JP4625478B2 - Amine recovery method and apparatus, and decarbonation apparatus equipped with the same - Google Patents

Amine recovery method and apparatus, and decarbonation apparatus equipped with the same Download PDF

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JP4625478B2
JP4625478B2 JP2007078617A JP2007078617A JP4625478B2 JP 4625478 B2 JP4625478 B2 JP 4625478B2 JP 2007078617 A JP2007078617 A JP 2007078617A JP 2007078617 A JP2007078617 A JP 2007078617A JP 4625478 B2 JP4625478 B2 JP 4625478B2
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富雄 三村
貴司 野条
裕士 田中
琢也 平田
一男 石田
裕 中小路
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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
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Description

本発明はアミン回収方法及び装置並びにこれを備えた脱炭酸ガス装置に関し、アミン化合物含有吸収液により、二酸化炭素を含むガスから二酸化炭素を除去する脱炭酸プロセスにおいて、脱炭酸排ガスに同伴するアミン化合物を回収する場合に適用して有用なものである。   TECHNICAL FIELD The present invention relates to an amine recovery method and apparatus and a decarbonation gas apparatus equipped with the same, and an amine compound accompanying a decarbonation exhaust gas in a decarbonation process for removing carbon dioxide from a gas containing carbon dioxide by an amine compound-containing absorbent. It is useful to be applied when recovering.

近年、火力発電設備やボイラ設備では多量の石炭、重油或いは超重質油を燃料に用いており、大気汚染防止及び地球環境清浄化の見地から、二酸化硫黄を主とする硫黄酸化物、窒素酸化物、二酸化炭素等の放出に関する量的、濃度的抑制が問題となっている。なかでも、最近、二酸化炭素については、フロンガスやメタンガスとともに地球温暖化の見地から、その排出の抑制が検討されている。このため、例えば、ＰＳＡ（圧力スウィング）法、膜分離法及び塩基性化合物による反応吸収などの二酸化炭素除去方法が検討されている。   In recent years, thermal power generation facilities and boiler facilities use a large amount of coal, heavy oil, or ultra-heavy oil as fuel. From the viewpoint of air pollution prevention and global environmental purification, sulfur oxides mainly composed of sulfur dioxide, nitrogen oxides Quantitative and concentration suppression related to the release of carbon dioxide and the like is a problem. Among them, recently, suppression of emission of carbon dioxide from the viewpoint of global warming is being considered together with chlorofluorocarbon gas and methane gas. For this reason, for example, PSA (pressure swing) methods, membrane separation methods, and carbon dioxide removal methods such as reaction absorption using basic compounds have been studied.

これらのうち、塩基性化合物による二酸化炭素の除去方法の例としては、特開平５−１８４８６６号公報（関連米国特許５３１８７５８号）にアミン化合物（以下、単にアミンとも称する）の水溶液を二酸化炭素の吸収液として用いることにより、脱炭酸を行うという方法が提案されている。この方法においては、二酸化炭素とアミン化合物との反応が発熱反応であるため、二酸化炭素吸収部における吸収液温度が上昇してアミンの蒸気圧が高くなる。即ち、温度上昇によって多くのアミン含有吸収液が蒸発することから、脱炭酸ガスに同伴するアミン化合物の量が増加する。このため、吸収塔に水洗部を設け、この水洗部において脱炭酸ガスと洗浄水とを気液接触させることにより、脱炭酸ガスに同伴するアミン化合物を液相に回収していた。   Among these, as an example of a method for removing carbon dioxide with a basic compound, an aqueous solution of an amine compound (hereinafter also simply referred to as amine) is disclosed in JP-A-5-184866 (related US Pat. No. 5,318,758). A method of decarboxylation by using as a liquid has been proposed. In this method, since the reaction between carbon dioxide and the amine compound is an exothermic reaction, the temperature of the absorption liquid in the carbon dioxide absorption portion increases and the vapor pressure of the amine increases. That is, since a large amount of the amine-containing absorbing liquid evaporates due to the temperature rise, the amount of the amine compound accompanying the decarbonation gas increases. For this reason, the water washing part was provided in the absorption tower, and the amine compound accompanying the decarbonation gas was collect | recovered in the liquid phase by making the carbonic acid gas and washing water contact gas-liquid in this water washing part.

具体的には、上記特開平５−１８４８６６号公報では図２及び図３に示すような脱炭酸ガス装置を開示している。   Specifically, Japanese Patent Laid-Open No. 5-184866 discloses a decarbonation gas apparatus as shown in FIGS.

図２において、１は吸収塔、２は二酸化炭素吸収部、３は水洗部、４は排ガス供給部、６は吸収液供給口、７はノズル、８は水洗部における液保留部、９は循環ポンプ、１０は冷却器、１１はノズル、１２は吸収液排出口、１３はブロア、１４は排ガス供給口、１５は排ガス冷却器、１６は循環ポンプ、１７は冷却器、１８はノズル、１９は排出ラインである。   In FIG. 2, 1 is an absorption tower, 2 is a carbon dioxide absorption part, 3 is a water washing part, 4 is an exhaust gas supply part, 6 is an absorption liquid supply port, 7 is a nozzle, 8 is a liquid holding part in the water washing part, and 9 is a circulation. Pump, 10 is a cooler, 11 is a nozzle, 12 is an absorbent discharge port, 13 is a blower, 14 is an exhaust gas supply port, 15 is an exhaust gas cooler, 16 is a circulation pump, 17 is a cooler, 18 is a nozzle, 19 is It is a discharge line.

詳細な説明は省略するが、排ガス供給口１４から供給された燃焼排ガスは、冷却塔１５で冷却された後に吸収塔１に供給され、この吸収塔１の二酸化炭素吸収部２において、吸収液供給口６からノズル７を介して供給された吸収液と向流接触させられる。その結果、燃焼排ガス中の二酸化炭素が吸収液により吸収除去される。二酸化炭素を吸収した負荷吸収液は、吸収液排出口１２から図示しない再生塔へ送られ、ここで再生されて再び吸収液供給口１６から吸収塔１へと供給される。   Although detailed explanation is omitted, the combustion exhaust gas supplied from the exhaust gas supply port 14 is supplied to the absorption tower 1 after being cooled by the cooling tower 15, and the absorption liquid is supplied to the carbon dioxide absorption section 2 of the absorption tower 1. Countercurrent contact is made with the absorbent supplied from the mouth 6 via the nozzle 7. As a result, carbon dioxide in the combustion exhaust gas is absorbed and removed by the absorbing liquid. The load absorption liquid that has absorbed carbon dioxide is sent from the absorption liquid discharge port 12 to a regeneration tower (not shown), regenerated here, and supplied again from the absorption liquid supply port 16 to the absorption tower 1.

一方、二酸化炭素吸収部２で脱炭酸された燃焼排ガス（脱炭酸排ガス）は、二酸化炭素吸収部２における二酸化炭素とアミン化合物との発熱反応による温度上昇のため、多くのアミン蒸気を同伴した状態で上昇し、液保留部８を通って水洗部３へと向かう。そして、水洗部３では、液保留部８の保留水が循環ポンプ９によって輸送され、冷却器１０で冷却された後にノズル１１から洗浄水として水洗部３に供給される。その結果、この洗浄水と脱炭酸排ガスとが水洗部３において向流接触することにより、脱炭酸排ガス中のアミン化合物が液相に回収される。   On the other hand, the combustion exhaust gas (decarbonation exhaust gas) decarboxylated in the carbon dioxide absorption part 2 is accompanied by a large amount of amine vapor due to the temperature rise due to the exothermic reaction between carbon dioxide and the amine compound in the carbon dioxide absorption part 2. And goes to the water washing part 3 through the liquid holding part 8. In the washing unit 3, the retained water in the liquid storage unit 8 is transported by the circulation pump 9, cooled by the cooler 10, and then supplied from the nozzle 11 to the washing unit 3 as cleaning water. As a result, the wash water and the decarbonized exhaust gas come into countercurrent contact with each other in the water washing section 3, whereby the amine compound in the decarbonized exhaust gas is recovered in the liquid phase.

図３は再生塔還流水を利用することによってアミン回収能力を向上させたことを特徴とするものである。図３において、２１は吸収塔、２２は二酸化炭素吸収部、２３は水洗部、２４は排ガス供給口、２５は排ガス排出口、２６は吸収液供給口、２７はノズル、２８は再生塔還流抜き出し水供給口、２９はノズル、３０は冷却器、３１はノズル、３２は充填部、３３は循環ポンプ、３４は補給水供給ライン、３５は吸収液排出ポンプ、３６は熱交換器、３７は冷却器、３８は再生塔、３９はノズル、４０は下部充填部、４１はリボイラ、４２は上部充填部、４３は還流水ポンプ、４４は二酸化炭素分離器、４５は二酸化炭素排出ライン、４６は冷却器、４７はノズル、４８は還流水供給ライン、４９は燃焼ガス供給ブロアである。   FIG. 3 is characterized in that the amine recovery ability is improved by using the recycle tower reflux water. In FIG. 3, 21 is an absorption tower, 22 is a carbon dioxide absorption section, 23 is a water washing section, 24 is an exhaust gas supply port, 25 is an exhaust gas discharge port, 26 is an absorption liquid supply port, 27 is a nozzle, and 28 is a regeneration tower reflux extraction. Water supply port, 29 is a nozzle, 30 is a cooler, 31 is a nozzle, 32 is a filling unit, 33 is a circulation pump, 34 is a makeup water supply line, 35 is an absorption liquid discharge pump, 36 is a heat exchanger, 37 is cooling , 38 is a regeneration tower, 39 is a nozzle, 40 is a lower filling unit, 41 is a reboiler, 42 is an upper filling unit, 43 is a reflux water pump, 44 is a carbon dioxide separator, 45 is a carbon dioxide discharge line, and 46 is a cooling unit. , 47 is a nozzle, 48 is a reflux water supply line, and 49 is a combustion gas supply blower.

