WO2023237162A1 - Système et procédé de conversion de chaleur perdue en énergie mécanique et utilisation d'une installation frigorifique à absorption en tant que régulateur de température - Google Patents

Système et procédé de conversion de chaleur perdue en énergie mécanique et utilisation d'une installation frigorifique à absorption en tant que régulateur de température Download PDF

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Publication number
WO2023237162A1
WO2023237162A1 PCT/DE2023/100433 DE2023100433W WO2023237162A1 WO 2023237162 A1 WO2023237162 A1 WO 2023237162A1 DE 2023100433 W DE2023100433 W DE 2023100433W WO 2023237162 A1 WO2023237162 A1 WO 2023237162A1
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Prior art keywords
temperature
line
recuperator
heat
engine
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PCT/DE2023/100433
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German (de)
English (en)
Inventor
Thiago GOTELIP CORREA VELOSO
Uwe Gampe
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Technische Universität Dresden
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Publication of WO2023237162A1 publication Critical patent/WO2023237162A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K9/00—Plants characterised by condensers arranged or modified to co-operate with the engines
    • F01K9/003—Plants characterised by condensers arranged or modified to co-operate with the engines condenser cooling circuits
    • 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
    • F01K19/00—Regenerating or otherwise treating steam exhausted from steam engine plant
    • F01K19/10—Cooling exhaust steam other than by condenser; Rendering exhaust steam invisible
    • 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
    • F01K25/103—Carbon dioxide
    • 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
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide

Definitions

  • the invention relates to an arrangement and a method for converting waste heat into mechanical energy, in particular kinetic energy (also referred to as kinetic energy), using carbon dioxide (CO 2 ) in a supercritical state.
  • CO 2 in a supercritical state or supercritical CO 2 refers to carbon dioxide in a supercritical state, above the critical point at a temperature of 31 ° C and a pressure of 73.8 bar, also called supercritical CO 2 , hereinafter also briefly: sCO 2 .
  • Any heat source is considered waste heat within the meaning of the invention, even if it is not residual heat from an industrial process, but rather from a renewable source, for example.
  • the arrangement comprises a) a pump arrangement for increasing the pressure and further transporting the CO 2 under transcritical conditions from a line, the CO 2 at the inlet of the pump arrangement having a pressure above the critical CO 2 pressure and a temperature below the critical CO 2 temperature , b) at least two heat exchangers, a preheater and a main heater for transferring waste heat from a waste heat stream in a line to the CO 2 as a carrier medium and working medium, so that the CO 2 can be present in the supercritical state as sCO 2 , c) an engine for Generation of mechanical energy by means of the sCO 2 , and d) an absorption refrigeration system for the controlled cooling of the CO 2 emerging from the engine, from which heat has then already been removed in the recuperator, comprising an expeller and an evaporator in which the CO 2 is heat in two stages is removed by comprising a line that leads from the recuperator to the expeller and further comprising a line that leads from the expeller to the evaporator.
  • the method includes the steps a) pressure increase and transport of CO 2 by means of a pump arrangement), whereby the CO 2 at the inlet of the pump arrangement has a pressure above the critical CO 2 pressure and a temperature below the critical CO 2 temperature, b) transfer of waste heat from a waste heat stream to CO 2 as a carrier medium and working medium sequentially in at least two stages, so that the CO 2 is present in the supercritical state as sCO 2 after compression, and c) Generation of mechanical energy from the sCO 2 using a power machine.
  • the invention also relates to the use of an absorption refrigeration system as a bottoming system of an sCO 2 circuit, the absorption refrigeration system serving as a cooler for the topping system and comprising an expeller and an evaporator.
  • the regulation relates to the heat removal from the CO 2 system of an arrangement for converting waste heat into mechanical energy or specifically into kinetic energy, the arrangement according to the invention.
  • the arrangement for converting waste heat into mechanical energy is also referred to below as the energy system.
  • Waste heat is heat that is primarily generated by technical systems and is released into the environment or can also be used. From a thermodynamic point of view, most real processes are irreversible. As a result of the dissipation of energy, heat is inevitably generated during these processes. Technical devices and systems cannot be operated without generating waste heat. This usually has to be diverted to avoid malfunctions due to overheating or to restore the initial state of the working medium in cycle processes.
  • Carbon dioxide (CO 2 , ASHRAE number: R744) has a long tradition as a refrigerant, but was largely displaced as a refrigerant with the advent of synthetic refrigerants in the 1930s. It was only in the 1980s and 1990s, when it became clear that the most commonly used synthetic refrigerants were essentially responsible for ozone depletion and the greenhouse effect, that carbon dioxide came back into the spotlight.
  • CO 2 is non-flammable, does not contribute to ozone depletion and has a much lower global warming potential than conventional refrigerants. That is in small quantities Gas is also non-toxic, but high concentrations in the air pose a risk of suffocation.
  • systems that operate with CO 2 as a refrigerant must withstand higher system pressures and lower, critical temperatures. A system must be built and maintained accordingly safely.
  • the critical point is therefore very close to the operating range.
