EP0057120B1 - Verfahren zum Heizen eines Raumes mittels einer Kompressionswärmepumpe mit einem Gemisch als Arbeitsmedium - Google Patents

Verfahren zum Heizen eines Raumes mittels einer Kompressionswärmepumpe mit einem Gemisch als Arbeitsmedium Download PDF

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Publication number
EP0057120B1
EP0057120B1 EP82400042A EP82400042A EP0057120B1 EP 0057120 B1 EP0057120 B1 EP 0057120B1 EP 82400042 A EP82400042 A EP 82400042A EP 82400042 A EP82400042 A EP 82400042A EP 0057120 B1 EP0057120 B1 EP 0057120B1
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Prior art keywords
fluid
mixed
fraction
working fluid
vaporized
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EP82400042A
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French (fr)
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EP0057120A2 (de
EP0057120A3 (en
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Alexandre Rojey
Claude Ramet
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component

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  • the present invention relates to a method of heating a room by means of a compression heat pump, operating with a mixed working fluid.
  • the objective is to produce cold at 2 different temperature levels and the desired temperature difference is obtained by inserting a heat exchanger between the evaporators corresponding to each temperature level; heat exchange is carried out between the mixture of fluids being vaporized and the condensate from the compressor, before sending this condensate to the first evaporator.
  • the exchange thus carried out has the effect, not only of operating the 2 evaporators at different temperatures, but also of increasing the temperature difference between the inlet of the first evaporator and the outlet of the final evaporator, therefore increase the ⁇ T of heat removal from the external environment, which is exactly the opposite of the result obtained according to the invention.
  • a working fluid formed by at least two constituents of different boiling points in a thermal compression machine is also described in FR-A-2 337 855.
  • the objective is to recover calories on an external fluid over a relatively wide temperature range (for example between 0 and 100 ° C), and supply these calories to the condenser in a relatively close range (for example between 40 and 130 ° C) or narrower (for example between 70 and 85 ° C).
  • the heat exchange between the external fluid and the working fluid is carried out in an exchange zone comprising a single evaporator, so that the working fluid is completely vaporized.
  • the working fluid is previously introduced into the evaporator at the same temperature as the outside fluid and is thus sub-cooled before being expanded to recover the calories from the outside fluid.
  • the calories recovered are transferred to a second external fluid in a condensation zone in which the compressed working fluid at least partially condenses. Part of the liquid is then recycled to the evaporator.
  • This system comprising at the evaporator a simultaneous exchange of calories between the working fluid being vaporized and the two heat sources (external fluid and condensate) provides good results when the temperature range at the evaporator is relatively large. (for example 50 ° C).
  • the heat supplied to the evaporator is available in a relatively narrow temperature range, for example less than 10 ° C or even in some cases less than 5 ° C, while that heat must be supplied to the condenser in a relatively wide temperature range, for example greater than 10 ° C or even in some cases greater than 15 ° C.
  • the use of a mixed working fluid which condenses according to a temperature profile parallel to the temperature profile of the external fluid to which the heat pump supplies heat and according to a temperature interval close to the interval of temperature in which said external fluid evolves does not lead to a significant improvement compared to a pure body, because the evaporator the mixture vaporizes in general according to a temperature interval close to the temperature interval according to which it condenses and which, if it is close to the interval of temperature according to which the external fluid evolves to which the heat pump supplies heat, is much higher than the temperature interval according to which the external fluid evolves location from which the heat pump draws heat.
  • the mixed fluid is ill-suited to the conditions under which it must operate on the evaporator and does not bring any significant gain compared to the pure body.
  • the object of the process according to the invention is to heat a room by means of a compression heat pump delivering heat to said room over a temperature interval wider than that of the available heat source and operating with a mixed working fluid under conditions such that the mixture of constituents forming the mixed working fluid does not form an azeotrope.
