JP2011000528A - Co2 recovering device and co2 recovering method - Google Patents

Co2 recovering device and co2 recovering method Download PDF

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JP2011000528A
JP2011000528A JP2009144588A JP2009144588A JP2011000528A JP 2011000528 A JP2011000528 A JP 2011000528A JP 2009144588 A JP2009144588 A JP 2009144588A JP 2009144588 A JP2009144588 A JP 2009144588A JP 2011000528 A JP2011000528 A JP 2011000528A
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exhaust gas
amount
solution
absorption
recovery
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Masaki Iijima
正樹 飯嶋
Yuji Tanaka
裕士 田中
Miki Sorimachi
美樹 反町
Masahiko Tatsumi
雅彦 辰巳
Yasuyuki Yagi
靖幸 八木
Koki Ogura
幸喜 小椋
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Kansai Electric Power Co Inc
Mitsubishi Heavy Industries Ltd
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Kansai Electric Power Co Inc
Mitsubishi Heavy Industries Ltd
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Priority to JP2009144588A priority Critical patent/JP2011000528A/en
Priority to CA2689453A priority patent/CA2689453C/en
Priority to CA2779625A priority patent/CA2779625C/en
Priority to US12/649,928 priority patent/US8663363B2/en
Priority to CA2779621A priority patent/CA2779621C/en
Priority to AU2010200176A priority patent/AU2010200176B2/en
Priority to EP10151152.5A priority patent/EP2269713B1/en
Publication of JP2011000528A publication Critical patent/JP2011000528A/en
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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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • 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

Abstract

PROBLEM TO BE SOLVED: To provide a COrecovering device which can make an optimal operation when the COrecovery rate is kept constant, as well as a COrecovering method.SOLUTION: This COrecovering device comprises a COabsorption column 16 which removes COof an exhaust gas 12 by bringing the exhaust gas 12 containing COinto contact with a COabsorbing solution 15 and a regeneration column 18 which regenerates the COabsorbing solution 15 by removing COof a rich solution 17 which has absorbed COat the COabsorption column 16. That is, the COrecovering device reuses the COabsorbing solution 15 at the COabsorption column 16 as a lean solution with no COleft by removal using the regeneration column 18. In addition, the COrecovering device has a control means which measures the COconcentration (I) and the exhaust gas amount, then determines the exhaust gas amount when a target COrecovery rate is set in accordance with the COconcentration and decides the absorbing solution circulation amount according to the exhaust gas amount, and finally, performs a control process to decide the water vapor amount according to the decided absorbing solution circulation amount.

Description

本発明は、最適条件で一定のＣＯ2回収率を常に維持することができるＣＯ2回収装置及び方法に関する。 The present invention relates to a CO 2 recovery apparatus and method that can always maintain a constant CO 2 recovery rate under optimum conditions.

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。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（例えば、特許文献１参照）。 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. Moreover, as a process of removing and recovering CO 2 from the combustion exhaust gas using the CO 2 absorption liquid as described above, a process of bringing the combustion exhaust gas and the CO 2 absorption liquid into contact in an absorption tower, an absorption liquid that has absorbed CO 2 Is used in the regeneration tower to liberate CO 2 and regenerate the absorption liquid, which is then recycled to the absorption tower and reused (see, for example, Patent Document 1).

