JPH088976B2 - Removal of CO from combustion exhaust gas (2) Device and method - Google Patents
Removal of CO from combustion exhaust gas (2) Device and methodInfo
- Publication number
- JPH088976B2 JPH088976B2 JP2285851A JP28585190A JPH088976B2 JP H088976 B2 JPH088976 B2 JP H088976B2 JP 2285851 A JP2285851 A JP 2285851A JP 28585190 A JP28585190 A JP 28585190A JP H088976 B2 JPH088976 B2 JP H088976B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- combustion exhaust
- water
- mea
- supply port
- 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
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)
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CO2装置及び方法に
関する。Description: TECHNICAL FIELD The present invention relates to an apparatus and method for removing CO 2 gas in combustion exhaust gas, and more specifically to deCO 2 in combustion exhaust gas using alkanolamine as an absorbent. 2 Related to 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, there is known a method of absorbing and removing CO 2 gas in exhaust gas by using monoethanolamine as an absorbent. An example of this conventional method and apparatus will be described with reference to FIG. 2 in the case of using monoethanolamine (hereinafter abbreviated as MEA) 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CO2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保留部、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 Fig. 2, 01 is a CO 2 removal tower, 02 is a lower filling section, and 03.
Is an upper filling part, 04 is a combustion exhaust gas supply port, 05 is a de-CO 2 combustion exhaust gas discharge port, 06 is a MEA aqueous solution supply port, 07 is a first nozzle, 08 is a liquid holding part provided as necessary, 09 is water circulation Pump, 010 is cooler, 011 is second nozzle, 012 is CO 2 absorption
MEA aqueous solution outlet, 013 is a push blower.
燃焼排ガス供給口04より脱CO2塔01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07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 from the combustion exhaust gas supply port 04 to the CO 2 removal tower 01 is supplied from the MEA aqueous solution supply port 06 through the first nozzle 07, and has a constant concentration and temperature.
In brought into contact countercurrently, CO 2 in the combustion exhaust gas is absorbed and removed by the aqueous MEA solution, aqueous MEA solution which has absorbed CO 2 is discharged by the CO 2 absorbing aqueous MEA solution outlet 012, not shown MEA
It is sent to the aqueous solution regeneration tower and circulated through the MEA aqueous solution supply port 06.
一方、下部充填部02で脱CO2された燃焼排ガスは液保
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CO2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、そのまゝ脱CO2塔01から脱CO2燃焼排ガ
ス排出口05を経て系外に放出すると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により冷却気010に導
き、こゝで該循環水を冷却して該循環水を第２ノズル01
1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 deCO 2 in the lower filling section 02 goes to the upper filling section 03 through the liquid retaining section 08. The exhaust gas has a temperature of the exhaust gas (heat is generated due to an absorption reaction between the combustion exhaust gas and the MEA, and the temperature of the de-CO 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)
Saturated water vapor that meets the conditions. This de-CO 2 combustion exhaust gas containing a MEA of MEA vapor pressure of MEA aqueous solution under the temperature, releasing the orゝfrom leaving CO 2 tower 01 through the de-CO 2 combustion exhaust gas outlet 05 to the outside of the system Then with the loss of MEA,
Since the surrounding air may be polluted, an appropriate amount of condensed water after gas-liquid separation is guided to the cooling air 010 by the water circulation pump 09, and the circulating water is cooled by this, and the circulating water is supplied to the second nozzle 01.
Sprayed from 1, rises and comes de CO 2 combustion exhaust gas and the upper filling portion 03 is contacted countercurrent with lowering the temperature of the de-CO 2 combustion exhaust gas to condense the vapors of water and MEA, atmospheric an MEA I try not to let it escape.
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 method and apparatus for removing CO 2 described with reference to FIG. 2 are useful as such, the amount of the alkanolamine as the absorbent that is taken out of the CO 2 column to the outside of the system is large, and therefore it is valuable. However, there is a problem in that the loss of the absorbent is large and air pollution is generated.
