WO2015000701A1 - Installation de séparation de co2 et procédé permettant de faire fonctionner ladite installation - Google Patents

Installation de séparation de co2 et procédé permettant de faire fonctionner ladite installation Download PDF

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Publication number
WO2015000701A1
WO2015000701A1 PCT/EP2014/062843 EP2014062843W WO2015000701A1 WO 2015000701 A1 WO2015000701 A1 WO 2015000701A1 EP 2014062843 W EP2014062843 W EP 2014062843W WO 2015000701 A1 WO2015000701 A1 WO 2015000701A1
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WO
WIPO (PCT)
Prior art keywords
desorber
pressure
steam
compressor unit
plant
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2014/062843
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German (de)
English (en)
Inventor
Norbert Pieper
Henning Schramm
Michael Wechsung
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Siemens AG
Siemens Corp
Original Assignee
Siemens AG
Siemens Corp
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 AG, Siemens Corp filed Critical Siemens AG
Publication of WO2015000701A1 publication Critical patent/WO2015000701A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • 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 invention relates to a plant for the separation of C0 2 from an exhaust stream of a load-dependent combustion device, comprising a C0 2 -Abscheidevoriques, wherein the C0 2 -Abscheidevorides is fluidly coupled to the combustion device, wherein the C0 2 -Abscheidevorides a desorber and an absorber wherein the desorber fluidly downstream of a compressor unit, which is intended to densify a derived from the C0 2 -Abscheidevortechnisch, C0 2 -conducting gas mass flow. Furthermore, the invention relates to a method for operating such a system.
  • a known method is the separation of carbon dioxide from an exhaust gas after a combustion process (post-combustion C0 2 capture - Postcap). In this process, the carbon dioxide is separated off with a detergent in an absorption-desorption process.
  • the exhaust gas is in an absorption column with a selective The solvent is brought into contact as a detergent.
  • the absorption of carbon dioxide takes place by a chemical or physical process.
  • the purified exhaust gas is discharged from the absorption column for further processing or discharge.
  • the loaded with carbon dioxide solvent is passed to separate the carbon dioxide and regeneration of the solvent in a desorption column.
  • the separation in the desorption column can be carried out thermally. In this case, a gas-vapor mixture of gaseous carbon dioxide and vaporized solvent is expelled from the loaded solvent.
  • the evaporated solvent is then separated from the gaseous carbon dioxide.
  • the carbon dioxide can now be compressed and cooled in several stages. In liquid, supercritical or frozen state, the carbon dioxide can then be sent for storage or recycling.
  • the regenerated solvent is passed again to the absorber column, where it can again absorb carbon dioxide from the exhaust gas containing carbon dioxide.
  • a heat output at a temperature level of about 120 to 150 ° C is required. This heat output can be provided by steam, which is taken from the steam turbine plant. After passing through the desorption column, the vapor condenses and is returned to the steam cycle.
  • a steam turbine plant usually consists of one
  • High, medium and low pressure parts A steam introduced into the high-pressure part is gradually expanded via the middle and the subsequent low-pressure part. Between the high and the medium-pressure part regularly takes place reheating.
  • the delimitation of medium and low pressure part is usually characterized by a Dampfent Spotify réelle on the overflow between medium and low pressure part.
  • the removal of steam from the overflow line for the purpose of C0 2 separation is comparable to a process steam extraction, as is customary for example for district heating.
  • the amount of extracted steam is dependent on the operation of the process steam consumer or the separator and can vary quite from 0% to 65%.
  • the amount of steam removed leads to a reduction of the steam mass flow, which is supplied to the subsequent turbine stage.
  • the cost-effectiveness of such a steam power plant with process steam extraction is therefore significantly lower.
  • a first object of the invention is therefore to specify a plant for deposition of C0 2 , which avoids the above-mentioned problem.
  • a second task is the specification of a method for the operation of such a system.
  • the first object is achieved by specifying a system for the separation of C0 2 from a flue gas stream of a load-dependent combustion apparatus comprising a C0 device 2 -Abborge-, wherein the C0 2 -Abscheidevoriques fluid power cally with the combustion device coupled to said C0 2 -Abscheidevoriques having a desorber and an absorber, wherein the desorber fluidly a
  • Compressor unit is load-dependent adjustable.
  • Desorber pressure reduces the energy required for desorption of C0 2 . With the help of the invention, this degree of freedom is now used especially at partial loads. By the compressor unit, the desorber pressure is now adjusted load-dependent to the required level. It is the
  • Compressor unit now designed at least with a compressor.
