JPH08131767A - Method for separating and recovering carbon dioxide of high concentration - Google Patents
Method for separating and recovering carbon dioxide of high concentrationInfo
- Publication number
- JPH08131767A JPH08131767A JP6274819A JP27481994A JPH08131767A JP H08131767 A JPH08131767 A JP H08131767A JP 6274819 A JP6274819 A JP 6274819A JP 27481994 A JP27481994 A JP 27481994A JP H08131767 A JPH08131767 A JP H08131767A
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- adsorption tower
- stage
- stage adsorption
- adsorption column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、燃焼排ガス、例えば石
炭焚ボイラ排ガスから圧力スイング吸着法によって二酸
化炭素を高濃度に濃縮して分離回収する方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for concentrating carbon dioxide from a combustion exhaust gas, for example, a coal-fired boiler exhaust gas, to a high concentration by a pressure swing adsorption method to separate and recover the carbon dioxide.
【０００２】[0002]
【従来の技術】従来、石炭焚きボイラ排ガスから圧力ス
イング吸着法によって二酸化炭素を吸着分離回収する方
法は排ガス中の二酸化炭素を回収する第１段吸着塔と、
回収された二酸化炭素を高濃度に濃縮する第２段吸着塔
から構成されており、第１段吸着塔が回収を目的として
いるため、吸着工程に際して第１段吸着塔塔頂部から排
出されるガスは回収率に見合った二酸化炭素濃度１〜２
ｖｏｌ％のガスであるが、第２段吸着塔では第１段吸着
塔で減容濃縮された二酸化炭素５０ｖｏｌ％以上のガス
を更に９９ｖｏｌ％まで濃縮するため、第２段吸着塔で
は、吸着工程及び吸着工程終了後に高濃度の脱着ガスを
用いて吸着塔入口部よりパージを行う置換パージ工程の
各工程の吸着塔塔頂部から排出されるガスは原料ガスよ
り二酸化炭素が高濃度となることから、二酸化炭素除去
システムとして回収率を上げるために、これらの塔頂部
から排出されるガスは第１段吸着塔の入口へ戻す方法が
とられている。2. Description of the Related Art Conventionally, a method of adsorbing and separating carbon dioxide from a coal-fired boiler exhaust gas by a pressure swing adsorption method comprises a first stage adsorption tower for recovering carbon dioxide in the exhaust gas,
It is composed of a second-stage adsorption tower that concentrates the recovered carbon dioxide to a high concentration, and the first-stage adsorption tower is intended for recovery, so the gas discharged from the top of the first-stage adsorption tower during the adsorption process. Is a carbon dioxide concentration of 1 to 2 commensurate with the recovery rate
Although it is a gas of vol%, in the second-stage adsorption tower, since the gas of 50 vol% or more of the carbon dioxide volume-reduced and concentrated in the first-stage adsorption tower is further concentrated to 99 vol%, the adsorption step in the second-stage adsorption tower And, since the gas discharged from the top of the adsorption tower in each step of the displacement purging step of purging from the inlet of the adsorption tower using a high-concentration desorption gas after the adsorption step has a higher concentration of carbon dioxide than the raw material gas In order to increase the recovery rate as a carbon dioxide removal system, a method of returning the gas discharged from these tower tops to the inlet of the first stage adsorption tower is adopted.
【０００３】[0003]
【発明が解決しようとする課題】上記のように、第２段
吸着塔塔頂部から排出される全てのガスを第１段吸着塔
に戻す方式では回収率の増加は期待されるが、第１段吸
着塔入口の二酸化炭素濃度が原料ガス中の１３ｖｏｌ％
程度に対し２０〜３０ｖｏｌ％と増加し、第１段吸着塔
への二酸化炭素の負荷が増加する。このことは、第１段
吸着塔の吸着剤で吸着された二酸化炭素を減圧にして脱
着回収する際の脱着ガス量の増加となり、最終的には第
１段吸着塔の脱着用真空ポンプの容量増加、すなわち、
電力量の増加を生じることになる。本発明では、このよ
うな欠点を解消し、できるだけ少ない電力量で高濃度、
高回収率の二酸化炭素の分離、回収方法を提供しようと
するものである。As described above, in the system in which all the gas discharged from the top of the second-stage adsorption tower is returned to the first-stage adsorption tower, the recovery rate is expected to increase. The carbon dioxide concentration at the inlet of the single-stage adsorption tower is 13 vol% in the raw material gas.