図１にＣＯ2回収装置の一例を示す。図１に示すように、ＣＯ2回収装置１０は、ボイラやガスタービン等の産業燃焼設備１１から排出されたＣＯ2とＯ2とを含有する排ガス１２を冷却水１３によって冷却する排ガス冷却装置１４と、冷却されたＣＯ2を含有する排ガス１２とＣＯ2を吸収するＣＯ2吸収液（以下、「吸収液」ともいう。）１５とを接触させて排ガス１２からＣＯ2を除去するＣＯ2回収部１６Ａを有するＣＯ2吸収塔１６と、ＣＯ2を吸収したＣＯ2吸収液（以下、「リッチ溶液」ともいう。）１７からＣＯ2を放出させてＣＯ2吸収液を再生する再生塔１８とを有する。
そして、このＣＯ2回収装置１００では、再生塔１８でＣＯ2を除去した再生ＣＯ2吸収液（以下、「リーン溶液」ともいう。）１５はＣＯ2吸収塔１６でＣＯ2吸収液として再利用する。 FIG. 1 shows an example of a CO 2 recovery device. As shown in FIG. 1, a CO 2 recovery device 10 is an exhaust gas cooling device 14 that cools an exhaust gas 12 containing CO 2 and O 2 discharged from an industrial combustion facility 11 such as a boiler or a gas turbine with cooling water 13. If, CO 2 absorbing solution for absorbing the flue gas 12 and CO 2 containing the cooled CO 2 (hereinafter, also referred to as "absorbing solution".) 15 contacting the CO 2 removal from flue gas 12 CO 2 recovery and the CO 2 absorber 16 having a part 16A, CO 2 absorbent having absorbed CO 2 (hereinafter, also referred to as "rich solvent".) 17 to release CO 2 from the regenerator 18 to regenerate the CO 2 absorbing solution Have
Then, in the CO 2 recovery apparatus 100, reproduction CO 2 absorbing solution was removed CO 2 in the regeneration tower 18 (hereinafter, also referred to as "lean solvent".) 15 reused as the CO 2 absorbing solution in the CO 2 absorber 16 To do.

この従来のＣＯ2回収装置を用いたＣＯ2回収方法では、まず、ＣＯ2を含んだボイラやガスタービン等の産業燃焼設備からの排ガス１２は、排ガス送風機２０により昇圧された後、排ガス冷却装置１４に送られ、ここで冷却水１３により冷却され、ＣＯ2吸収塔１６に送られる。 In the CO 2 recovery method using this conventional CO 2 recovery device, first, exhaust gas 12 from an industrial combustion facility such as a boiler or a gas turbine containing CO 2 is pressurized by an exhaust gas blower 20, and then an exhaust gas cooling device. 14, where it is cooled by cooling water 13 and sent to a CO 2 absorption tower 16.

前記ＣＯ2吸収塔１６において、排ガス１２はアミン系溶液をベースとするＣＯ2吸収液１５と向流接触し、排ガス１２中のＣＯ2は、化学反応によりＣＯ2吸収液１５に吸収される。
ＣＯ2回収部１６ＡでＣＯ2が除去された後のＣＯ2除去排ガスは、ＣＯ2吸収塔１６内の水洗部１６Ｂでノズルから供給されるＣＯ2吸収液を含む循環する凝縮水１９と気液接触して、ＣＯ2除去排ガスに同伴するＣＯ2吸収液１５が回収され、その後ＣＯ2が除去された排ガス２１は系外に放出される。
また、ＣＯ2を吸収したＣＯ2吸収液１７であるリッチ溶液は、リッチソルベントポンプ２２により昇圧され、リッチ／リーンソルベント熱交換器２３において、再生塔１８で再生されたＣＯ2吸収液１５であるリーン溶液により加熱され、再生塔１８に供給される。 In the CO 2 absorption tower 16, the flue gas 12 is CO 2 absorbent 15 and then countercurrent contact based on amine-based solution, CO 2 in the flue gas 12 is absorbed by the CO 2 absorbent 15 by a chemical reaction.
CO CO 2 flue gas after CO 2 is removed in 2 recovery unit 16A, and the condensed water 19 circulating containing CO 2 absorbing liquid supplied from the nozzle at the water washing section 16B in the CO 2 absorber 16 gas-liquid contact with, CO 2 absorbent 15 accompanying the CO 2 flue gas is recovered, then the exhaust gas 21 from which CO 2 has been removed is released out of the system.
Further, the rich solution is CO 2 absorbing liquid 17 that has absorbed CO 2, is boosted by a rich solvent pump 22, in the rich / lean solvent heat exchanger 23, is CO 2 absorbent 15 that is reproduced by the regenerator 18 It is heated by the lean solution and supplied to the regeneration tower 18.

