JP5595243B2 - CO2 and H2S containing gas recovery system and method - Google Patents

CO2 and H2S containing gas recovery system and method Download PDF

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JP5595243B2
JP5595243B2 JP2010261841A JP2010261841A JP5595243B2 JP 5595243 B2 JP5595243 B2 JP 5595243B2 JP 2010261841 A JP2010261841 A JP 2010261841A JP 2010261841 A JP2010261841 A JP 2010261841A JP 5595243 B2 JP5595243 B2 JP 5595243B2
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晋也 立花
浩司 堀添
盛紀 村上
昌記 湯島
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Mitsubishi Heavy Industries Ltd
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Description

本発明は、例えば石炭やバイオマス等をガス化炉によりガス化して得られるガス化ガスに含まれるＣＯ2とＨ2ＳからＨ2Ｓを効率よく回収するＣＯ2及びＨ2Ｓを含むガスの回収システム及び方法に関する。 The present invention is, for example, coal and biomass such a gas containing CO 2 and H 2 S to efficiently recover H 2 S from CO 2 and H 2 S contained in the gasification gas obtained by gasifying the gasification furnace The present invention relates to a collection system and method.

石炭やバイオマス等をガス化炉でガス化したガス化ガス等に含まれるＣＯ2とＨ2Ｓ等の酸性ガスを除去する技術として、従来より、化学吸収法（例えば、アミン吸収液（例えば（Ｎ−メチルジエタノールアミン：ＭＤＥＡ等の吸収液利用））や物理吸収法（例えば、ポリエチレングリコール・ジメチルエーテルを用いるＳｅｌｅｘｏｌ吸収液利用)が提案されている。 Conventionally, as a technique for removing acid gas such as CO 2 and H 2 S contained in gasification gas obtained by gasifying coal or biomass in a gasification furnace, a chemical absorption method (for example, an amine absorption liquid (for example, ( N-methyldiethanolamine: using an absorbing solution such as MDEA)) and physical absorption methods (for example, using a Selexol absorbing solution using polyethylene glycol dimethyl ether) have been proposed.

ところで、ＩＧＣＣ（石炭ガス化複合発電）技術のようなシステムの場合、以下のような要求がある。
１） 発電システムにおいて、大気汚染物質であるＳＯＸの排出を規制値未満とするために、ＳＯＸの発生源となるＨ2Ｓの除去が必要となる。一方で、発電効率を上昇させる効果があるため、ＣＯ２は極力回収しないことが望ましい。
２） 回収したＨ2Ｓ含有ガス（オフガス）流量が少なく、Ｈ2Ｓ濃度が高い方が、回収ガスから化成品を製造する場合やＨ2Ｓを処理する場合に有利であり、Ｈ2Ｓを選択的に回収できることが望ましい。
３） ＩＧＣＣにＣＯシフトとＣＣＳ(二酸化炭素回収・貯留)とを組み合わせたシステムでは、ＣＯ2回収プロセスで回収したＣＯ2中のＨ2Ｓ濃度を規定値（例えば１０〜２０ｐｐｍ）程度に抑える必要がある。
４） 発電効率を向上させるためには、スチーム等の熱エネルギーの使用量は少ないほど好ましい。
すなわち、ＣＯ2とＨ2Ｓとを含むガスから、Ｈ2Ｓを熱エネルギーの面で効率的、かつ選択的に分離することが求められている。 By the way, in the case of a system such as IGCC (Coal Gasification Combined Cycle) technology, there are the following requirements.
1) In a power generation system, it is necessary to remove H 2 S, which is a source of SO X , in order to make the emission of SO X , which is an air pollutant, less than the regulated value. On the other hand, since it has the effect of increasing the power generation efficiency, it is desirable not to collect CO 2 as much as possible.
2) The recovered H 2 S-containing gas (off-gas) flow is low, H 2 S concentration is higher is the advantage when processing or when H 2 S to produce from collected gasification finished products, H 2 It is desirable that S can be selectively recovered.
3) a system that combines the CO shift and CCS (carbon capture and storage) is the IGCC, the concentration of H 2 S in the CO 2 recovered by the CO 2 recovery process specified value (e.g., 10 to 20 ppm) necessary to suppress the degree There is.
4) In order to improve the power generation efficiency, it is preferable that the amount of heat energy such as steam used is as small as possible.
That is, it is required to efficiently and selectively separate H 2 S from a gas containing CO 2 and H 2 S in terms of thermal energy.

そこで、従来では、Ｈ2Ｓを選択的に吸収する吸収液の提案がある（特許文献１、２）。 Therefore, conventionally, there is a proposal of an absorption liquid that selectively absorbs H 2 S (Patent Documents 1 and 2).

特開昭５３−８６６８１号公報JP-A-53-86681 特表平６−５００２５９号公報Japanese Patent Publication No. 6-500309

しかしながら、特許文献１、２の技術では、エネルギー効率が悪い、という問題がある。   However, the techniques of Patent Documents 1 and 2 have a problem that energy efficiency is poor.

よって、化学吸収プロセスにおいて、ＣＯ2とＨ2Ｓとを含むガスから、ＣＯ2の吸収とは別にＨ2Ｓを熱エネルギーの面で効率的、かつ選択的に分離することができる手段の出現が切望されている。 Therefore, in the chemical absorption process, the emergence of means capable of efficiently and selectively separating H 2 S from the gas containing CO 2 and H 2 S separately from the absorption of CO 2 in terms of thermal energy. Is anxious.

本発明は、前記問題に鑑み、例えば石炭やバイオマス等をガス化炉によりガス化して得られるガス化ガスに含まれるＨ2Ｓを効率よく回収するＣＯ2及びＨ2Ｓを含むガスの回収システム及び方法を提供することを課題とする。 In view of the above problems, the present invention provides a gas recovery system including CO 2 and H 2 S that efficiently recovers H 2 S contained in a gasification gas obtained by gasifying coal, biomass, or the like with a gasification furnace. And providing a method.

