EP0248296B1 - Procédé pour augmenter le coefficient de performance de machines frigorifiques ou de pompes à chaleur hybrides - Google Patents

Procédé pour augmenter le coefficient de performance de machines frigorifiques ou de pompes à chaleur hybrides Download PDF

Info

Publication number
EP0248296B1
EP0248296B1 EP87107514A EP87107514A EP0248296B1 EP 0248296 B1 EP0248296 B1 EP 0248296B1 EP 87107514 A EP87107514 A EP 87107514A EP 87107514 A EP87107514 A EP 87107514A EP 0248296 B1 EP0248296 B1 EP 0248296B1
Authority
EP
European Patent Office
Prior art keywords
heat
liquid
working medium
heat exchange
compression
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.)
Expired - Lifetime
Application number
EP87107514A
Other languages
German (de)
English (en)
Other versions
EP0248296A2 (fr
EP0248296A3 (en
Inventor
György Bergmann
Geza Hivessy
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.)
Energiagazdalkodasi Reszvenytarsasag
Original Assignee
Energiagazdalkodasi Reszvenytarsasag
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 Energiagazdalkodasi Reszvenytarsasag filed Critical Energiagazdalkodasi Reszvenytarsasag
Priority to AT87107514T priority Critical patent/ATE85695T1/de
Publication of EP0248296A2 publication Critical patent/EP0248296A2/fr
Publication of EP0248296A3 publication Critical patent/EP0248296A3/de
Application granted granted Critical
Publication of EP0248296B1 publication Critical patent/EP0248296B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • 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