再生塔１８の上部から内部に放出されたリッチ溶液は、吸熱反応を生じて、大部分のＣＯ2を放出する。再生塔１８内で一部または大部分のＣＯ2を放出したＣＯ2吸収液はセミリーン溶液と呼称される。このセミリーン溶液は、再生塔１８下部に至る頃には、ほぼ全てのＣＯ2が除去されたＣＯ2吸収液１５となる。このリーン溶液は再生過熱器２４で水蒸気２５により過熱され、再生塔１８内部に水蒸気を供給している。
一方、再生塔１８の頭頂部からは塔内においてリッチ溶液およびセミリーン溶液から放出された水蒸気を伴ったＣＯ2ガス２６が導出され、コンデンサ２７により水蒸気が凝縮され、分離ドラム２８にて水が分離され、ＣＯ2ガス２６が系外に放出されて別途回収される。この回収されたＣＯ2ガス２６は、石油増進回収法（ＥＯＲ：Enhanced Oil Recovery）を用いて油田中に圧入するか、帯水層へ貯留し、温暖化対策を図っている。
分離ドラム２８にて分離された水は凝縮水循環ポンプ２９にて再生塔１８の上部に供給される。再生されたＣＯ2吸収液（リーン溶液）１５は、リッチ／リーンソルベント熱交換器２３にてリッチ溶液１７により冷却され、つづいてリーンソルベントポンプ３０にて昇圧され、さらにリーンソルベントクーラ３１にて冷却された後、ＣＯ2吸収塔１６に供給される。なお、ＣＯ2吸収塔１６の底部液溜まりには液レベルを計測するレベル計４１が設置され、必要に応じてＣＯ2吸収液を補給液４２として供給するようにしている。 The rich solution released from the upper part of the regeneration tower 18 generates an endothermic reaction and releases most of the CO 2 . The CO 2 absorbing solution that has released a part or most of CO 2 in the regeneration tower 18 is called a semi-lean solution. This semi-lean solution becomes the CO 2 absorbent 15 from which almost all CO 2 has been removed by the time it reaches the lower part of the regeneration tower 18. This lean solution is superheated by the steam 25 in the regeneration superheater 24 to supply steam to the inside of the regeneration tower 18.
On the other hand, CO 2 gas 26 accompanied with water vapor released from the rich solution and the semi-lean solution is led out from the top of the regeneration tower 18, the water vapor is condensed by the condenser 27, and the water is separated by the separation drum 28. Then, the CO 2 gas 26 is discharged out of the system and collected separately. The recovered CO 2 gas 26 is injected into an oil field using an enhanced oil recovery (EOR) method or stored in an aquifer to take measures against global warming.
The water separated by the separation drum 28 is supplied to the upper part of the regeneration tower 18 by the condensed water circulation pump 29. The regenerated CO 2 absorbing solution (lean solution) 15 is cooled by the rich solution 17 in the rich / lean solvent heat exchanger 23, subsequently pressurized by the lean solvent pump 30, and further cooled by the lean solvent cooler 31. And then supplied to the CO 2 absorption tower 16. A level meter 41 for measuring the liquid level is installed in the bottom liquid reservoir of the CO 2 absorption tower 16 so that the CO 2 absorbing liquid is supplied as the replenishing liquid 42 as necessary.

なお、図１中、符号１１ａは排ガス１２の煙道であり、１１ｂは煙突、３２は水蒸気凝縮水である。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。煙突１１ｂには開閉可能な扉を設置し、ＣＯ2回収装置の運転時は閉止する。また排ガス源は稼動しているが、ＣＯ2回収装置の運転を停止した際は開放するように設定する。 In addition, in FIG. 1, the code | symbol 11a is the flue of the waste gas 12, 11b is a chimney, 32 is water vapor | steam condensed water. The CO 2 recovery device may be retrofitted for recovering CO 2 from an existing exhaust gas source, or may be simultaneously attached to a new exhaust gas source. The chimney 11b is provided with a door that can be opened and closed, and is closed when the CO 2 recovery device is in operation. Moreover, although the exhaust gas source is operating, it is set to be opened when the operation of the CO 2 recovery device is stopped.

特開平３−１９３１１６号公報Japanese Patent Laid-Open No. 3-193116

ところで、近年の地球温暖化対策として、排出するＣＯ2の回収率を一定に維持することが求められており、長期間に亙ってＣＯ2回収の運転を継続していく際には、一定の回収率（例えばＣＯ２回収率（９０％））を常に維持しつつ、最適な運転となることが切望されている。 By the way, as a measure against global warming in recent years, it is required to maintain a constant CO 2 emission recovery rate. When CO 2 recovery operation is continued over a long period of time, the CO 2 recovery operation is constant. It is eagerly desired to achieve an optimal operation while constantly maintaining the recovery rate (for example, CO 2 recovery rate (90%)).

