もしく
は第２吸着塔１６を経た原料空気を原空熱交換器２０に
供給するパイプであり、１９は再生ガスを外部に放出す
る放出弁１９ａ付きパイプであり、２８は第２吸着ユニ
ットＥの第１吸着塔２５もしくは第２吸着塔２６を経た
再生ガスを第１再生ヒーター１７に供給するパイプであ
る。このパイプ２８は、後述するバイパスパイプ３０，
バイパス弁３０ａによりバイパスされた再生ガスを第１
吸着ユニットＣの第１吸着塔１５もしくは第２吸着塔１
６に供給する作用もする。C is a first adsorption unit, and as shown in FIG. 3, it is equipped with a first adsorption tower 15 and a second adsorption tower 16 of a two-column alternating switching type by the TSA adsorption method, and a first regeneration heater 17. ing. Both of the adsorption towers 15 and 16 are filled with synthetic zeolite having a large water adsorption capacity, and in the refining step, the water content in the raw material air that has passed through the mist separator 11 is reduced to −70 ° C. or lower and CO 2 is set to 0. ~ 500pp
Adsorb and remove to about m. Also, the mist separator 11
The SO X, which remains partially when the condensed water is separated by, is adsorbed together with the water or is removed by reacting with the synthetic zeolite or the like. On the other hand, in the first regeneration heater 17, the second regeneration heater 17
The first adsorption tower 25 or the second adsorption tower 2 of the adsorption unit E
The regenerated gas after 6 is heated to about 170 ° C. In the figure, reference numeral 18 is a pipe for supplying the raw air having passed through the first adsorption tower 15 or the second adsorption tower 16 of the first adsorption unit C to the raw air heat exchanger 20, and 19 is a discharge for releasing the regeneration gas to the outside. Reference numeral 28 denotes a pipe with a valve 19a, and 28 denotes a pipe for supplying the regeneration gas, which has passed through the first adsorption tower 25 or the second adsorption tower 26 of the second adsorption unit E, to the first regeneration heater 17. This pipe 28 is a bypass pipe 30, which will be described later.
The regeneration gas bypassed by the bypass valve 30a is
The first adsorption tower 15 or the second adsorption tower 1 of the adsorption unit C
It also has the function of supplying to 6.
【００１５】Ｄは空気処理設備であり、図４に示すよう
に、第１吸着ユニットＣの第１吸着塔１５もしくは第２
吸着塔１６を経た原料空気（入口ガス）と後述する触媒
塔２２（空気処理塔）を経た原料空気（出口ガス）とを
熱交換させて入口ガスを加温させるとともに出口ガスを
降温させる原空熱交換器２０と、原空熱交換器２０によ
り加温された原料空気（上記入口ガス）を触媒塔２２で
の酸化反応温度まで再加温させる（この再加温は、原空
熱交換器２０の温端ロスおよび外部放熱分を補うために
行う）原空ヒーター２１と、原空ヒーター２１により再
加温された原料空気中のＣＯおよびＨ2 を酸化反応しそ
れぞれＣＯ2 およびＨ2 Ｏに変化させる触媒塔２２（パ
ラジウム触媒を使用している）とを備えている。この触
媒塔２２での一般的な酸化反応温度は、水素除去目的の
場合に１６０〜２８０℃であり、ＣＯ除去目的の場合に
９０〜１６０℃である。この実施の形態では、導入する
原料空気中に触媒毒が殆ど無く、反応の活性の高い乾燥
状態であるため、触媒塔２２での酸化反応温度を一般的
な反応温度に対して８０〜２００℃程度に低く設定する
ことができる。このような触媒塔２２は、性能，寿命と
もに現在の装置を上回る。また、触媒の充填量について
も、現在の量を２０〜５０％程度減少させることができ
る。D is an air treatment facility, and as shown in FIG. 4, the first adsorption tower 15 or the second adsorption tower 15 of the first adsorption unit C.
Raw air that heat-exchanges the raw material air (inlet gas) that has passed through the adsorption tower 16 and the raw material air (outlet gas) that has passed through the catalyst tower 22 (air processing tower) described below to heat the inlet gas and lower the temperature of the outlet gas. The heat exchanger 20 and the raw air (the inlet gas) heated by the raw air heat exchanger 20 are reheated to the oxidation reaction temperature in the catalyst column 22 (this reheating is performed by the raw air heat exchanger). 20) is performed in order to compensate for the heat end loss of 20 and the amount of external heat radiation) and the CO and H 2 in the raw material air reheated by the raw air heater 21 are oxidized to react with CO 2 and H 2 O, respectively. And a catalyst tower 22 (using a palladium catalyst). The general oxidation reaction temperature in the catalyst tower 22 is 160 to 280 ° C. for the purpose of removing hydrogen, and 90 to 160 ° C. for the purpose of removing CO. In this embodiment, since the raw material air to be introduced has almost no catalyst poison and the reaction is in a dry state with high activity, the oxidation reaction temperature in the catalyst tower 22 is 80 to 200 ° C. relative to the general reaction temperature. It can be set as low as possible. Such a catalyst tower 22 is superior in performance and life to the present apparatus. Also, regarding the filling amount of the catalyst, the present amount can be reduced by about 20 to 50%.
【００１６】Ｅは第２吸着ユニットであり、図３に示す
ように、ＴＳＡ吸着方式による２塔交互切替式の第１吸
着塔２５，第２吸着塔２６と、第２再生ヒーター２７と
を備えている。上記両吸着塔２５，２６には、ＣＯ2 の
吸着容量が大きい合成ゼオライトが充填されており、精
製工程では、第２原空冷却器１２を経た原料空気中の水
分を露点−７０℃以下まで、ＣＯ2 を１ｐｐｍ以下まで
吸着除去する。また、従来のＴＳＡ吸着方式により吸着
除去していたアセチレン等の炭化水素も同様に吸着除去
する。一方、第２再生ヒーター２７では、排熱回収器５
を経由した再生ガスを２１０℃程度に加熱する。図にお
いて、２９は冷却工程において再生ガスを第２吸着ユニ
ットＥの第１吸着塔２５もしくは第２吸着塔２６に直接
供給する切換弁２９ａ付きパイプであり、３０は再生ガ
スをバイパスしてパイプ２８に供給するバイパス弁３０
ａ付きバイパスパイプであり、３１は原料空気（精製ガ
ス）を第１および第２の主熱交換器４０ａ，４０ｂ（図
６参照）に送るパイプである。E is a second adsorption unit, and as shown in FIG. 3, it is provided with a first adsorption tower 25, a second adsorption tower 26 and a second regeneration heater 27, which are of the TSA adsorption system and which are alternately switched between two towers. ing. Both of the adsorption towers 25 and 26 are filled with synthetic zeolite having a large CO 2 adsorption capacity, and in the refining step, the water content in the raw material air that has passed through the second raw air cooler 12 is reduced to a dew point of −70 ° C. or lower. , CO 2 is adsorbed and removed to 1 ppm or less. Hydrocarbons such as acetylene, which have been adsorbed and removed by the conventional TSA adsorption method, are also adsorbed and removed. On the other hand, in the second regeneration heater 27, the exhaust heat recovery unit 5
The regenerated gas passing through is heated to about 210 ° C. In the figure, 29 is a pipe with a switching valve 29a for directly supplying the regenerated gas to the first adsorption tower 25 or the second adsorption tower 26 of the second adsorption unit E in the cooling step, and 30 is a pipe 28 bypassing the regenerated gas. Valve 30 to supply to
Reference numeral 31 is a bypass pipe with a, and 31 is a pipe for sending the raw material air (purified gas) to the first and second main heat exchangers 40a, 40b (see FIG. 6).