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 loss amount of the alkanolamine that is the absorbent as compared with the conventional CO 2 removal method and apparatus, thereby eliminating the risk of air pollution and saving the power cost. An object of the present invention is to provide a method and apparatus for removing CO 2 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CO2燃
焼排ガスと系外から供給された水とが向流接触する多段
トレイ形式の接触部を設けてなることを特徴とする燃焼
排ガスの脱CO2装置。The present invention (1) In an apparatus for contacting combustion exhaust gas with an alkanolamine aqueous solution to remove CO 2 in the combustion exhaust gas, in a downstream side of the combustion exhaust gas at a contact portion where the alkanolamine aqueous solution and the combustion exhaust gas come into countercurrent contact, removing CO 2 device flue gas and CO 2 is supplied from the de-CO 2 combustion exhaust gas and the outside of the system that has been removed water is characterized by comprising providing a contact portion of the multi-stage tray format that 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 de CO 2 system of the combustion exhaust gas of the above (1), the temperature of the de-CO 2 combustion exhaust gas, kept higher than the temperature of the water saturation of the combustion exhaust gas supplied from a combustion exhaust gas supply port, and de-CO 2 A method for removing CO 2 from combustion exhaust gas, which comprises supplying from a water supply port an amount of water commensurate with the combustion exhaust gas and flowing out of the system.
である。Is.
以下、本発明の燃焼排ガスの脱CO2装置及び方法の一
態様を第１図によって説明し、本発明の作用を説明す
る。Hereinafter, one mode of the apparatus and method for removing CO 2 from combustion exhaust gas of the present invention will be described with reference to FIG. 1, and the operation of the present invention will be described.
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CO
2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 CO 2 removal tower, 2 is a lower packing section, 3
Is an upper multi-stage tray section, 4 is a combustion exhaust gas supply port, and 5 is CO-free
2 is a combustion exhaust gas discharge port, 6 is a MEA aqueous solution supply port, 7 is a nozzle, 8 is a water supply port, 9 is a CO 2 absorbing 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M
EA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MEA水溶液供給口６に循環され
る。（こゝまでの装置及び方法は第２図に関して述べた
ことゝ同じである。） 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、こゝで
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除去系統より系外にもち出
される水蒸気に見合った量にすべきである。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C
O2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。The combustion exhaust gas supplied from the combustion exhaust gas supply port 4 to the CO 2 removal tower 1 is countercurrently contacted with the MEA aqueous solution having a constant concentration and temperature supplied from the MEA aqueous solution supply port 6 through the first nozzle 7 in the lower filling part 2. is, CO 2 in the combustion exhaust gas is absorbed and removed by the aqueous MEA solution, aqueous MEA solution which has absorbed CO 2 is the CO 2 absorbing M
It is discharged from the EA aqueous solution discharge port 9, sent to a MEA aqueous solution regeneration tower (not shown), and circulated to the MEA aqueous solution supply port 6. (The apparatus and method up to this point are the same as those described with reference to FIG. 2.) The combustion exhaust gas de-CO 2 in the lower filling part 2 flows upward together with MEA vapor, and the upper multi-stage tray part 3 Then, when the water is supplied from the water supply port 8 at the upper part of the CO 2 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 set to an amount commensurate with the water vapor discharged outside the system from the CO 2 removal system in the combustion exhaust gas. Otherwise, the water balance of the system consisting of the CO 2 removal tower 1 and the MEA regeneration tower (not shown) connected to the CO 2 removal tower will be lost, and the CO removal from the MEA solution supply port 6
This is because the concentration of the MEA aqueous solution supplied from the O 2 column 1 cannot be kept constant.
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 is the CO 2 combustion gas discharged from the CO 2 removal tower 1 or the MEA flowing down from the CO 2 removal tower 1.
