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DK2634383T3 - Method and assembly for storing energy - Google Patents

Method and assembly for storing energy Download PDF

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Publication number
DK2634383T3
DK2634383T3 DK13156878.4T DK13156878T DK2634383T3 DK 2634383 T3 DK2634383 T3 DK 2634383T3 DK 13156878 T DK13156878 T DK 13156878T DK 2634383 T3 DK2634383 T3 DK 2634383T3
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DK
Denmark
Prior art keywords
air
stage
compressor
heat exchanger
energy
Prior art date
Application number
DK13156878.4T
Other languages
Danish (da)
Inventor
Julia Dr Arndt
Björn Grossmann
Gunter Dr Kaiser
Moritz Kuhn
Gunar Schroeder
Ulrich Dr Zerweck-Trogisch
Jürgen Dr Klier
Original Assignee
Inst Für Luft- Und Kältetechnik Gemeinnützige Gmbh
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Publication of DK2634383T3 publication Critical patent/DK2634383T3/en

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/10—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with exhaust fluid of one cycle heating the fluid in another cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • 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
    • F25J1/02—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
    • 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
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams 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
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air

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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)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

An energy storage process and arrangement
The invention relates to a process and an arrangement for storing energy in the form of liquefied air, which can, during low-load periods of a power grid, store energy, preferably electrical energy, and retrieve it again during peak-load periods.
Since in many countries the proportion of the power generated from solar energy and wind power is constantly increasing, the storage of electrical energy is becoming more and more important. The reason why is that while hydroelectric power stations (in combination with reservoirs) can produce electrical energy largely as needed, and large power plants such as coal-fired power plants or nuclear power plants can at least produce constant power, central power plants or virtual power plants, which use wind power or solar energy, produce electric current completely independently of current demand. Solar current is regularly produced opposite to current demand.
Energy storage processes / arrangements known from the prior art such as pumped-storage power plants, compressed-air energy storage, and electrochemical storage have specific disadvantages.
For example, although pumped-storage power plants can achieve relatively high efficiencies of up to 80%, they can only be set up at a few suitable places, their size being largely determined by the local conditions (not scalable).
Electrochemical storage (batteries) can achieve very high efficiencies of up to 90%, however relative to their storage capacity they are very cost-intensive and so far the number of operating cycles that they can achieve is relatively small.
The prior art also discloses solutions that store electrical energy in the form of liquefied air.
For instance, in DE 31 39 567 A1, US 6,920,759 B2, and WO 2007/096656 A1 describe processes or arrangements that can store electrical energy by liquefying air, e.g., by means of the Linde process, and storing it in cryotanks.
However, the process according to DE 31 39 567 A1 can only achieve low overall efficiencies of about 20%. The systems described in US 6,920,759 B2 and WO 2007/096656 A1 use cold energy storage systems, which have the disadvantage that to achieve high efficiencies very large amounts (masses) of storage material have to be used; consequently, efficient systems with cold energy storage are comparatively costintensive. DE 195 27 882 A1 describes multiple embodiments of cooling systems or systems that operate with liquefied air: a first embodiment uses pentane for compressor cooling and this heat for power generation, that is for waste heat recovery. A second embodiment uses liquefied air to drive vehicles rather than to improve storage efficiency. Another embodiment uses the energy released as the air expands to drive an air conditioner.
And an alternative embodiment describes the principle of the storage process that can be considered to be prior art.
The scientific work CHINO ET AL.: “Evaluation of Energy Storage Method Using Liquid Air” describes the already known storage process using liquefied air. The air is also liquefied according to the Claude process. It is only indicated that the power generation also involves burning natural gas (LNG), which is used to achieve the inlet temperatures necessary for high process efficiencies.
The goal of the invention is to find a process which can store and retrieve energy in a comparatively economical manner and which should be able to achieve a very high number of cycles of operation. The process should allow overall efficiencies of 50% or more. It should be possible to carry out the process at the operating site irrespective of the geographic conditions. It should be possible to implement the system in a relatively simple modular structure made from available individual prior art components.
The goal of the invention is accomplished by the features of claims 1 and 8. Other advantageous embodiments of the invention follow from claims 2 through 7 and 9.
The inventive energy storage process is subdivided into two phases (steps). In the first phase, available excess energy is converted into a storable form and stored (storage).