【００１７】上記構成において、つぎのようにして、精
製および再生を行う。すなわち、精製工程では、原空圧
縮機Ａの圧縮機２，４により圧縮した原料空気をアフタ
ークーラー６により４０℃以下に冷却する。ついで、ア
フタークーラー６により冷却した原料空気を原空冷却器
ユニットＢの第１原空冷却器１０の冷却水により３４℃
以下に冷却し、この冷却により発生した凝縮水をミスト
セパレーター１１により原料空気から分離する。このと
き、原料空気中のＳＯX も、その大半が凝縮水に溶け込
んでいるため、原料空気から分離される。つぎに、ミス
トセパレーター１１を経由した原料空気を第１吸着ユニ
ットＣの精製工程の第１吸着塔１５もしくは第２吸着塔
１６（以下、精製塔という）に供給し、ここで原料空気
中の水分を露点−７０℃以下まで、ＣＯ2 を０〜５００
ｐｐｍ程度に吸着除去する。このとき、ミストセパレー
ター１１による凝縮水分離時に一部残っていたＳＯ
X も、水分とともに吸着されるか、もしくは、合成ゼオ
ライト等と反応し、除去される。また、水分吸着により
吸着熱が発生し、５〜３０℃程度原料空気が温度上昇す
る。With the above structure, purification and regeneration are performed as follows. That is, in the refining process, the raw air compressed by the compressors 2 and 4 of the raw air compressor A is cooled to 40 ° C. or lower by the aftercooler 6. Then, the raw air cooled by the aftercooler 6 is cooled to 34 ° C. by the cooling water of the first raw air cooler 10 of the raw air cooler unit B.
It cools below, and the condensed water generated by this cooling is separated from the raw material air by the mist separator 11. At this time, most of SO X in the raw material air is also dissolved in the condensed water, so that it is separated from the raw material air. Next, the raw material air that has passed through the mist separator 11 is supplied to the first adsorption tower 15 or the second adsorption tower 16 (hereinafter referred to as the purification tower) in the refining process of the first adsorption unit C, where the water content in the raw material air is increased. To a dew point of −70 ° C. or lower, CO 2 of 0 to 500
Adsorbed and removed to about ppm. At this time, the SO partially remaining when the condensed water was separated by the mist separator 11
X is also adsorbed together with water or reacts with synthetic zeolite or the like to be removed. Also, heat of adsorption is generated by water adsorption, and the temperature of the raw material air rises by about 5 to 30 ° C.
【００１８】つぎに、精製塔１５（１６）を経た原料空
気を空気処理設備Ｄの原空熱交換器２０に供給し、触媒
塔２２を経た原料空気と熱交換して加温したのち、原空
ヒーター２１により酸化反応温度まで再加温し触媒塔２
２に供給する。この触媒塔２２では、原料空気中のＣＯ
およびＨ2 を酸化反応し、それぞれＣＯ2 およびＨ2Ｏ
に変化させる。つぎに、触媒塔２２を経た原料空気を再
度原空熱交換器２０に供給し、精製塔１５（１６）を経
た原料空気と熱交換して降温したのち、第２原空冷却器
１２の冷却水により３４℃以下に冷却する。そののち、
第２原空冷却器１２を経た原料空気（水分：露点−７０
℃以下，ＣＯ2 ：０〜５００ｐｐｍ，温度３４℃以下）
を第２吸着ユニットＥの精製工程の第１吸着塔２５もし
くは第２吸着塔２６（以下、精製塔という）に供給し、
ここで水分：露点−７０℃以下，ＣＯ2 ：１ｐｐｍ以下
まで精製する。このとき、アセチレン等の炭化水素も同
様に吸着除去する。なお、原料空気を第２原空冷却器１
２により冷却することなく、第２吸着ユニットＥの精製
塔２５（２６）に供給する場合には、吸着温度が高く、
吸着剤のＣＯ2 を吸着する吸着容量が半減する。そし
て、第２吸着ユニットＥの精製塔２５（２６）を経た原
料空気（精製ガス）をパイプ３１により第１および第２
の主熱交換器４０ａ，４０ｂ，精留塔４１に送る（図６
参照）。Next, the raw material air that has passed through the refining tower 15 (16) is supplied to the raw air heat exchanger 20 of the air treatment facility D, and heat is exchanged with the raw material air that has passed through the catalyst tower 22 to heat the raw air. The catalyst tower 2 is reheated to the oxidation reaction temperature by the empty heater 21.
Supply to 2. In this catalyst tower 22, CO in the raw material air
And H 2 are oxidized to form CO 2 and H 2 O, respectively.
Change to. Next, the raw material air that has passed through the catalyst tower 22 is supplied again to the raw air heat exchanger 20, and heat exchange is performed with the raw material air that has passed through the purification tower 15 (16) to lower the temperature, and then the second raw air cooler 12 is cooled. Cool to below 34 ° C with water. after that,
Raw material air that has passed through the second original air cooler 12 (water content: dew point -70
(° C or lower, CO 2 : 0 to 500 ppm, temperature 34 ° C or lower)
Is supplied to the first adsorption tower 25 or the second adsorption tower 26 (hereinafter referred to as the purification tower) in the purification step of the second adsorption unit E,
Here, water: dew point-70 ° C. or lower, CO 2 : 1 ppm or lower. At this time, hydrocarbons such as acetylene are also adsorbed and removed. In addition, the raw air is supplied to the second raw air cooler 1
When supplying to the purification tower 25 (26) of the second adsorption unit E without cooling by 2, the adsorption temperature is high,
The adsorption capacity for adsorbing CO 2 of the adsorbent is halved. Then, the raw material air (purified gas) that has passed through the purification tower 25 (26) of the second adsorption unit E is passed through the pipe 31 to the first and second
To the main heat exchangers 40a, 40b and the rectification tower 41 (see FIG. 6).
reference).
