CA1197372A - Working medium for absorption heat pumps - Google Patents
Working medium for absorption heat pumpsInfo
- Publication number
- CA1197372A CA1197372A CA000420139A CA420139A CA1197372A CA 1197372 A CA1197372 A CA 1197372A CA 000420139 A CA000420139 A CA 000420139A CA 420139 A CA420139 A CA 420139A CA 1197372 A CA1197372 A CA 1197372A
- Authority
- CA
- Canada
- Prior art keywords
- heat
- difluorochloromethane
- absorber
- generator
- evaporator
- 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
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K5/00—Heat-transfer, heat-exchange or heat-storage materials, e.g. refrigerants; Materials for the production of heat or cold by chemical reactions other than by combustion
- C09K5/02—Materials undergoing a change of physical state when used
- C09K5/04—Materials undergoing a change of physical state when used the change of state being from liquid to vapour or vice versa
- C09K5/047—Materials undergoing a change of physical state when used the change of state being from liquid to vapour or vice versa for absorption-type refrigeration systems
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Organic Chemistry (AREA)
- Sorption Type Refrigeration Machines (AREA)
- Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
- Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)
- Medicines Containing Material From Animals Or Micro-Organisms (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
Abstract of the disclosure;
Mixtures of difluorochloromethane and triethylene glycol dimethyl ether can be used as the working medium in sorption heat pumps which can be operated as refrigerators or as thermal energy pumps.
Mixtures of difluorochloromethane and triethylene glycol dimethyl ether can be used as the working medium in sorption heat pumps which can be operated as refrigerators or as thermal energy pumps.
Description
3L~737~
-The present invention relates to a working medium which contains difluorochloromethane and can be used in an absorption~type heat pump for generating cold or heat.
The use of heat pumps for cooling or heating pur-S poses has been known for a long time~ While a~ first electrically driven co~pression refrigeratincJ machines ~ere at the center of interest, thermal energ~ pumps which are capable of saving energy have recently gained in importance. In principle, both compress;on heat pumps and ~0 sorption heat pumps can be used in th;s wayu However, sorption heat pumps have some advantages over electric-ally driven compression heat pumps, namely in essence the quietness, lower ~ear, s;nce there are hardly any mechan;-cally dr;ven parts present, lower maintenance requ;rement~
lower investment costs, but especially a lower prinlary-energy consumption. In the case of an electrically operated compression heat pump it should be appreciated that, for example~ about 2/3 of the primary energy is Lost in generating the current~
Pa;rs of materials for sorption heat pumps and ~h;ch consist of a solvent and a volatile material to be dissolved are already known~ Such pa;rs of Materials were f;rst developed for use in large-scale indus~r;al refrigerators ~water/amlmonia; and lithium brom;de/water)~
~n domest;c households, however, the use of amMon~a is restr;cted for tox;colog;cal and sa~ety reasons. Co~bina-tions with lithium bromide require great expense in respectof tightness, since the units work in a high vacuum.
The crystallization limit when the heat source is at low temperaturesmust also be allowed for.
It has been proposed to use systems which con-tain a fluorochlorohydrocarbon as the volatile phase in relatively small systems, in particular in domestic households, since this group of materials is non-flammable and comparatively non-toxic and non-corrosiveO
Pairs of working ma-terials which are intended for sorption heat purnps and in which the solvent is a phosphoramide having alkyl or phenyl groups and the volatile phase is a fluorochloroalkane are the subject of German Offenlegungsschrift
-The present invention relates to a working medium which contains difluorochloromethane and can be used in an absorption~type heat pump for generating cold or heat.
