EP2452051A2 - Centrale thermique au charbon avec lavage des fumées et récupération de chaleur - Google Patents

Centrale thermique au charbon avec lavage des fumées et récupération de chaleur

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Publication number
EP2452051A2
EP2452051A2 EP10728683A EP10728683A EP2452051A2 EP 2452051 A2 EP2452051 A2 EP 2452051A2 EP 10728683 A EP10728683 A EP 10728683A EP 10728683 A EP10728683 A EP 10728683A EP 2452051 A2 EP2452051 A2 EP 2452051A2
Authority
EP
European Patent Office
Prior art keywords
heat
heat exchanger
power plant
compression
flue gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP10728683A
Other languages
German (de)
English (en)
Inventor
Brian Stoever
Dieter König
Christian Bergins
Martin SCHÖNWÄLDER
Torsten Buddenberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hitachi Power Europe GmbH
Original Assignee
Hitachi Power Europe GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hitachi Power Europe GmbH filed Critical Hitachi Power Europe GmbH
Publication of EP2452051A2 publication Critical patent/EP2452051A2/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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 to a method for heat recovery by connecting a plurality of heat flows of a fossil-fired, especially coal-fired, power plant with downstream CO 2 scrubbing of the flue gas by means of chemical absorption and / or desorption and associated C0 2 compression. Furthermore, the invention is directed to a power plant, in particular fossil-fueled and preferably coal-fired power plant, with a combustion downstream of the CO 2 scrubbing of the flue gas by means of chemical absorption and / or desorption and associated CC> 2 compression.
  • the principle of pre-combustion is based on conversion of the fossil fuel to a synthesis gas consisting of carbon monoxide and hydrogen, in a further step the carbon monoxide is oxidised to carbon dioxide (CO 2 ) and then removed from the process.
  • the integrated separation is realized in the so-called oxy-fuel process.
  • a highly concentrated carbon dioxide (CO 2 ) -Abgasstrom produced by the combustion of fossil fuel, especially coal, with pure oxygen instead of air, which can be disposed of directly after condensation of the water vapor without additional washing.
  • the post-combustion which is used in particular in conventional power plants, the carbon dioxide (CO2) is separated by means of a wash.
  • CO2 carbon dioxide
  • the flue gas at the end of the flue gas purification line by means of a CO 2 scrubbing by chemical absorption from the flue gas is largely removed, so that a C0 2 -armes exhaust gas leaves the power plant.
  • This C0 2 scrubbing takes place in an absorber, wherein the chemical absorption by means of a detergent, in particular monoethanolamine (MEA), but also diethanolamine (DEA) or methyldiethanolamine (MDEA), takes place.
  • MEA monoethanolamine
  • DEA diethanolamine
  • MDEA methyldiethanolamine
  • the desorber or regenerator exits a high CO 2 -containing exhaust gas, which is liquefied in a subsequent C0 2 compression and then removed from the area of the power plant for final storage or reuse.
  • the big advantage of this method is that existing conventional power plants can be retrofitted.
  • the disadvantage of this method results from the high energy consumption necessary for the CO 2 deposition.
  • a high energy requirement is required for the regeneration of the detergent used, which is usually covered in the form of steam drawn from the water-steam circuit of the associated power plant. With this tapped steam is a reboiler or evaporator of the Desorber or regenerator fed, by means of which the recirculated detergent is heated to the necessary for the expulsion of CO 2 temperature.
  • the invention has for its object to provide a solution that allows a thermally favorable integration of a CO 2 scrubbing of the flue gas with associated CO 2 compression in the total heat flow and / or the total heat energy balance of a fossil-fired, especially coal-fired, preferably conventional power plant.
  • this object is achieved in that decoupled from the heat flow of the CO 2 scrubbing with associated C0 2 compression thermal energy in the form of at least a partial heat flow and in a direct or indirect to the heat flow of the boiler or steam generator the power plant coupled heat flow is coupled again and / or that is coupled out of the flue gas heat flow thermal energy in the form of at least a partial heat flow and coupled into the heat flow of the CO 2 scrubbing with associated C0 2 compression again.
  • this can be realized in that in the CO 2 scrubbing with associated CO 2 - compression existing thermal energy by means of at least a usable as a heat source plant component as part of the heat flow from the heat flow of CO 2 scrubbing with associated C0 2 compression ent or decoupled and / or in the range of a flue gas line existing thermal energy by means of at least one usable there as a heat source system component from the heat flow of the flue gas is decoupled and decoupled and each recovered by the decoupling or decoupling in the form of at least one partial heat flow thermal energy in the area of the power plant outside the respective decoupling or decoupling by means of at least one usable there for the thermal energy recovered as a heat sink further plant component again in the heat flow. of the power plant is coupled.
  • the above object is achieved in a power plant of the type described in more detail by the fact that in the area of C0 2 laundry with associated C0 2 compression at least one used as a heat source and the decoupling or decoupling of thermal energy from the heat flow of the CO 2 ⁇ Laundry arranged with associated CO 2 compression causing system component and / or is formed and / or at least one used as a heat source and the decoupling or decoupling of thermal energy from the flue gas stream in the range of a flue gas line and / or an air preheater bypassing flue gas line arranging plant component is arranged and / or trained and in the area of the power plant at least one heat energy with this component component connected and used as a heat sink and the re-coupling of the decoupled or decoupled thermal energy in the heat flow of the power plant outside the respective n decoupling or decoupling causing, preferably further, plant component arranged and / or trained.
  • the method is further characterized by the fact that, in the CO 2
  • the invention provides that thermal energy present in the flue gas is decoupled or decoupled in the area of the flue-gas line and / or in the region of a bypass flue-gas line which bypasses an air preheater.
  • the 2 scrubbing with associated CO 2 in the CO - corresponds compression or decoupled thermal energy outside the area of CO 2 scrubbing with associated CO 2 - compression, in particular in the water-steam cycle and / or a district heating circuit and / or in a coal-carrying coal line and / or a fresh air line, in particular with associated flue gas bypass line, in particular LuVo-bypass, for heat coupling in WT14, WT17 and / or WT13, is coupled back into the heat flow of the power plant.
  • the invention ensures that the CO 2 scrubbing of the flue gas by means of chemical absorption and / or desorption and associated C0 2 compression thermally beneficial and optimized in the total heat flow and thus the total heat energy balance of a fossil-fueled, especially coal-fired, preferably conventional power plant involved is and / or can be integrated.
  • the term heat source means the possibility of decoupling and decoupling thermal energy in the form of at least one partial heat stream from the respective waste heat stream, ie a thermal energy in the form of measurable heat medium, and thereafter heat energy line one elsewhere in the power plant outside the area to supply the CO 2 scrubbing of the flue gas with associated CO 2 compression arranged heat sink.
  • the smoke gas side in the flue gas flow direction before the CO 2 scrubbing is decoupled or decoupled from the heat energy contained in the flue gas thermal energy in the form of a partial heat flow and in the CO 2 Laundry, especially in the area of the reboiler or evaporator, is coupled into the heat flow of CO 2 - laundry again.
  • This embodiment can also be realized independently of the above-described decoupling and decoupling of thermal energy from the region of the CO 2 scrubbing with associated CO 2 compression.
  • This use or sudeinkoppelung flue gas side or a disengaged thermal energy is preferably used in combination with corresponding in the area of CO 2 scrubbing with associated CO 2 compression, or a disengaged and in the area outside of the CO 2 - washing with associated CO 2 - Kompression again in provided the heat flow of the power plant coupled thermal energy.
  • the boiler or steam generator of the power plant supplied fresh air is heated by a heat exchanger, the decoupled from the field of CO 2 scrubbing with associated C0 2 compression or decoupled thermal energy for delivery to the incoming fresh air mass flow is supplied.
