EP1927816B1 - Vapour compression device and method for performing an associated transcritical cycle - Google Patents

Vapour compression device and method for performing an associated transcritical cycle Download PDF

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Publication number
EP1927816B1
EP1927816B1 EP07354062.7A EP07354062A EP1927816B1 EP 1927816 B1 EP1927816 B1 EP 1927816B1 EP 07354062 A EP07354062 A EP 07354062A EP 1927816 B1 EP1927816 B1 EP 1927816B1
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Prior art keywords
fluid
cycle
source temperature
expansion
auxiliary
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EP07354062.7A
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German (de)
French (fr)
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EP1927816A1 (en
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Maxime Ducoulombier
Stéphane Colasson
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Commissariat a lEnergie Atomique et aux Energies Alternatives CEA
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Commissariat a lEnergie Atomique et aux Energies Alternatives CEA
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Classifications

    • 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
    • F25B1/00—Compression machines, plants or systems with non-reversible cycle
    • F25B1/10—Compression machines, plants or systems with non-reversible cycle with multi-stage 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B40/00—Subcoolers, desuperheaters or superheaters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being 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
    • F25B2309/00—Gas cycle refrigeration machines
    • F25B2309/06—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide
    • F25B2309/061—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide with cycle highest pressure above the supercritical pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/06—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point using expanders