  • the compressor unit may also include a compressor with appropriately upstream control element, eg a valve.
  • the Dersorberdruck can therefore either directly via the compressor or via the control organ adjustable be. Also, a setting on the compressor, which is supported by the control element, is conceivable.
  • the expelled from the detergent C0 2 mass flow is dissipated in each load condition of the compressor unit.
  • This can now promote the corresponding volume flow in a large storage volume constant pressure for further use.
  • the load range of the compressor can be extended also, as always a substantially constant C0 2 -Volumenstrom must be processed.
  • the half C0 2 volumetric flow at half the desorber pressure at partial load results in the same C0 2 volume flow as at full load the full C0 2 mass flow.
  • the desorber pressure can be adjusted load-dependent, above all, via the admission pressure of the compressor unit.
  • the desorber is preferably thermally coupled to a process steam-conducting device, wherein the process steam has a process steam pressure, and wherein the desorber pressure is adapted to the process steam pressure.
  • the process vapor pressure is designed as a sliding pressure.
  • the system preferably has at least two turbines. These are connected to each other via an overflow line. The process steam can be taken from the overflow line.
  • the desorber pressure in the desorber is adjusted depending on the load state such that the required process steam pressure corresponds to the natural sliding pressure, for example, between the medium-pressure and low-pressure turbine.
  • the throttle valve can be largely dispensed with a throttle valve according to the prior art.
  • the throttle losses at partial load which would amount to more than 10 MW, for example, in an 800 MW combustion system at half load.
  • the incinerator is a power plant, in particular a gas and steam power plant, which is operable with respect to a load, the desorber pressure decreasing as the load is reduced.
  • the desorber pressure on the operation of the compressor unit in particular the compressor, adjustable.
  • the mode of operation preferably comprises at least the drive power and / or the operating point. Depending on the drive power and operating point of the compressor unit adjusts load-dependent a certain form, which is also present in the desorber.
  • the operating point can now be changed either by changing the speed or by using a Vorleitgitters.
  • the pre-pressure and thus the adjusting desorber pressure of a constant-speed C0 2 -evaporator unit are kept constant by adjusting the position of a Vorleitgitters.
  • the C0 2 mass flow is now limited.
  • the process vapor pressure can be measured by arranging process steam measuring devices.
  • the desorber pressure can be measured by arranged desorber measuring devices.
  • the desorber measuring devices and the process steam measuring devices are arranged.
  • the compressor unit is now preferably adjustable on the basis of the measured values.
  • the task related to the method is characterized by specifying a method for operating a plant as described above for the deposition of C0 2 , comprising a C0 2 -Abscheide- device with a desorber and an absorber, wherein the desorber fluidly downstream of a compressor unit is, wherein the desorber has a desorber pressure, which is adjusted load-dependent via the compressor unit.
  • the desorber is preferably thermally coupled to a process steam-conducting device, wherein the process steam has a process steam pressure, and wherein the desorber pressure is adapted to the process steam pressure.
  • the temperature level of the desorption and thus the required process steam pressure in each load condition can be adjusted to the prevailing pressure in the conduit used for branching off the process steam, i. be adapted here in the overflow between medium pressure and low pressure turbine. If the load in the power plant drops, so does the process steam pressure and according to the invention
  • FIG. 3 shows a schematic diagram of the invention. 1 shows schematically and not conclusively a C0 2 -
  • the CO 2 separation device 1 comprises an absorber 3 and a desorber 5 connected fluidically thereto.
  • the flue gas is introduced into the C0 2 - Abscheidevor- direction 1 forwarded.
  • the flue gas is supplied to the absorber 3 via a flue gas line 7.
  • the absorber 3 there is an aqueous amino acid salt solution as the washing medium 9, which is used for separating off the imine
  • Flue gas contained carbon dioxide is used.
  • the flue gas in the absorber 3 is brought into contact with the washing medium 9 and the carbon dioxide contained in the flue gas in
  • Wash medium 9 absorbed.
  • the gas mass flow purified by carbon dioxide is released from the absorber 3 at the absorber head 11.
  • the absorber 3 is fluidically connected to a feed line 15 of the desorber 5, so that the loaded with carbon dioxide washing medium 9 can be pumped via these two lines 13, 15 with temperature increase by means of a pump 17 in the desorber 5.
  • the loaded washing medium 9 passes through a heat exchanger 19, in which the heat of the regenerated washing medium 9 flowing from the desorber 5 to the absorber 3 is transferred to the laden washing medium 9 supplied to the desorber 5 by the absorber 3.