Definitions

  • the invention relates to a method for transporting heat from a lower to a higher temperature level using a working medium consisting of a mixture of two components which are readily soluble in one another and have different boiling points.
  • the aim of the method described in US Pat. No. 3,698,202 is to generate low temperatures or to quickly start up the device suitable for producing such low temperatures, using a mixture of two phases as the working medium.
  • the component of the mixture with the lower boiling point is fed into the evaporator separately from the component with the higher boiling point.
  • DE-A-1 426 956 relates to a device for reaching very low temperatures, which is also operated with a mixture of substances as the working medium.
  • the essence of the circuit described is that an internal heat exchanger is installed after the condenser, which is also an evaporator.
  • DE-A-3 100 019 relates to a method for carrying out cold and heat pump processes which are operated with a multi-substance mixture as the working medium.
  • the inventive injection of the liquid phase of the coolant into the compressor improves the efficiency.
  • the aim of the invention is the further development of the known solutions and the increase in the power factor of the heat pumps and chillers.
  • the method according to the invention is used to operate compression-absorption heat pumps or refrigeration machines (of hybrid heat pumps or refrigeration machines) and represents a method for transporting heat from a lower to a higher temperature level using one of a mixture of two components which can be easily dissolved into one another with different boiling points of the working medium, in which, in a first heat exchange process when heat is dissipated, on the one hand steam of the component with a lower boiling point is dissolved or absorbed in liquid of the component with a higher boiling point and on the other hand steam of the component with a lower boiling point is condensed, the pressure of the working medium is reduced, after the pressure reduction in a second heat exchange process when heat is supplied, on the one hand the component with the lower boiling point is at least partially expelled from the solution and on the other hand the component with the higher boiling point eddling is at least partially evaporated, after which the working medium is compressed.
  • the desired aim is achieved according to the invention in that during the first heat exchange process the working medium is conducted in countercurrent to a heat-dissipating medium and that the temperature profile of the working medium is adapted to that of the heat-dissipating medium by the fact that the first heat exchange process takes place only in a partial area of the two-phase area of the Working medium is carried out with a temperature profile corresponding to that of the heat-dissipating medium, and the working medium is led out of the first heat exchange process as a mixture of two different phases with different concentrations.
  • the method according to the invention can preferably be implemented in such a way that an internal heat exchange is realized between the two-phase working medium emerging from the first heat exchange process, which is about to expand, and the working medium, which is coming before the compression, which is coming out of the second heat exchange process, the process from which working medium emerging from the first heat exchange process, dissolving and the condensation is continued.
  • the internal heat exchange is advantageously carried out in two sections, the condensation and dissolution being terminated in the first section and the entire working medium thereby changing into the liquid phase, while this liquid is further cooled in the second section.
  • the method according to the invention can preferably be implemented in such a way that wet steam is introduced into the suction line of the compressor, from which the liquid is partially or completely separated before the compression, the remaining dry or low-moisture steam is compressed and the separated liquid is injected into the flowing steam becomes.
  • the method according to the invention can furthermore preferably be carried out in such a way that the separated liquid on at least one before the compression and / or during the compression Pressure stage and / or after compression is returned to the steam.
  • the device suitable for realizing the method according to the invention is a hybrid heat pump or refrigerator which is designed in such a way that the circuit arrangement of its working medium cycle, connected in series in the flow direction of the working medium, is a condenser absorber, a liquid-cooling internal heat exchanger, a pressure reducer, and one Contains evaporator-degasser and a pressure booster, the output of the latter being connected to the input of the condenser absorber.
  • a steam-cooling internal heat exchanger is connected between the condenser absorber and the liquid-cooling internal heat exchanger.
  • a device suitable for the method according to the invention can also be designed in such a way that a liquid separator is switched on in the suction line of the compressor, on the outlet side of which a separate steam line and liquid line are branched off, from which the steam line is connected to the compressor, while in the Liquid line a pump is installed.
  • the liquid line can be connected to nozzles installed in the steam line upstream of the compressor and / or to nozzles installed in the compressor and / or to nozzles installed in the steam line after the compressor.
  • Regulator fittings are built into the branches of the liquid line connected to the nozzles.
  • 1 shows a device according to EP-A-0021205 which is known per se and which has already been mentioned in the introduction to this description and which is operated in a cycle with a solution circuit.
  • 1 shows the simplest variant of this solution using a circuit diagram and the theoretical cycle, shown in a T, s (temperature entropy) diagram.
  • the diagram shows the limit curve H of the working medium below which the medium is present in the form of a mixture of liquid and steam (wet steam); it was still in this wet steam area, the curves associated with the pressures p0 'and p1', between which pressure levels the cycle A'B'C'D 'takes place.
  • the working medium enters in a state A 'with a pressure p1' into a condenser absorber 1, where its more volatile component dissolves when a quantity of heat Q'1 is released in the less volatile component, while the vapors of the latter condense at the same time.
  • the temperature of the working medium gradually decreases.
  • the working medium emerges from the condenser absorber 1 in a liquid state B ′.
  • the pressure of the working medium in an expansion device (which could theoretically also be an expansion turbine, but in practice an expansion valve is usually installed, as is also shown in FIG. 1) from the value p 1 'to the value p 1' from and the working medium enters in a state C 'in an evaporator-degasser 3.
  • a state C 'in an evaporator-degasser 3 Here, most of the more volatile component is expelled from the working medium when a quantity of heat Q 3 'is supplied. The temperature of the working medium gradually increases.
  • the working medium exits the evaporator-degasser 3 in a state D ′, after which it is in a compressor 4 by applying a compression work Q4 ⁇ his state A ⁇ is reached with a pressure p1 ⁇ .
  • the working medium cools down further when a quantity of heat Q Ab is released and reaches the expansion valve 2 in the form of a supercooled liquid in state E, in which the pressure of the working medium decreases from p1 to p0, with part of the medium again going into the vapor phase (state C).
  • the working medium gets into the evaporator-degasser 3, where the evaporation and degassing is continued by supplying a quantity of heat Q3. From here, the medium exits in state D and enters the low-pressure side of the inner heat exchanger 5, where it absorbs the amount of heat Q5 given off by the working medium. The evaporation and degassing continue and the temperature of the working medium increases further. Finally, the pressure of the working medium in the state F is increased in the compressor 4 by supplying a compression work Q4 back to the pressure level p 1.
