JPH0751537A - Removal of co2 in co2-containing gas - Google Patents
Removal of co2 in co2-containing gasInfo
- Publication number
- JPH0751537A JPH0751537A JP5162078A JP16207893A JPH0751537A JP H0751537 A JPH0751537 A JP H0751537A JP 5162078 A JP5162078 A JP 5162078A JP 16207893 A JP16207893 A JP 16207893A JP H0751537 A JPH0751537 A JP H0751537A
- Authority
- JP
- Japan
- Prior art keywords
- steam
- containing gas
- regeneration
- regeneration tower
- tower
- 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)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は燃焼排ガスなどのＣＯ2
含有ガス中に含まれるＣＯ2 を除去する方法に関し、さ
らに詳しくは、エネルギ効率の改善されたＣＯ2 含有ガ
ス中のＣＯ2を除去する方法に関する。FIELD OF THE INVENTION The present invention relates to CO 2 such as combustion exhaust gas.
It relates to a method of removing CO 2 contained in containing gas, more particularly, to a method for removing CO 2 in the CO 2 containing gas having improved energy efficiency.
【０００２】[0002]
【従来の技術】近年、地球の温暖化現象の原因の一つと
して、ＣＯ2 による温室効果が指摘され、地球環境を守
る上で国際的にもその対策が急務となってきた。ＣＯ2
の発生源としては化石燃料を燃焼させるあらゆる人間の
活動分野に及び、その排出抑制への要求が一層強まる傾
向にある。これに伴い大量の化石燃料を使用する火力発
電所などの動力発生設備を対象に、ボイラの燃焼排ガス
をアミン系ＣＯ2 吸収液と接触させ、燃焼排ガス中のＣ
Ｏ2 を除去、回収する方法及び回収されたＣＯ2を大気
へ放出することなく貯蔵する方法が精力的に研究されて
いる。また前記のようなＣＯ2 吸収液を用い、燃焼排ガ
スからＣＯ2 を除去・回収する工程としては、吸収塔に
おいて燃焼排ガスとＣＯ2 吸収液とを接触させる工程、
ＣＯ2 を吸収した吸収液を再生塔において加熱し、ＣＯ
2 を遊離させると共に吸収液を再生して再び吸収塔に循
環して再使用するものが採用されている。2. Description of the Related Art In recent years, the greenhouse effect of CO 2 has been pointed out as one of the causes of the global warming phenomenon, and countermeasures against it have become urgent internationally in order to protect the global environment. CO 2
The sources of methane are all human activity fields that burn fossil fuels, and the demand for emission control tends to become stronger. Along with this, targeting power generation facilities such as thermal power plants that use a large amount of fossil fuels, the combustion exhaust gas of the boiler is brought into contact with the amine-based CO 2 absorbing liquid to generate C in the combustion exhaust gas.
A method for removing and recovering O 2 and a method for storing the recovered CO 2 without being released to the atmosphere have been vigorously studied. Further, as the step of removing and recovering CO 2 from the combustion exhaust gas using the CO 2 absorption liquid as described above, a step of contacting the combustion exhaust gas with the CO 2 absorption liquid in an absorption tower,
The absorption liquid that has absorbed CO 2 is heated in the regeneration tower to
It is adopted that 2 is released, the absorption liquid is regenerated, and is recycled to the absorption tower for reuse.
【０００３】[0003]
【発明が解決しようとする課題】前記ＣＯ2 吸収液及び
工程を用いて燃焼排ガスのようなＣＯ2 含有ガスからＣ
Ｏ2 を吸収除去・回収する方法においては、これらの工
程は燃焼設備に付加して設置されるため、その操業費用
もできるだけ低減させなければならない。特に前記工程
の内、再生工程は多量の熱エネルギを消費するので、可
能な限り省エネルギープロセスとする必要がある。By using the CO 2 absorbing solution and process described above, a C 2 -containing gas such as a combustion exhaust gas can be obtained.
In the method of absorbing / removing / recovering O 2 , these steps are installed in addition to the combustion equipment, and therefore the operating cost thereof must be reduced as much as possible. Particularly, of the above steps, the regeneration step consumes a large amount of heat energy, and therefore it is necessary to use an energy saving process as much as possible.
