WO2014129255A1 - Co2及びh2sを含むガスの回収システム及び方法 - Google Patents
Co2及びh2sを含むガスの回収システム及び方法 Download PDFInfo
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- WO2014129255A1 WO2014129255A1 PCT/JP2014/051282 JP2014051282W WO2014129255A1 WO 2014129255 A1 WO2014129255 A1 WO 2014129255A1 JP 2014051282 W JP2014051282 W JP 2014051282W WO 2014129255 A1 WO2014129255 A1 WO 2014129255A1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/16—Hydrogen sulfides
- C01B17/167—Separation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Definitions
- 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.
- a chemical absorption method for example, an amine absorption liquid (for example, (N -Methyldiethanolamine: using absorption liquid such as MDEA)) and physical absorption methods (for example, using Selexol absorption liquid using polyethylene glycol dimethyl ether) have been proposed.
- an amine absorption liquid for example, (N -Methyldiethanolamine: using absorption liquid such as MDEA)
- physical absorption methods for example, using Selexol absorption liquid using polyethylene glycol dimethyl ether
- 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 ⁇ 20 ppm) necessary to suppress the degree There is. 4)
- 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.
- Patent Document 1 there is a proposal of an energy saving process in which a part of the absorption liquid in which the dissolved components are partially dissipated in the pressure release container (regeneration tower upper stage) is supplied from below from the uppermost part of the absorption tower (Patent Document 1). .
- the present inventors extract a part of the absorption liquid from the middle of the absorption section of the absorption tower, and use the absorption liquid that absorbs CO 2 and H 2 S at a relatively low concentration as the regeneration section of the regeneration tower. It was proposed previously to supply in the middle (Patent Document 2).
- H 2 S can be efficiently and selectively separated from the gas containing CO 2 and H 2 S separately from the absorption of CO 2 in terms of thermal energy, and the cost can be reduced.
- the emergence of a system to achieve this is eagerly desired.
- 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.
- 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 bottom of the absorption tower, and the top side of the absorption line is drawn through the first supply line.
- an absorption liquid regeneration tower for regenerating the absorption liquid by releasing CO 2 and H 2 S by reboiler heat, a second supply line for returning the regenerated absorption liquid to the absorption tower, and the absorption
- a third supply line for extracting an absorbing liquid that has absorbed a part of CO 2 and H 2 S from the vicinity of the middle stage of the tower, and introducing the extracted absorbing liquid to the vicinity of the middle stage of the regeneration tower; Line and the intersection of the second supply line, the absorption The tower and the middle of CO 2 and H 2 S extracted from the vicinity absorbed absorbing liquid and regenerated absorbent liquid of the gas containing CO 2 and H 2 S which is characterized by comprising a heat exchanger for heat exchange, the In the recovery system.
- the second invention is a CO 2 and recovering method for a gas containing H 2 S with an absorption tower and the regeneration tower from an introduction gas containing CO 2 and H 2 S to recover CO 2 and H 2 S Then, a part of the absorption liquid is extracted from the vicinity of the middle stage of the absorption tower that absorbs CO 2 and H 2 S from the introduced gas, the flow rate of the absorption liquid flowing down below the absorption tower is reduced, and extracted from the bottom of the tower
- the absorption liquid is introduced from the vicinity of the top of the regeneration tower, and the absorption liquid extracted from the vicinity of the middle stage of the absorption tower is introduced to the vicinity of the middle stage of the regeneration tower to regenerate, and the middle stage of the absorption tower
- a method for recovering a gas containing CO 2 and H 2 S, characterized in that the absorbing solution that has absorbed CO 2 and H 2 S extracted from the vicinity exchanges heat with the regenerated absorbing solution regenerated in the regeneration tower. is there.
- a part of the absorption liquid is extracted from the vicinity of the middle stage of the absorption tower by the third supply line, and the flow rate of the absorption liquid flowing down below the absorption tower is reduced, so that H 2 S
- the amount of CO 2 absorbed is reduced, the selective separation of H 2 S is improved, and the amount of reboiler heat in the regeneration tower is reduced.
- FIG. 1 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the first embodiment.
- FIG. 2 is a schematic diagram in which an example of a temperature condition of the gas recovery system including CO 2 and H 2 S according to the first embodiment is added.
- FIG. 3 is a schematic diagram in which an example of a temperature condition of a gas recovery system including CO 2 and H 2 S according to a conventional example is added.