  • the critical point which is 31 °C and 73.8 bar, is already exceeded at an ambient temperature of 26 °C. This is then referred to as transcritical operation of the refrigeration system, especially when both subcritical and supercritical conditions occur.
  • the critical point is reached when the densities of the liquid and gaseous phases become so similar that there is no longer any difference in pressure and temperature between the two states of aggregation. When this critical point is exceeded, one speaks of a transcritical or supercritical system.
  • thermodynamic points usually do not play a role, but they are important when using CO 2 .
  • the critical point at 31 °C and 73.8 bar, very high pressures occur, which is why in subcritical systems, i.e. those that operate below the critical point, excessive heating of the system (for example due to the ambient temperature) must be avoided , for example through protective measures such as auxiliary cooling, an expansion tank or the release of CO 2 .
  • transcritical systems there is usually no condenser, but rather a gas cooler.
  • transcritical systems must withstand very high pressures of well over 75 bar.
  • the use of transcritical CO 2 refrigeration systems is particularly efficient when the ambient temperature or the temperature on the warm side is on average below 15 °C, because the higher the temperature, the lower the efficiency.
  • absorption refrigeration systems with sCO 2 energy systems, energy systems that use supercritical CO 2 , in order to make waste heat, for example from industrial exhaust gases, usable.
  • the absorption refrigeration system is often referred to as a bottoming system and the sCO 2 system as a topping system. These terms are also used below in the description of the invention.
  • CN 112412555 A an sCO 2 intercooling is used and the operating temperature of the CO 2 is higher than necessary for the supercritical state.
  • Combined sCO 2 /LiBr/H 2 O systems for heat sources such as nuclear reactors, solar systems and internal combustion engines work at high temperatures (above 600 ° C), as also described, for example, in the publication CN 112412555 A.
  • There the cooling water is used to reduce the CO 2 temperature in the intercooling before secondary compression.
  • Supercritical operation ie temperatures and pressures higher than the critical CO 2 pressure, is considered.
  • Ma/Liu et al. (2016) and Ma/Zhang et al. (2016) disclose a combination of sCO 2 cycle with LiBr absorption refrigeration system, whereby only part of the CO 2 mass flow is cooled using the LiBr system.
  • the sCO 2 circuit is designed as a recompression architecture.
  • the recompression architecture is one of the most common configurations of the sCO 2 cycle in application studies of this cycle, as it offers high thermal efficiency, mainly enabled by high heat recovery. This characteristic is due to the use of at least two heat recoverers: high temperature (HTR) and low temperature (LTR) recuperators. Due to the use of a recompression system and the high power consumption of the compressor, the specific work of this type of system is very high. This means that the recompression system is suitable for use with medium-temperature heat sources, such as: B. the use of waste heat is not economical.
  • medium-temperature heat sources such as: B. the use of waste heat is not economical.
  • the solution according to publication CN 109519243 B uses an sCO 2 system combined with an NH 3 /H 2 O absorption refrigeration system. Superheated ammonia drives its own turbine.
  • the sCO 2 cycle is a simple cycle.
  • the NH 3 /H 2 O vapor is used as a heat source for a LiBr absorption cooler.
  • the publication CN 109519243 B therefore describes an energy system based on an interconnection or combination of two Rankine cycle processes, consisting of a simple sCO 2 process as a preliminary process (topping cycle or topping process) and an ammonia/water (NH 3 /H 2 O) steam cycle process as a downstream process (bottoming cycle or bottoming cycle).
  • the non-workable heat from the two thermodynamic cycle processes is dissipated using a LiBr absorption refrigeration system and an additional, separate CO 2 cooler.
  • the heat dissipation is as follows:
  • the heat from the sCO 2 is first used in the expeller (generator) of a LiBr absorption refrigeration system.
  • the carbon dioxide is then further cooled in a separate CO 2 cooler with an unnamed external cooling medium and a downstream cooler, the evaporation condenser, until it is completely liquefied and then fed to the pump.
  • the latter cooler or CO 2 condenser represents the evaporator of the LiBr absorption refrigeration system.
  • heat is dissipated using three devices.
  • the publication CN 1 09 519 243 B does not provide any information about state and process variables, so that the process control and the gradual heat dissipation cannot be thermodynamically reproduced.
  • the object of the present invention is therefore to provide an arrangement and a method for converting waste heat into mechanical energy using carbon dioxide (CO 2 ) in the supercritical state (sCO 2 ), as well as to offer a method for its operation and the use of an absorption refrigeration system in which the disadvantages of the prior art are overcome and a constant cooling performance of a CO 2 energy system is combined with the highest possible efficiency or useful power when converting waste heat into kinetic energy.
  • the system should be as simple as possible and use as few components as possible. These should be as robust and less susceptible to failure as possible and at the same time be able to work independently of daily and seasonal fluctuations in the ambient temperature. In addition, a robust system should also be provided for off-design conditions, i.e. under conditions that differ from those for which the system was designed.