  • the condenser absorber is dimensioned in a heat pump, on one side the working medium consisting of two components (eg NH3 + H2O) passes from state A to state B (liquid), giving off a quantity of heat Q1 which leads to Water heating is used, then this process can be shown in a T, Q diagram (temperature - amount of heat) shown in FIG. 4.
  • the T, i diagram (temperature - enthalpy) of a working medium consisting of two components with the limit curve H was shown in FIG the field representing the wet steam conditions with the curves belonging to the pressures p1> p1 **> p1 *. It should be assumed that the pressure of the working medium is p 1 according to the cycle shown in Fig. 2 in the capacitor absorber and its state change from point A to point B continues. From Fig. 5 it can also be seen that this process takes place on the most curved section of the curve belonging to the pressure p 1.
  • the temperature belonging to state A * is lower than T A and the temperature belonging to state B * is lower than T B. It is known that the lower the temperature level to which the heat is to be reduced (the other conditions remain the same), the better the power factor of the heat pump or the chiller. If the cycle is designed in the sense of the inventive concept so that instead of liquid, but wet steam is led out of the condenser absorber 1, and in such a way that the enthalpy change of the working medium in the device may come close to the linear function of the temperature, then the Power factor of the heat pump or the chiller is larger.
  • the pressure p 1 * is lower than the pressure p 1, which on the one hand enables the use of a device operated at a lower nominal pressure, that is to say cheaper, and on the other hand improves the efficiency of the compressor by reducing the pressure ratio, which last In the end, the performance factor of the cycle improved.
  • FIG. 6 The simplest variant of implementing the method according to the invention is shown in FIG. 6.
  • the structure of the refrigeration machine or heat pump is identical to the known solution shown in FIG. 1, but its mode of operation differs from this. The most striking difference is clearly evident from the cycle shown in the T, s diagram, namely that point B is not on the limit curve H.
  • the size of the heat that can be transferred in the internal heat exchanger is determined by the amount of heat Q5 released during the cooling of the working medium in the liquid state between points B and E.
  • Point B is the pressure-associated liquid side point of the limit curve, which cannot be changed at a given pressure of the condenser absorber.
  • the temperature of point E is bound to point D and cannot be higher than the temperature at point D, even with an infinitely large and perfect countercurrent internal heat exchanger. This means that the theoretical limit of the cooling of the liquid inside Heat exchanger T B -T D is.
  • the internal heat exchange can be increased by increasing the pressure p 1 and / or reducing the pressure p 1, but this would not make sense after the advantage of the internal heat exchanger can be realized by reducing the pressure ratio and the pressure p 1.
  • Fig. 7 shows the circuit diagram of the device and the theoretical cycle in a T, s diagram.
  • the working medium in state A with a pressure p 1 enters the condenser absorber 1, where, when a quantity of heat Q 1 is released, the temperature of the working medium gradually decreases, with condensation and dissolution going on.
  • this double process is not ended here, but the wet steam in state B exits this unit and occurs on the high-pressure side of a steam-cooling internal heat exchanger 6, where it releases heat amount Q6 is cooled further and finally the condensation and dissolution are stopped.
  • the working medium in state G saturated liquid
  • the pressure reducer 2 can also be an expansion machine (for example a turbine). This changes the cycle shown in Fig. 7 that expansion work Q2 is withdrawn from the working medium in the unit denoted by 2, so that work is removed instead of throttling.
  • this solution improves the performance factor of the heat pump, on the other hand, it is quite expensive. Their application can be decided on a case-by-case basis using profitability calculations.
  • FIG. 8 is the isentropic compression of the superheated steam of a two-component working medium shown in a T, s diagram, with a single-stage intermediate recooling between the pressure limits p1 and p3 at the pressure level p2.
  • the hatched field ( ⁇ W) shows the gain of the recooling, ie the reduction in the compression work.
  • wet compression means recooling with an infinite number of stages, thus significantly reducing the workload of the cycle.
  • this beneficial effect only comes into play to the extent that the liquid in the compressor can follow the change in state of the vapor.
  • the volume of the vapor phase decreases during the compression, which is why the vapor phase warms up, whereas the temperature of the liquid phase hardly changes due to the pressure increase.
  • the much warmer vapor phase heats the liquid, which, however, does not reach equilibrium with the vapor phase until compression is complete.
  • the working medium is only in the compressor for a very short time, the temperatures of the liquid and the vapor phase can only come close to one another if there is a sufficiently large area available for heat transfer. It follows from this that the liquid should expediently be introduced into the vapor stream in the form of fine drops.
  • FIG. 9 A possible embodiment of this solution is shown in FIG. 9.
  • the liquid phase is partially or completely separated in the line upstream of the compressor by means of a liquid separator 7, while the steam continues to flow in the direction of the compressor in a steam line 13 and the separated liquid with the aid of a pump 8 via a liquid line 14 and nozzles 9 into the steam flow is sprayed into it.
  • the piston compressors can be less of a choice for realizing the wet compression, because there is a risk of liquid hammer. It follows that primarily rotary compressors, mainly screw compressors, can be used here. However, the rapidly rotating elements of these compressors push the liquid introduced into the vapor stream against the wall of the compressor housing during compression, so that the large liquid area produced by fine atomization is greatly reduced in this way.
  • the circuit shown in FIG. 10 was proposed, which means a further development of the solution according to FIG. 9.
  • the liquid conveyed by the pump is sprayed into the vapor stream not only in front of the compressor, but partly during the compression with the aid of nozzles 10.
  • the nozzles 10 can be installed in the compressor housing, but it is also conceivable that they are arranged in the bores of the rotor shaft. In the latter case, the centrifugal force also contributes to the atomization.
  • the nozzles 10 can introduce the liquid into the vapor at one or more pressure level (s) of the compression. It is obviously best if the liquid is substantially the same during compression is supplied moderately, so if the nozzles are arranged densely along the length of the compressor. Such a design naturally depends on the particular compressor design. In certain cases, the nozzle 9 can even be omitted.
  • the present invention offers a solution to this problem as shown in FIG. 11.
  • regulator fittings 12 are installed in the branches of the pressure line of the pump leading to the individual nozzles or nozzle groups. By setting these regulator fittings, the Distribution of the amount of liquid can be regulated among the individual supply points. This regulation can be carried out according to the respective operating conditions, and some nozzles can even be excluded.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Motor Or Generator Cooling System (AREA)
  • Compression-Type Refrigeration Machines With Reversible Cycles (AREA)