【０００４】[0004]
【課題を解決するための手段】本発明者らは前記課題に
鑑み、ＣＯ2 吸収液を再生塔にて再生させる工程におい
て省エネルギ工程を検討した結果、再生塔のリボイラで
使用された廃スチームを再利用することにより、エネル
ギ効率を一層向上させたＣＯ2 吸収プロセスとなるとの
知見を得て、本発明を完成させた。In view of the above problems, the present inventors have studied an energy-saving process in the step of regenerating a CO 2 absorbing solution in a regeneration tower, and as a result, found that the waste steam used in the reboiler of the regeneration tower. The present invention has been completed based on the knowledge that a CO 2 absorption process with further improved energy efficiency can be obtained by reusing.
【０００５】すなわち本発明は吸収塔によりＣＯ2 含有
ガスとＣＯ2 吸収液とを接触させてＣＯ2 含有ガス中の
ＣＯ2 をＣＯ2 吸収液に吸収させ、次いでＣＯ2 吸収液
を再生塔に導き、再生塔塔底のＣＯ2 吸収液を再生加熱
器を用いて加熱することによりＣＯ2 を遊離させると共
にＣＯ2 吸収液を再生し、再生したＣＯ2 吸収液を吸収
塔に循環し再使用することからなるＣＯ2 含有ガス中の
ＣＯ2 を除去する方法において、前記再生加熱器の加熱
熱源として使用したスチームをフラッシュドラムに導い
てフラッシュさせ、発生した低温スチームを再生塔の塔
底に供給することを特徴とするＣＯ2 含有ガス中のＣＯ
2 を除去する方法である。また本発明は前記ＣＯ2 含有
ガスが燃焼排ガスであることを特徴とするＣＯ2 含有ガ
ス中のＣＯ2 を除去する方法である。以下、本発明を詳
しく説明する。[0005] The present invention is absorbed by contacting the CO 2 containing gas and CO 2 absorbing solution of CO 2 CO 2 containing gas to the CO 2 absorbing solution by absorption column, then the CO 2 absorbing solution in the regeneration tower lead, reproduces the CO 2 absorbing solution with liberating CO 2 by heating with a regeneration heater of CO 2 absorbing solution regeneration tower bottoms, circulated and reused in the absorption tower the CO 2 absorbing solution regenerated In the method for removing CO 2 in a CO 2 -containing gas, the steam used as a heating heat source of the regeneration heater is introduced into a flash drum to be flashed, and the generated low temperature steam is supplied to the bottom of the regeneration tower. CO in a CO 2 -containing gas characterized by
It is a method of removing 2 . The present invention is also a method for removing CO 2 from a CO 2 -containing gas, wherein the CO 2 -containing gas is combustion exhaust gas. Hereinafter, the present invention will be described in detail.
【０００６】[0006]
【作用】本発明が適用されるＣＯ2 含有ガスとしては、
ＣＯ2 を含むものであれば特に限定されないが、以下燃
焼排ガス中のＣＯ2 を除去する場合を例として説明す
る。本発明により燃焼排ガス中のＣＯ2 を除去する際に
採用できるプロセスは限定するものではないが、典型例
を図１によって説明する。図１では主要設備のみ示し付
属設備は省略した。As the CO 2 -containing gas to which the present invention is applied,
There is no particular limitation as long as it contains CO 2 , but the case of removing CO 2 in the combustion exhaust gas will be described below as an example. Although the process that can be used to remove CO 2 in the combustion exhaust gas according to the present invention is not limited, a typical example will be described with reference to FIG. 1. In FIG. 1, only the main equipment is shown and the auxiliary equipment is omitted.