- FIG. 1 is a schematic diagram of a gas recovery system including CO 2 and H 2 S according to the first embodiment.
- the recovery system 10 of the gas containing CO 2 and H 2 S according to the present embodiment for example, coal CO 2 a and biomass, etc.
- the absorption liquid (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 14c, and the absorption tower 13 A second supply line L 2 back to the top 13a, withdrawn absorption liquid (semi-rich solution) 12C that has absorbed part of the tower middle 13b near the CO 2 and H 2 S absorption tower 13, the semi-rich solution 12C taken out
- the semi-rich solution 12C and the lean solution are interposed at the intersection of the third supply line L 3 introduced into the vicinity of the middle stage 14b of the regeneration tower 14 and the third supply line L 3 and the second supply line L 2.
- a semi-rich solution heat exchanger 17 for exchanging heat with 12B.
- 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.
- the gasified gas obtained in the gasification furnace for gasifying coal, biomass, or the like 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 portions 13A and 13B inside the tower, and the counterflow contact efficiency between the introduced gas 11 and the absorbing liquid 12 is improved when passing through these packed portions 13A and 13B.
- a plurality of filling portions may be provided.
- the introduction gas 11 and the absorbing liquid 12 are brought into counterflow contact by, for example, a spray method, a liquid column method, a shelf method, or the like.
- the introduced gas 11 is in counterflow contact with, for example, an amine-based absorbing liquid 12, and CO 2 and H 2 S in the introduced gas 11 are absorbed by the absorbing liquid 12 by a chemical reaction, and CO 2 and H 2
- the purified gas 21 from which 2 S has been removed is released out of the system.
- the absorbing liquid 12 that has absorbed CO 2 and H 2 S is also referred to as a “rich solution” 12A.
- the rich solution 12A is supplied to the top 14a side of the absorbent regenerator 14 through a rich solution pump (not shown) without heat exchange and with a low temperature.
- lean solution 12B The absorbent regenerated by removing almost all of the CO 2 and H 2 S is referred to as “lean solution” 12B.
- This lean solution 12B is indirectly heated by the saturated steam 23 in the reboiler 15, generates steam 22, and is returned to the tower bottom 14c side of the regeneration tower 14.
- CO 2 and H 2 S gas 25 accompanied with water vapor released from the rich solution 12A and the semi-lean solution are led out from the top 14a of the regeneration tower 14 and the water vapor is condensed by the condenser 26.
- water 28 is separated, and CO 2 and H 2 S gas 29 are discharged out of the system and recovered.
- the water 28 separated by the separation drum 27 is supplied to the tower top portion 14 a of the absorbent regeneration tower 14.
- the regenerated absorbing solution (lean solution) 12B is cooled by heat exchange with the semi-rich solution 12C in the semi-rich solution heat exchanger 17, and then pressurized by a lean solvent pump (not shown), and further the lean solvent. After being cooled by the cooler 30, it is supplied again to the absorption tower 13 and reused as the absorbent 12.
- the extraction amount is determined by measuring the temperature, pressure, flow rate, CO 2 concentration, H 2 S concentration, etc. of the introduced gas, and comprehensively judging these conditions to determine the optimal extraction position and extraction amount. Like to do.
- the extracted semi-rich solution 12C is heated by the semi-rich solution heat exchanger 17 by heat exchange with the high-temperature lean solution 12B discharged from the bottom 14c of the regeneration tower 14, and in the vicinity of the middle stage 14b of the regeneration tower 14 More preferably, it is supplied below the middle column 14b.
- the rich solution 12A having a high CO 2 and H 2 S concentration is introduced as it is from the top 14a of the regeneration tower 14 without heat exchange, and the CO 2 and H 2 S concentrations are relatively low compared to the rich solution 12A. Since the semi-rich solution 12C is heated by the semi-rich solution heat exchanger 17 and then supplied to the vicinity of the middle stage 14b of the regeneration tower 14 or the lower side thereof, the amount of heat of the reboiler 15 can be reduced. Steam consumption by the reboiler 15 can be reduced.
- the rich solution 12A and the semi-rich solution 12C extracted from the absorption tower 13 are respectively introduced into the flash drums 31 and 32, where non-condensable gases 33 (33a and 33b) such as N 2 , H 2 , and CO are used. ) Is separated. Then, it is combined with the CO 2 and H 2 S gas 29 separated by the separation drum 27.
