WO2011124425A1 - Dispositif de séparation pour co2 et centrale électrique - Google Patents

Dispositif de séparation pour co2 et centrale électrique Download PDF

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Publication number
WO2011124425A1
WO2011124425A1 PCT/EP2011/053032 EP2011053032W WO2011124425A1 WO 2011124425 A1 WO2011124425 A1 WO 2011124425A1 EP 2011053032 W EP2011053032 W EP 2011053032W WO 2011124425 A1 WO2011124425 A1 WO 2011124425A1
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WO
WIPO (PCT)
Prior art keywords
desorber
line
steam
absorption
separating device
Prior art date
Application number
PCT/EP2011/053032
Other languages
German (de)
English (en)
Inventor
Norbert Pieper
Henning Schramm
Michael Wechsung
Original Assignee
Siemens Aktiengesellschaft
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 Siemens Aktiengesellschaft filed Critical Siemens Aktiengesellschaft
Priority to EP11712492A priority Critical patent/EP2555855A1/fr
Publication of WO2011124425A1 publication Critical patent/WO2011124425A1/fr

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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
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/343—Heat recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/064—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle in combination with an industrial process, e.g. chemical, metallurgical
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
    • F01K7/16—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type
    • F01K7/22—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type the turbines having inter-stage steam heating
    • 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
    • B01D2252/10—Inorganic absorbents
    • B01D2252/102—Ammonia
    • 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
    • B01D2252/20478—Alkanolamines
    • B01D2252/20484—Alkanolamines with one hydroxyl group
    • 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
    • B01D2252/20494—Amino acids, their salts or derivatives
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/50—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers
    • 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
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/32—Direct CO2 mitigation