詳細な説明は省略するが、燃焼ガス供給ブロア４９によって供給された燃焼排ガスは、冷却塔３０で冷却された後に吸収塔２１に供給され、この吸収塔２１の二酸化炭素吸収部２２において、吸収液供給口２６からノズル２７を介して供給された吸収液と向流接触させられる。その結果、燃焼排ガス中の二酸化炭素が吸収液により吸収除去される。二酸化炭素を吸収した負荷吸収液は、吸収液排出口１２から吸収液排出ポンプ３５によって再生塔３８へ送られ、ここで再生されて再び吸収液供給口２６から吸収塔２１へと供給される。   Although detailed explanation is omitted, the combustion exhaust gas supplied by the combustion gas supply blower 49 is cooled by the cooling tower 30 and then supplied to the absorption tower 21. In the carbon dioxide absorption section 22 of the absorption tower 21, the absorption liquid Countercurrent contact is made with the absorbent supplied from the supply port 26 via the nozzle 27. As a result, carbon dioxide in the combustion exhaust gas is absorbed and removed by the absorbing liquid. The load absorption liquid that has absorbed carbon dioxide is sent from the absorption liquid discharge port 12 to the regeneration tower 38 by the absorption liquid discharge pump 35, regenerated here, and supplied again from the absorption liquid supply port 26 to the absorption tower 21.

一方、二酸化炭素吸収部２２で脱炭酸された燃焼排ガス（脱炭酸排ガス）は、二酸化炭素吸収部２２における二酸化炭素とアミン化合物との発熱反応による温度上昇のため、多くのアミン蒸気を同伴した状態で上昇し、水洗部２３へと向かう。そして、水洗部２３では、洗浄水として抜き出された再生塔還流水の一部が、再生塔還流抜き出し水供給口２８からノズル２９を介して水洗部２３に供給される。その結果、この洗浄水と脱炭酸排ガスとが水洗部２３において向流接触することにより、脱炭酸排ガス中のアミン化合物が液相に回収される。   On the other hand, the combustion exhaust gas (decarbonation exhaust gas) decarboxylated in the carbon dioxide absorption part 22 is in a state where a large amount of amine vapor is accompanied due to a temperature rise due to an exothermic reaction between carbon dioxide and an amine compound in the carbon dioxide absorption part 22. It goes up and goes to the water washing part 23. In the water washing section 23, a part of the regenerator reflux water extracted as the wash water is supplied from the regenerator reflux extraction water supply port 28 to the water wash section 23 through the nozzle 29. As a result, the wash water and the decarbonized exhaust gas come into countercurrent contact with each other in the water washing section 23, whereby the amine compound in the decarbonized exhaust gas is recovered in the liquid phase.

特開平５−１８４８６６号公報JP-A-5-184866

しかしながら、特に図２に示す上記従来の脱炭酸ガス装置では、水洗部が一段であるが故に洗浄水によって回収されたアミンの濃度が高くなるため、アミンの回収が不充分となり、アミンが脱炭酸排ガスに同伴されて脱炭酸プロセス系外に放出される。このため、アミンが無駄になり、運転コストの増大等を引き起こす恐れがあった。   However, particularly in the conventional decarbonation gas apparatus shown in FIG. 2, the concentration of the amine recovered by the cleaning water increases because the washing section is one stage, so that the amine recovery becomes insufficient, and the amine is decarboxylated. Along with the exhaust gas, it is discharged outside the decarbonation process system. For this reason, the amine is wasted, which may cause an increase in operating cost.

従って、本発明は上記の問題点に鑑み、アミン化合物含有吸収液により、二酸化炭素を含むガスから二酸化炭素を除去する脱炭酸プロセスにおいて、脱炭酸排ガスに同伴されるアミン化合物を効率的に回収することができるアミン回収方法及び装置並びにこれを備えた脱炭酸ガス装置を提供することを課題とする。   Therefore, in view of the above problems, the present invention efficiently recovers an amine compound accompanying a decarbonized exhaust gas in a decarbonation process in which carbon dioxide is removed from a gas containing carbon dioxide by an amine compound-containing absorbent. It is an object of the present invention to provide an amine recovery method and apparatus that can be used, and a decarbonation gas apparatus including the same.

上記課題を解決する第１発明のアミン回収方法は、二酸化炭素吸収部においてアミン化合物を含有する吸収液との気液接触により二酸化炭素が吸収除去された脱炭酸排ガスに対し、水洗部において洗浄水と気液接触させることより、前記脱炭酸排ガスに同伴するアミン化合物を回収するアミン回収方法において、
前記水洗部を複数段構成とし、且つ、各段では、前記水洗部の入口側に設けられた液保留部に保留されている洗浄水を、前記水洗部の出口側へと輸送して、前記水洗部へ供給し、前記複数段の水洗部において、順次、前記脱炭酸排ガスに同伴するアミン化合物の回収処理を行うとともに、
二酸化炭素吸収部及び各段の水洗部の出口にデミスタを設け、これらのデミスタによって脱炭酸排ガスに同伴する吸収液ミストや洗浄水ミストを除去し、
且つ、後段の水洗部における液保留部から洗浄水を抜き出し、前段のデミスタをバイパスして、前段の水洗部又は前段の水洗部における液保留部へ供給することを特徴とする。 The amine recovery method of the first invention that solves the above-mentioned problem is that the dewatering exhaust gas from which carbon dioxide has been absorbed and removed by gas-liquid contact with an absorbing solution containing an amine compound in the carbon dioxide absorbing portion is washed water in the washing portion. In the amine recovery method for recovering the amine compound entrained in the decarbonation exhaust gas by contacting with gas and liquid,
The flushing section has a multi-stage configuration, and in each stage, the washing water held in the liquid holding part provided on the inlet side of the flushing part is transported to the outlet side of the flushing part, Supplying to the water washing section, in the multi-stage water washing section, sequentially performing a recovery process of the amine compound accompanying the decarbonation exhaust gas,
A demister is provided at the outlet of the carbon dioxide absorption section and the water washing section of each stage, and the absorption mist and washing water mist accompanying the decarbonized exhaust gas are removed by these demisters,
In addition, the washing water is extracted from the liquid holding section in the subsequent water washing section, and is supplied to the liquid holding section in the preceding water washing section or the previous water washing section, bypassing the previous demister.

また、第２発明のアミン回収方法は、第１発明のアミン回収方法において、
再生塔還流水を、前記液保留部から前記水洗部の出口側へ輸送される洗浄水と合流させて、前記水洗部に供給することを特徴とする。 The amine recovery method of the second invention is the amine recovery method of the first invention,
The regeneration tower reflux water is combined with the washing water transported from the liquid holding section to the outlet side of the washing section, and supplied to the washing section.

また、第３発明のアミン回収方法は、第１又は第２明のアミン回収方法において、
前記液保留部から前記水洗部の出口側への前記洗浄水の輸送は循環ポンプによって行うことを特徴とする。 Further, the amine recovery method of the third invention is the first or second light amine recovery method,
The washing water is transported from the liquid holding section to the outlet side of the washing section by a circulation pump.

また、第４発明のアミン回収装置は、二酸化炭素吸収部においてアミン化合物を含有する吸収液との気液接触により二酸化炭素が吸収除去された脱炭酸排ガスに対し、水洗部において洗浄水と気液接触させることより、前記脱炭酸排ガスに同伴するアミン化合物を回収するように構成したアミン回収装置において、
前記水洗部を複数段構成とし、且つ、各段では、前記水洗部の入口側に設けられた液保留部に保留されている洗浄水を、前記水洗部の出口側へと輸送して、前記水洗部へ供給する構成として、
前記複数段の水洗部において、順次、前記脱炭酸排ガスに同伴するアミン化合物の回収処理を行うとともに、
二酸化炭素吸収部及び各段の水洗部の出口にデミスタを設け、これらのデミスタによって脱炭酸排ガスに同伴する吸収液ミストや洗浄水ミストを除去するように構成し、
且つ 後段の水洗部における液保留部から洗浄水を抜き出し、前段のデミスタをバイパスして、前段の水洗部又は前段の水洗部における液保留部へ供給するように構成したことを特徴とする。 Further, the amine recovery device according to the fourth aspect of the present invention is directed to a dewatering exhaust gas from which carbon dioxide has been absorbed and removed by gas-liquid contact with an absorbing solution containing an amine compound in the carbon dioxide absorbing portion, and in which the washing water and the gas-liquid are washed. In the amine recovery apparatus configured to recover the amine compound accompanying the decarbonation exhaust gas by contacting,
The flushing section has a multi-stage configuration, and in each stage, the washing water held in the liquid holding part provided on the inlet side of the flushing part is transported to the outlet side of the flushing part, As a configuration to supply to the washing section,
In the plurality of water washing sections, sequentially performing a recovery process of the amine compound accompanying the decarbonation exhaust gas,
A demister is provided at the outlet of the carbon dioxide absorption section and the water washing section of each stage, and is configured to remove absorption liquid mist and washing water mist accompanying the decarbonized exhaust gas by these demisters,
In addition, it is characterized in that the washing water is extracted from the liquid holding part in the subsequent water washing part, and is supplied to the liquid washing part in the previous water washing part or the previous water washing part, bypassing the previous demister.

また、第５発明のアミン回収装置は、第４発明のアミン回収装置において、
再生塔還流水を、前記液保留部から前記水洗部の出口側へ輸送される洗浄水と合流させて、前記水洗部に供給するように構成したことを特徴とする。 The amine recovery device of the fifth invention is the amine recovery device of the fourth invention,
The regeneration tower reflux water is combined with the washing water transported from the liquid holding section to the outlet side of the washing section and supplied to the washing section.