The use of heat pumps for cooling or heating pur-S poses has been known for a long time~ While a~ first electrically driven co~pression refrigeratincJ machines ~ere at the center of interest, thermal energ~ pumps which are capable of saving energy have recently gained in importance. In principle, both compress;on heat pumps and ~0 sorption heat pumps can be used in th;s wayu However, sorption heat pumps have some advantages over electric-ally driven compression heat pumps, namely in essence the quietness, lower ~ear, s;nce there are hardly any mechan;-cally dr;ven parts present, lower maintenance requ;rement~
lower investment costs, but especially a lower prinlary-energy consumption. In the case of an electrically operated compression heat pump it should be appreciated that, for example~ about 2/3 of the primary energy is Lost in generating the current~
Pa;rs of materials for sorption heat pumps and ~h;ch consist of a solvent and a volatile material to be dissolved are already known~ Such pa;rs of Materials were f;rst developed for use in large-scale indus~r;al refrigerators ~water/amlmonia; and lithium brom;de/water)~
~n domest;c households, however, the use of amMon~a is restr;cted for tox;colog;cal and sa~ety reasons. Co~bina-tions with lithium bromide require great expense in respectof tightness, since the units work in a high vacuum.
The crystallization limit when the heat source is at low temperaturesmust also be allowed for.
It has been proposed to use systems which con-tain a fluorochlorohydrocarbon as the volatile phase in relatively small systems, in particular in domestic households, since this group of materials is non-flammable and comparatively non-toxic and non-corrosiveO
Pairs of working ma-terials which are intended for sorption heat purnps and in which the solvent is a phosphoramide having alkyl or phenyl groups and the volatile phase is a fluorochloroalkane are the subject of German Offenlegungsschrift
2,~44,189.
The combina-tion of R-22 (difluorochloromethane) with tetraethylene glycol dimethyl ether is at present considered in the technical literatu:re as the most favorable system of a fluorochlorohydrocarbon with a solvent (B. Eisemann, Absorption refrigeration, ASHRAE Journal, Dec. 1959, p. 45 - 50; S.
Mastrangelo, Chlorofluorohydro carbons in tetraethylene glycol dimethyl ether, ASHRAE Journal, Oct. 1959, p. 64 - 67; and K.
Stephan and D. Seher, Arbeitsgemische fur Sorptions-Warmepumpen [Working mixtures for sorption heat pumps], Klima-Kalte-Heizung 1/1980 p. 874 and 875).
The present invention is directed to a working medium for use in sorption heat pumps and comprising the refrigerant ,~., ,"
y 7 ~'7q' diEluorochloromethane (R-22~ and an absorbent which is tri-ethylene glycol dimethyl ether.
The invention ls also directed to a process for trans-porting heat by means of an absorption heat pump which contains an evaporator, an absorber, a generator and a condenser, in which liquid difluorochloromethane absorbs heat and evaporates in the evaporator at temperatures of -20 -to +~0C, the vapor formed is passed into the absorber and dissolved there at 20 to 80C in an organic solvent, at least some of the heat which arises in the dissolving step is conducted away from the absorber, the resulting difluorochloromethane/ solvent mixture is pumped into the generator and heated up there to 90 to 180C, so that at least some of the difluorochloromethane is expelled from the solution, the expelled gaseous difluorochloromethane is passed into the condenser and condensed there at temperatures of 20 to 80C, as in th.e absorber, but at a temperature which is above the temperature in the evaporator, the heat of vaporization which arises in this step is given off, the liquid difluorochloromethane is returned to the evaporator, and the solution depleted in difluorochloromethane in the generator by expelling difluorochloromethane is returned to the abso.rber, which comprises using triethylene glycol dimethyl ether as the organic solvent.
A further :Eeature of the invention is a sorption heat pump which is capable of operation as a refrigerator or as a thermal ener~y pump,which contains as working medium the me~ium claimed in claim 1.
- 3a -Figure 1 shows in hiyhly simplified fashion an absorption heat pump cycle. The heat flow into the system and out of the system is labeled Q and indicated by the direction of the arrow.
- 3b -~ 4 --The cycle works as follows:
The refrigerant tfor example R-2Z) is evaporated by absorption of heat, at a low temperature ~for example 0C), ;n the evaporator (6~. The refrigerant vapor passes via line t7) ;nto the absorber (8~ and dissolves there in the solvent. This step liberates heat, which can be used, for example, to heat a water cyclea The refrigerant-rich solvent (strong solution) is pumped by means of a pump (12) via lines ~10) and (11) ;nto the generator (1).