  • the heat exchanger 19 thus uses the waste heat of the desorber 5 to preheat the washing medium 9 from the absorber 3 before entering the desorber 5.
  • the carbon dioxide absorbed in the washing medium 9 is thermally desorbed.
  • a discharge line 21 is connected to the desorber 5.
  • the desorber 5 leaves a largely exempt from other components of C0 2 - gas mass flow which a compressor unit is fed to the 30th
  • the compressor unit 30 can consist of a compressor with a number of compressor stages (not shown).
  • the compressor unit 30 may also have a compressor with a corresponding upstream control element (for example a valve) (not shown).
  • the desorber 5 is further connected to a return line 25.
  • the return line 25 is fluidically connected to a feed line 27 of the absorber 3.
  • the scrubbing medium 9 regenerated in the desorber 5 is returned to the absorber 3 via the fluidic connection between the return line 25 and the supply line 27 by means of a pump 29, where it is available for re-absorption of CO 2 from the flue gas.
  • the supply line 27 may still have a cooling device 32.
  • the desorber 5 is connected to a reboiler heat exchanger 31.
  • the loaded washing medium 9 is in this case by steam, which in the
  • Reboilertownleyer 31 is heated with process steam 50 from a connected steam power plant, which is not shown here. 2 shows a steam power plant 100 according to the state of
  • the steam power plant 100 comprises a steam turbine comprising a high-pressure turbine section 200, a medium-pressure turbine section 300 and a low-pressure turbine section 400, which are connected to one another in a torque-transmitting manner via a common shaft train 500.
  • a generator not shown, is arranged at the shaft strand 500.
  • the steam from the high-pressure turbine part 200 flows to a reheater 110.
  • the steam is reheated to a higher temperature. Subsequently, the steam flows into a medium-pressure steam inlet 130 of the medium-pressure turbine section 300.
  • the medium-pressure turbine part 300 comprises a first flood 140 and a second flood 150.
  • the first flood 140 and the second flood 150 each comprise stages, which are not shown in more detail Guides and blades not shown are formed.
  • the steam flowing into the medium-pressure turbine section 300 is divided into a first partial flow and a second partial flow, the first partial flow flowing through the first flow 140 and the second partial flow flowing in the opposite direction into the second flow 150.
  • the vapor in the first flood 140 flows into a first turbine outlet conduit 170 via a first mid-pressure turbine outlet 160.
  • the vapor in the second flood 150 flows through a second intermediate-pressure turbine outlet 180 into a second turbine exit conduit 190.
  • Both the first turbine exit conduit 170 and the second turbine exit conduit 190 open into an overflow line 120 symbolized by a horizontal line.
  • the overflow line 120 is fluidically connected to a low-pressure inlet 210 via a low-pressure inlet line 220.
  • a steam trap (not shown in detail) is provided in each case.
  • Stage a steam extraction line 230 arranged.
  • the steam flowing into the first flow 140 and into the second flow 150 flows, firstly, via the first 170 and the second turbine outlet line 190 to the low-pressure turbine section 400 and, secondly, via the steam extraction line 230 to the first
  • the steam power plant 100 therefore also has a throttle flap 240 in the overflow line 120.
  • this throttle valve 240 the pressure of the steam in the overflow 120 can be adjusted.
  • the pressure of the steam in the steam extraction line 230 depends on the setting of the throttle valve 240.
  • the disadvantage here is that in the Dampfentnähme from the steam extraction line 230, the entire steam flowing through the first turbine outlet line 170 and the second turbine outlet line 190 into the low-pressure turbine section 400 is throttled.
  • the disadvantage especially in partial load operation is that the throttling of the remaining steam thermodynamically leads to a high loss. Therefore occur in partial loads partly significant throttle losses, which in turn reduce the efficiency of the system.
  • the heat supplied to the desorber 5 through the so-called reboiler heat exchanger 31 is transferred by condensation.
  • the required temperature therefore also corresponds to a defined pressure.
  • the required pressure of the steam may vary.
  • all pressures in the turbines 300,400 behave approximately proportionally proportional to the load, while the process usually requires a constant temperature and thus a constant process steam pressure. It is therefore necessary, especially at partial load, to throttle the pressure via a throttle valve 240 independently of the load to a constant value. According to the invention is now the desorber over the
  • the required temperature level of the C0 2 deposition process in the desorber 5 (FIG. 1) is shifted by this variation of the desorber pressure.
  • the desorber pressure directly influences the temperature level in the desorber 5 (FIG. 1) via the boiling conditions in the compressor unit 30 (FIG. 1), which in turn determines the CO 2 solubility equilibrium.