  • the power plant solar thermal or geothermal energy production plants are assigned, the energy gained therein is supplied to the heat flow of the power plant in the form of thermal energy or made available.
  • the flow direction is located behind the C0 2 ⁇ compression - particularly advantageous when the unlocking or decoupling the C0 2 scrubbing-Desorber- or Regeneratorkopf and in CO 2.
  • Advantageous locations for the formation of heat sources or heat sinks for the decoupling or decoupling of thermal energy continue to exist in the field of CO 2 laundry absorber intercooling and in the area of CO 2 compression intermediate cooling.
  • particularly advantageous locations are the range of low pressure preheating and the area in the flow direction behind a arranged behind a condenser condensate pump, the above areas are all formed in the water-steam cycle of the power plant.
  • the inventive method is further characterized in that the decoupling or decoupling of the thermal energy by means of one or more on C0 2 ⁇ laundry desorber or regenerator head and / or in C ⁇ 2 -streaming direction behind the C0 2 compression and / or in
  • a further advantageous embodiment of the invention is that the decoupling or decoupling of the thermal energy by means of one or more formed in the flue gas line and / or in the bypass flue gas line heat source (s) and the re-coupling of the thermal energy in the water-steam Circulation in the field of low pressure preheating and / or high-pressure preheating and / or in the district heating circuit and / or in the field of CO 2 scrubbing, in particular in the reboiler, preferably a heat exchanger of the reboiler is performed.
  • the decoupled in the CO 2 scrubbing with associated CO 2 compression or decoupled thermal energy is coupled by means arranged in a Rankine cycle heat exchanger back into the heat flow of the power plant.
  • the method it is particularly expedient according to the invention if the method is carried out in a power plant according to one of claims 11 to 29.
  • the power plant embodiment of the invention therefore is characterized in that the C0 2 scrubbing-Desorber- or Regeneratorkopf and / or CO 2 in -Strömungsraum behind the CO 2 compression was / or in the CO 2 absorber -Wäsche- intercooling and / or in the field of CO 2 - compression intercooling one or more used for heat transfer as a heat source (s) plant component (s) is arranged and / or formed, each leading into a heat transfer medium heat energy with one or more in the field the low-pressure preheating and / or arranged in the condensate flow direction before the low-pressure preheating and / or in a district heating circuit and / or in the fresh air heating and / or in the coal drying and as a heat sink (s) heat transfer causing plant component (s) is / are connected.
  • a process engineering and plant technology to realize well-way to form heat sources and heat sinks is to use existing and / or designed as an additional heat exchanger system components.
  • the invention therefore also provides, with regard to the power plant in a further embodiment, in the area of the CO 2 scrubbing with associated CO 2 compression at least one system component, preferably a heat exchanger, which forms a heat source, in particular for a separate heat transfer medium, and in which heat energy line a medium, preferably the separate armeirtedium, leading manner with at least one arranged in the power plant further, a heat sink, in particular for the separate heat transfer medium, forming system component, preferably another heat exchanger is connected, wherein one or more of a heat exchanger on C0 2 scrubbing-Desorber- or Regeneratorkopf and / or a heat exchanger downstream of the CO 2 - compression and / or a heat exchanger of the CO 2 -Wäsche- ⁇ bsorber spakühlung and / or a heat exchanger of the CO 2
  • Plant component (s) each acting as a heat source heat exchanger and / or after a desorber high CO 2 - containing gas line leading used as a heat source system component and / or after the CO 2 compression liquid CO 2 leading line used as a heat source system component (n) and one or more of the plant component (s) selected from a heat exchanger of the low-pressure preheating and / or a heat exchanger before the low-pressure preheating and / or a heat exchanger in the district heating circuit and / or a heat exchanger of coal drying and / or a heat exchanger of the fresh air heating each form a functioning as a heat sink further heat exchanger.
  • One way to realize the decoupling of thermal energy and reincorporation of thermal energy is in particular that the heat source forming a heat exchanger on C0 2 scrubber desorber or Regeneratorkopf heat energy with a heat sink forming a heat exchanger of the low pressure preheating, in particular with an upstream side connected to the condensate flow direction condensate pump nearest heat exchanger.
  • a further possibility to realize advantageously the decoupling and re-coupling of thermal energy consists furthermore in that the heat exchanger forming a heat source behind the CO 2 - compression heat energy with a heat sink of the low pressure preheating forming a heat sink, in particular the heat exchanger closest to a feed water tank in condensate flow direction, and / or the heat sink forming a heat exchanger is connected before the low pressure preheating.
  • the heat exchanger before the low pressure preheating in a condensate line in the condensate flow direction behind a Kondensatpuiripe and / or the heat exchanger of the low pressure preheating is arranged in a branching off from the condensate line bypass line / are, which the invention also provides.
  • a heat-technically particularly favorable mutual coupling of the heat exchangers WT2 and WT5 can be achieved in that the return of the heat exchanger of the low-pressure preheating is connected by heat energy with the flow of the heat exchanger before the low-pressure preheating.
  • a further advantageous and expedient heat energy line connection between the individual heat sources and the individual heat sinks can be achieved, in particular, if a heat transfer medium is introduced between the heat sources and the heat sinks, in particular for the remaining material flow of the power plant, between them, which is preferably then Case is when the heat sources and heat sinks as a heat exchanger are formed.
  • the invention therefore provides in a further embodiment, therefore, that a heat transfer medium in one of the heat exchanger after the C0 2 compression, the condensate in the direction of flow of a feed water tank nearest heat exchanger and the heat exchanger before the low pressure preheating cycle formed and / or in a heat exchanger at C0 2 - Laundry desorber or regenerator head and the one formed in the upstream condensate flow direction located condensate pump nearest heat exchanger circuit is guided in each case by these heat exchangers.
  • a convenient way to form a heat recovery is also to re-couple the decoupled or decoupled thermal energy in the district heating circuit of a power plant, if such a district heating circuit is provided.
  • the invention therefore further provides in an embodiment that the heat exchanger on the C0 2 scrubber desorber or regenerator head and / or the heat exchanger behind the CO 2 compression is / are connected with one or more heat exchangers (n) arranged in the district heating circuit ,
  • a line connection and coupling between the arranged in the district heating circuit heat exchangers and the arranged in the water-steam circuit of the power plant heat exchangers be beneficial, which is why the invention is also characterized in that one or more arranged in the district heating circuit with heat exchanger one or more of the low pressure preheating upstream or upstream heat exchanger (s) is connected heat energy in accordance with / are.
  • the heat exchanger can be arranged before the low-pressure preheating in the return of the arranged in the district heating circuit heat exchanger and
  • thermo energy and “thermal energy” are used as synonyms herein.
  • An advantageous use according to the invention therefore further consists in that the heat exchanger on the CO 2 scrubber desorber or regenerator head and / or the heat exchanger behind the C0 2 compression with one or more arranged in a coal mill associated with a coal pipe of the power plant heat exchanger (n ) is connected by heat energy.
  • the invention also provides that the heat exchanger on the C0 2 scrubber desorber or regenerator head and / or the heat exchanger behind the CO 2 compression with one or more in a boiler of the power plant fresh air supplying fresh air supply arranged heat exchanger (s) heat energy line is connected / are.
  • the invention further provides that the at least one heat exchanger arranged in the bypass flue gas line is connected to the water-steam circuit of the power plant in the region of low-pressure preheating or high-pressure preheating.
  • a heat exchanger arranged in the bypass flue gas line is connected to the district heating circuit by means of heat energy.