The amount of carbon dioxide increases to 20 to 30% by volume, and the load of carbon dioxide on the first-stage adsorption tower increases. This increases the amount of desorbed gas when desorbing and recovering carbon dioxide adsorbed by the adsorbent of the first-stage adsorption tower under reduced pressure, and finally the capacity of the desorption vacuum pump of the first-stage adsorption tower. Increase, ie
This will cause an increase in the amount of electric power. In the present invention, such drawbacks are eliminated, and high concentration with a minimum amount of electric power,
It intends to provide a method for separating and collecting carbon dioxide with a high recovery rate.
【０００４】[0004]
【課題を解決するための手段】本発明は二酸化炭素吸着
剤を充填した吸着塔を２段に使用して、第１段吸着塔で
は排ガス中の二酸化炭素を５０ｖｏｌ％以上に減容濃縮
して回収し、次いで第２段吸着塔で上記減容濃縮された
二酸化炭素を更に９９ｖｏｌ％以上の高濃度の二酸化炭
素として回収する燃焼排ガスから圧力スイング吸着法に
よって高濃度二酸化炭素を分離回収する方法において、
第２段吸着塔における吸着時の第２段吸着塔からの排ガ
スは第１段吸着塔入口に戻し、第２段吸着塔の吸着工程
終了後、第２段吸着塔に高濃度二酸化炭素を流過させて
該吸着塔内のデッドスペースを消失させる置換パージ工
程における第２段吸着塔からの高濃度二酸化炭素含有排
ガスは第２段吸着塔入口に戻すことを特徴とする燃焼排
ガスから高濃度二酸化炭素の分離回収方法である。According to the present invention, an adsorption tower filled with a carbon dioxide adsorbent is used in two stages, and in the first-stage adsorption tower, the carbon dioxide in the exhaust gas is reduced to 50 vol% or more and concentrated. A method for separating and recovering high-concentration carbon dioxide from a combustion exhaust gas by recovering and then recovering the volume-reduced and concentrated carbon dioxide in the second-stage adsorption tower as high-concentration carbon dioxide of 99 vol% or more by a pressure swing adsorption method ,
Exhaust gas from the second-stage adsorption tower at the time of adsorption in the second-stage adsorption tower is returned to the inlet of the first-stage adsorption tower, and after the adsorption process of the second-stage adsorption tower is completed, high-concentration carbon dioxide is flowed to the second-stage adsorption tower. The high-concentration carbon dioxide-containing exhaust gas from the second-stage adsorption tower in the displacement purging step for eliminating the dead space in the adsorption tower is returned to the inlet of the second-stage adsorption tower to produce high-concentration dioxide. It is a carbon separation and recovery method.
【０００５】[0005]
【作用】図１は本発明に係る高濃度二酸化炭素を分離、
回収する方法を実施するための装置の概念図である。こ
の装置は前処理として排ガス中の水分を除去する水分吸
着塔１ａ，１ｂ（これらは交互に切換えられて使用され
る）と二酸化炭素の回収を目的とする第１段二酸化炭素
吸着塔２ａ，２ｂ，２ｃ（これらも交互に切換えられて
使用される）と、第１段吸着塔で回収した二酸化炭素を
高濃度に濃縮する第２段二酸化炭素吸着塔３ａ，３ｂ，
３ｃ（これらも交互に切換えられて使用される）からな
る。[Operation] FIG. 1 shows the separation of high-concentration carbon dioxide according to the present invention.
