WO2011132660A1 - Système de traitement de gaz d'échappement ayant un dispositif d'élimination de dioxyde de carbone - Google Patents

Système de traitement de gaz d'échappement ayant un dispositif d'élimination de dioxyde de carbone Download PDF

Info

Publication number
WO2011132660A1
WO2011132660A1 PCT/JP2011/059599 JP2011059599W WO2011132660A1 WO 2011132660 A1 WO2011132660 A1 WO 2011132660A1 JP 2011059599 W JP2011059599 W JP 2011059599W WO 2011132660 A1 WO2011132660 A1 WO 2011132660A1
Authority
WO
WIPO (PCT)
Prior art keywords
absorption
exhaust gas
tower
amine
boiler
Prior art date
Application number
PCT/JP2011/059599
Other languages
English (en)
Japanese (ja)
Inventor
島村　潤
祥悟 盛
斎藤　隆行
尾田　直己
一彦 梶川
Original Assignee
バブコック日立株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by バブコック日立株式会社 filed Critical バブコック日立株式会社
Publication of WO2011132660A1 publication Critical patent/WO2011132660A1/fr

Links

Images

Classifications

    • 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
    • B01D53/1475—Removing carbon dioxide
    • 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
    • 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
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • 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

Definitions

  • the present invention relates to an exhaust gas treatment system having a carbon dioxide removal device, and more particularly to an exhaust gas treatment system that removes carbon dioxide in combustion exhaust gas using an aqueous solution of amines as an absorbent of carbon dioxide.
  • the de-CO 2 facility consists of a denitration device 2, an air heater 3, an electrostatic precipitator 4, a wet desulfurization device 5, a press clubber 10, a CO 2 absorption tower 20, and a regeneration unit that are sequentially provided along the exhaust gas flow path from the boiler 1. It is composed of a tower 40 and a reboiler 60.
  • the exhaust gas generated by burning coal, etc., in the boiler 1 is introduced into the denitration device 2, and after NOx (nitrogen oxide) contained in the gas is decomposed and removed, the temperature is adjusted to 200 to 160 ° C by the air heater 3.
  • the press clubber 10 is composed of an absorbent 11 to be supplied into the system, a circulation pump 14 for circulating the absorbent, a cooler 15 for cooling the circulating absorbent, and a spray section 16 for spraying the absorbent in countercurrent contact with the exhaust gas. It is configured.
  • the SO 2 contained in the exhaust gas from the wet desulfurizer outlet is contained in an amount of about 40 ppm to 80 ppm, but the press clubber removed SO 2 that is a deterioration factor of the amine absorption liquid as much as possible (about 1 to several ppm at the press clubber outlet). Thereafter, it is introduced into the absorption tower 20 as the outlet gas 18.
  • the absorption tower 20 has a packed bed 21 that absorbs CO 2 in the exhaust gas into the amine absorption liquid, an absorbent spray portion 22 provided above it, and the temperature rises due to exothermic reaction by absorbing the CO 2 in the exhaust gas.
  • a demister 26 is installed in the upper part of the washing unit, and the mist of the absorbing solution that has passed through the washing unit is removed.
  • the process gas 37 discharged from the absorption tower outlet is introduced into a chimney inlet duct for discharge from a chimney (not shown).
  • the amine absorbing liquid that has absorbed CO 2 is sent from the liquid reservoir at the bottom of the absorption tower 20 through the absorption tower extraction pump 33 through the regeneration tower liquid supply pipe 35 and sent to the regeneration tower 40 to be packed in the middle of the regeneration tower 41.
  • CO 2 contained in the amine absorbing liquid is degassed.
  • the degassed CO 2 gas is entrained in the gas by the water washing section 43, and the mist that has passed through the water washing section is collected by the demister 45, and is discharged as CO 2 gas 46 from the upper part of the regeneration tower.
  • the CO 2 gas is cooled by a cooler 47 and separated into gas and condensed water by a CO 2 separator 48.
  • the CO 2 gas is introduced into a CO 2 liquefaction facility (not shown), and the condensed water is drained. It is supplied to the washing spray section 44 by the pump 50.
