US20120216540A1 - Coal power plant having an associated co2 scrubbing station and heat recovery - Google Patents

Coal power plant having an associated co2 scrubbing station and heat recovery Download PDF

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Publication number
US20120216540A1
US20120216540A1 US13/383,204 US201013383204A US2012216540A1 US 20120216540 A1 US20120216540 A1 US 20120216540A1 US 201013383204 A US201013383204 A US 201013383204A US 2012216540 A1 US2012216540 A1 US 2012216540A1
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Prior art keywords
heat
heat exchanger
power plant
compression
region
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Inventor
Brian Stoever
Dieter König
Christian Bergins
Martin Schönwälder
Torsten Buddenberg
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Hitachi Power Europe GmbH
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Hitachi Power Europe GmbH
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Assigned to HITACHI POWER EUROPE GMBH reassignment HITACHI POWER EUROPE GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BERGINS, CHRISTIAN, STOEVER, BRIAN, BUDDENBERG, TORSTEN, KONIG, DIETER, SCHONWALDER, MARTIN
Publication of US20120216540A1 publication Critical patent/US20120216540A1/en
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    • 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
    • F01K13/00—General layout or general methods of operation of complete plants
    • 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
    • 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • 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
    • 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
    • F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
    • F01K27/02—Plants modified to use their waste heat, other than that of exhaust, e.g. engine-friction heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L15/00—Heating of air supplied for combustion
    • F23L15/04—Arrangements of recuperators
    • 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
    • B01D2252/20478—Alkanolamines
    • B01D2252/20489—Alkanolamines with two or more hydroxyl groups
    • 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
    • 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
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • 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
    • Y02E20/32—Direct CO2 mitigation
    • 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
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention is directed towards a method for heat recovery by connecting a plurality of heat streams of a fossil-fired, in particular coal-fired, power plant having downstream CO 2 scrubbing of the flue gas by way of chemical absorption and/or desorption and associated CO 2 compression.
  • the invention is directed towards a power plant, in particular a fossil-fired power plant, and preferably a coal-fired power plant, having a CO 2 scrubbing station which is downstream of the combustion and is for the flue gas by means of chemical absorption and/or desorption and associated CO 2 compression.
  • the principle of separation before combustion is based on reaction of the fossil fuel to form a synthesis gas consisting of carbon monoxide and hydrogen, wherein, in a further step, the carbon monoxide is oxidized to carbon dioxide (CO 2 ) and is then removed from the process.
  • a synthesis gas consisting of carbon monoxide and hydrogen
  • the integrated separation is effected in what is termed the oxy-fuel process.
  • a highly concentrated carbon dioxide (CO 2 ) exhaust gas stream is generated by combustion of the fossil fuel, in particular coal, with pure oxygen instead of air, which exhaust gas stream, after condensation of the steam fraction, can be directly disposed of without additional scrubbing.
  • the carbon dioxide (CO 2 ) is separated off by a scrubbing station.
  • the flue gas is largely removed from the flue gas at the end of the flue gas purification line by means of a CO 2 scrubbing station by means of chemical absorption, and so a CO 2 -poor exhaust gas leaves the power plant.
  • This CO 2 scrubbing station is located in an absorber, wherein the chemical absorption proceeds using a scrubbing medium, in particular monoethanolamine (MEA), but also diethanolamine (DEA) or methyldiethanolamine (MDEA).
  • MEA monoethanolamine
  • DEA diethanolamine
  • MDEA methyldiethanolamine
  • the CO 2 -loaded scrubbing medium is freed from the CO 2 in a desorber or regenerator and treated and then recirculated to the absorber.
  • a very-high-CO 2 -content exhaust gas leaves the desorber or regenerator, which very-high-CO 2 -content exhaust gas is liquefied in a subsequent CO 2 compression and thereafter for final storage or reuse is removed from the region of the power plant.
  • the great advantage of this method is that existing conventional power plants can be retrofitted therewith.
  • the disadvantage of this method results from the high energy expenditure necessary for the CO 2 separation. Firstly, a high energy requirement is necessary for regeneration of the scrubbing medium used, which energy requirement is usually covered in the form of steam branched off from the water-steam circuit of the associated power plant.
  • a reboiler or evaporator of the desorber or regenerator is fed, by means of which the circulated scrubbing medium is heated to the temperature necessary for expelling CO 2 . Further energetic expenditure is necessary for subsequent CO 2 compression for liquefaction of the carbon dioxide.
  • the object of the invention is to provide a solution which makes possible a thermally favorable integration of a CO 2 scrubbing of the flue gas with associated CO 2 compression into the overall heat stream and/or the overall thermal energy balance of a fossil-fired, in particular coal-fired, preferably conventional, power plant.
  • this object is achieved in that, from the heat stream of the CO 2 scrubbing station with associated-CO 2 compression, thermal energy in the form of at least one heat substream is extracted and fed back into a heat stream that is coupled directly or indirectly to the heat stream of the boiler or steam generator of the power plant and/or in that, from the flue gas heat stream, thermal energy in the form of at least one heat substream is extracted and fed back into the heat stream of the CO 2 scrubbing station with associated CO 2 compression.
  • thermal energy available in the region of the CO 2 scrubbing station with associated CO 2 compression is decoupled or extracted from the heat stream of the CO 2 scrubbing station with associated CO 2 compression as a heat substream by means of at least one plant component that is utilizable there as a heat source
  • thermal energy available in the region of a flue gas line is decoupled or extracted from the heat stream of the flue gas by means of at least one plant component that is utilizable there as a heat source and the thermal energy in the region of the power plant obtained respectively by the decoupling or extraction in the form of the at least one heat substream is fed back into the heat stream of the power plant outside the respective decoupling or extraction region by means of at least one further plant component that is utilizable there in each case as heat sink for the thermal energy obtained.
  • the abovementioned object is achieved in a power plant of the type described in more detail at the outset in that, in the region of the CO 2 scrubbing station with associated CO 2 compression, at least one plant component that is utilized as heat source and effects the decoupling or extraction of thermal energy from the heat stream of the CO 2 scrubbing station with associated CO 2 compression is arranged and/or constructed, and/or, in the region of a flue gas line and/or a bypass flue gas line bypassing an air preheater, at least one plant component that is utilized as heat source and effects the decoupling or extraction of thermal energy from the flue gas stream is arranged and/or constructed, and in the region of the power plant, at least one, preferably a further, plant component which is connected in a heat-energy-conducting manner to the first plant component and is used as a heat sink and effects the feeding back of the decoupled or extracted thermal energy into the heat stream of the power plant outside the respective decoupling or extraction region is arranged and/or constructed.
  • the method is further distinguished in that thermal energy available in a CO 2 -rich gas stream and/or in the absorption medium used is decoupled or extracted in the region of the CO 2 scrubbing station with associated CO 2 compression.
  • the invention in an embodiment of the method, provides that thermal energy available in the flue gas is decoupled or extracted in the region of the flue gas line and/or in the region of a bypass flue gas line bypassing an air preheater.
  • the thermal energy that is decoupled or extracted in the region of the CO 2 scrubbing station with associated CO 2 compression is fed back into the heat stream of the power plant outside the region of the CO 2 scrubbing station with associated CO 2 compression, in particular into the water-steam circuit and/or a district heating circuit and/or into a coal-bearing coal line and/or a fresh air line, in particular having associated flue gas bypass line, in particular air preheater bypass, for feeding heat into WT14, WT17 and/or WT13.
  • the thermal energy which is decoupled or extracted in the region of the flue gas line and/or in the region of the bypass flue gas line is fed back outside the region of the flue gas line and/or the bypass flue gas line into the water-steam circuit and/or the district heating circuit and/or the region of the CO 2 scrubbing station with associated CO 2 compression, in particular into a heat exchanger of a reboiler.
  • the CO 2 scrubbing station of the flue gas by means of chemical absorption and/or desorption and associated CO 2 compression is and/or can be integrated thermally expediently and in an optimized manner into the overall heat stream and thereby the overall thermal energy balance of a fossil-fired, in particular coal-fired, preferably conventional, power plant.
  • waste heat streams formed in the region of the CO 2 scrubbing station and in the region of the CO 2 compression are used as heat source(s).
  • a heat source is taken to mean the possibility of decoupling and extracting unrequired thermal energy in the form of at least one heat substream from the respective waste heat stream, that is to say a medium carrying thermal energy in the form of measurable heat, and thereafter feeding it in a heat-energy-conducting manner to a heat sink arranged at another point of the power plant outside the region of the CO 2 scrubbing of the flue gas with associated CO 2 compression.
  • a heat sink in this case is taken to mean that the thermal energy that is fed in a heat-conducting manner and is extracted or decoupled in the region of the CO 2 scrubbing station with associated CO 2 compression is fed back into the heat stream of the power plant, i.e. it is transferred to a medium of a lower thermal energy level, i.e. a lower temperature, that is running or flowing there, and thereby heat taken off from the region of the CO 2 scrubbing station with associated CO 2 compression is recirculated and recovered.
  • a medium of a lower thermal energy level i.e. a lower temperature
  • the thermal energy which otherwise leaves unutilized the region of the CO 2 scrubbing station of the flue gas with associated CO 2 compression together with the purified flue gas stream or with the liquefied carbon dioxide stream is according to the invention therefore at least in part utilized and recirculated to the heat stream of the power plant in the course of heat recovery.
