EP0138041B1 - Méthode de réfrigération mécanique aidée chimiquement - Google Patents

Méthode de réfrigération mécanique aidée chimiquement Download PDF

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Publication number
EP0138041B1
EP0138041B1 EP84110693A EP84110693A EP0138041B1 EP 0138041 B1 EP0138041 B1 EP 0138041B1 EP 84110693 A EP84110693 A EP 84110693A EP 84110693 A EP84110693 A EP 84110693A EP 0138041 B1 EP0138041 B1 EP 0138041B1
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Prior art keywords
refrigerant
solution
zone
solvent
stream
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EP0138041A2 (fr
EP0138041A3 (en
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Arnold R. Vobach
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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
    • F25B25/00—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00
    • F25B25/02—Compression-sorption machines, plants, or systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B75/00—Other engines
    • F02B75/02—Engines characterised by their cycles, e.g. six-stroke
    • F02B2075/022—Engines characterised by their cycles, e.g. six-stroke having less than six strokes per cycle
    • F02B2075/027—Engines characterised by their cycles, e.g. six-stroke having less than six strokes per cycle four

Definitions

  • This invention relates generally to refrigeration and more particularly to a new and improved chemically assisted mechanical refrigeration cycle.
  • the typical mechanical refrigeration system employs a mechanical compressor to raise the pressure and to condense a gaseous refrigerant, which thereafter absorbs its heat of vaporization.
  • the typical vapor compression cycle uses an evaporator in which a liquid refrigerant, such as Freon-12, boils at a low pressure to produce cooling, a compressor to raise the pressure of the gaseous refrigerant after it leaves the evaporator; a condenser, in which the refrigerant condenses and discharges its heat to the environment, and an expansion valve through which the liquid refrigerant leaving the condenser expands from the high-pressure level in the condenser to the low pressure level in the evaporator.
  • a liquid refrigerant such as Freon-12
  • the resorption cycle has also been studied. Introduced in the earlier half of this century, the resorption cycle is similar in operation to the absorption cycle. However, a resorber replaces the condenser and the vapor is absorbed by a special week solution while condensing. This solution is then circulated to the evaporator where the refrigerant boils and the heats of disassociation and vaporization produce the refrigerating effect.
  • This discloses a chemically assisted mechanical refrigeration process comprising the steps of mixing a solvent and a refrigerant that in combination have a negative deviation from Raoult's Law, in a mixing zone under conditions to form a solution of the refrigerant in the solvent, effecting heat-exchange between said solution and a working medium to remove heat from the solution; passing a stream of the solution through an economizing zone to a refrigeration zone in which the pressure over the solution is reduced to allow evolution of refrigerant, thereby to form a gaseous refrigerant stream and a depleted solution stream; effecting heat-exchange in the refrigeration zone between a working medium and said solution to remove heat from the working medium; passing the depleted solution stream through the economizing zone in heat-exchange relation with the stream of solution passing therethrough to the refrigeration zone; transferring gaseous refrigerant evolved from the depleted solution stream in the economizing zone to the gaseous refrigerant stream; and pumping the gaseous refrigerant and deplete
  • both the gaseous refrigerant evolved in the refrigeration zone and the depleted solvent-refrigerant solution exiting the refrigeration zone are passed through the economizing zone, so that although there is mass transfer of refrigerant between the two streams in the economizing zone, the cooling effect of refrigerant evolution in the economizing zone is partly offset by the retention in that zone of heat in the refrigerant stream.
  • the streams of refrigerant and depleted solution exiting the economizing zone are separately compressed and passed to the mixing zone.
  • DE-A-2 850 403 also discloses a process of this general type but in which only the depleted solvent-refrigerant solution is passed through the economizing zone, the gaseous refrigerant evolved in the refrigeration zone being passed directly to a compressor in which it is compressed jointly with the stream of depleted solvent-refrigerant solution that has passed through the economizing zone.
