EP0057120A2 - 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

Info

Publication number
EP0057120A2
EP0057120A2 EP82400042A EP82400042A EP0057120A2 EP 0057120 A2 EP0057120 A2 EP 0057120A2 EP 82400042 A EP82400042 A EP 82400042A EP 82400042 A EP82400042 A EP 82400042A EP 0057120 A2 EP0057120 A2 EP 0057120A2
Authority
EP
European Patent Office
Prior art keywords
fluid
mixed
vaporized
fraction
heat exchange
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP82400042A
Other languages
English (en)
French (fr)
Other versions
EP0057120A3 (en
EP0057120B1 (de
Inventor
Alexandre Rojey
Claude Ramet
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Priority to AT82400042T priority Critical patent/ATE17273T1/de
Publication of EP0057120A2 publication Critical patent/EP0057120A2/de
Publication of EP0057120A3 publication Critical patent/EP0057120A3/fr
Application granted granted Critical
Publication of EP0057120B1 publication Critical patent/EP0057120B1/de
Expired legal-status Critical Current

Links

Images

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
    • 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

Definitions

  • the present invention relates to a heating and thermal conditioning process by means of a compression heat pump, operating with a mixed working fluid.
  • non-azeotropic mixed working fluid means a mixture of at least two individuals capable of vaporizing and of being condensed in the working domain of the pump without forming an azeotrope between them, in particular two chemically distinct individuals ( A) and (B) not forming an azeotrope between them in the working area of the pump or a chemical individual (A) and an azeotrope (C) formed between two or more other chemical individuals, azeotropically independent of the individual chemical (A), or even two azeotropes independent of each other (C ') and (C ").
  • the heat which is 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 the 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 an improvement sensitive with respect to a pure body in that, on 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 provides heat, is much higher than the temperature interval according to which the fluid ex 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 provide any significant gain compared to the pure body.
  • the method according to the invention makes it possible to improve the performances which can be obtained in such a case when a mixed fluid is used. It consists in carrying out the evaporation in at least two stages including at least a first stage which is carried out by exchanging heat with the external fluid which constitutes the heat source and at least a second stage which is carried out by exchanging heat with the liquid mixture from the condensation step.
  • the fraction of the mixture which is vaporized during said second stage must be at least 5% of what is vaporized in all of the two stages so that the process according to the invention can bring about a significant gain and is practically between 5 and 40% in molar fraction. Most often the fraction of the mixture vaporized during the first stage is between 60 and 95% in molar fraction of what is vaporized in the two stages.
  • the mixture arrives in liquid phase via line 1. It is expanded through the regulator V1, is sent via line 4 to the exchanger El and is partially vaporized in the exchanger El by taking heat from an external fluid which arrives via line 2 and leaves via
  • the liquid-vapor mixture, leaving the exchanger El, is sent by the conduit 5 in the exchanger E2 from which it emerges entirely vaporized and possibly superheated by the conduit 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 via line 8, then enters the tank Bl. Via line 9, the liquid phase is sent to exchanger E2 in which it cools providing the heat necessary for the end of vaporization and possible overheating of the mixture arriving via line 5 and leaving via 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 at the condenser.
  • the mixture is a binary mixture constituted by a first majority constituent and a second minority constituent, it is known that 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 which are sufficiently different, at a given temperature interval in condensation corresponds a well-defined composition.
  • the composition of a mixture of more than two constituents so as to obtain, at a certain pressure, a given temperature range during the condensation provided that constituents which have boiling temperatures are used. in a pure state and under the same pressure sufficiently different.
  • 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 a temperature at the end of vaporization 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 El. It also makes it possible to enter the regulator V1 at a temperature much lower than the temperature at the outlet of the condenser E3 and thus 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 to further improve the conditions of the heat exchange in the exchanger El.
  • the increase in 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 at suction.
  • 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 characterized in that: (a) the mixed working fluid is compressed in the vapor phase, (b) the compressed mixed fluid coming from step ( a) with a relatively cold external fluid, and this contact is maintained until substantially complete condensation of said mixed fluid, (c) the mixed fluid substantially completely condensed from step (b) is brought into heat exchange contact ) with a cooling fluid defined in step (f), so as to further cool said mixed fluid, (d) the cooled mixed fluid from step (c) is expanded, (e) the mixed fluid is put relaxed, coming from the stage (d), in heat exchange contact with an external fluid which constitutes a heat source, the contact conditions allowing the partial vaporization of said expanded mixed fluid, (f) the partially vaporized mixed fluid, coming from step, is put (e), in heat exchange contact with the substantially completely liquefied mixed fluid sent to step (c), said partially vaporized mixed fluid constituting the cooling fluid of said step (c), the contact conditions making it possible to continue the vaporization started in step (e), and (g) the