  • the amine liquid from which CO 2 has been degassed is stored in the regeneration tower liquid reservoir 51 and then sent to the reboiler 60 through the reboiler liquid supply pipe 52. Inside the reboiler 60, heat transfer pipes and the like are installed.
  • the amine solution is indirectly heated by the steam 62 supplied by the steam supply pipe 61, so that the steam generated inside the reboiler 60 passes through the steam supply pipe 65.
  • the absorption liquid extracted from the liquid reservoir at the lower part of the regeneration tower passes through the regeneration tower liquid extraction pipe 66, is cooled by the heat exchanger 34 and the cooler 31, and is then introduced into the absorption tower 20.
  • the steam 62 used in the reboiler 60 becomes steam drain in the heat transfer tube, is discharged to the condensed water drum 67, is mixed with the spray cooling water 68, and is sufficiently cooled to less than 100 ° C.
  • the steam drain 71 that is free from the risk of flushing in the return pipe is returned to the boiler 1 by the condensed water pump 69.
  • the spray cooling water 68 equivalent to the amount of steam is required.
  • An object of the present invention is to maintain a steam balance of the entire power generation system by adopting a new equipment and method for boiler steam cooling in a CO 2 removal equipment, and to efficiently use boiler heat, thereby reducing CO 2.
  • the purpose is to improve the efficiency of the removal equipment and thus the entire power generation system.
  • the present inventor uses the amine absorption liquid supplied to the regeneration tower 40 as a refrigerant without using the spray cooling water 68 to cool the drain of the condensed water drum 67, and generates power.
  • the condenser of the steam turbine equipment attached to the boiler 1 as the cooling water of the cooler 31 of the regeneration tower extraction pipe 66
  • the problem of heat recovery of the heat exchanger 34 was also solved. That is, the invention claimed in the present application is as follows.
  • An exhaust gas treatment system having a heat transfer tube to which steam is supplied and a condensed water drum for condensing the steam discharged from the heat transfer tube and recovering it as a steam drain, the amine absorption extracted from the CO 2 absorption tower
  • a heat transfer tube for circulating a liquid as a refrigerant in the condensed water drum
  • An exhaust gas treatment system provided with a flow rate adjustment valve for absorbing liquid passing through a heat transfer tube.
  • the boiler has steam turbine equipment and its condenser, and uses boiler water at the outlet of the condenser as a refrigerant for a cooler that cools the absorption liquid circulating in the CO 2 absorption tower.
  • the steam balance of the power generation system including the CO 2 removal facility can be maintained and can be stably operated, and the amine absorption discharged from the absorption tower to the refrigerant that cools the steam drain used in the reboiler.
  • the liquid By using the liquid, the sensible heat of the amine absorption liquid in the regeneration tower can be increased, and the amount of steam supplied to the CO 2 removal facility can be reduced.
  • FIG. 1 is an explanatory diagram of an exhaust gas treatment system including a CO 2 removal facility according to an embodiment of the present invention. Explanatory drawing of the waste gas processing system which shows the 2nd Example of this invention. Explanatory drawing of an exhaust gas treatment system including conventional CO 2 removal equipment.
  • FIG. 1 is an explanatory diagram of an exhaust gas treatment system including a CO 2 removal facility showing an embodiment of the present invention.
  • This system consists of a denitration device 2, an air heater 3, an electrostatic precipitator 4, a wet desulfurization device 5, a press clubber 10, a CO 2 absorption tower 20, and a CO 2 absorption tower, which are sequentially installed along the exhaust gas flow path of the boiler 1.
  • It mainly comprises a regeneration tower 40 that desorbs absorbed CO 2 and regenerates the amine absorption liquid, and a reboiler 60 attached to the regeneration tower 40.