  • the cooling effect of evolution of gaseous refrigerant from the depleted solution in the economizing zone is offset by a retention in that zone of heat in the refrigerant stream.
  • One object of the present invention is to provide an improved process of this general type represented by US-A-1 675 455 and DE-A-2 850 403 and accordingly, in one aspect of the invention provides such a process, in which (as in DE-A-2 850 403) the gaseous refrigerant stream from the refrigeration zone is passed to the mixing zone externally of the economizing zone and there is joint compression of both the gaseous refrigerant and the depleted solution, the process of the invention being characterised by providing a fluid communication between said depleted solution stream in said economizing zone and said gaseous refrigerant stream such that gaseous refrigerant evolving from said depleted solution stream may leave said economizing zone separately from said depleted solution stream and pass to said refrigerant stream.
  • the compressed refrigerant and depleted solution may be passed to the mixing zone through a precooling zone in heat-exchange relationship with the solution passing from the mixing zone to the economizing zone.
  • Preferably the temperature of the compressed refrigerant and depleted solution are raised in the precooling zone to a temperature approaching that in the mixing zone.
  • a further object of the invention is to provide apparatus for carrying out this improved process.
  • the invention further provides a chemically assisted mechanical refrigeration apparatus comprising a mixer configured to mix a solvent and a refrigerant that in combination have a negative deviation from Raoult's Law, under conditions to form a solution of the refrigerant in the solvent, and means for effecting heat-exchange between the solution and a working medium to remove heat from the solution; a refrigeration zone adapted for evolution of refrigerant from said solution while in heat-exchange relationship with a working medium to remove heat from that working medium, thereby to produce gaseous refrigerant and a depleted solvent-refrigerant solution; an economizer adapted to accomplish heat-exchange between said solution passing to the refrigeration zone and said depleted solvent-refrigerant solution exiting the refrigeration zone; compressor means for jointly compressing said gaseous refrigerant and said depleted solution, and flow path means external of said economizer for gaseous refrigerant evolved in the refrigeration zone,
  • the apparatus may also comprise a precooler for accomplishing heat-exchange between the compressed refrigerant and depleted solution passing from the compressor means to the mixer, and the refrigerant-solvent solution passing from the mixer to the economizer, respectively.
  • a chemically assisted mechanical refrigeration process including several steps.
  • the refrigerant and solvent have a negative deviation from Raoult's Law when in combination.
  • a stream of solution including a solvent and a liquefied refrigerant is passed to a refrigeration zone such as provided by an evaporator.
  • the pressure is then reduced over the solution to allow refrigerant to vaporize and separate from the solvent while concurrently therewith the evolving refrigerant and solvent are put in heat-exchange relation with a working medium to remove energy from the working medium and thereby form a depleted solution stream and a refrigerant stream leaving the refrigeration zone.
  • the refrigerant stream includes gaseous refrigerant.
  • the depleted solution stream leaving the refrigeration zone is then passed in heat-exchange relation with the solution stream passing to the refrigeration zone, in an economizing zone, so as to cause transfer of heat between the two solution streams.
  • the refrigerant stream does not pass through the economizing zone but the depleted solution stream in the economizing zone and the refrigerant stream are put in fluid communication with each other so as to accomplish mass transfer of gaseous refrigerant from the depleted solution stream to the refrigerant stream and so facilitate heat transfer in the economizing zone between the two solution streams.
  • the depleted solution and refrigerant streams are subsequently jointly compressed in a compression zone where the pressure over both streams is raised.
  • the compressed solvent and refrigerant are then passed to a mixing zone under a pressure sufficient to promote substantial dissolving of the refrigerant in the solvent to form the stream of solution for passage to the refrigeration zone.
  • a mixing zone is in heat-exchange relation with a working medium, energy to removed from the mixing zone.
  • the compressed refrigerant and solvent passing to the mixing zone from the compression zone may undergo heat-exchange in a precooling zone with the stream of solution leaving the mixing zone.