【００１９】一方、再生工程では、再生ガスを原空圧縮
機Ａの排熱回収器５に供給し、ここで圧縮機４の圧縮熱
を回収して加熱する（３０→１００℃）。ついで、排熱
回収器５を経た再生ガスを第２再生ヒーター２７により
２１０℃程度に加熱したのち、第２吸着ユニットＥの再
生工程の第２吸着塔２６もしくは第１吸着塔２５（以
下、再生塔という）に供給し加熱する。この実施の形態
では、再生ガスを効率よく利用するために、第２吸着ユ
ニットＥでの精製工程，再生工程（加熱工程＋冷却工
程）を第１吸着ユニットＣでの精製工程，再生工程（加
熱工程＋冷却工程）より１時間早める（図５参照）。On the other hand, in the regeneration step, the regeneration gas is supplied to the exhaust heat recovery unit 5 of the original air compressor A, where the compression heat of the compressor 4 is recovered and heated (30 → 100 ° C.). Then, the regenerated gas that has passed through the exhaust heat recovery unit 5 is heated to about 210 ° C. by the second regeneration heater 27, and then the second adsorption tower 26 or the first adsorption tower 25 (hereinafter referred to as regeneration) in the regeneration process of the second adsorption unit E is heated. It is supplied to a tower) and heated. In this embodiment, in order to efficiently use the regenerated gas, the purification process and the regeneration process (heating process + cooling process) in the second adsorption unit E are performed in the first adsorption unit C. 1 hour earlier than the process + cooling process) (see FIG. 5).
【００２０】第２吸着ユニットＥの再生塔２６（２５）
が加熱工程の初期１時間は、第１吸着ユニットＣが切替
中であるため、パイプ２８中の再生塔２６（２５）使用
済み再生ガスをパイプ１９，放出弁１９ａにより放出す
る。すなわち、再生ガスとして、精留塔４１で発生した
排ガスを使用しているため、再生ガス量を変動させるこ
とは精留塔４１の圧力等の制御に外乱を与えることにな
る。これを防止するために、この実施の形態では、再生
ガスが必要でない場合に（切替時に）、同一量を外部に
放出している。Regeneration tower 26 (25) of the second adsorption unit E
However, during the initial 1 hour of the heating step, since the first adsorption unit C is being switched, the regeneration tower 26 (25) used regeneration gas in the pipe 28 is released by the pipe 19 and the release valve 19a. That is, since the exhaust gas generated in the rectification column 41 is used as the regeneration gas, changing the amount of the regeneration gas causes disturbance in the control of the pressure in the rectification column 41. In order to prevent this, in this embodiment, when the regeneration gas is not needed (at the time of switching), the same amount is discharged to the outside.
【００２１】第２吸着ユニットＥの再生塔２６（２５）
の加熱工程の１時間経過後、第１吸着ユニットＣの第２
吸着塔１６もしくは第１吸着塔１５は加熱工程に入る。
この加熱工程では、再生塔２６（２５）を加熱した再生
ガスは第１再生ヒーター１７により１７０℃程度に再加
熱されたのち、上記加熱工程の第２吸着塔１６もしくは
第１吸着塔１５（以下、再生塔という）を加熱する。な
お、第２吸着ユニットＥの再生塔２６（２５）が加熱工
程に入ったとき、この再生塔２６（２５）の加温のため
に再生ガスは熱量を消費し、再生塔２６（２５）の塔出
口では常温の状態となっているが、加熱工程の約１時間
経過後には、次第に再生塔２６（２５）の塔本体が加温
され、上記再生塔２６（２５）の塔出口での再生ガスの
温度も上昇を始める。第１吸着ユニットＣの再生塔１６
（１５）の加熱工程は、上記再生塔２６（２５）の塔出
口での再生ガスが温度上昇を始めた時間にスタートす
る。Regeneration tower 26 (25) of the second adsorption unit E
After the lapse of 1 hour of the heating step of the first adsorption unit C,
The adsorption tower 16 or the first adsorption tower 15 enters a heating process.
In this heating step, the regeneration gas that has heated the regeneration tower 26 (25) is reheated to about 170 ° C. by the first regeneration heater 17, and then the second adsorption tower 16 or the first adsorption tower 15 (hereinafter , The regeneration tower). When the regeneration tower 26 (25) of the second adsorption unit E enters the heating step, the regeneration gas consumes heat due to the heating of the regeneration tower 26 (25), and the regeneration gas of the regeneration tower 26 (25) is consumed. Although the temperature at the outlet of the tower is normal temperature, after about 1 hour of the heating step, the tower main body of the regeneration tower 26 (25) is gradually heated and the regeneration at the outlet of the regeneration tower 26 (25) is performed. The gas temperature also begins to rise. Regeneration tower 16 of first adsorption unit C
The heating step (15) starts at the time when the temperature of the regeneration gas at the tower outlet of the regeneration tower 26 (25) starts to rise.
【００２２】つぎに、第２吸着ユニットＥの再生塔２６
（２５）の加熱工程終了後、冷却工程に入る。この冷却
工程は、パイプ２９，切換弁２９ａにより、再生ガスを
直接再生塔２６（２５）に導入して行う。第２吸着ユニ
ットＥの再生塔２６（２５）が冷却工程に入ったとき、
この再生塔２６（２５）の冷却のために再生ガスは高温
の状態となっている。そして、この高温の状態で再生ガ
スが第１吸着ユニットＣの再生塔１６（１５）に供給さ
れる。それ以降も第２吸着ユニットＥの再生塔２６（２
５）が常温になるまでは、第１吸着ユニットＣの再生塔
１６（１５）が加熱工程であるために、第２吸着ユニッ
トＥの再生塔２６（２５）において加熱に使用された熱
はほとんど第１吸着ユニットＣの再生塔１６（１５）の
加熱に再利用される。このように、両吸着ユニットＣ，
Ｅの切替時間を１時間遅らせることにより、再生熱の回
収を効率的に行うことができる。また、両吸着ユニット
Ｃ，Ｅの切替を同時に行わないことにより、精製ガスラ
インの圧力変動を低減することができる。Next, the regeneration tower 26 of the second adsorption unit E
After the heating step (25) is completed, the cooling step is started. This cooling step is performed by directly introducing the regeneration gas into the regeneration tower 26 (25) through the pipe 29 and the switching valve 29a. When the regeneration tower 26 (25) of the second adsorption unit E enters the cooling step,
Due to the cooling of the regeneration tower 26 (25), the regeneration gas is in a high temperature state. Then, in this high temperature state, the regeneration gas is supplied to the regeneration tower 16 (15) of the first adsorption unit C. After that, the regeneration tower 26 of the second adsorption unit E (2
Since the regeneration tower 16 (15) of the first adsorption unit C is in the heating step until 5) reaches room temperature, most of the heat used for heating in the regeneration tower 26 (25) of the second adsorption unit E is heated. It is reused for heating the regeneration tower 16 (15) of the first adsorption unit C. In this way, both suction units C,
By delaying the switching time of E by 1 hour, it is possible to efficiently recover the regeneration heat. Further, by not switching the adsorption units C and E at the same time, it is possible to reduce the pressure fluctuation of the purified gas line.