  • thermal energy in the form of a heat substream is decoupled or extracted from the thermal energy present in the flue gas and in the region of the CO 2 scrubbing station, in particular in the region of the reboiler or evaporator there, is fed back into the heat stream of the CO 2 scrubbing station.
  • This embodiment may also be implemented independently of the above-described decoupling and extraction of thermal energy from the region of the CO 2 scrubbing station with associated CO 2 compression.
  • This use or recoupling of thermal energy that is decoupled or extracted on the flue gas side is preferably provided in combination with thermal energy that is decoupled or extracted from the region of the CO 2 scrubbing station with associated CO 2 compression and fed back into the heat stream of the power plant in the region outside the CO 2 scrubbing station with associated CO 2 compression.
  • the fresh air fed to the boiler or steam generator of the power plant is then heated by way of a heat exchanger to which thermal energy which is decoupled or extracted from the region of the CO 2 scrubbing station with associated CO 2 compression is fed for delivery to the inflowing fresh air mass stream.
  • solar-heating or geo-thermal energy production systems are assigned to the power plant, the energy thereof that is produced therein being fed or made available to the heat stream of the power plant in the form of thermal energy.
  • the decoupling or extraction at the CO 2 scrubbing station desorber or regenerator top proceeds downstream of the CO 2 compression and in the direction of flow of CO 2 .
  • Advantageous sites for the construction of heat sources or heat sinks for the decoupling or extraction of thermal energy are, in addition, in the region of the CO 2 scrubbing station absorber intercooler and in the region of the CO 2 compression intercooler.
  • Particularly advantageous sites for feeding back in the extracted thermal energy are the region of the low-pressure pre-heater and also the region in the direction of flow downstream of a condensate pump arranged downstream of a condenser, wherein the above regions are all constructed in the water-steam circuit of the power plant.
  • the method according to the invention is further distinguished in that the thermal energy is decoupled or extracted by means of one or more heat sources formed at the CO 2 scrubbing station desorber or regenerator top and/or downstream of the CO 2 compression in the CO 2 flow direction and/or in the region of the CO 2 scrubbing station absorber intercooler and/or in the region of the CO 2 compression intercooler, and the thermal energy is fed back in by means of one or more heat sinks formed in the region of the low-pressure preheater and/or in the condensate flow direction upstream of the low-pressure preheater and/or in a district heating circuit and/or in a fresh air heater and/or in a coal drying station and heat-energy-conductingly connected to the heat source(s).
  • a further advantageous embodiment of the invention is that the thermal energy is decoupled or extracted by means of one or more heat sources formed in the flue gas line and/or in the bypass flue gas line and the thermal energy is fed back into the water-steam circuit in the region of the low-pressure preheater and/or the high-pressure preheater and/or into the district heating circuit and/or into the region of the CO 2 scrubbing station, in particular into the reboiler, preferably a heat exchanger of the reboiler.
  • the power plant in an embodiment of the invention, is therefore distinguished in that one or more plant components utilized as heat source(s) for heat transfer is/are arranged and/or formed at the CO 2 scrubbing station desorber or regenerator top and/or downstream of the CO 2 compression in the CO 2 flow direction and/or in the region of the CO 2 scrubbing station absorber intercooler and/or in the region of the CO 2 compression intercooler, each of which plant components is heat-energy-conductingly connected in a manner bearing a heat-carrier medium to one or more plant components arranged in the region of the low-pressure preheater and/or in the condensate flow direction upstream of the low-pressure preheater and/or in a district heating circuit and/or in the fresh air heater and/or in the coal drying station and, as heat sink(s), effecting a heat transfer.
  • one or more plant components utilized as heat source(s) for heat transfer is/are arranged and/or formed at the CO 2 scrubbing station desorber or regener
  • a possibility that may be readily implemented in terms of the method and the plant of forming heat sources and heat sinks is to use plant components that are present therefor and/or are formed as additional heat exchangers.
  • the invention also provides with respect to the power plant that at least one plant component, preferably a heat exchanger, forming a heat source, in particular for a separate heat-carrier medium, is formed in the region of the CO 2 scrubbing station with associated CO 2 compression and is connected in the manner heat-energy-conductingly bearing a medium, preferably the separate heat-carrier medium, to at least one further plant component arranged in the region of the power plant, preferably a further heat exchanger, forming a heat sink, in particular for the separate heat-carrier medium, wherein one or more of the plant components selected from a heat exchanger at the CO 2 scrubbing station desorber or regenerator top and/or a heat exchanger downstream of the CO 2 compression and/or a heat exchanger of the CO 2 scrubbing station absorber
  • the heat exchanger forming a heat source at the CO 2 scrubbing station desorber or regenerator top is heat-energy-conductingly connected to a heat exchanger, forming a heat sink, of the low-pressure preheater, in particular to the heat exchanger next to a condensate pump positioned on the upstream side to the condensate flow direction.
  • a further possibility for advantageously implementing the extraction of thermal energy and feeding it back in is, in addition, that the heat exchanger forming a heat source is heat-energy-conductingly connected downstream of the CO 2 compression to a heat exchanger, forming a heat sink, of the low-pressure preheater, in particular to the heat exchanger next to a feed water vessel in the condensate flow direction, and/or to the heat exchanger, forming a heat sink, upstream of the low-pressure preheater.
  • the heat exchanger, upstream of the low-pressure preheater is arranged in a condensate line downstream in the condensate flow direction of a condensate pump, and/or the heat exchangers of the low-pressure preheater are arranged in a bypass line branching off from the condensate line, which the invention likewise provides.
  • a thermally particularly expedient coupling together of the heat exchangers WT 2 and WT 5 may be achieved in that the return of the heat exchanger of the low-pressure pre-heater is heat-energy-conductingly connected to the flow of the heat exchanger upstream of the low-pressure preheater.
  • a further advantageous and expedient heat-energy-conducting connection between the individual heat sources and the individual heat sinks may be achieved, in particular, if, between the heat sources and the heat sinks, a heat-carrier medium, in particular a heat-carrier medium separate from the remaining mass flow of the power plant, is circulated between them, which is preferably the case when the heat sources and heat sinks are formed as heat exchangers.
  • the invention in a further embodiment, therefore also provides that a heat-carrier medium is conducted in a circuit formed by the heat exchanger downstream of the CO 2 compression, the heat exchanger next to a feed water vessel in the condensate flow direction and the heat exchanger upstream of the low-pressure preheater and/or is conducted in a circuit formed by the heat exchanger at the CO 2 scrubbing station desorber or regenerator top and the heat exchanger next to a condensate pump positioned in the upstream-side condensate flow direction, in each case through these heat exchangers.
  • An expedient possibility for forming heat recovery also comprises feeding the decoupled or extracted thermal energy back into the district heating circuit of a power plant, if such a district heating circuit is provided. Therefore, in an embodiment, the invention also provides that the heat exchanger at the CO 2 scrubbing station desorber or regenerator top and/or the heat exchanger downstream of the CO 2 compression is/are heat-energy-conductingly connected to one or more heat exchangers arranged in the district heating circuit.
  • a pipe connection and coupling between the heat exchangers arranged in the district heating circuit and the heat exchangers arranged in the region of the water-steam circuit of the power plant can be advantageous, for which reason the invention is also distinguished in that one or more of the heat exchangers arranged in the district heating circuit is/are heat-energy-conductingly connected to one or more of the heat exchangers associated with or arranged upstream of the low-pressure preheater.
  • the heat exchanger can be arranged upstream of the low-pressure preheater in the return of the heat exchanger arranged in the district heating circuit and/or in the return of the heat exchanger associated with the low-pressure preheater.
  • a further possibility for using the thermal energy recovered by extraction is to use it for coal drying and/or for fresh air heating.
  • An advantageous use according to the invention therefore comprises in addition that the heat exchanger at the CO 2 scrubbing station desorber or regenerator top and/or the heat exchanger downstream of the CO 2 compression is/are heat-energy-conductingly connected to one or more heat exchangers arranged in a power plant coal line connected to a coal mill.
  • the invention also provides that the heat exchanger at the CO 2 scrubbing station desorber or regenerator top and/or the heat exchanger downstream of the CO 2 compression is/are heat-energy-conductingly connected to one or more heat exchangers arranged in a fresh air line feeding fresh air to the boiler of the power plant.
  • the invention further provides that the at least one heat exchanger arranged in the bypass flue gas line is heat-energy-conductingly connected to the water-steam circuit of the power plant in the region of the low-pressure preheater or the high-pressure preheater.
  • a heat exchanger arranged in the bypass flue gas line is heat-energy-conductingly connected to the district heating circuit.
  • a heat exchanger arranged in the bypass flue gas line is heat-energy-conductingly connected to the reboiler and/or to a heat exchanger of the reboiler.
  • the invention also provides that the heat exchanger at the CO 2 scrubbing station desorber or regenerator top and/or the heat exchanger downstream of the CO 2 compression and/or the heat exchanger of the CO 2 scrubbing station absorber intercooler and/or the heat exchanger of the CO 2 compression intercooler is/are heat-conductingly connected to a heat exchanger arranged in a Rankine cycle.