上述した課題を解決するための本発明の第１の発明は、ＣＯ2及びＨ2Ｓを含むガスを導入ガスとし、該導入ガスとＣＯ2及びＨ2Ｓを吸収する吸収液とを接触させて前記導入ガスからＣＯ２及びＨ2Ｓを吸収させる吸収塔と、ＣＯ２及びＨ2Ｓを吸収した吸収液を吸収塔の塔底部から抜き出し、第１の供給ラインを介して塔頂部より導入し、リボイラの熱によりＣＯ２及びＨ2Ｓを放出させて吸収液を再生する吸収液再生塔と、再生された再生吸収液を吸収塔側に戻す第２の供給ラインと、前記導入ガスのＣＯ2濃度を計測する計測器とを具備すると共に、前記第２の供給ラインを複数分岐し、その分岐先を吸収塔の高さ方向の中段から塔頂側に沿って設けると共に、前記吸収塔の底部側から前記導入ガスを導入する際、前記計測器による前記導入ガス中のＣＯ2濃度が、１０ｍｏｌ％−ｄｒｙを超える場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段に変更する制御を行うと共に、前記計測器による導入ガス中のＣＯ 2 濃度が、１０ｍｏｌ％−ｄｒｙ以下の場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段よりも塔頂側に変更する制御を行い、Ｈ 2 Ｓの吸収量を所望に維持すると共に、ＣＯ 2 の回収量を低く保つように制御することを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収システムにある。
第２の発明は、第１の発明において、前記計測器による導入ガス中のＣＯ 2 濃度が、８ｍｏｌ％−ｄｒｙよりもさらに低い場合には、再生された吸収液の複数の導入位置をさらに塔頂側へ変更ことを特徴とするＣＯ 2 及びＨ 2 Ｓを含むガスの回収システムにある。 The first invention of the present invention for solving the above-described problem is that a gas containing CO 2 and H 2 S is used as an introduction gas, and the introduction gas is brought into contact with an absorption liquid that absorbs CO 2 and H 2 S. An absorption tower that absorbs CO 2 and H 2 S from the introduced gas and an absorption liquid that absorbs CO 2 and H 2 S are withdrawn from the tower bottom of the absorption tower and introduced from the top of the tower through the first supply line. An absorption liquid regeneration tower that regenerates the absorption liquid by releasing CO 2 and H 2 S by the heat of the reboiler, a second supply line that returns the regenerated regeneration absorption liquid to the absorption tower side, and the introduction gas together; and a measuring device for measuring the CO 2 concentration, together with the second supply line to a plurality branches, provided along the branch destination from the middle in the height direction of the absorption tower to tower top side, the absorption tower when the bottom side for introducing the gas introduced, by the measuring instrument CO 2 concentration of the serial introduction gas, together with the case of more than 10 mol% -dry controls to change the introduction position location of the regenerated absorption liquid to the middle in the height direction of the absorption tower, by the measuring instrument CO 2 concentration in the introduced gas is, if: 10 mol% -dry performs control to change the column top side of the middle in the height direction of the absorption column to the position of the introduction of regenerated absorption liquid, H 2 A gas recovery system containing CO 2 and H 2 S is characterized in that the absorption amount of S is maintained as desired and the CO 2 recovery amount is controlled to be low .
According to a second invention, in the first invention, when the CO 2 concentration in the introduced gas by the measuring instrument is lower than 8 mol% -dry, a plurality of introduction positions of the regenerated absorbing liquid are further provided. It is in the recovery system of the gas containing CO 2 and H 2 S, which is characterized by being changed to the top side .

第３の発明は、第１又は２の発明において、前記計測器による導入ガス中のＣＯ2濃度に応じて、前記吸収塔と前記吸収液再生塔との吸収液の循環量をさらに変化させる制御を行うことを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収システムにある。 The third invention is the control according to the first or second invention, wherein the circulating amount of the absorption liquid between the absorption tower and the absorption liquid regeneration tower is further changed according to the CO 2 concentration in the introduced gas by the measuring instrument. The gas recovery system includes CO 2 and H 2 S.

第４の発明は、第１乃至３のいずれか一つの発明において、前記吸収塔からＣＯ２及びＨ2Ｓを一部吸収した吸収液を外部に抜き出すと共に、導入する抜出・導入ラインと、該抜出・導入ラインに介装され、抜き出した吸収液を冷却する冷却器とを具備することを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収システムにある。 According to a fourth invention, in any one of the first to third inventions, an extraction / introduction line for extracting and introducing an absorption liquid partially absorbing CO 2 and H 2 S from the absorption tower to the outside A gas recovery system including CO 2 and H 2 S, which is provided in the extraction / introduction line and includes a cooler for cooling the extracted absorption liquid.

第５の発明は、ＣＯ2及びＨ2Ｓを含むガスを導入ガスからＣＯ2及びＨ2Ｓを回収する吸収塔と、ＣＯ２及びＨ2Ｓを吸収した吸収液からＣＯ２及びＨ2Ｓを放出させて吸収液を再生する吸収液再生塔とを用いたＣＯ2及びＨ2Ｓを含むガスの回収方法であって、前記吸収塔の底部側から前記導入ガスを導入する際、前記導入ガス中のＣＯ2濃度を計測し、前記計測による導入ガス中のＣＯ 2 濃度が、１０ｍｏｌ％−ｄｒｙを超える場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段に変更する制御を行うと共に、前記計測による導入ガス中のＣＯ 2 濃度が、１０ｍｏｌ％−ｄｒｙ以下の場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段よりも塔頂側に変更する制御を行い、Ｈ 2 Ｓの吸収量を所望に維持すると共に、ＣＯ 2 の回収量を低く保つように制御することを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収方法にある。
第６の発明は、第５の発明において、前記計測器による導入ガス中のＣＯ 2 濃度が、８ｍｏｌ％−ｄｒｙよりもさらに低い場合には、再生された吸収液の複数の導入位置をさらに塔頂側へ変更ことを特徴とするＣＯ 2 及びＨ 2 Ｓを含むガスの回収システムにある。 A fifth invention is, CO 2 and H 2 S gas from the introduction gas containing absorption tower to recover CO 2 and H 2 S, CO 2 and H 2 from the absorbent solution that has absorbed S CO 2 and H 2 S Is a method for recovering a gas containing CO 2 and H 2 S using an absorption liquid regeneration tower that regenerates the absorption liquid and introducing the introduced gas from the bottom side of the absorption tower. measuring the CO 2 concentration in the gas, the CO 2 concentration in the introduced gas by the measurement, if it exceeds 10 mol% -dry is the introduction position of the regenerated absorption liquid in the height direction of the middle of the absorption tower When the CO 2 concentration in the introduced gas by the measurement is 10 mol% -dry or less, the regenerative absorption liquid is introduced at a position higher than the middle stage in the height direction of the absorption tower. performs control to change to the side, to keep the absorption of H 2 S to the desired Both in the method of recovering gas comprising CO 2 and H 2 S, wherein the controller controls so as to keep low recovery of CO 2.
According to a sixth invention, in the fifth invention, when the CO 2 concentration in the introduced gas by the measuring instrument is lower than 8 mol% -dry, a plurality of introduction positions of the regenerated absorbing liquid are further provided. It is in the recovery system of the gas containing CO 2 and H 2 S, which is characterized by being changed to the top side .

