EP3030757A2 - Procédé de production d'énergie électrique et installation de production d'énergie - Google Patents

Procédé de production d'énergie électrique et installation de production d'énergie

Info

Publication number
EP3030757A2
EP3030757A2 EP14744776.7A EP14744776A EP3030757A2 EP 3030757 A2 EP3030757 A2 EP 3030757A2 EP 14744776 A EP14744776 A EP 14744776A EP 3030757 A2 EP3030757 A2 EP 3030757A2
Authority
EP
European Patent Office
Prior art keywords
air
refrigerant
temperature level
operating mode
level
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Withdrawn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
EP14744776.7A
Other languages
German (de)
English (en)
Inventor
Christoph Stiller
Sebastian Rehfeldt
Brian Stöver
Alexander Alekseev
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.)
Linde GmbH
Mitsubishi Power Europe GmbH
Original Assignee
Linde GmbH
Mitsubishi Hitachi Power Systems 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 Linde GmbH, Mitsubishi Hitachi Power Systems Europe GmbH filed Critical Linde GmbH
Priority to EP14744776.7A priority Critical patent/EP3030757A2/fr
Publication of EP3030757A2 publication Critical patent/EP3030757A2/fr
Withdrawn legal-status Critical Current

Links

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
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/004—Accumulation in the liquid branch of the circuit
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02K—DYNAMO-ELECTRIC MACHINES
    • H02K7/00—Arrangements for handling mechanical energy structurally associated with dynamo-electric machines, e.g. structural association with mechanical driving motors or auxiliary dynamo-electric machines
    • H02K7/18—Structural association of electric generators with mechanical driving motors, e.g. with turbines
    • H02K7/1807—Rotary generators
    • H02K7/1823—Rotary generators structurally associated with turbines or similar engines
    • 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
    • F01K13/02—Controlling, e.g. stopping or starting
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F02C6/14—Gas-turbine plants having means for storing energy, e.g. for meeting peak loads
    • F02C6/16—Gas-turbine plants having means for storing energy, e.g. for meeting peak loads for storing compressed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0042—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0251—Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/16—Mechanical energy storage, e.g. flywheels or pressurised fluids

Definitions

  • the invention relates to a method for generating electrical energy in a combined power generation plant comprising an air treatment unit and a power plant unit, and a corresponding power generation plant according to the preambles of the independent claims.
  • DE 31 39 567 A1 and EP 1 989 400 A1 disclose using liquid air or liquid nitrogen, ie cryogenic air liquefaction products, for regulating the network and for providing control power in power grids.
  • the air liquefaction product is stored in a tank system with cryogenic tanks. This mode of operation is referred to herein as "liquefaction operation”.
  • the air liquefaction product is withdrawn from the tank system, pressure increased by a pump and warmed to about ambient temperature or higher and thus converted to a gaseous or supercritical state.
  • a thereby obtained high pressure stream is in a power plant unit in an expansion turbine or more expansion turbines with
  • Oxidation reactions is initiated in a gas turbine.
  • the released during the transfer of the air liquefaction product in the gaseous or supercritical state cold can also be stored during the extraction operation and used during the liquefaction operation to provide cold for the recovery of the air liquefaction product.
  • compressed air storage power plants in which the feed air but not liquefied, but compressed in a compressor and in a
  • the compressed air from the cavern is directed into the combustion chamber of a gas turbine.
  • the gas turbine is supplied via a gas line fuel, such as natural gas, and burned in the atmosphere formed by the compressed air.
  • the formed exhaust gas is expanded in the gas turbine, thereby generating energy.
  • the economics of such methods and devices are greatly affected by the overall efficiency.
  • the invention has for its object to improve appropriate methods and devices in their economics.
  • the invention proposes a method for generating electrical energy in a combined power generation plant, which has a
  • Air treatment unit and a power plant unit comprises, and a corresponding power generation plant according to the features of the independent claims before.
  • Preferred embodiments are subject of the dependent claims and the following description.
  • a “power station unit” is understood here to mean a system or a system component which is or is set up for the generation of electrical energy.
  • a Power unit includes at least one expansion turbine, which is coupled to at least one generator. The mechanical power released during the expansion of a fluid in the at least one expansion turbine can be converted into electrical energy in the power station unit.
  • An “air treatment unit” is understood here to mean an installation which is set up for the purpose of obtaining at least one "air liquefaction product" from air. As explained above, this can be an air separation plant which can be set up to obtain corresponding air fractions, or even just a liquefaction unit of such an installation or a dedicated one
  • Air liquefaction product can be obtained, which can be used as a storage liquid and transferred to a tank system.
  • An "air separation plant” is charged with atmospheric air and has a distillation column system for decomposing the atmospheric air into its physical components, particularly nitrogen and oxygen. For this purpose, the air is first cooled to near its dew point and then introduced into the distillation column system.
  • Methods and apparatus for the cryogenic separation of air are known e.g. from Hausen / Linde, cryogenic technology, 2nd edition 1985, Chapter 4 (pages 281 to 337) known.
  • an "air liquefaction plant” does not include
  • Air separation plant with the delivery of an air liquefaction product.
  • air liquefaction product is any product that can be produced, at least by compressing, cooling, and then deflating air in the form of a cryogenic liquid. In particular, it can be at a
  • liquid oxygen and liquid nitrogen in each case also designate a cryogenic liquid which has oxygen or nitrogen in an amount which is above that of atmospheric air. It does not necessarily have to be pure liquids with high contents of oxygen or nitrogen.
  • Under Liquid nitrogen is thus understood to mean either pure or substantially pure nitrogen, as well as a mixture of liquefied air gases whose nitrogen content is higher than that of the atmospheric air. For example, it has a nitrogen content of at least 90, preferably at least 99 mole percent.
  • Air liquefaction product, electricity, etc. is understood to mean a liquid medium whose boiling point is significantly below the respective ambient temperature and, for example, 200 K or less, in particular 220 K or less.
  • Examples are liquid air, liquid oxygen, liquid nitrogen, etc.
  • a “heat exchanger system” is used to transfer heat indirectly between at least two countercurrent streams, such as a warm compressed air stream and one or more cold streams or a cryogenic air liquefaction product, and one or more hot streams.
  • Heat exchanger system may be formed of a single or multiple parallel and / or serially connected heat exchanger sections, e.g. from one or more plate heat exchanger blocks.
  • a "compressor system” is a device designed to compress at least one gaseous stream from at least one inlet pressure at which it is supplied to the compressor system to at least one final pressure at which it is taken from the compressor system.
  • the compressor system forms a structural unit, which, however, can have a plurality of "compressor stages” in the form of known piston, screw and / or Schaufelrad- or turbine assemblies (ie radial or axial compressor stages). In particular, these are
  • Compressor stages by means of a common drive, for example via a common shaft or a common electric motor driven.
  • a common drive for example via a common shaft or a common electric motor driven.
  • compressor systems e.g. a main and a post-compressor one
  • Air treatment unit can together form a "compressor assembly".
  • Expansion turbines or energy converters such as oil brakes, generators or compressor stages can be coupled, is set up to relax a gaseous or at least partially liquid stream.
  • expansion machines or expansion turbines are often referred to as expanders. If one or more expansion turbines designed as a turboexpander are coupled to one or more compressor stages, for example in the form of centrifugal compressor stages, and if necessary mechanically braked, these are, however, operated without externally supplied energy, for example by means of an electric motor
  • boosterturbine used. Such a booster turbine compresses at least one current by the relaxation of at least one other current, but without external, for example by means of an electric motor, supplied energy.
  • a gas turbine may further comprise at least one compressor stage driven by the expansion turbine via a common shaft, typically at least one axial compressor stage. A part of the mechanical energy generated in the expansion turbine is usually used to drive the at least one
  • Compressor stage used. Another part is regularly converted to generate electrical energy in a generator.
  • combustion turbine only the mentioned combustion chamber and one of these downstream expansion turbine.
  • a compressor is usually not provided.
  • a "hot gas turbine” has, in contrast to a gas turbine instead of a
  • a hot gas turbine can be designed in one stage with a heater and an expansion turbine. Alternatively, however, several expansion turbines, preferably with intermediate heating, may be provided. In any case, in particular downstream of the last expansion turbine, a further heater can be provided.
  • the hot gas turbine is also preferably coupled to one or more generators for generating electrical energy.
  • a "heater” is understood to mean a system for indirect heat exchange between a heating fluid and a gaseous fluid to be heated. By means of such a heater, residual heat, waste heat,
  • Process heat, solar heat, etc. transferred to the gaseous fluid to be heated and used to generate energy in a hot gas turbine.
  • a "waste heat steam generator”, also referred to as a heat recovery steam generator (HRSG), is capable of generating steam by heating water or for further heating, e.g. from cold steam to superheated steam, by means of a waste heat stream, for example by means of a still hot or reheated gas stream downstream of a gas turbine or hot gas turbine.
  • HRSG heat recovery steam generator
  • a “tank system” is an arrangement with at least one for storing a cryogenic air
  • Air liquefaction product established cryogenic storage tank understood.
  • a corresponding tank system has insulation means.
  • pressure level and "temperature level” to characterize pressures and temperatures, thereby indicating that corresponding pressures and temperatures in a given plant need not be used in the form of exact pressure or temperature values to realize the innovative concept.
  • pressures and temperatures typically range in certain ranges that are, for example, ⁇ 1%, 5%, 10%, 20% or even 50% about an average.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include unavoidable pressure drops or expected pressure drops, for example, due to cooling effects.
  • pressure levels indicated here in bar are absolute pressures.
  • cryogenic air liquefaction products or corresponding liquid streams are "converted into a gaseous or supercritical state by heating in the context of the present application, this closes on the one hand a regular one
  • Air treatment unit and a power plant unit comprises proposed.
  • a first mode of operation air is sequentially compressed, cooled and depressurized in the air handling unit and used to recover an air liquefaction product.
  • the air liquefaction product is preferably stored in a tank system.
  • an externally provided air liquefaction product for example from a separate air treatment unit, can also be transferred into a corresponding tank system.
  • a second mode of operation is in the air treatment unit a
  • Air liquefaction product evaporated at superatmospheric pressure or
  • a "derived" stream can thereby from the pressure stream by mixing or combining with at least one further stream and / or by at least partial chemical reaction of at least one component of the pressure stream, for example in the form of
  • Combustion reaction as described below with reference to the use of a corresponding pressure flow in a gas turbine or combustion turbine explained.
  • a portion of the pressure stream and / or the pressure stream derived therefrom for example 4 to 5%, is chemically reacted in the combustion chamber with a fuel by the combustion, ie, the fuel is in the combustion chamber with a significantly more than stoichiometric amount of the collection stream implemented therein contained oxygen.
  • the inventive method can also serve as
  • a third mode of operation air is compressed in the air treatment unit and used in the power plant unit to generate electrical energy.
  • the air is thus not liquefied in the third mode of operation but transferred directly under pressure in the power plant unit.
  • the third operating mode allows operation of a corresponding power generation plant even if, for example, no air liquefaction product is available. Although at first glance it may seem unfavorable to first compress air in the third operating mode and then to relax in the power unit, and thereby recover the previously invested electrical energy.
  • the use of a corresponding system can be improved by these measures overall, because the existing hardware components can be better utilized by the third mode of operation.
  • Several of these hardware components, such as heat exchangers and pumps, are used in both the first mode of operation and the second mode of operation. They can also be used in the third operating mode.
  • the third operating mode thus makes it possible, in particular
  • the system components can be operated continuously and gently.
  • the first operating mode is referred to in the context of the present application, as mentioned, as “liquefaction operation”.
  • the second operating mode is referred to in the context of the present application as “removal operation”.
  • the third operating mode in which compressed air from the air treatment unit is transferred directly into the power plant unit, is also referred to as "direct operation" in the context of the present application.
  • the air in the first operating mode which is used to obtain the air liquefaction product, successively in
  • Heat exchanger blocks may be, the first refrigerant is supplied at a first temperature level and after heating (i.e., partial transfer of its cold air) taken at a second temperature level.
  • the second refrigerant becomes part of the heat exchanger system on a third
  • the air liquefaction product is heated in reverse in the second mode of operation, i. one after the other in countercurrent to the second and against the first refrigerant in the heat exchanger system.
  • the second refrigerant is now fed to the heat exchanger system at the fifth temperature level and, after cooling (i.e., taking up refrigeration from the air liquefaction product), is withdrawn partly at the fourth temperature level and partly at the third temperature level from the heat exchanger system.
  • the first refrigerant is the
  • first temperature level (T1) 20 to 50 ° C
  • T2 second temperature level
  • the second and third temperature levels may therefore also correspond to one another in the context of the present invention.
  • two liquid refrigerants are used for cooling the air and heating the air liquefaction product.
  • These may be, for example, liquid or liquefied refrigerants such as lower alcohols and / or saturated or halogenated hydrocarbons such as propane.
  • the first refrigerant advantageously has a higher boiling point than the second refrigerant and is therefore also referred to as a "warm” refrigerant.
  • the second refrigerant is also referred to as a "cold" refrigerant due to its lower boiling point.
  • the heat exchange diagram of a heat exchanger system used can be made particularly favorable.
  • the two liquid refrigerants differ in their chemical composition and in particular in their boiling point.
  • the first liquid refrigerant comes
  • Refrigerants in particular liquefied propane (range up to -170 ° C) are used.
  • liquefied propane range up to -170 ° C
  • the refrigerants for use in the invention are therefore selected in particular on the basis of the particular boiling point. This must be selected so that the refrigerant is liquid in the entire work area.
  • the first (warm) refrigerants also include the lower-valency alcohols listed in the table below. Also suitable are aromatics such as toluene.
  • alkanes and alkenes such as ethane, ethylene, propane, propylene, butane, pentane, hexane etc. and / or their chlorinated and / or fluorinated derivatives (CFCs) can be used as the second (cold) refrigerant.
  • CFCs chlorinated and / or fluorinated derivatives
  • Refrigeration stored in the air liquefaction product will thus be at several
  • Atmospheric air or hot water vapor does not or does not completely lose the liquefaction cold from the air liquefaction product.
  • the number of hardware components such as heat exchangers, turbines and / or compressors is reduced, the costs for the entire power generation plant are reduced and the economy is increased.
  • one or more other refrigerants can be used.
  • the heat exchange diagram can be further optimized; However, the apparatus and control engineering effort is higher. The heating and cooling of the refrigerant is thereby in the
  • Heat exchanger system of the air treatment plant performed anyway for the cooling of the air in the first mode of operation and the warming of the
  • the second refrigerant in the first operating mode is supplied to the heat exchanger system in the form of partial flows at the third temperature level and at the fourth temperature level and to take it in the form of a collecting stream at the fifth temperature level.
  • the partial flows are combined in the heat exchanger system to the collecting stream.
  • the second refrigerant in the second operating mode is advantageously supplied to the heat exchanger system in the form of a collecting stream at the fifth temperature level and withdrawn in the form of partial streams at the fourth temperature level and at the third temperature level.
  • the distribution of the collecting stream in the partial flows takes place in the
  • Heat exchanger system are performed.
  • Particularly advantageous may be, in each case a stream of non-condensing gas in countercurrent to the first and the second refrigerant through the
  • a corresponding non-condensing gas for example nitrogen, can thereby superimpose the respective refrigerant in corresponding refrigerant tanks and be used for pressurizing.
  • the heating of the first liquid refrigerant in the first operating mode is thus preferably carried out in the same passage groups of the heat exchanger system, in which the cooling of the first liquid refrigerant takes place in the second operating mode.
  • the same apparatus can be used in both operating modes. Analogous to this in the first and in the second operating mode, the same pumps are used, one for the transport of the first and the second liquid refrigerant.
  • the first refrigerant is advantageously pumped between two refrigerant tanks (a "cold" refrigerant tank at the first temperature level and a “warm” refrigerant tank at the second temperature level) with a corresponding pumping system.
  • the first liquid refrigerant is pumped out of the cold into the warm refrigerant tank, and vice versa in the second operating mode.
  • the second refrigerant is between three, more precisely between one and two other refrigerant tanks (a "cold” refrigerant tank on the third, a “tempered” refrigerant tank on the fourth and a “warm” refrigerant tank on the fifth temperature level), also with a corresponding pump system, pumped back and forth.
  • the second refrigerant is removed from the cold and tempered refrigerant tank in the form of two partial streams and fed to the heat exchanger system. After heating and possibly merging into a collecting stream, the second refrigerant is transferred to the warm refrigerant tank.
  • the second refrigerant is removed as a collective flow to the warm refrigerant tank and the
  • Heat exchanger system over different heat exchange distances and is therefore cooled differently (to the fourth and the third temperature level).
  • the corresponding partial flows are then transferred in the second operating mode in the tempered and the cold refrigerant tank.
  • Another central aspect of the present invention is the stepwise
  • the air liquefaction product is in particular in the second operating mode heated to a fifth pressure level, which is below the fourth pressure level.
  • At least the fourth or fifth pressure level may be at supercritical pressure.
  • first pressure level (LP) 0 to 2 bar, in particular 1.4 bar
  • second pressure level (MP) 4 to 8 bar, in particular 5.6 bar
  • third pressure level (MP1) 12 to 50 bar, in particular 17 bar
  • fourth pressure level (HP) 50 to 100 bar, in particular 85 bar
  • fifth pressure level (HP1) 50 to 100 bar, in particular 65 bar
  • the compression of the air used to generate the electrical energy may be made in a first proportion to the third
  • Pressure level and a second proportion to the fourth pressure level or to the fifth pressure level are thereby transferred, in particular, separately from one another into the power station unit.
  • This allows a particularly effective operation of a corresponding power generation plant in the third operating mode, because in this case corresponding pressure levels of a power plant unit can be operated particularly efficiently.
  • Only part of the air used must actually be routed through the after-compressor.
  • the main compressor can be operated with a higher compressor capacity and deliver a larger amount of air. The air does not have to be completely recompressed, but can partly be transferred directly to the power plant unit.
  • the power plant unit is operated in the second operating mode and in the third operating mode, wherein in the second operating mode, the air liquefaction product heated under pressure and transferred to the gaseous or supercritical state, preferably at supercritical pressure, is passed through a combustion chamber in the power plant unit in which a fuel is burned.
  • An exhaust gas from the combustion chamber is at the third pressure level according to a first embodiment coupled to a generator
  • Supplied expansion turbine It is therefore a generation of electrical energy by means of a combustion turbine or a gas turbine. It can also be provided that, in the second operating mode, the air liquefaction product heated in the air treatment unit under pressure and transferred into the gaseous or supercritical state is supplied in the power plant unit to a further expansion unit coupled to a generator prior to passing through the combustion chamber at the fifth pressure level.
  • Supplied waste heat steam generator and used there to generate steam can be used.
  • a hot gas turbine as explained above, can be used. This can be used instead of a gas or combustion turbine.
  • one of the portions of the air which is compressed in the third mode of operation to a first proportion to the third pressure level and a second portion to the fourth pressure level or the fifth pressure level, can be pressure-increased by heating.
  • waste heat and / or solar heat can be used.
  • a corresponding heating may also be effected under pressure in the second operating mode in the air treatment unit and converted into the gaseous or supercritical state
  • this may also be formed with an axle or shaft which is equipped with expansion turbines arranged on both sides of the generator.
  • expansion turbines arranged on both sides of the generator.
  • a corresponding power generation plant is in particular configured to perform a corresponding method.
  • Figure 1A shows a power plant according to an embodiment of the
  • FIG. 1B shows the power generation system of FIG. 1A in a second embodiment
  • Figure 1C shows the power plant of Figure 1A in a third
  • FIG. 2A shows a first refrigerant subsystem according to an embodiment of the invention
  • FIG. 2B shows the refrigerant subsystem of FIG. 2A in the second mode of operation.
  • FIG. 3A shows a second refrigerant subsystem according to an embodiment of the invention
  • FIG. 3B shows the refrigerant subsystem of FIG. 3A in the second mode of operation.
  • FIG. 4A shows a power generation plant according to an embodiment of the invention
  • Figure 4B shows the power plant of Figure 4A in the second
  • Figure 4C shows the power plant of Figure 4A in the third
  • Figure 5 shows a heat exchanger system according to an embodiment of the
  • FIG. 6 shows a heat exchanger system according to an embodiment of the invention
  • FIG. 1A shows a power generation plant according to an embodiment of the invention in a first operating mode.
  • This first operating mode corresponds to the liquefaction operation, which has already been explained several times.
  • the term "liquefaction operation” is understood to mean that in the first operating mode, a certain amount of a cryogenic liquefaction product is generated from air and in a tank system
  • a corresponding tank system can also be partially supplied by an externally supplied, cryogenic
  • Air condensing product especially when the capacity of the power generation plant to produce their entire needs for a
  • the power generation plant illustrated in FIG. 1A comprises components of an air treatment unit, which includes dashed lines and are indicated as a whole by 10, as well as components of a power plant unit, which includes dashed lines and are indicated as 20 in total.
  • the power generation plant is designated 100 in total.
  • ambient air AIR is sucked through a filter 1 1 1 via a main compressor system.
  • the air AIR is at a first pressure level LP of typically 0 to 2 bar, for example 1.4 bar.
  • the main compressor system 11 may in particular have a plurality of compressor stages (not described in more detail) which can be driven via a common compressor drive M or a common shaft.
  • a main compressor system 11 may further comprise means for intermediate and post-cooling of a correspondingly stepwise compressed stream. Between the compressor stages, where more
  • the air AIR is at a second pressure level MP of typically 4 to 8 bar, for example, 5.6 bar before.
  • the main compressor system 11 as a whole is designed to compress the air AIR to a third pressure level MP1 of typically 12 to 50 bar, for example 17 bar, at its outlet.
  • a compressed to the third pressure level pressure MP1 stream a is in
  • Purification system 12 transferred, which may have, for example, a filled with a suitable adsorber adsorbent 121.
  • Adsorber essenceer 121 can be cyclically regenerated, which is also in the
  • a correspondingly purified stream b is then fed to a post-compressor system 13 where it is compressed to an even higher fourth pressure level HP of typically 50 to 100 bar, for example 85 bar.
  • the after-compressor system 13 may also have a plurality of compressor stages, which are driven by means of a common compressor drive M.
  • the recompressed stream c is fed to a heat exchanger unit 14, which in the illustrated example comprises a first heat exchanger block 141 and a second heat exchanger block 142.
  • the current c is thereby first by the first Heat exchanger block 141 and then passed through the second heat exchanger block 142.
  • a correspondingly cooled stream d is present. This is essentially still at the fourth pressure level HP before, whereby also caused by the cooling pressure losses, line losses and the like are taken into account.
  • the cooled stream d is then fed to a relaxation device 151, which may comprise, for example, an oil-braked expansion turbine.
  • the expansion device 151 is part of a liquefaction system 15.
  • the flow d is released to a lower pressure level, for example to the second pressure level MP.
  • the current d can be additionally relaxed with a valve not specified here.
  • the relaxed stream d is transferred after the expansion in a separator tank 152, in which a liquid fraction separates on the marsh side. From the top of the separator tank 152, a gaseous fluid (without designation) can be withdrawn. Since this is at the second pressure level MP, it can in the
  • Heat exchanger blocks 142 and 141 of the heat exchanger system 14 is heated and fed back to the main compressor system 11 at an intermediate point.
  • a liquid fraction ie an air liquefaction product of the air AIR, here liquid air LAIR
  • a subcooler 153 On the output side of the subcooler is thereby obtained a cryogenic, liquid stream e, which in a tank system 16 with a
  • Cryogenic tank can be transferred.
  • a further liquefaction product for example liquid air LAIR, can be supplied externally to the tank system 16.
  • the subcooler 153 may be operated with a partial flow of the cryogenic liquid stream e, which is expanded to the first pressure level LP and passed in countercurrent through the subcooler 153.
  • a correspondingly obtained current f can then be warmed in the heat exchanger blocks 142 and 141 of the heat exchanger system 14 and discharged, for example, to the amb environment.
  • the stream f can also upstream of the main compressor system 1 1 again the
  • Main compressor system 1 1 are supplied. For temperature control of the first heat exchanger block 141 and the second
  • a refrigerant system 17 which includes a first refrigerant subsystem 171 and a second refrigerant subsystem 171
  • Refrigerant subsystem 172 includes.
  • the first refrigerant subsystem 171 and the second refrigerant subsystem 172 of the refrigerant system 17 will be explained in detail with reference to the following FIGS. 2A to 3B.
  • FIGS. 2A to 3B already at this point it should be noted that by means of the first refrigerant subsystem 171 in the first
  • a refrigerant flow g of a first liquid refrigerant from the first refrigerant subsystem 171 from the cold end to the warm end through the first heat exchanger block 141 is performed.
  • Refrigerant flow g of the first refrigerant thereby heats up from the first temperature level T1 (see above) to the second temperature level T2 and cools the warm flow c countercurrently.
  • a gaseous stream h which is a superimposed one of the first refrigerant in respective refrigerant tanks of the first refrigerant subsystem 171, is not conducted
  • a current i and a current j of a second liquid refrigerant are supplied to the second heat exchanger block 142 of FIG.
  • Heat exchanger system 14 at its cold end (at the third temperature level T3) and at an intermediate point (at the fourth temperature level T4) supplied.
  • the current i and the current j of the second refrigerant are in the second
  • Heat exchanger block 142 previously heated thereafter, and taken as stream k from second heat exchanger block 142 at its warm end.
  • the second refrigerant heats up to the fifth temperature level T5.
  • a current I is a non-condensing gas that superimposes the second refrigerant i in corresponding storage tanks.
  • FIG. 1A shows the power plant unit 20 of the power generation plant 100 in operation or is operated only by means of externally supplied media. It is therefore explained in the following figures.
  • FIG. 1B shows the power generation plant 100 in a second operating mode. This is the removal operation explained several times, whereby a "removal operation" is understood as an operating mode in which the
  • Power plant 100 no air supplied, but only one
  • Air liquefaction product is removed from a tank system 16.
  • Primary compressor system 1 1 sucked.
  • the cleaning system 12 is in regeneration, wherein a heated stream (see links 3 and 4 and explanations below on the heat exchanger 21 of the power plant unit 20) in countercurrent to that in the first operating mode (see Figure 1A) by a corresponding adsorber tank 121st guided air flows through it and thus dissolves adsorbed components from the adsorber.
  • a corresponding regeneration stream can then be fed again downstream into the air treatment unit 10 or the power plant unit 20 (cf, flow o downstream of the first heat exchanger block 141 in this figure).
  • a current m of a low-temperature liquefaction product here liquid air LAIR
  • the stream m is brought liquid by means of a pump 154 to pressure. Downstream of the pump 154, a corresponding current n is present at a fifth pressure level HP1 of typically 50 to 100 bar, for example a pressure of 65 bar.
  • HP1 typically 50 to 100 bar
  • the stream n is then stored in the heat exchanger system 14, i. successively in the second heat exchanger block 142 and the first heat exchanger block 141, converted into a gaseous or supercritical state, ie vaporized or
  • the current n is typically converted into a supercritical state at a supercritical pressure, ie pseudo-evaporated.
  • the obtained current o is taken from the first heat exchanger block 141 at its warm end.
  • a partial flow can be branched off and later returned (see links 2 and 4), which after heating in the heat exchanger 21 explained below (see links 2 and 3) as regeneration gas in the cleaning system 12 (see links 3 and 4) 4) can be used.
  • the refrigerant system 17 is in the second operating mode of
  • Power generation plant 100 which is shown in Figure 1 B, inversely to the first operating mode, which is shown in Figure 1A, operated. This means that by means of the first refrigerant subsystem 171, a cold center Istrom q of the first refrigerant subsystem 171, a cold center Istrom q of the first refrigerant subsystem 171, a cold center Istrom q of the first refrigerant subsystem 171, a cold center Istrom q of the first
  • Heat exchanger block 141 is guided (a corresponding gas flow r is in
  • Refrigerant subsystem 172 is supplied to the second heat exchanger block 142 at its warm end (at the fifth temperature level T5). This will be split. The obtained substreams t and u are applied to the second heat exchanger block 142 at different colder temperatures, i. taken at the fourth temperature level T4 and at the third temperature level T3.
  • Cold ittelteil system 171 or 172 in the first heat exchanger block 141 and the second heat exchanger block 142 can be cooled in countercurrent to the current n.
  • the use of the refrigerant 17 thus allows the storage of the released during the evaporation or pseudoevaporation of the current n cold.
  • the current o can with the corresponding pressure, i. at the fifth pressure level HP1, are discharged from the air treatment unit 10 and transferred to the power plant unit 20.
  • the power station unit 20 has at least two fluid inputs 20a and 20b, wherein the current a is supplied to the fluid inlet 20a in the second operating mode illustrated in FIG. 1B. In the second operating mode shown in FIG. 1B, the fluid input 20b is not active or is not operated in the second operating mode.
  • the current o is passed through a heat exchanger 21 of the power plant unit 20 and heated there in countercurrent to exhaust gas of a gas turbine unit explained below.
  • Cleaning system 12 are heated as previously stated (see links 2 and 3). After heating in the heat exchanger 21 of the power plant unit 20, the flow is relaxed in an expansion turbine 23, which is coupled to a generator G. The relaxed stream o can then in another
  • Heat exchanger 22 is heated and passed through a combustion chamber 25.
  • a suitable fuel F for example natural gas
  • This site also other streams, such as an oxygen-enriched stream to be fed.
  • This can be an expansion turbine 24, which may also be coupled to a generator G, supplied.
  • the expansion turbines 23 and 24 may also be coupled to a common generator G. By relaxing in the expansion turbines 23 and 24, electrical energy is generated in the generators.
  • FIG. 1 C shows the power generation system of Figures 1A and 1B previously explained in a third mode of operation.
  • This third mode of operation is, as explained, referred to as direct mode in the context of this application.
  • the term "direct operation" means that in the main compressor system 1 1 and in the Nachverêtrsystem 13 compacted streams, here denoted by w and x, with the corresponding
  • Pressure level HP (power w) are transferred directly into the power plant unit 20. This direct operation permits operation of the power generation plant 100 even when the heat exchanger system 14 and / or the liquefaction system 15 are not in operation and thus no corresponding current o (see Figure 1 B) is ready.
  • Pressure level HP is now first passed through the expansion turbine 23 and then combined at a correspondingly reduced pressure level with the flow x at the third pressure level MP1.
  • a collecting stream obtained thereby is guided through the combustion chamber 25 and through the expansion turbine 24.
  • the first refrigerant subsystem 171 includes a first (cold) refrigerant tank 171 a and a second (warm) refrigerant tank 171 b.
  • the refrigerant used is respectively in liquid form and is superimposed with a corresponding non-condensing gas to ensure a sufficient pressurization of the refrigerant.
  • the non-condensing gas may be, for example, nitrogen.
  • a pump 171 p is provided.
  • Refrigerant subsystem 171 transferred. As a result, the stream c can be cooled.
  • Figure 2B shows the reverse operation of the first refrigerant subsystem 171 as implemented in the second mode of operation.
  • a current n in the first heat exchanger block 141 is evaporated or pseudo-evaporated.
  • a corresponding refrigerant flow q of the first refrigerant is generated in the first refrigerant subsystem 171 by adding refrigerant from the second
  • FIGS. 3A and 3B respectively show the second refrigerant subsystem 172 of the refrigerant system 17. In the second refrigerant subsystem 172, there are three
  • Refrigerant tanks a first (cold) refrigerant tank 172a, a second (tempered) refrigerant tank 172b and a third (warm) refrigerant tank 172c are provided. These are for storing a second refrigerant having different temperatures (first refrigerant tank 172a: third temperature level T3, second refrigerant tank 172b: fourth temperature level T4, third refrigerant tank 172c: fifth)
  • Heat exchanger system 14 two pumps 172p and 172q are provided in the illustrated example.
  • Non-condensing gas which is the second refrigerant here in the
  • Refrigerant tanks 172a to 172c superimposed produced. Accordingly, in the second operating mode (FIG. 3B), the currents or partial flows of the second refrigerant s, t, u or the flow of the noncondensing gas v are generated. The stream c and the stream n to be evaporated or pseudo evaporated are also indicated.
  • Refrigerant tank 171 a of the first refrigerant subsystem 171 has a lower temperature than the first refrigerant in the second refrigerant tank 171 b of the first
  • the second refrigerant subsystem 172 is the
  • FIGS. 4A to 4C a power generation plant according to a further embodiment of the invention is shown schematically and designated overall by 200.
  • Figure 4A corresponds to the first mode of operation
  • Figure 4B the second mode of operation
  • Figure 4C the third mode of operation.
  • the operation of the power plant 200 partially corresponds to that of
  • the refrigerant system 17 may be formed identically as there, and may include, for example, the refrigerant subsystems 171 and 172 shown in FIGS. 2A to 3B previously explained.
  • the power generation plant 200 differs essentially from the power generation plant 100 in that the heat exchanger system 14 additionally has expansion facilities 143 and 144. For each of the stream c, which is provided here in a larger amount, partial streams can be branched off (without designation). These partial flows can be found in the
  • Relaxation devices 143 and 144 which may have, for example, expansion turbines, which are each coupled to a generator G, relaxed. Instead of a generator G, an oil brake or another braking device can also be provided in the expansion devices 143 and 144 in each case.
  • the partial flows are relaxed, for example, from the fourth pressure level HP to the third pressure level MP1.
  • the heated streams can be combined and re-upstream into the air treatment unit
  • the feed can, for example, in the form of a feed upstream of the main compressor system 1 1, at an intermediate point of the
  • Main compressor system 1 or upstream of the Nachver Whyrsystems 13 done (see link 1).
  • the additional expansion devices 143 and 144 can generate additional refrigeration, whereby a larger amount of feed air AIR can be liquefied by means of the liquefaction system 15.
  • Power plant 200 is more likely than power plant 100 to be able to meet the demand for air liquefaction product LAIR in the second
  • Operating mode consists of cover.
  • the power generation plant 200 may also be externally supplied with an air liquefaction product.
  • the second mode of operation of the power plant 200 shown in FIG. 4B and the third mode of operation of the power plant 200 shown in FIG. 4C are substantially correspond to the respective operating modes of the
  • Air liquefaction product LAIR be waived.
  • the relaxation devices 143 and 144 are not active in the second and third modes of operation.
  • FIG. 5 shows a further alternative embodiment of a heat exchanger system 14. This can be used as an alternative to the heat exchanger systems 14 shown in FIGS. 1A to 1C and 4A to 4C, respectively.
  • Figure 5 is the first
  • a corresponding heat exchanger system 14 also has corresponding first and second heat exchanger blocks 141 and 142 which are connected to a refrigerant system 17 (not shown). Parallel to the first heat exchanger block 141 and the second heat exchanger block 142 further heat exchanger blocks 141 a and 142 a are provided.
  • the current c can in the
  • Partial flows c1 and c2 split and, as shown, in the first heat exchanger block 141 and the other heat exchanger block 141a are fed.
  • a partial flow of the second partial flow c2 can be in a relaxation device 143 and 144, for example, also an expansion turbine, which is coupled to a generator G, relaxed.
  • the embodiment of the heat exchanger system 14 illustrated in FIG. 5 differs therewith essentially from the previously explained embodiment, which is shown in FIGS. 4A to 4C, in that the heat exchanger blocks 141 a and 142 a are separated from the heat exchanger blocks 141 and 142.
  • FIG. 6 shows a further embodiment of a heat exchanger system 14, which can likewise be used as an alternative to the possibilities explained above in a corresponding energy generation plant 100 or 200. However, FIG. 6 shows the second operating mode. Again, here are
  • Relaxation devices 143 and 144 are provided, which are operated during this second mode of operation. These too can over

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Power Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un procédé de production d'énergie électrique dans une installation de production d'énergie combinée (100, 200) qui comprend une unité de traitement d'air (10) et une centrale (20). Dans un premier mode de fonctionnement, de l'air (AIR) est liquéfié pour donner un produit de liquéfaction d'air (LAIR) et, dans un deuxième mode de fonctionnement, ce produit de liquéfaction d'air (LAIR) est converti à un état gazeux ou supercritique dans lequel il est introduit dans la centrale (20) et utilisé pour produire de l'énergie électrique. Dans un troisième mode de fonctionnement, de l'air (AIR) est comprimé dans l'unité de traitement d'air (10) et utilisé directement dans la centrale (20) pour produire de l'énergie électrique. Selon l'invention, l'air (AIR) est refroidi dans le premier mode de fonctionnement par deux réfrigérants liquides à plusieurs niveaux de température (T1 ‑ T5) et le produit de liquéfaction d'air (LAIR) est chauffé de manière correspondante. En outre, dans le premier mode de fonctionnement, l'air (AIR) est comprimé par paliers à plusieurs niveaux de pression (LP, MP, MP1, HP). Dans le deuxième mode de fonctionnement, le produit de liquéfaction d'air (LAIR) est également chauffé à un autre niveau de pression (HP1) et introduit à ce niveau à l'état gazeux dans la centrale (20). Enfin, dans le troisième mode de fonctionnement, l'air (AIR) est introduit dans la centrale (20) sous forme de portions séparées et à des niveaux de pression (MP1, HP ou HP1) différents. L'invention concerne également une installation de production d'énergie (100, 200) correspondante.
EP14744776.7A 2013-08-09 2014-07-29 Procédé de production d'énergie électrique et installation de production d'énergie Withdrawn EP3030757A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP14744776.7A EP3030757A2 (fr) 2013-08-09 2014-07-29 Procédé de production d'énergie électrique et installation de production d'énergie

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP13003986.0A EP2835507B1 (fr) 2013-08-09 2013-08-09 Procédé pour la production d'énergie électrique et installation de production d'énergie
EP14744776.7A EP3030757A2 (fr) 2013-08-09 2014-07-29 Procédé de production d'énergie électrique et installation de production d'énergie
PCT/EP2014/002075 WO2015018505A2 (fr) 2013-08-09 2014-07-29 Procédé de production d'énergie électrique et installation de production d'énergie

Publications (1)

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EP3030757A2 true EP3030757A2 (fr) 2016-06-15

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EP13003986.0A Not-in-force EP2835507B1 (fr) 2013-08-09 2013-08-09 Procédé pour la production d'énergie électrique et installation de production d'énergie
EP14744776.7A Withdrawn EP3030757A2 (fr) 2013-08-09 2014-07-29 Procédé de production d'énergie électrique et installation de production d'énergie

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US (1) US10177629B2 (fr)
EP (2) EP2835507B1 (fr)
ES (1) ES2608643T3 (fr)
PT (1) PT2835507T (fr)
WO (1) WO2015018505A2 (fr)

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EP3032203A1 (fr) * 2014-12-09 2016-06-15 Linde Aktiengesellschaft Procédé et installation combinée destinés à stocker et à récupérer l'énergie
GB2537125A (en) * 2015-04-07 2016-10-12 Isentropic Ltd Liquid air energy storage system
DE102015206723A1 (de) * 2015-04-15 2016-10-20 Siemens Aktiengesellschaft Verfahren zum Betrieb einer Kraftwerksanlage an Standorten mit zu geringer Brennstoffversorgung
EP3293475A1 (fr) * 2016-09-07 2018-03-14 Linde Aktiengesellschaft Procédé et appareil de stockage et de récupération d'énergie
US10539364B2 (en) * 2017-03-13 2020-01-21 General Electric Company Hydrocarbon distillation
US20220320555A1 (en) * 2021-03-31 2022-10-06 Jay Stephen Kaufman Fuel Cell Generator with Cryogenic Compression and Co-Generation of Liquefied Air
EP4124726A1 (fr) * 2021-07-29 2023-02-01 TotalEnergies OneTech Installation de production d'électricité et de chaleur, comprenant une unité de turbine à gaz
US12258884B1 (en) * 2024-04-24 2025-03-25 Bayram ARI Power machine

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Publication number Publication date
US10177629B2 (en) 2019-01-08
US20160190896A1 (en) 2016-06-30
WO2015018505A2 (fr) 2015-02-12
EP2835507B1 (fr) 2016-09-21
EP2835507A1 (fr) 2015-02-11
PT2835507T (pt) 2016-12-29
ES2608643T3 (es) 2017-04-12
WO2015018505A3 (fr) 2015-04-16

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