JP3486220B2 - Combustion exhaust gas purification method and apparatus - Google Patents

Combustion exhaust gas purification method and apparatus

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Publication number
JP3486220B2
JP3486220B2 JP03715994A JP3715994A JP3486220B2 JP 3486220 B2 JP3486220 B2 JP 3486220B2 JP 03715994 A JP03715994 A JP 03715994A JP 3715994 A JP3715994 A JP 3715994A JP 3486220 B2 JP3486220 B2 JP 3486220B2
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JP
Japan
Prior art keywords
exhaust gas
absorption
liquid
heat
heater
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 - Fee Related
Application number
JP03715994A
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Japanese (ja)
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JPH07241440A (en
Inventor
元六 仲尾
Original Assignee
バブコック日立株式会社
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Priority to JP03715994A priority Critical patent/JP3486220B2/en
Publication of JPH07241440A publication Critical patent/JPH07241440A/en
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Publication of JP3486220B2 publication Critical patent/JP3486220B2/en
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Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02CCAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00Capture or disposal of greenhouse gases
    • Y02C20/40Capture or disposal of greenhouse gases of CO2
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/151Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Description

【発明の詳細な説明】Detailed Description of the Invention
【0001】[0001]
【産業上の利用分野】本発明は、燃焼排ガス浄化方法お
よび装置に係り、特にボイラなどの燃焼排ガス中の媒
塵、硫黄酸化物および炭酸ガスを、高効率かつ高性能に
除去しうる燃焼排ガス浄化方法および装置に関する。
BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for purifying combustion exhaust gas, and more particularly to a combustion exhaust gas capable of highly efficiently and efficiently removing dust particles, sulfur oxides and carbon dioxide gas in combustion exhaust gas such as boilers. The present invention relates to a purification method and device.
【0002】[0002]
【従来の技術】大気汚染公害防止の観点から、発電用ボ
イラ等のように、硫黄分を比較的多く含む石油や石炭等
の化石燃料を燃焼させる大型装置においては、排ガス中
の媒塵および硫黄酸化物(SO2 およびSO3 以下、S
x という)を除去低減するため電気集塵機および湿式
の排煙脱硫装置が多く取りつけられている。図6は、従
来型ボイラ排ガスの脱塵および湿式排煙脱硫装置のシス
テムフローを示す図である。
2. Description of the Related Art From the viewpoint of preventing air pollution and pollution, in a large apparatus for burning fossil fuel such as petroleum or coal containing a relatively large amount of sulfur, such as a boiler for power generation, dust and sulfur in exhaust gas are included. Oxides (SO 2 and SO 3 or less, S
Many electric dust collectors and wet flue gas desulfurizers are installed to remove and reduce O x ). FIG. 6 is a diagram showing a system flow of a conventional boiler exhaust gas dedusting and wet flue gas desulfurization apparatus.
【0003】ボイラ1からでた排ガスは、電気集塵機2
により脱塵され、ガス/ガスヒータ4で約90℃に冷却
された後、脱硫装置5に導入し、排ガス中のSOX が石
灰(CaCO3)を含むスラリによって石膏(CaSO4)
として除去回収される。SO X 分が取り除かれた無害排
ガスは、デミスタ6で水分を除去された後、前述ガス/
ガスヒータ4で再加熱され、煙突8から大気に放出され
る。途中にファン3と7を入れ、ガスを押込み、吸引し
ている。
Exhaust gas emitted from the boiler 1 is collected by the electric dust collector 2
Is removed by dust and cooled to approximately 90 ° C by the gas / gas heater 4.
After being treated, it is introduced into the desulfurization device 5, and SO in the exhaust gasXStone
Ash (CaCO3) Containing gypsum (CaSOFour)
Are removed and recovered. SO XHarmless discharge with minutes removed
After the moisture is removed by the demister 6, the gas is
It is reheated by the gas heater 4 and released into the atmosphere from the chimney 8.
It Insert fans 3 and 7 in the middle, push in the gas, and suck
ing.
【0004】こうした電気集塵機と石灰−石膏法湿式排
煙脱硫装置を組合わせた排煙浄化システムは、排出媒塵
濃度を30mg/Nm3以下に低減でき、脱硫率が95%以上
と高いこと、および副製石膏を利用できるメリットもあ
り、大気汚染防止に大いに役立つとともに多くのプラン
トが稼働している。しかしながら、最近では、排出媒塵
量を従来の約1/6の5mg/Nm3以下に規制しようとする
動きや要求がある。
A flue gas purification system that combines such an electric dust collector and a lime-gypsum method wet flue gas desulfurization device can reduce the concentration of exhaust dust to 30 mg / Nm 3 or less and has a high desulfurization rate of 95% or more, There is also an advantage that secondary plaster can be used, which is very useful for preventing air pollution and many plants are operating. However, recently, there is a movement and a demand to regulate the amount of discharged dust particles to 5 mg / Nm 3 or less, which is about 1/6 of the conventional amount.
【0005】さらに、地球温暖化防止または抑制の観点
から排ガス中の炭酸ガス(CO2)をも分離回収する要求
が高まってきている。図7は、アルカノールアミン(例
えばモノエタノールアミン)水溶液を用いた吸収法によ
る排ガス中のCO2 除去装置をボイラ排ガス浄化系に組
込んだシステムフローを示す図である。脱硫装置5、ミ
ストキャッチャー6を出た排ガスをブロア10、クーラ
11を経由してCO2吸収塔12に導入し、アミン吸収
液と気液接触させてCO2 を吸収させる。CO 2 が除去
された排ガスは、アミン洗浄系15、テミスタ16を経
由してガス中のアミンや水分が取り除かれたのちボイラ
排ガス煙道に戻され、ガス/ガスヒータ4で再加熱され
た後、ファン7で煙突から無害ガスとして排出される。
一方CO 2 を吸収したアミン水溶液は、ポンプ13で搬
送され、熱交換器17で再生塔18で再生された高温の
アミン吸収液との熱交換により加熱された後CO2 追出
し再生塔18に送られる。CO2 追出し再生塔18で
は、リボイラ20で前記熱交換器17にて加熱された高
温アミン吸収液が水蒸気により加熱され、アミン吸収液
からCO2 が追出される。追出されたCO2 ガスは、ミ
ストセパレータ19でミストが除去され、純CO2 回収
系22で回収される。CO2 を追出したアミン吸収液
は、熱交換器17およびクーラ11で冷却された後、吸
収塔に戻されて再度CO2 の吸収に用いられる。
Further, from the viewpoint of preventing or suppressing global warming
Carbon dioxide (CO2) Request to separate and collect
Is increasing. Figure 7 shows alkanolamines (example
For example, the absorption method using an aqueous solution of monoethanolamine)
CO in exhaust gas2Assembling the removal device into the boiler exhaust gas purification system
It is a figure which shows the integrated system flow. Desulfurization equipment 5, Mi
Exhaust gas from the Statcher 6 is blower 10, cooler
CO via 112Introduced into absorption tower 12
CO in liquid-gas contact2To absorb. CO 2Removed
The discharged exhaust gas passes through the amine cleaning system 15 and the thermistor 16.
