JPH05231A - Removal of co2 from combustion exhaust gas - Google Patents
Removal of co2 from combustion exhaust gasInfo
- Publication number
- JPH05231A JPH05231A JP3018675A JP1867591A JPH05231A JP H05231 A JPH05231 A JP H05231A JP 3018675 A JP3018675 A JP 3018675A JP 1867591 A JP1867591 A JP 1867591A JP H05231 A JPH05231 A JP H05231A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- removal
- gas
- combustion exhaust
- wet desulfurization
- 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)
Abstract
(57)【要約】
【目的】 燃焼排ガスから直接CO2 を除去する際のCO2
吸収液、吸着剤の劣化とCO2 分離効率の低下を防止す
る。
【構成】 燃焼排ガスからCO2 を除去する方法におい
て、この排ガスを湿式脱硫処理した後にCO2 を除去す
る。
【効果】 CO2 除去に先立って湿式脱硫処理するので、
燃焼排ガス中の粉塵、SOx 等が減少し、CO2 吸収液や吸
着剤の劣化とCO2 除去効率の低下を防止できる。
(57) [Summary] [Purpose] CO 2 when directly removing CO 2 from flue gas
Prevents deterioration of absorption liquid and adsorbent and reduction of CO 2 separation efficiency. [Configuration] In the method for removing CO 2 from the flue gas to remove CO 2 to the exhaust gas after wet desulfurization process. [Effects] Wet desulfurization treatment prior to CO 2 removal
Dust, SOx, etc. in the combustion exhaust gas are reduced, and deterioration of the CO 2 absorbing liquid and adsorbent and reduction of CO 2 removal efficiency can be prevented.
Description
【０００１】[0001]
【産業上の利用分野】本発明は火力発電所等の燃焼排ガ
ス中のCO2 除去方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of removing CO 2 in combustion exhaust gas from thermal power plants and the like.
【０００２】[0002]
【従来の技術】従来、鉄鋼、石油化学分野において、圧
力変動吸脱着法、温度変動吸脱着法やアミン吸収法など
のCO2 除去方法が用いられていた。しかしながら、化石
燃料の燃焼排ガスからCO2 を除去する方法については、
後述するように排ガス中の不純物、排ガス温度など多く
の問題点が未解決のままであり、したがって、燃焼排ガ
スに適用可能なCO2 除去方法は見いだされていないのが
現状である。2. Description of the Related Art Conventionally, CO 2 removal methods such as pressure fluctuation adsorption / desorption method, temperature fluctuation adsorption / desorption method and amine absorption method have been used in the fields of steel and petrochemistry. However, regarding the method of removing CO 2 from the combustion exhaust gas of fossil fuel,
As will be described later, many problems such as impurities in exhaust gas and exhaust gas temperature remain unsolved, and therefore, the present situation is that no CO 2 removal method applicable to combustion exhaust gas has been found.
【０００３】[0003]
【発明が解決しようとする課題】燃焼排ガスから直接CO
2 を除去すると、排ガス中の煤塵、SOx 、NOx 、等有害
物質のためにCO2 吸収液、吸着剤の劣化が早いばかりで
なく、分離されたCO2 の純度も低下する。また、CO2 分
離される排ガスの温度が高いとCO2 の吸収効率が低下す
る。更に、従来のCO2 分離方法は、上記有害物質を含む
ガスを処理する場合には、建設費、運転費とも高価であ
り、効率的な燃焼排ガスからのCO2 除去方法が強く求め
られている。[Problems to be solved by the invention] CO directly from combustion exhaust gas
When 2 is removed, not only the CO 2 absorbent and the adsorbent are deteriorated quickly due to harmful substances such as soot, SOx and NOx in the exhaust gas, but also the purity of the separated CO 2 is lowered. Further, if the temperature of the exhaust gas from which CO 2 is separated is high, the CO 2 absorption efficiency decreases. Furthermore, the conventional CO 2 separation method is expensive in terms of construction cost and operation cost when treating a gas containing the above-mentioned harmful substances, and an efficient CO 2 removal method from combustion exhaust gas is strongly demanded. ..
【０００４】本発明はかかる従来の欠点を解消しCO2 吸
収液の劣化とCO2 除去効率の低下を防止できる燃焼排ガ
ス中のCO2 除去方法を提供することを目的とするもので
ある。An object of the present invention is to provide a method for removing CO 2 in combustion exhaust gas, which can solve the above-mentioned conventional drawbacks and prevent the deterioration of the CO 2 absorbent and the decrease in CO 2 removal efficiency.