  • FIG. 1 illustrates an embodiment of this process.
  • a solvent-liquefied refrigerant solution stream is passed via line 25 to evaporator 10.
  • the refrigerant and solvent of the solvent-liquefied refrigerant stream have a negative deviation from Raoult's Law and may be chosen from a number of combinations of substances, as more fully discussed below.
  • the pressure over the solution is reduced in the evaporator in order to allow refrigerant to vaporize and separate from the solvent while concurrently placing the evolving refrigerant and solution in heat-exchange relation with the working medium to remove energy from the working medium.
  • a depleted solution stream which passes via line 24 and a refrigerant stream including gaseous refrigerant which passes via line 18.
  • the stream passing via line 24 may contain a material portion of refrigerant without hindering the efficiency of the process.
  • the depleted solution stream leaving the evaporator and passing via line 24 passes through an economizer 26 in which it is placed in heat-exchange relation with the solvent-refrigerant solution stream passing to the evaporator via lines 15 and 25. Further, the depleted solution stream in line 24 is placed in fluid communication with the refrigerant stream of line 18 such that gaseous refrigerant evolving from the stream 24 in the economizer may pass via conduit 92 to the external refrigerant stream 18.
  • Both the depleted solution (solvent) stream leaving the economizing zone and the refrigerant stream are then brought into thermal and physical contact in a joint compression zone as illustrated by compressor 88 in Figure 1.
  • the compression of the refrigerant in thermal contact wihh the liquid solvent in a joint compression zone such as compressor 88 is believed to provide several advantages.
  • the liquid solvent would generally have a higher heat capacity than the refrigerant and generally act as a coolant in the compressor, thus reducing the amount of work required to compress the refrigerant.
  • a liquid solvent may be chosen which acts both as a sealant and a lubricant as well as a coolant.
  • the solvent provides internal cooling of the overall apparatus thus permitting compression which is more polytropic than isentropic and hence generally more economical.
  • the presence of the solvent in the compressor permits higher pressures in the case of a centrifugal compressor, or severs as a lubricant and sealant in case of a rotary compressor.
  • the resulting combined solvent-refrigerant stream flows via line 90 through a heat-exchanger such as precooler 86 and into mixer 11.
  • the heat-exchanger or precooler 86 serves to further raise the temperature of the solvent-refrigerant combination passing to mixer 11 while concurrently beginning to cool the refrigerant-solvent stream passing via line 15 toward economizer 26.
  • the heat exchanger, such as precooler 86 should be operated so as to allow the temperature of the solvent-refrigerant combination stream entering mixer 11 to approach as closely as possible the temperature of mixer 11 without exceeding the same. Additionally, the precooler should be operated in a such a fashion that the temperature of the solvent-refrigerant combination passing via line 90 in such that the refrigerant will not start to substantially dissolve and give off heat prior to reaching the mixer 11.
  • the combined solvent-refrigerant stream is maintained at a pressure sufficient for the given temperature to promote substantial dissolving of the refrigerant in the solvent to form the stream of solution for passage to the evaporator 10 via lines 15 and 25.
  • the mixer is in heat exchange relation with a working medium which removes energy of heat given off by the dissolving and condensing refrigerant in the mixer 11.
  • the evaporator is so constructed as to allow substantial transfer of both the heat of vaporization and the heat of disassociation from the working medium.
  • the heat transfer surface may preferably be wetted by the solvent with or without dissolved refrigerant.
  • the refrigerant-solvent stream may be passed as a thin film over a heat transfer surface with embedded coils containing the working medium.
  • a working medium such as chilled water is passed via a line 22 through the shell side of a shell and tube type heat-exchanger while the refrigerant-solvent solution stream entering from a line 21 passes through the tube side.
  • the refrigerant evolves from the solution in the tubes and both depleted solution and refrigerant pass to a liquid-vapor separator 31 where the depleted solution and refrigerant are separated.