Therefore, after the amine and water in the gas have been removed, the boiler
Returned to the exhaust gas flue and reheated by the gas / gas heater 4.
After that, it is discharged from the chimney as harmless gas by the fan 7.
On the other hand CO 2The amine aqueous solution that absorbed
Of the high temperature that was sent and regenerated by the heat exchanger 17 in the regeneration tower 18.
CO after being heated by heat exchange with the amine absorbing liquid2Expulsion
It is then sent to the regeneration tower 18. CO2At the playout tower 18
Is the high temperature heated in the heat exchanger 17 in the reboiler 20.
The warm amine absorption liquid is heated by steam, and the amine absorption liquid
To CO2Is banished. The expelled CO2Gas is
The mist is removed by the strike separator 19 and pure CO2Recovery
Collected in system 22. CO2Absorbed amine absorption liquid
Is cooled by the heat exchanger 17 and the cooler 11 and then sucked.
CO is returned to the collecting tower2Used for absorption of.
【0006】こうした吸収法CO2 除去装置を排ガス浄
化系につけることにより、排ガス中のCO2 を90%以
上除去でき、99.9%以上の高純度のCO2 ガスを回
収できる。
By attaching such an absorption method CO 2 removal device to the exhaust gas purification system, 90% or more of CO 2 in the exhaust gas can be removed, and a CO 2 gas of high purity of 99.9% or more can be recovered.
【0007】[0007]
【発明が解決しようとする課題】地球温暖化を防止する
ためには、これ以上大気中のCO2 を増加させないこと
が必要であり、それを実現するための最も現実的な方法
は、比較的大量かつ一定箇所から排ガスを出す火力発電
所のCO2 を除去・回収する技術を確立することであ
る。
In order to prevent global warming, it is necessary not to increase CO 2 in the atmosphere any more, and the most practical method for achieving this is relatively It is to establish a technology for removing and recovering CO 2 from a thermal power plant that produces a large amount of exhaust gas from a fixed location.
【0008】上述したアミン液を用いたCO2 除去・回
収システムを図7に示したようにボイラ排ガス浄化系に
取りつけることによりCO2 は回収できるが、このシス
テムでの問題点は、CO2 を吸収したアミン液からCO
2 を追出すために多大な熱エネルギーが必要なことであ
る。通常90〜120℃に加熱しないとCO2 は追出せ
ないためボイラの高温蒸気を一部流用して加熱源にあて
ている。このため、試算では発電効率が10%以上低下
するといわれている。現状の石炭焚き火力発電所での発
電効率は、40%前後であるため、その効率が30%以
下になるとエネルギーロスが大きすぎ実現性は出てこな
い。
CO 2 can be recovered by installing the CO 2 removal / recovery system using the above-mentioned amine solution in the boiler exhaust gas purification system as shown in FIG. 7, but the problem with this system is that CO 2 CO from absorbed amine liquid
That is, a large amount of heat energy is required to expel 2 . Usually, CO 2 cannot be expelled unless it is heated to 90 to 120 ° C., so part of the high temperature steam of the boiler is diverted to the heating source. For this reason, it is said that the power generation efficiency is reduced by 10% or more in trial calculation. Since the power generation efficiency of the current coal-fired thermal power plant is around 40%, if the efficiency becomes less than 30%, the energy loss will be too large to be realized.
【0009】従って、ボイラ排ガスからCO2 を除去回
収する際の最大の課題は、多大なエネルギーを要するこ
とであり、本発明の目的は、従来技術のこの問題点を解
決することにある。また従来技術において、脱硫装置か
ら排出されるガスは、ガス/ガスヒータ等で再加熱され
70℃以上にして煙突から大気放出されてきたが、これ
は、微量(<30mg/Nm3)ながらも排ガス中に未処理の
媒塵が含まれるためで、これらを遠くへ飛散させるため
に昇温しているものである。媒塵量を極めて低いレベル
(例<5mg/Nm3)に低減できれば、排ガス温度を従来技
術より低下させることができ、より多くのボイラ排ガス
熱を回収することができる。
Therefore, the greatest problem in removing and recovering CO 2 from boiler exhaust gas is that a large amount of energy is required, and an object of the present invention is to solve this problem of the prior art. Moreover, in the prior art, the gas discharged from the desulfurization device was reheated by a gas / gas heater or the like and released to the atmosphere from the chimney at 70 ° C. or higher, but this is a small amount (<30 mg / Nm 3 ) of exhaust gas. This is because the untreated dust particles are contained in it, and the temperature is raised in order to disperse them in the distance. If the amount of dust particles can be reduced to an extremely low level (eg <5 mg / Nm 3 ), the exhaust gas temperature can be lowered as compared with the prior art, and more boiler exhaust gas heat can be recovered.