第７の発明は、第５又は６の発明において、計測器による導入ガス中のＣＯ2濃度に応じて、前記吸収塔と前記吸収液再生塔との吸収液の循環量をさらに変化させることを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収方法にある。 According to a seventh invention, in the fifth or sixth invention, the circulation amount of the absorption liquid between the absorption tower and the absorption liquid regeneration tower is further changed according to the CO 2 concentration in the introduced gas by the measuring instrument. in a method for recovering a gas containing CO 2 and H 2 S, wherein.

第８の発明は、第５乃至７のいずれか一つの発明において、吸収塔からＣＯ２及びＨ2Ｓを一部吸収した吸収液を外部に抜き出し、抜き出した吸収液を冷却した後、吸収塔に戻すことを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収方法にある。 According to an eighth invention, in any one of the fifth to seventh inventions, the absorption liquid partially absorbing CO 2 and H 2 S is extracted from the absorption tower, and the extracted absorption liquid is cooled and then absorbed. The method is for recovering a gas containing CO 2 and H 2 S, which is returned to the column.

本発明によれば、導入ガス中のＣＯ2濃度に応じて、吸収液流量を変化させることで、Ｈ2Ｓの回収量を満足しつつ、ＣＯ2の回収量を極力低くすることができる。 According to the present invention, the amount of CO 2 recovered can be made as low as possible while satisfying the amount of H 2 S recovered by changing the flow rate of the absorbing liquid according to the CO 2 concentration in the introduced gas.

図１は、実施例１に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。FIG. 1 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the first embodiment. 図２は、実施例２に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。FIG. 2 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the second embodiment. 図３は、実施例３に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。FIG. 3 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the third embodiment. 図４は、実施例３に係る他のＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。FIG. 4 is a schematic diagram of another gas recovery system including CO 2 and H 2 S according to the third embodiment. 図５は、実施例３に係る他のＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。FIG. 5 is a schematic diagram of another gas recovery system including CO 2 and H 2 S according to the third embodiment. 図６は、本試験例に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの吸収塔部分の模式図である。FIG. 6 is a schematic view of an absorption tower portion of a gas recovery system containing CO 2 and H 2 S according to this test example. 図７−１は、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の高さ位置（段数）との関係図である。FIG. 7-1 is a graph showing the relationship between the CO 2 recovery amount (left vertical axis) / H 2 S concentration in the outlet gas (right vertical axis) and the height position (stage number) of the absorption tower. 図７−２は、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の高さ位置（段数）との関係図である。FIG. 7-2 is a relationship diagram between the CO 2 recovery amount (left vertical axis) / H 2 S concentration in the outlet gas (right vertical axis) and the height position (stage number) of the absorption tower. 図７−３は、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の高さ位置（段数）との関係図である。FIG. 7-3 is a relationship diagram between the CO 2 recovery amount (left vertical axis) / the H 2 S concentration in the outlet gas (right vertical axis) and the height position (number of stages) of the absorption tower. 図８−１は、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の出口液温度との関係図である。FIG. 8-1 is a relationship diagram of CO 2 recovery amount (left vertical axis) / H 2 S concentration in the outlet gas (right vertical axis) and the outlet liquid temperature of the absorption tower. 図８−２は、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の出口液温度との関係図である。FIG. 8-2 is a relationship diagram of CO 2 recovery amount (left vertical axis) / H 2 S concentration in the outlet gas (right vertical axis) and the outlet liquid temperature of the absorption tower. 図８−３は、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の出口液温度との関係図である。FIG. 8-3 is a relationship diagram of CO 2 recovery amount (left vertical axis) / H 2 S concentration in the outlet gas (right vertical axis) and the outlet liquid temperature of the absorption tower.

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

本発明による実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システムについて、図面を参照して説明する。図１は、実施例１に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。
図１に示すように、本実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ａは、例えば石炭やバイオマス等をガス化するガス化炉等から得られたＣＯ2及びＨ2Ｓを含むガス化ガスを導入ガス１１とし、該導入ガス１１とＣＯ2及びＨ2Ｓを吸収する吸収液１２とを接触させて前記導入ガス１１からＣＯ２及びＨ2Ｓを吸収させる吸収塔１３と、ＣＯ２及びＨ2Ｓを吸収した吸収液（リッチ溶液）１２Ａを吸収塔１３の塔底部１３ｃより抜き出すと共に、第１の供給ラインＬ1を介して塔頂部１４ａより導入し、リボイラ１５の熱によりＣＯ２及びＨ2Ｓを放出させて吸収液１２を再生する吸収液再生塔（以下「再生塔」という）１４と、再生された吸収液（リーン溶液）１２Ｂを再生塔１４の塔底部１４ｃより抜き出し、吸収塔１３側に戻す第２の供給ラインＬ2と、前記導入ガス１１のＣＯ2濃度を計測する計測器４１とを具備すると共に、前記第２の供給ラインＬ2を複数（本実施例では４つ）に分岐して供給ラインＬ2-1、Ｌ2-2、Ｌ2-3、Ｌ2-4とすると共に、その分岐先の導入口１３b-１〜１３b-4を吸収塔１３の高さ方向に沿って設け、前記計測器４１による導入ガス１１中のＣＯ2濃度に応じて、再生された吸収液の導入位置又は導入量のいずれか一方又は両方を吸収塔の鉛直高さ方向のいずれかに変更するものである。
このシステムでは、前記再生塔１４でＣＯ２及びＨ2Ｓを除去し、再生された吸収液（リーン溶液）１２Ｂは吸収液１２として再利用される。 A gas recovery system including CO 2 and H 2 S according to an embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the first embodiment.
As shown in FIG. 1, recovery system 10A of the gas containing CO 2 and H 2 S according to the present embodiment, for example, coal CO 2 a and biomass, etc. obtained from the gasification furnace to gasify and H 2 S and introducing gas 11 gasification gas containing, the introduced gas 11 and CO 2 and H 2 S from the inlet gas 11 contacting the absorbing liquid 12 that absorbs CO 2 and H 2 absorption tower 13 to absorb S And the absorbent (rich solution) 12A that has absorbed CO 2 and H 2 S is extracted from the tower bottom 13c of the absorption tower 13 and introduced from the tower top 14a via the first supply line L 1 . An absorption liquid regeneration tower (hereinafter referred to as a “regeneration tower”) 14 that regenerates the absorption liquid 12 by releasing CO 2 and H 2 S by heat, and a regenerated absorption liquid (lean solution) 12B from the bottom of the regeneration tower 14 Extracted from 14c, absorption tower A second supply line L 2 back to the 3 side, as well as and a measuring instrument 41 for measuring the CO 2 concentration of the inlet gas 11, four in the second plurality of supply lines L 2 of (in this embodiment ) And supply lines L 2-1 , L 2-2 , L 2-3 , and L 2-4, and the branch destination inlets 13 b-1 to 13 b-4 are connected to the absorption tower 13. Depending on the CO 2 concentration in the introduced gas 11 by the measuring instrument 41, either or both of the introduction position and the introduction amount of the regenerated absorbing liquid are provided along the height direction, and the vertical height direction of the absorption tower. It is to change to either.
In this system, CO 2 and H 2 S are removed by the regeneration tower 14, and the regenerated absorbent (lean solution) 12 B is reused as the absorbent 12.

このＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ａを用いた精製方法では、石炭やバイオマス等をガス化するガス化炉で得られたガス化ガスは、ガス冷却装置（図示せず）に送られ、ここで冷却水により冷却され、導入ガス１１として吸収塔１３に導入される。
吸収塔１３は、塔内部に充填部１３Ａ〜１３Ｄが設けられ、これらの充填部１３Ａ〜１３Ｄを通過する際、導入ガス１１と吸収液１２との対向接触効率を向上させている。なお、充填部は複数設けてもよく、充填法以外に、例えばスプレー法、液柱法、棚段法等により導入ガス１１と吸収液１２とを対向接触させるようにしている。 In the refining method using the CO 2 and H 2 S-containing gas recovery system 10A, the gasification gas obtained in the gasification furnace for gasifying coal, biomass, etc. is supplied to a gas cooling device (not shown). It is sent here, cooled by cooling water, and introduced into the absorption tower 13 as the introduction gas 11.
The absorption tower 13 is provided with packed parts 13A to 13D inside the tower, and improves the opposing contact efficiency between the introduced gas 11 and the absorbing liquid 12 when passing through these packed parts 13A to 13D. A plurality of filling portions may be provided. In addition to the filling method, for example, the introduction gas 11 and the absorbing solution 12 are opposed to each other by a spray method, a liquid column method, a shelf method, or the like.

前記吸収塔１３において、導入ガス１１は例えばアミン系の吸収液１２と対向流接触し、導入ガス１１中のＣＯ２及びＨ2Ｓは、化学反応により吸収液１２に吸収され、ＣＯ２及びＨ2Ｓが除去された浄化ガス２１は塔頂部１３ａより系外に放出される。ＣＯ２及びＨ2Ｓを吸収した吸収液は「リッチ溶液」１２Ａとも呼称される。このリッチ溶液１２Ａは、リッチ溶液ポンプ３１を介し、熱交換器１６において、再生塔１４で再生された吸収液（リーン溶液）１２Ｂとの熱交換により加熱され、その後、再生塔１４に供給される。 In the absorption tower 13, the introduced gas 11 is in counterflow contact with, for example, an amine-based absorbent 12, and CO 2 and H 2 S in the introduced gas 11 are absorbed by the absorbent 12 by a chemical reaction, and CO 2 and H 2 The purified gas 21 from which 2 S has been removed is discharged out of the system from the tower top 13a. The absorbing solution that has absorbed CO 2 and H 2 S is also referred to as “rich solution” 12A. The rich solution 12A is heated by heat exchange with the absorption liquid (lean solution) 12B regenerated in the regeneration tower 14 in the heat exchanger 16 via the rich solution pump 31, and then supplied to the regeneration tower 14. .

この熱交換されたリッチ溶液１２Ａは、充填部１４Ａ、１４Ｂを有する吸収液再生塔１４の塔頂部１４ａ近傍から塔内に導入され、塔内を流下する際に、リボイラ１５からの水蒸気２２による吸熱反応を生じて、大部分のＣＯ２及びＨ2Ｓを放出し、再生される。吸収液再生塔１４内で一部または大部分のＣＯ２及びＨ2Ｓを放出した吸収液は「セミリーン溶液」と呼称される。このセミリーン溶液は、吸収液再生塔１４下部に至る頃には、ほぼ全てのＣＯ２及びＨ2Ｓが除去された吸収液となる。このほぼ全てのＣＯ２及びＨ2Ｓが除去されることにより再生された吸収液は「リーン溶液」１２Ｂと呼称される。このリーン溶液１２Ｂはリボイラ１５で飽和水蒸気２３により間接的に過熱され水蒸気２２を発生している。
また、吸収液再生塔１４の塔頂部１４ａからは塔内においてリッチ溶液１２Ａ及びセミリーン溶液から放出された水蒸気２２を伴ったＣＯ２及びＨ2Ｓガス２５が導出され、コンデンサ２６により水蒸気２２が凝縮され、分離ドラム２７にて水２８が分離され、ＣＯ２及びＨ2Ｓガス２９が系外に放出されて回収される。分離ドラム２７にて分離された水２８は吸収液再生塔１４の上部に供給される。
再生された吸収液（リーン溶液）１２Ｂは、熱交換器１６にてリッチ溶液１２Ａと熱交換されて冷却され、つづいてリーン溶液ポンプ３２にて昇圧され、さらにリーン溶液クーラ３３にて冷却された後、再び吸収塔１３に供給され、吸収液１２として再利用される。 The heat-exchanged rich solution 12A is introduced into the tower from the vicinity of the top 14a of the absorption liquid regeneration tower 14 having the packed parts 14A and 14B, and the heat absorption by the water vapor 22 from the reboiler 15 when flowing down the tower. A reaction occurs that releases most of the CO 2 and H 2 S and is regenerated. The absorbing solution from which a part or most of CO 2 and H 2 S has been released in the absorbing solution regeneration tower 14 is referred to as a “semi-lean solution”. This semi-lean solution becomes an absorption liquid from which almost all of CO 2 and H 2 S have been removed by the time it reaches the lower part of the absorption liquid regeneration tower 14. The absorption liquid regenerated by removing almost all of the CO 2 and H 2 S is referred to as “lean solution” 12B. This lean solution 12 </ b> B is indirectly heated by the saturated steam 23 in the reboiler 15 to generate steam 22.
Further, CO 2 and H 2 S gas 25 accompanied by water vapor 22 released from the rich solution 12A and the semi-lean solution are led out from the tower top portion 14a of the absorption liquid regeneration tower 14, and the water vapor 22 is condensed by the condenser 26. Then, the water 28 is separated by the separation drum 27, and the CO 2 and H 2 S gas 29 are discharged out of the system and collected. The water 28 separated by the separation drum 27 is supplied to the upper part of the absorption liquid regeneration tower 14.
The regenerated absorption liquid (lean solution) 12B is heat-exchanged with the rich solution 12A in the heat exchanger 16 and cooled, and then boosted by the lean solution pump 32 and further cooled by the lean solution cooler 33. Then, it is supplied again to the absorption tower 13 and reused as the absorbent 12.

