JPH0240366B2 - - Google Patents
Info
- Publication number
- JPH0240366B2 JPH0240366B2 JP57113643A JP11364382A JPH0240366B2 JP H0240366 B2 JPH0240366 B2 JP H0240366B2 JP 57113643 A JP57113643 A JP 57113643A JP 11364382 A JP11364382 A JP 11364382A JP H0240366 B2 JPH0240366 B2 JP H0240366B2
- Authority
- JP
- Japan
- Prior art keywords
- adsorption tower
- adsorption
- gas
- regeneration
- purified gas
- 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 - Lifetime
Links
- 238000001179 sorption measurement Methods 0.000 claims description 62
- 238000000034 method Methods 0.000 claims description 28
- 238000011069 regeneration method Methods 0.000 claims description 26
- 230000008929 regeneration Effects 0.000 claims description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 18
- 238000000746 purification Methods 0.000 claims description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 9
- 239000001569 carbon dioxide Substances 0.000 claims description 7
- 238000003795 desorption Methods 0.000 description 14
- 239000003463 adsorbent Substances 0.000 description 9
- 238000007796 conventional method Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
この発明は空気中に含まれる水分と二酸化炭素
をプレツシヤースイング法によつて除去して製品
ガスを得る気体精製法に関するものである。
例えば空気を液化分離する方法においては、原
料空気中の水分、二酸化炭素等を除去する必要が
あるが、この除去方法としてプレツシヤースイン
グ法による気体精製法が提案されている。第１図
に示す方法は、従来公知の一例を示したもので、
原料空気は管１より圧縮機２に送られ、ここで加
圧された後、切換弁８ａを経て切替使用される２
基の吸着塔４，５の一方の吸着塔４に導入され
る。上記吸着塔４，５には水分（以下、H2Oと
記す）および二酸化炭素（以下、CO2と記す）を
優先的に吸着する吸着剤がそれぞれ充填されてお
り加圧状態で吸着塔４に導入された原料空気中の
H2OおよびCO2が吸着剤に吸着される。このよう
にして得られた精製ガス（精製空気）は、切換弁
６ａ、管７、弁８を経て供給先に送られる。（吸
着工程）
次に、この精製ガスの一部は弁９により減圧さ
れ、切換弁１０ｂを経て他方の吸着塔５に送り込
まれる。吸着塔５に導入された減圧精製ガスは、
吸着塔５内の吸着剤中を通過し、吸着工程におい
て吸着したH2O、吸着CO2を脱着する。このよう
にしてH2O、CO2を脱着した吸着塔５の底部に至
つた再生用ガスは、切換弁１１ｂを経て排気され
る。（再生工程）
上記のように、切換弁８ａ，６ａ，１０ｂ，１
１ｂを開の状態に、そして切換弁８ｂ，６ｂ，１
０ａ，１１ａを閉の状態にすると吸着塔４内は吸
着操作中、吸着塔５内は脱着（再生）操作中とな
る。この関係を一定時間毎に切換えることによ
り、連続的に精製ガスを得ることができる。
ところで、この方法は上記のように吸着剤の再
生を得られる精製ガスの一部を再生ガ用ガスとし
て圧抜きした吸着塔にもどして吸着成分（H2O、
CO2）を脱着することにより行なつているので、
製品（精製ガス）収率が低いものとなる欠点があ
る。又上記の方法において消費される精製ガス
は、下記に述べるように従来の公知例よりH2O
の脱着に消費される量よりもCO2の脱着に消費さ
れる量の方が格段に多いことが判る。即ちH2O
の脱着に使用される精製ガスの消費率（Ｒ）は、
一般に空気圧力Ｐと再生時の圧力P0とによつて
次のように求めることができる。
Ｒ＝１／Ｐ／P0 …(1)
この(1)式によつて、例えば吸着圧6ata、再生圧
1ataとして、吸着H2Oの脱着に使われる精製ガ
スの消費率（Ｒ）を求めてみると、
Ｒ＝１／６／１×100％≒17％となる。
一方、吸着CO2に対しては、周知のようにCO2
がH2Oの脱着に比べ容易でないことから、CO2を
10ppm以下に減少させるには40％〜50％の精製ガ
スが必要である。
従つて、上記従来のプレツシヤースイング法に
よる気体精製法においてはH2O除去については
少ない精製ガス消費で済むが、CO2を同時に除去
するために多量の精製ガスを消費していることに
なる。
このように、第１図に示した従来のプレツシヤ
ースイング法による気体精製法は、その吸着剤の
再生を精製ガスの一部を再生用ガスとして再生工
程にある吸着塔にもどして吸着成分（H2O、