It has almost no effect on the temperature of the aqueous solution. That is, when the temperature of the water supplied is lower than the temperature of the de-CO 2 combustion gases will be water vapor removal CO 2 combustion gas is condensed, is offset by the generation of latent heat of condensation, from de-CO 2 column 1 Emission of CO 2
It does not significantly affect the temperature of the combustion gas and the MEA aqueous solution flowing down the CO 2 removal column 1 . Although the water temperature of the water supplied to the reverse is supplied is higher than the temperature of the de-CO 2 combustion gases would evaporate, since the water temperature is lowered by latent heat of evaporation, again leaving CO 2 not greatly affect the temperature of the aqueous MEA solution flowing down the de-CO 2 combustion gas and dehydration CO 2 column 1 is discharged from the 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CO2燃焼排ガスとの接触により、トレ
イ理論段一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
By contact with de-CO 2 combustion exhaust gas entrained the A vapor, MEA concentration in water vapor entrained tray theoretical one stage per schematically in de CO 2 combustion exhaust gas is reduced by about 2 orders of magnitude or more, suitably selected tray number As a result, the MEA discharged to the outside of the system together with the de-CO 2 combustion exhaust gas discharged from the de-CO 2 combustion gas discharge port 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 apparent from the above-described one aspect of the present invention, the device and method of the present invention can bring the loss absorbent into a state of almost nothing, and therefore, not only can the problem of air pollution be solved, but also that of FIG. Compared with the conventional device and method, the power of the water circulation pump can be saved, and devices 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 effect of the present invention will be proved by comparing the embodiment of FIG. 1 of the present invention with the embodiment of FIG. 2 showing the conventional apparatus and method.
〔発明の効果〕 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で低減され、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。 [Advantages of the Invention] According to the present invention, the loss of the alkanolamine which is a CO 2 absorbent is reduced to almost zero, and as a result, not only the problem of air pollution can be solved but also compared with the conventional method. Power consumption can be reduced and auxiliary 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 view of one embodiment of a CO 2 removal device and method of the present invention, and FIG. 2 is an illustration of one embodiment of a conventional CO 2 removal device and method.
Claims (2)
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CO2燃焼排ガスと系外から供給された水とが向流接触
する多段トレイ形式の接触部を設けてなることを特徴と
する燃焼排ガスの脱CO2装置。1. A device for contacting flue gas with an aqueous alkanolamine solution to remove CO 2 in the flue gas, wherein CO 2 is provided at the contact point of the flue gas with which the alkanolamine aqueous solution comes into countercurrent contact, 2 is a leaving CO 2 device flue gas, characterized in that the water supplied is provided with a contact portion of the multi-stage tray format countercurrent contact from de CO 2 combustion exhaust gas and the outside of the system that has been removed.
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. The apparatus for removing CO 2 from combustion exhaust gas according to claim 1, wherein the temperature of the exhaust gas from CO 2 removal is kept higher than the temperature of the water saturation state of the combustion exhaust gas supplied from the combustion exhaust gas supply port, and de CO 2 process flue gas to the amount of water to meet the water vapor out have out of the system and entrained in de CO 2 combustion exhaust gas and supplying from the water supply port.
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 JPH04161225A (en) | 1992-06-04 |
| JPH088976B2 true 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) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3969949B2 (en) | 2000-10-25 | 2007-09-05 | 関西電力株式会社 | Amine recovery method and apparatus, and decarbonation gas apparatus provided with the same |
| 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 |
| NO332812B1 (en) | 2009-03-13 | 2013-01-21 | Aker Clean Carbon As | Amine emission control |
| JP5185970B2 (en) * | 2010-04-05 | 2013-04-17 | 関西電力株式会社 | Amine recovery method and apparatus, and decarbonation apparatus equipped with the same |
-
1990
- 1990-10-25 JP JP2285851A patent/JPH088976B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH04161225A (en) | 1992-06-04 |
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