Claims (5)

  1. Procédé de transport de chaleur d'un niveau faible de chaleur à un niveau élevé en utilisant un milieu opératoire constitué d'un mélange de deux composés miscibles parfaitement l'un à l'autre ayant des points d'ébullition différents, dans lequel au cours d'un premier processus d'échange de chaleur par évacuation de chaleur on dilue ou on absorbe d'un côté le composé ayant le point d'ébullition le plus bas dans le liquide du composé à haut point d'ébullition et on condense de l'autre côté la vapeur du composé ayant le point d'ébullition le plus bas, la pression du milieu opératoire diminuant, après la réduction de pression au cours d'un second processus d'échange de chaleur on expulse au moins partiellement par introduction de chaleur d'un côté le composé ayant le point d'ébullition le plus bas hors de la solution, et on vaporise de l'autre côté au moins partiellement le composé ayant le point d'ébullition le plus élevé, le milieu opératoire étant alors comprimé, caractérisé en ce qu'au cours du premier processus d'échange de chaleur on introduit le milieu opératoire à contre-courant dans un milieu prélevant la chaleur, en ce qu'une adaptation de l'évolution de la température du milieu opératoire est entreprise vis-à-vis du milieu prélevant la chaleur, en ce que le premier processus d'échange de chaleur est conduit uniquement dans un domaine partiel du domaine à deux phases du milieu opératoire avec un cycle de température correspondant avec celui du milieu prélevant la chaleur et en ce que le milieu opératoire est prélevé au cours du premier processus d'échange de chaleur sous forme de mélange de deux phases différentes à concentration différente.
  2. Procédé selon la revendication 1, caractérisé en ce qu'on effectue un échange interne de chaleur entre le milieu opératoire en deux phases existant avant l'expansion, provenant du premier processus d'échange de chaleur, l'absorption et la condensation étant poursuivies dans le milieu opératoire provenant du premier processus d'échange de chaleur.
  3. Procédé selon la revendication 2, caractérisé en ce que l'échange de chaleur interne est réalisé en deux phases, l'absorption et la condensation étant achevées au cours d'une première phase provoquant ainsi le passage de tout le milieu opératoire dans la phase liquide, tandis que dans une seconde phase on poursuit le refroidissement de ce liquide.
  4. Procédé selon l'une des revendications 1 à 3, caractérisé en ce qu'on introduit de la vapeur humide dans la conduite d'aspiration du compresseur, on sépare le liquide partiellement ou totalement avant la compression, on comprime la vapeur sèche restante ou pauvre en humidité, et on injecte le liquide isolé dans la vapeur sous forme de fines gouttelettes.
  5. Procédé selon la revendication 4, caractérisé en ce que le liquide isolé est réintroduit sous forme de fines gouttelettes avant compression et /ou durant la compression du moins à un stade de pression et/ou après la compression sous forme de vapeur.
EP87107514A 1986-05-23 1987-05-22 Procédé pour augmenter le coefficient de performance de machines frigorifiques ou de pompes à chaleur hybrides Expired - Lifetime EP0248296B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87107514T ATE85695T1 (de) 1986-05-23 1987-05-22 Verfahren zur erhoehung des leistungsfaktors von hybriden kaeltemaschinen oder waermepumpen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
HU862182A HU198329B (en) 1986-05-23 1986-05-23 Method and apparatus for increasing the power factor of compression hybrid refrigerators or heat pumps operating by solution circuit
HU218286 1987-03-24

