US20150192330A1 - Method and device for generating electrical energy - Google Patents

Method and device for generating electrical energy Download PDF

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Publication number
US20150192330A1
US20150192330A1 US14/418,482 US201314418482A US2015192330A1 US 20150192330 A1 US20150192330 A1 US 20150192330A1 US 201314418482 A US201314418482 A US 201314418482A US 2015192330 A1 US2015192330 A1 US 2015192330A1
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liquid
air
heat exchanger
transfer medium
operating mode
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US14/418,482
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Alexander Alekseev
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Linde GmbH
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Linde GmbH
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Publication of US20150192330A1 publication Critical patent/US20150192330A1/en
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    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/14—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the cycle used, e.g. Stirling 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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B11/00—Compression machines, plants or systems, using turbines, e.g. gas turbines
    • F25B11/02—Compression machines, plants or systems, using turbines, e.g. gas turbines as expanders
    • 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
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    • 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
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    • 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
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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
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    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
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    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
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    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation

Definitions

  • the invention relates to a method and an apparatus for generating electrical energy as per the preamble of patent claim 1 and also to a corresponding apparatus.
  • a “cryogenic liquid” is understood to be a liquid the boiling point of which is below ambient temperature and is for example 220 K or lower, in particular lower than 200 K.
  • cryogenic liquid In its function as a “high-pressure stream”, the cryogenic liquid may be at subcritical pressure during “vaporization”. However, if the cryogenic liquid is brought to a superatmospheric pressure, which is above the critical pressure, there is no real phase change (“vaporization”), but rather what is termed “pseudo-vaporization”.
  • the “heat exchanger system” serves to cool feed air for the air treatment plant in indirect heat exchange with one or more cold streams. It may be formed from a single heat exchanger portion or a plurality of heat exchanger portions connected in parallel and/or in series, for example from one or more plate heat exchanger blocks.
  • the cryogenic liquid at a very high pressure (200 bar) is brought into indirect heat exchange firstly with a first liquid refrigeration transfer medium in the heat exchanger system, and in the process is warmed up to about ambient temperature, is then expanded in an expansion turbine to the lower pressure (10 to 15 bar) and thereby cooled (to approximately ⁇ 150° C.), and is then brought into indirect heat exchange with the second liquid refrigeration transfer medium, and warmed again in the process.
  • the cryogenic liquid is therefore brought into heat exchange with two liquid refrigeration transfer media at differing temperature, which emit sensible heat in the process.
  • both refrigeration transfer media remain liquid.
  • the refrigeration of the cryogenic liquid is therefore transferred to the two refrigeration transfer media at two different temperature levels, and is available again for generating the cryogenic liquid during the first operating mode.
  • a heat transfer medium such as atmospheric air or hot (water) vapor
  • the liquefaction refrigeration from the cryogenic storage liquid is not lost or is not entirely lost as a result.
  • Two refrigeration transfer media are required in this method owing to the intermediate expansion in an expansion turbine, since in this operation the generation of the mechanical energy is accompanied by cryogenic cooling of the working fluid.
  • the first phase (energy storage/liquefaction) of the method according to US 2001004830 A1 also consists of a plurality of steps: the incoming air (10 to 15 bar) is firstly brought into indirect heat exchange with the second liquid refrigeration transfer medium and cooled (to ⁇ 150° C.), is then compressed (to 40 bar), is thereby warmed ( ⁇ 60° C. at the outlet), and is then brought into indirect heat exchange with the first liquid refrigeration transfer medium and cooled again (to ⁇ 170° C.)
  • the invention is based on the object of improving a system of this type in terms of its economic viability and in particular of making a relatively simple design in terms of apparatus possible.
  • the feed air compressed in the air compression unit passes into indirect heat exchange with the first liquid refrigeration transfer medium and with the second liquid refrigeration transfer medium at the same pressure in the heat exchanger system. It is therefore the case that no machine needs to be used for increasing the pressure between the heat exchange with the first refrigeration transfer medium and the heat exchange with the second refrigeration transfer medium.