Definitions

  • thermodynamic refrigeration cycle or vapor compression cycle, using carbon dioxide CO 2 as a refrigerant
  • the hot source temperature is the minimum temperature at which the refrigerant can reject heat
  • the cold source temperature is the maximum temperature at which the refrigerant can absorb heat.
  • the critical temperature T crit of CO 2 is 31.1 ° C. Beyond this temperature, the CO 2 is neither in the liquid state nor in the gaseous state, but in the supercritical state, in the form of a dense gas.
  • the figure 1 represents an enthalphic diagram of the pressure P as a function of the enthalpy h of a conventional version, called Evans-Perkins, of a vapor compression transcritical cycle according to the prior art.
  • the cycle using carbon dioxide CO 2 , with and without internal heat exchanger, the temperature conditions are as follows, namely a hot source temperature T C of 35 ° C and a cold source temperature T F of 0 ° vs.
  • the vapor compression transcritical cycle according to Evans-Perkins, schematically represented by a solid line through points 1 to 4 on the figure 1 , works by following the following four transformations.
  • the cycle comprises a first stage 1-2 of isentropic compression of the fluid, that is to say without losses.
  • the CO 2 in the saturated vapor state (point 1) is compressed from the low pressure level (LP) to the high pressure level (HP), for example via a compressor.
  • w C represents the mass compression work.
  • the cycle comprises a second stage 2-3 of isobaric cooling of the fluid.
  • the CO 2 at the outlet of the compressor (point 2) is cooled substantially to the hot source temperature T C (point 3).
  • T C hot source temperature
  • Step 2-3 is performed, for example, through a gas cooler, commonly called “gas cooler” in English.
  • the cycle comprises a step 3-4 of isenthalpic expansion of the fluid, that is to say without exchange of work or heat.
  • the supercritical CO 2 is expanded to the low pressure level via, for example, an expansion valve, where it takes the form of a liquid-vapor mixture (point 4).
  • q R represents the refrigeration mass capacity
  • the first modification consists in making the compression of step 1-2 and non-isentropic isothermal, in order to reduce the mass compression work w C. This can be done by performing a staged compression, including the addition of an intermediate gas cooler.
  • the second modification consists of recovering the relaxation work to perform isentropic and nonisenthalpic relaxation between points 3 and 4 of the cycle.
  • piston, screw, ejector, spiro-orbital and other systems can be used.
  • the third modification consists in cooling the CO 2 at the outlet of the gas cooler (point 3 on the figure 1 ), in particular to reduce the relaxation losses.
  • an internal exchanger can be used.
  • On the figure 1 such a modification corresponds to the cycle passing through points 1 'to 4'. This is to cool the CO 2 high pressure between points 3 and 3 ', superheating the saturated steam recovered at the end of evaporation, namely between points 1 and 1'.
  • the increase in the compression work between the points 1 'and 2' is compensated by a greater increase in the cooling capacity between the points 4 'and 1.
  • heat exchange is limited by the difference in specific heat between CO 2 at high pressure and CO 2 at low pressure.
  • the internal exchanger is supposed to be perfect, that is to say having a temperature at point 1 'equal to the temperature at point 3 ( figure 1 )
  • the CO 2 can not be cooled down to the lowest temperature, namely the cold source temperature T F or the evaporation temperature.
  • the relaxation losses can therefore be further reduced provided that the CO 2 temperature approaches the cold source temperature T F before the isenthalpic expansion step 3-4, as shown schematically by the arrows between the points 3 'and 3 ". and 4 'and 4 "on the figure 1 .
  • the principle consists in using a mass fraction y of CO 2 at the outlet of the gas cooler, namely at point 6 on the figure 2 , in an auxiliary cooling circuit for cooling the remaining complementary mass fraction 1-y of CO 2 , flowing in a main circuit of the cycle.
  • the cycle comprises a CO 2 heating step 1-2, followed by a step 2-3 of isentropic compression and a step 3-4 of isobaric cooling. Then, according to the Lorentzen cycle, a new step 4-5 of isentropic compression is performed, followed by a new isobaric cooling step 5-6, in order to reach the hot source temperature T C. The fluid is then separated in two and the mass fraction y of fluid, according to the auxiliary cooling circuit shown in dotted lines on the figure 2 , is then relaxed between points 6 and 10 of the cycle until reaching an intermediate pressure P int .
  • the two-phase mixture is evaporated and then superheated between the points 10 and 4 of the cycle, until reaching the hot source temperature T C , the temperature at which the CO 2 at high pressure exits the gas cooler.
  • the mass fraction is determined in such a way that the complementary mass fraction 1-y of high pressure CO 2 at the outlet of the cooler reaches the saturation temperature T sat at the intermediate pressure, namely the temperature at point 7 and at point 10, of the order of 17.83 ° C.
  • the mass fraction 1-y of CO 2 at high pressure exiting the cooler then passes into an internal exchanger and its temperature decreases further between the points 7 and 8 of the cycle. Then, the fraction 1-y mass of CO 2 is expanded between points 8 and 9 of the cycle, to reach the cold source temperature T F.
  • the CO 2 at intermediate pressure P int namely between points 10 and 4 of the figure 2
  • the fluid at the inlet of the expansion valve intended to perform the expansion step on the main circuit of the cycle (point 8 of the cycle of the figure 2 ) can not reach the cold source temperature T F.
  • the vapor compression device 11 comprises an internal heat exchanger 12, a compressor 13 connected to the outlet of the exchanger 12, a gas cooler 14 connected to the outlet of the compressor 13, and a fluid distributor ( point 4 of the figure 3 ) separating the cycle into a main circuit 1-y and an auxiliary cooling circuit y.
  • the auxiliary cooling circuit y comprises an auxiliary expansion system 15, for example a turbine, connected to the inlet of the internal heat exchanger 12, so as to form a cooling loop, and the main circuit 1-y, preferably passing through the exchanger 12 connected to the output of the fluid distributor, comprises a main expansion system 16, for example an expansion valve, connected to the outlet of the exchanger 12.
  • the passage of the fluid in the exchanger 12 on the main circuit 1-y allows in particular to lower as much as possible the CO 2 high pressure temperature, before its passage through the main expansion system 16, to reduce the irreversibilities associated with relaxation.
  • the main circuit 1-y also comprises an evaporator 17, operating at low pressure, connected to the output of the main expansion system 16 and the inlet of the heat exchanger 12 internal heat, and therefore the output of the auxiliary relief system (point 1 of the figure 3 ).
  • the cycle conventionally comprises a heating step 1-2 between points 1 and 2 of the cycle ( Figures 3 and 4 ) via the internal heat exchanger 12 ( figure 3 ), until reaching the hot source temperature T C , followed by a step 2-3 of isentropic compression via the compressor 13 operating at low pressure ( figure 3 ). Then, a step 3-4 of isobaric cooling is carried out between the points 3 and 4 of the cycle, via the isobaric gas cooler 14, until the temperature of the hot source T C is reached again ( figure 3 ). The high pressure fluid, after having passed through the gas cooler 14, is then split in two, via the fluid distributor (point 4 of the figure 4 ). In a first main circuit, a mass fraction 1-y of fluid is cooled in a step 4-5 of isobaric cooling, by through the internal heat exchanger 12 until a temperature close to the cold source temperature T F ( figure 4 ).
  • a remaining mass fraction y of fluid is used in a second auxiliary cooling circuit, namely a "sub-cycle" of refrigeration passing through points 1 to 4, commonly referred to as the reverse Brayton cycle.
  • the cycle proposed by Meunier is an ideal cycle composed of isothermal compression (with heat rejection) and isothermal expansion (with absorption of heat).
  • an isentropic compression between the points 2 and 3 of the cycle and an isenthalpic expansion between the points 5 and 6 of the cycle are represented, these steps being closer to the technological reality of implementation of the cycle.
  • the relaxation of the mass fraction y of the fluid, between the points 4 and 1 of the cycle, is isentropic, that is to say that the work is recovered. If this were not the case, the coefficient of performance COP (Coefficient Of Performance) would be disadvantageous, notably less than the coefficient of performance obtained in a cycle according to Evans-Perkins as described above.
  • the low pressure fluid vapor, in particular CO 2 which enters the exchanger 12 of the figure 3 must not be overheated, otherwise the CO 2 at high pressure can not reach the minimum temperature, that of the evaporator 17, namely the cold source temperature T F.
  • the pressure before the expansion between points 4 and 1 of the cycle, that is to say the high pressure P HP can not fall below a certain threshold called minimum pressure P min .
  • This is the configuration of the figure 4 in which the high pressure P HP is equal to the minimum pressure P min .
  • the increase of the high pressure P HP can lead to a decrease in efficiency because, on the one hand, the compression work is more important and, on the other hand, the point 1 of the cycle moves under the saturation bell, that is to say under the parabola representative of the phase diagram of CO 2 delimiting the different states (solid, liquid, gaseous) of CO 2 .
  • the CO 2 is two- phase between points 1 and 2 of the cycle, which increases the irreversibilities in the heat exchanger 12 internal heat.
  • the Meunier cycle described above is not suitable, the cycle presenting in certain sections, in particular in the exchanger 12, two phases of the fluid (liquid and vapor).
  • the monophasic state of the fluid is therefore not possible throughout the exchanger 12, especially if the hot source temperature T C is less than 56 ° C.
  • the fluid is only monophasic in the heat exchanger 12, but at the cost of overconsumption of energy and a degraded performance of the cycle, the discharges being at non-acceptable temperatures, that is to say, too high, typically of the order of 56 ° C for CO 2 .
  • the document US-2005/0044865 discloses a vapor compression device for a fluid transcritical cycle, comprising an intermediate pressure vessel, wherein the mass of active fluid can be temperature controlled to control the efficiency and capacity of the device.
  • the object of the invention is to remedy all of the aforementioned drawbacks and is intended to provide a vapor compression device for a transcritical fluid cycle, to reduce the irreversibilities in the internal heat exchanger, in order to obtain a better cycle efficiency, by ensuring that the refrigerant, in particular carbon dioxide, remains monophasic throughout the cycle; internal heat exchanger.
  • the invention also relates to a method for producing a transcritical fluid cycle, more particularly carbon dioxide, by means of such a vapor compression device, which is easy to implement and which offers optimum performance. of the cycle.
  • the vapor compression device 11 ( figure 5 ) relates to a new thermodynamic refrigeration cycle, that is to say a vapor compression cycle. It is particularly suitable for the use of carbon dioxide CO 2 as a refrigerant.
  • CO 2 carbon dioxide
  • the interest in CO 2 comes from its low environmental impact with regard to the commonly used fluorinated synthetic refrigerants, the Freons, some of which destroy the ozone layer and which for others are greenhouse gases (generally more than a thousand times more powerful than CO 2 ).
  • CO 2 is neither toxic nor flammable.
  • the device 11 differs from the device according to the Meunier cycle ( figure 3 ) by adding a compressor 18, operating at high pressure, on the main circuit 1-y of the cycle.
  • the new compression stage defined by the high-pressure compressor 18 then requires the addition of a second associated isobaric gas cooler 19, placed on the main circuit of the fluid 1-y, after the fluid distributor (point 4 on the figure 5 ), between the output of the high-pressure compressor 18 and the inlet of the internal heat exchanger 12.
  • the vapor compression device 11 comprises the same elements as the device according to the Meunier cycle with an internal heat exchanger 12, a low-pressure compressor 13, an associated isobaric gas cooler 14, an auxiliary expansion system 15 on the auxiliary cycle cooling circuit y, a main expansion system 16, on the main circuit 1-y of the cycle, and an evaporator 17 operating at low pressure.
  • the operation of the device is the same with a fluid dispenser, more particularly CO 2 , placed at point 4 of the cycle ( figure 5 ), for separating the fluid so that a mass fraction y of the fluid follows the auxiliary cooling cycle and in particular allows to cool the fluid of the main circuit 1-y at the inlet of the heat exchanger 12 internal heat.
  • the auxiliary and main expansion systems can be simple systems, such as valve, capillary, etc.
  • the auxiliary and main expansion systems 15 may each be associated, or may even be each substituted, a system, respectively auxiliary and main, working recovery, more particularly the work of relaxation.
  • the auxiliary and main work recovery systems may be positive displacement machines, piston type, or non-positive displacement machines, turbine type.
  • the auxiliary and main work recovery systems are independent and it is possible to recover work on one and / or the other of the systems.
  • auxiliary and main work recovery systems can advantageously be mechanically and / or electrically coupled to one and / or the other of the low-pressure 13 and high-pressure compressors 18 ( figure 5 ), in particular to reduce the energy consumption of the steam compression device 11.
  • the high pressure compressor 18 is intended in particular to increase the CO 2 pressure, which circulates in the exchanger 12, so that it is supercritical, that is to say, it has a temperature above the critical temperature T crit of the order of 31.1 ° C ( figure 6 ).
  • such a device then makes it possible to increase the CO 2 pressure at the outlet of the high-pressure compressor 18, so that the corresponding isobaric cooling between points 6 and 7 takes place under supercritical conditions, as described hereinafter. That is to say that the CO 2 is monophasic, namely that it passes over the representative parabola of the phase diagram of CO 2 , representing the saturation bell delimiting the different states (solid, liquid, gas) of the CO 2 ( figure 4 ).
  • a method of performing a transcritical fluid cycle, more particularly CO 2 , by means of the vapor compression device 11 shown in FIG. figure 5 will be described in more detail with regard to figure 6 , showing an enthalpy diagram of pressure versus enerhalpy, between a hot source temperature T C of 35 ° C and a cold source temperature T F of 0 ° C.
  • the cycle comprises a heating step 1-2 between points 1 and 2 of the cycle, via the internal heat exchanger 12 ( figure 5 ), until reaching the hot source temperature T C , followed by a step 2-3 compression, preferably isentropic, through the low pressure compressor 13 ( figure 5 ).
  • a step 3-4 of CO 2 isobaric cooling is preferably carried out between points 3 and 4 of the cycle, via the isobaric gas cooler 14 ( figure 5 ), until reaching the hot source temperature T C again at point 4 of the cycle
  • the CO 2 is then split in two at point 4 of the device 11 ( figure 5 ) via the fluid distributor, to obtain, in a first circuit main, a mass fraction 1-y of CO 2 , and in a second auxiliary cooling circuit; a mass fraction y of CO 2 , used in a "sub-cycle" of refrigeration between points 1 to 4 of the cycle.
  • the CO 2 is then at a mean pressure P MP , or intermediate pressure, and at the hot source temperature T C.
  • the average pressure P MP is chosen so that the mass fraction y of the CO 2 after passing through the auxiliary expansion system, which is connected to the low pressure inlet of the internal heat exchanger 12 of the cycle ( figure 5 ), ie after step 4-1 of expansion of the mass fraction y of CO 2 , can be mixed with the remaining mass fraction 1-y of CO 2 leaving the evaporator 17, to reach a superheated vapor state ( figure 5 ), as close as possible to the state of saturated vapor.
  • Point 1 of the cycle represented on the figure 6 is then advantageously on the parabola representative of the phase diagram of CO 2 , representing the saturation curve delimiting the various states (solid, liquid, gas) CO 2 .
  • the relaxation step 4-1 described above, on the auxiliary cooling circuit y may be isenthalpic or isentropic. Furthermore, the cycle operating continuously, the steps below relating to the main circuit 1-y of the cycle are performed simultaneously with the step 4-1 of relaxation, performed on the circuit y auxiliary cooling.
  • the mass fraction 1-y of CO 2 then passes into the high-pressure compressor 18, in order to undergo a step 4-5 compression, preferably isentropic, between points 4 and 5 of the cycle ( Figures 5 and 6 ).
  • the high-pressure compressor 18 makes it possible in particular to reject the CO 2 at a maximum high pressure P HP supercritical, higher than the pressure Critical P crit of CO 2 , at which the CO 2 has a very high temperature, typically higher than 60 ° C (point 5 of the cycle).
  • the CO 2 is then in a supercritical state, that is to say that it passes over the representative parabola of the CO 2 phase diagram, associated with the critical temperature T crit , representing the saturation bell of the CO 2 delimiting the various states (solid, liquid, gaseous) of CO 2 .
  • the CO 2 is subjected to a step 5-6 of cooling, preferably isobaric through the associated gas cooler 19, connected to the output of the high pressure compressor 18, until it again substantially reaches the hot source temperature T C at point 6 of the cycle
  • the CO 2 passes back into the internal heat exchanger 12, on the main circuit 1-y of the cycle, which then performs a step 6-7 cooling, preferably isobaric of the mass fraction 1-y of CO 2 at high pressure, leaving the high pressure compressor 18 and the associated gas cooler 19.
  • a step 6-7 cooling preferably isobaric of the mass fraction 1-y of CO 2 at high pressure, leaving the high pressure compressor 18 and the associated gas cooler 19.
  • a step 7-8 of isenthalpic or isentropic expansion is then performed, on the main circuit 1-y of the cycle, through the main expansion system 16, in order to pass CO 2 from the high pressure value HP at a low pressure value P BP .
  • the fluid passes into the evaporator 17, operating at low pressure, in order to complete the cycle by an isobaric evaporation step 8-1, until reaching point 1, starting point of the cycle, at the temperature of cold source T F.
  • Such a method of carrying out a transcritical CO 2 cycle by means of such a vapor compression device 11 makes it possible to operate the main refrigeration cycle at a high pressure P HP higher than the critical pressure P crit , while the auxiliary cooling circuit operates at an average pressure P MP , lower than the high pressure P HP .
  • Such a vapor compression device 11 with a staged compression system formed by the low-pressure compressor 13 and the high-pressure compressor 18, is very simple to implement simply by adding two elements to the circuit main 1-y cycle (compressor and gas cooler operating at high pressure).
  • Such a vapor compression device 11 thus makes it possible to obtain a transcritical fluid cycle, more particularly of CO 2 , with a better efficiency of the internal heat exchanger 12, in particular thanks to the use of a monophasic fluid, which allows a minimum temperature difference between the low pressure side and the high pressure side of the vapor compression device 11 according to the invention.
  • figure 7 represents a graph illustrating the variation of the coefficient of performance COP as a function of the high pressure value P HP , for different transcritical cycles, namely according to Evans-Perkins (curve in solid single line), according to Lorentzen (curve with triangles), according to Meunier (curve with squares) and according to the invention (curve with circles). It appears from figure 7 that it is possible to optimize the performance of the transcritical cycle as a function of the high pressure P HP , for the hot source temperature values T C of 35 ° C and cold source T F of 0 ° C.
  • the COP goes through a maximum (black circle) at a pressure P HP of the order of 8.4 MPa, thus offering a relative improvement especially with respect to Evans-Perkins basic cycle (single solid curve) of the order of 34.4% and compared to the Lorentzen cycle (curve with triangles) of the order of 3.9%.
  • the invention is not limited to the various embodiments described above.
  • the method may include in particular a simple step 2-4 of fluid compression, to reach the average pressure P MP and to reach the hot source temperature T C , and a simple step 4-6 of fluid compression, to reach the maximum high pressure P HP , higher than the critical pressure P crit of the fluid, and to reach the hot source temperature T C.
  • the low pressure compressors 13 and high pressure 18 and the low pressure gas coolers 14 and high pressure 19 can be any vapor compression system and any gas cooling system capable of operating at high pressure and / or low pressure, depending on their position in the circuit associated with the vapor compression device 11.
  • the vapor compression device 11 may include any type of vapor compression system, any type of isobaric cooling system, any type of simultaneous compression cooling system, any type of fluid dispenser, any auxiliary expansion system, for the auxiliary cooling circuit, and any main expansion system, for the main circuit, as long as the vapor compression device makes it possible in particular to have a single-phase fluid on both sides of the heat exchanger 12 internal, in order to reduce the irreversibilities in the internal heat exchanger 12, while maintaining the temperature of the high pressure fluid at the outlet of the exchanger 12 as close as possible to the cold source temperature T F.