It is a conceptual diagram of the apparatus for implementing the collection method. As a pretreatment, this apparatus is a water adsorption tower 1a, 1b for removing water in exhaust gas (these are used by being switched alternately) and a first-stage carbon dioxide adsorption tower 2a, 2b for the purpose of carbon dioxide recovery. , 2c (these are also used by being switched alternately) and the second-stage carbon dioxide adsorption towers 3a, 3b for concentrating the carbon dioxide recovered in the first-stage adsorption tower to a high concentration,
3c (these are also used by being switched alternately).
【０００６】石炭焚きボイラから排出される排ガスは原
料ガスライン２を介してＮｏ．１ブロワ３で水分吸着塔
１ａ（又は１ｂ，１ｃ）に供給され、水分を除去された
排ガスはライン５を介して第１段吸着塔２ａ（又は２
ｂ，２ｃ）へ供給されて二酸化炭素を吸着分離し、水分
吸着塔１ａ（又は１ｂ）に吸着塔に吸着されている水分
の除去は第１段吸着塔２ａ（又は２ｂ，２ｃ）の塔頂部
からの排ガスをライン６より再生ガスとして用いると同
時に除湿用真空ポンプ４によって行われる。Exhaust gas discharged from the coal-fired boiler is fed through the raw material gas line 2 to No. The exhaust gas supplied to the water adsorption tower 1a (or 1b, 1c) by the 1 blower 3 and having the water removed therefrom is passed through the line 5 to the first stage adsorption tower 2a (or 2).
b, 2c) to adsorb and separate carbon dioxide, and to remove the water adsorbed by the water adsorption tower 1a (or 1b) from the adsorption tower 1a (or 2b, 2c). At the same time that the exhaust gas from is used as a regeneration gas from the line 6, the dehumidification vacuum pump 4 performs the same.
【０００７】第１段吸着塔２ａ（又は２ｂ，２ｃ）で吸
着分離された二酸化炭素はＮｏ．１真空ポンプ７によっ
て減圧下で脱着され、サージタンク８及びＮｏ．２ブロ
ワ９によって第２段二酸化炭素吸着塔３ａ（又は３ｂ，
３ｃ）へ供給される。第２段吸着塔では吸着工程で二酸
化炭素を吸着分離した残ガス中の二酸化炭素濃度は、ま
だ原料ガス中二酸化炭素より高いため、ライン１０を介
してＮｏ．１ブロワ３の入口側へ戻す。The carbon dioxide adsorbed and separated in the first-stage adsorption tower 2a (or 2b, 2c) is no. 1 vacuum pump 7 is attached and detached under reduced pressure, and surge tank 8 and No. The second blower 9 allows the second-stage carbon dioxide adsorption tower 3a (or 3b,
3c). In the second-stage adsorption tower, the carbon dioxide concentration in the residual gas obtained by adsorbing and separating carbon dioxide in the adsorption step is still higher than the carbon dioxide in the raw material gas. 1 Return to the inlet side of the blower 3.
【０００８】第２段吸着塔では、次の工程として、高濃
度に濃縮するため、第２段吸着塔の脱着ガスの一部をラ
イン１１を介して吸着工程終了後に該第２段吸着塔内の
デッドスペースを高濃度ガスによって充填し、デッドス
ペースに残存している吸着工程時の低濃度ガスをパージ
する工程（置換パージ工程）がある。この置換パージ工
程の吸着塔塔頂部から排出されるガス濃度は第１段吸着
塔の脱着ガス濃度と同程度の高濃度であるため、ライン
１２を介して第２段吸着塔の入口へ戻す。次に、この置
換パージ工程終了後、Ｎｏ．２真空ポンプ１３により減
圧し高濃度のガスとしてサージタンク１４を介してライ
ン１５より回収する。In the second-stage adsorption tower, in the next step, in order to concentrate to a high concentration, a part of the desorption gas of the second-stage adsorption tower is passed through the line 11 into the second-stage adsorption tower after the adsorption step is completed. Of the dead space is filled with a high concentration gas, and the low concentration gas remaining in the dead space during the adsorption process is purged (displacement purging process). Since the gas concentration discharged from the top of the adsorption tower in this substitution purging step is as high as the desorption gas concentration of the first adsorption tower, it is returned to the inlet of the second adsorption tower via line 12. Next, after the completion of the replacement purging step, No. (2) The pressure is reduced by the vacuum pump 13 and recovered as high-concentration gas from the line 15 via the surge tank 14.