本発明は、上記問題に鑑みてなされたものであって、一定のＣＯ2回収率を常に維持しつつ最適な運転をすることができるＣＯ2回収装置及び方法を提供することを課題とする。 The present invention has been made in view of the above problems, and an object of the present invention is to provide a CO 2 recovery apparatus and method that can perform an optimal operation while always maintaining a constant CO 2 recovery rate.

上述した課題を解決し、目的を達成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前記排ガス中のＣＯ2を除去するＣＯ2吸収塔と、前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液中のＣＯ2を除去し、再生する再生塔と、前記再生塔でＣＯ2を除去したリーン溶液であるＣＯ2吸収液を前記ＣＯ2吸収塔で再利用するＣＯ2回収装置であって、ＣＯ2濃度及び排ガス量を計測し、その排ガス量とＣＯ2濃度に応じて目標ＣＯ2回収率を達成するために、吸収液循環量を決定し、該決定した吸収液循環量に応じた水蒸気量を決定する制御を行う制御手段を有することを特徴とするＣＯ2回収装置にある。 To solve the above problems, a first invention of the present invention for achieving the object, CO 2 absorption by contacting the exhaust gas and the CO 2 absorbing solution containing CO 2 to remove CO 2 in the flue gas A column, a regeneration tower that removes CO 2 in the rich solution that has absorbed CO 2 by the CO 2 absorption tower, and regenerates the CO 2 absorbent that is a lean solution from which CO 2 has been removed by the regeneration tower. 2 CO 2 recovery device to be reused in the absorption tower, measuring the CO 2 concentration and exhaust gas amount, and in order to achieve the target CO 2 recovery rate according to the exhaust gas amount and CO 2 concentration, the absorption liquid circulation rate It determines, in the CO 2 recovery apparatus, characterized in that it comprises a control means for performing control to determine the amount of water vapor corresponding to the absorption liquid circulation amount the determined.

第２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前記排ガス中のＣＯ2を除去するＣＯ2吸収塔と、前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液中のＣＯ2を除去し、再生する再生塔と、前記再生塔でＣＯ2を除去したリーン溶液であるＣＯ2吸収液を前記ＣＯ2吸収塔で再利用するＣＯ2回収方法であって、ＣＯ2濃度及び排ガス量を計測し、その排ガス量とＣＯ2濃度に応じて目標ＣＯ2回収率を達成するために、該決定した吸収液循環量に応じた水蒸気量を決定することを特徴とするＣＯ2回収方法にある。 A second invention is a rich solution that has absorbed the CO 2 absorption tower for contacting the exhaust gas and the CO 2 absorbing solution containing CO 2 to remove CO 2 in the flue gas, the CO 2 in the CO 2 absorption tower the CO 2 is removed in, a regenerator and, CO 2 recovery method of the CO 2 absorbing liquid is a lean solution obtained by removing CO 2 in the regeneration tower is reused in the CO 2 absorption tower to play, CO 2) Measure the concentration and the amount of exhaust gas, and determine the amount of water vapor according to the determined absorption liquid circulation rate in order to achieve the target CO 2 recovery rate according to the exhaust gas amount and CO 2 concentration It is in the CO 2 recovery method.

本発明によれば、一日あたりのＣＯ2回収率を所定値に設定し、これに応じたエネルギー効率が最適な運転をすることができる。 According to the present invention, the CO 2 recovery rate per day can be set to a predetermined value, and the operation with the optimum energy efficiency can be performed.

図１は、ＣＯ2回収装置の一例を示す図である。FIG. 1 is a diagram illustrating an example of a CO 2 recovery device. 図２は、ＣＯ2回収装置の吸収塔と再生塔とを模式的に示す図である。FIG. 2 is a diagram schematically showing an absorption tower and a regeneration tower of the CO 2 recovery apparatus.

以下に、本発明にかかるＣＯ2回収装置の実施例を図面に基づいて詳細に説明する。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。 Embodiments of a CO 2 recovery device according to the present invention will be described below in detail with reference to the drawings. Note that the present invention is not limited to the embodiments.