  • the liquid-vapor separator 31 may be equipped with a wire mesh 32 to catch entrained droplets, which collect below wire mesh 32.
  • the depleted solution passes via a line 24 to the economizer while the refrigerant passes via line 18 to the compressor.
  • the conduit 22 is substantially immersed in liquid in the evaporator, the refrigerant substantially disassociates and boils off from the solution, thus cooling the working medium.
  • the evaporator may be similar in construction to a shell and tube heat exchanger wherein the working medium circulates through the tubes, which are substantially immersed in liquid.
  • the working medium may pass through a coil, which passes through the lower portion of the evaporator and so is substantially immersed in liquid.
  • the refrigerant-solvent stream may circulate and undergo separation in a single-tube coil of 13 mm (2 inch) diameter for a one to four ton apparatus and then further separate in a liquid-vapor separator.
  • the evaporator may comprise any one of several modified heat exchangers or evaporators.
  • an eliminator may be employed at the vapor outlet of the evaporator if the vapor and liquid separate into two streams in the evaporator.
  • the compressor may be any one of several mecahnical types. Regardless of the type of compressor used, in keeping with the spirit of the present invention, its operating cost should generally be less than that of its counterpart in a typical vapor compression refrigeration system for a given application. This is possible due to the increased efficiency of the present system. This increased efficiency over prior mechanical vapor compression cycles is believed to result in part from the fact that the solubility of the refrigerant in the solvent reduces the level of required mechanical compression.
  • the refrigerant need only be pressurized sufficiently to dissolve in the solvent in the mixer at the given operating conditions and concentrations. There is believed to be little or no wasted compression of the refrigerant to pressurize it sufficiently to condense at the mixer temperature as in the usual vapor compression cycle. Additionally, since the refrigerant is at a lower temperature as it leaves the mixer than.in the case of a pure refrigerant cycle, less heat transfer is required and hence less working medium need be circulated to the mixer.
  • the compressor chosen may vary with operating conditions, the refrigerant-solvent combination chosen or the application to which the system is applied.
  • a centrifugal, rotary or screw compressor may be preferred.
  • the refrigerant-solvent combination comprises at least two constituents-a refrigerant and a solvent.
  • the refrigerant and solvent are chosen such that the refrigerant will separate as a gas from the solvent under the operating conditions in the evaporator while preferably absorbing substantial amounts of the heats of demixing, dilution, or disassociation as well as vaporization.
  • a governing principle for the selection of a refrigerant-solvent combination is that the refrigerant be highly soluble in the solvent, such that the pair exhibits negative deviations from Raoult's Law.
  • the solvent constituent should be a substantially non-volatile liquid at the operating conditions of the cycle or be at least such when in solution with a portion of the refrigerant.
  • the solvent for example, nitrous oxide, can be a gas at room temperature.
  • the solvent may be an ether, an ester, an amide, an amine or polymeric derivatives of these, for example, dimethyl formamide and dimethyl ether of tetraethylene glycol as well as halogenated hydrocarbons, such as carbon tetrachloride and dichlorethylene; or appropriate combinations of these
  • a halogenated salt such as lithium bromide may also be a constituent of the solvent.
  • solvents are methanol, ethanol, acetone, chloroform and trichloroethane.
  • Organic physical solvents such as propylene carbonate and sulfolane or other organic liquids containing combined oxygen may be used.
  • the comparative efficiency of the instant invention is illustrated by reference to available data for a refrigerant-solvent pair comprising CHCIF 2 (refrigerant R22) and dimethyl formamide (DMF).
  • CHCIF 2 refrigerant R22
  • DMF dimethyl formamide
  • the R22 will boil out of the DMF, absorbing a combined heat of vaporization and heat of mixing of slightly more than 167.36 J/kg (72 But/lb).
  • the heat of mixing can be calculated from Equation (14) in Tyagi, K.P., Heat of Mixing, Ind. Jnl. of Tech., 14 (1976), pp. 167-169, herein incorporated by reference, to be 44.93 J/kg (19.33 Btu/ib) while the heat of vaporization of the R22 is 129.98 J/kg (55.92 Btu/Ib) of solution.
