JP5232361B2 - CO2 recovery device and CO2 recovery method - Google Patents

CO2 recovery device and CO2 recovery method Download PDF

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JP5232361B2
JP5232361B2 JP2006111302A JP2006111302A JP5232361B2 JP 5232361 B2 JP5232361 B2 JP 5232361B2 JP 2006111302 A JP2006111302 A JP 2006111302A JP 2006111302 A JP2006111302 A JP 2006111302A JP 5232361 B2 JP5232361 B2 JP 5232361B2
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condensed water
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JP2007284272A (en
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裕士 田中
徹 高品
琢也 平田
正樹 飯嶋
富雄 三村
靖幸 八木
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Kansai Electric Power Co Inc
Mitsubishi Heavy Industries Ltd
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    • 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
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    • 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]
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    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

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Description

本発明は、ＣＯ2除去排ガスに同伴するＣＯ2吸収液の放出量を軽減しＣＯ2吸収液の回収効率の向上を図ったＣＯ2回収装置及びＣＯ2回収方法に関する。 The present invention relates to a CO 2 recovery apparatus and a CO 2 recovery method that reduce the amount of CO 2 absorption liquid that accompanies CO 2 removal exhaust gas and improve the recovery efficiency of the CO 2 absorption liquid.

近年、地球の温暖化現象の原因の一つとして、ＣＯ2による温室効果が指摘され、地球環境を守る上で国際的にもその対策が急務となってきた。ＣＯ2の発生源としては化石燃料を燃焼させるあらゆる人間の活動分野に及び、その排出抑制への要求が一層強まる傾向にある。これに伴い大量の化石燃料を使用する火力発電所などの動力発生設備を対象に、ボイラの燃焼排ガスをアミン系ＣＯ2吸収液と接触させ、燃焼排ガス中のＣＯ2を除去、回収する方法及び回収されたＣＯ2を大気へ放出することなく貯蔵する方法が精力的に研究されている。 In recent years, the greenhouse effect due to CO 2 has been pointed out as one of the causes of global warming, and countermeasures have become urgent internationally to protect the global environment. The source of CO 2 extends to all human activity fields that burn fossil fuels, and there is a tendency for the demand for emission control to become stronger. Along with this, for a power generation facility such as a thermal power plant that uses a large amount of fossil fuel, a method for removing the CO 2 in the combustion exhaust gas by bringing the combustion exhaust gas of the boiler into contact with the amine-based CO 2 absorbent and recovering it, and A method of storing the recovered CO 2 without releasing it to the atmosphere has been energetically studied.

また前記のようなＣＯ2吸収液を用い、燃焼排ガスからＣＯ2を除去・回収する工程としては、吸収塔において燃焼排ガスとＣＯ2吸収液とを接触させる工程、ＣＯ2を吸収した吸収液を再生塔において加熱し、ＣＯ2を遊離させると共に吸収液を再生して再び吸収塔に循環して再使用するものが採用されている（特許文献１）。 Further, as a step of removing and recovering CO 2 from the combustion exhaust gas using the above-mentioned CO 2 absorption liquid, a step of bringing the combustion exhaust gas and the CO 2 absorption liquid into contact with each other in an absorption tower, an absorption liquid that has absorbed CO 2 is used. Heating is performed in a regeneration tower to liberate CO 2 and regenerate the absorption liquid, which is then recycled to the absorption tower and reused (Patent Document 1).

前記従来のＣＯ2回収装置は、図５に示すように、例えばボイラやガスタービン等の産業設備から排出されたＣＯ2を含有するＣＯ2含有排ガス１Ａを冷却水２ａによって冷却する冷却塔２と、冷却されたＣＯ2含有排ガス１ＡとＣＯ2を吸収するＣＯ2吸収液２４とを接触させてＣＯ2含有排ガス１ＡからＣＯ2を除去する吸収塔３と、ＣＯ2を吸収したＣＯ2吸収液２４からＣＯ2を放出させてＣＯ2吸収液２４を再生する再生塔９とを有する。
ここで、この装置で用いられるＣＯ2吸収液２４は、ＣＯ2を吸収したＣＯ2吸収液２４を「リッチ溶液２４Ａ」と呼称し、またリッチ溶液２４Ａから再生塔９でほぼ全てのＣＯ2が除去され再生されたＣＯ2吸収液２４を「リーン溶液２４Ｂ」と呼称する。このように、ＣＯ2吸収液２４は吸収塔３と再生塔９の間を循環しており、吸収塔３から再生塔９にはリッチ溶液２４Ａが送給され、再生塔９から吸収塔３にはリーン溶液２４Ｂが送給されている。 As shown in FIG. 5, the conventional CO 2 recovery apparatus includes a cooling tower 2 that cools CO 2 -containing exhaust gas 1A containing CO 2 discharged from industrial equipment such as a boiler and a gas turbine with cooling water 2a. , and the absorption tower 3 for removing CO 2 from contacting the CO 2 absorbing liquid 24 to absorb the cooled CO 2 containing exhaust gas 1A and CO 2 and CO 2 containing exhaust gas 1A, CO 2 absorbent having absorbed CO 2 And a regeneration tower 9 for regenerating the CO 2 absorbent 24 by releasing CO 2 from the fluid 24.
Here, the CO 2 absorbing liquid 24 used in this apparatus, the CO 2 absorbing liquid 24 that has absorbed CO 2 is called "rich solution 24A", also almost all CO 2 in the regeneration tower 9 from the rich solution 24A is The CO 2 absorbent 24 removed and regenerated is referred to as “lean solution 24B”. Thus, the CO 2 absorbent 24 circulates between the absorption tower 3 and the regeneration tower 9, and the rich solution 24 A is fed from the absorption tower 3 to the regeneration tower 9, and from the regeneration tower 9 to the absorption tower 3. Is supplied with a lean solution 24B.

この従来のＣＯ2回収装置を用いたＣＯ2回収方法では、まずＣＯ2含有排ガス１Ａは、図示しない排ガス送風機により昇圧された後、冷却塔２に送られ、ここで冷却水２ａにより冷却され、吸収塔３に送られる。 In the CO 2 recovery method using this conventional CO 2 recovery device, the CO 2 -containing exhaust gas 1A is first pressurized by an exhaust gas blower (not shown) and then sent to the cooling tower 2, where it is cooled by the cooling water 2a, It is sent to the absorption tower 3.