  • Exhaust gas generated by burning coal or the like in the boiler 1 is introduced into the denitration device 2, and NOx (nitrogen oxide) contained in the gas is decomposed and removed.
  • NOx nitrogen oxide
  • the temperature of the gas discharged from the denitration device 2 is adjusted to 200 to 160 ° C. by the air heater 3 and then the dust is removed by the electric dust collector 4. Dust gas is supplied to the wet desulfurization system 5 SO 2 is removed, after removed as much as possible the remaining SO 2 in the press scrubber 10, is introduced into the CO 2 absorber 20.
  • the press clubber 10 is contained in the exhaust gas at the outlet of the wet desulfurization unit about 40ppm to 80ppm, and removes SO 2 that causes deterioration of the amine absorption liquid as much as possible to about 1 to several ppm at the outlet of the press clubber.
  • the inside of the absorption tower 20 generates heat when the CO 2 in the exhaust gas is absorbed by the absorbing liquid, the packed bed 21 that absorbs the CO 2 in the exhaust gas into the amine absorption liquid, the absorption liquid spray part 22 that sprays the absorption liquid, and the absorption liquid.
  • the CO 2 gas 23 whose temperature has risen due to the reaction is cooled and washed with water, and the water washing part 24 and the water washing spray part 25 for washing the amine absorbing liquid entrained in the exhaust gas, and the water washing water reservoir part 27 for collecting the water washed with water
  • the cooler 28 cools the circulating flush water and the flush pump 29 circulates the flush water.
  • a demister 26 is installed on the upper part of the washing spray part, and the mist of the absorbing liquid that has passed through the washing part 24 is removed.
  • the processing gas 37 discharged from the top of the absorption tower 20 is discharged out of the system from a chimney not shown in the figure.
  • the amine absorption liquid that has absorbed CO 2 is extracted from the liquid reservoir at the bottom of the absorption tower 20 by the absorption tower extraction pump 33, and part of the condensed water is condensed by the branched heat transfer tube 70 before entering the heat exchanger 34.
  • the heat is exchanged with the drain of the steam 62 through the heat transfer tube 70 after being sent to the drum 67 and then returned to the original pipe through the return heat transfer tube 70.
  • the amine absorption liquid flow rate sent to the condensed water drum 67 is controlled by the flow rate adjusting valve 72 in order to control the temperature of the condensed water drum outlet drain 71.
  • the amine absorption liquid is joined from the heat transfer tube 70 to the regeneration tower liquid supply pipe 35, then passes through the heat exchanger 34, is introduced into the regeneration tower 40, and is sprayed from the spray section 42 above the packed bed 41, and the packed bed 41 CO 2 contained in the amine absorbing liquid is degassed by coming into gas-liquid contact with the vapor rising from the lower part of the gas.
  • the degassed CO 2 gas is entrained in the gas by the water washing section 43, and the mist containing amine that has passed through the water washing section is collected by the demister 45, and is discharged as CO 2 gas 46 from the upper part of the regeneration tower.
  • the CO 2 gas is cooled by a cooler 47 and separated into gas and condensed water by a CO 2 separator 48.
  • the CO 2 gas is introduced into a CO 2 liquefaction facility (not shown), and the condensed water is drained. It is supplied to the washing spray section 44 by the pump 50.
  • the amine absorption liquid from which CO 2 has been degassed is stored in the regeneration tower liquid reservoir 51 and then sent to the reboiler 60 through the reboiler liquid supply pipe 52.
  • a steam supply pipe 61 is arranged as a heat transfer pipe. After the amine absorbing liquid is indirectly heated by the steam passing through the reboiler 60, it is returned from the reboiler 60 to the regeneration tower 40. Further, the absorption liquid extracted from the liquid reservoir at the lower part of the regeneration tower 40 passes through the regeneration tower liquid extraction pipe 66, is cooled by the heat exchanger 34 and the cooler 31, and is then introduced into the absorption tower 20.