また、第６発明のアミン回収装置は、第４又は第５発明のアミン回収装置において、
前記液保留部から前記水洗部の出口側への前記洗浄水の輸送は循環ポンプによって行う構成としたことを特徴とする。 The amine recovery device of the sixth invention is the amine recovery device of the fourth or fifth invention ,
The washing water is transported from the liquid holding part to the outlet side of the washing part by a circulation pump.

また、第７発明の脱炭酸ガス装置は、第４，第５又は第６発明の何れかのアミン回収装置を吸収塔に備えたことを特徴とする。 The decarbonation apparatus of the seventh invention is characterized in that the absorption tower is equipped with the amine recovery device of any one of the fourth, fifth or sixth invention.

第１発明のアミン回収方法によれば、二酸化炭素吸収部においてアミン化合物を含有する吸収液との気液接触により二酸化炭素が吸収除去された脱炭酸排ガスに対し、水洗部において洗浄水と気液接触させることより、前記脱炭酸排ガスに同伴するアミン化合物を回収するアミン回収方法において、前記水洗部を複数段構成とし、且つ、各段では、前記水洗部の入口側に設けられた液保留部に保留されている洗浄水を、前記水洗部の出口側へと輸送して、前記水洗部へ供給し、前記複数段の水洗部において、順次、前記脱炭酸排ガスに同伴するアミン化合物の回収処理を行うとともに、二酸化炭素吸収部及び各段の水洗部の出口にデミスタを設け、これらのデミスタによって脱炭酸排ガスに同伴する吸収液ミストや洗浄水ミストを除去し、且つ、後段の水洗部における液保留部から洗浄水を抜き出し、前段のデミスタをバイパスして、前段の水洗部又は前段の水洗部における液保留部へ供給することを特徴とするため、脱炭酸排ガスに同伴されるアミン化合物を非常に効率良く回収することができ、運転コストの低減が可能となる。
また、二酸化炭素吸収部に供給される吸収液ミストの一部や各段の水洗部に供給される洗浄水ミストの一部が脱炭酸排ガスとともに系外へ放出されて水分やアミン化合物がロスするのを防止することができる。
また、前段の水洗部の洗浄水に含まれるアミン濃度が低減されて前段の水洗部におけるアミン回収能力が向上し、また、これに伴って後段の水洗部の洗浄水に含まれるアミン濃度も更に低減することにもなり、全体としてアミン回収能力が更に向上する。 According to the amine recovery method of the first invention, with respect to the decarbonized exhaust gas from which carbon dioxide has been absorbed and removed by gas-liquid contact with the absorbing liquid containing the amine compound in the carbon dioxide absorbing section, the washing water and the gas liquid in the washing section. In the amine recovery method for recovering the amine compound accompanying the decarbonation exhaust gas by contacting, the water washing section has a plurality of stages, and in each stage, a liquid holding section provided on the inlet side of the water washing section The wash water retained in the tank is transported to the outlet side of the water washing section, supplied to the water washing section, and in the plurality of water washing sections, the amine compound accompanying the decarbonation exhaust gas is sequentially recovered. In addition, a demister is provided at the outlet of the carbon dioxide absorption section and the water washing section of each stage, and these demisters remove absorption liquid mist and washing water mist accompanying the decarbonized exhaust gas, and In order to remove the washing water from the liquid holding part in the subsequent water washing part, bypass the previous demister, and supply it to the liquid holding part in the previous water washing part or the previous water washing part. The accompanying amine compound can be recovered very efficiently, and the operating cost can be reduced.
In addition, part of the absorbent mist supplied to the carbon dioxide absorption part and part of the washing water mist supplied to the water washing part of each stage are released out of the system together with the decarbonized exhaust gas, and moisture and amine compounds are lost. Can be prevented.
In addition, the amine concentration contained in the washing water of the preceding water washing section is reduced and the amine recovery ability in the preceding water washing section is improved, and accordingly, the amine concentration contained in the washing water of the latter washing section is further increased. As a whole, the amine recovery ability is further improved.

また、第２発明のアミン回収方法によれば、第１発明のアミン回収方法において、再生塔還流水を、前記液保留部から前記水洗部の出口側へ輸送される洗浄水と合流させて、前記水洗部に供給することを特徴とするため、水洗部の洗浄水に含まれるアミン濃度が低減されてアミン回収能力が更に向上する。 Further, according to the amine recovery method of the second invention, in the amine recovery method of the first invention, the regeneration tower reflux water is combined with the wash water transported from the liquid holding part to the outlet side of the water washing part, Since it supplies to the said water-washing part, the amine density | concentration contained in the wash water of a water-washing part is reduced, and an amine collection | recovery capability further improves.

また、第３発明のアミン回収方法によれば、第１又は第２発明のアミン回収方法において、前記液保留部から前記水洗部の出口側への前記洗浄水の輸送は循環ポンプによって行うことを特徴とするため、第１又は第２発明と同様の効果が得られる。 Further, according to the amine recovery method of the third invention, in the amine recovery method of the first or second invention, the washing water is transported from the liquid holding part to the outlet side of the water washing part by a circulation pump. Since it is characterized, the same effect as the first or second invention can be obtained.

また、第４発明のアミン回収装置によれば、二酸化炭素吸収部においてアミン化合物を含有する吸収液との気液接触により二酸化炭素が吸収除去された脱炭酸排ガスに対し、水洗部において洗浄水と気液接触させることより、前記脱炭酸排ガスに同伴するアミン化合物を回収するように構成したアミン回収装置において、前記水洗部を複数段構成とし、且つ、各段では、前記水洗部の入口側に設けられた液保留部に保留されている洗浄水を、前記水洗部の出口側へと輸送して、前記水洗部へ供給する構成として、前記複数段の水洗部において、順次、前記脱炭酸排ガスに同伴するアミン化合物の回収処理を行うとともに、二酸化炭素吸収部及び各段の水洗部の出口にデミスタを設け、これらのデミスタによって脱炭酸排ガスに同伴する吸収液ミストや洗浄水ミストを除去するように構成し、且つ 後段の水洗部における液保留部から洗浄水を抜き出し、前段のデミスタをバイパスして、前段の水洗部又は前段の水洗部における液保留部へ供給するように構成したことを特徴とするため、脱炭酸排ガスに同伴されるアミン化合物を非常に効率良く回収することができ、運転コストの低減が可能となる。
また、二酸化炭素吸収部に供給される吸収液ミストの一部や各段の水洗部に供給される洗浄水ミストの一部が脱炭酸排ガスとともに系外へ放出されて水分やアミン化合物がロスするのを防止することができる。
また、前段の水洗部の洗浄水に含まれるアミン濃度が低減されて前段の水洗部におけるアミン回収能力が向上し、また、これに伴って後段の水洗部の洗浄水に含まれるアミン濃度も更に低減することにもなり、全体としてアミン回収能力が更に向上する。 Further, according to the amine recovery device of the fourth invention, the dewatering exhaust gas from which carbon dioxide has been absorbed and removed by gas-liquid contact with the absorbing liquid containing the amine compound in the carbon dioxide absorbing section, In the amine recovery apparatus configured to recover the amine compound entrained in the decarbonized exhaust gas by gas-liquid contact, the water washing section has a plurality of stages, and each stage has an inlet side of the water washing section. The decarbonation exhaust gas is sequentially disposed in the plurality of water washing units as a configuration in which the washing water held in the liquid holding unit provided is transported to the outlet side of the water washing unit and supplied to the water washing unit. In addition to the recovery process of the amine compound accompanying the sorbent, a demister is provided at the outlet of the carbon dioxide absorption section and the water washing section of each stage, and the absorption liquid accompanying the decarbonized exhaust gas by these demisters The wash water is extracted from the liquid holding part in the subsequent water washing part, bypasses the previous demister, and goes to the liquid washing part in the previous water washing part or the previous water washing part. Since it is configured to be supplied, the amine compound entrained in the decarbonized exhaust gas can be recovered very efficiently, and the operating cost can be reduced.
In addition, part of the absorbent mist supplied to the carbon dioxide absorption part and part of the washing water mist supplied to the water washing part of each stage are released out of the system together with the decarbonized exhaust gas, and moisture and amine compounds are lost. Can be prevented.
In addition, the amine concentration contained in the washing water of the preceding water washing section is reduced and the amine recovery ability in the preceding water washing section is improved, and accordingly, the amine concentration contained in the washing water of the latter washing section is further increased. As a whole, the amine recovery ability is further improved.

また、第５発明のアミン回収装置によれば、第４発明のアミン回収装置において、再生塔還流水を、前記液保留部から前記水洗部の出口側へ輸送される洗浄水と合流させて、前記水洗部に供給するように構成したことを特徴とするため、水洗部の洗浄水に含まれるアミン濃度が低減されてアミン回収能力が更に向上する。 Further, according to the amine recovery device of the fifth invention, in the amine recovery device of the fourth invention, the regenerated tower reflux water is combined with the wash water transported from the liquid holding part to the outlet side of the water washing part, Since it comprises so that it may supply to the said water-washing part, the amine density | concentration contained in the wash water of a water-washing part is reduced, and an amine collection | recovery capability further improves.

また、第６発明のアミン回収装置によれば、第４又は第５発明のアミン回収装置において、前記液保留部から前記水洗部の出口側への前記洗浄水の輸送は循環ポンプによって行う構成としたことを特徴とするため、第５，第６又は第７発明と同様の効果が得られる。 Further, according to the amine recovery device of the sixth invention, in the amine recovery device of the fourth or fifth invention , the wash water is transported from the liquid holding part to the outlet side of the water washing part by a circulation pump. Since it is characterized, the same effect as the fifth, sixth or seventh invention can be obtained.