  • a heat exchanger arranged in the bypass flue gas line is connected to the reboiler and / or a heat exchanger of the reboiler in terms of thermal energy.
  • a heat conduction connected to the district heating circuit heat exchanger and / or with the water-steam cycle of the power plant, preferably in the region of the low pressure preheating, thermally conductively connected heat exchanger is arranged in the reboiler return.
  • the invention also provides that the heat exchanger on the CO 2 scrubber desorber or regenerator head and / or the heat exchanger behind the C0 2 compression and / or the heat exchanger of CO 2 scrubber
  • Compression intermediate cooling is thermally conductively connected to a arranged in a Rankine cycle heat exchanger / are.
  • FIG. 1 shows a schematic representation of power plant components of a coal-fired, in particular lignite-fired, power plant
  • FIG. 2 shows a schematic representation of power plant components of a coal-fired power plant with heat (re) coupling of thermal energy coupled out in the region of the CO 2 scrubbing with associated CO 2 compression into the water.
  • FIG. 3 in a schematic representation of the district heating circuit of Figure 2 with additionally integrated
  • Fig. 4 is a schematic representation of an alternative
  • FIG. 5 in a schematic representation of a
  • FIG. 6 in a schematic representation of a
  • 7 is a schematic representation of a heat (rear) coupling of decoupled in the region of CO 2 - laundry with associated CO 2 compression and in the area of a bypass
  • FIG. 8 in a schematic representation of a
  • 11 is a schematic representation of an auxulation of thermal energy in the region of a bypass
  • Fig. 13 is a schematic diagram of various components
  • FIG. 13 shows, in schematic schematic representation, a power plant designated as a whole by 1, comprising the steam generator or boiler 2, a turbine set 76 comprising, preferably high-pressure turbines 3, medium-pressure turbines 4 and low-pressure turbines 5, one CO 2 scrubbing 58 with associated CO 2 compression 27 comprehensive CO 2 -Abscheidung 77 and an associated, a district heating cycle 44 comprehensive district heating network 78.
  • a power plant designated as a whole by 1 comprising the steam generator or boiler 2
  • a turbine set 76 comprising, preferably high-pressure turbines 3, medium-pressure turbines 4 and low-pressure turbines 5, one CO 2 scrubbing 58 with associated CO 2 compression 27 comprehensive CO 2 -Abborgung 77 and an associated, a district heating cycle 44 comprehensive district heating network 78.
  • these plant components 2, 76, 77 and 78 via different partial heat flows with each other, these Sectionskyri ⁇ estr ⁇ me together form the total heat flow and the total heat energy balance of the power plant 1.
  • FIG. 1 shows, in
  • partial heat flows Q 8 to Qu are branched off and decoupled from the heat flow forming within the CO 2 separation 77 and, as indicated by the correspondingly marked arrows indicated by the solid line, returned to other partial heat flows and thus the total heat flow of the power plant 1.
  • the partial heat flows Q12 to Q 14 are branched off or decoupled from the flue-gas side partial heat flow Q 3 and likewise coupled back into the total heat flow of the power plant 1 (back) according to the arrow.
  • the partial heat flow Q 8 is decoupled from the CO 2 separation 77 and coupled into the run in the water-steam cycle of the power plant 1 partial heat flow Qi.
  • the partial heat flow Q 9 is decoupled from the CO 2 capture 77 and coupled into the district heating circuit 44 of the district heating network 78 and thus in principle the partial heat flow Q 2 .
  • the partial heat flow Q 10 is decoupled or decoupled from the CO 2 separation 77 and fed to the partial heat flow Q 4 of the fresh air supply and coupled into this again (back).
  • the partial heat flow Q 11 is likewise coupled out of the heat flow of the CO 2 precipitation 77 and then coupled back into the partial heat flow Q 5 guided in a coal line 55 leading to a coal mill 54 and / or the boiler 2.
  • the designated in Figure 1 in total with 1 power plant is in the upper part of the picture with its connected to the boiler 2 water-steam cycle and the lower part of the image with its flue gas side connected to the boiler 2 flue gas path with the successful completion of combustion in the boiler 2 CO 2 scrubbing of the flue gas by means of chemical absorption and associated CO 2 compression 27 shown schematically.
  • the power plant On the side of the water-steam cycle, the power plant comprises a high-pressure turbine 3, two medium-pressure turbines 4 and four low-pressure turbines 5, the number of turbines being merely exemplary.
  • a generator 6 is arranged at the end of the turbine section.
  • a condenser 7 is arranged in the water-steam circuit, which is connected as usual with a cooling tower 8.
  • a condensate pump 9 is arranged, which supplies the condensate to a five heat exchanger comprehensive Niedertownvor Suiter 10.
  • the low-pressure preheater 10 is adjoined by a feed water tank 11 with associated feed water pump 12, which feeds the feed water originating from the feed water tank 11 to a high-pressure preheater 13, after which it then enters the steam generator of the boiler 2. Furthermore, in the water-steam cycle of the respective turbines 3, 4, 5 outgoing steam lines are located.
  • this part of the power plant consists of components, as they are known from conventional coal-fired power plants.
  • the water-steam circuit of the power plant 1 also has three heat exchangers WTl, WT2 and WT5. Of these, the heat exchanger WT5 before the low-pressure preheating, in the condensate flow behind the condensate pump 9, but before the Niederbuchvor Sonr 10 in the leading to the feed water tank 11 condensate line 14 is involved.
  • the heat exchangers WT1 and WT2 are arranged in a bypass line 15 which branches off from the condensate line 14 in the direction of the condensate flow behind the heat exchanger WT5 and past the low-pressure preheater 10 but before the feedwater tank again into the condensate line 14.
  • the boiler is fired 2 as indicated by the arrow 16, with air and coal.
  • the flue gas leaving the boiler 2 via the flue gas duct 17 is fed to a flue-gas treatment 18 comprising at least the components denitrification unit, electrostatic filter and flue-gas desulphurisation plant and then passes into a decarbonization unit 19 comprising a CO 2 ⁇ wash 58 with associated CO 2 compression 27.
  • a flue-gas treatment 18 comprising at least the components denitrification unit, electrostatic filter and flue-gas desulphurisation plant and then passes into a decarbonization unit 19 comprising a CO 2 ⁇ wash 58 with associated CO 2 compression 27.
  • Dekarbonmaschinesstrom 19 is contained in the flue gas
  • a detergent is preferably MEA (monoethanolamine, H 2 N-CH 2 -CH 2 -OH) but also DEA
  • the actual washing of the smoke or exhaust gas takes place by means of the detergent in an absorber 20 or an absorption column, which / which flows through the flue gas in countercurrent to the detergent.
  • the flue gas leaves the absorber 20 at its head end as C ⁇ 2 -armed exhaust 21.
  • a desorber or regenerator 22 preferably in the form of a Desorption, followed by the C0 2 -rich washing or solvent is supplied after flowing through the absorber 20.
  • the first pressureless flue gas is isothermally compressed to a pressure of less than 10 bar, for example 2 bar, and then passed through the absorber 20, where it is the washing or solvent contrary flows.
  • the CO 2 -rich detergent or solvent is then introduced while flowing through a heat exchanger 25 in the desorber / regenerator 22.
  • the C0 2 -rich detergent is broken up by heating and regenerated, so that at the top of the desorber / regenerator 22, a nearly pure CO 2 -H 2 O mixture exits, which can be separated by a condensation process, so that then a circa 90% pure C0 2 stream is released, which is supplied via a line 26 in the embodiment of a ten-stage C0 2 compression system of CO 2 ⁇ compression 27, which compresses the C0 2 stream to about 100 bar and liquefied. Thereafter, the liquefied CO 2 is supplied by means of a line 28 for further use or storage.