  • the subject of the invention is an arrangement for converting waste heat into mechanical energy, in particular kinetic energy, comprising an energy system in which CO 2 is used in its state as sCO 2 to convert waste heat into mechanical energy a) a pump arrangement for increasing the pressure and further transporting the CO 2 under transcritical conditions from a line, the CO 2 at the inlet of the pump arrangement having a pressure above the critical CO 2 pressure and a temperature below the critical CO 2 temperature, b) at least two heat exchangers, a preheater and a main heater for transferring waste heat from a waste heat stream in a line to the CO 2 as a carrier medium and working medium, so that the CO 2 can be present in the supercritical state as sCO 2 , c) an engine for generating mechanical Energy by means of the sCO 2 , and d) an absorption refrigeration system for the controlled cooling of the CO 2 emerging from the engine, from which
  • the use of the cooling system with the main components: expeller, condenser, evaporator and absorber serves primarily to remove heat from the two streams that pass through the absorption refrigeration system.
  • the first stream in a preferred embodiment, is the heat source in the expeller for evaporating water from the mixture of water (refrigerant) and lithium bromide (absorbent) represented by the stream.
  • the current after the recuperator is therefore the main drive for the expeller.
  • the flow from the condenser to the evaporator with a temperature of 15 °C is the cooling medium for the second stage of heat removal from the CO 2 stream in the evaporator.
  • the evaporator is the main cooler of the sCO 2 circuit.
  • a recuperator a heat exchanger
  • the recuperator as a special heat exchanger serves to transfer heat from the CO 2 emerging from the engine to the sCO 2 leading to the engine.
  • a line leads from the engine to this recuperator, from there to the expeller and from the expeller to an evaporator (also called an evaporator), from which the line runs to the pump arrangement.
  • a pump or a compressor or compressor is used as a pump arrangement.
  • the recuperator and the preheater there is a flow divider for dividing the CO 2 flow into a first partial flow to the recuperator and a second partial flow for transferring waste heat by means of the first heat exchanger, the preheater, arranged.
  • the arrangement according to the invention is a thermoeconomically optimized SH (Sequential Heating) architecture.
  • the present invention also includes the fact that the line can lead to further, additional components along its course.
  • the expeller and evaporator are therefore coolers for a topping process, whereby the evaporator is known to evaporate the coolant of the absorption refrigeration system.
  • the evaporator serves as a condenser for the CO 2 emerging from the turbine, so that it is then present as subcritical CO 2 , preferably with a temperature of 20 ⁇ 5 °C, in particular 20 ⁇ 2 °C. This temperature range represents a central part of the invention.
  • the CO 2 at the inlet of the pump arrangement has a pressure above the critical CO 2 pressure and a temperature below the critical CO 2 temperature.
  • the CO 2 preferably has a pressure above the critical pressure, but at least 75 bar, and a temperature between 20 ° C and 28 ° C.
  • the flow divider is designed or set in such a way that a mass flow ratio of 55 to 65% for the first partial flow of CO 2 under high pressure in the first line in relation to the partial flow in the second line, which both lead to the recuperator.
  • the first line leads directly from the flow divider to the recuperator, while the second line leads from the engine or turbine to the recuperator so that the CO 2 flowing there can release the residual heat from the engine to the first partial flow.
  • the division into partial streams is an important feature of the preheating architecture.
  • the CO 2 mass flow is passed through the flow divider after Main compressor divided into two streams.
  • the entire CO 2 mass flow is routed in the heat dissipation circuit and then to the main compressor.
  • the previously known recompression architecture only part of the total mass flow is directed to heat removal and then to the main compression and only this part of the mass flow is used in the absorption system.
  • the CO 2 flow is divided according to the low-temperature recuperator as the main feature of the recompression architectures. With such an arrangement, only part of the CO 2 mass flow is passed into the absorption refrigeration machine, while the rest goes into the recompressor.
  • the entire mass flow expanded in the engine, in particular the turbine is directed to the recuperator and subsequently completely to the driver of the absorption refrigeration machine.
  • the precooler regularly takes over the heat dissipation, with part of the heat also being dissipated by supplying energy to the absorption refrigeration machine. Therefore, the previously known application differs in terms of cooling water consumption and temperature levels.
  • the absorption chiller instead transfers the heat of the CO 2 directly to the evaporator and keeps the CO 2 temperature at the pump or compressor inlet below the critical CO 2 temperature as indicated.
  • CO 2 under high pressure in a first partial stream from the recuperator, CO 2 under high pressure in a further partial stream, which is brought in from the preheater, are combined through a mixer into a line that runs to the main heater.
  • the preheating architecture thus created allows better utilization of the heat source by recovering heat at two temperature levels, with the main heater acting as a heat exchanger at higher temperatures.
  • the preheater allows additional heat to be recovered from the heat source downstream of the main heater. This creates an additional mass flow, which increases the performance of the Engine (or electricity generation by a connected generator) and a more efficient cycle.
  • the line from the engine leads via the recuperator to the absorption refrigeration system. It has proven to be advantageous if a line between the expeller and the evaporator of the absorption refrigeration system runs past a sub-cooler, whereby the CO 2 is further cooled and the cooling capacity at the evaporator is increased.