In the second phase, if additional energy is required, the stored energy is retrieved (retrieval).
To store energy, preferably electrical energy, air is sucked in at the inlet (suction side) of a one or more stage compressor and the air pressure is increased to a value above the ambient pressure, the air is liquefied by means of an isenthalpic expansion, and finally it is fed to a thermally insulated storage tank. That is, the energy fed to the compressor is converted into a storable form, namely liquefied air, which can be stored in a straightforward way in a cryotank.
After the last stage of the compressor (corresponding to after the compressor exclusively when the compressor has a single stage) the air compressed to the final pressure is cooled by cold vapor. To accomplish this, one side of a counterflow heat exchanger is introduced into the line which recirculates the cold vapor formed when the air is liquefied (to the suction side of the compressor), and the other side of the counterflow heat exchanger in question (fluid) is connected after the last stage of the compressor.
The energy storage medium is liquefied using the Linde-Claude process by dividing the compressed air into two partial flows after it passes through the compressor, and passing the second mass flow through a liquefaction-expansion turbine (expander). The first mass flow is cooled by the second mass flow exiting from the liquefaction-expansion turbine using a Claude heat exchanger (usually a counterflow heat exchanger). The energy obtained in the liquefaction-expansion turbine is fed to the compressor, e.g., by coupling the liquefaction-expansion turbine to the compressor through a transmission.
Preferably the air is liquefied using a multistage compressor and heat is transferred between the compressed air and the environment after every compressor stage (each having one intercooler).
To retrieve energy, e.g., during peak load periods of a power grid, the stored liquefied air is converted into a continuous mass flow with a pressure of several 100 bar and the highest possible temperature, and used to drive an expansion turbine (main turbine) to which, e.g., a power generator is coupled.
To accomplish this, liquefied air is removed from the storage tank and the air pressure is increased to a pressure of several 100 bar, preferably 200 bar, by means of a pump and/or by means of thermal compression. Although in theory the pressure can be increased by mechanical means, e.g., by means of a piston pump, the required (electrical) energy reduces the overall efficiency of the process. Therefore, it is preferable for the air pressure to be increased using exclusively thermal means by increasing the air temperature in a closed vessel until the air pressure has reached the required process pressure. After that, the air temperature is brought to the ambient temperature, or if a waste heat source is available, to the temperature level of the waste heat source.
The temperature can be increased using a heat exchanger, e.g., a shell and tube heat exchanger, one side of which is connected with the removed air during energy retrieval, and whose other side is connected with the temperature level of the environment (or a waste heat source). Using a waste heat source increases the specific amount of energy recovered from the liquid air, since the air is heated to a temperature higher than the ambient temperature after removal from the storage tank.
According to the invention, the efficiency of the entire process (or of a system working according to the inventive process) is increased to as high as 50%, if the energy retrieval involves not only the usual use of the liquid air by the main turbine, but also using the (low) temperature level of the liquid air for condensation of a coolant (whose boiling point is usually far below that of water) at the lowest stage of a one- or more- stage Rankine cycle process (steam turbine process). The stage(s) of the Rankine machine, usually use low-boiling substances, such as, e.g., nitrogen, pure hydrocarbons or fully halogenated or partially halogenated hydrocarbons, such as, e.g., R134a, R600a, or natural coolants, such as, e.g., water, carbon dioxide, or mixtures of the previously mentioned substances. If organic coolants are used, the Rankine process is a so-called ORC (Organic Rankine Cycle) process.
If the process is used for storage of electrical energy, then the individual stages of the Rankine machine drive power generators through turbines. The electrical energy produced by the power generators is fed into the power grid to be supplied along with the electrical energy produced by the power generator of the main turbine.
The arrangement for performing the process comprises a one or more stage compressor, a liquefaction-expansion turbine, through which a second mass flow of the air exiting from the last stage of the compressor is fed; at least one counterflow heat exchanger, which exchanges heat between the second mass flow exiting from the liquefaction-expansion turbine and the first mass flow, an expansion valve through which the first mass flow undergoes isenthalpic expansion at a liquefaction pressure; a phase separator, in which the liquefied air is separated from the gaseous component (cold vapor), a thermally insulated storage tank that serves to store the liquefied air, a regasification unit that is set up to increase the pressure in liquid air removed from the storage tank and to bring the air temperature to at least the ambient temperature, and a turbine that can be driven by the compressed air produced in the regasification unit. Every compressor stage is followed by an intercooler, in which the compressed air is cooled to almost the ambient temperature after compression.