【０００５】[0005]
【課題を解決するための手段】上記目的を達成する本発
明は、燃焼排ガスからCO2 を除去する方法において、該
排ガスを湿式脱硫処理し、次いで該脱硫処理をした排ガ
スからCO2 を除去した後に該CO2 を除去した排ガス中の
有害物質の除去処理を行なうことを特徴とするものであ
る。Means for Solving the Problems The present invention, which achieves the above object, is a method for removing CO 2 from combustion exhaust gas, wherein the exhaust gas is subjected to wet desulfurization treatment, and then CO 2 is removed from the exhaust gas subjected to the desulfurization treatment. After that, a treatment for removing harmful substances in the exhaust gas from which the CO 2 has been removed is performed.
【０００６】以下本発明を図１にもとづき説明する。燃
焼排ガスＧをガスガスヒーター (以下、ＧＧＨと略記)
１に供給し、本発明の方法で処理された排ガスＧ３との
熱交換により冷却した後に、湿式脱硫工程２において湿
式脱処をし、SOx 、煤塵を除去する。本発明の方法にお
いて被処理対象となる燃焼排ガスＧは、如何なる種類の
ものであっても良いが、特に本発明の方法は化石燃料排
ガスに対して効果的である。The present invention will be described below with reference to FIG. Combustion exhaust gas G is a gas gas heater (hereinafter abbreviated as GGH)
After being supplied to No. 1 and cooled by heat exchange with the exhaust gas G3 treated by the method of the present invention, it is subjected to wet desulfurization in the wet desulfurization step 2 to remove SOx and dust. The combustion exhaust gas G to be treated in the method of the present invention may be of any type, but the method of the present invention is particularly effective for fossil fuel exhaust gas.
【０００７】また、本発明の方法において採用される湿
式脱硫法としては、既存の全ての湿式脱硫方法を採用す
ることができるが、ガスバブリング方法（たとえば、特
公昭58-43140号）が好ましく、SO2、煤塵を効果的に分
離できる。湿式脱硫工程で使用する吸収剤としては、Ca
CO3, Ca(OH)2, NaOH, Na2CO3, Mg(OH)2 などのCa, Na,M
gのアルカリ性物質を使用できる。As the wet desulfurization method used in the method of the present invention, all existing wet desulfurization methods can be adopted, but the gas bubbling method (for example, Japanese Patent Publication No. 58-43140) is preferable, SO 2 and soot and dust can be effectively separated. As the absorbent used in the wet desulfurization process, Ca
CO 3 , Ca (OH) 2 , NaOH, Na 2 CO 3 , Mg (OH) 2 etc.Ca, Na, M
g alkaline material can be used.
【０００８】この湿式脱硫処理によって、排ガス中のSO
x 濃度を湿式脱硫処理前の燃焼排ガスでは250ppm以上で
あるのを、150ppm以下、好ましくは80ppm 以下に低下さ
せることができる。さらに、煤塵濃度は、燃焼排ガスＧ
では、 200mg／Nm3-dry以上であるのに対して、10mg／N
m3-dry以下、好ましくは５mg／Nm3-dry以下に低下させ
ることができる。By this wet desulfurization treatment, SO in exhaust gas is
The x concentration in the flue gas before wet desulfurization treatment can be reduced from 250 ppm or more to 150 ppm or less, preferably 80 ppm or less. Furthermore, the dust concentration is the combustion exhaust gas G
Is more than 200mg / Nm 3 -dry, while 10mg / N
It can be reduced to m 3 -dry or less, preferably 5 mg / Nm 3 -dry or less.