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Description

Domaine technique de l'inventionTechnical field of the invention

L'invention concerne un dispositif à compression de vapeur, pour un cycle transcritique de fluide, comportant au moins :

  • un échangeur de chaleur interne,
  • un premier système de compression de vapeur, relié à la sortie de l'échangeur de chaleur interne,
  • un premier système de refroidissement isobare, relié à la sortie du premier système de compression de vapeur,
  • un distributeur de fluide, placé à la sortie du premier système de refroidissement isobare et séparant le fluide dans un circuit principal du cycle et dans un circuit de refroidissement auxiliaire du cycle,
  • un système de détente auxiliaire, placé sur le circuit de refroidissement auxiliaire entre le distributeur de fluide et l'entrée de l'échangeur de chaleur interne,
  • un système de détente principal, placé sur le circuit principal et relié à la sortie de l'échangeur de chaleur interne,
  • un évaporateur fonctionnant à basse pression, placé entre la sortie du système de détente principal et l'entrée de l'échangeur de chaleur interne.
The invention relates to a vapor compression device for a transcritical fluid cycle comprising at least:
  • an internal heat exchanger,
  • a first steam compression system, connected to the outlet of the internal heat exchanger,
  • a first isobaric cooling system connected to the outlet of the first vapor compression system,
  • a fluid distributor, placed at the outlet of the first isobaric cooling system and separating the fluid in a main circuit of the cycle and in an auxiliary cooling circuit of the cycle,
  • an auxiliary expansion system, placed on the auxiliary cooling circuit between the fluid distributor and the inlet of the internal heat exchanger,
  • a main expansion system, placed on the main circuit and connected to the outlet of the internal heat exchanger,
  • an evaporator operating at low pressure, placed between the output of the main expansion system and the inlet of the internal heat exchanger.

L'invention concerne également un procédé de réalisation d'un cycle transcritique de fluide, entre une température de source chaude et une température de source froide, au moyen d'un tel dispositif à compression de vapeur, comportant au moins les étapes de :

  • chauffage du fluide dans l'échangeur de chaleur interne, jusqu'à atteindre la température de source chaude,
  • compression du fluide, pour atteindre une pression moyenne et pour atteindre la température de source chaude,
  • séparation du fluide par le distributeur de fluide dans un circuit principal du cycle et dans un circuit de refroidissement auxiliaire du cycle,
  • détente du fluide sur le circuit de refroidissement auxiliaire, par le système de détente auxiliaire, jusqu'à atteindre la température de source froide,
  • détente du fluide sur le circuit principal, par le système de détente principal, jusqu'à atteindre la température de source froide,
  • évaporation isobare du fluide sur le circuit principal.
The invention also relates to a method for producing a transcritical fluid cycle, between a hot source temperature and a cold source temperature, by means of such a vapor compression device, comprising at least the steps of:
  • heating the fluid in the internal heat exchanger until reaching the hot source temperature,
  • compression of the fluid, to reach a mean pressure and to reach the hot source temperature,
  • separating the fluid from the fluid distributor in a main circuit of the cycle and in an auxiliary cooling circuit of the cycle,
  • expansion of the fluid on the auxiliary cooling circuit, by the auxiliary expansion system, until reaching the cold source temperature,
  • expansion of the fluid on the main circuit, by the main expansion system, until reaching the cold source temperature,
  • isobaric evaporation of the fluid on the main circuit.

État de la techniqueState of the art

De manière classique, un cycle thermodynamique de réfrigération, ou cycle à compression de vapeur, utilisant le dioxyde de carbone CO2 comme réfrigérant, fonctionne entre une température de source chaude TC et une température de source froide TF. La température de source chaude est la température minimale à laquelle le fluide frigorigène peut rejeter la chaleur, alors que la température de source froide est la température maximale à laquelle le fluide frigorigène peut absorber la chaleur. La température critique Tcrit du CO2 est de 31.1°C. Au-delà de cette température, le CO2 n'est ni à l'état liquide, ni à l'état gazeux, mais à l'état supercritique, sous la forme d'un gaz dense.Conventionally, a thermodynamic refrigeration cycle, or vapor compression cycle, using carbon dioxide CO 2 as a refrigerant, operates between a hot source temperature T C and a cold source temperature T F. The hot source temperature is the minimum temperature at which the refrigerant can reject heat, while the cold source temperature is the maximum temperature at which the refrigerant can absorb heat. The critical temperature T crit of CO 2 is 31.1 ° C. Beyond this temperature, the CO 2 is neither in the liquid state nor in the gaseous state, but in the supercritical state, in the form of a dense gas.

Or, dans la plupart des applications de production de froid (mode réfrigérateur) ou de production de chaud (mode pompe à chaleur), la température de rejet de la chaleur est supérieure à la température critique du CO2. Un cycle à compression de vapeur au CO2 fonctionnera ainsi généralement entre une température de source froide « souscritique » et une température de source chaude « supercritique ». Un tel cycle est alors communément appelé « transcritique ».However, in most applications of cold production (refrigerator mode) or production of heat (heat pump mode), the heat rejection temperature is higher than the critical temperature of CO 2 . A CO 2 vapor compression cycle will thus generally operate between a "subcritical" cold source temperature and a "supercritical" hot source temperature. Such a cycle is then commonly called "transcritical".

À titre d'exemple, la figure 1 représente un diagramme enthalphique de la pression P en fonction de l'enthalpie h d'une version classique, appelée Evans-Perkins, d'un cycle transcritique à compression de vapeur selon l'art antérieur. Le cycle utilisant le dioxyde de carbone CO2, avec et sans échangeur de chaleur interne, les conditions de températures sont les suivantes, à savoir une température de source chaude TC de 35°C et une température de source froide TF de 0°C.For example, the figure 1 represents an enthalphic diagram of the pressure P as a function of the enthalpy h of a conventional version, called Evans-Perkins, of a vapor compression transcritical cycle according to the prior art. The cycle using carbon dioxide CO 2 , with and without internal heat exchanger, the temperature conditions are as follows, namely a hot source temperature T C of 35 ° C and a cold source temperature T F of 0 ° vs.

Le cycle transcritique à compression de vapeur, selon Evans-Perkins, représenté schématiquement par un trait plein passant par les points 1 à 4 sur la figure 1, fonctionne en suivant les quatre transformations suivantes.The vapor compression transcritical cycle, according to Evans-Perkins, schematically represented by a solid line through points 1 to 4 on the figure 1 , works by following the following four transformations.

Entre les points 1 et 2, le cycle comporte une première étape 1-2 de compression isentropique du fluide, c'est-à-dire sans pertes. Pendant cette transformation, le CO2 à l'état de vapeur saturée (point 1) est comprimé du niveau basse pression (BP) au niveau haute pression (HP), par l'intermédiaire, par exemple, d'un compresseur. Sur la figure 1, wC représente le travail massique de compression.Between points 1 and 2, the cycle comprises a first stage 1-2 of isentropic compression of the fluid, that is to say without losses. During this transformation, the CO 2 in the saturated vapor state (point 1) is compressed from the low pressure level (LP) to the high pressure level (HP), for example via a compressor. On the figure 1 , w C represents the mass compression work.

Entre les points 2 et 3, le cycle comporte une deuxième étape 2-3 de refroidissement isobare du fluide. Pendant cette transformation, le CO2 en sortie du compresseur (point 2) est refroidi sensiblement jusqu'à la température de source chaude TC (point 3). Il y a un glissement de température, car le fluide est monophasique, c'est-à-dire qu'il n'y a pas de condensation. L'étape 2-3 est réalisée, par exemple, par l'intermédiaire d'un refroidisseur de gaz, communément appelé « gas cooler » en anglais.Between points 2 and 3, the cycle comprises a second stage 2-3 of isobaric cooling of the fluid. During this transformation, the CO 2 at the outlet of the compressor (point 2) is cooled substantially to the hot source temperature T C (point 3). There is a temperature shift, because the fluid is monophasic, that is to say that there is no condensation. Step 2-3 is performed, for example, through a gas cooler, commonly called "gas cooler" in English.

Entre les points 3 et 4, le cycle comporte une étape 3-4 de détente isenthalpique du fluide, c'est-à-dire sans échange de travail, ni de chaleur. Pendant cette transformation, le CO2 supercritique est détendu jusqu'au niveau basse pression, par l'intermédiaire, par exemple, d'une valve de détente, où il prend la forme d'un mélange liquide-vapeur (point 4).Between points 3 and 4, the cycle comprises a step 3-4 of isenthalpic expansion of the fluid, that is to say without exchange of work or heat. During this transformation, the supercritical CO 2 is expanded to the low pressure level via, for example, an expansion valve, where it takes the form of a liquid-vapor mixture (point 4).

Entre les points 4 et 1, le cycle se reboucle par une étape 4-1 d'évaporation par l'intermédiaire, par exemple, d'un évaporateur. Pendant cette transformation, la phase liquide du CO2 est totalement évaporée, ce qui correspond à une absorption de chaleur. Sur la figure 1, qR représente la capacité massique de réfrigération.Between points 4 and 1, the cycle loops back by a step 4-1 of evaporation via, for example, an evaporator. During this transformation, the liquid phase of the CO 2 is completely evaporated, which corresponds to a heat absorption. On the figure 1 , q R represents the refrigeration mass capacity.

Le CO2, quand il est utilisé dans un tel cycle, a une efficacité inférieure à celle des réfrigérants conventionnels, du type Fréon, utilisés dans un cycle « souscritique » fonctionnant entre les mêmes températures de source chaude TC et de source froide TF. Deux raisons principales peuvent être avancées. La première est que la température moyenne de rejet de la chaleur est plus élevée, pour une température de source chaude TC donnée, puisque ce rejet ne se fait pas à température constante. La seconde raison est que des irréversibilités importantes pendant la détente isenthalpique (étape 3-4) sont observées, à savoir des pertes de détente, sous forme de travail non récupéré et d'une diminution équivalente de la capacité frigorifique δw (figure 1).CO 2 , when used in such a cycle, has a lower efficiency than conventional refrigerants, of the Freon type, used in a "subcritical" cycle operating between the same hot source temperatures T C and cold source T F . Two main reasons can be advanced. The first is that the average temperature of heat rejection is higher for a given hot source temperature T C , since this rejection is not done at constant temperature. The second reason is that significant irreversibilities during the isenthalpic expansion (step 3-4) are observed, namely relaxation losses, in the form of unrecovered work and an equivalent decrease in cooling capacity δw ( figure 1 ).

Afin d'améliorer la performance du CO2, il faut donc adapter le cycle thermodynamique de réfrigération. Trois types de modification sont généralement proposés. La première modification consiste à rendre isotherme la compression de l'étape 1-2 et non isentropique, afin de réduire le travail de compression massique wC. Cela peut se faire en réalisant une compression étagée, avec notamment l'ajout d'un refroidisseur de gaz intermédiaire.In order to improve the performance of CO 2 , it is necessary to adapt the thermodynamic refrigeration cycle. Three types of modification are generally proposed. The first modification consists in making the compression of step 1-2 and non-isentropic isothermal, in order to reduce the mass compression work w C. This can be done by performing a staged compression, including the addition of an intermediate gas cooler.

La deuxième modification consiste à récupérer le travail de détente pour effectuer une détente isentropique et non isenthalpique entre les points 3 et 4 du cycle. À titre d'exemple, des systèmes à piston, à vis, à éjecteur, spiro-orbital et d'autres peuvent être utilisés.The second modification consists of recovering the relaxation work to perform isentropic and nonisenthalpic relaxation between points 3 and 4 of the cycle. For example, piston, screw, ejector, spiro-orbital and other systems can be used.