  • step (a) the mixed working fluid is compressed in the vapor phase
  • step (b) the compressed mixed fluid coming from step (a) is brought into heat exchange contact with a relatively cold external fluid, constituting the local heating agent, so as to transfer the heat of compression to said external fluid, and this contact is maintained until condensation substantially complete of said mixed fluid
  • step (c) at least one liquid fraction of the mixed fluid substantially completely condensed in step (b) is brought into heat exchange contact with a cooling fluid defined in step (f), so further cooling said fraction of the mixed fluid and heating said cooling fluid defined in step (f),
  • step (d) expanding the fraction of cooled mixed fluid from step (c), (e) putting the fraction of expanded mixed fluid, originating from stage (d), in heat exchange contact with an external fluid which constitutes a heat source, the contact conditions allowing the partial vaporization of said fraction of the expanded mixed fluid, and ( f) said fraction of the partially vaporized mixed fluid from step (e) is placed in heat exchange contact with the fraction of the substantially completely liquefied mixed fluid sent to
  • step (f) The method is characterized in that the contact conditions of step (f) are chosen so as to complete the vaporization started in step (e), in that the proportion of fraction of mixed fluid vaporized in step (f) represents at least 5 mol% of the fraction of mixed fluid vaporized in all of steps (e) and (f) and in that the fraction of fully vaporized mixed fluid, originating from step, is returned (f), directly in step (a).
  • the proportion of fraction of the mixed fluid which is vaporized in step (f) represents practically between 5 and 40% by mole, that fraction vaporized in step (e) between 60 and 95% by mole of what is vaporized in the two stages (e and f).
  • the mixture arrives in the liquid phase via line 1. It is expanded through the expansion valve V1, is sent via line 4 to the exchanger E1 and is partially vaporized in the exchanger E1 by taking heat from an external fluid which arrives via line 2 and leaves via line 3.
  • the liquid-vapor mixture, leaving the exchanger E1 is sent by line 5 into the exchanger E2 from which it emerges fully vaporized and possibly overheated by line 6
  • It is compressed in the compressor K1 and the compressed vapor phase mixture is sent via line 7 to the exchanger E3 where it condenses by yielding heat to an external fluid which arrives via line 10 and leaves via line 11.
  • the mixture is discharged from the exchanger E3 through line 8, then enters the balloon B1.
  • the liquid phase is sent to the exchanger E2 in which it cools, supplying the heat necessary for the end of vaporization and for possible overheating of the mixture arriving via the line 5 and leaving via the line 6.
  • the composition of the mixture must be selected so that the temperature range during the condensation is close to the difference between the inlet and outlet temperatures. of the external fluid which is heated in the condenser.
  • the mixture is a binary mixture constituted by a first majority constituent and a second minority constituent
  • the temperature interval during the condensation at a given pressure increases with the proportion of this second constituent and that, consequently, if the two constituents have vaporization temperatures in the pure state and under the same pressure sufficiently different, at a given temperature interval in condensation corresponds a well defined composition.
  • the regulator V1 must ensure a pressure after expansion such that the mixture comes out completely vaporized at the outlet of the exchanger E2.
  • This condition reveals one of the advantages of the method according to the invention. It makes it possible to operate with an end of vaporization temperature and a pressure higher than those which would be achieved in the case of the usual techniques involving complete vaporization at the outlet of the exchanger E1. It allows, on the other hand, to enter the regulator V1 at a temperature much lower than the temperature at the outlet of the condenser E3 and thus to reduce the vaporized fraction due to the expansion. It is thus possible to bring the temperature at the start of vaporization of the mixture closer to the bubble temperature and thus further improve the conditions of the heat exchange in the exchanger E1. Increasing the pressure at the inlet of the compressor has a double advantage: it improves the coefficient of performance by reducing the compression ratio and increases the thermal capacity of the heat pump by reducing the molar volume to aspiration.
  • This second advantage is particularly important when seeking to reduce the investment corresponding to a given installation.
  • it is essential that the mixed working fluid at the outlet of the condenser E3 is fully condensed.
  • the condensation is carried out in part in the exchanger E2