  • 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 p 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 1 , 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 Ml 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; likely to improve the exchange and wound in .spirale.
  • the liquid-vapor mixture leaving the evaporator E4 by the conduit 22 completes to vaporize in the exchanger E5 in contact with the mixture arriving by the conduit 21 and leaves the exchanger E5 by the conduit 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 by the intake duct G2 and leaves the enclosure D2 by the discharge duct G3 and thus flows from bottom to top.
  • the condensed mixed fluid leaves through line 25 and it is collected in balloon B 2.
  • the liquid mixed fluid leaves through line 21 and it is sub-cooled. in the exchanger E5 by heating the mixed fluid which vaporizes. It leaves via the conduit 24 by which it arrives at the regulator V 2, from where it is sent by 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 in the exchanger E10, into which it enters through the conduit 30 and exits through the conduit 31; heat exchange in E10 is carried out with a first fraction of the external fluid constituting the cold source, arriving via the tube 43 and leaving via the tube 44.
  • the vaporization of the mixed fluid continues in the exchanger E11, in which the mixed fluid enters into liquid mixture- vapor via line 31, leaves via line 32 and takes the heat of vaporization from the mixed liquid fluid, which circulates against the current, enters E11 through line 41 and exits through line 42.
  • the liquid-vapor mixture is discharged through channel 32 into 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 1 , to an intermediate stage of the compressor K 2.
  • 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 the pressure P 21 cycle lower 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 entrance to the E10 interchange. 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 via line 38; he is mixed with the course compression with the mixed fluid vaporized at pressure P and sucked in through line 33.
  • the final mixture is discharged from K2 through channel 39 at pressure P 3 '. which is the high pressure of the cycle (P 3 >P> P2). 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 to the intermediate pressure of the cycle P l .
  • 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" operation to "summer” operation is obtained for example by implementing a reversing valve 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 mixture used is generally a mixture of constituents of the "Freons" type.
  • the mixtures can thus be formed by binary mixtures comprising a majority constituent such as monochlorodifluoromethane (R-22), dichlorofluoromethane (R-12), chloropentafluoroethane (R-115) or even an azeotro mixture spike such as R-502, an azeotrope of R-22 and R-115 and a second constituent such as trichlorofluoromethane (R-11), dichlorotetrafluoroethane (R-114), dichlorohexafluoropropane (R-216), dichlorofluoromethane (R-21), monochlorotrifluoromethane (R-13), trifluoromethane (R-23), trifluorobromomethane (R-13B1). Specific examples are:
  • the expansion valve In heat pumps used for space heating, the expansion valve 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 above 0 ° 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.
  • 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 -indicators, drying cartridge, anti-liquid blow bottle at the compressor inlet, etc ...
  • Example 1 is illustrated in Figure 1.
  • the cold source is cons formed by water extracted from a water table. This water, the flow rate of which is 1500 l / h, arrives in the evaporator El via the pipe 2 at a temperature of 12 ° C. and leaves the evaporator El through the pipe 3 at a temperature of 5 ° C.
  • the heating water arrives via the conduit 10 at a temperature of 21.3 ° C. and leaves via the conduit 11 at a temperature of 34.5 ° C.
  • the working fluid is a binary mixture whose molar composition is as follows:
  • the mixture leaves the evaporator El at a temperature of 3.5 ° C.
  • the molar fraction vaporized at the outlet of El 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 El 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 4864 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 1084 m3 / h of air coming from the room to be heated, which arrives on the condenser E6 at a temperature of 21.1 ° C and comes out heated to a temperature of 33 , 4 ° C.
  • the working fluid is a ternary mixture, the molar composition of which is as follows:
  • 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 allows both to increase the coefficient of performance of S. 7% and to reduce the volume flow at the compressor suction by 7.4% compared to an installation identical 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 in 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 in 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 Ell, it is 0.5 in fraction molar at the outlet of the evaporator E13 the vaporized fraction is a total of 0.8 in molar fraction (ie 0.3 in the evaporator E13).
  • the vaporization ends completely in the evaporator E12
  • the condensation interval in the exchanger E 14 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 Ell) are neighbors of 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 operating 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.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Compression-Type Refrigeration Machines With Reversible Cycles (AREA)
  • Beverage Vending Machines With Cups, And Gas Or Electricity Vending Machines (AREA)
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.