  • the steam 62 of the heat transfer tube in the reboiler 60 becomes steam drain and is discharged to the condensed water drum 67. Therefore, the steam drain is sufficiently cooled to less than 100 ° C. by exchanging heat with the amine absorbing liquid passing through the heat transfer tube 70.
  • the outlet drain 71 of the condensed water drum which is free from the risk of flushing, is returned to the boiler 1 by a condensed water pump 69 through a return pipe (not shown).
  • the flow rate of the absorption liquid in the heat transfer tube 70 can be adjusted by the amine flow rate adjustment valve A72 and the amine flow rate adjustment valve B73.
  • the temperature of the condensed water drum outlet drain 71 is detected by a thermometer (not shown),
  • the flow rate control valves 72 and 73 can be adjusted so as to reach a predetermined temperature.
  • the inlet pipe of the heat exchanger 34 is branched into a heat transfer pipe 70, and the heat transfer pipe 70 is used as a heat exchange pipe with the drain water of the condensed water drum 67 of the regeneration tower 40, and then the original heat exchanger.
  • the return pipe returning to the inlet of 34 the temperature of the amine absorbing liquid introduced into the regeneration tower 40 can be increased, and the amount of steam supplied to the regeneration tower can be reduced.
  • the heat transfer pipe 70 is installed in the condensate water drum 67, and the amine absorption liquid is passed as a refrigerant in the condensate water drum 67, thereby cooling the drain of the steam 62 without the spray cooling water 68 (FIG. 3).
  • the use of an absorption liquid of the amine discharged from the absorption tower 20 (absorption tower extraction pump 33) as a refrigerant can contribute to an increase in the temperature of the amine absorption solution in the regeneration tower 40. This also reduces the amount of heat supplied from the reboiler 60, leading to a reduction in the amount of heat in the entire CO 2 absorption system.
  • the steam absorption of about 60 to 60 ° C. discharged from the absorption tower 20 is cooled to about 85 to 90 ° C.
  • the spray cooling water 68 can be reduced to 0, and the recovered heat can be supplied to the regeneration tower 40.
  • FIG. 2 is an explanatory view of an exhaust gas treatment system showing a second embodiment of the present invention adapted to such a demand.
  • 1 is different from the system of FIG. 1 in that a bypass pipe and a bypass valve 68 are provided to connect the upstream side and the downstream side of the heat exchanger 34 provided in the middle of the extraction pipe 66 of the regeneration tower 40.
  • the cooling water of the cooler 31 provided in the amine liquid return pipe 66 to the absorption tower 20 the flow rate of the regenerative amine liquid (lean amine liquid) flowing through is controlled to adjust the heat exchange amount. This is because the outlet boiler water 32 of the condenser 82 of the turbine equipment attached to the boiler 1 is used.
  • This turbine equipment includes a steam turbine 81 and a generator 90 connected to the boiler 1, a condenser 82, a condensate pump 83, a low-pressure feed water heater 84, as shown in a broken-line frame in FIG. 2.
  • the outlet boiler water of the condenser 82 is indicated by reference numeral 32.
  • 85 is seawater
  • 86 and 87 are extracted steam
  • 88 is condensate
  • 89 is water supply.
  • the amine absorbent supplied to the regeneration tower 20 can flow down in a stable state.
  • the temperature can be controlled to 100 ° C or lower.
  • boiler water 32 having a temperature of about 35 ° C. at the outlet of the condenser 82 is used as cooling water for the cooler 31, and the boiler water 32 whose temperature has risen in the cooler 31 has a feed water temperature of 50 to 60 ° C. in the low-pressure feed water heater 84. It is returned to the place where it becomes and is supplied to the boiler.
  • the temperature rise of the cooling water in the cooler 31 of FIG. 1 was 5 ° C. (35 ° C. ⁇ 40 ° C.), but in this embodiment of FIG. Therefore, since this temperature rise can be used as the temperature rise of boiler feed water, an improvement in turbine output can be expected.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