  • the temperature level in the desorber 5 (FIG. 1) increases.
  • a higher process steam temperature is required for a C0 2 separation in the desorber 5 (FIG. 1), ie, as the desorber pressure increases, the energy requirement, which must be supplied by the process steam 50 (FIG. 1, 2), increases for desorption of the C0 2 .
  • the same can also be transferred to a decreasing pressure, ie as the pressure decreases
  • the desorber pressure in the desorber 5 (FIG. 1) is now preferably adapted depending on the load state such that the required process steam pressure corresponds to the natural sliding pressure between the medium-pressure 300 and low-pressure part turbine 400 (FIG. 2).
  • the process steam pressure is therefore not constant, but adapted to the sliding pressure. This eliminates the throttle losses at partial load, which would be more than 10 MW, for example, in an 800 MW plant at half load.
  • the expelled from the detergent C0 2 mass flow is therefore removed in each load condition of the compressor unit 30 (FIG 1), which is essential for trouble-free operation.
  • the desorber pressure is now set via the admission pressure in the compressor unit 30 (FIG. 1). This is preferably possible via the mode of operation of the compressor unit 30 (FIG. 1).
  • the mode of operation includes, for example, the drive power or the operating point.
  • the operating point can now be changed either via a change in the rotational speed or through the use of a guiding grille (not shown).
  • Vorleitgitter can deflect the flow to the impeller (not shown), for the conversion of flow rate in pressure energy.
  • the desorber pressure is adjusted to this process steam pressure such that sufficient CO 2 separation takes place in the detergent of the desorber 5 (FIG. 1) despite lower process steam pressure (and therefore process steam temperature). That is, via the reboiler heat exchanger 31 (FIG. 1), the detergent, which is subject to the desorber pressure, is still heated in such a way that a C0 2 separation takes place despite, for example, a lower process steam temperature.
  • the desorber pressure is reduced depending on the load via the compressor unit 30 (FIG a C0 2 -Ab ⁇ cutting even at a lower process steam temperature, ie temperature in the reboiler heat exchanger 31 (FIG 1) and thus at lower temperature heating of the detergent in the desorber 5 (FIG 1) instead.
  • the Dersorberdruck can be adjustable either directly via the compressor or else via the control element (not shown). Also, a setting on the compressor, which is supported by the control element, is conceivable. In this case, the form and thus the desorber pressure of a constant-speed C0 2 -Verêtr Ober 30 (FIG 1) by eg adjusting the position of a Vorleitgitters (not shown) are kept constant.
  • the compressor unit 30 (FIG.
  • the load range of the compressor unit 30 (FIG. 1) can also be expanded.
  • other means for adjusting the admission pressure and thus the adjusting desorber pressure in the compressor unit 30 (FIG. 1) can also be used.
  • the admission pressure and the process vapor pressure can also be determined via suitably arranged sensors (pressure sensors, temperature sensors).
  • the pre-pressure of the compressor unit 30 (FIG. 1) and thus the desorber pressure can thus be suitably adjusted almost at the same time as the process steam pressure 50 drops.
  • the compressor unit 30 (FIG. 1) has a final compressor pressure which is advantageously largely constant in the various load ranges.
  • the invention provides for adjusting the desorber pressure in the desorber 5 (FIG. 1) to the load state of the power plant.
  • the temperature level of the desorption and thus the required process steam pressure in each load state can be adapted to the prevailing pressure in the line, which is used for branching off the process steam, ie here in the overflow line 120 between medium-pressure 300 and low-pressure turbine 400. If the load in the power plant drops, so does the process vapor pressure and according to the invention the desorber pressure in Desorber 5 off.
  • the process steam pressure is therefore not constant, but adapted to the natural sliding pressure. Also can be dispensed with the throttle valve 240 behind the Listeffentnähme.
  • a process vapor pressure of 5 bar (about 152 ° C) may be present, corresponding to a desorber pressure of 2.3 bar (about 125 ° C) in the detergent, such as an aqueous amine solution.
  • the process steam 50 (FIG. 1, 2) has a process steam pressure of 2.5 bar (approximately 127 ° C.). This corresponds in an aqueous amine solution, for example, 1 bar (about 100 ° C).
  • FIG. 3 again shows schematically the relationship which should be briefly repeated here again, specifically with reference to the example in which a power plant operated at full load passes into partial load.
  • the invention is also applicable to a lifting of the load, for example, partial load to full load.
  • the compressor unit 30 (FIG. 1) is set 401 to this new lower pressure, e.g. over the operating point.
  • a pressure matching the process steam pressure is now present 402.
  • a desorber pressure 404 matching the process steam pressure is established.
  • the process steam 50 flows 405 with a lower process steam pressure and therefore a lower temperature to the
  • Compressor unit 30 (FIG 1).