  • a particularly advantageous embodiment of the absorption refrigeration system is a LiBr/H 2 O absorption refrigeration system.
  • the Li Br absorption system generally works with a heat source temperature of over 75 ° C on the engine. Therefore, the absorption system with LiBr offers better operating characteristics for the proposed system.
  • absorption systems based on ammonia/water for example, require a heat source with temperatures above 100 °C, which would mean a loss of performance for the topping system (sCO 2 ).
  • a preferred embodiment of the arrangement according to the invention comprises a generator for generating electricity, mechanically connected to the engine designed as a turbine.
  • the invention also relates to a method for converting waste heat into mechanical energy, in particular kinetic energy, comprising the steps: a) increasing the pressure of CO 2 and transporting it through a line by means of a pump arrangement, the CO 2 having a pressure at the inlet of the pump arrangement (1). above the critical CO 2 pressure and a temperature below the critical CO 2 temperature, b) transferring waste heat from a waste heat stream to CO 2 as a carrier medium and working medium sequentially in at least two stages, so that the CO 2 after compression in the supercritical State as sCO 2 is present, c) generation of mechanical energy from the sCO 2 using a power machine.
  • the CO 2 is divided by a flow divider, with a first part (as sCO 2 leading to the engine) being passed to the recuperator (in step e) and a second part for the transfer of waste heat in method step b) (ie to the heat exchanger in paragraph b) of the energy system).
  • the transfer of waste heat in process step b) expediently takes place by means of at least one heat exchanger.
  • the flow of CO 2 is split after cooling at the extractor and evaporator and immediately after the output of the pump by the flow divider, which is arranged between the pump, recuperator and the preheater, with a first part going to the recuperator (in step e) of the method or paragraph e) of the energy system), and another, second part is directed to the heat exchanger according to the invention in step b) of the method or paragraph b) of the energy system. It therefore makes sense to have lines leading from the flow divider to the recuperator and from the flow divider to the heat exchanger (from paragraph b) of the description of the energy system components). Operating the recuperator with two mass flow rates enables better thermodynamic performance of the system.
  • the mass flow rate that comes directly from the flow divider corresponds to 55 to 65% of the mass flow rate that comes from the engine or turbine. This means that this mass flow ratio allows for greater heat transfer between the low pressure and high temperature flow coming from the compressor and the high pressure and low temperature flow coming directly from the flow divider.
  • the lower irreversibility means that the recuperator has better thermodynamic performance.
  • the pressure increase and transport by means of the pump arrangement the CO 2 is transported to the inlet of the pump arrangement under transcritical conditions.
  • the CO 2 at the inlet of the pump arrangement has a pressure above the critical CO 2 pressure and a temperature below the critical CO 2 temperature.
  • the CO 2 has a pressure above the critical pressure, but at least 75 bar, and a temperature between 20 ° C and 28 ° C.
  • the imbalance of heat capacity at the (low temperature) recuperator is a common feature of sCO 2 operation.
  • the higher heat capacity on the cold side of the recuperator limits heat transfer and limits the effectiveness of the system by reducing the power outlet temperature.
  • the preheat architecture offers an alternative to overcome this limitation by employing different mass flows between the two streams passing through the recuperator.
  • a multi-criteria optimization of the proposed system has surprisingly shown that a mass flow ratio of 55 to 65% for a first CO 2 partial flow under high pressure in the line from the flow divider to the recuperator in relation to a second flow in the line from the drive machine to the recuperator Enables increasing the thermal performance of the recuperator and offers the best thermo-economic compromise for the sCO 2 cycle for waste heat recovery applications.
  • the two CO 2 partial streams which were previously divided by the flow divider, are combined in the mixer.
  • the first partial flow after it has passed through the recuperator and there the heat transfer has taken place from the CO 2 emerging from the engine to the sCO 2 in a line leading to the engine according to step e) explained above, is mixed with the second partial flow CO 2 stream combined.
  • the second partial stream had previously passed through the preheater and absorbed heat from the waste heat stream that had already cooled down in the main heater.
  • the combined CO 2 partial streams can together absorb the waste heat at a higher temperature level in the main heater in the previously explained step b).
  • the CO 2 has a temperature between 20 and 28 ° C before entering the pump arrangement and the CO 2 is present there in the transcritical state.
  • step b) the waste heat is transferred from a medium that has a maximum temperature of 450 ° C. Higher temperatures can also be used in other ways, while the advantages of the method according to the invention are realized precisely when the waste heat has a temperature of not more than 450 ° C.
  • the temperature of the CO 2 emerging from the engine or turbine should preferably be 240 ⁇ 20 °C and after the heat transfer in step e) should be 75 ⁇ 10 °C.
  • the temperature of the CO 2 to be cooled at the inlet of the expeller is preferably 75 ⁇ 10 ° C.
  • recuperator outlet temperature of 75 ⁇ 10 °C enables a better thermo-economic compromise for the system application.
  • CO 2 flow in this temperature range at the generator inlet enables smooth operation of the system as a drive heat source for the absorption cooling system.