本実施例では、導入ガス１１のＣＯ2濃度を計測器４１で計測し、その濃度に応じて、吸収塔に導入される再生されたリーン溶液１２Ｂである吸収液１２の導入位置を吸収塔の高さ方向のいずれかに変更する制御を制御手段４２により行うようにしている。
切り替えの際には、制御手段４２より、供給ラインＬ2-1、Ｌ2-2、Ｌ2-4に介装されたバルブＶ1〜Ｖ4の開閉度を調整しつつ行うようにしている。
本実施例では吸収塔１３を複数の充填層１３Ａ〜１３Ｄを用いているので、その充填高さを変更している。なお、吸収塔における導入ガス１１と吸収液１２との接触方法を棚段方式とする場合はトレイ段数の高さを変更するようにすればよい。その他のスプレー塔方式や液柱塔方式とする場合には、吸収塔１３内の供給位置(高さ)を変更するようにすればよい。 In the present embodiment, the CO 2 concentration of the introduced gas 11 is measured by the measuring instrument 41, and the introduction position of the absorbing liquid 12 which is the regenerated lean solution 12B introduced into the absorption tower is determined according to the concentration. Control for changing to any one of the height directions is performed by the control means 42.
When switching, the control means 42 adjusts the opening / closing degrees of the valves V 1 to V 4 interposed in the supply lines L 2-1 , L 2-2 and L 2-4 . .
In this embodiment, since the absorption tower 13 uses a plurality of packed beds 13A to 13D, the packed height is changed. In addition, what is necessary is just to change the height of the tray stage number, when making the contact method of the introduction gas 11 and the absorption liquid 12 in an absorption tower into a shelf type. In the case of using another spray tower system or liquid column tower system, the supply position (height) in the absorption tower 13 may be changed.

［試験例１］
図６は、本試験例に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの吸収塔部分の模式図である。
ここで、図６においては、吸収塔１３内の充填層を８段１３Ａ〜１３Ｈとし、計測器４１で計測した結果、ＣＯ2濃度が低い場合(１０ｍｏｌ％−ｄｒｙ以下)、には４段から塔頂部側とするのが好適である。
また、計測器４１で計測した結果、ＣＯ2濃度が高い場合(１０ｍｏｌ％−ｄｒｙを超える)、には４段から下方（底部）側とするのが好適である。 [Test Example 1]
FIG. 6 is a schematic view of an absorption tower portion of a gas recovery system containing CO 2 and H 2 S according to this test example.
Here, in FIG. 6, when the packed bed in the absorption tower 13 is set to 8 stages 13A to 13H and measured by the measuring instrument 41, the CO 2 concentration is low (10 mol% -dry or less). The tower top side is preferred.
Further, when the CO 2 concentration is high (exceeding 10 mol% -dry) as a result of measurement by the measuring instrument 41, it is preferable to shift from the fourth stage to the lower (bottom) side.

これは、吸収塔１３の高さが低い場合、所定量のＨ2Ｓを回収できない場合があるため、所定量のＨ2Ｓを吸収するだけの高さが最低限必要となるが、吸収塔１３を高くしすぎると、逆にＨ2Ｓの吸収性が低下することとなる。
図７−１〜図７−３に、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の高さ位置（段数）との関係を示す。
図７−１は、導入ガス１１中のＣＯ2濃度が６ｍｏｌ％−ｄｒｙの場合では、高さによる出口ガス中のＨ2Ｓ濃度（右縦軸）の変化は少しであった。
ところが、導入ガス１１中のＣＯ2濃度が６ｍｏｌ％−ｄｒｙから８ｍｏｌ％−ｄｒｙ（図７−２）、１０ｍｏｌ％−ｄｒｙ（図７−３）と上昇するにつれて、Ｈ2Ｓの放散量が増大する傾向となることが判明した。
よって、例えば棚段の場合においては、１０ｍｏｌ％−ｄｒｙのＣＯ2濃度が高い場合、８段の棚段を用いた際には、４段程度の高さに位置を変更することが好適であることが判明した。 This is because when the height of the absorption tower 13 is low, a predetermined amount of H 2 S may not be recovered, so that a minimum height for absorbing the predetermined amount of H 2 S is required. On the other hand, if 13 is set too high, the absorbability of H 2 S will decrease.
FIGS. 7-1 to 7-3 show the relationship between the CO 2 recovery amount (left vertical axis) / H 2 S concentration in the outlet gas (right vertical axis) and the height position (stage number) of the absorption tower.
FIG. 7A shows that when the CO 2 concentration in the introduced gas 11 is 6 mol% -dry, the change in the H 2 S concentration (right vertical axis) in the outlet gas with the height is small.
However, as the CO 2 concentration in the introduced gas 11 increases from 6 mol% -dry to 8 mol% -dry (FIG. 7-2) and 10 mol% -dry (FIG. 7-3), the amount of H 2 S emitted increases. It turned out to be a tendency to.
Therefore, for example, in the case of a shelf, when the CO 2 concentration of 10 mol% -dry is high, it is preferable to change the position to a height of about 4 when using an 8 shelf. It has been found.

これは、吸収塔１３において、Ｈ2Ｓの吸収のほかにＣＯ2を吸収する発熱反応に起因することに伴う吸収液１２の温度上昇により、Ｈ2Ｓの飽和吸収量が低下することによるものである。 This is because, in the absorption tower 13, due to the fact that the temperature rise of the absorbing solution 12 due to the fact that due to the exothermic reaction that absorbs CO 2 in addition to the absorption of H 2 S, saturated absorption amount of H 2 S is reduced It is.

そこで、本実施例のように、導入ガス１１のＣＯ2濃度を計測する計測器４１を設けると共に、再生吸収液であるリーン溶液１２Ｂを導入する第２の供給ラインＬ2を複数（図１に示す実施例では３つ）分岐して供給ラインＬ2-1、Ｌ2-2、Ｌ2-3とすると共に、その分岐先の導入口１３b-１〜１３b-3を吸収塔１３の高さ方向に沿って設け、高さ方向の各位置に吸収液を状況に応じて供給するようにすることで、Ｈ2Ｓが効率的に除去できるように、吸収液１２（リーン溶液１２Ｂ）の供給位置を適宜変更させるようにしている。
これにより、Ｈ2Ｓの吸収量を所望に維持すると共に、ＣＯ2の回収量を可能な限り低く保つようにすることができる。
また、吸収液１２を供給する位置を一つの位置に固定せず、多段の位置に供給するようにし、それぞれの供給位置における吸収液流量をそれぞれ変化させるようにしてもよい。 Therefore, as in this embodiment, a measuring instrument 41 for measuring the CO 2 concentration of the introduced gas 11 is provided, and a plurality of second supply lines L 2 for introducing the lean solution 12B, which is a regenerated absorbent, are provided (see FIG. 1). In the embodiment shown, three branches) to supply lines L 2-1 , L 2-2 and L 2-3, and the branch destination inlets 13 b-1 to 13 b-3 are connected to the absorption tower 13. The absorption liquid 12 (lean solution 12B) is provided along the height direction so that the H 2 S can be efficiently removed by supplying the absorption liquid to each position in the height direction according to the situation. The supply position is appropriately changed.
This makes it possible to maintain the H 2 S absorption amount as desired and keep the CO 2 recovery amount as low as possible.
Further, the position at which the absorbent 12 is supplied may not be fixed at one position, but may be supplied to multiple stages, and the absorbent flow rate at each supply position may be changed.