  • the result is for a given thermal power an increase in the volume flow rate at suction and therefore the size of the compressor required.
  • this generally leads to placing the reserve tank B1 at the outlet of the condenser E3 and then collecting the mixed working fluid in the liquid phase via the conduit 9 and sub-cooling it in the exchanger E2.
  • the method according to the invention is therefore particularly suitable for a heat pump using air as the heat source, whether it is an air-air heat pump or an air-water heat pump.
  • FIG. 2 shows an operating diagram according to the invention of an air-air heat pump, intended for space heating, which is illustrated by example 2.
  • the box D1 unlike the box D2, is located outside the room to be heated, (split system), but it is clear that the method of the invention can be implemented in a one-piece installation.
  • the expanded mixture is partially vaporized in the evaporator E4.
  • the evaporator E4 In the evaporator E4, it generally flows against the current of the outside air (F l , F 2 ). This outside air is sucked in at the base of the enclosure D1 by the helical fan VE1 driven by the electric motor M1 and it is discharged outside through the protective grid GP1.
  • the evaporator E4 can be constituted, for example, by a tube provided with fins or needles, such as to improve the exchange and wound in a spiral.
  • the liquid-vapor mixture leaving the evaporator E4 through the line 22 finishes vaporizing in the exchanger E5 in contact with the mixture arriving through the line 21 and leaves the exchanger E5 through the line 20 in the superheated state.
  • the E6 exchanger is made up of several separate batteries which are traversed in series by the mixture which generally flows from top to bottom against the flow of air. This is sucked in through the intake duct G2 and leaves the enclosure D2 through the discharge duct G3 and thus flows from bottom to top. The condensed mixed fluid leaves through the conduit 25 and it is collected in the balloon B2.
  • the liquid mixed fluid leaves through the conduit 21 and it is sub-cooled in the exchanger E5 by heating the mixed fluid which vaporizes. It leaves via the conduit 24 via which it arrives at the regulator V2, from where it is sent via the conduit 26 to the evaporator E4.
  • such an installation can take heat from outside air, but also from extracted air or a combination of outside air and extracted air.
  • the points of introduction of the extracted air and the outside air may be different.
  • the method according to the invention can also be implemented in a heat pump using air as a heat source and heating water.
  • the condenser of the heat pump can be constituted for example by a double tube exchanger operating against the current.
  • the mixed working fluid is partially vaporized at a first pressure level P 1 in the exchanger E lo , into which it enters through the conduit 30 and exits through the conduit 31; the heat exchange in E10 is carried out with a first fraction of the external fluid constituting the cold source, arriving by the tube 43 and leaving by the tube 44.
  • the vaporization of the mixed fluid continues in the exchanger E11, in which the fluid mixed enters liquid-vapor mixture via line 31, leaves via line 32 and takes the heat of vaporization on the mixed liquid fluid, which flows against the current, enters E11 through line 41 and exits through line 42.
  • the liquid-vapor mixture is discharged through channel 32 in the flask B3, where the liquid and vapor phases separate.
  • the vapor phase is evacuated through the tube 33 and is sucked, still at the pressure P i , to an intermediate stage of the compressor K2.
  • the arrangement described therefore assumes that the compression is carried out in at least two stages.
  • the liquid phase is evacuated through line 34, sub-cooled in the exchanger E12, then is sent through line 35 through the expansion valve V4, where it is expanded to low pressure of cycle P 2 , less than P 1 .
  • the mixed fluid is sent via line 36 in the exchanger E13 and emerges therefrom in the liquid vapor state via line 37.
  • the exchanger provides partial vaporization of the mixed fluid at pressure P 2 , by taking heat from a second fraction of the external fluid extracted from the cold source, arriving through the tube 45 and leaving through the tube 46.
  • the end of the vaporization of the mixed fluid and possible overheating is carried out in the exchanger E12; the partially vaporized mixed fluid enters E12 through the tube 37, exits from it through the tube 38 and takes the heat required at the end of vaporization from the sub-cooled liquid which enters through the conduit 34 and leaves via the conduit 35.