  • the object according to the invention is thus achieved by a combined system configuration in which the SH (Sequential Heating) sCO 2 system, optimized for waste heat utilization with a maximum process temperature of around 450 ° C, is used as a topping system with an H 2 O/LiBr system.
  • Absorption refrigeration system is combined as a bottom ing system in such a way that the bottom ing system controls the heat dissipation or forms the controller.
  • the process temperature is preferably between 350 and 400 °C.
  • the invention ensures a constant subcritical inlet temperature (e.g. 20 ° C) in the pump arrangement, e.g. B. the compressor or the pump. This enables efficient use of heat even in a medium temperature range between 350 to 400 °C, e.g.
  • B. in the form of waste heat from a technical process.
  • this is done by means of a recuperated, transcritical sCO 2 process, ie a process with a subcritical entry temperature into the pressure increase of e.g. B. 20 °C at supercritical pressure, e.g. B. 75 bar.
  • This is not possible or not implemented in this way with a conventional sCO 2 recompression cycle and represents a significant difference between the invention and the prior art.
  • the invention therefore relates to recuperated, transcritical sCO 2 process architectures, which, for. B. can be used for heat sources in the temperature range of 350 to 400 °C, e.g. B. for the utilization of waste heat from gas turbines, engines or industrial processes.
  • the performance of these transcritical sCO 2 process architectures depends heavily on recooling.
  • the non-working heat is removed from the sCO 2 process in such a way that the inlet temperature into the pump arrangement is kept constant regardless of seasonal and daily temperature fluctuations, e.g. B. at 20 °C, and thus the mentioned performance fluctuations can be compensated for during operation.
  • the arrangement and the proposed method proposed on this basis are therefore essentially characterized by: the combination of a recuperated, transcritical sCO 2 preliminary or topping process (with the associated topping system) with an absorption refrigeration process (preferably an H 2 O/LiBr absorption refrigeration process) as a downstream or bottoming process (with the associated bottoming system); the heat removal from the sCO 2 process through sequential cooling in the expeller and evaporator of the bottoming process; the process architecture without additional precooler and refrigeration circuit, in which the heat dissipation in the entire operating range is controlled exclusively by the bottoming process, so that the bottoming process serves as a controller for the heat dissipation; It has surprisingly been shown that the solution according to the invention achieves a constant subcritical inlet temperature into the pump arrangement while maintaining the cycle architecture that is thermo-economically optimized for the technical application and with minimal expenditure on equipment.
  • an absorption refrigeration process preferably an H 2 O/LiBr absorption refrigeration process
  • the subject of the invention is in particular the use of the energy system according to the invention in the method according to the invention. Furthermore, the subject of the invention is the use of an absorption refrigeration system as a temperature controller.
  • the absorption refrigeration system includes an expeller and an evaporator, in cooperation with a recuperator, which serves to transfer heat between two CO 2 streams of this energy system.
  • the absorption refrigeration system serves as a temperature controller for the removal of heat from the CO 2 system of an energy system.
  • expeller and evaporator which are parts of the absorption refrigeration system, with the recuperator enables, depending on the mass flow or flow rate of the streams, the constant setting of the cooling capacity of the energy system - independent of external cooling, e.g. B. using cooling water and its temperature. This has the advantage that the energy system can be operated independently of the season.
  • an absorption cooling system is envisaged as the bottoming system of an sCO 2 circuit, which serves as a cooler for the topping system.
  • the first CO 2 stream that leaves the recuperator is the exclusive heat source for driving the expeller, which evaporates the water (refrigerant) from the mixture with lithium bromide (absorbent) and removes the heat from the CO 2 stream.
  • the steam is passed into the condenser and the stream with temperatures in the range of 15 °C ⁇ 5 °C is the cooling medium in the evaporator, which removes the heat from the second CO 2 stream leaving the expeller.
  • the evaporator controls the temperature of the CO 2 stream at the inlet of the pump assembly to subcritical temperature conditions of 20 to 28 °C, independent of the seasonal fluctuations in the ambient temperature. In this way, the evaporator is the main cooler of the topping system.
  • the absorption cooling system works without a solution heat exchanger, which is unnecessary due to the invention and which increases the heat dissipation in the expeller. Both absorption cooling systems are arranged in parallel to the first CO 2 stream To extract heat, which enables sufficient cooling performance in the evaporator. This makes the absorption cooling system more efficient and can better control the topping system or the topping process.
  • the waste heat used is, for example, waste heat from an exhaust gas, for example an industrial exhaust gas, which is produced during an industrial process.
  • an exhaust gas for example an industrial exhaust gas
  • the operation of the absorption refrigeration system is explained in more detail in the exemplary embodiments using the drawings.
  • the CO 2 in the entire system of the energy system or over the entire process sequence maintains the supercritical state as sCO 2 , that is, for example, that the sCO 2 in front of the pump arrangement still has a temperature of 35 ° C and is therefore in the supercritical state is under an appropriate pressure.
  • the invention provides for the use of sCO 2 as a carrier medium for the energy of the waste heat and as a working medium in the energy system, whereby the thermal energy is to be converted into mechanical and in particular kinetic energy with the CO 2 as the working medium in a thermal power process, preferably with subsequent generation of Electric energy.