According to the invention, the arrangement additionally has a one or more stage Rankine machine, which serves to increase the overall efficiency of the storage and retrieval process.
The lowest stage of the Rankine machine, that is, the stage at the lowest temperature, is thermally coupled, through a counterflow heat exchanger (condenser), to the temperature level of the liquid air (when the air is removed, that is as soon as liquefied air flows out of the storage tank), i.e., in the lowest stage the cold released when the process medium air is evaporated and heated is used to condense a coolant, e.g., nitrogen. The one side of the counterflow heat exchanger is connected between the outlet of the storage tank and the inlet of the main turbine, and its other side has coolant used in the lowest stage of the Rankine turbine flowing through it.
Every stage of the Rankine machine (ORC machine) comprises a regenerator, a condenser, a coolant pump, an evaporator, and a turbine (with a generator connected).
The invention is explained in detail below on the basis of a sample embodiment; for this purpose the following figures are provided:
Fig. 1: The connection diagram of a system for storage of energy by means of liquefied air;
Fig. 2: The pressure-enthalpy diagram of the air liquefaction process;
Fig. 3: A listing of the thermodynamic states of the air during the liquefaction process;
Fig. 4: The temperature-enthalpy diagram of regasification.
The air liquefaction system shown in Fig. 1, which works according to the Linde-Claude process, consists of a three-stage compressor 1, which is in the form of a rotary screw compressor and has an isentropic compression efficiency of about 90%, a first heat exchanger 2 (counterflow heat exchanger) and a second heat exchanger 3 (Claude heat exchanger), a single-stage turboexpander 4 (liquefaction-expansion turbine), that has an isentropic expansion efficiency of 90%, a Joule-Thomson throttle valve 5 (expansion valve), a phase separator 6, and a thermally insulated storage tank 7, which ensures low heat losses.
Fig. 2 shows the position, on the pressure-enthalpy diagram, of the air to be stored at each of the points A-l marked in Fig. 1 (the points A-l relate exclusively to the storage); the thermodynamic states of the air at the points A-l are listed in tabular form in Fig. 3.
To liquefy the air (energy storage), dried and purified air from the environment and air recycled from the process (cold vapor) is sucked in (point A) at the inlet 1.1 of the compressor 1, the pressure of the air is increased to a final pressure of about 8 bar, and the compressed air is fed through an outlet 1.2 (point B) into a counterflow heat exchanger 2, in which it is cooled to a temperature of about 143 K (point C) with the cold vapor. The compressor 1 has intercooling, i.e., every stage has one heat exchanger (not shown) after it that cools the compressed air to almost ambient temperature (points A through B).
After the air passes through the counterflow heat exchanger 2, it is divided in a first and a second mass flow (the first mass flow is supposed to be cooled using the second mass flow). The second mass flow is fed into the inlet 4.1 of the liquefaction-expansion turbine 4 (expander).
The residual gaseous portion of the air (point E(g)) exiting from the phase separator 6 and the second mass flow (point I) exiting from the liquefaction-expansion turbine 4 are mixed (cold vapor, point F), and used as described above for cooling of the compressed air in the heat exchangers 2, 3, in order to reach the lowest possible temperature at point D.
For cooling at point D, the first mass flow is passed through the one side of the Claude heat exchanger 3 and the cold vapor through the other side of it, which lowers the air temperature of the first mass flow enough that the air is first completely liquefied and then supercooled (point D).
Then, the first mass flow undergoes isenthalpic expansion through the expansion valve 5. The air is cooled further (Joule-Thomson effect) and a large part of the air remains liquid (despite the lower pressure), a residual component becomes gaseous (point E(g)). In a phase separator 6, the liquefied air is separated from the residual gaseous component and fed into the thermally insulated storage tank 7, where it is stored at ambient pressure (pressureless storage) and a temperature of about 80 K (point E(f)).
The possible storage duration is determined almost exclusively by the heat losses of the storage tank.
The second mass flow is not liquefied, but rather undergoes polytropic expansion from point C to point I by means of the liquefaction-expansion turbine 4. During the expansion, the second mass flow performs mechanical work, which is supplied to the compression process, since the shafts of the liquefaction-expansion turbine 4 and the compressor 1 are mechanically coupled with one another by means of a transmission (not shown).