本実施例によれば、導入ガス１１のＣＯ2濃度に応じて、吸収塔１３に導入する吸収液１２（リーン溶液１２Ｂ）の供給位置を適宜変更させることで、Ｈ2Ｓの回収量を満足しつつ、ＣＯ2の回収量を極力低くすることができることとなる。
すなわち、導入ガス１１中のＣＯ2濃度に応じて、吸収塔１３に導入する吸収液１２（リーン溶液１２Ｂ）の供給位置を適宜変更させることで、Ｈ2ＳとＣＯ2とのを選択分離性の向上を図ることができる。 According to the present embodiment, the amount of H 2 S recovered is satisfied by appropriately changing the supply position of the absorbent 12 (lean solution 12B) introduced into the absorption tower 13 according to the CO 2 concentration of the introduced gas 11. However, the amount of CO 2 recovered can be reduced as much as possible.
That is, by selectively changing the supply position of the absorbing liquid 12 (lean solution 12B) to be introduced into the absorption tower 13 in accordance with the CO 2 concentration in the introduced gas 11, selective separation of H 2 S and CO 2 is achieved. Can be improved.

なお、本実施例では吸収液の分岐を４本として４箇所の導入する場合や、試験例では吸収液の分岐を５本として５箇所の導入する場合について、説明したが、本発明はこれらに限定されるものではなく、吸収塔１３の容積及び高さに応じて適宜変更するようにすればよい。   In addition, although the case where four branches are introduced in this example with four branches of the absorbing liquid and the case where five branches are introduced in the test example with five branches of the absorbing liquid have been described, the present invention includes these. It is not limited, and may be appropriately changed according to the volume and height of the absorption tower 13.

本発明による実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システムについて、図面を参照して説明する。図２は、実施例２に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。なお、図１に示す実施例１の構成と同様の構成については同一の符号を付してその説明は省略する。
図２に示すように、本実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ｂは、実施例１に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ａにおいて、前記計測器４１による導入ガス１１中のＣＯ2濃度に応じて、前記吸収塔１３と前記再生塔１４との吸収液の循環量を変化させる制御を制御手段４２により行い、リーン溶液ポンプ３２の流量を調節する制御を制御手段４２により行い、吸収液１２の循環量を変化させるようにしている。 A gas recovery system including CO 2 and H 2 S according to an embodiment of the present invention will be described with reference to the drawings. FIG. 2 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the second embodiment. In addition, the same code | symbol is attached | subjected about the structure similar to the structure of Example 1 shown in FIG. 1, and the description is abbreviate | omitted.
As shown in FIG. 2, the gas recovery system 10B containing CO 2 and H 2 S according to the present embodiment is the same as the measuring device in the gas recovery system 10A containing CO 2 and H 2 S according to the first embodiment. According to the concentration of CO 2 in the introduced gas 11 by 41, the control means 42 performs control to change the circulation amount of the absorption liquid in the absorption tower 13 and the regeneration tower 14 and adjusts the flow rate of the lean solution pump 32. Control is performed by the control means 42 so that the circulation amount of the absorbent 12 is changed.

すなわち、導入ガス１１中のＣＯ2濃度に応じて、吸収塔１３の例えば充填高さ、棚段の場合はトレイ段数等の高さを変更するのに加え、吸収塔１３に導入する吸収液量をさらに変化させるようにしている。
また、吸収塔１３の高さは一定として、吸収液量をさらに変化させるようにしてもよい。
このように、導入ガス１１中のＣＯ2濃度に応じて、吸収液流量を変化させることで、Ｈ2Ｓの回収量を満足しつつ、ＣＯ2の回収量を極力低くすることができることとなる。 That is, in accordance with the CO 2 concentration in the introduced gas 11, for example, in addition to changing the height of the absorption tower 13, for example, the height of the tray stage in the case of a shelf, the amount of absorption liquid introduced into the absorption tower 13 Is going to change further.
Further, the height of the absorption tower 13 may be constant, and the amount of absorption liquid may be further changed.
Thus, by changing the absorption liquid flow rate according to the CO 2 concentration in the introduced gas 11, the recovered amount of CO 2 can be made as low as possible while satisfying the recovered amount of H 2 S. .

本発明による実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システムについて、図面を参照して説明する。図３は、実施例３に係るＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。図４及び図５は、各々実施例３に係る他のＣＯ2及びＨ2Ｓを含むガスの回収システムの概略図である。なお、図１に示す実施例１の構成と同様の構成については同一の符号を付してその説明は省略する。
図３に示すように、本実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ｃは、実施例１に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ａにおいて、前記計測器４１による導入ガス１１中のＣＯ2濃度に応じて、前記吸収塔１３と前記再生塔１４との吸収液１２のリーン溶液クーラ３３における冷却量を変化させる制御を制御手段４２により行い、ＣＯ2濃度が高い場合には、吸収液１２の温度を下げるようにしている。 A gas recovery system including CO 2 and H 2 S according to an embodiment of the present invention will be described with reference to the drawings. FIG. 3 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the third embodiment. 4 and 5 are schematic views of another gas recovery system including CO 2 and H 2 S according to the third embodiment. In addition, the same code | symbol is attached | subjected about the structure similar to the structure of Example 1 shown in FIG. 1, and the description is abbreviate | omitted.
As shown in FIG. 3, the gas recovery system 10C containing CO 2 and H 2 S according to the present embodiment is the same as the measuring device in the gas recovery system 10A containing CO 2 and H 2 S according to the first embodiment. 41 in accordance with the CO 2 concentration in the incoming gas 11 by, performs control to change the amount of cooling in the lean solution cooler 33 of the absorbent 12 and the regeneration tower 14 and the absorption tower 13 by the control unit 42, the CO 2 concentration Is high, the temperature of the absorbent 12 is lowered.

また、図４に示す実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ｄに示すように、吸収塔１３の各位置から吸収液１２を抜き出し、再度導入する抜出・導入ラインＬ11〜Ｌ13を設け、各ラインに冷却器３５−１〜３５−３を介装して、ＣＯ2濃度が高い場合には、吸収液１２の温度を下げるにしてもよい。 Further, as shown in the recovery system 10D for the gas containing CO 2 and H 2 S according to the embodiment shown in FIG. 4, an extraction / introduction line L for extracting the absorbing liquid 12 from each position of the absorption tower 13 and introducing it again. 11 ~L 13 a provided by interposing a condenser 35-1～35-3 each line, when the CO 2 concentration is high, may be lowering the temperature of the absorption liquid 12.