【０００７】図１において、１はＣＯ2 吸収塔、２は下
部充填部、３は上部充填部またはトレイ、４はＣＯ2 吸
収塔燃焼排ガス供給口、５はＣＯ2 吸収塔燃焼排ガス排
出口、６は吸収液供給口、７，７′はノズル、８は必要
に応じて設けられる燃焼排ガス冷却器、９はノズル、１
０は充填部、１１は加湿冷却水循環ポンプ、１２は補給
水供給ライン、１３はＣＯ2 を吸収した吸収液排出ポン
プ、１４は熱交換器、１５は再生塔、１６はノズル、１
７は下部充填部、１８は再生加熱器（リボイラ）、１９
は上部充填部、２０は還流水ポンプ、２１はＣＯ2 分離
器、２２は回収ＣＯ2 排出ライン、２３は再生塔還流冷
却器、２４はノズル、２５は再生塔還流水供給ライン、
２６は燃焼排ガス供給ブロア、２７は必要に応じて設け
られる冷却器、２８は再生塔還流水供給口、２９はスチ
ーム供給ライン、３０はフラッシュバルブ、３１はフラ
ッシュドラム、３２は低温スチーム供給ライン、３３は
凝縮水排出ラインである。In FIG. 1, 1 is a CO 2 absorption tower, 2 is a lower packing part, 3 is an upper packing part or tray, 4 is a CO 2 absorption tower combustion exhaust gas supply port, 5 is a CO 2 absorption tower combustion exhaust gas discharge port, 6 is an absorption liquid supply port, 7 and 7'is a nozzle, 8 is a combustion exhaust gas cooler provided as needed, 9 is a nozzle, 1
0 is a filling part, 11 is a humidification cooling water circulation pump, 12 is a makeup water supply line, 13 is an absorption liquid discharge pump absorbing CO 2 , 14 is a heat exchanger, 15 is a regeneration tower, 16 is a nozzle, 1
7 is a lower filling part, 18 is a regenerative heater (reboiler), 19
Is an upper filling part, 20 is a reflux water pump, 21 is a CO 2 separator, 22 is a recovered CO 2 discharge line, 23 is a regenerator reflux condenser, 24 is a nozzle, 25 is a regenerator reflux water supply line,
26 is a combustion exhaust gas supply blower, 27 is a cooler provided as needed, 28 is a regeneration tower reflux water supply port, 29 is a steam supply line, 30 is a flash valve, 31 is a flash drum, 32 is a low temperature steam supply line, 33 is a condensed water discharge line.
【０００８】図１において、燃焼排ガスは燃焼排ガス供
給ブロア２６により燃焼排ガス冷却器８に供給され、ノ
ズル９からの加湿冷却水と充填部１０で接触して加湿冷
却され、ＣＯ2 吸収塔燃焼排ガス供給口４を通ってＣＯ
2 吸収塔１へ導かれる。燃焼排ガスと接触した加湿冷却
水は燃焼排ガス冷却器８の下部に溜り、ポンプ１１によ
りノズル９へ循環使用される。加湿冷却水は燃焼排ガス
を加湿冷却することにより徐々に失われるので、補給水
供給ライン１２により補充される。In FIG. 1, the combustion exhaust gas is supplied to a combustion exhaust gas cooler 8 by a combustion exhaust gas supply blower 26, and is brought into contact with humidification cooling water from a nozzle 9 at a filling portion 10 to be humidified and cooled, and CO 2 absorption tower combustion exhaust gas CO through the supply port 4
2 Guided to absorption tower 1. The humidified cooling water that has come into contact with the combustion exhaust gas collects in the lower part of the combustion exhaust gas cooler 8 and is circulated to the nozzle 9 by the pump 11. Since the humidified cooling water is gradually lost by humidifying and cooling the combustion exhaust gas, it is replenished by the makeup water supply line 12.
【０００９】ＣＯ2 吸収塔１に供給された燃焼排ガスは
吸収液供給口６を経てノズル７から供給される所定濃度
の吸収液と下部充填部２で向流接触させられ、燃焼排ガ
ス中のＣＯ2 は吸収液により吸収除去され、ＣＯ2 が吸
収除去された残りの燃焼排ガスは上部充填部３へと向
う。ＣＯ2 吸収塔１に供給される吸収液はＣＯ2 を吸収
し、その吸収による反応熱のため通常供給口６における
温度よりも高温となり、ＣＯ2 を吸収した吸収液排出ポ
ンプ１３により熱交換器１４に送られ、加熱されて再生
塔１５へ導かれる。The combustion exhaust gas supplied to the CO 2 absorption tower 1 is countercurrently contacted with the absorption liquid of a predetermined concentration supplied from the nozzle 7 through the absorption liquid supply port 6 in the lower filling section 2 to remove CO in the combustion exhaust gas. 2 is absorbed and removed by the absorption liquid, and the remaining combustion exhaust gas from which CO 2 has been absorbed and removed goes to the upper filling portion 3. Absorbing liquid supplied to the CO 2 absorber 1 absorbs CO 2, heated to a high temperature than the temperature in the normal supply port 6 for reaction heat by the absorption heat exchanger by absorbing solution discharge pump 13 that has absorbed CO 2 It is sent to 14, heated, and guided to the regeneration tower 15.