【0010】[0010]
【課題を解決するための手段】上記目的を達成するため
本願で特許請求する発明は以下のとおりである。 (1)燃焼排ガスをCO2 吸収塔内でアルカノールアミ
ン水溶液を用いた吸収液と接触させて前記燃焼排ガス中
のCO2 を吸収し、該CO2 を吸収した吸収液を加熱し
てCO2 追出し再生塔内でCO2 を追出して再生したの
ち、CO2 吸収塔に循環する燃焼排ガス浄化方法におい
て、前記CO2 を吸収した吸収液を吸収液加熱用熱交換
器を用いて燃焼排ガスの保有熱および該燃焼ガス中の液
体蒸気の凝縮熱を利用して加熱したのち、CO2 追出し
再生塔内で再生することを特徴とする燃焼排ガス浄化方
法。
In order to achieve the above object, the invention claimed in the present application is as follows. (1) flue gas is contacted with the absorption liquid with an aqueous alkanolamine solution in a CO 2 absorption tower to absorb the CO 2 of the combustion exhaust gas, CO 2 purge by heating the absorbent solution that has absorbed the CO 2 In the method for purifying combustion exhaust gas in which CO 2 is expelled and regenerated in the regeneration tower and then circulated to the CO 2 absorption tower, the absorption liquid having absorbed the CO 2 is used to heat the combustion exhaust gas by using a heat exchanger for heating the absorption liquid. And a method for purifying combustion exhaust gas, which comprises heating by utilizing the heat of condensation of liquid vapor in the combustion gas, and then regenerating the CO 2 in a regeneration tower.
【0011】(2)燃焼排ガス中の媒塵を除去する集塵
機と、該排ガス中の硫黄酸化物を除去する脱硫装置と、
該排ガス中のCO2 を吸収液を用いて吸収除去するCO
2 除去装置とを備えた燃焼排ガス浄化装置において、燃
焼装置から出た直後の高温排ガスによってCO2 を吸収
した吸収液を加熱してCO2 追出し再生塔に送るCO2
吸収液最終加熱器と、該最終加熱器で熱回収された前記
排ガス中の媒塵を除去する集塵機と、該集塵機を出た排
ガスによってCO2 吸収塔から抜出したCO2 吸収液を
加熱して排ガス中の蒸気の凝縮熱を回収するCO2 吸収
液の第1の加熱器と、該第1加熱器を出た排ガス中の硫
黄酸化物を除去する湿式排ガス脱硫装置と、該脱硫装置
を出た排ガス中のCO2 を吸収液を用いて吸収除去する
CO2 吸収塔と、前記CO2 吸収液第1加熱器で加熱さ
れた吸収液をCO2 追出し再生塔で再生された吸収液で
加熱したのち前記CO2 吸収液最終加熱器に送る熱交換
装置と、CO2 吸収液最終加熱器で加熱されたCO2
収液を受入れ該吸収液中のCO2 を除去するCO2 追出
し再生塔とを設けたことを特徴とする燃焼排ガス浄化装
置。
(2) A dust collector for removing dust particles in the combustion exhaust gas, and a desulfurization device for removing sulfur oxides in the exhaust gas,
CO for absorbing and removing CO 2 in the exhaust gas by using an absorbing liquid
In the combustion exhaust gas purifying apparatus that includes a 2 removing device, by heating the absorbent solution that has absorbed CO 2 by the hot exhaust gas immediately after exiting from the combustion device sends a CO 2 purge regenerator CO 2
Absorbing liquid final heater, dust collector for removing dust particles in the exhaust gas heat-recovered by the final heater, and heating the CO 2 absorbing liquid extracted from the CO 2 absorption tower by the exhaust gas exiting the dust collector A first heater for CO 2 absorbing liquid that recovers the heat of condensation of vapor in the exhaust gas, a wet exhaust gas desulfurization device that removes sulfur oxides in the exhaust gas that exits the first heater, and a desulfurization device. And a CO 2 absorption tower that absorbs and removes CO 2 in the exhaust gas using an absorption liquid, and the absorption liquid heated by the CO 2 absorption liquid first heater is heated by the absorption liquid regenerated by the CO 2 discharge regeneration tower a heat exchange device for feeding the CO 2 absorbing solution final heater After, CO 2 absorbing liquid final heater CO 2 absorbing liquid that has been heated by the CO 2 removal acceptance the absorbing solution in CO 2 purge regeneration tower and A combustion exhaust gas purifying device characterized by being provided.
【0012】(3)燃焼排ガス中の媒塵を除去する集塵
機と、該排ガス中の硫黄酸化物を除去する脱硫装置と、
該排ガス中のCO2 を吸収液を用いて吸収除去するCO
2 除去装置とを備えた燃焼排ガス浄化装置において、ボ
イラから出た直後の高温の排ガスによってCO2 を吸収
した吸収液を加熱するとともに吸収液中のCO2 を追出
す一体型排ガス熱回収CO2 追出し塔と、該一体型排ガ
ス熱回収CO2 追出し塔で熱回収された排ガスにカルシ
ウム化合物脱硫剤と水を噴霧する装置と、該噴霧装置を
出た排ガス中の媒塵を除去する電気集塵機と、該電気集
塵機を出た排ガスによってCO2 吸収塔から抜出したC
2 吸収液を加熱して排ガス中の蒸気の凝縮熱を回収す
るCO2 吸収液の第1の加熱器と、該第1の加熱器を出
た排ガス中の硫黄酸化物を除去する湿式排ガス脱硫装置
と、該脱硫装置を出た排ガス中のCO2 を吸収液を用い
て吸収除去するCO2 吸収塔と、前記CO2 吸収液第1
加熱器で加熱された吸収液を前記一体型排ガス熱回収C
2 追出し塔からの再生吸収液により加熱するととも一
体型排ガス熱回収CO2 追出しに該塔に供給する熱交換
装置とを設けたことを特徴とする燃焼排ガス浄化装置。
(3) A dust collector for removing dust particles in the combustion exhaust gas, and a desulfurizer for removing sulfur oxides in the exhaust gas,
CO for absorbing and removing CO 2 in the exhaust gas by using an absorbing liquid
In a combustion exhaust gas purifying apparatus equipped with a 2 removal device, an integrated exhaust gas heat recovery CO 2 that heats the absorption liquid that has absorbed CO 2 by the high temperature exhaust gas immediately after it leaves the boiler and expels CO 2 in the absorption liquid A discharge tower, an apparatus for spraying a calcium compound desulfurizing agent and water to the exhaust gas heat-recovered by the integrated exhaust gas heat recovery CO 2 discharge tower, and an electrostatic precipitator for removing dust particles in the exhaust gas exiting the spray apparatus. , C extracted from the CO 2 absorption tower by the exhaust gas leaving the electric dust collector
Wet exhaust gas by heating the O 2 absorbing solution for removing the first heater CO 2 absorbing solution for recovering heat of condensation of the vapors in the exhaust gas, sulfur oxides in the exhaust gas exiting the first heater A desulfurizer, a CO 2 absorption tower for absorbing and removing CO 2 in the exhaust gas leaving the desulfurizer using an absorbing liquid, and the CO 2 absorbing liquid first
The integrated exhaust gas heat recovery C for absorbing liquid heated by a heater
A combustion exhaust gas purifying apparatus, which is provided with a heat exchange device which is heated by a regenerated absorption liquid from an O 2 purging tower and is supplied to the tower for integrated exhaust gas heat recovery CO 2 purging.