  • FIG. 1 shows, schematically, power plant components of a coal-fired, in particular brown-coal-fired, power plant,
  • FIG. 2 shows, schematically, power plant components of a coal-fired power plant having heat (re-) feeding of thermal energy extracted in the region of the CO 2 scrubbing station having associated CO 2 compression into the water-steam circuit and into a district heating circuit associated with the power plant,
  • FIG. 3 shows, schematically, the district heating circuit according to FIG. 2 having additionally integrated evaporator heating
  • FIG. 4 shows, schematically, an alternative embodiment of a heat (re-)feeding into a district heating circuit
  • FIG. 5 shows, schematically, a heat (re-)feeding into a coal conveyor and/or coal dryer of a coal mill associated with a power plant
  • FIG. 6 shows, schematically, a heat (re-)feeding into the fresh air heating of a fresh air line feeding fresh air to burners of a boiler of the power plant
  • FIG. 7 shows, schematically, a heat (re-)feeding of thermal energy extracted in the region of the CO 2 scrubbing station with associated CO 2 compression and of thermal energy extracted in the region of a bypass flue gas line into the water-steam circuit of the power plant,
  • FIG. 8 shows, schematically, a heat (re-)feeding corresponding to FIG. 7 with additional heat (re-)feeding into an associated district heating circuit
  • FIG. 9 shows, schematically, an indirect steam heater of a water circuit of an indirect heating system of a reboiler
  • FIG. 10 shows, schematically, heat (re-)feeding into a Rankine cycle
  • FIG. 11 shows, schematically, extraction of thermal energy in the region of a bypass flue gas line and feeding of the thermal energy in the region of the evaporator/reboiler of the desorber of the CO 2 scrubbing station,
  • FIG. 12 shows, schematically, a heat (re-)feeding according to FIG. 11 supplemented by a fresh air preheater and
  • FIG. 13 shows, schematically, an outline diagram of various heat substreams of a power plant having a plurality of heat substreams connecting heat streams of the power plant for heat recovery.
  • FIG. 13 schematically, shows an outline diagram of a power plant overall designated 1 , the steam generator or boiler 2 , a turbine set 76 , preferably comprising high-pressure turbines 3 , medium-pressure turbines 4 and low-pressure turbines 5 , a CO 2 separator 77 comprising a CO 2 scrubbing station 58 with associated CO 2 compression 27 , and an associated district heating grid 78 comprising a district heating circuit 44 .
  • These plant components 2 , 76 , 77 and 78 are mutually connected to one another via various heat substreams, wherein these heat substreams together form the total heat stream and the total thermal energy balance of the power plant 1 .
  • FIG. 13 shows an outline diagram of a power plant overall designated 1 , the steam generator or boiler 2 , a turbine set 76 , preferably comprising high-pressure turbines 3 , medium-pressure turbines 4 and low-pressure turbines 5 , a CO 2 separator 77 comprising a CO 2 scrubbing station 58 with associated CO 2
  • the water-steam circuit is designated Q 1 , the district heating integration Q 2 , the flue-gas-side heat stream connection of the CO 2 separator 77 to the boiler 2 as Q 3 , the heat stream fed with the air to the boiler as Q 4 , the heat stream fed by way of the coal to the boiler 2 as Q 5 , the low-CO 2 waste gas heat stream leaving the CO 2 separator as Q 6 and the heat substream leaving the CO 2 separator 77 of the high-CO 2 -content medium as Q 7 , wherein all substreams Q 1 to Q 7 are shown with dashed lines.
  • heat substreams Q 8 to Q 11 are branched off and decoupled from the heat stream forming within the CO 2 separator 77 , as indicated by the correspondingly labeled arrows shown in continuous lines, and recirculated to other heat substreams and thereby the total heat stream of the power plant 1 .
  • the heat substreams Q 12 to Q 14 are branched off or decoupled and, corresponding to the arrow drawing, likewise fed (back) into the total heat stream of the power plant 1 .
  • the heat substream Q 8 is extracted from the CO 2 separator 77 and fed into the heat substream Q 1 conducted in the water-steam circuit of the power plant 1 .
  • the heat substream Q 9 is extracted from the CO 2 separator 77 and fed into the district heating circuit 44 of the district heating grid 78 and thereby, in principle, to the heat substream Q 2 .
  • the heat substream Q 10 is extracted or decoupled from the CO 2 separator 77 and fed to the heat substream Q 4 of the fresh air feed and fed (back) into this.
  • the heat substream Q 11 is likewise extracted from the heat stream of the CO 2 separator 77 and then fed (back) into the heat substream Q 5 conducted in a coal line 55 leading to a coal mill 54 and/or the boiler 2 .
  • a heat substream Q 12 is extracted from the flue-gas-side heat substream Q 3 , which heat substream Q 12 is fed (back) into the heat substream conducted in the CO 2 separator 77 .
  • the heat substreams Q 13 and Q 14 are extracted, of which the heat substream Q 13 is fed back into the heat substream Q 1 of the water-steam circuit of the power plant 1 and the heat substream Q 14 is fed back into the district heating circuit 44 of the district heating grid 78 .
  • the power plant designated in FIG. 1 overall with 1 is shown schematically in the upper partial picture with the water-steam circuit thereof connected to the boiler 2 and in the lower partial picture with the flue gas path thereof connected on the flue gas side to the boiler 2 with the flue gas CO 2 scrubbing by way of chemical absorption and associated CO 2 compression 27 downstream of the combustion proceeding in the boiler 2 .
  • the power plant On the water-steam circuit side, the power plant comprises a high-pressure turbine 3 , two medium-pressure turbines 4 and four low-pressure turbines 5 , wherein the number of turbines is merely by way of example.
  • a generator is arranged at the end of the turbine section.
  • a condenser 7 Downstream of the last low-pressure turbine 5 , in the water-steam circuit a condenser 7 is arranged which as usual is connected to a cooling tower 8 .
  • a condensate pump 9 In the direction of flow of the condensate, a condensate pump 9 is arranged downstream of the condenser 7 in the water-steam circuit, which condensate pump 9 feeds the condensate to a low-pressure preheater 10 comprising five heat exchangers.
  • the low-pressure preheater 10 is connected to a feed water vessel 11 with associated feed water pump 12 which feeds the feed water originating from the feed water vessel 11 to a high-pressure preheater 13 , whereafter it then passes into the steam generator of the boiler 2 .
  • steam lines departing from the respective turbines 3 , 4 , 5 are drawn in the water-steam circuit.
  • this part of the power plant comprises components as are known from conventional coal-fired power plants.
  • the water-steam circuit of the power plant 1 has, furthermore, three heat exchangers WT 1 , WT 2 and WT 5 .
  • the heat exchanger WT 5 thereof is integrated into the condensate line 14 leading to the feed water vessel 11 upstream of the low-pressure preheater, more precisely in the direction of flow of the condensate, downstream of the condensate pump 9 , but upstream of the low-pressure preheater 10 .
  • the heat exchangers WT 1 and WT 2 are arranged in a bypass line 15 branching off from the condensate line 14 , in the direction of flow of the condensate downstream of the heat exchanger WT 5 , and opening out back into the condensate line 14 downstream of the low-pressure preheater 10 , but upstream of the feed water vessel.
  • the boiler 2 is fired, as indicated by the arrow 16 , with air and coal.
  • the flue gas leaving the boiler 2 via the flue gas line 17 is fed to a flue gas treatment 18 at least comprising the components denitration system, electrostatic precipitator and flue gas desulfurization system, and then passes into a decarbonization system 19 comprising a CO 2 scrubbing station 58 with associated CO 2 compression 27 .
  • the CO 2 present in the flue gas is removed by way of chemical absorption using a scrubbing medium.
  • the scrubbing medium used is preferably MEA (monoethanolamine, H 2 N—CH 2 —CH 2 —OH) or else DEA (diethanolamine, HO—CH 2 —CH 2 —NH—CH 2 —CH 2 —OH) or MDEA (methyldiethanolamine, HO—CH 2 —CH 2 —NCH 3 —CH 2 —CH 2 —OH).
  • the actual scrubbing of the flue gas or exhaust gas by way of the scrubbing medium takes place in an absorber 20 or an absorption column through which the flue gas flows in countercurrent to the scrubbing medium.
  • the flue gas leaves the absorber 20 at the top end thereof as a low-CO 2 exhaust gas 21 .
  • desorber or regenerator 22 preferably in the form of a desorption column, is connected downstream of the absorber 20 , to which desorber or regenerator the CO 2 -rich scrubbing medium or solvent is fed after it flows through the absorber 20 .
  • a high energy requirement is necessary which is fed to the evaporator or the reboiler 23 of the desorber/regenerator 22 in the form of steam tapped off from the water-steam circuit, as is indicated in the upper partial picture of FIG. 1 by the dashed line and the letters D 1 in this region and also at the reboiler 23 .
  • the return S 1 of the heat exchanger 24 arranged in or on the evaporator 23 opens out into the condensate line of the water-steam circuit downstream, in the direction of flow of the condensate, of the low-pressure preheater 10 and upstream of the feed water vessel 11 .
  • the flue gas which is at first unpressurized is isothermally compressed to a pressure of below 10 bar, for example 2 bar, and then conducted through the absorber 20 , wherein the scrubbing medium or solvent flows countercurrently thereto.
  • the CO 2 -rich scrubbing medium or solvent is thereafter, with flow through a heat exchanger 25 , introduced into the desorber/regenerator 22 .
  • the CO 2 -rich scrubbing medium is broken up and regenerated by heating, and so at the top end of the desorber/regenerator 22 a virtually pure CO 2 —H 2 O mixture exits which can be separated by a condensation process, and so then an approximately 90% pure CO 2 stream is released which is fed via a line 26 to a CO 2 compression system, which is ten-stage in the working example, to the CO 2 compression 27 , which compresses the CO 2 stream to approximately 100 bar and liquefies it. Thereafter the liquefied CO 2 is fed by way of a line 28 to further use or storage.