  • the two refrigeration transfer media are warmed in the first operating mode to the same temperature level T 2 or T 4 , from which they are cooled in the second operating mode. Conversely, they are cooled in the second operating mode to the same temperature T 1 or T 3 , from which they are warmed in the first operating mode.
  • the same temperature level is to be understood as meaning not only exactly the same temperature, but also a temperature band with a range of up to 20 K. It is of course desirable to achieve the smallest possible temperature difference between the two operating modes.
  • the heat exchange diagram of the heat exchanger system can have a particularly favorable configuration.
  • the temperature levels preferably lie in the following ranges:
  • the two refrigerants differ in their chemical composition, in particular in their boiling point. They have to be selected in such a way that they are liquid throughout the respective working range. Suitable for this purpose are, for example, ethanol (C 2 H 5 OH) as the first (hotter) refrigeration transfer medium and propane (C 3 H 8 ) as the second (cooler) refrigeration transfer medium. Moreover, the substances indicated in the table below are suitable in the invention for use as the first or second refrigeration transfer medium.
  • liquid refrigeration transfer media and also the mixtures thereof can also be used in the invention.
  • the heat exchange diagram can be optimized further; however, the complexity in terms of apparatus and control is also increased.
  • refrigeration transfer medium cooled in the second operating mode is available at the same temperature level for the first operating mode for cooling (and vice versa).
  • the warming and cooling of the refrigeration transfer media is carried out here in the heat exchanger system of the air treatment plant, which is present in any case for the cooling of the feed air in the first operating mode and the warming of the cryogenic liquid in the second operating mode.
  • mechanical energy is generated from the high-pressure storage fluid in the second operating mode by either the storage fluid itself or a fluid derived therefrom being expanded in the gas expansion unit so as to perform work.
  • the fluid derived therefrom may be formed for example by a mixture of the storage fluid with one or more other fluids, or by a reaction product of the storage fluid with one or more other substances.
  • the latter may be formed for example by combustion exhaust gas if the storage fluid contains oxygen and is used for the combustion of a fuel.
  • the warming of the first refrigeration transfer medium in the first operating mode is preferably carried out in the same groups of passages of the heat exchanger system, in which the cooling of the first refrigeration transfer medium in the second operating mode is preferably carried out in the same groups of passages of the heat exchanger system, in which the cooling of the second refrigeration transfer medium in the second operating mode is carried out in the same groups of passages of the heat exchanger system. It is therefore possible for the same apparatus to be used in both operating modes.
  • the same pumps can be used in the first and in the second operating mode, in each case one for transporting the first and the second refrigeration transfer medium.
  • the temperature ranges of the two refrigeration transfer media can in principle be disjoint (T 4 ⁇ T 1 ). It is preferable, however, that they overlap, in that the first temperature level T 1 is more than 18 K, in particular 20 to 70 K, below the fourth temperature level T 4 . This makes it possible to particularly effectively optimize the heat exchange diagram.
  • the air compression unit can be switched off in the second operating mode; in this case, heat for the (pseudo-)vaporization of the cryogenic liquid is supplied exclusively by the natural gas to be liquefied.
  • feed air is compressed in the air compression unit and cooled in the heat exchanger system in the second operating mode, too.
  • the air compression unit does not have to be switched off and on when switching over between the operating modes, but instead continues to operate continuously.
  • the quantity of compressed feed air can be obtained as high-pressure gas and electrical energy can additionally be obtained therefrom.
  • a “gas turbine system” has a gas turbine (gas turbine expander) and a combustion chamber. In the gas turbine, hot gases from the combustion chamber are expanded so as to perform work.
  • the gas turbine system may also have a gas turbine compressor driven by the gas turbine. Some of the mechanical energy generated in the gas turbine is commonly used to drive the gas turbine compressor. More of the mechanical energy is regularly converted in a generator to generate electrical energy.
  • At least part of the generation of mechanical energy from the gaseous high-pressure storage fluid is performed in the gas turbine system of the power plant, that is to say in an apparatus present in any case in the power plant for converting pressure energy into mechanical drive energy.
  • an additional separate system for the work-performing expansion of the high-pressure storage fluid may be of less complex design or may be dispensed with entirely.
  • the high-pressure storage fluid is then fed to the gas turbine system, for example at the pressure at which it is (pseudo-)vaporized.
  • the gas expansion unit has a hot-gas turbine system having at least one heater and a hot-gas turbine.