本発明による実施例に係るＣＯ2回収装置について、図１を参照して説明する。
図１は、従来技術で説明したＣＯ2回収装置の構成を示す概略図である。
図１に示すように、本発明の実施例に係るＣＯ2回収装置１０は、ＣＯ2を含有する排ガス１２とＣＯ2吸収液１５とを接触させて前記排ガス１２中のＣＯ2を除去するＣＯ2吸収塔１６と、前記ＣＯ2吸収塔１６でＣＯ2を吸収したリッチ溶液１７中のＣＯ2を除去し、再生する再生塔１８と、前記再生塔１８でＣＯ2を除去したリーン溶液であるＣＯ2吸収液１５を前記ＣＯ2吸収塔１６で再利用するＣＯ2回収装置であって、ＣＯ2濃度（I）及び排ガス量（II）とを計測し、その排ガス量とＣＯ2濃度に応じて目標ＣＯ2回収率を達成するために、吸収液循環量（III）を決定し、該決定した吸収液循環量（III）に応じた水蒸気量（IV）を決定する制御を行う制御手段を有するものである。
ここで、排ガス１２は全量を系内に引き込むことを前提としている。また、吸収液の濃度は常に一定に保つことを条件としている。 A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to FIG.
FIG. 1 is a schematic diagram showing the configuration of the CO 2 recovery apparatus described in the prior art.
As shown in FIG. 1, CO 2 recovery apparatus 10 according to an embodiment of the present invention comprises contacting the flue gas 12 and the CO 2 absorbing liquid 15 containing CO 2 to remove CO 2 in the flue gas 12 by CO 2 is an absorption tower 16, a regeneration tower 18 that removes CO 2 from the rich solution 17 that has absorbed CO 2 by the CO 2 absorption tower 16 and regenerates it, and a lean solution that has CO 2 removed by the regeneration tower 18. A CO 2 recovery device for reusing the CO 2 absorbing liquid 15 in the CO 2 absorption tower 16, measuring the CO 2 concentration (I) and the exhaust gas amount (II), and depending on the exhaust gas amount and the CO 2 concentration In order to achieve the target CO 2 recovery rate, control means for determining the absorption liquid circulation amount (III) and performing control for determining the water vapor amount (IV) according to the determined absorption liquid circulation amount (III) is provided. It is what you have.
Here, it is assumed that the exhaust gas 12 is entirely drawn into the system. Further, it is a condition that the concentration of the absorbing solution is always kept constant.

これにより、地球温暖化対策の一環としてＣＯ2回収率を一定（９０％）に維持する場合において、最適な運転を確保することができ、水蒸気の消費量をできるだけ最適化させることができる。 As a result, when maintaining the CO 2 recovery rate constant (90%) as a part of global warming countermeasures, it is possible to ensure optimal operation and optimize the water vapor consumption as much as possible.

ここで、排ガス中のＣＯ2濃度は、ボイラ１１の燃焼条件により変動する。
そこで、表１に示すように、基準の場合には、（Ａ）ガス中のＣＯ2濃度が一定とする場合には、目標ＣＯ2回収率（９０％）とする場合の排ガス量（II）を求め、求めた排ガス量に応じた吸収液循環量（III）を決定し、求めた吸収液循環量（III）に応じた水蒸気量（IV）を決定する制御を行うようにしている。 Here, the CO 2 concentration in the exhaust gas varies depending on the combustion conditions of the boiler 11.
Therefore, as shown in Table 1, in the case of the standard, (A) when the CO 2 concentration in the gas is constant, the amount of exhaust gas when the target CO 2 recovery rate (90%) is set (II) Control is performed to determine the amount of circulated absorption liquid (III) corresponding to the determined amount of exhaust gas, and to determine the amount of water vapor (IV) corresponding to the determined amount of circulated absorbent (III).

そして、排ガス中のＣＯ2濃度が基準よりも０．９５倍と低下した場合には、吸収液循環量は基準と同じ（１．０倍）とし、これに応じた水蒸気量は基準の０．９９倍に変更する制御を行うようにしている。この結果、目標のＣＯ2回収率（９０％）を維持する場合には、水蒸気量を１％減少して運転することができ、エネルギーの削減を図ることができる。 When the CO 2 concentration in the exhaust gas is lowered by 0.95 times from the standard, the absorption liquid circulation rate is the same as the standard (1.0 times), and the water vapor amount corresponding to this is 0. The control for changing to 99 times is performed. As a result, when the target CO 2 recovery rate (90%) is maintained, the operation can be performed with the steam amount reduced by 1%, and the energy can be reduced.