【０００９】次に本発明の方法においては、脱硫処理を
した排ガスＧ１を排ガスファン３により昇圧してCO2 除
去工程４に送る。CO2 除去工程４の入口ガスＧ１は、燃
焼排ガス温度は 100℃以上であるのに対して、65℃以
下、好ましくは55℃以下である。ガス温度は、たとえば
空冷の冷却器による循環、冷却水との気液接触によっ
て、簡易に低下させることができることから、ガス冷却
部をCO2 分離の前段に設けることは分離効率面から効果
的である。冷却水と気液接触させることは脱硫後の排ガ
スＧ１を再度、洗浄することになり、脱硫工程からのミ
ストを含めて、不純物を除去することができる。また併
わせて、煤塵濃度を効果的に削限することもできる。Next, in the method of the present invention, the desulfurized exhaust gas G1 is pressurized by the exhaust gas fan 3 and sent to the CO 2 removal step 4. The inlet gas G1 of the CO 2 removal step 4 has a combustion exhaust gas temperature of 100 ° C. or higher, whereas it has a temperature of 65 ° C. or lower, preferably 55 ° C. or lower. Since the gas temperature can be easily lowered by, for example, circulation by an air-cooled cooler or gas-liquid contact with cooling water, it is effective from the standpoint of separation efficiency to provide the gas cooling unit in the preceding stage of CO 2 separation. is there. The gas-liquid contact with the cooling water means washing the exhaust gas G1 after desulfurization again, and impurities including the mist from the desulfurization step can be removed. In addition, it is possible to effectively reduce the soot and dust concentration.
【００１０】CO2 除去の対象となる排ガスＧ１は湿式脱
硫した排ガスの全量であっても良いが、一部をライン６
を経て抜き出すことも排ガスＧ１の性状に応じて好まし
いことである。このように、湿式脱硫した排ガスＧ１の
一部をCO2 除去処理すれば、排ガスファン３の必要動力
を小さくすることができる。また、全体のCO2 除去率を
CO2 分離工程で処理するガス量と、分離効率によって、
効率良く、容易に制御することができる。CO2 除去工程
４ではCO2 の分離、ミストおよび煤塵等の除去が行なわ
れる。CO2 の除去には、膜分離、化学／物理吸収、吸着
方法を採用できるが、吸収液としてアルカノールアミン
水溶液を用いる方法が好ましい。The exhaust gas G1 to be subjected to CO 2 removal may be the entire amount of the wet desulfurized exhaust gas, but a part of the exhaust gas G1 is supplied to the line 6
It is also preferable to extract the gas through the exhaust gas according to the properties of the exhaust gas G1. As described above, if a part of the wet desulfurized exhaust gas G1 is subjected to CO 2 removal treatment, the required power of the exhaust gas fan 3 can be reduced. In addition, the overall CO 2 removal rate
Depending on the amount of gas processed in the CO 2 separation process and the separation efficiency,
It can be controlled efficiently and easily. In the CO 2 removal step 4, CO 2 is separated and mist, dust and so on are removed. Membrane separation, chemical / physical absorption, and adsorption methods can be used to remove CO 2 , but a method using an alkanolamine aqueous solution as the absorption liquid is preferable.
【００１１】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などが用いられ、処理温
度は常温付近、圧力は水中で20〜100mmH2O である。CO
2 除去後のガスＧ２は、CO2 吸収液や吸着剤中の有機物
や重金属類を低濃度ではあるが含有する。そこで本発明
の方法では、CO2 を除去した排ガスＧ２を有害物質処理
工程５に送る。この処理工程５においては、排ガスＧ２
中に残存する不純物、すなわち煤塵、CO2 除去工程４か
らのCO2 吸収剤、たとえばアルカノールアミンの分解生
成物および飛散CO2 吸収剤の除去を行なう。すなわち、
有害物質処理工程５では、例えば、ＧＧＨ１における熱
交換管の閉塞の原因となる煤塵および悪臭の発生原因と
なるアミン等の分解生成物が排ガスＧ２から除去され
る。この除去は、一般的には排ガスＧ２の水洗によって
行なわれ、充てん塔またはスプレー塔等が採用される。
また、排ガスＧ２中のアルカリ物質の存在で洗浄水のpH
が7.５〜11になることを考慮して硫酸によってpHを４〜
７に調整した水の使用が好ましい。As the alkanolamine, monoethanolamine, diethanolamine and the like are used, the treatment temperature is around room temperature, and the pressure is 20 to 100 mmH 2 O in water. CO
Gas G2 after 2 removal, albeit at low concentration organic substances and heavy metals in the CO 2 absorbing solution and the adsorbent is contained. Therefore, in the method of the present invention, the exhaust gas G2 from which CO 2 has been removed is sent to the harmful substance treatment step 5. In this treatment step 5, the exhaust gas G2
Impurities remaining in, that performs dust, CO 2 absorbent from CO 2 removal step 4, for example, the removal of the decomposition products of the alkanolamine and scattered CO 2 absorbent. That is,
In the harmful substance treatment step 5, for example, decomposition products such as soot dust that causes clogging of the heat exchange tube in the GGH 1 and amines that cause generation of a bad smell are removed from the exhaust gas G2. This removal is generally performed by washing the exhaust gas G2 with water, and a filling tower, a spray tower or the like is used.