The generator ~1~ is heated (for example at 130C)~ whereby refrigerant is desorbed from the solution and passed v;a line (2) into the condenser ~3)~ The condenser (3~ con- -denses the refrigerant vapor a~ an elevated tempera~ure~
for exa~ple 50C. The heat of vaporization ~hich is evolved in this step can be used, for example~ to heat a water cycle. It is reasonable to operate the heat pump in such a ~ay that the condenser and the absorber give off heat at the same temperature ~for example 50C~.
The liquid refrigerant returns from -the condenser ~0 S3~ to the evapora~or ~6) via line ~4) and the expansion valve t5).
The solution ~weak soLution) depleted in refriger-ant in the generator ~1) by desorption of refrigerant passes back ;nto the absorber ~8) via line ~9) and capacity-control valve ~13) and can there redissolve refr;gerant vapor from the evaporator ~6).
The heat pump cycle takes place between t~o pres sure levels The pressure on the low pressure side ~after expans;on valve, evaporator and absorber to the solution pump) results f rom the sa~uration vapor pressure of ~he refrigerant at the evaporation temperature. For example~
R-2Z has 3 saturation vapor pressure of 5 bar at ~C.
The pressure on the high pressure side tfrom the discharge end of the solut;on pump~ generator, condenser to expan-sion valve) results from the saturation vapor pressure of the refrigerant at the temperature of condensation. For example, R-22 has a saturation vapor pressure of 19 bar at 50C~
It is obvious that the more heat can be trans-ported in the un;t per kg of solvent the larger the difference bet~een the solubil;ties of the refrigerant in ~he absorber and generator. This solubility difference in kg of refrîgerant per kg of solvent is called the de-gassing range. If the degassing range i5 multiplied by the heat of vapor;zat;on of the refrigerant (R Z2 has a heat of vapor;zat;on of 154 kJ per kg at 50C), the amount of heat which can be transported per kg of solvent is obtained.
The R-22/tetraethylene glycol dimethyl ether sys~
tem described in the literature has according to our own experiments a degassing range of 0~19 kg of R-22 per kg of solvent. The measurement was carried out under the follow-;ng conditions: evaporator/absorber part: 5 bar vapor Z5 pressure of R-22 and a solution temperature of 50C;
generator/condenser part: ~9 bar vapor pressure of R-22 and a solut;on temperature of 130C.
Accordingly, the amount of heat which can be transported is 29~3 kJ per kg of solvent~
.
It is the object of the invention to provide a pair of ~orking materials which transports a considerably higher a~ount of h~at per unit weight of the solvent but nevertheless satisfies the remaining demands placed on such a system~ For exa~ple, ~ithin the operating range the system should have a low viscosity and be non-corrosive~
It should b~ possible to extract heat from the environment at -20C. It should be possibie to expel the volatile compound f rom the solvent at temperatures of 90C to 180C.
It has now been found that the pair of materials difluorochloromethane (R-22)/triethylene glycol dimethyl ether (TEG) satisfies these requirements. The degassing range of this system is about 50X larger than in ~he R~22t tetraethylene glycol dimethy~ ether system. The amount of heat which can be transported per kg of solvent is ~here-fore in the present case about 46.2 kJ per kg of solvent.
; It ;s also advantageous that the solvent TEG has a vis-cosity of only 3.0 mPa.s at 20C, while tetraethylene glycol dimethyl ether has a viscosity of SD1 mPa.s~ Sorption heat pumps f;lled with the pair of mater;als according to the invent;on can be operated not only as refrigerators but also as thermal energy pumps.
The pair of mater;als according to the invention can be used ~ithin certain temperature ranges. The tem-perature ranges for various parts of the unit are listedbelow.
1. Evaporator~ ~
Evaporation can take place within a range of -20C
to ~OoC, preferably with;n a range of -10C to ~20C
~s~
and, in particular, ~ithin a range of -5C to ~10C.
Condensation:
The condensat;on can take place ~ithin a range of 20C to 80C, preferably between 3~C and 65C.
The combina-tion of R-22 (difluorochloromethane) with tetraethylene glycol dimethyl ether is at present considered in the technical literatu:re as the most favorable system of a fluorochlorohydrocarbon with a solvent (B. Eisemann, Absorption refrigeration, ASHRAE Journal, Dec. 1959, p. 45 - 50; S.