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  • 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)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne une installation permettant de séparer le CO2 présent dans un flux de gaz d'échappement d'un dispositif de combustion fonction de la charge, l'installation comprenant un dispositif de séparation du CO2 (1), le dispositif de séparation du CO2 (1) étant raccordé fluidiquement au dispositif de combustion, le dispositif de séparation du CO2 (1) présentant un désorbeur (5) et un absorbeur (3), le désorbeur (5) étant monté fluidiquement en aval d'un groupe compresseur (30) qui est conçu pour comprimer un flux massique de gaz d'acheminement du CO2 provenant du dispositif de séparation du CO2, le désorbeur (5) présentant une pression de désorption qui peut être réglée en fonction de la charge par le groupe compresseur (30). L'invention concerne par ailleurs un procédé permettant de faire fonctionner l'installation selon l'invention.
PCT/EP2014/062843 2013-07-02 2014-06-18 Installation de séparation de co2 et procédé permettant de faire fonctionner ladite installation Ceased WO2015000701A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013212897 2013-07-02
DE102013212897.5 2013-07-02

Publications (1)

Publication Number Publication Date
WO2015000701A1 true WO2015000701A1 (fr) 2015-01-08

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Application Number Title Priority Date Filing Date
PCT/EP2014/062843 Ceased WO2015000701A1 (fr) 2013-07-02 2014-06-18 Installation de séparation de co2 et procédé permettant de faire fonctionner ladite installation

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112023638A (zh) * 2020-09-27 2020-12-04 赵道沛 工业生产过程中尾气净化吸收装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1900415A1 (fr) * 2006-09-06 2008-03-19 Mitsubishi Heavy Industries, Ltd. Système de récupération de CO2 et procédé de récupération de CO2
EP2105191A1 (fr) * 2008-03-27 2009-09-30 Siemens Aktiengesellschaft Procédé et dispositif de séparation de dioxyde de carbone d'un gaz d'échappement d'une centrale à combustible fossile
EP2105187A1 (fr) * 2008-03-27 2009-09-30 Siemens Aktiengesellschaft Procédé et dispositif de séparation de dioxyde de carbone d'un gaz d'échappement d'une centrale à combustible fossile
DE102010003676A1 (de) * 2010-04-07 2011-10-13 Siemens Aktiengesellschaft Abscheidevorrichtung für CO2 und Kraftwerk

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1900415A1 (fr) * 2006-09-06 2008-03-19 Mitsubishi Heavy Industries, Ltd. Système de récupération de CO2 et procédé de récupération de CO2
EP2105191A1 (fr) * 2008-03-27 2009-09-30 Siemens Aktiengesellschaft Procédé et dispositif de séparation de dioxyde de carbone d'un gaz d'échappement d'une centrale à combustible fossile
EP2105187A1 (fr) * 2008-03-27 2009-09-30 Siemens Aktiengesellschaft Procédé et dispositif de séparation de dioxyde de carbone d'un gaz d'échappement d'une centrale à combustible fossile
DE102010003676A1 (de) * 2010-04-07 2011-10-13 Siemens Aktiengesellschaft Abscheidevorrichtung für CO2 und Kraftwerk

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112023638A (zh) * 2020-09-27 2020-12-04 赵道沛 工业生产过程中尾气净化吸收装置

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