また、第７発明の脱炭酸ガス装置は、第４，第５又は第６発明の何れかのアミン回収装置を吸収塔に備えたことを特徴とするため、アミン化合物の回収能力が高くて運転コストの安価な装置となる。 Further, the decarbonation gas apparatus of the seventh invention is characterized in that the amine recovery apparatus according to any of the fourth, fifth and sixth inventions is provided in the absorption tower, so that the recovery performance of the amine compound is high. It becomes an inexpensive device.

以下、本発明の実施の形態を図面に基づき詳細に説明する。   Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.

図１は本発明の実施の形態に係る脱炭酸ガス装置の主要部を示す構成図である。図１に示すように、本実施の形態の脱炭酸ガス装置では、吸収塔６１と、再生塔６２と、冷却塔６３とを備えている。   FIG. 1 is a configuration diagram showing a main part of a decarbonation gas apparatus according to an embodiment of the present invention. As shown in FIG. 1, the decarbonation apparatus of the present embodiment includes an absorption tower 61, a regeneration tower 62, and a cooling tower 63.

そして、詳細は後述するが、本実施の形態の脱炭酸ガス装置では吸収塔６１の水洗部を一段水洗部６４と二段水洗部６５の二段構成としたこと、二段水洗部６５の洗浄水を抜き出して一段水洗部６４に供給すること、再生塔還流水を洗浄水として二段水洗部に供給すること、二酸化炭素吸収部７３、一段水洗部６４及び二段水洗部６５の出口にデミスタ８３，８４，８５を設置したことなどを特徴としている。   And although the details will be described later, in the decarbonation gas apparatus of the present embodiment, the water washing part of the absorption tower 61 has a two-stage configuration of a single-stage water washing part 64 and a two-stage water washing part 65, and the two-stage water washing part 65 is washed. The water is extracted and supplied to the first-stage water washing section 64, the regeneration tower reflux water is supplied as washing water to the second-stage water washing section, the carbon dioxide absorbing section 73, the first-stage water washing section 64, and the two-stage water washing section 65 at the demister. 83, 84, and 85 are installed.

詳述すると、火力発電設備やボイラ設備などにおいて発生した燃焼排ガスは、排ガス供給ライン６６を介して冷却塔６３に供給される。冷却塔６３の底部６７には水が保留されており、この水が循環ポンプ６８によって汲み上げられ、熱交換器６９で冷却された後にノズル７０から充填部７１へ供給される。その結果、充填部７１において、燃焼排ガスが、ノズル７０から放散された冷却水と向流接触して冷却される。その後、燃焼排ガスは排ガス供給ライン７２を介して吸収塔６１の下部に設けられた二酸化炭素吸収部７３に供給される。   More specifically, combustion exhaust gas generated in a thermal power generation facility, a boiler facility, or the like is supplied to the cooling tower 63 via an exhaust gas supply line 66. Water is retained at the bottom 67 of the cooling tower 63, and this water is pumped up by the circulation pump 68, cooled by the heat exchanger 69, and then supplied from the nozzle 70 to the filling unit 71. As a result, in the filling unit 71, the combustion exhaust gas is cooled in countercurrent contact with the cooling water diffused from the nozzle 70. Thereafter, the combustion exhaust gas is supplied via an exhaust gas supply line 72 to a carbon dioxide absorber 73 provided at the lower part of the absorption tower 61.

吸収塔６１に供給された燃焼排ガスは図中に点線の矢印で示すように吸収塔内を上昇していく。一方、再生塔６２の底部７６に保留されている再生吸収液（アミン化合物の水溶液）が、吸収液供給ライン７４に設けられた吸収液供給ポンプ７７により輸送され、熱交換器７８及び熱交換器７９において冷却された後、二酸化炭素吸収部７３の出口に設けられたノズル７５から二酸化炭素吸収部７３へと供給される。その結果、二酸化炭素吸収部７３において、燃焼排ガスと吸収液とが気液接触（向流接触）するため、燃焼排ガス中に含まれる二酸化炭素が吸収液中に吸収されて除去される。   The combustion exhaust gas supplied to the absorption tower 61 ascends in the absorption tower as indicated by dotted arrows in the figure. On the other hand, the regenerated absorbent (amine compound aqueous solution) retained in the bottom 76 of the regenerator 62 is transported by an absorbent supply pump 77 provided in the absorbent supply line 74, and the heat exchanger 78 and the heat exchanger are transported. After being cooled in 79, the carbon dioxide absorption unit 73 is supplied from a nozzle 75 provided at the outlet of the carbon dioxide absorption unit 73. As a result, in the carbon dioxide absorber 73, the combustion exhaust gas and the absorption liquid are in gas-liquid contact (countercurrent contact), so that the carbon dioxide contained in the combustion exhaust gas is absorbed into the absorption liquid and removed.

なお、吸収液に含まれるアミン化合物としては、モノエタノールアミン、２−アミノ−２−メチル−１−プロパノールのようなアルコール性水酸基含有１級アミン類、ジエタノールアミン、２−メチルアミノエタノールのようなアルコール性水酸基含有２級アミン類、トリエタノールアミン、Ｎ−メチルジエタノールアミンのようなアルコール性水酸基含有３級アミン類、エチレンジアミン、トリエチレンジアミン、ジエチレントリアミンのようなポリエチレンポリアミン類、ピペラジン類、ピペリジン類、ピロリジン類のような環状アミン類、キシリレンジアミンのようなポリアミン類、メチルアミノカルボン酸のようなアミノ酸類等及びこれらの混合物が挙げられる。これらのアミン類は通常１０〜７０重量％の水溶液として使用される。また、吸収液には二酸化炭素吸収促進剤或いは腐食防止剤、更には、その他の媒体としてメタノール、ポリエチレングリコール、スルフォラン等を加えることができる。   The amine compound contained in the absorbing solution includes monoethanolamine, alcoholic hydroxyl group-containing primary amines such as 2-amino-2-methyl-1-propanol, alcohols such as diethanolamine and 2-methylaminoethanol. Secondary hydroxyl group-containing secondary amines, alcoholic hydroxyl group-containing tertiary amines such as triethanolamine and N-methyldiethanolamine, polyethylenepolyamines such as ethylenediamine, triethylenediamine and diethylenetriamine, piperazines, piperidines and pyrrolidines And cyclic amines, polyamines such as xylylenediamine, amino acids such as methylaminocarboxylic acid, and the like, and mixtures thereof. These amines are usually used as an aqueous solution of 10 to 70% by weight. In addition, carbon dioxide absorption accelerators or corrosion inhibitors, and methanol, polyethylene glycol, sulfolane, etc. can be added to the absorbing solution as other media.

二酸化炭素を吸収した負荷吸収液は、流下して吸収塔底部８０に保留された後、吸収液排出ライン８６に設けられた吸収液排出ポンプ８７により排出され、熱交換器７８において再生吸収液と熱交換して加熱された後、再生塔６２の下部充填部８８の出口に設けられたノズル８９から放散され、下部充填部８８を流下して再生塔底部７６に保留される。   The load absorption liquid that has absorbed carbon dioxide flows down and is held at the bottom 80 of the absorption tower, and is then discharged by an absorption liquid discharge pump 87 provided in the absorption liquid discharge line 86. After being heated by heat exchange, it is emitted from a nozzle 89 provided at the outlet of the lower packed portion 88 of the regeneration tower 62, flows down the lower packed portion 88 and is retained on the regeneration tower bottom 76.

再生塔底部７６に保留された負荷吸収液はリボイラ９０において供給スティームにより例えば１２０℃程度に加熱される。その結果、負荷吸収液中の二酸化炭素が放出されて吸収液が再生される。この再生吸収液は再生塔底部７６に保留され、再び、吸収塔６１の二酸化炭素吸収部７３へと供給される。つまり、吸収液は循環使用されており、ロスが無いかぎり外部へ排出したり外部から供給したりする必要はない。一方、放出された二酸化炭素は図中に点線の矢印で示すように上昇し、下部充填部８８及び上部充填部９１を経て再生塔頂部１１１の二酸化炭素排出ライン９３から再生塔外へと排出される。   The load absorbing liquid retained at the regeneration tower bottom 76 is heated to, for example, about 120 ° C. by the supply steam in the reboiler 90. As a result, carbon dioxide in the load absorbent is released and the absorbent is regenerated. This regenerated absorbent is retained at the regenerator bottom 76 and supplied again to the carbon dioxide absorber 73 of the absorber 61. That is, the absorbing liquid is circulated and does not need to be discharged or supplied from the outside unless there is a loss. On the other hand, the released carbon dioxide rises as shown by dotted arrows in the figure, and is discharged out of the regeneration tower from the carbon dioxide discharge line 93 at the regeneration tower top 111 through the lower filling portion 88 and the upper filling portion 91. The

このとき二酸化炭素には水分が含まれているため、二酸化炭素排出ライン９３に設けられたコンデンサ（冷却器）９４において冷却することにより、二酸化炭素に含まれる水分を凝縮し、この凝縮水と二酸化炭素とを二酸化炭素分離器９５によって分離する。凝縮水と分離された高純度の二酸化炭素は二酸化炭素放出ライン９６から脱炭酸プロセス系外（以下、単に系外という）へと放出され、後の工程において利用又処分される。凝縮水は循環ポンプ９６によって輸送され、その一部は再生塔還流水供給ライン９７側へと抜き出される。この再生塔還流抜き出し水は熱交換器９８で冷却された後、二段水洗部６５の出口に設けられたノズル９９から二段水洗部６５の頂部へ洗浄水として供給される。この再生塔還流抜き出し水はアミン濃度が非常に低い。前記凝縮水の残りは再生塔６２に還流される。即ち、還流ライン１００を介してノズル９２から上部充填部９１の頂部へと供給され、流下して再生塔底部７６に保留される。   At this time, since the carbon dioxide contains moisture, it is cooled by a condenser (cooler) 94 provided in the carbon dioxide discharge line 93 to condense the moisture contained in the carbon dioxide. Carbon is separated by a carbon dioxide separator 95. The high-purity carbon dioxide separated from the condensed water is discharged from the carbon dioxide discharge line 96 to the outside of the decarboxylation process system (hereinafter simply referred to as “outside of the system”), and is used or disposed of in a later step. The condensed water is transported by a circulation pump 96, and a part of the condensed water is withdrawn to the regeneration tower reflux water supply line 97 side. The regeneration tower reflux water is cooled by the heat exchanger 98 and then supplied as washing water from the nozzle 99 provided at the outlet of the two-stage water washing section 65 to the top of the two-stage water washing section 65. The regeneration tower reflux water has a very low amine concentration. The remaining condensed water is returned to the regeneration tower 62. That is, it is supplied from the nozzle 92 to the top of the upper packed portion 91 through the reflux line 100, flows down, and is retained in the regeneration tower bottom portion 76.