【0013】[0013]
【作用】以下、本発明での構成要素の作用について記述
する。各要素番号は、後述する図1および図2の番号で
ある。石炭焚きボイラ1から排出される排ガスは、通常
200〜300℃であり、排ガス出口にCO2 吸収アミ
ン加熱器(1)23を設置することによりCO2 を吸収
したアミン液の加熱に用い、排ガスを60〜90℃に冷
却する。60〜90℃に冷却された排ガスを低温電気集
塵機に導入し、排ガス中の石炭灰や媒塵を回収除去す
る。電気集塵機は、通常200〜300℃の排ガス雰囲
気に設置されることが多いが、60〜90℃の低温、あ
る意味では高湿度で集塵する方法(低温電気集塵機)の
方が効率的で、排ガス中の媒塵量を5mg/Nm3以下に低減
できるメリットを有している。
The operation of the constituent elements of the present invention will be described below. Each element number is a number in FIGS. 1 and 2 described later. The exhaust gas discharged from the coal-fired boiler 1 is usually at 200 to 300 ° C., and the CO 2 absorbing amine heater (1) 23 is installed at the exhaust gas outlet to heat the amine liquid that has absorbed CO 2 , Is cooled to 60-90 ° C. The exhaust gas cooled to 60 to 90 ° C. is introduced into a low temperature electrostatic precipitator to collect and remove coal ash and dust particles in the exhaust gas. An electric dust collector is usually installed in an exhaust gas atmosphere of 200 to 300 ° C., but a method of collecting dust at a low temperature of 60 to 90 ° C., in a sense of high humidity (low temperature electric dust collector) is more efficient, It has the advantage of reducing the amount of dust particles in the exhaust gas to 5 mg / Nm 3 or less.
【0014】60〜90℃に冷却され、媒塵を除去され
た排ガスは、次にCO2 吸収アミン加熱器(2)25に
ファン3で送られ、30〜50℃に冷却される。排ガス
中には、10〜15%の水蒸気が含まれていることか
ら、30〜50℃に冷却されると水分が凝縮し、温度降
下の他に水蒸気の凝縮熱まで回収できる。いいかえれば
CO2 を吸収したアミン液の加熱に排ガスの回収熱を有
効に利用できる。
The exhaust gas, which has been cooled to 60 to 90 ° C. and whose dust has been removed, is then sent to the CO 2 absorption amine heater (2) 25 by the fan 3 and cooled to 30 to 50 ° C. Since the exhaust gas contains 10 to 15% of water vapor, water is condensed when cooled to 30 to 50 ° C., and the heat of condensation of water vapor can be recovered in addition to the temperature drop. In other words, the heat of recovery of exhaust gas can be effectively used for heating the amine liquid that has absorbed CO 2 .
【0015】排ガス温度を従来の90〜120℃よりも
はるかに低温度の30〜50℃に冷却し凝縮液を得る
と、凝縮熱を含めた回収熱をアミン加熱に利用できる他
に脱硫装置5の補給水を低減または皆無にすることがで
き、さらに石灰スラリによる脱硫反応を促進できるメリ
ットがある。湿式排煙脱硫装置5においても、排ガス温
度を30〜50℃の低温に冷却すると吸収液の温度も低
下し、脱硫反応を促進することができ、脱硫装置の性能
の点からもメリットがでる。
When the condensate is obtained by cooling the exhaust gas temperature to 30 to 50 ° C., which is much lower than the conventional temperature of 90 to 120 ° C., the recovery heat including the condensation heat can be utilized for the amine heating and the desulfurization apparatus 5 There is an advantage that the make-up water of the above can be reduced or eliminated, and the desulfurization reaction by the lime slurry can be promoted. Also in the wet flue gas desulfurization apparatus 5, when the exhaust gas temperature is cooled to a low temperature of 30 to 50 ° C., the temperature of the absorbing solution is also lowered, the desulfurization reaction can be promoted, and there is an advantage in terms of the performance of the desulfurization apparatus.
【0016】脱硫装置5で、硫黄酸化物が除去され、ミ
ストキャッチャー6で水分が除去された排ガスは、CO
2 吸収塔12でCO2 が除去され、窒素、酸素および蒸
気圧分の水分のみを含む極めてクリーンかつ無害なガス
になって煙突8から排出される。CO2 を吸収したアミ
ン液は、ポンプ13により搬送され、CO2 吸収アミン
加熱器(2)25、熱交換器17およびCO2 吸収アミ
ン加熱器(1)23により加熱され、CO2 追出し再生
塔18でCO2 が追出され、再度、熱交換器17を経由
してCO2 吸収塔12に戻される。
Exhaust gas from which sulfur oxides have been removed by the desulfurization device 5 and water has been removed by the mist catcher 6 is CO
The CO 2 is removed in the 2 absorption tower 12, and becomes an extremely clean and harmless gas containing only nitrogen, oxygen and water of vapor pressure, and is discharged from the chimney 8. The amine liquid having absorbed CO 2 is conveyed by the pump 13 and heated by the CO 2 absorption amine heater (2) 25, the heat exchanger 17 and the CO 2 absorption amine heater (1) 23, and the CO 2 displacement regeneration tower. CO 2 is expelled at 18 and is returned to the CO 2 absorption tower 12 via the heat exchanger 17 again.