Definitions

  • the invention relates to a separator for CO2 to ⁇ collectively an absorption unit and a desorption unit, wherein the absorption unit has a discharge line and a feed line for an absorption medium, and wherein the desorption, a plurality of between the discharge line and the feed line includes switched desorbers. Furthermore, the invention relates to a power plant with such a separation device.
  • the invention is concerned with the problem of reducing the CO 2 emission of a steam power plant by incorporating an absorption unit, the overall efficiency should remain as high as possible.
  • a carbon dioxide-containing exhaust gas is generated.
  • the minimization of emitted CO2 can be achieved here by the separation from the exhaust gas.
  • a nachgeschal ⁇ ended absorption process in separating the exhaust gas from CO2 can be cleaned.
  • the CO2 is usually washed out of the exhaust gas by an absorption-desorption process by means of a suitable absorption medium.
  • the exhaust gas is brought into contact with the absorption medium in an absorption unit, where it is absorbed or reversibly bound.
  • the GE- cleaned exhaust gas is discharged from the absorption unit, whereas the absorption medium loaded with CO2 is passed into a desorption unit for separating off the CO2 and for regenerating the absorption medium under temperature increase.
  • the separation takes place in the desorption übli ⁇ chide thermally, that is, the CO2 is desorbed by the application of heat and expelled.
  • the CO2 is finally condensed in several stages and cooled and sent for storage or recycling.
  • the regenerated solvent is passed to ⁇ back to the absorption unit, where it is available again for From ⁇ sorption of CO2.
  • the heat from ⁇ coupled process steam is used for the regeneration of the absorption medium.
  • large amounts of heat are needed at a fairly low ⁇ engined temperature level.
  • the heat is transferred under condensation.
  • the heat required can ⁇ example, by a Dampfentnähme from an overflow line between two turbine sections of the plant, especially Zvi ⁇ rule a medium pressure and a low pressure turbine, are made available.
  • the pressure is usually higher than that of the required condensation temperature Tempe ⁇ corresponding saturated vapor pressure in this case. Therefore, the withdrawal mass flow must be throttled lossy. This is per ⁇ but associated with significant thermodynamic losses, resulting in an undesirable deterioration in efficiency of the power plant.
  • a second object is to provide a power plant with a pre ⁇ called separation device, which has the highest possible overall efficiency.
  • the first object of the invention is achieved by a separation device with the feature combination according to claim 1.
  • the separation device for CO 2 comprises an absorption unit and a desorption unit, wherein the absorption unit has a discharge line and a supply line for an absorption medium, and wherein the desorption unit comprises a plurality of desorbers connected between the discharge line and the supply line ,
  • the desorber fluidly connected in parallel and to couple heat technology in series.
  • the invention takes into consideration that the available steam in a ⁇ power plant process steam may be be blank on its pressure level ⁇ if a separator is used with a plurality of desorbers which are thermally coupled in series.
  • the first desorber can be adjusted in was ⁇ nem temperature level to the available process steam pressure. The excess heat from the first
  • desorber is discharged to the downstream desorber for desorption so that the heat remains within the system.
  • desorber is discharged to the downstream desorber for desorption so that the heat remains within the system.
  • the desorbers are fluidically connected in parallel to each other. This makes it possible to adjust the pressure and temperature levels of the individual desorbers independently of one another, so that the heat in each individual desorber can be utilized as optimally as possible for the regeneration of the absorption medium.
  • the desorbers are connected in parallel in terms of flow on the brine side and are thermally coupled in series on the heating side. In other words, the supply of the loaded absorbent divides on the desorber, while ⁇ the discharge sides of the desorber are thermally coupled in series with each other.
  • the process steam between turbine stages having a predetermined temperature and a predetermined pressure, particularly after removal from egg ⁇ ner overflow must, prior to forwarding to the separator not be throttled to achieve compared to the removal decreased Kon ⁇ densations temperature.
  • the extracted process steam is used directly for the desorption unit.
  • the absorption medium is through
  • the extracted from the absorption unit C0 2 -rich solution is via the discharge line to a number divided by Desorber, which can be operated at different pressure and temperature levels.
  • the heat is made available to the first desorber, in terms of heat technology, in particular from extracted process steam.
  • the pressure level in the desorbers can be adjusted accordingly via pumps, compressors or compressors.
  • the desorption unit preferably comprises two desorbers connected in series by heating technology.
  • the invention also includes a corresponding juxtaposition of three and more desorbers.
  • the discharge line of the desorber are strö ⁇ ment technically connected to the supply of the absorption unit, wherein the discharge line of a thermally upstream each first desorber is thermally coupled in each case with a subsequent second or next desorber.
  • a suitable heat exchanger is used for heat transfer to the second desorber. This heat exchanger uses the waste heat in the From ⁇ yaksön the first desorber to raise the absorbing medium in the second desorber to the required for the regeneration temperature level there.
  • the discharge line of the first desorber for heat transfer to the second desorber via a insbe ⁇ special from the discharge line of the second desorber to heat the recirculated here in the desorber absorption medium.
  • This is also referred to as a so-called natural circulation process.
  • the return line can also be led out separately from the trigger side of the desorber.
  • the desorbers connected in series behind one another by heat technology are each reduced in relation to the preceding desorber
  • Pressure level designed. This allows multiple optimal overall succession the waste heat in a Kas ⁇ kade decreasing temperature be used.
  • the residual heat taken from the first desorber is passed on to the second desorber, which has a lower temperature level for regeneration by reducing the pressure.
  • the discharge line of the absorption unit is branched into the supply line of the desorber.
  • the loaded with CO 2 absorption medium is thus divided into the respective desorber.
  • the divided absorption medium is regenerated in parallel in the different desorbers at different pressure and thus temperature level.
  • the absorption medium flows after regeneration from the individual partial desorbers back into the absorber.
  • the refluxing absorption medium can be effectively cooled by means of a corresponding heat exchanger from egg ⁇ nem cooling circuit back to the temperature required for the absorption.
  • the respective discharge lines of the desorber are thermally coupled with the respective supply lines.
  • the waste heat still present in the absorption medium after the desorption of the CO 2 is used to preheat the supplied absorption medium already.
  • a return line from the withdrawal side is returned to the first desorber, which can be thermally coupled with Pro ⁇ zessdampf a steam power plant.
  • the particular ⁇ a heat exchanger is provided, which heats the recirculated through the return line in the first desorber absorption medium by means of heating steam.
  • Heating steam can basically be taken anywhere an expansion in a steam turbine.
  • process steam from an overflow line between two sub-turbines is preferably used as heating steam.
  • the absorption medium is a fluid.
  • ⁇ with liquids such as aqueous ammonium salt solutions or amino acid salt solutions are preferably used.
  • other liquids such as aqueous ammonia solutions, amine solutions such as monoethanolamine (MEA) or gaseous fluids are conceivable.