In addition, the pH of the washing water due to the presence of alkaline substances in the exhaust gas G2
Considering that pH becomes 7.5-11, the pH is adjusted to 4-
The use of water adjusted to 7 is preferred.
【００１２】また、前記したように、脱硫処理後の排ガ
スＧ１の一部のみをCO2 除去工程４および有害物質処理
工程５で処理すれば、このような有機物や重金属類を、
CO2 除去工程４および有害物質処理工程５で処理された
ガスＧ３によって、希釈することができるから、これら
有機物や重金属の影響を大幅に低減できる。本発明の方
法では、吸着除去されたCO2 を回収し、CO2 の利用をは
かることもできる。Further, as described above, if only a part of the exhaust gas G1 after desulfurization is treated in the CO 2 removal step 4 and the harmful substance treatment step 5, such organic substances and heavy metals are
Since the gas G3 processed in the CO 2 removal step 4 and the harmful substance processing step 5 can be used for dilution, the influence of these organic substances and heavy metals can be greatly reduced. In the method of the present invention, CO 2 that has been adsorbed and removed can be recovered and CO 2 can be used.
【００１３】吸収や吸着されたCO2 放出工程では操作温
度が高いほうが放出効率が高い。そこで、高温の脱硫前
の燃焼排ガスを用いて、放出工程の操作温度を高めるこ
とは優利であり、効果的な方法である。また、本発明の
方法においては、各工程や排ガスファン３あるいはＧＧ
Ｈ１の配置場所の順序は適宜、各工程に用いる方法によ
って、決められる。たとえば、CO2 の吸着や吸収法で
は、ガス圧が高く、また、温度が低い方がCO2 分離効率
が高い。排ガスファンの動力としてはガス温度が低い方
が好ましい。In the absorbed or adsorbed CO 2 releasing step, the higher the operating temperature, the higher the releasing efficiency. Therefore, it is an advantageous and effective method to raise the operating temperature of the discharge process by using the hot exhaust gas before desulfurization. Further, in the method of the present invention, each step, the exhaust gas fan 3 or the GG
The order of the location of H1 is appropriately determined by the method used in each step. For example, in the CO 2 adsorption or absorption method, the higher the gas pressure and the lower the temperature, the higher the CO 2 separation efficiency. The power of the exhaust gas fan is preferably low in gas temperature.
【００１４】なお、排ガスファン３を脱硫工程２の後、
CO2 除去工程４の手前におくと、CO2 除去工程の圧力が
高まり、CO2 吸収効率が向上する。以下、本発明の実施
例を述べる。After the desulfurization step 2 of the exhaust gas fan 3,
If it is placed before the CO 2 removal step 4, the pressure in the CO 2 removal step will increase and the CO 2 absorption efficiency will improve. Examples of the present invention will be described below.
【００１５】[0015]
【実施例】以下に示す組成の模擬燃焼排ガス500Nl/hr
を、湿式脱硫工程としての石灰石石膏法のガスバブリン
グ方法で処理した。次いで、CO2 分離工程として、15％
モノエタノールアミン法（スチーム再生工程を含む）で
pH9.０でガス処理した。この結果、CO2 分離効率は初期
には23％で、５時間経過後でも22％であった。[Example] 500Nl / hr of simulated combustion exhaust gas having the following composition
Was treated by the gas bubbling method of the limestone gypsum method as a wet desulfurization step. Then, as a CO 2 separation step, 15%
By monoethanolamine method (including steam regeneration process)
Gas treated at pH 9.0. As a result, the CO 2 separation efficiency was 23% at the beginning and 22% even after 5 hours.