［試験例２］
図８−１、図８−３に、ＣＯ2回収量（左縦軸）／出口ガス中Ｈ2Ｓ濃度（右縦軸）と吸収塔の出口液温度との関係を示す。
図８−１は、導入ガス１１中のＣＯ2濃度が６ｍｏｌ％−ｄｒｙの場合では、温度変化があっても高さによる出口ガス中のＨ2Ｓ濃度（右縦軸）の変化は少しであった。
ところが、導入ガス１１中のＣＯ2濃度が６ｍｏｌ％−ｄｒｙから８ｍｏｌ％−ｄｒｙ（図８−２）、１０ｍｏｌ％−ｄｒｙ（図８−３）と上昇するにつれて、出口液温度の温度上昇があると、Ｈ2Ｓの放散量が増大する傾向となることが判明した。 [Test Example 2]
FIGS. 8-1 and 8-3 show the relationship between the CO 2 recovery amount (left vertical axis) / the H 2 S concentration in the outlet gas (right vertical axis) and the outlet liquid temperature of the absorption tower.
FIG. 8A shows that when the CO 2 concentration in the introduced gas 11 is 6 mol% -dry, the change in the H 2 S concentration (right vertical axis) in the outlet gas with the height is small even if there is a temperature change. there were.
However, as the CO 2 concentration in the introduced gas 11 increases from 6 mol% -dry to 8 mol% -dry (FIG. 8-2) and 10 mol% -dry (FIG. 8-3), the temperature of the outlet liquid temperature increases. It was found that the amount of H 2 S diffused tends to increase.

これは、吸収塔１３において、Ｈ2Ｓの吸収のほかにＣＯ2を吸収する発熱反応に起因することに伴う吸収液１２の温度上昇により、Ｈ2Ｓの飽和吸収量が低下することによるものである。 This is because, in the absorption tower 13, due to the fact that the temperature rise of the absorbing solution 12 due to the fact that due to the exothermic reaction that absorbs CO 2 in addition to the absorption of H 2 S, saturated absorption amount of H 2 S is reduced It is.

そこで、本実施例のように、導入ガス１１のＣＯ2濃度を計測する計測器４１を設けると共に、再生吸収液であるリーン溶液１２Ｂの導入温度をリーン溶液クーラ３３により冷却させることで、Ｈ2Ｓの吸収量を所望に維持すると共に、ＣＯ2の回収量を可能な限り低く保つようにすることができる。 Therefore, as in the present embodiment, a measuring instrument 41 for measuring the CO 2 concentration of the introduced gas 11 is provided, and the introduction temperature of the lean solution 12B, which is a regenerated absorbent, is cooled by the lean solution cooler 33, thereby causing H 2. The amount of S absorbed can be maintained as desired, and the amount of CO 2 recovered can be kept as low as possible.

また、図５に示す実施例に係るＣＯ2及びＨ2Ｓを含むガスの回収システム１０Ｅに示すように、吸収塔１３の各位置から吸収液１２を抜き出し、再度導入する抜出・導入ラインＬ11〜Ｌ13を設け、抜出ライン及び導入ラインを集合させて、冷却器３５を一台としたものである。 Further, as shown in the recovery system 10E for the gas containing CO 2 and H 2 S according to the embodiment shown in FIG. 5, an extraction / introduction line L for extracting the absorbing liquid 12 from each position of the absorption tower 13 and introducing it again. the 11 ~L 13 provided by a set of discharge line and inlet line, is a cooler 35 which was a single.

このように、導入ガス１１中のＣＯ2濃度に応じて、吸収液１２の温度を変化させることで、Ｈ2Ｓの回収量を満足しつつ、ＣＯ2の回収量を極力低くすることができることとなる。 In this way, by changing the temperature of the absorbent 12 according to the CO 2 concentration in the introduced gas 11, the amount of CO 2 recovered can be reduced as much as possible while satisfying the amount of H 2 S recovered. It becomes.

以上のように、本発明に係るＣＯ2及びＨ2Ｓを含むガスの回収システム及び方法によれば、ＣＯ2との吸収とは別にＨ2Ｓを熱エネルギーの面で効率的、かつ選択的に分離することができ、例えば石炭やバイオマス等をガス化炉によりガス化して得られるガス化ガスに含まれるＨ2Ｓを効率よく回収することができる。 As described above, according to the gas recovery system and method including CO 2 and H 2 S according to the present invention, H 2 S is efficiently and selectively used in terms of thermal energy separately from the absorption with CO 2. For example, H 2 S contained in a gasification gas obtained by gasifying coal, biomass, or the like with a gasification furnace can be efficiently recovered.

１０Ａ〜１０Ｅ ＣＯ2及びＨ2Ｓを含むガスの回収システム
１１ 導入ガス
１２ 吸収液
１２Ａ リッチ溶液
１２Ｂ リーン溶液
１３ 吸収塔
１４ 吸収液再生塔（再生塔）
１５ リボイラ
１６ 熱交換器
４１ 計測器
４２ 制御手段
Recovery system for gas containing 10A to 10E CO 2 and H 2 S 11 Introduced gas 12 Absorbent liquid 12A Rich solution 12B Lean solution 13 Absorption tower 14 Absorption liquid regeneration tower (regeneration tower)
15 Reboiler 16 Heat exchanger 41 Measuring instrument 42 Control means

Claims (8)