CO2）を脱着することにより行なつているので、
再生用、特に吸着CO2の脱着に使われる精製ガス
の消費率が高くなつており、そのために製品収率
が低くなつてしまうという欠点がある。
この発明は上記事情に鑑みてなされたもので、
その目的は製品収率の高いプレツシヤースイング
法によるガス精製法を提供することにあり、吸着
塔を水分吸着塔（以下、H2O吸着塔と記す）と
二酸化炭素吸着塔（以下、CO2吸着塔と記す）に
分割し、H2O吸着塔の再生は従来通り精製ガス
による脱着によつて行ない、CO2吸着塔の再生は
真空引きによつて行なうことによつて再生用とし
て使われる精製ガスの消費率を低減化したもので
ある。
以下、この発明を図面を参照して説明する。第
２図はこの発明を実施するに最適な気体精製装置
の一例を示すもので、第１図と共通する部分には
同一符号を付して説明を簡略化する。この発明の
特徴は前記したように従来H2OおよびCO2の吸着
を同時に行なつていた吸着塔をH2O吸着塔２１，
２２とCO2吸着塔２３，２４とに分割したこと
と、CO2吸着塔２３，２４の再生を真空引きにて
行なうことにある。上記H2O吸着塔２１，２２
にはシリカゲル、活性アルミナなどのH2Oを優
先的に吸着する吸着剤が充填されており、上記
CO2吸着塔２３，２４には５Ａあるいは１３Ｘ系
の合成ゼオライトなどのCO2を優先的に吸着する
吸着塔が充填されている。なお、図中符号２５は
真空ポンプ、２６ａ，２６ｂ，２６ｃ，２６ｄ，
２７ａ，２７ｂ，２７ｃ，２７ｄは切換弁、２８
は調整弁をそれぞれ示すものである。この実施例
において、原料空気は管１より圧縮機２に送ら
れ、ここで加圧された後、切換弁３ａを経て
H2O吸着塔２１に導入される。H2O吸着塔２１
に加圧状態で導入された原料空気は、その中の
H2OがこのH2O吸着塔２１中の吸着剤に吸着除
去された後切換弁２６ａを経てCO2吸着塔２３に
導入される。CO2吸着塔に送り込まれた空気はそ
の中のCO2がこのCO2吸着塔２３中の吸着剤に吸
着され、このようにしてH2OおよびCO2の除去さ
れた空気（精製ガス）は切換弁２６ｄ、管２９を
経て供給先に送られる。（吸着工程）
次に、この精製ガスの一部は調整弁２８で減圧
された後、管３０、切換弁２７ｂを経てH2O吸
着塔２２に供給される。H2O吸着塔２２に導入
された減圧精製ガスは、H2O吸着塔２２の吸着
剤中を通過し、吸着H2Oを脱着する。このよう
にしてH2O吸着塔２２の底部に至つた再生用ガ
スは、切換弁１１ｂを経て排気される。一方CO2
吸着塔２４は切換弁２７ｃを開（２７ａ，ｄは
閉）にし、真空ポンプ２５を作動して、該塔２４
を真空引きし、吸着CO2を脱着する。（再生工程）
なお、この再生工程に先立つて切換弁１１ｂ、２
７ａを開にしてH2O吸着塔２２およびCO2吸着塔
２４を大気圧にしておく。
上記のようにして所定量のH2OおよびCO2を吸
着してH2O吸着塔２１およびCO2吸着塔２３が飽
和寸前となつたら、各切換弁を上記の場合と逆に
してH2O吸着塔２２とCO2吸着塔２４側で吸着工
程を行ない、H2O吸着塔２１およびCO2吸着塔２
３側は再生工程を行なう。このようにH2O吸着
塔２１、CO2吸着塔２３とH2O吸着塔２２、CO2
吸着塔２４を交互に切換え使用することにより連
続的に精製ガスを得ることができる。
この発明においては、上記のようにCO2吸着塔
２３，２４の再生を真空引きにて行なうので、再
生用として使われる精製ガスを大巾に少なくする
ことができる。そして、真空引きによる再生は
CO2吸着塔２３，２４内の圧力を強制的に下げる
ものなので、精製ガスにより吸着CO2を洗い流す
従来の方法と比べて効率のよい脱着が行なわれ
る。また、従来の精製ガスにより行なう再生で
は、原料空気を所定の吸着圧まで昇圧した後、減
圧して再生用ガスとして用いるため、その再生用
ガスをつくるためのエネルギーが多く必要であつ
たが、この発明では従来CO2の脱着に使われてい
た再生用ガスが全く無用となるので、多くのエネ
ルギーを節約することになる。
以上説明したように、この発明はCO2の脱着が
H2Oの脱着より容易でない点に着目して、H2O
の脱着を従来法と同じように精製ガスの一部を利
用して行ない、CO2の脱着を真空再生法を用いる
ことにより行なうものなので、再生用として使用
される精製ガスの消費率を大巾に減圧化すること
ができるとともに効率の良い再生を行なうことが
でき製品収率の向上ばかりでなく、生産コストの
低減化も図ることができる。
このようなこの発明の効果を定量的に確認する
ために下記のような実験を行なつた。
実験例
(i) 実験条件
第２図に示す構造の装置を使い、表１のよう
な条件で実験を行なつた。
This invention relates to a gas purification method for obtaining a product gas by removing moisture and carbon dioxide contained in the air by a pressure swing method. For example, in a method of liquefying and separating air, it is necessary to remove moisture, carbon dioxide, etc. from the raw air, and a gas purification method using a pressure swing method has been proposed as a method for this removal. The method shown in FIG. 1 is an example of a conventionally known method.
The raw air is sent from the pipe 1 to the compressor 2, where it is pressurized and then passed through the switching valve 8a to be switched to the compressor 2.
It is introduced into one of the two adsorption towers 4 and 5. The adsorption towers 4 and 5 are each filled with an adsorbent that preferentially adsorbs moisture (hereinafter referred to as H 2 O) and carbon dioxide (hereinafter referred to as CO 2 ), and the adsorption towers 4 and 5 are charged under pressure. raw material introduced into the air
H 2 O and CO 2 are adsorbed on the adsorbent. The purified gas (purified air) thus obtained is sent to the supply destination via the switching valve 6a, the pipe 7, and the valve 8. (Adsorption Step) Next, a portion of this purified gas is depressurized by the valve 9 and sent to the other adsorption tower 5 via the switching valve 10b. The vacuum purified gas introduced into the adsorption tower 5 is
It passes through the adsorbent in the adsorption tower 5 and desorbs the H 2 O and adsorbed CO 2 adsorbed in the adsorption step. The regeneration gas that has thus desorbed H 2 O and CO 2 and has reached the bottom of the adsorption tower 5 is exhausted through the switching valve 11b. (Regeneration process) As mentioned above, the switching valves 8a, 6a, 10b, 1
1b in the open state, and the switching valves 8b, 6b, 1
When 0a and 11a are closed, the inside of the adsorption tower 4 is in an adsorption operation, and the inside of the adsorption tower 5 is in a desorption (regeneration) operation. By switching this relationship at regular intervals, purified gas can be obtained continuously. By the way, in this method, as described above, a part of the purified gas from which the adsorbent can be regenerated is returned to the depressurized adsorption tower as a regeneration gas, and the adsorbed components (H 2 O,
This is done by desorbing CO 2 ).
There is a drawback that the product (purified gas) yield is low. In addition, the purified gas consumed in the above method is H 2 O
It can be seen that the amount consumed for desorption of CO 2 is much larger than the amount consumed for desorption of CO 2 . i.e. H2O
The consumption rate (R) of the purified gas used for desorption of
Generally, it can be determined as follows from the air pressure P and the pressure P 0 during regeneration. R=1/P/P 0 ...(1) According to this equation (1), for example, the adsorption pressure is 6ata, the regeneration pressure is
1ata, the consumption rate (R) of purified gas used for desorption of adsorbed H 2 O is calculated as R = 1/6/1 x 100% ≒ 17%. On the other hand, for adsorbed CO 2 , as is well known, CO 2
Since desorption of CO 2 is not as easy as desorption of H 2 O,
40% to 50% purified gas is required to reduce it to below 10ppm. Therefore, in the conventional gas purification method using the pressure swing method described above, only a small amount of purified gas is consumed to remove H 2 O, but a large amount of purified gas is consumed to remove CO 2 at the same time. Become. In this way, in the conventional gas purification method using the pressure swing method shown in Figure 1, the adsorbent is regenerated by returning a part of the purified gas to the adsorption column in the regeneration process as regeneration gas. ( H2O ,
This is done by desorbing CO 2 ).