Publications (3)

Publication Number Publication Date
EP0248296A2 EP0248296A2 (fr) 1987-12-09
EP0248296A3 EP0248296A3 (en) 1988-05-25
EP0248296B1 true EP0248296B1 (fr) 1993-02-10

Family

ID=10958168

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87107514A Expired - Lifetime EP0248296B1 (fr) 1986-05-23 1987-05-22 Procédé pour augmenter le coefficient de performance de machines frigorifiques ou de pompes à chaleur hybrides

Country Status (10)

Country Link
US (1) US4967566A (fr)
EP (1) EP0248296B1 (fr)
JP (1) JPS6325463A (fr)
AT (1) ATE85695T1 (fr)
CA (1) CA1317771C (fr)
DD (1) DD262478A5 (fr)
DK (1) DK168675B1 (fr)
FI (1) FI91441C (fr)
HU (1) HU198329B (fr)
RU (1) RU2018064C1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102020110357A1 (de) 2020-04-16 2021-10-21 Wolfram Ungermann Systemkälte GmbH & Co. KG Verfahren zur Regelung eines hybriden Kühlsystems sowie hybrides Kühlsystem

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5931587A (ja) * 1982-08-12 1984-02-20 松下電器産業株式会社 ヒ−タ
HU210994B (en) * 1990-02-27 1995-09-28 Energiagazdalkodasi Intezet Heat-exchanging device particularly for hybrid heat pump operated by working medium of non-azeotropic mixtures
US5271235A (en) * 1991-03-12 1993-12-21 Phillips Engineering Company High efficiency absorption cycle of the gax type
US5367884B1 (en) 1991-03-12 1996-12-31 Phillips Eng Co Generator-absorber-heat exchange heat transfer apparatus and method and use thereof in a heat pump
US5570584A (en) 1991-11-18 1996-11-05 Phillips Engineering Co. Generator-Absorber heat exchange transfer apparatus and method using an intermediate liquor
DE4230818A1 (de) * 1992-09-15 1994-03-17 Fritz Egger Gmbh Verfahren und Einrichtung zur Leistungsregelung einer Kompressions-Wärmepumpe und/oder Kältemaschine
US5579652A (en) 1993-06-15 1996-12-03 Phillips Engineering Co. Generator-absorber-heat exchange heat transfer apparatus and method and use thereof in a heat pump
US5490393A (en) * 1994-03-31 1996-02-13 Robur Corporation Generator absorber heat exchanger for an ammonia/water absorption refrigeration system
US5582020A (en) * 1994-11-23 1996-12-10 Mainstream Engineering Corporation Chemical/mechanical system and method using two-phase/two-component compression heat pump
US5782097A (en) 1994-11-23 1998-07-21 Phillips Engineering Co. Generator-absorber-heat exchange heat transfer apparatus and method and use thereof in a heat pump
US5791157A (en) * 1996-01-16 1998-08-11 Ebara Corporation Heat pump device and desiccant assisted air conditioning system
US6112547A (en) * 1998-07-10 2000-09-05 Spauschus Associates, Inc. Reduced pressure carbon dioxide-based refrigeration system
US6073454A (en) * 1998-07-10 2000-06-13 Spauschus Associates, Inc. Reduced pressure carbon dioxide-based refrigeration system
DE19959439A1 (de) * 1999-12-09 2001-06-21 Bosch Gmbh Robert Klimaanlage für Kraftfahrzeuge und Verfahren zum Betreiben einer Klimaanlage für Kraftfahrzeuge
WO2006102941A2 (fr) * 2005-03-30 2006-10-05 Miwe Ökokälte Gmbh Dispositif permettant d'eliminer l'eau d'une solution aqueuse
FR2922557A1 (fr) * 2007-10-19 2009-04-24 Denis Jean Christian Chretien Composition de refrigerant et cycle frigorifique associe pour air conditionne et surgeles
GB0817672D0 (en) * 2008-09-29 2008-11-05 Al Mayahi Abdulsalam Ammonia cerntrifugal heat pump
RU2528452C2 (ru) * 2013-01-10 2014-09-20 Закрытое акционерное общество Научно-производственное предприятие "Машпром" (ЗАО НПП "Машпром") Способ подогрева в паровых теплообменниках и установка для его осуществления
BE1021700B1 (nl) * 2013-07-09 2016-01-11 P.T.I. Inrichting voor energiebesparing
WO2016072958A1 (fr) * 2014-11-05 2016-05-12 Общество С Ограниченной Ответственностью "Научно-Производственное Общество "Днипро-Мто" Procédé d'obtention de bases températures et dispositif récupérateur d'échange de chaleur
JP7114079B2 (ja) * 2018-03-30 2022-08-08 満夫 山田 発電機能付き冷房装置