  • the second object of the invention is achieved by a power plant with the feature combination according to claim 8.
  • the power plant comprises a steam turbine having at ⁇ plurality of turbine sections which are flowed through each of vapor, as well as an overflow, which is disposed between two turbine sections.
  • a ⁇ tap line for the removal of process steam is connected, which is thermally coupled to a separating device of the type described above.
  • the pressures in an overflow line between medium and low-pressure turbines are usually between 4 and 8 bar.
  • the pressure of the process steam to be used which is necessary for a conventional separation device, can vary and be considerably lower. For aqueous solutions and at atmospheric pressure, for example, it is between 2 and 2.5 bar.
  • the necessary adaptation of the pressure level of the process steam leads to the above-mentioned unnecessary thermodynamic losses.
  • the steam power plant can be designed with a fired boiler for steam generation or as a gas and steam combined cycle power plant (combined cycle power plant).
  • the sub-turbines can each be designed for different pressures.
  • high pressure (HD), medium pressure (HD) and low pressure (MD) turbine engines are common.
  • a steam turbine has a plurality of ⁇ turbines that are designed for the same pressures.
  • process steam is preferably supplied via a bleed line, which is connected to an overflow line between the medium-pressure and low-pressure turbine sections.
  • FIG. 1 shows a separation device with an absorption unit and a desorption unit for separating CO 2 from an exhaust gas
  • FIG. 1 A first figure.
  • FIG. 1 shows a CO 2 separation device.
  • the separation device 1 has an absorption unit 3 and a desorption 5, which are connected to each other strömungstech ⁇ African.
  • the absorption unit 3 is used to absorb CO 2 from an exhaust gas, whereas in the desorption unit 5, the CO 2 is expelled again and finally fed to storage or recycling.
  • the exhaust gas is brought into this, the Absorptionsein ⁇ integrated 3 with an absorption medium in contact and bound there reversible.
  • the purified exhaust gas is discharged from the absorption unit 3 and the CO 2 loaded Ab ⁇ sorption medium is supplied to separate the carbon dioxide and regeneration of the absorption medium with temperature increase of the desorption 5.
  • the separation in the De ⁇ sorption 5 takes place thermally.
  • the absorption unit 3 has a discharge line 7 and a feed line 9 via which the absorption medium 3 located in the absorption medium of the absorption unit 3 to ⁇ performs or this can be supplied.
  • the absorption medium is an aqueous amino salt solution which has a
  • the absorption unit 3 has an inlet 11 for flue gas and an outlet 13 for the purified exhaust gas.
  • the incoming, liquid absorption medium washes in the counterflow direction from the rising flue gas CO 2 .
  • the desorption unit 5 For desorption of the carbon dioxide, the desorption unit 5 has a first and a second desorber 15, 17. For supplying laden absorption medium, both desorbers 15, 17 are connected in terms of flow with the discharge line 7 of the absorption unit 3. For this purpose, the discharge line 7 to a branch point 19, at which the absorption medium via feed lines 21, 23 is divided on the two desorber 15, 17. For this purpose, a pump 25 is provided which pumps the absorption medium in the direction of the desorbers 15, 17.
  • a heat exchanger 27, 29 is connected in each case.
  • the heat exchanger 27, 29 takes that Absorbent medium, which flows via the discharge line 7 from the absorption unit 3 to the desorbers 15, 17, remaining ⁇ heat of C0 2 ⁇ poor absorption medium, which flows back from the desorbers 15, 17 via the supply line 9 to the absorption unit 3.
  • both desorber 15, 17 depending ⁇ wells a withdrawal conduit 31, 33 that the desorber 15, 17 connects with the flow through the heat exchanger 27, 29 in fluid communication with the supply line 7 of the absorption unit.
  • the desorbers 15, 17 are thus connected in parallel fluidically.
  • the first desorber 15 is operated at a pressure of 3 bar and the second desorber 17 at 1 bar.
  • the absorption medium is cooled from 60 ° C to about 40 ° C and returned to the absorption device 3 after merging of two partial streams in the feed line 9 via a cooler 35 which is connected to a cooling circuit.
  • a return line 37 which bleed pipe thermally to a check is coupled for process steam from an overflow line between a medium-pressure and a low pressure turbine section of a steam power plant.
  • the coupled-Pro ⁇ zessdampf with a pressure of 4.5 bar and a temperature of about 260 ° C transfers the condensation heat in the saturated steam temperature of 148 ° C.
  • a bleed line 78 can be seen in FIG. The escaping from the absorbing medium in the first desorber 15 CO 2 can be ⁇ collected via an outlet.
  • the after absorption from the first desorber still heated absorption medium is a part of its residual heat via a heat exchanger 41 to the second desorber 17 from.
  • heated the absorption medium in the second desorber 17 from 90 ° C to about 120 ° C.
  • FIG. 2 shows a power plant 51 with a separation device 1 according to FIG.
  • the power plant is designed as a steam power plant ⁇ with seven sub-turbines 53, 55, 57, 59, 61, 63, 65, which are designed for different pressures.
  • the sub-turbines are arranged on a common shaft 67.
  • water is heated in a steam boiler 69 and heated via a first reheater 71 to above the condensation point of the steam.
  • the superheated steam is introduced via a pipe into a high-pressure turbine section 53, where the steam is released.
  • the steam is passed via a overflow line 73 into a second reheater 75 where it is reheated and then passed into a double-flow medium-pressure turbine section 55, 57.
  • the steam expands again to a predetermined pressure.
  • the steam expanded in the intermediate-pressure turbine sections 55, 57 is guided via a second overflow line 77 into two, respectively, double-flow low-pressure turbine sections 59, 61, 63, 65.
  • a tapping line 78 is connected to process steam.
  • the withdrawn process steam is provided directly to the separator 1 available.
  • the heat of the extracted process steam for the separation of CO 2 from flue gas according to the description of FIG 1 is used.
  • the tapping line 78 is thermally coupled with the evaporator forming return line 37 of the arranged there first desorber 15. The heat is transferred under condensation.
  • the Dampfentnähme from an overflow is described here ⁇ play and shown.
  • the heating steam can basically any point of expansion in one
  • a generator 79 is ben ⁇ industry , which converts the mechanical power into electrical power.
  • the relaxed and cooled steam leaving the double-flow low-pressure turbine sections 59, 61 and 63, 65 flows through the condensers 81, 83 where it condenses by heat transfer to the environment and collects as liquid water.
  • the condensate is combined and collected via a condensate pump 85 and two preheaters 87, 89 in a feedwater tank 91. Via a feedwater pump 93 and a further preheater 95, the water is again supplied to the steam boiler 69.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un dispositif de séparation (1) pour CO2, comprenant une unité d'absorption (3) ainsi qu'une unité de désorption (5), l'unité d'absorption (3) présentant un conduit d'évacuation (7) et un conduit d'amenée (9) pour un milieu d'absorption, et l'unité de désorption (5) comprenant une pluralité de désorbeurs (15, 17) intercalés entre le conduit d'évacuation (7) et le conduit d'amenée (9). Il est prévu que les désorbeurs (15, 17) soient montés en parallèle en termes de technique des fluides et en série en termes de technique de la chaleur. L'invention concerne également une centrale électrique (51) équipée d'un tel dispositif de séparation (1). Pour le dispositif de séparation (1), on peut utiliser directement de la vapeur de processus prélevée dans un conduit trop-plein (73, 77). Le rendement d'une centrale électrique (51) équipée d'un tel dispositif de séparation (1) est comparativement élevé.
PCT/EP2011/053032 2010-04-07 2011-03-01 Dispositif de séparation pour co2 et centrale électrique WO2011124425A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP11712492A EP2555855A1 (fr) 2010-04-07 2011-03-01 Dispositif de séparation pour co2 et centrale électrique