  • the CO 2 system of the energy system is also used to operate the expeller (also referred to as a generator) of the absorption refrigeration system.
  • the CO 2 that emerges from the engine or, for example, the turbine is cooled sequentially by the expeller and the evaporator using the absorption refrigeration system.
  • a pre-cooling of the CO 2 emerging from the turbine takes place beforehand, in return the CO 2 that goes to the engine or, for example, the turbine is carried out, is preheated.
  • This recuperator which is also called a regenerator or internal recuperator, is a heat exchanger, preferably a high-temperature recuperator.
  • the recuperator is necessary to be able to increase the mass flow in the CO 2 circuit. Without the recuperator, the low temperature of the waste heat from some industrial exhaust gases would be an obstacle to efficient conversion into mechanical energy or, in particular, kinetic energy. Because it is a significant advantage of the invention that heat transfer media with which the waste heat is discharged at a low temperature, namely a maximum temperature of 450 ° C, can also be used and converted with high efficiency into mechanical energy or, in particular, kinetic energy.
  • the process temperature is preferably between 350 and 400 °C.
  • the cycle of the absorption refrigeration system benefits from the waste heat that the CO 2 carries after the recuperator from step d) of the method or paragraph d) of the description of the energy system, because it is the energy source that is necessary to run the absorption refrigeration system operate.
  • absorption systems such as a LiBr/H 2 O system
  • an energy source is required in the expeller in order to evaporate the water from the water-LiBr mixture (mixture of refrigerant and salt solution of the absorption refrigeration system).
  • This refrigerant vapor is then condensed in the condenser, expanded (preferably using an expansion valve) and fed into the evaporator in the liquid phase at a low temperature, whereby the coolant water evaporates.
  • the CO 2 mass flow which represents a partial flow of the CO 2 emerging from the engine or the turbine, is used to cool.
  • the condenser of the absorption refrigeration system is cooled with cooling water, whereby the temperature of this cooling water has little to no influence on the stable operation of the energy system.
  • conventional absorption systems such as LiBr/H 2 O absorption systems
  • SHX equipment internal heat recovery device
  • the present invention discloses a simplified absorption system in which the internal heat recovery occurring within the Absorption refrigeration system using an internal recuperator can be omitted.
  • the advantage is that the costs of the energy system can be reduced and a higher level of heat removal from the sCO 2 system is possible.
  • the absorption refrigeration system supplies the coolant to keep the topping process at an optimal temperature. This significantly increases the performance of the energy system according to the invention.
  • no commonly used cooling water is required for cooling the CO 2 , which can be subject to external, seasonal fluctuations and would require adjustment of the entire system, including efficiency.
  • the CO 2 can be cooled so effectively and consistently that the subcritical range of approx. 20 ⁇ 5 °C of the CO 2 in front of the pump arrangement can be reached and operated consistently and over seasonal fluctuations (as is the case with cooling water, for example). above all, it is stable and consistent.
  • the useful performance of the sCO 2 process for utilizing waste heat is hardly reduced, despite the seasonal increase in outside temperatures.
  • the configuration according to the invention has high thermoeconomic performance even under off-design conditions. Furthermore, local two-phase flows do not occur at the entry into the pump arrangement. This would have a negative impact on the stability of the process and the service life of the energy system. This results in regulated cooling.
  • Expellers and evaporators of the absorption refrigeration system serve as temperature controllers for heat dissipation. The temperature control preferably takes place sensibly by changing the mass flows.
  • the invention represents a "circuit architecture" through the general arrangement of the engine or turbine, pumps, compressors or compressors, recuperators and external heat exchangers of the sCO 2 circuit and achieves a stabilization of the operating behavior of the arrangement according to the invention.
  • the evaporator of the absorption refrigeration system works as a cooler of the energy system (ie the topping system), so that heat is transferred from the CO 2 stream present there to CO 2 streams with a lower temperature.
  • the arrangement according to the invention advantageously works with higher, supercritical pressures, so that the CO 2 immediately in front of the engine, for example the turbine, is in the supercritical range, which increases the efficiency of the generator.
  • Another advantage is that there is no need for internal recuperators in the absorption refrigeration system.
  • the invention therefore also requires fewer components.
  • the invention is therefore easy to implement, reduces the number of components in the system and ultimately the useful absorption and conversion of waste heat is improved.
  • An external heat source for the absorption system is no longer necessary.
  • the sCO 2 is cooled exclusively by the absorption refrigeration system, using step d) of the method or the recuperator in paragraph d) according to claim 1, directed to the arrangement for converting waste heat into mechanical or kinetic energy, or the description of the Arrangement according to the invention the hot CO 2 is pre-cooled.
  • the invention is characterized by, but is not limited to, the following preferred embodiments.
  • step b) of the method according to the invention the waste heat is transferred to the CO 2 as a carrier medium sequentially in at least two stages.
  • the first partial stream of the CO 2 stream after the recuperator in method step d) is combined with the second partial stream of the CO 2 stream, which is led from the flow divider to the heat exchanger in paragraph b), in such a way that both partial streams together pass through the heat exchanger as the first heat exchanger, the main heater to absorb the waste heat through the CO 2 .