【0017】特に本発明のポイントになることは、CO
2 吸収アミン加熱器を排ガス熱回収系に設け、当該アミ
ン吸収液の加熱にボイラ排ガスの熱を最大限に有効に利
用することである。アミン吸収液からCO2 を追出すの
にボイラ排ガス熱では不十分な場合は、図2にも示した
ように、リボイラ20を設置し、ボイラ補助蒸気で補充
することも必要である。
Particularly, the point of the present invention is that CO
(2) An absorption amine heater is provided in the exhaust gas heat recovery system so that the heat of the boiler exhaust gas is used to the maximum extent possible for heating the amine absorption liquid. When the boiler exhaust gas heat is not sufficient to drive CO 2 out of the amine absorbing solution, it is also necessary to install the reboiler 20 and supplement the boiler auxiliary steam as shown in FIG.
【0018】[0018]
【実施例】本発明の実施例を以下図面をもって説明す
る。図1は、本発明になる高性能高効率排煙浄化システ
ムのフローを示し、図2は、同システムフローの詳細を
示す。排ガスの流れで装置を列挙すると、ボイラ1、C
2 吸収アミン加熱器(1)23、低温電気集塵機2
4、ファン3、CO2 吸収アミン加熱器(2)25、脱
硫装置5、ミストキャッチャー6、ブロア10、CO2
吸収塔12、アミン洗浄系15、ファン7、煙突8にし
たものである。
Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 shows a flow of a high performance and high efficiency flue gas purification system according to the present invention, and FIG. 2 shows details of the system flow. When the devices are listed by the flow of exhaust gas, boiler 1, C
O 2 absorption amine heater (1) 23, low temperature electrostatic precipitator 2
4, fan 3, CO 2 absorption amine heater (2) 25, desulfurization device 5, mist catcher 6, blower 10, CO 2
The absorption tower 12, the amine cleaning system 15, the fan 7, and the chimney 8 are used.
【0019】CO2 吸収用アミン液の流れに沿っては、
CO2 吸収塔12、ポンプ13、CO2 吸収アミン加熱
器(2)25、熱交換器17、CO2 吸収アミン加熱器
(1)23、CO2 追出し再生塔18、リボイラ20を
設置している。図2では、CO2 吸収アミン加熱器
(1)23、と低温電気集塵機24の間に石灰(CaC
3)または消石灰(Ca( OH)2) 供給系26、と水ス
プレイ系27を記述しているが、こうした装置を設置す
ることにより、低温電気集塵機24内で脱硫反応を生じ
させ、一部または大部分のSOx をあらかじめ除去しよ
うとするものであるが、これらの装置が設置されている
ものもいないものも本発明の範囲になる。
Along the flow of the CO 2 absorbing amine liquid,
A CO 2 absorption tower 12, a pump 13, a CO 2 absorption amine heater (2) 25, a heat exchanger 17, a CO 2 absorption amine heater (1) 23, a CO 2 removal regeneration tower 18, and a reboiler 20 are installed. . In FIG. 2, between the CO 2 absorption amine heater (1) 23 and the low temperature electrostatic precipitator 24, lime (CaC
Although an O 3 ) or slaked lime (Ca (OH) 2 ) supply system 26 and a water spray system 27 are described, by installing such devices, a desulfurization reaction occurs in the low temperature electrostatic precipitator 24, and a part thereof is generated. Alternatively, most of the SO x are to be removed in advance, but it is within the scope of the present invention whether or not these devices are installed.
【0020】本発明システムの効果および特徴は、ボイ
ラ排ガスの持つ熱量を最大限有効に利用できることであ
り、CO2 を追出すのに必要な熱量を低減でき、火力発
電所での発電効率を従来のように40→30%以下に下
げることはなく、数%以下の低下に抑えることができ
る。本発明システムでは、ガス/ガスヒータを取りつけ
てなく、脱硫および脱CO 2 された排ガスは、比較的低
温(30〜50℃)で煙突から排出される。有害ガスを
含まない排ガスを低温で排出することは、液化天然ガス
(LNG)を燃焼させるボイラやLNG燃焼ガスタービ
ン熱回収蒸気発生器(HRSG)でも実施されているこ
とであり、問題はない。別の見方をすれば、LNG焚き
ボイラ等のように排ガス中に媒塵やSOx を含まないシ
ステムでは、低温電気集塵機や脱硫装置は、必要ではな
く排ガス中のCO2 のみ除去回収すればよいことにな
る。従って、LNG焚き等の場合は、図2での低温電気
集塵機24、ファン3、脱硫装置5、ミストキャッチャ
ー6、石灰または消石灰供給系26、水スプレイ系27
は不要になるがこのシステムも本発明に属する。
The advantages and features of the system of the present invention are:
It is possible to use the heat quantity of exhaust gas as effectively as possible.
CO2Can reduce the amount of heat required to drive the
Reduce power generation efficiency at power stations from 40 to 30% or less as before
Can be reduced to a few percent or less
It In the system of the present invention, a gas / gas heater is installed
Desulfurization and CO removal 2Generated exhaust gas is relatively low
Exhausted from the chimney at a temperature (30-50 ° C). Harmful gas
Emitting exhaust gas that does not contain liquefied natural gas
Boiler that burns (LNG) or LNG combustion gas turbine
Heat recovery steam generator (HRSG)
And there is no problem. From another perspective, LNG-fired
Dust and SO in exhaust gas such as boilersxDoes not include
In the stem, a low temperature electrostatic precipitator or desulfurizer is not necessary.
CO in exhaust gas2Only remove and collect
It Therefore, in the case of LNG burning, low temperature electricity
Dust collector 24, fan 3, desulfurization device 5, mist catcher
-6, lime or slaked lime supply system 26, water spray system 27
However, this system also belongs to the present invention.
【0021】図3および図4は、本発明になる高性能高
効率排煙浄化システムフローの他の実施例を示す。図3
は、図2の高性能高効率排煙浄化システムに対して、C
2 吸収アミン加熱器(1)とCO2 追出し再生塔を一
体化した排ガス熱利用CO2 追出し再生塔28をボイラ
出口に設置したものである。図3のシステムは、熱効率
の点では、図2と同じであるが装置数を少なくでき、省
スペース、コンパクト化に有効である。
FIGS. 3 and 4 show another embodiment of the flow of the high performance and high efficiency flue gas purification system according to the present invention. Figure 3
Is the C for the high-performance and high-efficiency flue gas purification system of FIG.