  • the pressure levels P1 and P2 obtained using the expansion members V3 and V4 are fixed so that the temperature of the liquid vapor mixture at the inlet of the exchanger E13 is close to the temperature of the liquid vapor mixture at the inlet of the exchanger E10. It is therefore clear that the temperature interval between the start and the end of spraying is reduced. A direct consequence of this is that instead of having to compress the entire vapor mixture from the pressure level P2, it is possible to compress a fraction of this vapor mixture from the intermediate pressure level P1 greater than the pressure level P2.
  • the mixed fluid vaporized at the pressure P 2 is evacuated to the first stage of the compressor K1 by the line 38; it is mixed during compression with the mixed fluid vaporized at the pressure P 1 and sucked up through the pipe 33.
  • the final mixture is discharged from K2 through the channel 39 at the pressure P 3 , which is the high pressure of the cycle ( P 3 > P 1 > P 2 ). It is then desuperheated and condensed in the exchanger E14, by heating the external fluid which arrives against the current by the conduit 47 and leaves again by the conduit 48.
  • the mixed fluid once condensed, is collected via the tube 40 in the storage flask B4.
  • the mixed liquid fluid is discharged through the tube 41, is sub-cooled in the exchanger E11, then sent via the conduit 42 to the valve V3. There it is relaxed until the intermediate pressure of the cycle P i .
  • the mixture can be formed for example by a mixture of hydrocarbons or halogenated hydrocarbons of the “Freons” type, or alternatively of alcohols, ketones, esters, ethers, amines. It may be advantageous, in particular for installations operating at relatively high temperatures, to use a mixture of water and a water-soluble constituent, such as ammonia or even such as methanol.
  • a particularly important field of application of the method according to the invention relates to applications in space heating and in particular the heat pumps fitted to dwellings.
  • the invention also applies to installations which operate as a heat pump in winter and in air conditioning in summer and in which the transition from “winter to summer” operation is obtained for example by using a valve of inversion according to a well-known principle in air conditioning.
  • the method according to the invention corresponding to diagram 3 is suitable for applications of the industrial or collective heating type, in which the temperature variation of the heating fluid is significantly greater than the cooling of the fluid from the cold source.
  • the adjustment of the expansion device which precedes the evaporator must be carried out taking into account the composition of the mixture.
  • the regulator In heat pumps used for space heating, the regulator is generally provided with a bulb which contains the refrigerant used as working fluid.
  • the expansion pressure obtained corresponds to a pressure such that the same refrigerant at the bulb temperature is superheated from 5 to 15 ° C; this overheating being adjusted by adjusting the calibration of the regulator.
  • the same type of regulator can be used in the case of a mixture.
  • the pressure after expansion must, however, be adjusted so that the mixed working fluid is only partially vaporized during the exchange with the external fluid which serves as a heat source and comes out slightly overheated from the exchanger in which it draws heat from the mixture leaving the condenser.
  • This adjustment can be carried out both by adjusting the setting of the regulator and the position of the bulb as well as the nature of the fluid which fills the bulb which can be for example R-22 or R-12.
  • the bulb can be placed at different points and brought into temperature equilibrium with the mixed working fluid, for example at the end of step (e) or at the end of step (f) or at the end of the step (c) or at an intermediate point in any one of these steps.
  • step (f) it is possible either to increase the pressure if it is found that the overheating at the end of step (f) is excessive by moving the bulb towards a point whose temperature is higher, or to decrease pressure by moving the bulb to a point with a lower temperature.
  • step (f) it is possible to obtain an automatic adjustment of the pressure in the evaporator in response to a variation in the outside temperature.
  • the operating conditions are generally chosen so that the pressure of the mixture in the evaporator is greater than atmospheric pressure and that the pressure of the mixture in the condenser does not reach excessive values, for example greater than 30 bar. .
  • the inlet temperature of the external fluid which serves as a heat source is generally higher than 9 ° C for at least part of the operating time of the heat pump during the year.
  • the apparatus implementing the method can be carried out using different equipment for each of the components.
  • the exchanger in which the final vaporization step is carried out which is carried out by exchange with the mixture leaving the condenser, can for example be a double tube exchanger, different types of fins being able to be introduced either into the inner tube or tubes. and the annular space between the inner tube (s) and the outer tube.
  • Said exchanger may also be constituted by an exchanger with flat or spiral plates, the only condition to be observed being to carry out an exchange which is as close as possible to a pure counter-current.
  • the exchangers in contact with the external fluids can also be of any type provided that they are adapted to the nature of the external fluid with which the exchange takes place.
  • the compressor can be for example a lubricated piston compressor of the hermetic or open type, a dry piston compressor or for higher powers, a screw compressor or a centrifugal compressor.
  • FIGS 1, 2 and 3 which serve to illustrate the invention constitute only schematic diagrams and do not mention certain secondary elements which may form part of the usual installations of heat pumps, such as sight glass, drying cartridge, anti-blow bottle liquid at the compressor inlet, etc ...
  • Example 1 is illustrated in Figure 1.
  • the cold source consists of water extracted from a water table. This water, the flow rate of which is 1,500 l / h, arrives in the evaporator E1 via the pipe 2 at a temperature of 12 ° C. and leaves the evaporator E1 through the pipe 3 at a temperature of 5 ° C.
  • the heating water arrives via line 10 at a temperature of 21.3 ° C. and leaves via line 11 at a temperature of 34.5 ° C.
  • the mixture leaves the evaporator E1 at a temperature of 3.5 ° C.
  • the molar fraction vaporized at the outlet of E1 is 0.86.
  • the mixture finishes vaporizing in the exchanger E2 at a temperature of 9.3 ° C. It is observed that the introduction of the exchanger E2 in which the mixture leaving the evaporator E1 finishes vaporizing and in which the mixture leaving the reserve tank B1 is sub-cooled makes it possible both to increase the coefficient of 6.1% performance and reduce the volume flow rate at the compressor suction by 4.4%, compared to an identical installation without the E2 exchanger and operating with the same mixture.
  • Example 2 is illustrated in Figure 2.
  • the evaporator E4 receives an outside air flow of 4,864 m 3 / h arriving at a temperature of 8.3 ° C. This air comes out at a temperature of 6.3 ° C.
  • the condenser E6 allows the heating of a flow of 1,084 m 3 / h of air coming from the room to be heated, which arrives on the condenser E6 at a temperature of 21.1 ° C and leaves warmed up to a temperature of 33, 4 ° C.
  • the mixture leaves the evaporator E4 at a temperature of 0.6 ° C.
  • the molar fraction vaporized at the outlet of the evaporator E4 is 0.85.
  • the mixture finishes vaporizing in the E5 exchanger at a temperature of 5.1 ° C.
  • the introduction of the E5 exchanger makes it possible both to increase the coefficient of performance by 5.7% and to reduce the volume flow rate at the compressor suction by 7.4% compared to an identical installation without the E5 exchanger and operating with the same mixture.
  • Example 3 is illustrated in Figure 3.
  • the heat source to the evaporators E10 and E13 consists of water sent to 40 ° C and cooled to 33 ° C.
  • the water flow circulating in the evaporators E10 and E13 is identical and equal to 75 m 3 / h.
  • the heating fluid which is heated at the condenser E14 is water which enters the condenser E14 at a temperature of 45 ° C and which is reheated to a temperature of 82 ° C. Its flow is 35 m 3 / h.
  • the working fluid is an equimolar binary mixture consisting of dichlorodifluoromethane (R-12) and trichlorotrifluoroethane (R-113).
  • the compressor is a two-stage centrifugal type compressor.
  • the first stage sucks the steam mixture at a pressure of 1.31 bar and discharges it at an intermediate pressure of 2.49 bar.
  • the second stage compresses the mixture leaving the first stage and the mixture arriving via line 33 to a final pressure of 6.54 bar.
  • the sub-cooled liquid mixture leaving the exchanger E11 via the conduit 42 begins to vaporize in the evaporator E10.
  • the vaporized fraction is 0.4 in molar fraction; at the outlet of the evaporator E11, it is 0.5 in molar fraction; at the outlet of the evaporator E13, the vaporized fraction is a total of 0.8 in molar fraction (i.e. 0.3 in the evaporator E12.
  • the condensation interval in the exchanger E14 is 39 ° C. while the vaporization intervals at low pressure (vaporization operated in exchangers E13 and E12) and at intermediate pressure (vaporization operated in exchangers E10 and E11) are close 18 ° C. It is thus verified that the arrangement shown diagrammatically in FIG. 3 makes it possible to recover heat over a temperature interval much smaller than the temperature interval according to which it is supplied, by carrying out heat exchanges under good conditions of reversibility. This results in a gain on the coefficient of performance which, in the example considered, is approximately 25% compared to a cycle comprising a single evaporator and using the same mixture.