  • the generation of electrical energy from the gaseous high-pressure storage fluid is carried out here at least partially as work-performing expansion in a hot-gas turbine system which has at least one heater and a hot-gas turbine.
  • the generation of energy from the high-pressure storage fluid takes place outside the gas turbine system.
  • the “hot-gas turbine system” may be formed with a single stage with a heater and a single-stage turbine. Alternatively, it may have a plurality of turbine stages, preferably with intermediate heating. It is expedient in any case to provide a further heater downstream of the last stage of the hot-gas turbine system.
  • the hot-gas turbine system is preferably coupled to one or more generators for generating electrical energy.
  • a “heater” is understood here to be a system for the indirect heat exchange between a heating fluid and the gaseous storage fluid. It is thus possible to transfer residual heat or waste heat to the storage fluid and to use this heat for generating energy in the hot-gas turbine system.
  • the two variants may also be combined by the gas expansion unit having one or more hot-gas turbines as well as one or more gas turbine systems.
  • the gaseous high-pressure storage fluid is then expanded in two steps, the first step being carried out as a work-performing expansion in the hot-gas turbine system and the second step being carried out in the gas turbine system, the gaseous high-pressure storage fluid being fed to the hot-gas turbine system, where it is expanded to an intermediate pressure, and a gaseous intermediate-pressure storage fluid being removed from the hot-gas turbine system and finally being fed to the gas turbine system.
  • the air treatment plant in which the cryogenic liquid is generated in the first operating mode, can be in the form of a cryogenic air separation plant or of an air liquefaction plant.
  • a “cryogenic air separation plant” is charged with atmospheric air and has a distillation column system for separating atmospheric air into its physical components, in particular into nitrogen and oxygen. To this end, the feed air is firstly cooled close to its dew point and is then introduced into the distillation column system.
  • the distillation column system of the invention can be in the form of a one-column system for nitrogen-oxygen separation, in the form of a two-column system (for example in the form of a conventional Linde double column system) or else in the form of a three-column system or multi-column system.
  • it can have further apparatuses for the recovery of high-purity products and/or other air components, in particular noble gases, for example argon recovery and/or krypton-xenon recovery.
  • An “air liquefaction plant” does not contain any distillation column part. Otherwise, the structure thereof corresponds to that of a cryogenic air separation plant, with the delivery of a liquid product. It goes without saying that liquid air can also be generated as a byproduct in a cryogenic air separation plant.
  • the cryogenic liquid can be formed by liquefied air and/or liquid nitrogen, or in general terms by a fluid which contains less oxygen than the atmospheric air. It is also possible for a combination of two or more storage fluids of identical or differing composition from the same air treatment plant or from a plurality of air treatment plants to be used within the context of the invention.
  • “Nitrogen” is understood here to be both pure or substantially pure nitrogen and a mixture of air gases, the nitrogen content of which is higher than that of the atmospheric air.
  • the liquid nitrogen has a nitrogen content of at least 90%, preferably at least 99% (all percentages relate here and hereinbelow to the molar quantity, unless specified otherwise).
  • the high-pressure stream passes into indirect heat exchange with the second liquid refrigeration transfer medium and with the first liquid refrigeration transfer medium at the same superatmospheric pressure in the heat exchanger system ( 21 ). It is therefore the case that no machine needs to be used for increasing the pressure between the heat exchange with the second refrigeration transfer medium and the heat exchange with the first refrigeration transfer medium.
  • the invention also relates to an apparatus for generating energy as per patent claim 12 .
  • a “control device” is to be understood here to be an apparatus which automatically controls the system at least during the first operating mode and during the second operating mode. It is preferably capable of automatically carrying out the transition from the first operating mode to the second operating mode, and vice versa.
  • the apparatus according to the invention may be complemented by apparatus features which correspond to the features of the dependent method claims.
  • FIGS. 1 a and 1 b show the basic principle of the invention, respectively in the first and second operating mode
  • FIGS. 2 a and 2 b show a detailed illustration of a first embodiment of an air treatment plant which can be used in the invention
  • FIGS. 3 a and 3 b show a detailed illustration of a second embodiment of an air treatment plant which can be used in the invention.
  • FIG. 4 shows possible embodiments of the gas expansion unit.
  • the overall plant in FIGS. 1 a and 1 b consists of three units: an air treatment plant 100 , a liquid tank 200 and a gas expansion unit 300 .
  • FIG. 1 a shows the first operating mode (cheap power phase—generally at night).
  • atmospheric air AIR
  • a cryogenic liquid 101 which is formed for example as liquid air, is produced in the air treatment plant.