La troisième modification consiste à refroidir le CO2 en sortie du refroidisseur de gaz (point 3 sur la figure 1), afin notamment de réduire les pertes de détente. Pour réaliser cette modification, un échangeur interne peut être utilisé. Sur la figure 1, une telle modification correspond au cycle passant par les points 1' à 4'. Il s'agit de refroidir le CO2 haute pression entre les points 3 et 3', en surchauffant la vapeur saturée récupérée en fin d'évaporation, à savoir entre les points 1 et 1'. Dans ce cas, l'augmentation du travail de compression entre les points 1' et 2' est compensée par une augmentation plus importante de la capacité frigorifique entre les points 4' et 1.The third modification consists in cooling the CO 2 at the outlet of the gas cooler (point 3 on the figure 1 ), in particular to reduce the relaxation losses. To make this change, an internal exchanger can be used. On the figure 1 such a modification corresponds to the cycle passing through points 1 'to 4'. This is to cool the CO 2 high pressure between points 3 and 3 ', superheating the saturated steam recovered at the end of evaporation, namely between points 1 and 1'. In this case, the increase in the compression work between the points 1 'and 2' is compensated by a greater increase in the cooling capacity between the points 4 'and 1.

Cependant, l'échange de chaleur est limité par la différence de chaleur massique entre le CO2 à haute pression et le CO2 à basse pression. Autrement dit, même si l'échangeur interne est supposé parfait, c'est-à-dire présentant une température au point 1' égale à la température au point 3 (figure 1), le CO2 ne peut être refroidi jusqu'à la température la plus basse, à savoir la température de source froide TF ou température d'évaporation.However, heat exchange is limited by the difference in specific heat between CO 2 at high pressure and CO 2 at low pressure. In other words, even if the internal exchanger is supposed to be perfect, that is to say having a temperature at point 1 'equal to the temperature at point 3 ( figure 1 ), the CO 2 can not be cooled down to the lowest temperature, namely the cold source temperature T F or the evaporation temperature.

Les pertes de détente peuvent donc encore être réduites à condition que la température du CO2 approche la température de source froide TF avant l'étape 3-4 de détente isenthalpique, comme représenté schématiquement par les flèches entre les points 3' et 3" et 4' et 4" sur la figure 1.The relaxation losses can therefore be further reduced provided that the CO 2 temperature approaches the cold source temperature T F before the isenthalpic expansion step 3-4, as shown schematically by the arrows between the points 3 'and 3 ". and 4 'and 4 "on the figure 1 .

Une première solution a été proposée, notamment dans l'article « Revival of carbon dioxide as a refrigérant » de G. Lorentzen (1994, International Journal of Refrigeration, 17(5), pp. 292-301 ), qui décrit l'utilisation du CO2 comme son propre réfrigérant pour le refroidir avant la détente. Pour cela, un cycle avec un fluide fractionné est utilisé, ce qui donne lieu à une compression étagée.A first solution has been proposed, particularly in the article "Revival of carbon dioxide as a refrigerant" by G. Lorentzen (1994, International Journal of Refrigeration, 17 (5), pp. 292-301 ), which describes the use of CO 2 as its own refrigerant to cool it before relaxation. For this, a cycle with a fractional fluid is used, which gives rise to a staged compression.

Comme représenté sur le diagramme enthalpique de la figure 2, illustrant le cycle thermodynamique selon la solution proposée par Lorentzen, le principe consiste à utiliser une fraction massique y du CO2 en sortie du refroidisseur de gaz, à savoir au point 6 sur la figure 2, dans un circuit de refroidissement auxiliaire permettant de refroidir la fraction massique restante complémentaire 1-y du CO2, circulant dans un circuit principal du cycle.As shown in the enthalpy diagram of the figure 2 , illustrating the thermodynamic cycle according to the solution proposed by Lorentzen, the principle consists in using a mass fraction y of CO 2 at the outlet of the gas cooler, namely at point 6 on the figure 2 , in an auxiliary cooling circuit for cooling the remaining complementary mass fraction 1-y of CO 2 , flowing in a main circuit of the cycle.

Sur la figure 2, le cycle comporte une étape 1-2 de chauffage du CO2, suivie d'une étape 2-3 de compression isentropique et d'une étape 3-4 de refroidissement isobare. Puis, selon le cycle de Lorentzen, une nouvelle étape 4-5 de compression isentropique est réalisée, suivie par une nouvelle étape 5-6 de refroidissement isobare, afin d'atteindre la température de source chaude TC. Le fluide est alors séparé en deux et la fraction massique y de fluide, suivant le circuit de refroidissement auxiliaire représenté en traits pointillés sur la figure 2, est alors détendue entre les points 6 et 10 du cycle jusqu'à atteindre une pression intermédiaire Pint.On the figure 2 the cycle comprises a CO 2 heating step 1-2, followed by a step 2-3 of isentropic compression and a step 3-4 of isobaric cooling. Then, according to the Lorentzen cycle, a new step 4-5 of isentropic compression is performed, followed by a new isobaric cooling step 5-6, in order to reach the hot source temperature T C. The fluid is then separated in two and the mass fraction y of fluid, according to the auxiliary cooling circuit shown in dotted lines on the figure 2 , is then relaxed between points 6 and 10 of the cycle until reaching an intermediate pressure P int .

Ensuite, le mélange diphasique est évaporé puis surchauffé entre les points 10 et 4 du cycle, jusqu'à atteindre la température de source chaude TC, température à laquelle le CO2 à haute pression sort du refroidisseur de gaz. La fraction massique y est notamment déterminée, de façon à ce que la fraction massique complémentaire 1-y de CO2 à haute pression en sortie de refroidisseur atteigne la température de saturation Tsat à la pression intermédiaire, à savoir la température au point 7 et au point 10, de l'ordre de 17,83°C. La fraction massique 1-y de CO2 à haute pression sortant du refroidisseur passe alors ensuite dans un échangeur interne et sa température diminue encore entre les points 7 et 8 du cycle. Puis, la fraction massique 1-y de CO2 est détendue entre les points 8 et 9 du cycle, pour atteindre la température de source froide TF.Then, the two-phase mixture is evaporated and then superheated between the points 10 and 4 of the cycle, until reaching the hot source temperature T C , the temperature at which the CO 2 at high pressure exits the gas cooler. In particular, the mass fraction is determined in such a way that the complementary mass fraction 1-y of high pressure CO 2 at the outlet of the cooler reaches the saturation temperature T sat at the intermediate pressure, namely the temperature at point 7 and at point 10, of the order of 17.83 ° C. The mass fraction 1-y of CO 2 at high pressure exiting the cooler then passes into an internal exchanger and its temperature decreases further between the points 7 and 8 of the cycle. Then, the fraction 1-y mass of CO 2 is expanded between points 8 and 9 of the cycle, to reach the cold source temperature T F.

Cependant, une telle solution décrite ci-dessus présente deux limites. D'une part, le CO2 à pression intermédiaire Pint, à savoir entre les points 10 et 4 de la figure 2, est diphasique et sa température est constante, ce qui entraîne dans le refroidisseur un écart de température avec le CO2 à haute pression et donc des irréversibilités. D'autre part, le fluide à l'entrée de la valve de détente, destinée à réaliser l'étape de détente sur le circuit principal du cycle (point 8 du cycle de la figure 2), ne peut atteindre la température de source froide TF.However, such a solution described above has two limitations. On the one hand, the CO 2 at intermediate pressure P int , namely between points 10 and 4 of the figure 2 , is biphasic and its temperature is constant, which causes in the cooler a temperature difference with CO 2 at high pressure and therefore irreversibilities. On the other hand, the fluid at the inlet of the expansion valve, intended to perform the expansion step on the main circuit of the cycle (point 8 of the cycle of the figure 2 ), can not reach the cold source temperature T F.

Une autre solution utilisant un fluide comme son propre réfrigérant dans un cycle de liquéfaction a également été proposée dans l'article « Refrigeration Carnot-type cycle based on isothermal vapour compression » de F. Meunier, (2006, International Journal of Refrigeration, 29, pp. 155-158 ). L'article décrit l'adaptation du cycle de liquéfaction de Claude, pour l'utiliser comme cycle de réfrigération transcritique. Un mode particulier de réalisation d'un dispositif à compression de vapeur 11, pour la réalisation d'un cycle selon Meunier, est représenté schématiquement sur la figure 3.Another solution using a fluid as its own refrigerant in a liquefaction cycle has also been proposed in the article "Refrigeration Carnot-type cycle based on isothermal vapor compression" by F. Meunier, (2006, International Journal of Refrigeration, 29, pp. 155-158). ). The article describes the adaptation of Claude's liquefaction cycle to use as a transcritical refrigeration cycle. A particular embodiment of a vapor compression device 11, for carrying out a cycle according to Meunier, is shown schematically on the figure 3 .

Sur la figure 3, le dispositif à compression de vapeur 11 comporte un échangeur 12 de chaleur interne, un compresseur 13, relié à la sortie de l'échangeur 12, un refroidisseur de gaz 14, relié à la sortie du compresseur 13, et un distributeur de fluide (point 4 de la figure 3) séparant le cycle en un circuit principal 1-y et un circuit de refroidissement auxiliaire y. Le circuit de refroidissement auxiliaire y comporte un système de détente 15 auxiliaire, par exemple une turbine, relié à l'entrée de l'échangeur 12 de chaleur interne, de manière à former une boucle de refroidissement, et le circuit principal 1-y, passant de préférence par l'échangeur 12 relié à la sortie du distributeur de fluide, comporte un système de détente 16 principal, par exemple une vanne de détente, relié à la sortie de l'échangeur 12.On the figure 3 the vapor compression device 11 comprises an internal heat exchanger 12, a compressor 13 connected to the outlet of the exchanger 12, a gas cooler 14 connected to the outlet of the compressor 13, and a fluid distributor ( point 4 of the figure 3 ) separating the cycle into a main circuit 1-y and an auxiliary cooling circuit y. The auxiliary cooling circuit y comprises an auxiliary expansion system 15, for example a turbine, connected to the inlet of the internal heat exchanger 12, so as to form a cooling loop, and the main circuit 1-y, preferably passing through the exchanger 12 connected to the output of the fluid distributor, comprises a main expansion system 16, for example an expansion valve, connected to the outlet of the exchanger 12.