An exhaust gas heat utilization CO 2 removal regeneration tower 28 in which an O 2 absorption amine heater (1) and a CO 2 removal regeneration tower are integrated is installed at the boiler outlet. The system of FIG. 3 is the same as that of FIG. 2 in terms of thermal efficiency, but the number of devices can be reduced, which is effective for space saving and compactness.
【0022】ボイラ排ガス保有熱でCO2 を吸収したア
ミン水溶液を加熱する場合、石炭焚きボイラ排ガスはC
2 ガスが最も多く、水分が少ないため熱回収的にはよ
り厳しくなる。以下石炭焚きボイラを対象として、CO
2 濃度:12%、水分:10%と設定した場合の熱回収
計算結果を記述する。ボイラ排ガス中のCO2 を吸収法
で除去回収するシステムは、通常L/G(Lは吸収液循
環流量、Gは排ガス流量)が3〜4で運転され、排ガス
量;106 Nm 3/h 、液循環量;3.5×103 m3/hの場
合、排ガス温度を100℃下げるまで熱回収するとCO
2 吸収液を約10℃昇温でき、200℃下げるまで熱回
収すると約20℃昇温できる。また排ガス中には約10
%の水蒸気が含まれており、排ガス温度を30〜50℃
以下に冷却して水蒸気を凝縮させると熱回収率90%と
仮定してもCO2 吸収液を12℃昇温させることができ
る。従来のCO2 吸収装置では、アミン吸収液温度30
〜50℃でCO2 を吸収し、熱交換器17で70℃まで
加熱し、リボイラで100〜120℃まで加熱してCO
2 を追出していたが、本発明システムでは、ボイラ排ガ
スの熱を利用し、CO2 吸収アミン加熱器(1)(2)
で20〜30℃吸収液を昇温できるのでリボイラでは1
0〜20℃加熱すればよいことになり、必要熱量を1/
3〜1/5に低減でき発電効率低下も従来の1/3〜1
/5にすることができる。
CO is generated by the heat of the boiler exhaust gas2Which has absorbed
When heating the aqueous mining solution, the coal-fired boiler exhaust gas is C
O2The gas is the most and the water is little
Gets stricter. CO targeting coal-fired boilers
2Heat recovery when concentration: 12%, water: 10%
Describe the calculation result. CO in boiler exhaust gas2Absorption method
The system for removing and recovering is usually L / G (where L is the absorption liquid cycle).
Circulation flow rate, G is the flow rate of exhaust gas)
Quantity; 106Nm 3/ h, liquid circulation amount; 3.5 × 103m3/ h
In this case, if heat is recovered until the exhaust gas temperature is lowered by 100 ° C, CO
2The absorption liquid can be heated up to about 10 ℃ and heated up to 200 ℃.
When collected, the temperature can be raised by about 20 ° C. Also, about 10 in exhaust gas
% Of water vapor is included, and the exhaust gas temperature is 30 to 50 ° C.
When it is cooled to the temperature below and the water vapor is condensed, the heat recovery rate is 90%.
Assuming CO2The absorption liquid can be heated up to 12 ° C
It Conventional CO2In the absorber, the amine absorbing liquid temperature is 30
CO at ~ 50 ° C2Up to 70 ° C in the heat exchanger 17
Heat and heat to 100-120 ° C with a reboiler
2However, in the system of the present invention, the boiler discharge
Utilizing the heat of water, CO2Absorption amine heater (1) (2)
Since the absorption liquid can be heated up to 20 to 30 ° C in the reboiler,
It suffices to heat 0 to 20 ° C, and
It can be reduced to 3 to 1/5 and power generation efficiency can be reduced to 1/3 to 1 of the conventional one.
It can be / 5.
【0023】図4は、CO2 追出し再生塔18から排出
されるCO2 ガス(通常90〜120℃)の熱をもCO
2 吸収アミンの加熱に利用し、熱効率をさらに向上させ
ようとしたもので、CO2 追出し再生塔18の上部につ
けたクーラ11の代わりにCO2 吸収アミン加熱器
(3)29を設置したものである。図4のシステムにす
ることにより発電効率低下をより低減できる。
[0023] Figure 4, CO 2 purge CO also heat the CO 2 gas discharged from the regenerator 18 (usually 90 to 120 ° C.)
It is intended to further improve the thermal efficiency by using it for heating the 2 absorption amine, and the CO 2 absorption amine heater (3) 29 is installed in place of the cooler 11 attached to the upper part of the CO 2 removal regeneration tower 18. is there. The system of FIG. 4 can further reduce the decrease in power generation efficiency.
【0024】従来型システムでは、CO2 除去装置を設
置すると発電効率は40%から30%に低減していた
が、本発明システムを用いると発電効率の低下を1/3
〜1/5にすることができるので33〜38%の発電効
率で運転できることになる。図5は、ボイラ燃料にLN
G等のSOx や媒塵を発生しない燃料を用いた場合の排
ガス中CO2 除去システムフローを示すものである。排
ガス中にSOx や媒塵を含まないため、脱硫装置5およ
び低温電気集塵機24が不要になるのでこれらを取り除
いたシステムである。このシステムも本発明に属する。
In the conventional system, the power generation efficiency was reduced from 40% to 30% when the CO 2 removal device was installed, but the use of the system of the present invention reduced the power generation efficiency by 1/3.
Since it can be reduced to ⅕, it can be operated with a power generation efficiency of 33 to 38%. Fig. 5 shows that LN is used as boiler fuel.
7 shows a flow chart of a CO 2 removal system in exhaust gas when using a fuel that does not generate SO x or dust such as G. Since the exhaust gas does not contain SO x or dust particles, the desulfurization device 5 and the low-temperature electrostatic precipitator 24 are not required, and therefore the system is removed. This system also belongs to the present invention.
