JPH04161225A - Apparatus and method for removing co2 from combustion exhaust gas - Google Patents
Apparatus and method for removing co2 from combustion exhaust gasInfo
- Publication number
- JPH04161225A JPH04161225A JP2285851A JP28585190A JPH04161225A JP H04161225 A JPH04161225 A JP H04161225A JP 2285851 A JP2285851 A JP 2285851A JP 28585190 A JP28585190 A JP 28585190A JP H04161225 A JPH04161225 A JP H04161225A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- combustion exhaust
- mea
- water
- aqueous
- 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.)
- Granted
Links
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000007864 aqueous solution Substances 0.000 claims description 27
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 230000002745 absorbent Effects 0.000 abstract description 7
- 239000002250 absorbent Substances 0.000 abstract description 7
- 238000003915 air pollution Methods 0.000 abstract description 6
- 230000008929 regeneration Effects 0.000 abstract description 4
- 238000011069 regeneration method Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 38
- 239000000567 combustion gas Substances 0.000 description 8
- 238000011049 filling Methods 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 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
- 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)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は燃焼排ガス中のＣＯ２ガスを除去する装置及び
同方法に関し、更に詳しくはアルカノールアミンを吸収
剤として使用する燃焼排ガス中の脱ＣＯ、装置及び方法
に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to an apparatus and method for removing CO2 gas from combustion exhaust gas, and more particularly, to a method for removing CO2 gas from combustion exhaust gas using an alkanolamine as an absorbent. Apparatus and method.
従来、モノエタノールアミンを吸収剤として使用して排
ガス中のＣＯ２ガスを吸収除去する方法が知られている
。この従来方法及び装置の一例を、吸収剤としてモノエ
タノールアミン（以下、ＭＥＡと略称）を用いた場合に
つき第２図によって説明する。Conventionally, a method is known in which monoethanolamine is used as an absorbent to absorb and remove CO2 gas in exhaust gas. An example of this conventional method and apparatus will be explained with reference to FIG. 2 in the case where monoethanolamine (hereinafter abbreviated as MEA) is used as an absorbent.
第２図において、０１は脱ＣＯ２塔、０２は下部充填部
、０３は上部充填部、０４は燃焼排ガス供給口、０５は
脱ＣＯ□燃焼排ガス排出口、０６はＭＥＡ水溶液供給口
、０７は第１ノズル、０８は必要に応じて設けられる液
体留部、０９は水循環ポンプ、０１０は冷却器、０１１
は第２ノズル、０１２はＣＯ２吸収ＭＥＡ水溶液排出口
、０１３は押込ブロワである。In Figure 2, 01 is the CO2 removal tower, 02 is the lower filling section, 03 is the upper filling section, 04 is the combustion exhaust gas supply port, 05 is the CO□ combustion exhaust gas discharge port, 06 is the MEA aqueous solution supply port, and 07 is the 1 nozzle, 08 is a liquid reservoir provided as necessary, 09 is a water circulation pump, 010 is a cooler, 011
is a second nozzle, 012 is a CO2 absorption MEA aqueous solution outlet, and 013 is a forced blower.
燃焼排ガス供給口０４より脱ＣＯ２塔Ｏ１に供給された
燃焼排ガスはＭＥＡ水溶液供給口０６から第１ノズル０
７を経て供給された一定の濃度、温度のＭＥＡ水溶液と
下部充填部０２で向流接触させられ、燃焼排ガス中のＣ
［］、はＭＥＡ水溶液によって吸収除去され、ＣＯｚを
吸収したＭＥＡ水溶液はＣＯ２吸収ＭＥＡ水溶液排出口
０１２により排出され、図示省略のＭＥＡ水溶液再生塔
に送られ、前記のＭＥＡ水溶液供給口０６に循環される
。The combustion exhaust gas supplied to the CO2 removal tower O1 from the combustion exhaust gas supply port 04 is transferred from the MEA aqueous solution supply port 06 to the first nozzle 0.