Dans le mode particulier de réalisation de la figure 3, le passage du fluide dans l'échangeur 12 sur le circuit principal 1-y permet notamment de baisser le plus possible la température du CO2 à haute pression, avant son passage dans le système de détente 16 principal, pour diminuer les irréversibilités associées à la détente. Par ailleurs, le circuit principal 1-y comporte également un évaporateur 17, fonctionnant à basse pression, relié à la sortie du système de détente 16 principal et à l'entrée de l'échangeur 12 de chaleur interne, et par conséquent à la sortie du système de détente 15 auxiliaire (point 1 de la figure 3).In the particular embodiment of the figure 3 , the passage of the fluid in the exchanger 12 on the main circuit 1-y allows in particular to lower as much as possible the CO 2 high pressure temperature, before its passage through the main expansion system 16, to reduce the irreversibilities associated with relaxation. Furthermore, the main circuit 1-y also comprises an evaporator 17, operating at low pressure, connected to the output of the main expansion system 16 and the inlet of the heat exchanger 12 internal heat, and therefore the output of the auxiliary relief system (point 1 of the figure 3 ).

Sur la figure 4, représentant un diagramme enthalpique illustrant le cycle selon le principe de Meunier, au moyen du dispositif à compression de vapeur 11 comme décrit ci-dessus, la différence de chaleur massique entre le fluide à haute pression (CO2) et le fluide à basse pression est compensée par une différence de débit massique dans l'échangeur de chaleur interne.On the figure 4 , showing an enthalpy diagram illustrating the cycle according to the Meunier principle, by means of the vapor compression device 11 as described above, the difference in specific heat between the high pressure fluid (CO 2 ) and the low pressure fluid is compensated by a mass flow difference in the internal heat exchanger.

Le cycle comporte classiquement une étape 1-2 de chauffage entre les points 1 et 2 du cycle (figures 3 et 4) par l'intermédiaire de l'échangeur 12 de chaleur interne (figure 3), jusqu'à atteindre la température de source chaude TC, suivie d'une étape 2-3 de compression isentropique par l'intermédiaire du compresseur 13 fonctionnant à basse pression (figure 3). Puis, une étape 3-4 de refroidissement isobare est réalisée entre les points 3 et 4 du cycle, par l'intermédiaire du refroidisseur de gaz 14 isobare, jusqu'à atteindre de nouveau la température dé source chaude TC (figure 3). Le fluide à haute pression, après être passé dans le refroidisseur de gaz 14, est alors fractionné en deux, par l'intermédiaire du distributeur de fluide (point 4 de la figure 4). Dans un premier circuit principal, une fraction massique 1-y de fluide est refroidie dans une étape 4-5 de refroidissement isobare, par l'intermédiaire de l'échangeur 12 de chaleur interne, jusqu'à atteindre une température proche de la température de source froide TF (figure 4).The cycle conventionally comprises a heating step 1-2 between points 1 and 2 of the cycle ( Figures 3 and 4 ) via the internal heat exchanger 12 ( figure 3 ), until reaching the hot source temperature T C , followed by a step 2-3 of isentropic compression via the compressor 13 operating at low pressure ( figure 3 ). Then, a step 3-4 of isobaric cooling is carried out between the points 3 and 4 of the cycle, via the isobaric gas cooler 14, until the temperature of the hot source T C is reached again ( figure 3 ). The high pressure fluid, after having passed through the gas cooler 14, is then split in two, via the fluid distributor (point 4 of the figure 4 ). In a first main circuit, a mass fraction 1-y of fluid is cooled in a step 4-5 of isobaric cooling, by through the internal heat exchanger 12 until a temperature close to the cold source temperature T F ( figure 4 ).

Une fraction massique restante y de fluide est utilisée dans un second circuit de refroidissement auxiliaire, à savoir un « sous cycle » de réfrigération passant par les points 1 à 4, communément appelé cycle de Brayton inverse. Sur la figure 4, la fraction massique y doit alors répondre à la contrainte suivante : (1- y)(h 4 - h 5)=h 2 - h 1.A remaining mass fraction y of fluid is used in a second auxiliary cooling circuit, namely a "sub-cycle" of refrigeration passing through points 1 to 4, commonly referred to as the reverse Brayton cycle. On the figure 4 , the mass fraction must then respond to the following constraint: (1- y ) ( h 4 - h 5 ) = h 2 - h 1 .

Initialement, le cycle proposé par Meunier est un cycle idéal composé d'une compression isotherme (avec rejet de chaleur) et d'une détente isotherme (avec absorption de chaleur). Sur la figure 4, une compression isentropique entre les points 2 et 3 du cycle et une détente isenthalpique entre les points 5 et 6 du cycle sont représentées, ces étapes étant plus proches de la réalité technologique de mise en oeuvre du cycle. La détente de la fraction massique y du fluide, entre les points 4 et 1 du cycle, est isentropique, c'est-à-dire que le travail est récupéré. Si ce n'était pas le cas, le coefficient de performance COP (« Coefficient Of Performance » en anglais) serait désavantageux, notamment inférieur au coefficient de performance obtenu dans un cycle selon Evans-Perkins comme décrit précédemment.Initially, the cycle proposed by Meunier is an ideal cycle composed of isothermal compression (with heat rejection) and isothermal expansion (with absorption of heat). On the figure 4 , an isentropic compression between the points 2 and 3 of the cycle and an isenthalpic expansion between the points 5 and 6 of the cycle are represented, these steps being closer to the technological reality of implementation of the cycle. The relaxation of the mass fraction y of the fluid, between the points 4 and 1 of the cycle, is isentropic, that is to say that the work is recovered. If this were not the case, the coefficient of performance COP (Coefficient Of Performance) would be disadvantageous, notably less than the coefficient of performance obtained in a cycle according to Evans-Perkins as described above.

Pour que le cycle puisse fonctionner, la vapeur de fluide à basse pression, notamment du CO2, qui rentre dans l'échangeur 12 de la figure 3, ne doit pas être surchauffée, sinon le CO2 à haute pression ne peut atteindre la température minimale, celle de l'évaporateur 17, à savoir la température dé source froide TF. La pression avant la détente entre les points 4 et 1 du cycle, c'est-à-dire la pression haute PHP, ne peut donc pas descendre en dessous d'un certain seuil appelé pression minimale Pmin. C'est la configuration de la figure 4, dans laquelle la pression haute PHP est égale à la pression minimale Pmin.For the cycle to operate, the low pressure fluid vapor, in particular CO 2 , which enters the exchanger 12 of the figure 3 must not be overheated, otherwise the CO 2 at high pressure can not reach the minimum temperature, that of the evaporator 17, namely the cold source temperature T F. The pressure before the expansion between points 4 and 1 of the cycle, that is to say the high pressure P HP , can not fall below a certain threshold called minimum pressure P min . This is the configuration of the figure 4 , in which the high pressure P HP is equal to the minimum pressure P min .

Cependant, dans de telles conditions, l'augmentation de la pression haute PHP peut entraîner une diminution de l'efficacité, car, d'une part, le travail de compression est plus important et, d'autre part, le point 1 du cycle se déplace sous la cloche de saturation, c'est-à-dire sous la parabole représentative du diagramme de phase du CO2 délimitant les différents états (solide, liquide, gazeux) du CO2. Il en résulte que le CO2 est diphasique entre les points 1 et 2 du cycle, ce qui augmente les irréversibilités dans l'échangeur 12 de chaleur interne.However, under such conditions, the increase of the high pressure P HP can lead to a decrease in efficiency because, on the one hand, the compression work is more important and, on the other hand, the point 1 of the cycle moves under the saturation bell, that is to say under the parabola representative of the phase diagram of CO 2 delimiting the different states (solid, liquid, gaseous) of CO 2 . As a result, the CO 2 is two- phase between points 1 and 2 of the cycle, which increases the irreversibilities in the heat exchanger 12 internal heat.

De plus, pour une température de source chaude TC la plus faible possible, généralement comprise entre 10°C et 50°C, le cycle de Meunier décrit ci-dessus n'est pas adapté, le cycle présentant dans certaines sections, en particulier dans l'échangeur 12, deux phases du fluide (liquide et vapeur). L'état monophasique du fluide n'est donc pas possible dans tout l'échangeur 12, notamment si la température de source chaude TC est inférieure à 56°C. Au-dessus de 56°C, le fluide est bien uniquement monophasique dans l'échangeur 12, mais au prix d'une surconsommation d'énergie et d'un rendement dégradé du cycle, les rejets étant à des températures non acceptables, c'est-à-dire trop élevées, typiquement de l'ordre de 56°C pour le CO2.Moreover, for a lowest possible hot source temperature T C , generally between 10 ° C. and 50 ° C., the Meunier cycle described above is not suitable, the cycle presenting in certain sections, in particular in the exchanger 12, two phases of the fluid (liquid and vapor). The monophasic state of the fluid is therefore not possible throughout the exchanger 12, especially if the hot source temperature T C is less than 56 ° C. Above 56 ° C, the fluid is only monophasic in the heat exchanger 12, but at the cost of overconsumption of energy and a degraded performance of the cycle, the discharges being at non-acceptable temperatures, that is to say, too high, typically of the order of 56 ° C for CO 2 .

Le document US-A-2005/0044865 décrit un dispositif à compression de vapeur pour un cycle transcritique de fluide, comportant un récipient à pression intermédiaire, dans lequel la masse de fluide actif peut être régulée en température pour contrôler l'efficacité et la capacité du dispositif.The document US-2005/0044865 discloses a vapor compression device for a fluid transcritical cycle, comprising an intermediate pressure vessel, wherein the mass of active fluid can be temperature controlled to control the efficiency and capacity of the device.

Objet de l'inventionObject of the invention

L'invention a pour but de remédier à l'ensemble des inconvénients précités et a pour objet la réalisation d'un dispositif à compression de vapeur, pour un cycle transcritique de fluide, permettant de réduire les irréversibilités dans l'échangeur de chaleur interne, afin d'obtenir un meilleur rendement du cycle, en s'assurant que le fluide frigorigène, en particulier du dioxyde de carbone, reste monophasique dans tout l'échangeur de chaleur interne.The object of the invention is to remedy all of the aforementioned drawbacks and is intended to provide a vapor compression device for a transcritical fluid cycle, to reduce the irreversibilities in the internal heat exchanger, in order to obtain a better cycle efficiency, by ensuring that the refrigerant, in particular carbon dioxide, remains monophasic throughout the cycle; internal heat exchanger.

L'invention a également pour objet un procédé de réalisation d'un cycle transcritique de fluide, plus particulièrement du dioxyde carbone, au moyen d'un tel dispositif à compression de vapeur, qui soit facile à mettre en oeuvre et qui offre un rendement optimal du cycle.The invention also relates to a method for producing a transcritical fluid cycle, more particularly carbon dioxide, by means of such a vapor compression device, which is easy to implement and which offers optimum performance. of the cycle.

Selon l'invention, ce but et ces objets sont réalisés par les revendications annexées.According to the invention, this object and these objects are realized by the appended claims.