【0025】[0025]
【発明の効果】本発明になる高性能高効率排煙浄化シス
テムを用いることにより、火力発電用ボイラから排出さ
れる排ガス中のCO2 を多大なエネルギーロスや発電効
率の低下を招くことなく除去でき、地球温暖化防止に寄
与できる。また電気集塵機および脱硫装置を従来より低
温部に配置していることから脱塵、脱硫効率が向上し、
おなじ大きさなら性能が向上し、同じ性能ならコンパク
トにすることができる。
By using the high-performance and high-efficiency flue gas purification system according to the present invention, CO 2 in exhaust gas discharged from a boiler for thermal power generation can be removed without causing a large energy loss and a reduction in power generation efficiency. Yes, it can contribute to the prevention of global warming. In addition, because the electric dust collector and desulfurization device are placed in a lower temperature section than before, dust removal and desulfurization efficiency is improved,
If it is the same size, the performance will improve, and if it is the same, it can be made compact.
【0026】本発明によれば、吸収法CO2 除去回収装
置を現実的なものにすることができる。
According to the present invention, the absorption-type CO 2 removal and recovery device can be made practical.
【図面の簡単な説明】[Brief description of drawings]
【図1】本発明になる高性能高効率排煙浄化システムの
フロー図。
FIG. 1 is a flow chart of a high performance and high efficiency flue gas purification system according to the present invention.
【図2】本発明になる高性能高効率排煙浄化システムの
フロー図。
FIG. 2 is a flow chart of a high performance and high efficiency flue gas purification system according to the present invention.
【図3】本発明になる高性能高効率排煙浄化システムフ
ローの他の実施例図。
FIG. 3 is another embodiment of the high-performance and high-efficiency flue gas purification system flow according to the present invention.
【図4】本発明になる高性能高効率排煙浄化システムフ
ローの他の実施例図。
FIG. 4 is another embodiment of the high-performance and high-efficiency flue gas purification system flow according to the present invention.
【図5】本発明になる高性能高効率排煙浄化システムフ
ローの他の実施例図。
FIG. 5 is another embodiment of the high-performance and high-efficiency flue gas purification system flow according to the present invention.
【図6】従来技術になるボイラ排ガス浄化システムのフ
ロー図。
FIG. 6 is a flow chart of a boiler exhaust gas purification system according to a conventional technique.
【図7】従来技術になるボイラ排ガス浄化システムにア
ミン吸収法によるCO2 除去回収装置を設置したフロー
図。
FIG. 7 is a flow chart in which a CO 2 removal and recovery device by an amine absorption method is installed in a boiler exhaust gas purification system which is a conventional technique.
【符号の説明】[Explanation of symbols]
1…ボイラ、3…送風ファン、5…脱硫装置、6…ミス
トキャッチャー、7…誘引ファン、8…煙突、10…ブ
ロア、11…クーラ、12…CO2 吸収塔、13…ポン
プ、14…吸収液供給系、15…アミン洗浄系、16…
デミスタ、17…熱交換器、18…CO2 追出し再生
塔、19…ミストセパレータ、20…加熱器(リボイ
ラ)、22…純CO2 回収系、23…CO2 吸収アミン
加熱器(1)、24…低温電気集塵機、25…CO2
収アミン加熱機(2)、26…石灰または消石灰供給
系、27…水スプレイ系、28…排ガス熱利用CO2
出し再生塔、29…CO2 吸収アミン加熱器(3)。
1 ... boiler, 3 ... blower fan, 5 ... desulfurizer, 6 ... mist catcher, 7 ... induction fan, 8 ... chimney, 10 ... blower, 11 ... cooler, 12 ... CO 2 absorption tower, 13 ... pump, 14 ... absorbent Liquid supply system, 15 ... Amine cleaning system, 16 ...
Demister, 17 ... Heat exchanger, 18 ... CO 2 drive-out regeneration tower, 19 ... Mist separator, 20 ... Heater (reboiler), 22 ... Pure CO 2 recovery system, 23 ... CO 2 absorption amine heater (1), 24 ... low temperature electrostatic precipitator, 25 ... CO 2 absorption amine heater (2), 26 ... lime or slaked lime supply system, 27 ... water spray system, 28 ... exhaust gas heat utilization CO 2 drive-out regeneration tower, 29 ... CO 2 absorption amine heater (3).

Claims (3)

    (57)【特許請求の範囲】(57) [Claims]
  1. 【請求項1】 燃焼排ガスをCO2 吸収塔内でアルカノ
    ールアミン水溶液を用いた吸収液と接触させて前記燃焼
    排ガス中のCO2 を吸収し、該CO2 を吸収した吸収液
    を加熱してCO2 追出し再生塔内でCO2 を追出して再
    生したのち、CO2 吸収塔に循環する燃焼排ガス浄化方
    法において、前記CO2 を吸収した吸収液を吸収液加熱
    用熱交換器を用いて燃焼排ガスの保有熱および該燃焼ガ
    ス中の液体蒸気の凝縮熱を利用して加熱したのち、CO
    2 追出し再生塔内で再生することを特徴とする燃焼排ガ
    ス浄化方法。
    1. The combustion exhaust gas is brought into contact with an absorption liquid using an alkanolamine aqueous solution in a CO 2 absorption tower to absorb CO 2 in the combustion exhaust gas, and the absorption liquid absorbing the CO 2 is heated to produce CO. In the method for purifying combustion exhaust gas in which CO 2 is expelled and regenerated in the repulsion regeneration tower and then circulated in the CO 2 absorption tower, the absorption liquid that has absorbed the CO 2 is converted into combustion exhaust gas by using a heat exchanger for heating the absorption liquid. After heating by using the retained heat and the condensation heat of the liquid vapor in the combustion gas, CO