【００１０】再生塔１５では、再生加熱器１８による加
熱で吸収液が再生され、熱交換器１４および必要に応じ
て設けられた冷却器２７により冷却されてＣＯ2 吸収塔
１へ戻される。再生塔１５の上部において、吸収液から
分離されたＣＯ2 はノズル２４より供給される還流水と
接触し、再生塔還流冷却器２３により冷却され、ＣＯ 2
分離器２１にてＣＯ2 に同伴した水蒸気が凝縮した還流
水と分離され、回収ＣＯ2 排出ライン２２より系外へ送
出される。還流水の一部は還流水ポンプ２０で再生塔１
５へ還流され、一部は再生塔還流水供給口２８を経てノ
ズル７′よりＣＯ2 吸収塔１へ供給される。In the regeneration tower 15, heating by the regeneration heater 18 is applied.
The heat regenerates the absorption liquid, and the heat exchanger 14 and, if necessary,
CO is cooled by the cooler 272Absorption tower
Returned to 1. In the upper part of the regeneration tower 15,
CO separated2Is the reflux water supplied from the nozzle 24
Contacted, cooled by the regenerator reflux condenser 23, 2
CO in the separator 212Reflux with condensed water vapor
CO separated from water and recovered CO2Send from the discharge line 22 to outside the system
Will be issued. A part of the reflux water is recycled by the reflux water pump 20 to the regeneration tower 1
5, and part of it is fed through the regeneration tower reflux water supply port 28 to
CO from cheat 7 '2It is supplied to the absorption tower 1.
【００１１】本発明で使用できるＣＯ2 吸収液としては
限定的ではないが、アルカノールアミンやアルコール性
水酸基を有するヒンダードアミン類を例示することがで
きる。このようなアルカノールアミンとしてはモノエタ
ノールアミン、ジエタノールアミン、トリエタノールア
ミン、メチルジエタノールアミン、ジイソプロパノール
アミン、ジグリコールアミンなどを例示することができ
るが、通常モノエタノールアミン（ＭＥＡ）が好んで用
いられる。またアルコール性水酸基を有するヒンダード
アミンとしては２−アミノ−２−メチル−１−プロパノ
ール（ＡＭＰ）、２−（エチルアミノ）−エタノール
（ＥＡＥ）、２−（メチルアミノ）−エタノール（ＭＡ
Ｅ）、２−（ジエチルアミノ）−エタノール（ＤＥＡ
Ｅ）などを例示できる。The CO 2 absorbent that can be used in the present invention is not limited, and examples thereof include alkanolamines and hindered amines having an alcoholic hydroxyl group. Examples of such alkanolamines include monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diisopropanolamine, and diglycolamine, but monoethanolamine (MEA) is usually preferred. As hindered amines having an alcoholic hydroxyl group, 2-amino-2-methyl-1-propanol (AMP), 2- (ethylamino) -ethanol (EAE), 2- (methylamino) -ethanol (MA
E), 2- (diethylamino) -ethanol (DEA
E) etc. can be illustrated.
【００１２】本発明の特徴は再生塔１５の再生加熱器１
８の加熱熱源として使用されたスチームをフラッシュド
ラム３１に導いてフラッシュさせ、発生した低温スチー
ムを再生塔１５の塔底に供給することにある。すなわ
ち、吸収液の再生のために再生加熱器１８の熱源として
スチーム供給ライン２９により供給されるスチームは、
再生加熱器１８で加熱に使用されて凝縮水となり、フラ
ッシュバルブ（またはスチームトラップ）３０により、
再生加熱器１８内の加熱温度を一定に保つように制御さ
れてフラッシュドラム３１に排出される。フラッシュド
ラム３１は供給凝縮水よりも低圧に制御されているので
一部がスチームとなる。排出されたスチームはフラッシ
ュドラム３１の下部に凝縮水を分離し、上部から低温ス
チーム供給ライン３２により再生塔１５の塔底部に供給
される。この低温スチームはスチーム供給ライン２９に
より再生加熱器１８に供給されるスチームよりも低温で
はあるが、再生加熱器１８により加熱された塔底吸収液
と同温度またはそれよりも高温に設定することができ
る。The feature of the present invention is that the regeneration heater 1 of the regeneration tower 15 is used.