- non-condensable gases 33 33a and 33b
- N 2 , H 2 , and CO are used.
- FIG. 2 is a schematic diagram in which an example of a temperature condition of the gas recovery system including CO 2 and H 2 S according to the first embodiment is added.
- the square frame indicates the temperature.
- the introduced gas 11 is introduced into the absorption tower 13.
- the absorption liquid 12 (lean solution 12B) is introduced into the tower so as to oppose this, and absorbs CO 2 and H 2 S. Since this absorption is an exothermic reaction, the semi-rich solution 12C withdrawn from the vicinity of the middle stage 13b of the absorption tower 13 is 46 ° C.
- the rich solution 12A extracted from the tower bottom 13c is 44 ° C.
- the rich solution 12A is introduced from the top 14a of the regeneration tower 14 at a temperature of 44 ° C. without heat exchange as it is.
- the semi-rich solution 12C is heat-exchanged with the high-temperature (123 ° C.) lean solution 12B in the semi-rich solution heat exchanger 17, and the semi-rich solution 12C becomes 113 ° C. and is introduced from the vicinity of the middle stage 14b of the regeneration tower 14.
- the temperature of the CO 2 and H 2 S gas 25 accompanied by water vapor from the top 14a of the regeneration tower 14 is 116 ° C., and the temperature after passing through the condenser 26 is 40 ° C.
- the reboiler heat quantity of the reboiler 15 in the regeneration tower 14 is reduced.
- FIG. 3 shows a gas recovery system of the prior art (Patent Document 2).
- Patent Document 2 the rich solution 12A extracted from the tower bottom 13c of the absorption tower 13 is heat-exchanged by the rich solution heat exchanger 16. These are introduced from the top 14a side of the regeneration tower 14.
- the introduced gas 11 is introduced into the absorption tower 13.
- the absorption liquid 12 (lean solution 12B) is introduced into the tower so as to oppose this, and absorbs CO 2 and H 2 S. Since this absorption is an exothermic reaction, the semi-rich solution 12C extracted from the vicinity of the middle column 13b of the absorption tower 13 is 49 ° C.
- the rich solution 12A extracted from the tower bottom 13c is 44 ° C.
- the rich solution 12A and the semi-rich solution 12C are heat-exchanged in series by the high-temperature (122 ° C.) lean solution 12B in the rich solution heat exchanger 16 and the semi-rich solution heat exchanger 17, respectively.
- the semi-rich solution 12C reaches 104 ° C. and is introduced from the vicinity of the middle column 14b of the regeneration tower 14.
- the temperature of the CO 2 and H 2 S gas 25 with water vapor from the top 14 a of the regeneration tower 14 is 118 ° C., and the temperature after passing through the condenser 26 is 40 ° C.
- Table 1 shows the load of the reboiler 15 of each regeneration tower, the load of the rich solution heat exchanger 16, and the load of the semi-rich solution heat exchanger 17 in the recovery system of the example and the gas recovery systems of the conventional examples 1 and 2. This is a comparison of the load of the capacitor 26.
- Patent Document 2 the rich solution heat exchanger 16 and the semi-rich solution heat exchanger 17 exchange heat between the rich solution 12A and the semi-rich solution 12C with the lean solution 12B.
- the rich solution 12A is heat-exchanged with the lean solution 12B by the heat exchanger 16 for rich solution.