Applications Claiming Priority (2)

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

Publications (3)

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

Family

ID=9254262

Family Applications (1)

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

Country Status (6)

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

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0174027A2 (de) * 1984-09-06 1986-03-12 Matsushita Electric Industrial Co., Ltd. Wärmepumpengerät
EP0192496A1 (de) * 1985-01-09 1986-08-27 Institut Français du Pétrole Verfahren zur Kälte- und/oder Wärmeproduktion bei Verwendung einer nichtazeotropischen Mischung von Fluiden in einem Ejektorzyklus
FR2578638A1 (fr) * 1985-03-08 1986-09-12 Inst Francais Du Petrole Procede de transfert de chaleur d'un fluide chaud a un fluide froid utilisant un fluide mixte comme agent caloporteur
EP0248296A2 (de) * 1986-05-23 1987-12-09 Energiagazdálkodási Részvénytársaság Verfahren zur Erhoehung des Leistungsfaktors von hybriden Kaeltemaschinen oder Waermepumpen
EP0179225B1 (de) * 1984-09-19 1988-10-19 Kabushiki Kaisha Toshiba Wärmepumpe
DE3922950A1 (de) * 1989-07-12 1991-01-17 Mayer Schuh Gmbh Skistiefel

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59157446A (ja) * 1983-02-22 1984-09-06 松下電器産業株式会社 冷凍サイクル装置
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
HU198328B (en) * 1984-12-03 1989-09-28 Energiagazdalkodasi Intezet Method for multiple-stage operating hibrid (compression-absorption) heat pumps or coolers
US4724679A (en) * 1986-07-02 1988-02-16 Reinhard Radermacher Advanced vapor compression heat pump cycle utilizing non-azeotropic working fluid mixtures
FR2607142B1 (fr) * 1986-11-21 1989-04-28 Inst Francais Du Petrole Melange de fluides de travail utilisables dans les cycles thermodynamiques a compression comprenant du trifluoromethane et du chlorodifluoroethane
US5237828A (en) * 1989-11-22 1993-08-24 Nippondenso Co., Ltd. Air-conditioner for an automobile with non-azeotropic refrigerant mixture used to generate "cool head" and "warm feet" profile
US5076064A (en) * 1990-10-31 1991-12-31 York International Corporation Method and refrigerants for replacing existing refrigerants in centrifugal compressors
CH691743A5 (de) * 1996-04-01 2001-09-28 Satag Thermotechnik Ag Anlage zur Energieumformung nach dem Kaltdampf-Kompressionsverfahren.
US8769972B2 (en) * 2008-12-02 2014-07-08 Xergy Inc Electrochemical compressor and refrigeration system
US11118816B2 (en) * 2009-05-01 2021-09-14 Xergy Inc. Advanced system for electrochemical cell
US8627671B2 (en) * 2009-05-01 2014-01-14 Xergy Incorporated Self-contained electrochemical heat transfer system
US9464822B2 (en) * 2010-02-17 2016-10-11 Xergy Ltd Electrochemical heat transfer system
DE102013211084A1 (de) * 2013-06-14 2014-12-18 Siemens Aktiengesellschaft Verfahren zum Betrieb einer Wärmepumpe und Wärmepumpe
WO2018017980A1 (en) 2016-07-21 2018-01-25 Exency Ltd. Exploiting internally generated heat in heat engines