【００２３】第２吸着ユニットＥの再生塔２６（２５）
の冷却工程終了１時間前に、第１吸着ユニットＣの再生
塔１６（１５）は冷却工程を開始する。その時点では、
再生塔２６（２５）使用済み再生ガスの温度はほぼ常温
となっているため、第１吸着ユニットＣの再生塔１６
（１５）の冷却に支障はない。なお、第１再生ヒーター
１７は作動停止の状態になっている。そして、第２吸着
ユニットＥは冷却工程終了後に、切替工程に入る。その
とき、第１吸着ユニットＣの再生塔１６（１５）は冷却
工程を続けているために、バイパスパイプ３０，バイパ
ス弁３０ａ，パイプ２８により再生ガスを直接第１吸着
ユニットＣの再生塔１６（１５）に送る。以上のような
プロセスにより、非常に効率良く、前処理装置を運転す
ることができる。また、切替工程には、昇圧・並列・脱
圧工程があり、精製は連続的に行われる。Regeneration tower 26 (25) of the second adsorption unit E
One hour before the end of the cooling step, the regeneration tower 16 (15) of the first adsorption unit C starts the cooling step. At that time,
Regeneration tower 26 (25) Since the temperature of the used regeneration gas is almost room temperature, the regeneration tower 16 of the first adsorption unit C is
There is no hindrance to the cooling of (15). The first regeneration heater 17 is in a deactivated state. Then, the second adsorption unit E enters the switching process after the cooling process is completed. At that time, since the regeneration tower 16 (15) of the first adsorption unit C continues the cooling process, the regeneration gas is directly supplied to the regeneration tower 16 (of the first adsorption unit C by the bypass pipe 30, the bypass valve 30a, and the pipe 28. Send to 15). With the above process, the pretreatment device can be operated very efficiently. In addition, the switching process includes a pressurizing / parallel / depressurizing process, and the purification is continuously performed.
【００２４】上記の前処理装置により精製された原料空
気（精製ガス）は、図６に示すように、第１および第２
の主熱交換器４０ａ，４０ｂに送られる。図６におい
て、４０ａは第１の主熱交換器であり、上記の前処理装
置により精製された原料空気がパイプ３１により送り込
まれる。４０ｂは第２の主熱交換器であり、第１の主熱
交換器４０ａを経た原料空気が送り込まれる。４１は、
塔頂に、凝縮器４２ａ内蔵の分縮器４２を備えた精留塔
であり、第１および第２の主熱交換器４０ａ，４０ｂに
より超低温に冷却されパイプ４３を経て送り込まれる原
料空気をさらに冷却し、その一部を液化し液体空気４４
として底部に溜め、窒素のみを気体状態で上部天井部に
溜めるようになっている。As shown in FIG. 6, the raw material air (purified gas) purified by the above-mentioned pretreatment device is the first and second air.
To the main heat exchangers 40a and 40b. In FIG. 6, reference numeral 40a is a first main heat exchanger, and the raw material air purified by the above-mentioned pretreatment device is fed into the pipe 31. 40b is a 2nd main heat exchanger, and the raw material air which passed the 1st main heat exchanger 40a is sent in. 41 is
It is a rectification column equipped with a condenser 42a with a built-in condenser 42a at the top of the column, and further feeds raw air cooled to ultra-low temperature by the first and second main heat exchangers 40a, 40b and fed through a pipe 43. Cool and liquefy a part of the liquid air 44
As a result, only nitrogen is stored in the upper ceiling part in a gas state.
【００２５】４５は液体窒素貯槽であり、内部の液体窒
素（高純度品）を、導入路パイプ４６を経由させて精留
塔４１の上部側に送入し、精留塔４１内に供給される原
料空気の寒冷源にする。ここで精留塔４１についてより
詳しく説明すると、上記精留塔４１は天井板４１ａの上
側に分縮器４２を備えており、上記分縮器４２内の凝縮
器４２ａには、精留塔４１の上部に溜る窒素ガスの一部
が第１の還流液パイプ４７を介して送入される。この分
縮器４２内は、精留塔４１内よりも減圧状態になってお
り、精留塔４１の底部の貯留液体空気（Ｎ2 ５０〜７０
％，Ｏ2 ３０〜５０％）４４が膨脹弁４９ａ付きパイプ
４９を経て送り込まれ、気化して内部温度を液体窒素の
沸点以下の温度に冷却するようになっている。この冷却
により、凝縮器４２ａ内に送入された窒素ガスが液化す
る。Reference numeral 45 is a liquid nitrogen storage tank, and the liquid nitrogen (high-purity product) therein is sent to the upper side of the rectification column 41 via an introduction path pipe 46 and supplied into the rectification column 41. Use the source air as a cold source. The rectification column 41 will be described in more detail. The rectification column 41 is provided with a partial condenser 42 on the upper side of the ceiling plate 41a, and the condenser 42a in the partial condenser 42 includes a rectification column 41. A part of the nitrogen gas accumulated in the upper part of the is supplied through the first reflux liquid pipe 47. The inside of the dephlegmator 42 is in a reduced pressure state as compared with the inside of the rectification tower 41, and the stored liquid air (N 2 50 to 70) at the bottom of the rectification tower 41.
%, O 2 30 to 50%) 44 is fed through a pipe 49 with an expansion valve 49a, vaporized and cooled to an internal temperature below the boiling point of liquid nitrogen. Due to this cooling, the nitrogen gas fed into the condenser 42a is liquefied.
【００２６】５１は液面計であり、分縮器４２内の液体
空気４４の液面が一定レベルを保つようその液面に応じ
てバルブ４６ａを制御し液体窒素貯槽４５からの液体窒
素の供給量を制御する。精留塔４１の上部側の部分に
は、上記分縮器４２内の凝縮器４２ａで生成した液体窒
素が第２の還流液パイプ４８を通って流下供給されると
ともに、液体窒素貯槽４５から液体窒素が導入路パイプ
４６を経て供給され、これらが精留塔４１内を下方に流
下し、精留塔４１の底部から上昇する原料空気と向流的
に接触し冷却してその一部を液化するようになってい
る。この過程で原料空気中の高沸点成分は液化されて精
留塔４１の底部に溜り、低沸点成分の窒素ガスが精留塔
４１の上部に溜る。A liquid level gauge 51 controls the valve 46a according to the liquid level of the liquid air 44 in the dephlegmator 42 so as to maintain a constant level, and supplies the liquid nitrogen from the liquid nitrogen storage tank 45. Control the amount. The liquid nitrogen produced in the condenser 42a in the dephlegmator 42 is supplied to the upper part of the rectification column 41 through the second reflux liquid pipe 48 while being supplied from the liquid nitrogen storage tank 45. Nitrogen is supplied through the inlet pipe 46, and these flow downward in the rectification column 41, come into countercurrent contact with the raw material air rising from the bottom of the rectification column 41, and cool it to liquefy a part thereof. It is supposed to do. In this process, the high boiling point component in the raw material air is liquefied and accumulated at the bottom of the rectification column 41, and the nitrogen gas of the low boiling point component accumulates at the upper part of the rectification column 41.