Mastrangelo, Chlorofluorohydro carbons in tetraethylene glycol dimethyl ether, ASHRAE Journal, Oct. 1959, p. 64 - 67; and K.
Stephan and D. Seher, Arbeitsgemische fur Sorptions-Warmepumpen [Working mixtures for sorption heat pumps], Klima-Kalte-Heizung 1/1980 p. 874 and 875).
The present invention is directed to a working medium for use in sorption heat pumps and comprising the refrigerant ,~., ,"
y 7 ~'7q' diEluorochloromethane (R-22~ and an absorbent which is tri-ethylene glycol dimethyl ether.
The invention ls also directed to a process for trans-porting heat by means of an absorption heat pump which contains an evaporator, an absorber, a generator and a condenser, in which liquid difluorochloromethane absorbs heat and evaporates in the evaporator at temperatures of -20 -to +~0C, the vapor formed is passed into the absorber and dissolved there at 20 to 80C in an organic solvent, at least some of the heat which arises in the dissolving step is conducted away from the absorber, the resulting difluorochloromethane/ solvent mixture is pumped into the generator and heated up there to 90 to 180C, so that at least some of the difluorochloromethane is expelled from the solution, the expelled gaseous difluorochloromethane is passed into the condenser and condensed there at temperatures of 20 to 80C, as in th.e absorber, but at a temperature which is above the temperature in the evaporator, the heat of vaporization which arises in this step is given off, the liquid difluorochloromethane is returned to the evaporator, and the solution depleted in difluorochloromethane in the generator by expelling difluorochloromethane is returned to the abso.rber, which comprises using triethylene glycol dimethyl ether as the organic solvent.
A further :Eeature of the invention is a sorption heat pump which is capable of operation as a refrigerator or as a thermal ener~y pump,which contains as working medium the me~ium claimed in claim 1.
- 3a -Figure 1 shows in hiyhly simplified fashion an absorption heat pump cycle. The heat flow into the system and out of the system is labeled Q and indicated by the direction of the arrow.
- 3b -~ 4 --The cycle works as follows:
The refrigerant tfor example R-2Z) is evaporated by absorption of heat, at a low temperature ~for example 0C), ;n the evaporator (6~. The refrigerant vapor passes via line t7) ;nto the absorber (8~ and dissolves there in the solvent. This step liberates heat, which can be used, for example, to heat a water cyclea The refrigerant-rich solvent (strong solution) is pumped by means of a pump (12) via lines ~10) and (11) ;nto the generator (1).
The generator ~1~ is heated (for example at 130C)~ whereby refrigerant is desorbed from the solution and passed v;a line (2) into the condenser ~3)~ The condenser (3~ con- -denses the refrigerant vapor a~ an elevated tempera~ure~
for exa~ple 50C. The heat of vaporization ~hich is evolved in this step can be used, for example~ to heat a water cycle. It is reasonable to operate the heat pump in such a ~ay that the condenser and the absorber give off heat at the same temperature ~for example 50C~.
The liquid refrigerant returns from -the condenser ~0 S3~ to the evapora~or ~6) via line ~4) and the expansion valve t5).
The solution ~weak soLution) depleted in refriger-ant in the generator ~1) by desorption of refrigerant passes back ;nto the absorber ~8) via line ~9) and capacity-control valve ~13) and can there redissolve refr;gerant vapor from the evaporator ~6).
The heat pump cycle takes place between t~o pres sure levels The pressure on the low pressure side ~after expans;on valve, evaporator and absorber to the solution pump) results f rom the sa~uration vapor pressure of ~he refrigerant at the evaporation temperature. For example~
R-2Z has 3 saturation vapor pressure of 5 bar at ~C.
The pressure on the high pressure side tfrom the discharge end of the solut;on pump~ generator, condenser to expan-sion valve) results from the saturation vapor pressure of the refrigerant at the temperature of condensation. For example, R-22 has a saturation vapor pressure of 19 bar at 50C~
It is obvious that the more heat can be trans-ported in the un;t per kg of solvent the larger the difference bet~een the solubil;ties of the refrigerant in ~he absorber and generator. This solubility difference in kg of refrîgerant per kg of solvent is called the de-gassing range. If the degassing range i5 multiplied by the heat of vapor;zat;on of the refrigerant (R Z2 has a heat of vapor;zat;on of 154 kJ per kg at 50C), the amount of heat which can be transported per kg of solvent is obtained.