一方、吸収塔６１の二酸化炭素吸収部７３において二酸化炭素が除去された燃焼排ガス（脱炭酸排ガス）は、二酸化炭素吸収部７３の出口に設けられたデミスタ８３を経て一段水洗部６４へと流入する。このとき脱炭酸排ガスには多くのアミン蒸気が同伴されている。つまり、二酸化炭素吸収部７３での二酸化炭素とアミン化合物との発熱反応によって温度が上昇するため、多くの吸収液が蒸発して脱炭酸排ガスとともに上昇していく。なお、このときの脱炭酸排ガスに同伴する水分は後述する水洗部での洗浄水の供給源となる。一段水洗部６４に流入する脱炭酸排ガスの温度は例えば約５０〜８０℃となる。   On the other hand, the combustion exhaust gas (decarbonation exhaust gas) from which carbon dioxide has been removed in the carbon dioxide absorption part 73 of the absorption tower 61 flows into the one-stage water washing part 64 through the demister 83 provided at the outlet of the carbon dioxide absorption part 73. . At this time, a large amount of amine vapor is accompanied in the decarbonation exhaust gas. That is, since the temperature rises due to the exothermic reaction between carbon dioxide and the amine compound in the carbon dioxide absorption part 73, a large amount of the absorbing liquid evaporates and rises with the decarbonized exhaust gas. In addition, the water | moisture content accompanying the decarbonation waste gas at this time becomes a supply source of the washing water in the washing part mentioned later. The temperature of the decarbonized exhaust gas flowing into the first-stage water washing section 64 is, for example, about 50 to 80 ° C.

デミスタ８３では脱炭酸排ガスに同伴する吸収液ミストを除去する。つまり、ノズル７５からは吸収液がミストとなって放散されるが、この吸収液ミストの一部が脱炭酸排ガスに同伴して上昇してしまう。従って、このまま吸収液ミストが脱炭酸排ガスとともに吸収塔外に放出されてしまうと、アミン化合物のロスになってしまう。そこで、二酸化炭素吸収部出口にデミスタ８３を設けて脱炭酸排ガスに同伴する吸収液ミストを除去するようにしている。デミスタ８３で除去した水分（吸収液）は流下して吸収塔底部８８に保留される。   The demister 83 removes the absorption liquid mist accompanying the decarbonized exhaust gas. That is, the absorbing liquid is diffused as mist from the nozzle 75, but a part of the absorbing liquid mist is accompanied by the decarboxylated exhaust gas and rises. Therefore, if the absorbent mist is discharged out of the absorption tower together with the decarbonized exhaust gas as it is, a loss of the amine compound is caused. Therefore, a demister 83 is provided at the outlet of the carbon dioxide absorption part to remove the absorption liquid mist accompanying the decarbonized exhaust gas. The water (absorbing liquid) removed by the demister 83 flows down and is retained at the absorption tower bottom 88.

そして、一段水洗部６４では、この一段水洗部６４における液保留部８１の保留水が、循環ライン１０１に設けられた循環ポンプ１０２により輸送され、熱交換器１０３で冷却された後、一段水洗部６４の出口に設けられたノズル１０４から一段水洗部６４の頂部へ洗浄水として供給される。その結果、この洗浄水と脱炭酸排ガスとが一段水洗部６４において向流接触することにより、脱炭酸排ガスの温度が低下して脱炭酸排ガスに同伴する水蒸気が凝縮するとともに同脱炭酸排ガスに同伴するアミン化合物が回収される。このときの凝縮水及び放散された洗浄水は流下して液保留部８１に保留される。   In the first-stage water washing section 64, the retained water in the liquid storage section 81 in the first-stage water washing section 64 is transported by the circulation pump 102 provided in the circulation line 101 and cooled by the heat exchanger 103, and then the first-stage water washing section. The water is supplied as washing water from the nozzle 104 provided at the outlet of 64 to the top of the single-stage washing unit 64. As a result, the washing water and the decarbonized exhaust gas come into countercurrent contact with each other in the single-stage water washing section 64, so that the temperature of the decarbonized exhaust gas is lowered and the water vapor accompanying the decarbonized exhaust gas is condensed and accompanied by the decarbonated exhaust gas. The amine compound is recovered. At this time, the condensed water and the dissipated washing water flow down and are retained in the liquid retaining portion 81.

液保留部８１の保留水は一定水位に維持されるようになっている。即ち、液保留部８１の保留水が増加して一定水位以上になると、保留水排出ライン１０５を介して吸収塔底部８０へとオーバフローされるようになっている。なお、ポンプよって液保留部８１の保留水を吸収塔底部８０へ輸送するようにしてもよい。   The retained water in the liquid retaining unit 81 is maintained at a constant water level. That is, when the retained water in the liquid retaining unit 81 increases to a certain level or higher, it overflows to the absorption tower bottom 80 through the retained water discharge line 105. In addition, you may make it transport the reserved water of the liquid storage part 81 to the absorption tower bottom part 80 with a pump.

一段水洗部６４では脱炭酸排ガスに同伴するアミン化合物の大部分が回収されるが、このとき液保留部８１の保留水（洗浄水）中のアミン濃度は高くなる。このため、気液平衡の関係からアミン蒸気圧が高くなり、これ以上は脱炭酸排ガス中のアミン濃度を低減させることができない。即ち、水洗部が一段だけでは脱炭酸排ガス中のアミン濃度を充分に低減させることができない。そこで、本実施の形態では水洗部を一段水洗部６４と二段水洗部６５の二段構成としている。一段水洗部６４においてアミン回収された脱炭酸排ガスは、一段水洗部６４の出口に設けられたデミスタ８４を経て二段水洗部６５へと流れる。   Although most of the amine compound accompanying the decarbonized exhaust gas is recovered in the first-stage water washing section 64, the amine concentration in the retained water (wash water) of the liquid retaining section 81 is increased at this time. For this reason, the amine vapor pressure increases due to the vapor-liquid equilibrium relationship, and the amine concentration in the decarbonized exhaust gas cannot be reduced beyond this. That is, the amine concentration in the decarbonized exhaust gas cannot be sufficiently reduced if there is only one washing section. Therefore, in the present embodiment, the flushing section has a two-stage configuration of a one-stage flushing section 64 and a two-stage flushing section 65. The decarboxylated exhaust gas recovered by the amine in the first-stage water washing section 64 flows to the two-stage water washing section 65 via the demister 84 provided at the outlet of the first-stage water washing section 64.

デミスタ８４では脱炭酸排ガスに同伴する洗浄水ミストを除去する。つまり、ノズル１０４からは洗浄水がミストとなって放散されるが、この洗浄水ミストの一部が脱炭酸排ガスに同伴して上昇してしまう。従って、このまま洗浄水ミストが脱炭酸排ガスとともに吸収塔外に放出されてしまうと、アミン化合物のロスになってしまう。そこで、一段水洗部出口にもデミスタ８４を設けて脱炭酸排ガスに同伴する洗浄水ミストを除去するようにしている。デミスタ８３で除去した水分（洗浄水）は流下して液保留部８１に保留される。   In the demister 84, the cleaning water mist accompanying the decarbonized exhaust gas is removed. That is, the cleaning water is diffused as a mist from the nozzle 104, but a part of the cleaning water mist rises with the decarbonation exhaust gas. Accordingly, if the washing water mist is discharged out of the absorption tower together with the decarbonized exhaust gas as it is, a loss of the amine compound is caused. Therefore, a demister 84 is also provided at the outlet of the one-stage water washing section so as to remove the washing water mist accompanying the decarbonized exhaust gas. The water (washing water) removed by the demister 83 flows down and is retained in the liquid retaining part 81.

二段水洗部６５では、この二段水洗部６５における液保留部８２の保留水が、循環ライン１０６に設けられた循環ポンプ１０７により輸送され、熱交換器９８で冷却された後、二段水洗部６５の出口に設けられたノズル９９から二段水洗部６５の頂部へ洗浄水として供給される。なお、この洗浄水には再生塔側から供給されてきた再生塔還流抜き出し水も合流する。その結果、これらの洗浄水と脱炭酸排ガスとが二段水洗部６５において向流接触することにより、脱炭酸排ガスに同伴されてきたアミン化合物が回収される。   In the two-stage water washing section 65, the retained water in the liquid storage section 82 in the two-stage water washing section 65 is transported by the circulation pump 107 provided in the circulation line 106, cooled by the heat exchanger 98, and then the two-stage water washing section 65. The nozzle 99 provided at the outlet of the section 65 is supplied as washing water to the top of the two-stage water washing section 65. In addition, the regenerative tower reflux extraction water supplied from the regeneration tower side also joins with this washing water. As a result, the wash water and the decarbonized exhaust gas come in countercurrent contact with each other in the two-stage water washing unit 65, whereby the amine compound that has been accompanied by the decarbonized exhaust gas is recovered.