Description sommaire des dessinsBrief description of the drawings

D'autres avantages et caractéristiques ressortiront plus clairement de la description qui va suivre de modes particuliers de réalisation de l'invention donnés à titre d'exemples non limitatifs et représentés aux dessins annexés, dans lesquels :

  • La figure 1 représente un diagramme enthalpique selon l'art antérieur, illustrant un cycle transcritique de fluide selon Evans-Perkins.
  • La figure 2 représente un diagramme enthalpique selon l'art antérieur, illustrant un cycle transcritique de fluide selon Lorentzen.
  • La figure 3 représente schématiquement un dispositif à compression de vapeur selon l'art antérieur, pour la réalisation d'un cycle transcritique de fluide selon Meunier.
  • La figure 4 représente un diagramme enthalpique selon l'art antérieur, illustrant un cycle transcritique de fluide selon Meunier, réalisé au moyen d'un dispositif à compression de vapeur selon la figure 3.
  • La figure 5 représente schématiquement un dispositif à compression de vapeur selon l'invention, pour la réalisation d'un cycle transcritique de fluide selon l'invention.
  • La figure 6 représente un diagramme enthalpique illustrant un cycle transcritique de fluide selon l'invention, réalisé au moyen d'un dispositif à compression de vapeur selon la figure 5.
  • La figure 7 représente un diagramme du coefficient de performance en fonction de la pression haute, pour le cycle transcritique de fluide selon les figures 5 et 6.
Other advantages and features will emerge more clearly from the following description of particular embodiments of the invention given by way of non-limiting example and represented in the accompanying drawings, in which:
  • The figure 1 represents an enthalpy diagram according to the prior art, illustrating a Evans-Perkins fluid transcritical cycle.
  • The figure 2 represents an enthalpy diagram according to the prior art, illustrating a transcritical fluid cycle according to Lorentzen.
  • The figure 3 schematically represents a vapor compression device according to the prior art, for carrying out a transcritical fluid cycle according to Meunier.
  • The figure 4 represents an enthalpy diagram according to the prior art, illustrating a Meunier fluid transcritical cycle, carried out by means of a vapor compression device according to the figure 3 .
  • The figure 5 schematically represents a vapor compression device according to the invention, for carrying out a transcritical fluid cycle according to the invention.
  • The figure 6 represents an enthalpy diagram illustrating a transcritical fluid cycle according to the invention, realized by means of a vapor compression device according to the figure 5 .
  • The figure 7 represents a diagram of the coefficient of performance as a function of the high pressure, for the transcritical fluid cycle according to the Figures 5 and 6 .

Description de modes particuliers de réalisationDescription of particular embodiments

En référence aux figures 5 à 7, le dispositif à compression de vapeur 11 selon l'invention (figure 5) concerne un nouveau cycle thermodynamique de réfrigération, c'est-à-dire un cycle à compression de vapeur. Il est en particulier adapté à l'usage du dioxyde de carbone CO2 comme réfrigérant. L'intérêt porté sur le CO2 provient de son faible impact environnemental au regard des réfrigérants synthétiques fluorés couramment utilisés, les fréons, qui pour certains détruisent la couche d'ozone et qui pour d'autres sont des gaz à effet de serre (généralement plus de mille fois plus puissant que le CO2). En outre, le CO2 n'est ni toxique, ni inflammable.With reference to Figures 5 to 7 , the vapor compression device 11 according to the invention ( figure 5 ) relates to a new thermodynamic refrigeration cycle, that is to say a vapor compression cycle. It is particularly suitable for the use of carbon dioxide CO 2 as a refrigerant. The interest in CO 2 comes from its low environmental impact with regard to the commonly used fluorinated synthetic refrigerants, the Freons, some of which destroy the ozone layer and which for others are greenhouse gases (generally more than a thousand times more powerful than CO 2 ). In addition, CO 2 is neither toxic nor flammable.

Sur la figure 5, un mode particulier de réalisation du dispositif à compression de vapeur 11 est représenté sous forme schématique. Le dispositif 11 se distingue du dispositif selon le cycle de Meunier (figure 3) par l'ajout d'un compresseur 18, fonctionnant à haute pression, sur le circuit principal 1-y du cycle. Le nouvel étage de compression défini par le compresseur haute pression 18 nécessite alors l'ajout d'un deuxième refroidisseur de gaz 19 isobare associé, placé sur le circuit principal du fluide 1-y, après le distributeur de fluide (point 4 sur la figure 5), entre la sortie du compresseur haute pression 18 et l'entrée de l'échangeur 12 de chaleur interne.On the figure 5 a particular embodiment of the vapor compression device 11 is shown schematically. The device 11 differs from the device according to the Meunier cycle ( figure 3 ) by adding a compressor 18, operating at high pressure, on the main circuit 1-y of the cycle. The new compression stage defined by the high-pressure compressor 18 then requires the addition of a second associated isobaric gas cooler 19, placed on the main circuit of the fluid 1-y, after the fluid distributor (point 4 on the figure 5 ), between the output of the high-pressure compressor 18 and the inlet of the internal heat exchanger 12.

Le dispositif à compression de vapeur 11 comporte les mêmes éléments que le dispositif selon le cycle de Meunier avec un échangeur 12 de chaleur interne, un compresseur basse pression 13, un refroidisseur de gaz 14 isobare associé, un système de détente 15 auxiliaire, sur le circuit y de refroidissement auxiliaire du cycle, un système de détente 16 principal, sur le circuit principal 1-y du cycle, et un évaporateur 17 fonctionnant à basse pression. Le fonctionnement du dispositif est le même avec un distributeur de fluide, plus particulièrement du CO2, placé au point 4 du cycle (figure 5), permettant de séparer le fluide afin qu'une fraction massique y du fluide suive le cycle de refroidissement auxiliaire et permette notamment de refroidir le fluide du circuit principal 1-y à l'entrée de l'échangeur 12 de chaleur interne.The vapor compression device 11 comprises the same elements as the device according to the Meunier cycle with an internal heat exchanger 12, a low-pressure compressor 13, an associated isobaric gas cooler 14, an auxiliary expansion system 15 on the auxiliary cycle cooling circuit y, a main expansion system 16, on the main circuit 1-y of the cycle, and an evaporator 17 operating at low pressure. The operation of the device is the same with a fluid dispenser, more particularly CO 2 , placed at point 4 of the cycle ( figure 5 ), for separating the fluid so that a mass fraction y of the fluid follows the auxiliary cooling cycle and in particular allows to cool the fluid of the main circuit 1-y at the inlet of the heat exchanger 12 internal heat.

Sur la figure 5, les systèmes de détente 15 auxiliaire et 16 principal peuvent être des systèmes simples, du type valve, capillaire, etc. Dans des variantes de réalisation non représentées, les systèmes de détente 15 auxiliaire et 16 principal peuvent être associés chacun, ou peuvent même être substitués chacun, à un système, respectivement auxiliaire et principal, de récupération de travail, plus particulièrement du travail de détente. À titre d'exemple, les systèmes auxiliaire et principal de récupération de travail peuvent être des machines à déplacement positif, du type piston, ou bien des machines à déplacement non positif, du type turbine. Les systèmes auxiliaire et principal de récupération de travail sont indépendants et il est possible de récupérer du travail sur l'un et/ou sur l'autre des systèmes.On the figure 5 the auxiliary and main expansion systems can be simple systems, such as valve, capillary, etc. In alternative embodiments not shown, the auxiliary and main expansion systems 15 may each be associated, or may even be each substituted, a system, respectively auxiliary and main, working recovery, more particularly the work of relaxation. For example, the auxiliary and main work recovery systems may be positive displacement machines, piston type, or non-positive displacement machines, turbine type. The auxiliary and main work recovery systems are independent and it is possible to recover work on one and / or the other of the systems.

Par ailleurs, de tels systèmes auxiliaire et principal de récupération de travail peuvent être avantageusement couplés mécaniquement et/ou électriquement à l'un et/ou à l'autre des compresseurs basse pression 13 et haute pression 18 (figure 5), afin notamment d'alléger la consommation énergétique du dispositif à compression de vapeur 11.Moreover, such auxiliary and main work recovery systems can advantageously be mechanically and / or electrically coupled to one and / or the other of the low-pressure 13 and high-pressure compressors 18 ( figure 5 ), in particular to reduce the energy consumption of the steam compression device 11.

Sur les figures 5 et 6, le compresseur haute pression 18 a notamment pour but d'augmenter la pression du CO2, qui circule dans l'échangeur 12, de façon à ce qu'il soit supercritique, c'est-à-dire qu'il ait une température supérieure à la température critique Tcrit de l'ordre de 31,1 °C (figure 6).On the Figures 5 and 6 , the high pressure compressor 18 is intended in particular to increase the CO 2 pressure, which circulates in the exchanger 12, so that it is supercritical, that is to say, it has a temperature above the critical temperature T crit of the order of 31.1 ° C ( figure 6 ).

Contrairement au cycle de Meunier (figure 4), un tel dispositif permet alors d'augmenter la pression du CO2 à la sortie du compresseur haute pression 18, afin que le refroidissement isobare correspondant entre les points 6 et 7 se fasse en condition supercritique, comme décrit ci-après, c'est-à-dire que le CO2 soit monophasique, à savoir qu'il passe au-dessus de la parabole représentative du diagramme de phase du CO2, représentant la cloche de saturation délimitant les différents états (solide, liquide, gazeux) du CO2 (figure 4).Unlike the Meunier cycle ( figure 4 ), such a device then makes it possible to increase the CO 2 pressure at the outlet of the high-pressure compressor 18, so that the corresponding isobaric cooling between points 6 and 7 takes place under supercritical conditions, as described hereinafter. that is to say that the CO 2 is monophasic, namely that it passes over the representative parabola of the phase diagram of CO 2 , representing the saturation bell delimiting the different states (solid, liquid, gas) of the CO 2 ( figure 4 ).