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Abstract
Description
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。
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10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の塔頂部13aに戻す第2の供給ラインL2と、吸収塔13の塔中段13b近傍からCO2及びH2Sの一部を吸収した吸収液(セミリッチ溶液)12Cを抜き出し、抜き出したセミリッチ溶液12Cを再生塔14の塔中段14b近傍に導入する第3の供給ラインL3と、第3の供給ラインL3と第2の供給ラインL2との交差部に介装され、セミリッチ溶液12Cとリーン溶液12Bとを熱交換するセミリッチ溶液用熱交換器17と、を具備する。
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。
吸収塔13は、塔内部に充填部13A、13Bが設けられ、これらの充填部13A、13Bを通過する際、導入ガス11と吸収液12との対向流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とを対向流接触させるようにしている。
本発明のように、吸収塔13の塔中段13b近傍から吸収液の一部を第3の供給ラインL3により抜き出すようにして、吸収塔13の下方に流下する吸収液の流量を低減させることで、H2Sはガス側の物質移動、CO2は液側の物質移動が支配的であることから、CO2の方がより吸収速度が低下する。
これにより、CO2吸収量が低下、すなわち吸収液中のCO2濃度が低下する分、H2Sの吸収量は増加する。
吸収液12の流量の低下によるH2S吸収量の低下を考慮しても、H2S吸収量はほとんど低下しない。
よって、H2Sの選択性の向上を図ることができる。
図2に示すように、CO2及びH2Sを含むガスの回収システム10Aにおいて、導入ガス11は吸収塔13に導入される。これに対向するように吸収液12(リーン溶液12B)は塔内に導入され、CO2及びH2Sを吸収する。
この吸収は発熱反応であるので、吸収塔13の塔中段13b近傍から抜き出されるセミリッチ溶液12Cは46℃である。一方、塔底部13cから抜き出されるリッチ溶液12Aは44℃である。
このリッチ溶液12Aは、そのまま熱交換せずに、再生塔14の塔頂部14aから44℃の温度のままで導入される。
これにより、再生塔14でのリボイラ15のリボイラ熱量の低減を図るようにしている。
図3に示すように、CO2及びH2Sを含むガスの回収システム100では、吸収塔13の塔底部13cから抜出されるリッチ溶液12Aを、リッチ溶液用熱交換器16で熱交換した後、再生塔14の塔頂部14a側から導入するものである。
この吸収は発熱反応であるので、吸収塔13の塔中段13b近傍から抜き出されるセミリッチ溶液12Cは49℃である。一方、塔底部13cから抜き出されるリッチ溶液12Aは44℃である。
このリッチ溶液12Aとセミリッチ溶液12Cとは、リッチ溶液用熱交換器16及びセミリッチ溶液用熱交換器17において、それぞれ高温(122℃)のリーン溶液12Bにより直列で熱交換され、リッチ溶液12Aは77℃となり、再生塔14の塔頂部14aから導入される。またセミリッチ溶液12Cは104℃となり、再生塔14の塔中段14b近傍から導入される。再生塔14の塔頂部14aからの水蒸気を伴ったCO2及びH2Sガス25の温度は118℃、コンデンサ26を通過した後の温度は40℃である。
従来例1(特許文献2)は、リッチ溶液用熱交換器16及びセミリッチ溶液用熱交換器17でリッチ溶液12Aとセミリッチ溶液12Cとを、リーン溶液12Bで熱交換するものである。
従来例2は、リッチ溶液用熱交換器16でリッチ溶液12Aをリーン溶液12Bで熱交換するものである。
また、従来例1及び2に較べて、再生塔14から排出される水蒸気を伴ったCO2及びH2Sガス25を冷却するコンデンサ26の負荷を、大幅に抑えることができた。
また、熱交換器を従来例1から削減することで、コスト低減のみならず、プロセス全体の熱収支を向上することができた。
11 導入ガス
12 吸収液
12A リッチ溶液
12B リーン溶液
12C セミリッチ溶液
13 吸収塔
14 吸収液再生塔(再生塔)
15 リボイラ
17 セミリッチ溶液用熱交換器
Claims (2)
- 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前記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側より導入し、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前記吸収塔に戻す第2の供給ラインと、
前記吸収塔の塔中段近傍からCO2及びH2Sの一部を吸収した吸収液を抜き出し、抜き出した吸収液を前記再生塔の塔中段近傍に導入する第3の供給ラインと、
前記第3の供給ラインと、前記第2の供給ラインとの交差部に介装され、前記吸収塔の塔中段近傍から抜き出したCO2及びH2Sを吸収した吸収液と再生吸収液とを熱交換する熱交換器と、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。 - CO2及びH2Sを含む導入ガスからCO2及びH2Sを回収する吸収塔と再生塔とを用いたCO2及びH2Sを含むガスの回収方法であって、
前記導入ガスからCO2及びH2Sを吸収させる前記吸収塔の塔中段近傍から吸収液の一部を抜き出し、吸収塔の下方に流下する吸収液の流量を低減させ、
塔底部から抜き出した吸収液を前記再生塔の塔頂部近傍から導入させると共に、前記吸収塔の塔中段近傍から抜き出した吸収液を、前記再生塔の塔中段近傍に導入して再生すると共に、
前記吸収塔の塔中段近傍から抜出されるCO2及びH2Sを吸収した吸収液が、前記再生塔で再生された再生吸収液と熱交換することを特徴とするCO2及びH2Sを含むガスの回収方法。
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