La présente invention concerne un système de traitement de gaz d'échappement ayant un dispositif d'élimination de CO2 qui maintient l'équilibre de vapeur du système générateur entier en adoptant un nouveau dispositif et un procédé pour refroidir la vapeur de chaudière dans le dispositif d'élimination de CO2, et améliore l'efficacité du dispositif d'élimination de CO2, et par conséquent du système générateur entier, au moyen de l'utilisation efficace de chaleur de chaudière. Le système de traitement de gaz d'échappement décrit est pourvu d'une tour d'absorption de CO2 qui amène une solution d'absorption d'amine en contact avec le gaz d'échappement contenant du CO2 émis par une chaudière ; une tour de régénération de solution d'absorption qui chauffe la solution d'absorption qui a absorbé ledit CO2, et détache le CO2 ; un passage de circulation de solution d'absorption qui élimine la solution d'absorption détachée de CO2 par l'intermédiaire d'un tuyau de décharge de tour de régénération, et, après refroidissement avec un échangeur de chaleur et un refroidisseur, cycle ladite solution vers la tour d'absorption de CO2 ; et un rebouilleur qui, après retrait d'une partie de la solution d'absorption détachée de CO2 mentionnée ci-dessus et élévation de la température, retourne celle-ci vers la tour de régénération mentionnée ci-dessus. Le système décrit est en outre pourvu d'un tube échangeur de chaleur pour cyclage à l'intérieur du cylindre de condensat de la solution d'absorption d'amine déchargée depuis la tour d'absorption de CO2 mentionnée ci-dessus en tant que réfrigérant, et une vanne de régulation de débit pour la solution d'absorption s'écoulant à travers ledit tube échangeur de chaleur.
PCT/JP2011/059599 2010-04-20 2011-04-19 Système de traitement de gaz d'échappement ayant un dispositif d'élimination de dioxyde de carbone WO2011132660A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
JP2010-096848 2010-04-20
JP2010096848 2010-04-20
JP2010-178438 2010-08-09
JP2010178438A JP2011240321A (ja) 2010-04-20 2010-08-09 二酸化炭素除去装置を有する排ガス処理システム