Un procédé de réalisation d'un cycle transcritique de fluide, plus particulièrement du CO2, au moyen du dispositif à compression de vapeur 11 représenté sur la figure 5, va être décrit plus en détail au regard de la figure 6, représentant un diagramme enthalpique de la pression en fonction de l'énthalpie, entre une température de source chaude TC de 35°C et une température de source froide TF de 0°C. Le cycle comporte une étape 1-2 de chauffage entre les points 1 et 2 du cycle, par l'intermédiaire de l'échangeur 12 de chaleur interne (figure 5), jusqu'à atteindre la température de source chaude TC, suivie d'une étape 2-3 de compression, de préférence, isentropique, par l'intermédiaire du compresseur basse pression 13 (figure 5). Puis, une étape 3-4 de refroidissement, de préférence, isobare du CO2 est réalisée entre les points 3 et 4 du cycle, par l'intermédiaire du refroidisseur de gaz 14 isobare (figure 5), jusqu'à atteindre de nouveau la température de source chaude TC au point 4 du cycleA method of performing a transcritical fluid cycle, more particularly CO 2 , by means of the vapor compression device 11 shown in FIG. figure 5 , will be described in more detail with regard to figure 6 , showing an enthalpy diagram of pressure versus enerhalpy, between a hot source temperature T C of 35 ° C and a cold source temperature T F of 0 ° C. The cycle comprises a heating step 1-2 between points 1 and 2 of the cycle, via the internal heat exchanger 12 ( figure 5 ), until reaching the hot source temperature T C , followed by a step 2-3 compression, preferably isentropic, through the low pressure compressor 13 ( figure 5 ). Then, a step 3-4 of CO 2 isobaric cooling is preferably carried out between points 3 and 4 of the cycle, via the isobaric gas cooler 14 ( figure 5 ), until reaching the hot source temperature T C again at point 4 of the cycle

Le CO2 est alors fractionné en deux au point 4 du dispositif 11 (figure 5) par l'intermédiaire du distributeur de fluide, pour obtenir, dans un premier circuit principal, une fraction massique 1-y de CO2, et, dans un deuxième circuit de refroidissement auxiliaire; une fraction massique y de CO2, utilisée dans un « sous cycle » de réfrigération entre les points 1 à 4 du cycle. Comme précédemment pour le cycle de Meunier, la fraction massique y répond à la contrainte suivante : (1-y).(h 6 -h7 )= h 2 -h 1 . The CO 2 is then split in two at point 4 of the device 11 ( figure 5 ) via the fluid distributor, to obtain, in a first circuit main, a mass fraction 1-y of CO 2 , and in a second auxiliary cooling circuit; a mass fraction y of CO 2 , used in a "sub-cycle" of refrigeration between points 1 to 4 of the cycle. As previously for the Meunier cycle, the mass fraction satisfies the following constraint: (1- y ). ( H 6 -h 7 ) = h 2 -h 1 .

Après l'étape 3-4 de refroidissement isobare, le CO2 est alors à une pression moyenne PMP, ou pression intermédiaire, et à la température de source chaude TC. La pression moyenne PMP est choisie de sorte que la fraction massique y du CO2 après son passage dans le système de détente 15 auxiliaire, lequel est connecté à l'entrée basse pression de l'échangeur 12 de chaleur interne du cycle (figure 5), à savoir après l'étape 4-1 de détente de la fraction massique y de CO2, puisse être mélangée à la fraction massique restante 1-y du CO2 sortant de l'évaporateur 17, pour atteindre un état de vapeur surchauffée (figure 5), le plus proche possible de l'état de vapeur saturée. Le point 1 du cycle représenté sur la figure 6 se trouve alors avantageusement sur la parabole représentative du diagramme de phase du CO2, représentant la courbe de saturation délimitant les différents états (solide, liquide, gazeux) du CO2.After the isobaric cooling step 3-4, the CO 2 is then at a mean pressure P MP , or intermediate pressure, and at the hot source temperature T C. The average pressure P MP is chosen so that the mass fraction y of the CO 2 after passing through the auxiliary expansion system, which is connected to the low pressure inlet of the internal heat exchanger 12 of the cycle ( figure 5 ), ie after step 4-1 of expansion of the mass fraction y of CO 2 , can be mixed with the remaining mass fraction 1-y of CO 2 leaving the evaporator 17, to reach a superheated vapor state ( figure 5 ), as close as possible to the state of saturated vapor. Point 1 of the cycle represented on the figure 6 is then advantageously on the parabola representative of the phase diagram of CO 2 , representing the saturation curve delimiting the various states (solid, liquid, gas) CO 2 .

L'étape 4-1 de détente décrite ci-dessus, sur le circuit y de refroidissement auxiliaire, peut être isenthalpique ou isentropique. Par ailleurs, le cycle fonctionnant en continu, les étapes ci-dessous relatives au circuit principal 1-y du cycle sont réalisées simultanément avec l'étape 4-1 de détente, réalisée sur le circuit y de refroidissement auxiliaire.The relaxation step 4-1 described above, on the auxiliary cooling circuit y, may be isenthalpic or isentropic. Furthermore, the cycle operating continuously, the steps below relating to the main circuit 1-y of the cycle are performed simultaneously with the step 4-1 of relaxation, performed on the circuit y auxiliary cooling.

Dans le circuit principal, la fraction massique 1-y de CO2 passe alors dans le compresseur haute pression 18, afin de subir une étape 4-5 de compression, de préférence, isentropique, entre les points 4 et 5 du cycle (figures 5 et 6). Le compresseur haute pression 18 permet notamment de rejeter le CO2 à une pression haute maximale PHP supercritique, supérieure à la pression critique Pcrit du CO2, à laquelle le CO2 a une température très élevée, typiquement supérieure à 60°C (point 5 du cycle). Le CO2 est alors dans un état supercritique, c'est-à-dire qu'il passe au-dessus de la parabole représentative du diagramme de phase du CO2, associée à la température critique Tcrit, représentant la cloche de saturation du CO2 délimitant les différents états (solide, liquide, gazeux) du CO2.In the main circuit, the mass fraction 1-y of CO 2 then passes into the high-pressure compressor 18, in order to undergo a step 4-5 compression, preferably isentropic, between points 4 and 5 of the cycle ( Figures 5 and 6 ). The high-pressure compressor 18 makes it possible in particular to reject the CO 2 at a maximum high pressure P HP supercritical, higher than the pressure Critical P crit of CO 2 , at which the CO 2 has a very high temperature, typically higher than 60 ° C (point 5 of the cycle). The CO 2 is then in a supercritical state, that is to say that it passes over the representative parabola of the CO 2 phase diagram, associated with the critical temperature T crit , representing the saturation bell of the CO 2 delimiting the various states (solid, liquid, gaseous) of CO 2 .

Puis, entre les points 5 et 6 du cycle, le CO2 est soumis à une étape 5-6 de refroidissement, de préférence, isobare par l'intermédiaire du refroidisseur de gaz 19 associé, connecté à la sortie du compresseur haute pression 18, jusqu'à atteindre de nouveau sensiblement la température de source chaude TC, au point 6 du cycleThen, between points 5 and 6 of the cycle, the CO 2 is subjected to a step 5-6 of cooling, preferably isobaric through the associated gas cooler 19, connected to the output of the high pressure compressor 18, until it again substantially reaches the hot source temperature T C at point 6 of the cycle

Puis, entre les points 6 et 7 du cycle (figures 5 et 6), le CO2 repasse dans l'échangeur 12 de chaleur interne, sur le circuit principal 1-y du cycle, qui réalise alors une étape 6-7 de refroidissement, de préférence, isobare de la fraction massique 1-y de CO2 à haute pression, sortant du compresseur haute pression 18 et du refroidisseur de gaz 19 associé. Une telle étape permet de faire descendre la température du CO2 en dessous de la température de source chaude TC, jusqu'à atteindre sensiblement la température de source froide TF, soit 0°C.Then, between points 6 and 7 of the cycle ( Figures 5 and 6 ), the CO 2 passes back into the internal heat exchanger 12, on the main circuit 1-y of the cycle, which then performs a step 6-7 cooling, preferably isobaric of the mass fraction 1-y of CO 2 at high pressure, leaving the high pressure compressor 18 and the associated gas cooler 19. Such a step makes it possible to lower the temperature of the CO 2 below the hot source temperature T C until it reaches substantially the cold source temperature T F , ie 0 ° C.

Une étape 7-8 de détente isenthalpique ou isentropique est ensuite réalisée, sur le circuit principal 1-y du cycle, par l'intermédiaire du système de détente 16 principal, afin de faire passer le CO2 de la valeur de pression haute PHP à une valeur de pression basse PBP.A step 7-8 of isenthalpic or isentropic expansion is then performed, on the main circuit 1-y of the cycle, through the main expansion system 16, in order to pass CO 2 from the high pressure value HP at a low pressure value P BP .

Enfin, le fluide passe dans l'évaporateur 17, fonctionnant à basse pression, afin de terminer le cycle par une étape 8-1 d'évaporation isobare, jusqu'à atteindre le point 1, point de départ du cycle, à la température de source froide TF.Finally, the fluid passes into the evaporator 17, operating at low pressure, in order to complete the cycle by an isobaric evaporation step 8-1, until reaching point 1, starting point of the cycle, at the temperature of cold source T F.

Ainsi, c'est le mélange du CO2 à basse pression en sortie de l'évaporateur 17 du circuit principal 1-y et du CO2 à basse pression en sortie du système de détente 15 auxiliaire du circuit de refroidissement auxiliaire y, qui est chauffé au départ du cycle dans l'échangeur 12 de chaleur interne, avant d'être entraîné dans le compresseur basse pression 13.Thus, it is the mixture of CO 2 at low pressure leaving the evaporator 17 of the main circuit 1-y and CO 2 at low pressure at the outlet of the auxiliary expansion system 15 of the auxiliary cooling circuit y, which is heated at the start of the cycle in the internal heat exchanger 12, before being driven into the low pressure compressor 13.

À titre d'exemple, pour une température de source froide TF de l'ordre de 0°C, pour une température de source chaude TC de 35°C et pour une pression critique Pcrit de l'ordre de 7,5MPa, la pression moyenne PMP est de l'ordre de 5,5MPa et la pression haute PHP est de l'ordre de 8,4MPa (figures 6 et 7).By way of example, for a cold source temperature T F of the order of 0 ° C., for a hot source temperature T C of 35 ° C. and for a critical pressure P crit of the order of 7.5 MPa the average pressure P MP is of the order of 5,5MPa and high pressure HP P is of the order of 8,4MPa ( figures 6 and 7 ).

Un tel procédé de réalisation d'un cycle transcritique de CO2 au moyen d'un tel dispositif à compression de vapeur 11 (figure 5) permet donc de faire fonctionner le cycle principal de réfrigération à une pression haute PHP supérieure à la pression critique Pcrit, alors que le circuit de refroidissement auxiliaire fonctionne à une pression moyenne PMP, inférieure à la pression haute PHP.Such a method of carrying out a transcritical CO 2 cycle by means of such a vapor compression device 11 ( figure 5 ) makes it possible to operate the main refrigeration cycle at a high pressure P HP higher than the critical pressure P crit , while the auxiliary cooling circuit operates at an average pressure P MP , lower than the high pressure P HP .

Par ailleurs, un tel dispositif à compression de vapeur 11, avec un système de compression étagée formé par le compresseur basse pression 13 et le compresseur haute pression 18, est très simple à mettre en oeuvre avec simplement l'ajout de deux éléments sur le circuit principal 1-y du cycle (compresseur et refroidisseur de gaz fonctionnant à haute pression). Un tel dispositif à compression de vapeur 11 permet donc d'obtenir un cycle transcritique de fluide, plus particulièrement de CO2, avec une meilleure efficacité de l'échangeur 12 de chaleur interne, notamment grâce à l'utilisation d'un fluide monophasique, ce qui permet un écart minimum de température entre le côté à basse pression et le côté à haute pression du dispositif à compression de vapeur 11 selon l'invention.Moreover, such a vapor compression device 11, with a staged compression system formed by the low-pressure compressor 13 and the high-pressure compressor 18, is very simple to implement simply by adding two elements to the circuit main 1-y cycle (compressor and gas cooler operating at high pressure). Such a vapor compression device 11 thus makes it possible to obtain a transcritical fluid cycle, more particularly of CO 2 , with a better efficiency of the internal heat exchanger 12, in particular thanks to the use of a monophasic fluid, which allows a minimum temperature difference between the low pressure side and the high pressure side of the vapor compression device 11 according to the invention.