【００２７】５２は精留塔４１の上部天井部に溜った窒
素ガスを製品窒素ガスとして取り出す取出パイプで、超
低温の窒素ガスを第２および第１の主熱交換器４０ｂ，
４０ａ内に案内し、そこに送り込まれる原料空気と熱交
換させて常温にしメインパイプ５３に送り込む作用をす
る。この場合、精留塔４１内における最上部には、窒素
ガスとともに、沸点の低いＨｅ（−２６９℃），Ｈ
2 （−２５３℃）が溜りやすいため、取出パイプ５２
は、精留塔４１の最上部よりかなり下側に開口してお
り、Ｈｅ，Ｈ2 の混在しない純窒素ガスのみを製品窒素
ガスとして取り出すようになっている。５４は分縮器４
２内の気化液体空気を第２および第１の主熱交換器４０
ｂ，４０ａに送り込んだのちにパイプ８に供給する放出
パイプであり、５４ａはその保圧弁である。Reference numeral 52 is an extraction pipe for taking out the nitrogen gas accumulated in the upper ceiling portion of the rectification tower 41 as product nitrogen gas. The ultra low temperature nitrogen gas is supplied to the second and first main heat exchangers 40b, 40b.
It guides the inside of 40a, heat-exchanges with the raw material air sent there, and makes it normal temperature, and acts to send it into the main pipe 53. In this case, at the uppermost part in the rectification column 41, together with nitrogen gas, He (−269 ° C.) and H having a low boiling point are used.
2 (-253 ° C) easily collects, so the extraction pipe 52
Is opened considerably below the uppermost part of the rectification column 41, and only pure nitrogen gas in which He and H 2 are not mixed is taken out as product nitrogen gas. 54 is a demultiplexer 4
The vaporized liquid air in the second main heat exchanger 40
b, 40a is a discharge pipe which is supplied to the pipe 8 after being sent to b, 40a, and 54a is its pressure-holding valve.
【００２８】５５はバックアツプ系ラインであり、空気
圧縮系ラインが故障したときに液体窒素貯槽４５内の液
体窒素を蒸発器５６により蒸発させてメインパイプ５３
に送り込み、窒素ガスの供給がとだえることのないよう
にする。５７は不純物分析計であり、メインパイプ５３
に送り出される製品窒素ガスの純度を分析し、純度の低
いときは、弁５８，５９を作動させて製品窒素ガスを矢
印Ｆのように外部に逃気する作用をする。６０は真空保
冷函（一点鎖線で示す）であり、その内部に精留塔４１
および第１，第２の主熱交換器４０ａ，４０ｂを収容す
ることにより、精留効率の向上を図っている。Reference numeral 55 is a back-up system line, and when the air compression system line fails, the liquid nitrogen in the liquid nitrogen storage tank 45 is evaporated by the evaporator 56 and the main pipe 53 is used.
To prevent the nitrogen gas supply from stalling. 57 is an impurity analyzer, which is the main pipe 53
The purity of the product nitrogen gas sent out to is analyzed. When the purity is low, the valves 58 and 59 are operated to let the product nitrogen gas escape to the outside as shown by arrow F. Reference numeral 60 denotes a vacuum cold storage box (shown by a one-dot chain line), in which the rectification column 41 is provided.
By accommodating the first and second main heat exchangers 40a and 40b, the rectification efficiency is improved.
【００２９】上記構成において、つぎのようにして製品
窒素ガスの製造を行う。すなわち、上記の前処理装置に
より精製された原料空気を、精留塔４１からパイプ５２
を経て送り込まれる製品窒素ガス等によって冷やされて
いる第１，第２の主熱交換器４０ａ，４０ｂに送り込ん
で超低温に冷却し、その状態で精留塔４１の下部内に投
入する。ついで、この投入原料空気を、液体窒素貯槽４
５から導入路パイプ４６を経由して精留塔４１内に送り
込まれた液体窒素および第２の還流液パイプ４８から流
下する液体窒素と接触させて冷却し、一部を液化して精
留塔４１の底部に液体空気４４として溜める。この過程
において、窒素と酸素の沸点の差（酸素の沸点−１８３
℃，窒素の沸点−１９６℃）により、原料空気中の高沸
点成分である酸素が液化し、窒素が気体のまま残る。つ
いで、この気体のまま残った窒素を取出パイプ５２から
取り出して第２および第１の主熱交換器４０ｂ，４０ａ
に送り込み、常温近くまで昇温させメインパイプ５３か
ら製品窒素ガスとして送り出す。この場合、精留塔４１
内は、圧縮機２，４の圧縮力および液体窒素の蒸気圧に
より高圧になっているため、取出パイプ５２から取り出
される製品窒素ガスの圧力も高い。他方、精留塔４１の
下部に溜った液体空気４４については、これを分縮器４
２内に送り込み凝縮器４２ａを冷却させる。この冷却に
より、精留塔４１の上部から凝縮器４２ａに送入された
窒素ガスが液化して精留塔４１用の還流液となり、第２
の還流液パイプ４８を経て精留塔４１に戻る。そして、
凝縮器４２ａを冷却し終えた液体空気４４は気化し、放
出パイプ５４により第２および第１の主熱交換器４０
ｂ，４０ａに送られ両主熱交換器４０ｂ，４０ａを冷や
したのちパイプ８に供給される。なお、液体窒素貯槽４
５から導入路パイプ４６を経由して精留塔４１内に送り
込まれた液体窒素は、原料空気液化用の寒冷源として作
用し、それ自身は気化して取出パイプ５２から製品窒素
ガスの一部として取り出される。With the above structure, the product nitrogen gas is manufactured as follows. That is, the raw material air purified by the above pretreatment device is supplied from the rectification tower 41 to the pipe 52.
The product is sent to the first and second main heat exchangers 40a and 40b which are cooled by the product nitrogen gas or the like to be cooled to an ultralow temperature, and in that state, it is charged into the lower part of the rectification column 41. Then, this feed raw material air is supplied to the liquid nitrogen storage tank 4
5, the liquid nitrogen sent into the rectification column 41 via the introduction path pipe 46 and the liquid nitrogen flowing down from the second reflux liquid pipe 48 are brought into contact with each other to be cooled, and a part thereof is liquefied to rectify the column. It is stored as liquid air 44 at the bottom of 41. In this process, the difference between the boiling points of nitrogen and oxygen (oxygen boiling point-183
C., boiling point of nitrogen −196 ° C.), oxygen, which is a high-boiling point component in the raw material air, is liquefied and nitrogen remains as a gas. Then, the nitrogen remaining as the gas is taken out from the take-out pipe 52, and the second and first main heat exchangers 40b, 40a are taken out.
Then, the temperature is raised to near room temperature and the product nitrogen gas is sent out from the main pipe 53. In this case, the rectification tower 41
Since the inside has a high pressure due to the compressive force of the compressors 2 and 4 and the vapor pressure of liquid nitrogen, the pressure of the product nitrogen gas taken out from the take-out pipe 52 is also high. On the other hand, for the liquid air 44 accumulated in the lower part of the rectification column 41, the liquid air 44 is
2 to cool the condenser 42a. By this cooling, the nitrogen gas fed into the condenser 42a from the upper part of the rectification column 41 is liquefied and becomes the reflux liquid for the rectification column 41, and the second
It returns to the rectification column 41 through the reflux liquid pipe 48 of FIG. And
The liquid air 44 that has finished cooling the condenser 42a is vaporized and is discharged by the discharge pipe 54 to the second and first main heat exchangers 40.
b, 40a, the main heat exchangers 40b, 40a are cooled, and then supplied to the pipe 8. Liquid nitrogen storage tank 4
5, the liquid nitrogen sent into the rectification column 41 via the introduction path pipe 46 acts as a cold source for liquefying the raw material air, and is itself vaporized and a part of the product nitrogen gas is taken out from the extraction pipe 52. Is taken out as.
【００３０】このように、上記実施の形態では、触媒塔
２２に原料空気を導入する前に、触媒塔２２の触媒に対
し、触媒毒となる水分・ＳＯX をほとんど除去すること
ができる。このため、触媒塔２２に充填する触媒量を低
減することができる。また、触媒塔２２での反応状態が
ドライの状態であるため、触媒が粉化しにくい。また、
触媒塔２２での高反応率を長時間維持することができ、
精製ガスの高純度化が図れる。また、触媒塔２２での外
部放熱量を低減することができ、エネルギーを節約する
ことができる。しかも、原空熱交換器２０の熱交換量が
減り、設備が小さくなり、設備コストが下がる。さら
に、上記実施の形態では、原料空気の冷却手段として、
冷凍機を用いる必要がない。さらに、第１吸着ユニット
Ｃを水分精製用（粗精製）とし、第２吸着ユニットＥを
水分精製用（精密精製）とＣＯ2 精製用としているた
め、第１吸着ユニットＣの両吸着塔１５，１６およびは
第２吸着ユニットＥの両吸着塔２５，２６の吸着剤の充
填量を低減することができる。しかも、第１および第２
の吸着ユニットＣ，Ｅに分離したことにより、第２吸着
ユニットＥで再生に使用した再生ガスを第１吸着ユニッ
トＣの再生に使用することができる。さらに、両吸着ユ
ニットＣ，Ｅの工程を１時間ずらすことにより、第２吸
着ユニットＥの再生に利用した熱を第１吸着ユニットＣ
の再生にほとんど回収することができ、省エネルギーを
実現することができる。As described above, in the above-described embodiment, most of the water and SO x which are catalyst poisons to the catalyst in the catalyst tower 22 can be removed before the raw material air is introduced into the catalyst tower 22. Therefore, the amount of catalyst filled in the catalyst tower 22 can be reduced. Further, since the reaction state in the catalyst tower 22 is a dry state, the catalyst is hard to be pulverized. Also,
It is possible to maintain a high reaction rate in the catalyst tower 22 for a long time,
The purified gas can be highly purified. Moreover, the amount of external heat radiation in the catalyst tower 22 can be reduced, and energy can be saved. Moreover, the heat exchange amount of the raw air heat exchanger 20 is reduced, the equipment becomes small, and the equipment cost is reduced. Further, in the above embodiment, as a means for cooling the raw material air,
There is no need to use a refrigerator. Further, since the first adsorption unit C is used for water purification (rough purification) and the second adsorption unit E is used for water purification (precision purification) and CO 2 purification, both adsorption towers 15 of the first adsorption unit C, It is possible to reduce the filling amount of the adsorbent in both adsorption towers 25 and 26 of the second adsorption unit E. Moreover, the first and second
By separating into the adsorption units C and E, the regeneration gas used for regeneration in the second adsorption unit E can be used in regeneration of the first adsorption unit C. Furthermore, the heat used for the regeneration of the second adsorption unit E is transferred to the first adsorption unit C by shifting the steps of both adsorption units C and E by 1 hour.
Almost all can be recovered for recycling, and energy saving can be realized.
【００３１】また、上記実施の形態では、精留塔４１の
上部に凝縮器４２ａ内蔵型の分縮器４２を設け、凝縮器
４２ａ内へ精留塔４１内の窒素ガスの一部を常時案内し
て液化するため、凝縮器４２ａ内へ液化窒素が所定量溜
まったのちはそれ以降生成する液化窒素が還流液として
常時精留塔４１内に戻るようになる。したがって、凝縮
器４２ａからの還流液の流下供給の断続に起因する製品
純度のばらつきを生じず、常時安定した純度の製品窒素
ガスを供給することができる。しかも、この実施の形態
では、製品窒素ガスの需要量に変動が生じても、液面計
５１がバルブ４６ａの開度等を制御し、精留塔４１に対
する液体窒素の供給量を制御することにより分縮器４２
内の液体空気４４の液面を一定に制御するため、需要量
の変動に迅速に対応できる。Further, in the above embodiment, the condenser 42a built-in type partial condenser 42 is provided in the upper portion of the rectification column 41, and a part of the nitrogen gas in the rectification column 41 is constantly guided into the condenser 42a. Since the liquefied nitrogen is accumulated in the condenser 42a in a predetermined amount, the liquefied nitrogen produced thereafter returns to the rectification column 41 as a reflux liquid at all times. Therefore, variation in product purity due to intermittent supply of reflux liquid from the condenser 42a does not occur, and product nitrogen gas with stable purity can be always supplied. Moreover, in this embodiment, even if the demand amount of the product nitrogen gas fluctuates, the liquid level gauge 51 controls the opening degree of the valve 46a and the like to control the supply amount of liquid nitrogen to the rectification column 41. By the decompressor 42
Since the liquid level of the liquid air 44 inside is controlled to be constant, it is possible to quickly respond to fluctuations in demand.
【００３２】図７は本発明の空気分離装置の他の実施の
形態を示している。この実施の形態では、精留塔４１内
に第２の凝縮器６１を設けている。すなわち、上記精留
塔４１内に第２の凝縮器６１を設け、ここに、導入路パ
イプ４６から液体窒素貯槽４５の液体窒素を寒冷源とし
て供給し、精留塔４１内を上昇する原料空気を冷却し酸
素等の高沸点分を液化して精留塔４１の底部に溜め、沸
点の低い窒素ガスを精留塔４１の上部に溜めるようにし
ている。そして、第２の凝縮器６１内において寒冷とし
ての作用を終えて気化した気化液体窒素を放出路パイプ
６２に入れ、第２および第１の主熱交換器４０ｂ，４０
ａを経由させて熱交換させたのち系外に放出するように
している。それ以外の部分は上記実施の形態と同様であ
り、同様の部分には同じ符号を付している。この実施の
形態でも、上記実施の形態と同様の作用・効果を奏す
る。FIG. 7 shows another embodiment of the air separation device of the present invention. In this embodiment, a second condenser 61 is provided inside the rectification column 41. That is, the second condenser 61 is provided in the rectification column 41, and the liquid nitrogen in the liquid nitrogen storage tank 45 is supplied as a cold source from the introduction path pipe 46 to the raw condenser air which rises in the rectification column 41. Is cooled to liquefy high-boiling-point components such as oxygen and store them at the bottom of the rectification column 41, and nitrogen gas having a low boiling point is stored at the top of the rectification column 41. Then, in the second condenser 61, the vaporized liquid nitrogen that has finished the action as cold and is vaporized is put into the discharge passage pipe 62, and the second and first main heat exchangers 40b, 40 are provided.