  • the CO 2 -rich scrubbing medium stream or solvent stream in the heat exchanger 25 is heated to approximately 95° C. This is achieved using low-CO 2 scrubbing medium or cleaning agent 29 which is likewise passed through the heat exchanger 25 and regenerated in the desorber/regenerator 22 and sufficiently heated/cooled in the evaporator/reboiler 23 .
  • the evaporator or reboiler 23 vaporizes a part of the solvent, as a result of which the carbon dioxide is desorbed from the scrubbing medium or solvent, in such a manner that at the top end a virtually pure CO 2 —H 2 O mixture forms which passes into the condenser 31 at the top of the desorber/regenerator 22 where the water condenses out, in such a manner that a virtually pure CO 2 stream is withdrawn.
  • the regenerated low-CO 2 scrubbing medium or solvent 29 is taken off at the bottom of the desorber/regenerator 22 , conducted via the heat exchanger 25 in which the countercurrently flowing, loaded, CO 2 -rich scrubbing medium stream or solvent stream 30 is heated.
  • the low-CO 2 scrubbing medium or solvent 29 is fed back to the absorber 20 . Since, during the entire process, losses of water and scrubbing medium result, these are added to the system again at a mixing point 32 .
  • a plant component is arranged in line 26 on the CO 2 scrubbing station desorber top or regenerator top of the desorber/regenerator 22 , which plant component is used as a heat source in the form of a heat exchanger 33 .
  • a condensate collection vessel 34 is arranged in the line 26 , using which, owing to the cooling of the CO 2 —H 2 O stream conducted in line 26 , as a consequence of the heat exchanger 33 , H 2 O which condenses out can be collected.
  • a further heat exchanger 35 likewise forming a plant component which is used as a heat source, serving for cooling the liquefied CO 2 stream is arranged in line 28 downstream of the CO 2 compression station 27 .
  • Further plant components utilized as heat sources in the form of heat exchangers 36 are provided as heat exchangers of the CO 2 scrubbing station absorber intercooler, wherein a heat exchanger 36 arranged at the top of the absorber 20 is also considered to belong to the CO 2 scrubbing station absorber intercooler. In total, in the working example, four heat exchangers 36 are present.
  • plant components used as heat sources are also arranged between the compressors 38 of the CO 2 compression station 27 in the form of heat exchangers 37 of the CO 2 compression intercooler.
  • heat exchangers 37 are shown between the compressors 38 , but in the case of the ten compressors 38 that are present, up to nine heat exchangers 37 of the CO 2 compression intercooler can be present. Since all these heat exchangers 33 , 35 , 36 and 37 serve for cooling, at the same time they form a heat source for the heat-carrier medium still otherwise conducted in each case in the heat exchangers 33 , 35 to 37 .
  • This function of the heat exchangers 33 , 35 to 37 as heat source is then utilized according to the invention for recovering a part of the energy taken off via the tapped-off steam line D 1 from the water-steam circuit of the power plant 1 and to feed it back to the power plant 1 , in particular to the water-steam circuit or other regions or plant parts which are connected to the power plant 1 .
  • heat exchangers WT 1 -WT 11 positioned at the corresponding points which, as will be explained hereinafter, each form a plant component utilized as a heat sink, using which in each case thermal energy may be transferred to a heat substream.
  • thermal energy is decoupled from the heat stream of the decarbonization system 19 , transferred to the heat-carrier medium flowing in the heat exchangers 33 , 35 to 37 and thereafter, by release from this heat-carrier medium using the heat exchangers WT 1 -WT 11 forming heat sinks for the heat-carrier medium, is fed back as thermal energy into the heat stream of the power plant system at another point.
  • decoupling or extraction of thermal energy proceeds from the heat stream of the CO 2 scrubbing station 58 with associated regenerator 22 and associated CO 2 compression 27 by means of the heat exchangers 33 and 35 .
  • the heat exchanger 33 acting as a heat source is connected in the flow via the line 39 and in the return via the line 40 to the heat exchanger WT 1 of the low-pressure preheater that is arranged in the bypass line 15 acting and used as heat sink.
  • a heat-carrier medium circulates which takes up thermal energy in the heat exchanger 33 and releases it in the heat exchanger WT 1 to the condensate flowing in the bypass line 15 and thus feeds it back into the actual heat stream of the power plant 1 .
  • the heat exchanger 35 acting as a heat source is connected via a line 41 to the heat exchanger WT 2 arranged in the bypass line 15 that is acting and utilized as a heat sink.
  • the return of the heat exchanger WT 2 of the low-pressure preheater is connected via a line 42 to the heat exchanger WT 5 arranged in the condensate line 14 and likewise forming a heat sink.
  • the return of the heat exchanger WT 5 is connected via a line 43 again to the heat exchanger 35 .
  • a heat-carrier medium circulates in the lines 41 , 42 and 43 .
  • thermal energy is decoupled from the heat stream of the CO 2 scrubbing station 58 with associated desorber 22 and associated CO 2 compression 27 and fed back into the actual heat stream of the power plant 1 at two points, namely the plant components in the form of the heat exchangers WT 2 and WT 5 used as heat sinks.
  • one plant component in the present example the heat exchangers 35 and WT 2 combined to form one unit and the heat exchangers 33 and WT 1 combined to form one unit are present, which in the region of the CO 2 scrubbing station with associated CO 2 compression are both used as heat source and effect the decoupling or extraction of thermal energy and are used as heat sink in the region of the power plant 1 and effect the feeding back of the thermal energy extracted or decoupled in the region of the CO 2 scrubbing station with associated CO 2 compression.
  • the liquid CO 2 stream transported in the line 28 is at a temperature of approximately 185° C., wherein the heat exchanger 35 serves as heat source for the heat-carrier medium conveyed in the lines 41 , 42 and 43 which gives off the thermal energy taken up to the cool condensate at approximately 18° C.
  • the return of the heat exchanger WT 2 leading to the heat exchanger WT 5 then still has a temperature high enough that the heat exchanger WT 5 likewise can, and according to the working example also is, used as a heat source for the heat retransfer into the condensate flowing in the line 14 , wherein the heat exchanger WT 5 in the context of the invention, however, forms a heat sink for the thermal energy obtained in the region of the CO 2 scrubbing station.
  • a further heat exchanger 24 is provided on the reboiler or evaporator 23 of the desorber/regenerator 22 .
  • This heat exchanger 24 forms a heat sink, in the meaning of the terminology used here, using which thermal energy is fed back into the heat stream of the CO 2 scrubbing station with associated CO 2 compression.
  • tapped steam D 1 taken off from the water-steam circuit is used for heating the low-CO 2 scrubbing medium or solvent 29 , wherein the return S 1 of the heat exchanger 24 opens out into the condensate line 14 upstream of the feed water vessel 11 and there condensate returns into the condensate line 14 at a temperature of approximately 120° C.
  • This return point forms a heat source for the condensate flowing in the condensate line 14 .
  • the temperature of the CO 2 -containing gas conducted in the line 26 is high enough that a temperature of 95° C. can be set in the circuit conducted between the heat exchanger 33 and the heat exchanger WT 1 in the flow of the heat exchanger 33 via the line 26 .
  • FIG. 2 shows schematically a power plant 1 which is likewise formed with a CO 2 scrubbing station which is not shown in FIG. 2 with associated CO 2 compression as in the working example according to FIG. 1 .
  • the same reference signs are used for identical and equal parts, elements and components.
  • a district heating circuit 44 is associated with the power plant 1 , the heat requirement of which district heating circuit is substantially fed by the steam lines 45 a - 45 d from the water-steam circuit of the power plant 1 .
  • heat exchangers WT 3 and WT 4 are provided that are used in the district heating circuit 44 as heat sinks.
  • thermal energy is fed back into the district heating circuit 44 , which thermal energy was likewise produced at the heat exchangers 33 and 35 used as heat source of the CO 2 scrubbing station with associated CO 2 compression 27 by decoupling or extraction there from the heat stream of the CO 2 scrubbing station.
  • the lines 39 , 40 and 41 , 43 connecting the heat exchangers WT 4 and WT 3 to the heat exchangers 33 and 35 can be seen in FIG. 2 .
  • the heat exchanger WT 4 is arranged in a bypass line 48 bridging the entire preheating and heating section from a condensate pump 46 to a district heating takeoff point 47
  • the heat exchanger WT 3 is arranged in a bypass line 49 between condensate pump 46 and district heating takeoff point 47 only bridging the first half of the preheating and heating section of the district heating circuit 44 .
  • the interconnection or pipework is such that the heat exchanger 35 downstream of the CO 2 compression station 27 is heat-energy-conductingly connected in the flow thereof to the heat exchanger WT 2 via the line 41 as known from the working example according to FIG.
  • the heat exchanger WT 1 is arranged and heat-energy-conductingly connected to the flow line 39 of the heat exchanger 33 at the CO 2 scrubbing station desorber top or regenerator top.
  • the return of the heat exchanger WT 1 is connected to the return line 40 of the heat exchanger 33 .
  • a line 52 branches off which leads to the heat exchanger WT 3 in the district heating circuit 44 , wherein on the return side the heat exchanger WT 3 is connected via a line 53 to the return line 40 .
  • thermal energy which is obtained by decoupling using the plant components used as a heat source in the form of heat exchangers 33 and 35 from the heat stream of the CO 2 scrubbing station with associated CO 2 compression not only to be introduced into the heat stream of the power plant 1 in the region of the low-pressure preheater 10 via the heat exchangers WT 1 , WT 2 and WT 5 , but also to perform in the region of the district heating circuit 44 using the plant components formed there as heat sinks in the form of heat exchangers WT 3 and WT 4 .
  • the interconnection can be made in various ways.
  • a temperature of 46° C. at 13 bar is achieved, and in the region of the opening out of the bypass line 48 into the district heating circuit 44 a temperature of 136° C. at approximately 14 bar is set. It is natural, depending on the desired arrangement or use of one or more heat exchangers WT 1 , WT 2 , WT 3 , WT 4 and/or WT 5 , to provide in each case only the feed lines or interconnections of lines which are necessary for the desired operation.
  • FIG. 3 shows, in an extract, a further alternative embodiment which is substantially identical to the embodiment shown in FIG. 2 with the sole difference that the reboiler or evaporator 23 is now no longer fed with the steam D 1 from the water-steam circuit, and its return S 1 fed to the condensate line 14 . Rather, the reboiler 23 is now integrated into the district heating circuit 44 , in such a manner that the thermal energy necessary for CO 2 expulsion is provided from the district heating circuit 44 using the tapped-off steam lines 45 a - 45 d and also the heat exchangers WT 3 and WT 4 arranged and interconnected therein as in the working example according to FIG. 2 .
  • the same reference signs are again provided for the same or identical parts or elements to the working examples of the preceding FIGS. 1 and 2 .
  • FIG. 4 shows a working example in which the plant components formed as a heat sink in the form of heat exchangers WT 6 and WT 7 are the only plant components arranged in the district heating circuit 44 for warming/heating up the district heating circuit 44 . Therefore, there are no steam feeds 45 a - 45 d present, as are present in the working example according to FIG. 3 and the working example according to FIG. 2 . Also, the further heat exchangers WT 3 and WT 4 that are present in the other working examples are no longer present in the district heating circuit 44 . In this working example, it is provided that all of the thermal energy decoupled in the region of the CO 2 scrubbing station with associated CO 2 compression 27 is entirely and completely fed to the district heating circuit 44 .
  • the heat exchanger WT 6 is connected to the heat exchanger 33 at the CO 2 scrubbing station desorber or regenerator top, which is indicated by the lines 39 and 40 .
  • the heat exchanger WT 7 is connected to the heat exchanger 35 downstream of the CO 2 compression 27 , which is indicated by the lines 41 and 43 .
  • a heat-carrier medium separately present in each case is continuously recirculated in a circuit formed by the lines 41 and 43 between the heat exchangers 35 and WT 7 , and also a circuit formed by the lines 39 and 40 between the heat exchangers 33 and WT 6 .
  • the heating circuit for the reboiler or evaporator 33 with flow D 2 ′ and return S 2 ′ can be integrated into the district heating circuit 44 .
  • a heat exchanger WT 5 is arranged and formed downstream of the condensate pump and upstream of the low-pressure preheater 10 , there is also the possibility to dispense with such and to feed back the recovered thermal energy solely via at least one or more of the heat exchangers WT 1 and/or WT 2 and/or WT 3 and/or WT 4 .
  • the further heat exchangers 36 of the CO 2 scrubbing station absorber intercooler and/or the heat exchangers 37 of the CO 2 compression intercooler can also form plant components used as heat source in the form of heat exchangers for heat transfer which then are used to interact with one of the plant components WT 1 -WT 7 formed as a heat sink and also the plant components described hereinafter in the form of heat exchangers WT 8 -WT 11 .
  • the feed from the district heating circuit 44 forms the flow or the evaporator heating D 2 ′ and the return S 2 ′ forms the return of the evaporator 23 into the district heating circuit 44 .
  • the thermal energy extracted from the heat exchangers 33 and 35 can also be fed into the air preheater or fresh air heater of the fresh air feed to the boiler 2 of the power plant 1 or for coal drying in the coal stream fed to a mill 54 , as the further working examples according to FIG. 5 and FIG. 6 show schematically.
  • FIG. 5 shows a coal feed line 55 leading to the coal mill 54 , in the course of which two heat exchangers WT 8 and WT 9 formed as heat sinks are arranged, wherein the heat exchanger WT 8 is connected to at least one of the heat exchangers 36 and/or 37 and the heat exchanger WT 9 is connected to at least one of the heat exchangers 33 and/or 35 , wherein, in particular, in turn, a heat-carrier medium is circulated through the lines 39 , 40 and/or 41 , 43 .
  • the coal that is fed can be, in particular, brown coal.
  • the heat exchangers WT 8 and WT 9 are preferably constructed in the form of drum dryers in which the coal stream and the heat-carrier medium stream fed in each case through the lines 39 and 40 are conducted countercurrently separately from one another. As indicated by the dotted line to the heat exchanger WT, still more (or fewer, however) than the two heat exchangers WT 8 and WT 9 can be arranged in the line 55 .
  • FIG. 6 shows a working example in which heat exchangers WT 10 and WT 11 are arranged as heat sinks in a fresh air feed (supply) line 56 upstream of the air preheater 57 .
  • the heat exchanger WT 10 is in turn connected via lines 39 , 40 to the heat exchanger 33 and the heat exchanger WT 11 is connected via lines 41 , 43 to the heat exchanger 35 , wherein in the lines 39 / 40 and 41 / 43 , in turn a separate heat-carrier medium is circulated.
  • more or fewer heat exchangers WT can be arranged in the line 56 .
  • the heat exchangers 33 and 35 are designed in such a manner that at the heat exchanger WT 1 and the heat exchanger WT 3 a flow temperature of the supplied heat-carrier medium of 95° C. is set and a return temperature of the recirculated heat-carrier medium of approximately 50-60° C. is set.
  • the same temperature level of flow and return is set in the heat carriers WT 6 , WT 8 and WT 10 .
  • the temperature management at the heat exchanger 35 is designed in such a manner that, there, a temperature of 185° C. is set as flow of the departing heat-carrier medium stream.
  • FIG. 7 shows a power plant additionally equipped with further recovered energy streams which do not solely consist of energy streams recovered from the region of the CO 2 scrubbing station which are then recirculated to the water-steam circuit.
  • a heat exchanger WT 12 is provided through which the return S 1 flows from the reboiler 23 or the heat exchanger 24 arranged there, wherein the return S 1 then opens out into the condensate line 14 in the direction of flow of the condensate upstream of the feed water vessel 11 .
  • condensate branched off from the condensate line 14 flows through the heat exchanger WT 12 in countercurrent to the reboiler return S 1 , which condensate is fed to a further heat exchanger WT 13 arranged in a bypass flue gas line 59 of the air preheater 57 .
  • the condensate heated by hot flue gas in heat exchanger WT 13 flows from there back into the condensate line 14 , in the direction of flow of the condensate, upstream of the last heat exchanger in the direction of flow of the condensate of the low-pressure preheater 10 .
  • a further heat exchanger 14 is arranged, through which condensate likewise flows in countercurrent to the flue gas conducted in the bypass flue gas line 59 , which condensate is branched off from the condensate line 14 downstream of the feed water vessel 11 and upstream of the high-pressure heater 13 , in the direction of flow of the condensate.
  • the condensate is recirculated back into the condensate line 14 downstream, in the direction of flow of the condensate, of the last heat exchanger of the high-pressure preheater 13 .
  • FIG. 7 also shows the heat exchanger WT 10 arranged in the fresh air line 56 , which heat exchanger WT 10 is connected upstream of the air preheater 57 .
  • the condensate conducted through the heat exchanger WT 14 can also open out into the condensate line 14 , in the direction of flow of the condensate, downstream of the first heat exchanger of the high-pressure preheater 13 .
  • FIG. 8 shows a similar embodiment in connection with feeding heat into an associated district heating circuit 44 in a development of the working example according to FIG. 2 .
  • a heat exchanger WT 15 fed from the return S 1 of the reboiler 23 is present, after a passage through which the return liquid of the return S 1 opens out into the condensate line 14 .
  • condensate is conducted through the heat exchanger WT 15 from the condensate line 14 in a line branching off, in the direction of flow of the condensate, upstream of the last heat exchanger of the low-pressure preheater 10 through the heat exchanger WT 15 opening out again into the condensate line 14 likewise in turn, in the direction of flow of the condensate 14 , upstream of the last heat exchanger of the low-pressure preheater 10 .
  • a heat exchanger WT 16 is arranged through which likewise flows return S 1 of the reboiler 23 .
  • fluid conducted through the heat exchanger WT 16 in the district heating circuit 44 is conducted through the heat exchanger WT 16 .
  • a line 60 branches off from the district heating circuit 44 , which line 60 leads to a further heat exchanger WT 17 through which flows flue gas conducted in the bypass line 59 countercurrently to the fluid branched off from the heating circuit 44 .
  • the heat exchanger WT 17 is connected to the district heating circuit 44 .
  • a reboiler takeoff in the district heating circuit 44 , can be provided with flow D′ 2 and return S′ 2 with branching off from and recirculation to the district heating circuit 44 , as shown in FIG. 3 .
  • the feed D 1 to the reboiler 23 and the return S 1 from the reboiler 23 with the heat exchangers WT 15 and WT 16 integrated therein are then omitted, such as are still present in the working example according to FIG. 8 .
  • the arrangement of a heat exchanger WT 13 and/or WT 14 and/or WT 17 in the bypass flue gas line 59 through which flue gas flows has the advantage that, for maintaining the flue gas stream, no additional fan is necessary, since flow passes through the bypass flue gas line 59 in the direction of the general flue gas flow direction.
  • this has the disadvantage that the respective heat exchanger WT 13 , WT 14 , WT 17 comes into contact with dirty flue gas, for which reason the respective heat exchanger must be fabricated from high-quality steel.
  • the risk of forming ammonium bisulfate exists, which precipitates onto the heat exchanger surfaces.
  • FIG. 6 additionally shows, it is also possible to provide on the air side a return line 62 in which a further heat exchanger WT 18 is arranged which is then pipeline-connected to the condensate line 14 in the region of the low-pressure preheater 10 or the high-pressure preheater 13 .
  • the return line 62 in the direction of flow of the fresh air, branches off from the air supply line 56 downstream of the air preheater 57 and opens out again into the fresh air line 56 in the direction of flow of air upstream of the heat displacement system 63 .
  • the bypass flue gas line 59 on the flue gas side branches off from the flue gas line 17 in the direction of flow of flue gas upstream of the air preheater 57 and opens out again into the flue gas line 17 in the direction of flow of flue gas downstream of the air preheater 57 and upstream of the heat displacement system 63 .
  • a fan 64 is arranged in order to be able to move the fresh air recirculated therein against the general direction of flow of the fresh air in the line 56 .
  • the heat-carrier medium circuit 65 On the flow section to the heat exchanger 24 , in the heat-carrier medium circuit 65 , three heat exchangers 66 , 67 and 68 are arranged which are heated with supplied steam, more precisely, for example, fresh steam to the heat exchanger 66 , medium-pressure steam to the heat exchanger 67 and low-pressure steam to the heat exchanger 68 , wherein the steam is taken off from the water-steam circuit of a power plant 1 according to the designation D 1 .
  • This indirect (warm water) heating of the reboiler 23 by way of the heat-carrier medium circuit 65 reduces the risk, compared with direct and immediate steam heating, that the feed water is contaminated with the chemical absorption medium 29 due to possible leaks in the reboiler heat exchanger 24 .
  • a Rankine cycle can also be supplied with low-temperature heat from the CO 2 scrubbing station/CO 2 compression 58 / 27 , as FIG. 10 shows.
  • two heat exchangers WT 19 and WT 20 are arranged in a Rankine cycle 69 , in particular in an organic Rankine cycle.
  • a circuit is operated in which low-temperature waste heat from the CO 2 scrubbing station 58 /CO 2 compression 27 is used.
  • the heat exchanger WT 19 is arranged in the “cold step” of the Rankine cycle 69 and waste heat is fed thereto from the absorber intercooler 36 or the CO 2 compression intercooler 37 .
  • waste heat which is not required in the CO 2 scrubbing station from the desorber top, i.e. thermal energy obtained via the heat exchanger 33 , or thermal energy from the CO 2 compression, i.e. thermal energy produced via the heat exchanger 35 , is fed to the Rankine cycle 69 .
  • the consumer 75 associated with the turbine step of the Rankine cycle 69 can be a generator for power generation, or else a mechanical drive of a feed pump or of a CO 2 compressor. Even if in the working example according to FIG. 10 , both a heat exchanger WT 19 and a heat exchanger WT 20 are provided, it is also possible, depending on the design of the power plant, to provide only one of the two heat exchangers WT 19 or WT 20 .
  • FIGS. 11 and 12 show the use of a heat exchanger WT 21 which, on the flue gas side, takes up thermal energy from the flue gas flowing through the bypass flue gas line 59 , wherein the bypass flue gas line 59 is a plant component utilized as heat source.
  • the heat exchanger WT 21 releases the absorbed heat to the flow D 3 leading to the heat exchanger 24 of the reboiler 23 , wherein the heat-carrier medium is recirculated to the heat exchanger WT 21 from the heat exchanger 24 via the reboiler return S 3 .
  • the heat exchanger WT 21 is designed as a plant component fed on the flue gas side and used as a heat source, and then the heat exchanger 24 associated with the reboiler 23 is a plant component used as a heat sink.
  • the working example according to FIG. 12 differs from the working example according to FIG. 11 only in that here a heat exchanger WT 11 fed from the heat exchangers 37 of the intercooler of the compressor 27 is arranged in the fresh air line 56 upstream, in the direction of flow of the air, of the heat displacement system 63 , which heat exchanger WT 11 therefore represents as plant component a heat sink fed from the CO 2 compression 27 .
  • FIG. 11 shows a flue gas line 17 which, in the direction of flow of the flue gas, leads downstream of a denitration system 70 to the air preheater 57 and thereafter to an electrostatic precipitator 71 .
  • the bypass flue gas line 59 that branches off from the flue gas line 17 and opens out again into it bypasses the air preheater 57 , but opens out again into the flue gas line 17 upstream of the electrostatic precipitator 71 .
  • a heat displacement system 63 is arranged in the flue gas line 17 , in which heat displacement system are arranged two heat exchangers 73 and 74 that are connected to one another via a circulated heat-carrier medium, of which heat exchangers, thermal energy is taken off from the flue gas stream conducted in the line 17 by the heat exchanger 73 , and given off to the heat-carrier medium circulated in the heat displacement system 63 .
  • Downstream of the heat displacement system 63 is then, in addition, a further flue gas desulfurization system 72 which is then followed by the CO 2 scrubbing station 58 comprising the absorber 20 with associated desorber 22 for CO 2 separation, before the low-CO 2 exhaust gas 21 then leaves the plant.
  • the fresh air line 56 is provided, which, in the direction of flow of fresh air, upstream of the air preheater 57 , is first passed through the heat displacement system 63 and there, in the heat exchanger 74 , takes up the thermal energy given off by the flue gas via the heat exchanger 74 to the heat carrier medium circulated in the heat displacement system 63 .
  • the low-temperature heat present upstream of the flue gas desulfurization system 72 is transferred to the fresh air stream upstream, in the direction of flow of fresh air, of the air preheater 57 .
  • the fresh air stream that is preheated thereby, in the air preheater 57 then requires only a relatively small heat energy supply, in order to have the temperature envisaged downstream of the air preheater 57 in the direction of flow. This is used for passing the amount of heat which, although it is present in the flue gas, is then no longer required for heating the fresh air in the air preheater 57 , via the bypass flue gas line 59 and there, in the heat exchanger WT 18 , to transfer it to the heat-carrier medium ZM passed therein and as flow D 3 to the heat exchanger 24 of the reboiler 23 .
  • a further 12 MW may be obtained, in the embodiment according to FIG. 12 , by the heat exchanger WT 11 fed from the intercooler 37 of the CO 2 compression 27 being heated to a temperature of below 60° C. such that the heat displacement system 63 can develop undiminished its complete intended action, but nevertheless the fresh air in this case is already preheated, in such a manner that in the air preheater 57 , less thermal energy only need be taken off from the flue gas, in such a manner that an increased amount of thermal energy is available in the bypass flue gas line 59 . In this manner 72 MW th can be obtained in the heat exchanger WT 18 .
  • the heat exchanger 33 , the line 26 , the heat exchanger 35 , the line 28 , the heat exchanger 36 and the heat exchanger 37 are formed as plant components utilized as a heat source and are arranged in a power plant, wherein these heat sources are fed with thermal energy present in the region of the CO 2 scrubbing station 58 with associated CO 2 compression 27 or thermal energy which is produced there.
  • Plant components used as heat sinks which release again thermal energy fed in from the existing heat sources, that is to say from the region of the CO 2 scrubbing station 58 with associated CO 2 compression 27 are the heat exchangers WT 1 -WT 12 , and also the heat exchangers WT 15 and WT 16 .
  • the heat exchangers WT 1 , WT 2 , WT 5 , WT 12 and WT 15 feed the thermal energy obtained from the CO 2 scrubbing station 58 with associated CO 2 compression 27 into the steam-water circuit of the power plant 1 .
  • the heat exchangers WT 3 , WT 4 , WT 6 , WT 7 and WT 16 feed the thermal energy obtained into the district heating circuit 44 .
  • the heat exchangers WT 8 and WT 9 feed the thermal energy obtained or taken up into the coal line 55 leading to the coal mill 54 .
  • the heat exchangers WT 10 and WT 11 feed the thermal energy obtained or taken up into the fresh air line 56 .
  • the heat exchangers WT 19 and WT 20 that are likewise fed with thermal energy from the CO 2 scrubbing station 58 with associated CO 2 compression 27 release the thermal energy taken up to the Rankine cycle 69 in their function as heat sink.
  • Plant components taking up flue gas thermal energy from the flue gas side, i.e. conducted in the bypass flue gas line 59 that have the function of a heat source are, in addition, the heat exchangers WT 13 , WT 14 , WT 17 and WT 21 , wherein the heat exchangers WT 13 and WT 14 feed in the thermal energy taken up into the plant component of the water-steam circuit of the power plant 1 , to this extent forming a heat sink, and the heat exchanger WT 17 gives off the thermal energy taken up into the district heating circuit 44 as the plant component forming the associated heat sink.
  • the heat exchanger WT 21 gives off the heat taken up to the flow D 3 to the heat exchanger 24 of the reboiler 23 , in such a manner that the heat exchanger 24 likewise develops the function of a plant component having a function as a heat sink giving off thermal energy to the CO 2 scrubbing station.
  • the heat exchanger WT 18 forms a heat source fed immediately by the thermal energy of the fresh air leaving the air preheater 57 , but thereby indirectly a heat source fed by thermal energy from the region of the CO 2 scrubbing station 58 and/or CO 2 compression 27 , since heat taken off from the region of the CO 2 scrubbing station 58 and/or CO 2 compression 27 is fed back or fed into the fresh air via the heat exchangers WT 10 and/or WT 11 upstream of the return line 62 , in the direction of flow of the air.
  • the heat source WT 18 releases the heat taken up to the condensate line 14 acting as a heat sink in the region of the low-pressure preheater and/or the high-pressure preheater 10 and/or 13 at the water-steam circuit of the power plant 1 .
  • the present invention relates to a method for the “optimal” integration of heat streams into a conventional power plant process.
  • the conventional power plant process can be all known fossil-fired power plant processes. In particular, it is a hard-coal-fired power plant process in the net output range between 500 and 1000 MW el . In the working example, it is a hard-coal-fired power plant process having a net output of approximately 850 MW el .
  • the heat streams that are to be integrated can be in a temperature range between 50 and 400° C. In particular, the heat energies to be integrated are in a temperature range between 50 and 200° C.
  • the source of the heat streams can be systems for obtaining solar heating or geothermal energy or can be systems which are in direct link to said conventional power plant process.
  • the systems which are in a direct link to said conventional power plant process can be waste heat streams which originate from a fuel drying system.
  • the waste heat streams can originate from a chemical CO 2 scrubbing station having an absorber and desorber system and subsequent compression of the separated carbon dioxide connected downstream of the power plant process.
  • a conventional hard-coal-fired power plant block having a net output of 850 MW el is assumed.
  • This hard-coal-fired power plant block has a gross electrical efficiency of 47.83% and a net electrical efficiency of 45.25%.
  • the in-house electrical consumption is approximately 40 MW el , with the feed pump being electrically driven.
  • the power plant block without recirculation of the waste heat, has a gross electrical efficiency of 32.42% and a net electrical efficiency of 32.86% at an in-house electrical consumption of 93 MW thermal.
  • the power plant block optionally offers the possibility of extracting district heat 44 .
  • the preheating section of the water/steam circuit consists of five low-pressure preheaters 10 and three high-pressure preheaters 13 .
  • the temperatures of the fuel, the fresh air and the cooling water are assumed to be 15° C.
  • a heat stream of at least 510 MW th is required at a temperature level between 120 and 170° C.
  • the specific total energy requirement for the CO 2 scrubbing station in an absorber and desorber system is 3600 kJ (kg of CO 2 ).
  • the required process heat for the chemical CO 2 scrubbing station is taken off from the power plant process in a suitable manner D 1 via a collector system between the various turbine stages 3, 4, 5. It is of importance in the takeoff of process steam from the water/steam circuit that the pressure differences of the subsequent turbine stages remain in the material-specific limits. It is the purpose of the present invention to minimize the loss of efficiency of the overall process which is caused by the high demand of thermal energy in the chemical CO 2 scrubbing station.
  • additional heat exchangers are installed in the water-steam circuit of the conventional power plant, in which heat exchangers, at a suitable point and at a suitable temperature level, waste heat from the CO 2 scrubbing station system and the CO 2 compression is recirculated and therefore an improved efficiency for the overall system is achieved.
  • a further purpose is to keep as low as possible the demand for cooling water which is increased by the chemical CO 2 scrubbing station/compression 58 / 27 . That is to say, the more heat can be recirculated from the CO 2 scrubbing station/compression 58 / 27 to the conventional water-steam circuit, the less additional cooling capacity (cooling tower capacity) need be installed.
  • the CO 2 scrubbing station is an absorber 20 and desorber 22 system in which the CO 2 is separated off from the flue gas stream by chemical absorption.
  • chemical absorption owing to the chemical reaction, heat is liberated which is removed by intercoolers 26 to achieve a better degree of conversion.
  • the loaded scrubbing medium then arrives in the desorption column 22 in which the energy is fed via a reboiler 23 which is required for breaking the chemical bond between the scrubbing medium and the CO 2 .
  • the water loading of the CO 2 that is liberated again at the desorber top owing to the higher temperature, is higher than that of the flue gas treated in the absorber 20 , and so for this purpose likewise energy must be supplied.
  • the compressed CO 2 stream has a temperature of about 190° C. This temperature is too high for further processing of the CO 2 , and so further cooling 35 is necessary. Then, the CO 2 is at approximately 25° C./200 bar and in the liquid state.
  • Plant components that are usable as “heat source” are:
  • WT 1 transfers heat from a substream 33 of the desorber top heat to the LP preheating section 10 .
  • approximately 50% (100% at 200 MW district heat extraction) of the incoming condensate is warmed from 20 (29° C. at 200 MW district heat extraction) to 100° C.
  • approximately 32 MW (approximately 60 MW at 200 MW district heat extraction) are transferred to the water-steam circuit.
  • the increase in efficiency via this heat exchanger WT 1 is 0.38% point (0.79% point for 200 MW district heat extraction).
  • WT 2 transfers heat 25 from the last stage of the CO 2 compression to the LP preheating section 10 .
  • approximately 50% of the incoming condensate is heated from 20 to 120° C.
  • approximately 49 MW are transferred to the water-steam circuit.
  • the increase in efficiency due to this heat exchanger WT 2 is 1.19% points.
  • This heat exchanger is alternatively used for WT 4 which is only used when district heat 44 is extracted.
  • WT 3 transfers heat 33 from a substream of the desorber top heat to the district heating circuit 44 .
  • approximately 60% of the district heating return is heated from 46° C. to 100° C.
  • approximately 80 MW are transferred to the district heating circuit 44 .
  • the increase in efficiency due to this heat exchanger WT 3 is 1.70% points.
  • WT 4 transfers heat 35 from the last stage of the CO 2 compression 27 to the district heating circuit 44 .
  • approximately 20% of the district heating return is heated from 46° C. to 136° C.
  • approximately 40 MW are transferred to the district heating circuit 44 .
  • the increase in efficiency due to this heat exchanger WT 4 is 1.36% points.
  • This heat exchanger is alternatively used for WT 2 which is only used when no district heat is extracted.
  • the heat exchanger WT 5 transfers heat 35 from the last stage of the CO 2 compression 27 to the LP preheating section 10 .
  • the heat exchanger WT 5 is not fed directly from the CO 2 compression, but preferably from the return from WT 4 .
  • the heat exchanger WT 5 is therefore, preferably, only used when the heat exchanger WT 4 is operating, that is to say when district heat is extracted.
  • the reason for this is that the return from WT 4 is, at approximately 50° C., markedly higher than that from WT 2 at 25° C., and therefore is still suitable both for further cooling the compressed CO 2 stream and also for heating up 100% of the condensate from 20 to 30° C. In this case approximately 10 MW are transferred to the condensate upstream of the LP preheaters.
  • the increase in efficiency due to this heat exchanger is 0.36% point.
  • WT 6 transfers heat 33 from a substream of the desorber top heat to the district heating circuit 44 .
  • a district heat generation is considered which is exclusively fed with waste heat from the CO 2 scrubbing station/compression 58 / 27 . In this process approximately 30 MW are transferred to the district heating circuit 44 .
  • WT 7 transfers heat 35 from the last stage of the CO 2 compression 27 to the district heating circuit 44 .
  • a district heat generation is considered which is exclusively fed with waste heat from the CO 2 scrubbing station/compression 58 / 27 . In this process approximately 20 MW are transferred to the district heating circuit.
  • WT 10 transfers heat 33 from a substream of the desorber top heat to the fresh air 50 .
  • approximately 57 MW of heat are transferred to the fresh air which enters at a mass flow rate of approximately 640 kg/s at 15° C. and exits at 100° C.
  • the increase in efficiency due to this heat exchanger is 1.22% points (1.16% points at 200 MW district heat extraction).
  • the heat exchanger WT 11 can be operated in two ways: a) by way of waste heat ( 36 ) from the absorber inter-cooler, or b) by way of the compression intercooler 37 . In both ways, WT 11 is used with a flow temperature of approximately 60° C. This heat exchanger WT 11 can be used if only a small substream of the flue gas is treated in the CO 2 scrubbing station/compression 58 / 27 . The recyclable amount of heat from the CO 2 scrubbing station/compression 58 / 27 is thereby lower, and so waste heat from the absorber intercooler 36 or the compression intercooler 37 needs to be used in WT 11 .
  • WT 14 is operated using an air preheater bypass 59 .
  • This heat exchanger WT 14 can be used, since, owing to WT 10 , the fresh air enters the air preheater 57 approximately 85° C. hotter.
  • the air preheater exit temperature of the fresh air is, however, limited to 340° C., and so here, by the air preheater bypass 59 , heat at a higher temperature level must be taken off.
  • this heat exchanger WT 14 approximately 150 kg/s of flue gas is cooled from 380° C. to 170° C.
  • approximately 200 kg/s of water can be heated from 160° C. to 205° C.
  • This mass flow rate of water is used for bridging the first HP preheater of the high-pressure heater 13 .
  • This heat exchanger WT 14 approximately 40 MW are transferred.
  • the increase in efficiency due to this heat exchanger WT 14 is 1.3% points (likewise at 200 MW of district heat also).
  • the heat exchanger WT 16 transfers heat 35 from the reboiler return S 1 to the district heating circuit 44 .
  • the entire district heating mass stream is heated from 95° C. to 105° C.
  • the reboiler return S 1 is cooled in this process from approximately 120° C. to 100° C. Approximately 20 MW of heat are transferred in this case.
  • the heat exchanger is used between the third and fourth heat exchanger of the district heating circuit 44 having in each case four heat exchangers in the working example of FIGS. 2 , 3 , 7 and 8 , and considerably reduces the requirement of cold intermediate superheated steam.
  • the increase in efficiency due to the heat exchanger WT 16 is 0.90% point.
  • the heat exchangers WT 12 and WT 15 transfer heat from the reboiler return S 1 to the LP preheating section.
  • the entire mass stream heated in WT 1 to 100° C. is heated to 116° C.
  • the reboiler return is cooled in this process from approximately 120° C. to 110° C. In this case approximately 8 MW of heat are transferred.
  • These heat exchangers WT 12 and WT 15 are used both between the fourth and fifth heat exchangers of the LP preheating section of the low-pressure preheater 10 having in each case five heat exchangers in the working examples of FIGS. 1 , 2 , 7 and 8 , and reduce the requirement for MP steam.
  • the increase in efficiency due to this heat exchanger is 0.4% point.
  • WT 9 transfers heat from: a) a substream of the desorber top heat 33 and b) the last stage of the CO 2 compression 35 , to the fuel in order to preheat it starting from 15° C.
  • the heat exchanger WT 8 can be operated in two ways: a) by way of waste heat from the absorber intercooler 36 or b) by way of the compression intercooler 37 . In both ways, WT 8 is used at a flow temperature of approximately 60° C.
  • the method according to the invention and/or the power plant 1 according to the invention can also be designed in such a manner that heat from solar-heating and/or geothermal heat sources WT 1 , WT 2 , WT 5 is used or is usable for low-pressure preheating, for heating a district heating circuit WT 3 , WT 4 associated with the power plant 1 and/or for fresh air preheating WT 10 , WT 11 with associated air preheater bypass 59 for a heat displacement in a heat stream in the region of the water-steam circuit of the power plant 1 , in particular in the low-pressure and/or high-pressure preheater, and/or a district heating circuit associated with a power plant 1 , preferably in combination with a CO 2 scrubbing station 58 .

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DE102009032537A DE102009032537A1 (de) 2009-07-10 2009-07-10 Kohlekraftwerk mit zugeordneter CO2-Wäsche und Wärmerückgewinnung
PCT/EP2010/059615 WO2011003892A2 (fr) 2009-07-10 2010-07-06 Centrale thermique au charbon avec lavage des fumées et récupération de chaleur

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US20110214427A1 (en) * 2010-03-04 2011-09-08 Xu Zhao Process for reducing coal consumption in coal fired power plant with steam piping drying
US20110232286A1 (en) * 2010-03-29 2011-09-29 Hitachi, Ltd. Boiler Apparatus
US20120132080A1 (en) * 2010-11-30 2012-05-31 Kia Motors Corporation Apparatus for regenerating a carbon dioxide absorption solution
US20120180657A1 (en) * 2009-09-02 2012-07-19 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for producing at least one gas having a low co2 content and at least one fluid having a high co2 content
US20130139509A1 (en) * 2011-12-06 2013-06-06 Nuovo Pignone S.P.A. Heat recovery in carbon dioxide compression and compression and liquefaction systems
US20130269631A1 (en) * 2010-12-21 2013-10-17 Inbicon A/S Steam Delivery System for Biomass Processing
US20130298559A1 (en) * 2011-11-03 2013-11-14 Alstom Technology, Ltd. Steam power plant with high-temperature heat reservoir
US20140202156A1 (en) * 2012-12-13 2014-07-24 Alstom Technology Ltd Steam power plant with an additional flexible solar system for the flexible integration of solar energy
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US20150330628A1 (en) * 2014-05-08 2015-11-19 Alstom Technology Ltd Oxy boiler power plant with a heat integrated air separation unit
CN105582794A (zh) * 2016-01-19 2016-05-18 河北工程大学 太阳能地热能co2朗肯循环辅助燃煤机组脱碳脱硝系统
JPWO2014038412A1 (ja) * 2012-09-06 2016-08-08 三菱重工業株式会社 熱回収システム及び熱回収方法
WO2018108561A1 (fr) * 2016-12-12 2018-06-21 Mitsubishi Hitachi Power Systems Europe Gmbh Procédé et dispositif de traitement de gaz de fumée de centrales thermiques à vapeur à combustibles fossiles au moyen d'un adsorbant
US10006634B2 (en) 2014-05-08 2018-06-26 General Electric Technology Gmbh Coal fired oxy plant with air separation unit including parallel coupled heat exchanger
JP2019081121A (ja) * 2017-10-27 2019-05-30 株式会社東芝 二酸化炭素分離回収システムおよび二酸化炭素分離回収システムの運転方法
US20220259989A1 (en) * 2019-07-03 2022-08-18 Ormat Technologies, Inc. Geothermal district heating power system

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8459030B2 (en) 2009-09-30 2013-06-11 General Electric Company Heat engine and method for operating the same
WO2012054049A1 (fr) * 2010-10-22 2012-04-26 General Electric Company Moteur thermique et son procédé de fonctionnement
JP5704937B2 (ja) * 2011-01-31 2015-04-22 三菱日立パワーシステムズ株式会社 二酸化炭素分離回収装置を備えた火力発電システム
CA2831818A1 (fr) * 2011-03-31 2012-10-04 Alstom Technology Ltd Systeme et procede pour commander une chaleur perdue pour la capture de co2
WO2012154313A1 (fr) * 2011-03-31 2012-11-15 Alstom Technology Ltd Système et procédé de régulation de chaleur résiduelle pour la capture de co2
WO2012163847A1 (fr) * 2011-05-27 2012-12-06 Evonik Industries Ag Verfahren und vorrichtung zur abtrennung von kohlendioxid aus gasströmen procédé et dispositif destinés à séparer du dioxyde de carbone contenu dans des flux de gaz
EP2551477A1 (fr) * 2011-07-29 2013-01-30 Siemens Aktiengesellschaft Procédé et centrale à énergie fossile destinée à la récupération d'un condensat
EP2559866B1 (fr) * 2011-08-18 2014-01-01 Alstom Technology Ltd Intégration de la chaleur d'une centrale électrique
JP5450540B2 (ja) * 2011-09-12 2014-03-26 株式会社日立製作所 Ｃｏ２回収装置を備えたボイラーの熱回収システム
DE102012208221A1 (de) * 2012-02-22 2013-08-22 Siemens Aktiengesellschaft Verfahren zum Nachrüsten eines Gasturbinenkraftwerks
US9157369B2 (en) * 2012-03-01 2015-10-13 Linde Aktiengesellschaft Waste heat utilization for energy efficient carbon capture
EP2644853B8 (fr) * 2012-03-29 2016-09-14 General Electric Technology GmbH Économie d'énergie et récupération de chaleur dans des systèmes de compression de dioxyde de carbone et système permettant de les mettre en oeuvre
FR3006911B1 (fr) * 2013-06-12 2019-12-27 IFP Energies Nouvelles Procede de captage de co2 avec production d'electricite
DE102014105067A1 (de) * 2014-04-09 2015-10-15 Mitsubishi Hitachi Power Systems Europe Gmbh Verfahren und Vorrichtung zur Flexibilisierung von mit kohlenstoffhaltigen Brennstoffen befeuerten Kraftwerken mittels der Produktion kohlenstoffhaltiger Energieträger

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5025631A (en) * 1990-07-16 1991-06-25 Garbo Paul W Cogeneration system with low NOx combustion of fuel gas
JP2792777B2 (ja) * 1992-01-17 1998-09-03 関西電力株式会社 燃焼排ガス中の炭酸ガスの除去方法
NO993704D0 (no) * 1999-03-26 1999-07-29 Christensen Process Consulting Fremgangsmåte for å kontrollere CO2 innholdet i en utslippsgass fra et brennkammer
WO2007073201A1 (fr) * 2005-12-21 2007-06-28 Norsk Hydro Asa Procede energetiquement efficace d’elimination et de sequestration de co2 dans un gaz d’echappement d’unites de traitement d’energie

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US20150330628A1 (en) * 2014-05-08 2015-11-19 Alstom Technology Ltd Oxy boiler power plant with a heat integrated air separation unit
KR101892334B1 (ko) 2014-05-08 2018-08-27 제네럴 일렉트릭 테크놀러지 게엠베하 열 통합을 갖는 석탄 연소 순산소 플랜트
US10203112B2 (en) * 2014-05-08 2019-02-12 General Electric Technology Gmbh Oxy boiler power plant oxygen feed system heat integration
CN105582794A (zh) * 2016-01-19 2016-05-18 河北工程大学 太阳能地热能co2朗肯循环辅助燃煤机组脱碳脱硝系统
WO2018108561A1 (fr) * 2016-12-12 2018-06-21 Mitsubishi Hitachi Power Systems Europe Gmbh Procédé et dispositif de traitement de gaz de fumée de centrales thermiques à vapeur à combustibles fossiles au moyen d'un adsorbant
AU2018217997B2 (en) * 2017-10-27 2019-10-24 Kabushiki Kaisha Toshiba Carbon dioxide capturing system and operation method of carbon dioxide capturing system
JP2019081121A (ja) * 2017-10-27 2019-05-30 株式会社東芝 二酸化炭素分離回収システムおよび二酸化炭素分離回収システムの運転方法
US20220259989A1 (en) * 2019-07-03 2022-08-18 Ormat Technologies, Inc. Geothermal district heating power system
US11905856B2 (en) * 2019-07-03 2024-02-20 Ormat Technologies, Inc. Geothermal district heating power system

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CA2767590A1 (fr) 2011-01-13

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