The drawback is that the consumption rate of purified gas used for regeneration, especially for desorption of adsorbed CO 2 , is high, resulting in a low product yield. This invention was made in view of the above circumstances,
The purpose is to provide a gas purification method using a pressure swing method with a high product yield . The H 2 O adsorption tower is regenerated by desorption using purified gas as before, and the CO 2 adsorption tower is regenerated by vacuum evacuation. This reduces the consumption rate of purified gas. The present invention will be explained below with reference to the drawings. FIG. 2 shows an example of a gas purification apparatus most suitable for carrying out the present invention, and parts common to those in FIG. 1 are given the same reference numerals to simplify the explanation. The feature of this invention is that, as mentioned above, the adsorption tower that previously adsorbed H 2 O and CO 2 at the same time is replaced by the H 2 O adsorption tower 21,
22 and CO 2 adsorption towers 23 and 24, and the CO 2 adsorption towers 23 and 24 are regenerated by vacuuming. The above H 2 O adsorption tower 21, 22
is filled with adsorbents such as silica gel and activated alumina that preferentially adsorb H 2 O.
The CO 2 adsorption towers 23 and 24 are filled with adsorption towers that preferentially adsorb CO 2 such as 5A or 13X synthetic zeolite. In addition, the code|symbol 25 in the figure is a vacuum pump, 26a, 26b, 26c, 26d,
27a, 27b, 27c, 27d are switching valves, 28
indicate the regulating valves, respectively. In this embodiment, raw air is sent from a pipe 1 to a compressor 2, where it is pressurized and then passed through a switching valve 3a.
It is introduced into the H 2 O adsorption tower 21 . H 2 O adsorption tower 21
The raw air introduced under pressure into the
After H 2 O is adsorbed and removed by the adsorbent in the H 2 O adsorption tower 21, it is introduced into the CO 2 adsorption tower 23 via the switching valve 26a. The CO 2 in the air sent to the CO 2 adsorption tower is adsorbed by the adsorbent in the CO 2 adsorption tower 23, and the air (purified gas) from which H 2 O and CO 2 have been removed is It is sent to the destination via the switching valve 26d and the pipe 29. (Adsorption Step) Next, a portion of this purified gas is depressurized by the regulating valve 28 and then supplied to the H 2 O adsorption tower 22 via the pipe 30 and the switching valve 27b. The vacuum purified gas introduced into the H 2 O adsorption tower 22 passes through the adsorbent of the H 2 O adsorption tower 22 and desorbs the adsorbed H 2 O. The regeneration gas that has reached the bottom of the H 2 O adsorption tower 22 in this way is exhausted through the switching valve 11b. Meanwhile CO2
The adsorption tower 24 is opened by opening the switching valve 27c (27a and d are closed) and operating the vacuum pump 25.
is evacuated and the adsorbed CO 2 is desorbed. (Regeneration process)
Note that, prior to this regeneration process, the switching valves 11b and 2
7a is opened to keep the H 2 O adsorption tower 22 and the CO 2 adsorption tower 24 at atmospheric pressure. When a predetermined amount of H 2 O and CO 2 is adsorbed as described above and the H 2 O adsorption tower 21 and CO 2 adsorption tower 23 are on the verge of saturation, each switching valve is reversed to the above case to remove H 2 O and CO 2 . The adsorption process is performed on the O adsorption tower 22 and CO 2 adsorption tower 24 side, and the H 2 O adsorption tower 21 and CO 2 adsorption tower 2
The third side performs a regeneration process. In this way, H 2 O adsorption tower 21, CO 2 adsorption tower 23, H 2 O adsorption tower 22, CO 2
Purified gas can be obtained continuously by alternately switching and using the adsorption towers 24. In this invention, since the CO 2 adsorption towers 23 and 24 are regenerated by evacuation as described above, the amount of purified gas used for regeneration can be greatly reduced. And regeneration by vacuuming
Since the pressure inside the CO 2 adsorption towers 23 and 24 is forcibly lowered, desorption is performed more efficiently than in the conventional method of washing away the adsorbed CO 2 with purified gas. In addition, in conventional regeneration using purified gas, the feed air is pressurized to a predetermined adsorption pressure and then depressurized and used as regeneration gas, which requires a large amount of energy to produce the regeneration gas. With this invention, the regeneration gas conventionally used for CO 2 desorption is completely unnecessary, resulting in a large amount of energy savings. As explained above, this invention is effective in desorption of CO2 .