  • the air treatment plant is operated as a liquefier (in particular as an air liquefier).
  • the cryogenic liquid 101 is introduced into the liquid tank 200 , which is operated at a low pressure LP of less than 2 bar.
  • the feed air is sucked in via a filter 1 by an air compression unit 2 and compressed to a pressure MP (4 to 8 bar, in particular 5 to 8 bar), cooled in a pre-cooling device 3 and dried in a molecular sieve adsorber station 4 and purified of contaminants such as CO 2 and hydrocarbons.
  • the compressed and purified air is cooled and liquefied in a heat exchanger system 21 .
  • the cryogenic liquid 101 is conducted into the liquid tank 200 (the heat exchanger system 21 is shown only in a very schematic manner in FIGS. 1 a and 1 b ; further details are shown in FIGS. 2 a to 3 b ).
  • a first cold refrigeration transfer medium store 151 contains liquid ethanol (C 2 H 5 OH) as the “first refrigeration transfer medium” at a first temperature level T 1 of ⁇ 110° C. and at a low pressure of less than 2 bar.
  • the liquid first refrigerant is fed via a line 161 at T 1 into a first passage group of the heat exchanger system 21 by means of a first refrigeration transfer medium pump 29 .
  • a first refrigeration transfer medium pump 29 At the hot end of the heat exchanger system 21 , it is removed again—still in a liquid state—at a second, higher temperature level T 2 of 19° C. and introduced into a first hot refrigeration transfer medium store 152 , which is operated at the second temperature level and likewise at a low pressure of less than 2 bar.
  • a second cold refrigeration transfer medium store 153 contains liquid propane (C 3 H 8 ) as the “second refrigeration transfer medium” at a third temperature level T 3 of ⁇ 180° C. and at a low pressure of less than 2 bar.
  • the liquid second refrigerant is fed via a line 163 at T 3 into a second passage group of the heat exchanger system 21 , that is to say at the cold end thereof, by means of a second refrigeration transfer medium pump 28 .
  • a second refrigeration transfer medium pump 28 At an intermediate point of the heat exchanger system 21 , it is removed again—still in a liquid state—at a fourth, higher temperature level T 4 of ⁇ 90° C. and introduced into a second hot refrigeration transfer medium store 154 , which is operated at the fourth temperature level and likewise at a low pressure of less than 2 bar.
  • FIG. 1 b shows the second operating mode (peak power phase—generally during the day).
  • the cryogenic liquid 103 for example liquid air
  • HP 1 is greater than 12 bar, for example approximately 60 bar
  • a pump 27 vaporized in the air treatment plant as a “high-pressure stream” and warmed to approximately ambient temperature and drawn off as a gaseous high-pressure storage fluid 104 .
  • the vaporized high-pressure storage fluid 104 is conducted at the pressure HP 1 to the gas expansion unit 300 .
  • the power P 3 which is available at the gas expansion unit 300 in the second operating mode is for example 20 to 70%, preferably 40 to 65%, of the power P 1 which is consumed in the first operating mode by the air treatment plant 100 .
  • the heat required for the vaporization of the high-pressure stream is supplied by the two refrigeration transfer media, which are delivered through the same groups of passages of the heat exchanger system 21 as in the first operating mode, but in the reverse direction.
  • the first refrigerant is conveyed via the pump 29 and a line 162 from the first hot refrigeration transfer medium store 152 to the hot end of the heat exchanger system, and, after cooling from the second temperature level T 2 to the first temperature level T 1 , is introduced via a line 164 into the first cold refrigeration transfer medium store 151 .
  • the second refrigerant is conveyed via the pump 28 and the line 164 from the second hot refrigeration transfer medium store 154 to the heat exchanger system 21 , and, after cooling from the fourth temperature level T 4 to the third temperature level T 3 , is introduced via the line 163 into the second cold refrigeration transfer medium store 153 .
  • the vaporization refrigeration of the cryogenic liquid 103 is stored as sensible heat in the refrigeration transfer media and is available again in the first operating mode for generating cryogenic liquid.
  • the production of the cryogenic liquid and the transfer of heat to the refrigeration transfer media on the one hand and the vaporization of the high-pressure stream of cryogenic liquid and the transfer of refrigeration to the refrigeration transfer media on the other hand are carried out in the same process units.
  • the same apparatuses can therefore be used in the first and second operating mode. This gives rise to a relatively low complexity in terms of apparatus.
  • the air compression unit 2 can be switched off during the second operating mode (see FIG. 2 b at the bottom); in a second embodiment variant ( FIG. 3 b at the bottom), it continues to operate in the second operating mode too and supplies additional compressed air into the line 104 to the gas expansion unit 300 .
  • a liquefaction phase (continuous operation in the first operating mode) and a vaporization phase (continuous operation in the second operating mode) can each last for one to ten hours. Over the course of a day, one or more vaporization and respectively liquefaction phases can be carried out. Depending on demand, the air treatment plant can be switched off in the period of time of transition between two such respective phases.
  • FIGS. 2 a and 2 b show a possible design of the air treatment plant 100 shown in FIG. 1 , which here is in the form of an air liquefier.