Publications (1)

Publication Number Publication Date
WO2011132660A1 true WO2011132660A1 (fr) 2011-10-27

Family

ID=44834179

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2011/059599 WO2011132660A1 (fr) 2010-04-20 2011-04-19 Système de traitement de gaz d'échappement ayant un dispositif d'élimination de dioxyde de carbone

Country Status (2)

Country Link
JP (1) JP2011240321A (fr)
WO (1) WO2011132660A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2832420A3 (fr) * 2013-07-29 2015-06-10 Kabushiki Kaisha Toshiba Système de collecte et de séparation de dioxyde de carbone et son procédé de fonctionnement
AU2013300693B2 (en) * 2012-08-09 2015-11-12 Mitsubishi Heavy Industries, Ltd. Exhaust gas treatment system
CN115253608A (zh) * 2022-08-31 2022-11-01 西安热工研究院有限公司 一种燃煤发电机组的烟气碳捕集系统及方法

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5582960B2 (ja) 2010-10-22 2014-09-03 株式会社東芝 二酸化炭素分離回収システム及びリボイラー入熱量測定方法
US8961665B2 (en) 2012-03-28 2015-02-24 Mitsubishi Heavy Industries, Ltd. Exhaust gas treatment system
JP2013226487A (ja) * 2012-04-24 2013-11-07 Mitsubishi Heavy Ind Ltd Ｃｏ２回収装置およびｃｏ２回収方法
US10195561B2 (en) * 2012-09-20 2019-02-05 Mitsubishi Heavy Industries Engineering, Ltd. Steam supply system and CO2 recovery unit including the same
JP6361909B2 (ja) * 2014-03-26 2018-07-25 三菱重工エンジニアリング株式会社 Ｃｏ２回収装置及びｃｏ２回収方法
JP2018038979A (ja) * 2016-09-08 2018-03-15 株式会社東芝 二酸化炭素の分離回収装置、分離回収方法および液体捕捉装置
CN108499316B (zh) * 2018-02-24 2020-04-07 天津普洛仙科技有限公司 一种洗涤塔预降温装置
JP7177734B2 (ja) * 2019-03-20 2022-11-24 三菱重工エンジニアリング株式会社 吸収液再生装置及びｃｏ２回収装置並びに吸収液再生装置の改造方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03121357U (fr) * 1990-03-27 1991-12-12
JPH07232033A (ja) * 1994-02-22 1995-09-05 Kansai Electric Power Co Inc:The 燃焼排ガス中の二酸化炭素の除去方法
JP2002530187A (ja) * 1998-11-23 2002-09-17 フルー・コーポレイシヨン 分流プロセスおよびその装置
JP2005254212A (ja) * 2004-03-15 2005-09-22 Mitsubishi Heavy Ind Ltd Ｃｏ２回収装置及び方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03121357U (fr) * 1990-03-27 1991-12-12
JPH07232033A (ja) * 1994-02-22 1995-09-05 Kansai Electric Power Co Inc:The 燃焼排ガス中の二酸化炭素の除去方法
JP2002530187A (ja) * 1998-11-23 2002-09-17 フルー・コーポレイシヨン 分流プロセスおよびその装置
JP2005254212A (ja) * 2004-03-15 2005-09-22 Mitsubishi Heavy Ind Ltd Ｃｏ２回収装置及び方法

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2013300693B2 (en) * 2012-08-09 2015-11-12 Mitsubishi Heavy Industries, Ltd. Exhaust gas treatment system
EP2832420A3 (fr) * 2013-07-29 2015-06-10 Kabushiki Kaisha Toshiba Système de collecte et de séparation de dioxyde de carbone et son procédé de fonctionnement
US9464842B2 (en) 2013-07-29 2016-10-11 Kabushiki Kaisha Toshiba Carbon dioxide separating and capturing system and method of operating same
CN115253608A (zh) * 2022-08-31 2022-11-01 西安热工研究院有限公司 一种燃煤发电机组的烟气碳捕集系统及方法

Also Published As

Publication number Publication date
JP2011240321A (ja) 2011-12-01

Similar Documents

Publication Publication Date Title
WO2011132660A1 (fr) Système de traitement de gaz d'échappement ayant un dispositif d'élimination de dioxyde de carbone
US9399939B2 (en) Combustion exhaust gas treatment system and method of treating combustion exhaust gas
JP5450540B2 (ja) Ｃｏ２回収装置を備えたボイラーの熱回収システム
JP6072055B2 (ja) 排ガス処理システム及び方法
JP5639814B2 (ja) 脱ｃｏ２設備付き火力発電システム
US8828130B2 (en) Exhaust gas treatment system equipped with carbon dioxide removal device
WO2013039041A1 (fr) Dispositif et procédé de récupération de co2
JP5959882B2 (ja) 燃焼排ガス中の二酸化炭素化学吸収システム
WO2012014831A1 (fr) Système de traitement des effluents gazeux comportant un équipement d'élimination de co2
WO2011105120A1 (fr) Dispositif de récupération de co2 et méthode de récupération du co2
JP5738137B2 (ja) Ｃｏ２回収装置およびｃｏ２回収方法
JP5478921B2 (ja) 排煙処理装置と方法
JP2011194292A (ja) 排ガス処理方法および装置
EA025463B1 (ru) Способ улавливания coиз co-содержащего газа
WO2012067101A1 (fr) Procédé et dispositif de contrôle d'un système pour absorber chimiquement du dioxyde de carbone
JP6021932B2 (ja) Ｃｏ２回収装置およびｃｏ２回収方法
CA2785287C (fr) Systeme et procede de recuperation de chaleur a partir d'un dispositif de recuperation de co2
JP6173734B2 (ja) 排ガス処理システム
JP6004821B2 (ja) Ｃｏ２回収装置およびｃｏ２回収方法
AU2021331004A1 (en) Ammonia-based carbon dioxide abatement system and method, and direct contact cooler therefore

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11771995

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 11771995

Country of ref document: EP

Kind code of ref document: A1