The R-22/tetraethylene glycol dimethyl ether sys~
tem described in the literature has according to our own experiments a degassing range of 0~19 kg of R-22 per kg of solvent. The measurement was carried out under the follow-;ng conditions: evaporator/absorber part: 5 bar vapor Z5 pressure of R-22 and a solution temperature of 50C;
generator/condenser part: ~9 bar vapor pressure of R-22 and a solut;on temperature of 130C.
Accordingly, the amount of heat which can be transported is 29~3 kJ per kg of solvent~
.
It is the object of the invention to provide a pair of ~orking materials which transports a considerably higher a~ount of h~at per unit weight of the solvent but nevertheless satisfies the remaining demands placed on such a system~ For exa~ple, ~ithin the operating range the system should have a low viscosity and be non-corrosive~
It should b~ possible to extract heat from the environment at -20C. It should be possibie to expel the volatile compound f rom the solvent at temperatures of 90C to 180C.
It has now been found that the pair of materials difluorochloromethane (R-22)/triethylene glycol dimethyl ether (TEG) satisfies these requirements. The degassing range of this system is about 50X larger than in ~he R~22t tetraethylene glycol dimethy~ ether system. The amount of heat which can be transported per kg of solvent is ~here-fore in the present case about 46.2 kJ per kg of solvent.
; It ;s also advantageous that the solvent TEG has a vis-cosity of only 3.0 mPa.s at 20C, while tetraethylene glycol dimethyl ether has a viscosity of SD1 mPa.s~ Sorption heat pumps f;lled with the pair of mater;als according to the invent;on can be operated not only as refrigerators but also as thermal energy pumps.
The pair of mater;als according to the invention can be used ~ithin certain temperature ranges. The tem-perature ranges for various parts of the unit are listedbelow.
1. Evaporator~ ~
Evaporation can take place within a range of -20C
to ~OoC, preferably with;n a range of -10C to ~20C
~s~
and, in particular, ~ithin a range of -5C to ~10C.
Condensation:
The condensat;on can take place ~ithin a range of 20C to 80C, preferably between 3~C and 65C.
3. Absorber:
Absorption can take place at temperatures between 20 and 80C, preferably bet~een 35C and 6~C.
Absorption can take place at temperatures between 20 and 80C, preferably bet~een 35C and 6~C.
4~ Generator.
R-22 can be expelled from the solution between 90C and 18nC, preferably between 110C and 150C.
The position of the centers of machine parts 1 (generator~, 3 (condenser), 6 ~evaporator~ and 8 (absorber) in respect o~ the coordinate system drawn in Figure 1 ;llustrates at the same time preferable operating condi-tions for a heat pwmp using the working medium accordingto the ;nvention.
Under the conditions already mentioned in the evaporator/absorber part and generator/condenser partf R-22 has the following solubilities in TEG andr for com-parison, tetraethylene glycol dimethyl ether.
Triethylene glycol Tetraethylene dimethyl ether tTEG) glycol dimethyl ether ~E-181) 25 Evaporator/
Absorber part0~61 kg/kg 0.53 kg/kg Generator/
Condenser part0.31 kg/kg 0.34 kg/kg Degassing range 0.3 kg/kg 0019 kg/kg It is surprising that the system according to the invention, ~hich contains TEG, is superior to the analogous 73`7~:
system based on tetraethylene glycol d;methyl e~her. It ~is kno~n, from U.S~ Patent 2,040~901, that both the ethers are good solvents for R-21. However~ the same reference states that no inferences can be dra~n from the solubility S properties of a certain halogen derivative of ~ethane in respect of the solubil;ty properties of a different halo-gen derivative of methaneO The lower the temperature in the absorber, the higher the load factor which is achieved with R-2Z in TEG. The higher the temperature in the generator~ the lower the residual load factor. The mixing ratio of TEG to R-Z2 thus depends on the operating condi~
tions~ In rrlost cases the R-22 content ;s 10 o 75X by ~eight~ preferably 20 ~ 40X by ~eight~
R-22 can be expelled from the solution between 90C and 18nC, preferably between 110C and 150C.