The C in the combustion exhaust gas is brought into countercurrent contact with the MEA aqueous solution at a constant concentration and temperature supplied through the lower filling part 02.
[ ] is absorbed and removed by the MEA aqueous solution, and the MEA aqueous solution that has absorbed COz is discharged from the CO2 absorption MEA aqueous solution outlet 012, sent to the MEA aqueous solution regeneration tower (not shown), and circulated to the MEA aqueous solution supply port 06. Ru.
一方、下部充填部０２で脱ＣＯ２された燃焼排ガスは液
体留部０８を通って上部充填部０３へと向う。該排ガス
は該排ガスの温度（燃焼排ガスとＭＥＡの吸収反応によ
り発熱し、気液分離後の脱Ｃ［］２燃焼排ガスの温度は
、燃焼排ガス供給口より供給される燃焼排ガス温度より
高くなる）条件に見合う水蒸気を飽和している。この脱
ＣＯ２燃焼排ガスはその温度下でＭＥＡ水溶液のＭＥＡ
蒸気圧分のＭＥＡを含有しているので、そのま＼脱Ｃ［
］２塔０１から脱［”［］２燃焼排ガス排出口０５を経
て系外に放呂するとＭＥＡの損失と共に、周囲の大気を
汚染するおそれがあるため、気液分離後の適当量の凝縮
水を水循環ポンプ０９により冷却器０１０に導き、こ−
で該循環水を冷却して該循環水を第２ノズル０１１より
噴霧し、上昇してくる脱ＣＯ２燃焼排ガスと上部充填部
０３で向流接触させて脱ＣＯ２燃焼排ガスの温度を低下
させると共に、水及びＭＥＡの蒸気を凝縮し、ＭＥＡを
大気中に放散させないようにしている。On the other hand, the combustion exhaust gas from which CO2 has been removed in the lower filling part 02 passes through the liquid storage part 08 and heads to the upper filling part 03. The exhaust gas has a temperature of the exhaust gas (heat is generated due to the absorption reaction between the combustion exhaust gas and MEA, and the temperature of the de-C[]2 combustion exhaust gas after gas-liquid separation is higher than the temperature of the combustion exhaust gas supplied from the combustion exhaust gas supply port). It is saturated with water vapor that meets the conditions. This CO2-depleted combustion exhaust gas is converted into an MEA aqueous solution under that temperature.
Since it contains MEA equivalent to the vapor pressure, it can be directly removed from carbon.
] 2 From the tower 01 [" [] 2 If the flue gas is discharged from the system through the combustion exhaust port 05, there is a risk of loss of MEA and contamination of the surrounding atmosphere. Therefore, an appropriate amount of condensed water after gas-liquid separation is is guided to the cooler 010 by the water circulation pump 09, and this
The circulating water is cooled, the circulating water is sprayed from the second nozzle 011, and brought into countercurrent contact with the rising CO2-depleted combustion exhaust gas in the upper filling part 03 to lower the temperature of the CO2-depleted combustion exhaust gas, Water and MEA vapor are condensed to prevent MEA from escaping into the atmosphere.
上記第２図によって説明した従来の脱ＣＯ２方法及び装
置はそれなりに有用なものであるが、なお脱ＣＯ２塔よ
り系外にもち出される吸収剤であるアルカノールアミン
の量が多く、従って貴重な吸収剤の損失が大きく、かつ
それに伴う大気汚染を発生するという不具合があった。Although the conventional CO2 removal method and device explained in FIG. There was a problem that there was a large loss of agent and the resulting air pollution.
本発明は上記技術水準に鑑み、従来の脱ＣＯ２方法及び
装置に比し、大幅に吸収剤であるアルカノールアミンの
損失量を低減し、それに伴い大気汚染のおそれをなくし
、かつ動力費も節約できる燃焼排ガスの脱ＣＯ２方法及
び装置を提供しようとするものである。In view of the above-mentioned state of the art, the present invention significantly reduces the amount of loss of alkanolamine, which is an absorbent, compared to conventional CO2 removal methods and devices, eliminates the risk of air pollution, and saves power costs. The present invention aims to provide a method and device for removing CO2 from combustion exhaust gas.