【０００９】本発明では、上記のように、第２段吸着塔
の置換パージ工程の排出ガスを第２段吸着塔の吸着工程
の排出ガスと同様に第１段吸着塔のブロワ３の入口へ戻
すのではなく、ラインを分け第２段吸着塔の入口へ戻す
ことによって、第１段吸着塔への二酸化炭素の負荷を下
げ、Ｎｏ．１真空ポンプ７の負荷を下げ、システムの動
力原単位を低減することができる。又、第２段吸着塔か
らの循環ガス量が減少するため、ライン２を介してＮ
ｏ．１ブロワ３より系全体へ導入されるガス量の増加が
可能となる。In the present invention, as described above, the exhaust gas from the displacement purge step of the second-stage adsorption tower is introduced into the inlet of the blower 3 of the first-stage adsorption tower in the same manner as the exhaust gas from the adsorption step of the second-stage adsorption tower. Instead of returning it, the line is divided and returned to the inlet of the second-stage adsorption tower to reduce the carbon dioxide load on the first-stage adsorption tower, and (1) The load of the vacuum pump 7 can be reduced to reduce the power consumption of the system. Also, since the amount of circulating gas from the second stage adsorption tower decreases, N
o. It is possible to increase the amount of gas introduced into the entire system from one blower 3.
【００１０】[0010]
【実施例】図１の装置を用い、石炭焚ボイラ排ガスから
二酸化炭素の回収を行った。分離操作の諸元は次の通り
である。[Example] Carbon dioxide was recovered from exhaust gas from a coal-fired boiler using the apparatus shown in FIG. The specifications of the separation operation are as follows.
【００１１】[0011]
【表１】 [Table 1]
【００１２】[0012]
【表２】 [Table 2]
【００１３】第１段吸着塔に供給する排ガス量を約２，
０００〜２，２００ｍ3 Ｎ／ｈｒとすると、従来法では
第２段吸着塔の吸着時の排ガス及び第２段吸着塔の置換
パージ工程の排ガスを全て第１段吸着塔に戻すので、そ
の循環量は約６５０ｍ3 Ｎ／ｈｒ程度となり、ガス中の
二酸化炭素濃度は２２〜２５ｖｏｌ％となっていたが、
図１に示すフローによる本発明の実施例では第１段吸着
塔に戻すガス量は第２段吸着塔の吸着時の排ガスのみで
あるため、その循環量は１５０〜２００ｍ3 Ｎ／ｈｒ程
度に減少し、その第１段吸着塔入口の排ガスの二酸化炭
素濃度は約１５ｖｏｌ％になった。The amount of exhaust gas supplied to the first stage adsorption tower is about 2,
If it is 000 to 2,200 m 3 N / hr, in the conventional method, all the exhaust gas at the time of adsorption of the second-stage adsorption tower and the exhaust gas of the substitution purge step of the second-stage adsorption tower are returned to the first-stage adsorption tower. The amount was about 650 m 3 N / hr, and the carbon dioxide concentration in the gas was 22 to 25 vol%,
In the embodiment of the present invention according to the flow shown in FIG. 1, since the amount of gas returned to the first-stage adsorption tower is only the exhaust gas at the time of adsorption in the second-stage adsorption tower, the circulation amount thereof is about 150 to 200 m 3 N / hr. The carbon dioxide concentration of the exhaust gas at the inlet of the first-stage adsorption tower became about 15 vol%.