  • the total heat absorbed, per kilogram of solution entering the evaporator is 174.91 J (75.25 Btullb), in close agreement with the enthalpy-concentration diagram mentioned above.
  • the refrigerant-solvent mixture or combination be chosen such that a substantial amount of refrigerant vaporizes from solution in the evaporator, this need not always be the case.
  • a refrigerant with a comparatively high heat of vaporization may be circulated in small proportions relative to the amount of solvent because the refrigerant-solvent leaving the mixer is placed in heat exchange relation with the depleted solution leaving the evaporator.
  • the refrigerant-solvent combination may be used to cool the refrigerant-solvent solution stream exiting the mixer. Since this combination passing via line 90 is at mixer pressure as it enters the mixer, but below mixer temperature as it begins its passage through precooler 86, it is assumed that solution of refrigerant into solvent will have begun in the precooler 86. With R22 as a refrigerant and 1,1,1-trichloroethane as the solvent at the temperature shown, a theoretical maximum of only half the heat exchange theoretically available for inert liquids is available, and the resultant theoretical coefficient of performance is 7.13. (The theoretical maximum coefficient of performance for a perfect (Carnot) cycle is 7.14).
  • the 0.310 kg (0.684 Ibs) of TCE enters the compressor at 21.63°C (70.93°F), absent precooler 86, or 20.91°C (69.64°F) with precooler 86 between the compressor 88 and mixer 11, and the entering temperature of the 0.163 kg (0.36 Ibs) of R22 including warmer than 4.44°C (40°F) gas from the economizing zone is calculated as 5.90°C (42.62°F), absent the precooler 86, or 5.83°C (42.5°F) with the precooler 86.
  • Isentropic compression of the gas alone would give a discharge temperature of 64.44°C (148°F), so that the discharge temperature of the liquid and gas is 38.06°C (100.51°F), or in case precooler 86 is used, 37.36°C (99.25°F).
  • the work of compression is that is, 21.61 kJ per 0.143 kg (2.05 Btu per 0.316 Ib) R22 vaporized.
  • V and V 2 are taken from the superheat tables of American Society of Heating, Refrigerating and Air Conditioning Engineers, Thermodynamic Properties of Refrigerants, 1980).
  • the density of the stripped TCE leaving the economizer 26 is 1345.23 kg/m l (83.98 Ib/ft 3 )
  • the pressure head across the 482.63 kPa (70 psi) differential is 36.70 m (120.42 ft)
  • the work of pumping 0.310 kg (0.684 lb) of TCE is 0.112 kJ (0.106 Btu).
  • the total work of compressing the gas and pumping the liquid is 5.02 J/kg '(2.16 Btu/Ib) of mixture.
  • the net available refrigerating effect is 15.27 kJ/kg (14.48 Btu/Ib) of gas-liquid circulating mass, absent the precooler 86.
  • the coefficient of performance is now 7.13, compared with 6.71 without the precooler 86 and as compared to 5.75 for pure R22. Since the theoretically perfect Carnot efficiency between 4.44°C (40°F) and 43.33°C (110°F) is 7.14, it appears that the precooler provides an even greater efficiency, since 7.13 is about 25% better than 5.75.
  • the present invention may also be used in conjunction with other systems.
  • a generator-absorber pair might be hooked up in tandem with the compressor to provide a back-up for the same.
  • the generator could function off a secondary source of heat, such as from an exhaust, or a form of solar energy.
  • valves could be placed on both sides of compressor 88 in lines 18 and 90 to hook a generator-absorber pair into the system.
  • a portion of the vaporized refrigerant could then pass from line 18 to the absorber, be absorbed in an appropriate secondary solvent and then be pumped in solution to the generator.
  • the now compressed vapor could be passed via line 90 to the mixer 11, while secondary solvent was returned to the absorber.