  • FIG. 2 a shows in turn the first operating mode (the liquefaction phase).
  • ambient air AIR
  • MP 4 to 8 bar, in particular 5 to 8 bar
  • the compressed and purified air at MP is split into a first partial stream and a second partial stream.
  • the first partial stream is conducted to a separate compressor, the circuit compressor 11 , where it is compressed from the pressure MP to a higher pressure HP 2 of 50 to 100 bar, is cooled in an aftercooler to approximately ambient temperature and is then cooled and pseudo-liquefied at HP 2 in the heat exchanger system 21 , is expanded in a throttle valve to the pressure MP and finally is fed in an at least partially liquid state into a phase separating device (separator) 23 .
  • the gaseous fraction from the phase separating device 23 is conducted through the heat exchanger system 21 , where it is warmed, and is guided together with the air from the molecular sieve adsorber station 4 to the suction pipe of the circuit compressor 11 , and thereby forms an air circuit.
  • the second partial stream is post-compressed to a still higher pressure MP 2 in a post-compressor 6 a having an aftercooler and is then cooled in the heat exchanger system 12 from approximately ambient temperature to a first intermediate temperature of 140 to 180 K.
  • a turbine 5 b the second partial stream is expanded to the low pressure LP (LP ⁇ 2 bar) so as to perform work.
  • the post-compressor 5 a is driven by the turbine 12 b via a common shaft.
  • the second partial stream of the feed air which is expanded to perform work is warmed again to ambient temperature in the heat exchanger system 21 and released into the atmosphere (amb).
  • a partial quantity can also be used as regenerating gas for the molecular sieve adsorber station 4 .
  • the regenerating gas is warmed by steam, an electric heater or natural gas firing (quantity of heat Q).
  • the molecular sieve adsorber station 4 is not regenerated at all during the first operating mode, but rather merely in the second operating mode. If the continuous operation in the first operating mode lasts for less than approximately 6 hours, this is readily possible.
  • the molecular sieve adsorber station is then not switched over within an operating mode; it can then also be realized by means of a single adsorber container or by means of a plurality of containers which are operated in parallel.
  • the liquid from the phase separating device 23 is subcooled in a subcooler 24 and conducted for the most part ( 101 ) as a cryogenic liquid into the liquid tank 200 .
  • a partial quantity 26 of liquid air which is removed after the subcooling 24 , is expanded in a throttle valve 25 to the pressure LP and is conducted together with the turbine exhaust gas through the heat exchanger system 21 .
  • the second operating mode will now be described with reference to FIG. 2 b .
  • the turbine 5 b , the post-compressor 5 a, the circuit compressor 11 , the air compression unit 2 and the Joule-Thomson stage are switched off.
  • Liquid air (LAIR) 103 is removed from the liquid tank 200 , is brought to the required pressure HP 1 of for example 50 to 80 bar, preferably 40 to 80 bar, in the pump 27 , and is introduced as a high-pressure stream into the heat exchanger system 21 , where it is pseudo-vaporized and warmed to approximately ambient temperature.
  • the pseudo-vaporized air is finally conducted as a gaseous high-pressure storage fluid 104 to the gas expansion unit 300 .
  • the two refrigeration transfer medium streams are cooled in countercurrent to the (pseudo-)vaporizing air 103 , as described above in relation to FIG. 1 b.
  • some of the gaseous high-pressure storage fluid 104 , some of the gaseous high-pressure storage fluid heated in the gas expansion unit 300 or some of the exhaust gas of the gas expansion unit 300 can be used as regenerating gas (not shown in the drawing).
  • the heat exchanger system 21 of the air treatment plant is used both for the air liquefaction and refrigeration transfer medium heating (in the first operating mode) and for the air vaporization and refrigeration transfer medium cooling (in the second operating mode).
  • the second variant of the invention is operated like the first variant ( FIG. 1 a ).
  • FIG. 3 b corresponds substantially to FIG. 1 b , but here the air compression unit 2 , the circuit compressor and the turbine/post-compressor combination 5 a / 5 b continue to operate in the second operating mode, too.
  • FIG. 4 shows possible embodiments of the gas expansion unit 300 .
  • a conventional gas turbine is used for the expansion, the compressed air from the air treatment plant being introduced into the gas turbine upstream of the combustion chamber.
  • the heat of the flue gas at the outlet can be used in a heat recovery steam generator (HRSG) ( 4 a ); alternatively, it is used in another way, for example to preheat the compressed air from the air treatment plant ( 4 b ).
  • HRSG heat recovery steam generator
  • a converted gas turbine is used for the expansion; in this gas turbine, the compressor part is removed.
  • the compressed air from the air treatment plant is introduced into the combustion chamber of the rest of the gas turbine.
  • the heat of the flue gas can be used in a similar manner to the method with the gas turbine.
  • the compressed air from the air treatment plant is firstly warmed and expanded in a plurality of successive turbines/turbine stages, the air being additionally warmed between the individual expansion stages.
  • the embodiment variants 4 a and 4 b and also 4 c and 4 d may be combined with one another.