ＣＯ2及びＨ2Ｓを含むガスを導入ガスとし、該導入ガスとＣＯ2及びＨ2Ｓを吸収する吸収液とを接触させて前記導入ガスからＣＯ２及びＨ2Ｓを吸収させる吸収塔と、
ＣＯ２及びＨ2Ｓを吸収した吸収液を吸収塔の塔底部から抜き出し、第１の供給ラインを介して塔頂部より導入し、リボイラの熱によりＣＯ２及びＨ2Ｓを放出させて吸収液を再生する吸収液再生塔と、
再生された再生吸収液を吸収塔側に戻す第２の供給ラインと、
前記導入ガスのＣＯ2濃度を計測する計測器とを具備すると共に、
前記第２の供給ラインを複数分岐し、その分岐先を吸収塔の高さ方向の中段から塔頂側に沿って設けると共に、
前記吸収塔の底部側から前記導入ガスを導入する際、
前記計測器による前記導入ガス中のＣＯ2濃度が、１０ｍｏｌ％−ｄｒｙを超える場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段に変更する制御を行うと共に、
前記計測器による導入ガス中のＣＯ 2 濃度が、１０ｍｏｌ％−ｄｒｙ以下の場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段よりも塔頂側に変更する制御を行い、Ｈ 2 Ｓの吸収量を所望に維持すると共に、ＣＯ 2 の回収量を低く保つように制御することを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収システム。 A gas containing CO 2 and H 2 S and introducing a gas, an absorption tower for absorbing CO 2 and H 2 S from the gas introduced by contacting the absorption liquid to absorb the introduction gas and CO 2 and H 2 S ,
The absorbing liquid that has absorbed CO 2 and H 2 S is extracted from the bottom of the absorption tower, introduced from the top of the tower through the first supply line, and CO 2 and H 2 S are released by the heat of the reboiler to absorb the absorbing liquid. An absorption liquid regeneration tower for regenerating
A second supply line for returning the regenerated absorption liquid to the absorption tower side;
A measuring instrument for measuring the CO 2 concentration of the introduced gas,
A plurality of the second supply lines are branched, and the branch destinations are provided from the middle in the height direction of the absorption tower along the tower top side ,
When introducing the introduction gas from the bottom side of the absorption tower,
The CO 2 concentration of the introduced gas by the instrument, along with if it exceeds 10 mol% -dry controls to change the introduction position location of regenerated absorption liquid in the middle of the height direction absorption tower,
When the CO 2 concentration in the introduced gas by the measuring instrument is 10 mol% -dry or less, the control is performed to change the introduction position of the regenerated absorption liquid to the tower top side from the middle stage in the height direction of the absorption tower. A gas recovery system including CO 2 and H 2 S, wherein the system is controlled to maintain a desired amount of H 2 S absorption and to keep the CO 2 recovery amount low . 請求項１において、In claim 1,
前記計測器による導入ガス中のＣＯCO in the introduced gas by the measuring instrument 22 濃度が、８ｍｏｌ％−ｄｒｙよりもさらに低い場合には、再生された吸収液の複数の導入位置をさらに塔頂側へ変更することを特徴とするＣＯWhen the concentration is lower than 8 mol% -dry, a plurality of introduction positions of the regenerated absorbent are further changed to the top of the column. 22 及びＨAnd H 22 Ｓを含むガスの回収システム。A gas recovery system containing S. 請求項１又は２において、
前記計測器による導入ガス中のＣＯ2濃度に応じて、前記吸収塔と前記吸収液再生塔との吸収液の循環量をさらに変化させる制御を行うことを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収システム。 In claim 1 or 2 ,
CO 2 and H 2 S, characterized in that control is performed to further change the circulation amount of the absorption liquid between the absorption tower and the absorption liquid regeneration tower in accordance with the CO 2 concentration in the introduced gas by the measuring instrument. Including gas recovery system. 請求項１乃至３のいずれか一つにおいて、
前記吸収塔からＣＯ２及びＨ2Ｓを一部吸収した吸収液を外部に抜き出すと共に、導入する抜出・導入ラインと、
該抜出・導入ラインに介装され、抜き出した吸収液を冷却する冷却器とを具備することを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収システム。 In any one of Claims 1 thru | or 3 ,
An extraction / introduction line for extracting and introducing an absorption liquid partially absorbing CO 2 and H 2 S from the absorption tower;
A gas recovery system including CO 2 and H 2 S, which is provided in the extraction / introduction line and includes a cooler for cooling the extracted absorption liquid. ＣＯ2及びＨ2Ｓを含むガスを導入ガスからＣＯ2及びＨ2Ｓを回収する吸収塔と、ＣＯ２及びＨ2Ｓを吸収した吸収液からＣＯ２及びＨ2Ｓを放出させて吸収液を再生する吸収液再生塔とを用いたＣＯ2及びＨ2Ｓを含むガスの回収方法であって、
前記吸収塔の底部側から前記導入ガスを導入する際、
前記導入ガス中のＣＯ2濃度を計測し、
前記計測による導入ガス中のＣＯ 2 濃度が、１０ｍｏｌ％−ｄｒｙを超える場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段に変更する制御を行うと共に、
前記計測による導入ガス中のＣＯ 2 濃度が、１０ｍｏｌ％−ｄｒｙ以下の場合には、再生された吸収液の導入位置を吸収塔の高さ方向の中段よりも塔頂側に変更する制御を行い、Ｈ 2 Ｓの吸収量を所望に維持すると共に、ＣＯ 2 の回収量を低く保つように制御することを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収方法。 CO 2 and H and the absorption tower for recovering the CO 2 and H 2 S gas from the introduction gas containing 2 S, absorbing liquid by releasing CO 2 and H 2 S from the absorbent having absorbed CO 2 and H 2 S A method for recovering a gas containing CO 2 and H 2 S using an absorption liquid regeneration tower for regenerating
When introducing the introduction gas from the bottom side of the absorption tower,
Measure the CO 2 concentration in the introduced gas,
When the CO 2 concentration in the introduced gas by the measurement exceeds 10 mol% -dry, control is performed to change the introduction position of the regenerated absorption liquid to the middle stage in the height direction of the absorption tower,
When the CO 2 concentration in the introduced gas by the measurement is 10 mol% -dry or less, control is performed to change the introduction position of the regenerated absorption liquid from the middle in the height direction of the absorption tower to the tower top side. A method for recovering a gas containing CO 2 and H 2 S, characterized in that the amount of H 2 S absorbed is maintained as desired and the amount of CO 2 recovered is controlled to be low . 請求項５において、In claim 5,
前記計測器による導入ガス中のＣＯCO in the introduced gas by the measuring instrument 22 濃度が、８ｍｏｌ％−ｄｒｙよりもさらに低い場合には、再生された吸収液の複数の導入位置をさらに塔頂側へ変更することを特徴とするＣＯWhen the concentration is lower than 8 mol% -dry, a plurality of introduction positions of the regenerated absorbent are further changed to the top of the column. 22 及びＨAnd H 22 Ｓを含むガスの回収システム。A gas recovery system containing S. 請求項５又は６において、
計測器による導入ガス中のＣＯ2濃度に応じて、前記吸収塔と前記吸収液再生塔との吸収液の循環量をさらに変化させることを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収方法。 In claim 5 or 6 ,
Recovery of gas containing CO 2 and H 2 S, wherein the circulating amount of the absorption liquid between the absorption tower and the absorption liquid regeneration tower is further changed according to the CO 2 concentration in the introduced gas by the measuring instrument Method. 請求項５乃至７のいずれか一つにおいて、
吸収塔からＣＯ２及びＨ2Ｓを一部吸収した吸収液を外部に抜き出し、抜き出した吸収液を冷却した後、吸収塔に戻すことを特徴とするＣＯ2及びＨ2Ｓを含むガスの回収方法。 In any one of Claims 5 thru | or 7 ,
Recovery of gas containing CO 2 and H 2 S, wherein an absorption liquid partially absorbing CO 2 and H 2 S is extracted from the absorption tower, the extracted absorption liquid is cooled, and then returned to the absorption tower Method.
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