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010003676.5 2010-04-07
DE102010003676A DE102010003676A1 (de) 2010-04-07 2010-04-07 Abscheidevorrichtung für CO2 und Kraftwerk

Publications (1)

Publication Number Publication Date
WO2011124425A1 true WO2011124425A1 (fr) 2011-10-13

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DE (1) DE102010003676A1 (fr)
WO (1) WO2011124425A1 (fr)

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CN103357250A (zh) * 2012-04-06 2013-10-23 李志远 从气体混合物中收集二氧化碳和/或硫化氢的设施和过程
CN110966618A (zh) * 2019-12-26 2020-04-07 杭州新世纪能源环保工程股份有限公司 一种采用三级换热的蒸汽烟气换热装置

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Publication number Priority date Publication date Assignee Title
WO2015000701A1 (fr) * 2013-07-02 2015-01-08 Siemens Aktiengesellschaft Installation de séparation de co2 et procédé permettant de faire fonctionner ladite installation
CN106540519B (zh) * 2016-11-03 2022-10-11 中国神华能源股份有限公司 烟气处理装置和应用其的烟气处理方法
WO2020131309A1 (fr) * 2018-12-20 2020-06-25 Entegris, Inc. Système actif de filtration par épuration par voie humide
CN114515497B (zh) * 2020-11-19 2023-06-06 中国石油化工股份有限公司 一种二乙烯基苯生产尾气的处理系统和处理方法

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