  • the secondary solvent may be the same as used in the primary system.
  • the generator-absorber pair should not be completely substituted for the compressor 88. Rather, the generator-absorber pair and the mechanical compressor are complementary means of generating pressurized refrigerant gas.
  • the Wankel-type compressor manufactured by Ogura Clutch of Japan, or the rolling piston compressors of Rotorex (Fedders) and Mitsubishi may prove useful.
  • the multistage centrifugal compressor-pump of the type manufactured by Sihi In this device, a gas-liquid mixture enters a first, closed impeller axially and the denser liquid is thrown to the periphery. The lighter gas is ported off to the second and subsequent stages nearer the center of the chamber and both gas and liquid are then carried together through second and subsequent impeller stages.
  • a turbine may be installed in the refrigerant-solvent stream between the economizer and evaporator to function as a pressure reducing device, supplementing throttling devices. Under appropriate operating conditions. It is believed that a subcooled stream exiting the economizer is least likely to flash refrigerant gas at this point and the resultant shaft work may be used to power booster pumps, compressors for the system, auxiliary fans or the like.
  • Additional items of equipment may be employed within the framework of the present invention.
  • control of the system as well as system versatility may be enhanced through the use of appropriate process controls, though the use of essentially manual control devices may suffice for many operations.
  • a low pressure drop mixing of gaseous refrigerant and liquid could be achieved by using an inline motionless mixer such as one offered by the Mixing Equipment Co., Inc. of Avon, New York.

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  • Engineering & Computer Science (AREA)
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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
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Claims (5)

1. Procédé de réfrigération mécanique assistée chimiquement, comprenant les étapes qui consistant à mélanger un solvant et un réfrigérant qui, en combinaison, présentent un écart négatif par rapport à la loi de Raoult, dans une zone de mélangeage dans des conditions amenant à former une solution du réfrigérant dans ledit solvant; à effectuer un échange de chaleur entre ladite solution et un milieu de travail pour éliminer de la chaleur de la solution; à faire passer un courant de ladite solution à travers une zone économiseuse vers une zone de réfrigération dans laquelle la pression exercée sur la solution est réduite pour permettre un dégagement du réfrigérant, afin de former un courant de réfrigérant gazeux et un courant de solution épuisée; à effectuer un échange de chaleur dans ladite zone de réfrigération entre un milieu de travail et ladite solution pour éliminer de la chaleur dudit milieu de travail; à faire passer ledit courant de solution épuisée à travers ladite zone économiseuse en relation d'échange de chaleur avec le courant de solution la traversant vers la zone de réfrigération; et à faire passer par pompage ledit réfrigérant gazeux et ladite solution épuisée de la zone économiseuse dans ladite zone de mélangeage par passage dudit courant de réfrigérant gazeux de la zone de réfrigération dans la zone de mélangeage extérieurement à la zone économiseuse et, conjointement, compression du réfrigérant et de la solution épuissée, caractérisé par l'établissement d'une communication de fluide entre ledit courant de solution épuisée dans ladite zone économiseuse et ledit courant de réfrigérant gazeux de manière que le réfrigérant gazeux se dégageant dudit courant de solution épuisée puisse quitter ladite zone économiseuse séparément dudit courant de solution épuissé et passer dans ledit courant de réfrigérant.
2. Procédé selon la revendication 1, caractérisé en outre en ce qu'il consiste à faire passer le réfrigérant comprimé et la solution épuisée dans la zone de mélangeage à travers une zone de prérefroidissement en relation d'échange de chaleur avec la solution passant de la zone de mélangeage dans la zone économiseuse.
3. Procédé selon la revendication 2, caractérisé en outre en ce que la température du réfrigérant comprimé et de la solution épuisée est élevée dans ladite zone de prérefroidissement jusqu'à une température approchant celle régnant dans la zone de mélangeage.