The steam used as the heating heat source of No. 8 is guided to the flash drum 31 to be flashed, and the generated low temperature steam is supplied to the bottom of the regeneration tower 15. That is, the steam supplied by the steam supply line 29 as the heat source of the regenerative heater 18 for regenerating the absorbing liquid is
It is used for heating in the regenerative heater 18 to become condensed water, and by the flash valve (or steam trap) 30,
It is discharged to the flash drum 31 while being controlled to keep the heating temperature in the regenerative heater 18 constant. Since the flash drum 31 is controlled to have a pressure lower than that of the condensed water supplied, part of the flash drum 31 becomes steam. The discharged steam separates condensed water in the lower part of the flash drum 31, and is supplied from the upper part to the tower bottom of the regeneration tower 15 by the low temperature steam supply line 32. This low-temperature steam is lower in temperature than the steam supplied to the regenerator 18 by the steam supply line 29, but may be set to the same temperature as or higher than the temperature of the bottom absorption liquid heated by the regenerator 18. it can.
【００１３】なお、本発明により再生塔１５の塔底に低
温スチームが供給される結果、系内の水バランスが変化
する。すなわちＣＯ2 吸収塔１及び再生塔１５を循環す
る水量が増加する。従って、その増加分は例えばＣＯ2
分離器２１から還流される還流水を系外へ排出すること
により、あるいはＣＯ2 吸収塔燃焼排ガス排出口５から
多量に排出されるガスの温度を僅かに上昇させることに
より、容易に調節できるので特に問題とはならない。本
発明を採用することにより、再生加熱器１８の加熱に使
用された後に、スチームが有する残余の熱エネルギを有
効に活用することができることとなった。As a result of the low temperature steam being supplied to the bottom of the regeneration tower 15 according to the present invention, the water balance in the system changes. That is, the amount of water circulating in the CO 2 absorption tower 1 and the regeneration tower 15 increases. Therefore, the increase is, for example, CO 2
It can be easily adjusted by discharging the reflux water refluxed from the separator 21 to the outside of the system, or by slightly raising the temperature of the gas discharged in large quantities from the CO 2 absorption tower combustion exhaust gas discharge port 5. There is no particular problem. By adopting the present invention, it is possible to effectively utilize the residual heat energy of steam after being used for heating the regenerative heater 18.
【００１４】[0014]
【実施例】比較例として、図１に示すＣＯ2 の吸収及び
再生工程において、低温スチーム供給ライン３２を使用
しないで、３０重量％ＭＥＡ水溶液を用いて燃焼排ガス
からのＣＯ2 回収を行った。燃焼排ガスの処理量は３
６，５００Ｎｍ3 ／Ｈ、定常時における再生加熱器１８
への２．４ｋｇ／ｃｍ2 Ｇスチーム（高温スチーム）の
供給量は１１．１５Ｔ／Ｈであり、フラッシュバルブ３
０から排出されるスチームは全量大気中に廃棄した。EXAMPLES As a comparative example, in the CO 2 absorption and regeneration step shown in FIG. 1, CO 2 was recovered from combustion exhaust gas using a 30 wt% MEA aqueous solution without using the low temperature steam supply line 32. Processing amount of combustion exhaust gas is 3
6,500 Nm 3 / H, regeneration heater 18 in steady state
The amount of 2.4 kg / cm 2 G steam (high temperature steam) supplied to the flash valve 3 is 11.15 T / H.
All the steam discharged from 0 was discarded in the atmosphere.