【００１６】 模擬燃焼排ガス ガス温度 150℃ SO2, 500ppm 煤塵, 300mg／Nm3-dry CO2, 10vol％ H2O, ８vol％ CO2 分離工程で処理された排ガスをL/G=0.6l/Nm3 で市
水を用いて、スプレー塔で水洗したところ、ガス中の有
機物は0.1ppm以下に減少した。Simulated combustion exhaust gas temperature 150 ° C. SO 2 , 500 ppm soot dust, 300 mg / Nm 3 -dry CO 2 , 10 vol% H 2 O, 8 vol% CO 2 The exhaust gas treated in the separation process was L / G = 0.6 l / When water was washed with a spray tower using Nm 3 city water, the organic matter in the gas was reduced to 0.1 ppm or less.
【００１７】なお脱硫工程処理後のガス条件を以下に示
す。 模擬燃焼排ガス ガス温度 43℃ SO2, 13ppm 煤塵, ４mg/Nm3-dry CO2, 10vol％ H2O, 11vol％ 比較例 実施例と同様の模擬燃焼排ガス500Nl/hrをCO2 分離工程
としての15％モノエタノールアミン法（スチーム再生工
程を含む）でpH9.０でガス処理した。その結果CO2 分離
効率は初期には21％であったが、５時間経過時点では６
％まで低下した。さらに処理ガス中には吸収液ミストを
含めて、有機物が５ppm 程度含有されていた。The gas conditions after the desulfurization process are shown below. Simulated combustion exhaust gas temperature 43 ° C SO 2 , 13ppm soot dust, 4mg / Nm 3 -dry CO 2 , 10vol% H 2 O, 11vol% Comparative example Simulated combustion exhaust gas 500Nl / hr similar to the example was used as CO 2 separation process. Gas treatment was carried out at pH 9.0 by the 15% monoethanolamine method (including the steam regeneration step). As a result, the CO 2 separation efficiency was 21% at the beginning, but was 6 after 5 hours.
Fell to%. Further, the treated gas contained about 5 ppm of organic substances including the absorbing liquid mist.
【００１８】[0018]
【発明の効果】本発明の方法では、CO2 除去に先立っ
て、燃焼排ガスが湿式脱硫処理されるので、排ガス中の
粉塵、SOx 等が減少する。脱硫吸収液の選定によっては
同時にNOx も減少する。その結果、 膜処理や吸着処
理における煤塵による目詰りが防止され、 SOx 、NO
x 、有機化合物（HC）煤塵中に含まれる重金属類等によ
るCO2 吸収液や吸着剤の劣化が防止され、膜、吸着剤あ
るいは吸収剤の交換や再生処理等にかかるコストが大幅
に軽減される。特に、煤煙中に含有するMn, Fe, Co, V
等の選移金属は酸化触媒になり、アルカノールアミンの
分解を促進させる。According to the method of the present invention, since the combustion exhaust gas is subjected to the wet desulfurization treatment prior to CO 2 removal, dust, SOx, etc. in the exhaust gas are reduced. Depending on the choice of desulfurization absorbent, NOx will also decrease at the same time. As a result, clogging due to soot and dust during the membrane treatment and adsorption treatment is prevented, and SOx, NO
x, Deterioration of CO 2 absorbent and adsorbent due to heavy metals contained in organic compound (HC) dust is prevented, and the cost for replacement of membrane, adsorbent or absorbent and regeneration treatment is greatly reduced. It In particular, Mn, Fe, Co, V contained in soot
Selective metals such as act as an oxidation catalyst and accelerate the decomposition of alkanolamine.
【００１９】また、CO2 分離工程には上記の不純物が除
去された排ガスが導入されるので、CO2 再生工程で得ら
れるCO2 は純度の高いものとなり、分離後のCO2 の固定
化や各種原料の利用に対して有利である。さらに、湿式
脱硫後の排ガスを冷却すれば、CO2 分離工程に入る排ガ
スの温度が更に低下するので、CO2 の吸収にとって有利
に働く。吸収効率の向上や吸収液、吸着剤、膜の劣化の
防止にも効果的である。Further, since the exhaust gas from which the above impurities have been removed is introduced into the CO 2 separation step, the CO 2 obtained in the CO 2 regeneration step has a high degree of purity, and the CO 2 after separation or immobilization It is advantageous for the use of various raw materials. Further, if the exhaust gas after the wet desulfurization is cooled, the temperature of the exhaust gas entering the CO 2 separation step is further lowered, which is advantageous for CO 2 absorption. It is also effective in improving absorption efficiency and preventing deterioration of absorbent, adsorbent and membrane.