これに対し、排ガス中のＣＯ2濃度が基準よりも１．１倍増加した場合には、吸収液循環量は基準の１．０４倍とし、これに応じた水蒸気量は基準の１．０６倍に変更する制御を行うようにしている。この結果、水蒸気量は６％増加するが、目標のＣＯ2回収率（９０％）を維持することができる。 On the other hand, when the CO 2 concentration in the exhaust gas is increased 1.1 times from the standard, the circulating amount of the absorbing liquid is 1.04 times the standard, and the amount of water vapor corresponding to this is 1.06 times the standard. The control to change to is done. As a result, the amount of water vapor increases by 6%, but the target CO 2 recovery rate (90%) can be maintained.

さらに、排ガスの流量が変動する場合について考慮すると、表１に示すように、（Ｂ）排ガスの流量が基準よりも０．９５倍低下した場合には、吸収液循環量は基準の０．９４倍とし、これに応じた水蒸気量は基準の０．９４倍に変更する制御を行うようにしている。この結果、目標のＣＯ2回収率（９０％）を維持する場合には、水蒸気量を６％減少して運転することができ、エネルギーの削減を図ることができる。 Further, considering the case where the flow rate of the exhaust gas fluctuates, as shown in Table 1, when the flow rate of the exhaust gas is reduced by 0.95 times from the standard, the absorption liquid circulation amount is 0.94 of the standard. The amount of water vapor corresponding to this is controlled to be changed to 0.94 times the standard. As a result, when the target CO 2 recovery rate (90%) is maintained, the operation can be performed with the water vapor amount reduced by 6%, and the energy can be reduced.

これに対し、排ガスの流量が基準よりも１．１倍増加した場合には、吸収液循環量は基準の１．１倍とし、これに応じた水蒸気量は基準の１．１倍に変更する制御を行うようにしている。この結果、水蒸気量は１０％増加するが、目標のＣＯ2回収率（９０％）を維持することができる。 On the other hand, when the flow rate of the exhaust gas increases 1.1 times from the standard, the absorption liquid circulation amount is 1.1 times the standard, and the water vapor amount corresponding to this is changed to 1.1 times the standard. Control is performed. As a result, the amount of water vapor increases by 10%, but the target CO 2 recovery rate (90%) can be maintained.

よって、排ガス中のＣＯ2濃度の変動と共に排ガス流量の変動が重なった場合には、それらを掛け合わせた変更の制御が必要となる。 Therefore, when fluctuations in the exhaust gas flow rate overlap with fluctuations in the CO 2 concentration in the exhaust gas, it is necessary to control the change by multiplying them.

また、吸収塔に導入する導入ガスの温度を考慮すると、表１に示すように（Ｃ）導入ガス温度が５℃低下した場合には、循環量を０．９１倍とし、水蒸気供給量を０．９７倍と３％減少する制御をすれば良いことがわかる。
一方、吸収塔に導入する導入ガスの温度を考慮すると、導入ガス温度が５℃上昇した場合には、循環量１．０９倍とし、水蒸気供給量を１．０３倍と３％増加する制御をすれば良いことがわかる。 Further, considering the temperature of the introduced gas introduced into the absorption tower, as shown in Table 1, when the temperature of the introduced gas (C) decreases by 5 ° C., the circulation rate is 0.91 times and the steam supply rate is 0. It can be seen that it is sufficient to perform control that decreases by 97% and 3%.
On the other hand, when the temperature of the introduced gas introduced into the absorption tower is taken into account, when the introduced gas temperature rises by 5 ° C., the circulation rate is set to 1.09 times, and the water vapor supply rate is increased to 1.03 times and 3%. You can see that

Figure 2011000528
Figure 2011000528

この結果、一日あたりのＣＯ2回収率を目標値（例えば９０％）に維持するための、最適な運転をすることができる。この結果、一日のＣＯ2回収率を厳守できるといいう要求に常に応じることができ、温暖化対策に寄与することができる。 As a result, an optimum operation for maintaining the CO 2 recovery rate per day at a target value (for example, 90%) can be performed. As a result, it is possible to always meet the demand that the daily CO 2 recovery rate can be strictly observed, and to contribute to measures against global warming.