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Claims (11)

1. Verfahren zur Erwärmung eines Raums mittels einer Druck-Wärmepumpe, welche dem Raum die Wärme über einen Temperaturbereich liefert, der größer ist, als derjenige der zur Verfügung stehenden Wärmequelle, und der mit einem Flüssigkeitsgemisch unter solchen Bedingungen arbeitet, daß die Mischung der Bestandteile, welche das Flüssigkeitsgemisch bilden kein Azeotrop bildet, wobei man (a) die flüssige Arbeitsmischung in Dampfphase komprimiert, (b) die aus Stufe (a) stammende komprimierte Flüssigkeitsmischung in Wärmeaustausch-Kontakt mit einer relativ kalten Außenflüssigkeit bringt, welche das Wärmemittel des Raumes darstellt, so daß die Kompressionswärme an diese Außenflüssigkeit abgegeben wird, und man diesen Kontakt bis zur praktisch vollständigen Kondensation des Flüssigkeitsgemischs aufrecht erhält, (c) mindestens eine flüssige Fraktion des in Stufe (b) praktisch vollständig kondensierten Flüssigkeitsgemischs mit der in Stufe (f) definierten Kälteflüssigkeit in Wärmeaustausch- Kontakt bringt, so daß diese Fraktion der Flüssigkeitsmischung noch mehr abgekühlt und die in Stufe (f) definierte Kälteflüssigkeit erwärmt wird, (d) die aus Stufe (c) stammende abgekühlte Fraktion der Flüssigkeitsmischung entspannt, (e) die aus Stufe (d) stammende entspannte Fraktion der Flüssigkeitsmischung mit einer Außenflüssigkeit, welche eine Wärmequelle darstellt, in Wärmeaustauschkontakt bringt, wobei die Kontaktbedingungen eine partielle Verdampfung dieser Fraktion der entspannten Flüssigkeitsmischung erlauben, und (f) die aus Stufe (e) stammende partiell verdampfte Fraktion der Flüssigkeitsmischung mit der praktisch völlig verflüssigten Fraktion der Flüssigkeitsmischung, die in die Stufe (c) geschickt wird, in Wärmeaustauschkontakt bringt, wobei diese partiell verdampfte Fraktion der Flüssigkeitsmischung aus der Kälteflüssigkeit der Stufe (c) besteht, dadurch gekennzeichnet, daß die Kontakbedingungen der Stufe (f) so ausgewählt werden, daß die in Stufe (e) begonnene Verdampfung vollendet wird, daß die Menge der in Stufe (f) verdampften Fraktion der Flüssigkeitsmischung mindestens 5 Mol.-% der Menge der in den beiden Stufen (e) und (f) verdampften Flüssigkeitsmischung darstellt und daß man die völlig verdampfte Fraktion der Flüssigkeitsmischung aus Stufe (f) direkt in die Stufe (a) zurückleitet.
2. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, daß der Wärmeaustausch, der zwischen der flüssigen Arbeitsmischung in Stufe (f) und der flüssigen Arbeitsmischung in Stufe (c) durchgeführt wird, im Gegenstrom erfolgt.
3. Verfahren gemäß Ansprüchen 1 und 2, dadurch gekennzeichnet, daß die Molfraktion der flüssigen Arbeitsmischung, die während der Stufe (e) verdampft wird, 60 bis 95 % und diejenige, die in Stufe (f) verdampft wird, 5 bis 40 % beträgt, jeweils bezogen auf die Gesamtmenge der während dieser beiden Stufen verdampften Flüssigkeitsmischung.
4. Verfahren gemäß Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der während der Stufe (b) durchgeführte Wärmeaustausch im Gegenstrom erfolgt.
5. Verfahren gemäß Ansprüchen 1 bis 4, dadurch gekennzeichnet, daß der während der Stufe (e) durchgeführte Wärmeaustausch im Gegenstrom erfolgt.
6. Verfahren gemäß Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß das Temperaturintervall von Stufe (e) weniger als 10 °C und dasjenige von Stufe (b) mehr als 10 °C beträgt.
7. Verfahren gemäß Anspruch 6, dadurch gekennzeichnet, daß das Temperaturintervall von Stufe (e) niedriger als 5°C und dasjenige von Stufe (b) höher als 15 °C ist.
8. Verfahren gemäß Ansprüchen 1 bis 7, dadurch gekennzeichnet, daß die flüssige Arbeitsmischung ein nicht-azeotropes Gemisch von Bestandteilen aus der Gruppe der Kohlenwasserstoffe und Halogenkohlenwasserstoffe ist.
9. Verfahren gemäß Ansprüchen 1 bis 7, dadurch gekennzeichnet, daß das flüssige Arbeitsgemisch einen überwiegenden Bestandteil aus der Gruppe R-22, R-12, R-115 und R-502 sowie einen zweiten Bestandteil aus der Gruppe R-11, R-114, R-216, R-21, R-13, R-23 und R-13 B 1 enthält.
10. Verfahren gemäß Ansprüchen 1 bis 9, dadurch gekennzeichnet, daß die Zusammensetzung der flüssigen Arbeitsmischung so ausgewählt wird, daß das für die praktisch vollständige Kondensation in Stufe (b) erforderliche Temperaturintervall etwa gleich der Differenz zwischen der Eingangs- und Ausgangs-Temperatur der relativ kalten Außenflüssigkeit derselben Stufe (b) ist.
11. Verfahren gemäß Ansprüchen 1 bis 10, dadurch gekennzeichnet, daß man den Entspannungsdruck entsprechend der Temperaturänderung am Ausgang der Stufe (e) steuert, so daß die flüssige Arbeitsmischung in Stufe (e) partiell verdampft und die Verdampfung in Stufe (f) vollendet wird.
EP82400042A 1981-01-15 1982-01-11 Verfahren zum Heizen eines Raumes mittels einer Kompressionswärmepumpe mit einem Gemisch als Arbeitsmedium Expired EP0057120B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT82400042T ATE17273T1 (de) 1981-01-15 1982-01-11 Verfahren zum heizen eines raumes mittels einer kompressionswaermepumpe mit einem gemisch als arbeitsmedium.