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2255585A (en) * 1937-12-27 1941-09-09 Borg Warner Method of and apparatus for heat transfer
US2255584A (en) * 1937-12-11 1941-09-09 Borg Warner Method of and apparatus for heat transfer
FR973795A (fr) * 1947-10-20 1951-02-14 Petrocarbon Ltd Perfectionnements apportés aux procédés et appareils de réfrigération
US2794329A (en) * 1954-06-29 1957-06-04 Gen Electric Variable temperature refrigeration
US2952139A (en) * 1957-08-16 1960-09-13 Patrick B Kennedy Refrigeration system especially for very low temperature
FR2177785A1 (de) * 1972-03-24 1973-11-09 Monsator Haushaltsgrossgeraete
US3889485A (en) * 1973-12-10 1975-06-17 Judson S Swearingen Process and apparatus for low temperature refrigeration
FR2296827A1 (fr) * 1974-12-31 1976-07-30 Vignal Maurice Perfectionnements a la pompe a chaleur
FR2337855A1 (fr) * 1976-01-07 1977-08-05 Inst Francais Du Petrole Procede de production de chaleur utilisant une pompe de chaleur fonctionnant avec un melange de fluides
FR2356097A1 (fr) * 1976-06-23 1978-01-20 Krieger Heinrich Procede et installation pour produire du froid avec au moins un circuit en cascade incorpore
EP0021205A2 (de) * 1979-06-08 1981-01-07 Energiagazdalkodasi Intezet Hybrides Kompressions-Absorphionsverfahren für das Betreiben von Wärmepumpen oder Kältemaschinen

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2041725A (en) * 1934-07-14 1936-05-26 Walter J Podbielniak Art of refrigeration
US2581558A (en) * 1947-10-20 1952-01-08 Petrocarbon Ltd Plural stage cooling machine
US2794328A (en) * 1954-06-29 1957-06-04 Gen Electric Variable temperature refrigeration
US2841965A (en) * 1954-06-29 1958-07-08 Gen Electric Dual capacity refrigeration
US2867094A (en) * 1954-09-30 1959-01-06 Gen Electric Variable temperature refrigeration
DE1241468B (de) * 1962-12-01 1967-06-01 Andrija Fuderer Dr Ing Kompressionsverfahren zur Kaelterzeugung
US4167101A (en) * 1975-08-14 1979-09-11 Institut Francais Du Petrole Absorption process for heat conversion
FR2474151A1 (fr) * 1980-01-21 1981-07-24 Inst Francais Du Petrole Procede de production de chaleur au moyen d'une pompe a chaleur utilisant un melange specifique de fluides comme agent de travail
FR2476287A1 (fr) * 1980-02-15 1981-08-21 Inst Francais Du Petrole Procede de production de froid et/ou de chaleur par cycle a absorption utilisable notamment pour le chauffage de locaux
SU1035354A1 (ru) * 1980-10-16 1983-08-15 Всесоюзный Научно-Исследовательский Экспериментально-Конструкторский Институт Электробытовых Машин И Приборов Способ получени холода в одноступенчатой компрессионной холодильной машине