  • the CO 2 -rich washing or solvent stream in the heat exchanger 25 is heated to about 95 ° C. This is done with the aid of also through the heat exchanger 25 isedem, in the desorber / regenerator 22 regenerated C0 2 -armem washing or cleaning agent 29 which is sufficiently heated in the evaporator / reboiler 23rd
  • the evaporator or reboiler 23 vaporizes some of the solvent, thereby desorbing the carbon dioxide from the scrubber or solvent to form a near-pure CO 2 -H 2 O mixture at the top of the condenser, into the condenser 31 at the top of the desorber / Regenerator 22, where the water condenses out, so that a nearly pure C0 2 -trom is discharged.
  • the regenerated, low-CO 2 scrubbing or solvent 29 is withdrawn at the bottom of the desorber / regenerator 22, passed through the heat exchanger 25, in which the countercurrent, loaded, CÜ 2 -rich washing or solvent stream 30 is heated. After passing through a pump brought to the necessary absorber pressure and cooled correspondingly, the low-CO 2 scrubbing or solvent 29 is fed back to the absorber 20. As results in losses of water and detergent throughout the process, they are added back to the system at a mixing point 32.
  • a system component used as a heat source in the form of a heat exchanger 33 is arranged in the line 26.
  • a condensate collecting vessel 34 is further arranged in the conduit 26 behind the heat exchanger 33, with which H due to the cooling associated with the heat exchanger 33 of the guided in the conduit 26 CO 2 H 2 0 stream H condensing 2 O can be caught.
  • the cooling of the liquefied C ⁇ 2 stream after the C0 2 compression 27 serving and also used as a heat source system component forming heat exchanger 35 is the CO 2 compression 27 arranged downstream in the line 28.
  • heat exchangers 36 Further system components used as heat sources in the form of heat exchangers 36 are provided as heat exchangers of the CO 2 scrubber-absorber intercooling, whereby a heat exchanger 36 arranged at the head of the absorber 20 is also considered to belong to the CO 2 scrubber absorber intercooling. Overall, four heat exchanger 36 are present in the embodiment. Furthermore, system components used as heat sources are also arranged in the form of heat exchangers 37 of the C0 2 compression intermediate cooling between the compressors 38 of the CO 2 compression 27. In the embodiment, six heat exchangers 37 are shown between the compressors 38, but it can be present in the ten existing compressors 38 up to nine heat exchanger 37 of the CO 2 compression intercooling.
  • heat exchanger WTl-WTIl which, as will be explained below, each form a used as a heat sink system component, with the help of each thermal energy can be transferred to a partial heat flow.
  • heat transfer medium heat exchanger 33, 35 to 37 thermal energy is decoupled from the heat flow of the decarburization 19 in the CÜ 2 laundry and the associated C0 2 compression 27 decarburization system 19 on the transferred in the heat exchangers 33, 35 to 37 flowing heat transfer medium and then coupled by discharge from this heat transfer medium with the help of forming for the heat transfer medium heat sinks heat exchangers WTl-WTlI elsewhere as thermal energy in the heat flow of the power plant system.
  • a decoupling or decoupling of thermal energy from the heat flow of the CO 2 scrubbing 58 with associated regenerator 22 and associated CO 2 compression 27 takes place by means of the heat exchangers 33 and 35.
  • the heat exchanger 33 functioning as a heat source is in the flow over the Line 39 and in the return via the line 40 with the heat sink acting as and used, arranged in the bypass line 15 heat exchanger WTl the low pressure preheating.
  • the lines 39, 40 circulates a heat transfer medium, which absorbs thermal energy in the heat exchanger 33 and this gives off in the heat exchanger WTl to the flowing in the bypass line 15 condensate and is coupled back into the actual heat flow of the power plant 1.
  • the heat exchanger 35 functioning as a heat source is connected via a line 41 to the heat exchanger WT2 which functions as a heat sink and is used in the bypass line 15.
  • the return of the heat exchanger WT2 the low-pressure preheating is connected via a line 42 with the disposed in the condensate line 14 and also forming a heat sink heat exchanger WT5.
  • On the return side of the return of the heat exchanger WT5 via a line 43 is in turn connected to the heat exchanger 35.
  • a heat transfer medium circulates in the lines 41, 42 and 43, a heat transfer medium.
  • a plant component in the present example, the unitized into a heat exchanger 35 and WT2 and the unit together contained heat exchanger 33 and WTl, present in the CO 2 scrubbing with assigned CO 2 Compression used both as a heat source and the decoupling or decoupling of thermal energy causes and which is used in the area of the power plant 1 as a heat sink and the coupling of in the range of CO 2 scrubbing with associated CO 2 compression out or decoupled thermal energy causes.
  • the heat exchanger 35 serves as a heat source for the conveyed in the lines 41, 42 and 43 heat transfer medium, the absorbed thermal energy to the condensate in the direction behind the condensate pump 9 circa 18 ° C cool condensate, which passes in an amount of about 2/3 of the total guided through the condensate line 14 condensate flow through the bypass line 15 to the low pressure preheater 10 and with Help the acting as a heat sink heat exchanger WT2 is heated so that the condensate before re-entry into the conduit 14 or the feedwater tank 11 has a temperature of about 120 0 C.
  • the leading back to the heat exchanger WT5 return of the heat exchanger WT2 then still has such a high temperature that the heat exchanger WT5 also as a heat source for the heat transfer back into the flowing in the line 14 Condensate can be used and according to embodiment also, wherein the heat exchanger WT5 in the context of the invention, however, forms a heat sink for the thermal energy obtained in the CO 2 scrubbing.
  • 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, by means of which thermal energy is coupled into the heat flow of the CO 2 scrubbing with associated CO 2 compression.
  • the return Sl of the heat exchanger 24 opens in front of the feed water tank 11 in the condensate line 14 and there condensate with a temperature of approx 120 0 C in the condensate line 14 returns. This return point forms a heat source for the condensate flowing in the condensate line 14.
  • the temperature of the guided in the conduit 26 CO 2 -containing gas is so high that in the flow of the heat exchanger 33 through the line 26, a temperature of 95 ° C in the guided between the heat exchanger 33 and the heat exchanger WTl cycle is adjustable.
  • FIG. 2 shows a schematic representation of a power plant
  • thermo energy is coupled back into the district heating circuit, which also to the used as a heat source heat exchangers 33 and 35 of the CO 2 - laundry with associated CO 2 compression 27 by local decoupling or decoupling from the heat flow of C ⁇ 2 wash was won.
  • the heat exchangers WT4 and WT3 with the heat exchangers 33 and 35 connecting lines 39, 40 and 41, 43 can be seen from Figure 2.
  • the heat exchanger WT4 is arranged in a bypass line 48 bridging the entire preheating and heating section from a condensate pump 46 to a district heat removal point 47
  • the heat exchanger WT3 in a condensate pump 46 and district heating removal point 47 is only the first half of the preheating and heating section the district heating circuit 44 bridging bypass line 49 is arranged.
  • the interconnection or piping is such that the heat exchanger 35 is behind the CO2 compression 27 heat energy in its flow via the line 41 as known from the embodiment of Figure 1, connected to the heat exchanger WT2 whose return to the heat exchanger 35th recirculating line 43 is connected.
  • the return of the heat exchanger WT2 with the flow of the Heat exchanger WT5 connected the return of which in turn opens into the line 43.
  • the heat exchanger WTl is in turn arranged in the region of the low-pressure preheating and the low-pressure preheater 10 and is connected to the supply line 39 of the heat exchanger 33 on the C0 2 scrubber-desorber or regenerator head in terms of thermal energy.