一段水洗部６４において脱炭酸排ガスに同伴するアミン化合物の大部分が回収されるため、二段水洗部６５では液保留部８２のアミン濃度、即ち、ノズル９９から供給する洗浄水中に含まれるアミン濃度が非常に低い状態で維持される。このため、二段水洗部６５では気液平衡の関係から脱炭酸排ガス中のアミン濃度が充分に低減される。即ち、二段水洗部６５では、一段水洗部６４から放出された脱炭酸排ガスから更にアミン化合物を回収することができ、脱炭酸排ガス中のアミン濃度を充分に低減させることができる。   Since most of the amine compound accompanying the decarbonized exhaust gas is recovered in the first-stage water washing section 64, the amine concentration in the liquid holding section 82, that is, the amine concentration contained in the wash water supplied from the nozzle 99 in the two-stage water washing section 65. Is maintained in a very low state. For this reason, the amine concentration in the decarbonized exhaust gas is sufficiently reduced in the two-stage water washing section 65 due to the vapor-liquid equilibrium relationship. That is, in the two-stage water washing section 65, the amine compound can be further recovered from the decarbonation exhaust gas discharged from the first stage water washing section 64, and the amine concentration in the decarbonation exhaust gas can be sufficiently reduced.

しかも、二段水洗部６５の洗浄水が抜き出され、デミスタ８４をバイパスして、一段水洗部６４に供給されるようになっている。具体的には、液保留部８２の保留水（洗浄水）の一部が抜き出され、デミスタ８４をバイパスして、一段水洗部６４の液保留部８１へ供給されるようになっている。つまり、液保留部８２でも一定水位に維持されるようになっており、液保留部８２の保留水が増加して一定水位以上になると、保留水排出ライン１０８を介して液保留部８１へとオーバフローされる。なお、これに限定するものではなく、ポンプよって液保留部８２の保留水（洗浄水）を液保留部８１へ供給するようにしてもよい。   In addition, the wash water from the two-stage water washing section 65 is extracted, and the demister 84 is bypassed and supplied to the first-stage water washing section 64. Specifically, a part of the retained water (washing water) of the liquid retaining part 82 is extracted and supplied to the liquid retaining part 81 of the one-stage water washing part 64, bypassing the demister 84. In other words, the liquid holding unit 82 is also maintained at a constant water level, and when the reserved water in the liquid holding unit 82 increases and becomes a certain level or higher, the liquid holding unit 82 passes through the reserved water discharge line 108 to the liquid holding unit 81. Overflowed. However, the present invention is not limited to this, and the retained water (wash water) of the liquid retaining unit 82 may be supplied to the liquid retaining unit 81 by a pump.

二段水洗部６５においてアミン回収された脱炭酸排ガスは、二段水洗部６５の出口に設けられたデミスタ８５を経て吸収塔頂部１０９のガス放出ライン１１０から系外に放出される。この系外に放出される脱炭酸排ガス中に含まれるアミン濃度は、非常に小さな値となる。   The decarboxylated exhaust gas recovered by the amine in the two-stage water washing section 65 is discharged out of the system from the gas discharge line 110 at the top of the absorption tower 109 via the demister 85 provided at the outlet of the two-stage water washing section 65. The amine concentration contained in the decarbonation exhaust gas discharged out of the system is a very small value.

デミスタ８５では脱炭酸排ガスに同伴する洗浄水ミストを除去する。つまり、ノズル９９からは洗浄水がミストとなって放散されるが、この洗浄水ミストの一部が脱炭酸排ガスに同伴して上昇してしまう。従って、このまま洗浄水ミストが脱炭酸排ガスとともに吸収塔外に放出されてしまうと、アミン化合物のロスになってしまう。そこで、二段水洗部出口にもデミスタ８５を設けて脱炭酸排ガスに同伴する洗浄水ミストを除去するようにしている。デミスタ８５で除去した水分は流下して液保留部８２に保留される。   In the demister 85, the cleaning water mist accompanying the decarbonized exhaust gas is removed. That is, the cleaning water is diffused as a mist from the nozzle 99, but a part of the cleaning water mist rises with the decarbonation exhaust gas. Accordingly, if the washing water mist is discharged out of the absorption tower together with the decarbonized exhaust gas as it is, a loss of the amine compound is caused. Therefore, a demister 85 is also provided at the outlet of the two-stage water washing section so as to remove the washing water mist accompanying the decarbonized exhaust gas. The water removed by the demister 85 flows down and is retained in the liquid retaining part 82.

なお、排ガス供給ライン７２から燃焼排ガスとともに吸収塔内に持ち込まれる水分量と、ガス放出ライン１１０から脱炭酸排ガスとともに吸収塔外に持ち出される水分量とを等しくして水バランスが維持されるように熱交換器９８の冷却能力などを調整して、ロスが無いかぎり外部への排水や外部からの給水が不要となるようにしている。   It should be noted that the water balance is maintained by equalizing the amount of water brought into the absorption tower together with the combustion exhaust gas from the exhaust gas supply line 72 and the amount of water taken out of the absorption tower together with the decarbonized exhaust gas from the gas discharge line 110. The cooling capacity of the heat exchanger 98 is adjusted so that drainage to the outside and water supply from the outside are unnecessary as long as there is no loss.

また、ガス放出ライン１１０から放出される脱炭酸排ガスの温度は二段水洗部６５の入口側と同じになるように熱交換器９８の冷却能力などを調整している。つまり、この場合には、二段水洗部６５の出入口温度が同じであるため、二段水洗部６５での脱炭酸排ガス中の水蒸気の凝縮はなく、液保留部８２では再生塔還流抜き出し水の水量分だけが溢れて、一段水洗部６４の液保留部８１に供給されることになる。なお、必ずしもこれに限定するものではなく、二段水洗部６５の出口温度が入口温度よりも低くなるように調整して、二段水洗部６５でも脱炭酸排ガス中の水分の凝縮が生じるようにし、この凝縮水の水量分が液保留部８２で溢れて一段水洗部６４の液保留部８１に供給されるようにしてもよい。   In addition, the cooling capacity of the heat exchanger 98 is adjusted so that the temperature of the decarboxylated exhaust gas discharged from the gas discharge line 110 is the same as that of the inlet side of the two-stage water washing section 65. That is, in this case, since the inlet / outlet temperature of the two-stage flushing section 65 is the same, there is no condensation of water vapor in the decarbonized exhaust gas in the two-stage flushing section 65, and the retentate reflux water extracted in the liquid holding section 82 Only the amount of water overflows and is supplied to the liquid holding part 81 of the one-stage water washing part 64. However, the present invention is not necessarily limited to this, and the outlet temperature of the two-stage water washing unit 65 is adjusted to be lower than the inlet temperature so that the water in the decarbonized exhaust gas is condensed also in the two-stage water washing unit 65. The amount of the condensed water may overflow from the liquid holding unit 82 and be supplied to the liquid holding unit 81 of the one-stage water washing unit 64.

以上、詳細に説明したように、本実施の形態によれば、水洗部を一段水洗部６４と二段水洗部６５の二段構成とすることにより、脱炭酸排ガスに対して、一段水洗部６４でアミン回収処理をした後、更に、二段水洗部６５でもアミン回収処理をするようにしたため、脱炭酸排ガスに同伴されるアミン化合物を非常に効率良く回収することができ、運転コストの低減が可能となる。   As described above in detail, according to the present embodiment, the single-stage flush unit 64 is configured to remove the decarbonized exhaust gas by providing the flush unit with the two-stage configuration of the single-stage flush unit 64 and the two-stage flush unit 65. After the amine recovery process, the amine recovery process is also performed in the two-stage water washing section 65, so that the amine compound entrained in the decarbonation exhaust gas can be recovered very efficiently, and the operating cost can be reduced. It becomes possible.

付言すると、水洗部を一段構成としたまま高さだけを高くしても、アミン化合物の回収性能は向上するが、水洗部における洗浄水中のアミン濃度が高くなるため、どうしても、気液平衡上、脱炭酸排ガス中のアミン濃度を充分に低くすることはできない。このことからも、水洗部を二段構成とすることが非常に有効な手段であることが分かる。   In addition, even if only the height is increased while the washing part is configured in one stage, the amine compound recovery performance is improved, but the amine concentration in the washing water in the washing part is increased, so for the vapor-liquid equilibrium, The amine concentration in the decarbonation exhaust gas cannot be made sufficiently low. From this, it can be seen that it is a very effective means to have a two-stage washing section.

また、本実施の形態によれば、二段水洗部６５の洗浄水を抜き出して一段水洗部６４に供給するようにしたことにより、一段水洗部６４の洗浄水に含まれるアミン濃度が低減されて一段水洗部６４におけるアミン回収能力が向上し、また、これに伴って二段水洗部６５の洗浄水に含まれるアミン濃度も更に低減することにもなり、全体としてアミン回収能力が更に向上する。   Further, according to the present embodiment, the concentration of amine contained in the washing water of the first-stage water washing unit 64 is reduced by extracting the washing water of the second-stage water washing unit 65 and supplying it to the first-stage water washing unit 64. The amine recovery capability in the first-stage water washing section 64 is improved, and accordingly, the amine concentration contained in the wash water of the second-stage water washing section 65 is further reduced, and the amine recovery capacity is further improved as a whole.

また、本実施の形態によれば、再生塔還流水を洗浄水として二段水洗部６５に供給することにより、二段水洗部６５の洗浄水に含まれるアミン濃度が更に低減されるため、二段水洗部６５におけるアミン回収能力が更に向上する。更には、この二段水洗部６５の洗浄水が抜き出されて一段水洗部６４に供給されることにより、一段水洗部６４の洗浄水のアミン濃度も低減されるため、一段水洗部６４におけるアミン回収能力も向上する。   In addition, according to the present embodiment, the concentration of amine contained in the washing water of the two-stage water washing section 65 is further reduced by supplying the regeneration tower reflux water as washing water to the two-stage water washing section 65. The amine recovery capability in the water washing section 65 is further improved. Further, since the wash water of the two-stage water washing section 65 is extracted and supplied to the first-stage water washing section 64, the amine concentration of the washing water in the first-stage water washing section 64 is also reduced. The collection capacity is also improved.