The position of the centers of machine parts 1 (generator~, 3 (condenser), 6 ~evaporator~ and 8 (absorber) in respect o~ the coordinate system drawn in Figure 1 ;llustrates at the same time preferable operating condi-tions for a heat pwmp using the working medium accordingto the ;nvention.
Under the conditions already mentioned in the evaporator/absorber part and generator/condenser partf R-22 has the following solubilities in TEG andr for com-parison, tetraethylene glycol dimethyl ether.
Triethylene glycol Tetraethylene dimethyl ether tTEG) glycol dimethyl ether ~E-181) 25 Evaporator/
Absorber part0~61 kg/kg 0.53 kg/kg Generator/
Condenser part0.31 kg/kg 0.34 kg/kg Degassing range 0.3 kg/kg 0019 kg/kg It is surprising that the system according to the invention, ~hich contains TEG, is superior to the analogous 73`7~:
system based on tetraethylene glycol d;methyl e~her. It ~is kno~n, from U.S~ Patent 2,040~901, that both the ethers are good solvents for R-21. However~ the same reference states that no inferences can be dra~n from the solubility S properties of a certain halogen derivative of ~ethane in respect of the solubil;ty properties of a different halo-gen derivative of methaneO The lower the temperature in the absorber, the higher the load factor which is achieved with R-2Z in TEG. The higher the temperature in the generator~ the lower the residual load factor. The mixing ratio of TEG to R-Z2 thus depends on the operating condi~
tions~ In rrlost cases the R-22 content ;s 10 o 75X by ~eight~ preferably 20 ~ 40X by ~eight~
Claims (3)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A working medium for use in sorption heat pumps and comprising the refrigerant difluorochloromethane (R-22) and an absorbent which is triethylene glycol dimethyl ether.
2. A sorption heat pump which is capable of operation as a refrigerator or as a thermal energy pump, which contains as working medium the medium claimed in claim 1.
3. A process for transporting heat by means of an absorption heat pump which contains an evaporator, an absorber, a generator and a condenser, in which liquid difluorochloromethane absorbs heat and evaporates in the evaporator at temperatures of -20 to +40°C, the vapor formed is passed into the absorber and dissolved there at 20 to 80°C in an organic solvent, at least some of the heat which arises in the dissolving step is con-ducted away from the absorber, the resulting difluorochloro-methane/solvent mixture is pumped into the generator and heated up there to 90 to 180°C, so that at least some of the difluoro-chloromethane is expelled from the solution, the expelled gaseous difluorochloromethane is passed into the condenser and condensed there at temperatures of 20 to 80°C, as in the absorber, but at a temperature which is above the temperature in the evaporator, the heat of vaporization which arises in this step is given off, the liquid difluorochloromethane is returned to the evapora-tor, and the solution depleted in difluorochloromethane in the generator by expelling difluorochloromethane is returned to the absorber, which comprises using triethylene glycol dimethyl ether as the organic solvent.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19823202377 DE3202377A1 (en) | 1982-01-26 | 1982-01-26 | WORKING MEDIUM FOR ABSORPTION HEAT PUMPS |
| DEP3202377.4 | 1982-01-26 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1197372A true CA1197372A (en) | 1985-12-03 |
Family
ID=6153921