【００１４】従来法に比し第１段吸着塔への第２段吸着
塔からの循環量が６５０ｍ3 Ｎ／ｈｒから１５０〜２０
０ｍ3 Ｎ／ｈｒと減少することにより、Ｎｏ．１ブロワ
３の流量を一定にすると原料ガスライン２からの排ガス
導入量はその分増加させることができるようになると共
に、Ｎｏ．１真空ポンプ７の電力量も従来法に比べて約
１５％減少させることができた。Compared with the conventional method, the circulation amount from the second-stage adsorption tower to the first-stage adsorption tower is 650 m 3 N / hr to 150-20.
No. 3 by decreasing to 0 m 3 N / hr. When the flow rate of the blower 1 is kept constant, the amount of exhaust gas introduced from the raw material gas line 2 can be increased by that amount, and No. The power amount of the one vacuum pump 7 could be reduced by about 15% as compared with the conventional method.
【００１５】[0015]
【発明の効果】本発明によれば下記のような効果を奏し
うる。 （１）第１段吸着塔の二酸化炭素の負荷が低下し、第１
段吸着塔の脱着時に使用する真空ポンプの電力量の低下
を生じ、システムの動力原単位を低減することができ
た。 （２）第１段吸着塔への第２段吸着塔からの排ガスの循
環ガス量の減少により、同一容量で、より多くのボイラ
排ガスを処理することができた。 （３）第１段吸着塔の二酸化炭素の負荷低下により脱着
ガス量が減少し、同一の真空ポンプ容量でより再生圧力
を低く設定できるようになり、再生効果をあげることが
できた。According to the present invention, the following effects can be obtained. (1) The carbon dioxide load on the first-stage adsorption tower is reduced,
The power consumption of the vacuum pump used during desorption of the stage adsorption tower was reduced, and the power consumption of the system could be reduced. (2) Due to the reduction of the circulating gas amount of the exhaust gas from the second-stage adsorption tower to the first-stage adsorption tower, more boiler exhaust gas can be treated with the same capacity. (3) The amount of desorption gas was reduced due to the reduction of the carbon dioxide load in the first-stage adsorption tower, and the regeneration pressure could be set lower with the same vacuum pump capacity, and the regeneration effect could be improved.
【図１】本発明の高濃度二酸化炭素の分離回収方法の一
態様の説明図。FIG. 1 is an explanatory diagram of one embodiment of a method for separating and collecting high-concentration carbon dioxide according to the present invention.
フロントページの続き (72)発明者 森本 敬 長崎県長崎市深堀町五丁目717番１号 三 菱重工業株式会社長崎研究所内 (72)発明者 泉 順 長崎県長崎市深堀町五丁目717番１号 三 菱重工業株式会社長崎研究所内 (72)発明者 野原 博 長崎県長崎市飽の浦町１番１号 三菱重工 業株式会社長崎造船所内 (72)発明者 景山 靖夫 東京都千代田区丸の内二丁目５番１号 三 菱重工業株式会社本社内Front page continuation (72) Inventor Kei Morimoto 5-717-1 Fukahori-cho, Nagasaki-shi, Nagasaki Sanryo Heavy Industries Ltd. Nagasaki Research Institute (72) Inventor Jun Izumi 5-717, Fukahori-cho, Nagasaki-shi, Nagasaki Sanryo Heavy Industries Co., Ltd. Nagasaki Research Institute (72) Inventor Hiroshi Nohara 1-1, Atsunoura-machi, Nagasaki City, Nagasaki Mitsubishi Heavy Industries, Ltd. Nagasaki Shipyard (72) Inventor Yasuo Kageyama 2-5-1 Marunouchi, Chiyoda-ku, Tokyo No. Sanryo Heavy Industries Co., Ltd.
Claims (1)
段に使用して、第１段吸着塔では排ガス中の二酸化炭素
を５０ｖｏｌ％以上に減容濃縮して回収し、次いで第２
段吸着塔で上記減容濃縮された二酸化炭素を更に９９ｖ
ｏｌ％以上の高濃度の二酸化炭素として回収する燃焼排
ガスから圧力スイング吸着法によって高濃度二酸化炭素
を分離回収する方法において、第２段吸着塔における吸
着時の第２段吸着塔からの排ガスは第１段吸着塔入口に
戻し、第２段吸着塔の吸着工程終了後、第２段吸着塔に
高濃度二酸化炭素を流過させて該吸着塔内のデッドスペ
ースを消失させる置換パージ工程における第２段吸着塔
からの高濃度二酸化炭素含有排ガスは第２段吸着塔入口
に戻すことを特徴とする燃焼排ガスから高濃度二酸化炭
素の分離回収方法。1. A two-column adsorption tower filled with a carbon dioxide adsorbent.
Used in the first stage, the first stage adsorption tower reduces the volume of carbon dioxide in the exhaust gas to 50 vol% or more and recovers it.
The volume-reduced and concentrated carbon dioxide in the two-stage adsorption tower is further increased to 99 v.
In the method of separating and recovering high-concentration carbon dioxide by the pressure swing adsorption method from the combustion exhaust gas recovered as high-concentration carbon dioxide of ol% or more, the exhaust gas from the second-stage adsorption tower at the time of adsorption in the second-stage adsorption tower is After returning to the inlet of the 1st-stage adsorption tower and after the adsorption step of the 2nd-stage adsorption tower, the second purging step in which the high-concentration carbon dioxide is passed through the 2nd-stage adsorption tower to eliminate the dead space in the adsorption tower A method for separating and recovering high-concentration carbon dioxide from combustion exhaust gas, characterized in that the exhaust gas containing high-concentration carbon dioxide from the two-stage adsorption tower is returned to the inlet of the second-stage adsorption tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6274819A JPH08131767A (en) | 1994-11-09 | 1994-11-09 | Method for separating and recovering carbon dioxide of high concentration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6274819A JPH08131767A (en) | 1994-11-09 | 1994-11-09 | Method for separating and recovering carbon dioxide of high concentration |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH08131767A true JPH08131767A (en) | 1996-05-28 |
Family
ID=17547014
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6274819A Pending JPH08131767A (en) | 1994-11-09 | 1994-11-09 | Method for separating and recovering carbon dioxide of high concentration |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH08131767A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7731782B2 (en) | 2007-05-18 | 2010-06-08 | Exxonmobil Research And Engineering Company | Temperature swing adsorption of CO2 from flue gas utilizing heat from compression |
| CN101785957A (en) * | 2010-02-10 | 2010-07-28 | 毛恒松 | Carbon dioxide separation and storage method |
| EP2567746A1 (en) | 2011-09-12 | 2013-03-13 | Hitachi Ltd. | Carbon dioxide recovery system |
| JP2013103166A (en) * | 2011-11-14 | 2013-05-30 | Jfe Steel Corp | Method for separating co2 by pressure swing adsorption method |
| CN104857811A (en) * | 2015-05-06 | 2015-08-26 | 中石化石油工程设计有限公司 | Oil field carbon dioxide driving extraction gas carbon dioxide separating recovery system |
| JP2016052285A (en) * | 2014-09-04 | 2016-04-14 | 本田技研工業株式会社 | Carbon dioxide recovery apparatus |
| WO2023037854A1 (en) * | 2021-09-07 | 2023-03-16 | エア・ウォーター株式会社 | Method for manufacturing purified gas, method for manufacturing dry ice, device for manufacturing purified gas, and device for manufacturing dry ice |
| WO2023140238A1 (en) * | 2022-01-18 | 2023-07-27 | エア・ウォーター株式会社 | Method and apparatus for manufacturing purified gas |
-
1994