なお、上記のように再生塔還流水は二段水洗部６５に供給し、この二段水洗部６５の洗浄水を抜き出して一段水洗部６４に供給するようにすることが望ましいが、必ずしもこれに限定するものではなく、再生塔還流水を二段水洗部６５と一段水洗部６４とに同時に供給するようにしてもよい。   As described above, it is desirable that the recirculation tower reflux water is supplied to the two-stage water washing section 65, and the washing water from the two-stage water washing section 65 is extracted and supplied to the first-stage water washing section 64, but this is not necessarily the case. The present invention is not limited to this, and the regeneration tower reflux water may be supplied to the two-stage water washing section 65 and the one-stage water washing section 64 at the same time.

また、本実施の形態によれば、二酸化炭素吸収部７３、一段水洗部６４及び二段水洗部６５の出口にデミスタ８３，８４，８５を設置したことにより、二酸化炭素吸収部７３に供給される吸収液ミストの一部や一段水洗部６４及び二段水洗部６５に供給される洗浄水ミストの一部が脱炭酸排ガスとともに吸収塔外へ放出されて水分やアミン化合物がロスするのを防止することができる。   Further, according to the present embodiment, the demisters 83, 84, and 85 are installed at the outlets of the carbon dioxide absorption unit 73, the first-stage water washing unit 64, and the second-stage water washing unit 65, so that the carbon dioxide absorption unit 73 is supplied. A part of the absorption liquid mist and a part of the washing water mist supplied to the first-stage water washing unit 64 and the second-stage water washing unit 65 are prevented from being released to the outside of the absorption tower together with the decarbonized exhaust gas, thereby losing moisture and amine compounds. be able to.

そして、上記のようなアミン回収装置を備えた脱炭酸ガス装置は、アミン化合物の回収能力が高くて運転コストの安価な装置となる。   And the decarbonation gas apparatus provided with the above amine collection | recovery apparatuses becomes an apparatus with a high collection | recovery capability of an amine compound, and a low operating cost.

なお、一段水洗部６４及び二段水洗部６５は充填塔であっても、棚段塔であってもよい。   In addition, the 1st stage water washing part 64 and the 2nd stage water washing part 65 may be a packed tower, or a shelf tower.

また、上記実施の形態では水洗部を二段構成としているが、必ずしもこれに限定するものではなく、水洗部を三段以上の複数段構成としてもよい。この場合にも、アミン化合物を含む脱炭酸排ガスに対して、前段（脱炭酸排ガス流の上流段）の水洗部でアミン回収処理をした後、更に、後段（脱炭酸排ガス流の下流段）の水洗部でもアミン回収処理を行う。即ち、複数段の水洗部において、順次、脱炭酸排ガスに同伴するアミン化合物の回収処理を行う。また、この場合には、複数段の水洗部のうちの最も後段の水洗部に再生塔還流抜き出し水を供給するとともに、この最も後段の水洗部から、その前段の水洗部へ、更に、その前段の水洗部へと、順次、洗浄水を抜き出して供給するようにすればよい。   Moreover, in the said embodiment, although the water washing part is made into 2 steps | paragraphs structure, it is not necessarily limited to this, and a water washing part is good also as a multistage structure more than 3 steps | paragraphs. In this case as well, after the decarbonation exhaust gas containing the amine compound is subjected to amine recovery treatment in the water washing section of the first stage (upstream stage of the decarbonation exhaust gas stream), the second stage (downstream stage of the decarbonation exhaust gas stream) The amine recovery process is also performed in the water washing section. That is, the recovery process of the amine compound accompanying the decarbonized exhaust gas is sequentially performed in a plurality of water washing sections. Further, in this case, the recirculation tower reflux water is supplied to the rearmost water washing section of the plurality of water washing sections, and from the rearmost water washing section to the front water washing section, further to the front water washing section. The washing water may be sequentially extracted and supplied to the water washing section.

また、上記実施の形態では燃料の燃焼排ガスに含まれる二酸化炭素を吸収する場合を例に挙げて説明したが、これに限定するものではなく、脱炭酸処理の対象となる二酸化炭素含有ガスとしては、燃料用ガスなどのプロセスガスであってもよく、その他様々なガスが適用できる。また、脱炭酸処理の対象となる二酸化炭素含有ガスの圧力は加圧であっても、常圧であってもよく、温度は低温であっても、高温であってもよく、特に制限はない。好ましくは、常圧の燃焼排ガスである。   In the above embodiment, the case where carbon dioxide contained in the combustion exhaust gas of fuel is absorbed is described as an example. However, the present invention is not limited to this, and the carbon dioxide-containing gas to be decarboxylated is Further, it may be a process gas such as a fuel gas, and various other gases can be applied. Further, the pressure of the carbon dioxide-containing gas to be decarboxylated may be pressurized or normal pressure, the temperature may be low or high, and there is no particular limitation. . Preferably, it is an atmospheric pressure combustion exhaust gas.

［具体的な実験例の説明］
ここで、実験例により本発明を具体的に説明するが、本発明はこれらに限定されるものではない。 [Explanation of specific experimental examples]
Here, although the present invention will be specifically described by way of experimental examples, the present invention is not limited thereto.

＜実験例＞
本発明の方法として次のような実験を行った。即ち、二酸化炭素１０％を含む燃焼排ガス３０Nm3/h を吸収塔６１の二酸化炭素吸収部７３に供給し、アルコール性水酸基含有２級アミンの水溶液（吸収液）と向流接触させて二酸化炭素を吸収した。残りの脱炭酸排ガスを二酸化炭素吸収部出口のデミスタ８３に供給後、一段水洗部６４にて洗浄水と液／ガス比2.2l/Nm3で向流接触させ、一段水洗部出口のデミスタ８４を通過させた。更に、二段水洗部６５にて脱炭酸排ガスを洗浄水と液／ガス比2.2l/Nm3で向流接触させ、二段水洗部出口のデミスタ８５を通過させた後に系外へ放出した。この際、一段水洗部出口ガス温度及び二段水洗部出口ガス温度が共に４６℃となるように運転するとともに、二段水洗部６５には再生塔還流抜き出し水を1.1l/hで供給し、二段水洗部６５の洗浄水を抜き出して一段水洗部６４に供給した。その結果、吸収塔６１から系外に放出された脱炭酸排ガス中のアミン濃度は８ppm であった。 <Experimental example>
The following experiment was conducted as the method of the present invention. That is, the combustion exhaust gas 30Nm 3 / h containing 10% carbon dioxide is supplied to the carbon dioxide absorption part 73 of the absorption tower 61, and is brought into countercurrent contact with an aqueous solution (absorbing liquid) of an alcoholic hydroxyl group-containing secondary amine so that carbon dioxide is brought into contact. Absorbed. The remaining decarbonation exhaust gas is supplied to the demister 83 at the outlet of the carbon dioxide absorption section, and then brought into countercurrent contact with the cleaning water at a liquid / gas ratio of 2.2 l / Nm 3 in the first stage washing section 64, and the demister 84 at the first stage washing section exit is I let it pass. Further, the decarbonized exhaust gas was brought into countercurrent contact with the wash water at a liquid / gas ratio of 2.2 l / Nm 3 in the two-stage water washing section 65, passed through the demister 85 at the outlet of the two-stage water washing section, and then discharged out of the system. At this time, the operation was performed so that the outlet gas temperature of the first-stage flushing section and the outlet gas temperature of the second-stage flushing section were both 46 ° C., and the recirculated tower reflux water was supplied to the second-stage flushing section 65 at 1.1 l / h. The washing water from the two-stage water washing section 65 was extracted and supplied to the first-stage water washing section 64. As a result, the amine concentration in the decarbonation exhaust gas discharged from the absorption tower 61 to the outside of the system was 8 ppm.

＜比較例１＞
従来法として、上記実験例において水洗部を一段とし、再生塔還流抜き出し水を一段水洗部に供給する他は、上記実験例と同様に実施した。その結果、吸収塔６１から系外に放出された脱炭酸排ガス中のアミン濃度は２５ppm と上記実施例に比較して高かった。 <Comparative Example 1>
As a conventional method, it was carried out in the same manner as in the above experimental example, except that in the above experimental example, the washing section was one stage and the recirculation tower reflux water was supplied to the single stage washing section. As a result, the amine concentration in the decarbonation exhaust gas discharged out of the system from the absorption tower 61 was 25 ppm, which was higher than that in the above example.

＜比較例２＞
上記実験例において、二段水洗部抜き出し液（洗浄水）を一段水洗部６４に供給せず、その他は上記実験例と同様に実施した。その結果、吸収塔から系外に放出された脱炭酸排ガス中のアミン濃度は１１ppm であった。この値は上記比較例１と比較すると充分に低い値であるが、上記実験例と比較すると高い値であった。このことから、二段水洗部６５の洗浄水を抜き出して一段水洗部６４に供給することの有効性が確認できた。 <Comparative Example 2>
In the above experimental example, the two-stage water washing part extraction liquid (washing water) was not supplied to the single-stage water washing part 64, and the others were carried out in the same manner as in the above experimental example. As a result, the amine concentration in the decarbonation exhaust gas discharged out of the system from the absorption tower was 11 ppm. This value is a sufficiently low value as compared with Comparative Example 1, but is a high value as compared with the Experimental Example. From this, the effectiveness of extracting the wash water from the two-stage water washing section 65 and supplying it to the first-stage water washing section 64 could be confirmed.