  • the other, second partial stream of the CO 2 stream has previously passed through a second heat exchanger, the preheater - for absorbing the waste heat through the CO 2 - before this second partial stream is combined with the first partial stream and both together the first Heat exchangers happen.
  • the temperature that the first heat exchanger provides is higher than the temperature provided by the second heat exchanger, since the medium that provides the waste heat and brings it in as a waste heat flow is still significantly hotter at the first heat exchanger than at the second heat exchanger.
  • the last described embodiment therefore uses sequential heating by means of the first heat exchanger and the second heat exchanger.
  • the line between the expeller and the evaporator of the absorption refrigeration system passes a sub-cooler.
  • the absorption refrigeration system is a LiBr/H 2 O absorption refrigeration system. It is particularly advantageous if the absorption refrigeration system works without a solution heat exchanger recuperator between the expeller and the absorber. This is required according to the prior art, but is not required for the system according to the invention, as has surprisingly been shown.
  • the energy system advantageously comprises a generator for generating electrical power, mechanically connected to the engine, designed as a turbine, or in step c) of the method, the mechanical or kinetic energy of the engine or turbine is additionally supplied to the engine by means of a Mechanically coupled generator generates electricity.
  • the temperature of the CO 2 before entering the pump arrangement is preferably 20 ⁇ 5 °C, so that the CO 2 is in the subcritical state there.
  • the waste heat is transferred from a medium, a waste heat stream, which has a maximum temperature of 450 ° C, preferably between 350 and 400 ° C.
  • the temperature of the CO 2 emerging from the turbine is at 240 ⁇ 20 °C and after the heat transfer in step d) at 75 ⁇ 10 °C, preferably before at 235-245 °C and afterwards at 70-80°C.
  • the sCO 2 leading to the turbine is particularly preferably heated from 40-60 °C to 225 ⁇ 20 °C, in particular from 50 ⁇ 5 °C to 205-235 °C.
  • the temperature of the CO 2 to be cooled at the inlet of the expeller is at least 60 ° C, preferably at least 65 ° C.
  • a temperature range of 75 ⁇ 10 °C has been established proven to be advantageous, with the temperature range between 70 °C and 80 °C producing the best results. This corresponds to an embodiment in which the CO 2 flowing from the turbine to the recuperator has these temperatures after exiting the recuperator. The thermal effectiveness of heat exchange is therefore limited and is around 85-95%.
  • Another advantage of the invention is a simplification of the absorption system by eliminating the SHX, the internal heat exchanger with SHX equipment (solution heat exchanger).
  • This device is a heat exchanger between the expeller and absorber of the absorption cooling system. The use of this equipment is standard in the art for an absorption system, but requires additional effort. The elimination of this device, which the invention makes possible, means a simplification of the system.
  • the use of the system according to the invention for utilizing waste heat from industrial processes is particularly advantageous in the thermal use of heat sources classified as medium temperatures. Because their use represents a technical and economic challenge for energy production through sCO 2 systems. The proposed changes are therefore suitable for creating greater application potential for the combined system. However, for high-temperature heat sources, the operating characteristics are completely different.
  • Figure 1 shows a first embodiment of the invention.
  • Figure 2 shows a second embodiment of the invention with an additional sub-cooler.
  • Fig. 3 shows the location of the supercritical region in an entropy-temperature diagram.
  • FIG. 1 A circuit of supercritical CO 2 , sCO 2 is shown schematically in FIG. 1, in particular the arrangement according to the invention for converting waste heat into mechanical energy.
  • the CO 2 is consistently referred to as the working medium, since it represents the working medium of a thermal power process or a heat engine for the method according to the invention, carried out in the arrangement according to the invention, the preferred embodiments of which are described.
  • the pressure of the working medium is raised above the critical pressure by a pump 1 as an embodiment of the pump arrangement, which then prevails at the outlet of the pump 1 and in line 2.
  • a flow divider 3 the working medium is divided into two partial flows between lines 4 and 5, with the first partial flow in line 4 being passed through a high-temperature recuperator 6 and the second partial flow in line 5 being passed through a heat exchanger, a preheater 7.
  • the recuperator 6 is designed to operate with two different mass flow rates, with the mass flow rate in line 4, the first partial flow, corresponding to 55 to 65% of the mass flow rate in line 19, the second partial flow after exiting the engine 17. This enables better thermodynamic performance of the entire system because this ratio of mass flows allows greater heat transfer between the low pressure and high temperature flow in line 19 and the high pressure and low temperature flow in line 4.
  • the lower irreversibility means that the recuperator 6 has better thermodynamic performance.
  • the proposed mass flow rate allows a better balance between the heat capacities on both sides of the heat exchanger. This results in a better temperature gradient in the heat exchanger, which increases the overall heat transfer efficiency and the Irreversibility reduced. This therefore leads to improved thermal efficiency of the heat exchanger.