To retrieve energy, liquefied air is removed from the storage tank 7, its pressure is increased first to 200 bar exclusively by the addition of heat in a closed vessel (not shown), and the compressed air produced in this way is then brought to ambient temperature (about 300 K) or possibly to the temperature of a waste heat source (to increase the overall efficiency), by passing the air in the countercurrent principle through the one side of a first Rankine cycle heat exchanger 8 of a two-stage Rankine machine 9, whose first/lowest stage 10 is operated with nitrogen (as a coolant) and whose second stage 11 is operated with a low-boiling coolant. The first Rankine heat exchanger 8 is connected with the nitrogen of the first stage 10 of the Rankine machine 9, which is operated at the lowest temperature level.
The compressed air is expanded from 200 bar to 1 bar into a main turbine 12 with connected power generator 13. In order to increase the efficiency of the expansion process, the turboexpander has a six-stage design, and is equipped with interheating (not shown) after every expansion stage. The six-stage design of the turboexpander ensures that the temperature of the expanded air is no less than 230 K. Fig. 4 shows the associated temperature-entropy diagram (energy retrieval / regasification).
Each of the two stages 10,11 of the Rankine machine 9 use two heat exchangers 8,15, 16, one of the two heat exchangers being used for coupling to a lower temperature level and the other heat exchanger being used for coupling to a higher temperature level. Thus, the second Rankine heat exchanger 16 couples the two stages 10, 11 of the
Rankine machine 9 to one another, since the high temperature level of the first stage 10 approximately corresponds to the low temperature level of the second stage 11 . The third Rankine heat exchanger 15 is connected with the ambient temperature level, which corresponds to the high temperature level of the second stage 11. Cascading of more than two stages is also conceivable.
Each of the stages of the Rankine machine has a closed design, i.e., the outlet of the heat exchanger at the higher temperature level is connected with the inlet of the heat exchanger at the lower temperature level, always through an expansion turbine 14, where expansion work is performed. The outlet of the heat exchanger at the lower temperature level is always connected with the inlet 17.1 of a condensate pump 17, which returns the coolant, and the inlet of the heat exchanger at the higher temperature level is connected with the outlet 17.2 of the condensate pump 17.
Each of the expansion turbines 14 is mechanically coupled to electrical generators 18. When energy is retrieved, both the electrical energy of the generators 18 operated by the Rankine machine and also that from generator 13 driven by the main turbine 12 is fed back into the power grid to be to supplied.
List of reference numbers used 1 Compressor 1.1 Inlet of the compressor 1.2 Outlet of the compressor 2 Counterflow heat exchanger 3 Claude heat exchanger 4 Liquefaction-expansion turbine / turboexpander 4.1 Inlet of the liquefaction-expansion turbine 4.2 Outlet of the liquefaction-expansion turbine 5 Expansion valve / Joule-Thomson throttle valve 6 Phase separator 7 Storage tank 8 First Rankine cycle heat exchanger 9 Rankine machine 10 First stage of the Rankine machine 11 Second stage of the Rankine machine 12 Main turbine 13 Power generator of the main turbine 14 Expansion turbine 15 Third Rankine cycle heat exchanger 16 Second Rankine cycle heat exchanger 17 Condensate pump 17.1 Inlet of condensate pump 17.2 Outlet of condensate pump 18 Power generator of Rankine machine

Claims (9)

1. Fremgangsmåde til lagring af energi, der omfatter - et energilagringstrin, hvor luft suges ind i indløbet (1.1) på en ét- eller flertrinskompressor (1), dets tryk forøges til en værdi, der er højere end det omgivende tryk, luften fortættes ved hjælp af isentalpisk ekspansion og ledes ind i en varmeisoleret lagringstank (7), idet den kolde luftdamp, der dannes under luftfortætningsprocessen, ledes tilbage til indløbet (1.1) på kompressoren (1) gennem mindst én modstrømsvarmeveksler (2), der åbner mulighed forvarmeveksling mellem den komprimerede luft og den kolde damp bag det mindst ene trin af kompressoren (1), hvor den komprimerede luft fordeles i to delstrømme efter modstrømsvarmeveksleren (2), og den anden massestrøm ledes gennem en fortætnings-ekspansionsturbin (4), og energien, der opnås i fortætningsekspansionsturbinen (4), ledes til kompressoren (1), hvor den første massestrøm nedkøles ved hjælp af en Claude-varmeveksler (3) af den anden massestrøm, der udgår fra fortætnings-ekspansionsturbinen (4), og den anden kolde damp, der dannes under luftfortætningsprocessen, - og et energifjernelsestrin, hvorved den væskeformige luft fjernes fra lagringstanken (7) og omdannes til gas igen, hvor lufttrykket forøges ved hjælp af en pumpe og/eller ved hjælp af termisk kompression, og lufttemperaturen herefter øges til mindst den omgivende temperatur, idet den komprimerede luft, der dannes på denne måde, driver en hovedturbine (12), der er kendetegnet ved, at temperaturniveauet for den væskeformige luft, der fjernes fra lagringstanken, yderligere anvendes til kondensering af en kølervæske med lavt kogepunkt på det laveste trin afen ét- eller flertrins-Rankine-cyklusproces, idet energien, der dannes i Rankine-cyklusprocessen, føres sammen med energien, der dannes i hovedturbinen (12).A method of storing energy comprising - an energy storage step in which air is sucked into the inlet (1.1) of a single or multiple stage compressor (1), its pressure is increased to a value higher than the ambient pressure, the air is condensed by means of isental whisk expansion and fed into a heat-insulated storage tank (7), the cold air vapor generated during the air-sealing process is fed back to the inlet (1.1) of the compressor (1) through at least one countercurrent heat exchanger (2), which allows pre-heat exchange between the compressed air and the cold steam behind the at least one stage of the compressor (1), where the compressed air is distributed in two partial flows after the countercurrent heat exchanger (2) and the second mass flow is conducted through a condensate expansion turbine (4) and the energy, obtained in the condensate expansion turbine (4) is directed to the compressor (1), where the first mass flow is cooled by means of a Claude heat exchanger (3) of the second mass flow, starting from the condensate expansion turbine (4) and the second cold steam generated during the air-sealing process, - and an energy removal step whereby the liquid air is removed from the storage tank (7) and converted to gas again, where the air pressure is increased by means of a pump and / or by thermal compression, and the air temperature thereafter is increased to at least the ambient temperature, the compressed air thus formed driving a main turbine (12) characterized in that the temperature level of the liquid air which removed from the storage tank, further used to condense a low boiling coolant at the lowest stage of a single or multi-stage Rankine cycle process, bringing the energy generated in the Rankine cycle process together with the energy generated in the main turbine (12) . 2. Fremgangsmåde ifølge krav 1, der er kendetegnet ved, at kølervæsken, der anvendes på det laveste trin af ét- eller flertrins-Rankine-cyklusprocessen, har et kogepunkt, der er lavere end vands kogepunkt.Process according to claim 1, characterized in that the coolant used in the lowest stage of the single or multi-stage Rankine cycle process has a boiling point lower than the boiling point of water. 3. Fremgangsmåde ifølge et af kravene 1 og 2, der er kendetegnet ved, at nitrogen anvendes som kølervæsken på det laveste trin af Rankine-cyklusprocessen.Process according to one of Claims 1 and 2, characterized in that nitrogen is used as the coolant at the lowest stage of the Rankine cycle process. 4. Fremgangsmåde ifølge et af kravene 1 til 3, der er kendetegnet ved, at nitrogen, rene hydrocarboner eller fuldt halogenerede eller delvist halogenerede hydrocarboner, naturlige kølervæsker og/eller blandinger af disse stoffer anvendes som kølervæsken i ét- eller flertrins-Rankine-cyklusprocessen.Process according to one of claims 1 to 3, characterized in that nitrogen, pure hydrocarbons or fully halogenated or partially halogenated hydrocarbons, natural coolants and / or mixtures of these substances are used as the coolant in the single or multi-stage Rankine cycle process. . 5. Fremgangsmåde ifølge et af kravene 1 til 4, der er kendetegnet ved, at en organisk Rankine-cyklusproces anvendes som ét- eller flertrins-Rankine-cyklusprocessen.Process according to one of Claims 1 to 4, characterized in that an organic Rankine cycle process is used as the single or multistage Rankine cycle process. 6. Fremgangsmåde ifølge et af kravene 1 til 5, der er kendetegnet ved, at en flertrinskompressor anvendes til fortætning af luften, hvor varmeveksling mellem den komprimerede luft og omgivelserne udføres bag hvert trin af kompressoren til nedkøling af den komprimerede luft.Process according to one of claims 1 to 5, characterized in that a multi-stage compressor is used for densifying the air, where heat exchange between the compressed air and the environment is carried out behind each step of the compressor for cooling the compressed air. 7. Fremgangsmåde ifølge et af kravene 1 til 6, der er kendetegnet ved, at luften i energifjernelsestrinet opvarmes til en temperatur, der er højere end den omgivende temperatur, ved anvendelse afen spildvarmekilde.Process according to one of claims 1 to 6, characterized in that the air in the energy removal stage is heated to a temperature higher than the ambient temperature, using a waste heat source. 8. Indretning til udførelse af fremgangsmåden ifølge krav 1 med en et- eller flertrinskompressor med mellemkøling (1), hvor det sidste kompressortrin følges af en modstrømsvarmeveksler (2), hvis ene side kan have den komprimerede luft strømmende derigennem, og hvis anden side kan have kold damp strømmende derigennem; en fortætnings-ekspansionsturbine (4), som kan have en anden massestrøm af luften, der udgår fra modstrømsvarmeveksleren (2), ledt derigennem; en Claude-varmeveksler (3), der fungerer som varmeveksler mellem den anden massestrøm, der udgår fra fortætnings-ekspansionsturbinen (4), og anden kold damp, der dannes under luftfortætningsprocessen, og en første massestrøm; en ekspansionsventil (5), hvorigennem den første massestrøm kan gennemgå isentalpisk ekspansion ved et fortætningstryk; en faseseparator (6), hvori den fortættede luft kan adskilles fra den gasformige luft; en varmeisoleret lagringstank (7), der fungerer til lagring af den fortættede luft; en gengasificeringsenhed, der er indrettet til at øge trykket i den væskeformige luft, der fjernes fra lagringstanken (7), og bringe lufttemperaturen til mindst den omgivende temperatur; en hovedturbine (12), der kan drives ved hjælp af den komprimerede luft, der dannes i gengasificeringsenheden, hvilken indretning omfatter en et- eller flertrins-Rankine-maskine (9), der er indrettet til at udføre Rankine-cyklusprocessen, idet det laveste trin af Rankine-maskinen (9) er termisk koblet til gengasificeringsenheden ved hjælp af en modstrømsvarmeveksler, hvis ene side er forbundet mellem udløbet af lagringstanken og indløbet af hovedturbinen (9), og hvis anden side kan have kølervæsken, der anvendes i Rankine-maskinen, strømmende derigennem.Apparatus for carrying out the method according to claim 1 with a one or several stage compressor with intermediate cooling (1), the last compressor stage being followed by a countercurrent heat exchanger (2), one side of which can have the compressed air flowing through it and the other side of which can having cold steam flowing through it; a condensation expansion turbine (4) which may have a second mass flow of air exiting the countercurrent heat exchanger (2) passed therethrough; a Claude heat exchanger (3) acting as a heat exchanger between the second mass flow exiting the condensate expansion turbine (4) and second cold steam generated during the air-sealing process and a first mass flow; an expansion valve (5) through which the first mass flow can undergo isental whisk expansion at a condensing pressure; a phase separator (6) in which the condensed air can be separated from the gaseous air; a heat insulated storage tank (7) which functions to store the condensed air; a gasification unit adapted to increase the pressure in the liquid air removed from the storage tank (7) and bring the air temperature to at least the ambient temperature; a main turbine (12) operable by the compressed air formed in the gasification unit, comprising a single or multi-stage Rankine machine (9) adapted to perform the Rankine cycle process, the lowest steps of the Rankine machine (9) are thermally coupled to the gasification unit by means of a countercurrent heat exchanger, one side of which is connected between the outlet of the storage tank and the inlet of the main turbine (9) and the other side of which may have the coolant used in the Rankine machine , flowing through it. 9. Indretning ifølge krav 8, der er kendetegnet ved, at kompressoren (1) er eldrevet, og både hovedturbinen (12) og Rankine-turbinen (14) hver især er koblet til en elgenerator (13, 18), hvilket gør indretningen egnet til lagring af elektrisk energi.Device according to claim 8, characterized in that the compressor (1) is electrically powered and both the main turbine (12) and the Rankine turbine (14) are each connected to an electric generator (13, 18), making the device suitable for storing electrical energy.
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