本発明は
（１）燃焼排ガスとアルカノールアミン水溶液を接触さ
せ、燃焼排ガス中のＣＯ２を除去する装置において、ア
ルカノールアミン水溶液と燃焼排ガスが向流接触する接
触部の燃焼排ガスの後流側に、ＣＯ２が除去された脱Ｃ
Ｏ２燃焼排ガスと系外から供給された水とが向流接触す
る接触部を設けてなることを特徴とする燃焼排ガスの脱
ＣＯ□装置。The present invention provides (1) an apparatus for removing CO2 from the combustion exhaust gas by bringing the combustion exhaust gas into contact with an alkanolamine aqueous solution, in which CO2 De-C removed
A combustion exhaust gas deCO□ device characterized by being provided with a contact portion where O2 combustion exhaust gas and water supplied from outside the system come into countercurrent contact.
（２）上記（１）の燃焼排ガスの脱ＣＯ２装置において
、脱ＣＯ２燃焼排ガスの温度を、燃焼排ガス供給口より
供給される燃焼排ガスの水飽和状態の温度より高く保ち
、かつ脱ＣＯ２燃焼排ガスに帯同して系外にもち出され
る水蒸気に見合う量の水を水供給口より供給することを
特徴とする燃焼排ガスの脱ＣＯ２方法。(2) In the combustion exhaust gas deCO2 device of (1) above, the temperature of the CO2-depleted flue gas is maintained higher than the water-saturated temperature of the flue gas supplied from the flue gas supply port, and the CO2-depleted flue gas is A method for removing CO2 from combustion exhaust gas, characterized by supplying water from a water supply port in an amount commensurate with the water vapor carried out of the system.
である。It is.
以下、本発明の燃焼排ガスの脱ＣＬ装置及び方法の一態
様を第１図によって説明し、本発明の詳細な説明する。EMBODIMENT OF THE INVENTION Hereinafter, one aspect of the combustion exhaust gas deCLing apparatus and method of the present invention will be explained with reference to FIG. 1, and the present invention will be explained in detail.
第１図において、１は脱ＣＯ２塔、２は下部充填部、３
は上部多段トレイ部、４は燃焼排ガス供給口、５は脱Ｃ
Ｏ２燃焼排ガス排出口、６はＭＥＡ水溶液供給口、７は
ノズル、８は水供給口、９はＣＯ２吸収ＭＥＡ水溶液排
出口、１０は押込ブロワである。In Fig. 1, 1 is a CO2 removal tower, 2 is a lower packing section, and 3 is a CO2 removal column.
is the upper multistage tray section, 4 is the combustion exhaust gas supply port, and 5 is the decarbonization port.
6 is an MEA aqueous solution supply port, 7 is a nozzle, 8 is a water supply port, 9 is a CO2 absorption MEA aqueous solution discharge port, and 10 is a forced blower.