また、ＣＯ2回収装置の吸収塔と再生塔とを模式的に示す図２に示すように、ＣＯ2吸収塔１６と、ＣＯ2再生塔１８との間を吸収液が循環しているので、吸収塔に導入された吸収液が一巡するまでに時間がかかることとなる。
よって、［Ａ］吸収塔１６の充填部を通過する時間（例えば９分）、［Ｂ］吸収塔液溜まり部を通過する時間（例えば１６分）、［Ｃ］熱交換器２３を通過する時間（例えば１分）、［Ｄ］再生塔１８の充填部を通過する時間（例えば３分）、［Ｅ］再生塔１８の液溜まり部を通過する時間（例えば５分）、［Ｆ］配管を通過する時間（例えば６分）の合計の時間の時間遅れの制御が必要となる。 Further, as shown in FIG. 2 schematically showing the absorption tower and the regeneration tower of the CO 2 recovery apparatus, the absorption liquid circulates between the CO 2 absorption tower 16 and the CO 2 regeneration tower 18. It takes time for the absorption liquid introduced into the absorption tower to complete a circuit.
Therefore, [A] time to pass through the packed part of the absorption tower 16 (for example, 9 minutes), [B] time to pass through the absorption tower liquid reservoir (for example, 16 minutes), [C] time to pass through the heat exchanger 23 (For example, 1 minute), [D] time for passing through the packed part of the regeneration tower 18 (for example, 3 minutes), [E] time for passing through the liquid reservoir of the regeneration tower 18 (for example, 5 minutes), [F] piping It is necessary to control the time delay of the total time of passage (for example, 6 minutes).

よって、制御は時間遅れを考慮して制御とすることで最適な運転とすることができる。   Therefore, the control can be performed optimally by considering the time delay.

以上のように、本発明に係るＣＯ2回収装置及び方法は、一日あたりのＣＯ2回収率を常に達成することができ、長期間に亙ってのガス中のＣＯ2処理に用いるのに適している。 As described above, the CO 2 recovery apparatus and method according to the present invention can always achieve a CO 2 recovery rate per day and can be used for CO 2 treatment in gas over a long period of time. Is suitable.

１０ ＣＯ2回収装置
１２ ＣＯ2を含有する排ガス
１５ ＣＯ2吸収液（リーン溶液）
１６ ＣＯ2吸収塔
１７ ＣＯ2を吸収したＣＯ2吸収液（リッチ溶液）
１８ 再生塔
４１ 液レベル計
４２ 補給液 Exhaust gas 15 CO 2 absorbing solution containing 10 CO 2 recovering apparatus 12 CO 2 (lean solution)
16 CO 2 absorption tower 17 CO 2 absorbs the CO 2 absorbing solution (rich solution)
18 Regeneration tower 41 Liquid level meter 42 Replenisher

Claims (2)

ＣＯ2を含有する排ガスとＣＯ2吸収液とを接触させて前記排ガス中のＣＯ2を除去するＣＯ2吸収塔と、前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液中のＣＯ2を除去し、再生する再生塔とを具備し、前記再生塔でＣＯ2を除去したリーン溶液であるＣＯ2吸収液を前記ＣＯ2吸収塔で再利用するＣＯ2回収装置であって、
ＣＯ2濃度及び排ガス量を計測し、その排ガス量とＣＯ2濃度に応じて目標ＣＯ2回収率を達成するために、吸収液循環量を決定し、該決定した吸収液循環量に応じた水蒸気量を決定する制御を行う制御手段を有することを特徴とするＣＯ2回収装置。 Removing the CO 2 absorption tower for contacting the exhaust gas and the CO 2 absorbing solution for removing CO 2 in the flue gas, the CO 2 rich solution that has absorbed CO 2 in the CO 2 absorption tower containing CO 2 And a regeneration tower for regenerating, and a CO 2 recovery device for reusing the CO 2 absorption liquid, which is a lean solution obtained by removing CO 2 in the regeneration tower, in the CO 2 absorption tower,
In order to measure the CO 2 concentration and the amount of exhaust gas, and to achieve the target CO 2 recovery rate according to the amount of exhaust gas and the CO 2 concentration, the amount of absorption liquid circulation is determined, and the water vapor corresponding to the determined amount of absorption liquid circulation A CO 2 recovery device comprising control means for performing control for determining the amount. ＣＯ2を含有する排ガスとＣＯ2吸収液とを接触させて前記排ガス中のＣＯ2を除去するＣＯ2吸収塔と、前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液中のＣＯ2を除去し、再生する再生塔と、前記再生塔でＣＯ2を除去したリーン溶液であるＣＯ2吸収液を前記ＣＯ2吸収塔で再利用するＣＯ2回収方法であって、
ＣＯ2濃度及び排ガス量を計測し、その排ガス量とＣＯ2濃度に応じて目標ＣＯ2回収率を達成するために、該決定した吸収液循環量に応じた水蒸気量を決定することを特徴とするＣＯ2回収方法。 Removing the CO 2 absorption tower for contacting the exhaust gas and the CO 2 absorbing solution for removing CO 2 in the flue gas, the CO 2 rich solution that has absorbed CO 2 in the CO 2 absorption tower containing CO 2 A CO 2 recovery method in which a regeneration tower to be regenerated and a CO 2 absorption liquid, which is a lean solution obtained by removing CO 2 in the regeneration tower, are reused in the CO 2 absorption tower,
It measures CO 2 concentration and exhaust gas amount, and determines the water vapor amount according to the determined absorption liquid circulation amount in order to achieve the target CO 2 recovery rate according to the exhaust gas amount and CO 2 concentration. CO 2 recovery method.
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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013114488A1 (en) 2012-02-03 2013-08-08 三菱重工業株式会社 Co2 recovery device
JP2014004525A (en) * 2012-06-25 2014-01-16 Toshiba Corp Carbon dioxide recovery apparatus and method for operating the same
JP2015136687A (en) * 2014-01-24 2015-07-30 三菱重工業株式会社 Co2 recovery apparatus and co2 recovery method
US9950296B2 (en) 2014-09-22 2018-04-24 Kabushiki Kaisha Toshiba Carbon dioxide separation and capture apparatus and method of controlling operation of carbon dioxide separation and capture apparatus
CN112473322A (en) * 2019-09-12 2021-03-12 株式会社东芝 Carbon dioxide recovery system and method for operating same

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10165761A (en) * 1996-12-16 1998-06-23 Kansai Electric Power Co Inc:The Control method for flue gas decarboxylation equipment

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10165761A (en) * 1996-12-16 1998-06-23 Kansai Electric Power Co Inc:The Control method for flue gas decarboxylation equipment

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013114488A1 (en) 2012-02-03 2013-08-08 三菱重工業株式会社 Co2 recovery device
US9186620B2 (en) 2012-02-03 2015-11-17 Mitsubishi Heavy Industries, Ltd. CO2 recovery device
JP2014004525A (en) * 2012-06-25 2014-01-16 Toshiba Corp Carbon dioxide recovery apparatus and method for operating the same
JP2015136687A (en) * 2014-01-24 2015-07-30 三菱重工業株式会社 Co2 recovery apparatus and co2 recovery method
WO2015111454A1 (en) * 2014-01-24 2015-07-30 三菱重工業株式会社 Co2 recovery apparatus and co2 recovery process
AU2015210213B2 (en) * 2014-01-24 2017-12-14 Mitsubishi Heavy Industries, Ltd. CO2 recovery apparatus and CO2 recovery process
US10427093B2 (en) 2014-01-24 2019-10-01 Mitsubishi Heavy Industries Engineering, Ltd. CO2 recovery apparatus and CO2 recovery process
US9950296B2 (en) 2014-09-22 2018-04-24 Kabushiki Kaisha Toshiba Carbon dioxide separation and capture apparatus and method of controlling operation of carbon dioxide separation and capture apparatus
CN112473322A (en) * 2019-09-12 2021-03-12 株式会社东芝 Carbon dioxide recovery system and method for operating same
US11559764B2 (en) 2019-09-12 2023-01-24 Kabushiki Kaisha Toshiba Carbon dioxide capturing system and method of operating the same
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