The heat is exchanged via a and then discharged to the outside of the system. The other parts are the same as those in the above embodiment, and the same parts are denoted by the same reference numerals. Also in this embodiment, the same actions and effects as those of the above-mentioned embodiment are exhibited.
【００３３】なお、上記両実施の形態では、再生工程に
おいて、再生ガスとして、精留塔４１で発生した排ガス
を用いているが、第２吸着ユニットＥの両吸着塔２５，
２６の塔出口の精製ガスを用いてもよい。また、上記両
実施の形態では、再生ガスを排熱回収器５に導入してい
るが、この排熱回収工程は省エネルギーのための工程で
あり、必要不可欠なものではない。また、上記両実施の
形態では、切替時間を１時間に設定しているが、１時間
に限定するものではない。In both of the above embodiments, the exhaust gas generated in the rectification column 41 is used as the regeneration gas in the regeneration step, but both adsorption columns 25 of the second adsorption unit E,
The purified gas at the tower outlet of 26 may be used. Further, in both of the above-described embodiments, the regeneration gas is introduced into the exhaust heat recovery device 5, but this exhaust heat recovery process is a process for energy saving and is not essential. Further, in both of the above embodiments, the switching time is set to 1 hour, but it is not limited to 1 hour.
【００３４】[0034]
【発明の効果】以上のように、本発明の空気分離装置に
よれば、凝縮水分離器により凝縮水を分離するときに、
原料空気中の水分、および凝縮水に溶け込んだ原料空気
中の大半のＳＯX を除去することができ、また、第１の
吸着塔によりさらに水分およびＳＯX を除去することが
できる。したがって、触媒塔に原料空気を導入する前
に、原料空気中の水分・ＳＯX をほとんど除去すること
ができる。その結果、反応環境がドライになり、つぎの
効果が得られる。すなわち、触媒の反応率が高くなり、
このため、ガスの精製度が良くなり、高純度のガスが得
られる。しかも、触媒毒の水分がないため、ガスの精製
度が良くなり、高純度のガスが得られるとともに、触媒
が長寿命になる。しかも、触媒が水分により膨脹しない
ため、触媒が粉化しにくくなり、長寿命になる。また、
反応環境に触媒毒であるＳＯX がなく、つぎの効果が得
られる。すなわち、触媒の反応率が高くなり、このた
め、ガスの精製度が良くなり、高純度のガスが得られる
とともに、触媒が長寿命になる。また、上記の効果か
ら、従来の仕様を満足させる装置を設計した場合に、触
媒の反応温度を低下させることができ、つぎの効果が得
られる。すなわち、触媒本体（貴金属等）が酸化しにく
くなるため、触媒の寿命が長くなる。しかも、触媒本体
の加熱温度が低くなるため、触媒が粉化しにくくなり、
長寿命になる。しかも、第２の熱交換器の熱交換量が少
なくなるため、第２の熱交換器を小さくすることがで
き、低コストになる。しかも、触媒の充填量を少なくす
ることができるため、触媒量を減らすことができ、低コ
ストになる。しかも、触媒量を減らすことができるた
め、触媒塔が小さくなり、低コストになる。さらに、第
２の熱交換器の熱交換量が少ないこと、触媒の充填量が
少ないこと、および、触媒量が減少することから、放熱
が少なくなり、ヒーターを小さくすることができて低コ
ストになるうえ、消費電力が減って省エネになる。この
ように、本発明によれば、高純度化，低コスト化，省エ
ネ化を実現することができる。As described above, according to the air separation device of the present invention, when the condensed water is separated by the condensed water separator,
Moisture in the raw material air and most of SO X in the raw material air dissolved in the condensed water can be removed, and the first adsorption tower can further remove the water and SO X. Therefore, before introducing the raw material air into the catalyst tower, most of the water and SO x in the raw material air can be removed. As a result, the reaction environment becomes dry, and the following effects are obtained. That is, the reaction rate of the catalyst becomes high,
Therefore, the degree of purification of the gas is improved, and a high-purity gas can be obtained. Moreover, since there is no water that is a catalyst poison, the degree of purification of the gas is improved, high-purity gas is obtained, and the catalyst has a long life. Moreover, since the catalyst does not expand due to water, it becomes difficult for the catalyst to be pulverized and the life becomes long. Also,
Since the reaction environment does not contain SO X which is a catalyst poison, the following effects can be obtained. That is, the reaction rate of the catalyst becomes high, so that the degree of purification of gas is improved, high-purity gas is obtained, and the catalyst has a long life. Further, from the above effects, the reaction temperature of the catalyst can be lowered when the device that meets the conventional specifications is designed, and the following effects can be obtained. That is, the catalyst body (noble metal or the like) is less likely to be oxidized, so that the life of the catalyst is extended. Moreover, since the heating temperature of the catalyst body becomes low, it becomes difficult for the catalyst to powder,
It has a long life. Moreover, since the amount of heat exchange of the second heat exchanger is small, the size of the second heat exchanger can be made small and the cost can be reduced. Moreover, since the filling amount of the catalyst can be reduced, the amount of the catalyst can be reduced and the cost can be reduced. Moreover, since the amount of catalyst can be reduced, the size of the catalyst column becomes smaller and the cost becomes lower. Further, since the heat exchange amount of the second heat exchanger is small, the catalyst filling amount is small, and the catalyst amount is reduced, the heat radiation is reduced, and the heater can be made smaller and the cost can be reduced. In addition, it consumes less power and saves energy. As described above, according to the present invention, high purity, low cost, and energy saving can be realized.
【００３５】また、本発明では、反応温度が２５０℃以
上である場合に、ＣＨ4 が酸化反応し、ＣＨ4 の除去が
可能となる。従来の方式では、２５０℃以上であって
も、ＣＨ4 が酸化反応せず、最低でも３５０℃程度は必
要であった。これは、反応環境に水が存在したため、反
応率が低下していたことが原因であった。また、従来の
ＴＳＡ方式の吸着塔では、ＣＨ4 を吸着除去することが
できないため、後段のコールドボックスにて処理してい
た。本発明でも、後段の処理設備を外すことはできない
が、安全性は数段向上する。Further, in the present invention, when the reaction temperature is 250 ° C. or higher, CH 4 undergoes an oxidation reaction, and CH 4 can be removed. In the conventional method, CH 4 does not undergo an oxidation reaction even at 250 ° C. or higher, and at least about 350 ° C. is required. This was because water was present in the reaction environment and the reaction rate was reduced. Further, in the conventional TSA type adsorption tower, CH 4 cannot be adsorbed and removed, so that it is treated in the cold box in the latter stage. Even in the present invention, it is not possible to remove the processing equipment in the subsequent stage, but the safety is improved by several steps.