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2255584A (en) * 1937-12-11 1941-09-09 Borg Warner Method of and apparatus for heat transfer
US2255585A (en) * 1937-12-27 1941-09-09 Borg Warner Method of and apparatus for heat transfer
FR973795A (fr) * 1947-10-20 1951-02-14 Petrocarbon Ltd Perfectionnements apportés aux procédés et appareils de réfrigération
US2794329A (en) * 1954-06-29 1957-06-04 Gen Electric Variable temperature refrigeration
US2952139A (en) * 1957-08-16 1960-09-13 Patrick B Kennedy Refrigeration system especially for very low temperature
FR2177785A1 (de) * 1972-03-24 1973-11-09 Monsator Haushaltsgrossgeraete
US3889485A (en) * 1973-12-10 1975-06-17 Judson S Swearingen Process and apparatus for low temperature refrigeration
FR2296827A1 (fr) * 1974-12-31 1976-07-30 Vignal Maurice Perfectionnements a la pompe a chaleur
FR2337855A1 (fr) * 1976-01-07 1977-08-05 Inst Francais Du Petrole Procede de production de chaleur utilisant une pompe de chaleur fonctionnant avec un melange de fluides
FR2356097A1 (fr) * 1976-06-23 1978-01-20 Krieger Heinrich Procede et installation pour produire du froid avec au moins un circuit en cascade incorpore
EP0021205A2 (de) * 1979-06-08 1981-01-07 Energiagazdalkodasi Intezet Hybrides Kompressions-Absorphionsverfahren für das Betreiben von Wärmepumpen oder Kältemaschinen

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0174027A2 (de) * 1984-09-06 1986-03-12 Matsushita Electric Industrial Co., Ltd. Wärmepumpengerät
EP0174027A3 (en) * 1984-09-06 1987-12-23 Matsushita Electric Industrial Co., Ltd. Heat pump apparatus
EP0179225B1 (de) * 1984-09-19 1988-10-19 Kabushiki Kaisha Toshiba Wärmepumpe
EP0192496A1 (de) * 1985-01-09 1986-08-27 Institut Français du Pétrole Verfahren zur Kälte- und/oder Wärmeproduktion bei Verwendung einer nichtazeotropischen Mischung von Fluiden in einem Ejektorzyklus
FR2578638A1 (fr) * 1985-03-08 1986-09-12 Inst Francais Du Petrole Procede de transfert de chaleur d'un fluide chaud a un fluide froid utilisant un fluide mixte comme agent caloporteur
EP0195704A1 (de) * 1985-03-08 1986-09-24 Institut Français du Pétrole Verfahren zum Wärmeaustausch zwischen einer warmen und einer kalten Flüssigkeit mittels einer gemischten Flüssigkeit als Wärmeträger
EP0248296A2 (de) * 1986-05-23 1987-12-09 Energiagazdálkodási Részvénytársaság Verfahren zur Erhoehung des Leistungsfaktors von hybriden Kaeltemaschinen oder Waermepumpen
EP0248296A3 (en) * 1986-05-23 1988-05-25 Energiagazdalkodasi Intezet Method and device for increasing the coefficient of performance of hybrid refrigeration machines or heat pumps
DE3922950A1 (de) * 1989-07-12 1991-01-17 Mayer Schuh Gmbh Skistiefel

Also Published As

Publication number Publication date
DE3268192D1 (en) 1986-02-20
EP0057120A3 (en) 1983-05-04
FR2497931A1 (fr) 1982-07-16
EP0057120B1 (de) 1986-01-02
FR2497931B1 (de) 1984-09-28
ATE17273T1 (de) 1986-01-15
JPS57184860A (en) 1982-11-13
US4406135A (en) 1983-09-27