上記実験例と上記比較例１，２の結果をまとめると、［表１］のとおりである。水洗部を二段構成にすることにより、系外に放出されるアミン濃度を充分に低く抑えることができ、また、二段水洗部６５の洗浄水を抜き出して一段水洗部６４に供給すれば更に系外に放出されるアミン濃度を低く抑えることができる。   The results of the experimental example and the comparative examples 1 and 2 are summarized as shown in [Table 1]. By making the washing section into a two-stage configuration, the amine concentration released to the outside of the system can be kept sufficiently low, and if the washing water from the two-stage washing section 65 is extracted and supplied to the one-stage washing section 64 The amine concentration released out of the system can be kept low.

Figure 0004625478
Figure 0004625478

本発明の実施の形態に係る脱炭酸ガス装置の主要部を示す構成図であるである。It is a block diagram which shows the principal part of the decarboxylation gas apparatus which concerns on embodiment of this invention. 従来の脱炭酸ガス装置の主要部を示す構成図である。It is a block diagram which shows the principal part of the conventional decarbonation gas apparatus. 従来の脱炭酸ガス装置の主要部を示す構成図である。It is a block diagram which shows the principal part of the conventional decarbonation gas apparatus.

符号の説明Explanation of symbols

６１ 吸収塔
６２ 再生塔
６３ 冷却塔
６４ 一段水洗部
６５ 二段水洗部
６６ 排ガス供給ライン
６７ 冷却塔底部
６８ 循環ポンプ
６９ 熱交換器
７０ ノズル
７１ 充填部
７２ 排ガス供給ライン
７３ 二酸化炭素吸収部
７４ 吸収液供給ライン
７５ ノズル
７６ 再生塔底部
７７ 吸収液供給ポンプ
７８ 熱交換器
７９ 熱交換器
８０ 吸収塔底部
８１，８２ 液保留部
８３，８４，８５ デミスタ
８６ 吸収液排出ライン
８７ 吸収液排出ポンプ
８８ 下部充填部
８９ ノズル
９０ リボイラ
９１ 上部充填部
９２ ノズル
９３ 二酸化炭素排出ライン
９４ コンデンサ
９５ 二酸化炭素分離器
９６ 循環ポンプ
９７ 再生塔還流水供給ライン
９８ 熱交換器
９９ ノズル
１００ 還流ライン
１０１ 循環ライン
１０２ 循環ポンプ
１０３ 熱交換器
１０４ ノズル
１０５ 保留水排出ライン
１０６ 循環ライン
１０７ 循環ポンプ
１０８ 保留水排出ライン
１０９ 吸収塔頂部
１１０ ガス放出ライン
１１１ 再生塔頂部 61 Absorption tower 62 Regeneration tower 63 Cooling tower 64 Single-stage flushing section 65 Two-stage flushing section 66 Exhaust gas supply line 67 Cooling tower bottom 68 Circulation pump 69 Heat exchanger 70 Nozzle 71 Filling section 72 Exhaust gas supply line 73 Carbon dioxide absorption section 74 Absorbing liquid Supply line 75 Nozzle 76 Regeneration tower bottom 77 Absorption liquid supply pump 78 Heat exchanger 79 Heat exchanger 80 Absorption tower bottom 81,82 Liquid holding part 83,84,85 Demister 86 Absorption liquid discharge line 87 Absorption liquid discharge pump 88 Lower filling Part 89 nozzle 90 reboiler 91 upper filling part 92 nozzle 93 carbon dioxide discharge line 94 condenser 95 carbon dioxide separator 96 circulation pump 97 regeneration tower reflux water supply line 98 heat exchanger 99 nozzle 100 reflux line 101 circulation line 102 circulation pump 103 heat Exchanger 104 Le 105 hold water discharge line 106 circulation line 107 circulating pump 108 hold water discharge line 109 absorption tower top 110 gas discharge line 111 regenerator top

Claims (7)

二酸化炭素吸収部においてアミン化合物を含有する吸収液との気液接触により二酸化炭素が吸収除去された脱炭酸排ガスに対し、水洗部において洗浄水と気液接触させることより、前記脱炭酸排ガスに同伴するアミン化合物を回収するアミン回収方法において、
前記水洗部を複数段構成とし、且つ、各段では、前記水洗部の入口側に設けられた液保留部に保留されている洗浄水を、前記水洗部の出口側へと輸送して、前記水洗部へ供給し、
前記複数段の水洗部において、順次、前記脱炭酸排ガスに同伴するアミン化合物の回収処理を行うとともに、
二酸化炭素吸収部及び各段の水洗部の出口にデミスタを設け、これらのデミスタによって脱炭酸排ガスに同伴する吸収液ミストや洗浄水ミストを除去し、
且つ、後段の水洗部における液保留部から洗浄水を抜き出し、前段のデミスタをバイパスして、前段の水洗部又は前段の水洗部における液保留部へ供給することを特徴とするアミン回収方法。 The decarbonized exhaust gas from which carbon dioxide has been absorbed and removed by gas-liquid contact with the absorbing liquid containing an amine compound in the carbon dioxide absorbing part is brought into contact with the washing water in the water washing part, thereby accompanying the decarbonized exhaust gas. In an amine recovery method for recovering an amine compound to be
The flushing section has a multi-stage configuration, and in each stage, the washing water held in the liquid holding part provided on the inlet side of the flushing part is transported to the outlet side of the flushing part, Supply to the water washing section,
In the plurality of water washing sections, sequentially performing a recovery process of the amine compound accompanying the decarbonation exhaust gas,
A demister is provided at the outlet of the carbon dioxide absorption section and the water washing section of each stage, and the absorption mist and washing water mist accompanying the decarbonized exhaust gas are removed by these demisters,
And the amine recovery method characterized by extracting wash water from the liquid storage part in a subsequent water washing part, bypassing a front demister, and supplying to a liquid storage part in a front water washing part or a front water washing part. 請求項１に記載するアミン回収方法において、
再生塔還流水を、前記液保留部から前記水洗部の出口側へ輸送される洗浄水と合流させて、前記水洗部に供給することを特徴とするアミン回収方法。 In the amine recovery method according to claim 1,
A method for recovering an amine, characterized in that the recirculating tower reflux water is combined with the washing water transported from the liquid holding section to the outlet side of the washing section and supplied to the washing section. 請求項１又は２に記載するアミン回収方法において、
前記液保留部から前記水洗部の出口側への前記洗浄水の輸送は循環ポンプによって行うことを特徴とするアミン回収方法。 In the amine recovery method according to claim 1 or 2 ,
The amine recovery method is characterized in that the cleaning water is transported from the liquid holding section to the outlet side of the water washing section by a circulation pump. 二酸化炭素吸収部においてアミン化合物を含有する吸収液との気液接触により二酸化炭素が吸収除去された脱炭酸排ガスに対し、水洗部において洗浄水と気液接触させることより、前記脱炭酸排ガスに同伴するアミン化合物を回収するように構成したアミン回収装置において、
前記水洗部を複数段構成とし、且つ、各段では、前記水洗部の入口側に設けられた液保留部に保留されている洗浄水を、前記水洗部の出口側へと輸送して、前記水洗部へ供給する構成として、
前記複数段の水洗部において、順次、前記脱炭酸排ガスに同伴するアミン化合物の回収処理を行うとともに、
二酸化炭素吸収部及び各段の水洗部の出口にデミスタを設け、これらのデミスタによって脱炭酸排ガスに同伴する吸収液ミストや洗浄水ミストを除去するように構成し、
且つ 後段の水洗部における液保留部から洗浄水を抜き出し、前段のデミスタをバイパスして、前段の水洗部又は前段の水洗部における液保留部へ供給するように構成したことを特徴とするアミン回収装置。 The decarbonized exhaust gas from which carbon dioxide has been absorbed and removed by gas-liquid contact with the absorbing liquid containing an amine compound in the carbon dioxide absorbing part is brought into contact with the washing water in the water washing part, thereby accompanying the decarbonized exhaust gas. In the amine recovery device configured to recover the amine compound to be
The flushing section has a multi-stage configuration, and in each stage, the washing water held in the liquid holding part provided on the inlet side of the flushing part is transported to the outlet side of the flushing part, As a configuration to supply to the washing section,
In the plurality of water washing sections, sequentially performing a recovery process of the amine compound accompanying the decarbonation exhaust gas,
A demister is provided at the outlet of the carbon dioxide absorption section and the water washing section of each stage, and is configured to remove absorption liquid mist and washing water mist accompanying the decarbonized exhaust gas by these demisters,
The amine recovery is characterized in that the wash water is extracted from the liquid holding section in the subsequent water washing section, and is supplied to the liquid washing section in the previous water washing section or the previous water washing section, bypassing the previous demister. apparatus. 請求項４に記載するアミン回収装置において、
再生塔還流水を、前記液保留部から前記水洗部の出口側へ輸送される洗浄水と合流させて、前記水洗部に供給するように構成したことを特徴とするアミン回収装置。 In the amine recovery device according to claim 4 ,
The amine recovery apparatus, wherein the regeneration tower reflux water is combined with the washing water transported from the liquid holding section to the outlet side of the washing section and supplied to the washing section. 請求項４又は５に記載するアミン回収装置において、
前記液保留部から前記水洗部の出口側への前記洗浄水の輸送は循環ポンプによって行う構成としたことを特徴とするアミン回収装置。 In the amine recovery device according to claim 4 or 5 ,
The amine recovery apparatus is characterized in that the washing water is transported from the liquid holding section to the outlet side of the washing section by a circulation pump. 請求項４，５又は６の何れか１項に記載するアミン回収装置を吸収塔に備えたことを特徴とする脱炭酸ガス装置。 A decarbonation gas apparatus comprising the absorption tower of the amine recovery apparatus according to any one of claims 4, 5 and 6 .
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