  • the exhaust gas as a carrier of the waste heat in line 15 first heats the working medium by means of the second heat exchanger, the preheater 7, so that the working medium reaches an increased temperature at which it then flows into line 9.
  • a mixer 10 mixes the working media from lines 8 and 9, the resulting working medium flows in line 11 to a first heat exchanger, a main heater 12, while the exhaust gas as a carrier of the waste heat intended for use as an energy source flows through line 14 entering the heat exchanger 12 the already preheated working medium is heated further.
  • the turbine 17 relaxes the working medium that flows to it in line 13 until it enters line 19, and transmits the resulting or converted mechanical energy to a generator 18.
  • a generator 18 At the exit of the turbine 17, when it enters line 19, remains the working medium in subcritical pressure.
  • the working medium reaches the high-temperature recuperator 6 through line 19, is cooled there by the working medium from line 4, from the cold side, and flows via the line
  • the use of the cooling system with the main components expeller 23, condenser 25, evaporator 31, absorber 33 primarily serves to dissipate heat from the streams 20 and 21.
  • Stream 20 is the heat source in expeller 23 for evaporating water from the mixture of water (refrigerant) and lithium bromide (absorbent) represented by stream 36.
  • the current 20 after the recuperator 6 is therefore the main drive for the expeller 23.
  • the Stream 30 with a temperature of 15 °C is the cooling medium for the heat removal from the CO 2 stream 21 in the evaporator 31.
  • the evaporator 31 is the main cooler of the sCO 2 circuit.
  • water H2O
  • lithium bromide LiBr
  • the weak lithium bromide solution absorbs heat from the working medium flowing in line 20 in order to evaporate the refrigerant (water).
  • the water vapor then flows from the expeller 23 as refrigerant vapor in line 24 into the condenser 25 and condenses to the state in which it enters the outlet 28.
  • Coolant for example cooling water, is supplied via the coolant connections 26, 27.
  • the high-pressure liquid refrigerant flowing through the line 28 expands at an expansion valve 29, whereby the pressure of the refrigerant in the line 30 leaving the expansion valve 29 drops to the low pressure in the evaporator 31.
  • the refrigerant evaporates to the saturated vapor refrigerant by absorbing the heat from the cooled working fluid in line 21 in the evaporator 31 and enters line 32.
  • the refrigerant here water in the state of saturated vapor, enters through line 32 into an absorber 33 to be absorbed by the strong salt solution (LiBr solution).
  • An absorber pump 35 increases the pressure of the now diluted LiBr-H 2 O solution flowing to it via line 34 and leads it via line 36 to the inlet into the expeller 23, where the water is expelled.
  • the now concentrated LiBr salt solution leaves the expeller 23 via line 37, expands at a throttle valve 38 and enters the absorber 33 via line 39. Heat is dissipated in the absorber 33 via cooling connections 40, 41, for example by means of cooling water.
  • FIG. 3 shows in a Ts diagram with the specific entropy s as the abscissa and the absolute temperature T as the ordinate the schematic supercritical region 50, as used, for example, in CO 2 processes such as the method according to the invention.
  • the subcritical region 51 has a higher specific entropy s and the mixed phase region 52 is at a lower temperature? shown.

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  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
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  • Combustion & Propulsion (AREA)
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Abstract

L'invention concerne un système et un procédé de conversion de chaleur perdue en énergie mécanique au moyen de sCO2 surcritique, comprenant un ensemble pompe (1) pour augmenter la pression du CO2 à travers une conduite (2), deux échangeurs de chaleur, un appareil de préchauffage (7) et un appareil de chauffage principal (12) pour transférer la chaleur perdue d'un flux de chaleur perdue dans une conduite (14, 15, 16) au CO2 en tant que fluide de travail, de sorte que le CO2 puisse être à l'état supercritique, une machine motrice (17) pour générer de l'énergie mécanique au moyen du sCO2, et une installation frigorifique à absorption pour le refroidissement régulé du CO2 provenant de la machine motrice (17), comprenant un bouilleur (23) et un évaporateur (31), une conduite pour le CO2 (19) sortant de la machine motrice (17) allant de cette machine motrice (17) au bouilleur (23) et à l'évaporateur (31) de l'installation frigorifique à absorption. Selon l'invention, l'installation frigorifique à absorption maintient la température à l'entrée de l'ensemble pompe (1) constante en dessous de la température critique, un récupérateur (6) est placé entre la machine motrice (17) et le bouilleur (23) pour transférer la chaleur du CO2 sortant de la machine motrice (17) au sCO2 entrant dans la machine motrice (17), et un diviseur de flux (3) est disposé entre l'ensemble pompe (1), le récupérateur (6) et l'appareil de préchauffage (7) pour diviser le flux de CO2 en un premier flux partiel vers le récupérateur (6) et un deuxième flux partiel pour transférer la chaleur perdue au moyen des deux échangeurs de chaleurs (7, 12).
PCT/DE2023/100433 2022-06-08 2023-06-07 Système et procédé de conversion de chaleur perdue en énergie mécanique et utilisation d'une installation frigorifique à absorption en tant que régulateur de température WO2023237162A1 (fr)

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