En effet, la figure 7 représente un graphique illustrant la variation du coefficient de performance COP en fonction de la valeur de pression haute PHP, pour différents cycles transcritiques, à savoir selon Evans-Perkins (courbe en trait plein simple), selon Lorentzen (courbe avec des triangles), selon Meunier (courbe avec des carrés) et selon l'invention (courbe avec des ronds). Il ressort de la figure 7 qu'il est possible d'optimiser la performance du cycle transcritique en fonction de la pression haute PHP, pour les valeurs de température de source chaude TC de 35°C et de source froide TF de 0°C.Indeed, the figure 7 represents a graph illustrating the variation of the coefficient of performance COP as a function of the high pressure value P HP , for different transcritical cycles, namely according to Evans-Perkins (curve in solid single line), according to Lorentzen (curve with triangles), according to Meunier (curve with squares) and according to the invention (curve with circles). It appears from figure 7 that it is possible to optimize the performance of the transcritical cycle as a function of the high pressure P HP , for the hot source temperature values T C of 35 ° C and cold source T F of 0 ° C.

En regardant la courbe correspondant au cycle selon l'invention (courbe avec les ronds), le COP passe par un maximum (rond noir) à une pression PHP de l'ordre de 8.4MPa, offrant ainsi une amélioration relative notamment par rapport au cycle de base d'Evans-Perkins (courbe en trait plein simple) de l'ordre de 34.4% et par rapport au cycle de Lorentzen (courbe avec des triangles) de l'ordre de 3,9%.By looking at the curve corresponding to the cycle according to the invention (curve with circles), the COP goes through a maximum (black circle) at a pressure P HP of the order of 8.4 MPa, thus offering a relative improvement especially with respect to Evans-Perkins basic cycle (single solid curve) of the order of 34.4% and compared to the Lorentzen cycle (curve with triangles) of the order of 3.9%.

L'invention n'est pas limitée aux différents modes de réalisation décrits ci-dessus. D'une façon générale, il existe plusieurs chemins possibles, pour passer d'un point à un autre du cycle transcritique selon l'invention, le fluide pouvant suivre les courbes isobares, les courbes isothermes, les courbes isenthalpiques ou les courbes isentropiques, sur le diagramme enthalpique comme représenté sur la figure 6. De façon générale, le procédé peut notamment comporter une simple étape 2-4 de compression du fluide, pour atteindre le pression moyenne PMP et pour atteindre la température de source chaude TC, et une simple étape 4-6 de compression du fluide, pour atteindre la pression haute maximale PHP, supérieure à la pression critique Pcrit du fluide, et pour atteindre la température de source chaude TC.The invention is not limited to the various embodiments described above. In general, there are several possible paths for passing from one point to another of the transcritical cycle according to the invention, the fluid being able to follow the isobaric curves, the isothermal curves, the isenthalpic curves or the isentropic curves, on the enthalpy diagram as represented on the figure 6 . In general, the method may include in particular a simple step 2-4 of fluid compression, to reach the average pressure P MP and to reach the hot source temperature T C , and a simple step 4-6 of fluid compression, to reach the maximum high pressure P HP , higher than the critical pressure P crit of the fluid, and to reach the hot source temperature T C.

Les compresseurs basse pression 13 et haute pression 18 et les refroidisseurs de gaz basse pression 14 et haute pression 19 peuvent être tout système de compression de vapeur et tout système de refroidissement de gaz pouvant fonctionner à haute pression et/ou à basse pression, en fonction de leurs places dans le circuit associé au dispositif à compression de vapeur 11.The low pressure compressors 13 and high pressure 18 and the low pressure gas coolers 14 and high pressure 19 can be any vapor compression system and any gas cooling system capable of operating at high pressure and / or low pressure, depending on their position in the circuit associated with the vapor compression device 11.

Le dispositif à compression de vapeur 11 selon l'invention peut notamment comporter tout type de système à compression de vapeur, tout type de système de refroidissement isobare, tout type de système de refroidissement simultané à une compression, tout type de distributeur de fluide, tout système de détente auxiliaire, pour le circuit de refroidissement auxiliaire, et tout système de détente principal, pour le circuit principal, tant que le dispositif à compression de vapeur permet notamment d'avoir un fluide monophasé des deux côtés de l'échangeur 12 de chaleur interne, afin de réduire les irréversibilités dans l'échangeur 12 de chaleur interne, tout en maintenant la température du fluide à haute pression en sortie de l'échangeur 12 la plus proche possible de la température de source froide TF.The vapor compression device 11 according to the invention may include any type of vapor compression system, any type of isobaric cooling system, any type of simultaneous compression cooling system, any type of fluid dispenser, any auxiliary expansion system, for the auxiliary cooling circuit, and any main expansion system, for the main circuit, as long as the vapor compression device makes it possible in particular to have a single-phase fluid on both sides of the heat exchanger 12 internal, in order to reduce the irreversibilities in the internal heat exchanger 12, while maintaining the temperature of the high pressure fluid at the outlet of the exchanger 12 as close as possible to the cold source temperature T F.

Claims (15)

  1. A vapour compression device (11) for a transcritical fluid cycle, comprising at least:
    - an internal heat exchanger (12),
    - a first vapour compression system (13) connected to the outlet of the internal heat exchanger (12),
    - a first isobaric cooling system (14) connected to the outlet of the first vapour compression system (13),
    - a fluid distributor placed at the outlet of first isobaric cooling system (14) and separating the fluid into a main circuit (1-y) of the cycle and an auxiliary cooling circuit (y) of the cycle,
    - an auxiliary expansion system (15) placed on the auxiliary cooling circuit (y) between the fluid distributor and the inlet of the internal heat exchanger (12),
    - a main expansion system (16) placed on the main circuit (1-y) and connected to the outlet of the internal heat exchanger (12),
    - an evaporator (17) operating at low pressure placed between the outlet of the main expansion system (16) and the inlet of the internal heat exchanger (12),
    characterized in that it comprises a second vapour compression system (18) and a second isobaric cooling system (19) connected to the outlet of the second vapour compression system (18), the second vapour compression system (18) and the second isobaric cooling system (19) being placed on the main circuit (1-y) of the cycle after the fluid distributor and before the inlet of the internal heat exchanger (12).
  2. The device according to claim 1, characterized in that the fluid is carbon dioxide (CO2).
  3. The device according to one of claims 1 and 2, characterized in that the isobaric cooling systems (14, 19) are gas coolers.
  4. The device according to any one of claims 1 to 3, characterized in that the main expansion system (16) is associated with a main work recovery system.
  5. The device according to claim 4, characterized in that it comprises mechanical and/or electrical coupling means between said main work recovery system and the first vapour compression system (13) and/or the second vapour compression system (18).
  6. The device according to any one of claims 1 to 5, characterized in that the auxiliary expansion system (15) is associated with an auxiliary work recovery system.
  7. The device according to claim 6, characterized in that it comprises mechanical and/or electrical coupling means between said auxiliary work recovery system and the first vapour compression system (13) and/or the second vapour compression system (18).
  8. The device according to any one of claims 1 to 7, characterized in that the internal heat exchanger (12) is connected to the outlet of the second isobaric cooling system (19) and to the inlet of the main expansion system (16) on the main circuit (1-y) of the cycle.
  9. The device according to any one of claims 1 to 8, characterized in that the pressure in the main circuit (1-y) of the cycle is a maximum high pressure (PHP) greater than the critical pressure (Pcrit) of the fluid.
  10. The device according to claim 9, characterized in that the pressure in the auxiliary cooling circuit (y) of the cycle is a medium pressure (PMP) of the fluid, lower than said maximum high pressure (PHP).
  11. A method for performing a transcritical fluid cycle between a hot source temperature (TC) and a cold source temperature (TF), by means of a vapour compression device (11) according to any one of claims 1 to 10, comprising at least the steps of:
    - heating (1-2) the fluid in the internal heat exchanger (12) until the hot source temperature (TC) is reached,
    - compression (2-4) of the fluid to reach a medium pressure (PMP) and to reach the hot source temperature (TC),
    - separation (4) of the fluid by the fluid distributor into a main circuit (1-y) of the cycle and an auxiliary cooling circuit (y) of the cycle,
    - expansion of the fluid (4-1) on the auxiliary cooling circuit (y), by means of the auxiliary expansion system (15), until the cold source temperature (TF) is reached,
    - expansion of the fluid (7-8) on the main circuit (1-y), by means of the main expansion system (16), until the cold source temperature (TF) is reached,
    - isobaric evaporation (8-1) of the fluid on the main circuit (1-y),
    a method characterized in that it comprises a compression step (4-6) of the fluid on the main circuit (1-y) of the cycle, after the fluid separation step (4) and before the associated expansion step (7-8), to reach a maximum high pressure (PHP), greater than a critical pressure (Pcrit) of the fluid, and to substantially reach the hot source temperature (TC), and a cooling step (6-7) of the fluid to substantially reach the cold source temperature (TF).
  12. The method according to claim 11, characterized in that said compression step (2-4) of the fluid to reach a medium pressure (PMP) and to reach the hot source temperature (TC) comprises the steps of:
    - isentropic compression (2-3) of the fluid by the first vapour compression system (13) to reach said medium pressure (PMP),
    - isobaric cooling (3-4) of the fluid by the first isobaric cooling system (14) to reach the hot source temperature (TC).
  13. The method according to one of claims 11 and 12, characterized in that said expansion step (4-1) of the fluid on the auxiliary cooling circuit (y) of the cycle is isenthalpic or isentropic.
  14. The method according to any one of claims 11 to 13, characterized in that said expansion step (7-8) of the fluid on the main circuit (1-y) of the cycle is isenthalpic or isentropic.
  15. The method according to any one of claims 11 to 14, characterized in that said compression step (4-6) of the fluid, to reach a maximum high pressure (PHP) greater than a critical pressure (Pcrit) of the fluid, and to substantially reach the hot source temperature (TC), comprises an isentropic compression step (4-5) of the fluid followed by an isobaric cooling step (5-6) of the fluid.
EP07354062.7A 2006-12-01 2007-11-16 Vapour compression device and method for performing an associated transcritical cycle Not-in-force EP1927816B1 (en)

Applications Claiming Priority (1)

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FR0610507A FR2909439B1 (en) 2006-12-01 2006-12-01 VAPOR COMPRESSION DEVICE AND METHOD OF REALIZING A TRANSCRITICAL CYCLE THEREFOR

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JP2008139014A (en) 2008-06-19
FR2909439B1 (en) 2009-02-13
US7818978B2 (en) 2010-10-26
US20080127672A1 (en) 2008-06-05
JP5231002B2 (en) 2013-07-10
FR2909439A1 (en) 2008-06-06

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