燃焼排ガス供給口４より脱ＣＯ２塔１に供給された燃焼
排ガスはＭＥＡ水溶液供給口６から第１ノズル７を経て
供給された一定濃度、温度のＭＥＡ水溶液と下部充填部
２で向流接触させられ、燃焼排ガス中のＣＯ２はＭＥＡ
水溶液によって吸収除去され、ＣＯ２を吸収したＭＥＡ
水溶液はＣＯ２吸収ＭＥＡ水溶液排出口９により排出さ
れ、図示省略のＭＥＡ水溶液再生塔に送られ、前記ＭＥ
Ａ水溶液供給口６に循環される。（こ＼までの装置及び
方法は第２図に関して述べたこと−同じである。）
下部充填部２で脱ＣＯ２された燃焼排ガスはＭＥＡ蒸気
を帯同して上方に流れ、上部多段トレイ部３に至り、こ
〜で脱ＣＯ２塔１の上部の水供給口８より供給されると
水と向流接触させられる。この時、水供給口８より供給
される水の量は燃焼排ガス中のＣＯ２除去系統より糸外
にもち出される水蒸気に見合った量にすべきである。The combustion exhaust gas supplied to the CO2 removal tower 1 from the combustion exhaust gas supply port 4 is brought into countercurrent contact with the MEA aqueous solution at a constant concentration and temperature supplied from the MEA aqueous solution supply port 6 through the first nozzle 7 in the lower filling section 2. , CO2 in the combustion exhaust gas is MEA
MEA that absorbed and removed CO2 by aqueous solution
The aqueous solution is discharged through the CO2 absorption MEA aqueous solution outlet 9 and sent to an MEA aqueous solution regeneration tower (not shown),
It is circulated to the A aqueous solution supply port 6. (The equipment and method up to this point are the same as those described in connection with FIG. 2.) The combustion exhaust gas, which has been deCO2-eliminated in the lower filling section 2, flows upward accompanied by MEA steam and flows into the upper multi-stage tray section 3. At this point, when the water is supplied from the water supply port 8 at the top of the CO2 removal tower 1, it is brought into countercurrent contact with water. At this time, the amount of water supplied from the water supply port 8 should be commensurate with the water vapor carried out from the CO2 removal system in the combustion exhaust gas.
さもないと脱ＣＯ２塔１及びこれに接続する図示省略の
ＭＥＡ再生塔よりなる系の水バランスが崩れ、ＭＥＡ水
溶液供給口６から脱ＣＯ２塔１の供給するＭＥＡ水溶液
の濃度が一定に保たれないからである。Otherwise, the water balance of the system consisting of the CO2 removal tower 1 and the MEA regeneration tower (not shown) connected thereto will be disrupted, and the concentration of the MEA aqueous solution supplied from the CO2 removal tower 1 from the MEA aqueous solution supply port 6 will not be kept constant. It is from.
この際、系外から供給される水の温度は脱ＣＯ２塔１よ
り排出する脱ＣＯ２燃焼ガスや、脱ＣＯ２塔１を流下す
るＭＥＡ水溶液の温度に殆んど影響を与えない。すなわ
ち、供給される水の温度が脱ＣＯ２燃焼ガスの温度より
低い場合は脱ＣＯ２燃焼ガス中の水蒸気が凝縮すること
になるが、凝縮潜熱の発生と相殺され、脱ＣＯ２塔１よ
り排出する脱ＣＯ２燃焼ガス及び該脱ＣＯ２塔１を流下
するＭＥＡ水溶液の温度に大きく影響を与えることはな
い。また、逆に供給される水の温度が脱 ＣＯ２燃焼ガ
スの温度より高い場合には供給される水は蒸発すること
になるが、蒸発潜熱によって水温は低下するので、この
場合も脱ＣＯ２塔１から排出される脱ＣＯ２燃焼ガス及
び該脱ＣＯ２塔１を流下するＭＥＡ水溶液の温度に大き
く影響を与えることはない。At this time, the temperature of the water supplied from outside the system has almost no effect on the temperature of the CO2-free combustion gas discharged from the CO2-removing tower 1 or the temperature of the MEA aqueous solution flowing down the CO2-removing tower 1. In other words, if the temperature of the supplied water is lower than the temperature of the CO2-depleted combustion gas, the water vapor in the CO2-depleted combustion gas will condense, but this will be offset by the generation of latent heat of condensation, and the This does not significantly affect the temperature of the CO2 combustion gas and the MEA aqueous solution flowing down the CO2 removal tower 1. Conversely, if the temperature of the supplied water is higher than the temperature of the deCO2 combustion gas, the supplied water will evaporate, but the latent heat of vaporization will lower the water temperature, so in this case as well, the CO2 This does not significantly affect the temperature of the CO2-depleted combustion gas discharged from the CO2-depleted combustion gas and the temperature of the MEA aqueous solution flowing down the CO2-depleted tower 1.