【００３６】また、本発明において、触媒塔に用いる触
媒がパラジウムである場合には、原料空気中の一酸化炭
素および水素を効果的に酸化させることができる。Further, in the present invention, when the catalyst used in the catalyst tower is palladium, carbon monoxide and hydrogen in the raw material air can be effectively oxidized.
【図１】本発明の空気分離装置の前処理装置のフローシ
ートを示す図である。FIG. 1 is a diagram showing a flow sheet of a pretreatment device for an air separation device of the present invention.
【図２】上記フローシートの要部を示す図である。FIG. 2 is a diagram showing a main part of the flow sheet.
【図３】上記フローシートの要部を示す図である。FIG. 3 is a diagram showing a main part of the flow sheet.
【図４】上記フローシートの要部を示す図である。FIG. 4 is a diagram showing a main part of the flow sheet.
【図５】精製工程および再生工程の説明図である。FIG. 5 is an explanatory diagram of a purification process and a regeneration process.
【図６】上記前処理装置により精製された原料空気のフ
ローシートを示す図である。FIG. 6 is a view showing a flow sheet of raw material air purified by the pretreatment device.
【図７】本発明の空気分離装置の他の実施の形態を示す
構成図である。FIG. 7 is a configuration diagram showing another embodiment of the air separation device of the present invention.
２，４ 圧縮機 １０ 第１原空冷却器 １１ ミストセパレーター １２ 第２原空冷却器 １５ 第１吸着塔 １６ 第２吸着塔 ２０ 原空熱交換器 ２１ 原空ヒーター ２２ 触媒塔 ２５ 第１吸着塔 ２６ 第２吸着塔 Ｃ 第１吸着ユニット Ｅ 第２吸着ユニット 2,4 compressor 10 1st original air cooler 11 Mist separator 12 Second original air cooler 15 First adsorption tower 16 Second adsorption tower 20 original air heat exchanger 21 Air heater 22 catalyst tower 25 First adsorption tower 26 Second adsorption tower C 1st adsorption unit E 2nd adsorption unit
───────────────────────────────────────────────────── フロントページの続き (72)発明者 裏久保 嘉昭 大阪府堺市築港新町２丁６番地40 大同 ほくさん株式会社 堺工場内 (56)参考文献 特開 平３−194381（ＪＰ，Ａ) 特開 平９−33166（ＪＰ，Ａ) 特開 平５−172458（ＪＰ，Ａ) 特開 平５−177115（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) F25J 1/00 - 5/00 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Yoshiaki Urakubo 2-6-6 Tsukikoshinmachi, Sakai City, Osaka 40 Daido Hokusan Co., Ltd. in Sakai Plant (56) Reference JP-A-3-194381 (JP, A) JP Hei 9-33166 (JP, A) JP 5-172458 (JP, A) JP 5-177115 (JP, A) (58) Fields investigated (Int.Cl. 7 , DB name) F25J 1 / 00-5/00
Claims (2)
圧縮機と、この圧縮機による圧縮熱によって昇温した原
料空気を水と熱交換させて冷却する第１の熱交換器と、
この第１の熱交換器による冷却によって発生した凝縮水
を分離する凝縮水分離器と、この凝縮水分離器を経た原
料空気中の水分をさらに吸着して除湿するとともに酸化
イオウを代表とする触媒毒を吸着する第１の吸着塔と、
原料空気中の一酸化炭素および水素を酸化する触媒塔
と、上記第１の吸着塔を経た原料空気と触媒塔を経た原
料空気とを熱交換させて上記第１の吸着塔を経た原料空
気を昇温させるとともに上記触媒塔を経た原料空気を降
温させる第２の熱交換器と、この第２の熱交換器を経た
原料空気を加熱するヒーターと、このヒーターにより加
熱された原料空気を上記触媒塔に導入して原料空気中の
一酸化炭素および水素を酸化させる導入路と、上記触媒
塔から取り出されたのち第２の熱交換器を経由した原料
空気を冷却水により冷却する第３の熱交換器と、この第
３の熱交換器により冷却された原料空気中の炭酸ガスと
水とを吸着して除去する第２の吸着塔と、この第２の吸
着塔を経た原料空気を超低温に冷却する主熱交換手段
と、この主熱交換手段により超低温に冷却された原料空
気の一部を液化して底部に溜め窒素のみを気体として上
部側から取り出す精留塔と、この精留塔から気体として
取り出される窒素を上記主熱交換手段を経由させその内
部を通る原料空気と熱交換させることにより温度上昇さ
せ取り出す窒素ガス取出路とを備えたことを特徴とする
空気分離装置。1. A compressor for compressing raw material air taken from the outside, and a first heat exchanger for cooling the raw material air that has been heated by the heat of compression by the compressor by exchanging heat with water.
A condensed water separator that separates condensed water generated by cooling by the first heat exchanger, and a catalyst typified by sulfur oxide while further adsorbing moisture in the raw material air that has passed through the condensed water separator to dehumidify A first adsorption tower for adsorbing poison,
The catalyst tower that oxidizes carbon monoxide and hydrogen in the raw material air and the raw material air that has passed through the first adsorption tower and the raw material air that has passed through the catalyst tower are heat-exchanged to obtain the raw material air that has passed through the first adsorption tower. A second heat exchanger that raises the temperature and lowers the temperature of the raw material air that has passed through the catalyst tower, a heater that heats the raw material air that has passed through the second heat exchanger, and the raw material air that has been heated by the heater An introduction path for introducing carbon monoxide and hydrogen in the raw material air to oxidize the raw material air, and a third heat for cooling the raw material air, which has been taken out from the catalyst tower and passed through the second heat exchanger, with cooling water. An exchanger, a second adsorption tower that adsorbs and removes carbon dioxide gas and water in the raw material air cooled by the third heat exchanger, and the raw material air that has passed through the second adsorption tower is brought to an ultralow temperature. Main heat exchange means for cooling and this main heat exchange means A rectification column that liquefies a part of the raw air cooled to a much lower temperature and collects it at the bottom and takes out only nitrogen as a gas from the upper side, and nitrogen taken out as a gas from this rectification column via the main heat exchange means An air separation device comprising: a nitrogen gas take-out path for raising the temperature by taking out heat from the raw material air passing through the inside of the apparatus and raising the temperature.
金属触媒および銅系触媒である請求項１記載の空気分離
装置。2. The air separation device according to claim 1, wherein the catalyst used in the catalyst tower is a noble metal catalyst such as palladium and a copper catalyst.
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|---|---|---|---|
| JP20685199A JP3532466B2 (en) | 1999-07-21 | 1999-07-21 | Air separation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20685199A JP3532466B2 (en) | 1999-07-21 | 1999-07-21 | Air separation device |
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| Publication Number | Publication Date |
|---|---|
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| JP3532466B2 true JP3532466B2 (en) | 2004-05-31 |
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