【００１５】実施例として、低温スチーム供給ライン３
２を使用し、フラッシュドラム３１で発生した１１８℃
（約０．８５ｋｇ／ｃｍ2 Ｇ）のスチームを流量０．３
８Ｔ／Ｈで再生塔１５塔底に供給した。これにより、再
生加熱器１８への高温スチームの供給必要量は約１０．
８Ｔ／Ｈとなり、再生塔塔底に供給した低温スチーム量
に相当する高温スチームの節減が達成された。As an example, the low temperature steam supply line 3
No. 2 used, 118 ° C. generated by flash drum 31
(About 0.85 kg / cm 2 G) steam flow rate 0.3
It was supplied to the bottom of the regeneration tower 15 at 8 T / H. As a result, the required supply amount of high temperature steam to the regenerative heater 18 is about 10.
It became 8 T / H, and reduction of high temperature steam corresponding to the amount of low temperature steam supplied to the bottom of the regeneration tower was achieved.
【００１６】[0016]
【発明の効果】以上詳細に述べたごとく、本発明により
前記低温スチームを再生塔塔底に供給するという工夫に
より、ＣＯ2 含有ガスからＣＯ2 を除去する方法におい
て、省エネルギを達成することができた。As described in detail above, energy saving can be achieved in the method of removing CO 2 from the CO 2 -containing gas by the invention of supplying the low temperature steam to the bottom of the regeneration tower according to the present invention. did it.
【図１】本発明で採用できる工程の一例の説明図。FIG. 1 is an explanatory diagram of an example of a process that can be adopted in the present invention.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 須藤 晋平 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 (72)発明者 岡部 明 東京都新宿区富久町15番１号 菱和エンジ ニアリング株式会社内 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Shinpei Sudo, Shinhei Sudo Marunouchi 2-5-1-5, Chiyoda-ku, Tokyo Sanryo Heavy Industries Co., Ltd. (72) Inventor Akira Okabe 15-1 Fukucho, Shinjuku-ku, Tokyo Ryohei Wa Engineering Co., Ltd.
Claims (2)
収液とを接触させてＣＯ2 含有ガス中のＣＯ2 をＣＯ2
吸収液に吸収させ、次いでＣＯ2 吸収液を再生塔に導
き、再生塔塔底のＣＯ2 吸収液を再生加熱器を用いて加
熱することによりＣＯ2 を遊離させると共にＣＯ2 吸収
液を再生し、再生したＣＯ2 吸収液を吸収塔に循環し再
使用することからなるＣＯ2 含有ガス中のＣＯ2 を除去
する方法において、前記再生加熱器の加熱熱源として使
用したスチームをフラッシュドラムに導いてフラッシュ
させ、発生した低温スチームを再生塔の塔底に供給する
ことを特徴とするＣＯ2 含有ガス中のＣＯ2 を除去する
方法。1. A CO 2 contained by absorption column is contacted with a CO 2 containing gas and the CO 2 absorbing liquid CO 2 containing gas CO 2
Is absorbed into the absorbing solution, then leads to the CO 2 absorbing liquid to the regenerator, reproduces the CO 2 absorbing solution with liberating CO 2 by heating with a regeneration heater of CO 2 absorbing solution regeneration tower bottoms a method of removing CO 2 in the CO 2 containing gas which comprises reused circulated to the absorption tower the CO 2 absorbing solution regenerated, direct the steam used as a heating heat source for the regeneration heater to a flash drum A method for removing CO 2 in a CO 2 -containing gas, which comprises flushing and supplying the generated low temperature steam to the bottom of a regeneration tower.
を特徴とする請求項１記載のＣＯ2 含有ガス中のＣＯ2
を除去する方法。Wherein CO 2 containing gas, characterized in that a flue gas according to claim 1 in CO 2 containing gas according CO 2
How to remove.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5162078A JPH0751537A (en) | 1993-06-30 | 1993-06-30 | Removal of co2 in co2-containing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5162078A JPH0751537A (en) | 1993-06-30 | 1993-06-30 | Removal of co2 in co2-containing gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0751537A true JPH0751537A (en) | 1995-02-28 |
Family
ID=15747672
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5162078A Pending JPH0751537A (en) | 1993-06-30 | 1993-06-30 | Removal of co2 in co2-containing gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0751537A (en) |
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