上部多段トレイ部３における落下する水と上昇するＭＥ
Ａ蒸気を帯同する脱ＣＯ３燃焼排ガスとの接触により、
トレイ理論段−段につき概略的に脱ＣＯ２燃焼排ガスに
帯同する水蒸気中のＭＥＡ濃度は約２桁以上低減し、ト
レイ段数を適宜選定することによって結果的に脱ＣＯ２
燃焼ガス排出口５から排出される脱ＣＯ２燃焼排ガスに
帯同して系外にもち出されるＭＥＡは殆んど零にするこ
とができる。Falling water and rising ME in the upper multi-stage tray section 3
Due to contact with CO3-free combustion exhaust gas accompanied by A steam,
The MEA concentration in the water vapor accompanying the CO2-depleted combustion exhaust gas is reduced by more than two orders of magnitude for each tray theoretical stage, and by appropriately selecting the number of tray stages, CO2 can be removed as a result.
The amount of MEA carried out of the system along with the CO2-free combustion exhaust gas discharged from the combustion gas outlet 5 can be reduced to almost zero.
上記本発明の一態様によって明らかなように、本発明装
置及び方法によれば損失吸収剤を皆無に近い状態にする
ことができ、従って大気汚染の問題も解消できるばかり
でなく、第２図の従来の装置及び方法に比べると水循環
ポンプの動力が節約でき、かつ冷却器などの機器を省略
できる効果を奏し得る。As is clear from the above-mentioned embodiment of the present invention, according to the apparatus and method of the present invention, it is possible to reduce the amount of loss absorbent to almost no state, and therefore not only can the problem of air pollution be solved, but also the problem of air pollution can be solved. Compared to conventional devices and methods, the power of the water circulation pump can be saved, and equipment such as a cooler can be omitted.
以下、本発明の第１図の実施態様と従来の装置及び方法
を示す第２図の態様とを対比して、本発明の効果を立証
する。Hereinafter, the effects of the present invention will be demonstrated by comparing the embodiment of the present invention shown in FIG. 1 with the embodiment of FIG. 2 showing a conventional apparatus and method.
本発明により、ＣＯ２吸収剤であるアルカノールアミン
の損失が殆んど零になるほど低減され、その結果大気汚
染の問題をも解消できるばかりでなく、従来法に比し動
力の消費量が節減でき、かつ付帯機器を省略することが
できる。According to the present invention, the loss of alkanolamine, which is a CO2 absorbent, is reduced to almost zero, and as a result, not only can the problem of air pollution be solved, but also power consumption can be reduced compared to conventional methods. Moreover, ancillary equipment can be omitted.
第１図は本発明の脱ＣＯ２装置及び方法の一実施態様の
説明図、第２図は従来の脱ＣＯ２装置及び方法の一態様
の説明図である。FIG. 1 is an explanatory diagram of one embodiment of the CO2 removing apparatus and method of the present invention, and FIG. 2 is an explanatory diagram of one embodiment of the conventional CO2 removing apparatus and method.