    2 Combustion exhaust gas purification method characterized by regeneration in a drive-out regeneration tower.
  2. 【請求項2】 燃焼排ガス中の媒塵を除去する集塵機
    と、該排ガス中の硫黄酸化物を除去する脱硫装置と、該
    排ガス中のCO2 を吸収液を用いて吸収除去するCO2
    除去装置とを備えた燃焼排ガス浄化装置において、燃焼
    装置から出た直後の高温排ガスによってCO2 を吸収し
    た吸収液を加熱してCO2 追出し再生塔に送るCO2
    収液最終加熱器と、該最終加熱器で熱回収された前記排
    ガス中の媒塵を除去する集塵機と、該集塵機を出た排ガ
    スによってCO2 吸収塔から抜出したCO2 吸収液を加
    熱して排ガス中の蒸気の凝縮熱を回収するCO2 吸収液
    の第1の加熱器と、該第1加熱器を出た排ガス中の硫黄
    酸化物を除去する湿式排ガス脱硫装置と、該脱硫装置を
    出た排ガス中のCO2 を吸収液を用いて吸収除去するC
    2 吸収塔と、前記CO2 吸収液第1加熱器で加熱され
    た吸収液をCO2 追出し再生塔で再生された吸収液で加
    熱したのち前記CO2 吸収液最終加熱器に送る熱交換装
    置と、CO2 吸収液最終加熱器で加熱されたCO2 吸収
    液を受入れ該吸収液中のCO2 を除去するCO2 追出し
    再生塔とを設けたことを特徴とする燃焼排ガス浄化装
    置。
    2. A dust collector for removing dust particles in combustion exhaust gas, a desulfurization device for removing sulfur oxides in the exhaust gas, and CO 2 for absorbing and removing CO 2 in the exhaust gas by using an absorption liquid.
    In a flue gas purifying apparatus equipped with a removing device, a CO 2 absorbing solution final heater that heats an absorbing solution that has absorbed CO 2 by high-temperature flue gas immediately after it leaves the combustion apparatus and sends it to a CO 2 expelling regeneration tower, A dust collector that removes dust particles in the exhaust gas heat-recovered by the final heater, and the CO 2 absorbing liquid extracted from the CO 2 absorption tower by the exhaust gas that exits the dust collector to heat the condensation heat of the vapor in the exhaust gas. A first heater of the CO 2 absorbing liquid to be recovered, a wet exhaust gas desulfurization device for removing sulfur oxides in the exhaust gas discharged from the first heater, and absorption of CO 2 in the exhaust gas discharged from the desulfurization device Absorbs and removes using liquid C
    A heat exchange device that heats the absorption liquid heated by the O 2 absorption tower and the CO 2 absorption liquid first heater by the absorption liquid regenerated by the CO 2 discharge regeneration tower, and then sends it to the CO 2 absorption liquid final heater When the combustion exhaust gas purifying apparatus is characterized by providing a CO 2 purge regeneration tower for removing CO 2 acceptance the absorbent solution in the CO 2 absorbing liquid that has been heated by the CO 2 absorbing solution final heater.
  3. 【請求項3】 燃焼排ガス中の媒塵を除去する集塵機
    と、該排ガス中の硫黄酸化物を除去する脱硫装置と、該
    排ガス中のCO2 を吸収液を用いて吸収除去するCO2
    除去装置とを備えた燃焼排ガス浄化装置において、ボイ
    ラから出た直後の高温の排ガスによってCO2 を吸収し
    た吸収液を加熱するとともに吸収液中のCO2 を追出す
    一体型排ガス熱回収CO2 追出し塔と、該一体型排ガス
    熱回収CO2 追出し塔で熱回収された排ガスにカルシウ
    ム化合物脱硫剤と水を噴霧する装置と、該噴霧装置を出
    た排ガス中の媒塵を除去する電気集塵機と、該電気集塵
    機を出た排ガスによってCO2 吸収塔から抜出したCO
    2 吸収液を加熱して排ガス中の蒸気の凝縮熱を回収する
    CO2 吸収液の第1の加熱器と、該第1の加熱器を出た
    排ガス中の硫黄酸化物を除去する湿式排ガス脱硫装置
    と、該脱硫装置を出た排ガス中のCO2 を吸収液を用い
    て吸収除去するCO2 吸収塔と、前記CO2 吸収液第1
    加熱器で加熱された吸収液を前記一体型排ガス熱回収C
    2 追出し塔からの再生吸収液により加熱するとともに
    該一体型排ガス熱回収CO2 追出し塔に供給する熱交換
    装置とを設けたことを特徴とする燃焼排ガス浄化装置。
    3. A dust collector for removing dust particles in combustion exhaust gas, a desulfurizer for removing sulfur oxides in the exhaust gas, and CO 2 for absorbing and removing CO 2 in the exhaust gas by using an absorption liquid.
    In a combustion exhaust gas purifying apparatus equipped with a removal device, an integrated exhaust gas heat recovery CO 2 expelling method for heating the absorption liquid that has absorbed CO 2 by the high-temperature exhaust gas immediately after it leaves the boiler and expelling CO 2 in the absorption liquid A tower, an apparatus for spraying a calcium compound desulfurizing agent and water to the exhaust gas heat-recovered by the integrated exhaust gas heat recovery CO 2 drive tower, an electrostatic precipitator for removing dust particles in the exhaust gas exiting the spray apparatus, CO extracted from the CO 2 absorption tower by the exhaust gas discharged from the electric dust collector
    Wet flue gas desulfurization to remove the first heater CO 2 absorbing solution by heating the 2 absorbing solution to recover heat of condensation of the vapors in the exhaust gas, sulfur oxides in the exhaust gas exiting the first heater Apparatus, a CO 2 absorption tower that absorbs and removes CO 2 in the exhaust gas leaving the desulfurization apparatus using an absorption liquid, and the CO 2 absorption liquid first
    The integrated exhaust gas heat recovery C for absorbing liquid heated by a heater
    A combustion exhaust gas purifying device, comprising: a heat exchange device that is heated by a regenerated absorption liquid from an O 2 discharge column and is supplied to the integrated type exhaust gas heat recovery CO 2 discharge column.
JP03715994A 1994-03-08 1994-03-08 Combustion exhaust gas purification method and apparatus Expired - Fee Related JP3486220B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP03715994A JP3486220B2 (en) 1994-03-08 1994-03-08 Combustion exhaust gas purification method and apparatus

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP03715994A JP3486220B2 (en) 1994-03-08 1994-03-08 Combustion exhaust gas purification method and apparatus

Publications (2)

Publication Number Publication Date
JPH07241440A JPH07241440A (en) 1995-09-19
JP3486220B2 true JP3486220B2 (en) 2004-01-13

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Country Link
JP (1) JP3486220B2 (en)

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