4. Appareil de réfrigération mécanique assistée chimiquement comprenant un mélangeur (11) configuré pour mélanger un solvant et un réfrigérant qui, en combinaison, présentent un écart négatif par rapport à la loi de Raoult, dans des conditions telles qu'il se forme une solution du réfrigérant dans le solvant, et des moyens destinés à effectuer un échange de chaleur entre la solution et un milieu de travail pour éliminer de la chaleur de la solution; une zone de réfrigération (10) conçue pour un dégagement du réfrigérant de ladite solution tandis qu'une relation d'échange de chaleur est établie avec un milieu de travail pour éliminer de la chaleur de ce milieu de travail, afin de produire un réfrigérant gazeux et une solution de réfrigérant dans le solvant épuisé; un économiseur (26) conçu pour effectuer un échange de chaleur entre ladite solution se dirigeant vers la zone de réfrigération (10) et ladite solution de réfrigérant dans un solvant épuisé sortant de la zone de réfrigération; des moyens compresseurs (88) destinés à comprimer conjointement ledit réfrigérant gazeux et ladite solution épuisée; et des moyens (18) de trajet d'écoulement extérieure audit économiseur (26) pour le réfrigérant gazeux dégagé de la zone de réfrigération (10), caractérisé par un trajet d'écoulement (92) s'étendant entre l'économiseur (26) et les moyens (18) de trajet d'écoulement du réfrigérant gazeux, en un point situé entre la zone de réfrigération (10) et les moyens compresseurs (88) pour transférer le réfrigérant se dégageant de la solution épuisée dans l'économiseur (26) vers les moyens (18) de trajet d'écoulement du réfrigérant gazeux.
5. Appareil selon la revendication 4, caractérisé en outre par un prérefroidisseur (86) destiné à effectuer un échange de chaleur entre le réfrigérant comprimé et la solution épuisée se dirigeant des moyens compresseurs (88) vers la mélangeur (11), et la solution réfrigérant-solvant se dirigeant du mélangeur (11) vers l'économiseur (26), respectivement.
EP84110693A 1983-09-29 1984-09-07 Méthode de réfrigération mécanique aidée chimiquement Expired EP0138041B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84110693T ATE41506T1 (de) 1983-09-29 1984-09-07 Chemisch unterstuetzter mechanischer kuehlprozess.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US53772483A 1983-09-29 1983-09-29
US537724 1983-09-29

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EP0138041A2 EP0138041A2 (fr) 1985-04-24
EP0138041A3 EP0138041A3 (en) 1986-03-26
EP0138041B1 true EP0138041B1 (fr) 1989-03-15

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EP (1) EP0138041B1 (fr)
JP (1) JPS60105869A (fr)
AT (1) ATE41506T1 (fr)
CA (1) CA1233655A (fr)
DE (1) DE3477259D1 (fr)

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HU198329B (en) * 1986-05-23 1989-09-28 Energiagazdalkodasi Intezet Method and apparatus for increasing the power factor of compression hybrid refrigerators or heat pumps operating by solution circuit
US4724679A (en) * 1986-07-02 1988-02-16 Reinhard Radermacher Advanced vapor compression heat pump cycle utilizing non-azeotropic working fluid mixtures
DE4230818A1 (de) * 1992-09-15 1994-03-17 Fritz Egger Gmbh Verfahren und Einrichtung zur Leistungsregelung einer Kompressions-Wärmepumpe und/oder Kältemaschine
FR2726895B1 (fr) * 1994-11-10 1997-01-17 Electricite De France Pompe a chaleur a compression-absorption fonctionnant avec transfert de chaleur du circuit d'huile vers le circuit de solution pauvre
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ATE41506T1 (de) 1989-04-15
JPH0532664B2 (fr) 1993-05-17
EP0138041A2 (fr) 1985-04-24
EP0138041A3 (en) 1986-03-26
CA1233655A (fr) 1988-03-08
DE3477259D1 (en) 1989-04-20
JPS60105869A (ja) 1985-06-11

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