Focusing on the fact that it is less easy to desorb than H 2 O, H 2 O
As in the conventional method, desorption of CO 2 is performed using part of the purified gas, and desorption of CO 2 is performed using a vacuum regeneration method, so the consumption rate of purified gas used for regeneration can be greatly reduced. It is possible to reduce the pressure and perform efficient regeneration, which not only improves product yield but also reduces production costs. In order to quantitatively confirm the effects of this invention, the following experiment was conducted. Experimental Example (i) Experimental Conditions Using an apparatus having the structure shown in FIG. 2, experiments were conducted under the conditions shown in Table 1.
【表】 (ii) 実験結果 その結果、表２の数値が得られた。【table】 (ii) Experimental results As a result, the values shown in Table 2 were obtained.
【表】
この表２に見るようにこの発明の再生空気（精
製ガス）消費率30％となつており、前記従来の方
法での再生空気消費率のほぼ半分となつている。
また、この実験に基づいて、その再生空気消費
率、精製空気量、消費動力を従来の方法と比較し
たところ表８に示す結果となり、この発明の製品
収率および経済性の向上が明らかとなつた。[Table] As shown in Table 2, the regeneration air (purified gas) consumption rate of the present invention is 30%, which is approximately half of the regeneration air consumption rate of the conventional method. Furthermore, based on this experiment, the recycled air consumption rate, purified air amount, and power consumption were compared with those of the conventional method, and the results are shown in Table 8, making it clear that the product yield and economic efficiency of this invention are improved. Ta.
第１図は従来のプレツシヤースイング法による
気体精製法に使われていた気体精製装置の構成
図、第２図はこの発明の一実施例を説明するため
のもので、この発明を実施するのに最適な気体精
製装置の構成図である。
２…空気圧縮機、２１，２２…水分吸着塔、２
３，２４…二酸化炭素吸着塔、２５…真空ポン
プ。
Fig. 1 is a block diagram of a gas purification device used in a conventional pressure swing gas purification method, and Fig. 2 is a diagram for explaining an embodiment of the present invention. FIG. 1 is a configuration diagram of a gas purification device most suitable for 2... Air compressor, 21, 22... Moisture adsorption tower, 2
3, 24... Carbon dioxide adsorption tower, 25... Vacuum pump.
Claims (1)
に吸着する複数の吸着塔を吸着・再生の各工程に
切換えることにより連続的に精製ガスを得るプレ
ツシヤースイング法による気体精製法において、
上記吸着塔を水分吸着塔と二酸化炭素吸着塔とに
分割し、原料空気をそれぞれの吸着塔に流して精
製すると共に水分吸着塔には、精製ガスの一部を
再生用ガスとして導入することにより又、二酸化
炭素吸着塔は、真空引きによりそれぞれ再生する
ことを特徴とするプレツシヤースイング法による
気体精製法。1. In a gas purification method using a pressure swing method in which purified gas is continuously obtained by switching a plurality of adsorption towers that selectively adsorb moisture and carbon dioxide in the raw air to each adsorption/regeneration process,
The above adsorption tower is divided into a moisture adsorption tower and a carbon dioxide adsorption tower, and the raw air is purified by flowing through each adsorption tower, and a part of the purified gas is introduced into the moisture adsorption tower as a regeneration gas. Further, a gas purification method using a pressure swing method is characterized in that each carbon dioxide adsorption tower is regenerated by evacuation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57113643A JPS594414A (en) | 1982-06-30 | 1982-06-30 | Method for purifying gas by pressure swinging method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57113643A JPS594414A (en) | 1982-06-30 | 1982-06-30 | Method for purifying gas by pressure swinging method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS594414A JPS594414A (en) | 1984-01-11 |
| JPH0240366B2 true JPH0240366B2 (en) | 1990-09-11 |
Family
ID=14617434
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57113643A Granted JPS594414A (en) | 1982-06-30 | 1982-06-30 | Method for purifying gas by pressure swinging method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS594414A (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01174879A (en) * | 1987-12-28 | 1989-07-11 | Teisan Kk | Air separator |
| US5156657A (en) * | 1990-03-29 | 1992-10-20 | The Boc Group, Inc. | Process for pre-purification of air for separation |
| GB9303844D0 (en) * | 1993-02-25 | 1993-04-14 | Boc Group Plc | Purification method and apparatus |
| US5531808A (en) * | 1994-12-23 | 1996-07-02 | The Boc Group, Inc. | Removal of carbon dioxide from gas streams |
-
1982
- 1982-06-30 JP JP57113643A patent/JPS594414A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS594414A (en) | 1984-01-11 |
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