EP2049231A1 - Procédé de séparation du co2 d'un flux de gaz, dispositif de séparation de co2 permettant la mise en oeuvre du procédé, buse de tourbillonnement pour dispositif de séparation de co2 et application du dispositif de séparation de co2 - Google Patents

Procédé de séparation du co2 d'un flux de gaz, dispositif de séparation de co2 permettant la mise en oeuvre du procédé, buse de tourbillonnement pour dispositif de séparation de co2 et application du dispositif de séparation de co2

Info

Publication number
EP2049231A1
EP2049231A1 EP07787692A EP07787692A EP2049231A1 EP 2049231 A1 EP2049231 A1 EP 2049231A1 EP 07787692 A EP07787692 A EP 07787692A EP 07787692 A EP07787692 A EP 07787692A EP 2049231 A1 EP2049231 A1 EP 2049231A1
Authority
EP
European Patent Office
Prior art keywords
swirl nozzle
gas stream
cooled
separation device
gas
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.)
Withdrawn
Application number
EP07787692A
Other languages
German (de)
English (en)
Inventor
Gianfranco Dr. Guidati
Alexander Prof. Dr. Ni
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.)
General Electric Technology GmbH
Original Assignee
Alstom Technology AG
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 Alstom Technology AG filed Critical Alstom Technology AG
Publication of EP2049231A1 publication Critical patent/EP2049231A1/fr
Withdrawn legal-status Critical Current