  • the return of the heat exchanger WTL is connected to the return line 40 of the heat exchanger 33. From the flow line 39 branches off to the heat exchanger WT3 in the district heating circuit 44 leading line 52, wherein the return side of the heat exchanger WT3 is connected via a line 53 to the return line 40.
  • this heat energy-conducting guide it is possible by means of this heat energy-conducting guide to dissipate thermal energy, which is obtained by decoupling by means of the system components used as a heat source in the form of the heat exchangers 33 and 35 from the heat flow of the CO 2 scrubbing with associated CO 2 compression, into the heat flow of the power plant 1
  • the circuit can be designed differently.
  • a temperature of 46 0 C is reached at 13 bar behind the condensate pump 46 in the region of the diversion of the bypass lines 48, 49 and in the region of the junction of the bypass line 48 in the district heating circuit 44, a temperature of 136 ° C. set at about 14 bar. It is, of course, depending on the desired arrangement or use of one or more heat exchanger (s) WTl, WT2, WT3, WT4 and / or WT5 only provide the leads or circuits of lines that are required for the desired operation.
  • FIG. 3 shows a detail of a further alternative embodiment, which is essentially identical to the embodiment shown in FIG. 2, with the sole difference that the reboiler or evaporator 23 is no longer supplied with the steam DI from the water-steam cycle Return Sl of the condensate line 14 is supplied. Rather, the reboiler 23 is now integrated into the district heating circuit 44, so that the thermal energy necessary for the CO 2 expulsion from the district heating circuit 44 by means of the bleed steam lines 45a-45d and the therein arranged as in the embodiment of Figure 2 and interconnected heat exchanger WT3 and WT4 is provided.
  • the same or identical parts or elements to the embodiments of the preceding Figures 1 and 2 are again provided with the same reference numerals.
  • FIG. 4 shows an exemplary embodiment in which the system components designed as heat sink in the form of heat exchangers WT6 and WT7 are the only system components arranged in the district heating circuit 44 for heating / heating the district heating circuit 44. It thus, there are no steam feeds 45a-45d, as they are present in the exemplary embodiment according to FIG. 3 and the exemplary embodiment according to FIG. Also, the other heat exchangers WT3 and WT4 present in the other exemplary embodiments are no longer present in the district heating circuit 44. In this embodiment, it is provided that the entire decoupled in the CO 2 scrubbing with associated C0 2 compression 27 thermal energy is completely and completely supplied to the district heating circuit 44.
  • the heat exchanger WT6 is connected to the heat exchanger 33 on the CO 2 scrubber-desorber or regenerator head, which is indicated by the lines 39 and 40.
  • the heat exchanger WT7 is connected to the heat exchanger 35 behind the CO 2 compression 27, which is indicated by the lines 41 and 43.
  • a separately present heat transfer medium is continuously guided recirculating in a circuit formed by the lines 41 and 43 between the heat exchangers 35 and WT7 and a circuit formed by the lines 39 and 40 between the heat exchangers 33 and WT6.
  • Analogously to the embodiment according to Figure 3 can also be arranged in the embodiment according to FIG 4 in the district heating circulation 44 of the heating circuit for the reboiler or evaporator 33 Ü 2 ⁇ and return S 2 ⁇ integrated with lead.
  • each have a heat exchanger WT5 after the condensate pump and before the low-pressure preheating 10 is arranged and formed it is also possible to dispense with such and exclusively via at least one or more of the heat exchanger WTl and / or WT2 and / or WT3 and / or WT4 perform the re-integration of the recovered thermal energy.
  • the feed from the district heating circuit 44 forms the supply or the evaporator heating D 2 ⁇ and the return S 2 1 the return of the evaporator 23 in the district heating circuit 44.
  • FIG. 5 shows a coal feed line 55 leading to the coal mill 54, in the course of which two heat exchangers WT8 and WT9 designed as heat sinks are arranged, wherein the heat exchanger WT8 with at least one of the heat exchangers 36 and / or 37 and the heat exchanger WT9 with at least one of the heat exchangers 33 and / or 35 is connected, in particular, in turn, through the lines 39, 40 and / or 41, 43, a heat transfer medium is circulated.
  • the supplied coal may be in particular lignite.
  • the heat exchangers WT8 and WT9 are preferably in the form of drum dryers, in which the Coal flow and the lines 39 and 40 respectively supplied heat transfer medium flow are guided separately from each other in countercurrent. As indicated by the dotted line to the heat exchanger WT, but also more (or less) than the two heat exchangers WT8 and WT9 can be arranged in the line 55 but.
  • FIG. 6 shows an exemplary embodiment in which heat exchangers WTlQ and WTIl are arranged as heat sinks in a fresh air supply line 56 in front of the air preheater 57.
  • the heat exchanger WTlO via lines 39, 40 to the heat exchanger 33 and the heat exchanger WTIl via lines 41, 43 connected to the heat exchanger 35, wherein in the lines 39/40 and 41/43 in turn a separate heat transfer medium is circulated.
  • further or fewer heat exchangers WT can be arranged in the line 56.
  • the heat exchangers 33 and 35 are designed in the embodiments such that at the heat exchanger WTl and on
  • Heat exchanger WT3 a flow temperature of the supplied
  • the temperature control on the heat exchanger 35 is designed so that there sets a outgoing as a preliminary heat transfer medium flow a temperature of 185 0 C.
  • each heat sink forming a heat exchanger WTl - WTIl and / or any heat source forming a heat exchanger 33 on CO 2 scrubber desorber or regenerator head and / or heat exchanger 35 behind the CO 2 compression and / or line 26 and / or line 28 in any combination both with each other and with each other to connect such that a thermal decoupling takes place at the heat sources and a re-coupling of thermal energy to the heat sinks or is feasible.
  • FIG. 7 A supplemented with further recovered energy streams, not exclusively from the field of CO 2 scrubbing recovered energy flows, which are then returned to the water-steam cycle, equipped power plant is shown in FIG. 7.
  • a heat exchanger WT12 is provided, which is flowed through by the outgoing from the reboiler 23 and the arranged there heat exchanger 24 return Si, the return Si then opens into the condensate line 14 in the direction of condensate flow in front of the feedwater tank 11.
  • the heat exchanger WT12 is flowed through by condensate diverted from the condensate line 14 in countercurrent to Reboiler return Si, which condensate is fed to a arranged in a bypass flue gas line 59 of the air preheater 57 further heat exchanger WT13. From the heat exchanger WT 13, the condensate heated there by hot flue gas flows back into the condensate line 14 in the condensate flow direction upstream of the last heat exchanger of the low-pressure preheater 10 in the condensate flow direction.
  • a further heat exchanger 14 is arranged, which in countercurrent to that in the
  • Condensate is flowed through, in the direction of condensate behind the feedwater tank 11 and before the
  • the condensate guided through the heat exchanger WT14 can also open into the condensate line 14 behind the first heat exchanger of the high-pressure preheater 13 in the flow direction of the condensate.
  • a heat exchanger WT16 Parallel to the heat exchanger WT15, a heat exchanger WT16, also through which the return flow Si of the reboiler 23 flows, is arranged.
  • fluid conducted through the heat exchanger WT16 in the district heating circuit 44 is passed through the heat exchanger WTI 6.
  • the heat exchanger WT17 is connected to the district heating circuit 44.
  • a reboiler removal with flow D ⁇ 2 and return S ⁇ 2 with branching from and return to the district heating circuit 44 may be provided, as shown in Fig. 3.
  • the inlet D 1 to the reboiler 23 and the return Si from the reboiler 23 with the heat exchangers WT15 and WT16 integrated therein, as they are still contained in the exemplary embodiment according to FIG. 8, are then eliminated.
  • the arrangement of a heat exchanger WT13 and / or WT14 and / or WT17 in the flue gas flowed through by the flue gas line 59 has the advantage that no additional blower is necessary to maintain the flue gas flow, since the bypass flue gas line 59 is flowed through in the direction of the general flue gas flow direction ,
  • this has the disadvantage that the respective heat exchanger WT13, WT14, WT17 comes into contact with dirty flue gas, which is why the respective heat exchanger must be made of high-grade steel.
  • the risk of formation of ammonium bisulfate which is reflected on the heat exchanger surfaces.
  • FIG. 6 shows, it is also possible to provide a return line 62 on the air side, in which a further heat exchanger WT18 is arranged, which is then in line connection with the condensate line 14 in the region of the low-pressure preheater 10 or the high-pressure preheater 13 ,
  • the return line 62 branches off in the flow direction of the fresh air behind the air preheater 57 from the air supply line 56 and flows in the air flow direction before the heat transfer system 63 back into the fresh air line 56.
  • the bypass flue gas line 59 on the flue gas side branches in the flue gas flow direction in front of the air preheater 57 of the flue gas duct 17th and flows back into the flue gas duct 17 in the flue gas flow direction behind the air preheater 57 and before the heat displacement system 63.
  • a fan 64 is arranged to the recirculated fresh air against the to be able to move the general flow direction of the fresh air in the line 56.
  • heat exchangers 66, 67 and 68 are arranged in the heat transfer medium 65, which are heated with supplied steam, for example live 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 according to the name Di is taken from the water-steam cycle of a power plant 1.
  • This indirect (warm water) heating of the reboiler 23 by means of the heat transfer medium circuit 65 reduces the risk that the feed water will be contaminated by possible leaks in the reboiler heat exchanger 24 with the chemical absorbent 29.
  • the arrangement of the heat exchangers in the flow direction of the heat transfer medium water guided in the heat transfer medium circuit 65 in the order heat exchanger 68, heat exchanger 67 and then heat exchanger 66 a stepped heating provided with low-temperature heat from the C0 2 scrubbing / C0 2 compression 58/27 can also be supplied to a Rankine cycle, such as 10, two heat exchangers WT19 and WT20 are arranged in a Rankine cycle 69, in particular in an Organic Rankine cycle Solvent or preferably ammonia (NH 3 ) operated a circuit in which Niedertemperaturabisserr ⁇ e from the CO 2 scrubbing 58 / C0 2 ⁇ compression 27 is used.
  • a Rankine cycle such as 10
  • two heat exchangers WT19 and WT20 are arranged in a Rankine cycle 69, in particular in an Organic Rankine cycle Solvent or preferably ammonia (NH 3 ) operated a circuit in which Niedertemperaturabisserr ⁇ e from the
  • the heat exchanger WT19 is arranged in the "cold stage" of the Rankine cycle 69 and is supplied to it in waste heat from the absorber intermediate cooling 36 or the CQ 2 compression intermediate cooling 37.
  • the heat exchanger WT20 which in the "hot Stage "of the Rankine cycle 69 is disposed in the CO2 ⁇ scrubbing waste heat from the Desorberkopf, ie, obtained via the heat exchanger 33 thermal energy, or from the CO 2 ⁇ compression, ie via the heat exchanger 35 recovered thermal energy, the Rankine cycle 69 fed.
  • the customer 75 associated with the turbine stage of the Rankine cycle 69 may be a generator for power generation, but also a mechanical drive of a feed pump or a CO 2 compressor.
  • both a heat exchanger WT19 and a heat exchanger WT20 are provided in the exemplary embodiment according to FIG. 10, it is also possible to provide only one of the two heat exchangers WT19 or WT20, depending on the design of the power plant.
  • the heat exchanger WT21 indicates the absorbed heat the heat exchanger 24 of the Reboilers 23 leading flow D 3 , wherein the heat transfer medium from the heat exchanger 24 via the reboiler return S 3 to the heat exchanger WT21 is recycled.
  • the heat exchanger WT21 is designed as a flue-gas-fed and used as a heat source system component and the reboiler 23 associated heat exchanger 24 is then used as a heat sink system component.
  • the exemplary embodiment according to FIG. 12 differs from the exemplary embodiment according to FIG.
  • FIG. 11 shows a flue gas duct 17, which leads in the flow direction of the flue gas to a denitrification plant 70 to the air preheater 57 and then to an electrostatic precipitator 71.
  • the denitrification 70 and the electrostatic filter 71 bypasses the branching off of the flue gas line 17 and back into this opening bypass flue gas line 59 the air preheater 57, but flows back into the flue gas duct 17 before the electrostatic filter 71.
  • a heat displacement system 63 Downstream of the electrostatic filter 71, a heat displacement system 63 is arranged in the flue gas line 17, in which two heat exchangers 73 and 74 connected to each other via a circulating heat transfer medium are arranged, from which the heat exchanger 73 removes thermal energy from the flue gas flow conducted in the line 17 and to the in the heat transfer system 63 in circulation guided heat transfer medium. Downstream of the heat transfer system 63 is still a Flue gas desulfurization system 72, which then follows the absorber 20 with associated desorber 22 comprehensive CO 2 scrubbing 58 for CO 2 separation, before then the C0 2 -arm gas 21 leaves the plant.
  • the fresh air line 56 is provided, which is first performed in the fresh air flow direction in front of the air preheater 57 through the heat transfer system 63 and there in the heat exchanger 74 receives the heat energy from the flue gas via the heat exchanger 74 to the circulated in the heat transfer system 63 heat transfer medium thermal energy.
  • the low-temperature heat present in front of the flue-gas desulphurisation plant 72 in the fresh-air flow direction in front of the air preheater 57 is transferred into the fresh-air flow in the heat-displacement system 63.
  • the preheated fresh air stream required in the air preheater 57 then only a lower heat energy supply to have the provided in the flow direction behind the air preheater 57 temperature.
  • This is used to perform the flue gas in the existing but in the air preheater 57 for heating the fresh air now no longer required amount of heat through the bypass flue gas line 59 and there in the heat exchanger WT18 to the therein and as a flow D 3 to the heat exchanger 24 of Reboilers 23 guided heat transfer medium ZM transferred.
  • this heat transfer medium can be provided so much energy to the reboiler 23 that the heat transfer medium has a temperature of about 120 0 C to a maximum of 360 0 C.
  • the heat exchanger 33, the line 26, the heat exchanger 35, the line 28, the heat exchanger 36 and the heat exchanger 37 are thus formed as used as a heat source system components and arranged in a power plant, these heat sources from in the CO 2 - laundry 58 are supplied with associated C0 2 compression 27 existing or incurred there thermal energy.
  • System components used as heat sinks, which depart from the above-mentioned heat sources, ie from the area of the CO2 scrubbing 58 with associated CO 2 compression 27, are the heat exchangers WT1-WT12 and the heat exchangers WT15 and WTl ⁇ .
  • the heat exchangers WT1, WT2, WT5, WT12 and WT15 feed the thermal energy obtained from the CO 2 scrubbing 58 with associated CO 2 compression 27 into the steam-water circuit of the power plant 1.
  • the heat exchangers WT3, WT4, WT6, WT7 and WT16 feed the obtained thermal energy into the district heating circuit 44.
  • the heat exchangers WT8 and WT9 feed the received or received thermal energy into the coal mill 55 leading to the coal mill 54.
  • the heat exchangers WTlO and WTlI feed the obtained or absorbed thermal energy in the fresh air line 56 a.
  • the heat exchangers WT19 and WT20 which are likewise supplied with thermal energy by the CO 2 scrubbing 58 with associated CO 2 compression 27, release the absorbed thermal energy in its function as a heat sink to the Rankine cycle 69.
  • flue gas heat energy system components with the function of a heat source continue to represent the heat exchanger WT13, WT14, WT17 and WT21, the heat exchanger WT13 and WT14 the absorbed thermal energy in the extent a heat sink feed the forming system component of the water-steam cycle of the power plant 1 and the heat exchanger WT17 outputs the absorbed thermal energy in the district heating circuit 44 as the associated heat sink forming system component.
  • the heat exchanger WT21 is the heat absorbed to the flow D 3 to the heat exchanger 24 of the reboiler 23, so that the heat exchanger 24 also forms the function of a thermal energy to the CO 2 leaching donating system component function as a heat sink.
  • the heat exchanger WT18 forms a directly from the thermal energy of the air preheater 57 leaving fresh air, but thus indirectly by a thermal energy from the range of CO 2 scrubbing 58 and / or C0 2 compression 27 fed heat source, as from the field of CO 2 ⁇ scrubbing 58 and / or CO 2 compression 27 extracted heat in the air flow direction in front of the return line 62 via the heat exchanger WTlO and / or WTlI is coupled into the fresh air or fed.
  • the heat source WT18 outputs the heat absorbed to the condensate line 14 functioning as a heat sink in the region of the low pressure and / or the High-pressure preheating 10 and / or 13 to the water-steam cycle of the power plant 1 from.
  • the present invention relates to a process for "optimally" incorporating heat streams into a conventional power plant process
  • the conventional power plant process may be any known fossil fuel fired power plant process, in particular a coal fired power plant process in the net power range of 500 to 1000 MW e i in the embodiment, is it is a coal-fired power plant process with a net capacity of about 850 MWe.
  • the to be integrated heat flows can be used in a temperature range between 50 and 400 0 C. are particular to be integrated heating in a temperature range between 50 and 200 "C.
  • the source of heat flows may be solar thermal or geothermal energy plants, or it may be plants directly related to the conventional power plant process.
  • the plants that are directly related to the conventional power plant process can be waste heat streams from a fuel drying plant.
  • the waste heat streams can originate from a chemical CO 2 scrubbing downstream of the power plant process with an absorber and desorber system and a subsequent compression of the separated carbon dioxide.
  • the preheat section of the water / steam cycle should consist 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 flow of at least 510 MW th at a temperature level between 120 and 170 ° C needed is assumed to be 15 ° C.
  • the assumption here is that the specific total energy demand for CO 2 scrubbing in an absorber and desorber system is 3600 kJ (kg CO 2 ).
  • the required process heat for the chemical CO 2 scrubbing is taken from the power plant process in a suitable manner D 1 via a collector system between the various turbine stages 3, 4, 5.
  • D 1 a collector system between the various turbine stages 3, 4, 5.
  • the aim of the present invention is to minimize the efficiency loss of the overall process, which is caused by the high demand for thermal energy in the chemical CO 2 scrubbing.
  • the Co 2 washing is an absorber 20 and desorber 22 system in which the CO 2 is separated from the flue gas stream by means of chemical absorption. Due to the chemical reaction, the chemical absorption releases heat, which is dissipated by intermediate cooling 26 in order to achieve a better conversion.
  • the loaded detergent then passes into the desorption column 22 in which via a reboiler 23, the energy is supplied, which is required for breaking the chemical bond between the detergent and the CO 2 .
  • the water loading of the released CO 2 at the desorber head is higher than that of the treated in the absorber 20 flue gas due to the higher temperature, so this also energy must be supplied. Total demand 3600 kJ / (kg CO 2 ) for MEA / water ratio of 30/70.
  • the temperature which is necessary in the desorption column 22 for the breaking of the chemical bond is in the system described at about 120 ° C. This results in the desorber head a completely water-saturated C0 2 stream having a temperature of about 115 0 C.
  • a C0 2 compression can take place.
  • the CO 2 is compressed in a nine-stage compression to 200 bar.
  • an intermediate cooling 37 is interposed in each case due to an energy-efficient compression between the first seven stages.
  • the intermediate cooling takes place at a temperature level of about 65 to 30 0 C.
  • the last compression stages are lined up without intercooling.
  • the compressed CO 2 - stream has a temperature of about 190 ° C. This temperature is too high for further processing of the CO 2 , so that a further cooling 35 is necessary. Afterwards, the CO2 is present at approx. 25 ° C / 200 bar and in liquid state.
  • heat source usable plant components are:
  • the CO2 exiting the top of the desorber 22 is completely saturated with water and has a temperature of about 115 ° C at a pressure of about 2 bar.
  • a mass flow of about 250 kg / s about 40% water is contained.
  • a water mass flow of about 1050 kg / s can be heated to about 105 0 C.
  • the heat exchanger 33 is the plant component which can be used as a "heat source.”
  • the water mass flow can also be used as heat sink WTl and / or WT3 and / or WT6 and / or WTlO and / or WT9.
  • the C0 2 mass flow is about 150 kg / s. With this C0 2 mass flow, the system components used as "heat sink" can be used
  • Heat exchanger WT2 or alternatively WT4 or WT7 and WT5 or WT9 are operated.
  • heat source used system components are in this case the heat exchanger 35 and / or the line 28th
  • the mass flow of warm water is approx. 220 kg / s. This allows the heat exchangers WT12 and / or WT15 and / or WT16 to be operated.
  • the heat exchanger 24 in this case (FIGS. 7 and 8) represents a system component used as a "heat source”.
  • heat sinks in the embodiment of a coal-fired 850 MW power plant unit serve ei:
  • the LP preheating section 10 with a temperature range of 20 to 120 ° C.
  • the heat exchangers WTl, WT2, WT5, WT12 and WT15 are added.
  • the HD preheating section 13 with a temperature range of 160 to 290 0 C.
  • the heat exchanger WT14 is added. This is a special case, since it is not heated directly from CO 2 scrubbing / compression, but from a windward bypass 59, which is made possible by WTlO.
  • Heat exchangers WT3, WT4 and WT16 added.
  • the fresh air preheating whereby the fresh air is present depending on the season with a temperature between -10 and 30 0 C.
  • the heat exchanger WTlO is added.
  • Input temperature of 15 0 C is present.
  • the heat exchanger WT9 is added.
  • the recoverable amounts of heat from the CO 2 scrubbing / compression become smaller, so that waste heat from the absorber intermediate cooling 37 of the intermediate compression cooling 36 are to be used in the heat exchanger WT8.
  • the WT 1 transfers heat from a substream 33 of the Desorberkopf Vietnamese to the ND preheat section 10.
  • This is about 50% (100% with 200 MW district heating decoupling) of the incoming condensate of 20 (29 ° C with 200 MW district heat extraction) to 100 0 C. heated.
  • About 32 MW (about 60 MW with 200 MW district heat extraction) are transferred to the water-steam cycle.
  • the efficiency increase through this heat exchanger WTl is 0.38 percentage points (0.79 percentage points for 200 MW district heat extraction).
  • the WT2 25 transfers heat from the last stage of the CO 2 - compression on the ND preheating section 10. Here, approximately 50% of the incoming condensate is heated from 20 to 120 0 C. About 49 MW will be transferred to the water-steam cycle.
  • the increase in efficiency through this heat exchanger WT2 is 1.19 percentage points.
  • This heat exchanger is used as an alternative to the WT4, which is only used when district heating 44 is decoupled.
  • the WT3 transfers heat 33 from a partial flow of Desorberkopfizi on the district heating circuit 44.
  • about 60% of the district heating return from 46 0 C to 100 0 C is heated.