Family Cites Families (16)

* 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
US2945355A (en) * 1955-12-20 1960-07-19 Heat X Inc Capacity control of refrigeration system
DE1426956A1 (de) * 1964-07-17 1969-05-08 Fuderer Michael Verfahren zur Tiefkuehlung
US3470707A (en) * 1968-02-12 1969-10-07 Andrew F Lofgreen Refrigeration system
US3500656A (en) * 1968-04-18 1970-03-17 Andrew F Lofgreen Refrigeration system with liquid and vapor pumps
US3698202A (en) * 1971-08-16 1972-10-17 Gulf & Western Industries Control system for low temperature refrigeration system
US3733845A (en) * 1972-01-19 1973-05-22 D Lieberman Cascaded multicircuit,multirefrigerant refrigeration system
US3872682A (en) * 1974-03-18 1975-03-25 Northfield Freezing Systems In Closed system refrigeration or heat exchange
US4014181A (en) * 1974-11-05 1977-03-29 Burger Manfred R Air conditioning methods and apparatus
DE2850403A1 (de) * 1978-11-21 1980-05-29 Luft U Kaeltetechnik Veb K Kompressionskaeltemaschine mit loesungskreislauf
HU186726B (en) * 1979-06-08 1985-09-30 Energiagazdalkodasi Intezet Hybrid heat pump
DE3100019A1 (de) * 1981-01-02 1982-09-23 Werner Dr.-Ing. 1000 Berlin Malewski Verfahren zur durchfuehrung von kaelte- und waermepumpenprozessen nach dem kompressionsprinzip mit loesungskreislauf
FR2497931A1 (fr) * 1981-01-15 1982-07-16 Inst Francais Du Petrole 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
US4495776A (en) * 1981-10-13 1985-01-29 Vsesojuzny Nauchno-Issledovatelsky Experminetalno Konstruktorsky Institut Elektrobytovyky Machin I Priborov Method and cooling agent for freezing and storing products
CA1233655A (fr) * 1983-09-29 1988-03-08 Arnold R. Vobach Procede de refrigeration mecanique assiste par voie chimique
HU198328B (en) * 1984-12-03 1989-09-28 Energiagazdalkodasi Intezet Method for multiple-stage operating hibrid (compression-absorption) heat pumps or coolers

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102020110357A1 (de) 2020-04-16 2021-10-21 Wolfram Ungermann Systemkälte GmbH & Co. KG Verfahren zur Regelung eines hybriden Kühlsystems sowie hybrides Kühlsystem
DE102020110357B4 (de) 2020-04-16 2024-06-20 Wolfram Ungermann Systemkälte GmbH & Co. KG Verfahren zur Regelung eines hybriden Kühlsystems

Also Published As

Publication number Publication date
RU2018064C1 (ru) 1994-08-15
US4967566A (en) 1990-11-06
DK261887A (da) 1987-11-24
FI91441C (fi) 1994-06-27
CA1317771C (fr) 1993-05-18
EP0248296A2 (fr) 1987-12-09
HU198329B (en) 1989-09-28
DD262478A5 (de) 1988-11-30
DK168675B1 (da) 1994-05-16
ATE85695T1 (de) 1993-02-15
EP0248296A3 (en) 1988-05-25
JPS6325463A (ja) 1988-02-02
FI872281A (fi) 1987-11-24
DK261887D0 (da) 1987-05-22
FI872281A0 (fi) 1987-05-22
FI91441B (fi) 1994-03-15
HUT44851A (en) 1988-04-28