- 1994-11-09 JP JP6274819A patent/JPH08131767A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7731782B2 (en) | 2007-05-18 | 2010-06-08 | Exxonmobil Research And Engineering Company | Temperature swing adsorption of CO2 from flue gas utilizing heat from compression |
| CN101785957A (en) * | 2010-02-10 | 2010-07-28 | 毛恒松 | Carbon dioxide separation and storage method |
| EP2567746A1 (en) | 2011-09-12 | 2013-03-13 | Hitachi Ltd. | Carbon dioxide recovery system |
| JP2013103166A (en) * | 2011-11-14 | 2013-05-30 | Jfe Steel Corp | Method for separating co2 by pressure swing adsorption method |
| JP2016052285A (en) * | 2014-09-04 | 2016-04-14 | 本田技研工業株式会社 | Carbon dioxide recovery apparatus |
| CN104857811A (en) * | 2015-05-06 | 2015-08-26 | 中石化石油工程设计有限公司 | Oil field carbon dioxide driving extraction gas carbon dioxide separating recovery system |
| CN104857811B (en) * | 2015-05-06 | 2017-06-13 | 中石化石油工程设计有限公司 | Oil field carbon dioxide flooding produced gas carbon dioxide separation recovery system |
| WO2023037854A1 (en) * | 2021-09-07 | 2023-03-16 | エア・ウォーター株式会社 | Method for manufacturing purified gas, method for manufacturing dry ice, device for manufacturing purified gas, and device for manufacturing dry ice |
| WO2023140238A1 (en) * | 2022-01-18 | 2023-07-27 | エア・ウォーター株式会社 | Method and apparatus for manufacturing purified gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP2562326B2 (en) | How to get high concentration oxygen from air | |
| JP3902416B2 (en) | Gas separation method | |
| JPH09150028A (en) | Single bed pressure swing type adsorption method for recovering oxygen from air | |
| JPH0838846A (en) | Method for recovering light substance containing hydrogen orhelium from high pressure flow of feeding matter | |
| JPH1024208A (en) | Treatment of gaseous mixture by pressure swing adsorption | |
| KR880000803B1 (en) | Separation process of mixed gas and apparatus thereof | |
| JPH08131767A (en) | Method for separating and recovering carbon dioxide of high concentration | |
| JPH07277702A (en) | Process and apparatus for adsorptively separating argon and hydrogen in high concentration from ammonia plant purge gas | |
| JP3571672B2 (en) | Method for enriching carbon dioxide in flue gas | |
| CN210915955U (en) | Device for increasing combustion heat value of blast furnace gas | |
| JP4895467B2 (en) | Oxygen concentration method and oxygen concentration apparatus | |
| JPH09187622A (en) | Method for separating and recovering concentrated carbon dioxide | |
| JP2994843B2 (en) | Recovery method of low concentration carbon dioxide | |
| JPH0733404A (en) | Production of high concentration oxygen | |
| CN1140418A (en) | Serial flow pressure swing adsorption process for gas separation | |
| JP3654661B2 (en) | Oxygen generation method by pressure fluctuation adsorption separation method | |
| JPS61230715A (en) | Method for concentrating and recovering gas by using psa apparatus | |
| JP2893394B2 (en) | Concentrated oxygen recovery method | |
| JP2948402B2 (en) | Recovery method of low concentration sulfur dioxide | |
| JPH0691126A (en) | Method for separating and recording co2 from combustion exhaust gas and device therefor | |
| JP3025653B2 (en) | Improved pressure swing adsorption method | |
| JP3354648B2 (en) | Carbon dioxide separation method | |
| JPH0967104A (en) | Oxygen concentrating method by pressure swing adsorption | |
| JPS61157322A (en) | Separation and concentration of co2 from-containing gas | |
| JPH08301604A (en) | Psa for low-concentration oxygen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A02 | Decision of refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A02 Effective date: 20040302 |