前記吸収塔３において、ＣＯ2含有排ガス１Ａは、吸収塔３の下部側に設けられたＣＯ2回収部４において、例えばアルカノールアミンをベースとするＣＯ2吸収液２４と対向流接触し、ＣＯ2含有排ガス１Ａ中のＣＯ2は、化学反応（Ｒ−ＮＨ2＋Ｈ2Ｏ＋ＣＯ2→Ｒ−ＮＨ3ＨＣＯ3）によりＣＯ2吸収液２４に吸収される。
そしてＣＯ2除去後のＣＯ2除去排ガス１Ｂは水洗部５を上昇し、水洗部５の頂部から供給される水（水貯槽６からの供給水）又はＣＯ2吸収液回収用水２２と気液接触して、ＣＯ2除去排ガス１Ｂに同伴するＣＯ2吸収液２４を水（水貯槽６からの供給水）又はＣＯ2吸収液回収用水２２に回収する。その後、吸収塔３の頂部からＣＯ2吸収液２４の除去されたＣＯ2吸収液除去排ガス１Ｃが排出される。リッチ溶液２４Ａは、図示しないリッチソルベントポンプにより昇圧され、リッチ・リーン溶液熱交換器８において、再生塔９で再生されたリーン溶液２４Ｂにより加熱され、再生塔９に供給される。 In the absorption tower 3, CO 2 containing exhaust gas. 1A, in the CO 2 recovery unit 4 provided on the lower side of the absorption tower 3, for example an alkanolamine contact the CO 2 absorbing liquid 24 and a counter-flow based, CO 2 CO 2 in the contained exhaust gas 1A is absorbed in the CO 2 absorbent 24 by a chemical reaction (R—NH 2 + H 2 O + CO 2 → R—NH 3 HCO 3 ).
The CO 2 flue gas 1B after CO 2 removal increased the washing unit 5, (supply water from the water reservoir 6) water supplied from the top of the washing unit 5 or CO 2 absorbing solution recovered water 22 and gas-liquid contact Then, the CO 2 absorption liquid 24 accompanying the CO 2 removal exhaust gas 1B is recovered in water (supply water from the water storage tank 6) or CO 2 absorption liquid recovery water 22. Thereafter, the CO 2 absorbent-removed exhaust gas 1C from which the CO 2 absorbent 24 has been removed is discharged from the top of the absorption tower 3. The rich solution 24A is pressurized by a rich solvent pump (not shown), heated by the lean solution 24B regenerated in the regeneration tower 9 in the rich / lean solution heat exchanger 8, and supplied to the regeneration tower 9.

前記再生塔９の上部から再生塔９内部に放出されたリッチ溶液２４Ａは、吸熱により、大部分のＣＯ2を放出する。再生塔９内で一部または大部分のＣＯ2を放出したＣＯ2吸収液２４は「セミリーン溶液」と呼称される。この図示しないセミリーン溶液は、再生塔９底部に至る頃には、ほぼ全てのＣＯ2が除去されたリーン溶液２４Ｂとなる。このリーン溶液２４Ｂは図示しない再生加熱器で図示しない飽和スチームにより加熱される。 The rich solution 24A released from the top of the regeneration tower 9 into the regeneration tower 9 releases most of the CO 2 by endotherm. The CO 2 absorbent 24 that has released a part or most of the CO 2 in the regeneration tower 9 is referred to as a “semi-lean solution”. This semi-lean solution (not shown) becomes a lean solution 24B from which almost all of the CO 2 has been removed by the time it reaches the bottom of the regeneration tower 9. This lean solution 24B is heated by saturated steam (not shown) by a regenerative heater (not shown).

一方、再生塔９の塔頂部からは塔内においてリッチ溶液２４Ａ及び図示しないセミリーン溶液から水蒸気を伴ったＣＯ2ガス２６が放出される。そして、水蒸気を伴ったＣＯ2ガス２６が導出され、コンデンサ１０により水蒸気が凝縮され、分離ドラム１１にて水が分離され、ＣＯ2ガス２８が系外に放出されて回収される。分離ドラム１１にて分離された水は図示しない凝縮水循環ポンプにて再生塔９の上部に供給される。また残りの水はＣＯ2吸収液回収用水２２として水洗部５の頂部に供給され、ＣＯ2除去排ガス１Ｂに同伴するＣＯ2吸収液２４を吸収する。 On the other hand, from the top of the regeneration tower 9, CO 2 gas 26 accompanied by water vapor is released from the rich solution 24A and a semi-lean solution (not shown) in the tower. Then, the CO 2 gas 26 accompanied with the water vapor is led out, the water vapor is condensed by the condenser 10, the water is separated by the separation drum 11, and the CO 2 gas 28 is discharged out of the system and collected. The water separated by the separation drum 11 is supplied to the upper part of the regeneration tower 9 by a condensed water circulation pump (not shown). The remaining water is fed to the top of the washing unit 5 as the CO 2 absorbing liquid recovery water 22, to absorb the CO 2 absorbing liquid 24 accompanying the CO 2 flue gas 1B.

水貯槽６に貯蔵された水の一部は流量計１６により流量を測定し、調節弁１７により所定量の水がＣＯ2回収部４へ供給され、残りの水は水洗部５の頂部へ供給される。 A part of the water stored in the water storage tank 6 is measured by a flow meter 16, and a predetermined amount of water is supplied to the CO 2 recovery unit 4 by the control valve 17, and the remaining water is supplied to the top of the flush unit 5. Is done.

なお、図５中、前記ＣＯ2回収装置は、既設の排ガス源からＣＯ2を回収するために後付で設けられる場合と、新設排ガス源に同時付設される場合とがある。 In FIG. 5, the CO 2 recovery device may be provided later in order to recover CO 2 from an existing exhaust gas source, or may be provided at the same time as a new exhaust gas source.

特開平１０−２０２０５４号公報Japanese Patent Laid-Open No. 10-202054

ここで、例えば吸収塔３内に供給される導入されるＣＯ2含有排ガス１Ａは、冷却塔２を通過することにより４０℃前後に冷却される。そしてＣＯ2回収部４を通過したＣＯ2除去排ガス１Ｂは６０℃を超えるような高い温度となり、水洗部５においてＣＯ2除去排ガス１Ｂに同伴するＣＯ2吸収液２４が水に回収されて冷却される。そして、ＣＯ2除去排ガス１Ｂに同伴するＣＯ2吸収液２４が回収されたＣＯ2吸収液除去排ガス１Ｃは４０℃前後となる。 Here, for example, the introduced CO 2 -containing exhaust gas 1 </ b > A supplied into the absorption tower 3 is cooled to around 40 ° C. by passing through the cooling tower 2. The CO 2 flue gas 1B having passed through the CO 2 recovery unit 4 becomes a high temperature exceeding 60 ° C., CO 2 absorbing liquid 24 accompanying the CO 2 flue gas 1B is cooled is recovered in water at washing unit 5 The Then, the CO 2 absorbing liquid removing gas 1C to the CO 2 absorbing liquid 24 accompanying the CO 2 flue gas 1B was recovered becomes longitudinal 40 ° C..

しかしながら、通常４０℃程度で吸収塔３に供給されるＣＯ2含有排ガス１Ａが、冷却塔２で十分に冷却されずＣＯ2含有排ガス１Ａの温度が４５〜５５℃に上昇する場合があるが、前記ＣＯ2回収装置では、水貯槽６が吸収塔３の外に配置されており、液保有量が多いため、吸収塔３に供給されるＣＯ2含有排ガス１Ａの温度が変化して急激に上昇した場合等には、吸収塔３から排出されるＣＯ2吸収液除去排ガス１Ｃに同伴するＣＯ2吸収液２４の外効への放出量が増大する、という問題がある。 However, the CO 2 -containing exhaust gas 1A normally supplied to the absorption tower 3 at about 40 ° C. may not be sufficiently cooled by the cooling tower 2 and the temperature of the CO 2 -containing exhaust gas 1A may rise to 45 to 55 ° C., In the CO 2 recovery device, the water storage tank 6 is disposed outside the absorption tower 3 and has a large amount of liquid, so the temperature of the CO 2 -containing exhaust gas 1A supplied to the absorption tower 3 changes and rises rapidly. the like when you, the amount of emitted out effect of the CO 2 absorbing liquid 24 to be entrained in the CO 2 absorbing solution removed exhaust gas 1C discharged from the absorption tower 3 increases, there is a problem that.

本発明は、前記問題に鑑み、ＣＯ2除去排ガスに同伴するＣＯ2吸収液の放出量を軽減しＣＯ2吸収液の回収効率を一層向上させたＣＯ2回収装置及びＣＯ2回収方法を提供することを課題とする。 In view of the above problems, the present invention provides a CO 2 recovery device and a CO 2 recovery method that reduce the amount of CO 2 absorption liquid that accompanies CO 2 removal exhaust gas and further improve the recovery efficiency of the CO 2 absorption liquid. This is the issue.

上述した課題を解決するための本発明の第１の発明は、ＣＯ2を含有する排ガスとＣＯ2吸収液とを接触させてＣＯ2を除去する吸収塔と、ＣＯ2を吸収したリッチ溶液を再生する再生塔と、前記再生塔でＣＯ2が除去されたリーン溶液を吸収塔で再利用するＣＯ2回収装置であって、前記吸収塔が、ＣＯ2吸収液で排ガス中のＣＯ2を吸収するＣＯ2回収部と、前記ＣＯ2回収部の上部側に設けられ、ＣＯ2を除去したＣＯ 2 除去排ガスを冷却すると共に、同伴するＣＯ2吸収液を凝縮水で回収する凝縮水受部を有する水洗部と、前記水洗部で凝縮されたＣＯ2吸収液を含む凝縮水を、前記水洗部の頂部から直接循環する循環ラインと、前記再生塔から前記吸収塔へ前記リーン溶液を供給するリーン溶液供給管に、前記ＣＯ2吸収液を含む凝縮水の余剰分を供給する余剰凝縮水供給ラインと、前記水洗部内の凝縮水を回収する凝縮水受部に、前記ＣＯ 2 吸収液を含む凝縮水の液面を測定する液面計測部とを具備することを特徴とするＣＯ2回収装置にある。 The first aspect of the present invention to solve the above problems, an absorption tower for removing CO 2 by contacting the exhaust gas and the CO 2 absorbing solution containing CO 2, the rich solution that has absorbed CO 2 A regeneration tower for regenerating and a CO 2 recovery device for reusing the lean solution from which CO 2 has been removed in the regeneration tower in an absorption tower, wherein the absorption tower absorbs CO 2 in exhaust gas with a CO 2 absorbent. and the CO 2 recovery unit for the provided on the upper side of the CO 2 recovery unit, to cool the CO 2 removal exhaust gas to remove CO 2, the condensed-water receiver for collecting the entrained CO 2 absorbing solution in the condensed water supplying a washing section, the condensed water containing CO 2 absorbing liquid that has been condensed in the water-washing section, a circulation line that circulates directly from the top of the washing section, the lean solution to the absorption tower from the regeneration tower having the lean-solution supply pipe, over the condensed water containing the CO 2 absorbing solution Min and the surplus condensed water supplying line for supplying, to the condensed-water receiver for collecting the condensed water in the washing unit, be provided with a liquid level measuring portion for measuring the liquid level of the condensed water containing the CO 2 absorbing solution It is in the CO 2 recovery device characterized by this.

第２の発明は、第１の発明において、前記余剰凝縮水供給ラインが、前記循環ラインの一部から分岐していることを特徴とするＣＯ2回収装置にある。 A second invention is the CO 2 recovery apparatus according to the first invention, wherein the surplus condensed water supply line is branched from a part of the circulation line.

第３の発明は、ＣＯ2を含有するガスとＣＯ2吸収液とを接触させてＣＯ2を除去する吸収塔と、ＣＯ2を吸収したリッチ溶液を再生する再生塔と、前記再生塔でＣＯ2が除去されたリーン溶液を吸収塔で再利用するＣＯ2回収方法であって、排ガス中のＣＯ2を吸収するＣＯ2回収部の上部側に設けられた水洗部において、ＣＯ2を除去したガスから回収されたＣＯ2吸収液を含む凝縮水を循環ラインに直接供給し、前記ＣＯ2吸収液を含む凝縮水を用いてＣＯ2が除去されたガスの冷却と同伴するＣＯ2吸収液の回収とを行うと共に、前記ＣＯ2吸収液を含む凝縮水を前記水洗部内の凝縮水受部で液面計測し、その余剰分を余剰凝縮水供給ラインにより、前記再生塔から前記吸収塔へ供給するリーン溶液へ供給することを特徴とするＣＯ2回収方法にある。 A third invention is an absorption tower for removing CO 2 by contacting the gas with CO 2 absorbing liquid containing CO 2, and regeneration tower for reproducing rich solution that has absorbed CO 2, CO in the regenerator A CO 2 recovery method in which the lean solution from which 2 has been removed is reused in an absorption tower, wherein CO 2 is removed in a water washing section provided on the upper side of the CO 2 recovery section that absorbs CO 2 in exhaust gas. the condensed water containing CO 2 absorbing liquid that has been recovered from the gas was supplied directly to the circulation line, the CO 2 absorbing liquid CO 2 is accompanied by cooling of the gas which is removed with the condensed water containing the CO 2 absorbing solution In addition to performing recovery, the liquid level of the condensed water containing the CO 2 absorption liquid is measured at the condensed water receiving section in the washing section, and the surplus is supplied from the regeneration tower to the absorption tower through an excess condensed water supply line. CO 2 recovery method, characterized by supplying to the lean solution A.

本発明によれば、水洗部で凝縮されたＣＯ 2 吸収液を含む凝縮水を水洗部の頂部から直接循環する循環ラインと、リーン溶液供給管に前記ＣＯ 2 吸収液を含む凝縮水の余剰分を直接供給する余剰凝縮水供給ラインとを具備している。これにより、ＣＯ 2 吸収液を含む凝縮水を直接循環ラインに供給し、常時循環させることができるため、吸収塔に供給されるＣＯ 2 含有排ガスの温度が変化して急激に上昇した場合等でもＣＯ 2 除去排ガスに同伴するＣＯ 2 吸収液を回収することができる。また水洗部の凝縮水受部において凝縮されたＣＯ 2 吸収液を含む凝縮水の余剰分は余剰凝縮水供給ラインを介してリーン溶液供給管に供給して、リーン溶液と共にＣＯ 2 吸収液としても用いることができる。その結果前記ＣＯ 2 吸収液のロスを低減することができる。 According to the present invention, the circulation line that circulates the condensed water containing the CO 2 absorbing liquid condensed in the washing part directly from the top of the washing part, and the excess of the condensed water containing the CO 2 absorbing liquid in the lean solution supply pipe And a surplus condensed water supply line for directly supplying water. As a result, the condensed water containing the CO 2 absorption liquid can be directly supplied to the circulation line and constantly circulated . Therefore, even when the temperature of the CO 2 -containing exhaust gas supplied to the absorption tower changes and rises rapidly, etc. the CO 2 absorbing solution accompanying the CO 2 flue gas can be recovered. Moreover, the excess of the condensed water containing the CO 2 absorption liquid condensed in the condensed water receiving part of the water washing part is supplied to the lean solution supply pipe through the excess condensed water supply line, and can be used as the CO 2 absorption liquid together with the lean solution. Can be used. As a result, the loss of the CO 2 absorbent can be reduced.

以下、この発明につき図面を参照しつつ詳細に説明する。なお、この実施例によりこの発明が限定されるものではない。また、下記実施例における構成要素には、当業者が容易に想定できるもの、あるいは実質的に同一のものが含まれる。   Hereinafter, the present invention will be described in detail with reference to the drawings. Note that the present invention is not limited to the embodiments. In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art or those that are substantially the same.

本発明による実施例１に係るＣＯ2回収装置について、図１を参照して説明する。
図１は、本発明にかかるＣＯ2回収装置の実施例１の概略図である。図中、前記図５に示した装置と同一構成には同一符号を付して重複した説明は省略する。 A CO 2 recovery apparatus according to Embodiment 1 of the present invention will be described with reference to FIG.
FIG. 1 is a schematic view of Example 1 of a CO 2 recovery apparatus according to the present invention. In the figure, the same components as those shown in FIG.

図１に示すように、本実施例にかかるＣＯ2回収装置１００Ａは、ＣＯ2を含有するＣＯ2含有排ガス１ＡとＣＯ2吸収液（リーン溶液２４Ｂ）とを接触させてＣＯ2を除去する吸収塔３と、ＣＯ2を吸収したＣＯ2吸収液（リッチ溶液２４Ａ）を再生する再生塔９と、前記再生塔９でＣＯ2が除去されたリーン溶液２４Ｂを吸収塔３で再利用するＣＯ2回収装置であって、前記吸収塔３が、ＣＯ2吸収液２４（リーン溶液２４Ｂ）でＣＯ2含有排ガス１Ａ中のＣＯ2を吸収するＣＯ2回収部４と、前記ＣＯ2回収部４の上部側に設けられ、ＣＯ2除去排ガス１Ｂを冷却すると共に、同伴するＣＯ2吸収液２４を回収する水洗部５と、前記水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を前記水洗部５の頂部から直接循環する循環ラインＬ1と、前記再生塔９から前記吸収塔３へ前記リーン溶液２４Ｂを供給するリーン溶液供給管Ｌ0に、前記ＣＯ2吸収液２４を含む凝縮水３３の余剰分３４を供給する余剰凝縮水供給ラインＬ2とを具備してなるものである。 As shown in FIG. 1, CO 2 recovery apparatus 100A according to this embodiment, CO 2 containing exhaust gas 1A and CO 2 absorbing solution containing CO 2 with (lean solution 24B) and contacting the CO 2 removal absorption a tower 3, a regeneration tower 9 for reproducing CO 2 absorbent having absorbed CO 2 (the rich solution 24A), to reuse the lean solution 24B which CO 2 has been removed by the regeneration tower 9 in the absorption tower 3 CO 2 a recovery device, the absorption tower 3, and CO 2 absorbing liquid 24 CO 2 recovery unit 4 that absorbs CO 2 in the CO 2 containing exhaust gas 1A in (lean solution 24B), the upper portion of the CO 2 recovery unit 4 provided on the side, to cool the CO 2 flue gas 1B, the water-washing section 5 for collecting the CO 2 absorbing liquid 24 entrained, the condensed water 33 containing the CO 2 absorbing liquid 24 that has been condensed in the water-washing section 5 a circulation line L 1 which circulates directly from the top of the washing unit 5 The regeneration tower to the lean-solution supply pipe L 0 supplies the lean solution 24B to the absorption tower 3 through 9, the CO 2 absorbing solution surplus condensed water supplying line L 2 supplies the surplus 34 of the condensed water 33 containing 24 It comprises.

また、本実施例では、水洗部５の下部側には前記ＣＯ2吸収液２４を含む凝縮水３３を回収する凝縮水受部４０と前記ＣＯ2吸収液２４を含む凝縮水３３の液面を測定する液面計測部５０とが具備されている。これにより水洗部５においては前記ＣＯ2吸収液２４を含む凝縮水３３がオーバーフローしないように水洗部５内の凝縮水受部４０における前記ＣＯ2吸収液を含む凝縮水３３の液面を測定している。 Further, in this embodiment, the liquid level of the condensate 33 in the lower side including the CO 2 absorbing liquid 24 and condensed water receiving portion 40 for collecting the condensed water 33 containing the CO 2 absorbing solution 24 in the washing unit 5 A liquid level measuring unit 50 for measurement is provided. Thereby, the liquid level of the condensed water 33 containing the CO 2 absorbing solution in the condensed water receiving unit 40 in the washing unit 5 is measured so that the condensed water 33 containing the CO 2 absorbing solution 24 does not overflow in the washing unit 5. ing.

また、リーン溶液２４Ｂは再生塔９から吸収塔３にリーン溶液供給管Ｌ0により供給されている。そして、前記リッチ溶液供給管３５には、前記リーン溶液２４Ｂの余熱によりリッチ溶液２４Ａを加熱するリッチ・リーン溶液熱交換器８が設けられている。 Further, the lean solution 24B is supplied by the lean-solution supply pipe L 0 into the absorber 3 from the regeneration tower 9. The rich solution supply pipe 35 is provided with a rich / lean solution heat exchanger 8 for heating the rich solution 24A by the residual heat of the lean solution 24B.

本実施例においては、水洗部５で凝縮されたＣＯ2吸収液を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1と、リーン溶液供給管Ｌ0に前記ＣＯ2吸収液２４を含む凝縮水３３の余剰分３４を直接供給する余剰凝縮水供給ラインＬ2を具備している。これにより、ＣＯ2吸収液２４を含む凝縮水３３を直接循環ラインＬ1に供給し、常時循環させることができるため、吸収塔３に供給されるＣＯ2含有排ガス１Ａの温度が変化して急激に上昇した場合等でもＣＯ2除去排ガス１Ｂに同伴するＣＯ2吸収液２４を回収することができる。また水洗部５の凝縮水受部４０において凝縮されたＣＯ2吸収液２４を含む凝縮水３３の余剰分３４は余剰凝縮水供給ラインＬ2を介してリーン溶液供給管Ｌ0に供給して、リーン溶液２４Ｂと共にＣＯ2吸収液２４としても用いることができる。その結果前記ＣＯ2吸収液２４のロスを低減することができる。 In the present embodiment, a circulation line L 1 which circulates directly condensed water 33 containing the CO 2 absorbing liquid that has been condensed from the top of the washing unit 5 in the washing unit 5, the CO 2 absorbing solution to the lean-solution supply pipe L 0 The surplus condensate supply line L 2 for directly supplying the surplus 34 of the condensate 33 including 24 is provided. As a result, the condensed water 33 containing the CO 2 absorbent 24 can be directly supplied to the circulation line L 1 and constantly circulated, so that the temperature of the CO 2 -containing exhaust gas 1A supplied to the absorption tower 3 changes rapidly. it can also be recovered CO 2 absorbing liquid 24 accompanying the CO 2 flue gas 1B in such case rose to. Further, the surplus portion 34 of the condensed water 33 containing the CO 2 absorbent 24 condensed in the condensed water receiving portion 40 of the water washing section 5 is supplied to the lean solution supply pipe L 0 via the excess condensed water supply line L 2 . It can be used as the CO 2 absorbent 24 together with the lean solution 24B. As a result, the loss of the CO 2 absorbent 24 can be reduced.

この結果、本実施例によれば、吸収塔３に供給されるＣＯ2含有排ガス１Ａの温度が変化して急激に上昇した場合などにおいても、水洗部５内でＣＯ2除去排ガス１Ｂに同伴するＣＯ2吸収液２４を回収することができる。更に吸収塔３内で使用するＣＯ2吸収液２４のロスも低減することができる。 As a result, according to the present embodiment, even when the temperature of the CO 2 -containing exhaust gas 1A supplied to the absorption tower 3 changes and rapidly increases, the CO 2 removal exhaust gas 1B is accompanied in the water washing section 5. The CO 2 absorbent 24 can be recovered. Furthermore, the loss of the CO 2 absorbent 24 used in the absorption tower 3 can be reduced.

また、本実施例においては、循環ラインＬ1よってＣＯ2吸収液２４を含む凝縮水３３を水洗部５内で直接循環するようにすると共に、余剰凝縮水供給ラインＬ2によって吸収塔３内だけでＣＯ2吸収液２４を含む凝縮水３３を直接循環するようにしている。その結果、前記効果に加え吸収塔３内の凝縮水３３をリッチ溶液２４Ａと共に再生塔９に供給する必要がなくなる。そのため再生塔９においてリッチ溶液２４Ａの加熱及びスチーム供給量をも低減することもでき、コストを低減することができる。更には、再生塔９のコンデンサーで必要な冷却水量の低減をも図ることができる。 In the present embodiment, the condensed water 33 containing the CO 2 absorbent 24 is directly circulated in the water washing section 5 by the circulation line L 1 and only in the absorption tower 3 by the surplus condensed water supply line L 2 . The condensed water 33 containing the CO 2 absorbent 24 is circulated directly. As a result, in addition to the above effects, it is not necessary to supply the condensed water 33 in the absorption tower 3 to the regeneration tower 9 together with the rich solution 24A. Therefore, the heating of the rich solution 24A and the steam supply amount can be reduced in the regeneration tower 9, and the cost can be reduced. Furthermore, the amount of cooling water required by the condenser of the regeneration tower 9 can be reduced.

本実施例で用いる熱交換器の種類は特に限定されるものではなく、例えばプレート熱交換器、シュエル＆チューブ熱交換器等の公知の熱交換器を用いればよい。   The kind of heat exchanger used in the present embodiment is not particularly limited, and for example, a known heat exchanger such as a plate heat exchanger or a shell & tube heat exchanger may be used.

また、本発明で使用できるＣＯ2 吸収液２４としては特に限定されるものではないが、アルカノールアミンやアルコール性水酸基を有するヒンダードアミン類を例示することができる。このようなアルカノールアミンとしてはモノエタノールアミン、ジエタノールアミン、トリエタノールアミン、メチルジエタノールアミン、ジイソプロパノールアミン、ジグリコールアミンなどを例示することができるが、通常モノエタノールアミン（ＭＥＡ）が好んで用いられる。またアルコール性水酸基を有するヒンダードアミンとしては２−アミノ−２−メチル−１−プロパノール（ＡＭＰ）、２−（エチルアミノ）−エタノール（ＥＡＥ）、２−（メチルアミノ）−エタノール（ＭＡＥ）、２−（ジエチルアミノ）−エタノール（ＤＥＡＥ）などを例示できる。 Further, the CO 2 absorbent 24 that can be used in the present invention is not particularly limited, and examples thereof include alkanolamines and hindered amines having an alcoholic hydroxyl group. Examples of such alkanolamines include monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diisopropanolamine, and diglycolamine, but monoethanolamine (MEA) is usually preferred. Examples of the hindered amine having an alcoholic hydroxyl group include 2-amino-2-methyl-1-propanol (AMP), 2- (ethylamino) -ethanol (EAE), 2- (methylamino) -ethanol (MAE), 2- (Diethylamino) -ethanol (DEAE) etc. can be illustrated.

［試験例１］
次に、冷却塔２の出口のガス温度が変化した場合に冷却塔２の出口のガス温度が通常の状態に落ち着くまでの間に吸収塔３からＣＯ2吸収液除去排ガス１Ｃに同伴して放出されてしまうＣＯ2吸収液２４であるアミン量の試験結果について説明する。 [Test Example 1]
Next, when the gas temperature at the outlet of the cooling tower 2 is changed, the gas at the outlet of the cooling tower 2 is discharged from the absorption tower 3 along with the CO 2 absorbent-removed exhaust gas 1C until it settles to a normal state. The test result of the amount of amine that is the CO 2 absorbent 24 that will be performed will be described.

［試験例１の反応条件］
試験例１は、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1と、ＣＯ2吸収液を含む凝縮水３３の余剰水をリーン溶液供給管Ｌ0に供給する余剰凝縮水供給ラインＬ2とを具備してなるものである。
また、比較例１は、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1を有しない従来型の図５に対応するものである。 [Reaction conditions of Test Example 1]
Test Example 1 is a circulation line L 1 for directly circulating the condensed water 33 containing the CO 2 absorbing solution 24 condensed in the washing unit 5 from the top of the washing unit 5, and surplus water of the condensed water 33 containing the CO 2 absorbing solution. Is provided with a surplus condensed water supply line L 2 for supplying to the lean solution supply pipe L 0 .
In Comparative Example 1, which corresponds to a conventional 5 having no circulation line L 1 which circulates directly condensed water 33 containing the CO 2 absorbing liquid 24 that has been condensed in the washing unit 5 from the top of the washing unit 5 It is.

ＣＯ2吸収液を含む凝縮水３３の液面を計測する液面計測部５０は、試験例１では吸収塔３内の水洗部５を設け、比較例１では吸収塔３外の図５に示す水貯槽６を設けた。
また、水洗部５内のＣＯ2吸収液２４を含む凝縮水３３の保存される液量については、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1を有しない比較例１において水洗部５のＣＯ2吸収液２４を含む凝縮水３３の保存される液量を基準値として１としたとき、循環ラインＬ1と余剰凝縮水供給ラインＬ2とを有する試験例１における水洗部５のＣＯ2吸収液２４を含む凝縮水３３の保液量を０．１とした。
試験例１と比較例１のＣＯ2吸収液２４を含む凝縮水３３の液面を計測する液面計測部５０を設けた位置と水洗部５内のＣＯ2吸収液２４を含む凝縮水３３の保存される液量とを、下記表１に示す。
尚、表１では、試験例１及び比較例１とのＣＯ2吸収液除去排ガス１Ｃに同伴して放出されたロス分のアミン量の比についても併せて示す。 The liquid level measuring unit 50 for measuring the liquid level of the condensed water 33 containing the CO 2 absorbing liquid is provided with the water washing unit 5 in the absorption tower 3 in Test Example 1 and shown in FIG. 5 outside the absorption tower 3 in Comparative Example 1. A water storage tank 6 was provided.
Also, the conserved liquid amount of the condensed water 33 containing the CO 2 absorbing liquid 24 in the washing section 5, the condensed water 33 containing the CO 2 absorbing liquid 24 that has been condensed in the washing unit 5 from the top of the washing unit 5 In Comparative Example 1 that does not have a circulation line L 1 that circulates directly, when the amount of the condensate 33 that contains the CO 2 absorbent 24 of the water washing section 5 is 1 as a reference value, the circulation line L 1 and the excess condensation The liquid retention amount of the condensed water 33 containing the CO 2 absorbent 24 of the water washing section 5 in Test Example 1 having the water supply line L 2 was set to 0.1.
Test Example 1 and Comparative Example 1 of the CO 2 absorbing liquid 24 condensed water 33 containing the CO 2 absorbing liquid 24 of the liquid level of the condensed water 33 and a position in which a liquid level measuring unit 50 for measuring the water washing unit 5 comprising The amount of liquid to be stored is shown in Table 1 below.
Table 1 also shows the ratio of the amine amount of the loss released along with the CO 2 absorbing liquid-removed exhaust gas 1C in Test Example 1 and Comparative Example 1.

Figure 0005232361
Figure 0005232361

［試験例１でのＣＯ2吸収液回収性能］
ＣＯ2吸収液回収性能として、冷却塔２の出口温度を５５℃から３５℃とした時点から冷却塔２の出口のガス温度が３５℃程度の通常状態のときにＣＯ2吸収液除去排ガス１Ｃに同伴して放出されるアミン量（定常値）の状態に落ち着くまでの間にＣＯ2吸収液除去排ガス１Ｃに同伴して排出されてしまうアミン量について検討した。 [CO 2 absorbent recovery performance in Test Example 1]
As the CO 2 absorbing liquid recovery performance, the CO 2 absorbing liquid removing exhaust gas 1C is used when the gas temperature at the outlet of the cooling tower 2 is in a normal state of about 35 ° C. from the time when the outlet temperature of the cooling tower 2 is changed from 55 ° C. to 35 ° C. The amount of amine discharged along with the CO 2 absorbent-removed exhaust gas 1C until the state of the amount of amine released along with it (steady value) settled was examined.

水洗部５から排出されるＣＯ2吸収液除去排ガス１Ｃの温度は、冷却塔２の出口ガス温度に依存する。
そして冷却塔２の出口ガス温度が５５℃のときの運転条件に対し、冷却塔２の出口ガス温度が３５℃のときではＣＯ2除去排ガス１Ｂ中の水分の凝縮量が多いため、水洗部５に供給されるＣＯ 2 除去排ガス１Ｂに同伴される水中のＣＯ2吸収液の濃度は低くなる。
水洗部５に供給されるＣＯ 2 除去排ガス１Ｂに同伴される水中のＣＯ2吸収液の濃度が低くなれば、水洗部５から排出されるＣＯ2吸収液除去排ガス１Ｃ中のＣＯ2吸収液の濃度も低くなる。 Temperature of the CO 2 absorbing liquid removing gas 1C discharged from the water washing section 5 depends on the outlet gas temperature of the cold却塔2.
And when the outlet gas temperature of the cooling tower 2 is 55 ° C., when the outlet gas temperature of the cooling tower 2 is 35 ° C., the amount of condensed water in the CO 2 removal exhaust gas 1B is large. The concentration of the CO 2 absorbing solution in water accompanying the CO 2 removal exhaust gas 1B supplied to the water becomes low.
The lower the concentration of CO 2 absorbing solution in water entrained in the CO 2 reducing gas 1B to be supplied to the water washing section 5, the CO 2 absorbing solution in a CO 2 absorbing solution removed exhaust gas 1C discharged from the washing unit 5 The concentration of is also lowered.

図２は冷却塔２の出口温度を５５℃から３５℃とした時点からのＣＯ2吸収液除去排ガス１Ｃ中のアミン濃度と運転時間との変化について示す。
即ち、冷却塔２の出口温度を５５℃から３５℃とした時点から冷却塔２の出口温度が３５℃程度のときにＣＯ2吸収液除去排ガス１Ｃに同伴して排出されるＣＯ2吸収液濃度（定常値）に到達するまでのＣＯ2吸収液除去排ガス１Ｃ中のＣＯ2吸収液濃度の時間変化を示すものである。 FIG. 2 shows changes in amine concentration and operating time in the CO 2 absorbent-removed exhaust gas 1C when the outlet temperature of the cooling tower 2 is changed from 55 ° C. to 35 ° C.
That, CO 2 absorbing solution concentration discharged by accompanying the CO 2 absorbing solution removed exhaust gas 1C at about 35 ° C. outlet temperature of the cooling tower 2 outlet temperature of the cooling tower 2 from the time of the 35 ° C. from 55 ° C. It shows the time variation of the CO 2 absorbing solution concentration in the CO 2 absorbing liquid removing gas 1C to reach (steady value).

図２に示すように、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1とリーン溶液供給管Ｌ0に前記ＣＯ2吸収液２４を含む凝縮水３３の余剰分３４を直接供給する余剰凝縮水供給ラインＬ2とを有する試験例１は、冷却塔２の出口温度を５５℃から３５℃に戻した時点から５時間以内には吸収塔３のＣＯ2吸収液除去排ガス１Ｃ中のアミン濃度が低くなり安定していた。 As shown in FIG. 2, the condensed water 33 containing the CO 2 absorbent 24 condensed in the water washing section 5 is directly circulated from the top of the water washing section 5 to the circulation line L 1 and the lean solution supply pipe L 0 to absorb the CO 2. Test Example 1 having an excess condensed water supply line L 2 for directly supplying an excess 34 of the condensed water 33 containing the liquid 24 is within 5 hours from the time when the outlet temperature of the cooling tower 2 is returned from 55 ° C. to 35 ° C. The amine concentration in the exhaust gas 1C for removing the CO 2 absorbent from the absorption tower 3 was low and stable.

これに対し、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1を有しない比較例１は、冷却塔２の出口温度を５５℃から３５℃とした時点から徐々に吸収塔３のＣＯ2吸収液除去排ガス１Ｃ中のアミン濃度が低くなり、冷却塔２の出口温度を５５℃から３５℃とした時点から３０時間後に循環ラインＬ1と余剰凝縮水供給ラインＬ2とを有する試験例１とほぼ同じくらいにまでＣＯ2吸収液除去排ガス１Ｃ中のアミン濃度が低くなった。 In contrast, Comparative Example 1 having no circulation line L 1 which circulates directly from the top of the washing section 5 the condensed water 33 containing the CO 2 absorbing liquid 24 that has been condensed in the washing section 5, the outlet temperature of the cooling tower 2 The amine concentration in the CO 2 absorption liquid removal exhaust gas 1C of the absorption tower 3 gradually decreases from 55 ° C. to 35 ° C., and circulates 30 hours after the cooling tower 2 outlet temperature is changed from 55 ° C. to 35 ° C. The amine concentration in the CO 2 absorbent-removed exhaust gas 1C was lowered to about the same as in Test Example 1 having the line L 1 and the surplus condensed water supply line L 2 .

また、水洗部５で凝縮されたＣＯ2吸収液を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1とリーン溶液供給管Ｌ0に前記ＣＯ2吸収液２４を含む凝縮水３３の余剰分３４を直接供給する余剰凝縮水供給ラインＬ2とを有する試験例１及び水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1を有しない比較例１について、冷却塔２の出口のガス温度が通常の状態に落ち着くまでの間に吸収塔３からＣＯ2吸収液除去排ガス１Ｃに同伴して放出されたアミン量の比を表した関係についての結果を前記表１及び図３に示す。 Further, the condensed water containing the CO 2 absorbing liquid 24 condensed water 33 containing the CO 2 absorbing liquid that has been condensed in the washing unit 5 into the circulation line L 1 and the lean-solution supply pipe L 0 circulating directly from the top of the washing unit 5 The condensed water 33 containing the CO 2 absorbent 24 condensed in the test example 1 and the water washing section 5 having the surplus condensed water supply line L 2 for directly supplying the surplus portion 34 of 33 is directly circulated from the top of the water washing section 5. Comparative example 1 having no circulation line L 1, the amine amount released by entrained from the absorption tower 3 to CO 2 absorbing solution removed exhaust gas 1C between the gas temperature to settle to the normal state at the outlet of the cooling tower 2 The results of the relationship representing the ratio are shown in Table 1 and FIG.

図３に示すように、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1を有しない比較例１において、冷却塔２の出口のガス温度が３５℃の通常の状態に落ち着くまでの間に吸収塔３からＣＯ2吸収液除去排ガス１Ｃに同伴して放出されたロス分のアミン量を基準値として１とすると、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1とリーン溶液供給管Ｌ0に前記ＣＯ2吸収液２４を含む凝縮水３３の余剰分３４を直接供給する余剰凝縮水供給ラインＬ2とを有する試験例１において、冷却塔２の出口のガス温度が３５℃の通常の状態に落ち着くまでの間に吸収塔３からＣＯ2吸収液除去排ガス１Ｃに同伴して放出されたロス分のアミン量は、０．８７となった。 As shown in FIG. 3, in the circulation line L 1 Comparative Example 1 having no circulating directly from the top of the washing section 5 the condensed water 33 containing the CO 2 absorbing liquid 24 that has been condensed in the washing section 5, a cooling tower 2 If the amount of amine released from the absorption tower 3 along with the CO 2 absorbent removal exhaust gas 1C until the gas temperature at the outlet settles to a normal state of 35 ° C. is set to 1 as a reference value, the water washing section The excess of the condensed water 33 containing the CO 2 absorbent 24 in the circulation line L 1 and the lean solution supply pipe L 0 for circulating the condensed water 33 containing the CO 2 absorbent 24 condensed in 5 directly from the top of the washing section 5 In Test Example 1 having the surplus condensed water supply line L 2 for directly supplying the fraction 34, the CO 2 absorption liquid from the absorption tower 3 until the gas temperature at the outlet of the cooling tower 2 settles to a normal state of 35 ° C. Loss released along with the removed exhaust gas 1C Amine amount became 0.87.

このように水洗部５における水中のアミン濃度の変化は、液保有量の多い比較例１に対し、循環ラインＬ1と余剰凝縮水供給ラインＬ2とを有する試験例１では、液保有量が凝縮水受部４０のみであって残りは余剰分３４としているため液保有量が少ない。そのため、水洗部５における水中のアミン濃度が短時間で通常冷却塔２の出口温度が４０℃程度のときの水洗部５における水中のアミン濃度に達することができるため、通常冷却塔２の出口温度が４０℃程度のときのＣＯ2吸収液除去排ガス１Ｃに同伴して排出されるアミン量に達することができる。 As described above, the change in the amine concentration in the water in the water washing section 5 shows that the liquid holding amount is higher in the test example 1 having the circulation line L 1 and the surplus condensed water supply line L 2 than in the comparative example 1 in which the liquid holding amount is large. Since only the condensate receiver 40 is used and the remainder is the surplus 34, the amount of liquid retained is small. Therefore, since the amine concentration in the water in the water washing part 5 can reach the amine concentration in the water in the water washing part 5 when the outlet temperature of the normal cooling tower 2 is about 40 ° C. in a short time, the outlet temperature of the normal cooling tower 2 It is possible to reach the amount of amine discharged accompanying the CO 2 absorbing liquid-removed exhaust gas 1C when is about 40 ° C.

よって、本試験例によれば、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を循環ラインＬ1を用いて循環させることにより、水洗部５で凝縮されたＣＯ2吸収液２４を含む凝縮水３３を水洗部５の頂部から直接循環する循環ラインＬ1を有しない比較例１に比べて、吸収塔３に供給されるＣＯ2含有排ガス１Ａの温度が５５℃から３５℃とした時点から早い段階で吸収塔３の出口ガス中のアミン濃度を低くし、安定させることができ、アミン放出ロス量を低減することができることが確認された。 Therefore, according to the present test example, the condensed water 33 containing the CO 2 absorbing liquid 24 condensed in the rinsing section 5 is circulated using the circulation line L 1 , whereby the CO 2 absorbing liquid condensed in the rinsing section 5. 24 as compared to having no Comparative example 1 the circulation line L 1 which circulates directly condensed water 33 from the top of the washing unit 5 comprising, 35 ° C. temperature of the CO 2 containing exhaust gas 1A supplied to the absorption tower 3 from 55 ° C. It was confirmed that the amine concentration in the outlet gas of the absorption tower 3 can be lowered and stabilized at an early stage from the point of time, and the amount of amine release loss can be reduced.

本発明による実施例２に係るＣＯ2回収装置について、図４を参照して説明する。
図４は、実施例２に係るＣＯ2回収装置を示す概念図である。なお、実施例１と同様の部材については、同一符号を付してその説明は省略する。
図４に示すように、本実施例にかかるＣＯ2回収装置１００Ｂは、余剰凝縮水供給ラインＬ2が、循環ラインＬ1の一部から分岐して構成されるものである。そのため、水洗部５の凝縮水受部４０において凝縮されたＣＯ2吸収液２４を含む凝縮水３３の余剰分３４は余剰凝縮水供給ラインＬ2のライン上に設けられているバルブ３６を開放して、余剰凝縮水供給ラインＬ2を介してリーン溶液供給管Ｌ0に供給して、リーン溶液２４Ｂと共にＣＯ2吸収液２４としても用いることができる。 A CO 2 recovery apparatus according to Embodiment 2 of the present invention will be described with reference to FIG.
FIG. 4 is a conceptual diagram illustrating a CO 2 recovery apparatus according to the second embodiment. In addition, about the member similar to Example 1, the same code | symbol is attached | subjected and the description is abbreviate | omitted.
As shown in FIG. 4, the CO 2 recovery apparatus 100B according to the present embodiment is configured such that the surplus condensed water supply line L 2 is branched from a part of the circulation line L 1 . Therefore, the excess 34 of the condensed water 33 containing the CO 2 absorbing liquid 24 condensed in the condensed water receiving unit 40 of the water washing unit 5 opens the valve 36 provided on the excessive condensed water supply line L 2. Then, it can be supplied to the lean solution supply pipe L 0 via the surplus condensed water supply line L 2 and used as the CO 2 absorbent 24 together with the lean solution 24B.

このように、循環ラインＬ1を介してＣＯ2吸収液２４を含む凝縮水３３を直接循環ラインＬ1に供給し、水洗部５内を循環させるようにすることができるため、吸収塔３に供給されるＣＯ2含有排ガス１Ａの温度が変化して急激に上昇した場合等においても、安定して水洗部５内でＣＯ2除去された排ガス１Ｂに同伴するＣＯ2吸収液２４を回収することができる。
更に循環ラインＬ1の一部から分岐するように余剰凝縮水供給ラインＬ2を設けることにより、前記ＣＯ2吸収液２４を含む凝縮水３３の余剰分３４を余剰凝縮水供給ラインＬ2を介してリーン溶液供給管Ｌ0に供給してリーン溶液２４Ｂと共にＣＯ2吸収液２４としても用いることができる。このため吸収塔３内で使用する前記ＣＯ2吸収液２４のロスを低減することができる。 Since the condensed water 33 containing the CO 2 absorbing liquid 24 through the circulation line L 1 fed directly into the circulation line L 1, can be made to circulate through the washing unit 5, the absorption tower 3 Even when the temperature of the supplied CO 2 -containing exhaust gas 1A changes and rises rapidly, the CO 2 absorbent 24 that accompanies the exhaust gas 1B from which CO 2 has been stably removed in the water washing section 5 is recovered. Can do.
Further, by providing the surplus condensed water supply line L 2 so as to branch from a part of the circulation line L 1 , the surplus portion 34 of the condensed water 33 containing the CO 2 absorbent 24 is passed through the surplus condensed water supply line L 2 . It can be supplied to the lean solution supply pipe L 0 and used as the CO 2 absorbent 24 together with the lean solution 24B. For this reason, the loss of the CO 2 absorbent 24 used in the absorption tower 3 can be reduced.

以上のように、本発明にかかるＣＯ2回収装置は、ＣＯ2吸収液を含む凝縮水を水洗部内で直接循環させる循環ラインと前記ＣＯ2吸収液を含む凝縮水の余剰分を余剰凝縮水供給ラインを用いることで、ＣＯ2除去排ガスに同伴するＣＯ2吸収液の放出量を軽減しＣＯ2吸収液の回収効率を向上させると共に、前記ＣＯ2吸収液のロスを低減することに用いて適している。 As described above, CO 2 recovery apparatus according to the present invention, the excess condensed water supply circulation line for circulating directly the surplus condensed water containing the CO 2 absorbing solution condensed water containing CO 2 absorbing solution in the washing portion by using the line, to reduce the emission of CO 2 absorbing solution accompanying the CO 2 removing gas thereby improving the recovery efficiency of the CO 2 absorbing solution, using to reduce the loss of the CO 2 absorbing solution suitable ing.

実施例１におけるＣＯ2回収装置の概略図である。1 is a schematic view of a CO 2 recovery device in Example 1. FIG. 冷却塔の出口温度を５５℃から３５℃とした時点からのＣＯ2吸収液除去排ガス中のアミン濃度と運転時間との変化について示す図である。The outlet temperature of the cooling tower is a diagram showing a change in the CO 2 absorbing solution removing amine concentration and the operating time of the exhaust gas from the time of the 35 ° C. from 55 ° C.. 試験例１及び比較例１における冷却塔の出口のガス温度が通常の状態に落ち着くまでの間に吸収塔からＣＯ2吸収液除去排ガスに同伴して放出されたアミン量の比を表した関係についての結果を示す図である。About the relationship that represents the ratio of the amount of amine released along with the CO 2 absorbent removal exhaust gas from the absorption tower until the gas temperature at the outlet of the cooling tower in Test Example 1 and Comparative Example 1 settles to the normal state. It is a figure which shows the result. 実施例２に係るＣＯ2回収装置を示す概念図である。FIG. 5 is a conceptual diagram showing a CO 2 recovery device according to a second embodiment. 従来のＣＯ2回収装置の概略図である。It is a schematic view of a conventional CO 2 recovery apparatus.

１００Ａ、１００Ｂ ＣＯ2回収装置
１Ａ ＣＯ2含有排ガス
１Ｂ ＣＯ2除去排ガス
１Ｃ ＣＯ2吸収液除去排ガス
３ 吸収塔
４ ＣＯ2回収部
５ 水洗部
６ 水貯槽
８ リッチ・リーン溶液熱交換器
９ 再生塔
１０ コンデンサ
２４ ＣＯ2吸収液
２４Ａ リッチ溶液
２４Ｂ リーン溶液
３３ ＣＯ2吸収液を含む凝縮水
３４ 余剰分
３５ リッチ溶液供給管
３６ バルブ
４０ 凝縮水受部
５０ 液面計測部
Ｌ0 リーン溶液供給管
Ｌ1 循環ライン
Ｌ2 余剰凝縮水供給ライン
100A, 100B CO 2 recovery device 1A CO 2 containing exhaust gas 1B CO 2 removal exhaust gas 1C CO 2 absorbent removal exhaust gas 3 Absorption tower 4 CO 2 recovery section 5 Water washing section 6 Water storage tank 8 Rich / lean solution heat exchanger 9 Regeneration tower 10 Capacitor 24 CO 2 absorbent 24A Rich solution 24B Lean solution 33 Condensed water containing CO 2 absorbent 34 Excess 35 Rich solution supply pipe 36 Valve 40 Condensed water receiving part 50 Liquid level measuring part L 0 Lean solution supply pipe L 1 Circulation Line L 2 surplus condensed water supply line

Claims (3)

ＣＯ2を含有する排ガスとＣＯ2吸収液とを接触させてＣＯ2を除去する吸収塔と、ＣＯ2を吸収したリッチ溶液を再生する再生塔と、前記再生塔でＣＯ2が除去されたリーン溶液を吸収塔で再利用するＣＯ2回収装置であって、
前記吸収塔が、ＣＯ2吸収液で排ガス中のＣＯ2を吸収するＣＯ2回収部と、
前記ＣＯ2回収部の上部側に設けられ、ＣＯ2を除去したＣＯ 2 除去排ガスを冷却すると共に、同伴するＣＯ2吸収液を凝縮水で回収する凝縮水受部を有する水洗部と、
前記水洗部で凝縮されたＣＯ2吸収液を含む凝縮水を、前記水洗部の頂部から直接循環する循環ラインと、
前記再生塔から前記吸収塔へ前記リーン溶液を供給するリーン溶液供給管に、前記ＣＯ2吸収液を含む凝縮水の余剰分を供給する余剰凝縮水供給ラインと、
前記水洗部内の凝縮水を回収する凝縮水受部に、前記ＣＯ 2 吸収液を含む凝縮水の液面を測定する液面計測部と
を具備することを特徴とするＣＯ2回収装置。 An absorption tower for removing CO 2 by contacting the exhaust gas and the CO 2 absorbing solution containing CO 2, and regeneration tower for reproducing rich solution that has absorbed CO 2, lean which CO 2 has been removed by the regeneration tower A CO 2 recovery device for reusing a solution in an absorption tower,
A CO 2 recovery section in which the absorption tower absorbs CO 2 in the exhaust gas with a CO 2 absorbent;
Provided on the upper side of the CO 2 recovery unit, to cool the CO 2 removal exhaust gas to remove CO 2, and water washing unit having a condensed-water receiver for collecting the entrained CO 2 absorbing solution in the condensed water,
A circulation line that circulates the condensed water containing the CO 2 absorbent condensed in the water washing section directly from the top of the water washing section;
An excess condensed water supply line for supplying an excess of condensed water containing the CO 2 absorbent to a lean solution supply pipe for supplying the lean solution from the regeneration tower to the absorption tower;
Wherein the condensed-water receiver for collecting the condensed water in the washing section, the CO 2 absorbing solution CO 2 recovery, characterized by comprising a liquid level measurement unit for measuring the liquid level of the condensate water <br/> comprising apparatus. 請求項１において、
前記余剰凝縮水供給ラインが、前記循環ラインの一部から分岐していることを特徴とするＣＯ2回収装置。 In claim 1,
The CO 2 recovery apparatus, wherein the surplus condensed water supply line branches off from a part of the circulation line. ＣＯ2を含有するガスとＣＯ2吸収液とを接触させてＣＯ2を除去する吸収塔と、ＣＯ2を吸収したリッチ溶液を再生する再生塔と、前記再生塔でＣＯ2が除去されたリーン溶液を吸収塔で再利用するＣＯ2回収方法であって、
排ガス中のＣＯ2を吸収するＣＯ2回収部の上部側に設けられた水洗部において、ＣＯ2を除去したガスから回収されたＣＯ2吸収液を含む凝縮水を循環ラインに直接供給し、前記ＣＯ2吸収液を含む凝縮水を用いてＣＯ2が除去されたガスの冷却と同伴するＣＯ2吸収液の回収とを行うと共に、前記ＣＯ2吸収液を含む凝縮水を前記水洗部内の凝縮水受部で液面計測し、その余剰分を余剰凝縮水供給ラインにより、前記再生塔から前記吸収塔へ供給するリーン溶液へ供給することを特徴とするＣＯ2回収方法。 An absorption tower for removing CO 2 by contacting the gas with CO 2 absorbing liquid containing CO 2, and regeneration tower for reproducing rich solution that has absorbed CO 2, lean which CO 2 has been removed by the regeneration tower A CO 2 recovery method for reusing a solution in an absorption tower,
In the water washing section provided on the upper side of the CO 2 recovery section that absorbs CO 2 in the exhaust gas, the condensed water containing the CO 2 absorbing liquid recovered from the gas from which CO 2 has been removed is directly supplied to the circulation line, The condensed water containing the CO 2 absorbing liquid is used to cool the gas from which CO 2 has been removed and to recover the accompanying CO 2 absorbing liquid, and the condensed water containing the CO 2 absorbing liquid is condensed into the condensed water in the washing section. A CO 2 recovery method, characterized in that the liquid level is measured at a receiving part, and the excess is supplied to a lean solution supplied from the regeneration tower to the absorption tower through an excess condensed water supply line.
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CN103143248A (en) * 2013-02-08 2013-06-12 珠海共同机械设备有限公司 System for absorbing and desorbing low-content CO2 in industrial exhaust gas
CN111747411B (en) * 2020-07-15 2021-07-20 广州市华达石化有限公司 Low-pressure low-temperature treatment method for industrial carbon dioxide gas

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