Claims (1)
せ、燃焼排ガス中のＣＯ＿２を除去する装置において、
アルカノールアミン水溶液と燃焼排ガスが向流接触する
接触部の燃焼排ガスの後流側に、ＣＯ＿２が除去された
脱ＣＯ＿２燃焼排ガスと系外から供給された水とが向流
接触する接触部を設けてなることを特徴とする燃焼排ガ
スの脱ＣＯ＿２装置。（２）請求項（１）の燃焼排ガス
の脱ＣＯ＿２装置において、脱ＣＯ＿２燃焼排ガスの温
度を、燃焼排ガス供給口より供給される燃焼排ガスの水
飽和状態の温度より高く保ち、かつ脱ＣＯ＿２燃焼排ガ
スに帯同して系外にもち出される水蒸気に見合う量の水
を水供給口より供給することを特徴とする燃焼排ガスの
脱ＣＯ＿２方法。(1) In an apparatus that brings combustion exhaust gas into contact with an alkanolamine aqueous solution to remove CO_2 from the combustion exhaust gas,
A contact section is provided on the downstream side of the combustion exhaust gas where the alkanolamine aqueous solution and the combustion exhaust gas come into countercurrent contact with each other, and where the CO_2-depleted combustion exhaust gas from which CO_2 has been removed comes into countercurrent contact with water supplied from outside the system. A combustion exhaust gas CO_2 removal device characterized by: (2) In the combustion exhaust gas deCO_2 apparatus of claim (1), the temperature of the CO_2-depleted combustion exhaust gas is maintained higher than the water-saturated temperature of the combustion exhaust gas supplied from the combustion exhaust gas supply port, and the CO_2-depleted combustion exhaust gas A method for removing CO_2 from combustion exhaust gas, characterized by supplying water from a water supply port in an amount commensurate with the water vapor carried out of the system along with the water vapor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2285851A JPH088976B2 (en) | 1990-10-25 | 1990-10-25 | Removal of CO from combustion exhaust gas (2) Device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2285851A JPH088976B2 (en) | 1990-10-25 | 1990-10-25 | Removal of CO from combustion exhaust gas (2) Device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04161225A true JPH04161225A (en) | 1992-06-04 |
| JPH088976B2 JPH088976B2 (en) | 1996-01-31 |
Family
ID=17696883
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2285851A Expired - Lifetime JPH088976B2 (en) | 1990-10-25 | 1990-10-25 | Removal of CO from combustion exhaust gas (2) Device and method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH088976B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2002034369A1 (en) * | 2000-10-25 | 2002-05-02 | The Kansai Electric Power Co., Inc. | Method and apparatus for recovering amine and system for removing carbon dioxide comprising the apparatus |
| JP2007190553A (en) * | 2007-03-26 | 2007-08-02 | Kansai Electric Power Co Inc:The | Method and apparatus for recovering amine and decarbonator provided with the apparatus |
| JP2010172894A (en) * | 2010-04-05 | 2010-08-12 | Kansai Electric Power Co Inc:The | Method and apparatus for recovering amine and decarbonator provided with the same |
| JP2012520167A (en) * | 2009-03-13 | 2012-09-06 | エイカー クリーン カーボン エーエス | Method and plant for amine emissions control |
-
1990
- 1990-10-25 JP JP2285851A patent/JPH088976B2/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2002034369A1 (en) * | 2000-10-25 | 2002-05-02 | The Kansai Electric Power Co., Inc. | Method and apparatus for recovering amine and system for removing carbon dioxide comprising the apparatus |
| AU772954B2 (en) * | 2000-10-25 | 2004-05-13 | Kansai Electric Power Co., Inc., The | Method and apparatus for recovering amine and system for removing carbon dioxide comprising the apparatus |
| US6784320B2 (en) | 2000-10-25 | 2004-08-31 | The Kansai Electric Power Co., Inc. | Amine recovery method and apparatus and decarbonation apparatus having same |
| US7316737B2 (en) | 2000-10-25 | 2008-01-08 | The Kansai Electric Power Co., Inc. | Amine recovery apparatus and decarbonation apparatus having same |
| JP2007190553A (en) * | 2007-03-26 | 2007-08-02 | Kansai Electric Power Co Inc:The | Method and apparatus for recovering amine and decarbonator provided with the apparatus |
| JP4625478B2 (en) * | 2007-03-26 | 2011-02-02 | 関西電力株式会社 | Amine recovery method and apparatus, and decarbonation apparatus equipped with the same |
| JP2012520167A (en) * | 2009-03-13 | 2012-09-06 | エイカー クリーン カーボン エーエス | Method and plant for amine emissions control |
| US9155990B2 (en) | 2009-03-13 | 2015-10-13 | Aker Clean Carbon As | Method and plant for amine emission control |
| JP2010172894A (en) * | 2010-04-05 | 2010-08-12 | Kansai Electric Power Co Inc:The | Method and apparatus for recovering amine and decarbonator provided with the same |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH088976B2 (en) | 1996-01-31 |
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