Similar Documents

Publication Publication Date Title
EP0248296B1 (fr) Procédé pour augmenter le coefficient de performance de machines frigorifiques ou de pompes à chaleur hybrides
EP0855009B1 (fr) Convertisseur thermique par sorption dote de composants supplementaires
DE2754626C2 (de) Mit einer Energiequelle relativ niedriger Temperatur, insbesondere Solarenergie, arbeitende Kälteanlage
DE102006050232B9 (de) Kälteanlage
EP0021205B1 (fr) Procédé de compression-absorption hybride pour pompes à chaleur ou machine frigorifique
DE4036854C1 (fr)
EP3099985B1 (fr) Système de réfrigération
WO1985004216A1 (fr) Procede et installation destines a un cycle thermodynamique
EP3540332B1 (fr) Pompe à chaleur a absorption et procédé de circuit à absorption
DE1140957B (de) Absorptionskuehlsystem und Verfahren fuer den Betrieb desselben
DE2538730C2 (de) Verfahren zur Kälteerzeugung mittels eines Kompressions-Absorptions-Kreisprozesses und Anlage zur Durchführung des Verfahrens
EP3540333B1 (fr) Pompe à chaleur à absorption et procédé de circuit à absorption
EP2215412A1 (fr) Installation pour le refroidissement, le chauffage ou la climatisation, en particulier installations frigorifiques
DE19533755C2 (de) Vorrichtung und Verfahren zur Erzeugung von Wärme und Kälte
DE2438418A1 (de) Gaskompressor der verdraengerbauart, insbesondere fuer kaeltemaschinen
DE19538348C2 (de) Sorptionswärmewandleranlage mit Zusatzkomponenten zur Steigerung der Nutzleistung bzw. Erweiterung der Grenzen für die Antriebs-, Nutz- oder Kühltemperaturen
EP0184181B1 (fr) Pompe à chaleur
EP2369280A2 (fr) Procédé et dispositif de production d'air froid sous forme gazeuse ou liquide
CH392576A (de) Verfahren zum Betrieb von Kältemaschinen
EP3087330A1 (fr) Moteur thermique et procédé pour faire fonctionner un moteur thermique
AT398631B (de) Kühlanlage
DE3834302C2 (fr)
DE102014100916A1 (de) Kälteanlage
DE3129999A1 (de) "waermepumpe mit einer speichereinrichtung und verfahren zu ihrem betrieb"
DE1751367C (de) Absorptionskälteanlage

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

Kind code of ref document: A2

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

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Kind code of ref document: A3

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

17P Request for examination filed

Effective date: 19880614

17Q First examination report despatched

Effective date: 19890203

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: ENERGIAGAZDALKODASI RESZVENYTARSASAG

AK Designated contracting states

Kind code of ref document: B1

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

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

Ref country code: GB

Effective date: 19930210

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRE;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.SCRIBED TIME-LIMIT

Effective date: 19930210

Ref country code: SE

Effective date: 19930210

Ref country code: NL

Effective date: 19930210

REF Corresponds to:

Ref document number: 85695

Country of ref document: AT

Date of ref document: 19930215

Kind code of ref document: T

REF Corresponds to:

Ref document number: 3784098

Country of ref document: DE

Date of ref document: 19930325

ET Fr: translation filed
NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
GBV Gb: ep patent (uk) treated as always having been void in accordance with gb section 77(7)/1977 [no translation filed]

Effective date: 19930210

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: BE

Payment date: 19950425

Year of fee payment: 9

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

Ref country code: CH

Payment date: 19950427

Year of fee payment: 9

Ref country code: FR

Payment date: 19950427

Year of fee payment: 9

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

Ref country code: AT

Payment date: 19950530

Year of fee payment: 9

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

Ref country code: DE

Payment date: 19950606

Year of fee payment: 9

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

Ref country code: AT

Effective date: 19960522

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

Ref country code: CH

Effective date: 19960531

Ref country code: BE

Effective date: 19960531

Ref country code: LI

Effective date: 19960531

BERE Be: lapsed

Owner name: ENERGIAGAZDALKODASI RESZVENYTARSASAG

Effective date: 19960531

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

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

Ref country code: FR

Effective date: 19970131

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

Ref country code: DE

Effective date: 19970201

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST