JP2010100492A - Method and apparatus for recovering carbon dioxide - Google Patents

Method and apparatus for recovering carbon dioxide Download PDF

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JP2010100492A
JP2010100492A JP2008274547A JP2008274547A JP2010100492A JP 2010100492 A JP2010100492 A JP 2010100492A JP 2008274547 A JP2008274547 A JP 2008274547A JP 2008274547 A JP2008274547 A JP 2008274547A JP 2010100492 A JP2010100492 A JP 2010100492A
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carbon dioxide
absorption liquid
chemical
liquid
gas
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Hakaru Ogawa
川 斗 小
Yukio Ohashi
橋 幸 夫 大
Tadashi Yamanaka
中 矢 山
Katsuya Yamashita
下 勝 也 山
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Toshiba Corp
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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]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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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Abstract

<P>PROBLEM TO BE SOLVED: To provide a method and an apparatus for recovering carbon dioxide, wherein energy required for expelling the carbon dioxide from an absorption liquid where the carbon dioxide is absorbed can be reduced. <P>SOLUTION: There are provided the method and the apparatus for recovering the carbon dioxide, wherein a gas containing the carbon dioxide is brought into contact with a chemical absorption liquid to remove the carbon dioxide from the gas, and the CO<SB>2</SB>-rich chemical absorption liquid where the carbon dioxide is absorbed is brought into direct contact with a physical absorption liquid to regenerate the carbon dioxide, and the carbon dioxide is separated from the physical absorption liquid. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

本発明は、二酸化炭素の回収方法および装置に係わり、とくに吸収液方式による二酸化炭素の回収方法および装置に関する。   The present invention relates to a carbon dioxide recovery method and apparatus, and more particularly to an absorption liquid type carbon dioxide recovery method and apparatus.

近年、化石燃料の燃焼生成物である二酸化炭素（以下、ＣＯ２とも表記する。）の温室効果による地球温暖化の問題が大きくなっている。気候変動に関する国際連合枠組条約の京都議定書において、わが国の温室効果ガス・排出削減目標は、1990年比でマイナス６％を2008〜2012年の間に達成することになっている。 In recent years, the problem of global warming due to the greenhouse effect of carbon dioxide (hereinafter also referred to as CO 2 ), which is a combustion product of fossil fuel, has been increasing. Under the Kyoto Protocol of the United Nations Framework Convention on Climate Change, Japan's greenhouse gas / emission reduction target is to be reduced by 6% from 2008 to 2012 between 2008 and 2012.

このような事情の下、種々の方法が提供されているが、大量の化石燃料を使用する火力発電プラント等を対象にして、燃焼排ガスとアミン系吸収液とを接触させて燃焼ガス中の二酸化炭素を分離回収する方法（アミン法）、および回収された二酸化炭素を大気中へ放出することなく貯蔵する方法の研究が進められている。   Under such circumstances, various methods have been provided. For a thermal power plant that uses a large amount of fossil fuel, the combustion exhaust gas and the amine-based absorbent are brought into contact with each other, and the carbon dioxide in the combustion gas is contacted. Research on methods for separating and recovering carbon (amine method) and methods for storing the recovered carbon dioxide without releasing it into the atmosphere is underway.

上記吸収液を用い、燃焼排ガスから二酸化炭素を分離回収する工程としては、
(1) 吸収塔において燃焼ガスと吸収液とを接触させて二酸化炭素を吸収させる工程、
(2) 二酸化炭素を吸収した吸収液を再生塔において加熱し、二酸化炭素を吸収液から追い出すとともに、吸収液を再生して吸収塔に循環させる工程と、
を含む（特許文献１参照）。
特開2004-323339号公報 As a process of separating and recovering carbon dioxide from combustion exhaust gas using the absorption liquid,
(1) a step of absorbing the carbon dioxide by bringing the combustion gas into contact with the absorbing liquid in the absorption tower;
(2) heating the absorption liquid that has absorbed carbon dioxide in the regeneration tower, expelling the carbon dioxide from the absorption liquid, regenerating the absorption liquid and circulating it to the absorption tower;
(See Patent Document 1).
JP 2004-323339 A

二酸化炭素を分離回収する工程は、既設の発電設備等に付加して設置されるため、その運転コストをできるだけ低減させる必要がある。これまでの調査結果によると、発電量の20〜30%に相当する熱エネルギーが二酸化炭素の分離回収に必要とされており、このエネルギーを低減することが要望されている。   Since the process of separating and recovering carbon dioxide is installed in addition to existing power generation facilities and the like, it is necessary to reduce its operating cost as much as possible. According to the survey results so far, thermal energy corresponding to 20 to 30% of the power generation amount is required for separation and recovery of carbon dioxide, and it is desired to reduce this energy.

特に、再生工程は、二酸化炭素を吸収した吸収液から二酸化炭素を追出すのに多量の熱エネルギーを必要とすることから、熱エネルギーをいかに最小にするかが重要である。   In particular, since the regeneration process requires a large amount of thermal energy to expel carbon dioxide from the absorbing solution that has absorbed carbon dioxide, how to minimize the thermal energy is important.

本発明は上述の点を考慮してなされたもので、二酸化炭素を吸収した吸収液から二酸化炭素を分離回収するのに必要な熱エネルギーを低減し得る二酸化炭素の回収方法および回収装置を提供することを目的とする。   The present invention has been made in consideration of the above-described points, and provides a carbon dioxide recovery method and recovery apparatus that can reduce the thermal energy required to separate and recover carbon dioxide from an absorption liquid that has absorbed carbon dioxide. For the purpose.

上記目的達成のため、本願では、下記の方法の発明および装置の発明を提供する。   In order to achieve the above object, the present invention provides the following method invention and device invention.

まず方法の発明は、
二酸化炭素を含有するガスと化学吸収液とを接触させて、前記ガスから二酸化炭素を除去し、
二酸化炭素を吸収したＣＯ２リッチな前記化学吸収液を物理吸収液と直接接触させることにより前記化学吸収液から二酸化炭素を分離して前記化学吸収液を再生する
二酸化炭素の回収方法、
である。また、装置の発明は、
二酸化炭素を含有するガスと化学吸収液とを接触させて前記ガスから二酸化炭素を除去する吸収塔と、
二酸化炭素を吸収したＣＯ２リッチな前記化学吸収液を物理吸収液との直接接触させることにより前記化学吸収液から二酸化炭素を分離して前記化学吸収液を再生する直接接触器と、
前記物理吸収液から二酸化炭素を分離する気液分離器と
をそなえた二酸化炭素の回収装置、
である。 First, the invention of the method is
Contacting a gas containing carbon dioxide with a chemical absorbent to remove carbon dioxide from the gas,
Carbon dioxide collection methods for reproducing the chemical absorbent liquid the chemical absorption liquid by separating carbon dioxide from by contacting the absorbed CO 2 rich the chemical absorption liquid carbon dioxide directly with physical absorption liquid,
It is. The invention of the device
An absorption tower for removing carbon dioxide from the gas by contacting a gas containing carbon dioxide with a chemical absorption liquid;
Direct contactor for reproducing the chemical absorption liquid by separating carbon dioxide from the chemical absorbent liquid by direct contact with the CO 2 rich said that absorb carbon dioxide chemical absorption liquid physical absorption liquid,
A carbon dioxide recovery device comprising a gas-liquid separator for separating carbon dioxide from the physical absorption liquid;
It is.

本願の発明者らは、再生塔で二酸化炭素を吸収液から追出すことは吸収液中の約５０％を占める水の蒸発が生じ、気化熱としての多大の熱エネルギーを必要としていることに着目した。   The inventors of the present application pay attention to the fact that expelling carbon dioxide from the absorption liquid in the regeneration tower causes evaporation of water occupying about 50% of the absorption liquid and requires a large amount of heat energy as heat of vaporization. did.

そこで、水を蒸発させることなく吸収液から二酸化炭素を追い出すことができれば、再生のための熱量が少なくて済む。そのために、化学吸収液の外に物理吸収液を介在させることとした。   Therefore, if carbon dioxide can be expelled from the absorbing solution without evaporating water, the amount of heat for regeneration can be reduced. Therefore, the physical absorption liquid is interposed outside the chemical absorption liquid.

本発明は上述のように、二酸化炭素を吸収したＣＯ２リッチな化学吸収液を物理吸収液と直接接触させて二酸化炭素を再生し、前記化学吸収液から二酸化炭素を分離するようにしたため、水の蒸発なく化学吸収液から二酸化炭素を追出すのに必要なエネルギーを低減することができる。 The invention as described above, since the CO 2 rich chemical absorbent that has absorbed carbon dioxide physical absorption liquid and direct the contacted playing carbon dioxide, and to separate the carbon dioxide from the chemical absorbent solution, water It is possible to reduce the energy required to expel carbon dioxide from the chemical absorption solution without evaporation.

以下、添付図面を参照して、本発明の実施例について説明する。   Embodiments of the present invention will be described below with reference to the accompanying drawings.

（実施例１）
図１は、本発明の第１の実施例の構成を示す説明図である。この実施例１は、吸収塔１と直接接触器（再生塔）３とを循環している化学吸収液を用いて吸収塔１に与えられた排ガス中のＣＯ２を吸収させた後に、物理吸収液への転移を行い、ＣＯ２を吸収した物理吸収液から気液分離によりＣＯ２を回収する。 Example 1
FIG. 1 is an explanatory diagram showing the configuration of the first embodiment of the present invention. In Example 1, the chemical absorption liquid circulating in the absorption tower 1 and the direct contactor (regeneration tower) 3 is used to absorb the CO 2 in the exhaust gas supplied to the absorption tower 1 and then the physical absorption. performing a transfer of the liquid, the CO 2 recovered by the gas-liquid separation from the physical absorbent having absorbed CO 2.

そのために、ＣＯ２を吸収した化学吸収液を直接接触器３に送り、ＣＯ２を化学吸収液から物理吸収液に移した上で物理吸収液からＣＯ２を分離し、さらに気液分離によりＣＯ２を回収するとともに、物理吸収液を直接接触器３に、また化学吸収液を吸収塔１にそれぞれ戻すように構成されている。 For this purpose, the chemical absorption liquid that has absorbed CO 2 is sent directly to the contactor 3, the CO 2 is transferred from the chemical absorption liquid to the physical absorption liquid, and then the CO 2 is separated from the physical absorption liquid. 2 is recovered, and the physical absorption liquid is directly returned to the contactor 3 and the chemical absorption liquid is returned to the absorption tower 1.

（構成）
この実施例１は、次の各要素を有する。すなわち、二酸化炭素を含有する排ガスと二酸化炭素の化学吸収液とを接触させて二酸化炭素を除去する吸収塔１と、二酸化炭素を吸収したＣＯ２リッチな化学吸収液と二酸化炭素物理吸収液とを直接接触させて化学吸収液から物理吸収液へ二酸化炭素を移動させ、二酸化炭素を排出した化学吸収液と二酸化炭素を含んだ物理吸収液とを分離させる直接接触器３と、二酸化炭素を含有した物理吸収液を減圧後に気液分離する気液分離器８と、分離された物理吸収液の含有気体から物理吸収液を凝縮回収するための冷却器１０と、気液分離器１１と、をそなえる。そして、化学吸収液または物理吸収液を循環流通させるために、ポンプ２，４，７，９，１２が各所に設けられている。 (Constitution)
Example 1 has the following elements. That is, an absorption tower 1 that removes carbon dioxide by contacting an exhaust gas containing carbon dioxide with a chemical absorption liquid of carbon dioxide, a CO 2 rich chemical absorption liquid that absorbs carbon dioxide, and a carbon dioxide physical absorption liquid. Direct contactor 3 for transferring carbon dioxide from the chemical absorption liquid to the physical absorption liquid by direct contact and separating the chemical absorption liquid from which carbon dioxide has been discharged and the physical absorption liquid containing carbon dioxide, and carbon dioxide A gas-liquid separator 8 that gas-liquid separates the physical absorption liquid after decompression, a cooler 10 for condensing and recovering the physical absorption liquid from the gas contained in the separated physical absorption liquid, and a gas-liquid separator 11 are provided. . And in order to circulate and distribute a chemical absorption liquid or a physical absorption liquid, the pumps 2, 4, 7, 9, and 12 are provided in various places.

（作用）
排ガスはまず吸収塔１に与えられ、吸収塔１で冷却器５から供給されたＣＯ２リーンな化学吸収液と接触する。これにより、排ガス中の二酸化炭素が化学吸収液に吸収され、ＣＯ２除去済みガスとして吸収塔１から外部に排出される。 (Function)
First, the exhaust gas is supplied to the absorption tower 1, and then contacts the CO 2 lean chemical absorption liquid supplied from the cooler 5 in the absorption tower 1. As a result, carbon dioxide in the exhaust gas is absorbed by the chemical absorption liquid, and discharged from the absorption tower 1 to the outside as a CO 2 -removed gas.

このとき吸収塔１内では、海水を用いた製塩プロセスにおける塩水濃縮工程と同様に、化学吸収液が排ガス中に降雨状に滴下する。そして、化学吸収液の滴表面と接触した排ガス中のＣＯ２が、化学吸収液の滴に吸収されて吸収塔１の下部に落下する。 At this time, in the absorption tower 1, the chemical absorption liquid is dripped into the exhaust gas in the form of rain as in the salt water concentration step in the salt production process using seawater. Then, CO 2 in the exhaust gas in contact with the surface of the chemical absorbing liquid drops is absorbed by the chemical absorbing liquid drops and falls to the lower part of the absorption tower 1.

吸収塔１で二酸化炭素を吸収したＣＯ２リッチな化学吸収液は、ポンプ２で昇圧後、直接接触器３でポンプ９，１２から供給されたＣＯ２リーンな物理吸収液と直接接触され、ＣＯ２は化学吸収液から物理吸収液に移動する。 The CO 2 -rich chemical absorption liquid that has absorbed carbon dioxide in the absorption tower 1 is directly brought into contact with the CO 2 -lean physical absorption liquid supplied from the pumps 9 and 12 by the direct contactor 3 after being pressurized by the pump 2, 2 moves from the chemical absorption liquid to the physical absorption liquid.

そして、二酸化炭素が移動した物理吸収液は比重が大となるため直接接触器３の下部に溜まり、二酸化炭素を物理吸収液に渡して比重が小さくなった化学吸収液は直接接触器３の上部に押し上げられる。   Since the physical absorption liquid to which carbon dioxide has moved has a large specific gravity, it accumulates directly in the lower part of the contactor 3, and the chemical absorption liquid whose specific gravity has decreased by passing carbon dioxide to the physical absorption liquid is the upper part of the direct contactor 3. Pushed up.

このように、二酸化炭素を吸収してＣＯ２リッチで比重が大きくなった物理吸収液は、二酸化炭素を放出して比重が小さくなった化学吸収液と分離されて直接接触器３の下部に溜まる。そして、この直接接触器３の下部からポンプ７で気液分離器８に供給され、ＣＯ２リーンな物理吸収液と二酸化炭素を含有した物理吸収液の蒸気とに分離される。 In this way, the physical absorption liquid that has absorbed carbon dioxide and is rich in CO 2 and has a high specific gravity is separated from the chemical absorption liquid that has released carbon dioxide and has a low specific gravity, and accumulates directly under the contactor 3. . Then, the direct contactor is supplied from the lower part of the 3 to the gas-liquid separator 8 by the pump 7 is separated into a vapor of physical absorption solution containing CO 2 lean physical absorption liquid with carbon dioxide.

気液分離器８でＣＯ２と分離されたＣＯ２リーンな物理吸収液は、ポンプ９で加圧されて直接接触器３に供給される。一方、二酸化炭素を含有する物理吸収液の蒸気は、冷却器１０で冷却された後に、気液分離器１１に送られてＣＯ２とＣＯ２リーンな物理吸収液とに分離される。 The CO 2 -lean physical absorption liquid separated from CO 2 by the gas-liquid separator 8 is pressurized by the pump 9 and directly supplied to the contactor 3. On the other hand, the vapor of the physical absorbent containing carbon dioxide, after being cooled by the cooler 10 is separated is sent to the gas-liquid separator 11 to the CO 2 and CO 2 lean physical absorption liquid.

分離されたＣＯ２リーンな物理吸収液は、ポンプ１２で加圧されて直接接触器３に還流される。直接接触器３は、ヒータ６を用いて加熱することにより、ＣＯ２リッチな化学吸収液が二酸化炭素を放出するためのエネルギーを供給する。ヒータ６としては、火力タービンの蒸気配管を利用してもよい。 The separated CO 2 lean physical absorption liquid is pressurized by the pump 12 and directly refluxed to the contactor 3. Direct contactor 3 by heating with a heater 6, and supplies the energy for CO 2 rich chemical absorption solution releases carbon dioxide. As the heater 6, a steam pipe of a thermal turbine may be used.

（効果）
従来のＣＯ２吸収システムでは、加熱してＣＯ２リッチな化学吸収液から二酸化炭素を放出するため、化学吸収液中の水が蒸発する。これに対し、本発明では、ＣＯ２リーンな物理吸収液に二酸化炭素を吸収させる工程を介在させるため、化学吸収液中の水が蒸発するほど加熱しなくてよい。この結果、ＣＯ２リッチな化学吸収液の再生エネルギーを低減できる。 (effect)
In a conventional CO 2 absorption system, carbon dioxide is released from a CO 2 rich chemical absorption liquid by heating, so that water in the chemical absorption liquid evaporates. In contrast, in the present invention, since the interposing a step of absorbing carbon dioxide in the CO 2 lean physical absorption liquid, water chemical absorption liquid may not be heated enough to evaporate. As a result, the regeneration energy of the CO 2 rich chemical absorption liquid can be reduced.

しかもこの実施例１では、直接接触器３は吸収塔１とほぼ同じ温度で運転するため、従来例に比べ化学吸収液に加えられる温度が低く、化学吸収液の熱劣化が少なくなる。   Moreover, in the first embodiment, since the direct contactor 3 is operated at substantially the same temperature as the absorption tower 1, the temperature applied to the chemical absorption liquid is lower than that of the conventional example, and thermal deterioration of the chemical absorption liquid is reduced.

また、この実施例１では、直接接触器３内にヒータ６を設置しているが、ＣＯ２リッチな化学吸収液、ＣＯ２リーンな物理吸収液を個別に加熱してもよい。また、直接接触器３が気液分離器を兼ねているが、気液分離器を別に設置してもよい。 In the first embodiment, the heater 6 is installed directly in the contactor 3, but the CO 2 rich chemical absorbent and the CO 2 lean physical absorbent may be individually heated. Further, although the direct contactor 3 also serves as a gas-liquid separator, the gas-liquid separator may be installed separately.

ここで、実施例１に用いた化学吸収液は、アミン、アミノ酸塩の水溶液を用い、また、物理吸収液は、水に対して不溶性である非極性液体（フロリナート、フッ化炭素高分子、シリコンオイル）を用いる。   Here, the chemical absorption liquid used in Example 1 is an aqueous solution of an amine or an amino acid salt, and the physical absorption liquid is a nonpolar liquid (fluorinate, fluorocarbon polymer, silicon, which is insoluble in water). Oil).

（実施例２）
図２は、本発明の第２の実施例の構成を示している。この実施例は、第１の実施例における基本構成を基に、いくつかの任意付加的要素を備えている。 (Example 2)
FIG. 2 shows the configuration of the second embodiment of the present invention. This embodiment includes some optional elements based on the basic configuration in the first embodiment.

第１に、直接接触器３の化学吸収液の出口と直接接触機３への化学吸収液の入り口との間に熱交換器１３を設けた点である。これにより、直接接触器３の出口で化学吸収液に与えられている熱エネルギーを入り口から与えられる化学吸収液に還元して熱エネルギーの利用効率を高めることができる。   First, a heat exchanger 13 is provided between the chemical absorbent liquid outlet of the direct contactor 3 and the chemical absorbent liquid inlet to the direct contactor 3. Thereby, the thermal energy given to the chemical absorption liquid at the outlet of the direct contactor 3 can be reduced to the chemical absorption liquid given from the inlet to increase the utilization efficiency of the thermal energy.

第２に、直接接触器３の出口に圧力維持弁４を設けた点である。これにより、直接接触器３を含む処理系の動作安定を図ることができる。   Second, the pressure maintaining valve 4 is provided at the outlet of the direct contactor 3. Thereby, operation | movement stability of the processing system containing the direct contactor 3 can be aimed at.

第３に、直接接触器３の頂部に繋がれた気液分離機１５およびこの気液分離機１５で分離した化学吸収液を冷却して吸収塔１に戻す冷却器１６を設けた点である。これにより、化学吸収液の循環性を向上することができる。   Thirdly, a gas-liquid separator 15 connected directly to the top of the contactor 3 and a cooler 16 that cools the chemical absorption liquid separated by the gas-liquid separator 15 and returns it to the absorption tower 1 are provided. . Thereby, the circulatory property of a chemical absorption liquid can be improved.

本発明の実施例１の構成を示す接続図。The connection diagram which shows the structure of Example 1 of this invention. 本発明の実施例２の構成を示す接続図。The connection diagram which shows the structure of Example 2 of this invention.

符号の説明Explanation of symbols

１ 吸収塔、２,４,７,９,１２ ポンプ、３ 直接接触器、５，１０ 冷却器、
６ ヒータ、８，１１ 気液分離器。 1 absorption tower, 2, 4, 7, 9, 12 pump, 3 direct contactor, 5,10 cooler,
6 Heater, 8, 11 Gas-liquid separator.

Claims (9)

二酸化炭素を含有するガスと化学吸収液とを接触させて、前記ガスから二酸化炭素を除去し、
二酸化炭素を吸収したＣＯ２リッチな前記化学吸収液を物理吸収液と直接接触させることにより前記化学吸収液から二酸化炭素を分離して前記化学吸収液を再生する
二酸化炭素の回収方法。 Contacting a gas containing carbon dioxide with a chemical absorbent to remove carbon dioxide from the gas,
Method for recovering carbon dioxide for reproducing the chemical absorption liquid by separating carbon dioxide from the chemical absorbent solution by contacting the CO 2 rich the chemical absorbent that has absorbed carbon dioxide directly with physical absorption liquid. 二酸化炭素を含有するガスと化学吸収液とを接触させて前記ガスから二酸化炭素を除去する吸収塔と、
二酸化炭素を吸収したＣＯ２リッチな前記化学吸収液を物理吸収液との直接接触させることにより前記化学吸収液から二酸化炭素を分離して前記化学吸収液を再生する直接接触器と、
前記物理吸収液から二酸化炭素を分離する気液分離器と
をそなえた二酸化炭素の回収装置。 An absorption tower for removing carbon dioxide from the gas by contacting a gas containing carbon dioxide with a chemical absorption liquid;
Direct contactor for reproducing the chemical absorption liquid by separating carbon dioxide from the chemical absorbent liquid by direct contact with the CO 2 rich said that absorb carbon dioxide chemical absorption liquid physical absorption liquid,
A carbon dioxide recovery device comprising a gas-liquid separator that separates carbon dioxide from the physical absorption liquid. 前記吸収塔の出口で前記化学吸収液を加圧して前記直接接触器へ供給することを特徴とする請求項２記載の二酸化炭素の回収装置。   The carbon dioxide recovery apparatus according to claim 2, wherein the chemical absorption liquid is pressurized at the outlet of the absorption tower and supplied to the direct contactor. 前記物理吸収液を加圧して前記直接接触器へ供給することを特徴とする請求項２または３記載の二酸化炭素の回収装置。   The carbon dioxide recovery apparatus according to claim 2 or 3, wherein the physical absorption liquid is pressurized and supplied to the direct contactor. 前記物理吸収液と前記化学吸収液とを比重差により分離することを特徴とする請求項２ないし４の何れかに記載の二酸化炭素の回収装置。   The carbon dioxide recovery device according to any one of claims 2 to 4, wherein the physical absorption liquid and the chemical absorption liquid are separated by a specific gravity difference. 前記化学吸収液が、アミン、アミノ酸塩水溶液であることを特徴とする請求項２ないし５の何れかに記載の二酸化炭素の回収装置。   6. The carbon dioxide recovery apparatus according to claim 2, wherein the chemical absorption solution is an amine or amino acid salt aqueous solution. 前記物理吸収液が、非極性液体であることを特徴とする請求項２ないし６の何れかに記載の二酸化炭素の回収装置。   The carbon dioxide recovery device according to claim 2, wherein the physical absorption liquid is a nonpolar liquid. 前記非極性液体が、シリコンオイル、フロリナート、フッ化カーボン化合物であることを特徴とする請求項７記載の二酸化炭素の回収装置。   The carbon dioxide recovery apparatus according to claim 7, wherein the nonpolar liquid is silicon oil, fluorinate, or a carbon fluoride compound. 前記直接接触器に、前記化学吸収液からの二酸化炭素分離用の熱を供給するヒータを有することを特徴とする請求項２ないし８の何れかに記載の二酸化炭素の回収装置。   The carbon dioxide recovery apparatus according to claim 2, further comprising a heater that supplies heat for carbon dioxide separation from the chemical absorption liquid to the direct contactor.
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