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Application Number Priority Date Filing Date Title
FR8100847 1981-01-12
FR8100847A FR2497931A1 (fr) 1981-01-15 1981-01-15 Procede de chauffage et de conditionnement thermique au moyen d'une pompe a chaleur a compression fonctionnant avec un fluide mixte de travail et appareil pour la mise en oeuvre dudit procede

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EP0057120A2 EP0057120A2 (de) 1982-08-04
EP0057120A3 EP0057120A3 (en) 1983-05-04
EP0057120B1 true EP0057120B1 (de) 1986-01-02

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EP82400042A Expired EP0057120B1 (de) 1981-01-15 1982-01-11 Verfahren zum Heizen eines Raumes mittels einer Kompressionswärmepumpe mit einem Gemisch als Arbeitsmedium

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US (1) US4406135A (de)
EP (1) EP0057120B1 (de)
JP (1) JPS57184860A (de)
AT (1) ATE17273T1 (de)
DE (1) DE3268192D1 (de)
FR (1) FR2497931A1 (de)

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FR2561363B1 (fr) * 1984-03-14 1987-03-20 Inst Francais Du Petrole Procede de mise en oeuvre d'une pompe a chaleur et/ou d'une machine frigorifique a compression comportant un degivrage periodique par inversion de cycle
FR2564955B1 (fr) * 1984-05-28 1987-03-20 Inst Francais Du Petrole Procede de production de chaleur et/ou de froid au moyen d'une machine a compression fonctionnant avec un fluide mixte de travail
JPS6166053A (ja) * 1984-09-06 1986-04-04 松下電器産業株式会社 熱ポンプ装置
KR860002704A (ko) * 1984-09-06 1986-04-28 야마시다 도시히꼬 열펌프장치
EP0179225B1 (de) * 1984-09-19 1988-10-19 Kabushiki Kaisha Toshiba Wärmepumpe
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FR2575812B1 (fr) * 1985-01-09 1987-02-06 Inst Francais Du Petrole Procede de production de froid et/ou de chaleur mettant en oeuvre un melange non-azeotropique de fluides dans un cycle a ejecteur
FR2578638B1 (fr) * 1985-03-08 1989-08-18 Inst Francais Du Petrole Procede de transfert de chaleur d'un fluide chaud a un fluide froid utilisant un fluide mixte comme agent caloporteur
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WO2020021555A1 (en) * 2016-07-21 2020-01-30 Exency Ltd. Exploiting compression heat in heat engines

Also Published As

Publication number Publication date
JPS57184860A (en) 1982-11-13
FR2497931A1 (fr) 1982-07-16
EP0057120A2 (de) 1982-08-04
EP0057120A3 (en) 1983-05-04
FR2497931B1 (de) 1984-09-28
ATE17273T1 (de) 1986-01-15
DE3268192D1 (en) 1986-02-20
US4406135A (en) 1983-09-27

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