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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)
  • Separation By Low-Temperature Treatments (AREA)
  • Motor Or Generator Cooling System (AREA)
US14/418,482 2012-08-02 2013-08-02 Method and device for generating electrical energy Abandoned US20150192330A1 (en)

Applications Claiming Priority (3)

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EP12005617.1 2012-08-02
EP12005617 2012-08-02
PCT/EP2013/002305 WO2014026738A2 (fr) 2012-08-02 2013-08-02 Procédé et dispositif servant à produire de l'énergie électrique

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WO2022064533A1 (fr) * 2020-09-25 2022-03-31 Energy Dome S.P.A. Centrale et procédé de stockage d'énergie
WO2023244883A1 (fr) 2022-06-16 2023-12-21 Praxair Technology, Inc. Système et procédé de stockage d'énergie d'azote liquide
US12607399B2 (en) 2022-06-16 2026-04-21 Praxair Technology, Inc. Liquid nitrogen energy storage system

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US9608498B2 (en) 2013-03-21 2017-03-28 Linde Aktiengesellschaft Method and device for generating electrical energy
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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
EP3293475A1 (fr) * 2016-09-07 2018-03-14 Linde Aktiengesellschaft Procédé et appareil de stockage et de récupération d'énergie
DE202017004193U1 (de) 2017-08-10 2017-09-14 Linde Aktiengesellschaft Anlage zum Speichern und Rückgewinnen von Energie

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DE19527882A1 (de) * 1995-07-29 1997-04-17 Hartmann Joerg Dipl Math Verfahren zur Energiespeicherung mittels flüssiger Luft
DE19757588A1 (de) * 1996-12-24 1998-07-02 Hitachi Ltd Stromerzeugungssystem mit Gasturbine und Energiespeicher
US20090145130A1 (en) * 2004-08-20 2009-06-11 Jay Stephen Kaufman Building energy recovery, storage and supply system
EP1989400B2 (fr) 2006-02-27 2023-06-28 Highview Enterprises Limited Procédé de stockage d'énergie et système de stockage d'énergie cryogénique
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WO2019077343A1 (fr) * 2017-10-17 2019-04-25 Innovatium Llp Appareil et procédé de stockage de gaz
GB2593615A (en) * 2017-10-17 2021-09-29 Innovatium Llp Gas storage apparatus and method
US20210372322A1 (en) * 2017-10-17 2021-12-02 Innovatium Llp Gas storage apparatus and method
GB2593615B (en) * 2017-10-17 2023-07-12 Innovatium Group Ltd Company Number Sc689285 Gas storage apparatus and method
US12065962B2 (en) * 2017-10-17 2024-08-20 Innovatium Llp Gas storage apparatus and method
WO2022064533A1 (fr) * 2020-09-25 2022-03-31 Energy Dome S.P.A. Centrale et procédé de stockage d'énergie
JP2023547991A (ja) * 2020-09-25 2023-11-15 エナジー ドーム エス．ピー．エー． エネルギー貯蔵のためのプラント及びプロセス
JP7554920B2 (ja) 2020-09-25 2024-09-20 エナジー ドーム エス．ピー．エー． エネルギー貯蔵のためのプラント及びプロセス
US12140052B2 (en) 2020-09-25 2024-11-12 Energy Dome S.P.A. Plant and process for energy storage
AU2020469637B2 (en) * 2020-09-25 2025-12-04 Energy Dome S.P.A. Plant and process for energy storage
WO2023244883A1 (fr) 2022-06-16 2023-12-21 Praxair Technology, Inc. Système et procédé de stockage d'énergie d'azote liquide
US12607399B2 (en) 2022-06-16 2026-04-21 Praxair Technology, Inc. Liquid nitrogen energy storage system

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