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000420139A Expired CA1197372A (en) | 1982-01-26 | 1983-01-25 | Working medium for absorption heat pumps |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP0084869B1 (en) |
| JP (1) | JPS58131130A (en) |
| AT (1) | ATE15060T1 (en) |
| AU (1) | AU550260B2 (en) |
| CA (1) | CA1197372A (en) |
| DE (2) | DE3202377A1 (en) |
| DK (1) | DK28583A (en) |
| ES (1) | ES8308914A1 (en) |
| FI (1) | FI830228L (en) |
| NO (1) | NO830235L (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2567140B1 (en) * | 1984-07-06 | 1986-11-07 | Gaz De France | APPLICATION OF STABLE MIXTURES OF CHLOROFLUORIC HYDROCARBONS AND SOLVENTS AS A CALOGEN COMPOSITION FOR AN ABSORPTION HEAT PUMP |
| DE3543171A1 (en) * | 1985-12-06 | 1987-06-11 | Hoechst Ag | FABRIC PAIR FOR ABSORPTION HEAT TRANSFORMERS |
| CA1270710A (en) * | 1986-01-09 | 1990-06-26 | Takao Yamauchi | Chemical heat pump utilizing clathrate formation reaction |
| US4990277A (en) * | 1987-10-30 | 1991-02-05 | Atochem, Gaz De France | Compositions based on chlorofluorinated ether and solvent and their application in absorption apparatus |
| FR2622576B1 (en) * | 1987-10-30 | 1991-06-07 | Atochem | COMPOSITIONS BASED ON CHLOROFLUORIC ETHER AND SOLVENT |
| FR2622593B1 (en) * | 1987-10-30 | 1991-04-26 | Gaz De France | APPLICATION OF A MIXTURE OF FLUIDS BASED ON CHLOROFLUORIC ETHER AND SOLVENTS TO ABSORPTION MACHINES |
| WO1990006979A1 (en) * | 1988-12-14 | 1990-06-28 | The Lubrizol Corporation | Liquid compositions containing carboxylic esters |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54152257A (en) * | 1978-05-19 | 1979-11-30 | Sanyo Electric Co Ltd | Freezing composition for use in absorption type freezer |
| NL7811002A (en) * | 1978-11-06 | 1980-05-08 | Philips Nv | WORKING MEDIUM FOR AN ABSORPTION HEAT PUMP COMPRISING A SOLUTION OF A FLUORCHLORANE ALKANE. |
| JPS5679175A (en) * | 1979-11-30 | 1981-06-29 | Daikin Ind Ltd | Absorption refrigerant carrier composition |
| JPS5844713B2 (en) * | 1981-04-07 | 1983-10-05 | 松下電器産業株式会社 | absorption refrigerant composition |
| EP0062516B1 (en) * | 1981-04-07 | 1985-08-07 | Matsushita Electric Industrial Co., Ltd. | Composition for absorption refrigeration |
-
1982
- 1982-01-26 DE DE19823202377 patent/DE3202377A1/en not_active Withdrawn
-
1983
- 1983-01-21 EP EP83100506A patent/EP0084869B1/en not_active Expired
- 1983-01-21 AT AT83100506T patent/ATE15060T1/en not_active IP Right Cessation
- 1983-01-21 DE DE8383100506T patent/DE3360578D1/en not_active Expired
- 1983-01-24 ES ES519216A patent/ES8308914A1/en not_active Expired
- 1983-01-24 FI FI830228A patent/FI830228L/en not_active Application Discontinuation
- 1983-01-25 NO NO830235A patent/NO830235L/en unknown
- 1983-01-25 AU AU10763/83A patent/AU550260B2/en not_active Ceased
- 1983-01-25 DK DK28583A patent/DK28583A/en not_active Application Discontinuation
- 1983-01-25 CA CA000420139A patent/CA1197372A/en not_active Expired
- 1983-01-25 JP JP58009453A patent/JPS58131130A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| AU1076383A (en) | 1983-08-04 |
| DE3202377A1 (en) | 1983-07-28 |
| NO830235L (en) | 1983-07-27 |
| AU550260B2 (en) | 1986-03-13 |
| ES519216A0 (en) | 1983-10-16 |
| DK28583D0 (en) | 1983-01-25 |
| JPS58131130A (en) | 1983-08-04 |
| DE3360578D1 (en) | 1985-09-26 |
| EP0084869B1 (en) | 1985-08-21 |
| FI830228A0 (en) | 1983-01-24 |
| EP0084869A1 (en) | 1983-08-03 |
| DK28583A (en) | 1983-07-27 |
| FI830228L (en) | 1983-07-27 |
| ATE15060T1 (en) | 1985-09-15 |
| ES8308914A1 (en) | 1983-10-16 |
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| MKEC | Expiry (correction) | ||
| MKEX | Expiry |