Similar Documents

Publication Publication Date Title
EP0057120B1 (de) Verfahren zum Heizen eines Raumes mittels einer Kompressionswärmepumpe mit einem Gemisch als Arbeitsmedium
EP1355716B1 (de) Verfahren und vorrichtung zur entfernung von kohlendioxid durch desublimation in hinblick auf seine endlagerung
CA1172054A (fr) Procede de production de chaleur au moyen d'une pompe a chaleur utilisant un melange de fluides comme agent de travail et l'air comme source de chaleur
FR2476240A1 (fr) Appareil de recuperation d'energie pour installation de compresseur de gaz
EP0041005A1 (de) Verfahren zur mechanischen Energieerzeugung aus Wärme mit Mehrstoffgemischen als Arbeitsmittel
FR2514875A1 (fr) Procede de chauffage et/ou de conditionnement thermique d'un local au moyen d'une pompe a chaleur a compression utilisant un melange specifique de fluides de travail
CA1295140C (fr) Procede de production de froid et/ou de chaleur a absorption utilisant un melange de plusieurs constituants comme fluide de travail
FR2474151A1 (fr) Procede de production de chaleur au moyen d'une pompe a chaleur utilisant un melange specifique de fluides comme agent de travail
US4809521A (en) Low pressure ratio high efficiency cooling system
EP0192496B1 (de) Verfahren zur Kälte- und/oder Wärmeproduktion bei Verwendung einer nichtazeotropischen Mischung von Fluiden in einem Ejektorzyklus
WO2019110628A1 (fr) Système et procédé de refroidissement d'un flux gazeux au moyen d'un évaporateur
EP0081395B1 (de) Flüssigkeit für Wärmepumpe und Verfahren zur Heizung und/oder Klimatisierung eines Raumes durch eine Kompressionswärmepumpe die eine spezielle Mischung von Arbeitsflüssigkeiten verwendet
EP0956485A1 (de) Absorptionskälteanlage und arbeitsgemisch dazu
EP2411743B1 (de) Anlage und verfahren zur erzeugung von kälte und/oder wärme
US20060242974A1 (en) Evaporation process control for use in refrigeration technology
BE1013535A3 (fr) Dispositif de refroidissement combinant l'utilisation d'une boucle diphasique et d'un systeme de refrigeration a absorption, notamment applicable pour le reffroidissement de l'air d'admission d'un moteur a combustion interne.
WO2016146858A1 (fr) Dispositif thermodynamique reversible de transfert de chaleur
FR3075934A1 (fr) Centrale de traitement de l'air comprenant un dispositif a absorption et procede associe
FR2699087A1 (fr) Dispositif d'amélioration des performances des colonnes de distillation.
FR2508617A1 (fr) Procede et appareil pour extraire de l'energie thermique d'une substance
EP4330603A1 (de) Wärmepumpe und phasenwechselenergiespeichervorrichtung
FR2683301A1 (fr) Dispositif de refrigeration mixte compression-absorption.
DK178705B1 (en) A heat pump system using water as the thermal fluid
EP4325150A1 (de) Verfahren und vorrichtung zur kühlung von wasserstoff
FR2755753A1 (fr) Melange frigorigene de type zeotrope sans derives chlores

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): AT BE CH DE GB IT NL SE

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Designated state(s): AT BE CH DE GB IT LI NL SE

17P Request for examination filed

Effective date: 19830930

ITF It: translation for a ep patent filed

Owner name: ST. ASSOC. MARIETTI & PIPPARELLI

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): AT BE CH DE GB IT LI NL SE

REF Corresponds to:

Ref document number: 17273

Country of ref document: AT

Date of ref document: 19860115

Kind code of ref document: T

REF Corresponds to:

Ref document number: 3268192

Country of ref document: DE

Date of ref document: 19860220

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19890131

Year of fee payment: 10

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 19910103

Year of fee payment: 10

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19910111

Year of fee payment: 10

ITTA It: last paid annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19910308

Year of fee payment: 10

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Effective date: 19920111

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Effective date: 19920131

Ref country code: CH

Effective date: 19920131

Ref country code: BE

Effective date: 19920131

BERE Be: lapsed

Owner name: INSTITUT FRANCAIS DU PETROLE

Effective date: 19920131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19920801

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19921223

Year of fee payment: 12

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19930107

Year of fee payment: 12

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19930306

Year of fee payment: 12

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19940111

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19940112

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19940111

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19941001

EUG Se: european patent has lapsed

Ref document number: 82400042.6

Effective date: 19940810