  • about 80 MW are transferred to the district heating circuit 44.
  • the increase in efficiency of this heat exchanger WT3 is 1.70 percentage points.
  • the WT4 transfers heat 35 from the last stage of the CO 2 compression 27 to the district heating circuit 44.
  • the increase in efficiency through this Heat exchanger WT4 is 1.36 percentage points.
  • This heat exchanger is used as an alternative to the WT2, which is only used if no district heating is decoupled.
  • the WT5 transfers heat 35 from the last stage of CO 2 compression 27 to the LP preheat section 10. However, the WT 5 heat exchanger is not fed directly from the CO 2 compression but preferably from the return from WT 4.
  • the heat exchanger WT5 is therefore preferably used only when the heat exchanger WT4 works, ie when district heating is coupled out.
  • the reason is that the return of WT4 with about 5O 0 C is significantly higher than that of WT 2 with 25 ° C and thus still being suitable for both further cool as the compressed C0 2 stream and 100% of the condensate from 20 to 3O 0 C to warm up.
  • About 10 MW are transferred to the condensate before the LP preheaters.
  • the increase in efficiency through this heat exchanger is 0.36 percentage points.
  • the WT6 transfers heat 33 from a partial stream of Desorberkopfizi on the district heating circuit 44.
  • a district heat generation is considered, which is fed exclusively with waste heat from the CO2 scrubbing / compression 58/27. In this case, about 30 MW are transferred to the district heating circuit 44.
  • the WT7 transfers heat 35 from the last stage of the CO 2 compression 27 to the district heating circuit 44.
  • FIG. 4 is considered a district heat generation powered solely by waste heat from CO 2 scrubbing / compression 58/27. About 20 MW will be transferred to the district heating circuit.
  • the WTlO transfers heat 33 from a partial flow of Desorberkopfizi on the fresh air 50. This will be about 57 MW transfer heat to the fresh air entering at a mass flow of about 640 kg / s at 15 0 C and exits at 100 0 C.
  • the increase in efficiency through this heat exchanger is 1.22 percentage points (1.16 percentage points for 200 MW district heat extraction).
  • the heat exchanger WTlI can be operated in two ways: a) by waste heat (36 ⁇ from the absorber intermediate cooling or b) by the compression intermediate cooling 37. In both ways, the WTIl with a flow temperature of about 60 ° C is used.
  • This heat exchanger WTIII can be used if only a small partial flow of the flue gas in the CO 2 scrubber / compression 58/27 is treated. Thus, the traceable amount of heat from the CO 2 scrubbing / compression 58/27 is lower, so that waste heat from the absorber intercooler 36 or the compression intercooler 37 are to be used in WTIl.
  • the WT14 is operated by a Luvo bypass 59.
  • This heat exchanger can be used as the fresh air enters through the WTlO by about 85 0 C warmer in the air heater 57th
  • the Luvoaustrittemperatur of the fresh air is, however, limited to 34O 0 C, so here must be removed by the Luvo- bypass 59 heat at a higher temperature level.
  • this heat exchanger WT14 about 150 kg / s flue gas from 380 0 C to 170 0 C are cooled.
  • this amount of heat about 200 kg / s of water from 160 0 C to 205 0 C are heated. This water mass flow is used to bridge the first HD preheater of the high pressure heating 13. With this heat exchanger WT14 approx. 40 MW are transferred.
  • the increase in efficiency of this heat exchanger WT14 is 1.3 percentage points (also for 200 MW district heating, too).
  • the heat exchanger WT16 transfers heat 35 from the reboiler return Sl on the district heating circuit 44. Here, the entire district heat mass flow of 95 0 C to 105 0 C is heated.
  • the reboiler return Sl is cooled from about 120 0 C to 100 0 C. In this case, about 20 MW of heat are transferred.
  • the heat exchanger is used between the third and fourth heat exchanger in the embodiment of Figures 2, 3, 7 and 8 each have four heat exchanger having district heating circuit 44 and reduces the need for KZÜ steam considerably.
  • the efficiency increase through the heat exchanger WT16 is 0.90 percentage points.
  • the heat exchangers WT12 and WT15 transfer heat from the reboiler return Sl to the LP preheat line.
  • the entire mass heated to 100 0 C in the WTl is heated to 116 ° C.
  • the reboiler reflux is cooled from about 120 0 C to HO 0 C.
  • These heat exchangers WT12 and WTl5 are used both between the fourth and fifth heat exchanger of the ND preheating section of the low-pressure preheating 10 having five heat exchangers each in the exemplary embodiments of FIGS. 1, 2, 7 and 8 and reduce the need for MD steam.
  • the increase in efficiency through this heat exchanger is O, 4% -points.
  • the WT9 transfers heat: a) a partial stream of the desorber head heat 33 and b) the last stage of the CO 2 compression 35 to the fuel to preheat it from 15 0 C.
  • the WT8 heat exchanger can be operated in two ways: a) by waste heat from the absorber intercooler 36 or b) by the compression intercooler 37. In both ways the WT8 with a flow temperature of approx. 6O 0 C used. If one assumes a power plant 1 with a 200 MW thermal Fernmérmauskoppelung without the waste heat utilization according to the invention, one can assume a total electrical gross efficiency of 31.4% and a net efficiency of 25.91% with an internal electrical demand of 94 MW.
  • the total gross efficiency of the power plant block including the complete CO 2 scrubbing / C0 2 compression by the heat input is 43.13% a net efficiency of 37.42% and an electrical consumption of about 93 MW.
  • the inventive method and / or the power plant 1 according to the invention can also be designed such that heat from solar thermal and / or geothermal heat sources WTl, WT2, WT5 for low-pressure preheating, for heating the power plant 1 associated district heating circuit WT3, WT4 and / or Fresh air preheating WTlO, WTIl with associated LuVo bypass 59 to a heat transfer in a heat flow in the water-steam cycle of the power plant 1, especially in the low-pressure and / or high-pressure preheating, and / or a power plant 1 associated district heating circuit, preferably in combination with a CO2 wash 58, is used or usable.

Abstract

L'invention concerne un procédé de récupération de chaleur par association de plusieurs flux de chaleur d'une centrale thermique (1) à combustible fossile, en particulier au charbon, avec lavage post-combustion des fumées (58) par absorption et/ou désorption chimique du CO2 et compression du CO2 (27). Le but de l'invention est de fournir une solution permettant d'intégrer de manière avantageuse sur le plan thermique un lavage des fumées, associé à la compression du CO2, dans le flux énergétique total et/ou le bilan énergétique total d'une centrale thermique à combustible fossile, en particulier au charbon, de préférence classique. Ce but est atteint par le fait que l'énergie thermique est extraite du flux de chaleur résultant du lavage des fumées (58) avec compression du CO2 (27) sous la forme d'au moins un flux de chaleur partiel (Q8, Q9, Q10, Q11) puis réinjectée dans un flux de chaleur associé directement ou indirectement au flux de chaleur de la chaudière (2) ou du générateur de vapeur de la centrale thermique (1) et/ou par le fait que l'énergie thermique est extraite du flux de chaleur des fumées (Q3) sous la forme d'au moins un flux de chaleur partiel (Q12, Q13, Q14) et réinjectée dans le flux de chaleur résultant du lavage des fumées (58) avec compression du CO2 (27).
EP10728683A 2009-07-10 2010-07-06 Centrale thermique au charbon avec lavage des fumées et récupération de chaleur Withdrawn EP2452051A2 (fr)

Applications Claiming Priority (2)

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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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WO (1) WO2011003892A2 (fr)

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CA2767590A1 (fr) 2011-01-13
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WO2011003892A3 (fr) 2011-06-23

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