Links

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
    • B01D53/24—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 centrifugal force
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
    • 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
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06—Construction of inlets or outlets to the vortex chamber
    • 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
    • F01K23/10—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 with exhaust fluid of one cycle heating the fluid in another cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/34—Gas-turbine plants characterised by the use of combustion products as the working fluid with recycling of part of the working fluid, i.e. semi-closed cycles with combustion products in the closed part of the cycle
    • 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
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C2003/006—Construction of elements by which the vortex flow is generated or degenerated
    • 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
    • Y02E20/14—Combined heat and power generation [CHP]
    • 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 present invention relates to the field of climate protection technology. It relates to a process for the separation of CO 2 from a gas stream, a CO 2 - separation device for carrying out the method, a swirl nozzle for such a CO 2 separation device, and various applications of the CO 2 - separation device.
  • the gas stream is compressed in a first step to separate off CO2 from a gas stream which is produced as exhaust gas or flue gas during the combustion of fossil fuels, that the compressed gas stream is cooled down in a second step the cooled gas stream is supplied in a third step of a swirl nozzle and separated from the gas stream CO2 in the swirl nozzle, and that in a fourth step, the separated CO2 in the swirl nozzle for separate further treatment is removed from the swirl nozzle.
  • An embodiment of the method according to the invention is characterized in that, within the second step, the compressed gas stream is first precooled in a heat exchanger operating with cooling water, and the gas stream preheated in the heat exchanger is further cooled by means of at least one refrigeration circuit operating with compressor, condenser, expansion valve and evaporator.
  • the pre-cooled gas stream for further cooling by means of two working with compressor, condenser, expansion valve and evaporator cooling circuits can be further cooled sequentially.
  • the preheated gas stream is sent to the further cooling by the evaporator (s) of the refrigeration cycle or refrigeration circuits.
  • Another embodiment of the method according to the invention is characterized in that the gas flow is supplied to the compression at approximately room temperature and, after the compression in the heat exchanger, is again pre-cooled to approximately room temperature.
  • Another embodiment is characterized in that the gas flow is further cooled by means of the first refrigeration cycle only to the extent that no water from the gas stream in the associated heat exchanger freezes, and that the gas flow by means of the second refrigeration cycle to a temperature of about - 50 0 C further cooled is, wherein the evaporator of the second refrigeration circuit to de-ice at certain time intervals is de-iced and the De-icing of the evaporator, the pre-cooling of the gas stream is interrupted in working with cooling water heat exchanger.
  • the C ⁇ 2-poor gas stream exiting from the swirl nozzle is sent through the condenser of the second refrigeration cycle for cooling the refrigerant in the second refrigeration cycle.
  • Another embodiment is characterized in that the separated in the swirl nozzle CO2 is supplied to the liquefaction of a liquefaction plant.
  • a further embodiment of the method according to the invention is characterized in that the cooled-down gas stream in an input section of the swirl nozzle is first set in rotation about the axis of the swirl nozzle, that the resulting rotating flow is then reduced in diameter, that the reduced diameter in the rotating flow then is passed through a central portion of the swirl nozzle with a constant diameter, wherein CO2 accumulates in the outer edge region of the swirl nozzle, and that at the end of the central portion before an end portion of the enriched CO2 is separated at a arranged on the outer circumference of the swirl nozzle CO 2 outlet, wherein in the end portion the swirl nozzle is increased by increasing the diameter of the pressure in the gas stream flowing to the gas outlet.
  • An embodiment of the CO 2 separation device according to the invention is characterized in that the plurality of cooling devices provided upstream of the swirl nozzle comprises at least one heat exchanger through which cooling water flows and at least one refrigeration circuit connected downstream of the heat exchanger and operating with compressor, condenser, expansion valve and evaporator.
  • the heat exchanger two successively arranged, each working with compressor, condenser, expansion valve and evaporator Refrigeration circuits downstream, wherein the condenser of the first refrigeration cycle is flowed through by cooling water, and the condenser of the second refrigeration circuit is flowed through by the swirl nozzle emerging from CO 2 gas stream, and wherein the two compressors of the cooling circuits are driven by a common motor.
  • the swirl nozzle can be followed by a liquefaction plant for the liquefaction of the separated CO 2 .
  • An embodiment of the swirl nozzle according to the invention is characterized in that radially arranged inlet guide vanes are arranged in the input section for impressing the rotation, and in that the inlet guide vanes are designed to be adjustable.
  • Another embodiment is characterized in that between the middle section and the end portion on the outer circumference of the swirl nozzle, a CO 2 outlet is provided.
  • means for accelerating the gas flow in the circumferential direction can be provided in the input section of the swirl nozzle, the acceleration means comprising either concentric annular nozzles, through which air is injected in a direction adapted to the rotation of the gas flow in the swirl nozzle, or wall segments rotating about the axis of the swirl nozzle, whose rotational speed is adapted to the rotation of the gas flow in the swirl nozzle.
  • Fig. 2 in three sub-figures 2 (a), 2 (b) and 2 (c) a swirl nozzle according to a preferred embodiment of the invention in an axial view
  • FIG. 4 shows the application of the CO 2 separator of FIG. 1 in a steam power plant
  • Fig. 5 shows the application of the CO 2 separator of FIG. 1 in one
  • Fig. 6 shows the application of the CO 2 separator of FIG. 1 in one
  • Fig. 7 shows the application of the CO 2 separator of FIG. 1 in one
  • Fig. 8 shows the application of the CO 2 separator of FIG. 1 at a
  • Fig. 10 is an alternative to Fig. 9 CO 2 separation device, in which the
  • Swirl nozzle is arranged
  • FIG. 11 shows an alternative CO 2 separation device to FIG. 10, in which FIG.
  • Turbine and compressors are arranged on a common shaft.
  • the present invention relates to the capture of CO2 from the flue gas or flue gas of an engine or plant using carbon (e.g., coal) or hydrocarbons (e.g., methane, methanol, ethanol, etc.) as a fuel.
  • carbon e.g., coal
  • hydrocarbons e.g., methane, methanol, ethanol, etc.
  • the fuel is oxidized, causing
  • CO2 is formed.
  • the heat generated during the oxidation process is either converted to mechanical or electrical energy (e.g., by a generator) or used directly as process heat or for heating (e.g., a building).
  • Such machine may be a coal-fired or gas fired or oil fired power plant (e.g., a gas turbine)
  • Combined cycle power station a stationary diesel engine, a building heating or a vehicle engine or the like.
  • the principle of the invention is a treatment of the CO 2 -enriched exhaust gases or flue gases, which comprises the following steps:
  • the exhaust gas or flue gas is cooled by means of a heat exchanger to ambient temperature (about 20 0 C - 25 ° C);
  • the first refrigeration cycle CC1 extracts heat from the exhaust gas in the first evaporator 15 and delivers it to the cooling water flowing through the first condenser 26.
  • the outlet temperature of the first evaporator 15 is selected so that no water can freeze on the heat exchanger surfaces of the first evaporator 15.
  • the exhaust gas then flows through the second evaporator 16 of the second Refrigeration circuit CC2.
  • the second evaporator 16 lowers the temperature of the exhaust to about -50 0 C.
  • the capacitor 21 is arranged of this circuit at the output of the twisting nozzle 17 to utilize the cold of the exiting there residual gas.
  • the two refrigeration circuits CC1 and CC2 are kept in motion by compressors 24, 25, which in the exemplary embodiment are driven by a common motor 23. Because of the low temperatures at the second evaporator 16, the residual water will be deposited in the exhaust gas at the local heat exchanger surfaces as ice film. Therefore, a defrosting process is required in which, at certain intervals, the water cooling in the heat exchanger 14 is reduced or completely switched off. It flows then exhaust gas with a temperature of about 100 0 C introduced into the evaporator 16, which leads to a deicing. De-icing takes up about 1% of the total operating time.
  • the exhaust gas After leaving the second evaporator 16, the exhaust gas enters one (or more parallel) swirl nozzle (s) 17, where it is further cooled (as will be explained below) by acceleration. This further cooling leads to a separation of CO2 from the exhaust gas.
  • the CO2 is extracted from the swirl nozzle 17 and then sent to a liquefaction plant 18 where it is liquefied and processed for further transport in a pipeline 19.
  • FIG. 2 An essential component of the CO 2 separation device 10 of FIG. 1 is the swirl nozzle 17, which is shown in different views in FIG. 2.
  • the swirl nozzle 17 is constructed coaxially and extends along an axis 38. It has in concentric arrangement an inner wall 29 and an outer wall 28, between which an annular channel for the exhaust gas flow is formed.
  • the swirl nozzle 17 is divided into a tapered diameter inlet section 30, a central section 32 of constant (or slightly increasing or decreasing) diameter, and an end section 34 of rapidly expanding diameter.
  • FIG. 2 (a) shows the input section 30 with radially acting inlet guide vanes 31 in the axial direction.
  • FIG. 2 (b) shows the longitudinal section through the swirl nozzle 17.
  • the exhaust gas (flue gas) enters from the left into the swirl nozzle 17 at a diameter Ri.
  • the reason for the re-sublimation of the CO 2 particles is that the total pressure, the release of the heat of desublimation in the
  • the gaseous CO2 remains concentrated in the outer zone of the swirl nozzle 17 because it (1) has a density 50% higher than air, and (2) the centrifugal flow field generates forces approximately 50,000 times the gravitational acceleration.
  • the concentrated CO2 is extracted through slots in the outer wall 28 of the swirl nozzle 17 and passed via a CO2 outlet 33 to a liquefaction plant (18 in FIG. 1).
  • the remaining offgas content is separated off and the resulting liquid is discharged via a pipeline (19 in FIG. 1).
  • the main energy consumption during the CO 2 separation concerns the compressor 13, which increases the total pressure upstream of the evaporators 15, 16 of the refrigeration circuits CC1 and CC2. This increased total pressure is necessary to compensate for the pressure losses in the heat exchangers and especially in the swirl nozzles 17. Since the velocity in the swirl nozzle is predominantly oriented in the circumferential direction, the wall friction of the flow is governed by the azimuthal component of the velocity. In order to minimize the wall friction, two ways can be used, which are exemplified in Fig. 3 (a) and Fig. 3 (b).
  • a swirl nozzle 17 ' air is injected through annular slots (ring nozzles 36) in the wall at an angle corresponding to the helix angle of the core flow.
  • the flow is thereby accelerated in azimuthal direction and thus reduces the total pressure loss.
  • the slots can be arranged concentrically in the inner wall 29 and / or the outer wall 28.
  • a slot is created by arranging individual wall elements at a distance. The distance between the wall elements is maintained by ribs arranged to achieve the desired helix angle of the injected air.
  • a similar acceleration of the flow can be achieved according to Fig.
  • both techniques insufflation and rotation
  • both techniques can be used on both the inner wall 29 and the outer wall 28.
  • both techniques can also be used in the predominantly straight central part and in the terminal end section 34 both on the outside and on the inside.
  • the end portion 34 of the swirl nozzle 17 acts as a diffuser which decelerates the flow to a low speed, with which it then leaves the swirl nozzle.
  • This section is primarily responsible for the loss of total pressure that must be applied by the compressor 13. Diffusion can be enhanced by providing exhaust vanes that convert the residual swirl into an increase in static pressure.
  • FIG. 4 shows the integration of a CO 2 separator 10 into a coal-fired, steam turbine steam power plant 40.
  • Coal provided via a fuel feed 44 is burned in a boiler 41 comprising a combustor 43 and a steam generator 42.
  • the steam generator provides high pressure, high temperature steam for a Rankine cycle.
  • the flue gas leaves the boiler 41 at about 200 ° C.
  • the flue gas is cooled down in a heat exchanger 39 through which cooling water flows, in order to cool the flue gas Flue gas temperature at the entrance of the CO 2 -Abtrennhchtung 10 to about 25 ° C to decrease.
  • FIGS. 5 and 6 show two exemplary possibilities for integrating the CO 2 separating device 10 into a combined cycle power station 50 or 60 equipped with gas turbines 46.
  • the compressor 49 of the gas turbine 46 compresses ambient air supplied via the air supply 47, heats it by combustion of hydrocarbons (eg natural gas, oil, syngas etc.) in a combustion chamber 51 and relaxes the hot gas under working power in a turbine 52, which drives the compressor 49 and a generator 48.
  • hydrocarbons eg natural gas, oil, syngas etc.
  • HRSG heat recovery steam generator
  • a variant of the combined cycle power plant 50 from FIG. 5 is the combined cycle power plant 60 from FIG. 6.
  • a portion of the exhaust gas is branched off at a branch 55 located in the exhaust gas line 54 behind the heat exchanger 39 and returned via a return 56 to the inlet of the compressor 49.
  • the amount of CO 2 in the exhaust gas led to the CO 2 separation device 10 is increased while the exhaust gas as a whole is reduced. This reduces the power consumption of the compressor 13 in the CO 2 separation device 10.
  • Both variants can also be used in gas turbines with sequential combustion (eg of the type GT24 / GT26 of the applicant).
  • FIG. 7 shows an example of the integration of the CO 2 separation device 10 from FIG. 1 into a combined heat and power plant 64, which is equipped, for example, with an internal combustion engine (diesel) 59, which receives the fuel via a fuel supply 61.
  • a combined heat and power plant 64 which is equipped, for example, with an internal combustion engine (diesel) 59, which receives the fuel via a fuel supply 61.
  • Such facilities can be larger buildings or groups of houses with Supply heat and electricity.
  • the internal combustion engine 59 burns by means of ambient air hydrocarbons (eg diesel fuel) and generates mechanical or electrical energy.
  • the exhaust gas exits the engine at high temperatures of 500-800 0 C.
  • a power circuit PC which comprises an evaporator 58, a power turbine 63, a condenser 68 and a pump 62nd
  • the heat released in the condenser 68 is used for heating purposes.
  • the exhaust gas flows through the evaporator 58 of the power circuit PC and gives off further heat for heating purposes at a downstream, water-cooled heat exchanger 57.
  • the exhaust gas temperature at the inlet of the CO 2 separator 10 is then again about 25 ° C.
  • the power turbine 63 of the power circuit PC can thereby drive the compressor 13 of the CO 2 separation device 10.
  • the system diagram of Fig. 7 can also be applied to land vehicles or watercraft with internal combustion engine.
  • a boiler 65 is supplied with fuel (coal, oil, natural gas, etc.) via a fuel supply 67.
  • fuel coal, oil, natural gas, etc.
  • the existing in the exhaust CO2 can be separated without loss of energy, because the heater provides the power that is necessary to drive the compressor 13 of the CO 2 separator 10 via a power circuit PC. Instead of using the high temperature heat directly for the heater, it is introduced into the power circuit, partially converted to mechanical energy and then removed at lower temperatures for heating purposes (capacitor 68).
  • Capacitor 68 Capacitor 68
  • the exhaust gas flow can be expanded by means of a turbine 70 in the case of CO 2 separation devices 10 b or 10 c, in order to bring about the initial cooling in front of the swirl nozzle 17.
  • the stream is further expanded, the CO 2 extracted, and the Stream with a downstream compressor 13 again compressed to atmospheric pressure.
  • compressor 13 and turbine 70 are separated.
  • the turbine 70 drives a generator 69.
  • turbine 70 and compressor 13 are arranged on a common shaft.
  • the exhaust gas stream can also be expanded directly into the swirl nozzle 17 and is then compressed back to atmospheric pressure by means of a compressor 13 which is arranged behind the swirl nozzle 17.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Exhaust Gas After Treatment (AREA)
  • Chimneys And Flues (AREA)
  • Treating Waste Gases (AREA)

Abstract

La présente invention concerne un procédé de séparation du CO2 d'un flux de gaz, en particulier d'un flux de gaz d'échappement d'un processus de combustion se déroulant avec des combustibles fossiles. Le procédé se caractérise en ce que le flux de gaz est comprimé au cours d'une première étape, le flux de gaz comprimé est refroidi au cours d'une deuxième étape, le flux de gaz refroidi alimente une buse de tourbillonnement (17') et le CO2 est séparé du flux de gaz dans la buse de tourbillonnement (17) au cours d'une troisième étape, et le CO2 isolé dans la buse de tourbillonnement (17) est expulsé hors de la buse de tourbillonnement (17) au cours d'une quatrième étape, pour subir un traitement ultérieur séparé.
EP07787692A 2006-08-07 2007-07-18 Procédé de séparation du co2 d'un flux de gaz, dispositif de séparation de co2 permettant la mise en oeuvre du procédé, buse de tourbillonnement pour dispositif de séparation de co2 et application du dispositif de séparation de co2 Withdrawn EP2049231A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US82159106P 2006-08-07 2006-08-07
CH3632007 2007-03-07
PCT/EP2007/057434 WO2008017577A1 (fr) 2006-08-07 2007-07-18 Procédé de séparation du co2 d'un flux de gaz, dispositif de séparation de co2 permettant la mise en oeuvre du procédé, buse de tourbillonnement pour dispositif de séparation de co2 et application du dispositif de séparation de co2

Publications (1)

Publication Number Publication Date
EP2049231A1 true EP2049231A1 (fr) 2009-04-22

Family

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EP07787692A Withdrawn EP2049231A1 (fr) 2006-08-07 2007-07-18 Procédé de séparation du co2 d'un flux de gaz, dispositif de séparation de co2 permettant la mise en oeuvre du procédé, buse de tourbillonnement pour dispositif de séparation de co2 et application du dispositif de séparation de co2

Country Status (5)

Country Link
US (1) US7985278B2 (fr)
EP (1) EP2049231A1 (fr)
JP (1) JP5334849B2 (fr)
CN (1) CN101522286B (fr)
WO (1) WO2008017577A1 (fr)

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US8534094B2 (en) * 2008-04-09 2013-09-17 Shell Oil Company Method and apparatus for liquefying a hydrocarbon stream
CH700310A1 (de) 2009-01-23 2010-07-30 Alstom Technology Ltd Verfahren zur CO2 Abscheidung aus einem Kombikraftwerk und Kombikraftwerk mit einer Gasturbine mit Strömungsteilung und Rezirkulation.
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EP2290202A1 (fr) * 2009-07-13 2011-03-02 Siemens Aktiengesellschaft Installation de cogénération et procédé de cogénération
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WO2008017577A1 (fr) 2008-02-14
JP2010500163A (ja) 2010-01-07
US20090173073A1 (en) 2009-07-09
US7985278B2 (en) 2011-07-26
CN101522286A (zh) 2009-09-02
JP5334849B2 (ja) 2013-11-06
CN101522286B (zh) 2012-08-15

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