【００２０】 CO2 除去後の排ガス中の有害物質を有
害物質処理工程で除去することができるので、環境汚染
を回避することができる。Since harmful substances in the exhaust gas after CO 2 removal can be removed in the harmful substance treatment step, environmental pollution can be avoided.
【図１】本発明の工程を示す工程図である。FIG. 1 is a process drawing showing a process of the present invention.
２ 湿式脱硫工程 ４ CO2 除去工程 ５ 有害物質工程2 Wet desulfurization process 4 CO 2 removal process 5 Hazardous substance process
───────────────────────────────────────────────────── フロントページの続き (72)発明者 小林 健二 神奈川県横須賀市湘南鷹取１―26―16 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Kenji Kobayashi 1-26-16 Shotori Takatori, Yokosuka City, Kanagawa Prefecture
Claims (1)
いて、該排ガスを湿式脱硫処理し、次いで該脱硫処理を
した排ガスからCO2 を除去した後に該CO2 を除去した排
ガス中の有害物質の除去処理を行なうことを特徴とする
燃焼排ガスのCO2 除去方法。Claim: What is claimed is: 1. A method for removing CO 2 from combustion exhaust gas, wherein the exhaust gas is subjected to a wet desulfurization treatment, and then CO 2 is removed from the desulfurized exhaust gas, and then the CO 2 is removed. A method for removing CO 2 from combustion exhaust gas, which comprises removing harmful substances in exhaust gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3018675A JPH05231A (en) | 1991-02-12 | 1991-02-12 | Removal of co2 from combustion exhaust gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3018675A JPH05231A (en) | 1991-02-12 | 1991-02-12 | Removal of co2 from combustion exhaust gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH05231A true JPH05231A (en) | 1993-01-08 |
Family
ID=11978182
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3018675A Pending JPH05231A (en) | 1991-02-12 | 1991-02-12 | Removal of co2 from combustion exhaust gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH05231A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0671199A3 (en) * | 1994-03-09 | 1996-03-27 | Kansai Electric Power Co | Method for the removal of carbon dioxide and sulfor oxides from combustion exhaust gas. |
| EP0815922A3 (en) * | 1996-05-28 | 1998-10-07 | Mitsubishi Heavy Industries, Ltd. | Desulfurization and decarbonation process |
| JP2002081691A (en) * | 2000-09-04 | 2002-03-22 | Takasago Thermal Eng Co Ltd | Air purification air conditioning apparatus and air purification air conditioning method |
| JP2005040683A (en) * | 2003-07-25 | 2005-02-17 | Kansai Electric Power Co Inc:The | Method and apparatus for removing nitrogen dioxide and carbon dioxide |
| JP2006503692A (en) * | 2002-10-23 | 2006-02-02 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Method for removing and capturing carbon dioxide from flue gas |
| JP2006263676A (en) * | 2005-03-25 | 2006-10-05 | Fujikasui Engineering Co Ltd | Combustion waste gas-purification system |
| US10589214B2 (en) | 2016-02-02 | 2020-03-17 | University Of Kentucky Research Foundation | CO2 mass transfer enhancement of aqueous amine solvents by particle additives |
-
1991
- 1991-02-12 JP JP3018675A patent/JPH05231A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0671199A3 (en) * | 1994-03-09 | 1996-03-27 | Kansai Electric Power Co | Method for the removal of carbon dioxide and sulfor oxides from combustion exhaust gas. |
| EP0815922A3 (en) * | 1996-05-28 | 1998-10-07 | Mitsubishi Heavy Industries, Ltd. | Desulfurization and decarbonation process |
| JP2002081691A (en) * | 2000-09-04 | 2002-03-22 | Takasago Thermal Eng Co Ltd | Air purification air conditioning apparatus and air purification air conditioning method |
| JP2006503692A (en) * | 2002-10-23 | 2006-02-02 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Method for removing and capturing carbon dioxide from flue gas |
| JP2005040683A (en) * | 2003-07-25 | 2005-02-17 | Kansai Electric Power Co Inc:The | Method and apparatus for removing nitrogen dioxide and carbon dioxide |
| JP2006263676A (en) * | 2005-03-25 | 2006-10-05 | Fujikasui Engineering Co Ltd | Combustion waste gas-purification system |
| US10589214B2 (en) | 2016-02-02 | 2020-03-17 | University Of Kentucky Research Foundation | CO2 mass transfer enhancement of aqueous amine solvents by particle additives |
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